EP0138041A2 - Chemisch unterstützter mechanischer Kühlprozess - Google Patents

Chemisch unterstützter mechanischer Kühlprozess Download PDF

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Publication number
EP0138041A2
EP0138041A2 EP84110693A EP84110693A EP0138041A2 EP 0138041 A2 EP0138041 A2 EP 0138041A2 EP 84110693 A EP84110693 A EP 84110693A EP 84110693 A EP84110693 A EP 84110693A EP 0138041 A2 EP0138041 A2 EP 0138041A2
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Prior art keywords
refrigerant
solvent
stream
evaporator
solution
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EP84110693A
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French (fr)
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EP0138041A3 (en
EP0138041B1 (de
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Arnold R. Vobach
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B25/00—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00
    • F25B25/02—Compression-sorption machines, plants, or systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B75/00—Other engines
    • F02B75/02—Engines characterised by their cycles, e.g. six-stroke
    • F02B2075/022—Engines characterised by their cycles, e.g. six-stroke having less than six strokes per cycle
    • F02B2075/027—Engines characterised by their cycles, e.g. six-stroke having less than six strokes per cycle four

Definitions

  • This invention relates generally to refrigeration and more particularly to a new and improved chemically assisted mechanical refrigeration cycle.
  • the typical mechanical refrigeration system employs a mechanical compressor to raise the pressure and to condense a gaseous refrigerant, which thereafter absorbs its heat of vaporization.
  • the typical vapor compression cycle uses an evaporator in which a liquid refrigerant, such as Freon-12, boils at a low pressure to produce cooling; a compressor to raise the pressure of the gaseous refrigerant after it leaves the evaporator; a condenser, in which the refrigerant condenses and discharges its heat to the environment; and an expansion valve through which the liquid refrigerant leaving the condenser expands from the high-pressure level in the condenser to the low pressure level in the evaporator.
  • a liquid refrigerant such as Freon-12
  • the resorption cycle has also been studied. Introduced in the earlier half of this century, the resorption cycle is similar in operation to the absorption cycle. However, a resorber replaces the condenser and the vapor is absorbed by a special weak solution while condensing. This solution is then circulated to the evaporator where the refrigerant boils and the heats of disassociation and vaporization produce the refrigerating effect.
  • prior systems suffer from one or more of several limitations. For example, prior systems fail to take advantage of both the heat of vaporization and the heat of dilution to ultimately cool a working medium in a compression type cycle. Additionally, prior systems utilizing a compressor require a heavy duty compressor capable of sustaining relatively high compression ratios. Other systems operate at comparatively high pressures which require heavier duty components. Still, other systems have relatively inefficient heat transfer mechanics. Yet other systems fail to allow auxiliary heat exchange between refrigerant-solvent and solvent without decreasing the density of the flow to the compressor while other systems fail to provide sensible heat transfer in an auxiliary heat exchange between refrigerant-solvent and solvent. Still other systems fail to provide secondary evolution of gaseous refrigerant from the solvent after the solvent leaves the evaporator to facilitate overall efficiency. These and other problems encountered by the prior systems are substantially reduced, if not eliminated, by the present invention.
  • a chemically assisted mechanical refrigeration process using a refrigerant and a solvent having a negative deviation from Raoult's Law when in combination with each other.
  • a stream of solution including the solvent and a liquified refrigerant is passed to an evaporator.
  • the pressure over the solution is then reduced to allow refrigerant to vaporize and separate from the solvent.
  • the evolving refrigerant and solvent are placed in heat exchange relation with a working medium to remove energy from the working medium.
  • a solvent stream and a refrigerant stream including gaseous refrigerant are formed and leave the evaporator.
  • the refrigerant stream undergoes mechanical compression and the refrigerant stream and solvent stream are contacted at a pressure sufficient to promote substantial dissolving of the refrigerant and the solvent.
  • a stream of solution is thus formed for passage to the evaporator.
  • the solvent stream leaving the evaporator is preferably passed in heat exchange relation with the solution stream passing to the evaporator. This occurs in an economizing zone so as to cause transfer of heat between the solvent stream and the solution stream.
  • Such heat transfer may be facilitated by the mass transfer of gaseous refrigerant in relation to one or more of the streams passing through the economizing zone.
  • the solvent stream leaving the evaporator includes a material portion of the dissolved refrigerant.
  • the solvent stream is placed in fluid communication with the refrigerant stream leaving the evaporator to accomplish mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream. This in turn facilitates heat transfer in the economizing zone prior to passage of the solvent stream and refrigerant stream to the mixing zone.
  • a mixing zone may be provided including a mixer and a joint compression or compressing zone.
  • the joint compression zone the refrigerant and solvent stream are brought into contact with each other and the pressure on the refrigerant-solvent is raised sufficiently to facilitate dissolving of the refrigerant in the solvent in the mixer.
  • the compressor may be a rotary compressor, centrifugal compressor or rotary screw compressor.
  • refrigerant and solvent streams leaving the evaporator may be brought into contact in the compressing zone to form a combined solvent-refrigerant stream.
  • the solvent-refrigerant stream leaving the compressing zone and passing to the mixer may then be placed in heat exchange relation with the stream of solution leaving the mixer prior to passage of the stream of solution to the economizing zone. It is believed that the temperature of the combined solvent-refrigerant stream preferably approaches the temperature of the mixer just prior to entering the mixer.
  • the mass transfer of gaseous refrigerant is accomplished by passing a portion of the refrigerant stream leaving the compression zone to the stream of solution in the economizing zone, whereby the percentage of refrigerant in the solution stream is increased.
  • a chemically assisted mechanical refrigeration process including several steps.
  • a stream of solution including a solvent and a liquified refrigerant is passed to an evaporator.
  • the refrigerant and solvent have a negative deviation from Raoult's Law when in combination.
  • the pressure is then reduced over the solution to allow refrigerant to vaporize and separate from the solvent while concurrently therewith the evolving refrigerant and solvent are put in heat exchange relation with a working medium to remove energy from the working medium and thereby form a solvent stream and a refrigerant stream leaving the evaporator.
  • the refrigerant stream includes gaseous refrigerant.
  • the solvent stream leaving the evaporator is then passed in heat exchange relation with the solution stream passing to the evaporator in an economizing zone so as to cause transfer of heat between the solvent stream and the solution.
  • the solvent and refrigerant streams are put in fluid communication with each other so as to accomplish mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream and so facilitate heat transfer in the economizing zone between the solvent and solution streams.
  • the solvent and refrigerant streams are subsequently contacted in a joint compressing zone where the pressure over both streams is raised to form a combined solvent-refrigerant stream.
  • the combined solvent-refrigerant stream is then passed to a mixer under a pressure sufficient to promote substantial dissolving of the refrigerant in the solvent to form the stream of solution for passage to the evaporator.
  • a mixer is in heat exchange relation with a working medium, energy is removed from the mixer.
  • the vaporized refrigerant may be compressed by passing a high velocity liquid jet of solvent into the refrigerant. A portion of the refrigerant may also be passed to a generator-absorber pair prior to entering the mixer.
  • a chemically assisted mechanical refrigeration apparatus including a mechanical compressor for compressing a refrigerant and a mixing zone including a mixer for receiving a solvent and the compressed refrigerant at a pressure sufficient to promote substantial solution of the refrigerant in the solvent and form a solvent-refrigerant stream.
  • an evaporator zone including or consisting of an evaporator for receiving the refrigerant-solvent stream from the mixer and ultimately returning the refrigerant to the mixer after allowing at least a substantial portion of the refrigerant to separate from the solvent and absorb heats of vaporization and dissolution from a working medium, which medium is in heat exchange relation with the evolving refrigerant-solvent.
  • an economizing zone for placing the solvent passing from the evaporator zone to the mixing zone in heat exchange relation with the refrigerant-solvent stream passing from the mixer to the evaporator zone.
  • a heat exchanger including a conduit for passage of solvent and a surface adjacent to the conduit for receiving a thin film of solvent-refrigerant may be provided.
  • an injection mechanism for passing a portion of the compressed refrigerant directly into solution with the refrigerant-solvent stream after the mixture passes from the mixer as well as a heat exchanger for placing the refrigerant-solvent stream leaving the mixer in heat exchange relation with the solvent or both compressed refrigerant and solvent entering the mixer.
  • Coils may be substantially immersed in liquid in the evaporator for circulating the working medium or the evaporator may comprise a shell and tube heat exchanger arrangement.
  • the mechanical compressor may be a jet compressor adapted to use solvent from the evaporator to compress the refrigerant leaving the evaporator.
  • a chemically assisted mechanical refrigeration apparatus including an evaporator zone for receiving a refrigerant-solvent stream at a pressure sufficient to allow the refrigerant to separate from the solvent and absorb a substantial portion of the heats of vaporization and dissolution of the solvent-refrigerant stream from a working medium which is in heat exchange relation with the evolving refrigerant-solvent combination.
  • a compressor is provided and adapted to accept a gaseous stream and a liquid stream and raise the pressure of said streams upon combination.
  • a solvent conduit connects the evaporator and the compressor to allow passage of solvent from the evaporator to the compressor.
  • a refrigerant conduit connects the evaporator and the compressor for passage of a gaseous refrigerant from the evaporator to the compressor.
  • the refrigerant conduit is in fluid communication with the solvent conduit such that the refrigerant conduit may receive gases evolving from the solvent passing through the solvent conduit.
  • a solution conduit having one end connected to the mixer and the other end connected to the evaporator is also provided.
  • the solution conduit is adapted to facilitate any reduction in pressure between the mixer and the evaporator.
  • An economizer is also provided for placing the solvent conduit and the solution conduit in heat exchange relation with each other.
  • a second heat exchanger is provided for placing the solution conduit and a combined solvent-refrigerant conduit running from the compressor to the mixer in heat exchange relation with each other.
  • the compressor may be a rotary compressor, centrifugal compressor or rotary screw compressor.
  • FIG. 1 there is shown a schematic view of a chemically assisted mechanical refrigeration cycle.
  • An appropriate solvent-refrigerant stream preferably having the refrigerant totally in solution is introduced into evaporator 10 from line 21.
  • refrigerant vaporizes and separates from solvent under the operating conditions in the evaporator 10, such that heats of dissolution and vaporization are transferred to a working medium, such as water, circulating in conduit 22.
  • a solvent stream leaves as a liquid and is pumped by solvent pump 13 via line 19 to mixer-condenser 11, while a refrigerant stream of vaporized refrigerant leaves the evaporator via line 18 and through normally open valve 76 to be compressed in compressor 12 before being transferred to mixer 11 via line 14.
  • Valves 71 and 74 are operated to prevent any flow from occurring in lines 72 and 73, respectively.
  • valve 81 prevents flow through line 82.
  • the solvent-refrigerant stream passes via line 15 through expansion valve 16 where it is reduced in pressure before entering evaporator 10 via line 21.
  • the evaporator-effervescer 10 is so constructed as to allow substantial transfer of both the heat of vaporization and the heat of disassociation from the working fluid circulating through line 22.
  • the heat transfer surface may preferably be wetted by the solvent with or without dissolved refrigerant.
  • the refrigerant-solvent stream may be passed as a thin film over a heat transfer surface with embedded coils containing the working fluid.
  • a working fluid such as chilled water
  • a working fluid is passed via line 22 through the shell side of a shell and tube type heat exchanger while the refrigerant-solvent stream entering from line 21 passes through the tube side.
  • the refrigerant separates from the solvent in the tubes and both solvent and refrigerant pass to a liquid-vapor separator 31 where the solvent and refrigerant are separated.
  • the liquid-vapor separator 31 may be equipped with a wire mesh 32 to catch entrained droplets which collect below wire mesh 32.
  • the solvent passes via line 33 to pump 13 while the refrigerant passes via line 18 to compressor 12.
  • the conduit 22 is substantially immersed in liquid in the evaporator.
  • the refrigerant-solvent stream enters the evaporator the refrigerant substantially disassociates and boils off from the solvent, thus cooling the working fluid.
  • the evaporator may be similar in construction to a shell and tube heat exchanger wherein the working medium circulates through the tubes, which are substantially immersed in liquid.
  • the working medium may pass through a coil, which passes through the lower portion of the evaporator and so is substantially immersed in liquid.
  • the refrigerant-solvent stream may circulate and undergo separation in a single-tube coil of 1/2' diameter for a one to four ton apparatus and then further separate in a liquid-vapor separator.
  • the evaporator may comprise any one of several modified heat exchangers or evaporators.
  • an eliminator may be employed at the vapor outlet of the evaporator if the vapor and liquid separate into two streams in the evaporator. This may be particularly appropriate when the refrigerant is passed separately from the solvent to a mechanical compressor.
  • the compressor may be any one of several mechanical types. Regardless of the type of compressor used, in keeping with the spirit of the present invention, its operating cost should generally be less than that of its counterpart in a typical vapor compression refrigeration system for a given application. This is possible due to the increased efficiency of the present system. This increased efficiency over prior mechanical vapor compression cycles is believed to result in part from the fact that the solubility of the refrigerant in the solvent reduces the level of required mechanical compression.
  • the refrigerant need only be pressurized sufficiently to dissolve in the solvent in the condenser at the given operating conditions and concentrations. There is believed to be little or no wasted compression of the refrigerant to pressurize it sufficiently to condense at the condenser temperature as in the usual vapor compression cycle. Additionally, since the refrigerant is at a lower temperature as it leaves the mixer than in the case of a pure refrigerant cycle, less heat transfer is required and hence less working fluid need be circulated to the mixer.
  • the compressor chosen may vary with operating conditions, the refrigerant-solvent combination chosen or the application to which the system is applied.
  • a centrifugal, rotary or screw compressor may be preferred since the gas refrigerant passing through line 18 may still have some entrained liquid despite the use of an eliminator at the outlet of the evaporator 10.
  • the compressor may be a rotary compressor, centrifugal compressor or rotary screw compressor.
  • the solvent pump 13 may be any type suitable to pump the liquid solvent to the mixer under the operating conditions of the system.
  • a centrifugal pump may be preferred due to its simplicity, low first cost, uniform nonpulsating flow, low maintenance expense, quiet operation and adaptability to use with either a motor or a turbine drive.
  • a positive displacement pump such as a rotary, screw or gear pump may be preferred.
  • the mixer may be of a design similar to that of the evaporator, such that the system may serve as a heater as well as a refrigerator.
  • the refrigerant-solvent combination comprises at least two constituents - a refrigerant and a solvent.
  • the refrigerant and solvent are chosen such that the refrigerant will separate as a gas from the solvent under the operating conditions in the evaporator while preferably absorbing substantial amounts of the heats of demixing, dilution, or disassociation as well as vaporization.
  • a governing principle for the selection of a refrigerant-solvent combination is that the refrigerant be highly soluble in the solvent, such that the pair exhibits negative deviations from Raoult's Law.
  • refrigerants which are believed to be suitable for use in the present invention with appropriate solvents include hydrocarbons such as methane, ethane, ethylene and propane; halogenated hydrocarbons, such as refrigerants R20, R21, R22, R23, R30, R32, R40, R41, R161 and R1132a; amines, including methylamine, or gases used in certain refrigeration processes such as methyl chloride, sulfur dioxide, ammonia, carbon monoxide and carbon dioxide or any appropriate combinations of these.
  • hydrocarbons such as methane, ethane, ethylene and propane
  • halogenated hydrocarbons such as refrigerants R20, R21, R22, R23, R30, R32, R40, R41, R161 and R1132a
  • amines including methylamine, or gases used in certain refrigeration processes such as methyl chloride, sulfur dioxide, ammonia, carbon monoxide and carbon dioxide or any appropriate combinations of these.
  • the solvent constituent should be a substantially non-volatile liquid at the operating conditions of the cycle or be at least such when in solution with a portion of the refrigerant.
  • the solvent for example, nitrous oxide, can be a gas at room temperature.
  • the solvent may be an ether, an ester, an amide, an amine or polymeric derivatives of these, for example, dimethyl formamide and dimethyl ether of tetraethylene glycol as well as halogenated hydrocarbons, such as carbon tetrachloride and dichlorethylene; or appropriate combinations of these.
  • a halogenated salt such as lithium bromide may also be a constituent of the solvent.
  • solvents are methanol, ethanol, acetone, chloroform and trichloroethane.
  • Organic physical solvents such as propylene carbonate and sulfolane or other organic liquids containing combined oxygen may be used.
  • constituents may be added to the basic pair for other purposes, including foaming, lubrication, inhibition of corrosion, lowering of the freezing point, raising of the boiling point or indication of leaks.
  • constituents should preferably be chosen so as not substantially to detract from the heat of disassociation or vaporization produced in the evaporator. Further, the constituents are preferably such as to not detract from any negative deviations from Raoult's Law.
  • the comparative efficiency of the instant invention is illustrated by reference to available data for a refrigerant-solvent pair comprising CHCIF 2 (refrigerant 22) and dimethyl formamide (DMF).
  • a refrigerant-solvent pair comprising CHCIF 2 (refrigerant 22) and dimethyl formamide (DMF).
  • CHCIF 2 refrigerant 22
  • DMF dimethyl formamide
  • the R 22 will boil out of the DMF, absorbing a combined heat of vaporization and heat of mixing of slightly more than 72 Btu/lb.
  • the heat of mixing can be calculated from Equation (14) in Tyagi, K.P., Heat of Mixing --, Ind. Jnl. of Tech., 14 (1976), pp. 167-169, herein incorporated by reference, to be 19.33 Btu/lb., while the heat of vaporization of the R 22 is 55.92 Btu/lb. of solution.
  • the total heat absorbed, per pound of solution entering the evaporator is 75.25 Btu/lb., in close agreement with the enthalpy-concentration diagram mentioned above.
  • the refrigerant-solvent mixture or combination be chosen such that a substantial amount of refrigerant vaporizes from solution in the evaporator, this need not always be the case.
  • a refrigerant with a comparatively high heat of vaporization may be circulated in small proportions relative to the amount of solvent when the refrigerant-solvent leaving the mixer is placed in heat exchange relation with the solvent leaving the evaporator, as shall hereinafter be more fully described in conjunction with Figure 2.
  • the solvent leaving the evaporator can be passed through an economizer or auxiliary heat exchanger.
  • an economizer or auxiliary heat exchanger there is no need to directly heat the suction vapor passing to the compressor, thus reducing its density and increasing the volume of gas handled by the compressor.
  • FIG. 2 One form of this embodiment is illustrated in Figure 2. The operation of this embodiment is similar to that of the embodiment shown in Fig. 1. However, an economizer, which may be similar to a Baudelot cooler, is employed. Additionally, valves 41 and 42 will generally be closed unless the compressor is to be assisted by the absorber-generator pair as shall hereinafter be more fully described.
  • the refrigerant-solvent solution flows downward in a film over surfaces in the economizer-heat exchanger 26. These surfaces are chilled by cold solvent returning through conduit 24 from the evaporator-effervescer 10.
  • the cooling cascading refrigerant-solvent may also be bathed in the atmosphere of still coool refrigerant bled by valve 79 from the compressor outlet through conduit 27. Consequently, the heat of condensation as well as the heat of mixing of additional refrigerant absorbed by the cooled refrigerant-solvent stream is transferred to the cold solvent circulating through the economizer.
  • valve 79 may be closed and exchanger 26 operated only as a heat exchanger without any mixing occurring therein.
  • the compressor 12 pumps and compresses the refrigerant gas and pumps the compressed gas through conduit 14, while valve 79 is opened and another portion of the compressed gas is pumped through conduit 27.
  • the compressed gas going to the mixer 11 is mixed with the solvent and the refrigerant-solvent stream is directed through conduit 15 to the economizer 26 and expansion valve 16.
  • the refrigerant-solvent is then directed to the evaporator 10 as in Fig. 1.
  • the solvent from the evaporator is conducted via conduit 24 to the economizer 26 by the solvent pump 13 for recycling through the system.
  • the compressor 12 draws or sucks vaporized refrigerant through conduit 18 to complete the cycle.
  • Valve 79 may be operated to regulate or prevent flow through line 27 such that a specified portion or all of the compressed refrigerant passes to condenser-mixer 11.
  • valves 81 and 83 which are normally closed, may be opened such that compressed refrigerant passes via line 82 to heat exchanger 85 where it exchanges heat with the solvent-refrigerant stream passing through line 15.
  • the compressed refrigerant then passes via line 84 to mixer 11 as already described.
  • a chemically assisted mechanical refrigeration process including several steps.
  • the refrigerant and solvent have a negative deviation from Raoult's Law when in combination.
  • a stream of solution including a solvent and a liquified refrigerant is passed to an evaporator.
  • the pressure is then reduced over the solution to allow refrigerant to vaporize and separate from the solvent while concurrently therewith the evolving refrigerant and solvent are put in heat exchange relation with a working medium to remove energy from the working medium and thereby form a solvent stream and a refrigerant stream leaving the evaporator.
  • the refrigerant stream includes gaseous refrigerant.
  • the solvent stream leaving the evaporator is then passed in heat exchange relation with the solution stream passing to the evaporator in an economizing zone so as to cause transfer of heat between the solvent stream and the solution.
  • the solvent and refrigerant streams are put in fluid communication with each other so as to accomplish mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream and so facilitate heat transfer in the economizing zone between the solvent and solution streams.
  • the solvent and refrigerant streams are subsequently contacted in a joint compression zone where the pressure over both streams is raised to form a combined solvent-refrigerant stream.
  • the combined solvent-refrigerant stream is then passed to a mixer under a pressure sufficient to promote substantial dissolving of the refrigerant in the solvent to form the stream of solution for passage to the evaporator.
  • a mixer is in heat exchange relation with a working medium, energy is removed from the mixer.
  • a solvent-liquified refrigerant stream is passed via line 25 to evaporator 10.
  • the refrigerant and solvent of the solvent-liquified refrigerant stream have a negative deviation from Raoult's Law and may be chosen from a number of combinations of substances already described.
  • a refrigerant-solvent combination of R 22 -triechloroethane might be employed.
  • the pressure over the solvent-refrigerant stream is reduced in the evaporator in order to allow refrigerant to vaporize and separate from the solvent while concurrently placing the evolving refrigerant and solvent in heat exchange relation with the working medium to remove energy from the working medium.
  • a solvent stream which passes via line 24 and the refrigerant stream including gaseous refrigerant which passes via line 18.
  • the solvent stream passing via line 24 may contain a material portion of refrigerant without hindering the efficiency of the process. More particularly, the solvent stream leaving the evaporator and passing via line 24 is placed in heat exchange relation with the solvent-refrigerant stream passing to the evaporator via lines 15 and 25. Further, the solvent stream in line 24 is placed in fluid communication with the refrigerant stream of line 18 such that gaseous refrigerant evolving from the solvent stream 24 may pass via conduit 92 to refrigerant stream 18. This evolution of gas tends to cool the solvent stream, thus facilitating heat transfer in the economizer or economizing zone, which in turn increases the temperature drop in the solvent-refrigerant stream as it passes through the economizing zone.
  • any inefficiencies in the evaporator caused by a failure of the refrigerant to separate from the solvent are believed diminished since the refrigerant is allowed to further evolve from the solvent and the resulting change in energy is transferred indirectly to the working medium passing through the evaporator by virtue of the lowering of temperature of the solvent-refrigerant stream as it enters the evaporator.
  • Both the solvent stream and the refrigerant stream are then brought into contact in a joint compression zone as illustrated by compressor 88 in Figure 4.
  • the compression of the refrigerant along with the liquid in a joint compression zone such as compressor 88 is believed to provide several advantages.
  • the liquid solvent would generally have a higher heat capacity than the refrigerant and generally act as a coolant in the compressor, thus reducing the amount of work required to compress the refrigerant.
  • a liquid solvent may be chosen which acts both as a sealant and lubricant as well as a coolant.
  • the solvent provides internal cooling of the overall apparatus thus permitting compression which is more polytropic than isentropic and hence generally more economical. Additionally, it is believed that the presence of the solvent in the compressor permits higher pressures in the case of a centrifugal compressor, or serves as a lubricant and sealant in case of a rotary compressor.
  • the resulting combined solvent-refrigerant stream flows via line 90 through a heat exchanger such as precooler 86 and into mixer 11.
  • the heat exchanger or precooler 86 serves to further raise the temperature of the solvent-refrigerant combination passing to mixer 11 while concurrently beginning to cool the refrigerant-solvent stream passing via line 15 toward economizer 26.
  • the heat exchanger, such as precooler 86 should be operated so as to allow the temperature of the solvent-refrigerant combination stream entering mixer 11 to approach as closely as possible the temperature of mixer 11 without exceeding the same. Additionally, the precooler should be operated in such a fashion that the temperature of the solvent-refrigerant combination passing via line 90 is such that the refrigerant will not start to substantially dissolve and give off heat prior to reaching the mixer 11.
  • the mixer 11 in the mixer 11 the combined solvent-refrigerant stream is maintained at a pressure sufficient for the given temperature to promote substantial dissolving of the refrigerant in the solvent to form the stream of solution for passage to the evaporator 10 via lines 15 and 25. Concurrently therewith, the mixer is in heat exchange relation with a working medium which removes energy or heat given off by the dissolving and condensing refrigerant in the mixer 11.
  • the refrigerant-solvent combination may be used to cool the refrigerant-solvent stream exiting the mixer. Since this combination passing via line 90 is at mixer pressure as it enters the mixer, but below mixer temperature as it begins its passage through heat exchanger 86, it is assumed that solution of refrigerant into solvent will have begun in the precooler 86.
  • R 22 as a refrigerant and 1,1,1-trichloroethane as the solvent at the temperatures shown, a theoretical maximum of only half the heat exchange theoretically available for inert liquids is available, and the resultant theoretical coefficient of performance is 7.13 (The theoretical maximum coefficient of performance for a perfect (Carnot) cycle is 7.14.)
  • n 1.09.
  • the work of compression in Btu, J(1-n), is 2.05 Btu per .316 lb R 22 vaporized.
  • V 1 and V 2 are taken from the superheat tables of [American Society of Heating, Refrigerating and Air Conditioning Engineers, Thermodynamic Properties of Refrigerants, 1980].
  • the density of the stripped TCE leaving the economizer 26 is 83.98 1b/ft 3
  • the pressure head across the 70 psi differential is 120.42 ft.
  • the Btu of pumping .684 lb of TCE is .106.
  • the total work of compresing the gas and pumping the liquid is 2.16 Btu/lb of mixture.
  • the pump type compressor 12 may be replaced with a jet compressor.
  • a high velocity liquid jet of solvent supplied to the jet compressor by a portion of the solvent from line 19 may be used to compress the refrigerant gas coming from the evaporator-effervescer 10.
  • the presence of a higher specific heat solvent is believed to result in more efficient compression, due to the greater heat capacity of a liquid. More particularly, the compression becomes more nearly isothermal, hence more efficient.
  • compressor 12 and solvent pump 13 may both be replaced by a liquid ring compressor which compresses the refrigerant gas, circulates the solvent and initiates mixing of gas and solvent prior to entry into mixer 11 through a single conduit. Compression is understood to be more nearly isothermal and hence more efficient.
  • valve 76 may be closed off and valve 71 and liquid ring compressor 77 operated such that both solvent and refrigerant pass from evaporator 10 via line 72 to ring compressor 77. The compressed mixture would then pass to mixer 11.
  • the ring compressor 77 might be a double lobe compressor manufactured by Nash Engineering Co. of South Norwalk, Connecticut and described in that company's Bulletin No. 474-C dated 1971.
  • the refrigerant may be foamed with the solvent and solvent pump 13 could be eliminated from the embodiment shown in Figure 1. Both refrigerant and solvent would be circulated from evaporator 10 to the compressor 12 and hence to mixer 11.
  • the embodiment shown in Figure 2 may also be modified.
  • the solvent pump 13 may be replaced with a device to inject the compressed refrigerant gas from conduit 14 into the solvent stream in conduit 24, thus propelling both refrigerant gas and solvent liquid to condenser-mixer 11.
  • valves 71 and 74 may be operated so as to allow at least a portion of solvent to bypass solvent pump 13 while valve 74 is operated to allow a sufficient amount of vapor to pass from line 14 into line 72 via line 73.
  • a generator-absorber pair might be hooked up in tandem with the compressor to provide a back-up for the same.
  • the generator could function off a secondary source of heat, such as from an exhaust, or a form of solar energy.
  • valves 41 and 42 could be placed on both sides of compressor 12 in lines 18 and 14 to hook a generator-absorber pair 48, 44 into the system.
  • a portion of the vaporized refrigerant could then pass from line 18 via line 43 to the absorber, absorbed in an appropriate secondary solvent and then be pumped in solution by pump 46 through lines 45 and 47 to the generator 48.
  • the now compressed vapor could be passed via line 49, valve 42 and line 14 to the mixer 11, while secondary solvent was returned to the absorber 44, via line 50.
  • the secondary solvent may be the same as used in the primary system.
  • the generator-absorber pair should not be completely substituted for the compressor 12. Rather, the generator-absorber pair and the mechanical compressor are complementary means of generating pressurized refrigerant gas.
  • the Wankel-type compressor manufactured by Ogura Clutch of Japan, or the rolling piston compressors of Rotorex (Fedders) and Mitsubishi may prove useful.
  • the multistage centrifugal compressor-pump of the type manufactured by Sihi In this device, a gas-liquid mixture enters a first, closed impeller axially and the denser liquid is thrown to the periphery. The lighter gas is ported off to the second and subsequent stages nearer the center of the chamber and both gas and liquid are then carried together through second and subsequent impeller stages.
  • a turbine may be installed in the refrigerant-solvent stream between the economizer and evaporator to function as a pressure reducing device, supplementing throttling devices.
  • a subcooled stream exiting the economizer is least likely to flash refrigerant gas at this point and..the resultant shaft work may be used to power booster pumps, compressors for the system, auxilliary fans or the like.
  • Additional items of equipment may be employed within the framework of the present invention.
  • control of the system as well as system versatility may be enhanced through the use of appropriate process controls, though the use of essentially manual control devices may suffice for many operations.
  • a low pressure drop mixing of gaseous refrigerant and liquid could be achieved by using an inline motionless mixer such as one offered by the Mixing Equipment Co., Inc. of Avon, New York.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Surface Acoustic Wave Elements And Circuit Networks Thereof (AREA)
  • Measuring Temperature Or Quantity Of Heat (AREA)
EP84110693A 1983-09-29 1984-09-07 Chemisch unterstützter mechanischer Kühlprozess Expired EP0138041B1 (de)

Priority Applications (1)

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

Applications Claiming Priority (2)

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

Publications (3)

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

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

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0248296A2 (de) * 1986-05-23 1987-12-09 Energiagazdálkodási Részvénytársaság Verfahren zur Erhoehung des Leistungsfaktors von hybriden Kaeltemaschinen oder Waermepumpen
EP0276251A1 (de) * 1986-07-02 1988-08-03 RADERMACHER, Reinhard Wärmepumpenkeislauf mit dampfkompression unter verwendung einer mischung von nichtazeotropen fluidtreibmitteln
WO1994007095A1 (de) * 1992-09-15 1994-03-31 Fritz Egger Gmbh Verfahren und einrichtung zur leistungsregelung einer kompressions-wärmepumpe und/oder kältemaschine
FR2726894A1 (fr) * 1994-11-10 1996-05-15 Electricite De France Pompe a chaleur a compression-absorption avec separation d'huile en phase liquide
FR2726895A1 (fr) * 1994-11-10 1996-05-15 Electricite De France Pompe a chaleur a compression-absorption fonctionnant avec transfert de chaleur du circuit d'huile vers le circuit de solution pauvre
DE102007016738A1 (de) * 2007-04-07 2008-10-09 pro Kühlsole GmbH Neuer Wärmeträger für Solaranlagen
US9909791B2 (en) 2013-04-11 2018-03-06 Carrier Corporation Combined vapor absorption and mechanical compression cycle design

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102013211084A1 (de) * 2013-06-14 2014-12-18 Siemens Aktiengesellschaft Verfahren zum Betrieb einer Wärmepumpe und Wärmepumpe

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US1675455A (en) * 1928-07-03 System of refrigeration
DE485656C (de) * 1925-09-25 1929-11-02 Chicago Pneumatic Tool Co Verfahren zur Kaelteerzeugung durch Kompression und Absorption
DE593548C (de) * 1932-01-19 1934-03-02 Carl Lindstroem Akt Ges Verfahren zur Kaelteerzeugung
US2182453A (en) * 1936-01-18 1939-12-05 William H Sellew Heat transfer process and apparatus
DE953378C (de) * 1950-08-29 1956-11-29 Margarete Altenkirch Geb Schae Verfahren und Vorrichtung zum Betrieb einer Waermepumpe
FR2308885A1 (fr) * 1975-04-28 1976-11-19 Zeilon Sten Olof Procede de refrigeration utilisant la loi compression-absorption et appareil destine a le mettre en oeuvre
DE2801529A1 (de) * 1978-01-14 1979-07-19 Gustav Schaefer Fa Kaeltemaschine
USRE30252E (en) * 1974-11-14 1980-04-08 Carrier Corporation High temperature heat recovery in refrigeration
DE2850403A1 (de) * 1978-11-21 1980-05-29 Luft U Kaeltetechnik Veb K Kompressionskaeltemaschine mit loesungskreislauf
GB2044907A (en) * 1979-03-15 1980-10-22 Vaillant J Gmbh & Co Heat pump, particularly vapour- compressing jet type heat pump
EP0021205A2 (de) * 1979-06-08 1981-01-07 Energiagazdalkodasi Intezet Hybrides Kompressions-Absorphionsverfahren für das Betreiben von Wärmepumpen oder Kältemaschinen
EP0056147A1 (de) * 1981-01-08 1982-07-21 Dieter Dr.-Ing. Markfort Resorptions-Anlage zur Wärmetransformation
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
DE3204460A1 (de) * 1982-02-09 1983-08-18 Braukmann Kessel GmbH, 6966 Seckach Resorptionswaermepumpe

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5864470A (ja) * 1981-10-13 1983-04-16 工業技術院長 圧縮式冷凍装置

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1675455A (en) * 1928-07-03 System of refrigeration
DE485656C (de) * 1925-09-25 1929-11-02 Chicago Pneumatic Tool Co Verfahren zur Kaelteerzeugung durch Kompression und Absorption
DE593548C (de) * 1932-01-19 1934-03-02 Carl Lindstroem Akt Ges Verfahren zur Kaelteerzeugung
US2182453A (en) * 1936-01-18 1939-12-05 William H Sellew Heat transfer process and apparatus
DE953378C (de) * 1950-08-29 1956-11-29 Margarete Altenkirch Geb Schae Verfahren und Vorrichtung zum Betrieb einer Waermepumpe
USRE30252E (en) * 1974-11-14 1980-04-08 Carrier Corporation High temperature heat recovery in refrigeration
FR2308885A1 (fr) * 1975-04-28 1976-11-19 Zeilon Sten Olof Procede de refrigeration utilisant la loi compression-absorption et appareil destine a le mettre en oeuvre
DE2801529A1 (de) * 1978-01-14 1979-07-19 Gustav Schaefer Fa Kaeltemaschine
DE2850403A1 (de) * 1978-11-21 1980-05-29 Luft U Kaeltetechnik Veb K Kompressionskaeltemaschine mit loesungskreislauf
GB2044907A (en) * 1979-03-15 1980-10-22 Vaillant J Gmbh & Co Heat pump, particularly vapour- compressing jet type heat pump
EP0021205A2 (de) * 1979-06-08 1981-01-07 Energiagazdalkodasi Intezet Hybrides Kompressions-Absorphionsverfahren für das Betreiben von Wärmepumpen oder Kältemaschinen
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
EP0056147A1 (de) * 1981-01-08 1982-07-21 Dieter Dr.-Ing. Markfort Resorptions-Anlage zur Wärmetransformation
DE3204460A1 (de) * 1982-02-09 1983-08-18 Braukmann Kessel GmbH, 6966 Seckach Resorptionswaermepumpe

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
W.B.GOSNEY, Priciples of Refrigeration, Cambridge University Press, page 470 *

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0248296A2 (de) * 1986-05-23 1987-12-09 Energiagazdálkodási Részvénytársaság Verfahren zur Erhoehung des Leistungsfaktors von hybriden Kaeltemaschinen oder Waermepumpen
EP0248296A3 (en) * 1986-05-23 1988-05-25 Energiagazdalkodasi Intezet Method and device for increasing the coefficient of performance of hybrid refrigeration machines or heat pumps
EP0276251A1 (de) * 1986-07-02 1988-08-03 RADERMACHER, Reinhard Wärmepumpenkeislauf mit dampfkompression unter verwendung einer mischung von nichtazeotropen fluidtreibmitteln
EP0276251A4 (de) * 1986-07-02 1988-11-22 Reinhard Radermacher Wärmepumpenkeislauf mit dampfkompression unter verwendung einer mischung von nichtazeotropen fluidtreibmitteln.
WO1994007095A1 (de) * 1992-09-15 1994-03-31 Fritz Egger Gmbh Verfahren und einrichtung zur leistungsregelung einer kompressions-wärmepumpe und/oder kältemaschine
FR2726894A1 (fr) * 1994-11-10 1996-05-15 Electricite De France Pompe a chaleur a compression-absorption avec separation d'huile en phase liquide
FR2726895A1 (fr) * 1994-11-10 1996-05-15 Electricite De France Pompe a chaleur a compression-absorption fonctionnant avec transfert de chaleur du circuit d'huile vers le circuit de solution pauvre
DE102007016738A1 (de) * 2007-04-07 2008-10-09 pro Kühlsole GmbH Neuer Wärmeträger für Solaranlagen
US9909791B2 (en) 2013-04-11 2018-03-06 Carrier Corporation Combined vapor absorption and mechanical compression cycle design

Also Published As

Publication number Publication date
ATE41506T1 (de) 1989-04-15
JPH0532664B2 (de) 1993-05-17
EP0138041A3 (en) 1986-03-26
EP0138041B1 (de) 1989-03-15
CA1233655A (en) 1988-03-08
DE3477259D1 (en) 1989-04-20
JPS60105869A (ja) 1985-06-11

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