JP2003014318A - Ejector cycle - Google Patents

Abstract

PROBLEM TO BE SOLVED: To keep a high ejector efficiency irrespective of the flow rate and the kind of a refrigerant. SOLUTION: The ratio (D2/D1) of an equivalent diameter D2 of a mixing section 420 to an equivalent diameter D1 of a nozzle 410 is set to 1.05-10. Then, an ejector cycle can be operated while keeping a high ejector efficiency.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an ejector cycle.

[0002]

2. Description of the Related Art An ejector cycle is, for example, as described in Japanese Patent Laid-Open No. 149652/1993, in which a refrigerant is decompressed and expanded to suck a vapor phase refrigerant evaporated in an evaporator. , A refrigeration cycle having an ejector for converting expansion energy into pressure energy to increase suction pressure of a compressor.

Therefore, the refrigerant is expanded under reduced pressure to suck the vapor phase refrigerant evaporated in the evaporator, and the expansion energy is converted into pressure energy. However, if the ejector efficiency ηe is low, the efficiency of the refrigeration cycle is reduced. Becomes worse. The ejector efficiency ηe is defined by Equation 1 described later.

Incidentally, in JP-A-57-129360, the diameter of the mixing portion of the ejector is set to 3 to 7 mm, the length of the mixing portion is set to 8 to 12 times the diameter of the mixing portion, and the spread angle of the diffuser is set to 4 ° to 4. Although it is set to 6 ° and the length of the diffuser is set to 10 to 14 times that of the mixing portion, the inventors did not obtain sufficient performance (ejector efficiency ηe) according to the test and examination.

In view of the above points, the present invention has an object to improve ejector efficiency.

[0006]

In order to achieve the above-mentioned object, the present invention provides a compressor (100) for sucking and compressing a refrigerant and a compressor (100) for discharging the refrigerant. A radiator (200) that cools the refrigerant, an evaporator (300) that evaporates the refrigerant to exert a refrigerating capacity, and the pressure energy of the high-pressure refrigerant that has flowed out of the radiator (200) is converted into velocity energy to convert the refrigerant. The nozzle (410) for expanding under reduced pressure, the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) is sucked, and the refrigerant and the evaporator (300) injected from the nozzle (410). ), The ejector (400) having a pressure increasing unit (420, 430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant with the refrigerant, A gas-liquid separator (500) for separating the refrigerant into a refrigerant and a liquid-phase refrigerant to store the refrigerant is provided, and the nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage, and The dimension (B) from the throat (410a) to the outlet of the nozzle (410) is the dimension (A) from the portion where the passage cross-sectional area begins to decrease to the throat (410a).
Is a larger Suehiro nozzle,
30) to the minimum equivalent diameter (D2) of the booster (42
0, 430) has a length (L) ratio of 120 or less, and further, the ratio (D2) of the minimum equivalent diameter (D2) of the booster section (420, 430) to the equivalent exit diameter (D1) of the nozzle (410). / D1) is 1.05 or more and 10 or less.

As a result, as shown in FIGS. 4 and 5 which will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe regardless of the refrigerant flow rate and the kind of the refrigerant.

In the invention described in claim 2, carbon dioxide may be used as the refrigerant.

According to the third aspect of the invention, the compressor (100) for sucking and compressing the refrigerant, the radiator (200) for cooling the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and the refrigerant by separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) for storing a nozzle (410) has throat passage area is reduced most in the middle passage (410a), and the throat portion (41
0a) to the outlet of the nozzle (410) has a larger dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), and the mixing section (420) The equivalent diameter (D2) of the mixing part (42
The ratio (L / D2) of the length (L) of 0) is 120 or less, and further, the diameter (D1) corresponding to the outlet of the nozzle (410).
Ratio of equivalent diameter (D2) of the mixing part to (D2 / D1)
Is 1.05 or more and 10 or less.

As a result, as shown in FIG. 4 described later,
It is possible to operate the ejector cycle while maintaining the ejector efficiency ηe of 20% or more. Therefore,
The annual COP is superior to that of a normal vapor compression refrigeration cycle using R134a as a refrigerant, and the spread of the ejector cycle can be promoted.

The annual COP referred to here is, for example, 15 ° C, 20 ° C, 25 ° C in Tokyo. 30 ° C and 35
Frequency of outside temperature of ℃, 0km / h, 40k
CO of m / h, 60 km / h, and 100 km / h, which are used in the average year, are used depending on the frequency of appearance of vehicle speed.
Say P.

In the invention according to claim 4, the nozzle (41
Mixing part (420) for the outlet equivalent diameter (D1) of 0)
The equivalent diameter (D2) ratio (D2 / D1) of 1.3 or more,
It is characterized in that it is 5.3 or less.

As a result, as shown in FIG. 4 described later,
The ejector cycle can be operated while maintaining the ejector efficiency ηe of 40% or more. Therefore,
When the present invention is applied to a vehicle air conditioner, the COP is superior to the vehicle air conditioner using R134a as a refrigerant even in a situation where the outside air temperature is high and the COP is likely to drop (during idling operation). .

According to the fifth aspect of the invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and the refrigerant by separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) for storing a nozzle (410) has throat passage area is reduced most in the middle passage (410a), and the throat portion (41
0a) to the outlet of the nozzle (410) has a larger dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), and the mixing section (420) The equivalent diameter (D2) of the mixing part (42
The ratio (L / D2) of the length (L) of 0) is 120 or less, and CFC is used as the refrigerant, and the nozzle (41
The ratio (D2 / D1) of the equivalent diameter (D2) of the mixing portion to the equivalent exit diameter (D1) of 0) is 1.05 or more and 4.5 or less.

As a result, as shown in FIG.
The ejector cycle can be operated while maintaining a high ejector efficiency ηe of 20% or more.

In a sixth aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and the refrigerant by separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) for storing a nozzle (410) has throat passage area is reduced most in the middle passage (410a), and the throat portion (41
0a) to the outlet of the nozzle (410) has a larger dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), and the mixing section (420) The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the diffuser (430) is 120 or less, and the spread angle (θd) of the diffuser (430).
Is 0.2 degrees or more and 34 degrees or less.

As a result, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the seventh aspect of the invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and the refrigerant by separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) for storing a nozzle (410) has throat passage area is reduced most in the middle passage (410a), and the throat portion (41
0a) to the outlet of the nozzle (410) has a larger dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), and the mixing section (420) The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the diffuser (430) is 120 or less, and the spread angle (θd) of the diffuser (430).
Is 0.2 degrees or more and 7 degrees or less.

As a result, a thin profit of gas-liquid two-phase flow is less likely to occur in the diffuser (230), so that the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the invention described in claim 8, the compressor (100) for sucking and compressing the refrigerant, the radiator (200) for cooling the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and the refrigerant by separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. A gas-liquid separator (500) for storing, a ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and the nozzle is (410) is a tapered nozzle in which the passage area decreases toward the tip side, and the tapered angle (θn1) is 0.05 degrees or more and 20 degrees or less.

As a result, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the ninth aspect of the invention, the compressor (100) for sucking and compressing the refrigerant, the radiator (200) for cooling the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and the refrigerant by separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. A gas-liquid separator (500) for storing, a ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and the nozzle is (410) is a divergent nozzle having a throat portion with the smallest passage area in the middle of the passage, and the taper angle (θn1) on the inlet side is 0.05 degrees or more, 2
It is characterized in that it is 0 degrees or less, and the divergence angle (θn2) on the outlet side is 0.05 degrees or more and 17.5 degrees or less.

As a result, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the tenth aspect of the invention, the compressor (100) for sucking and compressing the refrigerant, the radiator (200) for cooling the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). The mixing unit (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the refrigerant flow, and the velocity energy while mixing the refrigerant injected from the nozzle (410) with the refrigerant sucked from the evaporator (300). An ejector (400) having a diffuser (430) for converting the refrigerant into pressure energy to increase the pressure of the refrigerant, and cooling the refrigerant by separating it into a gas-phase refrigerant and a liquid-phase refrigerant. And a ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, The nozzle (410) is the nozzle (41
It is characterized in that it has a shape such that the refrigerant changes substantially isentropically from the refrigerant inlet side of 0) to the refrigerant outlet side.

As a result, in the nozzle (410),
Since the refrigerant can be expanded adiabatically, the expansion energy that can be boosted (energy recovered) by the diffuser (430) can be increased, and the ejector efficiency ηe can be improved.

In the eleventh aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerant evaporates to absorb heat. Evaporator (300) and radiator (200)
A plurality of nozzles (4) that convert the pressure energy of the high-pressure refrigerant flowing out from the
Nozzle group (440) and nozzle group (4)
A pressure increasing section (42) for increasing the pressure of the refrigerant by converting the velocity energy into pressure energy while mixing the refrigerant injected from the evaporator (40) and the refrigerant sucked from the evaporator (300).
0, 430), and the 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) to form a liquid-phase refrigerant. Gas-liquid separator (50
0) and valves (451 to 45) that independently control the flow rates of the refrigerant flowing into the plurality of nozzles (410).
3) and the ratio (L / D) of the equivalent diameter (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420).
2) is 120 or less.

As a result, each valve (4
51), the ejector efficiency ηe is high.
The ejector cycle can be operated while maintaining the above.

In the twelfth aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerant evaporates to absorb heat. Evaporator (300) and radiator (200)
A plurality of nozzles (4) that convert the pressure energy of the high-pressure refrigerant flowing out from the
Nozzle group (440) and nozzle group (4)
A pressure increasing section (42) for increasing the pressure of the refrigerant by converting the velocity energy into pressure energy while mixing the refrigerant injected from the evaporator (40) and the refrigerant sucked from the evaporator (300).
0, 430), and the 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) to form a liquid-phase refrigerant. Gas-liquid separator (50
0) and a valve (454) for controlling the flow rate of the refrigerant flowing into the nozzle group (440).

As a result, the valve (45
By controlling 4), the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

Further, the number of valves can be reduced as compared with the invention in which each nozzle (410) is controlled independently.

According to the thirteenth aspect of the invention, the plurality of nozzles (410) are arranged in a concentric circle.

As a result, as compared with the case where a plurality of nozzles (410) are arranged in parallel, the size of the nozzle group (440) is prevented from increasing and the driving refrigerant flow jetted from the nozzle group (440) is prevented. With this, it is possible to increase the contact area with the suction refrigerant flow that is sucked from the evaporator (300) to the ejector (400). Therefore, since the suction refrigerant flow can be surely sucked, the mixing property between the suction refrigerant flow and the driving refrigerant flow can be improved.

In the fourteenth aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerant evaporates to absorb heat. Evaporator (300) and radiator (200)
The nozzles (410, 4) for converting the pressure energy of the high-pressure refrigerant flowing out of the tank into velocity energy to expand the refrigerant under reduced pressure.
40), and a pressure increasing unit (420, 430) for increasing the pressure of the refrigerant by converting velocity energy into pressure energy while mixing the refrigerant injected from the nozzles (410, 440) with the refrigerant sucked from the evaporator (300). And an ejector (400) having a gas phase refrigerant and a liquid phase refrigerant for separating the refrigerant into the compressor (1).
00) is supplied to the suction side, and the liquid-phase refrigerant is supplied to the evaporator (300).
And a gas-liquid separator (500) for supplying to the nozzle (4
10) is the throat (4 with the smallest passage area in the middle of the passage)
10a), and the dimension (B) from the throat (410a) to the outlet of the nozzle (410) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a). It is a Suehiro nozzle, and the pressure booster (420, 43
0) the minimum equivalent diameter (D2) of the booster (420,
430) has a length (L) ratio of 120 or less, and the pressure increasing portion (423) is configured such that the refrigerant passage cross-sectional area is substantially constant from the upstream side to the downstream side of the refrigerant flow. Characterize.

Thus, as will be described later, while maintaining a sufficient function (pressure boosting ability), the mixing section and the diffuser are integrated to simplify the structure of the ejector (400) and the manufacturing cost of the ejector (400). It can be reduced.

Further, as shown in FIG. 14 described later, in the conventional product (where the mixing section and the diffuser are clearly separated), a pressure loss due to a sudden expansion occurs at the connecting section between the mixing section and the diffuser. Therefore, in order to raise the pressure to the pressure equivalent to that of the ejector (400) according to the present invention, it is necessary to make the length of the diffuser sufficiently long.

Therefore, the ejector (4
According to (00), even if the length of the mixing section (423) is reduced, the ejector (400) can obtain a refrigerant pressure equal to or higher than that of a conventional product (where the mixing section and the diffuser are clearly separated). Ejector (400)
Can be miniaturized.

According to the invention as set forth in claim 15, the compressor (100) for sucking and compressing the refrigerant, the radiator (200) for cooling the refrigerant discharged from the compressor (100), and evaporating the refrigerant to absorb heat. Evaporator (300) and radiator (200)
The nozzles (410, 4) for converting the pressure energy of the high-pressure refrigerant flowing out of the tank into velocity energy to expand the refrigerant under reduced pressure.
40), and a pressure increasing unit (420, 430) for increasing the pressure of the refrigerant by converting velocity energy into pressure energy while mixing the refrigerant injected from the nozzles (410, 440) with the refrigerant sucked from the evaporator (300). And an ejector (400) having a gas phase refrigerant and a liquid phase refrigerant for separating the refrigerant into the compressor (1).
00) is supplied to the suction side, and the liquid-phase refrigerant is supplied to the evaporator (300).
And a gas-liquid separator (500) for supplying to the nozzle (4
10) is the throat (4 with the smallest passage area in the middle of the passage)
10a), and the dimension (B) from the throat (410a) to the outlet of the nozzle (410) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a). It is a Suehiro nozzle, and the pressure booster (420, 43
0) the minimum equivalent diameter (D2) of the booster (420,
430) has a length (L) ratio of 120 or less, and the pressurizing section (423) is configured such that the refrigerant passage cross-sectional area increases from the refrigerant flow upstream side toward the refrigerant flow downstream side. To do.

Thus, as will be described later, while maintaining a sufficient function (pressure boosting ability), the mixing section and the diffuser are integrated to simplify the structure of the ejector (400), thereby reducing the manufacturing cost of the ejector (400). It can be reduced.

Further, as shown in FIG. 14 described later, in the conventional product (the one in which the mixing section and the diffuser are clearly separated), a pressure loss due to a sudden expansion occurs in the mixing section and the connecting section with the diffuser. Therefore, in order to raise the pressure to the pressure equivalent to that of the ejector (400) according to the present invention, it is necessary to make the length of the diffuser sufficiently long.

Therefore, the ejector (4
According to (00), even if the length of the mixing section (423) is reduced, the ejector (400) can obtain a refrigerant pressure equal to or higher than that of a conventional product (where the mixing section and the diffuser are clearly separated). Ejector (400)
Can be miniaturized.

According to the invention described in claim 16,
The spread angle (θd) of the booster section (423) is preferably 4 ° or less.

According to the invention described in claim 17,
The nozzle (440) may be composed of a nozzle group including a plurality of nozzles (410).

In the eighteenth aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerant evaporates to absorb heat. Evaporator (300) and radiator (200)
The nozzles (410, 4) for converting the pressure energy of the high-pressure refrigerant flowing out of
40), and a pressure increasing unit (420, 430) for increasing the pressure of the refrigerant by converting velocity energy into pressure energy while mixing the refrigerant injected from the nozzles (410, 440) with the refrigerant sucked from the evaporator (300). And an ejector (400) having a gas phase refrigerant and a liquid phase refrigerant for separating the refrigerant into the compressor (1).
00) is supplied to the suction side, and the liquid-phase refrigerant is supplied to the evaporator (300).
And a gas-liquid separator (500) for supplying to the nozzle (4
10) is the throat (4 with the smallest passage area in the middle of the passage)
10a), and the dimension (B) from the throat (410a) to the outlet of the nozzle (410) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a). It is a Suehiro nozzle, and the pressure booster (420, 43
0) the minimum equivalent diameter (D2) of the booster (420,
430) has a length (L) ratio of 120 or less, and the pressurizing section (423) has a shape such that the refrigerant changes substantially isentropically from the refrigerant inlet side to the refrigerant outlet side. To do.

As a result, in the mixing section (423),
Since the refrigerant can be expanded adiabatically, the ejector efficiency ηe can be improved.

In the nineteenth aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. An evaporator (300) that exerts heat, a nozzle (410) that converts the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant, and the refrigerant is a gas-phase refrigerant and a liquid-phase refrigerant. And a gas-liquid separator (500) for storing a refrigerant to store the refrigerant, and connecting the refrigerant injection port (410a, 411a) side of the nozzle (410) to the gas-liquid separation (500). 5
00), the vapor-phase refrigerant evaporated in the evaporator (300) is sucked by the high-speed refrigerant flow injected from the nozzle (410), and the sucked refrigerant and the nozzle (4
It is characterized in that the velocity energy is converted into pressure energy and the pressure of the refrigerant is increased while mixing with the refrigerant injected from 10).

As a result, the manufacturing cost of the ejector cycle can be reduced.

In the invention as set forth in claim 20, a compressor (100) for sucking and compressing the refrigerant, a radiator (200) for cooling the refrigerant discharged from the compressor (100), and a refrigerating capacity by evaporating the refrigerant. And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and a refrigerant injection port (of the nozzle (410) ( 410
a, 411a) and sucks the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and injects the drawn refrigerant and the nozzle (410). And a gas-liquid separator (500) for storing the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and a refrigerant outlet side of the mixing section (420). Is connected to the gas-liquid separation (500) to convert the velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy in the gas-liquid separation (500) to increase the pressure of the refrigerant. Characterize.

As a result, it is possible to reduce the manufacturing cost while reducing the size of the ejector cycle.

In the twenty-first aspect of the present invention, the compressor (100) sucks and compresses the refrigerant, the radiator (200) that cools the refrigerant discharged from the compressor (100), and the refrigerant evaporates to absorb heat. Evaporator (300) and radiator (200)
The first nozzle (41) for converting pressure energy of the high-pressure refrigerant flowing out of the refrigerant into velocity energy to expand the refrigerant under reduced pressure.
0), a second nozzle (411) arranged in the first nozzle (410) and sucked and ejected from the evaporator (300) by the refrigerant ejected from the first nozzle (410), and the first nozzle (410). From the second nozzle (41
1) Ejector (40) having a booster (420, 430) for converting velocity energy into pressure energy while mixing with the refrigerant to be jetted, and boosting the pressure of the refrigerant
0) and the refrigerant is stored by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, supplying the gas-phase refrigerant to the suction side of the compressor (100), and supplying the liquid-phase refrigerant to the evaporator (300). And a first and second nozzle (410,
The position of the refrigerant injection port (410a, 411a) of 411) is in the refrigerant flow path in the ejector (400),
It is characterized in that they are provided at substantially the same position.

By the way, if the first nozzle (410) is located closer to the refrigerant inlet side of the ejector (400) than the second nozzle (411), the refrigerant injected from the first nozzle (410) and the second nozzle (410). If the mixed flow with the refrigerant injected from 411) is decompressed and the performance is reduced, while the first nozzle (410) is located closer to the refrigerant outlet side of the ejector (400) than the second nozzle (411). Therefore, the ability to secure the distance required to sufficiently mix the refrigerant ejected from the first nozzle (410) and the refrigerant ejected from the second nozzle (411) is deteriorated.

On the other hand, in the present invention, the refrigerant injection ports (410a, 411) of the first and second nozzles (410, 411) are used.
Since the position a) is provided at substantially the same position in the refrigerant flow path in the ejector (400), the performance of the ejector cycle can be improved.

According to the twenty-second aspect of the invention, the compressor (100) for sucking and compressing the refrigerant, the radiator (200) for cooling the refrigerant discharged from the compressor (100), and the refrigerating capacity by evaporating the refrigerant. The nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the evaporator (300) exhibiting the heat and the radiator (200) into velocity energy to decompress and expand the refrigerant, and the high velocity of the jetting from the nozzle (410). From the mixing section (420) and the mixing section (420), the vapor phase refrigerant evaporated in the evaporator (300) is sucked by the refrigerant flow, and the sucked suction flow and the driving flow jetted from the nozzle (410) are mixed. An ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out into pressure energy, and a refrigerant is separated into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant. The ejector (400) is provided with a gas-liquid separator (500), and the refrigerant flows into the diffuser (430) after the flow velocity of the suction flow and the flow velocity of the drive flow become substantially the same in the mixing section (420). It is characterized in that it is configured to flow in.

By the way, in the mixing section (420),
As shown in FIG. 19, which will be described later, the driving flow refrigerant and the suction flow refrigerant are mixed so that the sum of the momentum of the driving flow refrigerant and the momentum of the suction flow refrigerant is preserved, so that the refrigerant is also used in the mixing section (420). The pressure (static pressure) rises. On the other hand, in the diffuser 430, as described above, the velocity energy (dynamic pressure) of the refrigerant is converted into pressure energy (static pressure) by gradually enlarging the passage cross-sectional area. Therefore, in the ejector (400), the mixing is performed. The refrigerant pressure is increased by both the portion (420) and the diffuser 430.

That is, in the ideal ejector (400), the refrigerant pressure increases so that the sum of the momentum of the driving flow refrigerant and the momentum of the suction flow refrigerant is stored in the mixing section (420), and the diffuser (430). ) Increases the refrigerant pressure so that energy is conserved.

At this time, at the outlet of the mixing section (420) (the inlet of the diffuser (430)), the flow velocity of the driving flow refrigerant and the flow velocity of the suction flow refrigerant are not substantially the same,
If there is a large deviation in the flow velocity distribution, the diffuser (43
At 0), the velocity energy (dynamic pressure) of the refrigerant cannot be efficiently converted into pressure energy (static pressure), so the amount of pressure increase in the diffuser (430) is reduced.

On the contrary, after the flow velocity of the driving flow refrigerant and the flow velocity of the suction flow refrigerant become approximately the same speed (after the drive flow refrigerant and the suction flow refrigerant are sufficiently mixed), the passage cross-sectional area is substantially constant. If the portion (the portion that does not have the diffuser function) continues, the flow velocity of the refrigerant when flowing into the diffuser (430) will decrease due to pipe friction, so in this case as well, the amount of pressure increase in the diffuser (430) Will fall.

On the other hand, in the present invention, in the ejector (400), the refrigerant flows into the diffuser (430) after the flow velocity of the suction flow and the flow velocity of the drive flow become substantially the same in the mixing section (420). Since it is configured to flow in, the ejector efficiency ηe can be improved.

In the twenty-third aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes equal to or higher than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing unit for sucking the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) and mixing the sucked suction flow with the driving flow injected from the nozzle (410). (420) and an ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy, and a refrigerant for separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) that stores the pressure, and the ejector (400) increases the pressure in the mixing section (420) with respect to the total pressure increase amount (ΔP) in the ejector (400). The ratio of (ΔPm) (ΔPm / ΔP)
Is configured to be 50% or more.

As a result, the ejector efficiency ηe can be improved, as will be apparent from FIGS.

In the twenty-fourth aspect of the present invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes equal to or higher than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing unit for sucking the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) and mixing the sucked suction flow with the driving flow injected from the nozzle (410). (420) and an ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy, and a refrigerant for separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) that stores the pressure, and the ejector (400) increases the pressure in the mixing section (420) with respect to the total pressure increase amount (ΔP) in the ejector (400). The ratio of (ΔPm) (ΔPm / ΔP)
Is 55% or more and 80% or less.

As a result, the ejector efficiency ηe can be improved, as will be apparent from FIGS.

According to the twenty-fifth aspect of the invention, in the ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing unit for sucking the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) and mixing the sucked suction flow with the driving flow injected from the nozzle (410). (420) and an ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy, and a refrigerant for separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) that stores the pressure, and the ejector (400) increases the pressure in the mixing section (420) with respect to the total pressure increase amount (ΔP) in the ejector (400). The ratio of (ΔPm) (ΔPm / ΔP)
Is configured to be 30% or more.

As a result, the ejector efficiency ηe can be improved, as will be apparent from FIGS. 23 and 24 described later.

According to the twenty-sixth aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing unit for sucking the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) and mixing the sucked suction flow with the driving flow injected from the nozzle (410). (420) and an ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy, and a refrigerant for separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) that stores the pressure, and the ejector (400) increases the pressure in the mixing section (420) with respect to the total pressure increase amount (ΔP) in the ejector (400). The ratio of (ΔPm) (ΔPm / ΔP)
Is 35% or more and 80% or less.

As a result, the ejector efficiency ηe can be improved as will be apparent from FIGS. 23 and 24 described later.

According to the twenty-seventh aspect of the invention, in the ejector cycle in which the refrigerant pressure on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 55% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and further, the equivalent diameter (D) of the outlet of the nozzle (410).
The ratio (D2 / D1) of the minimum equivalent diameter (D2) of the booster section (420, 430) to 1) is set to 1.05 or more and 10 or less.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the twenty-eighth aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and further, the equivalent diameter (D) of the outlet of the nozzle (410).
Ratio (D2 / D) of equivalent diameter (D2) of mixing part to 1)
1) is 1.05 or more and 10 or less.

As a result, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the twenty-ninth aspect of the invention, in the ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing unit for sucking the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) and mixing the sucked suction flow with the driving flow injected from the nozzle (410). (420) and an ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy, and a refrigerant for separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) that stores the pressure, and the ejector (400) increases the pressure in the mixing section (420) with respect to the total pressure increase amount (ΔP) in the ejector (400). The ratio of (ΔPm) (ΔPm / ΔP)
Is 35% or more and 80% or less, and the mixing portion (42) with respect to the equivalent diameter (D2) of the mixing portion (420).
The ratio (L / D2) of the length (L) of 0) is 120 or less, and further, the diameter (D1) corresponding to the outlet of the nozzle (410).
Ratio of equivalent diameter (D2) of the mixing part to (D2 / D1)
Is 1.05 or more and 10 or less.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the thirtieth aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing unit for sucking the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410) and mixing the sucked suction flow with the driving flow injected from the nozzle (410). (420) and an ejector (400) having a diffuser (430) for converting velocity energy of the refrigerant flowing out of the mixing section (420) into pressure energy, and a refrigerant for separating the refrigerant into a vapor phase refrigerant and a liquid phase refrigerant. And a gas-liquid separator (500) that stores the pressure, and the ejector (400) increases the pressure in the mixing section (420) with respect to the total pressure increase amount (ΔP) in the ejector (400). The ratio of (ΔPm) (ΔPm / ΔP)
Is 35% or more and 80% or less, and the mixing portion (42) with respect to the equivalent diameter (D2) of the mixing portion (420).
The ratio (L / D2) of the length (L) of 0) is 120 or less, and CFC is used as the refrigerant, and the nozzle (41
The ratio (D2 / D1) of the equivalent diameter (D2) of the mixing portion to the equivalent exit diameter (D1) of 0) is 1.05 or more and 4.5 or less.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-first aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes equal to or higher than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 55% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and the spread angle (θd) of the diffuser (430).
Is 0.2 degrees or more and 34 degrees or less.

As a result, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-second aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and the spread angle (θd) of the diffuser (430).
Is 0.2 degrees or more and 34 degrees or less.

As a result, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-third aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes equal to or higher than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 55% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and the spread angle (θd) of the diffuser (430).
Is 0.2 degrees or more and 7 degrees or less.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-fourth aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less, and the spread angle (θd) of the diffuser (430).
Is 0.2 degrees or more and 7 degrees or less.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-fifth aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes equal to or higher than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 55% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, and the mixing part (420) and the diffuser (430).
Is characterized in that the cross section of the refrigerant passage is substantially constant from the upstream side to the downstream side of the refrigerant flow.

As a result, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the thirty-sixth aspect of the invention, in the ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, and the mixing part (420) and the diffuser (430).
Is characterized in that the cross section of the refrigerant passage is substantially constant from the upstream side to the downstream side of the refrigerant flow.

Thus, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the thirty-seventh aspect of the present invention, in the ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, and the mixing part (420) and the diffuser (430).
Is characterized in that the refrigerant passage cross-sectional area increases from the refrigerant flow upstream side toward the downstream side.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-eighth aspect of the present invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, and the mixing part (420) and the diffuser (430).
Is characterized in that the refrigerant passage cross-sectional area increases from the refrigerant flow upstream side toward the downstream side.

Thus, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

In the thirty-ninth aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, and the mixing part (420) and the diffuser (430).
Is characterized in that it has a shape such that the refrigerant changes substantially isentropically from the refrigerant inlet side to the refrigerant outlet side.

As a result, as described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

According to the forty-third aspect of the invention, the ejector cycle is such that the refrigerant pressure on the high-pressure side becomes less than the critical pressure of the refrigerant, and the compressor (100) sucks and compresses the refrigerant, and discharges from the compressor (100). A radiator (2
00), an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity, and a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out from the radiator (200) into velocity energy to decompress and expand the refrigerant. , A mixing section (420) for sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow injected from the nozzle (410), and the refrigerant and the evaporator (300) injected from the nozzle (410). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing the refrigerant sucked from the refrigerant, and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant. A gas-liquid separator (500) for storing a refrigerant, and the ejector (400),
Ratio (ΔPm / Δ) of the amount of pressure increase (ΔPm) in the mixing section (420) to the total amount of pressure increase (ΔP) in the ejector (400)
P) is 35% or more and 80% or less,
The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of the mixing part (420) is 120 or less, and the mixing part (420) and the diffuser (430).
Is characterized in that it has a shape such that the refrigerant changes substantially isentropically from the refrigerant inlet side to the refrigerant outlet side.

As a result, as will be described later, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

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

[0095]

BEST MODE FOR CARRYING OUT THE INVENTION (First Embodiment)
The ejector cycle according to the present invention is applied to a vehicle air conditioner using carbon dioxide as a refrigerant, and FIG. 1 is a schematic diagram of the ejector cycle according to the present embodiment.

Reference numeral 100 denotes a compressor for obtaining a driving force from a driving source (not shown) such as a running engine to suck and compress the refrigerant, and 200 denotes heat exchange between the refrigerant discharged from the compressor 100 and the outdoor air. Radiator (gas cooler) that cools the refrigerant by cooling
Is.

Numeral 300 is an evaporator which exerts refrigerating capacity by exchanging the liquid-phase refrigerant by exchanging heat between the air blown out into the room and the liquid-phase refrigerant, and 400 decompresses and expands the refrigerant flowing out from the radiator 200. Is an ejector that sucks the vapor-phase refrigerant evaporated in the evaporator 300 and converts the expansion energy into pressure energy to raise the suction pressure of the compressor 100.

Here, as shown in FIG. 2, the ejector 400 converts the pressure energy (pressure head) of the high-pressure refrigerant flowing out from the radiator 200 into velocity energy (velocity head).
410 for injecting the vapor-phase refrigerant evaporated in the evaporator 300 by the high-speed refrigerant flow (jet flow) ejected from the nozzle 410, and the nozzle 410 for injecting from the nozzle 410. The diffuser 430 is configured to convert the velocity energy into pressure energy while increasing the pressure of the refrigerant while mixing the refrigerant and the refrigerant sucked from the evaporator 300.

In this embodiment, the equivalent diameter ratio D2 / D1 which is the ratio (= D2 / D1) of the equivalent diameter of the mixing section 420 to the equivalent outlet diameter D1 of the nozzle 410 is 1.0.
The hole diameters of the nozzle 410 and the mixing section 420 are selected so as to be 5 or more.

The equivalent diameter means the diameter when the cross-sectional area of the refrigerant passage is converted to a circle. In this embodiment, the outlet of the nozzle 410 and the mixing section 420 are circular, so the equivalent diameter D Is the outlet of the nozzle 410 and the mixing section 42
It has a diameter of 0.

In this embodiment, the equivalent diameter D2 of the mixing section 420 is constant up to the diffuser 430, but the cross-sectional area S2 of the mixing section 420 may be tapered so as to increase toward the diffuser 430. However, in this case, the equivalent diameter of the mixing section 420 is defined by the inlet of the mixing section 420.

Incidentally, the nozzle 410 according to the present embodiment.
Has a throat portion 410a having the smallest passage area in the middle of the passage, and the dimension B from the throat portion 410a to the outlet of the nozzle 410 starts from the portion where the passage cross-sectional area starts to decrease.
A divergent nozzle larger than size A up to 0a
ent Nozzle, de Laval Nozzl
e).

Further, in FIG. 1, 500 is an ejector 400.
Is a gas-liquid separator that stores the refrigerant by separating the inflowing refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the separated gas-phase refrigerant is sucked into the compressor 100, The separated liquid-phase refrigerant is sucked toward the evaporator 300 side.

The refrigerant passage 301 connecting the gas-liquid separator 500 and the evaporator 300 reduces the pressure of the refrigerant sucked into the evaporator 300 to surely lower the pressure (evaporation pressure) in the evaporator 300. Like a capillary tube and a fixed throttle, a predetermined pressure loss is generated by the circulation of the refrigerant.

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

When the compressor 100 starts up, the gas-liquid separator 5
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 at 00 is expanded under reduced pressure by the nozzle 410 of the ejector 400 to suck the refrigerant inside the evaporator 300.

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

On the other hand, the ejector 400 is used for the evaporator 300.
Since the refrigerant in the inside is sucked, the liquid-phase refrigerant flows into the evaporator 300 from the gas-liquid separator 500, and the inflowing refrigerant is
It absorbs heat from the air blown into the room and evaporates.

Incidentally, FIG. 3 is a ph diagram showing the operation of the ejector cycle according to the present embodiment, and the numbers shown in FIG. 3 show the state of the refrigerant at the positions of the numbers shown in FIG.

Then, the suction pressure increase ΔP of the compressor 100
, The absolute value of which varies depending on the efficiency of the mixing section 420 and the diffuser 430, but at the refrigerant inlet of the nozzle 410 (point indicated by 6 in FIG. 3) and the refrigerant inlet of the diffuser 430 (point indicated by 3 in FIG. 2). The larger the specific enthalpy difference of (adiabatic heat drop), the larger.

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

FIG. 4 is a numerical simulation result showing the relationship between the equivalent diameter ratio D2 / D1 and the ejector efficiency ηe with the mass flow rate of the refrigerant (hereinafter abbreviated as the refrigerant flow rate) as a parameter, which is also apparent from this graph. When the equivalent diameter ratio D2 / D1 is 1.05 or more, the ejector efficiency ηe sharply improves regardless of the refrigerant flow rate, and the equivalent diameter ratio D
It can be seen that 2 / D1 gradually decreases after about 4.

Therefore, the equivalent diameter ratio D2 / D1 is 1.
If it is at least 05, preferably at least 10 and at most 100, the ejector cycle can be operated while maintaining a high ejector efficiency ηe.

If the equivalent diameter ratio D2 / D1 is set to 1.3 or more and 5.3 or less, the ejector cycle can be operated while maintaining the ejector efficiency ηe of 40% or more, so that the outside temperature is high. Even in a situation where the COP is likely to decrease (during idling operation), the COP is superior to the vehicle air conditioner using R134a as the refrigerant.

The ejector efficiency ηe is the radiator 2
00 (high-pressure side heat exchanger), the product of the refrigerant flow rate Gn and the enthalpy difference Δie at the inlet and outlet of the nozzle 410 is used as the denominator, and the numerator indicates how much energy is recovered as work of the compressor 100. Flow rate Gn and evaporator 300
This is defined by the sum of the flow rate Ge of the refrigerant flowing through the (low-pressure side heat exchanger) and the pressure recovery ΔP at the ejector 400. Specifically, the velocity energy of the suction refrigerant before being sucked by the ejector 400 is taken into consideration and defined by the following mathematical formula 1.

[0116]

[Equation 1]

However, i2, i3, i8, and i8 'are the same as those in FIG.
2 shows the specific enthalpy at the points indicated by 2, 3, 8, and 8 '.

By the way, FIG. 5 is a numerical simulation result showing the relationship between the mixed shape ratio L / D2 and the ejector efficiency ηe. As is apparent from FIG. 5, the mixed shape ratio L / D2 is shown.
If D2 is 170 or less, an ejector efficiency ηe of 5% or more can be secured in the ejector cycle using carbon dioxide as the refrigerant.

The mixed shape ratio L / D2 means the mixed portion 4
This is also a ratio of the length L of the mixing section 420 to the equivalent diameter D2 of 20. In the present embodiment, the mixing shape ratio L / D2.
Is 120 or less, and the ejector efficiency ηe is 20% or more.
Has been secured.

Here, the length L of the mixing section 420 is as shown in FIG.
As shown in, the dimension from the refrigerant outlet of the nozzle 410 to the refrigerant inlet of the diffuser 430 is referred to.

If an ejector efficiency ηe of 20% or more is secured, as shown in FIG. 6, in the case where carbon dioxide is used as a refrigerant, it is about the same as in a simple vapor compression refrigeration cycle using an expansion valve. 3% or more, about 8% or more when R404a is the refrigerant, and 10% when R134a is the refrigerant.
% Or more, the coefficient of performance of the cycle can be improved.

Incidentally, in the numerical simulations shown in FIGS. 5 and 6, the outside air temperature (ambient temperature of the place where the radiator 200 is arranged) is set to −30 ° C. to 55, and the inside air temperature (where the evaporator 200 is arranged). The results are obtained when the operating conditions are changed while setting the atmospheric temperature of) to −30 ° C. to 55.

(Second Embodiment) In the first embodiment, carbon dioxide was used as the refrigerant, but in the present embodiment, Freon (R134a) is used as the refrigerant.

As is clear from the test results shown in FIG. 7, when chlorofluorocarbon was used as the refrigerant, when the equivalent diameter ratio D2 / D1 was 1.5 or more, regardless of the refrigerant flow rate,
It can be seen that the ejector efficiency ηe sharply improves. Therefore, in the present embodiment, the equivalent diameter ratio D2 / D1 is 1.
By setting it to 5 or more and 4.5 or less, the ejector efficiency η
We are trying to improve e.

As is clear from FIG. 7, if the equivalent diameter ratio D2 / D1 of freon is 1.02 or more, the ejector efficiency ηe sufficient for practical use can be obtained. Further, in the present embodiment and the following embodiments, unless otherwise specified, the ejector 400 has a mixing shape ratio L / D2 of 120 or less and employs a divergent nozzle as the nozzle 410.

(Third Embodiment) In this embodiment, the ejector efficiency ηe is improved by optimizing the spread angle θd (see FIG. 2) of the diffuser 430. Specifically, the spread angle θd is 0.2 degrees or more, 34
There are less than a degree. Incidentally, in the present embodiment, the spread angle θd
Is 6.5 degrees.

FIG. 8 is a numerical simulation result showing the relationship with the spread angle θd of the diffuser 430 and the ejector efficiency ηe. As is clear from FIG. 8, the spread angle θd is 0.2 degrees or more and 34 degrees. In the ejector cycle using carbon dioxide as a refrigerant
An ejector efficiency ηe of 0% or more can be secured.

Incidentally, in the numerical simulation shown in the numerical simulation shown in FIG. 8, the outside air temperature (ambient temperature of the place where the radiator 200 is arranged) is set to -30 ° C. to 55, and the inside air temperature (arrangement of the evaporator 200 is set. The results are obtained when the operating conditions are changed with the ambient temperature of the specified place) set to −30 ° C. to 55.

The upper graph of the two graphs shown in FIG. 8 shows the internal heat exchanger (heat exchanger for exchanging heat between the refrigerant sucked into the compressor 100 and the refrigerant at the outlet of the radiator 200). It is a numerical simulation result in the ejector cycle which has, and the lower graph is a numerical simulation result in the ejector cycle which does not have an internal heat exchanger.

(Fourth Embodiment) In this embodiment, the nozzle 4
By optimizing the shape of No. 10, the ejector efficiency ηe
It is intended to improve. Specifically, the nozzle 410
The shape of the refrigerant passage is such that the refrigerant changes substantially isentropically from the refrigerant inlet side of the nozzle 410 to the refrigerant outlet side.

As a result, since the refrigerant can be adiabatically expanded in the nozzle 410, the expansion energy that can be boosted (energy recovered) by the diffuser 430 can be increased, and the ejector efficiency ηe can be improved. Can be made.

In the present specification, the term “substantially isentropic change of the refrigerant from the refrigerant inlet side to the refrigerant outlet side of the nozzle 410” means that 70% or more of the adiabatic heat drop before and after the nozzle can be converted into kinetic energy. Say

Incidentally, FIG. 9 shows an example of the nozzle shape according to the present embodiment, and FIG. 9A shows a divergent nozzle (diver) having a throat portion with the smallest passage area in the middle of the passage.
gent Nozzle, de Laval Nozz
le), the taper angle θn1 on the inlet side is 0.05 degrees or more and 20 degrees or less, and the divergent angle θn on the outlet side.
2 is 0.05 degrees or more and 17.5 degrees or less, and (b) is a tapered nozzle (Convergent Nozzle) whose passage area decreases toward the tip side, and the tapered angle θn1 is 0. More than .05 degrees, 20
This is an example of less than or equal to degree.

The nozzle shape is determined by solving the simultaneous equations shown in the following mathematical formula 2.

[0135]

[Equation 2]

(Fifth Embodiment) In the above embodiment, 1
Although the ejector 400 including the nozzles 410 of the book is used, in the present embodiment, as shown in FIG. 10A, a plurality of nozzles 410 (three in the present embodiment) are arranged in a concentric circle to form the nozzle group 440. And a plurality of nozzles 410
The valves 451 to 453 for independently controlling the flow rates of the refrigerant flowing into the are provided. Also in this embodiment, the mixed shape ratio L / D2 is 120 or less, and the divergent nozzle is used as the nozzle 410.

Then, the openings of the valves 451 to 453 are controlled according to the operating state of the cycle. Specifically, the heat load of the cycle (the heat absorption capacity required by the evaporator 300,
Alternatively, when the heat dissipation capacity required by the radiator 200 increases, the nozzle 410 that operates (the nozzle 4 through which the refrigerant flows)
When the number of 10) is increased and the thermal load of the cycle is reduced, the number of operating nozzles 410 is reduced.

Further, since the plurality of nozzles 410 are arranged concentrically, the nozzle group 440 is prevented from increasing in size as compared with the case where the plurality of nozzles 410 are arranged in parallel, and the nozzle group 440 is A drive refrigerant flow that is injected,
It is possible to increase the contact area with the suction refrigerant flow that is sucked from the evaporator 300 to the ejector 400. Therefore, since the suction refrigerant flow can be surely sucked, the mixing property between the suction refrigerant flow and the driving refrigerant flow can be improved.

(Sixth Embodiment) In this embodiment, as shown in FIG. 11, a plurality of (three in this embodiment) nozzles 410 are arranged concentrically to form a nozzle group 440, and a nozzle group 440 is provided. 4 which controls the flow rate of the refrigerant flowing into the
54 is provided. Also in this embodiment, the mixed shape ratio L / D2 is 120 or less, and the divergent nozzle is used as the nozzle 410.

When the heat load of the cycle is increased, the opening degree of the valve 454 is increased to increase the flow rate of the refrigerant flowing into the nozzle group 440, and conversely, when the heat load of the cycle is decreased, the valve is opened. The opening degree of 454 is reduced to reduce the flow rate of the refrigerant flowing into the nozzle group 440.

As a result, the number of valves 454 can be reduced as compared with the fifth embodiment in which the nozzles 410 are controlled independently.

Incidentally, FIG. 11A shows each nozzle 410
This is an example in which the nozzles 410 are arranged so that the axes of the refrigerant blown out from the nozzles are substantially parallel, and FIG.
In this example, the nozzles 410 are arranged so that the axes of the refrigerant blown out from the nozzles 10 intersect.

(Seventh Embodiment) In the above-described embodiment, the mixing section 420, which is a boosting section, and the diffuser 430 in the ejector 400 are clearly distinguished from each other, but in the present embodiment, as shown in FIG. In addition, the mixing section 420 and the diffuser 430 are integrated with each other, and the refrigerant is injected from the nozzle 410 at a portion (hereinafter, referred to as a pressure increasing section 423) where the refrigerant passage cross-sectional area increases from the refrigerant flow upstream side to the downstream side. (Hereinafter, this refrigerant will be referred to as a driving flow.) And the evaporator 300.
The refrigerant pressure is increased (recovered) while being mixed with the refrigerant sucked from (hereinafter, this refrigerant is referred to as a suction flow).

By the way, FIG. 13 shows the spread angle θd of the booster 423 and the amount of boosting by the ejector 400 (evaporator 300).
The pressure P1 of the refrigerant drawn from the ejector 400 to the ejector 400 (see FIG. 12) and the refrigerant pressure P2 at the outlet of the ejector 400.
FIG. 13 is a result of numerical simulation showing a relationship with (differential pressure with respect to FIG. 12), and as is clear from FIG.
°), the above-described embodiment (the ejector 400 in which the mixing section 420 and the diffuser 430 are clearly distinguished).
It is possible to secure a boost amount equal to or higher than.

Incidentally, the calculation conditions are the same as those in the fourth and fifth embodiments. Further, as is clear from FIG. 12, the spread angle θd is an angle formed by the inner wall surface of the mixing section 423 and a reference line parallel to the center line of the mixing section 423.

Therefore, in the present embodiment, the manufacturing cost of the ejector 400 is reduced by securing the sufficient function (pressure boosting ability) and simplifying the structure of the ejector 400 by integrating the mixing section 420 and the diffuser 430. be able to.

Further, FIG. 14 shows the boosting of the ejector 400 according to the present embodiment (in which the mixing section 420 and the diffuser 430 are integrated) and the conventional product (the mixing section 420 and the diffuser 430 are clearly separated). Part 42
3 is a graph (numerical simulation result) showing the relationship between the distance from the 3 (mixing section 420) inlet and the refrigerant pressure.
As is clear from FIG. 4, in the conventional product (where the mixing section 420 and the diffuser 430 are clearly separated), a pressure loss due to a sudden expansion occurs in the connecting section between the mixing section 420 and the diffuser 430. In order to raise the pressure to a pressure equivalent to that of the ejector 400 according to the embodiment, the length of the diffuser 430 needs to be sufficiently long.

That is, the ejector 40 according to the present embodiment.
According to 0, even if the length of the mixing unit 423 (ejector 400) is reduced, the refrigerant pressure in the ejector 400 is equal to or higher than that of the conventional product (where the mixing unit 420 and the diffuser 430 are clearly separated). Therefore, the ejector 400 can be downsized.

As is clear from FIG. 13, even when the spread angle θd = 0 ° (the refrigerant passage cross-sectional area of the pressure increasing portion 423 is substantially constant), the refrigerant pressure is increased while mixing the drive flow and the suction flow ( Can be restored).

Further, in the ejector cycle, as shown in FIG. 12, the suction nozzle 411 for ejecting the suction flow is arranged coaxially in the nozzle 410 (drive nozzle, first nozzle) 410 for ejecting the drive flow. At the same time, the refrigerant injection ports 410a, 411 of both nozzles 410, 411 are
It is desirable that the position of 11a is arranged at substantially the same position (in the present embodiment, the inlet of the booster 423) in the refrigerant flow path in the ejector 400.

(Eighth Embodiment) As shown in FIG. 15, this embodiment is a combination of the eighth embodiment and the sixth and seventh embodiments. Specifically, the nozzles in the ejector 400 are a nozzle group 440 including a plurality of nozzles 410.
It is what

(Ninth Embodiment) In this embodiment, as shown in FIG. 16, in the pressure booster 423, the refrigerant changes substantially isentropically from the refrigerant inlet side to the refrigerant outlet side.

As a result, the refrigerant can be expanded adiabatically in the mixing section 423, so that the ejector efficiency ηe can be improved.

(Tenth Embodiment) In the present embodiment, FIG.
7, the mixing section 420 and the diffuser 430 are shown.
By eliminating the (mixing unit 423) and connecting the refrigerant injection port 410a side of the nozzle 410 to the gas-liquid separation 500, the gas-phase refrigerant evaporated in the evaporator 300 by the drive flow in the gas-liquid separation 500. Is sucked, and while the sucked refrigerant (suction flow) and the driving flow are mixed, velocity energy is converted into pressure energy to increase the pressure of the refrigerant.

This makes it possible to reduce the manufacturing cost of the ejector cycle.

(Eleventh Embodiment) This embodiment is shown in FIG.
As shown in FIG.
By connecting to 00, in the gas-liquid separation 500,
The velocity energy of the refrigerant flowing out of the mixing section 420 is converted into pressure energy to increase the pressure of the refrigerant.

Thus, the manufacturing cost of the ejector cycle can be reduced.

(Twelfth Embodiment) In the mixing section 420, as shown in FIG. 19, the driving flow refrigerant and the suction flow refrigerant are mixed so that the sum of the momentum of the driving flow refrigerant and the momentum of the suction flow refrigerant is stored. Are mixed, the refrigerant pressure (static pressure) also rises in the mixing section 420. Meanwhile, the diffuser 4
As described above, in 30, the velocity energy (dynamic pressure) of the refrigerant is converted into pressure energy (static pressure) by gradually expanding the passage cross-sectional area as described above.
At 0, the refrigerant pressure is increased by both the mixing section 420 and the diffuser 430.

That is, in the ideal ejector 400, the refrigerant pressure increases so that the sum of the momentum of the driving flow refrigerant and the momentum of the suction flow refrigerant is stored in the mixing section 420,
The refrigerant pressure increases so that energy is stored in the diffuser 430.

In FIG. 19, the gas velocity is the size when the velocity of the refrigerant injected from the nozzle 410 is 1, and the axial dimension is the dimension based on the refrigerant outlet of the nozzle 410 and the radial dimension. Represents the dimension from the center line of the ejector 400 as a rotationally symmetric body.

By the way, at the outlet of the mixing section 420 (the inlet of the diffuser 430), if the flow velocity of the driving flow refrigerant and the flow velocity of the suction flow refrigerant are not substantially the same, and there is a large deviation in the flow velocity distribution, the diffuser Since the velocity energy (dynamic pressure) of the refrigerant cannot be efficiently converted into pressure energy (static pressure) at 430, the diffuser 43
The amount of boosting at 0 decreases.

On the contrary, after the flow velocity of the driving flow refrigerant and the flow velocity of the suction flow refrigerant become substantially the same speed (after the drive flow refrigerant and the suction flow refrigerant are sufficiently mixed), the passage cross-sectional area is substantially constant. If the portion (the portion that does not have the diffuser function) continues, the flow velocity of the refrigerant when flowing into the diffuser 430 decreases due to the pipe friction, and therefore the diffuser 43 also in this case.
The amount of boosting at 0 decreases.

Therefore, in the present embodiment, the length L of the mixing section 420 is set so that the refrigerant flows into the diffuser 430 after the flow rate of the suction flow and the flow rate of the driving flow become substantially the same in the mixing section 420. By selecting it, the ejector efficiency ηe is increased.

When the flow velocity of the suction flow and the flow velocity of the drive flow become substantially the same in the mixing section 420, as shown in FIG.
Since the refrigerant pressure in the mixing section 420 is substantially constant (the rate of pressure increase is approximately 0), measuring the pressure change from the refrigerant outlet of the nozzle 410 results in a suction flow velocity and a driving flow velocity. It is possible to determine whether or not they have become substantially the same.

(Thirteenth Embodiment) In the ejector 400, as described above, the refrigerant pressure increases so that the sum of the momentum of the driving flow refrigerant and the momentum of the suction flow refrigerant is stored in the mixing section 420, and the diffuser 430 is used. Although the refrigerant pressure increases so that energy is stored in the mixing section 420, if the passage cross-sectional area of the mixing section 420 is increased in order to increase the pressure increase amount in the mixing section 420, the expansion amount of the passage cross-sectional area in the diffuser 430 increases. Since it decreases, the amount of pressure increase in the diffuser 430 decreases.

Therefore, the ratio of the boosting amount ΔPm in the mixing section 420 to the total boosting amount ΔP in the ejector 400 at which the ejector efficiency ηe becomes maximum (maximum) (= ΔPm /
ΔP) can be present. Note that the total boost amount ΔP is calculated by the mixing unit 4
20 is the sum of the boost amount ΔPm at 20 and the boost amount ΔPd at the diffuser 430, and hereinafter, ΔPm / ΔP is referred to as a boost ratio β.

FIG. 21 shows a flow rate ratio α (= refrigerant flow rate Ge / refrigerant flow rate G when carbon dioxide is used as the refrigerant).
It is a numerical simulation result showing the relationship between the boost ratio β and the ejector efficiency ηe when n) is a parameter,
FIG. 22 shows the relationship between the step-up ratio β and the flow rate ratio α that are the maximum ejector efficiency ηe. In the simulation, the outside air temperature was changed in the range of 15 ° C to 45 ° C.

FIG. 23 is a numerical simulation result showing the relationship between the boost ratio β and the ejector efficiency ηe when the flow rate ratio α is used as a parameter when HFC is used as the refrigerant, and FIG. 24 is the maximum ejector efficiency. It shows the relationship between ηe and the flow rate ratio α. In the simulation, the outside air temperature was changed in the range of -20 ° C to 45 ° C.

As is apparent from these, when carbon dioxide is used as the refrigerant, the pressurization ratio β should be 50% or more, preferably 55% or more and 80% or less. When the refrigerant is HFC, the boost ratio β may be 30% or more, preferably 35% or more and 80% or less.

(Other Embodiments) In the above embodiments, carbon dioxide or chlorofluorocarbon was used as the refrigerant, but the present invention is not limited to this. For example, hydrocarbons such as ethylene, ethane, nitric oxide, propane, etc. Other refrigerants such as a system refrigerant may be used.

Further, the present invention is not limited to the one shown in the above-mentioned embodiment, and for example, at least two kinds of the above-mentioned embodiments may be combined.

[Brief description of drawings]

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

FIG. 2 is an enlarged schematic diagram of an ejector according to an embodiment of the present invention.

FIG. 3 is a ph (Mollier) diagram of the ejector cycle according to the first embodiment of the present invention.

FIG. 4 is a graph showing the relationship between the ejector efficiency ηe and the equivalent diameter ratio in the ejector cycle according to the first embodiment of the present invention.

FIG. 5 is a graph showing the relationship between the mixing shape ratio L / D2 and the ejector efficiency ηe in the ejector cycle according to the first embodiment of the present invention.

FIG. 6 is a graph showing the relationship between the ejector efficiency ηe and the performance improvement ratio for a simple vapor compression refrigeration cycle using an expansion valve.

FIG. 7 is a graph showing the relationship between the ejector efficiency ηe and the equivalent diameter ratio in the ejector cycle according to the second embodiment of the present invention.

FIG. 8 is a graph showing a relationship between a spreader angle θd of a diffuser and an ejector efficiency ηe in an ejector cycle according to a third embodiment of the present invention.

FIG. 9 is a schematic diagram showing a cross-sectional shape of a nozzle in an ejector cycle according to a fourth embodiment of the present invention.

FIG. 10A is a schematic view of a nozzle in an ejector cycle according to a fifth embodiment of the present invention, and FIG. 10B is a right side view of FIG.

FIG. 11 is a schematic diagram of a nozzle in an ejector cycle according to a sixth embodiment of the present invention.

FIG. 12 is a schematic diagram of an ejector in an ejector cycle according to a seventh embodiment of the present invention.

FIG. 13 is a graph showing the relationship between the spread angle θd of the booster and the boost amount.

FIG. 14 is a graph showing the relationship between the boost amount and the distance from the inlet of the boost unit.

FIG. 15 is a schematic diagram of an ejector in an ejector cycle according to an eighth embodiment of the present invention.

FIG. 16 is a schematic diagram of an ejector in an ejector cycle according to a ninth embodiment of the present invention.

FIG. 17 is a schematic diagram of an ejector-integrated gas-liquid separator in an ejector cycle according to a tenth embodiment of the invention.

FIG. 18 is a schematic diagram of an ejector-integrated gas-liquid separator in an ejector cycle according to an eleventh embodiment of the present invention.

FIG. 19 is a three-dimensional characteristic diagram showing the relationship between the refrigerant flow velocity and the radial position with respect to the central portion of the cross section of the refrigerant passage of the ejector from the refrigerant outlet of the nozzle to the refrigerant outlet of the diffuser.

FIG. 20 is a graph showing the relationship between the distance from the nozzle outlet and the amount of pressure increase.

FIG. 21 is a graph showing the relationship between the boost ratio β and the ejector efficiency ηe when the flow rate ratio α is used as a parameter when carbon dioxide is used as the refrigerant.

FIG. 22 is a graph showing the relationship between the pressure increase ratio β and the flow rate ratio α that are the maximum ejector efficiency ηe when carbon dioxide is used as the refrigerant.

FIG. 23 is a flow rate ratio α when HFC is used as a refrigerant.
Step-up ratio β and ejector efficiency η
It is a graph which shows the relationship with e.

FIG. 24 is a graph showing the relationship between the pressure ratio β and the flow rate ratio α, which is the maximum ejector efficiency ηe when HFC is used as the refrigerant.

[Explanation of symbols]

400 ... Ejector, 410 ... Nozzle, 420 ... Mixing part, 430 ... Diffuser.

   ─────────────────────────────────────────────────── ─── Continued front page    (31) Priority claim number Japanese Patent Application No. 2001-128034 (P2001-128034) (32) Priority date April 25, 2001 (April 25, 2001) (33) Priority claiming country Japan (JP) (72) Inventor Hiroshi Oshiya             1-1, Showa-cho, Kariya city, Aichi stock market             Inside the company DENSO (72) Inventor Gota Ogata             1-1, Showa-cho, Kariya city, Aichi stock market             Inside the company DENSO

Claims (40)

[Claims] 1. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The vapor phase refrigerant evaporated at (300) is sucked, and the velocity energy is converted into pressure energy by mixing the refrigerant injected from the nozzle (410) and the refrigerant sucked from the evaporator (300) to convert the velocity energy into pressure energy. A pressure increasing unit (420, 43) for increasing the pressure.
0) having an ejector (400), and a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the nozzle (410) has a passage area in the middle of the passage. Has the most reduced throat (410a), and said throat (41a)
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), 420, 430) minimum equivalent diameter (D2)
The ratio of the length (L) of the pressure boosting section (420, 430) to 120 is 120 or less, and the outlet equivalent diameter (D1) of the nozzle (410).
The ejector cycle characterized in that the ratio (D2 / D1) of the minimum equivalent diameter (D2) of the pressure boosting section (420, 430) to 1.05 or more and 10 or less. 2. The ejector cycle according to claim 1, wherein carbon dioxide is used as the refrigerant. 3. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage. ), And the throat (41
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), the mixing section ( The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of 420) is 12
0 or less, and further, the equivalent diameter (D1) of the outlet of the nozzle (410)
Of the equivalent diameter (D2) of the mixing part to (D2 / D
The ejector cycle characterized in that 1) is 1.05 or more and 10 or less. 4. The equivalent diameter (D) of the mixing section (420) to the equivalent outlet diameter (D1) of the nozzle (410).
The ejector cycle according to claim 2, wherein the ratio (D2 / D1) of 2) is 1.3 or more and 5.3 or less. 5. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage. ), And the throat (41
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), the mixing section ( The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of 420) is 12
0 or less, and using Freon as a refrigerant, the nozzle (41
3. The ratio (D2 / D1) of the equivalent diameter (D2) of the mixing section to the equivalent outlet diameter (D1) of (0) is 1.05 or more;
An ejector cycle characterized by being 5 or less. 6. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage. ), And the throat (41
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), the mixing section ( The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of 420) is 12
The ejector cycle is 0 or less, and the spread angle (θd) of the diffuser (430) is 0.2 degrees or more and 34 degrees or less. 7. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage. ), And the throat (41
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), the mixing section ( The ratio (L / D2) of the length (L) of the mixing part (420) to the equivalent diameter (D2) of 420) is 12
The ejector cycle is 0 or less, and the spread angle (θd) of the diffuser (430) is 0.2 degrees or more and 7 degrees or less. 8. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant and storing the refrigerant, wherein the mixing section (420) has a corresponding diameter (D2) of the mixing section (420). Length (L) ratio (L / D2) is 12
0 or less, the nozzle (410) is a tapered nozzle whose passage area decreases toward the tip side, and the tapered angle (θ
The ejector cycle, wherein n1) is 0.05 degrees or more and 20 degrees or less. 9. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant and storing the refrigerant, wherein the mixing section (420) has a corresponding diameter (D2) of the mixing section (420). Length (L) ratio (L / D2) is 12
0 or less, the nozzle (410) is a divergent nozzle having a throat portion with the smallest passage area in the middle of the passage, and when the taper angle (θn1) on the inlet side is 0.05 degrees or more and 20 degrees or less. Yes,
And the divergence angle (θn2) on the outlet side is 0.05 degrees or more,
An ejector cycle characterized by being set to 17.5 degrees or less. 10. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant and storing the refrigerant, wherein the mixing section (420) has a corresponding diameter (D2) of the mixing section (420). Length (L) ratio (L / D2) is 12
The ejector cycle is 0 or less, and the nozzle (410) has a shape such that the refrigerant changes substantially isentropically from the refrigerant inlet side of the nozzle (410) to the refrigerant outlet side. 11. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and pressure energy of the high-pressure refrigerant flowing out from the radiator (200). Nozzle group (44) including a plurality of nozzles (410) for converting the heat energy into velocity energy to expand the refrigerant under reduced pressure.
0) and the refrigerant injected from the nozzle group (440) and the refrigerant sucked from the evaporator (300) are mixed with each other to convert velocity energy into pressure energy to increase the pressure of the refrigerant (420, And an ejector (400) having 430) to store the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and supplying the gas-phase refrigerant to the suction side of the compressor (100) to supply the liquid-phase refrigerant. A gas-liquid separator (500) to be supplied to the evaporator (300) and valves (451 to 453) for independently controlling the flow rates of the refrigerant flowing into the plurality of nozzles (410).
And the ratio (L / D2) of the equivalent diameter (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 120 or less. 12. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and pressure energy of the high-pressure refrigerant flowing out from the radiator (200). Nozzle group (44) including a plurality of nozzles (410) for converting the heat energy into velocity energy to expand the refrigerant under reduced pressure.
0) and the refrigerant injected from the nozzle group (440) and the refrigerant sucked from the evaporator (300) are mixed with each other to convert velocity energy into pressure energy to increase the pressure of the refrigerant (420, And an ejector (400) having 430) to store the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and supplying the gas-phase refrigerant to the suction side of the compressor (100) to supply the liquid-phase refrigerant. An ejector cycle comprising: a gas-liquid separator (500) supplied to the evaporator (300); and a valve (454) for controlling the flow rate of the refrigerant flowing into the nozzle group (440). 13. The nozzle according to claim 11, wherein the plurality of nozzles (410) are arranged in a concentric circle.
The ejector cycle described in 2. 14. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and pressure energy of the high-pressure refrigerant flowing out from the radiator (200). (410, 440) for converting the pressure into velocity energy to expand the refrigerant under reduced pressure, and the nozzle (41).
0, 440) and the refrigerant (300) that is injected from the refrigerant.
An ejector (400) having a booster section (420, 430) for boosting the pressure of the refrigerant by converting velocity energy into pressure energy while mixing with the refrigerant sucked from the
And separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, supplying the gas-phase refrigerant to the suction side of the compressor (100), and supplying the liquid-phase refrigerant to the evaporator (300). The nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage, and the throat portion (41).
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), 420, 430) minimum equivalent diameter (D2)
The ratio of the length (L) of the pressure boosting section (420, 430) to 120 is 120 or less, and the pressure boosting section (423) has a substantially constant refrigerant passage cross-sectional area from the refrigerant flow upstream side to the refrigerant flow side. An ejector cycle characterized by being configured as follows. 15. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and pressure energy of the high-pressure refrigerant flowing out from the radiator (200). (410, 440) for converting the pressure into velocity energy to expand the refrigerant under reduced pressure, and the nozzle (41).
0, 440) and the refrigerant (300) that is injected from the refrigerant.
An ejector (400) having a booster section (420, 430) for boosting the pressure of the refrigerant by converting velocity energy into pressure energy while mixing with the refrigerant sucked from the
And separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, supplying the gas-phase refrigerant to the suction side of the compressor (100), and supplying the liquid-phase refrigerant to the evaporator (300). The nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage, and the throat portion (41).
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), 420, 430) minimum equivalent diameter (D2)
The ratio of the length (L) of the pressure boosting section (420, 430) to 120 is 120 or less, and the pressure boosting section (423) has a refrigerant passage cross-sectional area increasing from the refrigerant flow upstream side toward the downstream side. An ejector cycle characterized by being configured. 16. The spread angle (θd) of the booster section (423) is 4 ° or less.
5. The ejector cycle according to item 5. 17. The ejector cycle according to claim 14, wherein the nozzle (440) is composed of a nozzle group including a plurality of nozzles (410). 18. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and pressure energy of the high-pressure refrigerant flowing out from the radiator (200). (410, 440) for converting the pressure into velocity energy to expand the refrigerant under reduced pressure, and the nozzle (41).
0, 440) and the refrigerant (300) that is injected from the refrigerant.
An ejector (400) having a booster section (420, 430) for boosting the pressure of the refrigerant by converting velocity energy into pressure energy while mixing with the refrigerant sucked from the
And separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, supplying the gas-phase refrigerant to the suction side of the compressor (100), and supplying the liquid-phase refrigerant to the evaporator (300). The nozzle (410) has a throat portion (410a) with the smallest passage area in the middle of the passage, and the throat portion (41).
0a) to the outlet of the nozzle (410), the dimension (B) is larger than the dimension (A) from the portion where the passage cross-sectional area starts to decrease to the throat (410a), 420, 430) minimum equivalent diameter (D2)
The ratio of the length (L) of the booster section (420, 430) to 120 is 120 or less, and the booster section (423) has a shape such that the refrigerant changes substantially isentropically from the refrigerant inlet side to the refrigerant outlet side. The ejector cycle is characterized by. 19. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
A nozzle (410) for converting pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure; and separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to generate a refrigerant. A gas-liquid separator (500) for storing, and a refrigerant injection port (410a, 411) of the nozzle (410).
By connecting the a) side to the gas-liquid separation (500), the nozzle (4
10) while sucking the vapor phase refrigerant evaporated in the evaporator (300) by the high speed refrigerant flow injected from
An ejector cycle characterized by increasing the pressure of the refrigerant by converting velocity energy into pressure energy while mixing the sucked refrigerant and the refrigerant ejected from the nozzle (410). 20. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
A nozzle (410) for converting pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure; and a refrigerant injection port (410a, 411) of the nozzle (410).
a) connected to the side a) to suck the vapor-phase refrigerant evaporated in the evaporator (300) by the high-speed refrigerant flow jetted from the nozzle (410), and from the sucked refrigerant and the nozzle (410). A mixing section (420) for mixing the injected refrigerant, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant and storing the refrigerant, the refrigerant of the mixing section (420). At the outlet side, the gas-liquid separation (5
00), and the gas-liquid separation (500)
An ejector cycle in which the velocity energy of the refrigerant flowing out of the mixing section (420) is converted into pressure energy to increase the pressure of the refrigerant. 21. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100), an evaporator (300) for evaporating the refrigerant and absorbing heat, and pressure energy of the high-pressure refrigerant flowing out from the radiator (200). From the evaporator (300) by a first nozzle (410) for converting the energy into velocity energy to expand the refrigerant under reduced pressure, and a refrigerant disposed in the first nozzle (410) and ejected from the first nozzle (410). A second nozzle (411) that sucks and ejects, and a refrigerant that ejects from the first nozzle (410) and a refrigerant that ejects from the second nozzle (411) are mixed to convert velocity energy into pressure energy. A pressure increasing unit (42) for increasing the pressure of the refrigerant.
0, 430), and a refrigerant that separates the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, and supplies the gas-phase refrigerant to the suction side of the compressor (100) to form a liquid phase. A gas-liquid separator (500) for supplying a refrigerant to the evaporator (300), and the refrigerant injection ports (410a, 411a) of the first and second nozzles (410, 411) are located at the ejector (4).
00), the ejector cycle is provided at substantially the same position in the refrigerant flow path. 22. A compressor (100) for sucking and compressing a refrigerant.
A radiator (200) for cooling the refrigerant discharged from the compressor (100); and an evaporator (300) for evaporating the refrigerant to exert a refrigerating capacity.
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, In the ejector (400), the refrigerant is diffused by the diffuser (430) after the flow velocity of the suction flow and the flow velocity of the drive flow become substantially the same in the mixing section (420). Ejector cycle, characterized in that it is configured to flow into. 23. An ejector cycle in which the refrigerant pressure on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, wherein the compressor (100) sucks and compresses the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, The ejector (400) is the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 50.
The ejector cycle is characterized in that it is configured to be at least%. 24. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, The ejector (400) is the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 55.
%, And 80% or less. 25. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, The ejector (400) is the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 30.
The ejector cycle is characterized in that it is configured to be at least%. 26. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, The ejector (400) is the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
%, And 80% or less. 27. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 55.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, and further, the equivalent diameter (D1) of the outlet of the nozzle (410)
The ejector cycle characterized in that the ratio (D2 / D1) of the minimum equivalent diameter (D2) of the pressure boosting section (420, 430) to 1.05 or more and 10 or less. 28. An ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, and further, the equivalent diameter (D1) of the outlet of the nozzle (410)
Of the equivalent diameter (D2) of the mixing part to (D2 / D
The ejector cycle characterized in that 1) is 1.05 or more and 10 or less. 29. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, The ejector (400) is the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, and further, the equivalent diameter (D1) of the outlet of the nozzle (410)
Of the equivalent diameter (D2) of the mixing part to (D2 / D
The ejector cycle characterized in that 1) is 1.05 or more and 10 or less. 30. An ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, wherein the compressor (100) sucks and compresses the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). A mixing section (420) for sucking the vapor phase refrigerant evaporated at (300) and mixing the sucked suction flow with the driving flow ejected from the nozzle (410), and a refrigerant flowing out of the mixing section (420). An ejector (400) having a diffuser (430) for converting velocity energy into pressure energy, and a gas-liquid separator (500) for separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant to store the refrigerant, The ejector (400) is the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, and using Freon as a refrigerant, the nozzle (41
3. The ratio (D2 / D1) of the equivalent diameter (D2) of the mixing section to the equivalent outlet diameter (D1) of (0) is 1.05 or more;
An ejector cycle characterized by being 5 or less. 31. An ejector cycle in which the refrigerant pressure on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, wherein the compressor (100) sucks and compresses the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 55.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
The ejector cycle is 0 or less, and the spread angle (θd) of the diffuser (430) is 0.2 degrees or more and 34 degrees or less. 32. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
The ejector cycle is 0 or less, and the spread angle (θd) of the diffuser (430) is 0.2 degrees or more and 34 degrees or less. 33. An ejector cycle in which the refrigerant pressure on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and the heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 55.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
The ejector cycle is 0 or less, and the spread angle (θd) of the diffuser (430) is 0.2 degrees or more and 7 degrees or less. 34. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
The ejector cycle is 0 or less, and the spread angle (θd) of the diffuser (430) is 0.2 degrees or more and 7 degrees or less. 35. An ejector cycle in which the refrigerant pressure on the high-pressure side is equal to or higher than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 55.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, the mixing unit (420) and the diffuser (430)
The ejector cycle is characterized in that the refrigerant passage cross-sectional area from the upstream side to the downstream side of the refrigerant flow is substantially constant. 36. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, the mixing unit (420) and the diffuser (430)
The ejector cycle is characterized in that the refrigerant passage cross-sectional area from the upstream side to the downstream side of the refrigerant flow is substantially constant. 37. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, the mixing unit (420) and the diffuser (430)
The ejector cycle is characterized in that the refrigerant passage cross-sectional area increases from the refrigerant flow upstream side toward the downstream side. 38. An ejector cycle in which the refrigerant pressure on the high-pressure side is less than the critical pressure of the refrigerant, wherein the compressor (100) sucks and compresses the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, the mixing unit (420) and the diffuser (430)
The ejector cycle is characterized in that the refrigerant passage cross-sectional area increases from the refrigerant flow upstream side toward the downstream side. 39. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, the mixing unit (420) and the diffuser (430)
Is an ejector cycle characterized in that the refrigerant is shaped so as to change substantially isentropically from the refrigerant inlet side to the refrigerant outlet side. 40. An ejector cycle in which the pressure of the refrigerant on the high-pressure side is less than the critical pressure of the refrigerant, the compressor (100) sucking and compressing the refrigerant, and heat radiation for cooling the refrigerant discharged from the compressor (100). Device (200) and evaporator (300) that exhibits refrigerating capacity by evaporating a refrigerant
And a nozzle (410) for converting the pressure energy of the high-pressure refrigerant flowing out of the radiator (200) into velocity energy to expand the refrigerant under reduced pressure, and the evaporator with a high-velocity refrigerant flow injected from the nozzle (410). The mixing section (420) for sucking the vapor phase refrigerant evaporated in (300), the refrigerant injected from the nozzle (410) and the evaporator (30).
Ejector (400) having a diffuser (430) for converting velocity energy into pressure energy and increasing the pressure of the refrigerant while mixing with the refrigerant sucked from 0).
And a gas-liquid separator (500) that stores the refrigerant by separating the refrigerant into a gas-phase refrigerant and a liquid-phase refrigerant, and the ejector (400) includes the ejector (40).
0) to the total boost amount (ΔP) at the mixing section (42
The ratio (ΔPm / ΔP) of the boosting amount (ΔPm) at 0) is 35.
% Or more and 80% or less, and the ratio (L / D2) of the length (L) of the mixing section (420) to the equivalent diameter (D2) of the mixing section (420) is 12
0 or less, the mixing unit (420) and the diffuser (430)
Is an ejector cycle characterized in that the refrigerant is shaped so as to change substantially isentropically from the refrigerant inlet side to the refrigerant outlet side.