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US3203194A - Compression process for refrigeration - Google Patents

Compression process for refrigeration Download PDF

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US3203194A
US3203194A US325875A US32587563A US3203194A US 3203194 A US3203194 A US 3203194A US 325875 A US325875 A US 325875A US 32587563 A US32587563 A US 32587563A US 3203194 A US3203194 A US 3203194A
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mixture
refrigerants
vapors
boiling component
refrigeration
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US325875A
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Fuderer Andrija
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Hoechst AG
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component

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  • two refrigeration units each consisting of a compressor, a condenser, and an evaporator, are combined in such a manner that the evaporator of the higher stage forms a heat exchanger with the condenser of the lower stage.
  • the low temperature required for condensing the lower boiling refrigerant is obtained by evaporating the previously condensed higher boiling refrigerant.
  • the present invention provides a compression process for refrigeration with the use of a mixture of refrigerants which comprises condensing the compressed vaporous mixture of refrigerants in a first condensation stage by partially condensing substantially the higher boiling component, separating the liquid phase from the vaporous phase, transferring the vaporous, lower boiling component to a second condensation stage where it is condensed, producing the required temperature of condensation by expanding and evaporating the higher boiling component of the mixture of refrigerants condensed in the first condensation stage, producing the required final temperature by expanding and evaporating the condensed lower boiling component of the mixture of refrigerants, mixing the components of the mixture with one another and conducting them to the compressor for closing the cycle.
  • the refrigeration process according to the invention can be used as lower or upper stage of a cascade connection, whereby one stage is saved. It is suitable for producing temperatures in the range of from 20 C. to 180 C., and preferably -50 C. to -160 C., for example for the liquefaction of methane and air.
  • the process of the invention presents advantages not only in smaller units with piston-type compressors but also in larger units with turbocompressors.
  • Suitable components of the refrigerant mixture are substances having low solidification temperatures, preferably hydrocarbons, especially alkanes and alkenes with 1 to 4 carbon atoms and the halogenated derivatives thereof, more especially partially or completely fiuorinated and/ or chlorinated methanes and ethanes. Nitrogen can likewise be used. In general, the higher as well as the lower boiling refrigerants constitute uniform chemical compounds. But this is not absolutely necessary.
  • the higher as well as the lower boiling component may be a mixture, namely a mixture forming an azeotrope on boiling or a mixture of components the boiling points of which are not too far from one another, for example air or a mixture of fiuorinated chlorohydrocarbons which does not form an azeotrope.
  • the boiling points of the combined refrigerants shall be sufficiently remote from one another, since otherwise the difference in the composition of the two phases is not great enough, i.e. the separation of the refrigerants is very incomplete.
  • the diiference in the boiling points of the higher boiling and the lower boiling refrigerants shall preferably range from 40 C. to 140 C. and more preferably from 60 C. to C. If one or both refrigerants constitute mixtures the differences in temperature as defined above shall be between the upper boiling limit of the lower boiling refrigerant and the lower boiling limit of the higher boiling refrigerant.
  • Suitable pairs of refrigerants are, for example, monofluorotrichloromethane/trifluoromonobromomethane; trifiuorotrichloroethane/difluorodichloromethane; monoliuorotrichloromethane/trifluoromonochloromethane; monofluorotrichloromethane/ethane; monofiuorodichloromethane/trifluoromonochloromethane; diiiuorodichloromethane/ethylene; difluoromonochloromethane/tetrafiuoromethane; propane/tetrafiuoromethane; propane/methane; trifluoromonochloromethane/methane; triiiuoromonochloromethane/nitrogen; ethane/ nitro gen tetrafluoromethane/ air; the azeotropic mixture of difluorodichlorom
  • Suitable pairs of refrigerants for turbocompressors are, for example, monofluorotrichloromethane/difluoromonochloromethane and tetrafluorodichloroethane/trifluoromonochloromethane.
  • a temperature of 25 C. can be obtained on the average with a pressure ratio of about 1:3 only, while with the second combination of refrigerants a temperature of -63 C. can be reached on the average with a pressure ratio of about 1:5. In either case a medium temperature of condensation above +30 C. is taken as a basis.
  • FIGURES 1 and 4 represent by way of example suitable flow sheets of the process of the invention and FIGURES 2 and 3 are phase diagrams.
  • the numerals have the following meaning:
  • FIGURES 2 and 3 represent phase diagrams according to Merkel Bosnjakovic (cf. Plank, Handbuch der Kaltetchnik, Springer Verlag, Berlin, vol. II, pp. 285, 291 et seq.). There are plotted on the ordinates the enthalpy i[kilocalories kgf and on the abscissas the percent by weight g of the lower boiling refrigerant.
  • Numerals 1-15 designate the thermal states occurring in the refrigerating process.
  • the diagram of FIGURE 2 shows the system at a (constant) pressure of liquefaction of 25 atmospheres.
  • the diagram of FIGURE 3 shows the system at a (constant) evaporation pressure of 2 atmospheres.
  • a mixture of 50% of CF Cl and 50% of CR corresponding to the initial state (2 atm., 10 C.) is aspirated by compressor and compressed to state 1 atm., 100 C.).
  • condenser 30 cooled by water cooling 120, part of the mixture is condensed (state 1+2). If necessary the condensation can be continued in auxiliary condenser 110 (state 2+3). About one half of the vapor is condensed.
  • state 3 the liquid phase 4 and the vaporous phase 5 exist which separate in liquid separator 4-0.
  • the liquid phase 4 contains 15% of CR; and the vaporous phase 5 contains 85% of CF.,,.
  • the liquid 4 is cooled in supercooling device '70 to about C.
  • auxiliary condenser 110 can be dispensed with.
  • thermodynamics of the process can be improved by applying a two-stage compression.
  • the twostage compression is of special advantage when the boiling points of the refrigerant used are more than C. remote from one another, for example when a mixture of about 80% by weight of difluorodichloromethane and 20% by weight of methane is used. In this case with a temperature of liquefaction of 32 C. on the average an evaporation temperature of 156 C. can be reached.
  • An essential feature of the process of the invention is the variable temperature.
  • the evaporation starts at 116 C.
  • the temperature has increased to about 112 C. (state 8+9).
  • a further part of the liquid evaporates in the supercooling device.
  • the temperature further increases from 112" C. to about 76 C. (state 9+10) whereby the condensate can be supercooled in countercurrent from about 55 C. to C. (state 6+7).
  • the condensate of the higher boiling refrigerant can be supercooled. It is remarkable that the cooling is accomplished by the evaporation of the phase taking place at rising temperature.
  • the process of the invention offers the further advantage that a thermodynamic efliciency is obtained which in many cases, especially with a suitable selection of the intermediate states and appropriate dimensions of the heat exchangers, may be more favorable than the efiiciency of a known two-stage refrigeration process operating under the same conditions.
  • zone of the device or in which states the two phases are again mixed with one another It is of importance in which zone of the device or in which states the two phases are again mixed with one another.
  • the addition of the substantially or completely evaporated lower boiling refrigerating component to the higher boiling component shall preferably take place directly after the place of the cycle of refrigerants where the higher boiling component is expanded. Thereby, the partial pressure of the higher boiling refrigerant suddenly decreases and the evaporation takes place at a lower temperature.
  • the condenser 30 consists of vertically arranged tubes.
  • the compressed mixture of refrigerants is introduced into the condenser from below.
  • the condensate essentially consisting of the higher boiling refrigerant streams downward owing to the force of gravity in con-tercurrent with the mixture of refrigerant and vapor, whereby an action of rectification is produced.
  • the condenser also acts as liquid separator and oil separator for the lower boiling phase, so that the liquid separator 40 shown in FIGURE 1 can be dispensed with.
  • Auxiliary condenser 110 now serves as a kind of dephlegrnator.
  • This condenser rectifier need not be heated since the vapors of refrigerent stream in at the bottom with a
  • the temperature in the upper part of the condenser is considerably lower than in the lower part'and state 3 plotted in FIGURE 2 does not consist of phases 4 and 5 but approximately of phases 17 (vapor 20 C.) and 18 (liquid +40 C.).
  • Liquid 18 may be cooled with Water to about +25 C. whereby a lower temperature is reached in evaporator 80.
  • FIGURE 4 additionally contains a gas tank 130 which is connected by means of valves with the high pressure side (directly towards the condenser) and with the low pressure side. At least one valve in the connection pipes to the container 130 must be closed, otherwise a short circuit occurs in the refrigeration process.
  • a greater amount of gaseous refrigerant mainly the low boiling component
  • the valve on the high pressure side is open, a greater amount of gaseous refrigerant, mainly the low boiling component, is in container 130, owing to the elevated pressure.
  • the valve on the high pressure side is closed, defined amounts of the lower boiling refrigerant can be introduced into the cycle through the other valve whereby a regulation becomes possible. With a greater amount of lower boiling refrigerant in the cycle the pressures everywhere in the refrigeration unit and, consequently, the volumetric refrigerating capacity and the expenditure of work of the compressor are a little higher.
  • the refrigeration process can be realized in a manner such that the cold produced by evaporating the higher boiling component is not used up tot-ally for condensing the lower boiling component and supercooling the own condensate. Part of the cold can be utilized for other purposes. Therefore it is a further advantage of the present process that simultaneously two different low temperaures can be produced, using a sole compressor.
  • the process of the invention may simultaneously serve two purposes, for example to manufacture Dry Ice and liquefy methane.
  • a compression process for refrigeration using a mixture of refrigerants which process comprises compressing said mixture of refrigerants, partially condensing substantially the higher boiling component from compressed vapors of said mixture of refrigerants in a first condensation stage, separating the resultant condensed and vapor phases, condensing the separated vapors of the lower boiling component of said mixture of refrigerants in a second condensation stage, expanding and evaporating the condensed components to produce refrigcrating temperatures, mixing the resultant vapors, and then recycling the vapors to the compression stage, the improvement wherein the expansion and evaporation of the separated condensed higher boiling component are used to cool and condense vapors of the lower boiling component in said second condensation stage.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

g- 3 1965 A. FUDERER' 3,203,194
COMPRESSION PROCESS FOR REFRIGERATION Filed Nov. 26, 1963 3 Sheets-Sheet 1 INVENTOR ANDRIJA FUDERER Y MWT%O%EYS 3 Sheets-Sheet 2 x k 3 3 M x Q E 5 T w n 0o 9 ON on co 0% on a 8? a I];
A. FUDERER COMPRESSION PROCESS FOR REFRIGERATION Aug. 31, 1965 Filed Nov. 26, 1963 91 03 m 0% m m "Q m aow mum mw Q is:awm w w M61 Hum n Us 5 5 w-.- N @R INVENTOR ANDR/JA FUDERER 41% W ATTORN Y5 Aug. 31, 1965 A. FUDERER 3,203,194
COMPRESSION PROCESS FOR REFRIGERATION Filed Nov. 26, 1963 3 Sheets-Sheet 3 INVENTOR ANDR/JA FUDERER BY M, M s- W ATTORN S United States Patent 3,293,194 COMPRESSION PROCESS FOR REFRIGERATIQN Andriia Fnderer, Zagreb, Yugoslavia, assignor to Fatb- Werke Hoechst Alrtiengesellschaft vormals Meister Lucius dz llruning, Frankfurt am Main, Germany, a corporation of Germany Filed Nov. 26, 1%3, Ser. No. 325,875 Claims priority, application Germany, Dec. ll, I962, F 38,442 7 Claims. (Cl. 62-114) The present invention relates to a compression process for refrigeration with the use of a mixture of refrigerants.
For refrigeration according to the compression process a readily vaporizable liquid refrigerant is evaporated, the vapors obtained are aspirated by a compressor, compressed, condensed in a condenser under high pressure, and again evaporated in an evaporator. Most of the known refrigeration units are operated with a uniform product as refrigerant. It is likewise known, however, how to use as refrigerant a mixture of substances of different boiling points. This measure serves to improve, in the first place, the volumetric refrigeration capacity of the compressor. In the known processes the refrigerant or mixture of refrigerants is completely condensed in the condenser. For obtaining still lower temperatures it has been proposed to connect two or more compression cycles in cascade connection. In this case two refrigeration units, each consisting of a compressor, a condenser, and an evaporator, are combined in such a manner that the evaporator of the higher stage forms a heat exchanger with the condenser of the lower stage. The low temperature required for condensing the lower boiling refrigerant is obtained by evaporating the previously condensed higher boiling refrigerant.
The present invention provides a compression process for refrigeration with the use of a mixture of refrigerants which comprises condensing the compressed vaporous mixture of refrigerants in a first condensation stage by partially condensing substantially the higher boiling component, separating the liquid phase from the vaporous phase, transferring the vaporous, lower boiling component to a second condensation stage where it is condensed, producing the required temperature of condensation by expanding and evaporating the higher boiling component of the mixture of refrigerants condensed in the first condensation stage, producing the required final temperature by expanding and evaporating the condensed lower boiling component of the mixture of refrigerants, mixing the components of the mixture with one another and conducting them to the compressor for closing the cycle.
In comparison with the aforesaid known process using a two-stage cooling system with cascade connection and two compressors, in the process of the invention only one compressor is necessary for obtaining the same low temperature, this representing considerable technical progress.
The refrigeration process according to the invention can be used as lower or upper stage of a cascade connection, whereby one stage is saved. It is suitable for producing temperatures in the range of from 20 C. to 180 C., and preferably -50 C. to -160 C., for example for the liquefaction of methane and air.
The process of the invention presents advantages not only in smaller units with piston-type compressors but also in larger units with turbocompressors.
Patented Aug. 31, 1965 "Ice Suitable components of the refrigerant mixture are substances having low solidification temperatures, preferably hydrocarbons, especially alkanes and alkenes with 1 to 4 carbon atoms and the halogenated derivatives thereof, more especially partially or completely fiuorinated and/ or chlorinated methanes and ethanes. Nitrogen can likewise be used. In general, the higher as well as the lower boiling refrigerants constitute uniform chemical compounds. But this is not absolutely necessary. The higher as well as the lower boiling component may be a mixture, namely a mixture forming an azeotrope on boiling or a mixture of components the boiling points of which are not too far from one another, for example air or a mixture of fiuorinated chlorohydrocarbons which does not form an azeotrope.
The boiling points of the combined refrigerants shall be sufficiently remote from one another, since otherwise the difference in the composition of the two phases is not great enough, i.e. the separation of the refrigerants is very incomplete.
The diiference in the boiling points of the higher boiling and the lower boiling refrigerants shall preferably range from 40 C. to 140 C. and more preferably from 60 C. to C. If one or both refrigerants constitute mixtures the differences in temperature as defined above shall be between the upper boiling limit of the lower boiling refrigerant and the lower boiling limit of the higher boiling refrigerant.
It is, therefore, possible to combine refrigerants in various ways. Suitable pairs of refrigerants are, for example, monofluorotrichloromethane/trifluoromonobromomethane; trifiuorotrichloroethane/difluorodichloromethane; monoliuorotrichloromethane/trifluoromonochloromethane; monofluorotrichloromethane/ethane; monofiuorodichloromethane/trifluoromonochloromethane; diiiuorodichloromethane/ethylene; difluoromonochloromethane/tetrafiuoromethane; propane/tetrafiuoromethane; propane/methane; trifluoromonochloromethane/methane; triiiuoromonochloromethane/nitrogen; ethane/ nitro gen tetrafluoromethane/ air; the azeotropic mixture of difluorodichloromcthane and difiuoromonochlorornethane/tetrafluoromethane.
Suitable pairs of refrigerants for turbocompressors are, for example, monofluorotrichloromethane/difluoromonochloromethane and tetrafluorodichloroethane/trifluoromonochloromethane.
With the first combination of refrigerants a temperature of 25 C. can be obtained on the average with a pressure ratio of about 1:3 only, while with the second combination of refrigerants a temperature of -63 C. can be reached on the average with a pressure ratio of about 1:5. In either case a medium temperature of condensation above +30 C. is taken as a basis.
The process of the invention is illustrated with reference to the accompanying drawings. FIGURES 1 and 4 represent by way of example suitable flow sheets of the process of the invention and FIGURES 2 and 3 are phase diagrams. In the drawings the numerals have the following meaning:
20-compressor Edi-condenser 40fiash chamber Sit-evaporator condenser 60supercooling device for condensate of lower boiling refrigerant '70supercooling device for condensate of higher boiling refrigerant 80evaporator 90first expansion valve 100second expansion valve 110auxiliary condenser (heat exchanger) 120pipes for cooling water FIGURES 2 and 3 represent phase diagrams according to Merkel Bosnjakovic (cf. Plank, Handbuch der Kaltetchnik, Springer Verlag, Berlin, vol. II, pp. 285, 291 et seq.). There are plotted on the ordinates the enthalpy i[kilocalories kgf and on the abscissas the percent by weight g of the lower boiling refrigerant.
Numerals 1-15 designate the thermal states occurring in the refrigerating process.
The following example serves to illustrate the invention but it is not intended to limit it thereto.
Example As higher boiling refrigerant difluorodichloromethane (CF CI boiling point 30 C.) and as lower boiling refrigerant tetrafiuoromethane (CF boiling point 128 C.) are used. The diagram of FIGURE 2 shows the system at a (constant) pressure of liquefaction of 25 atmospheres. The diagram of FIGURE 3 shows the system at a (constant) evaporation pressure of 2 atmospheres. With the expansion of the system (in the valves) is connected an isenthalpic transition of FIGURE 2 to FIGURE 3, with the compression is connected a transition with enthalpy increase of FIGURE 3 to FIGURE 2.
A mixture of 50% of CF Cl and 50% of CR corresponding to the initial state (2 atm., 10 C.) is aspirated by compressor and compressed to state 1 atm., 100 C.). In condenser 30, cooled by water cooling 120, part of the mixture is condensed (state 1+2). If necessary the condensation can be continued in auxiliary condenser 110 (state 2+3). About one half of the vapor is condensed. In state 3 the liquid phase 4 and the vaporous phase 5 exist which separate in liquid separator 4-0. The liquid phase 4 contains 15% of CR; and the vaporous phase 5 contains 85% of CF.,,. The liquid 4 is cooled in supercooling device '70 to about C. (state 4+1) and expanded in the first expansion valve 90 with constant enthalpy to 2 atmospheres (state I1+I1a). The vaporous phase 5 is condensed in evaporator-condenser (state 5+ 6). It is further cooled in supercooling device to 110" C. (state 6+7). Expansion to 2 atmospheres takes place then through the second expansion valve 100 with constant enthalpy i (state 7+ 8). Part of the liquid evaporates in evaporator 30 whereby the temperature rises from about 116 C. to 112 C. (state 8+9). A further part evaporates in undercooling device 60 (state 9+10). The two phases are here combined 11a and 10) and a mixture of the original composition of 50% of CR; and 50% of CF CI (state 12) is formed again. In condenser-evaporator 50 the major part of the liquid still present evaporates at gradually rising temperature (state 12+13). The increase in temperature and evaporation continue in supercooling device until state 14 is reached. The remainder of the liquid evaporates in auxiliary condenser 110 in which the vapor is slightly superheated (state 15). In this state the mixture is aspirated by the compressor.
In the i/& diagrams of FIGURES 2 and 3 the temperature conditions as well as the enthalpy amounts are well visible. It must be considered that from 1 kilogram mixture in state 3 about 500 grams of phases 4 and 5 respec- 'sufiiciently elevated temperature.
tively are formed. Therefore, the enthalpy differences in these phases must be multiplied by 0.5.
Instead of the expansion valves any other expansion device may be used. In many cases auxiliary condenser 110 can be dispensed with.
It is often sufiicient to use a one-stage compressor 20. If necessary, however, a multi-stage compressor may be used. The thermodynamics of the process can be improved by applying a two-stage compression. The twostage compression is of special advantage when the boiling points of the refrigerant used are more than C. remote from one another, for example when a mixture of about 80% by weight of difluorodichloromethane and 20% by weight of methane is used. In this case with a temperature of liquefaction of 32 C. on the average an evaporation temperature of 156 C. can be reached.
An essential feature of the process of the invention is the variable temperature. In the present example the evaporation starts at 116 C. When one half of the liquid has evaporated the temperature has increased to about 112 C. (state 8+9). A further part of the liquid evaporates in the supercooling device. The temperature further increases from 112" C. to about 76 C. (state 9+10) whereby the condensate can be supercooled in countercurrent from about 55 C. to C. (state 6+7). In analogous manner the condensate of the higher boiling refrigerant can be supercooled. It is remarkable that the cooling is accomplished by the evaporation of the phase taking place at rising temperature.
Owing to the variable temperatures a countercurrent heat exchange is favorable in the process of the invention and even necessary if-as in the present example-the temperatures vary within wide limits, i.e. with a combination of two refrigerants of very different boiling points. This substantial supercooling of the condensate at such favorable temperature conditions considerably reduces the loss of energy which mostly occurs when the liquid is expanded.
Besides the aforesaid advantage 'of saving one compressor, the process of the invention offers the further advantage that a thermodynamic efliciency is obtained which in many cases, especially with a suitable selection of the intermediate states and appropriate dimensions of the heat exchangers, may be more favorable than the efiiciency of a known two-stage refrigeration process operating under the same conditions.
It is of importance in which zone of the device or in which states the two phases are again mixed with one another. The addition of the substantially or completely evaporated lower boiling refrigerating component to the higher boiling component shall preferably take place directly after the place of the cycle of refrigerants where the higher boiling component is expanded. Thereby, the partial pressure of the higher boiling refrigerant suddenly decreases and the evaporation takes place at a lower temperature.
In the device diagrammatically illustrated in FIGURE 4 the condenser 30 consists of vertically arranged tubes. The compressed mixture of refrigerants is introduced into the condenser from below. The condensate essentially consisting of the higher boiling refrigerant streams downward owing to the force of gravity in con-tercurrent with the mixture of refrigerant and vapor, whereby an action of rectification is produced. In this case the condenser also acts as liquid separator and oil separator for the lower boiling phase, so that the liquid separator 40 shown in FIGURE 1 can be dispensed with. Auxiliary condenser 110 now serves as a kind of dephlegrnator. This condenser rectifier need not be heated since the vapors of refrigerent stream in at the bottom with a The temperature in the upper part of the condenser is considerably lower than in the lower part'and state 3 plotted in FIGURE 2 does not consist of phases 4 and 5 but approximately of phases 17 (vapor 20 C.) and 18 (liquid +40 C.). Liquid 18 may be cooled with Water to about +25 C. whereby a lower temperature is reached in evaporator 80.
FIGURE 4 additionally contains a gas tank 130 which is connected by means of valves with the high pressure side (directly towards the condenser) and with the low pressure side. At least one valve in the connection pipes to the container 130 must be closed, otherwise a short circuit occurs in the refrigeration process. When the valve on the high pressure side is open, a greater amount of gaseous refrigerant, mainly the low boiling component, is in container 130, owing to the elevated pressure. When the valve on the high pressure side is closed, defined amounts of the lower boiling refrigerant can be introduced into the cycle through the other valve whereby a regulation becomes possible. With a greater amount of lower boiling refrigerant in the cycle the pressures everywhere in the refrigeration unit and, consequently, the volumetric refrigerating capacity and the expenditure of work of the compressor are a little higher.
Alternatively, the refrigeration process can be realized in a manner such that the cold produced by evaporating the higher boiling component is not used up tot-ally for condensing the lower boiling component and supercooling the own condensate. Part of the cold can be utilized for other purposes. Therefore it is a further advantage of the present process that simultaneously two different low temperaures can be produced, using a sole compressor. Thus, the process of the invention may simultaneously serve two purposes, for example to manufacture Dry Ice and liquefy methane.
I claim:
1. In a compression process for refrigeration using a mixture of refrigerants, which process comprises compressing said mixture of refrigerants, partially condensing substantially the higher boiling component from compressed vapors of said mixture of refrigerants in a first condensation stage, separating the resultant condensed and vapor phases, condensing the separated vapors of the lower boiling component of said mixture of refrigerants in a second condensation stage, expanding and evaporating the condensed components to produce refrigcrating temperatures, mixing the resultant vapors, and then recycling the vapors to the compression stage, the improvement wherein the expansion and evaporation of the separated condensed higher boiling component are used to cool and condense vapors of the lower boiling component in said second condensation stage.
2. The process of claim 1, which comprises using a mixture of two individual refrigerating components, the boiling temperatures of which differ by 40 to C.
3. The process of claim 1, which comprises using a mixture of refrigerants of more than two individual components.
4. The process of claim 1, which comprises supercooling the condensates of the higher boiling component and of the lower boiling component by countercurrent heat exchangers, the cooling being brought about by the evaporation at rising temperatures of the corresponding component.
5. The process of claim 1, which comprises mixing the higher boiling component and the lower boiling component directly after the place of the cycle of the mixture of refrigerants where the higher boiling component is expanded.
6. The process of claim 1, which comprises varying the proportion of the lower boiling component of the mixture of refrigerants in the cycle by means of a container for the said component which is connected with the high pressure side and with the low pressure side of the cycle.
7. The process of claim 1, which comprises utilizing the cold produced by evaporating the higher boiling component only partially for condensing the lower boiling component and supercooling the condensate.
References Cited by the Examiner UNITED STATES PATENTS 2,255,5 84 9/ 41 Hubacker 62--502 X 2,794,322 6/ 5 7 Etherington 62-1l4 2,794,328 6/57 Herrick 62--114 2,794,329 6/ 57 Herrick 621 14 2,931,190 4/60 Dubitzky 62-114 3,019,614 2/62 Schubert et a1. 621l4 FOREIGN PATENTS 129,207 2/58 Russia.
ROBERT A. OLEARY, Primary Examiner.

Claims (1)

1. IN A COMPRESSIONN PROCESS FOR REFRIGERATION USING A MIXTURE OF REFRIGERANTS, WHICH PROCESS COMPRISES COMPRESSING SAID MIXTURE OF REFRIGEERANTS, PARTIALLY CONDENSING SUBSTANTIALLY THE HIGHER BOILING COMPONENT FROM COMPRESSED VAPORS OF SAID MIXTURE OF REFRIGERANTS IN A FIRST CONDENSATION STAGE, SEPARATING THE RESULTANT CONDENSED AND VAPOR PHASES, CONDENSING TTHE SEPARATED VAPORS OF THE LOWER BOILING COMPONENT OF SAID MIXTURE OF REFRIGERANTS IN A SECOND CONDENSATION STAGE, EXPANDING AND EVAPORATING THE CONDENSED COMPONENTS TO PRODUCE REFRIGERATING TEMPERATURESS, MIXING THE RESULTANT VAPORS, AND THEN RECYCLING THE VAPORS TO THE COMMPREESSIONN STAGE, THE IMPROVEMENT WHEREIN THE EXPANSION ANDD EVAPORATIONN OF THE SEPARATED CONDENSED HIGHER BOILING COMPONENT ARE USED TO COOL AND CONDENSE VAPORS OF THELLOWER BOILING COMPONENT IN SAID SECOND CONDENSATION STAGE.
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Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3309897A (en) * 1965-10-21 1967-03-21 Russell Jacob Bruce Constant pressure refrigeration cycle
US3336763A (en) * 1965-06-30 1967-08-22 Carrier Corp Refrigeration systems
US3353366A (en) * 1966-01-27 1967-11-21 Allied Chem Absorption refrigeration systems
US3487653A (en) * 1968-01-26 1970-01-06 Associated Testing Lab Inc Low temperature environmental test system
US3698202A (en) * 1971-08-16 1972-10-17 Gulf & Western Industries Control system for low temperature refrigeration system
US3768273A (en) * 1972-10-19 1973-10-30 Gulf & Western Industries Self-balancing low temperature refrigeration system
US3872682A (en) * 1974-03-18 1975-03-25 Northfield Freezing Systems In Closed system refrigeration or heat exchange
DE2628007A1 (en) * 1976-06-23 1978-01-05 Heinrich Krieger PROCESS AND SYSTEM FOR GENERATING COLD WITH AT LEAST ONE INCORPORATED CASCADE CIRCUIT
JPS5443215B1 (en) * 1970-06-03 1979-12-19
JPS54161145A (en) * 1978-06-09 1979-12-20 Hitachi Ltd Cooling method by furan mixed refrigerant
US4406135A (en) * 1981-01-15 1983-09-27 Institut Francais Du Petrole Heating and thermal conditioning process making use of a compression heat pump operating with a mixed working fluid
US4423603A (en) 1981-05-29 1984-01-03 Hitachi, Ltd. Heat pump type refrigeration system
US4459810A (en) * 1981-05-26 1984-07-17 Daikin Kogyo Co., Ltd. Working fluids for use with rankine cycle
US4481783A (en) * 1979-06-08 1984-11-13 Energiagazdalkodasi Intezet Hybrid heat pump
US4535597A (en) * 1984-01-25 1985-08-20 Marin Tek, Inc. Fast cycle water vapor cryopump
WO1986001881A1 (en) * 1984-09-17 1986-03-27 Sundstrand Corporation High efficiency refrigeration or cooling system
US4580415A (en) * 1983-04-22 1986-04-08 Mitsubishi Denki Kabushiki Kaisha Dual refrigerant cooling system
US4688397A (en) * 1984-12-03 1987-08-25 Energiagazdalkodasi Intezet Multi-stage heat pump of the compressor-type operating with a solution
US4689964A (en) * 1986-04-02 1987-09-01 Marin-Tek, Inc. Zero gravity (position-insensitive) low-temperature multi-component refrigerator
US5049296A (en) * 1989-01-28 1991-09-17 Chujun Gu Working media for a thermodynamic engineering device operating in accordance with the Gu thermodynamic cycle
US5062985A (en) * 1989-06-16 1991-11-05 Sanyo Electric Co., Ltd. Refrigerant composition containing dichloromonofluoromethane
US5157925A (en) * 1991-09-06 1992-10-27 Exxon Production Research Company Light end enhanced refrigeration loop
US5207077A (en) * 1992-03-06 1993-05-04 The University Of Maryland Refrigeration system
WO1993018357A1 (en) * 1992-03-06 1993-09-16 University Of Maryland College Park Subcooling system for refrigeration cycle
US5651263A (en) * 1993-10-28 1997-07-29 Hitachi, Ltd. Refrigeration cycle and method of controlling the same
US6644067B2 (en) * 2000-11-10 2003-11-11 Telmark Cryogenics Limited Discontinuous cryogenic mixed gas refrigeration system and method
FR2913762A1 (en) * 2007-03-16 2008-09-19 Usifroid Freeze-drying assembly cooling system, has condenser lowering temperature of mixture to value between boiling temperatures so that refrigerant is remained in gaseous state to guide towards derivative detent loop section
WO2010029839A1 (en) * 2008-09-10 2010-03-18 三洋電機株式会社 Refrigeration system
US20140341710A1 (en) * 2011-12-21 2014-11-20 Venus Systems Limited Centrifugal refrigerant vapour compressors
PL442284A1 (en) * 2022-09-14 2024-03-18 Politechnika Warszawska Refrigeration system with internal heat exchangers

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US2794322A (en) * 1954-06-29 1957-06-04 Gen Electric Variable temperature refrigeration
US2794328A (en) * 1954-06-29 1957-06-04 Gen Electric Variable temperature refrigeration
US2931190A (en) * 1957-05-29 1960-04-05 Coleman Co Jet refrigeration system
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Cited By (39)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3336763A (en) * 1965-06-30 1967-08-22 Carrier Corp Refrigeration systems
US3309897A (en) * 1965-10-21 1967-03-21 Russell Jacob Bruce Constant pressure refrigeration cycle
US3353366A (en) * 1966-01-27 1967-11-21 Allied Chem Absorption refrigeration systems
US3487653A (en) * 1968-01-26 1970-01-06 Associated Testing Lab Inc Low temperature environmental test system
JPS5443215B1 (en) * 1970-06-03 1979-12-19
US3698202A (en) * 1971-08-16 1972-10-17 Gulf & Western Industries Control system for low temperature refrigeration system
US3768273A (en) * 1972-10-19 1973-10-30 Gulf & Western Industries Self-balancing low temperature refrigeration system
US3872682A (en) * 1974-03-18 1975-03-25 Northfield Freezing Systems In Closed system refrigeration or heat exchange
DE2628007A1 (en) * 1976-06-23 1978-01-05 Heinrich Krieger PROCESS AND SYSTEM FOR GENERATING COLD WITH AT LEAST ONE INCORPORATED CASCADE CIRCUIT
JPS54161145A (en) * 1978-06-09 1979-12-20 Hitachi Ltd Cooling method by furan mixed refrigerant
US4481783A (en) * 1979-06-08 1984-11-13 Energiagazdalkodasi Intezet Hybrid heat pump
US4406135A (en) * 1981-01-15 1983-09-27 Institut Francais Du Petrole Heating and thermal conditioning process making use of a compression heat pump operating with a mixed working fluid
US4459810A (en) * 1981-05-26 1984-07-17 Daikin Kogyo Co., Ltd. Working fluids for use with rankine cycle
US4423603A (en) 1981-05-29 1984-01-03 Hitachi, Ltd. Heat pump type refrigeration system
US4624114A (en) * 1983-04-22 1986-11-25 Mitsubishi Denki Kabushiki Kaisha Dual refrigerant cooling system
US4580415A (en) * 1983-04-22 1986-04-08 Mitsubishi Denki Kabushiki Kaisha Dual refrigerant cooling system
US4535597A (en) * 1984-01-25 1985-08-20 Marin Tek, Inc. Fast cycle water vapor cryopump
WO1986001881A1 (en) * 1984-09-17 1986-03-27 Sundstrand Corporation High efficiency refrigeration or cooling system
US4598556A (en) * 1984-09-17 1986-07-08 Sundstrand Corporation High efficiency refrigeration or cooling system
US4688397A (en) * 1984-12-03 1987-08-25 Energiagazdalkodasi Intezet Multi-stage heat pump of the compressor-type operating with a solution
US4689964A (en) * 1986-04-02 1987-09-01 Marin-Tek, Inc. Zero gravity (position-insensitive) low-temperature multi-component refrigerator
US5049296A (en) * 1989-01-28 1991-09-17 Chujun Gu Working media for a thermodynamic engineering device operating in accordance with the Gu thermodynamic cycle
US5062985A (en) * 1989-06-16 1991-11-05 Sanyo Electric Co., Ltd. Refrigerant composition containing dichloromonofluoromethane
US5157925A (en) * 1991-09-06 1992-10-27 Exxon Production Research Company Light end enhanced refrigeration loop
US5207077A (en) * 1992-03-06 1993-05-04 The University Of Maryland Refrigeration system
WO1993018357A1 (en) * 1992-03-06 1993-09-16 University Of Maryland College Park Subcooling system for refrigeration cycle
US5651263A (en) * 1993-10-28 1997-07-29 Hitachi, Ltd. Refrigeration cycle and method of controlling the same
US6644067B2 (en) * 2000-11-10 2003-11-11 Telmark Cryogenics Limited Discontinuous cryogenic mixed gas refrigeration system and method
FR2913762A1 (en) * 2007-03-16 2008-09-19 Usifroid Freeze-drying assembly cooling system, has condenser lowering temperature of mixture to value between boiling temperatures so that refrigerant is remained in gaseous state to guide towards derivative detent loop section
WO2010029839A1 (en) * 2008-09-10 2010-03-18 三洋電機株式会社 Refrigeration system
US20110023532A1 (en) * 2008-09-10 2011-02-03 Sanyo Electric Co., Ltd. Refrigerating apparatus
CN101672543B (en) * 2008-09-10 2012-07-18 三洋电机株式会社 refrigeration unit
EP2322876A4 (en) * 2008-09-10 2014-12-10 Panasonic Healthcare Co Ltd REFRIGERATION SYSTEM
EP2950019A1 (en) * 2008-09-10 2015-12-02 Panasonic Healthcare Holdings Co., Ltd. Refrigerating apparatus
US9335070B2 (en) 2008-09-10 2016-05-10 Panasonic Healthcare Holdings Co., Ltd. Refrigerating apparatus
US9360238B2 (en) 2008-09-10 2016-06-07 Panasonic Healthcare Holdings Co., Ltd. Refrigerating apparatus
US20140341710A1 (en) * 2011-12-21 2014-11-20 Venus Systems Limited Centrifugal refrigerant vapour compressors
PL442284A1 (en) * 2022-09-14 2024-03-18 Politechnika Warszawska Refrigeration system with internal heat exchangers
PL245958B1 (en) * 2022-09-14 2024-11-04 Politechnika Warszawska Refrigeration system with internal heat exchangers

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CH420225A (en) 1966-09-15
SE311923B (en) 1969-06-30
DE1241468B (en) 1967-06-01

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