CN117073430A - Plate heat exchanger with multi-baffle straight plates - Google Patents
Plate heat exchanger with multi-baffle straight plates Download PDFInfo
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- CN117073430A CN117073430A CN202211462120.4A CN202211462120A CN117073430A CN 117073430 A CN117073430 A CN 117073430A CN 202211462120 A CN202211462120 A CN 202211462120A CN 117073430 A CN117073430 A CN 117073430A
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- 239000012530 fluid Substances 0.000 claims abstract description 155
- 239000011148 porous material Substances 0.000 claims description 68
- 238000009826 distribution Methods 0.000 claims description 36
- 238000005516 engineering process Methods 0.000 claims description 12
- 238000010146 3D printing Methods 0.000 claims description 11
- 230000000149 penetrating effect Effects 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 abstract description 26
- 230000001965 increasing effect Effects 0.000 description 18
- 230000000694 effects Effects 0.000 description 16
- 230000008859 change Effects 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 230000008569 process Effects 0.000 description 12
- 238000012546 transfer Methods 0.000 description 11
- 238000013461 design Methods 0.000 description 10
- 238000001816 cooling Methods 0.000 description 9
- 230000017525 heat dissipation Effects 0.000 description 9
- 238000012545 processing Methods 0.000 description 9
- 239000000110 cooling liquid Substances 0.000 description 8
- 238000002474 experimental method Methods 0.000 description 8
- 238000004088 simulation Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 5
- 239000011159 matrix material Substances 0.000 description 5
- 238000005057 refrigeration Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000007639 printing Methods 0.000 description 4
- 238000009792 diffusion process Methods 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000004378 air conditioning Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000004590 computer program Methods 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 230000002028 premature Effects 0.000 description 2
- 238000009827 uniform distribution Methods 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- 229910003407 AlSi10Mg Inorganic materials 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000005219 brazing Methods 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
- F28D15/04—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/24—Arrangements for promoting turbulent flow of heat-exchange media, e.g. by plates
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Fluid Mechanics (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The application provides a plate heat exchanger provided with a plurality of baffle straight plates, which is sequentially provided with a first layer, a second layer, a third layer and a fourth layer from top to bottom, wherein the first layer comprises a cold fluid inlet and a cold fluid outlet which are arranged on the front surface, the fourth layer is a hot fluid pipeline in thermal contact with the third layer, a cavity is arranged in the fourth layer, a heat supply fluid passes through the cavity, the bottom of the cavity of the fourth layer is provided with baffle straight plates and fins, the baffle straight plates comprise a center baffle straight plate positioned at the center of a bottom plate, a second baffle straight plate surrounding the center baffle straight plate, a third baffle straight plate surrounding the second baffle straight plate and an outer baffle straight plate surrounding the third baffle straight plate, and the fins are positioned between the baffle straight plates. The application aims to provide a plate heat exchanger, wherein a flow guide structure is arranged inside the plate heat exchanger, and particularly, a rectangular prismatic baffle straight plate with a multilayer vertical structure is arranged, so that the liquid flow range is wide, the cold liquid flow dead zone is effectively reduced, and the temperature uniformity of a heat flow surface is further improved.
Description
Technical Field
The application relates to a heat exchanger technology, in particular to a plate heat exchanger.
Background
A heat exchanger is a device that exchanges heat with a hot and cold fluid, also known as a heat exchanger. Heat exchangers are widely used in many fields. Because the working scene is special in the fields such as electronics, petrifaction, communication, aerospace and the like, the heat exchanger has special requirements on the size and the weight, and the heat exchange capability is required to be stronger. In 1981, a learner proposed to utilize a micro-channel to dissipate heat, so that the volume of the heat exchanger can be reduced, and the heat exchange capacity of the heat exchanger can be greatly improved by utilizing the higher specific surface area of the micro-channel. However, although the heat exchange capacity is strong, the overall pressure loss is also high due to the small hydraulic diameter of the microchannels.
The flat plate type heat exchanger is the heat exchanger with highest heat exchange efficiency in various heat exchangers at present, and has the advantages of small occupied space and convenient installation and disassembly. The heat exchanger consists of stamping formed concave-convex stainless steel plates, and concave-convex lines between two adjacent plates are combined relatively at 180 degrees, so that staggered contact points are formed by concave-convex ridge lines between the two plates of the plate heat exchanger, and after the contact points are combined in a vacuum welding mode, a high-pressure-resistant staggered circulation structure of the plate heat exchanger is formed, and the staggered circulation structures enable cold and hot liquid in the plate heat exchanger to generate strong turbulence so as to achieve a high heat exchange effect.
Flat tubes have been widely used in automotive air conditioning units and residential or commercial air conditioning heat exchangers in recent years. The interior of such flat tubes is provided with a plurality of small passages through which, in use, the heat exchange liquid flows. Because the heat exchange area of the flat tube is large, the heat exchange effect can be greatly improved.
The flat plate type heat exchanger is widely applied to industries such as chemical industry, petroleum, refrigeration, nuclear energy, power and the like, and the demand for the heat exchanger in industrial production is increased and the quality requirement for the heat exchanger is also increased due to the worldwide energy crisis so as to reduce energy consumption. In recent decades, although compact heat exchangers (plate-type, plate-fin-type, pressure-welded plate-type heat exchangers, etc.), heat pipe-type heat exchangers, direct contact heat exchangers, etc. have been rapidly developed, shell-and-tube heat exchangers still occupy the dominant position of yield and usage due to high reliability and wide adaptability, and the usage of the shell-and-tube heat exchangers in the current industrial devices still accounts for about 70% of the usage of all heat exchangers according to relevant statistics.
After the flat plate type heat exchanger is scaled, the heat exchanger is cleaned by adopting the conventional modes of steam sweeping, back flushing and the like, and the production practice proves that the effect is not very good. The heat exchanger seal heads can be detached only by adopting a physical cleaning mode, but the heat exchanger seal heads are cleaned by adopting the mode, so that the operation is complex, the time consumption is long, the investment of manpower and material resources is large, and great difficulty is brought to continuous industrial production.
Among the refrigeration equipment, various refrigeration heat exchangers are indispensable key equipment and also important equipment capable of improving the performance thereof. In small refrigeration systems, there are increasing demands on the mass, volume and heat transfer properties of the heat exchanger. In the common fin-tube heat exchanger, larger gap thermal resistance exists between the fins and the pipeline, so that the heat exchange effect is weakened, and the size and the volume are larger, so that the miniaturization and the light weight of the system are not facilitated. In the divided wall type miniature heat exchanger, however, the heat exchange plates are connected together through brazing, so that the heat exchange efficiency is improved. The partition type miniature heat exchanger has the outstanding advantages of small size, higher heat transfer coefficient and the like, and is increasingly commonly applied to small refrigeration systems.
In the indirect liquid cooling scheme, a heat exchanger is used for heat exchange. The heat exchanger is a metal heat exchange device with a flow channel structure therein, and is usually made of copper or aluminum. The heat exchange liquid is directly contacted with the bottom surface of the bottom plate of the heat exchanger, the heat of heat transfer is conducted to the heat exchanger, and then the heat exchanger and the cooling liquid in the heat exchanger conduct heat convection to take away the heat. The whole liquid cooling system utilizes the pump to provide power for the circulation of working medium, and compared with an air cooling system, the liquid cooling system has a more compact structure. And the cooling liquid is mostly deionized water compatible with heat exchanger materials, glycol-deionized water with specified percentage, nano liquid and other mediums, and has higher specific heat capacity and heat conductivity coefficient than air, and the heat dissipation effect is better than that of air cooling. In addition, the noise level of the indirect liquid cooling system is significantly reduced compared to an air cooling system.
In recent years, in order to meet the heat exchange requirement, research on an indirect liquid cooling system has been developed, and the heat exchanger structure is found to have particularly significant influence on heat exchange and power consumption of the liquid cooling system in terms of heat exchanger structure, cooling liquid selection, pipeline arrangement and the like. The heat exchanger can be divided into a bottom plate, a flow passage and a cover plate. The cover plate and the hose connector have no unified standard, different manufacturers have different structural forms, and the base plate and the flow channels can be configured in various ways according to equipment and heat design power consumption, which is also a main factor affecting the heat dissipation performance of the heat exchanger.
A rib: the additional provision of fins helps to increase the heat transfer area and can enhance the disturbance to the flow field. Heat exchange enhancement by adding fins has been widely used in heat exchangers. However, the heat dissipation effect cannot be considered singly in the design, and the situation that the pressure drop is increased sharply after the fins are added and the heat dissipation improvement effect is extremely small is avoided as far as possible from the aspect of system economy. And the temperature is relatively lower when the cooling liquid is imported, so that ribs are not arranged in the central high-flow-rate area so as to improve the pressure drop of the heat exchanger, cylindrical ribs are arranged in the peripheral low-flow-rate area, disturbance is enhanced, the heat exchange area is increased, and the loss of heat dissipation capacity caused by the temperature rise of the cooling liquid is compensated.
The flow guiding structure comprises: in order to avoid a flow dead zone in the convective heat exchange process of the cooling liquid and the heat exchanger, the heat exchanger is used as a baffle straight plate widely adopted, a plurality of long straight baffle straight plates are arranged in the heat exchanger to serve as a flow guiding structure, and the flow direction of the cooling liquid is changed in certain areas of the flow field so as to improve the flow field distribution of the cooling liquid in the heat exchanger.
However, the design of the plate heat exchanger is also considered in the process, and sometimes the plate heat exchanger is limited by various limitations, such as complex flow channel structure, which leads to difficult processing; under the condition that the total heat exchange area is unchanged, the thicker the fins are, the larger the distance is, the smaller the heat exchange area is, the lower the heat dissipation capacity of the cold plate is, and in order to increase the heat exchange area, the thickness of the fins is designed to be too small and densely distributed, so that the fins are difficult to process, the flow resistance is increased, and the flow distribution of a system is not facilitated. The optimal design achieves the aim of enhancing heat exchange by changing the form of the flow channel and reducing the volume of the fins, and is extremely important how to further increase the heat exchange area and improve the temperature uniformity due to the limited heat dissipation area of the flow channel so as to enhance the heat dissipation performance of the flow channel.
Aiming at the defects, the application improves the prior heat exchanger, and provides a novel plate heat exchanger which adopts porous materials, and the porous structure is studied and optimized in detail, so that the uniform distribution of fluid can be ensured, the heat exchange efficiency is improved, and the heat exchange area is further increased and the temperature uniformity is improved. And can 3D print porous material, make its processing simple, convenient operation can realize the structure that normal is difficult to realize. The hot fluid channel is improved, so that the flow resistance is reduced and the heat exchange efficiency is improved.
Disclosure of Invention
The application aims to provide a novel structural plate heat exchanger. By adopting the porous structure, the porous structure is studied and optimized in detail, so that the uniform distribution of fluid can be ensured, the heat exchange efficiency is improved, the heat exchange area is further increased, and the temperature uniformity is improved. The hot fluid channel is improved, so that the flow resistance is reduced and the heat exchange efficiency is improved. The hot fluid channel is improved, so that the flow resistance is reduced and the heat exchange efficiency is improved.
In order to achieve the above object, the technical scheme of the present application is as follows:
the utility model provides a plate heat exchanger who sets up many baffling straight plates, sets gradually first layer, second floor, third layer and fourth layer from the top down, and first layer is including setting up cold fluid inlet and the cold fluid outlet in openly, and the fourth layer is the hot fluid pipeline with the third layer thermal contact, sets up the cavity in the fourth layer, and the heating fluid passes through, set up baffling straight plate and fin on the bottom of fourth layer cavity, baffling straight plate includes the central baffling straight plate that is located the bottom plate center, surrounds at the outside second baffling straight plate of central baffling straight plate and surrounds at the outside third baffling straight plate of second baffling straight plate and surrounds at the outside baffling straight plate of third baffling straight plate, and the fin is located between the baffling straight plate.
Preferably, the central baffle plate comprises four central baffle plate walls, each central baffle plate comprises two baffle plate walls which are at a certain angle with each other, the extension lines of the baffle plate walls of the four central baffle plate walls form a first prismatic shape, and the baffle plate walls form a part of the edges of the first prismatic shape; a first interval is arranged between baffle straight plate walls of adjacent central baffle straight plates; the second baffle straight plates comprise four baffle straight plate walls which are perpendicular to each other, the extension lines of the baffle straight plate walls of the four second baffle straight plates form a first rectangular structure, and the baffle straight plate walls form a part of the side of the first rectangle; a second interval is arranged between baffle straight plate walls of the adjacent second baffle straight plates; the third baffle straight plates comprise four baffle straight plate walls which are at a certain angle with each other, the extension lines of the baffle straight plate walls of the four third baffle straight plates form a second prismatic structure, and the baffle straight plate walls form a part of the edges of the second prismatic structure; a third interval is arranged between baffle straight plate walls of adjacent third baffle straight plates; the external baffle straight plates comprise two external baffle straight plates, each external baffle straight plate comprises a first straight plate wall and two second straight plate walls which are perpendicular to each other and are arranged at two ends of the straight plate wall, the extension lines of the baffle straight plate walls of the two external baffle straight plates form a second rectangular structure, and the first straight plate wall and the second straight plate wall form a part of the side of the second rectangle; a fourth space is provided between adjacent second baffle walls of the two outer baffle plates.
Preferably, a plurality of ribs are arranged inside the central baffle plate; a plurality of ribs are arranged between the second baffle straight plate and the central baffle straight plate, and a plurality of ribs are arranged between the second baffle straight plate and the third baffle straight plate; a plurality of ribs are arranged between the third baffle plate and the external baffle plate.
Preferably, the extension line of the connecting line of the opposite first interval midpoints and the extension line of the opposite third interval midpoints pass through the perpendicular points of the two perpendicular baffle straight walls of the second baffle straight plate and the perpendicular points of the two perpendicular baffle straight walls of the outer baffle straight plate.
Preferably, the extension line of the connecting line of the middle points of the second interval opposite to each other, the extension line of the middle points of the fourth interval opposite to each other pass through the connecting point of the two baffle straight walls of which the central baffle straight plate forms a certain angle with each other, and the connecting point of the two baffle straight walls of which the third baffle straight plate forms a certain angle with each other.
Preferably, the fourth layer includes a hot fluid inlet and a hot fluid outlet disposed on the back surface, the hot fluid inlet is disposed at a central position of the first prism, the hot fluid outlets are disposed 2, are disposed at two opposite ends of the second rectangle, are disposed outside the first straight wall, and a line of central lines of the two outlets passes through a center of the first straight wall.
Preferably, the height of the ribs and the height of the baffle plates are the same and are equal to the height of the square cavity.
Preferably, the second layer comprises an inlet header, an outlet header, an inlet branch pipe, an outlet branch pipe, an inlet flow channel and an outlet flow channel which are arranged on the front surface, wherein the upstream of the inlet header and the downstream of the outlet header are respectively connected with a cold fluid inlet and a cold fluid outlet of the first layer, the inlet header and the outlet header are respectively connected with the inlet branch pipe and the outlet branch pipe, the front surface of the second layer comprises a plurality of bent plate-shaped structures, one side of each plate-shaped structure forms an inlet branch pipe, the other side forms an outlet branch pipe, and the inlet branch pipe and the outlet branch pipe are not directly communicated; through holes penetrating through the second layer are arranged in the inlet branch pipe and the outlet branch pipe, so that an inlet flow channel and an outlet flow channel are formed; the third layer comprises a porous material positioned on the front surface, and the porous material is connected with the inlet runner and the outlet runner; the porous material adopts a 3D printing technology, so that the porous material is of a pore-changing structure, and the pore diameter of the porous material at the fluid inlet of the inlet runner is larger than that of the porous material at the fluid outlet of the outlet runner.
Preferably, the porous material has a progressively increasing pore distribution density along the direction of flow of the fluid within the inlet header.
Compared with the prior art, the application has the following advantages:
1) The application aims to provide a plate heat exchanger, wherein a flow guide structure is arranged inside the plate heat exchanger, and particularly, a rectangular prismatic baffle straight plate with a multilayer vertical structure is arranged, so that the liquid flow range is wide, the cold liquid flow dead zone is effectively reduced, and the temperature uniformity of a heat flow surface is further improved.
2) The application adopts the capillary structure for the plate heat exchanger and adopts the 3D printing technology for the capillary structure, so that the plate heat exchanger can realize the pore structure change, the pore diameter at the fluid inlet is larger than the pore diameter at the fluid outlet, the working efficiency is improved, and the pore diameter change is more accurate.
3) The application adopts the 3D printing technology for the capillary structure, so that the variable pore density is gradually distributed along the fluid flow, the processing technology is improved, and the regular change can be accurately realized through a computer. Compared with the existing preparation process, the processing result is more accurate, accurate structural amplitude change is realized through a computer program, and the processing precision is greatly improved, so that the heat exchange efficiency is improved.
4) According to the application, the aperture at the fluid inlet is larger than the aperture at the fluid outlet, and the convection heat exchange capacity of the cold fluid at different apertures is different, so that the temperature uniformity and the convection heat exchange capacity of the whole cold plate are improved.
5) According to the application, the pore density is gradually distributed along the fluid flow, so that the fluid is uniformly distributed on the whole heat exchange surface, and the temperature uniformity and the convection heat exchange capacity of the whole cold plate are improved.
Drawings
FIG. 1 is a schematic view of the overall structure of a heat exchanger according to the present application;
FIG. 2 is a schematic view of a split structure of the heat exchanger of the present application;
FIG. 3 is a second layer block diagram of the heat exchanger of the present application;
FIG. 4 is a schematic diagram of the cold fluid flow of the heat exchanger of the present application;
FIG. 5 is a schematic view of a preferred embodiment of a fourth layer fin structure;
FIG. 6 is a schematic view of another preferred embodiment of a fourth layer fin structure.
In the figure: 1. a first layer; 2. a second layer; 3. a third layer; 4. a fourth layer; 11. a cold fluid inlet; 12. a cold fluid outlet; 21. an inlet header; 22. an outlet header; 23. an inlet branch pipe; 24. an outlet branch pipe; 31. a porous material; 41. a hot fluid inlet; 42. a hot fluid outlet; 43. a central baffle plate; 44. a second baffle plate; 45. a third baffle plate; 46. an external baffle plate; 47-50, fins.
Detailed Description
The following describes the embodiments of the present application in detail with reference to the drawings. The front side in the specification refers to the side facing upwards when being mounted.
Fig. 1-6 disclose a plate heat exchanger. As shown in fig. 1, a porous material plate heat exchanger comprises a first layer 1, a second layer 2, a third layer 3 and a fourth layer 4 which are sequentially arranged from top to bottom. The upper part of the first layer is provided with a cold fluid inlet and a cold fluid outlet. The fourth layer is provided with a hot fluid inlet and outlet.
Preferably, the fourth layer of hot fluid inlets 41 is disposed in the center of the back side of the fourth layer and the hot fluid outlets 42 are disposed on both sides of the fourth layer, as shown in fig. 1. The hot fluid flows in from the center and then flows out from both sides.
Preferably, the hot fluid flows in from one side of the fourth layer and flows out from the other side of the fourth layer. For example, from the left side of fig. 1, and from the right side.
As shown in fig. 2, the first layer 1 includes a cold fluid inlet 11 and a cold fluid outlet 12 provided at both ends of the front surface of the first layer, the second layer 2 includes an inlet header 21, an outlet header 22, an inlet branch pipe 23, an outlet branch pipe 24, an inlet flow path and an outlet flow path provided at the front surface of the second layer, wherein the upstream of the inlet header 21 and the downstream of the outlet header 22 are respectively connected to the cold fluid inlet 11 and the cold fluid outlet 12 of the first layer, the inlet header 21 and the outlet header 22 are respectively connected to the inlet branch pipe 23 and the outlet branch pipe 24, the second layer 2 includes a plurality of bent plate-like structures, one side of which forms the inlet branch pipe 23 and the other side of which forms the outlet branch pipe 24, and the inlet branch pipe 23 and the outlet branch pipe 24 are not directly connected; through holes penetrating the second layer are arranged in the inlet branch pipe 23 and the outlet branch pipe 24, so that an inlet flow channel and an outlet flow channel are formed; the third layer 3 comprises a porous material 31 on the front surface, and the porous material 31 is connected with the inlet flow channel and the outlet flow channel; the porous material 31 is formed by 3D printing, so that the porous material 31 has a pore structure, and the pore diameter at the fluid inlet of the inlet flow channel is larger than the pore diameter at the fluid outlet of the outlet flow channel. The fourth layer is a thermal fluid conduit in thermal contact with the third layer. The hot fluid flows through the fourth layer, transferring heat to the cold fluid of the third layer.
According to the application, the porous material is manufactured by adopting the porous material and the 3D printing technology, and the porous material structure is added at the bottom of the third layer, so that a more compact micro-channel is formed, the processing difficulty is reduced compared with that of a fin channel, the flowing space of cold fluid and the convection heat exchange area are increased, and the temperature uniformity of the bottom surface can be improved by changing the pore diameter of an inlet and an outlet of the porous material.
Compared with the traditional manufacturing technology, the porous material is manufactured by the 3D printing technology, the size of the aperture can be accurately realized, the working efficiency is improved, and the aperture change is more accurate.
According to the application, the pore diameter of the porous medium fluid inlet is larger than that of the fluid outlet, and the convection heat exchange capacity of the cold fluid at different pore diameters is different, so that the temperature uniformity and the convection heat exchange capacity of the whole cold plate are improved. For the flow heat exchange process under the uniform aperture, the temperature of the fluid at the inlet is lower, and the temperature difference between the fluid and the cold plate is larger, so the heat exchange process is more severe, and when the fluid flows to the outlet, the temperature of the fluid is raised to a certain extent due to the fact that the heat of a heat source is continuously absorbed in the previous flow process, so the heat exchange temperature difference between the fluid and the cold plate at the outlet is reduced, and the heat exchange capacity is greatly reduced compared with that at the inlet. This will result in more heat being carried away by the fluid at the inlet and less heat being carried away by the holes at the outlet, resulting in less uniform temperature of the soleplate. For the flow heat exchange process under the variable aperture, the heat conduction resistance is increased due to the fact that the aperture at the inlet is larger, the heat absorbed by the fluid at the inlet is reduced, the heat carrying capacity of the fluid at the outlet is enhanced, and meanwhile, the disturbance and the heat exchange can be enhanced due to the fact that the aperture at the outlet is smaller. However, the aperture ratio of the inlet and the outlet is preferably 1.5-2.5, otherwise the heat exchange process at the outlet is too severe, which also results in poor temperature uniformity of the bottom plate.
The porous medium is manufactured by adopting a 3D printing technology, a three-dimensional model of the porous medium is firstly built in Spacelaim software, the model is led into printing preparation software Preform, the direction, supporting material, component material and wall thickness of the model are determined, the porous medium is made of AlSi10Mg aluminum alloy material, and the Formlabs 3D printer is operated to print after the preparation work is determined. After printing, the construction platform is directly inserted into Form Wash, and the model is efficiently and uniformly automatically cleaned. After cleaning, the porous medium is removed from the printing surface by means of a rapid stripping technique, the support structure can be removed only for a few seconds, and finally the porous medium is transferred to Form Cure for curing, so that the material performance is improved to the maximum extent and the dimensional accuracy is ensured.
Preferably, the pore size of the porous material increases gradually along the flow direction of the fluid in the inlet header 21. Through the distribution, the capillary force is gradually enhanced along the direction away from the inlet of the inlet header, the flowing resistance is smaller and smaller, and the flowing of fluid with large resistance is more difficult to flow in the direction opposite to the direction with small resistance, so that the fluid distribution is more uniform along the flowing direction, and the problems of uneven heat exchange and over-high and over-low local temperature caused by uneven fluid distribution are avoided.
Preferably, the pore size of the porous material increases progressively in magnitude along the direction of flow of the fluid within the inlet header 21. The design of the variation amplitude is also a structure optimized through a large number of experiments and numerical simulation, so that the technical effect of uniform fluid distribution can be further realized, and the requirements of the application are more satisfied.
Preferably, the pore size of the porous material is changed according to the following rule:
the total length of the inlet header is L, and the aperture of the most downstream of the inlet header is D Powder (D) The aperture D at a distance l from the inlet header inlet is as follows: d (D) 2 ＝f×(D Powder (D) ) 2 +g×(D Powder (D) ) 2 ×（l/L） e Wherein e, f, g are coefficients, satisfying the following requirements:
1.083<e<1.104，0.995<f+g<1.011，0.499<f<0.625。
preferably, e increases gradually as L/L increases.
Preferably, 0.095< e <1.100, f+g=1, 0.565< f <0.578.
Through the arrangement, the fluid distribution is more uniform, the optimized formula is obtained through a large number of experiments and numerical simulation, and the technical effect of uniformly distributing the fluid can be optimally realized, so that the requirements of the application are more satisfied.
Preferably, the porous material has a progressively increasing pore distribution density along the direction of flow of the fluid within the inlet header 21. Through the distribution, the capillary force is gradually enhanced along the direction away from the inlet of the inlet header, the flowing resistance is smaller and smaller, and the flowing of fluid with large resistance is more difficult to flow in the direction opposite to the direction with small resistance, so that the fluid distribution is more uniform along the flowing direction, and the problems of uneven heat exchange and over-high and over-low local temperature caused by uneven fluid distribution are avoided.
Preferably, the porous material has a progressively increasing pore distribution density in the direction of flow of the fluid within the inlet header 21. The design of the variation amplitude is also a structure optimized through a large number of experiments and numerical simulation, so that the technical effect of uniform fluid distribution can be further realized, and the requirements of the application are more satisfied.
Preferably, the pore distribution density of the porous material is changed according to the following rule:
the total length of the inlet header is L, and the density of the most downstream of the inlet header is M Into (I) The density M at a distance l from the inlet header inlet is as follows: m=b×m Into (I) +c×M Into (I) ×（ l/L） a Wherein a, b, c are coefficients, satisfying the following requirements:
1.082<a<1.105，0.994<b+c<1.012，0.498<b<0.629。
preferably, a increases gradually as L/L increases.
Preferably, 0.095< a <1.100, b+c=1, 0.565< b <0.578.
Through the arrangement, the fluid distribution is more uniform, the optimized formula is obtained through a large number of experiments and numerical simulation, and the technical effect of uniformly distributing the fluid can be optimally realized, so that the requirements of the application are more satisfied.
Preferably, a plurality of through holes penetrating the second layer are provided in each of the inlet and outlet branch pipes. The distribution density of the through holes gradually increases along the flow direction of the fluid in the inlet header 21. Through the distribution, along the direction away from the inlet of the inlet header, along with the change of the flow area, the flow resistance is smaller and smaller, so that the inflow of fluid with large resistance is more difficult to be smaller than the inflow of fluid with small resistance, the distribution of the fluid along the flow direction is more uniform, and the problems of uneven heat exchange and over-high and over-low local temperature caused by uneven fluid distribution are avoided.
Preferably, the distribution density of the through holes gradually increases in the direction of flow of the fluid in the inlet header 21. The design of the variation amplitude is also a structure optimized through a large number of experiments and numerical simulation, so that the technical effect of uniform fluid distribution can be further realized, and the requirements of the application are more satisfied.
Preferably, a plurality of through holes penetrating the second layer are provided in each of the inlet and outlet branch pipes. The aperture of each through-hole gradually increases along the flow direction of the fluid in the inlet header 21. Through the distribution, the flow area is gradually increased along the direction away from the inlet header inlet, and along with the change of the flow area, the flow resistance is smaller and smaller, so that the inflow of fluid with large resistance is more difficult to be smaller than the inflow of fluid with small resistance, the fluid distribution is more uniform along the flow direction, and the problems of uneven heat exchange and over-high and over-low local temperature caused by uneven fluid distribution are avoided.
Preferably, the distribution density of the pore diameter of each through-hole gradually increases in the direction of the flow of the fluid in the inlet header 21. The design of the variation amplitude is also a structure optimized through a large number of experiments and numerical simulation, so that the technical effect of uniform fluid distribution can be further realized, and the requirements of the application are more satisfied.
Preferably, the porous material is manufactured by using a 3D printing technique. In the prior art manufacturing process, it is very difficult to achieve gradual pore change of the porous material. The application adopts the 3D printing technology for the capillary structure, so that the variable pore density is gradually distributed along the fluid flow, the processing technology is improved, and the regular change can be accurately realized through a computer. Compared with the existing preparation process, the gradual change printing process is designed, the processing result is more accurate, the accurate structural amplitude change is realized through the computer program, and the processing precision is greatly improved, so that the heat exchange efficiency is improved.
Preferably, the inlet header 21 and the outlet header 22 are designed in a tapered structure, and the flow passage area is smaller and smaller along the flow direction of the fluid in the inlet header and larger along the flow direction of the fluid in the outlet header 22. The even distribution of the fluid in the flow channel can be further ensured, so that the heat exchange efficiency can be improved, and the integral pressure drop can be reduced.
Preferably, the second layer 2 comprises a plurality of bent plate-like structures, one side of which forms an inlet branch pipe 23 and the other side forms an outlet branch pipe 24, the inlet branch pipe 23 and the outlet branch pipe 24 not being in direct communication. The capillary force of the fluid through the layer of capillary force of the hot fluid causes the fluid to flow from the inlet branch pipe 23 to the outlet branch pipe 24.
Preferably, the bent plate-like structure is a V-shaped structure or a trapezoid structure. The heat exchange micro-channels can be designed more in the same width, the heat exchange area is increased, and the whole heat exchange capacity is improved while the volume is reduced.
Preferably, as shown in fig. 3, the holes penetrating the second layer may be elongated. According to the application, through holes are formed in the second layer, so that fluid can enter the third layer 3 in a targeted manner through the holes, porous materials at corresponding positions of the third layer 3 can be arranged in a targeted manner, for example, the porous materials can be omitted for the positions where the holes are formed, and the porous materials are arranged at the rest positions. The above arrangement is thus achieved by 3D printing, avoiding the manufacturing difficulties of the prior art.
Preferably, the cold fluid inlet 11, the cold fluid outlet 12 are arranged diagonally on the first layer 1. The arrangement can ensure the heat exchange area of the fluid and reduce the occurrence of short circuit phenomenon.
The fourth layer is a layer of hot fluid piping. A cavity is arranged in the fourth layer, and the heating fluid passes through. Preferably, as shown in fig. 5, a rib matrix is provided in the cavity, said rib matrix being arranged in a spindle-shaped structure. The novel spindle-shaped structure is provided with the ribs, so that fluid can flow along the ribs, the flow resistance is reduced, heat is further fully exchanged with the capillary structure, and the heat exchange efficiency is improved.
As shown in FIG. 5, the rib matrix is a plurality of, and two adjacent rib matrixes are connected end to end. Preferably, each rib matrix is divided into multiple layers, each array comprising a central rib and multiple layers of peripheral ribs surrounding the central rib, each layer of ribs being of a fusiform (spindle) configuration. By providing multiple layers, the fluid is allowed to flow sufficiently therein for heat exchange.
The plurality of rib matrices form a group, the head of the first spindle-shaped structure of each group being opposite to the fluid direction of the liquid (facing the fluid flow direction), the tail of the first spindle-shaped structure being connected to the head of the second spindle-shaped structure, and so on, thereby forming a group. Through setting up the multilayer for the fluid can fully flow heat transfer therein, and the flow path of fluid carries out frequent flow and volume change along the shuttle shape along with flowing constantly moreover, further improves heat transfer efficiency.
Preferably, both the head and tail of the spindle are pointed.
Preferably, the tip angle of the head portion of the spindle-shaped structure is smaller than the tip angle of the tail portion. Through the structure, the fluid can be firstly slowly diffused along the shape of the shuttle, the characteristic of low heat exchange effect caused by rapid diffusion is avoided, the heat exchange is promoted, meanwhile, the guiding of the fluid is promoted, the resistance is reduced, and the heat exchange efficiency is improved.
Preferably, the line connecting the central ribs of each set is the same as the direction of fluid flow.
Preferably, the plurality of sets of rib matrices are arranged in parallel.
Preferably, the rib matrix is disposed at corresponding locations between the sets of ribs.
The cavity surface is provided with a streamline flow guiding module composed of fusiform rib matrixes, symmetrically distributed ribs also play a role in guiding flow in a fusiform distribution mode macroscopically, flow resistance is further reduced, heat is further fully exchanged with a capillary structure, and heat exchange efficiency is improved.
Preferably, the ribs extend from the top wall of the cavity toward the bottom wall.
Preferably, the upper plate of the cavity is the back side of the third layer.
Preferably, the rib is provided on the back of the third layer.
Preferably, the hot fluid flows in from the center of the fourth layer and then out from the four sides, as shown in FIG. 1, for example. The fourth layer is provided with a structure as shown in fig. 6. The bottom of the fourth-layer cavity is provided with baffle straight plates 43-46 and ribs 47-50, and the baffle straight plates comprise a center baffle straight plate 43 positioned at the center of the bottom plate, a second baffle straight plate 44 surrounding the outside of the center baffle straight plate 43, a third baffle straight plate 45 surrounding the outside of the second baffle straight plate 44 and an outer baffle straight plate 46 surrounding the outside of the third baffle straight plate 45;
preferably, as shown in fig. 6, the central baffle plate 43 comprises four baffle plate walls, each of the baffle plate walls 43 comprises two baffle plate walls which are at an angle to each other, the extension lines of the baffle plate walls of the four baffle plate walls form a first prismatic shape, and the baffle plate walls form a part of the edges of the first prismatic shape; a first interval is arranged between baffle straight plate walls of adjacent central baffle straight plates;
the second baffle plate 44 comprises four second baffle plate walls, each second baffle plate 44 comprises two baffle plate walls perpendicular to each other, the extension lines of the baffle plate walls of the four second baffle plate walls form a first rectangular structure, and the baffle plate walls form a part of the sides of the first rectangle; a second interval is arranged between baffle straight plate walls of the adjacent second baffle straight plates;
the third baffle straight plates 45 comprise four, each third baffle straight plate 45 comprises two baffle straight plate walls which are at a certain angle with each other, the extension lines of the baffle straight plate walls of the four third baffle straight plates form a second prismatic structure, and the baffle straight plate walls form a part of the edges of the second prismatic structure; a third space is arranged between baffle straight plate walls of the adjacent third baffle straight plates 45;
the outer baffle plate 46 comprises two outer baffle plates, each outer baffle plate 46 comprises a first baffle plate wall and two second baffle plate walls which are perpendicular to each other and are arranged at two ends of the baffle plate walls, the extension lines of the baffle plate walls of the two outer baffle plate plates form a second rectangular structure, and the first baffle plate wall and the second baffle plate wall form a part of the side of the second rectangle; a fourth spacing is provided between adjacent second straight walls of the two outer baffle-panels 46.
Preferably, a plurality of ribs 47 are provided inside the central baffle 43; a plurality of ribs 48 are arranged between the second baffle plate 44 and the central baffle plate 43, and a plurality of ribs 49 are arranged between the second baffle plate 44 and the third baffle plate 45; a plurality of ribs 50 are disposed between the third baffle 45 and the outer baffle 46.
The heat exchanger is internally provided with the flow guide structure, and particularly, the rectangular prismatic baffle straight plates with the multilayer vertical structures are arranged, so that the liquid flow range is wide, the cold liquid flow dead zone is effectively reduced, and the temperature uniformity of a hot flow surface is further improved.
In the heat exchanger, the cylindrical fins are arranged in the central baffle straight plate, between the central baffle straight plate and the second baffle straight plate, between the second baffle straight plate and the third baffle straight plate and between the third baffle straight plate and the external baffle straight plate, so that disturbance is enhanced in an increased area of the external space, namely disturbance of a convection field is enhanced, the heat exchange area is expanded, the heat exchange is enhanced, the overlarge flow resistance can be avoided, and the application range is wide.
Preferably, the extension of the line connecting the opposed first spaced midpoints, the extension of the opposed third spaced midpoints pass through the vertical points of the two baffle straight walls of the second baffle straight 44 and the vertical points of the two baffle straight walls of the outer baffle 46.
Preferably, the extension of the line connecting the midpoints of the second and fourth opposing spaces passes through the connection point of the two baffle walls of the central baffle 43 and the connection point of the two baffle walls of the third baffle 45.
Through above-mentioned preferred design, can make liquid distribution more even, the heat transfer effect is better.
Preferably, with respect to the structure of fig. 6, the fourth layer includes a hot fluid inlet 41 and a hot fluid outlet 42 disposed on the back surface, the hot fluid inlet 41 being disposed at a central position of the first prism, the hot fluid outlet 42 being disposed at 2, respectively, opposite ends of the second rectangle, being disposed outside the first straight wall, and a line connecting the central lines of the two outlets 42 passing through the center of the first straight wall. Through so setting, can make the fluid flow out from the fourth interval back detouring and get into the export to increase the flow area, improve heat exchange efficiency.
Through the structure, the hot liquid flows in from the central area of the cover plate, and when the hot liquid just enters the heat exchanger, the temperature is high, the temperature difference between the hot liquid and the heat source is large, the heat exchange capacity is strong, and the temperature of the heat source area can be controlled more effectively.
The application adopts a single-inlet and multi-outlet flow mode, so that cold liquid flows from the middle part to two sides, the phenomenon that the temperature gradually rises along the flow direction caused by the traditional single-inlet and single-outlet flow mode is improved, and the heat dissipation temperature uniformity is further improved.
The baffles 43-46 are flow directing structures and may be considered as elongated straight fins of larger dimensions. By arranging the baffle plates, the baffle plates can also play roles of turbulent flow and heat transfer enhancement.
Preferably, the hot fluid inlet 41 is located at a position intermediate the two liquid outlets. Through above-mentioned setting for liquid distribution is more even, and the heat dispersion is more even.
The ribs 47-50 are cylindrical.
The height of the ribs 47-50 is the same as the height of the baffle plates 43-46 and is equal to the height of the square cavity.
Preferably, as shown in FIG. 6, the vertical points of the vertical walls of the baffle plates 43-46 are positioned in a streamline configuration, preferably a circular arc configuration. Through setting up streamline structure, can reduce the flow resistance of liquid, reduce the dead zone of liquid, improve the heat transfer effect.
Preferably, the rib is provided on the back of the third layer.
The further from the center of the fourth layer, between the second and third straight-folded plates, outwardly from the center of the fourth layer, the further the distance between adjacent ribs 49. The flow space of the fluid is smaller and the flow resistance is increased as the third baffle plate is closer to the center, so that the flow speed of the fluid is kept relatively stable by arranging the adjacent ribs 49 further, the overall heat exchange can be relatively uniform, and local non-uniform heating and local premature damage are avoided.
It is further preferred that the distance between adjacent ribs 49 increases in magnitude the farther from the center of the fourth layer, between the second baffle and the third baffle, outwardly from the center of the fourth layer. The distribution is also in accordance with the change of the distribution rule of fluid flow and heat exchange, and the numerical simulation and experiments show that the heat exchange efficiency can be further improved.
The farther from the center of the fourth layer, between the third baffle and the outer baffle, the further the distance between adjacent ribs 50. The flow rate is relatively slow as the flow space resistance of the fluid is large along with the fact that the distance from the center is further, the fluid flow rate is relatively stable by arranging the distance between the adjacent ribs 50, the whole heat exchange can be relatively uniform, and local heating non-uniformity is avoided, so that local premature damage is caused.
It is further preferred that the distance between adjacent ribs 50 increases progressively in magnitude the farther from the center of the fourth tier, between the third baffle and the outer baffle, outwardly from the center of the fourth tier. The distribution is also in accordance with the change of the distribution rule of fluid flow and heat exchange, and the numerical simulation and experiments show that the heat exchange efficiency can be further improved.
In the designed central diffusion type flat tube, fluid enters the cavity of the flat tube from the inlet of the central area of the upper cover, passes through the bottom layer flow guiding structure, gradually flows to the periphery of the cavity of the flat tube from the central inlet area, exchanges heat with the surfaces of various flow passages (including ribs) in the flowing process, and finally flows out of outlets at two sides of the flat tube after being mixed at the connecting position of the heat exchanging area, so that heat exchange is performed.
However, compared with the traditional heat collecting tube plate, the central diffusion type flat tube changes the flow mode of single inlet and single outlet of fluid, and single inlet and double outlet are adopted instead, so that in the design, outlets are processed on two sides of the flat tube, and the temperature uniformity of the heat flow surface of the flat tube can be effectively improved.
Preferably, the ribs in fig. 5 and 6 are elastic members, and the elastic members can enable the cylinder ribs to be flushed when fluid flows, and the cylinder ribs can swing in a pulsating manner, so that scale removal is promoted, turbulence is caused by vibration, and heat transfer can be enhanced.
Preferably, the ribs are less and less resilient in the direction of the flow of the hot fluid. As the research shows that the temperature of the fluid is lower and lower along with the heat exchange of the fluid, the fluid is not easy to scale, and the scale degree is lighter and lighter along the flowing direction of the fluid, the elastic degree is continuously reduced, the purposes of further descaling and enhancing heat transfer are achieved, the heat conductor with large elasticity is reduced, and the cost is reduced.
It is further preferred that the elasticity of the ribs is increasing with a smaller and smaller amplitude along the flow direction of the hot fluid. The change is found according to the research, accords with the scaling rule, and can further reduce the cost, improve the heat exchange efficiency and reduce the scaling.
The heat exchanger work flow is as follows: the cold fluid is driven by the driving pump to flow from the cold fluid inlet 11 into the inlet header 21 and then into the porous material flow channel, then flows by the inlet branch pipe 23, is forced to flow downwards in the conical branch pipe under the barrier action of the top end, is received by the inlet flow channel below the branch pipe, flows in two opposite directions in the porous material because the two sides of the inlet flow channel are porous materials 31, absorbs heat transferred by the porous material 31 in the process, flows upwards under force after the heat absorption of the fluid is completed, flows into the outlet branch pipe 24 through the outlet flow channel, flows out through the outlet of the outlet branch pipe 24 and then flows into the outlet header 22 and finally flows out of the porous material flow channel through the cold fluid outlet 12, and the whole flow heat exchange process is completed.
While the application has been described in terms of preferred embodiments, the application is not so limited. Various changes and modifications may be made by one skilled in the art without departing from the spirit and scope of the application, and the scope of the application should be assessed accordingly to that of the appended claims.
Claims (9)
1. The utility model provides a plate heat exchanger who sets up many baffling straight plates, sets gradually first layer, second floor, third layer and fourth layer from the top down, and first layer is including setting up cold fluid inlet and the cold fluid outlet in openly, and the fourth layer is the hot fluid pipeline with the third layer thermal contact, its characterized in that sets up the cavity in the fourth layer, and the heating fluid passes through, set up baffling straight plate and fin on the bottom of fourth layer cavity, baffling straight plate includes the central baffling straight plate that is located the bottom plate center, surrounds at the outside second baffling straight plate of central baffling straight plate and surrounds at the outside baffling straight plate of second baffling straight plate and surround at the outside baffling straight plate of third baffling straight plate, and the fin is located between the straight plate.
2. The plate heat exchanger of claim 1 wherein the central baffle comprises four, each central baffle comprising two baffle walls at an angle to each other, the extensions of the baffle walls of the four central baffles forming a first prism, the baffle walls forming a portion of the sides of the first prism; a first interval is arranged between baffle straight plate walls of adjacent central baffle straight plates; the second baffle straight plates comprise four baffle straight plate walls which are perpendicular to each other, the extension lines of the baffle straight plate walls of the four second baffle straight plates form a first rectangular structure, and the baffle straight plate walls form a part of the side of the first rectangle; a second interval is arranged between baffle straight plate walls of the adjacent second baffle straight plates; the third baffle straight plates comprise four baffle straight plate walls which are at a certain angle with each other, the extension lines of the baffle straight plate walls of the four third baffle straight plates form a second prismatic structure, and the baffle straight plate walls form a part of the edges of the second prismatic structure; a third interval is arranged between baffle straight plate walls of adjacent third baffle straight plates; the external baffle straight plates comprise two external baffle straight plates, each external baffle straight plate comprises a first straight plate wall and two second straight plate walls which are perpendicular to each other and are arranged at two ends of the straight plate wall, the extension lines of the baffle straight plate walls of the two external baffle straight plates form a second rectangular structure, and the first straight plate wall and the second straight plate wall form a part of the side of the second rectangle; a fourth space is provided between adjacent second baffle walls of the two outer baffle plates.
3. The plate heat exchanger of claim 2 wherein a plurality of fins are disposed within the central baffle plate; a plurality of ribs are arranged between the second baffle straight plate and the central baffle straight plate, and a plurality of ribs are arranged between the second baffle straight plate and the third baffle straight plate; a plurality of ribs are arranged between the third baffle plate and the external baffle plate.
4. A plate heat exchanger according to claim 2, wherein the extension of the line connecting the opposed first spaced midpoints, the extension of the opposed third spaced midpoints pass through the vertical points of the two baffle straight walls of the second baffle straight plate which are mutually perpendicular, the vertical points of the two baffle straight walls of the outer baffle straight plate which are mutually perpendicular.
5. A plate heat exchanger as claimed in claim 2, wherein the extension of the line connecting the opposed second spaced midpoints, the extension of the opposed fourth spaced midpoints pass through the connection point of the two baffle straight walls of the central baffle straight plate at an angle to each other, the connection point of the two baffle straight walls of the third baffle straight plate at an angle to each other.
6. A plate heat exchanger according to claim 2, wherein the fourth layer comprises a hot fluid inlet and a hot fluid outlet arranged on the back side, the hot fluid inlet being arranged in the centre of the first prism, the hot fluid outlet being arranged in 2, respectively arranged at opposite ends of the second rectangle, arranged outside the first straight wall, the line connecting the centre lines of the two outlets passing through the centre of the first straight wall.
7. A plate heat exchanger according to claim 2, wherein the fins and the baffle plates have the same height, which is equal to the height of the square cavity.
8. A plate heat exchanger according to claim 1, wherein the second layer comprises an inlet header, an outlet header, an inlet branch pipe, an outlet branch pipe, an inlet flow channel and an outlet flow channel arranged on the front surface, wherein the upstream of the inlet header and the downstream of the outlet header are respectively connected with the cold fluid inlet and the cold fluid outlet of the first layer, the inlet header and the outlet header are respectively connected with the inlet branch pipe and the outlet branch pipe, the front surface of the second layer comprises a plurality of bent plate-like structures, one side of the plate-like structures forms the inlet branch pipe, the other side forms the outlet branch pipe, and the inlet branch pipe and the outlet branch pipe are not directly communicated; through holes penetrating through the second layer are arranged in the inlet branch pipe and the outlet branch pipe, so that an inlet flow channel and an outlet flow channel are formed; the third layer comprises a porous material positioned on the front surface, and the porous material is connected with the inlet runner and the outlet runner; the porous material adopts a 3D printing technology, so that the porous material is of a pore-changing structure, and the pore diameter of the porous material at the fluid inlet of the inlet runner is larger than that of the porous material at the fluid outlet of the outlet runner.
9. A plate heat exchanger as claimed in claim 8, wherein the pore distribution density of the porous material increases gradually in the direction of flow of the fluid in the inlet header.
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| CN202211374006 | 2022-11-04 | ||
| CN2022113740066 | 2022-11-04 |
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| CN202211462120.4A Active CN117073430B (en) | 2022-11-04 | 2022-11-17 | Plate heat exchanger with multi-baffle straight plates |
| CN202311203752.3A Pending CN117232297A (en) | 2022-11-04 | 2023-09-18 | Plate heat exchanger with multi-baffle straight plates |
| CN202311203278.4A Pending CN117232296A (en) | 2022-11-04 | 2023-09-18 | Plate heat exchanger of spindle-shaped hot runner |
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| CN202311203278.4A Pending CN117232296A (en) | 2022-11-04 | 2023-09-18 | Plate heat exchanger of spindle-shaped hot runner |
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| US20020056544A1 (en) * | 1999-07-23 | 2002-05-16 | Kaveh Azar | Heat sink with radial shape |
| CN108180773A (en) * | 2018-01-29 | 2018-06-19 | 西安热工研究院有限公司 | A kind of interruption fin structure printed circuit board heat exchanger core body |
| CN113108491B (en) * | 2020-01-11 | 2022-08-09 | 山东鑫瑞安装工程有限公司 | Solar heat collecting pipe |
| CN213811877U (en) * | 2020-10-13 | 2021-07-27 | 无锡万盛换热器制造有限公司 | Plate-fin cooler |
| CN112822913A (en) * | 2020-12-30 | 2021-05-18 | 西安交通大学 | Penetrating ultrathin liquid cooling plate integrated with low-flow-resistance manifold network |
| CN113776367B (en) * | 2021-11-03 | 2022-07-01 | 山东大学 | Manifold shell-and-tube heat exchanger |
| CN114136129B (en) * | 2021-12-20 | 2023-02-03 | 山东大学 | Manifold micro-column array flat plate heat exchanger |
| CN114353564B (en) * | 2022-01-12 | 2023-12-15 | 西安交通大学 | Grooved spindle-shaped fin printed circuit board heat exchanger core |
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2022
- 2022-11-17 CN CN202211438264.6A patent/CN116428897B/en active Active
- 2022-11-17 CN CN202211462120.4A patent/CN117073430B/en active Active
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2023
- 2023-09-18 CN CN202311203752.3A patent/CN117232297A/en active Pending
- 2023-09-18 CN CN202311203278.4A patent/CN117232296A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103477179A (en) * | 2010-12-09 | 2013-12-25 | 埃赛力达技术埃尔科斯有限责任公司 | Homogeneous liquid cooling of LED array |
| CN103206880A (en) * | 2012-01-16 | 2013-07-17 | 波音公司 | Multi-channel Cooling Plenum |
| CN111238265A (en) * | 2019-12-13 | 2020-06-05 | 山东大学 | Water-cooling plate heat exchanger with pulsating vibration |
| CN112033189A (en) * | 2020-01-08 | 2020-12-04 | 中国北方车辆研究所 | Plate heat exchanger cooled by liquid |
| TW202223319A (en) * | 2020-12-01 | 2022-06-16 | 財團法人金屬工業研究發展中心 | Heat exchanger |
Also Published As
| Publication number | Publication date |
|---|---|
| CN117073430B (en) | 2024-04-26 |
| CN117232297A (en) | 2023-12-15 |
| CN116428897B (en) | 2024-01-26 |
| CN117232296A (en) | 2023-12-15 |
| CN116428897A (en) | 2023-07-14 |
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