JPS60105869A - Chemically assisted machine refrigeration method - Google Patents

Abstract

There is provided a chemically assisted mechanical refrigeration process including the steps of: mechanically compressing a refrigerant stream which includes vaporized refrigerant; contacting the refrigerant with a solvent in a mixer (11) at a pressure sufficient to promote substantial dissolving of the refrigerant in the solvent in the mixer (11) to form a refrigerant-solvent solution while concurrently placing the solution in heat exchange relation with a working medium to transfer energy to the working medium, said refrigerant-solvent solution exhibiting a negative deviation from Raoult's Law; reducing the pressure over the refrigerant-solvent solution in an evaporator (10) to allow the refrigerant to vaporize and substantially separate from the solvent while concurrently placing the evolving refrigerant-solvent solution in heat exchange relation with a working medium to remove energy from the working medium to thereby form a refrigerant stream and a solvent stream; and passing the solvent and refrigerant stream from the evaporator.

Description

TECHNICAL FIELD OF THE INVENTION This invention relates generally to refrigeration, and more particularly to a new and improved chemically assisted mechanical refrigeration cycle.

[Background of the invention]

A typical mechanical refrigeration system uses a mechanical compressor to increase pressure and condense a gaseous refrigerant, which then absorbs its heat of vaporization. Thus, a typical vapor compression cycle consists of an evaporator in which a liquid refrigerant, such as Freon-12, is boiled at low pressure to produce refrigeration; a compressor that increases the pressure of the gaseous refrigerant after it leaves the evaporator; It uses a condenser that condenses and releases its heat to the environment; and an expansion valve where the liquid refrigerant leaving the condenser expands from a high pressure level in the condenser to a low pressure level in the evaporator.

Much effort has been expended over the past several decades to develop refrigeration systems that utilize cord energy sources, such as solar energy, without the need for compressors or pumps. Much of this effort has The so-called absorption cycle achieves compression by absorbing the refrigerant gas using a secondary fluid as a vapor compression cycle.A typical absorption system uses a condenser, expansion valve and evaporator as in a vapor compression cycle However, instead of a compressor an absorber-generator pair is used.Lithium bromide-water or water-
Ammonia is typical of the solvent-refrigerant mixtures used.

Resorption cycles have also been studied. In the first half of this century, resorption cycles were similar in operation to absorption cycles. However, a reabsorber is used instead of a condenser, and the vapor is absorbed by a special weak solution while condensing. This solution is then circulated to an evaporator in which the refrigerant boils and the heat of dissociation and vaporization produces a refrigeration effect.

While most conventional systems avoid the use of a compressor when using a solvent-refrigerant combination, the method of 2.3 uses a solvent-refrigerant pair together with a compressor in the system. There is. The system and method described in US Pat. No. 4,037,426 is illustrative. In this patent, a gaseous refrigerant is compressed and then mixed with a liquid solvent. The mixture is then cooled in a heat exchanger and then passed to a decanter in which the heavier liquid fraction is separated from the lighter liquid refrigerant. The liquid refrigerant then passes to a low pressure zone where it is evaporated and absorbs heat from the working fluid. U.S. Pat. No. 3,277.659 and 4,19
The system or method disclosed in No. 9,961 provides another example of a compressor-type system.

Corella's traditional system and other traditional systems are
Incur one or more of several disadvantages. For example, conventional systems typically cool the working medium in a compression-type cycle at the end.
It is not possible to take advantage of both heat of vaporization and heat of dilution. Additionally, conventional systems utilizing compressors require heavy duty compressors that can withstand relatively high compression ratios. Other systems operate at relatively high pressures.
Still other systems have relatively inefficient heat transfer dynamics. Still other systems reduce the flow intensity to the compressor. cannot enable supplementary heat exchange between refrigerant-solvent and solvent without a refrigerant, while other systems cannot provide sensible heat transfer in supplementary heat exchange between refrigerant-solvent and solvent. .

Still other systems fail to provide secondary generation of gaseous refrigerant from the solvent after it leaves the evaporator to increase overall efficiency. These σ) and other problems encountered by conventional systems are substantially reduced, if not eliminated, by the present invention.

[Summary of the invention]

A chemically assisted mechanical refrigeration method is provided that uses a refrigerant and a solvent that when combined with each other have a negative deviation from Raoult's law. A solution stream containing solvent and liquefied refrigerant is passed to an evaporator. The pressure above the bath liquid is then reduced to evaporate the refrigerant and separate it from the solvent. At the same time, the generated refrigerant and solvent are engaged in a heat exchange relationship with the working medium to remove energy from the working medium. A refrigerant stream comprising a solvent stream and a gaseous refrigerant is formed and leaves the evaporator. Thereafter, the refrigerant stream is subjected to mechanical compression and the refrigerant and solvent streams are contacted at a pressure sufficient to promote substantial dissolution of the refrigerant and solvent. A solution stream for passage to the evaporator is thus formed. Energy is removed therefrom when the refrigerant and solvent are in a heat exchange relationship with the working medium at least part of the time they are in contact and mixed.

In one embodiment, the solvent stream leaving the evaporator is preferably passed in heat exchange relationship with the solution stream passing to the evaporator. This means that the economizer band
ngzone θ) resulting in heat transfer between the solvent and solution streams.

Such heat transfer may be facilitated by mass transfer of gaseous refrigerant with respect to one or more streams passing through the economizer zone. For example: - In embodiments, the solvent stream leaving the evaporator contains a substantial portion of dissolved refrigerant. The solvent stream is placed in fluid communication with the refrigerant stream leaving the evaporator to effect mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream. This facilitates heat transfer within the economizer zone prior to passage of the solvent and refrigerant streams to the mixing zone.

In a modification of this example, mixer and co(j
oint) A mixing zone including a compression zone may be provided. In the co-compression zone, the refrigerant and solvent streams are brought into contact with each other and the pressure above the refrigerant-solvent is increased sufficiently to facilitate dissolution of the refrigerant into the solvent within the mixer.

2 after the refrigerant and solvent streams leaving the generator are placed in fluid communication with each other to enable the generation of gas σ from the solvent stream.
If the two streams pass through a joint compression zone containing a single compressor, the compressor can be a rotary compressor, a centrifugal compressor or a rotary screw compressor.

In still yet another modification, the refrigerant and solvent streams leaving the evaporator can be combined in a compression zone at °C to form a combined solvent-refrigerant stream. The solvent-refrigerant stream leaving the compression zone and passing through the mixer is then
Prior to passage of the solution stream to the zone, it may be placed in a heat exchange relationship with the solution stream leaving the mixer.

It is believed that the temperature of the combined solvent-refrigerant stream preferably approaches the temperature of the mixer immediately before introduction of the mixer.

In another embodiment, mass transfer of the gaseous refrigerant is accomplished by passing a portion of the refrigerant stream leaving the compression zone into the solution stream in an economizer zone, whereby the fraction of refrigerant in the solution stream is increased. be done.

In a more detailed embodiment, a chemically assisted mechanical refrigeration process involving several steps may be provided. A solution stream containing solvent and liquefied refrigerant is passed to an evaporator.

Refrigerant and solvent have a negative deviation from Raoult's law in #1 combination. Pressure is then reduced across the solution to vaporize the refrigerant and separate it from the solvent, while at the same time the generated refrigerant and solvent are placed in heat exchange relationship with the working medium to remove energy from the working medium and remove it from the working medium. forming a solvent stream and a refrigerant stream leaving the evaporator. The refrigerant stream includes gaseous refrigerant. Then,
The solvent stream leaving the evaporator is passed in an economizer zone in heat exchange relationship with the solution stream passing through the evaporator to effect heat transfer between the solvent stream and the solution. At the same time, the solvent stream and the refrigerant stream are placed in fluid communication with each other to achieve mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream, thus providing an economizer zone between the solvent stream and the solution stream. facilitates heat transfer within the Thereafter, the solvent and refrigerant streams are
They are contacted in a co-compression zone where the pressure on both streams is increased to form a combined solvent-refrigerant stream. The combined solvent-refrigerant stream is then passed through a mixer under sufficient pressure to promote substantial dissolution of the refrigerant in the solvent to form a solution stream for passage to the evaporator. Energy is removed from the mixer when the mixer is in heat exchange relationship with the working medium.

In another embodiment, the evaporated refrigerant may be compressed by passing a high velocity liquid jet of solvent through the refrigerant. A portion of the refrigerant may also be passed through the generator-absorber pair before introduction to the mixer.

According to the invention, a mechanical compressor compresses a refrigerant and a mixer receives the solvent and compressed refrigerant under sufficient pressure to promote substantial dissolution of the refrigerant in the solvent and form a solvent-refrigerant flow. A chemically assisted mechanical refrigeration device that includes a mixed zone of inclusion is also provided. a final step after receiving a refrigerant-solvent stream from the mixer and separating at least a substantial portion of the refrigerant from the solvent and absorbing the heat of vaporization and heat of solution from the working medium (the medium being in heat exchange relationship with the generated refrigerant-solvent); An evaporation zone is also provided which includes or consists of an evaporator which returns the refrigerant to the mixer.

The solvent passing from the evaporation zone to the mixing zone is placed in heat exchange relationship with the refrigerant-solvent stream passing from the mixer to the evaporation zone (economizer zones may also be provided).

For example, a heat exchanger may be provided that includes a conduit for the passage of a solvent and a surface adjacent to the conduit that receives a thin film of solvent-refrigerant. an injection mechanism that passes a portion of the compressed refrigerant directly into the solution together with the refrigerant-solvent stream after the mixture has passed through the mixer; A heat exchanger can also be provided in the heat exchange relationship.

The coils that circulate the working medium may be substantially immersed in the liquid within the evaporator, or may consist of a multi-tube heat exchanger arrangement. In embodiments, the mechanical compressor can be a jet compressor suitable for compressing refrigerant leaving the evaporator using solvent from the evaporator.

In a more detailed embodiment, the refrigerant is separated from the solvent and a substantial portion of the heat of vaporization and melting of the solvent-refrigerant stream is absorbed from the working medium in heat exchange relationship with the generated refrigerant-solvent sigma. A chemically assisted mechanical refrigeration system can be provided that includes an evaporation zone that receives a refrigerant-solvent flow under sufficient pressure to cause the refrigerant to evaporate. The compressor is arranged and adapted to receive a gas stream and a liquid stream and to increase the pressure of said streams upon their merging. A solvent conduit connects the evaporator and compressor to allow passage of solvent from the evaporator to the compressor. A refrigerant conduit connects the evaporator and compressor to pass gaseous refrigerant from the evaporator to the compressor. The refrigerant conduit is in fluid communication with the solvent conduit so as to receive gas generated from the solvent passing through the solvent conduit. A solution conduit is also provided having one end connected to the mixer and the other end connected to the evaporator. The solution conduit is suitable for facilitating pressure reduction between the mixer and the evaporator. An economizer is also provided which places the solvent conduit and solution conduit in heat exchange relationship with each other.

In still more detailed embodiments, a second heat exchanger is provided which places the solution conduit and the combined solvent-refrigerant conduit running from the compressor to the mixer in heat exchange relationship with each other. In any case where the refrigerant and solvent are contacted in a compressor, the compressor can be a rotary compressor, a centrifugal compressor or a rotary screw compressor.

[Detailed description of the invention]

A detailed description of embodiments of the present invention, including preferred embodiments of the present invention, will be described below together with the drawings. This description is to be construed as illustrative rather than limiting.

Referring first to FIG. 1, a schematic diagram of a chemically assisted mechanical refrigeration cycle is shown. A suitable solvent-refrigerant stream, preferably having the refrigerant completely in solution, is barreled into evaporator 1G from line 21. As will be described in more detail below, the refrigerant evaporates under operating conditions in the evaporator 10 and separates from the solvent, so that the heat of solution and vaporization is recycled into the conduit 22. transferred to a medium, such as water. The solvent stream leaves as a liquid and is pumped by solvent pump 13 through line 19 to mixer-condenser 11, while the refrigerant stream of evaporated refrigerant is pumped through line 8 (through normally open valve 76). ) leaves the evaporator and is compressed in compressor 12 before being transferred through line 14 to mixer 11. Valves 71 and 74 are operated so that no flow occurs in lines 72 and 73, respectively. Similarly, valve 81 prevents flow through line 82.

At the operating conditions of mixer 11, the now compressed refrigerant is dissolved in the solvent entering the mixer from line 19.

The heat of mixing and condensation is recovered from the condenser-mixer 11 by the working medium in line 23. In this way a solvent-coolant stream is formed.

The solvent-refrigerant stream passes via line 15 through an expansion valve 16 where it is depressurized before entering the evaporator 10 via line 21.

Evaporator-effervescer 10 is constructed to permit substantial transfer of both heat of vaporization and heat of dissociation from the working fluid circulating through line 22. Efficient heat transfer is facilitated by the use of a wet heat transfer surface, so that the heat transfer surface can preferably be wetted with a solvent with or without a dissolved refrigerant. Thus - in an embodiment, the refrigerant-solvent stream may be passed as a thin film over the heat transfer surface using an embedded coil containing the working fluid.

In another embodiment shown in FIG. 3, the working fluid, e.g. cooling water, is passed through the shell side of the shell-and-tube heat exchanger via line 22, while the refrigerant entering from line 21 -
The solvent flow passes through the tube side. The refrigerant is separated from the solvent in the tube and both solvent and refrigerant pass to a gas-liquid separator 31 where the solvent and refrigerant are separated. The gas-liquid separator 31 includes a wire mesh 3 that catches entrainment droplets that collect below the wire mesh 7 32.
2 can be provided. Solvent passes to pump 13 via line 33, while refrigerant passes to compressor 12 via line 18.

In another embodiment, conduit 22 is substantially immersed in the liquid within the evaporator. When the refrigerant-solvent stream enters the evaporator,
The refrigerant substantially dissociates and boils off from the solvent, thus cooling the working fluid. In such embodiments, the evaporator may be similar in construction to a shell-and-tube heat exchanger in which the working medium circulates through tubes that are substantially immersed in the liquid.

Alternatively, the working medium can be passed through the coil. It passes to the bottom of the evaporator and is thus virtually immersed in the liquid. As an example, the refrigerant-solvent stream may be circulated through a 1/2 foot diameter single tube coil for a 1 to 4 ton device and subjected to separation and then further separation in a gas-liquid separator. can do.

As would be known to those skilled in the art with the benefit of this disclosure:
The evaporator can consist of any of several modified heat exchangers or evaporators.

If it is desired to facilitate the separation of the evaporated refrigerant from the solvent, an eliminator (el, 1 m
1nator) can be used with an evaporator vapor volume of 1]. This may be particularly suitable when the refrigerant passes separately from the solvent to the mechanical compressor.

The compressor can be any of several mechanical types. In keeping with the spirit of the invention, regardless of the type of compressor used, its operating cost should generally be lower than that of its counterpart in a typical vapor compression refrigeration system for a given application. It is. This is possible due to the increased efficiency of the system. The increased efficiency over conventional mechanical vapor compression cycles is believed to result, in part, from the fact that the solubility of the refrigerant in the solvent is reduced to the level of mechanical compression required. The refrigerant need only be pressurized enough to dissolve in the solvent in the condenser at the given operating conditions and concentration. Wasting compression of the refrigerant to pressurize the culm enough to condense at the condensing temperature as in a normal vapor compression cycle)
It can be believed that there is no money or nothing. Additionally, because the refrigerant is cooler when it leaves the mixer than in a pure refrigeration cycle, less heat transfer is required and therefore less working fluid needs to be circulated to the mixer.

The compressor selected can vary depending on the operating conditions, the refrigerant-solvent combination being shielded, or the application to which the system is applied. For example, in the embodiment shown in FIGS. 1 and 2, the gaseous refrigerant passing through line 18 may still have some entrained liquid despite the use of an eliminator at the outlet of evaporator 10. Centrifugal, rotary or screw compressors may be preferred. Alternatively, the embodiment shown in FIG. 4 in which the refrigerant and solvent streams leaving the evaporator are brought into fluid communication with each other to enable generation of gas from the solvent stream, and then the two streams are passed to a single compressor. In examples, the compressor can be a rotary compressor, a centrifugal compressor or a rotary screw compressor.

If a solvent pump is to be used, such as in the embodiment described in FIGS. 1 and 2, the solvent pump 13 pumps liquid solvent into the mixer under the operating conditions of the system. Any FFR suitable for sending
It can also be 84. Centrifugal pumps may be preferred because of their simplicity, low primary cost, uniform non-pulsating flow, low maintenance costs, quiet operation and suitability for use with motor or turbine drives. On the other hand, positive displacement pumps, such as rotary, screw or gear pumps, may be preferred.

Keeping in mind the pressure difference between the evaporator 10 and the mixer, the mixer can have a similar design to that of the evaporator, so that the acid system can serve as a heater as well as a refrigerator.

A refrigerant-solvent combination consists of at least two components: a refrigerant and a solvent. The refrigerant and solvent are preferably such that the refrigerant will separate as a gas from the solvent under operating conditions in the evaporator while absorbing the effects of demixing heat, heat of dilution or dissociation, and heat of vaporization. selected. Thus, the governing principle for the selection of refrigerant-solvent combinations is that the refrigerant is readily soluble in the solvent such that the pair exhibits a negative deviation from Raoult's law.

Examples of refrigerants believed to be suitable for use in the present invention with suitable solvents are hydrocarbons such as methane, ethane, ethylene, propane; halogenated hydrocarbons such as refrigerants R20, R21, R22, R23, R3
0, R32, R40, R41, R161 and R113
2a; amines, such as methylamine, or gases used in refrigeration processes, such as methyl chloride, sulfur dioxide, ammonia, carbon oxide and carbon dioxide, or suitable combinations thereof.

The solvent component should be a substantially non-volatile liquid at the operating conditions of the cycle, or at least a non-volatile liquid when in solution with a portion of the refrigerant σ). Thus, the solvent, such as nitrous oxide, can be a gas at room temperature.

Solvents can be ethers, esters, amides, amines or polymeric derivatives thereof, such as dimethylformamide and dimethyl ether of tetraethylene glycol, and halogenated hydrocarbons, such as carbon tetrachloride and dichloroethylene; I believe it can be done. Halogenated salts, such as lithium bromide, can also be a component of the solvent.

Methanol, ethanol, acetone, chloroform and trichloroethane are also believed to be suitable as solvents. Organic solvents such as propylene carbonate and sulfolane or other organic liquids containing bound oxygen may be used.

A relatively large deviation from Raoult's law, and therefore a relatively large heat of mixing, is obtained when one or preferably both of the refrigerant and solvent molecules are polar. The excessive solubility is believed to be the result of dipole-dipole attraction (including hydrogen bonding) or induced dipole-dipole attraction.

Alternatively, limited experimental data and calculations indicate that certain combinations of refrigerant and solvent may not have satisfactory coefficients of performance. Thus, for the specific example shown in FIG.
It shows that the combination with -1-lichloroethane is not very efficient.

More specifically, with respect to FIG. 4, R22 and 1°1.
Calculations compared to those described below for 1-1lichloroethane are based on hypothetical evaporator temperatures of approximately -15, 5FC, and 5FC, respectively.
0℃) and mixer temperature 86FC (about 30°C, OC), operating coefficient 1.83, temporary evaporator temperature 40F (about 4
．． 44°C) and mixer temperature 110°F (approximately 43°C)
) yielded 1.49. This probably means that
The high critical temperature of carbon dioxide is 87.87 F (approximately 31.0
°C) and high critical pressure of 1069.96 psia.

It is believed that other chemical components may be added to the base pair for other purposes such as foaming, lubrication, corrosion control, freezing point depression, boiling point elevation, or leakage indication.

However, such additive components should preferably be selected so as not to substantially inhibit the heat of dissociation or vaporization generated in the evaporator. Furthermore, the ingredients are preferably such that they do not interfere with negative deviations from Raoult's law.

The comparative efficiency of the present invention is illustrated by reference to available data in the case of a refrigerant-solvent consisting of 0HOIF2 (refrigerant 22) and dimethylformamide (DMF). M., Zielinek et al., "Enthalpy-concentration diagram", A, S, H, R, A, B, '
1hns.

J and (1978), pt, n, pp 60-67
According to the entropy concentration diagram disclosed in R22-D
The MF solution was heated at 56.8 psig and 86F (approximately 30
．． C1 field distribution R22 that is in equilibrium at 0'l:l:)
60% and DMF 40%). If the pressure is reduced sufficiently, R22 will boil from DM11' and 72 Bt
It will absorb a total amount of heat of vaporization and heat of mixing slightly more than u/lb. Alternatively, the heat of mixing is K, P,
Kugi, "Mixed Heat", Ind, Jn Yu.

of TθOh, 14 (1976), 111
1:19.33 from formula (14) in 1.167-169
Btu/lb, while the heat of vaporization of R22 is 55.92 Btu/lb of solution.

Thus, the total heat absorbed per bond of solution entering the evaporator is 75.25 Btu/bond,
It almost matches the entropy-concentration diagram mentioned above.

It may be preferred, but not necessarily, that the refrigerant-solvent mixture or blend be selected such that a substantial amount of the refrigerant evaporates from solution in the evaporator. For example, as will be described in more detail below in conjunction with FIG. 2, the refrigerant-M medium leaving the mixer is
When placed in heat exchange relationship with the solvent leaving the evaporator, a refrigerant having a relatively high heat of vaporization may be circulated at a small rate compared to the solvent rut.

In another embodiment, the solvent leaving the evaporator may be passed to an economizer or auxiliary heat exchanger. Unlike many conventional systems, such as those described in U.S. Pat.
and increases the capacity of gas handled by the compressor.

One form of this embodiment is illustrated in FIG.

The operation of this example is similar to that of the example shown in FIG. However, Baude
ot) An economizer, which can be similar to a cooler, is used. Additionally, if the compressor is not to be assisted by an absorber-generator pair as described in more detail below, valves 41 and 42 will generally be closed.

The refrigerant-solvent solution flows down the membrane over the surfaces within the economizer-heat exchanger 26. These surfaces are cooled by cold solvent returned from the evaporator-boiler 10 through conduit U. The cooled crash refrigerant-solvent may also be immersed in an atmosphere of still cold refrigerant which is bled from the compressor outlet through conduit 27 by valve 79. Thus, the heat of condensation of the additional refrigerant absorbed by the cold refrigerant-solvent stream as well as the heat of mixing is transferred to the cold solvent circulating through the economizer.

At some degrees Celsius, cell 79 may be closed and exchanger 26 operated only as a heat exchanger without any mixing occurring.

In operation, compressor 12 pumps and compresses refrigerated 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. pumped through. mixer 11
The compressed gas going to is mixed with a solvent and the refrigerant-solvent stream is directed through conduit 15 to economizer 26 and expansion valve 16. Then, the refrigerant-solvent is
is directed to the evaporator 10 as in . Solvent from the evaporator is pumped through conduit 24 to economizer 26 by solvent pump 13, which circulates the system. Compressor 12 draws the evaporated refrigerant through conduit 18;
Or inhale to complete the cycle. In this way,
The efficiency of the process can be increased by using an economizer to subcool the refrigerant-solvent and increase the net refrigeration effect of the solution. Valve 79 may be operated to regulate or prevent flow through line 27 such that a particular portion or all of the compressed refrigerant passes to condenser-mixer 11.

The compressed gas leaving compressor 12 via conduit 14 is also placed in a heat exchange relationship with the refrigerant-solvent stream leaving mixer 11 such that the operating temperature of mixer 11 is higher than the operating temperature of the compressed gas in conduit 14. If so, the latter can be supercooled. Thus, as shown in FIG. 1, normally open valves 81 and 83 can be opened to allow compressed refrigerant to pass via line 82 to heat exchanger 85. At , heat is exchanged with a common medium-refrigerant stream passing through line [5]. The compressed refrigerant then passes to mixer 11 via line 84 as described above.

In a preferred embodiment of the invention, a chemically assisted mechanical refrigeration process involving several steps may be provided. Refrigerant and solvent, when combined, have a negative deviation from Raoult's law. A solution stream containing the solvent and liquefied refrigerant is passed to the generator. Pressure is then reduced across the solution to vaporize the refrigerant and separate the solvent, while simultaneously the generated refrigerant and solvent are placed in heat exchange relationship with the working medium to remove energy from the working medium, thereby Forming a solvent stream and a refrigerant stream that leave the evaporator. The refrigerant stream includes gaseous refrigerant. The solvent stream leaving the evaporator then passes to the evaporator in the economizer zone4. It is passed in heat exchange relationship with the liquid stream to allow heat transfer between the solvent stream and the solution. At the same time, the solvent stream and the refrigerant stream are placed in fluid communication with each other to achieve mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream, thus creating an economizer between the solvent stream and the bath liquid stream. - Facilitates heat transfer within the band. Thereafter, the solvent and refrigerant streams are
They are contacted in a co-compression zone where the pressure on both streams is increased to form a combined solvent-refrigerant stream. The combined solvent-refrigerant stream is then passed through a mixer under sufficient pressure to promote substantial dissolution of the refrigerant in the solvent to form a solution stream for passage to the evaporator.

Energy is removed from the mixer when the mixer is in heat exchange relationship with the working medium.

Referring now to FIG. 4, a more specific embodiment of the preferred embodiment of the invention will be described. The solvent-liquefied refrigerant stream is passed to evaporator 10 via line 25.

Solvent - The refrigerant and solvent of the liquefied refrigerant stream have a negative deviation from Raoult's law and can be chosen from the numerous combinations of substances already mentioned. As an example, a refrigerant-solvent combination of R22-trichloroethane may be used.

1 and 2, the pressure on the solvent-refrigerant stream is reduced in the evaporator to vaporize the refrigerant and separate it from the solvent; During one direction, the generated refrigerant and solvent are placed in heat exchange relationship with the working medium to remove energy from the working medium. the result,
A flow of solvent passing through line 24 and a refrigerant flow comprising gaseous refrigerant passing via line 18 are formed.

It is believed that the solvent stream passing through line 24 can contain a substantial portion of the refrigerant without interfering with the efficiency of the process.

More specifically, the solvent stream leaving the evaporator and passing via line 24 is placed in heat exchange relationship with the solvent-refrigerant stream passing to the evaporator via lines 15 and 25. Additionally, the solvent flow in line 24 is placed in oil body communication with the refrigerant flow in line 18 such that the gaseous refrigerant emanating from the solvent flow 24 can pass to the refrigerant flow 18 via conduit 92 . This gas evolution tends to cool the solvent stream, thus facilitating heat transfer in the economizer or economizer zone, allowing the solvent to cool as it passes through the economizer zone.
Increase the temperature drop of the refrigerant flow. In other words, the refrigerant is further generated from the solvent and the resulting energy change is transferred indirectly to the working medium passing through the evaporator by the temperature reduction of the solvent-refrigerant stream as it enters the evaporator. It is believed that evaporator inefficiency caused by failure to separate refrigerant from solvent is reduced as the refrigerant is reduced.

Both the solvent and refrigerant streams are then contacted in a co-compression zone as illustrated by compressor 88 in FIG. Compressing the refrigerant together with the liquid in a co-compression zone, such as compressor 88, is believed to provide several advantages. Thus, the liquid solvent will generally have a higher heat capacity than the refrigerant and will generally act as a refrigerant in the compressor, thus reducing the amount of work required to compress the refrigerant. Additionally, liquid solvents can be selected that act as sealants and lubricants as well as coolants. Thus, several advantages can occur when the refrigerant gas is compressed in a joint compression zone by a single compressor-pump, such as compressor 88, and the solvent is pumped at the same time.

For example, the solvent provides internal cooling of the entire device, thus allowing compression to be more polytropic and therefore generally more economical than reversible adiabatic. Additionally, the presence of solvent in the compressor is believed to enable high pressures in the case of centrifugal compressors, or act as a lubricant and sealant in the case of rotary compressors.

The resulting combined solvent-refrigerant stream flows via line 90 through a heat exchanger, such as precooler 86, to mixer 11. A heat exchanger or precooler 86 serves to further raise the temperature of the solvent-refrigerant introduction passing to the mixer, while occasionally cooling the refrigerant-solvent stream passing via line 15 toward economizer 26. Begin to. Heat exchanger,
For example, precooler 86 should be operated to bring the temperature of the combined solvent-refrigerant entering mixer 11 as close as possible to (without exceeding) the temperature of mixer 11 . Additionally, the precooler is such that the temperature of the solvent-refrigerant combination passing through line 90 is such that the refrigerant does not substantially begin to melt and give off heat before reaching mixer 11. should be operated in a manner.

1 and 2, in mixer 11 the combined solvent-refrigerant stream is transferred to line 15, promoting substantial dissolution of the refrigerant in the solvent for a given temperature. and 25 to form a flow of solution through to the evaporator 10. At the same time, the mixer is in heat exchange relationship with the working medium which removes the energy or heat dissipated by the melted and condensed refrigerant in the mixer 11.

The operation of the embodiment shown in FIG. 4 is further demonstrated by the various temperatures shown in the figure (all F). These temperatures were calculated based on the following assumptions. Cycle power ζ using R22 as refrigerant and 1.1.1-trichloroethane (Tel) as solvent, evaporator temperature 40 FC, s, 44'C) and mixer temperature 11
0 F (approximately 43'°C). Based on calculations obtained from the heat balance, if no precooler is present, the theoretical operating coefficient of the system is 6.71
It is believed that this value compares favorably with 5.75 for pure R22 vapor compression cycles commonly used in prior art systems. However, if a heat exchanger, such as precooler 86, is present, the refrigerant-solvent combination can be used to cool the refrigerant-solvent stream exiting the mixer. This combination passing through line 90 is at mixer pressure as it enters the mixer, but below mixer temperature when it begins passage through heat exchanger 86, so that the dissolution of the refrigerant into the solvent is pre-cooled. It is assumed that the process starts at the device 86.

When using R22 as the refrigerant and trichloroethane as the solvent at the temperatures indicated, a theoretical maximum of only half the heat exchange that would theoretically be obtained in the case of an inert liquid is obtained, and the theoretical maximum obtained The operating coefficient is 7
．． 13 [the theoretical maximum operating coefficient for a complete (Carnot) cycle is 7.14].

The results of these calculations compared to a pure R22 evaporative compression cycle are shown in Table 1. Various data necessary for calculations, such as vapor density and discharge temperature of reversible adiabatic compression for measuring polytropic discharge temperature, are provided by the American Society of Heating, Refrigerating, and Air Conditioning. Taken from Thermophysical Properties of Refrigerants J, 1976 and American Society of Heating, Refrigerating, and Air Conditioning Engineers, Thermodynamic Properties of Refrigerants, 1980. . When extrapolated, they are generally conservative estimates with respect to cycle operation.
estimates).

R22-T for evaporator temperature 40F (about 4.44°'C) and mixer temperature 110F (about 43"C)
Based on OE cycle and recycle 1 bond (approx. 453 g), 110 F (approx. 43 C) and 94.7
p81a, TOEO, 684 pounds (approx. 310
g, ) is in equilibrium with R220,316 bond (approximately 142 g') in liquid solution.

R220,262 bond (approx. 118.8 g) at 40F and 24.7 psia
) is evaporated and R220,054 bond (approximately 24.49
g) remains in solution. The enthalpy measurement is based on the generation R2
2 is the total refrigeration effect in the evaporator of 22.65 Bt.
Indicates that it absorbs u.

Table 1 Table 1 Comparison mass of theoretical cycles for 1 ton capacity between +40F and 110F 1.18 Bond 13.49 lbs - R224
, 26 lbs + TOE 9.23 Bont Gas 2.0 cubic feet R2210, 4 cubic feet (+ Tel O, 82 gal) Compression Ratio 2.88 3.83 High Pressure Side 241 psia g5 psia Low Side 8
4 psia 25 psia pressure difference 157 payu 7o psi applied horsepower 0.82 0.66 COP 5.75 7.13 Gas density 0.41 lb/ft3 Solvent density 8
4.0 bond/cubic foot gas/liquid volume ratio 95/
1 Gas/Liquid Mass Ratio 0.47/1 Complete Heat Exchange and Equal Outlet Temperature 69.6 F (
Approximately 20. 'F'c), 40FC approximately 4.4
As the solvent entering in 4'c) flows countercurrently to the incoming refrigerant-containing solution stream in lines 15 and 25, the remaining R22
0.054 bond (approximately 24.49 g) should be evaporated in the economizer. The outlet temperature in both cases is about 70F (about 21.1C). If precooler 86 is not used, temperatures closer to 71F (approximately 21.7"C) will be obtained, while in each case approximately 69.64F (approximately 20.91'"C) when precooler 86 is used.
The outlet temperature of is reached.

TOK O,684 bond (approximately 310 g), which has a specific heat of 0.258, has a specific heat of 70.93 without the precooler 86.
F (approximately 21.63"C), or 69.64F (approximately 20.91C) if precooler 86 is between compressor 88 and mixer 11;
and 40F (approximately 4.44℃) from the economizer zone.
The introduction temperature of R220.36 bond (approximately 163 g) containing gas warmer than the 42.5 p (approximately 5-
83'C).

Reversible adiabatic compression of gas alone is 148F (approximately 64.4'C
) σ1rI-1-...1KomaF6" fy辷Σ Mugoku Gokyoru) 2SyVzef The temperature taken out of the small sieve is 100.51 F (
approximately 38.06"C) or 99.25F (approximately 37.36"C) if precooler 86 is used.
It is.

The value of n, that is, the polytropic compression constant, is calculated by the following formula (where T
l = 502.62°R, T2-560.51°R1P
2=24.7×144 psf, P2-94-7
X 144 pBf.

n,,,t,oc+) Entangled.

p2v2- p, vl Compression work (Btu) y (1 k.) - is the evaporated R22
2.05 B per 0.316 bond (approximately 142 g)
It is tu. vl and V2 are taken from the Superheat Tables of the American Society of Heating, Refrigerating, and Air Conditioning Engineers, Thermodynamic Properties of Refrigerants J, 1980. Economizer-26 The density of the stripping TOR leaving the
．． The Btu of 42 feet (about 3670 am) and pumping TOKO,684 bond (about 310 g) is 0.106. Therefore, the total work of compressing the gas and pumping the liquid is 2.16 Btu per bond (0,4536 kg) of mixture.

A refrigerant-solvent solution with a specific heat of 0.264 is heated between 30.93 F (-0,594°'C) and 40 F in the evaporator.
Since the net effective refrigeration effect per pound (0,4536 g) of gas-liquid recycle is 14.48 Btu in the absence of precooler 86, It is.

Thus, the operating factor for the cycle is 6.71. The theoretical operating coefficient for a pure R22 cycle under these conditions is 5.75, so assuming no additional heat exchangers, e.g. precooler 86, are used, the example shown in FIG. , than a comparable vapor compression refrigeration cycle.
It is believed that this method shows a 6.7% efficient method.

The foregoing shows that, with the exception of the initial reference, the liquid-compressed gas mixture exiting the compressor is still colder than the mixer at no'F (approximately 43 C) and has the ability to subcool the refrigerant-solvent solution exiting the mixer. It ignores the fact that it exists. If there was no absorption of gas by the liquid and therefore no heat generation, the precooler 86 would subcool the effluent from the condenser to 105.62F (approximately 40.9"C). The temperature drop is (110°-105,62°
), the refrigerant-solvent solution is 1
107.81 F instead of 10 F
(approximately 42.12'C) into economizer 26.

If the above calculations are repeated for the economizer and compressor, it is believed that all of the R22 in the solvent stream in line 24 will still come out. The work of compression-pump feeding is per bond (0,4536 kg) of circulating material,
It becomes 2.08 Btu. The effluent from the condenser has been slightly cooled, so the recycle 1 bond (0,4536 k
The effective net refrigeration effect per g) is 14.83 B
tu theal.

The coefficient of performance is now 7.13 compared to 5.75 for pure R22 and 6.71 without precooler 86. 40F (approximately 4.44”C) and 110F
The theoretical perfect Carnot efficiency between temperatures (about 43° C.) is 7.14, so a precooler is likely to give higher efficiency. The reason is that 7.13 is about 2 times larger than 5.75.
This is because it is 5% better.

Numerous σ) modifications and substitutions to the embodiments shown in the drawings include:
It is possible. As an example, the specific example in FIG.
It is believed that a portion of the refrigerant from 9 can be sprayed into the refrigeration stream in line 24 and thus operated to develop a high pressure in the centrifugal compressor. The reason is that the pressure developed by a centrifugal pump is proportional to the product of the density of the medium being treated and the square of the tip velocity. In this way, considerably higher pressures can be developed for a given centrifugal pump,
Smaller pumps can therefore be used.

In another variation to the embodiment shown in FIG. 1, the pump compressor 12 can be replaced by a jet compressor. In this way, the high velocity liquid jet of solvent supplied to the jet compressor by a portion of the solvent from line 19 can be used to compress the refrigerant gas coming from the evaporator-boiler 10.

It is believed that the presence of a higher specific heat solvent results in more efficient compression due to the higher heat capacity of the liquid. More particularly, the compression will be more or less isothermal and therefore more efficient.

In another embodiment, both the compressor I2 and the solvent pump 13 are replaced by compressing the refrigerant gas, circulating the solvent, and passing the gas through a single conduit before introducing it into the mixer 11. A liquid ring compressor may be used to initiate the mixing of the solvent and the solvent. It is understood that the compression is largely isothermal and therefore more efficient.

For example, as shown in FIG. 1, valve 76 can be closed and valve 71 and liquid ring compressor 77 can be closed, allowing both solvent and refrigerant to pass from evaporator 10 via line 72 to ring compressor 77. can be manipulated to do so. The compressed mixture will then pass to mixer 11.

By way of example, ring compressor 77 is a double lobe compressor manufactured by Natsch Engineering Company of Sus Norwalk, Conn., and described in 1971 by said company, No. 47:4-0. be able to.

In yet another embodiment, the refrigerant can be foamed with a solvent;
The solvent pump 13 could then be eliminated from the example shown in FIG. Both refrigerant and solvent will be circulated from the evaporator 10 to the compressor 12 and thus to the mixer 11. Similarly, the specific example shown in FIG.
It can be fixed. For example, instead of solvent pump 130, an arrangement could be made to inject 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. , may be used.

Further, as shown in FIG. 1, the valves 71 and 74 are
At least a portion of the solvent can be operated to bypass solvent pump 13 , while valve 74 is operated to pass a sufficient amount of vapor from line 14 through line 73 to line 72 .

The invention may also be used with other systems. For example, a generator-absorber pair may be assembled and installed in conjunction with a compressor to provide a backup for the compressor.
) can be given. The generator could serve as a secondary heat source, for example from exhaust air or in the form of solar energy. For example, as shown in FIG.
2 can be installed on either side of the compressor 12 in lines 18 and 14 to assemble and install generator-absorber pairs 48, 44 into the system. A portion of the evaporated refrigerant can then be passed from line 18 via line 43 to the absorber where it is absorbed into a suitable secondary solvent and then passed by pump 46 through lines 45 and 47 to generator 4.
8 was pumped with solution. Upon evaporation of the refrigerant in the generator 48, the now compressed vapor is transferred to the line 49, valve 42.
and to the mixer via line 14, while the secondary solvent was returned to absorber 44 via line 50.

The secondary solvent can be the same as used in the main system.

Of course, to obtain all the benefits of the present invention, the generator-absorber pair should not be a complete replacement for compressor 12. Rather, the generator-absorber pair and mechanical compressor
A complementary means of generating pressurized refrigerant gas.

Additionally, in the embodiment of FIG. 4, there are numerous alternative embodiments for simultaneous compression-pumping of gaseous and liquid components, as will be known to those skilled in the art having the benefit of this disclosure. But it exists. For example, large multistage centrifugal compressors, such as those manufactured by Yoke, often Tift liquid refrigerant into the vapor stream as an alternative for flash intercooling between stages.
designed to radiate. However, such a block I
In this case, the liquid flow rate should be as reasonably uniform as possible. Also, Dunham Bunonyu (Dunh)
a) Spiral or rotary screw compressors, such as those manufactured by 1-Bush, may be suitable for use in the case of chemically assisted mechanical refrigeration systems such as those disclosed herein. However, in chemically assisted mechanical refrigeration systems, the solvent should preferably serve as a coolant, moisturizer and sealant. Furthermore, since the solvent is passed over the mixer together with the compressed gas, large oil separators and oil coolers should be eliminated.

For smaller capacities, Wanke-type compressors made by Okura Clutch of Japan or Rotorex (Fedde
rs)] and Mitsubishi rolling piston compressors have proven useful. A multi-stage centrifugal compressor-pump manufactured by 5ihi may also be useful.

In this device, the gas-liquid mixture enters the first hermetic impeller axially and the denser liquid enters the periphery. The lighter gas is admitted to the second stage closer to the center of the chamber, and then both gas and liquid are carried together through the second impeller stage.

Or, if an economizer is used and capital costs permit, a turbine between the economizer and the evaporator? F5 media - can be placed in the solvent stream to function as a pressure reducer and supplement a throttling device. Under suitable operating conditions, it is believed that the subcooled flow exiting the economizer is unlikely to flash any refrigerant gas at this point, and the resulting shaft work is sufficient to support system pumps, compressors, auxiliary fans, etc. Can be used to increase power.

Additional equipment items may be used within the framework of the invention. For example, while the use of substantial control devices may be sufficient for multiple operations, control of the system as well as system flexibility may be increased by the use of appropriate process controls. In the illustrated embodiment, the low pressure drop mixing of gaseous refrigerant and liquid is carried out by an in-line stationary mixer, reportedly at the Kneebon, New York, Mixing Company.
This was accomplished by using what is provided by Equipment Company.

Still other modifications and alternative embodiments of the devices and methods of the invention will be apparent to those skilled in the art in view of this description.

Accordingly, this description is to be construed as illustrative only and is for the purpose of teaching those skilled in the art how to practice the invention 4). It is to be understood that the form of the invention shown and described is to be construed as a preferred embodiment of the invention. Various changes may be made in the size, shape and arrangement of parts. For example, equivalent elements or materials may be used in place of those shown and described herein, parts may be substituted, and features constituting the invention may be independently utilized in the use of other features. obtain. All of these will be apparent to those skilled in the art after having the benefit of this description of the invention.

[Brief explanation of the drawing]

Figure 1 is a schematic diagram of a chemically assisted mechanical refrigeration cycle;
2 is a schematic diagram of another embodiment of a chemically assisted mechanical refrigeration cycle; FIG. 3 is a schematic diagram of an evaporator for use in the embodiments shown in FIGS. 1, 2 and 4; FIG. 4 is a schematic illustration of yet another embodiment of the invention. 10... Evaporator, 11... Mixer, 12... Compressor, 26... Economizer-144... Absorber,
48... Generator, 86... Precooler, 88... Compressor. Applicant's agent Kiyoshi Inomata

Claims (1)

[Claims] 1. Mechanically compressing a refrigerant stream consisting of evaporated refrigerant, and placing the refrigerant in a mixer under sufficient pressure to promote substantial dissolution of the refrigerant in a solvent in the mixer. A refrigerant-solvent solution is prepared by contacting the solvent with a solvent, while simultaneously placing the solution in a heat exchange relationship with a working medium to transfer heat to the working medium, such that the refrigerant-solvent solution exhibits a negative deviation from Raoult's law. ), pressure is reduced across the refrigerant-solvent solution in an evaporator to evaporate and substantially separate the refrigerant from the solvent, while simultaneously placing the generated refrigerant-solvent solution in heat exchange relationship with the working medium to transfer energy to the working medium. 1. A chemically assisted mechanical refrigeration process, characterized in that it removes from the evaporator, thereby forming a refrigerant stream and a solvent stream, and passing the solvent stream and the refrigerant stream from an evaporator. 2. The method of claim 1 further comprising the steps of: 2. placing the solvent stream leaving the evaporator in heat exchange relationship in an economizer zone with the refrigerant-solvent solution leaving the mixer. 3. The solvent stream leaving the evaporator contains a portion of the dissolved refrigerant, and the solvent stream is placed in fluid communication with the refrigerant stream leaving the evaporator in the economizer zone, thereby reducing the flow from the solvent stream to the refrigerant stream. 2. A method according to claim 2, which allows mass transfer of the gaseous refrigerant and is thus characterized by heat transfer in the economizer zone before the final passage of the solvent and refrigerant streams to the mixer. . 4. Before passing the solvent stream and the coolant stream to the mixer, -
4. A method according to claim 3, wherein the material is mechanically compressed together. 5. Passing a portion of the compressed refrigerant into the evaporator directly into the refrigerant-solvent solution; the solvent leaving the evaporator;
2. The method of claim 1, further comprising the step of placing in heat exchange relationship in an economizer zone with the refrigerant-solvent solution leaving the mixer. 6. The method of claim 1, wherein the evaporated refrigerant is compressed by passing a high velocity liquid jet of solvent through the refrigerant. 7. A method as claimed in claim 1, in which a portion of the refrigerant 1' is passed through a generator-absorber pair before introduction to the mixer. 8. Passing a solution stream consisting of a solvent and a liquefied refrigerant into an evaporator (the refrigerant and solvent having a negative deviation from Raoult's law when combined) and reducing the pressure across the solution to remove the refrigerant. A refrigerant stream consisting of a solvent stream and a gaseous refrigerant that is vaporized and separated from the solvent while simultaneously placing the starting refrigerant and solvent in heat exchange relationship with the working medium to remove energy from the working medium, thereby leaving the evaporator. The solvent stream leaving the evaporator is passed in an economizer zone in a heat exchange relationship with the solution stream passing through the evaporator to effect heat transfer between the solvent stream and the solution. heat is facilitated by mass transfer of the gaseous refrigerant with respect to one or more streams passing through the economizer zone) and the refrigerant and solvent streams in a mixing zone comprising a mixer.
contacting the refrigerant σ into the solvent under sufficient pressure to promote fractional dissolution of the refrigerant to form a solution stream for passage to the evaporator;
A chemically assisted mechanical refrigeration process characterized in that, at the same time, energy is removed from the mixer by placing the mixer in heat exchange relationship with the working medium. 9. The method of claim 8, wherein the refrigerant stream is mechanically compressed separately from the solvent stream before passing the refrigerant through the mixer. 10, the solvent stream leaving the evaporator contains a substantial portion of dissolved refrigerant, and the melt stream is placed in fluid communication with the refrigerant stream leaving the evaporator to transfer gaseous refrigerant from the solvent stream to the refrigerant stream. 9. A method as claimed in claim 8, characterized in that mass transfer is achieved and thus heat transfer in the economizer zone before passage of the solvent and refrigerant streams to the mixing zone. The mixing zone further comprises a co-compression zone in which the refrigerant stream and the solvent stream are brought into contact with each other and the pressure on the refrigerant and solvent causes dissolution of the refrigerant into the solvent in the mixer. boosted enough to facilitate
A method according to claim 10. ]2. The refrigerant stream and the solvent stream are contacted in a compression zone to form a combined solvent-refrigerant stream, and the combined solvent-refrigerant stream passes through the solution stream and the mixer before passing the solution stream to the economizer zone. 12. A method as claimed in claim 11, characterized by the further step of placing the two in heat exchange relationship with each other. 13. The temperature of the combined solvent-refrigerant stream approaches the temperature of the mixer immediately before the introduction of the mixer (the method according to claim 12). 14. Mass transfer of the gaseous refrigerant leaves the evaporator. 15. The method of claim 8, which is achieved by passing a portion of the refrigerant stream through the solution stream under pressure in an economizer zone, whereby the concentration of refrigerant in the solution stream is increased. , passing a solution stream consisting of a solvent and a liquefied refrigerant through an evaporator (the refrigerant and solvent having a negative deviation from Raoult's law when interdigitated) and reducing the pressure across the solution to evaporate the refrigerant. and separate it from the solvent, while simultaneously placing the generated refrigerant and solvent in heat exchange relationship with the working medium to remove energy from the working medium, thereby forming a refrigerant stream consisting of a solvent stream and a gaseous refrigerant, with both streams leaves the evaporator and the solvent stream leaving the evaporator is passed in heat exchange relationship with the solution stream passing through the evaporator in an economizer zone to effect heat transfer between the solvent stream and the solution, while at the same time A solvent stream and a refrigerant stream are placed in fluid communication to achieve mass transfer of gaseous refrigerant from the solvent stream to the refrigerant stream, thus facilitating heat transfer between the solvent stream and the solution stream in the economizer zone. contacting the solvent and refrigerant streams in a co-compression zone while increasing the pressure across both streams to form a combined solvent-refrigerant stream, applying a pressure sufficient to promote substantial dissolution of the refrigerant in the solvent; Passing the combined solvent-refrigerant stream through the mixer while maintaining the flow rate to form a solution stream for passage to the evaporator, while at the same time placing the mixer in heat exchange relationship with the working medium to remove energy from the mixer. 16. A chemically assisted mechanical refrigeration process characterized by:
16. The method of claim 15, further comprising the step of placing the solution stream in heat exchange relationship with each other prior to passing the solution stream through the zones. 17. A mechanical compressor for compressing a refrigerant, the mechanical compressor being arranged to receive the solvent and the compressed refrigerant at a pressure sufficient to promote substantial dissolution of the refrigerant in the solvent and to form a solvent-refrigerant flow. a mixer that receives a refrigerant-solvent stream from the mixer and separates at least a substantial portion of the refrigerant from the solvent and absorbs heat of vaporization and heat of solution from the working medium in heat exchange relationship with the generated refrigerant-solvent stream; characterized by comprising an evaporation zone for returning the refrigerant to the compressor, and a heat exchanger for placing the solvent passing from the evaporation zone to the mixing zone in a heat exchange relationship with the refrigerant-solvent stream passing from the mixer to the evaporation zone. , chemically assisted mechanical refrigeration equipment. 18. The apparatus of claim 17, wherein the heat exchanger consists of a conduit for the passage of a solvent and a surface adjacent to the conduit that receives a thin film of solvent-refrigerant solution. 19. The apparatus of claim 17 further comprising a coil substantially immersed in liquid within the evaporator for circulating the working medium. 20. The apparatus according to claim 17, wherein the evaporation zone comprises a multi-tube heat exchanger. 21. A mechanical compressor uses the solvent from the evaporation zone to
18. The device according to claim 17, comprising a jet compressor suitable for compressing the refrigerant leaving the evaporation zone. 22. At a pressure sufficient to separate the refrigerant from the solvent and to absorb a substantial portion of the heat of vaporization and dissolution of the solvent-refrigerant solution from the working medium in heat exchange relationship with the generated refrigerant-solvent solution, the refrigerant- an evaporation zone receiving a solvent solution; a compressor adapted to receive a gaseous stream and a liquid stream and to increase the pressure of said streams upon their joining; a compressor connected at one end to an evaporator and compressing at the other end; connected to the machine,
a solvent conduit for passing the solvent from the evaporator to the compressor, connected at one end to the evaporator and at the other end to the compressor;
a refrigerant conduit for passing gaseous refrigerant from the evaporator to the compressor, the refrigerant conduit being in fluid communication with a solvent conduit for receiving gases generated from the solvent passing through the solvent conduit;
, the refrigerant's air lip mark on Zhong Shan? A mixer arranged to receive the solvent and the refrigerant at a pressure sufficient to prepare the liquid, a confluent mixer connected to the compressor at one end and to the mixer at the other end. a solvent-refrigerant conduit, said conduit being arranged to allow passage of the combined refrigerant-solvent stream under pressure; a solution conduit having one end connected to a mixer and the other end connected to an evaporator; a conduit, said solution conduit being suitable for facilitating pressure reduction between the mixer and the evaporator, and an economizer for placing the solvent conduit and the solution conduit in heat exchange relationship with each other. A chemically assisted mechanical refrigeration device characterized by: 23. The apparatus of claim 22, further comprising a second heat exchanger for placing the solution conduit and the combined solvent-refrigerant conduit in heat exchange relationship with each other. 24. The apparatus according to claim 22, wherein the compressor is a centrifugal or rotary compressor.