CN221036913U - Microchannel heat exchanger, heat pump water heater and air conditioner - Google Patents
Microchannel heat exchanger, heat pump water heater and air conditioner Download PDFInfo
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- CN221036913U CN221036913U CN202322729453.5U CN202322729453U CN221036913U CN 221036913 U CN221036913 U CN 221036913U CN 202322729453 U CN202322729453 U CN 202322729453U CN 221036913 U CN221036913 U CN 221036913U
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Abstract
The present disclosure relates to a microchannel heat exchanger, a heat pump water heater and an air conditioner. The microchannel heat exchanger includes: a first liquid collecting pipe (10), a second liquid collecting pipe (20) and a plurality of flat pipes, wherein one end of each flat pipe is connected with the first liquid collecting pipe (10), the other end of each flat pipe is connected with the second liquid collecting pipe (20), and the flat pipe is provided with a plurality of micropores communicated with the first liquid collecting pipe (10) and the second liquid collecting pipe (20); wherein, a plurality of flat pipes include: the device comprises at least one super-heated area flat tube (31) for flowing the gas working medium in a super-heated state and at least one super-cooled area flat tube (33) for flowing the liquid working medium in a super-cooled state, wherein the total micropore cross-sectional area of the super-heated area flat tube (31) is larger than that of the super-cooled area flat tube (33).
Description
Technical Field
The disclosure relates to the technical field of heat exchange, in particular to a micro-channel heat exchanger, a heat pump water heater and an air conditioner.
Background
A microchannel heat exchanger is a heat exchange device that transfers heat through a microchannel of the micron order, having a smaller size and higher surface area to volume ratio, suitable for heat exchange requirements for high heat flux and compact space. The micro-channel heat exchanger is widely applied to a plurality of fields such as automobile air conditioner, electronic device heat dissipation, aerospace, energy fields and the like due to the advantages of high heat exchange efficiency, small volume, light weight, high reliability and the like.
For a general parallel flow micro-channel heat exchanger, the specification and the size of flat tubes and the internal structure of the flat tubes in different heat exchange areas of a micro-channel heat exchanger monomer are consistent under given design conditions.
Disclosure of utility model
The inventor finds that the flat tube with consistent specification and size and internal structure in the related technology is not easy to consider the heat exchange performance and pressure drop of the micro-channel heat exchanger, thereby influencing the improvement of the whole operation performance.
In view of the above, the embodiments of the present disclosure provide a micro-channel heat exchanger, a heat pump water heater and an air conditioner, which can give consideration to heat exchange performance and pressure drop of the micro-channel heat exchanger, and improve overall operation performance.
In one aspect of the present disclosure, there is provided a microchannel heat exchanger comprising: the device comprises a first liquid collecting pipe, a second liquid collecting pipe and a plurality of flat pipes, wherein one end of each flat pipe is connected with the first liquid collecting pipe, the other end of each flat pipe is connected with the second liquid collecting pipe, and the flat pipes are provided with a plurality of micropores communicated with the first liquid collecting pipe and the second liquid collecting pipe; wherein, a plurality of flat pipes include: the device comprises at least one super-heated area flat pipe for flowing a gas working medium in a super-heated state and at least one super-cooled area flat pipe for flowing a liquid working medium in a super-cooled state, wherein the total micropore cross-sectional area of the super-heated area flat pipe is larger than that of the super-cooled area flat pipe.
In some embodiments, the number of micropores in the superheater zone flat tube is greater than the number of micropores in the supercooler zone flat tube, and/or the cross-sectional area of each micropore in the superheater zone flat tube is greater than the cross-sectional area of each micropore in the supercooler zone flat tube.
In some embodiments, an internal tooth structure is disposed in at least part of the micropores of the flat tube of the supercooling region.
In some embodiments, the plurality of flat tubes are arranged at intervals along a first direction, and the internal tooth structure comprises at least one protrusion extending along a length direction of the micropores of the microporous cold zone flat tube, the protrusion protruding on at least one of two inner walls of the micropores of the supercooling zone flat tube opposite in the first direction.
In some embodiments, the internal tooth structure includes two of the protrusions protruding on two inner walls of the micro-holes of the flat tube of the supercooling region, respectively, opposite in the first direction.
In some embodiments, two of the protrusions are opposite in the first direction.
In some embodiments, the number of micropores in the flat tube of the superheating area is 24-28, and the number of micropores in the flat tube of the supercooling area is 19-23.
In some embodiments, the cross-sectional area of each micropore in the superheater zone flat tube is 0.403-0.542 mm 2, and the cross-sectional area of each micropore in the supercooler zone flat tube is 0.235-0.343 mm 2.
In some embodiments, in a second direction perpendicular to the microporous section, the outer profile cross-sectional area of the superheater zone flat tube and the outer profile cross-sectional area of the supercooling zone flat tube are both 32.38-33.53 mm 2.
In some embodiments, the ratio of the total cross-sectional area of the micropores of the flat tube in the superheating area to the total cross-sectional area of the micropores of the flat tube in the supercooling area is 1.3 to 3.4.
In some embodiments, the total cross-sectional area of the micropores of the flat tube in the superheating area is 10.32-15.176 mm 2, and the total cross-sectional area of the micropores of the flat tube in the supercooling area is 4.465-7.889 mm 2.
In some embodiments, the plurality of flat tubes further comprises at least one flat tube in a gas-liquid two-phase region for circulating a gas-liquid two-phase working medium, and the total cross-sectional area of the micropores of the flat tube in the gas-liquid two-phase region is larger than the total cross-sectional area of the micropores of the flat tube in the supercooling region.
In some embodiments, the number of micropores in the gas-liquid two-phase zone flat tube is greater than the number of micropores in the subcooling zone flat tube, and/or the cross-sectional area of each micropore in the gas-liquid two-phase zone is greater than the cross-sectional area of each micropore in the subcooling zone flat tube.
In some embodiments, the number of micropores in the gas-liquid two-phase area flat tube is 24-28.
In some embodiments, the cross-sectional area of each micropore in the gas-liquid two-phase zone flat tube is 0.403-0.542 mm 2.
In some embodiments, in a second direction perpendicular to the cross section of the micro-hole, the outer profile cross section of the flat tube in the gas-liquid two-phase region is 32.38-33.53 mm 2.
In some embodiments, the ratio of the total cross-sectional area of the micropores of the flat tube in the gas-liquid two-phase region to the total cross-sectional area of the micropores of the flat tube in the supercooling region is 1.3 to 3.4.
In some embodiments, the total cross-sectional area of the micropores of the flat tube in the gas-liquid two-phase region is 10.32-15.176 mm 2.
In some embodiments, the plurality of flat tubes are arranged at intervals along a first direction, in the first direction, the at least one gas-liquid two-phase region flat tube is located between the at least one super-cooling region flat tube and the at least one super-cooling region flat tube, and the number of the super-cooling region flat tubes in the microchannel heat exchanger is greater than the number of the super-cooling region flat tubes and greater than the number of the gas-liquid two-phase region flat tubes.
In one aspect of the present disclosure, a heat pump water heater is provided comprising the foregoing microchannel heat exchanger.
In one aspect of the present disclosure, an air conditioner is provided that includes the foregoing microchannel heat exchanger.
Therefore, according to the embodiment of the disclosure, the plurality of flat tubes connected with the first liquid collecting tube and the second liquid collecting tube include the super-heated flat tube for flowing the gas working medium in the super-heated state and the super-cooled flat tube for flowing the liquid working medium in the super-cooled state according to the flowing working medium forms, and the total micropore cross-sectional area of the super-heated flat tube is larger than that of the super-cooled flat tube, so that the flow velocity of the working medium is reduced by setting the larger total micropore cross-sectional area of the super-heated flat tube, the pressure drop is reduced, the flow velocity of the working medium is improved by setting the smaller total micropore cross-sectional area of the super-cooled flat tube, the heat exchange effect is enhanced, the heat exchange performance and the pressure drop of the micro-channel heat exchanger are considered, and the overall operation performance is improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description, serve to explain the principles of the disclosure.
The disclosure may be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings in which:
FIG. 1 is a schematic diagram of a micro-channel heat exchanger according to some embodiments of the present disclosure;
FIG. 2 is a schematic cross-sectional view of a superheater section flat tube in a microchannel heat exchanger according to some embodiments of the present disclosure;
FIG. 3 is a schematic cross-sectional view of a subcooling zone flat tube in a microchannel heat exchanger in accordance with some embodiments of the present disclosure;
Fig. 4 is a schematic cross-sectional view of a gas-liquid two-phase zone flat tube in a microchannel heat exchanger according to some embodiments of the disclosure.
It should be understood that the dimensions of the various elements shown in the figures are not drawn to actual scale. Further, the same or similar reference numerals denote the same or similar members.
Detailed Description
Various exemplary embodiments of the present disclosure will now be described in detail with reference to the accompanying drawings. The description of the exemplary embodiments is merely illustrative, and is in no way intended to limit the disclosure, its application, or uses. The present disclosure may be embodied in many different forms and is not limited to the embodiments described herein. These embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that: the relative arrangement of parts and steps, the composition of materials, numerical expressions and numerical values set forth in these embodiments should be construed as exemplary only and not limiting unless otherwise specifically stated.
The terms "first," "second," and the like, as used in this disclosure, do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. The word "comprising" or "comprises" and the like means that elements preceding the word encompass the elements recited after the word, and not exclude the possibility of also encompassing other elements. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, which may also be changed when the absolute position of the object to be described is changed.
In this disclosure, when a particular device is described as being located between a first device and a second device, there may or may not be an intervening device between the particular device and either the first device or the second device. When it is described that a particular device is connected to other devices, the particular device may be directly connected to the other devices without intervening devices, or may be directly connected to the other devices without intervening devices.
All terms (including technical or scientific terms) used in this disclosure have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs, unless specifically defined otherwise. It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense unless expressly so defined herein.
Techniques, methods, and apparatus known to one of ordinary skill in the relevant art may not be discussed in detail, but are intended to be part of the specification where appropriate.
In some related art, the flat tubes in different heat exchange areas of the parallel flow microchannel heat exchanger have uniformity in specification and size and internal structure. The inventor finds that the flat tube with consistent specification and size and internal structure in the related technology is not easy to consider the heat exchange performance and pressure drop of the micro-channel heat exchanger, thereby influencing the improvement of the whole operation performance.
In view of the above, the embodiments of the present disclosure provide a micro-channel heat exchanger, a heat pump water heater and an air conditioner, which can give consideration to heat exchange performance and pressure drop of the micro-channel heat exchanger, and improve overall operation performance.
Fig. 1 is a schematic structural view of a microchannel heat exchanger according to some embodiments of the present disclosure. Fig. 2 is a schematic cross-sectional view of a superheater section flat tube in a microchannel heat exchanger according to some embodiments of the present disclosure. Fig. 3 is a schematic cross-sectional view of a subcooling zone flat tube in a microchannel heat exchanger in accordance with some embodiments of the present disclosure.
Referring to fig. 1-3, embodiments of the present disclosure provide a microchannel heat exchanger. The microchannel heat exchanger comprises a first header 10, a second header 20 and a plurality of flat tubes. One end of each flat tube is connected to the first liquid collecting tube 10, and the other end is connected to the second liquid collecting tube 20, and has a plurality of micropores communicating the first liquid collecting tube 10 and the second liquid collecting tube 20.
The plurality of flat tubes includes: the device comprises at least one super-heated area flat tube 31 for flowing the gas working medium in a super-heated state and at least one super-cooled area flat tube 33 for flowing the liquid working medium in a super-cooled state, wherein the total micropore sectional area S1 of the super-heated area flat tube 31 is larger than the total micropore sectional area S3 of the super-cooled area flat tube 33.
The flat tube in the superheating area is a flat-shaped tube for treating gaseous working medium in a superheated state (exceeding saturated steam temperature) in the microchannel heat exchanger. In this region, the temperature of the working fluid increases, causing it to exceed the saturated vapor temperature, and to transition to the saturated vapor state. The flat tube in the supercooling region is a flat-shaped tube for processing liquid working medium in supercooling (exceeding the saturation temperature of liquid) state in the micro-channel heat exchanger. In this region, the temperature of the working medium is reduced so that it approaches the saturation temperature of the liquid.
In the present embodiment, the micropore total sectional area S1 of the superheat-zone flat pipe 31 refers to the sum of areas of formation regions of all the micropores 311 included in the superheat-zone flat pipe 31 on a section perpendicular to the extending direction of the micropores, that is, the sum of sectional areas of all the micropores 311. For the superheater area flat tubes 31 employing the same cross-sectional area of the micropores 311, the total cross-sectional area S1 of the micropores is the product of the number of micropores and the cross-sectional area of each micropore. For the superheater area flat tubes 31 using micropores of different cross-sectional areas, the total cross-sectional area S1 of the micropores is the sum of the cross-sectional areas of the respective micropores.
Similarly, the total micropore cross-sectional area S3 of the supercooling region flat pipe 33 refers to the sum of areas where all the micropores 311 included in the supercooling region flat pipe 33 are formed on a section perpendicular to the extending direction of the micropores, that is, the sum of cross-sectional areas of all the micropores 311. For the supercooling region flat tube 33 employing the same cross-sectional area of the microwells 311, the microwell total cross-sectional area S3 is the product of the number of microwells and the cross-sectional area of each microwell. For the supercooling region flat tube 33 employing micropores of different cross-sectional areas, the micropore total cross-sectional area S3 is the sum of the cross-sectional areas of the respective micropores.
Considering that the gaseous working medium flowing in the flat tube of the superheating area has phase change latent heat, can form more sufficient heat exchange area with the inner wall of the micropore and has higher flow velocity, the heat exchange coefficient is higher, the corresponding pressure drop is larger, the energy consumption is increased, the energy utilization efficiency is reduced, and the higher pressure drop has adverse effect on the operation stability. The flow velocity of the working medium is reduced by using a larger total micropore sectional area of the flat tube 31 in the overheating zone, so that the pressure drop is reduced, the energy consumption is reduced, the energy utilization efficiency is improved, and the operation stability of the heat exchanger is improved.
Considering that the heat exchange coefficient of the liquid working medium flowing in the flat pipe of the supercooling region is smaller than that of the gaseous working medium, the heat exchange efficiency is lower, and the heat exchange needs to be enhanced. Therefore, the flow velocity of the working medium is improved by using the small total micropore sectional area of the supercooling region flat pipe 33, and the heat exchange effect is enhanced. Therefore, the heat exchange performance and the pressure drop of the micro-channel heat exchanger can be considered, and the overall operation performance is improved.
In some embodiments, the ratio of the total cross-sectional area of the micropores of the flat tube 31 in the superheating area to the total cross-sectional area of the micropores of the flat tube 33 in the supercooling area is 1.3 to 3.4.
In this embodiment, if the total cross-sectional area of the micropores of the flat tube 31 in the superheating area is too high compared with the total cross-sectional area of the micropores of the flat tube 33 in the supercooling area, the flow rate of the working medium in the superheating area is reduced too much, which affects the heat exchange effect, while the pressure drop in the supercooling area is increased, which affects the stability of the heat exchanger; otherwise, if the total cross-sectional area of the micropores of the flat tube 31 in the superheating area is too low compared with the total cross-sectional area of the micropores of the flat tube 33 in the supercooling area, the pressure drop in the superheating area is higher, the operation stability of the heat exchanger is affected, the flow rate of the working medium in the supercooling area is reduced, and the heat exchange effect in the supercooling area is affected. Therefore, the ratio of the total micropore sectional area of the flat tube 31 in the superheating area to the total micropore sectional area of the flat tube 33 in the supercooling area is 1.3-3.4, so that the heat exchange effect and the operation stability of the heat exchanger are both considered.
In some embodiments, the total micropore sectional area of the superheater section flat tube 31 is 10.32-15.176 mm 2, and the total micropore sectional area of the supercooling section flat tube 33 is 4.465-7.889 mm 2.
For the flat tube 31 in the superheat region, if the total sectional area of the micropores is too large, the flow velocity of the working medium in the superheat region is reduced too much, the heat exchange effect is affected, and if the total sectional area of the micropores is too small, the working medium in the superheat region has higher flow velocity, the pressure drop is higher, and the operation stability of the heat exchanger is affected, so that the total sectional area of the micropores of the flat tube 31 in the superheat region is 10.32-15.176 mm 2, and the heat exchange effect and the operation stability of the heat exchanger are both considered.
For the flat tube 33 in the supercooling region, if the total cross-sectional area of the micropores is too large, the heat exchange effect is greatly reduced if the flow rate of the liquid working medium with a lower heat exchange coefficient in the supercooling region is lower, and if the total cross-sectional area of the micropores is too small, the flow rate of the working medium in the supercooling region is too fast, the pressure drop in the supercooling region is higher, the operation stability of the heat exchanger is affected, so that the total cross-sectional area of the micropores of the flat tube 33 in the supercooling region is 4.465-7.889 mm 2, and the heat exchange effect and the operation stability of the heat exchanger are both considered.
Referring to fig. 2 and 3, in some embodiments, the number of micro-holes N1 in the hot zone flat tube 31 is greater than the number of micro-holes N3 in the cold zone flat tube 33. The flat tube 31 in the superheating area adopts a large number of micropores, can improve the total sectional area of the micropores, reduce the flow velocity of working medium so as to reduce pressure drop, and increases the heat transfer surface area by increasing the contact area between gaseous working medium and the micropores, and more micropores can lead the heat distribution to be more uniform, thereby being beneficial to balancing heat exchange and reducing the risk of local overheating. The flat tube 33 in the supercooling region adopts a smaller number of micropores, which can reduce the total sectional area of the micropores, improve the flow velocity of working medium, improve the heat transfer efficiency, and is beneficial to reducing the complexity and cost of manufacturing and processing, and is beneficial to enabling the micropores to obtain larger spacing, thereby reducing the interference effect between adjacent micropores.
In some embodiments, the number N1 of micropores in the flat tube 31 in the superheating area is 24 to 28, for example 24, 25, 26, 27, 28, and the number N3 of micropores in the flat tube 33 in the superheating area is 19 to 23, for example 19, 20, 21, 22, 23. By making the number of micropores N1 in the flat tube 31 in the superheat region 24-28 and making the number of micropores N3 in the flat tube 33 in the supercooling region 19-23, the total cross-sectional area of the micropores in the flat tube 31 in the superheat region can be increased, the flow rate of the gaseous working medium in the flat tube 31 in the superheat region can be reduced, the pressure drop of the flat tube 31 in the superheat region can be reduced, the heat transfer surface area of the flat tube 31 in the superheat region can be increased, the risk of local overheating can be reduced, the complexity and cost of manufacturing and processing of the flat tube 33 in the supercooling region can be reduced, the micropores of the flat tube 33 in the supercooling region can be more widely spaced, and the interference between adjacent micropores in the flat tube 33 in the supercooling region can be reduced.
In some embodiments, the cross-sectional area of each micro-hole 311 in the hot zone flat tube 31 is greater than the cross-sectional area of each micro-hole 331 in the cold zone flat tube 33. The flat tube 31 in the superheating area adopts a larger micropore sectional area, so that the total micropore sectional area can be increased, the flow velocity of the working medium is reduced, the pressure drop is reduced, the flow resistance of the working medium when passing through the micropores is reduced through the larger micropore sectional area, and the pressure drop is also reduced. The flat tube 33 in the supercooling region adopts a smaller micropore sectional area, so that the flow velocity of working medium can be improved, and the heat transfer efficiency can be improved.
In some embodiments, the cross-sectional area of each micro-hole 311 in the super-heat zone flat tube 31 is 0.403-0.542 mm 2, such as 0.403mm 2、0.45mm2、0.5mm2、0.542mm2, and the cross-sectional area of each micro-hole 331 in the super-cooling zone flat tube 33 is 0.235-0.343 mm 2, such as 0.235mm 2、0.27mm2、0.3mm2、0.34mm2. By making the cross-sectional area of each micropore in the flat tube 31 in the superheat region be 0.403-0.542 mm 2 and making the cross-sectional area of each micropore in the flat tube 33 in the supercooling region be 0.235-0.343 mm 2, the total cross-sectional area of micropores in the flat tube 31 in the superheat region can be increased, the flow resistance of working medium passing through the micropores can be reduced, the flow velocity of gaseous working medium in the flat tube 31 in the superheat region can be reduced, the pressure drop of the flat tube 31 in the superheat region can be reduced, the flow velocity of working medium in the flat tube 33 in the supercooling region can be increased, and the heat transfer efficiency can be improved.
In the above embodiment, in the second direction x (which may be the length direction or the extending direction of the micropores) perpendicular to the section of the micropores, the outer profile section area of the flat tube 31 in the superheating area and the outer profile section area of the flat tube 33 in the supercooling area may be the same or substantially the same, for example, 32.38-33.53 mm 2, which is advantageous for making the overall structure size of the microchannel heat exchanger more uniform.
In some embodiments, the number of micropores N1 in the superheater section flat tube 31 is greater than the number of micropores N3 in the superheater section flat tube 33, and the cross-sectional area S of each micropore 311 in the superheater section flat tube 31 is greater than the cross-sectional area of each micropore 331 in the superheater section flat tube 33. The flat tube 31 in the superheating area adopts a larger number of micropores and a larger micropore sectional area, so that the total micropore sectional area can be increased, and the flow velocity of the working medium can be reduced to reduce the pressure drop. In addition, the contact area of the gaseous working medium and the micropores can be increased by more micropore quantity and larger micropore sectional area, the heat transfer surface area is increased, more micropores can enable heat distribution to be more uniform, balanced heat exchange is facilitated, the risk of local overheating is reduced, and the larger micropore sectional area reduces the flow resistance of the working medium when the working medium passes through the micropores and also is beneficial to reducing pressure drop.
Referring to fig. 3, in some embodiments, an internal tooth structure 332 is disposed within at least a portion of the micro-holes 331 of the subcooling region flat tube 33. The internal tooth structure 332 of the flat tube 33 in the supercooling region can increase the surface area of the micro-holes of the flat tube for heat transfer with the liquid working medium, and can increase the disturbance effect on the flow of the liquid working medium, so as to promote the turbulent flow effect of the liquid working medium and improve the flow velocity of the working medium.
In fig. 1 and 3, the plurality of flat tubes may be arranged at intervals along the first direction z. The first direction z may be perpendicular to the second direction x, and the micropores in each flat tube may be arranged at intervals along a third direction y perpendicular to the first direction z and the second direction x. The internal tooth structure 332 includes at least one protrusion extending in a length direction (i.e., the second direction x) of the micro-holes of the micro-hole cold zone flat pipe, the protrusion protruding on at least one of two inner walls of the micro-holes 331 of the supercooling zone flat pipe 33 opposite in the first direction z.
The protrusion means a structure protruding inward with respect to the inner walls of the micro-holes, the protrusion extending in the longitudinal direction of the micro-holes of the micro-hole cold zone flat pipe, and the protrusion being located at one or both of the two inner walls of the micro-holes 331 opposing each other in the first direction z. As can be seen in fig. 3, since the protrusions are provided on the inner walls of the micro holes corresponding to the flat outer surfaces (i.e., the wide side surfaces) of the flat tubes 33 of the supercooling region, the heat exchange efficiency of the wide side surfaces of the flat tubes is enhanced.
In fig. 3, the internal tooth structure 332 may include two protrusions respectively disposed on two inner walls of the micro-holes 331 of the supercooling region flat tube 33 opposite to each other in the first direction z. Thus, the protrusions are provided on both inner walls of the micro-holes 331 opposite to each other in the first direction z, which is advantageous in increasing heat exchange efficiency of the opposite wide side surfaces of the flat tube 33 in the supercooling region.
Referring to fig. 3, in some embodiments, two of the protrusions are opposite in the first direction z. By arranging two opposite protrusions on two opposite inner walls of the micro-hole 331 in the first direction z, the flow of the liquid working medium in the cross section area can be more uniform, and the energy consumption is reduced. Further, it is also possible that the protrusion is located at a middle position of the micro hole 331 in the third direction y.
Fig. 4 is a schematic cross-sectional view of a gas-liquid two-phase zone flat tube in a microchannel heat exchanger according to some embodiments of the disclosure. Referring to fig. 1 and 4, in some embodiments, the plurality of flat tubes further includes at least one gas-liquid two-phase region flat tube 32 for circulating a gas-liquid two-phase working medium, and a total micropore sectional area S2 of the gas-liquid two-phase region flat tube 32 is greater than a total micropore sectional area S3 of the supercooling region flat tube 33.
The flat tube in the gas-liquid two-phase region is a flat-shaped pipeline for treating working medium in a gas-liquid two-phase mixed state in the micro-channel heat exchanger. In this region, the working fluid contains both gas and liquid phases, and is typically used to perform gas-liquid phase change heat transfer, such as vaporization or condensation processes.
Considering that the gas-liquid two-phase region has effusion on the inner wall of the micropore, the actual through-flow size of the micropore becomes smaller, and the gas-liquid two-phase is disturbed mutually during flowing, so that energy loss is caused, the fluctuation of the liquid part in the micropore also causes energy loss, so that the pressure drop of the flat tube in the region is larger, the total micropore cross-section area S2 of the flat tube 32 in the gas-liquid two-phase region is larger than the total micropore cross-section area S3 of the flat tube 33 in the supercooling region, and the larger total micropore cross-section area S2 of the flat tube 32 in the gas-liquid two-phase region reduces the flow velocity of the working medium, so that the pressure drop is reduced, the energy consumption is reduced, the energy utilization efficiency is improved, and the running stability of the heat exchanger is improved.
In the present embodiment, the micropore total sectional area S2 of the gas-liquid two-phase region flat tube 32 refers to the sum of areas of formation regions of all the micropores 321 included in the gas-liquid two-phase region flat tube 32 on a section perpendicular to the extending direction of the micropores, that is, the sum of sectional areas of all the micropores 321. For the gas-liquid two-phase region flat tube 32 employing the same cross-sectional area of the micropores 321, the total cross-sectional area S2 of the micropores is the product of the number of micropores and the cross-sectional area of each micropore. For a gas-liquid two-phase zone flat tube 32 employing micropores of different cross-sectional areas, the total cross-sectional area of the micropores is the sum of the cross-sectional areas of the individual micropores.
In some embodiments, the ratio of the total cross-sectional area of the micropores of the gas-liquid two-phase area flat tube 32 to the total cross-sectional area of the micropores of the supercooling area flat tube 33 is 1.3 to 3.4.
In this embodiment, if the total cross-sectional area of the micropores of the flat tube 32 in the gas-liquid two-phase region is too high compared with the total cross-sectional area of the micropores of the flat tube 33 in the supercooling region, the flow velocity of the working medium in the gas-liquid two-phase region is reduced too much, which affects the heat exchange effect, while the pressure drop in the supercooling region is increased, which affects the stability of the heat exchanger; otherwise, if the total cross-sectional area of the micropores of the flat tube 32 in the gas-liquid two-phase region is too low compared with the total cross-sectional area of the micropores of the flat tube 33 in the supercooling region, the flow speed of the working medium in the gas-liquid two-phase region is too high, so that the mutual disturbance of the gas-liquid two-phase during flow is aggravated, the pressure drop in the gas-liquid two-phase region is higher, the operation stability of the heat exchanger is affected, the flow speed of the working medium in the supercooling region is reduced, and the heat exchange effect of the supercooling region is affected. Therefore, the ratio of the total micropore sectional area of the gas-liquid two-phase area flat pipe 32 to the total micropore sectional area of the supercooling area flat pipe 33 is 1.3-3.4, so that the heat exchange effect and the operation stability of the heat exchanger are both considered.
In some embodiments, the total cross-sectional area of the micropores of the flat tube 32 in the gas-liquid two-phase region is 10.32-15.176 mm 2.
For the flat tube 32 in the gas-liquid two-phase region, if the total cross-sectional area of the micropores is too large, the flow velocity of the liquid working medium with a low heat exchange coefficient in the gas-liquid two-phase region is low, the heat exchange effect is greatly reduced, and if the total cross-sectional area of the micropores is too small, the flow velocity of the working medium in the gas-liquid two-phase region is too high, the mutual disturbance of the gas-liquid two phases in the flowing process is aggravated, the pressure drop in the gas-liquid two-phase region is high, and the operation stability of the heat exchanger is affected, so that the total cross-sectional area of the micropores of the flat tube 32 in the gas-liquid two-phase region is 10.32-15.176 mm 2, and the heat exchange effect and the operation stability of the heat exchanger are both considered.
Referring to fig. 1, in some embodiments, the plurality of flat tubes are arranged at intervals along a first direction z, and in the first direction z, the at least one gas-liquid two-phase zone flat tube 32 is located between the at least one super-heating zone flat tube 31 and the at least one super-cooling zone flat tube 33. The number of the flat tubes 33 in the supercooling zone is greater than the number of the flat tubes 31 in the superheating zone and greater than the number of the flat tubes 32 in the gas-liquid two-phase zone in the microchannel heat exchanger. The heat exchange capacity of the flat tube 33 in the supercooling region is lower than that of the flat tube 31 in the superheating region and the heat tube 32 in the gas-liquid two-phase region, so that the heat exchange capacity of the microchannel heat exchanger is improved by arranging more flat tubes 33 in the supercooling region.
For example, the microchannel heat exchanger may be divided into three flows, wherein the first flow corresponds to the superheat zone and the gas-liquid two-phase zone of the microchannel heat exchanger, and thus comprises two superheat zone flat tubes 31 and three gas-liquid two-phase zone heat tubes 32, the second flow and the third flow each correspond to the supercooling zone of the microchannel heat exchanger, wherein the second flow comprises three supercooling zone flat tubes 33, and the third flow comprises two supercooling zone flat tubes 33, and thus the microchannel heat exchanger comprises five supercooling zone flat tubes 33.
Referring to fig. 3 and 4, in some embodiments, the number of micropores N2 in the gas-liquid two-phase zone flat tube 32 is greater than the number of micropores N3 in the supercooling zone flat tube 33. The flat tube 32 in the gas-liquid two-phase area adopts more micropores, can improve the total sectional area of the micropores, reduces the flow velocity of the working medium to reduce the pressure drop, and increases the heat transfer surface area by increasing the contact area between the gas-liquid two-phase working medium and the micropores, and more micropores can lead the heat distribution to be more uniform, thereby being beneficial to balancing heat exchange and reducing the risk of local overheating.
In some embodiments, the number of micropores N2 in the gas-liquid two-phase zone flat tube 32 is 24 to 28, such as 24, 25, 26, 27, 28, and the number of micropores N3 in the supercooling zone flat tube 33 is less than N2, and may be 19 to 23, such as 19, 20, 21, 22, 23. By making the number N2 of the micropores in the flat tube 32 in the gas-liquid two-phase region be 24-28, the total cross-sectional area S2 of the micropores in the flat tube 32 in the gas-liquid two-phase region can be increased, the flow rate of the gas-liquid two-phase working medium in the flat tube 32 in the gas-liquid two-phase region can be reduced, the pressure drop of the flat tube 32 in the gas-liquid two-phase region can be reduced, the heat transfer surface area of the flat tube 32 in the gas-liquid two-phase region can be increased, and the risk of local overheating can be reduced.
In some embodiments, the cross-sectional area of each micro-hole 321 in the gas-liquid two-phase zone flat tube 32 is larger than the cross-sectional area of each micro-hole 331 in the supercooling zone flat tube 33. The flat tube 32 in the gas-liquid two-phase region adopts a larger micropore sectional area, so that the total micropore sectional area can be increased, the flow velocity of the working medium is reduced, the pressure drop is reduced, the reduction of the through flow dimension of the micropores by accumulated liquid on the inner walls of the micropores can be offset to a certain extent, the flow resistance of the working medium when passing through the micropores is reduced, and the mutual disturbance of the gas-liquid two-phase working medium is reduced.
In some embodiments, the cross-sectional area of each micro-hole in the gas-liquid two-phase zone flat tube 32 is 0.403 to 0.542mm 2, such as 0.403mm 2、0.45mm2、0.5mm2、0.542mm2, and the cross-sectional area of each micro-hole 331 in the supercooling zone flat tube 33 is smaller than the micro-hole cross-sectional area of the gas-liquid two-phase zone flat tube 32, such as 0.235 to 0.343mm 2, such as 0.235mm 2、0.27mm2、0.3mm2、0.34mm2. By making the cross-sectional area of each micropore in the gas-liquid two-phase area flat tube 32 be 0.403-0.542 mm 2, the total cross-sectional area of micropores of the gas-liquid two-phase area flat tube 32 can be increased, the flow resistance when working medium passes through the micropores can be reduced, the flow velocity of the gas-liquid two-phase working medium of the gas-liquid two-phase area flat tube 32 can be reduced, and the pressure drop of the gas-liquid two-phase area flat tube 32 can be reduced.
In the above embodiment, in the second direction x (which may be the length direction or the extending direction of the micropores) perpendicular to the section of the micropores, the outer profile cross-sectional area of the gas-liquid two-phase area flat tube 32 may be the same or substantially the same as the outer profile cross-sectional areas of the super-heated area flat tube 31 and the super-cooled area flat tube 33, for example, 32.38-33.53 mm 2, which is beneficial to making the overall structure size of the microchannel heat exchanger more uniform.
In some embodiments, the number of micropores N2 in the gas-liquid two-phase zone flat tube 32 is greater than the number of micropores N3 in the supercooling zone flat tube 33, and the cross-sectional area of each micropore 321 in the gas-liquid two-phase zone flat tube 32 is greater than the cross-sectional area of each micropore 331 in the supercooling zone flat tube 33.
The flat tube 32 in the gas-liquid two-phase area adopts more micropore quantity and larger micropore sectional area, can improve micropore total sectional area, reduce working medium velocity of flow to reduce pressure drop, and through increasing the area of contact of gas-liquid two-phase working medium and micropore, increase heat transfer surface area, more micropores can make heat distribution more even in addition, be favorable to balanced heat transfer, reduce local overheated risk, and the reduction of micropore through-flow size can be offset to a certain extent to micropore inner wall hydrops to great micropore sectional area, flow resistance when the working medium passes through the micropore is reduced, mutual disturbance of gas-liquid two-phase working medium is reduced.
Referring to the previous embodiment, a plurality of flat tubes with different micropore total sectional areas are selected to carry out a cross collocation scheme of a flat tube in a superheat zone, a flat tube in a gas-liquid two-phase zone and a flat tube in a supercooling zone, and a complete machine test is carried out. The following table shows the test results corresponding to the 19 cross-collocation schemes.
The total cross sections of the micropores of the flat tube in the overheating zone, the flat tube in the gas-liquid two-phase zone and the flat tube in the overheating zone in the table above are the heat exchange amount, the system power consumption and the system refrigeration coefficient (Coefficient Of Performance, COP for short) realized under different values. Neglecting test errors caused by test precision, it can be seen from the table that in the schemes of 1, 2, 8, 9, 12, 13, 15, 16 and 17 cross collocations, the system COP can reach a better result of more than 3.1, and according to the values of the total cross sections of the micropores of the flat tube in the superheat region, the flat tube in the gas-liquid two-phase region and the flat tube in the superheat region, which correspond to the schemes, the value of the total cross section of the micropores of the flat tube in the superheat region is 10.32-15.176 mm 2, and when the value of the total cross section of the micropores of the flat tube in the superheat region is 4.465-7.889 mm 2, the better system COP can be realized, so that the overall running performance is improved.
The microchannel heat exchanger of the above embodiments may be applicable to various devices or service scenarios where heat exchange is required, such as a heat pump water heater or an air conditioner.
Accordingly, in one aspect of the present disclosure, there is provided a heat pump water heater comprising a microchannel heat exchanger of any of the preceding embodiments.
In another aspect of the disclosure, there is also provided an air conditioner comprising a microchannel heat exchanger of any of the preceding embodiments.
Thus, various embodiments of the present disclosure have been described in detail. In order to avoid obscuring the concepts of the present disclosure, some details known in the art are not described. How to implement the solutions disclosed herein will be fully apparent to those skilled in the art from the above description.
Although some specific embodiments of the present disclosure have been described in detail by way of example, it should be understood by those skilled in the art that the above examples are for illustration only and are not intended to limit the scope of the present disclosure. It will be understood by those skilled in the art that the foregoing embodiments may be modified and equivalents substituted for elements thereof without departing from the scope and spirit of the disclosure. The scope of the present disclosure is defined by the appended claims.
Claims (21)
1. A microchannel heat exchanger comprising: a first liquid collecting pipe (10), a second liquid collecting pipe (20) and a plurality of flat pipes, wherein one end of each flat pipe is connected with the first liquid collecting pipe (10), the other end of each flat pipe is connected with the second liquid collecting pipe (20), and the flat pipe is provided with a plurality of micropores communicated with the first liquid collecting pipe (10) and the second liquid collecting pipe (20);
Wherein, a plurality of flat pipes include: the device comprises at least one super-heated area flat tube (31) for flowing the gas working medium in a super-heated state and at least one super-cooled area flat tube (33) for flowing the liquid working medium in a super-cooled state, wherein the total micropore cross-sectional area of the super-heated area flat tube (31) is larger than that of the super-cooled area flat tube (33).
2. The microchannel heat exchanger according to claim 1, characterized in that the number of micro-holes in the hot zone flat tube (31) is greater than the number of micro-holes in the cold zone flat tube (33) and/or the cross-sectional area of each micro-hole in the hot zone flat tube (31) is greater than the cross-sectional area of each micro-hole in the cold zone flat tube (33).
3. The microchannel heat exchanger according to claim 2, wherein the supercooling zone flat tube (33) is provided with an internal tooth structure (332) at least partially within the micropores.
4. A microchannel heat exchanger according to claim 3, wherein the plurality of flat tubes are arranged at intervals along a first direction (z), the internal tooth structure (332) comprising at least one protrusion extending along the length of the micropores of the microporous cold zone flat tube, the protrusion protruding on at least one of two inner walls of the micropores of the supercooling zone flat tube (33) opposite in the first direction (z).
5. The microchannel heat exchanger according to claim 4, wherein the internal tooth structure (332) comprises two of the projections protruding on two inner walls of the micro-holes of the flat tube (33) of the supercooling region opposite in the first direction (z), respectively.
6. The microchannel heat exchanger according to claim 5, wherein two of the protrusions are opposite in the first direction (z).
7. The microchannel heat exchanger according to claim 2, wherein the number of micropores in the superheater zone flat tube (31) is 24 to 28, and the number of micropores in the supercooler zone flat tube (33) is 19 to 23.
8. The microchannel heat exchanger according to claim 2, wherein the cross-sectional area of each micropore in the superheater zone flat tube (31) is 0.403-0.542 mm 2, and the cross-sectional area of each micropore in the supercooling zone flat tube (33) is 0.235-0.343 mm 2.
9. The microchannel heat exchanger according to claim 2, wherein the outer contour cross-sectional area of the superheater zone flat tube (31) and the outer contour cross-sectional area of the supercooling zone flat tube (33) are 32.38-33.53 mm 2 in a second direction (x) perpendicular to the microporous cross-section.
10. The microchannel heat exchanger according to claim 1, wherein the ratio of the total cross-sectional area of the micropores of the flat tube (31) in the superheating region to the total cross-sectional area of the micropores of the flat tube (33) in the supercooling region is 1.3 to 3.4.
11. The microchannel heat exchanger according to claim 1, wherein the total micropore cross-sectional area of the flat tube (31) in the superheating area is 10.32-15.176 mm 2, and the total micropore cross-sectional area of the flat tube (33) in the supercooling area is 4.465-7.889 mm 2.
12. The microchannel heat exchanger according to any one of claims 1 to 11, wherein the plurality of flat tubes further comprises at least one gas-liquid two-phase zone flat tube (32) for circulating a gas-liquid two-phase working medium, the total cross-sectional area of micropores of the gas-liquid two-phase zone flat tube (32) being larger than the total cross-sectional area of micropores of the supercooling zone flat tube (33).
13. The microchannel heat exchanger according to claim 12, wherein the number of micropores in the gas-liquid two-phase zone flat tube (32) is greater than the number of micropores in the supercooling zone flat tube (33), and/or the cross-sectional area of each micropore in the gas-liquid two-phase zone is greater than the cross-sectional area of each micropore in the supercooling zone flat tube (33).
14. The microchannel heat exchanger according to claim 13, wherein the number of micropores in the gas-liquid two-phase zone flat tube (32) is 24-28.
15. The microchannel heat exchanger according to claim 13, wherein the cross-sectional area of each micropore in the gas-liquid two-phase zone flat tube (32) is 0.403-0.542 mm 2.
16. The microchannel heat exchanger according to claim 13, wherein the outer profile cross-sectional area of the gas-liquid two-phase zone flat tube (32) in the second direction (x) perpendicular to the microporous cross-section is 32.38-33.53 mm 2.
17. The microchannel heat exchanger according to claim 12, wherein a ratio of a total cross-sectional area of micropores of the gas-liquid two-phase zone flat tube (32) to a total cross-sectional area of micropores of the supercooling zone flat tube (33) is 1.3 to 3.4.
18. The microchannel heat exchanger according to claim 17, wherein the total cross-sectional area of micropores of the gas-liquid two-phase zone flat tube (32) is 10.32-15.176 mm 2.
19. The microchannel heat exchanger according to claim 12, wherein the plurality of flat tubes are arranged at intervals along a first direction (z), in the first direction (z), the at least one gas-liquid two-phase region flat tube (32) is located between the at least one super-heated region flat tube (31) and the at least one super-cooled region flat tube (33), and the number of the super-cooled region flat tubes (33) in the microchannel heat exchanger is greater than the number of the super-heated region flat tubes (31) and greater than the number of the gas-liquid two-phase region flat tubes (32).
20. A heat pump water heater, comprising:
the microchannel heat exchanger of any one of claims 1 to 19.
21. An air conditioner, comprising:
the microchannel heat exchanger of any one of claims 1 to 19.
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