Gas-liquid separator and taper design method thereof

Abstract

The invention provides a gas-liquid separator and a taper design method thereof.The gas-liquid separator comprises a shell, a heat insulation barrel, an inner gas-liquid separation pipe, an outer gas-liquid separation pipe, a gas phase heating pipe and a liquid phase heating pipe, and the heat insulation barrel, the inner gas-liquid separation pipe, the outer gas-liquid separation pipe, the gas phase heating pipe and the liquid phase heating pipe are located in the shell; the outer gas-liquid separation pipe is spirally wound outside the heat insulation cylinder upwards from the lower end of the inner gas-liquid separation pipe, and a plurality of liquid drainage holes are sequentially formed in the lower position, away from the spiral central axis side, of the pipe wall of the inner gas-liquid separation pipe in the pipe length direction. A plurality of exhaust holes are sequentially formed in the pipe wall of the outer gas-liquid separation pipe in the pipe length direction close to the upper side of the spiral central axis, the gas-phase heating pipe is spirally wound between the position above the bottom of the shell and the exterior of the heat insulation barrel, and the liquid-phase heating pipe is arranged in the heat insulation barrel and / or at the bottom of the shell. The gas-liquid separator can improve the degree of superheat and the degree of supercooling of the thermal management system.

Description

Technical Field

[0001] The present application relates to the technical field of gas-liquid separation, and in particular to a gas-liquid separator and a taper design method thereof. Background Art

[0002] The existing thermal management system only adjusts the superheat or subcooling by adjusting the opening of the throttling device. Due to the limited adjustment degree of the opening of the throttling device, there may be insufficient superheat or subcooling. In addition, the throttling device sometimes fails to adjust sensitively, resulting in the inability to adjust the superheat or subcooling.

[0003] Therefore, how to improve the superheat or supercooling is a technical problem that needs to be solved by technicians in this field. Summary of the invention

[0004] In order to solve the above technical problems, the present application provides a gas-liquid separator, which includes a shell and:

[0005] an insulating tube, wherein the central axis of the insulating tube extends in an up-down direction, a lower end of the insulating tube is provided with a lower port, a top of the insulating tube is provided with a vent, the insulating tube divides the internal space of the shell into an inner tube space and an outer tube space, the inner tube space is connected to the upper end of the outer tube space through the vent, and the inner tube space is connected to the lower end of the outer tube space through the lower port;

[0006] A gas-liquid separation tube, the gas-liquid separation tube comprising an inner gas-liquid separation tube and an outer gas-liquid separation tube, the inner gas-liquid separation tube being spirally wound from top to bottom inside the heat-insulating tube, the outer gas-liquid separation tube being spirally wound from the lower end of the inner gas-liquid separation tube upward outside the heat-insulating tube, a tube wall of the inner gas-liquid separation tube being provided with a plurality of drainage holes in sequence along the tube length direction at a position away from the spiral central axis side thereof;

[0007] A heating pipe is located inside the shell, and the heating pipe includes a gas phase heating pipe, and the gas phase heating pipe is spirally coiled above the bottom of the shell and outside the insulation tube.

[0008] In addition, the present application also provides a taper design method for a gas-liquid separator, wherein the gas-liquid separator is the above-mentioned gas-liquid separator, wherein the inner gas-liquid separation tube, the outer gas-liquid separation tube and the heat-insulating tube of the gas-liquid separator are all conical as a whole and have the same taper α, and the value of the taper α is determined by the taper design method, and the taper design method includes:

[0009] S1. Eliminate the unreasonable range of the taper α of the internal gas-liquid separation tube, and then select several angles within a reasonable range as the taper of the internal gas-liquid separation tube for model calculation;

[0010] S2. Calculate the equivalent dimensionless centrifugal force a of the internal gas-liquid separation tube * ;

[0011] S3. Calculate the equivalent dimensionless friction coefficient f of the internal gas-liquid separation tube * ;

[0012] S4. Define the dimensionless lateral area A1 of the insulation tube according to the minimum diameter, maximum diameter and single-sided lateral area of ​​the insulation tube. * ;or,

[0013] The dimensionless lateral area A2 of the insulation tube is defined based on the minimum diameter, maximum diameter, single-sided lateral area, and the diameter of the insulation tube corresponding to a circle of the external gas-liquid separation tube. * ;

[0014] S5. Define comprehensive performance parameter E * =a * (A1 * ) / f * Or define the comprehensive performance parameter F * =a * (A2 * ) 1 / 3 / f * , compare the comprehensive performance parameters corresponding to each taper selected in S1, and determine the value of the taper α according to the comparison result.

[0015] When the gas-liquid separator provided in the present application is working, the gas phase is mainly enriched between the bottom of the shell and the outside of the insulation tube, while the liquid phase is mainly enriched inside the insulation tube and the bottom of the shell. Since the gas phase and the liquid phase are enriched in different areas respectively, the gas phase heating tube arranged in the gas phase enriched area can basically heat the gas phase alone and has a high heating efficiency. Furthermore, the liquid phase heating tube arranged in the liquid phase enriched area can basically heat the liquid phase alone and has a high heating efficiency.

[0016] Since the gas phase heating tube can basically heat the gas phase alone and has a high heating efficiency, the gas-liquid separator can expand the superheat adjustment range of the thermal management system when used in the thermal management system, so that the thermal management system can effectively increase the superheat without adjusting the throttling device opening. Furthermore, since the liquid phase heating tube can basically heat the liquid phase alone and has a high heating efficiency, the gas-liquid separator can expand the subcooling adjustment range of the thermal management system when used in the thermal management system, so that the thermal management system can effectively increase the subcooling without adjusting the throttling device opening, and appropriately increase the system cooling capacity while increasing the subcooling.

[0017] This solves the problem that when a conventional thermal management system is used to adjust superheat or subcooling only by adjusting the opening of the throttling device, the requirements for superheat or subcooling under certain working conditions cannot be met due to the limited adjustment degree of the opening of the throttling device, and the superheat or subcooling cannot be adjusted when the throttling device is insensitive and fails. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 A schematic diagram of a first embodiment of a gas-liquid separator provided in the present application;

[0019] Figure 2 for Figure 1 perspective drawing;

[0020] Figure 3 for Figure 1 The gas-liquid separation tube in the

[0021] Figure 4 for Figure 1 The heat insulation tube and gas phase heating tube in the device;

[0022] Figure 5 A perspective view of a second embodiment of a gas-liquid separator provided by the present application;

[0023] Figure 6 A perspective view of a third embodiment of a gas-liquid separator provided by the present application;

[0024] Figure 7 A perspective view of a fourth embodiment of a gas-liquid separator provided by the present application;

[0025] Figure 8 A perspective view of a fifth embodiment of a gas-liquid separator provided by the present application;

[0026] Fig. 9 A perspective view of a sixth embodiment of a gas-liquid separator provided by the present application;

[0027] Fig.10 A perspective view of a seventh embodiment of a gas-liquid separator provided by the present application;

[0028] Fig.11 A perspective view of an eighth embodiment of a gas-liquid separator provided by the present application;

[0029] Fig.12 A perspective view of a ninth embodiment of a gas-liquid separator provided by the present application;

[0030] Fig.13 A schematic block diagram of a thermal management system using the gas-liquid separator provided by the present application;

[0031] Fig.14 A diagram of the enthalpy difference variation of subcooling and superheating adjusted by a gas-liquid separator for the thermal management system provided in the present application;

[0032] Fig.15 This is a calculation model diagram of the taper design method provided in this application.

[0033] The following are the descriptions of the reference numerals:

[0034] 100 shell, 101 gas phase outlet;

[0035] 200 heat insulation tube, 201 vent;

[0036] 300 gas-liquid separation tube, 301 inner gas-liquid separation tube, 301a liquid discharge hole, 302 outer gas-liquid separation tube, 302a exhaust hole;

[0037] 400 gas phase heating tube, 401 fin;

[0038] 500 liquid phase heating tube;

[0039] 600 control valve. DETAILED DESCRIPTION

[0040] In order to enable those skilled in the art to better understand the technical solution of the present application, the technical solution of the present application is further described in detail below in conjunction with the accompanying drawings and specific implementation methods.

[0041] The present application provides a gas-liquid separator. Figure 1 and Figure 2 As shown, the gas-liquid separator provided in the present application at least includes a shell 100, an insulating tube 200, a gas-liquid separation tube 300 and a heating tube.

[0042] Wherein, a gas phase outlet 101 is arranged at the upper end of the shell.

[0043] Among them, the heat-insulating cylinder is located inside the shell. The central axis of the heat-insulating cylinder extends in the up-down direction. The lower end of the heat-insulating cylinder is provided with a lower port, and the top of the heat-insulating cylinder is provided with a vent 201. The heat-insulating cylinder divides the internal space of the shell into an inner cylinder space and an outer cylinder space. The inner cylinder space is connected to the upper end of the outer cylinder space through the vent 201. The inner cylinder space is connected to the lower end of the outer cylinder space through the lower port of the heat-insulating cylinder.

[0044] The gas-liquid separation tube 300 is located inside the shell. The gas-liquid separation tube includes an inner gas-liquid separation tube 301 and an outer gas-liquid separation tube 302. The inner gas-liquid separation tube is spirally wound from top to bottom inside the heat-insulating tube. The outer gas-liquid separation tube is spirally wound upward from the lower end of the inner gas-liquid separation tube outside the heat-insulating tube. The wall of the inner gas-liquid separation tube is provided with a plurality of drainage holes 301a in sequence along the tube length direction at a position away from the spiral center axis side (see Figure 3 ), the so-called lower position refers to a position lower than the center line of the lumen of the internal gas-liquid separation tube.

[0045] The heating pipe is located inside the shell. The heating pipe includes at least a gas phase heating pipe 400. The gas phase heating pipe is spirally wound above the bottom of the shell and between the outside of the insulation tube. When working, a high temperature and high pressure medium flows in the gas phase heating pipe to heat the gas phase in the shell.

[0046] Furthermore, the heating tube may also include a liquid phase heating tube 500 (see Figure 9-12 ), the liquid phase heating tube is arranged inside the heat insulation tube and / or at the bottom of the shell. During operation, a high temperature and high pressure medium flows in the liquid phase heating tube to heat the liquid phase in the shell.

[0047] Furthermore, the gas-liquid separator may also include a control valve 600 (see Figure 9-12 ), overheat detection device and undercooling detection device (not shown in the figure).

[0048] Among them, the superheat detection device detects superheat. The undercooling detection device detects undercooling. The control valve is connected to the liquid phase heating tube and the gas phase heating tube, and is used to increase the mass flow rate of the medium inside the gas phase heating tube and reduce the mass flow rate of the medium inside the liquid phase heating tube when the superheat is insufficient, and to increase the mass flow rate of the medium inside the liquid phase heating tube and reduce the mass flow rate of the medium inside the gas phase heating tube when the undercooling is insufficient. The control valve is preferably a three-way control valve, one valve port of the three-way control valve is the inlet of high temperature and high pressure medium, one valve port is connected to the gas phase heating tube, and the other valve port is connected to the liquid phase heating tube.

[0049] The above gas-liquid separator can be used in thermal management systems, such as Fig.13 As shown, the thermal management system also includes a compressor, a condenser, an evaporator and a throttling device. The heating pipe of the gas-liquid separator is connected between the condenser outlet and the throttling device inlet, and the gas-liquid separation pipe of the gas-liquid separator is connected between the evaporator outlet and the compressor inlet.

[0050] When the above-mentioned gas-liquid separator is working, the gas-liquid two-phase flow flows into the upper end of the inner gas-liquid separation tube, and the gas-liquid two-phase flow moves downward along the spiral of the inner gas-liquid separation tube. Under the action of gravity and centrifugal force, the liquid phase will move toward the lower position of the tube wall of the inner gas-liquid separation tube away from the central axis of the spiral due to its large density. Since the tube wall of the inner gas-liquid separation tube is away from the central axis of the spiral and a plurality of drainage holes are provided in sequence along the length of the tube, the liquid phase will be dispersed and discharged from the drainage holes, and after being discharged into the insulation tube, it will flow downward through the lower end of the insulation tube and finally deposited at the bottom of the shell, so that it can fully contact and exchange heat with the liquid phase heating tube located inside the insulation tube and / or at the bottom of the shell to improve the degree of supercooling.

[0051] The gas phase spirals downward to the lower end of the inner gas-liquid separation tube, and then is discharged from the lower end of the inner gas-liquid separation tube to the lower end of the outer gas-liquid separation tube, and then spirals upward along the outer gas-liquid separation tube to be enriched between the bottom of the shell and the outside of the insulation tube, so that it can fully contact and exchange heat with the gas phase heating tube located between the bottom of the shell and the outside of the insulation tube to increase the superheat. In addition to this part of the gas phase, when the liquid phase flows out from the lower end of the insulation tube, part of the gas phase will also escape from it, and part of the gas phase may also escape from the liquid phase accumulated at the bottom of the shell, and the escaped gas phase will also be enriched upward between the bottom of the shell and the outside of the insulation tube, so that it can also fully contact and exchange heat with the gas phase heating tube. Finally, the gas phase is discharged through the vent at the upper end of the insulation tube and the gas phase outlet at the upper end of the shell.

[0052] That is to say, when the above-mentioned gas-liquid separator is working, the gas phase is mainly enriched between the bottom of the shell and the outside of the insulation tube, while the liquid phase is mainly enriched inside the insulation tube and the bottom of the shell. Since the gas phase and liquid phase are enriched in different areas respectively, the gas phase heating tube arranged in the gas phase enriched area can basically heat the gas phase alone and has a higher heating efficiency, and the liquid phase heating tube arranged in the liquid phase enriched area can basically heat the liquid phase alone and has a higher heating efficiency.

[0053] Since the gas phase heating tube of the above-mentioned gas-liquid separator can basically heat the gas phase alone and has a high heating efficiency, it can expand the superheat adjustment range of the thermal management system when used in the thermal management system, so that the thermal management system can effectively increase the superheat without adjusting the opening of the throttling device. Since the liquid phase heating tube of the above-mentioned gas-liquid separator can basically heat the liquid phase alone and has a high heating efficiency, it can expand the subcooling adjustment range of the thermal management system when used in the thermal management system, so that the thermal management system can effectively increase the subcooling without adjusting the opening of the throttling device, and appropriately increase the system cooling capacity while increasing the subcooling. This solves the problem that when a conventional thermal management system is used to adjust the superheat or subcooling only by adjusting the opening of the throttling device, the opening adjustment degree of the throttling device is limited and cannot meet the requirements of superheat or subcooling under certain working conditions, and the superheat or subcooling cannot be adjusted when the throttling device is insensitive and fails.

[0054] Combine the following Fig.14 To more clearly illustrate the above technical effects.

[0055] Fig.14 In the figure, m is the total mass flow rate of the low-pressure refrigerant in the thermal management system, point 1 corresponds to the inlet of the evaporator, point 2 corresponds to the outlet of the evaporator, point 3 corresponds to the inlet of the compressor, point 4 corresponds to the outlet of the compressor, point 5 corresponds to the outlet of the condenser, and point 6 corresponds to the outlet of the heating pipe of the gas-liquid separator.

[0056] In hot weather, considering the anti-liquid shock protection requirements of the compressor, it is necessary to make the superheat of the gas-liquid separation pipe outlet (point 3) of the gas-liquid separator higher. At this time, the control valve can be used to control the refrigerant mass flow rate in the gas phase heating pipe to be larger and the refrigerant mass flow rate in the liquid phase heating pipe to be smaller. In this way, the heating pipe of the gas-liquid separator mainly heats the refrigerant with higher gas dryness, which is different from the conventional heat recovery gas-liquid separator that heats the refrigerant in a two-phase state with relatively low dryness, thereby increasing the superheat (from point 3 to point 3'). Since the refrigerant heated is mainly enriched with a higher gas dryness, the liquid storage volume inside the gas-liquid separator shell is slightly higher than that of the conventional heat recovery gas-liquid separator, thereby reducing the total mass flow rate of the low-pressure refrigerant in the thermal management system (from m to m'), but within an acceptable range. When the throttling device, compressor speed, and environmental conditions remain unchanged, the high-pressure side and low-pressure side of the thermal management system provided by the present application may be slightly moved down on the enthalpy difference diagram compared to the thermal management system using a conventional heat-recovery gas-liquid separator. At the same time, the supercooling degree is reduced, and the corresponding point of the high-pressure outlet of the gas-liquid separator moves from point 6 to point 6' on the enthalpy difference diagram, and the evaporator inlet moves from point 1 to point 1'. Similarly, after heat exchange in the evaporator, the gas-liquid separator inlet moves from point 2 to point 2' with higher dryness, so that the larger gas phase inside the gas-liquid separator and the high-temperature and high-pressure refrigerant in the heating tube can be effectively exchanged with each other, thereby ensuring sufficient superheat.

[0057] Taking into account the influence of noise such as system howling (high supercooling is conducive to noise reduction), it is necessary to make the supercooling degree of the heating tube outlet (point 6) of the gas-liquid separator higher. At this time, the control valve can be used to control the refrigerant mass flow rate in the liquid phase heating tube of the heating tube to be larger, and the refrigerant mass flow rate in the gas phase heating tube of the heating tube to be smaller. In this way, the heating tube of the gas-liquid separator mainly heats the refrigerant with lower liquid dryness, which is different from the conventional heat recovery gas-liquid separator that heats the refrigerant in a two-phase state with relatively high dryness, thereby improving the supercooling degree (from point 6 to point 6"). Since the refrigerant mainly is enriched with lower liquid dryness, the liquid storage volume inside the gas-liquid separator shell is slightly lower than that of the conventional heat recovery gas-liquid separator, thereby increasing the total mass flow rate of the low-pressure refrigerant in the thermal management system (from m to m"). While improving the supercooling degree, the cooling capacity of the system is also appropriately increased. When the throttle valve, compressor speed, and environmental conditions remain unchanged, the high-pressure side and low-pressure side of the thermal management system provided by the present application may be slightly moved up on the enthalpy difference diagram compared to the thermal management system using a conventional heat recovery gas-liquid separator. At the same time, the supercooling degree increases, and the corresponding point of the low-pressure outlet of the gas-liquid separator moves from point 6 to point 6" on the enthalpy difference diagram, and the evaporator inlet moves from point 1 to point 1" on the enthalpy difference diagram. Similarly, after heat exchange in the evaporator, the gas-liquid separator inlet moves from point 2 to point 2" with a lower dryness, so that the more liquid phase inside the gas-liquid separator and the high-temperature and high-pressure refrigerant in the heating tube can be effectively exchanged with each other, thereby ensuring sufficient supercooling.

[0058] In a specific embodiment, the inner diameter of the tube cavity of the heating tube is smaller than the inner diameter of the tube cavity of the gas-liquid separation tube.

[0059] In a specific embodiment, the insulation cylinder is made of heat-insulating material, which is more conducive to the separate heating of the gas phase and the liquid phase.

[0060] In a specific embodiment, the gas phase heating tube is spirally wound between the heat insulation tube and the external gas-liquid separation tube and / or above the external gas-liquid separation tube. Figure 2 and Figure 5 In the embodiment, the lower part of the gas phase heating tube is located between the heat insulation tube and the outer gas-liquid separation tube, and the upper middle part of the gas phase heating tube is located above the outer gas-liquid separation tube. Figure 6 and Figure 7 In the embodiment, the gas phase heating tube is located above the outer gas-liquid separation tube. In addition, a plurality of exhaust holes 302a are sequentially arranged on the wall of the outer gas-liquid separation tube near the upper side of the spiral central axis along the tube length direction (see Figure 3 ), the so-called upper position refers to a position higher than the center line of the tube cavity of the external gas-liquid separation tube. In this way, during the upward movement of the gas phase along the external gas-liquid separation tube, under the action of centrifugal force, the gas phase will move toward the upper position of the tube wall of the external gas-liquid separation tube close to the spiral center axis due to its lower density. Since the tube wall of the external gas-liquid separation tube is close to the upper position of the spiral center axis and is provided with a plurality of exhaust holes in sequence along the tube length direction, the gas phase will be dispersed and discharged from each exhaust hole to between the insulation tube and the external gas-liquid separation tube and above the external gas-liquid separation tube, so as to be able to fully contact and exchange heat with the gas phase heating tube located between the insulation tube and the external gas-liquid separation tube and / or above the external gas-liquid separation tube. This design can improve the heating efficiency of the gas phase and also improve the gas-liquid separation effect. The improvement of the gas-liquid separation effect is conducive to the separate heating of the gas and liquid phases. It should be noted that the gas phase is not only discharged from the exhaust hole but also from the port of the external gas-liquid separation tube.

[0061] In a specific embodiment, Figure 8 As shown, the gas phase heating tube is arranged inside the outer gas-liquid separation tube. In this case, the outer gas-liquid separation tube is not provided with an exhaust hole 302a. Such a design can improve the compactness of the structure and the heat exchange effect.

[0062] In a specific embodiment, all spiral turns of the gas phase heating tube are arranged in sequence along the vertical direction, for example Figure 1 .

[0063] In a specific embodiment, all spiral turns of the gas phase heating tube are arranged in sequence along a horizontal direction perpendicular to the up-down direction, for example Figure 6 or Figure 7 In this case, for example Figure 7In the embodiment, only one group of horizontally arranged gas phase heating tubes can be provided and the group of gas phase heating tubes can be located in the middle of the heat insulation tube, or multiple groups of horizontally arranged gas phase heating tubes can be provided in sequence along the up and down directions, and then two adjacent groups of gas phase heating tubes are connected by connecting tubes, for example Figure 6 Two groups of gas phase heating tubes are arranged, one group is located at the lower part of the heat insulation tube, and the other group is located at the upper part of the heat insulation tube.

[0064] In a specific embodiment, some spiral coils of the gas phase heating tube are arranged in sequence along the up-down direction, and some spiral coils are arranged in sequence along the horizontal direction perpendicular to the up-down direction. For example Figure 5 , Figure 5 The horizontally arranged spiral coil is set at the uppermost end of the gas phase heating tube, which is easier to implement.

[0065] In a specific embodiment, the outer surface of the spiral coil of the gas phase heating tube is provided with fins 401, for example Figure 7 The fins block part of the area between adjacent spiral coils arranged in sequence in the horizontal direction, and the remaining area not blocked by the fins is the airflow passing area. Specifically, the airflow passing area can be avoided by opening through holes on the fins or arranging the fins at intervals. The present application does not limit the arrangement of the fins, for example, Figure 6 The horizontal setting shown can also be set upside down or tilted.

[0066] In a specific embodiment, the liquid phase heating tube is arranged inside the heat insulation tube and along the inner wall of the heat insulation tube and / or the liquid phase heating tube is arranged at the bottom of the shell. Fig. 9 In the embodiment, the liquid phase heating tube is arranged inside the heat insulation tube. Fig.10 In the embodiment, the liquid phase heating tube is arranged at the bottom of the shell. Fig.11 and Fig.12 In the invention, a part of the liquid phase heating tube is arranged inside the heat-insulating tube, and a part of the liquid phase heating tube is arranged at the bottom of the shell.

[0067] In a specific embodiment, the liquid phase heating tube inside the heat insulation cylinder is spirally wound from top to bottom, for example Fig. 9 , Fig.11 and Fig.12 , which can take into account both liquid phase heating efficiency and structural compactness.

[0068] In a specific embodiment, the liquid phase heating tube at the bottom of the shell is arranged to extend horizontally, for example Fig.11 .

[0069] In a specific embodiment, the liquid phase heating tube at the bottom of the shell is arranged in a horizontal spiral coil, for example Fig.10 , Fig.12 , which can take into account both liquid phase heating efficiency and structural compactness.

[0070] In a specific embodiment, Figure 3 As shown, the spiral diameter of each spiral circle of the inner gas-liquid separation tube gradually decreases from top to bottom, so that the inner gas-liquid separation tube is tapered as a whole. The diameter of the heat-insulating cylinder gradually decreases from top to bottom, so that the heat-insulating cylinder is tapered as a whole. The spiral diameter of each spiral circle of the outer gas-liquid separation tube gradually increases from bottom to top, so that the outer gas-liquid separation tube is tapered as a whole. With this design, on the one hand, a larger space can be formed between the smaller spiral diameter area of ​​the heat-insulating cylinder and the shell, so that other components of the gas-liquid separator (such as the outer gas-liquid separation tube) can be arranged, thereby improving the compactness of the structure. At the same time, since the heat-insulating cylinder is a tapered structure with a larger upper part and a smaller lower part, the outer gas-liquid separation tube is also designed to be a tapered structure with a larger upper part and a smaller lower part, so that the space utilization rate is higher. On the other hand, the horizontal projection of the inner gas-liquid separation tube and the heat-insulating cylinder in the horizontal direction perpendicular to the up and down direction can be a disc-shaped structure. In this way, when the gas phase outlet at the upper end of the shell is connected to the compressor inlet of the refrigeration equipment, when the refrigeration equipment is in the compressor startup stage or the four-way reversing valve reversing stage, it can prevent the liquid in the shell from splashing upward. On the other hand, the gas-liquid separation effect of the conical internal gas-liquid separation tube is better than that of the columnar internal gas-liquid separation tube whose spiral diameter is the same as its maximum spiral diameter.

[0071] In a specific embodiment, the tapers α of the inner gas-liquid separation tube, the heat-insulating tube and the outer gas-liquid separation tube are the same. In this way, on the one hand, it is more conducive to improving the compactness of the structure, and on the other hand, it is easy to determine the optimal taper. The range of the taper α is: 25°≤α<2·arctan(D max1 / (2·H), where D max1 D is the maximum spiral diameter of the internal gas-liquid separation tube, and H is the height of the internal gas-liquid separation tube. max1 and H are determined according to the internal space of the shell. 25°≤α has better structural compactness.

[0072] In a specific embodiment, the distance P between the outer conical surface of the outer gas-liquid separation tube and the outer conical surface of the inner gas-liquid separation tube is in the range of: 3d i ≤P≤5d i , where d i is the inner diameter of the gas-liquid separation tube.

[0073] In a specific embodiment, the length L1 of the inner gas-liquid separation tube is in the range of 0.6L≤L1≤0.85L, where L is the total length of the gas-liquid separation tube, so that both the gas-phase and liquid-phase heating efficiencies can be taken into account. When only a gas-phase heating tube is provided without a liquid-phase heating tube, based on the consideration of ensuring the gas-phase heating effect, the value range of L1 is more recommended to be between 0.6L-0.8L. When both a gas-phase heating tube and a liquid-phase heating tube are provided, based on the consideration of both the gas-phase heating effect and the liquid-phase heating effect, the value range of L1 is more recommended to be between 0.7L-0.85L.

[0074] In a specific embodiment, the equivalent number of spiral turns n1 of the inner gas-liquid separation tube is not greater than 15, and more preferably not greater than 8. H is the height of the inner gas-liquid separation tube, and s1 is the equivalent spiral pitch of the inner gas-liquid separation tube.

[0075] In a specific embodiment, the height h of the outer gas-liquid separation tube is in the range of 0.15H≤h≤0.35H, where H is the height of the inner gas-liquid separation tube. When only a gas phase heating tube is provided but no liquid phase heating tube is provided, the height h of the outer gas-liquid separation tube is preferably in the range of 0.2H≤h≤0.35H. When both a gas phase heating tube and a liquid phase heating tube are provided, the height h of the outer gas-liquid separation tube is preferably in the range of 0.15H≤h≤0.3H.

[0076] In a specific embodiment, the equivalent number of spiral turns n2 of the outer gas-liquid separation tube is not less than 0.5. Wherein, h is the height of the outer gas-liquid separation tube, and s2 is the equivalent spiral pitch of the outer gas-liquid separation tube. When only the gas phase heating tube is provided without the liquid phase heating tube, the equivalent spiral number n2 of the outer gas-liquid separation tube is preferably as close to 1 as possible, so that the gas phase heating effect is better.

[0077] In addition, the present application provides a taper design method for a gas-liquid separator, through which the value of the taper α can be determined.

[0078] Due to the limitation of external space, the size of the gas-liquid separator is usually limited to a certain range. Based on the maximization of space utilization and the maximization of the height of the internal gas-liquid separation tube, the following parameters can be obtained: the maximum spiral diameter D of the internal gas-liquid separation tube max1 , the height H of the inner gas-liquid separation tube, the length L of the gas-liquid separation tube, the inner diameter d of the inner gas-liquid separation tube and the outer gas-liquid separation tube i , the gas-liquid two-phase flow mass flow rate q, the gas-liquid two-phase flow dryness x and the saturation temperature T at the inlet of the internal gas-liquid separation tube.

[0079] When designing the taper,

[0080] Firstly, the unreasonable range of the taper α of the internal gas-liquid separation tube is eliminated, and then several angles are selected within a reasonable range as the taper of the internal gas-liquid separation tube for model calculation.

[0081] In a specific embodiment, the reasonable range of the taper α of the inner gas-liquid separation tube is: 25°≤α<2·arctan(D max1 / (2·H), where D max1 D is the maximum spiral diameter of the internal gas-liquid separation tube, and H is the height of the internal gas-liquid separation tube. max1and H are determined according to the internal space of the shell. 25°≤α can ensure the compactness of the structure of the gas-liquid separator. If the angle is too small, the space inside the shell except for the internal gas-liquid separation tube will be too small, which is not conducive to the layout of other components of the gas-liquid separator in the shell.

[0082] In a specific embodiment, an angle is selected at every other gradient within the range of the tapered angle α of the inner gas-liquid separation tube, preferably with equal gradients, for example, 25°, 30°, 35°, 40°, and a gradient of 5°.

[0083] Then, calculate the equivalent dimensionless centrifugal force a of the inner gas-liquid separation tube: * .

[0084] Since the inner gas-liquid separation tube is provided with a drainage hole 301a, when the gas-liquid two-phase flow moves along the inner gas-liquid separation tube, the liquid-rich phase part will be continuously discharged from the drainage hole 301a, so that the dryness of the medium in the inner gas-liquid separation tube gradually increases. The greater the dryness, the better the gas-liquid separation effect. Therefore, the dryness of the medium in the inner gas-liquid separation tube can well characterize the gas-liquid separation effect. However, the calculation of the dryness is relatively complicated. This application chooses to calculate the equivalent dimensionless centrifugal force. The calculation of the equivalent dimensionless centrifugal force is relatively simple. The equivalent dimensionless centrifugal force is positively correlated with the dryness of the medium in the inner gas-liquid separation tube. Therefore, it can also better characterize the gas-liquid separation effect.

[0085] In a specific embodiment, the calculation process is as follows:

[0086] Calculate the minimum spiral diameter D of the internal gas-liquid separation tube min1 =D max1 -2·H·tan(α / 2),

[0087] Then the equivalent spiral diameter D of the internal gas-liquid separation tube is obtained eq1 =2 / (1 / D min1 +1 / D max1 ),

[0088] Then the equivalent spiral pitch of the internal gas-liquid separation tube is obtained Among them, L1 is the length of the inner gas-liquid separation tube, L1=ωL, L is the length of the gas-liquid separation tube. When only the gas phase heating tube is set without the liquid phase heating tube, based on the consideration of ensuring the gas phase heating effect, the value range of ω is recommended to be between 0.6-0.8. When both the gas phase heating tube and the liquid phase heating tube are set, based on the consideration of both the gas phase heating effect and the liquid phase heating effect, the value range of ω is recommended to be between 0.7-0.85.

[0089] Then the equivalent number of spiral turns of the inner gas-liquid separation tube is obtained, n1=H / s1, preferably n1 is not greater than 15, if it is greater than 15, then the calculation is terminated, n1 is not greater than 8, which is even better. In addition, if the pitch s1 is smaller than the inner diameter d of the inner gas-liquid separation tube,i If , the calculation will also be exited.

[0090] Calculate the gas-liquid two-phase flow density: G = 4q / (π·d i 2 )

[0091] Calculate the void fraction of gas-liquid two-phase flow: Where, the gas phase density ρ g , liquid density ρ l , the surface tension σ is obtained by searching based on the saturation temperature T and general physical property software.

[0092] Then we can get the liquid phase velocity: u l =G(1-x) / (ρ l (1-∈)),

[0093] Then we can get the equivalent dimensionless centrifugal force: a * = k1·u l 2 / (g·D eq1 / 2), where k1 depends on the specific situation, for example, it can be equal to (1.125-0.065n1).

[0094] Then, calculate the equivalent dimensionless friction coefficient f of the inner gas-liquid separation tube: * , f * It is positively correlated with the pressure drop of the internal gas-liquid separation tube.

[0095] Often, the greater the centrifugal force, the greater the friction coefficient and the greater the system pressure drop. Therefore, the friction coefficient is used as one of the indicators to evaluate whether the taper is reasonable. In this way, the designed taper can ensure that the system pressure drop is within a reasonable range.

[0096] In a specific embodiment, the calculation process is as follows:

[0097] Calculate the homogeneous density:

[0098] Calculate the homogeneous viscosity:

[0099] Calculate the homogeneous phase velocity: u = G / ρ

[0100] Then we get the Reynolds number: Re = ρud i / μ

[0101] Then the equivalent dimensionless friction coefficient is obtained: The coefficient k depends on the specific situation. For example, k can be equal to 0.31. *The specific calculation formula is not limited to this, and can be obtained by fitting based on the field test data of the spiral pipeline.

[0102] Then, define the dimensionless lateral area of ​​the insulation cylinder.

[0103] When only gas phase heating tubes are provided but no liquid phase heating tubes are provided, the dimensionless side area A1 of the insulation tube is defined as * The process is:

[0104] Calculate the minimum diameter D of the insulation tube min3 =D min1 +0.5P, where P is the distance from the inner gas-liquid separation tube cone to the outer gas-liquid separation tube cone, and its range should be within 3d i To 5d i between,

[0105] Calculate the maximum diameter D of the insulation tube max3 =D max1 +0.5P,

[0106] Calculate the single-sided side area of ​​the insulation tube.

[0107] Calculate the height of the insulation tube corresponding to one circle around the external gas-liquid separation tube Among them, h is the height of the outer gas-liquid separation tube. Considering that it is mainly used to heat the gas phase, the height of the outer gas-liquid separation tube should not be too low. The recommended range is 0.2H-0.35H.

[0108] Calculate the diameter of the insulation tube corresponding to one circle around the outer gas-liquid separation tube

[0109] Calculate the average diameter of the insulation tube corresponding to one circle around the outer gas-liquid separation tube

[0110] Calculate the single-sided side area under the average diameter of the insulation tube:

[0111] Then the dimensionless lateral area of ​​the insulation tube is defined

[0112] The larger the dimensionless side area of ​​the insulation tube is, the larger the heat exchange area is, and the better the heat exchange effect between the low-pressure medium and the high-pressure medium in the gas-liquid separator is.

[0113] When both gas phase heating tubes and liquid phase heating tubes are provided, the dimensionless side area A2 of the insulation tube is defined as * The process is:

[0114] Calculate the minimum diameter D of the insulation tube min3=D min1 +0.5P, where P is the distance from the inner gas-liquid separation tube cone to the outer gas-liquid separation tube cone, and its range should be within 3d i To 5d i between,

[0115] Calculate the maximum diameter D of the insulation tube max3 =D max1 +0.5P,

[0116] Calculate the single-sided side area of ​​the insulation tube.

[0117] Then the dimensionless lateral area of ​​the insulation tube is defined

[0118] Then, the comprehensive performance parameters are defined.

[0119] When only the gas phase heating tube is set without the liquid phase heating tube, the comprehensive performance parameter E is defined. * =a * (A1 * ) / f * , and then compare the comprehensive performance parameters corresponding to the tapers selected in S1, and determine the value of the taper α according to the comparison result.

[0120] When both gas phase heating tube and liquid phase heating tube are provided, the comprehensive performance parameter F is defined. * =a * (A2 * ) 1 / 3 / f * , and then compare the comprehensive performance parameters corresponding to the tapers selected in S1, and determine the value of the taper α according to the comparison result.

[0121] The comprehensive performance parameters E* and F* take into account the gas-liquid separation capacity of the gas-liquid separator tube (characterized by a*), the pipeline pressure drop (characterized by f*), and the heat exchange effect between the low-pressure medium and the high-pressure medium in the gas-liquid separator (characterized by A1 * , A2*), therefore the comprehensive performance parameters E* and F* can characterize the comprehensive performance of the gas-liquid separator.

[0122] In addition, the equivalent spiral pitch s2 of the external gas-liquid separation tube and the equivalent spiral number n2 of the external gas-liquid separation tube can also be calculated. The calculation process is:

[0123] Calculate the minimum spiral diameter D of the external gas-liquid separation tube min2 =D max1 -2·H·tan(α / 2)+P,

[0124] Calculate the maximum spiral diameter D of the external gas-liquid separation tube max2 =Dmax1 -2·(Hh)·tan(α / 2)+P,

[0125] Then the equivalent spiral pitch of the external gas-liquid separation tube is obtained And the equivalent number of spiral turns of the external gas-liquid separation tube n2=h / s2, where h is the height of the external gas-liquid separation tube. When only a gas phase heating tube is set but no liquid phase heating tube is set, considering that it is mainly used to heat the gas phase, the height of the external gas-liquid separation tube should not be too low. The recommended range is 0.2H-0.35H. When both a gas phase heating tube and a liquid phase heating tube are set, considering both the gas phase heating effect and the liquid phase heating effect, the recommended range is 0.15H-0.3H.

[0126] If s2 is smaller than the inner diameter d of the external gas-liquid separation tube i If yes, exit the calculation.

[0127] When only gas phase heating tubes are provided but no liquid phase heating tubes are provided, it is preferred that n2 is not less than 1 or very close to 1 to ensure that the gas exchanges heat more fully with the heating tubes outside the insulation tube in most cases. If n2 is less than 1, the calculation can be exited. When both gas phase heating tubes and liquid phase heating tubes are provided, it is preferred that n2 is not less than 0.5 to ensure that the gas exchanges heat more fully with the heating tubes outside the insulation tube in most cases. If n2 is less than 0.5, the calculation can be exited.

[0128] The following is a calculation example when only a gas phase heating tube is provided and no liquid phase heating tube is provided.

[0129] In this calculation example, the maximum spiral diameter D of the internal gas-liquid separation tube max1 is 105mm, the height H of the inner gas-liquid separation tube is 110mm, the length L of the gas-liquid separation tube is 1100mm, and the inner diameter d of the inner gas-liquid separation tube and the outer gas-liquid separation tube is i is 15 mm, the medium in the inner gas-liquid separation tube and the outer gas-liquid separation tube is R1234yf, the mass flow rate q is 180 kg / h, the inlet dryness x is 0.5, the saturation temperature T is 7 °C, according to the above maximum spiral diameter D max1 and height H to calculate the maximum taper α max =50°, select 25°, 30°, 35°, 40°, and 45° in the range of 25°-50° for model calculation.

[0130] Take 25° as an example:

[0131] Calculate the minimum spiral diameter D of the internal gas-liquid separation tube min1 =56.2mm, and then the equivalent spiral diameter D of the internal gas-liquid separation tube is obtained eq1 =73.2mm, and then the equivalent spiral pitch of the internal gas-liquid separation tube is obtained Among them, L1=0.7L, and then the equivalent number of spiral turns of the internal gas-liquid separation tube n1=3.314 is obtained.

[0132] Calculate the gas-liquid two-phase flow density G = 282.9 kg / m 2 ·s, according to the saturation temperature T combined with the general physical property software to find the gas phase density ρ g =22.1kg / m 3 , liquid density ρ l =1153.9kg / m 3 , surface tension σ=0.0085024N / m, calculate the gas-liquid two-phase flow void ratio ∈=0.918, and then get the liquid phase velocity u l =1.5m / s, and then the equivalent dimensionless centrifugal force is obtained: a * =(1.125-0.065n1)·u l 2 / (g·D eq1 / 2)=5.727.

[0133] Calculate the homogeneous density ρ = 43.37 kg / m 3 , calculate the homogeneous viscosity μ = 0.01961Pa·s, calculate the homogeneous velocity u = 6.52m / s, and then get Re = 216, and then get the equivalent dimensionless friction coefficient

[0134] Calculate the minimum spiral diameter D of the external gas-liquid separation tube min2 =101.23mm(P takes 3d i ), calculate the maximum spiral diameter D of the external gas-liquid separation tube max2 =115.86mm(P takes 3d i , h is taken as 0.3H), and then the equivalent spiral diameter D of the external gas-liquid separation tube is obtained eq2 =108.05mm, and then the equivalent spiral pitch s2 of the external gas-liquid separation tube is obtained as 39.85mm and the equivalent number of spiral turns n2 as 0.97.

[0135] Calculate the minimum diameter D of the insulation tube min3 =93.36mm, calculate the maximum diameter D of the insulation tube max3 =127.5mm, calculate the single side area of ​​the insulation tube A1 = 36498mm 2 , calculate the height of the insulation tube corresponding to one circle of the outer gas-liquid separation tube h1=34.16mm, calculate the diameter of the insulation tube corresponding to one circle of the outer gas-liquid separation tube D max4 = 93.87 mm, calculate the average diameter D of the insulation tube corresponding to one circle around the outer gas-liquid separation tube max5=86.3mm, the single side area under the average diameter of the insulation tube is calculated as A2 = 4535mm 2 , and then the dimensionless side area A1 of the insulation tube is obtained * =0.72544.

[0136] Then calculate the comprehensive performance parameter E * =a * (A1 * ) / f * The calculated data are as follows. From the table, we can see that the comprehensive performance parameter E corresponding to 35° * Maximum, so the taper of the gas-liquid separation tube is determined to be 35°.

[0137]

[0138] The following is a calculation example when both a gas phase heating tube and a liquid phase heating tube are provided.

[0139] In this calculation example, the maximum spiral diameter D of the internal gas-liquid separation tube max1 is 105 mm, the height H of the inner gas-liquid separation tube is 112 mm, the length L of the gas-liquid separation tube is 1000 mm, and the inner diameters d of the inner gas-liquid separation tube and the outer gas-liquid separation tube are i is 15 mm, the medium in the inner gas-liquid separation tube and the outer gas-liquid separation tube is R1234yf, the mass flow rate q is 180 kg / h, the inlet dryness x is 0.5, the saturation temperature T is 7 °C, according to the above maximum spiral diameter D max1 and height H to calculate the maximum taper α max =50°, select 25°, 30°, 35°, 40°, and 45° in the range of 25°-50° for model calculation.

[0140] Take 25° as an example:

[0141] Calculate the minimum spiral diameter D of the internal gas-liquid separation tube min1 =55.34mm, and then the equivalent spiral diameter D of the internal gas-liquid separation tube is obtained eq1 =72.48mm, and then the equivalent spiral pitch of the internal gas-liquid separation tube is obtained Among them, L1=0.8L, and then the equivalent number of spiral turns of the internal gas-liquid separation tube n1=3.48 is obtained.

[0142] Calculate the gas-liquid two-phase flow density G = 282.9 kg / m 2 ·s, according to the saturation temperature T combined with the general physical property software to find the gas phase density ρ g =22.1kg / m 3 , liquid density ρ l =1153.9kg / m 3, surface tension σ=0.0085024N / m, calculate the gas-liquid two-phase flow void ratio ∈=0.918, and then get the liquid phase velocity u l =1.5m / s, and then the equivalent dimensionless centrifugal force is obtained: a * =(1.125-0.065n1)·u l 2 / (g·D eq1 / 2)=5.718.

[0143] Calculate the homogeneous density ρ = 43.37 kg / m 3 , calculate the homogeneous viscosity μ = 0.01961Pa·s, calculate the homogeneous velocity u = 6.52m / s, and then get Re = 216, and then get the equivalent dimensionless friction coefficient

[0144] Calculate the minimum spiral diameter D of the external gas-liquid separation tube min2 =101.34.mm(P takes 3d i ), calculate the maximum spiral diameter D of the external gas-liquid separation tube max2 =110.27mm(P takes 3d i , h is taken as 0.2H), and then the equivalent spiral diameter D of the external gas-liquid separation tube is obtained eq2 =105.07mm, and then the equivalent spiral pitch s2 of the external gas-liquid separation tube is obtained as 65.94mm and the equivalent number of spiral turns n2 as 0.594.

[0145] Calculate the minimum diameter D of the insulation tube min3 =127.5mm, calculate the maximum diameter D of the insulation tube max3 =87.7mm, calculate the single side area of ​​the insulation tube A1 = 37002.4mm 2 , and then the dimensionless side area A2 of the insulation tube is obtained * =0.8248.

[0146] Then calculate the comprehensive performance parameter F * =a * (A2 * ) 1 / 3 / f * The calculated data are as follows. From the table, we can see that the comprehensive performance parameter F corresponding to 35° * Maximum, so the taper of the gas-liquid separation tube is determined to be 35°.

[0147]

[0148] The above specific examples are used to illustrate the principles and implementation methods of the present application. 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: The gas-liquid separator comprises a shell and: an insulating tube, wherein the central axis of the insulating tube extends in an up-down direction, a lower end of the insulating tube is provided with a lower port, a top of the insulating tube is provided with a vent, the insulating tube divides the internal space of the shell into an inner tube space and an outer tube space, the inner tube space is connected to the upper end of the outer tube space through the vent, and the inner tube space is connected to the lower end of the outer tube space through the lower port; A gas-liquid separation tube, the gas-liquid separation tube comprising an inner gas-liquid separation tube and an outer gas-liquid separation tube, the inner gas-liquid separation tube being spirally wound from top to bottom inside the heat-insulating tube, the outer gas-liquid separation tube being spirally wound from the lower end of the inner gas-liquid separation tube upward outside the heat-insulating tube, a tube wall of the inner gas-liquid separation tube being provided with a plurality of drainage holes in sequence along the tube length direction at a position away from the spiral central axis side thereof; A heating pipe is located inside the shell, and the heating pipe includes a gas phase heating pipe, and the gas phase heating pipe is spirally coiled above the bottom of the shell and outside the insulation tube.

2. The gas-liquid separator according to claim 1, characterized in that: The gas phase heating tube is spirally coiled and located inside the outer gas-liquid separation tube; or, The gas phase heating tube is spirally coiled and located between the external gas-liquid separation tube and the insulation tube and / or above the external gas-liquid separation tube, and a plurality of exhaust holes are sequentially arranged on the tube wall of the external gas-liquid separation tube near the upper side of the spiral central axis along the tube length direction.

3. The gas-liquid separator according to claim 2, characterized in that: All the spiral turns of the gas phase heating tube are arranged in sequence along the up-down direction; or, All the spiral coils of the gas phase heating tube are arranged in sequence and at intervals along a horizontal direction perpendicular to the up-down direction; or, Some of the spiral turns of the gas phase heating tube are arranged in sequence along the up-down direction, and some of the spiral turns are arranged in sequence at intervals along the horizontal direction perpendicular to the up-down direction.

4. The gas-liquid separator according to claim 3, characterized in that: The outer surface of the spiral coil of the gas phase heating tube is provided with fins.

5. The gas-liquid separator according to claim 1, characterized in that: The spiral diameter of each spiral circle of the inner gas-liquid separation tube gradually decreases from top to bottom, so that the inner gas-liquid separation tube is cone-shaped as a whole. The diameter of the insulation tube gradually decreases from top to bottom, so that the insulation tube is cone-shaped as a whole. The spiral diameter of each spiral circle of the outer gas-liquid separation tube gradually increases from bottom to top, so that the outer gas-liquid separation tube is cone-shaped as a whole.

6. The gas-liquid separator according to claim 5, characterized in that: The tapers α of the inner gas-liquid separation tube, the heat-insulating tube and the outer gas-liquid separation tube are the same.

7. The gas-liquid separator according to claim 1, characterized in that: The upper end of the shell is provided with a gas phase outlet, and the upper end of the heat-insulating cylinder abuts against the surrounding area of ​​the gas phase outlet of the shell, so that the gas phase outlet of the shell is connected with the inner space of the heat-insulating cylinder.

8. The gas-liquid separator according to any one of claims 1 to 7, characterized in that: The heating tube comprises a liquid phase heating tube, the liquid phase heating tube is arranged inside the insulation tube and along the inner wall of the insulation tube and / or the liquid phase heating tube is arranged at the bottom of the shell.

9. The gas-liquid separator according to claim 8, characterized in that: The gas-liquid separator includes a control valve, a superheat detection device and a subcooling detection device. The control valve is connected to the liquid phase heating tube and the gas phase heating tube, and is used to increase the mass flow rate of the gas phase heating tube and reduce the mass flow rate of the liquid phase heating tube when the superheat is insufficient, and to increase the mass flow rate of the liquid phase heating tube and reduce the mass flow rate of the gas phase heating tube when the subcooling is insufficient.

10. A method for designing the taper 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, wherein the inner gas-liquid separation tube, the outer gas-liquid separation tube and the heat-insulating tube of the gas-liquid separator are all conical as a whole and have the same taper α, and the value of the taper α is determined by the taper design method, and the taper design method comprises: S1. Eliminate the unreasonable range of the taper α of the internal gas-liquid separation tube, and then select several angles within a reasonable range as the taper of the internal gas-liquid separation tube for model calculation; S2. Calculate the equivalent dimensionless centrifugal force a of the internal gas-liquid separation tube * ; S3. Calculate the equivalent dimensionless friction coefficient f of the internal gas-liquid separation tube * ; S4. Define the dimensionless lateral area A1 of the insulation tube according to the minimum diameter, maximum diameter and single-sided lateral area of ​​the insulation tube. * ;or, The dimensionless lateral area A2 of the insulation tube is defined based on the minimum diameter, maximum diameter, single-sided lateral area, and the diameter of the insulation tube corresponding to a circle of the external gas-liquid separation tube. * ; S5. Define comprehensive performance parameter E * =a * (A1 * ) / f * Or define the comprehensive performance parameter F * =a * (A2 * ) 1 / 3 / f * , compare the comprehensive performance parameters corresponding to each taper selected in S1, and determine the value of the taper α according to the comparison result.

Images