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

Abstract

The invention discloses a gas-liquid separator and a method for determining the taper angle of a rotational flow assembly of the gas-liquid separator. The gas-liquid separator comprises a shell and the rotational flow assembly located in the shell. The rotational flow assembly comprises a fixed shaft, blades and a separation cylinder; the separation barrel divides a shell cavity of the shell into an inner cavity and an outer cavity, the outer cavity surrounds the inner cavity, and a main body of the separation barrel is in a big-end-up conical shape; the fixed shaft is located in the middle of the separation cylinder, the blade spirally extends downwards along the inner wall of the separation cylinder, the inner edge of the blade is fixed to the fixed shaft, and the outer edge of the blade is fixed to the separation cylinder; a spiral channel is formed between the blade and the separation cylinder; a first liquid discharge hole is formed in the cylinder wall of the separation cylinder, an inlet of the gas-liquid separator is formed in the top of the shell and communicates with the spiral channel, and an outlet of the gas-liquid separator is connected with a lower port of the separation cylinder. According to the gas-liquid separator, through structural optimization, the rotational flow intensity of downstream gas-liquid two phases can be kept, the adverse effect on gas-liquid separation caused by attenuation of the rotational flow intensity is effectively overcome, and the gas-liquid separation efficiency is improved.

Description

Technical Field

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

[0002] The cyclone path of the cyclone gas-liquid separator is mostly set as a cyclone centrifugal channel of equal diameter. During the gas-liquid separation process, due to resistance and energy dissipation, the intensity of the swirl will rapidly decay along the direction of the rotation path, which can easily cause the liquid film state attached to the wall to be destroyed and secondary entrainment of droplets to occur, thereby reducing the gas-liquid separation efficiency. Summary of the invention

[0003] The purpose of the present application is to provide a gas-liquid separator which, through structural optimization, can maintain the swirl intensity of the downstream gas-liquid two-phase, effectively overcome the adverse effects of swirl intensity attenuation on gas-liquid separation, and improve the efficiency of gas-liquid separation.

[0004] In order to solve the above technical problems, the present application provides a gas-liquid separator, comprising a housing and a cyclone assembly, wherein the cyclone assembly is located inside the housing; the cyclone assembly comprises a fixed shaft, blades and a separation cylinder;

[0005] The separation cylinder divides the shell cavity of the outer shell into an inner cavity and an outer cavity, the outer cavity surrounds the inner cavity, and the main body of the separation cylinder is in a conical shape with a larger top and a smaller bottom; the fixed shaft is located in the middle of the separation cylinder, and the blades extend downward in a spiral along the inner wall of the separation cylinder, the inner edges of the blades are fixed to the fixed shaft, and the outer edges of the blades are fixed to the separation cylinder; a spiral channel is formed between the blades and the separation cylinder;

[0006] A first liquid discharge hole is arranged on the wall of the separation cylinder, an inlet of the gas-liquid separator is arranged at the top of the shell and communicated with the spiral channel, and an outlet of the gas-liquid separator is communicated with the lower port of the separation cylinder.

[0007] The gas-liquid separator sets the separation cylinder of the cyclone assembly to a conical structure with a large top and a small bottom, and also sets the blades in the separation cylinder to a conical spiral structure with a large top and a small bottom, so that a spiral channel with a large top and a small bottom is formed between the separation cylinder and the blades. In this way, after the gas-liquid two-phase flow flows from the inlet into the spiral channel of the gas-liquid separator, the fluid state is a spiral flow state. Under the action of the rotating centrifugal force, the liquid phase medium is thrown to the inner wall of the separation cylinder, and a part of it can be discharged to the outer cavity of the gas-liquid separator through the first liquid discharge hole set on the separation cylinder, and the other part will be discharged to the outer cavity through the lower port of the separation cylinder along the inner wall of the separation cylinder under the action of gravity. The gas phase medium flows downward in a spiral near the fixed axis side and is discharged from the outlet of the gas-liquid separator through the lower port of the separation cylinder, thereby achieving gas-liquid separation.

[0008] When the gas-liquid separator is performing gas-liquid separation, the cross-sectional area of ​​the spiral channel is reduced in the flow direction, and the flow velocity of the gas-liquid two-phase flow is accelerated, which can maintain the swirl intensity of the downstream gas-liquid two-phase to a certain extent and slow down the attenuation of the swirl intensity. At the same time, part of the liquid phase medium is discharged through the first liquid discharge hole, and the downward rotating force does not need to push the part of the liquid phase medium, which is also conducive to maintaining the swirl intensity, thereby keeping the gas-liquid two-phase interface in a relatively stable state, and can effectively improve the efficiency of gas-liquid separation.

[0009] In an optional implementation, a spiral flow channel portion is formed on the inner cylinder wall surface of the separation cylinder, and the spiral direction of the flow channel portion is consistent with the spiral direction of the blades.

[0010] In an optional implementation, part of the wall of the separation cylinder is recessed toward the direction of the outer cavity to form the flow channel portion, and the first liquid drainage hole is located in the flow channel portion.

[0011] In an optional implementation, a plurality of the first liquid drainage holes are provided, and the plurality of the first liquid drainage holes are arranged along an extension direction of the flow channel portion.

[0012] In an optional implementation, the flow channel portion includes an upper flow channel portion and a lower flow channel portion, the upper flow channel portion and the lower flow channel portion extend downward in an equidistant spiral, the height of the center of the upper flow channel portion relative to the outer shell is higher than the height of the center of the lower flow channel portion relative to the outer shell, and the first drainage hole is arranged in the lower flow channel portion.

[0013] In an optional implementation, the outer edge of the blade is staggered from the flow channel portion of the separation tube at a fixed position of the separation tube and is located in the middle of two adjacent flow channel portions.

[0014] In an optional implementation, the vortex assembly also includes a liquid collecting tray, which includes a circumferential wall and a bottom wall, the upper port of the circumferential wall is connected to the lower port of the separation cylinder, the middle portion of the bottom wall has a discharge port, and the bottom wall also has a second liquid drainage hole, which is radially located outside the discharge port and connects the inner cavity and the outer cavity.

[0015] In an optional implementation, the liquid collecting tray is further provided with a baffle in the shape of a cone, a lower port of the baffle is connected to the discharge port, the baffle is located in the tray cavity of the liquid collecting tray, and the outer dimensions of the baffle gradually decrease from top to bottom.

[0016] In an optional implementation, the shell includes a cylindrical shell peripheral wall, a shell bottom wall and a shell top wall; the inlet of the gas-liquid separator is arranged on the shell top wall.

[0017] The present application also provides a method for determining the taper angle of a cyclone component of a gas-liquid separator, wherein the gas-liquid separator is any of the gas-liquid separators described above, and the taper angle α of the cyclone component has a set value range, and within the value range, the comprehensive performance coefficient V of the cyclone component is selected. * The taper angle corresponding to the maximum value of is the optimal taper angle actually set for the swirl component;

[0018] The comprehensive performance coefficient V of the swirl component * By formula V * =a * / f * Sure;

[0019] Among them, a * is the equivalent dimensionless centrifugal force of the cyclone component, f * is the equivalent dimensionless friction coefficient of the swirl component.

[0020] The determination method is used to determine the taper angle of the cyclone component 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.

[0021] In an optional implementation, the equivalent dimensionless centrifugal force a of the cyclone component is * Determined by the following formula:

[0022] a * = k1·u l 2 / (g·D eq / 2);

[0023] u l =G(1-x) / (ρ l (1-∈));

[0024]

[0025] G=4q / (π·d i 2 );

[0026]

[0027] D eq =2 / (1 / D min1 +1 / D max1 ), D max1 =k2·D max ;

[0028] D min1 =k2·D min = k2·(D max -2·H·tan(α / 2));

[0029] Among them, k1 and k2 are correction coefficients, u l is the velocity of the liquid medium, D eq is the equivalent spiral diameter of the spiral channel, H is the axial height of the spiral channel, L is the length of the spiral channel, 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 equivalent inner diameter of the spiral channel, D max is the maximum diameter of the separation cylinder or the maximum diameter of the blade, D min is the minimum diameter of the separation tube or the minimum diameter of the blade, D max1 is the maximum spiral diameter of the spiral channel, D min1 is the minimum spiral diameter of the spiral channel.

[0030] In an optional implementation, k1 = 1.125-0.065n, n = H / s,

[0031] Wherein, n is the equivalent number of spiral turns of the spiral channel, and s is the equivalent spiral pitch of the spiral channel.

[0032] In an optional implementation, the equivalent dimensionless friction coefficient f * Determined by the following formula:

[0033]

[0034] Re=ρud i / μ;

[0035] u=G / ρ;

[0036] 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.

[0037] In an optional implementation, the equivalent dimensionless friction coefficient f * It is determined according to the following formula:

[0038] Where k is a constant.

[0039] In an optional implementation, when the value of the taper angle α of the swirl component corresponding to the equivalent number of spiral turns n of the spiral channel is greater than a preset value, the value of the taper angle α is excluded.

[0040] 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));

[0041] Among them, D max is the maximum diameter of the separation cylinder or the maximum diameter of the blade, and H is the axial height of the spiral channel. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] Figure 1 A schematic structural diagram of an embodiment of a gas-liquid separator provided in the present application;

[0043] Figure 2 for Figure 1 A cross-sectional schematic diagram of a gas-liquid separator is shown;

[0044] Figure 3 for Figure 2 A partial enlarged view of the area where the central liquid collecting tray is located;

[0045] Figure 4 for Figure 1 Schematic diagram of the partial structure of the gas-liquid separator;

[0046] Figure 5 for Figure 4 A schematic diagram of a partial structure of the gas-liquid separator from another perspective is shown;

[0047] Figure 6 It is a model diagram of the cyclone component of the gas-liquid separator in a specific embodiment.

[0048] Description of reference numerals:

[0049] Shell 10, shell peripheral wall 11, shell top wall 12, shell bottom wall 13, inner cavity 101, outer cavity 102;

[0050] Swirl assembly 20, separation cylinder 21, first liquid drain hole 211, flow channel portion 212, upper flow channel portion 2121, lower flow channel portion 2122, fixed shaft 22, blades 23, liquid collecting tray 24, tray peripheral wall 241, tray bottom wall 242, discharge port 2421, second liquid drain hole 2422, baffle 243;

[0051] The inlet pipe is connected to 31 and the outlet pipe is connected to 32. DETAILED DESCRIPTION

[0052] In order to enable those skilled in the art to better understand the present application, the present application is further described in detail below in conjunction with the accompanying drawings and specific implementation methods.

[0053] Please refer to Figure 1 and Figure 2 , Figure 1 A schematic structural diagram of an embodiment of a gas-liquid separator provided in the present application; Figure 2 for Figure 1 Schematic cross-sectional view of the gas-liquid separator shown.

[0054] In this embodiment, the gas-liquid separator includes a shell 10 and a cyclone component 20 , and the cyclone component 20 is located inside the shell 10 .

[0055] The housing 10 has an inlet and an outlet. The inlet is located at the top of the housing 10, and the outlet is located at the bottom of the housing 10. Generally, the inlet of the housing 10 can be connected to an inlet pipe 31, and the outlet can be connected to an outlet pipe 32, so as to facilitate connection with relevant pipelines in the thermal management application scenario through the pipe.

[0056] The cyclone assembly 20 includes a separation cylinder 21, a fixed shaft 22 and blades 23; the separation cylinder 21 separates the shell cavity of the outer shell 10 into an inner cavity 101 and an outer cavity 102, and the outer cavity 102 surrounds the inner cavity 101; the main body of the separation cylinder 21 is in a conical shape with a larger top and a smaller bottom; the fixed shaft 22 is located in the middle of the separation cylinder 21, and the blades 23 extend downward along the inner wall of the separation cylinder 21 in a spiral, the inner edge of the blades 23 is fixed to the fixed shaft 22, and the outer edge of the blades 23 is fixed to the separation cylinder 21, forming a spiral channel between the blades 23 and the separation cylinder 21. The inlet of the gas-liquid separator is connected to the aforementioned spiral channel.

[0057] A first liquid discharge hole 211 is provided on the wall of the separation cylinder 21 , and the lower port of the separation cylinder 21 is connected to the outlet of the gas-liquid separator. Specifically, the lower port of the separation cylinder 21 can be connected to the outlet of the gas-liquid separator through an outlet pipe 32 .

[0058] The gas-liquid separator is used to perform gas-liquid separation on a gas-liquid two-phase flow. With the above-mentioned structural arrangement, the gas-liquid two-phase flow flows into the gas-liquid separator from the inlet pipe 31. Specifically, the gas-liquid two-phase flow flowing in from the inlet pipe 31 enters the spiral channel formed between the blades 23 and the separation cylinder 21. Since the spiral channel is a spiral structure, the flow state of the fluid is also a spiral flow state. Under the action of the rotating centrifugal force, the liquid phase medium is thrown to the inner wall of the separation cylinder 21. Since the wall of the separation cylinder 21 is provided with a first liquid discharge hole 211, the liquid phase medium is discharged to the inner wall of the separation cylinder 21. A portion of the liquid medium will be discharged to the outer cavity 102 through the first drainage hole 211, and will be deposited at the bottom of the shell cavity of the outer shell 10 under the action of gravity. Another portion of the liquid medium will flow downward along the inner wall of the separation cylinder 21 under the action of gravity, and will be discharged to the outer cavity 102 through the lower port of the separation cylinder 21. During this process, the gaseous medium will flow downward in a spiral near the fixed axis 21, that is, near the middle of the separation cylinder 21, and will be discharged from the outlet pipe 32 at the bottom of the outer shell 10 through the lower port of the separation cylinder 21, thereby realizing gas-liquid separation.

[0059] Due to the above-mentioned structural arrangement, the channel of the gas-liquid separator for supplying the gas-liquid two-phase flow is a spiral channel in a conical shape that is larger at the top and smaller at the bottom. In the flow direction, the cross-sectional area of ​​the spiral channel decreases, and the flow velocity of the gas-liquid two-phase flow is accelerated, which can maintain the swirl intensity of the downstream gas-liquid two-phase to a certain extent and slow down the attenuation of the swirl intensity. At the same time, part of the liquid phase medium is discharged through the first liquid discharge hole, and the downward rotating force does not need to push the part of the liquid phase medium, which is also conducive to maintaining the swirl intensity, thereby keeping the gas-liquid two-phase interface in a relatively stable state, reducing the secondary entrainment phenomenon, and effectively improving the efficiency of gas-liquid separation.

[0060] In addition, the upper-larger-and-lower-smaller structure of the spiral channel can reduce the distance that the liquid medium moves toward the wall of the separation cylinder 21 in the downstream of the flow direction, which is conducive to the liquid medium quickly contacting the separation cylinder 21 and being discharged in time.

[0061] It should be noted here that the conical shape of the aforementioned separation cylinder 21 and the conical spiral structure of the blade 23 do not represent a cone in the strict mathematical sense. As long as the shape of the separation cylinder 21 is approximately conical and the spiral structure of the blade 23 is also approximately conical, they are within the protection scope of this application.

[0062] In the specific implementation, Figure 2 As shown, the height of the inner edge of the blade 23 connected to the fixed shaft 22 is higher than the outer edge of the blade 23 connected to the separation cylinder 21, that is, the blade 23 is in an inclined state with the inside higher and the outside lower. The blade 23 is formed in a spiral shape in this inclined state, which can improve the smoothness of the flow of the gas-liquid two-phase flow.

[0063] Please refer to Figures 3 to 5 , Figure 3 for Figure 2A partial enlarged view of the area where the central liquid collecting tray is located; Figure 4 for Figure 1 Schematic diagram of the partial structure of the gas-liquid separator; Figure 5 for Figure 4 A schematic diagram of the partial structure of the gas-liquid separator from another perspective is shown.

[0064] In one implementation, the swirl assembly 20 may further include a collecting plate 24, which includes a plate peripheral wall 241 and a plate bottom wall 242, wherein the upper port of the plate peripheral wall 241 is connected to the lower port of the separation cylinder 21, the middle of the plate bottom wall 242 has a discharge port 2421, and the discharge port 2421 is connected to the outlet of the gas-liquid separator, and the plate bottom wall 242 also has a second liquid discharge hole 2422, which is radially located outside the discharge port 2421 and connects the inner cavity 101 and the outer cavity 102. The radial direction here refers to the direction perpendicular to the axial direction of the gas-liquid separator, or the direction perpendicular to the axial direction of the separation cylinder 21.

[0065] In this way, a collecting plate 24 is set at the lower end of the separation cylinder 21, and the liquid medium flowing downward along the inner wall of the separation cylinder 21 can be first guided to the collecting plate 24, and then discharged to the outer cavity 102 through the second drainage hole 2422 of the collecting plate 24. The collecting plate 24 can effectively gather the liquid medium that is not discharged through the first drainage hole 211, and discharge it from the second drainage hole 2422 under the action of gravity sedimentation, thereby improving the effectiveness of gas-liquid separation.

[0066] In a specific configuration, the liquid collecting tray 24 may be provided with a plurality of second liquid drain holes 2422 , and the plurality of second liquid drain holes 2422 are distributed around the drain port 2421 .

[0067] Figure 5 In the example shown, the plurality of second drainage holes 2422 are distributed on a circumference around the discharge port 2421. In other implementations, the plurality of second drainage holes 2422 may also be distributed on different circumferences. The shape, size, number, and arrangement of the second drainage holes 2422 may be selected according to actual application requirements and are not limited here.

[0068] In the specific setting, the discharge port 2421 of the bottom wall 242 of the liquid collecting tray 24 is directly connected to the outlet of the gas-liquid separator, so that the gas phase medium separated by the spiral channel can be directly discharged from the outlet of the gas-liquid separator through the discharge port 2421, avoiding the gas phase medium from carrying the liquid phase medium after entering the outer cavity 102, thereby ensuring the effect of gas-liquid separation.

[0069] In one implementation, in order to simplify the structural arrangement, the outlet of the housing 10 corresponds to the outlet 2421 of the liquid collecting tray 24 in the axial direction, so that the outlet pipe 32 connected to the outlet can be directly connected to the outlet 2421. Figure 2 , Figure 4 and Figure 5 In other implementations, the discharge port 2421 of the liquid collecting tray 24 may also be connected to the outlet pipe 32 via an intermediate transfer pipe.

[0070] In a further solution, the liquid collecting tray 24 may also be provided with a baffle 243, which is a conical cylindrical structure, the lower port of the baffle 243 is connected to the discharge port 2421 of the tray bottom wall 242, the baffle 243 is located in the tray cavity of the liquid collecting tray 24, and the external dimensions of the baffle 243 gradually decrease from top to bottom. In other words, the peripheral wall of the discharge port 2421 of the tray bottom wall 242 extends upward and tilts outward to form the baffle 243. In this way, the baffle 243 is in a trumpet shape with a larger upper part and a smaller lower part, which is conducive to guiding the separated gas phase medium to flow from the discharge port 2421 to the outlet pipe 32, and at the same time, it can also prevent the liquid phase medium that flows along the wall of the separation tube 21 to the liquid collecting tray 24 from entering the discharge port 2421, which can further improve the gas-liquid separation effect.

[0071] In actual configuration, the peripheral wall 241 of the liquid collecting tray 24 may also be in a conical shape, consistent with the taper of the separation cylinder 21, as shown in the diagram, so that when the liquid phase medium flows along the cylinder wall of the separation cylinder 21 into the liquid collecting tray 24, the flow path is smooth, avoiding the increase of resistance, which is conducive to the gathering and discharge of the liquid phase medium. Of course, the shape of the liquid collecting tray 24 may also be other, not limited to that shown in the diagram.

[0072] In one implementation, a spiral flow channel portion 212 may be formed on the inner wall of the separation tube 21 , and the spiral direction of the spiral flow channel portion 212 is consistent with the blade 23 . It can be understood that the flow channel portion 212 also has a conical spiral structure as a whole.

[0073] The arrangement of the flow channel portion 212 can reduce the inertia of the liquid phase medium during discharge and the secondary entrainment caused by the shearing effect of the gas phase medium on the liquid phase medium, thereby improving the efficiency of gas-liquid separation.

[0074] The spiral direction of the flow channel portion 212 and the blades 23 may be clockwise or counterclockwise.

[0075] In the specific configuration, part of the wall of the separation cylinder 21 is recessed toward the direction of the outer cavity 102 to form the flow channel portion 212, so that the position corresponding to the flow channel portion 212 on the outer wall of the separation cylinder 21 is a convex structure. The first liquid discharge hole 211 is located at the flow channel portion 212, so that the liquid medium thrown toward the wall of the separation cylinder 21 can be discharged from the first liquid discharge hole 211 to the outer cavity in time.

[0076] Specifically, the outer edge of the blade 23 is staggered with the flow channel portion 212 at a fixed position of the separation tube 21 and is located in the middle of two adjacent flow channel portions 212 .

[0077] In the specific configuration, a plurality of first liquid discharge holes 211 are provided, and the plurality of first liquid discharge holes 211 are arranged along the extension direction of the flow channel portion 212. In this way, at different height directions, the liquid phase medium thrown toward the flow channel portion 212 of the separation cylinder 21 can be at least partially discharged from the first liquid discharge holes 211, which can slow down the decrease in the swirl intensity.

[0078] In the specific configuration, the flow channel portion 212 includes an upper flow channel portion 2121 and a lower flow channel portion 2122. The upper flow channel portion 2121 and the lower flow channel portion 2122 extend downward in an equidistant spiral. The height of the center of the upper flow channel portion 2121 relative to the outer shell 10 is higher than the height of the center of the lower flow channel portion 2122 relative to the outer shell 10. The first drainage hole 211 is located in the lower flow channel portion 2122, which is more conducive to the discharge of the liquid medium from the first drainage hole 211.

[0079] In one implementation, the outer shell 10 of the gas-liquid separator includes a cylindrical shell peripheral wall 11, a shell bottom wall 13, and a shell top wall 12. The shell peripheral wall 11 and the shell top wall 12 are both circular, and respectively block the upper end opening and the lower end opening of the shell peripheral wall 11. The aperture of the upper port of the separation cylinder 21 is consistent with the aperture of the shell peripheral wall 11, and the inlet of the gas-liquid separator is arranged on the shell top wall 12. In this way, it can be ensured that the gas-liquid two-phase flow flowing in from the inlet flows into the spiral channel for gas-liquid separation. At the same time, this structural setting can ensure the size of the spiral channel as much as possible within the same space size.

[0080] Specifically, the upper port of the separation cylinder 21 can be arranged flush with the upper port of the shell peripheral wall 11 to ensure that the gas-liquid two-phase flow flowing in through the inlet pipe 31 directly enters the spiral channel, so as to improve the gas-liquid separation effect of the gas-liquid separator.

[0081] The taper angle of the cyclone component 20 of the gas-liquid separator affects the relevant parameters of the spiral channel and correspondingly affects the gas-liquid separation effect. In order to achieve a better gas-liquid separation effect, an embodiment of the present application also provides a method for determining the taper angle of the cyclone component 20 of the gas-liquid separator.

[0082] For the convenience of determination, the taper angle α of the swirl assembly 20 may be represented by the taper angle of the partition cylinder 21 or the taper angle of the blade 23 .

[0083] Please refer to Figure 6 , Figure 6 It is a model diagram of the cyclone component of the gas-liquid separator in a specific embodiment.

[0084] In order to facilitate the determination of the taper angle α of the swirl assembly 20, the spiral channel formed between the separation cylinder 21 and the blades 23 can be equivalent to Figure 6 The maximum spiral diameter D of the conical helix in max1 It is smaller than the maximum diameter of the partition cylinder 21 and also smaller than the maximum diameter of the blade 23 . Figure 6The solid line in shows the actual conical structure of the swirl component 20, and the dotted line and the double-dotted line respectively show the conical structure of the swirl component 20 when the conical angle is minimum and maximum.

[0085] The taper angle α of the swirl component 20 has a set value range, within which the comprehensive performance coefficient V of the swirl component 20 is selected. * The taper angle corresponding to the maximum value of is the optimal taper angle actually set for the cyclone component. The structural parameters of the separation cylinder 21 and the blades 23 are set according to this optimal taper angle, so that the cyclone component 20 can achieve a relatively good gas-liquid separation effect.

[0086] The comprehensive performance coefficient V of the swirl assembly 20 * The formula V * =a * / f * Sure.

[0087] Among them, a * is the equivalent dimensionless centrifugal force of the cyclone assembly 20, f * is the equivalent dimensionless friction coefficient of the swirl component 20.

[0088] Here, considering that the first liquid discharge hole 211 is provided on the separation cylinder 21 of the conical cyclone component 20 to facilitate the escape of the liquid medium under the action of centrifugation, in the process of the low-pressure two-phase medium running downward along the cyclone component 20, the liquid medium keeps escaping, and the dryness of the medium flowing in the cyclone component 20 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. In order to simplify the calculation, this application is mainly evaluated by 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 cyclone component 20; 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 by relative comparison under different taper angles.

[0089] Here, the comprehensive performance coefficient V of the swirl assembly 20 is * By formula V * =a * / f * Determine, taking into account the centrifugal force a * The influence of the spiral channel pressure drop f * It can be considered that the greater the centrifugal force under the unit pressure drop condition, the better the taper angle condition.

[0090] In one implementation, the equivalent dimensionless centrifugal force a of the swirl assembly 20 is * Determined by the following formula:

[0091] a * = k1·u l 2 / (g·D eq / 2);

[0092] u l =G(1-x) / (ρ l (1-∈));

[0093]

[0094] G=4q / (π·d i 2 );

[0095]

[0096] D eq =2 / (1 / D min1 +1 / D max1 ), D max1 =k2·D max ;

[0097] D min1 =k2·D min =0.5(D max -2·H·tan(α / 2));

[0098] Among them, k1 and k2 are correction coefficients, u l is the velocity of the liquid medium, D eq is the equivalent spiral diameter of the spiral channel, H is the axial height of the spiral channel, L is the length of the spiral channel, 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 equivalent inner diameter of the spiral channel, D max D is the maximum diameter of the separator tube or the maximum diameter of the blade. min D is the minimum diameter of the separator or the minimum diameter of the blade. max1 is the maximum spiral diameter of the spiral channel, D min1 is the minimum spiral diameter of the spiral channel.

[0099] Among them, the equivalent inner diameter d of the spiral channel i The volume of the spiral channel is abstracted as the equivalent diameter d i Rotate along the spiral direction, then π(d i / 2) 2·L=1 / 3·π·H·(D max 2 +D min D max +D min 2 ) / 4, so we can get the above d i formula.

[0100] When the overall dimensions of the gas-liquid separator are determined, that is, when the dimensions of the housing 10 are determined, the maximum diameter D of the separation cylinder 21 or the blade 23 is max It can be determined that the axial height H of the spiral channel and the length L of the spiral channel can be determined in advance. According to the actual application scenario, the mass flow rate of the refrigerant, 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 swirl component 20, the corresponding equivalent dimensionless centrifugal force a can be calculated. * .

[0101] When setting specifically, the correction coefficient k1 can be determined by the formula: k1 = 1.125-0.065n; where n = H / s, n is the equivalent number of spiral turns of the spiral channel, and s is the equivalent spiral pitch of the spiral channel.

[0102] In specific settings, the correction coefficient k2 can be selected as 0.5, that is, the maximum spiral diameter of the spiral channel can be equivalent to half of the maximum diameter of the separation cylinder 21 or the blade 23, and the minimum spiral diameter of the spiral channel can be equivalent to half of the minimum diameter of the separation cylinder 21 or the blade 23.

[0103] Of course, the correction coefficients k1 and k2 can be adjusted according to different application scenarios.

[0104] When specifically configured, the equivalent dimensionless friction coefficient f of the swirl component 20 is * It can be determined by the following formula:

[0105]

[0106] Re=ρud i / μ;

[0107] u=G / ρ;

[0108] 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.

[0109] Specifically, the equivalent dimensionless friction coefficient f * It can be determined according to the following formula:

[0110] Where k is a constant and can be selected according to the actual application scenario. Equivalent dimensionless friction coefficient f * It can also be calculated using other formulas.

[0111] In specific settings, the taper angle α of the swirl component 20 has a value range of α min ≤α<α max .

[0112] 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 spiral channel will be increased, which is not conducive to improving the comprehensive performance of gas-liquid separation.

[0113] Among them, α max =2·arctan(D max / (2·H)), combined Figure 6 , which can be determined based on triangular geometric relationships.

[0114] When the taper angle α of the swirl assembly 20 is determined, a series of values ​​can be selected within the above value range to calculate the corresponding comprehensive performance coefficient V * According to the calculation results, select the comprehensive performance coefficient V * The corresponding taper angle α when it is at the maximum is the optimal value actually set for the swirl component 20 .

[0115] Specifically, multiple angle values ​​may be listed in the above value range in increments of a certain degree.

[0116] In practical applications, when the equivalent number of spiral turns n of the spiral channel corresponding to the value of the taper angle α of the swirl component 20 is greater than the preset value, the value of the taper angle α is excluded. According to experience, too large an equivalent number of spiral turns is not beneficial to the gas-liquid separation effect, so the preset value of the equivalent number of spiral turns 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.

[0117] The following is a specific example to illustrate the method for determining the taper angle α of the cyclone component 20 of the gas-liquid separator.

[0118] 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 cyclone assembly, in an application example, the parameters corresponding to the application scenario can be obtained: the maximum diameter of the separation cylinder 21 is D maxIt is 104mm, the axial height H of the spiral channel is 110mm, the length L of the spiral channel is 450mm, the refrigerant is R1234yf, its mass flow rate q is 180kg / h, the inlet dryness x of the gas-liquid separator is 0.5 and the saturation temperature T is 7°C.

[0119] First determine the setting range of the taper angle α of the swirl component 20, 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°.

[0120] 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.

[0121] According to a series of selected values ​​of the taper angle α, the maximum spiral diameter D of a series of corresponding spiral channels can be calculated: max1 , minimum spiral diameter D min1 , thus the equivalent spiral diameter D of the spiral channel can be determined eq , equivalent helical pitch s and equivalent inner diameter d of the helical channel i .

[0122] Taking the taper angle α as 25° as an example, the calculated D max1 52mm (k2 is 0.5), D min1 27.61mm, D eq is 36.07mm, s is 28.55mm, n is 3.852, d i It is 39.97mm.

[0123] According to the refrigerant saturation temperature of 7℃, the density of the gas phase medium ρ can be obtained by combining the general physical property table g 22.1kg / m 3 , the density of the liquid medium ρ l 1153.9kg / m 3 , surface tension σ is 0.0085024N / m), combined with the above-mentioned parameters and related formulas, the flow density G of the refrigerant can be determined to be 39.84kg / m 2 ·s, the refrigerant porosity ∈ is 0.8769, and the liquid medium u l The speed is 0.140278m / s, and the equivalent dimensionless centrifugal force a * It is 0.097.

[0124] According to the above physical parameters and the inlet dryness x, the homogeneous density ρ can be obtained as 43.369 kg / m 3 , the homogeneous viscosity μ is 0.019612 Pa·s, the homogeneous velocity u is 0.9187 m / s, and combined with the above-mentioned related parameters, the corresponding Reynolds number Re can be obtained as 81.2, so that the equivalent dimensionless friction coefficient f can be determined * is 0.0161 (k here is 0.31), so the comprehensive performance coefficient V of the swirl assembly 20 corresponding to the taper angle α of 25° can be calculated. * It is 6.02.

[0125] Similarly, the comprehensive performance coefficient V corresponding to other selected values ​​of the taper angle α can be determined: * , please refer to the following Table 1.

[0126] It can be seen from the table that when the taper angle α is 40°, the comprehensive performance coefficient V * Therefore, in the aforementioned application scenario, the cyclone component 20 can be set according to the taper angle of the cyclone component 20 being 40°, so that the gas-liquid separator has a relatively good gas-liquid separation effect.

[0127] Table 1- Correspondence table between the taper angle and related parameters of the swirl component 20 in an application scenario

[0128]

[0129] In other application scenarios, the relevant design parameters of the cyclone component 20 of the gas-liquid separator may also be set according to the above determination method, and will not be described in detail.

[0130] 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 comprises a housing and a swirl assembly, wherein the swirl assembly is located inside the housing; the swirl assembly comprises a fixed shaft, blades and a separation cylinder; The separation cylinder divides the shell cavity of the outer shell into an inner cavity and an outer cavity, the outer cavity surrounds the inner cavity, and the main body of the separation cylinder is in a conical shape with a larger top and a smaller bottom; the fixed shaft is located in the middle of the separation cylinder, and the blades extend downward in a spiral along the inner wall of the separation cylinder, the inner edges of the blades are fixed to the fixed shaft, and the outer edges of the blades are fixed to the separation cylinder; a spiral channel is formed between the blades and the separation cylinder; A first liquid discharge hole is arranged on the wall of the separation cylinder, an inlet of the gas-liquid separator is arranged at the top of the shell and communicated with the spiral channel, and an outlet of the gas-liquid separator is communicated with the lower port of the separation cylinder.

2. The gas-liquid separator according to claim 1, characterized in that: A spiral flow channel portion is formed on the inner cylinder wall surface of the separation cylinder, and the spiral direction of the flow channel portion is consistent with the spiral direction of the blades.

3. The gas-liquid separator according to claim 2, characterized in that: Part of the wall of the separation cylinder is recessed toward the direction of the outer cavity to form the flow channel portion, and the first liquid discharge hole is located in the flow channel portion.

4. The gas-liquid separator according to claim 3, characterized in that: A plurality of the first liquid drainage holes are provided, and the plurality of the first liquid drainage holes are arranged along the extension direction of the flow channel portion.

5. The gas-liquid separator according to claim 3, characterized in that: The flow channel portion includes an upper flow channel portion and a lower flow channel portion, and the upper flow channel portion and the lower flow channel portion extend downward in an equidistant spiral. The height of the center of the upper flow channel portion relative to the shell is higher than the height of the center of the lower flow channel portion relative to the shell, and the first drainage hole is arranged in the lower flow channel portion.

6. The gas-liquid separator according to claim 2, characterized in that: The outer edge of the blade is staggered from the flow channel portion of the separation tube at a fixed position of the separation tube and is located in the middle of two adjacent flow channel portions.

7. The gas-liquid separator according to any one of claims 1 to 6, characterized in that: The vortex assembly also includes a liquid collecting tray, which includes a tray circumferential wall and a tray bottom wall. The upper port of the tray circumferential wall is connected to the lower port of the separation cylinder. The middle part of the tray bottom wall has a discharge port. The tray bottom wall also has a second liquid discharge hole, which is radially located outside the discharge port and connects the inner cavity and the outer cavity.

8. The gas-liquid separator according to claim 7, characterized in that: The liquid collecting tray is also provided with a baffle in the shape of a cone, the lower port of the baffle is connected to the discharge port, the baffle is located in the tray cavity of the liquid collecting tray, and the external size of the baffle gradually decreases from top to bottom.

9. The gas-liquid separator according to any one of claims 1 to 8, characterized in that: The shell comprises a cylindrical shell peripheral wall, a shell bottom wall and a shell top wall; the inlet of the gas-liquid separator is arranged on the shell top wall.

10. A method for determining the taper angle of a cyclone component 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 α of the cyclone component has a set value range, within which the comprehensive performance coefficient V of the cyclone component is selected. * The taper angle corresponding to the maximum value of is the optimal taper angle actually set for the swirl component; The comprehensive performance coefficient V of the swirl component * By formula V * =a * / f * Sure; Among them, a * is the equivalent dimensionless centrifugal force of the cyclone component, f * is the equivalent dimensionless friction coefficient of the swirl component; The equivalent dimensionless centrifugal force a of the cyclone component * 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 min1 +1 / D max1 ),D max1 =k2·D max ; <h2 style=";text-align:left;direction:ltr">D<h2 style=";text-align:left;direction:ltr"> min1 <h2 style=";text-align:left;direction:ltr"> =k2·D<h2 style=";text-align:left;direction:ltr"> min <h2 style=";text-align:left;direction:ltr"> =k2·(D<h2 style=";text-align:left;direction:ltr"> max <h2 style=";text-align:left;direction:ltr"> -2·H·tan(α / 2)); The equivalent dimensionless friction coefficient f * Determined by the following formula: Re=ρud i / m; Among them, k1 and k2 are correction coefficients, u l is the velocity of the liquid medium, D eq is the equivalent spiral diameter of the spiral channel, H is the axial height of the spiral channel, L is the length of the spiral channel, 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 equivalent inner diameter of the spiral channel, D max is the maximum diameter of the separation cylinder or the maximum diameter of the blade, D min is the minimum diameter of the separation tube or the minimum diameter of the blade, D max1 is the maximum spiral diameter of the spiral channel, D min1 is the minimum spiral diameter of the spiral channel, 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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