JP3322263B1 - Ejector cycle, gas-liquid separator used therefor, and water heater and heat management system using this ejector cycle - Google Patents

Abstract

Abstract: PROBLEM TO BE SOLVED: To improve the coefficient of performance of a refrigeration cycle while taking measures against CFC removal. SOLUTION: In an ejector cycle, carbon dioxide is used as a refrigerant, and the ejector 400 expands under reduced pressure from a supercritical region. As a result, carbon dioxide has a large ratio (= Δh / ΔP) of the change amount of the specific enthalpy to the change amount of the pressure ΔP (= Δh / ΔP) and the pressure difference at the time of decompression and expansion becomes larger than that of CFCs. Enthalpy difference (adiabatic heat drop) between the refrigerant inlet of the nozzle and the refrigerant outlet of the nozzle 410 can be increased. In the supercritical region, the gas-phase refrigerant also has a density substantially equal to that of the liquid-phase state. It is accelerated to almost the same speed. For this reason, the energy conversion efficiency in the ejector 400 (nozzle 410) is increased, and the coefficient of performance is improved.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION The present invention relates to a method for reducing the pressure of a refrigerant, expanding the refrigerant, and sucking a vapor-phase refrigerant evaporated in an evaporator.
The present invention relates to an ejector cycle having an ejector that converts expansion energy (kinetic energy discarded by a decompressor such as an expansion valve in a normal vapor compression refrigeration cycle) into pressure energy to increase the suction pressure of a compressor.

[0002]

2. Description of the Related Art In recent years, as one of measures against defluorocarbon of a refrigerant used in a vapor compression type refrigeration cycle, for example,
A vapor compression refrigeration cycle (hereinafter, abbreviated as refrigeration cycle) using carbon dioxide has been proposed as described in Japanese Patent No. -18602.

[0003]

However, in a refrigeration cycle using carbon dioxide as a refrigerant, it is necessary to raise the high-pressure side pressure to a level higher than the critical pressure of the refrigerant. There is a problem that the coefficient of performance (efficiency) of the refrigeration cycle is lower than that of the refrigeration cycle using a refrigerant.

SUMMARY OF THE INVENTION In view of the foregoing, it is an object of the present invention to improve the coefficient of performance of a refrigeration cycle while taking measures against chlorofluorocarbons.

[0005]

According to the present invention, in order to achieve the above object, according to the first aspect of the present invention, there is provided a compressor (100) for suction-compressing a refrigerant and increasing its pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). and ejector (400) for raising the suction pressure, when the gas-liquid two-phase cooling <br/> medium from the ejector (400) is separated into a gas phase refrigerant and liquid phase refrigerant storing refrigerant bets
In particular, the gas-phase refrigerant is supplied to the suction side of the compressor (100),
A gas-liquid separator (5 ) that supplies the liquid-phase refrigerant to the evaporator (300)
00), wherein the pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to or above the critical pressure of the refrigerant, and the pressure of the refrigerant after the pressure is reduced is reduced to or below the critical pressure of the refrigerant.

[0006] Thus, the refrigerant used in the supercritical region generally has a larger ratio (= Δh / ΔP) of the change amount (Δh) of the specific enthalpy to the change amount (ΔP) of the pressure than Freon. In addition, since the pressure difference at the time of decompression expansion becomes large, more expansion energy generated at the time of decompression can be recovered.

Further, since the pressure from the intermediate pressure (lower than the discharge pressure of the compressor and higher than the internal pressure of the evaporator) flowing out of the ejector (400) is increased to the supercritical pressure, the internal pressure of the evaporator is increased by the compressor. The power consumption of the compressor can be reduced as compared with the cycle in which the pressure is increased to the supercritical pressure.

In the supercritical region, the gas-phase refrigerant also has a density substantially equal to that of the liquid-phase state, so that the refrigerant decompressed and expanded by the ejector (400) is both a liquid-phase refrigerant and a gas-phase refrigerant. It is accelerated to almost the same speed. For this reason, the energy conversion efficiency in the ejector (400) is increased, and the coefficient of performance is improved as compared with an ejector cycle using chlorofluorocarbon as a refrigerant.

By the way, the efficiency of an ejector using Freon as a refrigerant is about 20% to about 30%, while the efficiency of an ejector using carbon dioxide as a refrigerant is about 50%, and the efficiency is about twice that of Freon. . As a result, the effect of improving the coefficient of performance of the ejector cycle was 3
In the case where carbon dioxide is used as the refrigerant, the refrigerant becomes about 40% to about 60% as compared with 0% to 40%. As described above, according to the present invention, the refrigerant used in the supercritical region is used. By using this, it is possible to improve the coefficient of performance (efficiency) of the ejector cycle while eliminating the use of chlorofluorocarbon.

According to the second aspect of the present invention, a compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure,
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted into pressure energy to convert the refrigerant into the compressor ( 100) an ejector (400) for increasing the suction pressure, and the ejector (400)
Gas-liquid two-phase refrigerant from the compressor is separated into a gas-phase refrigerant and a liquid-phase refrigerant, and the refrigerant is stored.
0) and supplies the liquid-phase refrigerant to the evaporator (30).
A) a gas-liquid separator (500 ) for supplying to the compressor (100), and an oil return hole installed in the gas-liquid separator for guiding oil in the gas-liquid separator to the compressor (100). The pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more, and the pressure of the refrigerant after the pressure is reduced to the critical pressure of the refrigerant or less. According to the third aspect of the present invention, the ejector (40)
A pressure adjusting means (710, 720) for adjusting the pressure of the refrigerant pressurized in 0) below the critical pressure is provided.

Thus, the pressure in the gas-liquid separator (500) can be prevented from becoming higher than the critical pressure, so that the refrigerant can be reliably separated into the gaseous refrigerant and the liquid refrigerant.

According to a fourth aspect of the present invention, pressure adjusting means (710, 720) for adjusting the pressure of the refrigerant pressurized by the ejector (400) to a gas-liquid two-phase region is provided. I do.

Thus, the refrigerant can be surely separated into a gaseous refrigerant and a liquid refrigerant.

According to the fifth aspect of the invention, the gas-liquid separator (500) separates the refrigerant flowing out of the ejector (400) into gas and liquid, and furthermore, the pressure adjusting means (710,
720) is provided on the upstream side of the refrigerant flow from the ejector (400).

Thus, the pressure in the gas-liquid separator (500) can be prevented from becoming higher than the critical pressure, so that the refrigerant can be reliably separated into a gaseous refrigerant and a liquid-phase refrigerant while the flow resistance of the refrigerant ( Pressure loss) can be prevented from increasing.

The gas-liquid separator (500) is provided in claim 5
As described above, the refrigerant flowing out of the ejector (400) is separated into gas and liquid by the pressure adjusting means (710,
720) may be provided on the downstream side of the refrigerant flow from the ejector (400).

[0017] In the invention according to claim 7, a compressor (100) that sucks and compresses a refrigerant to increase the pressure to a supercritical pressure,
A radiator (200) for cooling the refrigerant discharged from the compressor (100), and an evaporator (30) for evaporating the refrigerant and absorbing heat.
0), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure and a cross section of the refrigerant passage of the ejector (400)
It is installed in the approximate center, and flows from the ejector (400).
Extract the liquid-phase refrigerant from the refrigerant before discharging, and separate and extract it.
Supply the liquid refrigerant to the evaporator (300) side,
Gas phase cooling from the refrigerant before flowing out of the ejector (400)
The medium is extracted, and the separated and extracted gas-phase refrigerant is supplied to a compressor (10
0) the gas-liquid separator is supplied to the suction side of the (500) and a refrigerant pressure of the refrigerant after pressure reduction with increasing the refrigerant pressure before being decompressed by the ejector (400) to or above the critical pressure of the refrigerant and wherein the benzalkonium reduced to critical pressure following.

According to the present invention, the coefficient of performance (efficiency) of the ejector cycle is improved while eliminating the use of chlorofluorocarbon by using a refrigerant used in the supercritical region, as in the first aspect of the present invention. Can be.

In the ejector cycle, when the ejector efficiency increases, the compression work of the compressor (100) decreases, but as described later, the evaporator (300)
The specific enthalpy of the refrigerant when flowing into the evaporator increases, and the refrigerating capacity generated in the evaporator (300) decreases.

On the other hand, in the present invention, the liquid-phase refrigerant is separated and extracted from the refrigerant before flowing out of the ejector (400), and the separated and extracted liquid-phase refrigerant is supplied to the evaporator (300) side. While the compression work of the compressor (100) is small (maintaining high ejector efficiency), the evaporator (30)
The refrigeration capacity can be increased by preventing the specific enthalpy of the refrigerant when flowing into 0) from increasing.

According to the invention described in claim 8 , a compressor (100) for suctioning and compressing a refrigerant to increase the pressure to a supercritical pressure ,
A radiator (200) for cooling the refrigerant discharged from the compressor (100), and an evaporator (30) for evaporating the refrigerant and absorbing heat.
0), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure and first and second gas-liquid separators (500, 510) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant are provided, and the pressure is reduced by the ejector (400). Refrigerant after raising the pressure of the previous refrigerant above the critical pressure of the refrigerant and depressurizing it
The pressure was reduced to below the critical pressure of the refrigerant, the first gas-liquid separator (500), a liquid-phase refrigerant separated and extracted from refrigerant before flowing out from the ejector (400), evaporation of the separated and extracted liquid phase refrigerant The second gas-liquid separator (510) separates the refrigerant flowing out of the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant, and separates the separated liquid-phase refrigerant. It is characterized in that it is supplied to the evaporator (300) side.

[0022] Thus, as in the invention described in claim 8, while phasing out of CFCs by using a refrigerant used in a supercritical region, while improving the coefficient of performance of the ejector cycle (efficiency) , The refrigeration capacity can be increased.

According to the ninth aspect of the present invention, the first gas-liquid separator (500) is configured to separate and extract the liquid-phase refrigerant at the refrigerant outlet side of the booster (420, 430) of the ejector (400). ) Is desirable.

[0024] Further, according to the tenth aspect of the present invention,
If the first gas-liquid separator (500) is configured to separate and extract the liquid-phase refrigerant substantially at the center of the cross section of the refrigerant passage of the ejector (400), the liquid-phase refrigerant can be efficiently separated and extracted.

According to the eleventh aspect of the present invention, the compressor (100) that sucks and compresses the refrigerant and raises the pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure; separating the gas-liquid two- phase refrigerant from the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant; storing the refrigerant; and compressing the gas-phase refrigerant. To the suction side of the machine (100),
A gas-liquid separator (5) that supplies the liquid-phase refrigerant to the evaporator (300)
00) and heating means (800, 810, 820, 830) for heating the refrigerant drawn into the compressor (100) , and the refrigerant pressure before being reduced by the ejector (400) is equal to or higher than the critical pressure of the refrigerant. It is characterized by being raised up to

Thus, the temperature of the refrigerant sucked into the compressor (100) can be increased, so that the temperature of the refrigerant discharged from the compressor (100) increases, and the temperature in the radiator (200) is increased. The ability and the coefficient of performance of the cycle can be improved.

The heating means (800) is provided in claim 12
As described in the invention described in the above, the refrigerant may be configured to exchange heat between the refrigerant flowing out of the radiator (200) and the refrigerant drawn into the compressor (100).

Further, the heating means (810) is provided in claim 13
As described in the invention described in the above, the drive source (Mo) for driving the compressor (100) and the refrigerant drawn into the compressor (100) may be configured to exchange heat.

[0029] According to the fourteenth aspect of the present invention, the compressor (100) that sucks and compresses the refrigerant and raises the pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure; separating the gas-liquid two- phase refrigerant from the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant; storing the refrigerant; and compressing the gas-phase refrigerant. To the suction side of the machine (100),
An oil return hole installed in the gas-liquid separator for supplying the liquid-phase refrigerant to the evaporator (300), for guiding oil in the gas-liquid separator to the compressor (100), and a gas-liquid separator (500) From
Adjust the flow rate of the liquid refrigerant supplied to the evaporator (300)
Ejector efficiency control means for controlling the conversion efficiency of the energy in the ejector (400) by Rukoto (730)
Wherein the pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more.

Thus, the ejector cycle can be operated while maintaining high energy conversion efficiency (ejector efficiency) in the ejector (400).

According to the present invention, the compressor (100) inhales and compresses the refrigerant to increase the pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure; separating the gas-liquid two- phase refrigerant from the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant; storing the refrigerant; and compressing the gas-phase refrigerant. To the suction side of the machine (100),
A gas-liquid separator (5) that supplies the liquid-phase refrigerant to the evaporator (300)
00), an oil return hole installed in the gas-liquid separator for guiding oil in the gas-liquid separator to the compressor (100);
Adjust the flow rate of the refrigerant discharged from the compressor (100).
And by the flow rate adjusting means for adjusting the flow rate of refrigerant flowing into the ejector (400) (Mo), the gas-liquid separator (500)
Regulates the flow rate of the liquid-phase refrigerant supplied to the evaporator (300).
Ejector efficiency control means (73 for controlling the conversion efficiency of the energy in the ejector (400) by section
0), and the pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more.

Thus, the ejector cycle can be operated while maintaining high energy conversion efficiency (ejector efficiency) in the ejector (400).

According to the present invention, the refrigerant is sucked.
Compressor (100) that compresses and raises pressure to supercritical pressure
And heat radiation for cooling the refrigerant discharged from the compressor (100)
(200) and evaporator for evaporating the refrigerant and absorbing heat
(300) and the refrigerant flowing out of the radiator (200) is reduced.
The gas-phase refrigerant that has been pressure-expanded and evaporated in the evaporator (300)
Along with suction, the expansion energy is converted to pressure energy
Eje to convert and increase the suction pressure of compressor (100)
Gas and liquid from the ejector (400)
Separates phase refrigerant into gas phase refrigerant and liquid phase refrigerant and stores refrigerant
At the same time, gas-phase refrigerant is supplied to the suction side of the compressor (100).
Gas-liquid separator for supplying liquid refrigerant to the evaporator (300)
(500) and the flow of the refrigerant discharged from the compressor (100)
Flow into the ejector (400) by adjusting the amount
Flow rate adjusting means (Mo) for adjusting the flow rate of the refrigerant;
The pressure of the refrigerant before the pressure is reduced by the
It is characterized in that the pressure is raised up to the field pressure or more.

[0034] Further, according to the invention of claim 17 ,
The energy conversion efficiency may be controlled by adjusting the pressure increase amount of the refrigerant in the ejector (400).

According to the present invention, the refrigerant is sucked.
Compressor (100) that compresses and raises pressure to supercritical pressure
And heat radiation for cooling the refrigerant discharged from the compressor (100)
Device (200), an evaporator that evaporates the refrigerant and absorbs heat
(300) and the refrigerant flowing out of the radiator (200) is reduced.
The gas-phase refrigerant that has been pressure-expanded and evaporated in the evaporator (300)
Along with suction, the expansion energy is converted to pressure energy
Eje to convert and increase the suction pressure of compressor (100)
Gas and liquid from the ejector (400)
Separates phase refrigerant into gas phase refrigerant and liquid phase refrigerant and stores refrigerant
At the same time, gas-phase refrigerant is supplied to the suction side of the compressor (100).
Gas-liquid separator for supplying liquid refrigerant to the evaporator (300)
(500), installed in the gas-liquid separator,
Oil return hole for guiding oil to compressor (100)
And supply from the radiator (300) to the ejector (400)
The ejector (4
Eject for controlling energy conversion efficiency in 00)
And an ejector (40).
The pressure of the refrigerant before being reduced in 0) is equal to or higher than the critical pressure of the refrigerant.
And the ejector (400)
Speed energy of the high-pressure refrigerant flowing out of (200)
Nozzle that converts pressure into energy and decompresses and expands the refrigerant
(410) and cold sprayed from the nozzle (410).
The medium and the refrigerant sucked from the evaporator (300) are mixed.
While converting velocity energy into pressure energy
It has a booster (420, 430) for increasing the pressure of the medium
It is characterized by comprising.

Further, according to the invention of claim 19 ,
Energy conversion efficiency may be controlled by adjusting the reduced pressure amount of the refrigerant before flowing into the evaporator (300).

According to the twentieth aspect ,
Energy conversion efficiency may be controlled by adjusting the temperature in the evaporator (300).

Further, according to the invention of claim 21 ,
Energy conversion efficiency may be controlled by adjusting the pressure in the evaporator (300).

Further, according to the invention described in claim 22 ,
Energy conversion efficiency may be controlled by adjusting the ratio of the flow rate (Gn) of the refrigerant flowing through the radiator (200) to the flow rate (Ge) of the refrigerant flowing through the evaporator (300).

According to the twenty- third aspect , the refrigerant is sucked.
Compressor (100) that compresses and raises pressure to supercritical pressure
And heat radiation for cooling the refrigerant discharged from the compressor (100)
Device (200), an evaporator that evaporates the refrigerant and absorbs heat
(300) and the refrigerant flowing out of the radiator (200) is reduced.
The gas-phase refrigerant that has been pressure-expanded and evaporated in the evaporator (300)
Along with suction, the expansion energy is converted to pressure energy
Eje to convert and increase the suction pressure of compressor (100)
Gas and liquid from the ejector (400)
Separates phase refrigerant into gas phase refrigerant and liquid phase refrigerant and stores refrigerant
At the same time, gas-phase refrigerant is supplied to the suction side of the compressor (100).
Gas-liquid separator for supplying liquid refrigerant to the evaporator (300)
(500), installed in the gas-liquid separator,
Oil return hole for guiding oil to compressor (100)
And supply from the radiator (300) to the ejector (400)
The ejector (4
Eject for controlling energy conversion efficiency in 00)
And an ejector (40).
The pressure of the refrigerant before being reduced in 0) is equal to or higher than the critical pressure of the refrigerant.
It is characterized by being raised up to

Further, according to the invention described in claim 24 ,
The hot water may be heated by exchanging heat between the high-pressure side refrigerant and the hot water in the radiator (200) of the ejector cycle according to any one of claims 1 to 23 .

Further, according to the twenty-fifth aspect of the present invention,
17. The radiator (200) of the ejector cycle according to any one of claims 14 to 16, wherein the high-pressure side refrigerant and the hot water are heat-exchanged to heat the hot water, and further, the ejector efficiency control means (730). The energy conversion efficiency may be controlled by adjusting the temperature of hot water after heat exchange.

Further, according to the invention described in claim 26 ,
17. The radiator (200) of the ejector cycle according to any one of claims 14 to 16, wherein the high-pressure side refrigerant and the hot water are heat-exchanged to heat the hot water, and further, the ejector efficiency control means (730). The energy conversion efficiency may be controlled by adjusting the difference between the temperature of the refrigerant flowing through the radiator (200) and the temperature of the hot water.

According to a twenty-seventh aspect of the present invention,
17. The radiator (200) of the ejector cycle according to any one of claims 14 to 16, wherein the high-pressure side refrigerant and the hot water are heat-exchanged to heat the hot water, and further, the ejector efficiency control means (730). The energy conversion efficiency may be controlled by adjusting the flow rate of hot water that exchanges heat with the high-pressure refrigerant.

According to the twenty-eighth aspect , in the twenty-fourth aspect,
27 to 27 , wherein a plurality of evaporators (300) are provided, and indoor air conditioning is performed by any of the plurality of evaporators (300). .

Thus, air conditioning can be performed while heating the hot water.

According to the twenty- ninth aspect of the present invention, the compressor (100) is provided with a hot water storage tank (750) for keeping the heated hot water hot and storing it, and using the hot water stored in the hot water storage tank (750). The method is characterized in that the refrigerant sucked into the heater is heated.

As a result, the temperature of the refrigerant sucked into the compressor (100) gradually increases, so that the compressor (10
The coefficient of performance of the ejector cycle can be improved while reducing the power consumption of 0) and improving the heating capacity of the radiator (200). In the invention according to claim 30,
An ejector (400) that expands the refrigerant under reduced pressure to suck the gas-phase refrigerant evaporated in the evaporator (300) , and converts expansion energy into pressure energy to increase the suction pressure of the compressor (100) ; And the ejector (4
The refrigerant pressure before being decompressed by 00) is applied to an ejector cycle is increased to above the critical pressure of the refrigerant, Eji
Ekuta gas-liquid two-phase refrigerant from the (400) is separated into a gas phase refrigerant and liquid-phase refrigerant, comprising a tank section (540) for storing the separated liquid-phase refrigerant, the gas-phase refrigerant compressor (100) of
Supply to the suction side and supply the liquid-phase refrigerant to the evaporator (300)
A that the gas-liquid separator (500), the tank (540)
Inside, the refrigerant flowing in the ejector (400) flows upward from the lower side, and the refrigerant outlet (431) of the ejector (400) is connected to the tank (54).
The ejector (400) is incorporated in the tank (540) so as to be located above the liquid level of the refrigerant in (0).

Thus, most of the ejector (400) up to the refrigerant outlet (431) can be immersed in the liquid-phase refrigerant, so that the vertical direction of the tank (540) for storing the ejector (400) can be improved. Dimensions can be reduced.

The ejector (400) is provided in claim 3
As in the first aspect of the invention, it is preferable that the refrigerant flowing inside is configured to flow vertically from the lower side to the upper side.

According to the thirty-second aspect of the present invention, the collision wall (54) against which the refrigerant flowing from the refrigerant outlet (431) collides is provided on the refrigerant outlet (431) side of the ejector (400).
1) is provided.

As a result, the refrigerant flowing out (spouting) from the ejector (400) scatters against the impingement wall (541), but the liquid-phase refrigerant having a higher density and viscosity than the gas-phase refrigerant impinges on the impingement wall. The liquid-phase refrigerant and the gas-phase refrigerant can be efficiently separated because the liquid-phase refrigerant and the gas-phase refrigerant are not scattered or scattered as compared with the gas-phase refrigerant.

[0053] In the invention described in claim 33, sucks the gas-phase refrigerant evaporated in the evaporator by the refrigerant is decompressed and expanded (300), by converting expansion energy into pressure energy compressor (100) has an ejector (400) for raising the suction pressure, and applies the refrigerant pressure before being decompressed by the ejector (400) to the ejector cycle is increased to above the critical pressure of the refrigerant, the ejector (4
00) is separated into a gas-phase refrigerant and a liquid-phase refrigerant, and a tank unit (54) for storing the separated liquid-phase refrigerant.
0) to supply the gas-phase refrigerant to the suction side of the compressor (100).
A gas-liquid separator (500) for supplying the liquid-phase refrigerant to the evaporator (300), wherein the refrigerant outlet (431) of the ejector (400) is above the refrigerant liquid level in the tank (540). The ejector (400) is incorporated in the tank (540) such that the refrigerant ejected from the refrigerant outlet (431) collides with the inner wall of the tank (540).

Thus, the liquid-phase refrigerant and the gas-phase refrigerant can be efficiently separated without providing the collision wall (541) as in the invention of the thirty-first aspect , so that the gas-liquid separator (500 2) It is possible to efficiently separate the liquid-phase refrigerant and the gas-phase refrigerant while reducing the production cost.

According to the thirty-first aspect of the present invention, as in the thirty-fourth aspect , the refrigerant may be ejected in a substantially horizontal direction from the refrigerant outlet (431) of the ejector (400). desirable.

In the invention according to claim 35 , the ejector (400) comprises: a nozzle (410) for converting pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to decompress and accelerate the refrigerant; A mixing section (420) for mixing the high-speed refrigerant flow injected from (410) with the gas-phase refrigerant evaporated in the evaporator (300) sucked by the refrigerant flow, and a refrigerant injected from the nozzle (410) And a diffuser (430) for converting velocity energy to pressure energy to increase the pressure of the refrigerant while mixing the refrigerant sucked from the evaporator (300), and comprising a diffuser (430) of the ejector (400). , At least the nozzle (410) is located outside the tank part (540).

As a result, in the ejector (400) in the tank section (540), the low-temperature refrigerant decompressed and expanded flows, so that the tank section (540)
It is possible to prevent the liquid refrigerant in the inside from evaporating, and it is possible to supply a sufficient amount of the liquid refrigerant to the evaporator (300).

As described in claim 36 ,
It is desirable that the outlet of the liquid-phase refrigerant connected to the evaporator (300) side of the tank section (540) is provided integrally with a throttle means (600) for reducing the pressure of the liquid-phase refrigerant flowing out of the outlet.

According to the invention of claim 37, a compressor (100) for suctioning and compressing a refrigerant to increase the pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to decompress and expand the refrigerant, and the refrigerant injected from the nozzle (410) and the evaporator (300). Pressure booster (420, 430) that converts velocity energy into pressure energy while mixing with the sucked refrigerant to increase the pressure of the refrigerant.
And ejector (400) having an ejector (40
0), the gas-liquid two-phase refrigerant is separated into a gas-phase refrigerant and a liquid-phase refrigerant, and the refrigerant is stored.
0), and a gas-liquid separator (500) for supplying the liquid-phase refrigerant to the evaporator (300) in the ejector cycle. And the shape of the ejector (400) is changed according to the operating condition of the cycle.

Thus, regardless of the operation state of the ejector cycle, the cycle can be operated while maintaining high ejector efficiency.

When the degree of heating at the refrigerant outlet side of the evaporator (300) increases, the flow rate (Ge) of the refrigerant flowing into the evaporator (300) increases. On the other hand, since the pump work in the ejector (400) is constant,
When the refrigerant flow rate (Ge) increases and the flow rate ratio (α) increases, the pressure increase (ΔP) in the ejector (400) decreases accordingly. For this reason, the ejector (40
0), there is a heating degree at which the energy conversion efficiency (hereinafter, referred to as ejector efficiency ηe) is maximized.

Here, the flow ratio (α) refers to the radiator (20)
0) with respect to the refrigerant flow rate (Gn) flowing through the evaporator (30).
0) Ratio of flow rate (Ge) of refrigerant flowing through (= Ge / Gn)
Say

According to the thirty-eighth aspect of the present invention, the compressor (1) that sucks and compresses the refrigerant to increase the pressure to a supercritical pressure.
00), a radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and decompressing and expanding the refrigerant flowing out of the radiator (200). An ejector (400) that sucks the vapor-phase refrigerant evaporated in the evaporator (300) and converts expansion energy into pressure energy to increase the suction pressure of the compressor (100) ; Gas liquid
The two-phase refrigerant is separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, and the gas-phase refrigerant is supplied to the suction side of the compressor (100) and the liquid-phase refrigerant is supplied to the evaporator (300). The liquid separator (500), the radiator (200) and the ejector (40)
A control valve (731) provided in the refrigerant passage between the evaporator (300) and the refrigerant outlet side of the evaporator (300) to change the opening based on the degree of refrigerant heating.
Since the pressure of the refrigerant before the pressure reduction is increased to the critical pressure of the refrigerant or more, the ejector cycle can be operated while maintaining the high ejector efficiency ηe.

Since the refrigerant passing through the nozzle of the ejector (400) is decompressed across the saturated liquid line, the refrigerant enters a gas-liquid two-phase state in the middle of the nozzle and the throat of the nozzle (inside the nozzle) The refrigerant boils in the vicinity of the wall surface (where the cross-sectional area becomes the smallest). On the other hand, in the central portion distant from the inner wall of the nozzle, it is difficult for the refrigerant to boil, so that it is difficult to atomize the liquid droplets of the refrigerant, which causes a decrease in the ejector efficiency ηe.

On the other hand, in the present invention, the refrigerant is depressurized (squeezed) in two stages of the control valve (731) and the nozzle (ejector). , The control valve (731)), the refrigerant is boiled once, and the refrigerant is expanded at the inlet of the second stage nozzle (nozzle in this example) to recover the pressure, thereby generating a boiling nucleus. It can be boiled with the second stage nozzle as it is.

Therefore, it is possible to promote the boiling of the refrigerant in the second stage nozzle, so that the nozzle (410)
The refrigerant can be boiled even in the central portion remote from the inner wall of the slab. Consequently, since the droplets of the refrigerant can be atomized, the ejector efficiency ηe can be improved.

When the high-pressure side pressure increases, the flow rate (Gn) of the refrigerant flowing through the radiator (200) decreases. On the other hand, since the pump work in the ejector (400) is constant, when the refrigerant flow rate (Gn) decreases and the flow rate ratio (α) increases, the pressure increase (ΔP) in the ejector (400) correspondingly increases. Decreases. Therefore, there is a high-pressure side pressure at which the ejector efficiency ηe is maximized.

According to the thirty-ninth aspect of the present invention, the compressor (1) which sucks and compresses the refrigerant to increase the pressure to a supercritical pressure.
00), a radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and decompressing and expanding the refrigerant flowing out of the radiator (200). An ejector (400) that sucks the vapor-phase refrigerant evaporated in the evaporator (300) and converts expansion energy into pressure energy to increase the suction pressure of the compressor (100) ; Gas liquid
The two-phase refrigerant is separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, and the gas-phase refrigerant is supplied to the suction side of the compressor (100) and the liquid-phase refrigerant is supplied to the evaporator (300). The liquid separator (500), the radiator (200) and the ejector (40)
0), and the ejector (40)
0), a control valve (732) for controlling the high pressure side pressure based on the refrigerant temperature before the pressure is reduced in the ejector (4).
Since the pressure of the refrigerant before the pressure is reduced to the critical pressure of the refrigerant is increased to a value higher than the critical pressure of the refrigerant, the ejector cycle can be operated while maintaining the high ejector efficiency ηe.

In the present invention, the refrigerant is supplied to the control valve (73
Since the pressure is reduced (squeezed) in two stages of 2) and the nozzle (ejector), the droplet of the refrigerant can be atomized as in the invention of claim 37, and the ejector efficiency can be improved. ηe can be improved.

According to the forty-seventh aspect, the compressor (100) in which the refrigerant is suction-compressed to increase the pressure to the supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure; separating the gas-liquid two- phase refrigerant from the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant; storing the refrigerant; and compressing the gas-phase refrigerant. To the suction side of the machine (100),
A gas-liquid separator (5) that supplies the liquid-phase refrigerant to the evaporator (300)
00), and a control valve (733) provided in the refrigerant passage between the radiator (200) and the ejector (400) and changing the opening degree based on the pressure in the evaporator (300). The pressure of the refrigerant before the pressure is reduced in (400) is increased to the critical pressure of the refrigerant or more.

Thus, even if the pressure in the evaporator (300) fluctuates, the ejector efficiency ηe can be kept high by controlling the opening according to the fluctuation.

In the present invention, the refrigerant is supplied to the control valve (73).
Since the pressure is reduced (squeezed) in two stages of 2) and the nozzle (ejector), the droplet of the refrigerant can be atomized as in the invention of claim 37, and the ejector efficiency can be improved. ηe can be improved.

According to the invention described in claim 41 ,
The control valve (731-733) and the ejector (400) may be integrated.

Further, according to the invention described in claim 42 ,
The control valve (731-733) and the nozzle (410) may be integrated.

According to the invention described in claim 43, the compressor (100) that sucks and compresses the refrigerant and raises the pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure; separating the gas-liquid two- phase refrigerant from the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant; storing the refrigerant; and compressing the gas-phase refrigerant. To the suction side of the machine (100),
A gas-liquid separator (5) that supplies the liquid-phase refrigerant to the evaporator (300)
00) and a control valve provided in a refrigerant passage between the gas-liquid separator (500) and the evaporator (300), and changing an opening degree based on a refrigerant heating degree at a refrigerant outlet side of the evaporator (300). (731), wherein the pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more.

Thus, the ejector cycle can be operated while maintaining the high ejector efficiency ηe, as in the invention of the thirty- eighth aspect.

Further, since the pressure acting on the control valve (731) can be made smaller than that of the thirty- eighth aspect, the size of the control valve (731) can be reduced and the manufacturing cost can be reduced.

According to the forty-fourth aspect, the compressor (100) in which the refrigerant is sucked and compressed to increase the pressure to a supercritical pressure.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (3) for evaporating the refrigerant and absorbing heat.
00), the refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the gas-phase refrigerant evaporated in the evaporator (300), and the expansion energy is converted to pressure energy to convert the refrigerant into the compressor (100). An ejector (400) for increasing the suction pressure; separating the gas-liquid two- phase refrigerant from the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant; storing the refrigerant; and compressing the gas-phase refrigerant. To the suction side of the machine (100),
A gas-liquid separator (5) that supplies the liquid-phase refrigerant to the evaporator (300)
00) and a control valve (733) provided in the refrigerant passage between the gas-liquid separator (500) and the evaporator (300) and changing the opening degree based on the pressure in the evaporator (300). The pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more.

Thus, the ejector cycle can be operated while maintaining the high ejector efficiency ηe, as in the invention of the thirty- eighth aspect.

Further, since the pressure acting on the control valve (731) can be made smaller than that of the thirty- eighth aspect, the size of the control valve (731) can be reduced and the manufacturing cost can be reduced.

In the invention according to claim 45 , the compressor (1)
The heat exchanger (800) for exchanging heat between the refrigerant sucked into the radiator (200) and the refrigerant on the outlet side of the radiator (200) is provided.

As a result, the refrigerant flowing into the control valves (731-733) is cooled, so that the ejector (400)
The expansion energy at the nozzle decreases, the flow velocity of the refrigerant flowing out of the nozzle decreases, and the dryness of the refrigerant at the nozzle outlet decreases.

For this reason, the flow rate of the suction refrigerant sucked from the evaporator (300) to the ejector (400) increases, and the flow velocity of the suction refrigerant increases. Speed difference becomes smaller.
Therefore, the loss (vortex loss) associated with the vortex generated when the suction refrigerant and the driving refrigerant are mixed is reduced, and the ejector efficiency ηe is improved.

According to the invention described in claim 46, an ejector that decompresses and expands a refrigerant to suck a vapor-phase refrigerant evaporated in an evaporator, and converts expansion energy into pressure energy to increase a suction pressure of a compressor. (400) ,
In addition, the present invention is applied to an ejector cycle in which the refrigerant pressure before being reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more, and the gas-liquid two-phase refrigerant from the ejector (400) is combined with the gas-phase refrigerant. The liquid refrigerant is separated into liquid refrigerant and
(551) and compresses the gas-phase refrigerant into the compressor.
(100), and supplies the liquid-phase refrigerant to the evaporator (30).
A 0) for supplying the gas-liquid separator (500), the tank unit (551), an ejector as the refrigerant circulating in the ejector (400) flows toward the lower side in the upper lateral side ( 400) and a part (552, 553) of the tank part (551 ) is connected to the ejector (4 ).
00) is constituted as a part of the diffuser (430).

As a result, a diffuser (430) having a sufficiently large refrigerant passage can be formed as compared with the case where the diffuser (430) is formed only by the ejector (400).

In addition, since the space in the gas-liquid separator (500) is used to constitute the diffuser (430) having a sufficiently large refrigerant passage, the ejector (400)
, The pace for mounting the ejector (400) can be reduced, and the installability of the ejector cycle can be improved.

According to the invention described in claim 47,
The diffuser (430), it is preferable to provide projections for positioning the diffuser (430) in <br/> contact with the tank body (511) and (433).

In the invention according to claim 48, an ejector that decompresses and expands a refrigerant to suck a vapor-phase refrigerant evaporated in an evaporator, and converts expansion energy into pressure energy to increase a suction pressure of a compressor. (400) ,
In addition, the present invention is applied to an ejector cycle in which the refrigerant pressure before being reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more, and the gas-liquid two-phase refrigerant from the ejector is separated into a gas-phase refrigerant and a liquid-phase refrigerant. To store the liquid-phase refrigerant in the tank
While supplying the gas-phase refrigerant to the suction side of the compressor (100).
Feeding, and a liquid phase refrigerant evaporator to be supplied to the (300) gas-liquid separator (500), the tank portion, toward the lower side in the refrigerant upper side in circulating in the ejector (400) The ejector (400) is arranged so as to circulate, and the diffuser (43) of the ejector (400) is arranged.
At the refrigerant flow downstream side of the refrigerant outlet of 0) is characterized by being configured to deflect in a direction toward the upper side from the direction toward the flow direction of the refrigerant downward.

Thus, the inlet and outlet of the refrigerant can be concentrated on the upper side of the gas-liquid separator (500) while minimizing the pressure loss in the ejector (400) (particularly, the diffuser (430)). Becomes

Incidentally, reference numerals in parentheses of the above means are examples showing the correspondence with specific means described in the embodiments described later.

[0091]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS (First Embodiment) This embodiment is one in which the ejector cycle according to the present invention is applied to a vehicle air conditioner using carbon dioxide as a refrigerant, and FIG. It is a schematic diagram of an ejector cycle.

Reference numeral 100 denotes a compressor that draws a refrigerant from a driving source (not shown) such as a running engine to suck and compress the refrigerant. Reference numeral 200 denotes heat exchange between the refrigerant discharged from the compressor 100 and the outdoor air. Radiator (gas cooler) that cools the refrigerant
It is.

Reference numeral 300 denotes an evaporator which exhibits a refrigerating ability by exchanging heat between the air blown into the room and the liquid-phase refrigerant to evaporate the liquid-phase refrigerant, and 400 denotes a decompression and expansion of the refrigerant flowing out of the radiator 200. This is an ejector that sucks the vapor-phase refrigerant evaporated by the evaporator 300 and converts expansion energy into pressure energy to increase the suction pressure of the compressor 100.

Note that the ejector 400 is
Energy (pressure head) of high-pressure refrigerant flowing out of
410 that converts pressure into velocity energy (velocity head) to decompress and expand the refrigerant, and a mixing section 420 that suctions a vapor-phase refrigerant evaporated in the evaporator 300 by a high-velocity refrigerant flow (jet flow) injected from the nozzle 410. And a diffuser 430 for converting the velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant injected from the nozzle 410 and the refrigerant sucked from the evaporator 300.
Etc.

Reference numeral 500 denotes a gas-liquid separator for storing the refrigerant by flowing the refrigerant flowing out of the ejector 400 and separating the flowed refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant.
The separated gas-phase refrigerant is drawn into the compressor 100, and the separated liquid-phase refrigerant is drawn into the evaporator 300.

Reference numeral 600 denotes a first decompressor (throttle means) for decompressing the liquid-phase refrigerant sucked from the gas-liquid separator 500 to the evaporator 300 side. Pressure (evaporation pressure) is surely reduced.

Next, the general operation of the ejector cycle will be described.

When the compressor 100 starts, the gas-liquid separator 5
From 00, the gas-phase refrigerant is sucked into the compressor 100, and the compressed refrigerant is discharged to the radiator 200. And radiator 2
The refrigerant cooled in 00 is decompressed and expanded in the nozzle 410 of the ejector 400 and sucks the refrigerant in the evaporator 300.

Next, while the refrigerant sucked from the evaporator 300 and the refrigerant blown out from the nozzle 410 are mixed in the mixing section 420, the dynamic pressure thereof is converted to static pressure by the diffuser 430, and the gas-liquid separator 500 Return to

On the other hand, the evaporator 300
Since the refrigerant inside is sucked, the liquid-phase refrigerant flows into the evaporator 300 from the gas-liquid separator 500, and the refrigerant flowing into the evaporator 300 is
It absorbs heat from the air that blows into the room and evaporates.

FIG. 2 is a ph diagram showing the operation of the ejector cycle according to this embodiment, and the numbers shown in FIG. 2 indicate the state of the refrigerant at the positions indicated by the numbers in FIG.

At this time, the suction pressure increase Δ
P is a refrigerant inlet (point 2 shown in FIG. 2) of the nozzle 410 and a refrigerant outlet (point 3 shown in FIG. 2) of the nozzle 410, although its absolute value changes depending on the efficiency in the mixing section 420 and the diffuser 430. The larger the specific enthalpy difference (adiabatic heat drop) in the above, the larger the difference.

Next, the features (effects) of this embodiment will be described.

In this embodiment, since carbon dioxide is used as the refrigerant, as shown in FIG.
The pressure of the refrigerant before being depressurized by the (nozzle 410) is increased by the compressor 100 to a value higher than the critical pressure of the refrigerant (supercritical region), and then the pressure is expanded under reduced pressure.

Accordingly, since the pressure difference during the decompression and expansion becomes large, the specific enthalpy difference between the refrigerant inlet (point 2 shown in FIG. 2) of the nozzle 410 and the refrigerant outlet (point 3 shown in FIG. 2) of the nozzle 410 is increased. (Adiabatic heat drop) can be increased. As a result, the expansion energy generated at the time of pressure reduction can be more reliably recovered, so that the suction pressure increase ΔP can be increased, and the coefficient of performance (efficiency) of the ejector cycle can be increased.
Can be improved.

By the way, in the supercritical region, the gas-phase refrigerant also has a density substantially equal to that of the liquid-phase state, so that the refrigerant depressurized and expanded by the ejector 400 (nozzle 410) is also a gas-phase refrigerant. It is accelerated to approximately the same speed as the phase refrigerant. For this reason, the energy conversion efficiency in the ejector 400 (nozzle 410) is increased (about twice as much as Freon), so that the expansion energy generated at the time of decompression can be more reliably recovered. Therefore, since the suction pressure increase ΔP can be increased, the coefficient of performance (efficiency) of the ejector cycle can be improved.

The isentropic line of carbon dioxide on the saturated liquid line side from the critical point has a change in specific enthalpy (Δh) with respect to a change in pressure (ΔP) as compared with Freon.
Is large (= Δh / ΔP), the ejector 400
When the pressure is expanded under reduced pressure, the specific enthalpy difference (adiabatic heat drop) between the refrigerant inlet of the nozzle 410 and the refrigerant inlet of the diffuser 430 can be increased as compared with an ejector cycle using Freon as a refrigerant.

As described above, according to the present embodiment, it is possible to improve the coefficient of performance (efficiency) of the ejector cycle while eliminating the use of chlorofluorocarbon as a refrigerant using carbon dioxide.

FIG. 3 shows the coefficient of performance (COP), refrigeration capacity (cooling capacity), and high-pressure side pressure (ejector 400 (nozzle 410)) of the ejector cycle according to this embodiment.
As shown in FIG. 3, as the high pressure side pressure is increased, the refrigeration capacity is increased, but the high pressure side pressure is excessively increased. And the coefficient of performance is deteriorated.
0 (nozzle 410) shape and size, and compressor 1
It is desirable to control and adjust the discharge flow rate of 00 and the like.

(Second Embodiment) In the ejector cycle, as described above, the expansion energy is recovered by the ejector 400 and the compressor 1
The suction pressure of the compressor 00 is increased to reduce the driving force of the compressor 100, but the refrigerant pressure on the outlet side of the diffuser 430 becomes higher than the critical pressure because the refrigerant pressure on the high pressure side is higher than supercritical. There is a risk.

When the refrigerant pressure at the outlet side of the diffuser 430 becomes higher than the critical pressure, the pressure in the gas-liquid separator 500 also becomes higher than the critical pressure, and the refrigerant in the gas-liquid separator 500 is separated from the gas-phase refrigerant and the liquid phase. Since the liquid-phase refrigerant cannot be separated from the refrigerant, the liquid-phase refrigerant cannot be supplied to the evaporator 300.

Therefore, in the present embodiment, as shown in FIG. 4, a second decompressor (pressure adjusting means) 710 for reducing the pressure of the refrigerant pressurized by the ejector 400 is disposed downstream of the ejector 400 on the refrigerant flow side. At the same time, the pressure of the refrigerant after being pressurized by the ejector 400 in the pressure reducer 710 is adjusted to a pressure lower than the critical pressure (gas-liquid two-phase region).

(Third Embodiment) In the second embodiment, a second decompressor (pressure adjusting means) 710 is provided downstream of the flow of the refrigerant in the ejector 400 to reduce the pressure of the refrigerant after the pressure in the ejector 400 is increased. Although the pressure was adjusted so as to be lower than the critical pressure, in the present embodiment, as shown in FIG. 5, a third decompressor (pressure adjusting means) 720 is disposed on the upstream side of the refrigerant flow of the ejector 400, and the third depressurization is performed. Bowl 72
At 0, the pressure of the refrigerant after being pressurized by the ejector 400 is reduced to a pressure lower than the critical pressure (gas-liquid two-phase region).

Incidentally, the third pressure reducer 7 according to the present embodiment.
20 and the second decompressor 710 according to the second embodiment both adjust the refrigerant pressure after being pressurized by the ejector 400 so as to be lower than the critical pressure. However, the refrigerant pressure on the high pressure side and the ejector 400 Depending on the efficiency of
Even if the refrigerant is not decompressed by the decompressors 710 and 720, the pressure of the refrigerant after the pressure is increased by the ejector 400 may be lower than the critical pressure.

In such a case, as in the second embodiment, the second decompressor 7 is located downstream of the refrigerant flow of the ejector 400.
When 10 is provided, the second decompressor 710 becomes a flow resistance (pressure loss) of the refrigerant, which is a factor of reducing the cycle efficiency.

On the other hand, if the third decompressor 720 is provided upstream of the refrigerant flow of the ejector 400 as in the present embodiment, the pressure is always reduced in the supercritical region. Make refrigerant pressure after being boosted Te is
It is possible to prevent the flow resistance (pressure loss) of the refrigerant from increasing while adjusting the pressure to be lower than the critical pressure.

(Fourth Embodiment) In the first to third embodiments, the refrigerant flowing out of the ejector 400 (after being pressurized by the diffuser 430) is separated into a gas-phase refrigerant and a liquid-phase refrigerant by the gas-liquid separator 500. And the gas-phase refrigerant flows out to the suction side of the compressor 100, and the liquid-phase refrigerant flows out to the evaporator 300 side. In the present embodiment, as shown in FIG. By providing at the refrigerant outlet of the mixing section 420, the liquid-phase refrigerant is separated and extracted from the refrigerant before flowing out of the ejector 400, and the separated and extracted liquid-phase refrigerant is supplied to the evaporator 300 side, and the gas-phase refrigerant is It is supplied to the suction side of the compressor 100.

Next, the features (effects) of this embodiment will be described.

FIG. 7A is a numerical simulation result showing the relationship between the ejector efficiency ηe and the refrigerating capacity Qe (= Ge × Δh) generated in the evaporator 300, and FIG. 7B is a graph showing the relationship between the ejector efficiency ηe and the ejector efficiency ηe. The suction pressure increase ΔP of the compressor 100
7C is a numerical simulation result showing the relationship between the specific enthalpy difference Δh between the refrigerant inlet side and the outlet side of the evaporator 300. FIG. 7C shows the ejector efficiency ηe and the mass flow rate of the refrigerant sucked into the compressor 100. It is a numerical simulation result showing the relationship between Gr and the mass flow rate Ge of the refrigerant flowing in the evaporator 300.

As is clear from FIG. 7, when the ejector efficiency ηe increases, the suction pressure increase ΔP increases and the work load of the compressor 100 can be reduced, but when the suction pressure increase ΔP increases. , Gas-liquid separator 5
Since the pressure inside 00 increases, the specific enthalpy of the refrigerant when flowing into the evaporator 300 increases, as shown by the broken line in FIG. Therefore, the evaporator 300
Enthalpy difference Δh between the refrigerant inlet side and the outlet side becomes smaller, and the refrigerating capacity Qe generated in the evaporator 300 also becomes smaller.

Incidentally, the ejector efficiency ηe is the mass flow rate G of the refrigerant flowing through the radiator 200 (high pressure side heat exchanger).
The product of n and the enthalpy difference Δie between the inlet and the outlet of the nozzle 410 is used as a denominator. Is defined with the sum of the mass flow rate Ge of the refrigerant flowing through and the pressure recovery ΔP at the ejector 400. Specifically, the ejector 400
Considering the velocity energy of the suction refrigerant before being sucked into
It was defined by Equation 1 below.

[0122]

(Equation 1)

On the other hand, in the present embodiment, the liquid-phase refrigerant is separated and extracted from the refrigerant before flowing out of the ejector 400, and the separated and extracted liquid-phase refrigerant is supplied to the evaporator 300 side. As shown by the solid line, even if the suction pressure increase ΔP increases, the pressure increase ΔPe of the liquid refrigerant flowing out of the gas-liquid separator 500 can be made smaller than the suction pressure increase ΔP.

Therefore, it is possible to prevent the specific enthalpy of the refrigerant from flowing into the evaporator 300 from being increased, so that the specific enthalpy difference Δhe between the refrigerant inlet and outlet of the evaporator 300 can be increased. , Evaporator 30
The refrigeration capacity Qe generated at 0 can be increased.

FIG. 9 is a numerical curve showing the relationship between the radial position from the refrigerant outlet of the nozzle 410 to the refrigerant outlet of the diffuser 430 with respect to the center of the cross section of the refrigerant passage of the ejector 400 and the flow velocity of the refrigerant. This is the result of the translation.

In the numerical simulation,
It is assumed that the nozzle 410, the mixing unit 420, and the diffuser 430 have a rotationally symmetric shape, and the flow velocity distribution is symmetrically distributed with respect to the central part (reference). Further, the refrigerant flow velocity (gas velocity) indicates a magnitude when the velocity at the nozzle 410 outlet is set to 1.

As is apparent from FIG. 9, the jet flow (driving gas) flowing out of the nozzle 410 decreases its flow velocity while sucking and accelerating the refrigerant from the evaporator 300. At this time, mixing is performed such that the flow rate of the suction gas (suction flow gas) sucked from the evaporator 300 and the flow rate of the drive flow gas are substantially equal at the refrigerant outlet of the mixing section 420 (the refrigerant inlet of the diffuser 430). The mixed refrigerant flows into the diffuser 430 and increases the pressure while decreasing the flow velocity.

That is, the refrigerant (driving gas) flowing through the ejector 400 stops sucking the suction gas at the refrigerant outlet of the mixing section 420 and its pressure is increased by the diffuser 430. As described above, if the gas-liquid separator 500 is provided at the refrigerant outlet of the mixing section 420 and the separated and extracted liquid-phase refrigerant is supplied to the evaporator 300 side, the suction pressure increase ΔP is secured and the high ejector efficiency ηe is maintained. In addition, it is possible to prevent the specific enthalpy of the refrigerant when flowing into the evaporator 300 from increasing, and to increase the refrigeration capacity Qe.

(Fifth Embodiment) In the present embodiment, as shown in FIG. 10, the liquid-phase refrigerant is separated from the refrigerant flowing through the ejector 400 at the refrigerant outlet side of the mixing section 420 as in the fourth embodiment. The extracted, separated and extracted liquid-phase refrigerant flows out to the evaporator 300 side, is added to the gas-liquid separator 500 (hereinafter, referred to as the first gas-liquid separator 500), and flows out of the ejector 400 (diffuser 430). A second gas-liquid separator 510 that separates the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant and supplies the separated liquid-phase refrigerant to the evaporator 300 side and supplies the gas-phase refrigerant to the suction side of the compressor 100 Is provided.

Thus, temporarily, the first gas-liquid separator 500
Even if it is not possible to separate and extract a sufficient amount of the liquid-phase refrigerant at, the second gas-liquid separator 510 separates the refrigerant flowing out of the ejector 400 into a gas-phase refrigerant and a liquid-phase refrigerant, Since the refrigerant is supplied to the evaporator 300, a sufficient amount of the liquid-phase refrigerant can be supplied to the evaporator 300.

The pressure in the second gas-liquid separator 500 is
Since the pressure becomes the pressure before the pressure is increased by the diffuser 430, in the present embodiment, the first gas-liquid separator 500 and the evaporator 3
No decompressor is provided in the refrigerant passage connecting to 00. On the other hand, the pressure in the second gas-liquid separator 510 becomes a pressure increased by the diffuser 510, so that the pressure reducing device 6 is provided in the refrigerant passage connecting the second gas-liquid separator 510 and the evaporator 300.
FIG. 11 shows the position of the refrigerant in the radial direction with respect to the center of the cross section of the refrigerant passage of the ejector 400 and the ratio of the liquid-phase refrigerant in the refrigerant. This is a numerical simulation result showing the relationship with (liquid volume ratio). As is clear from FIG. 11, the liquid volume ratio is the largest at the center of the cross section of the refrigerant passage. The calculation conditions are the same as in the fourth embodiment. In FIG. 11, the solid line indicates the vicinity of the exit of the nozzle 410, the broken line indicates the vicinity of the exit of the mixing unit 420, and the one-dot chain line indicates the diffuser 4
It shows the vicinity of exit 30.

Therefore, in the present embodiment, the introduction opening 50 of the refrigerant introduction pipe 501 for guiding the refrigerant to the first gas-liquid separator 500 is provided.
2 is arranged at the center of the cross section of the refrigerant passage of the ejector 400 (on the refrigerant outlet side of the mixing section 420),
Liquid phase refrigerant is efficiently separated and extracted.

(Sixth Embodiment) The present embodiment is directed to the first gas-liquid separator 5 according to the fifth embodiment.
00 and the second gas-liquid separator 510 are integrated into one gas-liquid separator 520, thereby improving miniaturization and mountability (installability).

More specifically, as shown in FIG. 12, a casing 521 is vertically divided by a partition member 523 having a plurality of orifices (small holes) 522 such as punched metal, and a refrigerant introduction pipe 501 is partitioned. The space 524 formed below the member 523 is communicated, and the refrigerant outlet side of the ejector 400 (diffuser 530) is communicated with the space 525 formed below the partition member 523.

Then, the space 525 side is communicated with the suction side of the compressor 100, and the gas phase refrigerant is sucked by the compressor 100.
The liquid-phase refrigerant accumulated in the space 524 is supplied to the evaporator 300 side. At this time, the orifice 522 decompresses the refrigerant flowing from the space 525 to the space 524 to reduce the pressure of the refrigerant.
Functioning as a pressure reducing means (throttling means) for suppressing the pressure increase on the side of the ejector 40 together with the partition member 523.
It functions as a disturbance prevention means for preventing the liquid-phase refrigerant in the gas-liquid separator 520 from being disturbed by the refrigerant flowing out from the zero (diffuser 530).

(Seventh Embodiment) In the present embodiment, as shown in FIG.
0, the gas-liquid separator 500 and the pressure reducer (throttling means) 600 are integrated, and the detailed structure will be described below.

In FIG. 13, reference numeral 540 denotes a metal tank portion (tank main body) for separating the refrigerant ejected from the ejector 400 (diffuser 430) into a gas-phase refrigerant and a liquid-phase refrigerant and storing the separated liquid-phase refrigerant. ) And the ejector 40
0 means that the refrigerant flowing in the ejector 400 flows vertically from the lower side to the upper side in the tank section 540, and the refrigerant flowing in the ejector 400 (the diffuser 43)
The refrigerant outlet part 431 of (0) is built in the tank part 540 so as to be located above the refrigerant liquid level LS in the dunk part 540 and open upward.

At this time, the mixing section 420
The refrigerant passage extending to the diffuser 430 through the nozzle is substantially linear so that unnecessary pressure loss does not occur in the refrigerant, and the nozzle 410 is located outside the tank portion 540 and exposed to the atmosphere. I have.

A collision wall (jam plate) 541 against which the refrigerant flowing from the refrigerant outlet 431 collides is provided on the refrigerant outlet 431 side of the ejector 400 (diffuser 430).
Are joined to the inner wall of the tank section 540.

Incidentally, reference numeral 542 denotes a gas-phase refrigerant outflow pipe through which gas-phase refrigerant accumulated above the tank section 540 flows out to the suction side of the compressor 100.
Is formed in a U-shape by bending at approximately 180 ° in the liquid-phase refrigerant accumulated below the tank portion 540.

The bent portion 542a located in the liquid-phase refrigerant in the gas-phase refrigerant outflow pipe 542 is provided with lubricating oil mixed in the liquid-phase refrigerant (refrigeration for lubricating sliding parts in the compressor 100). An oil return hole 543 for sucking (machine oil) is provided. Note that the lubricating oil sucked from the oil return hole 543 is actually a liquid refrigerant containing a large amount of lubricating oil.

Reference numeral 543 denotes a liquid-phase refrigerant outlet pipe for discharging the liquid-phase refrigerant collected below the tank section 540 to the evaporator 300 side. A vessel 600 (in this embodiment, an orifice such as a fixed throttle having a fixed opening) is provided.

Next, the features (effects) of the ejector-integrated gas-liquid separator according to this embodiment will be described.

[0144] The refrigerant flowing out (spouting) from the ejector 400 collides with the collision wall 541 and scatters. The liquid-phase refrigerant having a higher density and viscosity than the gas-phase refrigerant collides with the collision wall 541 and sticks. Alternatively, the liquid-phase refrigerant and the gas-phase refrigerant can be efficiently separated because they are not greatly scattered as compared with the gas-phase refrigerant. Note that the liquid-phase refrigerant that has adhered to the collision wall 541 falls down due to its own weight.

The ejector 400 (diffuser 4)
Since the refrigerant outlet portion 431 of (30) is located above the refrigerant liquid level LS in the dunk portion 540 and is open, the refrigerant flowing out (spouting) from the ejector 400 (diffuser 430) causes the inside of the tank portion 540 to be opened. Since the refrigerant can be prevented from being agitated, it is possible to prevent the refrigerant that has been gas-liquid separated from being mixed.

Further, since the refrigerant outlet 431 is open upward, the ejector 400 (the diffuser 43)
The liquid refrigerant having a high density is easily separated and extracted from the refrigerant flowing out (spouting) from 0).

When the ejector 400 is built in the gas-liquid separator 500 (tank section 540), as shown on the right side of the drawing of FIG. 14, the refrigerant flowing in the ejector 400 moves from the upper side to the lower side. That the refrigerant outlet 431 of the ejector 400 (diffuser 430) is positioned above the refrigerant liquid level LS in the dunk part 540 (hereinafter, this means is referred to as an upper built-in type). Although it is conceivable, this upper built-in type
For the reasons described below, the vertical dimension H of the gas-liquid separator 500 (tank portion 540) is rather large.

In other words, the refrigerant outlet portion is used for both the upper built-in gas-liquid separator and the gas-liquid separator according to the present embodiment (hereinafter referred to as the lower built-in gas-liquid separator). 431 needs to be positioned above the refrigerant liquid level LS in the dunk portion 540, so that the liquid level height h1 and the nozzle 4
Assuming that the dimensions from 10 to the refrigerant outlet 431 are the same for the upper built-in type and the lower built-in type, the upper built-in type gas-liquid separator sets the size c2 above the refrigerant liquid level LS to the nozzle 410.
Needs to be larger than the size from to the refrigerant outlet 431.

On the other hand, in the lower built-in type gas-liquid separator, most of the part (mixing part 420) from the nozzle 410 to the refrigerant outlet 431 can be immersed in the liquid-phase refrigerant. The vertical dimension H of the vessel 500 (tank section 540) can be made smaller than that of the upper built-in gas-liquid separator.

By the way, from the nozzle 410 to the refrigerant outlet 43
If the dimension up to 1 is sufficiently small, the vertical dimension H of the upper built-in gas-liquid separator can be reduced to the same degree as the vertical dimension H of the lower built-in gas-liquid separator.
If the dimension from the nozzle 410 to the refrigerant outlet 431 is small, there is a high possibility that the refrigerant cannot be sufficiently sucked from the evaporator 300 and the refrigerant cannot be sufficiently pressurized by the diffuser 430.

By the way, the nozzle 410 has the radiator 20
0, the refrigerant having a relatively high temperature flows into the ejector 400, including the nozzle 410.
When the whole is built in the tank unit 540, the liquid-phase refrigerant in the tank unit 540 evaporates with the high-temperature refrigerant before being decompressed and expanded, so that a sufficient amount of the liquid-phase refrigerant is supplied to the evaporator 300. May not be possible.

On the other hand, in the present embodiment, at least the nozzle 410 of the ejector 400 is connected to the tank 5.
40, the refrigerant flowing through the tank 540 out of the refrigerant flowing through the ejector 400 is
The low-temperature refrigerant is reduced in pressure and expanded by the nozzle 410. Therefore, it is possible to prevent the liquid-phase refrigerant in the tank unit 540 from evaporating, so that a sufficient amount of the liquid-phase refrigerant can be supplied to the evaporator 300.

In this embodiment, the ejector 400 is built into the gas-liquid separator 500 so that the refrigerant flowing in the ejector 400 flows vertically from the lower side to the upper side in the tank section 540. However, the present embodiment is not limited to this, and, for example, the refrigerant flowing in the ejector 400 may flow upward from the lower side in a state inclined with respect to the horizontal plane. .

In this embodiment, only the nozzle 410 is located outside the tank section 540, but in this embodiment,
For example, the mixing section 420 may be located outside the tank section 540.

In the present embodiment, the refrigerant passage from the nozzle 410 to the diffuser 430 via the mixing section 420 is substantially straight. However, in the present embodiment, at least the refrigerant passage from the nozzle 410 to the mixing section 420. The diffuser 430 may be bent since the passage may be substantially straight.

It should be noted that the “coolant passage is substantially straight” here.
The term does not mean strictly on a straight line, but includes a bending that does not cause a manufacturing error or a large pressure loss.

(Eighth Embodiment) In the seventh embodiment, the ejector 400 (the diffuser 4
30) The refrigerant flowing out from the refrigerant outlet portion 431 side is caused to collide with the collision wall 541. In the present embodiment, as shown in FIGS. 15 and 16, the refrigerant outlet portion 431 is positioned above the refrigerant liquid level LS. In this state, the ejector 400 is built in the tank unit 540 so that the refrigerant ejected from the refrigerant outlet 431 collides with the inner wall of the tank unit 540.

As a result, the collision wall 541 can be eliminated, so that the liquid-phase refrigerant and the gas-phase refrigerant can be efficiently separated while reducing the manufacturing cost of the gas-liquid separator 500.

In this embodiment, the nozzle 41
0 is located outside the tank section 540, so that the liquid-phase refrigerant in the tank section 540 can be prevented from evaporating as in the seventh embodiment, and a sufficient amount of the liquid-phase refrigerant is supplied to the evaporator 300. Can be supplied.

In this embodiment, the ejector 40
Although the longitudinal direction of the ejector 400 is set to be substantially horizontal so that the refrigerant flowing in the inner space 0 flows in a substantially horizontal direction, the present embodiment is not limited to this.
The refrigerant circulating inside 00 may flow from the lower side to the upper side in a state inclined with respect to the horizontal plane.

(Ninth Embodiment) As shown in FIG. 17, this embodiment uses a high-pressure side heat exchanger (radiator 2) of an ejector cycle using carbon dioxide as a refrigerant.
00) relates to an ejector cycle type water heater (hereinafter, abbreviated as a water heater) that heats the hot water by exchanging heat between the refrigerant and the hot water.

Then, the evaporator 30 is removed from the gas-liquid separator 500.
An electric flow control valve (variable throttle) 730 capable of adjusting the flow rate is provided in a refrigerant passage through which the liquid-phase refrigerant supplied to 0 flows, and the gas-liquid flow control valve 730 is provided on the outlet side of the ejector 400 (diffuser 430). A first refrigerant temperature sensor 741 for detecting the temperature of the refrigerant before flowing into the separator 500 and a second refrigerant temperature sensor 742 for detecting the temperature of the refrigerant flowing into the evaporator 300 at the outlet side of the flow control valve 730 are provided. The valve opening of the flow control valve (variable throttle) 730 is controlled (adjusted) based on the temperatures detected by the temperature sensors 741 and 742.
I do.

The radiator 200 (water-refrigerant heat exchanger)
Is configured such that heat exchange is performed in a state where the refrigerant and the hot water flow in opposite directions (including a direct opposite flow). In the compressor 100, the flow rate of the refrigerant flowing into the ejector 400 becomes a predetermined value. Motor M that drives the compressor 100
The rotation speed is controlled by o.

Incidentally, reference numeral 750 is a hot water storage tank for keeping hot water heated by the radiator 200 for storage, and reference numeral 751 is an electric pump for circulating hot water between the hot water storage tank 750 and the radiator 200. , 743 is a hot water storage tank 75
A hot water temperature sensor for detecting the temperature of hot water within 0 is provided. Reference numeral 740 denotes an electronic control unit (ECU) that controls the valve opening of the flow control valve 730, the electric motor Mo (compressor 100), and the pump 751. .

Next, the schematic operation and features of the water heater according to the present embodiment will be described.

Hot water (hot water) warmed and stored in hot water storage tank 750 is discharged according to a request from a user (user) of the water heater, and the amount of hot water in hot water storage tank 750 is reduced to a predetermined amount or less. Sometimes tap water is stored in a hot water storage tank 750
Supplied to

On the other hand, when the temperature of the hot water in the hot water storage tank 750 drops below the predetermined temperature, the pump 151 and the compressor 100 are controlled while controlling the valve opening of the flow control valve 730 to maintain a high ejector efficiency ηe. Is operated to heat the hot water in the hot water storage tank 750. Here, “controlling the valve opening degree of the flow control valve 730 to maintain a high ejector efficiency ηe” is specifically performed as follows.

That is, as described above, the ejector efficiency ηe is the ratio of the pressure energy recovered (boosted) by the diffuser 430 to the expansion energy generated by the ejector 400 (nozzle 410). The increased pressure energy increases the coefficient of performance of the cycle.

As is well known, the cycle coefficient of performance is the cycle output (in this case, the amount of heat radiated from the radiator 200) with respect to the energy input to the cycle (in this case, the power consumption of the compressor 100). Say the ratio.

On the other hand, the ejector efficiency ηe is, as is clear from the above equation 1, the refrigerant flow Ge flowing through the evaporator 300 with respect to the refrigerant flow Gn flowing through the radiator 200.
Flow rate ratio α (= Ge / Gn), pressure recovery (pressure rise) ΔP at the ejector 400 (diffuser 430), enthalpy difference Δie between the entrance and exit of the nozzle 410, and the evaporator 3
From 00, it becomes a function of the flow velocity Ue of the refrigerant sucked into the ejector 400, but the flow velocity Ue (Ge · Ue2 /
The value of 2) is negligibly small and ΔP / (ρg
.DELTA.ie) decreases as the flow rate ratio .alpha. Increases, and decreases. Therefore, if the relationship between the ejector efficiency .eta.e and the flow rate ratio .alpha. Is determined using .DELTA.P / (. Rho.g..DELTA.ie) as a parameter .beta. The characteristic has a maximum value as shown in FIG.

Note that the parameter β (n) and the parameter β (n + 1) do not indicate that the parameter β (n + 1) is larger than the parameter β (n). Parameter β (n + 1)
Is different from the value of.

Therefore, as the parameter β changes, the ejector efficiency ηe at that time at the parameter β
By controlling the valve opening of the flow control valve 730 such that the maximum value and the flow ratio α are satisfied, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

As described above, since the ejector cycle has the refrigerant flow on the high pressure side (before the pressure is reduced by the ejector 400) and the refrigerant flow on the low pressure side (the evaporator 300 side), the parameter β is set as follows. , At least the state of the high-pressure side refrigerant (enthalpy) and the function of the low-pressure side refrigerant (enthalpy).

Therefore, in the present embodiment, the ejector cycle (water heater) is controlled by determining the parameter β based on the detected temperatures of the two refrigerant temperature sensors 741 and 742 and controlling the valve opening of the flow control valve 730. Driving efficiently.

In this embodiment, the flow control valve 7
The ejector efficiency control means for controlling the energy conversion efficiency by adjusting the depressurized amount (flow rate) of the refrigerant before flowing into the evaporator 300 is constituted by the flow control valve 7.
When the opening degree of the valve 30 is changed, the pressure and temperature in the evaporator 300 and the ejector 400 (the diffuser 43) are changed.
0), the pressure increase amount also changes, so the flow control valve (ejector efficiency control means) 730 adjusts any one of the flow ratio α, the pressure and temperature in the evaporator 300, and the pressure increase amount by the ejector 400 (diffuser 430). Thus, it can be said that the ejector efficiency ηe is adjusted.

In this embodiment, the parameter β is determined based on the temperature of the high-pressure side refrigerant and the temperature of the low-pressure side refrigerant. However, the refrigerant state (enthalpy) can be specified from the pressure. Alternatively, the parameter β may be determined based on the pressure of the high-pressure side refrigerant and the pressure of the low-pressure side refrigerant.

When determining the parameter β, factors that vary depending on the environment in which the ejector cycle is operated, such as the outside air temperature, may be considered in addition to the temperature or pressure of the refrigerant.

The detection positions of sensors (detection means) for detecting the state of the high-pressure side refrigerant (enthalpy) and the state of the low-pressure side refrigerant (enthalpy) are limited to the positions shown in FIG. Instead, for example, the ejector 400
The state (enthalpy) of the high-pressure side refrigerant may be detected at the refrigerant inlet side of the refrigerant, and the state (enthalpy) of the low-pressure side refrigerant may be detected at the refrigerant outlet side of the evaporator 300.

(Tenth Embodiment) In the present embodiment, as shown in FIG.
At the refrigerant inlet side of the ejector 400,
A parameter β is determined based on the detected temperatures of the two refrigerant temperature sensors 741 and 742, and the valve opening of the flow rate control valve 730 is controlled so as to maintain a high ejector efficiency ηe.

In the present embodiment, the flow control valve 7
When the opening degree of the valve 30 is adjusted, the refrigerant pressure on the high pressure side also changes, so that the flow control valve (ejector efficiency control means) 7
30 can be said to adjust the ejector efficiency ηe by adjusting either the flow ratio α or the refrigerant pressure on the high pressure side.

(Eleventh Embodiment) In the ninth and tenth embodiments, the flow rate control valve 730 is provided in the ejector cycle to control the cycle so as to increase the ejector efficiency ηe. As shown, the flow control valve 730 is eliminated, the pump 751 is controlled based on the temperatures detected by the two refrigerant temperature sensors 741 and 742, and the flow rate of the hot water that exchanges heat with the high-pressure refrigerant in the radiator 200 is controlled. Thus, the energy conversion efficiency (ejector efficiency ηe) of the ejector 400 is increased by adjusting the temperature of the hot water after the heat exchange.

(Twelfth Embodiment) In the present embodiment, as shown in FIG. 21, a third refrigerant temperature sensor 74 for detecting the temperature of the refrigerant flowing out of the radiator 200
4 and a hot water temperature sensor 745 for detecting the temperature of hot water flowing into the radiator 200, and a pump 7 based on the detected temperatures of both refrigerant temperature sensors 741 and 742.
51 by controlling the difference between the temperature of the refrigerant flowing through the radiator 200 and the temperature of the hot water.
The conversion efficiency (ejector efficiency ηe) of the energy at 0 is increased.

(Thirteenth Embodiment) In the thirteenth embodiment, as shown in FIG. 22, a heat exchanger (heating means) 800 for exchanging heat between the refrigerant flowing out of the radiator 200 and the refrigerant drawn into the compressor 100 is used. Compressor 10
It is configured to heat the refrigerant of 0 drawn.

Next, the features (effects) of this embodiment will be described.

In the ejector cycle, the refrigerant pressurized by the ejector 400 (diffuser 430) is sucked into the compressor 100, so that the refrigerant is sucked into the compressor as compared with a normal vapor compression refrigeration cycle not using the ejector 400. (Saturated gas) refrigerant has a low enthalpy. For this reason, if the discharge pressure of the compressor in the ejector cycle is the same as the discharge pressure of the compressor in the normal vapor compression refrigeration cycle, the temperature of the refrigerant discharged from the compressor 100 is reduced by the normal vapor compression. The ejector cycle is lower than the refrigeration cycle.

On the other hand, in the present embodiment, the radiator 2
Heat exchange between the refrigerant flowing out of the compressor 00 and the refrigerant drawn into the compressor 100 is performed to heat the refrigerant drawn into the compressor 100. Therefore, the temperature of the refrigerant drawn into the compressor 100 can be increased. Therefore, the temperature of the refrigerant discharged from the compressor 100 increases, and the heating capacity (hot water supply capacity) of the radiator 200 and the coefficient of performance of the cycle can be improved.

(Fourteenth Embodiment) In the fourteenth embodiment, as shown in FIG. 23, the heat exchange between the electric motor Mo (drive source) for driving the compressor 100 and the refrigerant drawn into the compressor 100 is performed. Vessel (heating means) 810
Is provided to heat the refrigerant sucked into the compressor 100.

(Fifteenth Embodiment) In the present embodiment, as shown in FIG.
Is provided with a heat exchanger 820 for heating the refrigerant drawn into the compressor 100 by the hot water stored in the compressor.

As a result, the temperature of the refrigerant sucked into the compressor 100 gradually increases, so that the heating power of the radiator 200 is improved, the power consumption of the compressor 100 is reduced, and the coefficient of performance of the cycle is reduced. Can be improved.

(Sixteenth Embodiment) In the present embodiment, the ejector cycle according to the present invention is applied to a heat management (heat management) system for a whole building such as a home or a building including a water heater. In particular,
As shown in FIG. 25, a heat exchanger (heating means) 830 that collects waste heat (remaining hot water of a bath in the present embodiment) generated in the building and exchanges heat with refrigerant drawn into the compressor 100.
And the ejector 400 and the gas-liquid separator 50
A second evaporator 310 is provided between the first evaporator and the second evaporator.

As a result, the waste heat absorbs heat while improving the heating capacity (hot water supply capacity) of the radiator 200 and the coefficient of performance of the cycle while cooling the room (air conditioning) with the evaporator 300, for example. Heat absorbed and second evaporator 310
The hot water may be heated by the heat absorbed in the step.

In the present embodiment, indoor cooling (air conditioning) is performed by the evaporator 300. However, the present embodiment is not limited to this. Cooling may be performed. Also, two evaporators 3000,
At 310, indoor cooling may be performed.

Further, the present embodiment is not limited to the configuration shown in FIG. 25, and hot water storage tank 750 may be used as a hot-air exchanger for (floor) heating.

Further, the present embodiment is not limited to the configuration shown in FIG. 25. For example, as shown in FIG. May be supplied.

Thus, the heat supplied from the ejector cycle to the hot water can be efficiently used, and the hot water utilization equipment 7 which does not require the hot water storage tank 750 can be used.
Heat can be supplied in one ejector cycle to 53 and a water heater that requires a hot water storage tank 750 such as a water heater.

(Seventeenth Embodiment) In this embodiment, as shown in FIG. 27, a refrigerant passage between the radiator 200 and the ejector 400 is opened based on the refrigerant heating degree at the refrigerant outlet side of the evaporator 300. A control valve 731 for changing the degree is provided.

The control valve 731 according to the present embodiment is
A so-called external pressure equalizing type temperature expansion valve that mechanically senses the refrigerant temperature at the refrigerant outlet side of the evaporator 300 to maintain the degree of heating of the refrigerant at a predetermined constant value. And 731b is an equalizing (outer equalizing) tube.

Next, the features (effects) of this embodiment will be described.

When the degree of heating at the refrigerant outlet side of the evaporator 300 increases, the flow rate Ge of the refrigerant flowing into the evaporator 300 increases.
Becomes larger. On the other hand, since the pump work in the ejector 400 is constant, when the refrigerant flow rate Ge increases and the flow rate α increases, the ejector 40 responds accordingly.
The step-up ΔP at 0 decreases. For this reason, as shown in FIG. 28, there is a heating degree at which the ejector efficiency ηe is maximized.

Therefore, in the present embodiment, the control valve 731 is controlled so as to maintain the heating degree at which the ejector efficiency ηe is maximized.
To control the ejector cycle while maintaining a high ejector efficiency ηe.

In the present embodiment, the heating degree is controlled to be substantially constant. However, the present embodiment is not limited to this. For example, the control valve 731 may be electrically operated.
The control target heating degree may be changed according to the operation state of the ejector cycle.

(Eighteenth Embodiment) In this embodiment, as shown in FIG. 29, an ejector 400 is provided in a refrigerant passage between a radiator 200 and an ejector 400.
A control valve 732 for controlling the high-pressure side pressure based on the refrigerant temperature before the pressure is reduced (in this embodiment, before flowing out of the radiator 200 and reducing the pressure) is provided. here,
The high pressure refers to the control valve 732 and the ejector 400
This means the refrigerant pressure before the pressure is reduced by (nozzle 410).

The control valve 732 according to the present embodiment is
The refrigerant temperature at the refrigerant outlet side of the radiator 200 is mechanically sensed, and the high-pressure side pressure is controlled according to the sensed refrigerant temperature. Reference numeral 732a is a temperature sensing unit that senses the refrigerant temperature.

Next, the features (effects) of this embodiment will be described.

When the high-pressure side pressure increases, the radiator 200
, The flow rate Gn of the refrigerant flowing therethrough decreases. On the other hand, since the pump work in the ejector 400 is constant, when the refrigerant flow rate Gn decreases and the flow rate ratio α increases, the pressure increase ΔP in the ejector 400 decreases accordingly. For this reason, as shown in FIG.
There is a high pressure side at which e is maximum.

Therefore, in the present embodiment, the control valve 7 is controlled so as to maintain the high-pressure side pressure at which the ejector efficiency ηe is maximized.
32, the ejector cycle is operated while maintaining a high ejector efficiency ηe.

In the present embodiment, the mechanical control valve 7
Although 32 is used, the present embodiment is not limited to this, and an electric control valve may be used.

(Nineteenth Embodiment) In the nineteenth embodiment, as shown in FIG. 31, the pressure inside the evaporator 300 (heat load in the evaporator 300) is provided in the refrigerant passage between the radiator 200 and the ejector 400. Is provided with a control valve 733 whose valve opening is controlled based on.

[0209] The control valve 733 according to the present embodiment comprises:
733a has a structure similar to a so-called internal pressure equalization type temperature expansion valve in which the pressure in the evaporator 300 is mechanically sensed and the valve opening changes in accordance with the sensed pressure.
Is a pressure equalizing pipe for guiding the pressure in the evaporator 300 to the control valve 733.

For this reason, when the pressure in the evaporator 300 (heat load in the evaporator 300) increases, the opening of the control valve 733 increases, and conversely, the pressure in the evaporator 300 (evaporator 3) increases.
When the heat load at 00 is low, the opening of the control valve 733 decreases.

Next, features (effects) of this embodiment will be described.

According to the present embodiment, since the valve opening is controlled based on the pressure in the evaporator 300 (heat load in the evaporator 300), the pressure in the evaporator 300 (heat load in the evaporator 300) is controlled. ) Varies, the ejector efficiency ηe can be kept high by controlling the opening according to the variation.

In this embodiment, when the pressure in the evaporator 300 (heat load in the evaporator 300) increases, the opening of the control valve 733 increases, and conversely, the pressure in the evaporator 300 (evaporation) increases. When the heat load in the evaporator 300 decreases, the opening of the control valve 733 is controlled so as to decrease, so that the ejector efficiency ηe is maintained high while the flow rate of the refrigerant flowing into the evaporator 300 is set to an appropriate flow rate. It is possible to

(Twentieth Embodiment) In the seventeenth embodiment, the radiator 200 and the ejector 400
A control valve 731 is provided in the refrigerant passage between
0 based on the degree of heating of the refrigerant at the refrigerant outlet side.
The opening degree of the evaporator 300 is controlled by providing a control valve 731 in a refrigerant passage between the gas-liquid separator 500 and the evaporator 300 as shown in FIG. The opening of the control valve 731 is controlled based on the refrigerant heating degree on the side.

As a result, the pressure acting on the control valve 731 can be made smaller than in the seventeenth embodiment, so that the size of the control valve 731 can be reduced and the manufacturing cost can be reduced.

(Twenty-First Embodiment) In the nineteenth embodiment, the radiator 200 and the ejector 400
33, the control valve 733 is provided in the refrigerant passage between the gas and liquid separator 500 and the evaporator 300, as shown in FIG. The valve opening is controlled based on the pressure in the evaporator 300 (heat load in the evaporator 300).

(Twenty-second Embodiment) In this embodiment, as shown in FIGS.
The heat exchanger (internal heat exchanger) 800 for exchanging heat between the refrigerant flowing out of the compressor and the refrigerant drawn into the compressor 100 is provided.

As a result, the refrigerant flowing into the control valves 731 to 733 is cooled, so that the expansion energy in the nozzle 410 decreases, the flow velocity of the refrigerant flowing out of the nozzle 410 decreases, and the drying of the refrigerant at the outlet of the nozzle 410 decreases. Degree decreases.

For this reason, the ejector 4
Since the flow rate of the suction refrigerant sucked at 00 increases and the flow rate of the suction refrigerant increases, the speed difference between the flow rate of the driving refrigerant blown out from the nozzle 410 and the flow rate of the suction refrigerant decreases. Therefore, the loss (vortex loss) associated with the vortex generated when the suction refrigerant and the driving refrigerant are mixed is reduced, and the ejector efficiency ηe is improved.

FIG. 34 shows an example in which a heat exchanger 800 is provided in the ejector cycle according to the seventeenth embodiment, and FIG. 35 shows an example in which the heat exchanger 800 is provided in the ejector cycle according to the eighteenth embodiment. 36 shows an example in which a heat exchanger 800 is provided in the ejector cycle according to the nineteenth embodiment. FIG. 37 shows an example in which the heat exchanger 800 is provided in the ejector cycle according to the twentieth embodiment. Second
In the ejector cycle according to one embodiment, the heat exchanger 800
This is an example in which is provided.

(Twenty-third Embodiment) In the present embodiment, as shown in FIG.
Control valve 7 provided in the refrigerant passage between
The ejector 400 and the control valves 731 to 733 are integrated by integrating the nozzles 31 to 733 and the nozzle 410.

By the way, since the refrigerant passing through the nozzle 410 is depressurized across the saturated liquid line, the refrigerant enters a gas-liquid two-phase state in the middle of the nozzle 410,
The refrigerant boils near the wall surface of the throat portion 0 (the portion where the cross-sectional area is the smallest in the nozzle 410 (see FIG. 6)). On the other hand, in the central portion distant from the inner wall of the nozzle 410, the refrigerant is difficult to boil, so that it is difficult to atomize the droplets of the refrigerant, which causes a decrease in the ejector efficiency ηe.

On the other hand, the present embodiment and the seventeenth to seventeenth embodiments
In the ninth embodiment, the refrigerant is supplied to the control valves 731 to 733.
The pressure is reduced (squeezed) in the two stages of the nozzle and the nozzle 410, so that the first stage nozzle (in this example, the control valve 73
1 to 733), the refrigerant is once boiled, and the refrigerant is expanded at the inlet of the second stage nozzle (nozzle 410 in this example) to recover the pressure, so that the boiling nuclei are generated. It can be boiled by the stage nozzle 410.

Therefore, the boiling of the refrigerant in the second stage nozzle 410 can be promoted, so that the nozzle 41
The refrigerant can be boiled even in a central portion away from the inner wall of the zero. Consequently, since the droplets of the refrigerant can be atomized, the ejector efficiency ηe can be improved.

(Twenty-fourth Embodiment) In the present embodiment, a heat exchanger (internal heat exchanger) 800 for exchanging heat between the refrigerant flowing out of the radiator 200 and the refrigerant drawn into the compressor 100, the ejector 400, Liquid separator 50
0 and a pressure reducer (throttling means) 600 (an ejector-integrated gas-liquid separator). The detailed structure thereof will be described below with reference to FIGS.

FIG. 40 is a sectional view in the axial direction of the ejector-integrated gas-liquid separator, and FIG.
42 is an axial cross-sectional view seen from a direction shifted by an angle, FIG. 42 is a top view of FIG. 40, FIG. 43 is a cross-sectional view taken along AA of FIG. 40, FIG. 44 is a perspective view of the diffuser 430, FIG. 45A is a perspective view of the heat exchanger 800, and FIG.
(B) is a sectional view of a tube constituting the heat exchanger 800.

The gas-liquid separator 500 is the same as that shown in FIGS.
As shown in FIG. 1, a lower body (tank main body) 551 having a cylindrical shape whose one end is closed and an upper body 552 closing the other end are welded to each other. is fixed to the upper body 552 (upper side) as the refrigerant flowing through the ejector 400 flows vertically toward the lower side in the upper lateral side.

At this time, the diffuser 430 is
As shown at 1, 42 and 45, a trumpet-shaped (horn-shaped) first horn portion 431 and a lower end portion 552 of a lower body 551 are formed so that the cross-sectional area thereof gradually increases downward from the mixing portion 420. and the second horn section 432 that make up the diffuser 4301 together with a part of the side wall portion 553
Is configured.

The second horn section 432 is connected to the side wall section 5.
A substantially cylindrical portion 4 having a predetermined gap of 53 and opposed to each other.
32a, the first horn portion 431, and the curved portion 432b that smoothly connects the cylindrical portion 432a. In the present embodiment, the first horn portion 431 and the second horn 43
2 is integrally formed.

The cylindrical portion 432a has a side wall portion 553.
A positioning projection 433 for positioning the diffuser 430 with respect to the lower body 551 in contact therewith is provided.

The heat exchanger 800 is similar to that shown in FIGS.
As shown in (a), a flat first tube 840 through which a high-pressure refrigerant before being depressurized by the ejector 400 flows.
And a flat second tube 850, through which the low-pressure refrigerant sucked into the compressor 100 flows, being spirally wound in a state where the flat tube is in contact with the flat second tube 850.
850 is a multi-hole tube in which a number of refrigerant passages are formed in one tube, as shown in FIG. 45 (b).

Note that headers 841, 842, 851, 852 communicating with the refrigerant passages in the tubes 840, 850 are joined to both longitudinal ends of the tubes 840, 850, respectively. The headers 842 and 852 collect and collect the refrigerant flowing out of the respective refrigerant passages after completing the heat exchange.

Next, the operation (refrigerant flow) of the ejector-integrated gas-liquid separator according to this embodiment will be described.

The high-temperature and high-pressure refrigerant flowing out of the radiator 200 flows into the gas-liquid separator 500 through the first inlet 554 (see FIGS. 41 and 42), and the header 841, the first tube
8 40 and the communication port 555 in fluid communication in the order of the header 842
Ejector 400 (nozzle 4) via (see FIG. 40)
10).

The ejector 400 (nozzle 41)
0) flows into the evaporator 300 in the mixing section 420.
After the pressure is increased by the diffuser 430 while sucking the refrigerant evaporated in the above, the cylindrical portion 432a and the side wall 5
Through the gap with 53 (a part of the diffuser 430), it flows out above the lower body 551 (upper space in the gas-liquid separator 500). Note that the refrigerant evaporated in the evaporator 300 is sucked into the mixing section 420 from the second inlet 558 (see FIG. 42).

The gas-phase refrigerant (low-pressure side refrigerant) existing above the lower body 551 (the upper space in the gas-liquid separator 500) is disposed below the lower body 551 (in the gas-liquid separator 500). Is sucked into the U-shaped tube 556 from the upper end side opening 556a of the U-shaped U-shaped tube 556 bent in the U-shaped tube and flows into the second tube 850 from the header 851.
After performing heat exchange with the high-pressure side refrigerant (refrigerant flowing in the first tube 840), the refrigerant flows out from the first outlet 557 (see FIG. 41) and is sucked into the compressor 100.

In the lower bent portion of the U-shaped tube 556,
An oil return hole 556b (see FIG. 45) for taking in refrigerating machine oil (lubricating oil) separated from the refrigerant is provided, and the refrigerating machine oil taken in from the oil return hole 556b flows through the second tube 850 together with the low-pressure side refrigerant. And compressor 1
Sucked at 00.

On the other hand, the liquid-phase refrigerant present below the lower body 551 (the lower space in the gas-liquid separator 500)
Suction pipe 55 arranged coaxially with ejector 400
8 is sucked from the lower end side opening 558a of the second outlet 5
From 59 (see FIG. 40), it flows toward the evaporator 300. In addition, the second outlet 559 extends from the lower end side opening 558a.
By generating a predetermined pressure loss in the refrigerant passage leading to, a pressure reducing device (throttling means) 600 is configured.

Next, the features of this embodiment will be described.

In the present embodiment, a part of the diffuser 430 is constituted by a part of the gas-liquid separator 500 (a part of the lower end 552 of the lower body 551 and a part of the side wall 553). Compared to the case where the diffuser 430 is constituted by only one horn portion 431), the diffuser 430 having a sufficiently large refrigerant passage can be constituted.

Further, the diffuser 43 having a sufficiently large refrigerant passage utilizing the space in the gas-liquid separator 500 is used.
Since 0 is configured, it is possible to improve the performance of the ejector 400, reduce the pace for mounting the ejector 400, and improve the installation (mounting) of the ejector cycle.

(Twenty-fifth Embodiment) The present embodiment also relates to a gas-liquid separator integrated with an ejector. Specifically, as shown in FIG. 46, the ejector 400 is disposed in the gas-liquid separator 500 to the refrigerant flowing in the ejector 400 flows vertically toward the lower side in the upper lateral side At the same time, on the downstream side of the refrigerant flow from the refrigerant outlet of the diffuser 430 (the part where the cross-sectional area of the refrigerant passage is the largest), the flow direction of the refrigerant is turned by about 180 degrees from the downward direction to the upward direction. is there.

Accordingly, it is possible to concentrate the inlet and outlet of the refrigerant on the upper side of the gas-liquid separator 500 while minimizing the pressure loss in the ejector 400 (in particular, the diffuser 430).

Incidentally, reference numeral 560 denotes a gas-phase refrigerant (low-pressure side refrigerant) which is bent in a U-shape in the lower space in the gas-liquid separator 500 and exists in the upper space in the gas-liquid separator 500. A pipe 570 is a suction pipe for sucking a liquid-phase refrigerant existing in a lower space in the gas-liquid separator 500, and a refrigerating machine oil is provided at a bent portion at a lower end side of the U-shaped pipe 560. An oil return hole 561 for taking in oil is formed.

(Other Embodiments) In the above embodiment, carbon dioxide is used as the refrigerant. However, the present invention is not limited to this.
It may be ethane, nitric oxide or the like.

Further, decompressors 710 and 720 may be provided on both sides of the refrigerant flow upstream and downstream of the ejector 400.

The first pressure reducer 600 may be omitted by providing an appropriate pressure loss in the refrigerant passage itself.

In the first to third embodiments, the first to third decompressors 600, 710, and 720 are constituted by fixed apertures or capillary tubes having fixed openings, but the present invention is not limited to this. Instead, a variable opening valve that can variably control the opening may be used.

[0249] In the second embodiment, the second decompressor 710 is a variable opening valve, and when the refrigerant pressure after being raised by the ejector 400 is lower than the critical pressure, the valve opening is increased. When the pressure loss is reduced and the refrigerant pressure after being boosted by the ejector 400 is equal to or higher than the critical pressure, the valve opening may be adjusted so that the refrigerant pressure at the inlet of the gas-liquid separator 500 is lower than the critical pressure. For example, similarly to the third embodiment, it is possible to prevent the flow resistance (pressure loss) of the refrigerant from increasing while adjusting the refrigerant pressure after being boosted by the ejector 400 so as to be surely lower than the critical pressure. .

In the first to third embodiments, the second, third
Although the pressure of the refrigerant after being pressurized by the ejector 400 in the pressure reducers 710 and 720 is reduced to a pressure lower than the critical pressure (gas-liquid two-phase region), the present invention is not limited to this. By adjusting the flow rate of the refrigerant discharged from the compressor by means such as adjusting the rotational speed or the theoretical discharge amount of the compressor, the refrigerant pressure after being boosted by the ejector 400 is lower than the critical pressure (gas-liquid two-phase region). You may comprise the pressure adjustment means which adjusts to pressure reduction.

Also, in the fourth to sixth embodiments, the mixing section 42
The liquid refrigerant was separated and extracted near the outlet of 0.
The present invention is not limited to this.
During the pressure increase of 00 (between the entrance of the mixing unit 420 and the exit of the diffuser 430), the pressure may be anywhere.

In the ninth to sixteenth embodiments, the ejector cycle according to the present invention is applied to a water heater, but the present invention is not limited to this, and can be applied to, for example, an air conditioner. .

In the ninth to sixteenth embodiments, the flow rate of the refrigerant discharged from the compressor 100 is controlled by the electric motor Mo. However, the present invention is not limited to this, and the variable displacement type compressor is not limited to this. May control the flow rate of the refrigerant discharged from the compressor 100.

In the ninth to sixteenth embodiments, the compressor 1
Although the flow rate of the refrigerant discharged from 00 is controlled, the present invention is not limited to this. For example, the flow rate of the refrigerant discharged from the compressor (the number of revolutions of the compressor) may be a constant value.

Also, the present invention is limited to only the above-described embodiments, and may be a combination of at least two of the first to sixteenth embodiments.

Further, in the above-described embodiment, the ejector 4
00 shape (inlet diameter of nozzle 410, throat diameter of nozzle 410, outlet diameter of nozzle 410, diameter of mixing section 420,
The dimensions of the ejector such as the dimension from the nozzle inlet to the nozzle throat, the dimension from the nozzle throat to the nozzle outlet, the length of the mixing section 420, and the spread angle of the diffuser 430) are fixed. Is not limited to this, and the shape of the ejector 400 may be changed according to the operation state of the cycle. Thus, the cycle can be operated while maintaining high ejector efficiency regardless of the operating state of the ejector cycle.

Further, the definition formula of the ejector efficiency ηe is not limited to the above formula 1, but may be any formula that accurately indicates the energy conversion efficiency when converting expansion energy into pressure energy.

In the gas-liquid separators according to the sixth and seventh embodiments and the ejector cycles according to the eighth to twenty-fifth embodiments, the high pressure side using carbon dioxide as the refrigerant is equal to or higher than the critical pressure of the refrigerant. However, these embodiments are not limited to this, and can be applied to those in which the high pressure side pressure is lower than the critical pressure of the refrigerant.

In the above embodiment, the mixing section 420
And the diffuser 430 are clearly distinguished, but the present invention is not limited to this, and the functions of the mixing unit 420 and the function of the diffuser 430 are not clearly distinguished from the mixing unit 420 and the diffuser 430. The ejector 400 may be configured by the boosting unit having the combination of the above and the nozzle 410.

In the above embodiment, the nozzle 410
Although the (ejector 400) is a one-stage throttle, the present invention is not limited to this, and the nozzle 410 (the ejector 400) may have a multi-stage throttle structure.

[Brief description of the drawings]

FIG. 1 is a schematic diagram of an ejector cycle according to a first embodiment of the present invention.

FIG. 2 is a ph (Mollier) diagram of an ejector cycle according to the first embodiment of the present invention.

FIG. 3 is a graph showing the relationship between the high-pressure side pressure, the coefficient of performance, and the cooling capacity in the ejector cycle according to the first embodiment of the present invention.

FIG. 4 is a schematic view of an ejector cycle according to a second embodiment of the present invention.

FIG. 5 is a schematic view of an ejector cycle according to a third embodiment of the present invention.

FIG. 6 is an enlarged schematic view of an ejector and a gas-liquid separator of an ejector cycle according to a fourth embodiment of the present invention.

FIG. 7A is a graph showing a relationship between an ejector efficiency ηe and a refrigerating capacity Qe generated in an evaporator, and FIG. 7B is a graph showing an ejector efficiency ηe, a suction pressure increase ΔP of a compressor, and an evaporator refrigerant inlet. (C) is a graph showing the relationship between the specific enthalpy difference Δh between the outlet side and the outlet side, and (c) shows the ejector efficiency ηe, the mass flow rate Gr of the refrigerant drawn into the compressor, and the mass flow rate Ge of the refrigerant flowing through the evaporator. 6 is a graph showing a relationship with the graph.

FIG. 8 is a ph (Mollier) diagram of an ejector cycle according to a fourth embodiment of the present invention.

FIG. 9 is a three-dimensional characteristic diagram showing a relationship between a position in a radial direction with respect to a center portion of a cross section of a refrigerant passage of an ejector and a flow velocity of the refrigerant from a refrigerant outlet of a nozzle to a refrigerant outlet of a diffuser.

FIG. 10 is an enlarged schematic view of an ejector and a gas-liquid separator of an ejector cycle according to a fifth embodiment of the present invention.

FIG. 11 is a graph showing a relationship between a position in a radial direction based on a center portion of a cross section of a refrigerant passage of an ejector and a ratio (liquid volume ratio) of a liquid-phase refrigerant in the refrigerant.

FIG. 12 is an enlarged schematic view of an ejector and a gas-liquid separator of an ejector cycle according to a sixth embodiment of the present invention.

FIG. 13 is a schematic diagram of a gas-liquid separator applied to an ejector cycle according to a seventh embodiment of the present invention.

FIG. 14 is an explanatory diagram for explaining features of a gas-liquid separator applied to an ejector cycle according to a seventh embodiment of the present invention.

FIG. 15 is a schematic diagram of a gas-liquid separator applied to an ejector cycle according to an eighth embodiment of the present invention.

16 is a sectional view taken along line AA of FIG.

FIG. 17 is a schematic view of an ejector cycle according to a ninth embodiment of the present invention.

FIG. 18 is a graph showing the relationship between ejector efficiency and flow ratio.

FIG. 19 is a schematic view of an ejector cycle according to a tenth embodiment of the present invention.

FIG. 20 is a schematic diagram of an ejector cycle according to an eleventh embodiment of the present invention.

FIG. 21 is a schematic view of an ejector cycle according to a twelfth embodiment of the present invention.

FIG. 22 is a schematic view of an ejector cycle according to a thirteenth embodiment of the present invention.

FIG. 23 is a schematic view of an ejector cycle according to a fourteenth embodiment of the present invention.

FIG. 24 is a schematic view of an ejector cycle according to a fifteenth embodiment of the present invention.

FIG. 25 is a schematic view of an ejector cycle according to a sixteenth embodiment of the present invention.

FIG. 26 is a schematic view according to a modification of the ejector cycle according to the sixteenth embodiment of the present invention.

FIG. 27 is a schematic view of an ejector cycle according to a seventeenth embodiment of the present invention.

FIG. 28 is a graph showing the relationship between the degree of heating and the flow rate ratio α, the pressure increase ΔP in the ejector 400, and the ejector efficiency ηe.

FIG. 29 is a schematic view of an ejector cycle according to an eighteenth embodiment of the present invention.

FIG. 30 is a graph showing the relationship between the high-pressure side pressure and the flow rate ratio α, the pressure increase ΔP in the ejector 400, and the ejector efficiency ηe.

FIG. 31 is a schematic view of an ejector cycle according to a nineteenth embodiment of the present invention.

FIG. 32 is a schematic view of an ejector cycle according to a twentieth embodiment of the present invention.

FIG. 33 is a schematic view of an ejector cycle according to a twenty-first embodiment of the present invention.

FIG. 34 is a schematic view of an ejector cycle according to a twenty-second embodiment of the present invention.

FIG. 35 is a schematic view according to a modification of the ejector cycle according to the twenty-second embodiment of the present invention.

FIG. 36 is a schematic view according to a modification of the ejector cycle according to the twenty-second embodiment of the present invention.

FIG. 37 is a schematic view according to a modification of the ejector cycle according to the twenty-second embodiment of the present invention.

FIG. 38 is a schematic view according to a modification of the ejector cycle according to the twenty-second embodiment of the present invention.

FIG. 39 is an enlarged schematic diagram of an ejector applied to an ejector cycle according to a twenty-third embodiment of the present invention.

FIG. 40 is an axial sectional view of an ejector-integrated gas-liquid separator according to a twenty-fourth embodiment of the present invention.

FIG. 41 is an axial cross-sectional view seen from a direction shifted by approximately 90 degrees from FIG. 40;

FIG. 42 is a top view of FIG. 40.

FIG. 43 is a sectional view taken along line AA of FIG. 40;

FIG. 44 is a perspective view of a diffuser 430.

FIG. 45 (a) is a perspective view of a heat exchanger, and FIG. 45 (b) is a cross-sectional view of a tube constituting the heat exchanger.

FIG. 46 is an axial sectional view of an ejector-integrated gas-liquid separator according to a twenty-fifth embodiment of the present invention.

[Description of Signs] 100: compressor, 200: radiator, 300: evaporator, 4
00: ejector, 500: gas-liquid separator, 600: decompressor.

Continued on the front page (31) Priority claim number Japanese Patent Application 2001-40496 (P2001-40496) (32) Priority date February 16, 2001 (2001.2.16) (33) Priority claim country Japan (JP) ) Application for accelerated examination (72) Inventor Kunio Iriya 1-1-1, Showa-cho, Kariya-shi, Aichi Pref., Japan (72) Inventor Tetsu Nomura 1-1-1, Showa-cho, Kariya-shi, Aichi pref. Inventor Hisasuke Sakakibara 1-1-1, Showa-cho, Kariya-shi, Aichi Pref., Within DENSO Corporation (72) Inventor Makoto Ikegami 1-1-1, Showa-cho, Kariya-shi, Aichi pref. 1-1-1 Showa-cho, Denshi Co., Ltd. (72) Inventor Koji Yamanaka 1-1-1, Showa-cho, Kariya City, Aichi Prefecture (56) References JP-A-6-11197 (JP, A) JP-A-4-316962 (JP, A) JP-A-10-205898 (JP, A) JP-A-10-54617 (JP, A) JP-A 5-26522 (JP, A) JitsuHiraku Akira 57-77875 (JP, U) patent 2518776 (JP, B2) patent 2548962 (JP, B2) (58 ) investigated the field (Int.Cl. ^7, DB name) F25B 1/00 F24H 1/00 611 F25B 30/02 F25B 41/04 F25B 43/00

Claims (48)

(57) [Claims] 1. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. and ejector (400) to increase the suction pressure of the compressor (100), together with storing refrigerant by separating the gas-liquid two-phase refrigerant into a gas-phase refrigerant and liquid-phase refrigerant from the ejector (400), the gas phase
A refrigerant is supplied to the suction side of the compressor (100),
A gas-liquid separator (50 ) for supplying a medium to the evaporator (300)
0), wherein the pressure of the refrigerant before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more, and the pressure of the refrigerant after the pressure is reduced is reduced to the critical pressure of the refrigerant or less. Ejector cycle. 2. A compressor (100) for sucking and compressing a refrigerant to raise the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. and ejector (400) to increase the suction pressure of the compressor (100), together with storing refrigerant by separating the gas-liquid two-phase refrigerant into a gas-phase refrigerant and liquid-phase refrigerant from the ejector (400), the gas phase
A refrigerant is supplied to the suction side of the compressor (100),
A gas-liquid separator (50 ) for supplying a medium to the evaporator (300)
0), provided in the gas-liquid separator, an oil return hole for guiding oil in the gas-liquid separator to the compressor (100), before the pressure is reduced by the ejector (400). An ejector cycle characterized in that the refrigerant pressure of the refrigerant is increased above the critical pressure of the refrigerant, and the refrigerant pressure after the pressure is reduced is reduced to the critical pressure of the refrigerant. 3. A pressure adjusting means (710, 720) for adjusting the pressure of the refrigerant pressurized by the ejector (400) to less than a critical pressure is provided. Ejector cycle. 4. A pressure adjusting means (7) for adjusting the pressure of the refrigerant pressurized by said ejector (400) to a gas-liquid two-phase region.
The ejector cycle according to claim 1, wherein an ejector cycle is provided. 5. The gas-liquid separator (500) separates the refrigerant flowing out of the ejector (400) into gas and liquid, and the pressure adjusting means (710, 720) further comprises: The ejector cycle according to claim 3, wherein the ejector cycle is provided further upstream of the refrigerant flow. 6. The gas-liquid separator (500) separates the refrigerant flowing from the ejector (400) into gas and liquid, and the pressure adjusting means (710, 720) controls the refrigerant from the ejector (400). The ejector cycle according to claim 3, wherein the ejector cycle is provided downstream of the flow. 7. A compressor (100) for suctioning and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100), and a substantially central portion of a cross section of a refrigerant passage of the ejector (400);
Installed in the section and flows out of the ejector (400)
Liquid phase refrigerant is extracted from the previous refrigerant, and the separated and extracted liquid phase
A refrigerant is supplied to the evaporator (300) side and
From the refrigerant before flowing out of the ejector ( 400)
The refrigerant is extracted, and the separated and extracted gas-phase refrigerant is supplied to the compressor.
A gas-liquid separator (500) for supplying to the suction side of (100);
And a refrigerant pressure before the pressure is reduced by the ejector (400).
And depressurized to above the critical pressure of the refrigerant
An ejector cycle characterized in that the pressure of the subsequent refrigerant is reduced to a value lower than the critical pressure of the refrigerant . 8. A compressor (100) for sucking and compressing a refrigerant to raise the pressure to a supercritical pressure, a radiator (200) for cooling a refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing a suction pressure of the compressor (100); and first and second gas-liquid separators (500, 510) for separating a refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. The pressure of the refrigerant before the pressure is reduced in (400) is increased to the critical pressure of the refrigerant or more, and the pressure of the refrigerant after the pressure is reduced is reduced to or less than the critical pressure of the refrigerant. The first gas-liquid separator (500) Previous Note ejector (4
00) is separated and extracted from the refrigerant before flowing out of the evaporator (300).
And the second gas-liquid separator (510) separates the refrigerant flowing out of the ejector (400) into a gas-phase refrigerant and a liquid-phase refrigerant, and evaporates the separated liquid-phase refrigerant. Container (30
An ejector cycle, wherein the ejector cycle is supplied to the 0) side. 9. The ejector (400) includes: a nozzle (410) that converts pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to decompress and expand the refrigerant; and a nozzle (410). A pressure booster (420, 430) configured to convert velocity energy into pressure energy and increase the pressure of the refrigerant while mixing the refrigerant to be injected and the refrigerant sucked from the evaporator (300). The ejector cycle according to claim 8, wherein the first gas-liquid separator (500) further separates and extracts a liquid-phase refrigerant in the booster (420, 430). 10. The liquid-phase refrigerant according to claim 8, wherein the first gas-liquid separator (500) separates and extracts a liquid-phase refrigerant at a substantially central portion of a cross-section of a refrigerant passage of the ejector (400). Ejector cycle as described. 11. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling a refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0), and heating means (800, 810, 820, 830) for heating the refrigerant drawn into the compressor (100) , and the refrigerant pressure before the pressure is reduced by the ejector (400) An ejector cycle characterized in that the pressure is raised to a value higher than a critical pressure. 12. The heating means (800) includes a refrigerant flowing out of the radiator (200) and the compressor (100).
The ejector cycle according to claim 11, wherein the ejector cycle exchanges heat with a refrigerant sucked into the ejector. 13. The heating means ( 810 ) exchanges heat between a drive source (Mo) for driving the compressor (100) and a refrigerant sucked into the compressor (100). The ejector cycle according to claim 11 , wherein 14. A compressor (100) for sucking and compressing a refrigerant to raise the pressure to a supercritical pressure, a radiator (200) for cooling a refrigerant discharged from the compressor (100), and a heat absorbing device for evaporating the refrigerant to absorb heat. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0), an oil return hole installed in the gas-liquid separator for guiding oil in the gas-liquid separator to the compressor (100), and an evaporator from the gas-liquid separator (500). (300)
An ejector efficiency control unit (730) for controlling the energy conversion efficiency of the ejector (400) by adjusting the flow rate of the supplied liquid-phase refrigerant , wherein the refrigerant before being depressurized by the ejector (400) is provided. An ejector cycle characterized in that the pressure is increased to a value higher than the critical pressure of the refrigerant. 15. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0), an oil return hole installed in the gas-liquid separator for guiding oil in the gas-liquid separator to the compressor (100), and a flow rate of a refrigerant discharged from the compressor (100). Adjust
A flow rate adjusting means (Mo) for adjusting the flow rate of refrigerant flowing into the ejector (400) by Rukoto, the evaporator from the gas-liquid separator (500) to (300)
An ejector efficiency control unit (730) for controlling the energy conversion efficiency of the ejector (400) by adjusting the flow rate of the supplied liquid-phase refrigerant , wherein the refrigerant before being depressurized by the ejector (400) is provided. An ejector cycle characterized in that the pressure is increased to a value higher than the critical pressure of the refrigerant. 16. A refrigerant is sucked and compressed to rise to a supercritical pressure.
Compressor (100) for compressing , and heat radiation for cooling the refrigerant discharged from the compressor (100)
Device (200), an evaporator (300) that evaporates the refrigerant and absorbs heat, and decompresses and expands the refrigerant flowing out of the radiator (200).
To suck the vapor-phase refrigerant evaporated in the evaporator (300).
As well as converting expansion energy into pressure energy.
To increase the suction pressure of the compressor (100)
Motor (400) and a gas phase cooling gas-liquid two phase refrigerant from the ejector (400)
Medium and liquid-phase refrigerant, and store the refrigerant.
A refrigerant is supplied to the suction side of the compressor (100),
A gas-liquid separator (50) for supplying a medium to the evaporator (300)
0) and the flow rate of the refrigerant discharged from the compressor (100) is adjusted.
Refrigerant flowing into the ejector (400)
A flow rate adjusting means (Mo) for adjusting a flow rate, and a refrigerant pressure before the pressure is reduced by the ejector (400).
Is raised above the critical pressure of the refrigerant
Ejector cycle. 17. The ejector efficiency control means (73)
0) from the gas-liquid separator (500) to the evaporator (3).
By adjusting the flow rate of the liquid-phase refrigerant supplied to the
Ejector cycle according to claim 14 or 15, characterized in that to control the conversion efficiency of the energy by controlling the boosting amount of the refrigerant in the ejector (400) Ri. 18. A refrigerant is sucked and compressed to rise to a supercritical pressure.
A compressor (1 00) to pressure, cooling the refrigerant discharged from the compressor (100) heat dissipation
Device (200), an evaporator (300) that evaporates the refrigerant and absorbs heat, and decompresses and expands the refrigerant flowing out of the radiator (200).
To suck the vapor-phase refrigerant evaporated in the evaporator (300).
As well as converting expansion energy into pressure energy.
To increase the suction pressure of the compressor (100)
Motor (400) and a gas phase cold gas-liquid two-phase refrigerant from the ejector (400)
Medium and liquid-phase refrigerant, and store the refrigerant.
A refrigerant is supplied to the suction side of the compressor (100),
A gas-liquid separator (50) for supplying a medium to the evaporator (300)
0), which is installed in the gas-liquid separator, and
Oil return hole for guiding oil to the compressor (100)
And supply from the radiator (300) to the ejector (400)
The ejector by adjusting the flow rate of the refrigerant
To control energy conversion efficiency in (400)
Ejector efficiency control means (730), and the refrigerant pressure before the pressure is reduced by the ejector (400).
The ejector (400) converts the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to decompress and expand the refrigerant, and the ejector (400); A pressure booster (420, 430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300); Is composed
An ejector cycle characterized by: 19. The ejector efficiency control means (73)
0) from the gas-liquid separator (500) to the evaporator (3).
By adjusting the flow rate of the liquid-phase refrigerant supplied to the
Ri wherein adjusting the amount of pressure reduction of the refrigerant before flowing into the evaporator (300), an ejector cycle according to claim 14 or 15, characterized in that to control the conversion efficiency of energy. 20. The ejector efficiency control means (73)
0) from the gas-liquid separator (500) to the evaporator (3).
By adjusting the flow rate of the liquid-phase refrigerant supplied to the
Ri controlling the temperature of the evaporator (300) in claim 14 or 1, characterized in that to control the conversion efficiency of the energy
6. The ejector cycle according to 5 . 21. The ejector efficiency control means (73)
0) from the gas-liquid separator (500) to the evaporator (3).
By adjusting the flow rate of the liquid-phase refrigerant supplied to the
Ri to adjust the pressure of the evaporator (300) in claim 14 or 1, characterized in that to control the conversion efficiency of the energy
6. The ejector cycle according to 5 . 22. The ejector efficiency control means (73)
0) from the gas-liquid separator (500) to the evaporator (3).
By adjusting the flow rate of the liquid-phase refrigerant supplied to the
Claims Ri said adjusting the ratio between the radiator (200) flow rate of refrigerant flowing through the refrigerant flow rate (Gn) and the evaporator for circulation (300) and (Ge), and controlling the conversion efficiency of the energy Item 18. An ejector cycle according to item 14 or 15 . 23. A refrigerant is sucked and compressed to rise to a supercritical pressure.
Compressor (100) for compressing , and heat radiation for cooling the refrigerant discharged from the compressor (100)
Device (200), an evaporator (300) that evaporates the refrigerant and absorbs heat, and decompresses and expands the refrigerant flowing out of the radiator (200).
To suck the vapor-phase refrigerant evaporated in the evaporator (300).
As well as converting expansion energy into pressure energy.
To increase the suction pressure of the compressor (100)
Motor (400) and a gas phase cold gas-liquid two-phase refrigerant from the ejector (400)
Medium and liquid-phase refrigerant, and store the refrigerant.
A refrigerant is supplied to the suction side of the compressor (100),
A gas-liquid separator (50) for supplying a medium to the evaporator (300)
0), which is installed in the gas-liquid separator, and
Oil return hole for guiding oil to the compressor (100)
And supply from the radiator (300) to the ejector (400)
The ejector by adjusting the flow rate of the refrigerant
To control energy conversion efficiency in (400)
Ejector efficiency control means (730), and the refrigerant pressure before the pressure is reduced by the ejector (400).
Is raised above the critical pressure of the refrigerant
Ejector cycle. The hot water is heated by exchanging heat between the high-pressure side refrigerant and the hot water in the radiator (200) of the ejector cycle according to any one of claims 1 to 23. Water heater to do. 25. The radiator (200) of the ejector cycle according to any one of claims 14 to 16, wherein the high-pressure side refrigerant and the hot water are heat-exchanged to heat the hot water. The water heater, wherein the efficiency control means (730) controls the energy conversion efficiency by adjusting the temperature of the hot water after the heat exchange. 26. The radiator (200) of the ejector cycle according to any one of claims 14 to 16, wherein heat exchange is performed between the high-pressure side refrigerant and the hot water to heat the hot water. The water heater, wherein the efficiency control means (730) controls the energy conversion efficiency by adjusting the difference between the temperature of the refrigerant flowing through the radiator (200) and the temperature of the hot water. 27. The radiator (200) of the ejector cycle according to any one of claims 14 to 16, wherein heat exchange is performed between the high-pressure side refrigerant and the hot water to heat the hot water. A water heater, wherein the efficiency control means (730) controls energy conversion efficiency by adjusting a flow rate of hot water for heat exchange with the high-pressure refrigerant. 28. The water heater according to claim 24, wherein a plurality of the evaporators (300) are provided, and the plurality of evaporators (300) are provided. A heat management system characterized by performing indoor air conditioning. 29. A refrigerant which has a hot water storage tank (750) for keeping heated hot water hot and stores therein, and a refrigerant drawn into the compressor (100) by the hot water stored in the hot water storage tank (750). The heat management system according to claim 28, wherein the heat is heated. 30. The evaporator (30 ), wherein the refrigerant is expanded under reduced pressure.
Sucks the gas-phase refrigerant evaporated at 0), the compressor by converting expansion energy into pressure energy (100)
Has an ejector that increases the suction pressure (400), and the refrigerant pressure before being decompressed by the ejector (400) is applied to an ejector cycle is increased to above the critical pressure of the refrigerant, the ejector (400) A gas-liquid two-phase refrigerant from the compressor into a gas-phase refrigerant and a liquid-phase refrigerant, and a tank (540) for storing the separated liquid-phase refrigerant.
And supplying the liquid-phase refrigerant to the evaporator.
A gas-liquid separator (500 ) to be supplied to the (300) , wherein a refrigerant flowing in the ejector (400) flows from a lower side to an upper side in the tank section (540), and The ejector (400) such that the refrigerant outlet (431) of the ejector (400) is located above the refrigerant liquid level in the tank (540).
A gas-liquid separator, wherein the gas-liquid separator is incorporated in the tank section (540). 31. The ejector (400), wherein a refrigerant flowing inside the ejector (400) is configured to flow vertically from a lower side to an upper side.
The gas-liquid separator according to 0. 32. A collision wall (541) is provided on the refrigerant outlet (431) side of the ejector (400) to impinge the refrigerant flowing from the refrigerant outlet (431). The gas-liquid separator according to claim 30. 33. Evaporator (30 ) by expanding the refrigerant under reduced pressure.
Sucks the gas-phase refrigerant evaporated at 0), the compressor by converting expansion energy into pressure energy (100)
Has an ejector that increases the suction pressure (400), and the refrigerant pressure before being decompressed by the ejector (400) is applied to an ejector cycle is increased to above the critical pressure of the refrigerant, the ejector (400) A gas-liquid two-phase refrigerant from the compressor into a gas-phase refrigerant and a liquid-phase refrigerant, and a tank (540) for storing the separated liquid-phase refrigerant.
And supplying the liquid-phase refrigerant to the evaporator.
A gas-liquid separator (500) for supplying to the (300) , wherein a refrigerant outlet (431) of the ejector (400) is located above a refrigerant liquid level in the tank (540), and A gas-liquid separator characterized in that the ejector (400) is incorporated in the tank (540) such that the refrigerant ejected from the refrigerant outlet (431) collides with the inner wall of the tank (540). . 34. The gas-liquid separator according to claim 33, wherein the refrigerant is ejected in a substantially horizontal direction from a refrigerant outlet portion (431) of the ejector (400). 35. The ejector (400), comprising: a nozzle (410) that converts pressure energy of a high-pressure refrigerant flowing out of the radiator (200) into velocity energy to accelerate the pressure of the refrigerant; and a nozzle (410). A mixing section (420) for mixing with a high-speed refrigerant flow to be injected and a vapor-phase refrigerant sucked by the refrigerant flow and evaporating in the evaporator (300); a refrigerant injected from the nozzle (410); And a diffuser (430) for increasing the pressure of the refrigerant by converting velocity energy into pressure energy while mixing the refrigerant with the refrigerant sucked from the device (300). 35. Any of claims 30 to 34, wherein at least the nozzle (410) is located outside the tank part (540). Gas-liquid separator according to One. 36. A throttling means (60) for reducing the pressure of the liquid-phase refrigerant flowing out from the outlet of the liquid-phase refrigerant connected to the evaporator (300) in the tank section (540).
The gas-liquid separator according to any one of claims 30 to 35, wherein 0) is provided. 37. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. An evaporator (300), a nozzle (410) for converting pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to decompress and expand the refrigerant, and a refrigerant injected from the nozzle (410). A booster (420, 43) for converting velocity energy into pressure energy while increasing the pressure of the refrigerant while mixing the refrigerant sucked from the evaporator (300).
0), the gas-liquid two-phase refrigerant from the ejector (400) is separated into a gas-phase refrigerant and a liquid-phase refrigerant, and the refrigerant is stored. And a gas-liquid separator (50) for supplying the liquid-phase refrigerant to the evaporator (300).
0), the refrigerant pressure before being depressurized by the ejector (400) is increased to the critical pressure of the refrigerant or more, and the shape of the ejector (400) is changed according to the operation state of the cycle. An ejector cycle characterized by: 38. A compressor (100) for sucking and compressing a refrigerant to raise the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0), a control valve provided in a refrigerant passage between the radiator (200) and the ejector (400), and changing an opening degree based on a refrigerant heating degree at a refrigerant outlet side of the evaporator (300). (731), wherein the refrigerant pressure before being reduced in pressure by the ejector (400) is increased to a critical pressure of the refrigerant or higher. 39. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0), a control provided in a refrigerant passage between the radiator (200) and the ejector (400), and controlling the high-pressure side pressure based on the refrigerant temperature before the pressure is reduced by the ejector (400). An ejector cycle, comprising: a valve (732), wherein the refrigerant pressure before being reduced by the ejector (400) is increased to a critical pressure of the refrigerant or higher. 40. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0) and a control valve (733) provided in a refrigerant passage between the radiator (200) and the ejector (400), and changing an opening degree based on a pressure in the evaporator (300). An ejector cycle comprising: increasing a refrigerant pressure before the pressure is reduced by the ejector (400) to a critical pressure of the refrigerant or higher. 41. The ejector cycle according to claim 37, wherein the control valve (731 to 733) and the ejector (400) are integrated. 42. The ejector (400) converts a pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to decompress and expand the refrigerant, and a nozzle (410). A pressure booster (420, 430) configured to convert the velocity energy into pressure energy to increase the pressure of the refrigerant while mixing the refrigerant to be injected and the refrigerant sucked from the evaporator (300); The control valve (731-733) and the nozzle (410)
The ejector cycle according to any one of claims 38 to 40, wherein the ejector cycle is integrated with the ejector cycle. 43. A compressor (100) for sucking and compressing a refrigerant to raise the pressure to a supercritical pressure; a radiator (200) for cooling the refrigerant discharged from the compressor (100); Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0) is provided in a refrigerant passage between the gas-liquid separator (500) and the evaporator (300), and changes an opening degree based on a refrigerant heating degree at a refrigerant outlet side of the evaporator (300). An ejector cycle comprising: a control valve (731) for increasing the refrigerant pressure before the pressure is reduced by the ejector (400) to a critical pressure of the refrigerant or higher. 44. A compressor (100) for sucking and compressing a refrigerant to increase the pressure to a supercritical pressure, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and heat absorption by evaporating the refrigerant. Evaporator (300), and a refrigerant flowing out of the radiator (200) is decompressed and expanded to suck the vapor-phase refrigerant evaporated in the evaporator (300) and to convert expansion energy into pressure energy. An ejector (400) for increasing the suction pressure of the compressor (100); a gas-liquid two-phase refrigerant from the ejector (400) being separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant; A gas-liquid separator (50) that supplies a refrigerant to the suction side of the compressor (100) and supplies a liquid-phase refrigerant to the evaporator (300).
0), a control valve (733) that is provided in a refrigerant passage between the gas-liquid separator (500) and the evaporator (300), and that changes the opening degree based on the pressure in the evaporator (300). ), Wherein the refrigerant pressure before the pressure is reduced by the ejector (400) is increased to the critical pressure of the refrigerant or more. 45. A heat exchanger (800) for exchanging heat between the refrigerant drawn into the compressor (100) and the refrigerant at the outlet of the radiator (200).
The ejector cycle according to any one of Items 8 to 44. 46. An ejector (400) for decompressing and expanding the refrigerant to suck the gas-phase refrigerant evaporated in the evaporator, and for converting the expansion energy into pressure energy to increase the suction pressure of the compressor, And the ejector (4
00) is applied to an ejector cycle in which the refrigerant pressure before the pressure is reduced to the critical pressure of the refrigerant or more, and the gas-liquid two-phase refrigerant from the ejector (400) is separated into a gas-phase refrigerant and a liquid-phase refrigerant. The liquid-phase refrigerant into the tank (55
1) and the gas-phase refrigerant is stored in the compressor (10).
0) and supplies the liquid-phase refrigerant to the evaporator (30).
A 0) for supplying the gas-liquid separator (500), in said tank (551), such refrigerant flowing through the ejector 400 in the flows toward the lower side in the upper lateral side The ejector (400) is arranged and a part (552, 5 ) of the tank part (551) is arranged.
53) is a diffuser (4) of the ejector (400).
30. A gas-liquid separator characterized by constituting a part of 30). A diffuser (430) as claimed in claim 47, wherein the ejector (400), and wherein the protrusions for positioning the diffuser (430) in contact with said tank portion (511) of (433) is provided Claim 4
7. The gas-liquid separator according to 6. 48. An ejector (400) for decompressing and expanding the refrigerant to suck the gas-phase refrigerant evaporated in the evaporator, and for converting the expansion energy into pressure energy to increase the suction pressure of the compressor, And the ejector (4
00) is applied to an ejector cycle in which the refrigerant pressure before the pressure is reduced to the critical pressure of the refrigerant or more, and the gas-liquid two-phase refrigerant from the ejector (400) is separated into a gas-phase refrigerant and a liquid-phase refrigerant. To store the liquid-phase refrigerant in the tank
At the same time, the gas-phase refrigerant is supplied to the suction side of the compressor (100).
Supplied to a liquid-phase refrigerant the evaporator (300) to supply the gas-liquid separator (500), in the tank portion, wherein the ejector (400) in the lower side in the refrigerant from the upper side in the flowing The ejector (400) is arranged so as to circulate toward the outlet, and the refrigerant flows from the refrigerant outlet of the diffuser (430) of the ejector (400) downstream of the refrigerant outlet from the downward direction to the upward direction. gas-liquid separator which is characterized by being configured to deflect in a direction towards the side.