A vapor chamber

Abstract

The utility model discloses a kind of vapor chamber, the vapor chamber includes shell, inside is formed with the closed accommodating cavity, accommodating cavity is filled with working medium;Sorbent, including the main core along the height direction of shell and the sub-core bifurcated and extended to at least one side by main core, sorbent is set in accommodating cavity and is attached to shell inner wall;Wherein the height direction of shell is perpendicular to the plane direction of working medium, to solve how to improve the technical problem of heat transport capacity of vapor chamber in vertical direction.

Description

Technical Field

[0001] This utility model relates to the field of heat spreader technology, and in particular to a heat spreader. Background Technology

[0002] A vapor chamber is a common and highly efficient heat diffusion device, widely used in power battery packs, power devices, and high heat flux density equipment to achieve rapid heat conduction and uniform diffusion. Existing vapor chambers typically include a sealed cavity, capillary structure, and working medium, through which an internal phase change heat cycle is formed by the evaporation, condensation, and reflux processes of the working medium.

[0003] In practical applications, to meet the spatial layout requirements of specific structures or equipment, heat exchangers are often arranged vertically to cover a larger area of ​​the surface to be heated. However, when arranged vertically, the condensed liquid working fluid needs to rely on capillary structures to achieve anti-gravity recirculation. This process involves significant air resistance and gravitational resistance, especially when the heat exchanger is tall, resulting in a significant decrease in recirculation efficiency, obstructed thermal circulation, and a decline in heat exchange performance.

[0004] Therefore, the design of traditional vapor chambers is limited in terms of structural height, making it difficult to accommodate heat transfer surfaces exceeding their vertical heat transfer capacity. Against this backdrop, how to effectively overcome the height bottleneck of the vertical heat transfer capacity of vapor chambers has become a pressing technical problem to be solved in this field. Utility Model Content

[0005] One objective of this invention is to provide a heat spreader that addresses the technical problem of how to improve the heat transfer capability of a heat spreader in the vertical direction.

[0006] To achieve the above objectives, the present invention provides a solution as follows: a heat spreader, the heat spreader including a shell, an internally formed sealed receiving cavity, the receiving cavity being filled with a working medium; a liquid suction core including a main core extending along the height direction of the shell and a sub-core extending from the main core to at least one side, the liquid suction core being disposed in the receiving cavity and in contact with the inner wall of the shell; and the height direction of the shell being perpendicular to the plane of the working medium.

[0007] Along the height of the shell, the width of the main core gradually decreases, and the width of the sub-core gradually decreases.

[0008] Optionally, the maximum width of the main core is L1, and the minimum width of the sub-core is L2, satisfying the relationship: 2L2≤L1≤5L2; or the maximum width of the main core is L1, and the minimum width of the main core is L2, satisfying the relationship: 2L2≤L1≤5L2.

[0009] Optionally, the angle of inclination between the tangent at any point in the core and the working medium plane is θ, satisfying the relationship: 60°≤θ≤90°.

[0010] Optionally, the angle of inclination between the line connecting the two ends of the main core and the working medium plane is α, satisfying the relationship: 70°≤θ≤90°.

[0011] Optionally, the sub-core is located on one side of the main core, and the tilt direction of the main core is opposite to the direction in which the sub-core is located. The tilt direction is the offset direction of the line connecting the two ends of the main core relative to the height direction of the shell.

[0012] Optionally, the connection point between the sub-core and the main core is located within the range of 1 / 3 to 2 / 3 of the total length of the main core.

[0013] Optionally, the bifurcation angle β between the sub-core and the main core satisfies the relationship: 30°≤β≤60°.

[0014] Optionally, multiple suction cores are repeatedly arranged along the horizontal direction of the housing, with the multiple suction cores distributed in parallel at intervals.

[0015] Optionally, the heat spreader also includes a support column located within the receiving cavity, the support column being positioned between the inner surface of the liquid absorption core and its opposite inner surface.

[0016] Optionally, there are multiple support columns, which are spaced apart along the direction parallel to the extension of the absorbent core.

[0017] Optionally, the support column includes a first support column and a second support column, the cross-sectional area of ​​the first support column is larger than the cross-sectional area of ​​the second support column, the first support column is disposed on the inner wall of the shell near the bottom, and the second support column is disposed on the inner wall of the shell near the top.

[0018] The beneficial effects of this utility model are as follows: Compared to existing technologies, the single wick structure results in low vertical reflux efficiency. This application addresses this by designing a wick structure whose width gradually decreases along the height, effectively reducing the flow resistance of the condensed liquid during counter-gravity reflux and improving the climbing efficiency of the working medium. Simultaneously, the sub-wicks extending laterally from the main wick also employ a tapering structure, forming a bottom-up, layer-by-layer "tree-like structure" with the main wick, creating a multi-channel, branching capillary reflux network in the vertical direction. This not only significantly expands the reflux coverage area but also enables parallel wicking and reflux along multiple paths, effectively alleviating local capillary saturation and blockage, and improving the continuity and response efficiency of the capillary circulation system. Attached Figure Description

[0019] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on the structures shown in these drawings without creative effort.

[0020] Figure 1 This is a schematic diagram of the structure of a heat spreader provided in an embodiment of this utility model; Figure 2 This is a schematic diagram of the liquid-absorbing core provided in an embodiment of the present invention; Figure 3 This is a side sectional view of the heat spreader provided in an embodiment of this utility model.

[0021] Explanation of icon numbers: 10. Shell; 11. Receiving cavity; 20. Liquid suction core; 21. Main core; 22. Sub-core; 30. Support column; 31. First support column; 32. Second support column. Detailed Implementation

[0022] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0023] It should be noted that all directional indicators (such as up, down, left, right, front, back, etc.) in this utility model embodiment are only used to explain the relative positional relationship and movement of each component in a specific posture. If the specific posture changes, the directional indicator will also change accordingly.

[0024] It should also be noted that when a component is referred to as being "fixed to" or "set on" another component, it can be directly on the other component or may be connected to an intermediary component. When a component is referred to as being "connected to" another component, it can be directly connected to the other component or indirectly connected to the other component through an intermediary component.

[0025] Please see Figure 1 , Figure 1 This is a schematic diagram of the structure of a heat spreader provided in an embodiment of the utility model. Figure 1 The Z direction shown is the height direction of the housing 10.

[0026] This utility model provides a heat spreader designed to improve vertical heat transfer capacity, and is particularly suitable for applications requiring a large installation height and a long vertical heat exchange surface.

[0027] The heat spreader includes a housing 10 and a liquid absorption core 20 disposed inside the housing 10. The housing 10 may be made of metal material. A sealed receiving cavity 11 is formed inside the housing 10. The receiving cavity 11 is filled with an appropriate amount of working medium, such as deionized water, ethanol or other liquid working fluid with phase change characteristics.

[0028] The wick 20 is disposed within the receiving cavity 11, extending along the height direction of the housing 10 and fitting snugly against the inner wall of the housing 10, thereby forming a good thermal coupling relationship during heat conduction. The wick 20 includes a main wick 21 and a sub-wick 22. The main wick 21 extends along the height direction of the housing 10 and serves as the main channel for the return path of the working medium. The sub-wick 22 branches off from the main wick 21 and is positioned at a certain angle on at least one side of the main wick 21 to further expand the capillary structure coverage and improve capillary return capability. The height direction of the housing 10 refers to the direction perpendicular to the plane of the working medium.

[0029] Specifically, in this application, the width of the main core 21 gradually decreases in the height direction; that is, the cross-sectional width of the main core 21 varies from the lower part to the upper part of the shell 10. Similarly, the width of the sub-core 22 also gradually decreases with increasing height, thus creating a gradient layout in the height direction where the entire liquid-absorbing core 20 structure is wider at the bottom and narrower at the top. This variable-width design not only helps optimize capillary force distribution but also reduces the flow resistance of the liquid during the ascent process and improves the anti-gravity reflux efficiency of the working medium in the vertical direction.

[0030] In this embodiment, by setting the liquid suction core 20 so that its width gradually decreases in the height direction, the flow resistance of the condensate during the vertical rise is effectively reduced, so that the working medium has a higher climbing efficiency in the return path.

[0031] Meanwhile, the sub-cores 22, which branch out laterally from the main core 21, also adopt a tapered structure, forming a "tree-like structure" with the main core 21, distributed layer by layer from bottom to top. This creates a branched network of capillary reflux channels in the height direction of the liquid wick 20, which not only expands the coverage of the liquid reflux path but also structurally guides the condensate to rise in parallel along multiple paths, effectively reducing the risk of saturation in local capillary channels and thus improving the overall reflux efficiency.

[0032] Further, please refer to Figure 2 , Figure 2This is a schematic diagram of the structure of the absorbent core 20 provided in an embodiment of the present invention. In some embodiments, in order to further optimize the capillary reflux capability and structural stability of the absorbent core 20 in the height direction, the absorbent core 20 is provided with a specific gradient ratio range in its width dimension. Specifically, the maximum width of the absorbent core 20 is denoted as L1, which generally appears in the bottom region of the absorbent core 20, that is, the lower region of the main core 21; the minimum width of the absorbent core 20 is denoted as L2, which may appear at the upper end of the main core 21 or at the upper end of the sub-core 22. According to the actual structural arrangement, when the minimum width appears in the main core 21, this value is the minimum width L2 of the main core 21; when the minimum width appears in the sub-core 22, this value is the minimum width L2 of the sub-core 22.

[0033] To ensure that the suction core 20 has sufficient capillary drive capability in the vertical direction, and does not suffer from insufficient mechanical support or blockage of the liquid channel due to excessively thin structure, the following relationship must be satisfied between L1 and L2: 2L2 ≤ L1 ≤ 5L2.

[0034] If L1 is much greater than 5L2, the height of the wick 20 will change too drastically, which is not conducive to the continuous transmission of capillary force and may cause the refluxed liquid to stagnate at the abrupt change in gradient or reduce the counterflow efficiency. Conversely, if the difference between L1 and L2 is too small, i.e., L1 is close to 2L2 or even lower, the wick 20 will tend to be of uniform width, making it difficult to form sufficient capillary gradient driving force in the height direction, and thus failing to fully utilize the advantages of the gradient wick structure in improving the ability of liquid to flow back against gravity.

[0035] Therefore, by controlling the width gradient range of the wick 20 within the aforementioned range, the vertical reflux efficiency of the condensate can be effectively improved while ensuring the continuity of capillary drive, thereby enhancing the working stability and heat dissipation capacity of the heat spreader in scenarios with high vertical orientation.

[0036] In some optimized embodiments, the main core 21 can be either straight or curved, but the angle of inclination of the tangent at any point on the main core relative to the working medium plane is within a certain range. Specifically, the angle between the tangent at any point on the main core 21 and the working medium plane is θ, and this angle satisfies the following relationship: 60°≤θ≤90° This angle setting is a structural optimization based on the relative relationship between the working medium's return path in the cavity and the direction of gravity. When θ is close to 90°, the main core 21 is arranged almost vertically. This maximizes the effective height of the capillary return path, which is conducive to establishing a continuous and strong capillary suction gradient from bottom to top, thereby improving the climbing efficiency of the condensate over a large vertical distance. This is suitable for applications with extremely high vertical height requirements.

[0037] When θ is slightly less than 90°, for example, when the main core 21 is arranged between 60° and 85°, the main core 21 is set at a certain tilt angle, which can effectively alleviate problems such as liquid accumulation and unilateral flow deviation that may be caused by a completely vertical arrangement. At the same time, the tilted arrangement also makes the branch layout between the main core 21 and the sub-core 22 more spatially coordinated, which is conducive to forming a multi-layer capillary reflux network structure and further improving the thermal cycling stability of the entire plate.

[0038] If θ is less than 60°, the main core 21 tends to be arranged nearly horizontally. Since the return flow of condensed liquid from the cold end to the evaporation end mainly depends on the capillary force generated by the capillary structure, the vertical component of the capillary force decreases rapidly as θ decreases. The capillary force cannot provide sufficient vertical driving force, and the liquid has difficulty completing the necessary upward return flow, thereby reducing the heat dissipation performance of the heat spreader in the vertical direction.

[0039] Therefore, controlling θ between 60° and 90° can balance the efficiency of capillary suction drive and maintain the rationality of the liquid return channel distribution.

[0040] In addition, for the implementation of the main core 21 using a curved (such as arc, broken line or wavy line) layout, in order to ensure the capillary reflux height while taking into account the space utilization brought by the curved layout, this embodiment limits the overall "macro tilt angle" of the curved main core 21.

[0041] Specifically, a reference line is drawn connecting the starting and ending points of the main core 21 of the curve. The angle between this line and the free surface of the working medium is defined as α. Then, α satisfies: 70°≤θ≤90°. If α is less than 70°, the overall line of the main core 21 is significantly tilted, and the equivalent vertical height is significantly reduced. Under the interaction of gravity and capillary force, the capillary head is insufficient to overcome the static pressure difference caused by the gravity of the liquid column. The condensate is difficult to reliably transport back to the evaporation zone from bottom to top, which in turn causes the thermal conductivity of the heat spreader to decrease sharply in vertical installation or large-angle application scenarios.

[0042] By controlling α within the range of 70° to 90°, a balance can be achieved between the flexible arrangement space provided by the curved core 21 shape and the capillary recirculation driving capability, maximizing the heat dissipation performance of the heat sink under high power density and long path recirculation conditions.

[0043] Furthermore, in some embodiments, the sub-core 22 is located on one side of the main core 21, and the tilting direction of the main core 21 is opposite to the direction in which the sub-core 22 is located. Specifically, the main core 21 is tilted at a certain angle relative to the height direction of the housing 10, with the tilting direction facing one side of the housing 10, while the sub-core 22 is distributed on the opposite side of the tilting direction of the main core 21, that is, on the side of the main core 21 away from the tilting direction.

[0044] This structure allows the main core 21 and the sub-core 22 to form a "reverse unfolding" arrangement inside the cavity. The sub-core 22 unfolds towards the opposite side of the main core 21, effectively filling the gap area left by the inclined side of the main core 21, realizing "misaligned filling" of the internal space of the cavity, increasing the layout density of the liquid-absorbing core 20 in the unit cavity cross section, thereby expanding the coverage of the capillary structure without increasing the overall size of the shell 10.

[0045] Furthermore, the reverse arrangement between the sub-core 22 and the main core 21 helps to create a more uniform liquid reflux network. The condensate can flow back to the evaporation zone through the main core 21, while forming an auxiliary loop along the sub-core 22, avoiding uneven liquid distribution caused by unilateral offset arrangement, and improving the stability and efficiency of the thermal cycle.

[0046] In some embodiments, the branching point of the sub-core 22 from the main core 21 is limited to between 1 / 3 and 2 / 3 of the total length of the main core 21. Specifically, the main core 21 extends from bottom to top in the height direction of the housing 10, and its total length is denoted as L3. The branching point of the sub-core 22 is located in the middle region between L3 / 3 and L3×2 / 3 of the length from the bottom of the main core 21. This distribution ensures that the sub-core 22 does not branch at the extreme upper or lower ends of the main core 21, but rather concentrates in the middle for lateral expansion.

[0047] Structurally, the lower section of the main core 21 remains continuous, which is conducive to the overall strength support and the stable formation of the main liquid return path; the sub-core 22 extends in the middle to form branches, which can be arranged symmetrically on one or both sides, forming a certain angle with the axis of the main core 21, and adhering to the inner wall of the shell 10, so that the entire liquid absorption core 20 has a tree-like structure of "main trunk-middle branch" in the vertical space.

[0048] In this embodiment, the mid-section bifurcation structure design allows for the formation of a more rational and efficient capillary reflux network within the housing 10. On one hand, the bifurcation of the sub-core 22 is located in the 1 / 3 to 2 / 3 section of the main core 21, which helps guide the condensate back to its original flow at different heights, alleviating the capillary force attenuation problem that exists along a long vertical distance on a single main core 21 path, and improving the efficiency of liquid returning from the high-level region to the evaporation zone.

[0049] On the other hand, the selection of this bifurcation location also achieves a longitudinal gradient in the distribution of capillary structures, effectively expanding the capillary action coverage of the liquid wick 20, reducing the risk of liquid accumulation or backflow bottlenecks in local areas, and thus enhancing the circulation stability and heat transfer uniformity of the heat exchange plate under vertical heat exchange conditions. In addition, the central location of the bifurcation area can both ensure the structural support strength of the bottom of the main core 21 and facilitate the coordinated arrangement of the sub-cores 22 in the distribution space.

[0050] In some optimized embodiments, in order to achieve a more reasonable branch connection relationship between the sub-core 22 and the main core 21 and to construct an efficient capillary reflux network structure, the bifurcation angle β between the sub-core 22 and the main core 21 is limited to between 30° and 60°.

[0051] The sub-core 22 branches off from the central region of the main core 21, forming an angle β with the axis of the main core 21. β is the angle between the central axes of the sub-core 22 and the main core 21. Structurally, this angle causes the sub-core 22 to be arranged obliquely towards the housing 10 while maintaining a certain degree of inclination, allowing it to fit snugly along the inner wall of the housing 10, forming a capillary reflux channel that is connected to the main core 21 but distributed in a different direction. This angle setting avoids the sub-core 22 being arranged at a right angle to the main core 21, allowing the working medium to obtain continuous and stable capillary suction in the sub-core 22, thus smoothly flowing back to the bottom evaporation area of ​​the main core 21.

[0052] When the bifurcation angle is less than 30°, the sub-core 22 and the main core 21 tend to be arranged in parallel. Although the structure is compact, the return path of the condensate in the sub-core 22 is significantly lengthened, the return resistance increases, and the return efficiency decreases significantly. In addition, the small-angle arrangement results in a high degree of overlap between the distribution areas of the sub-core 22 and the main core 21, leading to excessively high local capillary density and insufficient capillary network coverage in other areas. This can easily form liquid stagnation or "dead zones," affecting the stability and uniformity of the overall thermal cycle.

[0053] When the bifurcation angle β is greater than 60°, the sub-core 22 extends excessively laterally towards the shell 10, tending to be arranged horizontally. Although this is beneficial for expanding the lateral coverage of the capillary structure, the angle between its capillary driving direction and the direction of gravity is too large, resulting in a decrease in the projection of the capillary force in the vertical direction. This makes it difficult for the condensate to flow back downward to the evaporation zone, and it is easy for it to accumulate in the middle or end region of the sub-core 22. At the same time, the excessively large angle will also cause the structural slope of the sub-core 22 to change abruptly when it branches off from the main core 21, which poses risks such as discontinuity of the capillary liquid transport path and interruption of the liquid bridge, thus compromising the stability of the thermal cycle.

[0054] Furthermore, in some embodiments, multiple absorbent cores 20 are repeatedly arranged along the horizontal direction of the housing 10, that is, multiple absorbent core 20 units are evenly distributed in the width direction of the housing 10. The multiple absorbent cores 20 are arranged parallel to each other, with their axes aligned, and are spaced apart within the horizontal cross-section of the housing 10, with a certain distance reserved between adjacent absorbent cores 20 to prevent interference. Each absorbent core 20 is an independent unit, attached to the inner wall of the housing 10 or supported and positioned by an internal structure, forming a composite capillary structure system distributed in a linear array or grid pattern within the cross-section.

[0055] In this embodiment, the parallel spacing of multiple wicking cores 20 ensures that condensate, regardless of its lateral location within the housing 10, can quickly enter the nearest wicking core 20 unit for capillary recirculation, reducing localized stagnation. Simultaneously, the main core 21-sub-core 22 network forms a main capillary recirculation pathway vertically and multi-point contact coverage laterally, enhancing the system's adaptability to non-uniform heat source distribution. Furthermore, the spacing and number of the multiple wicking cores 20 can be adjusted to match different housing 10 width specifications.

[0056] Additionally, in some embodiments, considering the stability of the heat spreader structure under internal pressure, and to prevent cavity deformation caused by gas pressure changes or thermal cycling, the heat spreader also includes a support column 30 structure disposed inside the receiving cavity 11. The support column 30 is disposed between the two inner walls of the housing 10, that is, between the inner surface to which the liquid-absorbing core 20 is attached and its opposite inner surface.

[0057] The support column 30 can be columnar, conical, or ribbed, with its two ends contacting or fixedly connected to the upper and lower inner walls to provide mechanical support for the internal space of the cavity. The support column 30 can be made of metal, ceramic, or other high-strength materials compatible with the working medium, and can also be fixed to the inner surface of the housing 10 by means of laser welding, spot welding, riveting, or structural pressing.

[0058] In this embodiment, the support column 30 effectively enhances the compressive strength and structural stability of the cavity 11 during internal operation. In practical applications, the vapor chamber is in a vacuum or low-pressure state, and there are instantaneous pressure fluctuations caused by phase change processes. Without a support structure, the upper and lower walls of the shell 10 are prone to deformation or even contact collapse under thermal expansion and contraction or localized heating conditions, resulting in capillary damage or disordered working fluid distribution. In addition, the introduction of the support column 30 not only maintains the stability of the cavity shape of the shell 10, but also helps to fix the liquid suction core 20, preventing it from shifting, warping, or detaching from the contact surface under the impact of the working medium flow.

[0059] Furthermore, in some optimized embodiments, there are multiple support columns 30, arranged at intervals parallel to the extension direction of the absorbent core 20. The absorbent core 20 typically extends along the height or inclined direction of the heat spreader. To adapt to its shape, the multiple support columns 30 are also arranged in rows on an axis parallel to the extension direction of the absorbent core 20, maintaining a preset distance between them to form a regular array. Each support column 30 can be positioned between absorbent core 20 units or directly below / above adjacent absorbent cores 20, and traverses or is located in the space area of ​​the receiving cavity 11 not completely occupied by the absorbent core 20. The number, spacing, and diameter of the support columns 30 can be adapted and adjusted according to the width of the housing 10, the number of absorbent cores 20, and the required pressure-bearing capacity, thereby balancing structural support requirements with the integrity of the internal capillary structure arrangement.

[0060] In this embodiment, by arranging multiple support columns 30 at intervals parallel to the absorbent core 20, the pressure load from the inner walls on both sides of the housing 10 can be more evenly distributed, preventing local depressions or warping. This also achieves continuous coverage of the overall support force, improving the internal pressure resistance stability of the cavity. Under thermal cycling or negative pressure conditions, the multiple spaced support columns 30 act as structural reinforcement "ribs," effectively preventing problems such as poor contact and capillary breaks caused by the sinking or detachment of the absorbent core 20, thus maintaining the integrity of the fit between the absorbent core 20 and the inner wall.

[0061] Considering that there is a two-phase gas-liquid circulation inside the heat spreader during operation, where the gas usually accumulates in the upper space and the liquid is mostly concentrated in the lower region, it is easy to cause uneven pressure distribution in the upper and lower cavities, resulting in problems such as gas accumulation and increased gas resistance.

[0062] In some optimized embodiments, please refer to Figure 1 and Figure 3 , Figure 1 This is a schematic diagram of the structure of a heat spreader provided in an embodiment of this utility model. Figure 3 This is a side cross-sectional view of the heat spreader provided in this embodiment of the utility model. To balance the gas flow resistance inside the heat spreader, the support columns 30 include two types: a first support column 31 and a second support column 32, with significant structural differences between the two types. The first support column 31 has a larger cross-sectional area than the second support column 32, used to enhance the mechanical support stability of the lower structure; while the second support column 32 has a relatively smaller cross-sectional area to reduce its impact on the gas flow path. Specifically, the first support column 31 is located on the inner wall of the shell 10 near the bottom region, i.e., the region where condensate mainly gathers and flows back; the second support column 32 is located on the inner wall of the shell 10 near the top region, i.e., the region where the gas phase is concentrated.

[0063] In this embodiment, the differentiated support column 30 structure can effectively alleviate the problem of decreased thermal cycling efficiency caused by air resistance. On the one hand, the liquid density in the lower region is high, which requires high structural support. By setting the first support column 31 with a larger cross-sectional area, it can not only provide stronger pressure resistance and stabilize the vertical structure of the liquid suction core 20, but also facilitate the uniform flow and collection of condensate on the larger support surface, preventing structural depression or detachment of the liquid suction core 20 that would damage the capillary circulation channel.

[0064] On the other hand, the upper region has a high gas content, and the gas diffusion path needs to be kept unobstructed. If the support column 30 is too large, it will easily cause flow blockage. By using a second support column 32 with a smaller cross-sectional area, more space for gas to flow can be provided without significantly increasing the mechanical load, reducing the gas resistance effect caused by structural obstruction, and maintaining smooth gas phase circulation between the evaporation and condensation regions.

[0065] Furthermore, the use of terms such as "first" and "second" in this utility model is for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. Additionally, the technical solutions of the various embodiments can be combined with each other, but only on the basis of being achievable by those skilled in the art. When the combination of technical solutions is contradictory or impossible to implement, such a combination of technical solutions should be considered non-existent and not within the scope of protection claimed by this utility model.

[0066] The above description is only a preferred embodiment of the present utility model and does not limit the patent scope of the present utility model. All equivalent structural transformations made under the inventive concept of the present utility model using the contents of the present utility model specification and drawings, or direct / indirect applications in other related technical fields, are included within the patent protection scope of the present utility model.

Claims

1. A vapor chamber, characterized by, include: The shell has a sealed cavity inside, which is filled with a working medium. The liquid-absorbing core includes a main core extending along the height direction of the housing and a sub-core extending from the main core to at least one side, the liquid-absorbing core being disposed in the receiving cavity and fitting against the inner wall of the housing; The height direction of the housing is perpendicular to the plane of the working medium.

2. The vapor chamber of claim 1, wherein In the height direction of the housing, the width of the main core gradually decreases, and the width of the sub-core gradually decreases.

3. The vapor chamber of claim 2, wherein The maximum width of the main core is L1, and the minimum width of the sub-core is L2, satisfying the relationship: 2L2≤L1≤5L2; Alternatively, the maximum width of the main core is L1, and the minimum width of the main core is L2, satisfying the relationship: 2L2≤L1≤5L2.

4. The vapor chamber of claim 1, wherein The angle of inclination between the tangent at any point in the main core and the working medium plane is θ, satisfying the relationship: 60°≤θ≤90°.

5. The vapor chamber of claim 4, wherein The angle of inclination between the line connecting the two ends of the main core and the working medium plane is α, satisfying the relationship: 70°≤θ≤90°.

6. The vapor chamber of claim 5, wherein The sub-core is located on one side of the main core, and the tilt direction of the main core is opposite to the direction in which the sub-core is located. The tilt direction is the offset direction of the line connecting the two ends of the main core relative to the height direction of the housing.

7. The vapor chamber of claim 1, wherein The connection point between the sub-core and the main core is located within the range of 1 / 3 to 2 / 3 of the total length of the main core.

8. The vapor chamber of claim 1, wherein The bifurcation angle β between the sub-core and the main core satisfies the following relationship: 30°≤β≤60°.

9. The vapor chamber of claim 1, wherein Multiple liquid-absorbing cores are repeatedly arranged along the horizontal direction of the shell, and the multiple liquid-absorbing cores are distributed in parallel and spaced apart.

10. The vapor chamber of claim 1, wherein The heat spreader also includes a support column located within the receiving cavity, the support column being positioned between the inner surface of the liquid absorption core and its opposite inner surface.

11. The vapor chamber of claim 10, wherein The number of support columns is multiple, and the multiple support columns are spaced apart along the extension direction parallel to the liquid absorption core.

12. The vapor chamber of claim 11, wherein, The support column includes a first support column and a second support column. The cross-sectional area of ​​the first support column is larger than that of the second support column. The first support column is located on the inner wall of the shell near the bottom, and the second support column is located on the inner wall of the shell near the top.

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