CN117232297B - A plate heat exchanger with multi-baffle straight plates - Google Patents
A plate heat exchanger with multi-baffle straight plates Download PDFInfo
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- CN117232297B CN117232297B CN202311203752.3A CN202311203752A CN117232297B CN 117232297 B CN117232297 B CN 117232297B CN 202311203752 A CN202311203752 A CN 202311203752A CN 117232297 B CN117232297 B CN 117232297B
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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
- F28D9/0031—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 the conduits for one heat-exchange medium being formed by paired plates touching each other
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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
- F28F9/02—Header boxes; End plates
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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
- F28F9/02—Header boxes; End plates
- F28F2009/0285—Other particular headers or end plates
- F28F2009/029—Other particular headers or end plates with increasing or decreasing cross-section, e.g. having conical shape
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
本发明提供了一种设置多折流直板的板式换热器，从上到下依次设置第一层、第二层、第三层和第四层，第一层包括设置在正面的冷流体进口和冷流体出口，第四层是与第三层热接触的热流体管道，其特征在于，第四层中设置空腔，供热流体通过，所述第四层空腔的底部上设置折流直板和肋片，所述折流直板包括位于底板中心的中心折流直板、包围在中心折流直板外部的第二折流直板和包围在第二折流直板外部的第三折流直板以及包围在第三折流直板外部的外部折流直板，肋片位于折流直板之间。本发明旨在提供一种板式换热器，内部设有导流结构，尤其是通过设置多层垂直结构的长方形棱形折流直板，使得液体流动范围广泛，有效减少冷液体流动死区，进一步改善热流面的均温性。
The present invention provides a plate heat exchanger with multiple baffle plates, wherein the first layer, the second layer, the third layer and the fourth layer are sequentially arranged from top to bottom, the first layer includes a cold fluid inlet and a cold fluid outlet arranged on the front, the fourth layer is a hot fluid pipeline in thermal contact with the third layer, and is characterized in that a cavity is arranged in the fourth layer for the hot fluid to pass through, and baffle plates and fins are arranged on the bottom of the fourth layer cavity, the baffle plates include a central baffle plate located at the center of the bottom plate, a second baffle plate surrounded by the outside of the central baffle plate, a third baffle plate surrounded by the outside of the second baffle plate, and an outer baffle plate surrounded by the outside of the third baffle plate, and the fins are located between the baffle plates. The present invention aims to provide a plate heat exchanger with a flow guide structure inside, especially by arranging multiple layers of vertically structured rectangular prism-shaped baffle plates, so that the liquid flows in a wide range, effectively reducing the dead zone of cold liquid flow, and further improving the temperature uniformity of the heat flow surface.
Description
Technical Field
The invention 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. In the fields such as electronics, petrifaction, communication, aerospace and the like, the special requirements on the size and the weight of the heat exchanger are met because the working scene is special, 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.
The fin is added, which is helpful to increase the heat exchange 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.
In order to avoid a flowing 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 the flow guide 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, and the processing technology is also considered, so that the plate heat exchanger is sometimes limited, for example, the flow channel structure is complex, the processing is difficult, the thicker the fins are, the larger the distance between the fins is, the smaller the heat exchange area is, the lower the heat dissipation capacity of the cold plate is, the thickness of the fins is designed to be too small and densely distributed for increasing the heat exchange area, the processing is difficult, the flow resistance is increased, and the flow distribution of the 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 invention improves the prior heat exchanger, and provides a novel plate heat exchanger, wherein the bedroom heat exchanger is made of 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 the porous material can be printed in a 3D way, so that the porous material is simple to process and convenient to operate, and a structure which is difficult to realize normally can be realized. The hot fluid channel is improved, so that the flow resistance is reduced and the heat exchange efficiency is improved.
Disclosure of Invention
The invention 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 invention 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, 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.
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, an extension line of each baffle plate wall of each four central baffle plate forms a first prismatic shape, a first interval is arranged between baffle plate walls of adjacent central baffle plate, each second baffle plate comprises four baffle plate walls, each second baffle plate wall comprises two baffle plate walls which are perpendicular to each other, an extension line of each baffle plate wall of each four second baffle plate walls forms a first rectangular structure, a first part of a first rectangular edge is formed between baffle plate walls of each adjacent second baffle plate, a second interval is arranged between baffle plate walls of each adjacent second baffle plate, each third baffle plate comprises four baffle plate walls which are at a certain angle to each other, a second prismatic structure is formed between extension line of baffle plate walls of each adjacent central baffle plate, a first part of baffle plate wall forms a second prismatic shape, a second rectangular structure is formed between extension line of baffle plate walls of each adjacent second baffle plate wall, and each second extension line of baffle plate wall of each adjacent second baffle plate wall is arranged between two adjacent baffle plate walls, and the second extension line of each second baffle plate wall is arranged between two adjacent baffle plate walls of each adjacent second baffle plate wall forms a second rectangular structure.
Preferably, a plurality of ribs 47 are arranged inside the central baffle straight plate, a plurality of ribs are arranged between the second baffle straight plate and the third baffle straight plate, and a plurality of ribs are arranged between the third baffle straight plate and the outer baffle straight 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 the inlet branch pipe, the other side forms the outlet branch pipe, the inlet branch pipe and the outlet branch pipe are not directly communicated, through holes penetrating the second layer are arranged in the inlet branch pipe and the outlet branch pipe so as to form the inlet flow channel and the outlet flow channel, the third layer comprises porous materials positioned on the front surface, the porous materials are connected with the inlet flow channel and the outlet flow channel, and the porous materials adopt a 3D printing technology so that the pore diameter of the porous materials is larger than the pore diameter of the fluid outlet of the outlet flow channel at the inlet position of the inlet flow channel.
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 invention has the following advantages:
1) The invention 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 invention 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 invention 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 of the computer can be accurately realized. 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 invention, 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 invention, 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 invention;
FIG. 2 is a schematic view of a split structure of the heat exchanger of the present invention;
FIG. 3 is a second layer block diagram of the heat exchanger of the present invention;
FIG. 4 is a schematic diagram of the cold fluid flow of the heat exchanger of the present invention;
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.
Detailed Description
The following describes the embodiments of the present invention 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 is disposed in the center of the back side of the fourth layer and the hot fluid outlets 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 comprises a cold fluid inlet 11 and a cold fluid outlet 12 arranged at two ends of the front surface of the third layer, the second layer 2 comprises an inlet header 21, an outlet header 22, an inlet header 23, an outlet header 24, an inlet runner 25 and an outlet runner 26 arranged 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 with the fluid inlet 11 and the fluid outlet 12 of the first layer, the inlet header 21 and the outlet header 22 are respectively connected with the inlet header 23 and the outlet header 24, the second layer 2 comprises a plurality of bent plate-shaped structures, one side of each plate-shaped structure forms the inlet header 23, the other side forms the outlet header 24, the inlet header 23 and the outlet header 24 are not directly communicated, through holes penetrating the second layer are arranged in the inlet header 23 and the outlet header 24, so as to form an inlet runner 25 and an outlet runner 26, the third layer 3 comprises a porous material 31 positioned at the front surface, the porous material 31 is connected with the inlet runner 25 and the outlet runner 26, and the porous material 31 is formed by adopting a 3D printing technology, so that the porous material 31 has a pore size larger than the pore size of the inlet runner at the outlet runner. 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 invention, 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 invention, 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 SPACECLAIM software, the model is imported into printing preparation software PreForm, the direction, supporting materials, component materials and wall thickness of the model are determined, the porous medium is made of an AlSi10Mg aluminum alloy material, and the operation Formlabs D 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 22. 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, the aperture of the most downstream of the inlet header is D Powder (D) , the aperture D rule at the position of the distance L from the inlet of the inlet header is as follows, D 2＝f×(D Powder (D) )2+g×(D Powder (D) )2×(l/L)e, wherein e, f and g are coefficients, and the following requirements are satisfied:
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 22. 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, the density of the most downstream of the inlet header is M Into (I) , and the density M at the position of L from the inlet of the inlet header is as follows, wherein M=b×M Into (I) +c×M Into (I) ×(l/L)a, and a, b and c are coefficients, and the following requirements are met:
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 increases progressively in magnitude along the direction of flow of the fluid within the inlet header 22. 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 is gradually increased in magnitude along the flow direction of the fluid in the inlet header 22. 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 invention adopts the 3D printing technology for the capillary structure, so that the variable pore density of the capillary structure is gradually distributed along the fluid flow, the processing technology is improved, and the regular change of the computer can be accurately realized. 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. By means of the isomorphic structure, fluid can be slowly diffused along the shape of the shuttle, the characteristic of low heat exchange effect caused by rapid diffusion is avoided, heat exchange is promoted, guiding of the fluid is promoted, resistance is reduced, and 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 central baffle plate 43 comprises two baffle plate walls which are at a certain angle with each other, and 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;
The second baffle straight plates 44 comprise four second baffle straight plates 44, each second baffle straight plate 44 comprises two baffle straight plate walls which are mutually perpendicular, and 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 sides of the first rectangle;
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 451 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;
the outer baffle 46 comprises two outer baffle plates 46, 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 plates form a second rectangular structure, the first baffle plate walls and the second baffle plate walls form a part of the sides of the second rectangle, and a fourth interval is arranged between the adjacent second baffle plate walls of the two outer baffle plates 46.
Preferably, a plurality of ribs 47 are provided inside the central baffle plate 43, a plurality of ribs 48 are provided between the second baffle plate 44 and the central baffle plate 43, a plurality of ribs 49 are provided between the second baffle plate 44 and the third baffle plate 45, and a plurality of ribs 50 are provided between the third baffle plate 45 and the outer baffle plate 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 441 of the second baffle straight 44 and the vertical points of the two baffle straight walls 461 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 further from the center of the fourth tier, between the third baffle and the fourth riser, 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, outwardly from the center of the fourth tier, between the third baffle and the fourth riser. 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 working flow of the heat exchanger is that cold fluid is driven by a driving pump to flow into an inlet branch pipe 21 from a fluid inlet 11, then flows into a porous material flow passage 22 and is split through an inlet branch pipe 23, the fluid is forced to flow downwards in a conical branch pipe under the barrier effect of the top end, the split flow is received by an inlet flow passage 25 below the branch pipe, and because the two sides of the inlet flow passage 25 are porous materials 31, the fluid flows in two opposite directions in the porous materials, absorbs heat transferred by the porous materials 31 in the process, and flows upwards under force after the heat absorption of the fluid is completed, flows into an outlet branch pipe 24 through an outlet flow passage 26, flows out through an outlet branch pipe 24, then flows into the outlet branch pipe 22 and flows out of the porous material flow passage, and finally flows out through a fluid outlet 12, so that the whole flow heat exchange process is completed.
While the invention has been described in terms of preferred embodiments, the invention 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 invention, and the scope of the invention should be assessed accordingly to that of the appended claims.
Claims (8)
1. The plate heat exchanger is characterized in that a cavity is arranged in the fourth layer, heat supply fluid passes through the cavity, a baffle straight plate and ribs are arranged on the bottom of the fourth layer cavity, the baffle straight plate comprises 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 ribs are positioned between the straight plates; 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 the inlet branch pipe, the other side forms the outlet branch pipe, the inlet branch pipe and the outlet branch pipe are not directly communicated, through holes penetrating the second layer are arranged in the inlet branch pipe and the outlet branch pipe so as to form an inlet flow channel and an outlet flow channel, the third layer comprises porous materials positioned on the front surface, the porous materials are connected with the inlet flow channel and the outlet flow channel, the porous materials adopt a 3D printing technology so that the pore diameter of the porous materials is larger than the pore diameter of the outlet flow channel at the fluid inlet position of the inlet flow channel, the pore size of the porous material gradually increases.
2. The plate heat exchanger of claim 1 wherein the central baffle comprises four central baffle walls, each central baffle wall comprising two baffle walls at an angle to each other, the extension lines of the four central baffle walls forming a first prismatic shape, the baffle walls forming a portion of a side of the first prismatic shape, a first spacer disposed between the baffle walls of adjacent central baffles, the second baffle comprising four second baffle walls, each second baffle wall comprising two baffle walls perpendicular to each other, the extension lines of the four second baffle walls forming a first rectangular structure, the baffle walls forming a first portion of a side of the first rectangular shape, the extension lines of the adjacent second baffle walls forming a second spacer disposed between the extension lines of the third baffle walls, each third baffle wall comprising two baffle walls at an angle to each other, the extension lines of the baffle walls of the fourth baffle walls forming a second rectangular structure, the extension lines of the baffle walls between the two adjacent baffle walls forming two side of the second rectangular structure, and the outer portion of the second baffle walls forming a rectangular structure between the two extension lines of the second baffle walls.
3. The plate heat exchanger of claim 2 wherein a plurality of fins are disposed within the central baffle plate, a plurality of fins are disposed between the second baffle plate and the third baffle plate, and a plurality of fins are disposed between the third baffle plate and the outer 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 pore distribution density of the porous material increases gradually in the direction of flow of the fluid in the inlet header.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211374006 | 2022-11-04 | ||
| CN2022113740066 | 2022-11-04 |
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| CN117232297A CN117232297A (en) | 2023-12-15 |
| CN117232297B true CN117232297B (en) | 2024-11-29 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202410030281.9A Active CN118208977B (en) | 2022-11-04 | 2022-11-17 | A plate heat exchanger with a multi-layer structure having through holes |
| CN202211438264.6A Expired - Fee Related CN116428897B (en) | 2022-11-04 | 2022-11-17 | A spindle-shaped hot runner plate heat exchanger |
| CN202211462120.4A Expired - Fee Related CN117073430B (en) | 2022-11-04 | 2022-11-17 | Plate heat exchanger with multi-baffle straight plates |
| CN202311203752.3A Active CN117232297B (en) | 2022-11-04 | 2023-09-18 | A plate heat exchanger with multi-baffle straight plates |
| CN202311203278.4A Active CN117232296B (en) | 2022-11-04 | 2023-09-18 | Plate heat exchanger of spindle-shaped hot runner |
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| CN202410030281.9A Active CN118208977B (en) | 2022-11-04 | 2022-11-17 | A plate heat exchanger with a multi-layer structure having through holes |
| CN202211438264.6A Expired - Fee Related CN116428897B (en) | 2022-11-04 | 2022-11-17 | A spindle-shaped hot runner plate heat exchanger |
| CN202211462120.4A Expired - Fee Related CN117073430B (en) | 2022-11-04 | 2022-11-17 | Plate heat exchanger with multi-baffle straight plates |
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| CN202311203278.4A Active CN117232296B (en) | 2022-11-04 | 2023-09-18 | Plate heat exchanger of spindle-shaped hot runner |
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| CN117029550B (en) * | 2023-07-20 | 2025-11-14 | 杭州沈氏节能科技股份有限公司 | A plate channel structure, a heat exchanger core, and a printed circuit board type heat exchanger. |
| CN118960471B (en) * | 2024-08-02 | 2025-11-11 | 西安交通大学 | Layered topological micro-channel radiator with low flow resistance manifold structure |
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| CN113776367A (en) * | 2021-11-03 | 2021-12-10 | 山东大学 | A manifold shell and tube heat exchanger |
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| US20020056544A1 (en) * | 1999-07-23 | 2002-05-16 | Kaveh Azar | Heat sink with radial shape |
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| US9494370B2 (en) * | 2010-12-09 | 2016-11-15 | GeramTec GmbH | Homogeneous liquid cooling of LED array |
| US10161691B2 (en) * | 2012-01-16 | 2018-12-25 | The Boeing Company | Multi-channel cooling plenum |
| CN104768356B (en) * | 2015-04-27 | 2017-06-06 | 中国电子科技集团公司第三十八研究所 | A kind of water cooling hardened structure of application 3D printing technique |
| CN104864751A (en) * | 2015-06-12 | 2015-08-26 | 浙江大学 | Micro-channel plate heat exchanger with triangular corrugated flowing channel |
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| CN110779372B (en) * | 2019-11-12 | 2021-01-29 | 山东大学 | Water-cooled tube plate heat exchanger with variable cylindrical fin spacing |
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- 2022-11-17 CN CN202410030281.9A patent/CN118208977B/en active Active
- 2022-11-17 CN CN202211438264.6A patent/CN116428897B/en not_active Expired - Fee Related
- 2022-11-17 CN CN202211462120.4A patent/CN117073430B/en not_active Expired - Fee Related
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2023
- 2023-09-18 CN CN202311203752.3A patent/CN117232297B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112033189A (en) * | 2020-01-08 | 2020-12-04 | 中国北方车辆研究所 | Plate heat exchanger cooled by liquid |
| CN113776367A (en) * | 2021-11-03 | 2021-12-10 | 山东大学 | A manifold shell and tube heat exchanger |
Also Published As
| Publication number | Publication date |
|---|---|
| CN118208977A (en) | 2024-06-18 |
| CN117232296B (en) | 2024-11-05 |
| CN118208977B (en) | 2025-01-28 |
| CN117073430B (en) | 2024-04-26 |
| CN116428897B (en) | 2024-01-26 |
| CN116428897A (en) | 2023-07-14 |
| CN117232296A (en) | 2023-12-15 |
| CN117073430A (en) | 2023-11-17 |
| CN117232297A (en) | 2023-12-15 |
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