Gas-liquid separator and method for determining taper angle of gas-liquid separator

Abstract

The invention discloses a gas-liquid separator and a taper angle determination method thereof. The gas-liquid separator comprises a shell, a heat insulation barrel, a low-pressure pipeline and a high-pressure pipeline. The heat insulation barrel divides a shell cavity of the shell into an inner cavity and an outer cavity, and the heat insulation barrel is in a big-end-up conical shape; a vent hole is formed in the top of the heat-insulating cylinder, the upper ends of the inner cavity and the outer cavity are communicated through the vent hole, and the lower ends of the inner cavity and the outer cavity are communicated through a lower port of the heat-insulating cylinder; the low-pressure pipeline comprises a low-pressure inlet section, a first low-pressure pipe section and a second low-pressure pipe section which are connected in sequence, the first low-pressure pipe section is of a spiral structure and located in the heat insulation barrel, and the second low-pressure pipe section is of a spiral structure and sleeves the bottom of the heat insulation barrel; the first low-pressure pipe section is provided with a liquid discharge hole; a low-pressure outlet is formed in the top of the shell; at least part of the high-pressure pipeline is located in the shell so as to exchange heat with the liquid-phase medium separated through the low-pressure pipeline. The gas-liquid separator can perform heat exchange on the collected liquid phase refrigerant, so that the supercooling degree of the heat management system can be improved, and the refrigerating capacity is increased.

Description

Technical Field

[0001] The present application relates to the field of thermal management technology, and in particular to a gas-liquid separator and a method for determining a taper angle thereof. Background Art

[0002] In refrigeration and air conditioning systems, under certain working conditions, when the system's superheat meets the requirements and has a margin, the system's subcooling is insufficient and will cause unstable noise in the system. When the cooling capacity decreases or even deteriorates, it is generally improved by increasing the indoor wind speed or increasing the compressor speed, but this method will increase additional energy consumption and reduce the system's COP (Coefficient of Performance).

[0003] How to improve the above problems is a technical problem that technicians in this field currently need to solve. Summary of the invention

[0004] The purpose of this application is to provide a gas-liquid separator and a method for determining its taper angle. By optimizing the structure of the gas-liquid separator, the gas-liquid separator can exchange heat with the collected liquid-phase refrigerant, thereby improving the supercooling of the thermal management system, increasing the cooling capacity, and achieving a noise reduction effect.

[0005] In order to solve the above technical problems, the present application provides a gas-liquid separator, comprising a shell, a heat-insulating cylinder, a low-pressure pipeline and a high-pressure pipeline;

[0006] The heat-insulating cylinder divides the shell cavity of the outer shell into an inner cavity and an outer cavity, the outer cavity surrounds the inner cavity, the heat-insulating cylinder is in a conical shape with a larger upper portion and a smaller lower portion, and a lower port is provided at the lower end of the heat-insulating cylinder; a vent hole is provided at the top of the heat-insulating cylinder, the upper ends of the inner cavity and the outer cavity are connected through the vent hole, and the lower ends of the inner cavity and the outer cavity are connected through the lower port of the heat-insulating cylinder:

[0007] The low-pressure pipeline includes a low-pressure inlet section, a first low-pressure pipe section and a second low-pressure pipe section connected in sequence, the low-pressure inlet section is connected to an external pipeline, the first low-pressure pipe section is a spiral structure and is located in the insulation cylinder, the second low-pressure pipe section is a spiral structure and is jacketed on the bottom of the insulation cylinder; the first low-pressure pipe section has a drainage hole; the top of the shell is provided with a low-pressure outlet;

[0008] At least a portion of the high-pressure pipeline is located in the shell for heat exchange with the liquid medium separated by the low-pressure pipeline.

[0009] During use of the gas-liquid separator, a gas-liquid two-phase low-pressure refrigerant flows in through the low-pressure inlet section of the low-pressure pipeline, and a high-pressure liquid-phase refrigerant can flow in the high-pressure pipeline. After the gas-liquid two-phase low-pressure refrigerant enters the low-pressure pipeline, because the first low-pressure pipe section located on the inner side of the thermal insulation cylinder has a spiral structure, when the gas-liquid two-phase low-pressure refrigerant passes through the first low-pressure pipe section, under the action of centrifugal force, the liquid phase medium can be discharged from the drain hole, and the discharged liquid phase medium can flow downward along the inner wall of the thermal insulation cylinder, and be discharged through the lower port of the thermal insulation cylinder under the action of gravity and gather in the outer cavity. In this process, the gas phase medium flows along the first low-pressure pipe section to the bottom of the first low-pressure pipe section, and then flows along the second low-pressure pipe section located on the outer side of the thermal insulation cylinder, and can be discharged from the second low-pressure pipe section. The discharged gas phase medium can flow upward and be discharged through the low-pressure outlet located at the top of the outer shell, thereby achieving a gas-liquid separation effect.

[0010] A high-pressure pipeline is also provided in the gas-liquid separator, and at least part of the high-pressure pipeline is located in the outer shell. The liquid medium discharged through the low-pressure pipeline, for example, the liquid medium accumulated in the outer cavity can exchange heat with the high-pressure liquid refrigerant flowing through the high-pressure pipeline. The high-pressure liquid refrigerant flowing in the high-pressure pipeline can heat the liquid medium after gas-liquid separation. The liquid medium after gas-liquid separation is a saturated liquid refrigerant. In this way, the overall heat exchange capacity can be increased and the supercooling degree of the outlet of the high-pressure pipeline of the gas-liquid separator can be increased. At the same time, the separated liquid medium in the gas-liquid separator can be discharged as a gas phase after heat exchange with the high-pressure pipeline, so that the liquid storage amount in the gas-liquid separator is reduced, which is beneficial to improve the refrigerant mass flow rate of the entire system and to optimize the system performance.

[0011] In an optional implementation, the high-pressure pipeline includes a high-pressure inlet section, a high-pressure pipe section and a high-pressure outlet section connected in sequence, the high-pressure inlet section and the high-pressure outlet section are both connected to an external pipeline, and at least a portion of the high-pressure pipe section is located in the insulation cylinder.

[0012] In an optional implementation, the high-pressure pipe section has a spiral structure and is located inside the insulation cylinder and extends downward in a spiral along the inner wall of the insulation cylinder. The high-pressure inlet section is connected to an external pipeline, the high-pressure outlet section is connected to an external pipeline, and the first low-pressure pipe section is located on the inner side of the high-pressure pipe section.

[0013] In an optional implementation, the high-pressure pipe section includes a first high-pressure pipe section and a second high-pressure pipe section, the first high-pressure pipe section spirally extends downward along the inner wall of the insulation tube inside the insulation tube, and the second high-pressure pipe section is located outside the insulation tube and below the insulation tube; the high-pressure inlet section is connected to an external pipeline, and the high-pressure outlet section is connected to an external pipeline; the first low-pressure pipe section is located on the inner side of the first high-pressure pipe section.

[0014] In an optional implementation, the second high-pressure pipe section is a planar bending structure, or the second high-pressure pipe section is a three-dimensional bending structure.

[0015] In an optional implementation, the high-pressure pipeline includes a high-pressure inlet section, a high-pressure pipe section and a high-pressure outlet section connected in sequence, the high-pressure inlet section and the high-pressure outlet section are both connected to an external pipeline, and the high-pressure pipe section is located outside the insulation cylinder and below the insulation cylinder.

[0016] In an optional implementation, the high-pressure pipe section has a planar bending structure; or, the high-pressure pipe section has a three-dimensional bending structure.

[0017] In an optional implementation, the first low-pressure pipe section extends spirally downward along the inner wall of the thermal insulation cylinder, and the second low-pressure pipe section extends spirally upward along the outer wall of the thermal insulation cylinder.

[0018] In an optional implementation, the outer shell includes a cylindrical shell peripheral wall, a shell bottom wall and a shell top wall, the aperture of the upper port of the insulation cylinder is consistent with the aperture of the shell peripheral wall; the shell top wall is penetrated by a low-pressure outlet connecting pipe, and the low-pressure outlet interface has the low-pressure outlet.

[0019] In an optional implementation, there are multiple drainage holes, and the multiple drainage holes are arranged along the extension direction of the first low-pressure pipe section; the drainage holes are located below the center line of the first low-pressure pipe section and on the pipe wall of the first low-pressure pipe section facing away from the axial center line of the insulation tube.

[0020] In an optional implementation, the second low-pressure pipe section has an exhaust hole.

[0021] In an optional implementation, a plurality of exhaust holes are provided, and the plurality of exhaust holes are arranged along the extension direction of the second low-pressure pipe section. The exhaust holes are located above the center line of the second low-pressure pipe section and on the pipe wall of the second low-pressure pipe section facing the axial center line of the gas-liquid separator.

[0022] In an optional implementation, the ratio of the axial height of the second low-pressure pipe section to the axial height of the first low-pressure pipe section is 0.1 to 0.25; and / or the radial distance between the first low-pressure pipe section and the second low-pressure pipe section is 3 to 5 times the diameter of the low-pressure pipeline; and / or the ratio of the pipe length of the first low-pressure pipe section to the sum of the pipe length of the first low-pressure pipe section and the pipe length of the second low-pressure pipe section is 0.75 to 0.95.

[0023] The present application also provides a method for determining the taper angle of a gas-liquid separator, wherein the gas-liquid separator is any one of the gas-liquid separators described above, the taper angle is the taper angle α of the first low-pressure pipe section, the taper angle α of the first low-pressure pipe section has a set value range, within the value range, the comprehensive performance coefficient Z of the first low-pressure pipe section is selected * The taper angle corresponding to the maximum value of is the optimal taper angle actually set for the first low-pressure pipe section;

[0024] The comprehensive performance coefficient Z of the first low-pressure pipe section * By formula Z * =a * / f * Sure;

[0025] Among them, a * is the equivalent dimensionless centrifugal force of the first low-pressure pipe section, f * is the equivalent dimensionless friction coefficient of the first low-pressure pipe section.

[0026] The determination method is used to determine the taper angle of the first low-pressure pipe section of the aforementioned gas-liquid separator. The determination of the taper angle can enable the gas-liquid separator to have a relatively better gas-liquid separation effect.

[0027] In an optional implementation, the equivalent dimensionless centrifugal force a of the first low-pressure pipe section is * Determined by the following formula:

[0028] a * =k1·u l 2 / (g·D eq / 2);

[0029] u l =G(1-x) / (ρ l (1-∈));

[0030]

[0031] G=4q / (π·d i 2 );

[0032] D eq =2 / (1 / D min +1 / D max ), D min =D max -2·H·tan(α / 2);

[0033] Among them, k1 is the correction coefficient, u l is the velocity of the liquid medium, D eqis the equivalent spiral diameter of the first low-pressure pipe section, G is the flow density of the refrigerant, x is the dryness at the inlet of the gas-liquid separator, ρ l is the density of the liquid medium, ∈ is the refrigerant porosity, ρ g is the density of the gas phase medium, σ is the surface tension of the refrigerant, q is the mass flow rate of the refrigerant, d i is the inner diameter of the first low-pressure pipe section, D max is the maximum spiral diameter of the first low-pressure pipe section, D min is the minimum spiral diameter of the first low-pressure pipe section, and H is the axial height of the first low-pressure pipe section.

[0034] In an optional implementation, k1 = 1.125-0.065n, n = H / s,

[0035] Among them, n is the equivalent number of spiral turns of the first low-pressure pipe section, s is the equivalent spiral pitch of the first low-pressure pipe section, ω is the ratio of the tube length of the first low-pressure pipe section to the sum of the tube length of the first low-pressure pipe section and the tube length of the second low-pressure pipe section, and L is the sum of the tube length of the first low-pressure pipe section and the tube length of the second low-pressure pipe section.

[0036] In an optional implementation, the equivalent dimensionless friction coefficient f of the first low-pressure pipe section is * Determined by the following formula:

[0037]

[0038] Re=ρud i / μ;

[0039] u=G / ρ;

[0040] Where Re is the Reynolds number, ρ is the homogeneous density, μ is the homogeneous viscosity, u is the homogeneous velocity, μ g is the viscosity of the gas phase medium, μ l is the viscosity of the liquid medium.

[0041] In an optional implementation, the equivalent dimensionless friction coefficient f * It is determined according to the following formula:

[0042] Where k is a constant.

[0043] In an optional implementation, when the value of the taper angle α of the first low-pressure pipe section corresponding to the equivalent number of spiral turns n of the first low-pressure pipe section is greater than a preset value, the value of the taper angle α is excluded; and,

[0044] The equivalent spiral pitch s of the first low-pressure pipe section corresponding to the taper angle α of the first low-pressure pipe section is smaller than the inner diameter d of the first low-pressure pipe section. i , the value of the taper angle α is also excluded.

[0045] In an optional implementation, the taper angle α has a value range of α min ≤α<α max , α min =25°, α max =2·arctan(D max / (2·H));

[0046] Among them, D max is the maximum spiral diameter of the first low-pressure pipe section, and H is the axial height of the first low-pressure pipe section. BRIEF DESCRIPTION OF THE DRAWINGS

[0047] Figure 1 This is a schematic structural diagram of the first embodiment of the gas-liquid separator provided in this application;

[0048] Figure 2 for Figure 1 A perspective view of the gas-liquid separator shown;

[0049] Figure 3 for Figure 1 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden;

[0050] Figure 4 for Figure 3 The structural diagram of the low-pressure pipeline of the gas-liquid separator;

[0051] Figure 5 for Figure 3 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator;

[0052] Figure 6 This is a schematic structural diagram of a second embodiment of the gas-liquid separator provided in this application;

[0053] Figure 7 for Figure 6 A perspective view of the gas-liquid separator shown;

[0054] Figure 8 for Figure 6 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden;

[0055] Fig. 9 for Figure 8 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator;

[0056] Fig.10 for Fig. 9A schematic diagram of the structure of the heat insulation cylinder and the high-pressure pipeline shown in another perspective;

[0057] Fig.11 A schematic structural diagram of a third embodiment of the gas-liquid separator provided in this application;

[0058] Fig.12 for Fig.11 A perspective view of the gas-liquid separator shown;

[0059] Fig.13 for Fig.11 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden;

[0060] Fig.14 for Fig.13 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator;

[0061] Fig.15 for Fig.14 A cross-sectional schematic diagram of the heat insulation cylinder and the high-pressure pipeline shown;

[0062] Fig.16 This is a schematic structural diagram of a fourth embodiment of the gas-liquid separator provided in the present application;

[0063] Fig.17 for Fig.16 A perspective view of the gas-liquid separator shown;

[0064] Fig.18 for Fig.16 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden;

[0065] Fig.19 for Fig.18 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator;

[0066] Fig. 20 for Fig.19 A schematic diagram of the structure of the heat insulation cylinder and the high-pressure pipeline shown in another perspective;

[0067] Fig.21 A structural block diagram of an embodiment of the thermal management system provided by the present application;

[0068] Fig. 22 for Fig.21 A comparison diagram of enthalpy difference between the thermal management system shown and the conventional thermal management system;

[0069] Fig.23 This is a simplified model diagram of the internal structure of the shell of the gas-liquid separator provided in this application.

[0070] Description of reference numerals:

[0071] Shell 10, shell peripheral wall 11, shell top wall 12, shell bottom wall 13, inner cavity 101, outer cavity 102;

[0072] Insulation tube 20, vent hole 21;

[0073] Low-pressure pipeline 30, low-pressure inlet section 31, first low-pressure pipe section 32, drainage hole 321, second low-pressure pipe section 33, exhaust port 331, low-pressure outlet pipe 34;

[0074] High-pressure pipeline 40 , high-pressure inlet section 41 , high-pressure pipe sections 42A, 42B, 42C, 42D, first high-pressure pipe sections 421C, 421D, second high-pressure pipe sections 422C, 422D, and high-pressure outlet section 43 . DETAILED DESCRIPTION

[0075] An embodiment of the present application provides a gas-liquid separator. Through structural optimization, a heat exchange pipeline is integrated in the gas-liquid separator so that the gas-liquid separator can exchange heat with the collected liquid-phase refrigerant, thereby improving the supercooling degree of the thermal management system using the gas-liquid separator, thereby increasing the cooling capacity and reducing noise.

[0076] The gas-liquid separator provided in the embodiment of the present application includes a shell, an insulation cylinder, a low-pressure pipeline and a high-pressure pipeline. The insulation cylinder separates the shell cavity of the shell into an inner cavity and an outer cavity, the outer cavity surrounds the inner cavity, the insulation cylinder is in a conical shape with a large top and a small bottom, and a lower port is provided at the lower end of the insulation cylinder; a vent is provided at the top of the insulation cylinder, the upper ends of the inner cavity and the outer cavity are connected through the vent, and the lower ends of the inner cavity and the outer cavity are connected through the lower port of the insulation cylinder. The low-pressure pipeline includes a low-pressure inlet section, a first low-pressure pipe section and a second low-pressure pipe section connected in sequence, the low-pressure inlet section is connected to an external pipeline, the first low-pressure pipe section is a spiral structure and is located in the insulation cylinder, the second low-pressure pipe section is a spiral structure and is jacketed at the bottom of the insulation cylinder; the first low-pressure pipe section has a drainage hole; and a low-pressure outlet is provided at the top of the shell. At least part of the high-pressure pipeline is located in the shell for heat exchange with the liquid medium separated by the low-pressure pipeline.

[0077] During use of the gas-liquid separator, a gas-liquid two-phase low-pressure refrigerant flows in through the low-pressure inlet section of the low-pressure pipeline, and a high-pressure liquid-phase refrigerant can flow in the high-pressure pipeline. After the gas-liquid two-phase low-pressure refrigerant enters the low-pressure pipeline, because the first low-pressure pipe section located on the inner side of the thermal insulation cylinder has a spiral structure, when the gas-liquid two-phase low-pressure refrigerant passes through the first low-pressure pipe section, under the action of centrifugal force, the liquid phase medium can be discharged from the drain hole, and the discharged liquid phase medium can flow downward along the inner wall of the thermal insulation cylinder, and be discharged through the lower port of the thermal insulation cylinder under the action of gravity and gather in the outer cavity. In this process, the gas phase medium flows along the first low-pressure pipe section to the bottom of the first low-pressure pipe section, and then flows along the second low-pressure pipe section located on the outer side of the thermal insulation cylinder, and can be discharged from the second low-pressure pipe section. The discharged gas phase medium can flow upward and be discharged through the low-pressure outlet located at the top of the outer shell, thereby achieving a gas-liquid separation effect.

[0078] The gas-liquid separator is also provided with a high-pressure pipeline, at least part of which is located in the shell. The liquid medium discharged through the low-pressure pipeline, for example, the liquid medium gathered in the outer cavity can be heat-exchanged with the high-pressure liquid refrigerant flowing through the high-pressure pipeline. The high-pressure liquid refrigerant flowing in the high-pressure pipeline can heat the liquid medium after gas-liquid separation. The liquid medium after gas-liquid separation is a saturated liquid refrigerant. In this way, the overall heat exchange capacity can be increased, and the supercooling degree of the outlet of the high-pressure pipeline of the gas-liquid separator can be increased. At the same time, the separated liquid medium in the gas-liquid separator can be discharged as a gas phase medium after heat exchange with the high-pressure pipeline, so that the liquid storage amount in the gas-liquid separator is reduced, which is beneficial to improving the refrigerant mass flow of the entire system and optimizing the system performance. In general, the structural setting of the above-mentioned gas-liquid separator can improve the supercooling degree, increase the cooling capacity, and make the system have a better noise reduction effect.

[0079] In the above-mentioned gas-liquid separator, there can be a variety of specific implementation methods according to the setting of the high-pressure pipeline. In order to enable personnel in this technical field to better understand the application scheme, the application is further described in detail below in conjunction with the drawings and specific implementation methods.

[0080] Please refer to Figures 1 to 5 , Figure 1 This is a schematic structural diagram of the first embodiment of the gas-liquid separator provided in this application; Figure 2 for Figure 1 A perspective view of the gas-liquid separator shown; Figure 3 for Figure 1 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden; Figure 4 for Figure 3 The structural diagram of the low-pressure pipeline of the gas-liquid separator; Figure 5 for Figure 3 Schematic diagram of the structure of the insulation cylinder and high-pressure pipeline of the gas-liquid separator.

[0081] In this embodiment, the gas-liquid separator includes a housing 10 , a heat-insulating cylinder 20 , a low-pressure pipeline 30 and a high-pressure pipeline 40 .

[0082] In a specific implementation, the housing 10 may include a cylindrical housing peripheral wall 11 , a housing top wall 12 and a housing bottom wall 13 , and the housing top wall 12 and the housing bottom wall 13 respectively block the upper end opening and the lower end opening of the housing peripheral wall 11 .

[0083] In this embodiment, the heat-insulating cylinder 20 is disposed in the shell cavity of the outer shell 10. The heat-insulating cylinder 20 is in a conical shape with a larger upper portion and a smaller lower portion. The heat-insulating cylinder 20 divides the shell cavity of the outer shell 10 into an inner cavity 101 and an outer cavity 102. The outer cavity 102 is disposed around the inner cavity 101. It can be understood that at least part of the inner cavity 101 is the cylinder cavity of the heat-insulating cylinder 20. The upper and lower ends of the heat-insulating cylinder 20 are connected, and the lower end of the heat-insulating cylinder 20 is connected to the outer cavity 102. In this way, the inner cavity 101 and the outer cavity 102 can be connected through the lower end of the heat-insulating cylinder 20.

[0084] In this embodiment, the low-pressure pipeline 30 includes a low-pressure inlet section 31, a first low-pressure pipe section 32 and a second low-pressure pipe section 33 which are connected in sequence.

[0085] Among them, the low-pressure inlet section 31 is connected with the external pipeline. Specifically, one end of the low-pressure inlet section 31 can pass through the top of the outer shell 10 to facilitate the connection of the external pipeline. The other end of the low-pressure inlet section 31 passes through the insulation tube 20 and is connected to the first low-pressure pipe section 32 in the insulation tube 20. The first low-pressure pipe section 32 has a spiral structure in the insulation tube 20. One end of the first low-pressure pipe section 32 located at the lower end of the insulation tube 20 is connected to the second low-pressure pipe section 33. The second low-pressure pipe section 33 has a spiral structure outside the insulation tube 20. The second low-pressure pipe section 33 is outermost at the bottom of the insulation tube 20. The end of the second low-pressure pipe section 33 that is not connected to the first low-pressure pipe section 32 can be connected to the outer cavity 102.

[0086] Exemplarily, the first low-pressure pipe section 32 may extend spirally downward along the inner wall of the insulation tube 20 to form a conical spiral structure, and the second low-pressure pipe section 33 may extend spirally upward along the outer wall of the insulation tube 20 to form a conical spiral structure.

[0087] The above-mentioned structural form of the first low-pressure pipe section 32 is conducive to achieving gas-liquid separation. When the gas-liquid two-phase low-pressure refrigerant flows in the first low-pressure pipe section 32, the liquid phase medium will be thrown to the pipe wall portion of the first low-pressure pipe section 32 away from the axial center line of the insulation tube 20 under the action of centrifugal force, and the gas phase medium will gather in the pipe wall portion of the first low-pressure pipe section 32 close to the axial center line of the insulation tube 20 and flow along the first low-pressure pipe section 32 to the second low-pressure pipe section 33. In order to facilitate the discharge of the separated liquid phase medium and gas phase medium, a drainage hole 321 is provided on the first low-pressure pipe section 32, and an exhaust hole 331 is provided on the second low-pressure pipe section 33.

[0088] In one implementation, a plurality of drainage holes 321 may be provided, and the plurality of drainage holes 321 are arranged along the extension direction of the first low-pressure pipe section 32, so that the liquid phase medium thrown onto the wall of the first low-pressure pipe section 32 can be discharged in time, which can reduce the secondary entrainment phenomenon and is beneficial to improving the gas-liquid separation efficiency.

[0089] Specifically, the drainage hole 321 is located below the center line of the first low-pressure pipe section 32 and on the pipe wall of the first low-pressure pipe section 32 facing away from the axial center line of the heat-insulating cylinder 20. In other words, the drainage hole 321 is arranged as far as possible on the path where the liquid phase medium is thrown toward the pipe wall under the action of centrifugal force, which is more conducive to the discharge of the separated liquid phase medium as soon as possible and is also more conducive to reducing the secondary entrainment phenomenon.

[0090] In one implementation, a plurality of exhaust holes 331 may be provided, and the plurality of exhaust holes 331 are arranged along the extension direction of the second low-pressure pipe section 33. The exhaust holes 331 are located above the center line of the second low-pressure pipe section 33 and on the pipe wall of the second low-pressure pipe section 33 facing the axial center line of the gas-liquid separator. During the gas-liquid separation process, the gas phase medium will gather on one side close to the axial center line of the isolation tube 20, and the gas phase medium has an upward flow characteristic. The exhaust holes 331 are arranged as above, which is more conducive to the discharge of the gas phase medium and is conducive to improving the gas-liquid separation effect.

[0091] The gas-liquid separator in this embodiment mainly uses the high-pressure pipeline 40 to heat the low-pressure liquid phase refrigerant, so the axial height and length of the second low-pressure pipe section 33 should not be set too large. In practical applications, the relevant parameter ratios can be determined based on experiments or simulations.

[0092] In a specific implementation, the axial height of the first low-pressure pipe section 32 can be as close as possible to the axial height of the heat-insulating tube 20, and the axial height of the second low-pressure pipe section 33 can be set smaller, and the outer sleeve can be placed on the bottom area of ​​the heat-insulating tube 20. In the illustrated example, the second low-pressure pipe section 33 surrounds the outside of the heat-insulating tube 20 for approximately two circles, and the diameter of the circle close to the bottom is smaller than the diameter of the circle far from the bottom, which can also be understood as a conical shape.

[0093] Specifically, the ratio of the axial height of the second low-pressure pipe section 33 to the axial height of the first low-pressure pipe section 32 may be in the range of 0.1 to 0.25.

[0094] Specifically, the radial distance between the first low-pressure pipe section 32 and the second low-pressure pipe section 33 (referring to the radial distance at the same height position in the axial direction) is 3 to 5 times the diameter of the low-pressure pipeline 30 .

[0095] Specifically, the ratio of the tube length of the first low-pressure tube section 32 to the sum of the tube length of the first low-pressure tube section 32 and the tube length of the second low-pressure tube section 33 may be in the range of 0.75 to 0.95.

[0096] In a specific implementation, the low-pressure inlet section 31, the first low-pressure pipe section 32 and the second low-pressure pipe section 33 can be wound by a single pipe, or can be arranged in sections and then fixed.

[0097] In a specific implementation, the low-pressure inlet section 31 of the low-pressure pipeline 30 passes through the upper end of the shell peripheral wall 11 close to the shell top wall 12 .

[0098] In this embodiment, a low-pressure outlet is provided at the top of the housing 10 to facilitate the discharge of the low-pressure gas phase medium after gas-liquid separation. In a specific implementation, the low-pressure pipeline 30 also includes a low-pressure outlet pipe 34, which is passed through the top of the housing 10 and has the aforementioned low-pressure outlet.

[0099] In a specific implementation, the low-pressure outlet pipe 34 can be fixedly inserted into the shell top wall 12 of the shell 10, and part of the low-pressure outlet pipe 34 extends into the shell 10, and part of it is located outside the shell 10 to facilitate external piping. The end of the low-pressure outlet pipe 34 located inside the shell 10 can be set to a flared bell mouth form to facilitate the discharge of the gas phase medium.

[0100] In a specific implementation, the aperture of the upper port of the insulation tube 20 can be consistent with the aperture of the shell peripheral wall 11 of the outer shell 10, so that the upper end of the outer cavity 102 separated by the insulation tube 20 will not be connected to the insulation tube 20. In order to facilitate the discharge of the gas phase medium in the outer cavity 102 through the low-pressure outlet pipe 34, at this time, the top of the insulation tube 20 can be circumferentially provided with ventilation holes 21, so that the upper ends of the inner cavity 101 and the outer cavity 102 are connected through the ventilation holes 21.

[0101] In applications, a plurality of vent holes 21 may be provided, and the plurality of vent holes 21 may be evenly arranged along the circumference of the heat insulation cylinder 20 .

[0102] In specific configuration, the upper end of the heat-insulating tube 20 may be flush with the upper end of the shell peripheral wall 11 , and the axial center line of the heat-insulating tube 20 may coincide with the axial center line of the shell 10 , so as to effectively utilize the space.

[0103] In this embodiment, the high-pressure pipeline 40 includes a high-pressure inlet section 41, a high-pressure pipe section 42A and a high-pressure outlet section 43 connected in sequence; wherein, the high-pressure inlet section 41 and the high-pressure outlet section 43 are both connected to an external pipeline. In a specific implementation, the high-pressure inlet section 41 and the high-pressure outlet section 43 can both pass through the housing 10, and the high-pressure pipe section 42A is located in the housing 10. That is, one end of the high-pressure inlet section 41 extends out of the housing 10 to facilitate external connection to an external pipeline, and the other end is located in the housing 10 to be connected to the high-pressure pipe section 42A; one end of the high-pressure outlet section 43 extends out of the housing 10 to facilitate external connection to an external pipeline, and the other end is located in the housing 10 to be connected to the high-pressure pipe section 42A.

[0104] In this embodiment, the high-pressure pipe section 42A is entirely located outside the insulation tube 20 and below the insulation tube 20 . Specifically, the high-pressure pipe section 42A can be disposed on the bottom wall of the shell cavity of the outer shell 10 and supported by the shell bottom wall 13 .

[0105] Specifically, the high-pressure inlet section 41 and the high-pressure outlet section 43 both extend out of the housing 10 at a position close to the bottom of the housing 10. In the illustrated example, the high-pressure inlet section 41 and the high-pressure outlet section 43 both pass through the housing circumferential wall 11 of the housing 10, and in other implementations, they may also pass through the housing bottom wall 13 of the housing 10.

[0106] In one implementation, the high pressure pipe section 42A is a planar curved structure. Figure 2 , 3 As shown in Figures 5 and 6, the high-pressure pipe section 42A is generally a planar spiral structure, that is, the high-pressure pipe section 42A is wound from the inside to the outside in a plane to form a spiral structure. In order to facilitate the connection of the two ends of the high-pressure pipe section 42A with the high-pressure inlet section 41 and the high-pressure outlet section 43, the high-pressure pipe section 42A can be bent to form two parallel pipe sections, and the two parallel pipe sections are wound together from the inside to the outside. In other implementations, the high-pressure pipe section 42A may not be spiral, for example, it may be bent back and forth in a serpentine shape to form a planar winding structure.

[0107] The working principle of the gas-liquid separator provided in this embodiment is as follows:

[0108] During operation, the gas-liquid two-phase low-pressure refrigerant flows into the low-pressure pipeline 30 from the low-pressure inlet section 31 near the top of the gas-liquid separator, and flows along the spiral first low-pressure pipeline section 32 of the low-pressure pipeline 30. Under the action of gravity and centrifugal force, due to the high density of the low-pressure liquid phase medium, most of it will adhere to the lower pipe wall on the outer side (away from the axial center line of the insulation tube 20) of the first low-pressure pipeline section 32, and be discharged through the drainage hole 321. Under the action of gravity, it can flow downward along the inner wall of the insulation tube 20 and be discharged from the lower port of the insulation tube 20 to the outer cavity 102, and gather at the bottom of the outer cavity 102; at the same time, due to the low density of the low-pressure gas phase medium in the first low-pressure pipeline section 32, most of it will gather on the inner wall of the first low-pressure pipeline section 32 (close to the axial center line of the insulation tube 20) and flow along the first low-pressure pipeline section 32 to the second low-pressure pipeline section 33, thereby achieving gas-liquid separation.

[0109] After the low-pressure gaseous medium flows to the second low-pressure pipe section 33 , it flows along the second low-pressure pipe section 33 , spirals upward in the second low-pressure pipe section 33 , and can be discharged through the exhaust hole 331 , or from the end port of the second low-pressure pipe section 33 .

[0110] During operation, the liquid-phase high-pressure refrigerant flows from the high-pressure inlet section 41 into the high-pressure pipe section 42A and then flows out from the high-pressure outlet section 43; the low-pressure liquid-phase medium gathered at the bottom of the outer cavity 102 after the gas-liquid separation mentioned above can exchange heat with the liquid-phase high-pressure refrigerant flowing through the high-pressure pipeline 40 arranged at the bottom of the outer cavity 102. After the heat exchange, superheated gaseous refrigerant will escape. At the same time, saturated gaseous refrigerant will also escape during the gathering process of the low-pressure liquid-phase medium after the separation mentioned above. These two parts of gaseous refrigerant are in the outer cavity 10 2 will flow upward, and after mixing with the low-pressure gaseous refrigerant discharged from the exhaust hole 331 of the second low-pressure pipe section 33 and the end port of the second low-pressure pipe section 33 after the aforementioned gas-liquid separation, it will gather in the top space outside the insulation tube 20. After mixing, these gaseous refrigerants are in a state of partial overheating as a whole. In the top space of the insulation tube 20, they can enter the interior of the insulation tube 20 through the vent hole 21 of the insulation tube 20, that is, they are gathered at the top of the inner cavity 101, and finally discharged through the low-pressure outlet pipe 34.

[0111] It can be seen from the above process that the gas-liquid separator provided in this embodiment can exchange heat for the liquid phase medium gathered after separation by optimizing its own structure to increase the supercooling of the application system. At the same time, it can reduce the liquid storage volume in the gas-liquid separator and increase the refrigerant mass flow rate of the entire system, which is beneficial to improving system performance.

[0112] Please refer to Figures 6 to 10 , Figure 6 This is a schematic structural diagram of a second embodiment of the gas-liquid separator provided in this application; Figure 7 for Figure 6 A perspective view of the gas-liquid separator shown; Figure 8 for Figure 6 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden; Fig. 9 for Figure 8 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator; Fig.10 for Fig. 9 A schematic structural diagram of the heat-insulating cylinder and the high-pressure pipeline shown in another perspective.

[0113] In this embodiment, the gas-liquid separator includes a housing 10 , a heat-insulating cylinder 20 , a low-pressure pipeline 30 and a high-pressure pipeline 40 .

[0114] The structures of the housing 10, the heat insulating tube 20 and the low-pressure pipeline 30 can refer to the aforementioned Figures 1 to 5 The first embodiment shown is understood and will not be described in detail here. Figure 4 The same is shown and no further illustration is given.

[0115] In this embodiment, the high-pressure pipeline 40 includes a high-pressure inlet section 41, a high-pressure pipe section 42B and a high-pressure outlet section 43 connected in sequence, wherein the high-pressure inlet section 41 and the high-pressure outlet section 43 also pass through the bottom of the outer shell 10, and the high-pressure pipe section 42B is also all located outside the insulation tube 20 and below the insulation tube 20, and is supported by the shell bottom wall 13 of the outer shell 10.

[0116] Different from the high-pressure pipe section 42A of the planar bending structure in the first embodiment, in this embodiment, the high-pressure pipe section 42B has a three-dimensional bending structure, which can be understood as the high-pressure pipe section 42B having at least two layers, each layer being bent, and the bending structure can be spirally wound or serpentine, etc. The figure illustrates a solution in which the high-pressure pipe section 42B has a two-layer bending structure, and in other implementations, it can also be three or more layers.

[0117] The working principle of the gas-liquid separator in this embodiment is consistent with that of the first embodiment described above, and can be understood by referring to the above, and will not be repeated here.

[0118] Please refer to Figures 11 to 15 , Fig.11 A schematic structural diagram of a third embodiment of the gas-liquid separator provided in this application; Fig.12 for Fig.11 A perspective view of the gas-liquid separator shown; Fig.13 for Fig.11 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden; Fig.14 for Fig.13 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator; Fig.15 for Fig.14 A schematic cross-sectional view of the thermal insulation cylinder and the high-pressure pipeline is shown.

[0119] In this embodiment, the gas-liquid separator includes a housing 10 , a heat-insulating cylinder 20 , a low-pressure pipeline 30 and a high-pressure pipeline 40 .

[0120] The structures of the housing 10, the heat insulating tube 20 and the low-pressure pipeline 30 can refer to the aforementioned Figures 1 to 5 The first embodiment shown is understood and will not be described in detail here. Figure 4 The same is shown and no further illustration is given.

[0121] Compared with the aforementioned first embodiment, in this embodiment, the structural arrangement of the high-pressure pipeline 40 is different. The high-pressure pipeline 40 in this embodiment is described in detail below.

[0122] The high pressure pipeline 40 in this embodiment includes a high pressure inlet section 41, a high pressure pipe section 42C and a high pressure outlet section 43 connected in sequence. The high pressure inlet section 41 and the high pressure outlet section 43 both pass through the housing 10 to facilitate connection with external pipelines.

[0123] Part of the high-pressure pipe section 42C is located inside the heat-insulating tube 20, and part of it is located outside the heat-insulating tube 20. It can be understood that part of the high-pressure pipe section 42C is located in the inner cavity 101, and part of it is located in the outer cavity 102. For the convenience of explanation, the high-pressure pipe section 42C is divided into a first high-pressure pipe section 421C and a second high-pressure pipe section 422C, wherein the first high-pressure pipe section 421C extends downward along the inner wall of the heat-insulating tube 20 in a spiral. It can be understood that the first high-pressure pipe section 421C is roughly a conical spiral structure, and the second high-pressure pipe section 422C is located outside the heat-insulating tube 20 and below the heat-insulating tube 20, and can be supported by the shell bottom wall 13; the first high-pressure pipe section 421C in a conical spiral structure in the heat-insulating tube 20 is located outside the first low-pressure pipe section 32 in a conical spiral structure.

[0124] The high-pressure inlet section 41 is connected to the first high-pressure pipe section 421C, the high-pressure outlet section 43 is connected to the second high-pressure pipe section 422C, the high-pressure inlet section 41 is in communication with an external pipeline, specifically, it can pass through the top of the shell 10, and the high-pressure outlet section 43 is in communication with an external pipeline, specifically, it can pass through the bottom of the shell 10. Specifically, the high-pressure inlet section 41 passes through the top of the shell peripheral wall 11, and the high-pressure outlet section 43 passes through the bottom of the shell peripheral wall 11.

[0125] After the above arrangement, when the gas-liquid two-phase low-pressure refrigerant flows in the first low-pressure pipe section 32, at least a portion of the liquid medium discharged from the drainage hole 321 of the first low-pressure pipe section 32 can flow to the first high-pressure pipe section 421C, thereby exchanging heat with the high-pressure liquid-phase refrigerant flowing through the first high-pressure pipe section 421C, thereby further increasing the degree of supercooling.

[0126] In a specific implementation, the first high-pressure pipe section 421C can be arranged to fit the wall of the heat-insulating pipe 20 as closely as possible to ensure that the liquid medium separated by the first low-pressure pipe section 32 can fully exchange heat with the first high-pressure pipe section 421C.

[0127] In this embodiment, the second high-pressure pipe section 422C located at the bottom of the housing 10 is a planar bending structure, and the bending form can be a spiral bending form or a serpentine bending form.

[0128] The working principle of the gas-liquid separator provided in this embodiment is as follows:

[0129] During operation, the gas-liquid two-phase low-pressure refrigerant flows into the low-pressure pipeline 30 from the low-pressure inlet section 31 near the top of the gas-liquid separator, and the liquid-phase high-pressure refrigerant flows in from the high-pressure inlet section 41 near the top, and flows through the first high-pressure pipe section 421C and the second high-pressure pipe section 422C of the high-pressure pipe section 42C in turn, and then flows out from the high-pressure outlet section 43.

[0130] The gas-liquid two-phase low-pressure refrigerant flows along the spiral first low-pressure pipe section 32 of the low-pressure pipeline 30. Under the action of gravity and centrifugal force, most of the low-pressure liquid phase medium will adhere to the outer side of the first low-pressure pipe section 32 (the side away from the axial center line of the insulation tube 20) and the lower pipe wall, and then be discharged through the drainage hole 321. Most of it can flow to the first high-pressure pipe section 421C and exchange heat with the liquid-phase high-pressure refrigerant flowing through the first high-pressure pipe section 421C. The heat exchange formed Part of the gaseous refrigerant rises, and the liquid medium retained on the first high-pressure pipe section 421C flows downward under the action of gravity and is discharged from the lower port of the insulation tube 20 to the outer cavity 102, and gathers at the bottom of the outer cavity 102; at the same time, the low-pressure gas medium in the first low-pressure pipe section 32 has a smaller density, and most of it gathers on the inner side of the first low-pressure pipe section 32 (close to the axial center line of the insulation tube 20) of the pipe wall, and flows along the first low-pressure pipe section 32 to the second low-pressure pipe section 33, thereby realizing gas-liquid separation.

[0131] After the low-pressure gaseous medium flows to the second low-pressure pipe section 33 , it flows along the second low-pressure pipe section 33 , spirals upward in the second low-pressure pipe section 33 , and can be discharged through the exhaust hole 331 , or from the end port of the second low-pressure pipe section 33 .

[0132] The low-pressure liquid medium accumulated at the bottom of the outer cavity 102 after the gas-liquid separation mentioned above can be heat exchanged with the liquid-phase high-pressure refrigerant flowing through the second high-pressure pipe section 422C arranged at the bottom of the outer cavity 102. After the heat exchange, superheated gaseous refrigerant will escape. At the same time, saturated gaseous refrigerant will also escape during the accumulation process of the low-pressure liquid medium after the separation mentioned above. These two parts of gaseous refrigerant will flow upward in the outer cavity 102, and after mixing with the low-pressure gaseous refrigerant discharged from the exhaust hole 331 of the second low-pressure pipe section 33 and the end port of the second low-pressure pipe section 33 after the gas-liquid separation mentioned above, and the gaseous refrigerant formed after heat exchange with the first high-pressure pipe section 421C, they will be accumulated in the top space outside the insulation tube 20. After these gaseous refrigerants are mixed, they are in a state of being slightly overheated as a whole. They can enter the interior of the insulation tube 20 through the air vent 21 of the insulation tube 20 in the top space of the insulation tube 20, that is, they are accumulated at the top of the inner cavity 101, and finally discharged through the low-pressure outlet pipe 34.

[0133] Please refer to Figures 16 to 20 , Fig.16 This is a schematic structural diagram of a fourth embodiment of the gas-liquid separator provided in the present application; Fig.17 for Fig.16 A perspective view of the gas-liquid separator shown; Fig.18 for Fig.16 The schematic diagram of the structure of the gas-liquid separator shown is shown with the outer shell hidden; Fig.19 for Fig.18 Structural diagram of the heat-insulating cylinder and high-pressure pipeline of the gas-liquid separator; Fig. 20 for Fig.19A schematic structural diagram of the heat-insulating cylinder and the high-pressure pipeline shown in another perspective.

[0134] In this embodiment, the gas-liquid separator includes a housing 10 , a heat-insulating cylinder 20 , a low-pressure pipeline 30 and a high-pressure pipeline 40 .

[0135] The structures of the housing 10, the heat insulating tube 20 and the low-pressure pipeline 30 can refer to the aforementioned Figures 1 to 5 The first embodiment shown is understood and will not be described in detail here. Figure 4 The same is shown and no further illustration is given.

[0136] In this embodiment, the high pressure pipeline 40 includes a high pressure inlet section 41, a high pressure pipe section 42D and a high pressure outlet section 43 connected in sequence. The high pressure inlet section 41 and the high pressure outlet section 43 also pass through the housing 10 to facilitate connection with external pipelines.

[0137] The high pressure pipe section 42D in this embodiment is the same as the Figures 11 to 15 The third embodiment shown is similar, the high-pressure pipe section 42D includes a first high-pressure pipe section 421D located inside the heat-insulating tube 20 and a second high-pressure pipe section 422D located outside the heat-insulating tube 20. The first high-pressure pipe section 421D extends downward in a spiral along the inner wall of the heat-insulating tube 20 inside the heat-insulating tube 20, and also has a roughly conical spiral structure, and the second high-pressure pipe section 422D is specifically located below the heat-insulating tube 20. The first low-pressure pipe section 32 is located inside the first high-pressure pipe section 421D.

[0138] Compared with the aforementioned third embodiment, the second high-pressure pipe section 422D in this embodiment is a three-dimensional curved structure, which can be understood as the high-pressure pipe section 42D having at least two layers, each of which is curved. The three-dimensional curved structure can be a conical spiral structure, such as Fig.19 and Fig. 20 As shown, it can of course also be a spiral winding structure with equal diameter, or other forms of winding, such as a serpentine structure formed by bending back and forth.

[0139] The working principle of the gas-liquid separator in this embodiment is consistent with that of the aforementioned third embodiment, and can be understood by referring to the aforementioned, and will not be repeated here.

[0140] In other embodiments, the structure of the gas-liquid separator is not limited to the description of the above four embodiments. For example, in some embodiments, the high-pressure pipe section of the high-pressure pipeline 40 can be entirely located in the insulation tube 20, which can be understood as omitting the structural setting of the second high-pressure pipe section on the basis of the third and fourth embodiments.

[0141] The present application also provides a thermal management system. Fig.21It is understood that the thermal management system includes a compressor, an evaporator, a condenser and a gas-liquid separator, and the gas-liquid separator can be the gas-liquid separator introduced in the aforementioned embodiments.

[0142] The connection relationship between the various components of the thermal management system is as follows: the outlet of the evaporator is connected to the low-pressure inlet section of the gas-liquid separator, the low-pressure outlet pipe of the gas-liquid separator is connected to the inlet of the compressor, the outlet of the compressor is connected to the inlet of the condenser, the outlet of the condenser is connected to the inlet end of the high-pressure pipeline of the gas-liquid separator (i.e., the high-pressure inlet section), the outlet end of the high-pressure pipeline of the gas-liquid separator (i.e., the high-pressure outlet section) is connected to the inlet of the throttling device, and the outlet of the throttling device is connected to the inlet of the evaporator.

[0143] The thermal management system adopts the gas-liquid separator of each embodiment above to improve the supercooling degree and cooling capacity without adjusting the throttling device. Fig. 22 Specifically, Fig. 22 A comparison diagram of enthalpy differences between the thermal management system provided by this embodiment and a conventional thermal management system is shown.

[0144] The conventional thermal management system here refers to a thermal management system that uses a conventional heat recovery gas-liquid separator. The conventional heat recovery gas-liquid separator refers to a high-pressure pipeline that heats both the gas phase and the liquid phase of the low-pressure refrigerant.

[0145] Fig. 22 The dotted line in the figure is the refrigeration cycle of a conventional thermal management system under a certain working condition. Under this working condition, the mass flow rate of the refrigerant is m', and points 1' to 2' marked on the dotted line correspond to the inlet to the outlet of the evaporator, points 2' to 3' correspond to the inlet to the outlet of the low-pressure pipeline of the gas-liquid separator, points 3' to 4' correspond to the inlet to the outlet of the compressor, points 4' to 5' correspond to the inlet to the outlet of the condenser, and points 5' to 6' correspond to the inlet to the outlet of the high-pressure pipeline of the gas-liquid separator.

[0146] Fig. 22 The solid line in the figure represents the refrigeration cycle of the thermal management system provided in the embodiment of the present application under the same working condition. Under this working condition, the mass flow rate of the refrigerant is m. Point 1 to point 2 marked on the solid line correspond to the inlet to the outlet of the evaporator, and point 2 to point 3 correspond to the inlet to the outlet of the low-pressure pipeline of the gas-liquid separator. Specifically, with respect to the gas-liquid separator provided in the aforementioned embodiment, point 2 to point 3 corresponds to the low-pressure inlet section 31 to the low-pressure outlet pipe 34 of the low-pressure pipeline 30, point 3 to point 4 corresponds to the inlet to the outlet of the compressor, point 4 to point 5 corresponds to the inlet to the outlet of the condenser, and point 5 to point 6 corresponds to the inlet to the outlet of the high-pressure pipeline of the gas-liquid separator. Specifically, with respect to the gas-liquid separator provided in the aforementioned embodiment, point 5 to point 6 corresponds to the high-pressure inlet section 41 to the high-pressure outlet section 43 of the high-pressure pipeline 40 of the gas-liquid separator.

[0147] After adopting the thermal management system provided by the present application, since the high-pressure pipeline in the gas-liquid separator heats the saturated liquid refrigerant gathered after gas-liquid separation, rather than the two-phase refrigerant heated in the conventional heat recovery gas-liquid separator, the overall heat exchange capacity will increase, so that the outlet of the high-pressure pipeline of the gas-liquid separator in the present application corresponds to point 6 with a higher degree of supercooling; because the low-pressure refrigerant heated inside the gas-liquid separator in the present application is a saturated liquid, the liquid storage volume in the gas-liquid separator is less than that in the conventional gas-liquid separator in the conventional thermal management system, so that the refrigerant mass flow rate m in the thermal management system in the present application is larger than the refrigerant mass flow rate m' in the conventional thermal management system. In this way, when the conditions such as the throttling device, the compressor speed and the environmental conditions remain unchanged, the high-pressure side and the low-pressure side in the thermal management system of the present application are slightly moved up on the enthalpy difference diagram compared with the high-pressure side and the low-pressure side in the conventional thermal management system.

[0148] from Fig. 22 It can be seen from the comparison that after adopting the thermal management system of the present application, the supercooling degree increases, the corresponding point of the outlet of the high-pressure pipeline of the gas-liquid separator moves from point 6' to point 6 on the enthalpy difference diagram, and the inlet of the evaporator moves from point 1' to point 1. After heat exchange in the evaporator, the inlet of the low-pressure pipeline of the gas-liquid separator moves from point 2' to point 2 with lower dryness, so that the saturated liquid refrigerant gathered inside the gas-liquid separator can be effectively exchanged with heat, and the superheat of the low-pressure outlet of the gas-liquid separator can be reduced within the allowable range.

[0149] The increased subcooling of the thermal management system also helps reduce noise.

[0150] The embodiment of the present application also provides a method for determining the taper angle of the aforementioned gas-liquid separator. In the gas-liquid separator provided in the present application, the main component for performing the gas-liquid separation function is the first low-pressure pipe section 32 of the low-pressure pipeline 30. It can be understood that the taper angle of the first low-pressure pipe section 32 affects the relevant parameters of the spiral channel of the first low-pressure pipe section 32, and correspondingly affects the gas-liquid separation effect. In order to achieve a better gas-liquid separation effect, the embodiment of the present application provides a method for determining the taper angle of the aforementioned gas-liquid separator, where the taper angle is the taper angle α of the first low-pressure pipe section 32 of the low-pressure pipeline 30, which can be combined with Fig.23 understand, Fig.23 A simplified model diagram illustrating the internal structure of the gas-liquid separator shell.

[0151] In this embodiment, the taper angle α of the first low-pressure pipe section 32 of the low-pressure pipeline 30 of the gas-liquid separator has a set value range. Within the value range, the comprehensive performance coefficient Z of the first low-pressure pipe section 32 is selected. * The taper angle corresponding to the maximum value is the optimal taper angle actually set for the first low-pressure pipe section 32. The structure of the first low-pressure pipe section 32 and the structure of the second low-pressure pipe section 33 associated with the parameters of the first low-pressure pipe section 32 are set according to this optimal taper angle.

[0152] The comprehensive performance coefficient Z of the first low-pressure pipe section 32 * By formula Z * =a * / f * Sure;

[0153] Among them, a * is the equivalent dimensionless centrifugal force of the first low-pressure pipe section 32, f * is the equivalent dimensionless friction coefficient of the first low-pressure pipe section 32 .

[0154] Here, considering that a drainage hole 321 is provided on the first low-pressure pipe section 32 to facilitate the escape of the liquid phase medium under the action of centrifugation, in the process of the low-pressure two-phase medium running downward along the first low-pressure pipe section 32, the liquid phase medium keeps escaping, and the dryness of the medium flowing in the first low-pressure pipe section 32 gradually increases. The larger the dryness, the better the gas-liquid separation ability. However, the dryness is an important indicator to characterize the separation ability of the gas-liquid separator, and its calculation is relatively complicated. To simplify the calculation, this application mainly evaluates it through dimensionless centrifugal force and dimensionless friction coefficient. It can be considered that the centrifugal force and the dryness of the medium are positively correlated, that is, the greater the centrifugal force, the greater the dryness of the medium flowing out of the first low-pressure pipe section 32; but the greater the centrifugal force, the greater the friction coefficient, and the greater the pressure drop generated by the system, which is not good for the system; the dimensionless centrifugal force and the dimensionless friction coefficient are not real values, and the relatively optimal taper angle is mainly obtained through relative comparison under different taper angles.

[0155] Here, the comprehensive performance coefficient Z of the first low-pressure pipe section 32 is * By formula Z * =a * / f * Determine, taking into account the centrifugal force a * The influence of the first low-pressure pipe section 32 is also taken into account. * It can be considered that the greater the centrifugal force under unit pressure drop conditions, the better the taper angle condition.

[0156] In one implementation, the equivalent dimensionless centrifugal force a of the first low-pressure pipe section 32 is * It can be determined by the following formula:

[0157] a * =k1·u l 2 / (g·D eq / 2);

[0158] u l =G(1-x) / (ρ l (1-∈));

[0159]

[0160] G=4q / (π·d i 2 );

[0161] D ea =2 / (1 / D min +1 / D max ), D min =D max -2·H·tan(α / 2);

[0162] Among them, k1 is the correction coefficient, u l is the velocity of the liquid medium, D eq is the equivalent spiral diameter of the first low-pressure pipe section 32, G is the flow density of the refrigerant, x is the dryness at the inlet of the gas-liquid separator, ρ l is the density of the liquid medium, ∈ is the refrigerant porosity, ρ g is the density of the gas phase medium, σ is the surface tension of the refrigerant, q is the mass flow rate of the refrigerant, d i is the inner diameter of the first low-pressure pipe section 32, D max is the maximum spiral diameter of the first low-pressure pipe section 32, D min is the minimum spiral diameter of the first low-pressure pipe section 32 , and H is the axial height of the first low-pressure pipe section 32 .

[0163] When the overall dimensions of the gas-liquid separator are determined, the dimensions of the heat-insulating tube 20 can be determined, so that the maximum spiral diameter D of the first low-pressure pipe section 32 located in the heat-insulating tube 20 is max and the axial height H can be determined in advance. According to the actual application scenario, the mass flow rate of the refrigerant in the system, the relevant physical parameters of the refrigerant, etc. can be determined in advance. In this way, according to a selected taper angle value of the first low-pressure pipe section 32, the equivalent dimensionless centrifugal force a relative to can be calculated. * .

[0164] In specific implementation, the above correction coefficient k1 can be obtained by the formula:

[0165] k1=1.125-0.065n is determined.

[0166] Where n = H / s, n is the equivalent number of spiral turns of the first low-pressure pipe section 32, s is the equivalent spiral pitch of the first low-pressure pipe section 32, ω is the ratio of the pipe length of the first low-pressure pipe section 32 to the sum of the pipe length of the first low-pressure pipe section 32 and the pipe length of the second low-pressure pipe section 33, and L is the sum of the pipe length of the first low-pressure pipe section 32 and the pipe length of the second low-pressure pipe section 33. In other words, ω·L is the pipe length of the first low-pressure pipe section 32.

[0167] Generally speaking, L can also be determined in advance. ω is a constant with an optional range, which can usually be selected in the range of 0.75 to 0.95 and can be adjusted according to the actual application.

[0168] In a specific implementation, the equivalent dimensionless friction coefficient f of the first low-pressure pipe section 32 is * It can be determined by the following formula:

[0169]

[0170] Re=ρud i / μ;

[0171] u=G / ρ;

[0172] Where Re is the Reynolds number, ρ is the homogeneous density, μ is the homogeneous viscosity, u is the homogeneous velocity, μ g is the viscosity of the gas phase medium, μ l is the viscosity of the liquid medium.

[0173] Specifically, the equivalent dimensionless friction coefficient f * It can be determined according to the following formula:

[0174] Wherein, k is a constant, which can be selected according to the actual application scenario. The formula can also be in other forms, and is not limited to this formula.

[0175] In one implementation, the taper angle α of the first low-pressure pipe section 32 has a value range of α min ≤α<α max Among them, α min It can be selected based on experience, for example, it can be 25°. Generally speaking, if the angle is too small, the spatial size of the outer cavity 102 of the gas-liquid separator will be too small, which is not conducive to liquid storage and the centrifugal effect will be relatively poor. If the angle is too large, the flow resistance of the first low-pressure pipe section 32 will be increased, which is not conducive to improving the comprehensive performance of gas-liquid separation.

[0176] Among them, α max =2·arctan(D max / (2·H)), combined Fig.23 , which can be determined based on triangular geometric relationships.

[0177] When the taper angle α of the first low-pressure pipe section 32 is determined, a series of values ​​can be selected within the above value range to calculate the corresponding comprehensive performance coefficient Z * According to the calculation results, the comprehensive performance coefficient Z is selected * The corresponding taper angle α when it is at the maximum is the optimal value actually set for the first low-pressure pipe section 32 .

[0178] Specifically, multiple angle values ​​may be listed in the above value range in increments of a certain degree.

[0179] In practical applications, when the equivalent spiral number n corresponding to the value of the taper angle α of the first low-pressure pipe section 32 is greater than the preset value, the value of the taper angle α is excluded. According to experience, a too large equivalent spiral number n is not beneficial to the gas-liquid separation effect, so the preset value of the equivalent spiral number n can be set as needed. If the calculated result exceeds the maximum value, the corresponding value of the taper angle α is not considered. The aforementioned preset value can be set to 15, etc. according to experience.

[0180] At the same time, the equivalent helical pitch s of the first low-pressure pipe section 32 should also be considered, which should not be less than the inner diameter d of the first low-pressure pipe section 32. i Therefore, in the calculation process, if the equivalent spiral pitch s of the first low-pressure pipe section 32 corresponding to a certain taper angle α is smaller than the inner diameter d of the first low-pressure pipe section 32 i , and the value of the taper angle α is also excluded.

[0181] The method for determining the taper angle α of the first low-pressure pipe section 32 of the gas-liquid separator is described below with a specific example.

[0182] The size of the gas-liquid separator is usually limited to a certain range. Based on the maximization of space utilization, the height of the first low-pressure pipe section 32 is maximized. In an application example, the parameters corresponding to the application scenario can be obtained:

[0183] The maximum spiral diameter of the first low-pressure pipe section 32 is D max is 105 mm, the axial height H is 112 mm, the total length L of the first low-pressure pipe section 32 and the second low-pressure pipe section 33 is 1000 mm, and the inner diameter d of the first low-pressure pipe section 32 is i The refrigerant in the system is R1234yf, the mass flow rate q is 180kg / h, the inlet dryness x is 0.5 and the saturation temperature T is 7℃.

[0184] First determine the setting range of the taper angle α of the first low-pressure pipe section 32, according to the formula α max =2·arctan(D max / (2·H)) and the above parameters can be obtained max is 50°. α is selected based on experience min is 25°.

[0185] A series of selected values ​​of the taper angle α are selected in increments of 5° within the setting range, namely 25°, 30°, 35°, 40° and 45°. In other applications, in order to obtain a better solution, the increment degree can also be set to be smaller, such as incrementing 1° or 2° each time.

[0186] According to a series of selected values ​​of the taper angle α, a series of corresponding minimum spiral diameters D of the first low-pressure pipe section 32 can be calculated. min , so that the equivalent spiral diameter D of the first low-pressure pipe section 32 can be determined eq , equivalent helical pitch s and equivalent number of helical turns n.

[0187] Here, taking the taper angle α as 25° and the constant ω as 0.9 as an example, the minimum spiral diameter D of the first low-pressure pipe section 32 can be obtained: min The equivalent spiral diameter D is 55.34 mm. ea It is 72.48mm, the equivalent spiral pitch s is 28.54mm, and the equivalent number of spiral turns n is 3.92.

[0188] According to the previously determined inner diameter d of the first low-pressure pipe section 32 i The flow density G of the refrigerant can be calculated from the mass flow rate q to be 282.9 kg / (m 2 ·s).

[0189] According to the refrigerant saturation temperature of 7℃, the density of the saturated gas phase medium ρ can be obtained by combining the general physical property table g is 22.1kg / m3, the density of the saturated liquid medium is ρ l is 1153.9kg / m3, surface tension σ is 0.0085024N / m), combined with the above parameters, it can be calculated that the refrigerant void ratio ∈ is 0.918, and the liquid medium u l The speed is 1.5m / s, and the equivalent dimensionless centrifugal force a * It is 5.535.

[0190] According to the above physical parameters and the inlet dryness x, the homogeneous density ρ can be obtained as 43.37 kg / m 3 , the homogeneous viscosity μ is 0.01961 Pa·s, the homogeneous velocity u is 6.52 m / s, and combined with the above-mentioned related parameters, the corresponding Reynolds number Re can be obtained as 216, so that the equivalent dimensionless friction coefficient f can be determined * is 0.006251, where the constant k is selected as 0.31, so that the comprehensive performance coefficient Z of the first low-pressure pipe section 32 corresponding to the taper angle α of 25° can be calculated. * It is 885.4.

[0191] Similarly, the comprehensive performance coefficient Z corresponding to other selected values ​​of the taper angle α can be determined: * , please refer to the following Table 1. Among them, when the taper angle α is 45°, the calculated equivalent helical pitch s of the first low-pressure pipe section 32 is smaller than the inner diameter d of the pipe i , so exit the calculation.

[0192] Table 1- Correspondence table between the taper angle of the first low-pressure pipe section 32 and related parameters in an application scenario

[0193]

[0194] It can be seen from Table 1 that when the taper angle is 35°, the comprehensive performance coefficient Z * Highest, so in the aforementioned application scenario, the first low-pressure pipe section 32 can be set according to the taper angle of the first low-pressure pipe section 32 being 35°, and the second low-pressure pipe section 33 can be set according to the parameter proportional relationship between the first low-pressure pipe section 32 and the second low-pressure pipe section 33, so that the gas-liquid separator has a relatively better gas-liquid separation effect.

[0195] Among them, the maximum spiral diameter D of the second low-pressure pipe section 33 is max2 and minimum spiral diameter D min2 Can be combined Fig.23 The triangular geometric relationship shown in FIG. 3 and the radial distance P between the first low-pressure pipe section 32 and the second low-pressure pipe section 33 mentioned above are the pipe diameter of the low-pressure pipeline (i.e., the inner diameter d of the first low-pressure pipe section 32). i ), other relevant parameters of the second low-pressure pipe section 33 can also be calculated using corresponding formulas, which are specifically listed below. The meanings of the relevant parameters involved in the formula are consistent with the above.

[0196] D max2 =D max -2·(Hh)·tan(α / 2)+P, wherein h can be determined based on the aforementioned ratio of the axial height h of the second low-pressure pipe section 33 to the axial height H of the first low-pressure pipe section 32 of 0.1 to 0.25, combined with the axial height H of the first low-pressure pipe section 32;

[0197] D min2 =D max -2·H·tan(α / 2)+P;

[0198] Equivalent spiral diameter of the second low-pressure pipe section 33: D eq2 =2 / (1 / D min2 +1 / D max2 );

[0199] The equivalent helical pitch of the second low-pressure pipe section 33 is: And the equivalent number of spiral turns n2 = h / s2.

[0200] In other application scenarios, the relevant design parameters of the first low-pressure pipe section 32 and the second low-pressure pipe section 33 of the gas-liquid separator may also be set according to the above determination method, and will not be described in detail.

[0201] Specific examples are used herein to illustrate the principles and implementation methods of the present application, and the description of the above embodiments is only used to help understand the method and core ideas of the present application. It should be pointed out that for ordinary technicians in this technical field, without departing from the principles of the present application, several improvements and modifications can be made to the present application, and these improvements and modifications also fall within the scope of protection of the claims of the present application.

Claims

1. A gas-liquid separator, characterized in that: It includes a shell, a heat-insulating cylinder, a low-pressure pipeline and a high-pressure pipeline; The heat-insulating tube divides the shell cavity of the outer shell into an inner cavity and an outer cavity, the outer cavity surrounds the inner cavity, the heat-insulating tube is in a conical shape with a larger upper portion and a smaller lower portion, and a lower end of the heat-insulating tube is provided with a lower port; a vent hole is provided on the top of the heat-insulating tube, the upper ends of the inner cavity and the outer cavity are connected through the vent hole, and the lower ends of the inner cavity and the outer cavity are connected through the lower port of the heat-insulating tube; The low-pressure pipeline includes a low-pressure inlet section, a first low-pressure pipe section and a second low-pressure pipe section connected in sequence, the low-pressure inlet section is connected to an external pipeline, the first low-pressure pipe section is a spiral structure and is located in the insulation cylinder, the second low-pressure pipe section is a spiral structure and is jacketed on the bottom of the insulation cylinder; the first low-pressure pipe section has a drainage hole; the top of the shell is provided with a low-pressure outlet; At least a portion of the high-pressure pipeline is located in the shell for heat exchange with the liquid medium separated by the low-pressure pipeline.

2. The gas-liquid separator according to claim 1, characterized in that: The high-pressure pipeline includes a high-pressure inlet section, a high-pressure pipe section and a high-pressure outlet section connected in sequence, the high-pressure inlet section and the high-pressure outlet section are both connected to an external pipeline, and at least a portion of the high-pressure pipe section is located in the insulation cylinder.

3. The gas-liquid separator according to claim 2, characterized in that: The high-pressure pipe section is located inside the insulation tube and spirally extends downward along the inner wall of the insulation tube. The high-pressure inlet section is connected to an external pipeline, the high-pressure outlet section is connected to an external pipeline, and the first low-pressure pipe section is located on the inner side of the high-pressure pipe section.

4. The gas-liquid separator according to claim 2, characterized in that: The high-pressure pipe section includes a first high-pressure pipe section and a second high-pressure pipe section, the first high-pressure pipe section spirally extends downward along the inner wall of the insulation tube inside the insulation tube, and the second high-pressure pipe section is located outside the insulation tube and below the insulation tube; the high-pressure inlet section is connected to an external pipeline, and the high-pressure outlet section is connected to an external pipeline; the first low-pressure pipe section is located on the inner side of the first high-pressure pipe section.

5. The gas-liquid separator according to claim 4, characterized in that: The second high-pressure pipe section is a planar bending structure, or the second high-pressure pipe section is a three-dimensional bending structure.

6. The gas-liquid separator according to claim 1, characterized in that: The high-pressure pipeline includes a high-pressure inlet section, a high-pressure pipe section and a high-pressure outlet section connected in sequence, the high-pressure inlet section and the high-pressure outlet section are both connected to an external pipeline, and the high-pressure pipe section is located outside the insulation cylinder and below the insulation cylinder.

7. The gas-liquid separator according to claim 6, characterized in that: The high-pressure pipe section has a planar bending structure; or, the high-pressure pipe section has a three-dimensional bending structure.

8. The gas-liquid separator according to any one of claims 1 to 7, characterized in that: The first low-pressure pipe section extends spirally downward along the inner wall of the thermal insulation tube, and the second low-pressure pipe section extends spirally upward along the outer wall of the thermal insulation tube.

9. The gas-liquid separator according to any one of claims 1 to 7, characterized in that: The shell includes a cylindrical shell peripheral wall, a shell bottom wall and a shell top wall. The aperture of the upper port of the insulation cylinder is consistent with the aperture of the shell peripheral wall. The shell top wall is penetrated by a low-pressure outlet connecting pipe, and the low-pressure outlet interface has the low-pressure outlet.

10. A method for determining the taper angle of a gas-liquid separator, characterized in that: The gas-liquid separator is the gas-liquid separator according to any one of claims 1 to 9, the taper angle is the taper angle α of the first low-pressure pipe section, the taper angle α of the first low-pressure pipe section has a set value range, within the value range, the comprehensive performance coefficient Z of the first low-pressure pipe section is selected * The taper angle corresponding to the maximum value of is the optimal taper angle actually set for the first low-pressure pipe section; The comprehensive performance coefficient Z of the first low-pressure pipe section * By formula Z * =a * / f * Sure; Among them, a * is the equivalent dimensionless centrifugal force of the first low-pressure pipe section, f * is the equivalent dimensionless friction coefficient of the first low-pressure pipe section; The equivalent dimensionless centrifugal force a of the first low-pressure pipe section * Determined by the following formula: a * =k1·u l 2 / (g·D eq / 2); you l =G(1-x) / (ρ l (1-∈)); G=4q / (π·d i 2 ); D eq =2 / (1 / D min +1 / D max ),D min =D max -2·H·tan(α / 2); The equivalent dimensionless friction coefficient f of the first low-pressure pipe section * Determined by the following formula: Re=ρud i / m; u=G / ρ; Among them, k1 is the correction coefficient, u l is the velocity of the liquid medium, D eq is the equivalent spiral diameter of the first low-pressure pipe section, G is the flow density of the refrigerant, x is the dryness at the inlet of the gas-liquid separator, ρ l is the density of the liquid medium, ∈ is the refrigerant porosity, ρ g is the density of the gas phase medium, σ is the surface tension of the refrigerant, q is the mass flow rate of the refrigerant, d i is the inner diameter of the first low-pressure pipe section, D max is the maximum spiral diameter of the first low-pressure pipe section, D min is the minimum spiral diameter of the first low-pressure pipe section, H is the axial height of the first low-pressure pipe section, Re is the Reynolds number, ρ is the homogeneous density, μ is the homogeneous viscosity, u is the homogeneous velocity, μ g is the viscosity of the gas phase medium, μ l is the viscosity of the liquid medium.

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