CN101443621A - Parallel flow heat exchanger with crimped channel entrance - Google Patents
Parallel flow heat exchanger with crimped channel entrance Download PDFInfo
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- CN101443621A CN101443621A CNA2005800475315A CN200580047531A CN101443621A CN 101443621 A CN101443621 A CN 101443621A CN A2005800475315 A CNA2005800475315 A CN A2005800475315A CN 200580047531 A CN200580047531 A CN 200580047531A CN 101443621 A CN101443621 A CN 101443621A
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- heat exchanger
- shrinkage
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- manifold
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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
- F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
- F28F9/0282—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by varying the geometry of conduit ends, e.g. by using inserts or attachments for modifying the pattern of flow at the conduit inlet or outlet
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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
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B39/00—Evaporators; Condensers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B41/00—Fluid-circulation arrangements
- F25B41/30—Expansion means; Dispositions thereof
- F25B41/37—Capillary tubes
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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
- F28D1/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
- F28D1/02—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid
- F28D1/04—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits
- F28D1/053—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being straight
- F28D1/0535—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being straight the conduits having a non-circular cross-section
- F28D1/05366—Assemblies of conduits connected to common headers, e.g. core type radiators
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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
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/02—Tubular elements of cross-section which is non-circular
- F28F1/025—Tubular elements of cross-section which is non-circular with variable shape, e.g. with modified tube ends, with different geometrical features
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B2500/00—Problems to be solved
- F25B2500/01—Geometry problems, e.g. for reducing size
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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
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0068—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for refrigerant cycles
- F28D2021/0071—Evaporators
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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
- F28F2260/00—Heat exchangers or heat exchange elements having special size, e.g. microstructures
- F28F2260/02—Heat exchangers or heat exchange elements having special size, e.g. microstructures having microchannels
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Geometry (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Compression-Type Refrigeration Machines With Reversible Cycles (AREA)
- Details Of Heat-Exchange And Heat-Transfer (AREA)
Abstract
A parallel flow (minichannel or microchannel) evaporator includes channels which are crimped at or adjacent to their entrance location which provides for a refrigerant expansion and pressure drop control resulting in the elimination of refrigerant maldistribution in the evaporator and prevention of potential compressor flooding. Progressive crimping to counter-balance factors effecting refrigerant distribution is also disclosed.
Description
The cross reference of related application
The application's reference and the title that requires to submit on February 2nd, 2005 are the U.S. Provisional Application No.60/649 of " the parallel type evaporimeter with shrinkage channel entrance ", and 383 priority, the application combine the full content of this application by reference.
Technical field
The present invention is broadly directed to conditioner, heat pump and refrigeration system, and more specifically relates to its parallel type evaporimeter.
Background technology
The definition of so-called parallel flow heat exchanger is widely used in conditioner and refrigerating industry, and refer in particular to the heat exchanger with a plurality of paralleled paths, cold-producing medium distributes in the paralleled path and flows on the orientation that is basically perpendicular to inlet manifold and the flow of refrigerant direction of outlet in the manifold.This definition is highly suitable for the present technique field and uses in the text.
It is well known phenomenon that cold-producing medium in the refrigerant system evaporimeter distributes improper.It causes the tangible degeneration of evaporimeter and whole system performance in large-scale operating condition.Since the flow impedance difference in the boiler channel, the non-homogeneous distribution of air flow on the external heat transfer surfaces, incorrect heat exchanger orientation or bad manifold and distribution system design may occur cold-producing medium distribute improper.Because it is about the particular design of the cold-producing medium that is routed to each refrigerant lines, the distribution in the parallel type evaporimeter is improper remarkable especially.Attempted eliminating or reduced of the influence of this phenomenon, but do not had or obtained less success the parallel type performance of evaporator.The main cause of this failure is generally expensive relevant with the mistake of the complexity of the technology of being advised and poor efficiency and solution.
In recent years, parallel flow heat exchanger, particularly furnace brazing aluminum heat exchanger have been subjected to a large amount of concerns, not only at automotive field but also at heating, ventilation, air conditioning and refrigeration (HVAC﹠amp; R) industry.Adopt the main cause of parallel type technology relevant with the corrosion resistance of its remarkable performance, high compactness and enhancing.Parallel flow heat exchanger is applied in the condenser and evaporator application of multiple product and system's design and structure now.Although indicating bigger benefit and income, evaporator application more has challenge and problem.It is to implement one of the main misgivings of this technology and obstacle in evaporator application that cold-producing medium distributes improper.
As is known because different pressure drop in channel interior and inlet manifold and the outlet manifold, and bad manifold and distribution system design, occur cold-producing medium in the parallel flow heat exchanger distribute improper.In manifold, the difference of refrigerant path length, be separated and gravity is to cause to distribute principal element improperly.In heat exchanger passages, the variation of the coefficient of overall heat transmission, distribution of air flow, manufacturing tolerance and gravity is the mastery factor.In addition, the trend of heat exchanger performance enhancement is impelled the miniaturization (so-called small size tunnel or minitype channel) of its passage recently, cold-producing medium distribution that this has transferred negative effect.Because the control all of these factors taken together is difficulty very, many trials of former managing system refrigerant distribution particularly in the parallel type evaporimeter, all end in failure.
In the refrigerant system that uses parallel flow heat exchanger, entrance and exit manifold or collector (these terms can be used alternatingly in the text) are generally traditional cylindricality.When two phase flow enters collector, vapor phase is separated mutually with liquid usually.Because two phase individual flow, it is improper to occur the cold-producing medium distribution easily.
If two phase flow enters inlet manifold with high relatively speed, liquid phase (drop) is carried the distal part of manifold entrance arrival collector further away from each other by the momentum of stream.Thereby the passage of close manifold entrance mainly receives vapor phase, and receives the liquid phase mostly away from the passage of manifold entrance.On the other hand, if it is low to enter the two phase flow speed of manifold, then there are not enough momentum to carry the liquid phase along collector.As a result, liquid enters the passage of close inlet mutually, and vapor phase advances to passage farthest.Equally, liquid phase and vapor phase in the inlet manifold can be separated by gravity, cause the improper consequence of similar distribution.In either event, distribute improper point to show as the degeneration of evaporimeter and whole system performance rapidly.
In addition, distribute improper point can cause two-phase (zero is overheated) state, impel compressor suction device place can be transformed into the potential overflow of compressor damage rapidly in the outlet of some passage.
Summary of the invention
Thereby the purpose of this invention is to provide a kind of system and method that overcomes above-mentioned prior art problems.
The objective of the invention is to introduce pressure drop control for the parallel type evaporimeter, the pressure drop of this pressure drop control process in a basic balance heat exchanger passages also thereby is eliminated cold-producing medium and is distributed improper and relative problem.In addition, the import that the objective of the invention is at each passage provides cold-producing medium to expand, thereby eliminates the main two phase flow in the inlet manifold and prevent to be separated, and this is that cold-producing medium distributes main reason improperly.
According to the present invention, each passage its entrance location or near shrinkage, making provides desirable restriction for each passage.If desired, restriction size can change at interchannel, so that adapt to other non-homogeneous factor (for example different coefficients of overall heat transmission) that influence distributes improper point.Passage can extreme portion/import shrinkage or apart from the shrinkage of import certain distance so that do not disturb the soldered fitting of inlet manifold.In addition, internal rigid (and/or conduct heat strengthen) blade can be in the shrinkage process simple compression or before shrinkage, machine.In addition, these restrictions can be used as low-cost elementary (and only) expansion gear of using or needs accurate cross thermal control and adopt fixing restriction device (for example capillary or orifice) of another area or thermostatic expansion valve (TXV) or electric expansion valve (EXV) as the situation of primary expansion device under as the compound expansion device.Equally, under latter event, it is extra high that the accuracy of shrinkage needs not to be tolerance.
Under two kinds of situations of above-outlined, if but especially provide the shrinkage restriction as primary expansion device at each channel entrance place of parallel type evaporimeter, their representatives are to the main resistance of the stream of the cold-producing medium in the evaporimeter.In this case, the main pressure drop region will passage or the change in pressure drop in the manifold of crossing these restrictions and parallel type evaporimeter plays the effect of less (unimportant).In addition, occur in the import of each passage because cold-producing medium expands, mainly be flow through inlet manifold and can not occur being separated before entering each boiler channel of the cold-producing medium of single-phase liquid.Thereby, realized that even cold-producing medium distributes, strengthened evaporimeter and systematic function, avoided the overflow situation at compressor suction place, can not lose simultaneously and cross thermal control (no matter when needing) accurately.In addition, the Ultra Low Cost of proposed method makes the present invention have a great attraction.
Can adopt any suitable shrinkage means, for example have the shrinkage instrument of pliers form of desired shrinkage face geometry or the stamping die that use has desired geometry.
Description of drawings
In order further to understand purpose of the present invention, with reference to the subsequent detailed description of the present invention that will read in conjunction with the accompanying drawings, wherein:
Fig. 1 is the schematic diagram according to the parallel flow heat exchanger of prior art;
Fig. 2 is the local Zoom Side cross sectional view that shows the parallel flow heat exchanger of one embodiment of the invention;
Fig. 3 a is the view that shows Fig. 2 of the second embodiment of the present invention;
Fig. 3 b is the view that shows Fig. 2 of the third embodiment of the present invention;
Fig. 3 c is the view that shows Fig. 2 of the fourth embodiment of the present invention;
Fig. 3 d is the view that shows Fig. 2 of the fifth embodiment of the present invention;
Fig. 4 is the end-view of shrinkage passage not;
Fig. 5 is the view that is crimped to the Fig. 4 behind the predetermined structure;
Fig. 6 is the view that is crimped to Fig. 4 of second structure;
Fig. 7 is second end-view of shrinkage passage not;
Fig. 8 is the view that is crimped to Fig. 7 of predetermined structure.
The specific embodiment
Referring now to 1, shown parallel type (small size tunnel or minitype channel) heat exchanger 10, it comprises inlet header or manifold 12, outlet header or manifold 14 and with a plurality of passages that be arranged 16 of inlet manifold 12 fluid interconnections to outlet manifold 14.Usually, inlet header and outlet header 12 and 14 are cylindricality in shape, and passage 16 is the pipe (or extrusion) of flat or circular cross-section.Passage 16 has a plurality of inside and external heat transfer enhancement elements usually, for example blade (fin).For example, evenly be arranged on therebetween so that the normally furnace brazing of the outer foil 18 that strengthens heat exchanging process and structural rigidity.Passage 16 can have also that internal heat transfer strengthens and structural detail (referring to Fig. 4-Fig. 6).
During operation, cold-producing medium flows into inlet opening 20 and enters the inner chamber 22 of inlet header 12.From inner chamber 22, the cold-producing medium admission passage opening 24 of liquid, steam or liquid and vapour mixture form (in the most typical situation that has under the evaporimeter situation of the expansion gear that is positioned at the upstream) is so that arrive the inner chamber 26 of outlet header 14 by passage 16.Thus, under the evaporator application situation, this moment, normally the cold-producing medium of vapor form flowed out exit opening 28 and the compressor reducer that arrives soon after (not shown).In passage 16 outsides, air is preferably by air moving device, fan (not shown) for example, and evenly circulation above passage 16 and associated vanes 18, making occurs conducting heat between the air of passage flows outside and the cold-producing medium in the passage interacts.
As shown in Figure 2, according to one embodiment of present invention, passage 16 at least in inlet end 30 shrinkages so that restriction is provided and guarantees that directly the cold-producing medium at each channel entrance place expands at each passage, cold-producing medium expand cause the pressure drop at restriction two ends and reduce and/or eliminates be separated and system in the cold-producing medium distribution improper.
Shown in Fig. 3 a, in the second embodiment of the present invention, passage is in extreme portion 32 and in the point 34 places shrinkage away from the attachment point certain distance of end and manifold 12.
Shown in Fig. 3 b, in the 3rd embodiment, passage is at distance channel end preset distance and once more away from the single position 36 places shrinkage of manifold 12 attachment points, so that do not disturb attaching process.
Shown in Fig. 3 c, in the 4th embodiment, passage is shrinkage predetermined length or distance " L " near channel end, changes/reduces but have than Fig. 2, Fig. 3 a and the littler area of section of Fig. 3 b.
Shown in Fig. 3 d, in the fifth embodiment of the present invention, near a plurality of positions 38,40 and 42 shrinkages of passage channel end form the alternately path of pucker ﹠ bloat, but inferior have than Fig. 2, Fig. 3 a and the littler area of section of Fig. 3 b change/reduce.
Fig. 4 has shown the cross section of the non-shrinkage passage 50 with flat pattern and the vertical support member 52 of one.
Fig. 5 has shown and has been crimped to the passage 50 that is applicable to predetermined structure 60 of the present invention.In this case, shrinkage appear at around the support member 52 and support member constant.
Fig. 6 has shown the passage 50 that is crimped to the structure 70 that is equally applicable to the more flattened among the present invention.In this case, shrinkage evenly occurs and support member 52 is changed over difformity and cross section 72.Significantly, can use different support members within the scope of the invention so that passage 16 internal separation are become the refrigerant passage in a plurality of triangles, trapezoidal, circular or other suitable cross section.Under all these situations, support member can change in the shrinkage process or remain unchanged.
Fig. 7 has shown the cross section (not having internal support in this project organization) of the non-shrinkage passage 80 of flat pattern.
Fig. 8 has shown and has been crimped to the passage 80 that is applicable to more flat structure 90 of the present invention.
Equally, have to be noted that shrinkage needs not to be uniform in all passages, but can gradually change to another cross section, for example so that the balance influence cold-producing medium distributes other factors improperly from a passage to another passage or from a channel cross-section.
In addition, have to be noted that shrinkage can also be used for condenser and evaporator application at the channel entrance place of intermediate manifold.For example, if heat exchanger has a plurality of coolant channels, intermediate manifold (between inlet manifold and outlet manifold) is combined in the heat exchanger designs.In intermediate manifold, cold-producing medium flows with two-phase state usually, and this heat converter structure can be by being benefited from the present invention is similar in conjunction with the passage shrinkage at the entrance point that directly is communicated with intermediate manifold.In addition, shrinkage can form at the port of export of passage 16 or along some centre position of passage length, and the uniformity and the pressure drop control and littler to the influence of whole heat exchanger performance of flowed friction only are provided.
Because for application-specific, the cold-producing medium that causes passage distributes improperly various factors generally just can know in the design phase, and the inventor has been found that and introduces their design feature of balance so that eliminate the adverse effect of evaporimeter and whole system performance and potential compressor reducer overflow and damage are practicable.For example, in many cases, generally know that cold-producing medium is so that still how low speed inflow inlet manifold and velocity amplitude influence the distribution improper point at a high speed.Those skilled in the art will recognize that how instruction of the present invention is applied to other system features.
Although reference preferred embodiment shown in the drawings specifically shows and described the present invention, it will be understood by those skilled in the art that under the situation that does not break away from the spirit and scope of the present invention defined by the claims and can carry out various modifications in detail.
Claims (36)
1. a parallel type (small size tunnel and minitype channel) heat exchanger comprises:
The inlet manifold of longitudinal extension, described inlet manifold have and are used to guide fluid to flow to into the inlet opening of described inlet manifold and are used for from a plurality of exit openings of the described fluid stream of described inlet manifold transverse guidance;
Become substantially parallel relation alignment and fluid to be connected to described a plurality of exit opening so that guide a plurality of passages of described fluid stream from described inlet manifold; And
Fluid is connected to described a plurality of passage so that receive the outlet manifold of described fluid stream from it;
At least one of wherein said passage by shrinkage to change the cross section of described passage.
2. parallel flow heat exchanger according to claim 1 is characterized in that: described passage is in its respective end shrinkage.
3. heat exchanger according to claim 2 is characterized in that: described shrinkage end is an inlet end.
4. heat exchanger according to claim 2 is characterized in that: described shrinkage end is an outlet end.
5. heat exchanger according to claim 2 is characterized in that: at least one the direct fluid in described shrinkage end and inlet manifold, outlet manifold or the intermediate manifold is communicated with.
6. parallel flow heat exchanger according to claim 2 is characterized in that: described passage is apart from least one channel end preset distance place's shrinkage.
7. heat exchanger according to claim 1 is characterized in that: described passage is at least one the centre position place's shrinkage along passage length.
8. parallel flow heat exchanger according to claim 1 is characterized in that: at least one in the described passage is in two disconnected position place shrinkages along its length.
9. parallel flow heat exchanger according to claim 1 is characterized in that: described passage is all at least one position shrinkage of its respective end.
10. parallel flow heat exchanger according to claim 8 is characterized in that: described passage is two pre-position shrinkages between its respective end all.
11. structure according to claim 1 is characterized in that: described heat exchanger is an evaporimeter.
12. structure according to claim 1 is characterized in that: described heat exchanger is a condenser.
13. a parallel type (small size tunnel and minitype channel) heat exchanger comprises:
The inlet manifold of longitudinal extension, described inlet manifold have and are used to guide fluid to flow to into the inlet opening of described inlet manifold and are used for from a plurality of exit openings of the described fluid stream of described inlet manifold transverse guidance;
Become the alignment of substantially parallel relation and is connected with described a plurality of exit opening fluids so that a plurality of passages that guide described fluid to flow from described inlet manifold; And
Fluid is connected to described a plurality of passage so that receive the outlet manifold of described fluid stream from it,
Wherein each described passage by shrinkage to change the cross section of described passage.
14. parallel flow heat exchanger according to claim 13 is characterized in that: each described passage is in its respective end shrinkage.
15. heat exchanger according to claim 13 is characterized in that: described shrinkage end is an inlet end.
16. heat exchanger according to claim 13 is characterized in that: described shrinkage end is an outlet end.
17. heat exchanger according to claim 13 is characterized in that: at least one the direct fluid in described shrinkage end and inlet manifold, outlet manifold and the intermediate manifold is communicated with.
18. heat exchanger according to claim 13 is characterized in that: described passage is at least one the centre position place's shrinkage along passage length.
19. parallel flow heat exchanger according to claim 14 is characterized in that: described passage is in the preset distance place shrinkage apart from least one channel end.
20. parallel flow heat exchanger according to claim 13 is characterized in that: at least one of described passage is in two disconnected position place shrinkages along its length.
21. parallel flow heat exchanger according to claim 13 is characterized in that: a plurality of passages in the described passage are at least one position shrinkage of its respective end.
22. parallel flow heat exchanger according to claim 13 is characterized in that: described passage is a plurality of pre-positions shrinkage between its respective end all.
23. heat exchanger according to claim 1 is characterized in that: described shrinkage is along described passage length gradual change.
24. heat exchanger according to claim 13 is characterized in that: described shrinkage is along described passage length gradual change.
25. heat exchanger according to claim 1 is characterized in that: describedly collapse upon gradual change in the described passage.
26. heat exchanger according to claim 13 is characterized in that: describedly collapse upon gradual change in the described passage.
27. heat exchanger according to claim 1 is characterized in that: described shrinkage is limited to the external channel wall.
28. heat exchanger according to claim 13 is characterized in that: described shrinkage is limited to the external channel wall.
29. heat exchanger according to claim 1 is characterized in that: external channel wall and internal support component are revised in described shrinkage.
30. heat exchanger according to claim 13 is characterized in that: external channel wall and internal support are revised in described shrinkage.
31. heat exchanger according to claim 1 is characterized in that: described shrinkage evenly changes described channel cross-section.
32. heat exchanger according to claim 13 is characterized in that: described shrinkage evenly changes described channel cross-section.
33. heat exchanger according to claim 1 is characterized in that: the described channel cross-section of the non-homogeneous change of described shrinkage.
34. heat exchanger according to claim 13 is characterized in that: the described channel cross-section of the non-homogeneous change of described shrinkage.
35. heat exchanger according to claim 1 is characterized in that: described shrinkage produces at least a in the pressure drop control and the control of expanding.
36. heat exchanger according to claim 13 is characterized in that: described shrinkage produces at least a in the pressure drop control and the control of expanding.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US64938305P | 2005-02-02 | 2005-02-02 | |
| US60/649,383 | 2005-02-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101443621A true CN101443621A (en) | 2009-05-27 |
Family
ID=36777703
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2005800475315A Pending CN101443621A (en) | 2005-02-02 | 2005-12-29 | Parallel flow heat exchanger with crimped channel entrance |
Country Status (10)
| Country | Link |
|---|---|
| US (1) | US20080105420A1 (en) |
| EP (1) | EP1859220A4 (en) |
| JP (1) | JP2008533415A (en) |
| KR (1) | KR20070091216A (en) |
| CN (1) | CN101443621A (en) |
| AU (1) | AU2005326710A1 (en) |
| BR (1) | BRPI0519905A2 (en) |
| CA (1) | CA2596364A1 (en) |
| MX (1) | MX2007009248A (en) |
| WO (1) | WO2006083442A2 (en) |
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|---|---|---|---|---|
| CN101738011B (en) * | 2009-12-15 | 2012-11-21 | 清华大学 | Microfine multi-channel heat pump type air-conditioner heat exchanger with automatic liquid distribution structure |
| CN105940281A (en) * | 2014-01-30 | 2016-09-14 | 达纳加拿大公司 | Flow balanced heat exchanger for battery thermal management |
| CN114144628A (en) * | 2019-05-20 | 2022-03-04 | 德累斯顿工业技术大学 | Heat exchanger and cooling method |
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|---|---|---|---|---|
| WO2008064199A1 (en) | 2006-11-22 | 2008-05-29 | Johnson Controls Technology Company | Multichannel evaporator with flow separating manifold |
| KR101518205B1 (en) | 2006-11-22 | 2015-05-08 | 존슨 컨트롤스 테크놀러지 컴퍼니 | Multichannel heat exchanger with dissimilar multichannel tubes |
| US8424551B2 (en) * | 2007-01-30 | 2013-04-23 | Bradley University | Heat transfer apparatus and method |
| WO2009018150A1 (en) | 2007-07-27 | 2009-02-05 | Johnson Controls Technology Company | Multichannel heat exchanger |
| US20090025405A1 (en) | 2007-07-27 | 2009-01-29 | Johnson Controls Technology Company | Economized Vapor Compression Circuit |
| US8327924B2 (en) | 2008-07-03 | 2012-12-11 | Honeywell International Inc. | Heat exchanger fin containing notches |
| US20100006276A1 (en) * | 2008-07-11 | 2010-01-14 | Johnson Controls Technology Company | Multichannel Heat Exchanger |
| US8234881B2 (en) | 2008-08-28 | 2012-08-07 | Johnson Controls Technology Company | Multichannel heat exchanger with dissimilar flow |
| CN102348953B (en) | 2009-03-13 | 2014-08-27 | 开利公司 | Manifold assembly for distributing a fluid to a heat exchanger |
| GB0905870D0 (en) * | 2009-04-03 | 2009-05-20 | Eaton Williams Group Ltd | A rear door heat exchanger |
| DE102009022986A1 (en) * | 2009-05-28 | 2010-12-02 | Behr Gmbh & Co. Kg | Heat exchanger |
| US8439104B2 (en) * | 2009-10-16 | 2013-05-14 | Johnson Controls Technology Company | Multichannel heat exchanger with improved flow distribution |
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- 2005-12-29 EP EP05855808A patent/EP1859220A4/en not_active Withdrawn
- 2005-12-29 KR KR1020077017115A patent/KR20070091216A/en not_active Application Discontinuation
- 2005-12-29 US US11/794,921 patent/US20080105420A1/en not_active Abandoned
- 2005-12-29 CN CNA2005800475315A patent/CN101443621A/en active Pending
- 2005-12-29 CA CA002596364A patent/CA2596364A1/en not_active Abandoned
- 2005-12-29 JP JP2007554086A patent/JP2008533415A/en not_active Withdrawn
- 2005-12-29 WO PCT/US2005/047309 patent/WO2006083442A2/en active Application Filing
- 2005-12-29 BR BRPI0519905-0A patent/BRPI0519905A2/en not_active IP Right Cessation
- 2005-12-29 MX MX2007009248A patent/MX2007009248A/en not_active Application Discontinuation
- 2005-12-29 AU AU2005326710A patent/AU2005326710A1/en not_active Abandoned
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101738011B (en) * | 2009-12-15 | 2012-11-21 | 清华大学 | Microfine multi-channel heat pump type air-conditioner heat exchanger with automatic liquid distribution structure |
| CN105940281A (en) * | 2014-01-30 | 2016-09-14 | 达纳加拿大公司 | Flow balanced heat exchanger for battery thermal management |
| US10180289B2 (en) | 2014-01-30 | 2019-01-15 | Dana Canada Corporation | Flow balanced heat exchanger for battery thermal management |
| CN114144628A (en) * | 2019-05-20 | 2022-03-04 | 德累斯顿工业技术大学 | Heat exchanger and cooling method |
| US11994346B2 (en) | 2019-05-20 | 2024-05-28 | Technische Universitat Dresden | Heat exchanger and cooling method |
Also Published As
| Publication number | Publication date |
|---|---|
| EP1859220A2 (en) | 2007-11-28 |
| MX2007009248A (en) | 2007-09-04 |
| EP1859220A4 (en) | 2010-08-04 |
| KR20070091216A (en) | 2007-09-07 |
| WO2006083442A3 (en) | 2009-04-09 |
| CA2596364A1 (en) | 2006-08-10 |
| JP2008533415A (en) | 2008-08-21 |
| AU2005326710A1 (en) | 2006-08-10 |
| BRPI0519905A2 (en) | 2009-09-08 |
| US20080105420A1 (en) | 2008-05-08 |
| WO2006083442A2 (en) | 2006-08-10 |
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