EP3730891A1 - Heat exchanger for high prandtl number fluids - Google Patents
Heat exchanger for high prandtl number fluids Download PDFInfo
- Publication number
- EP3730891A1 EP3730891A1 EP19212330.5A EP19212330A EP3730891A1 EP 3730891 A1 EP3730891 A1 EP 3730891A1 EP 19212330 A EP19212330 A EP 19212330A EP 3730891 A1 EP3730891 A1 EP 3730891A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluid
- segment
- flow
- heat exchanger
- channel
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000012530 fluid Substances 0.000 title claims abstract description 76
- 238000000034 method Methods 0.000 claims description 16
- 230000007423 decrease Effects 0.000 claims description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 230000003416 augmentation Effects 0.000 description 1
- 230000003190 augmentative effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
- F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
- F28F3/025—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being corrugated, plate-like elements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
- F28F13/12—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media by creating turbulence, e.g. by stirring, by increasing the force of circulation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/02—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by influencing fluid boundary
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
- F28F13/08—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media by varying the cross-section of the flow channels
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
- F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
- F28F3/04—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element
- F28F3/048—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element in the form of ribs integral with the element or local variations in thickness of the element, e.g. grooves, microchannels
-
- 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
- F28D2021/0098—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for viscous or semi-liquid materials, e.g. for processing sludge
Definitions
- the present disclosure relates to a heat exchanger, and more particularly to a heat exchanger for a high Prandtl number fluid.
- a fluid heat exchanger includes a channel for passing a first fluid therethrough arranged along a primary axis including at least two segments of a first flow pattern, wherein at least one segment of the at least two segments defines a length greater than five times a hydraulic diameter of the channel, and a first pattern flow disruptor interspersed between each of the segments of the first flow pattern configured to reduce a pressure loss of the fluid flow along the channel, and a second series of channels for passing a second fluid therethrough for transferring energy to the first fluid.
- a first segment of the at least two segments can define a length different from a length of a second segment of the at least two segments.
- the length of the first segment can be defined by the equation 5 D h ⁇ L ⁇ 4D h P r wherein L is the length of the first segment, D h is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment.
- the length of the second segment can be defined by the equation 5 D h ⁇ L ⁇ 4 D h Pr wherein L is the length of the second segment, D h is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment.
- the segments of the first flow pattern can be aligned in the same direction.
- the segments of the first flow pattern can be straight.
- the first pattern flow disruptor can narrow the flow channel.
- the first pattern flow disruptor can change a direction of flow of the first fluid.
- the first pattern flow disruptor can include multiple disruptors, wherein at least one of the flow disruptors includes a longer length than another disruptor.
- a method of transferring heat between fluids includes directing a fluid through a heat exchanger channel and developing a thermal boundary layer between the fluid and a surface of the channel and a momentum boundary layer between the fluid and the surface of the channel, wherein the thermal boundary layer of the fluid includes a different thickness than a thickness of the momentum boundary layer, and directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid.
- the fluid includes a Pradntl number greater than 1, or preferably a Prandtl number greater than 7.
- the thermal boundary layer of the fluid is thinner than the momentum boundary layer.
- a ratio of thermal boundary thickness to momentum boundary layer thickness can decrease along a flow direction of the fluid and the ratio of thermal boundary thickness to momentum boundary layer thickness can be greater than 1.
- FIG. 1 a partial view of an exemplary embodiment of a heat exchanger channel in accordance with the invention is shown in Fig. 1 and is designated generally by reference character 100.
- the methods and systems of the invention can be used to improve heat transfer using fluids with a high Prandtl number.
- the heat exchanger 100 includes a hot fluid inlet 102, a cold fluid inlet 104, and a header 106.
- the disclosure focuses on the structure of the individual channels for the hot fluid and the cold fluid.
- a channel 108 for passing a first fluid therethrough is arranged along a primary axis 110 including at least two segments 112, 114 of a first flow pattern.
- a first segment 112 defines a length L1 that may be different from a length L2 of a second segment 114, and a first pattern flow disruptor 116 is interspersed between each of the segments of the first flow pattern to enhance heat transfer of the fluid flow along the channel 108.
- the channel 108 can include multiple segments of the first flow pattern, and multiple disruptors 116.
- the length of the first segment L1 is defined by the equation 5 D h ⁇ L1 ⁇ 4D h Pr wherein L1 is the length of the first segment, D h is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment 112, and the length of the second segment is defined by the equation 5 D h ⁇ L2 ⁇ 4D h Pr wherein L2 is the length of the second segment, D h is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment 114.
- the Prandtl number can be calculated at the midpoint of each segment.
- Prandtl number is a dimensionless number defined as the ratio of momentum diffusivity to thermal diffusivity.
- momentum diffusion rate is dependent of the dynamic viscosity and density of the fluid along a heat exchange channel
- thermal diffusivity is dependent of the thermal conductivity and density of the fluid, which again varies along the flow path.
- the segments 112, 114 of the first flow pattern are aligned in the same direction.
- the segments 112, 114 of the first flow pattern can be straight.
- the flow disruptor 116 can be a sinusoidal path attached to the straight first flow pattern.
- the flow disruptor 116 can be straight flow and set-off from the first flow pattern.
- the first pattern flow disruptor 116 can narrow the flow channel or change a direction of flow of the first fluid.
- the first pattern flow disruptor 116 can include multiple disruptors between each of the first flow pattern portions 112, 114.
- the disruptors can be of various shapes and sizes.
- the disruptors can include various lengths along the same path, which can be beneficial for channels for larger changes in Pr.
- a method of transferring heat between fluids using a heat exchanger includes directing a first fluid through a heat exchanger channel and developing a thermal boundary layer between the first fluid and a surface of the channel and a momentum boundary layer between the first fluid and the surface of the channel, wherein the thermal boundary layer of the first fluid includes a different thickness than a thickness of the momentum boundary layer.
- the first fluid includes a Pradntl number greater than 1, or more specifically a Prandtl number greater than 7.
- the thermal boundary layer of the first fluid is thinner than the momentum boundary layer.
- a ratio of thermal boundary thickness to momentum boundary layer thickness decreases along with the flow of the fluid and the ratio is always greater than 1.
- the method described above is leveraged to augment heat transfer while reducing pressure drop penalty by intermittently disturbing the flow at desired intervals, where the momentum profile is allowed to recover while the thermal profile remains augmented.
- the flow through the first segement (L1) result in lower pressure drop with little degradation to the enhancement in heat transfer caused by the disruptor.
- the optimal length the disruptors can be selected based on expected steady state conditions and fluid properties. The implementation of this method has shown an improvement of approximately 30% more heat transfer with respect to conventional methods, while keeping the pressure drop penalty unchanged.
Abstract
Description
- The present disclosure relates to a heat exchanger, and more particularly to a heat exchanger for a high Prandtl number fluid.
- A variety of devices are known in the heat exchanger area. However High-Viscosity/Prandtl-number fluids such as oils or glycol solutions result in poor heat transfer and high pressure drop. Surface augmentations are often used to enhance heat transfer; however, result in even higher pressure drop.
- The conventional methods and systems have generally been considered satisfactory for their intended purpose. However, there is still a need in the art for heat exchanger having improved heat transfer capabilities. There also remains a need in the art for such heat exchangers and components that are economically viable. The present disclosure may provide a solution for at least one of these remaining challenges.
- A fluid heat exchanger includes a channel for passing a first fluid therethrough arranged along a primary axis including at least two segments of a first flow pattern, wherein at least one segment of the at least two segments defines a length greater than five times a hydraulic diameter of the channel, and a first pattern flow disruptor interspersed between each of the segments of the first flow pattern configured to reduce a pressure loss of the fluid flow along the channel, and a second series of channels for passing a second fluid therethrough for transferring energy to the first fluid. A first segment of the at least two segments can define a length different from a length of a second segment of the at least two segments. The length of the first segment can be defined by the equation 5Dh < L < 4DhPr wherein L is the length of the first segment, Dh is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment. The length of the second segment can be defined by the equation 5Dh < L < 4DhPr wherein L is the length of the second segment, Dh is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment.
- The segments of the first flow pattern can be aligned in the same direction. The segments of the first flow pattern can be straight. The first pattern flow disruptor can narrow the flow channel. The first pattern flow disruptor can change a direction of flow of the first fluid. The first pattern flow disruptor can include multiple disruptors, wherein at least one of the flow disruptors includes a longer length than another disruptor.
- A method of transferring heat between fluids includes directing a fluid through a heat exchanger channel and developing a thermal boundary layer between the fluid and a surface of the channel and a momentum boundary layer between the fluid and the surface of the channel, wherein the thermal boundary layer of the fluid includes a different thickness than a thickness of the momentum boundary layer, and directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid.
- The fluid includes a Pradntl number greater than 1, or preferably a Prandtl number greater than 7. The thermal boundary layer of the fluid is thinner than the momentum boundary layer. A ratio of thermal boundary thickness to momentum boundary layer thickness can decrease along a flow direction of the fluid and the ratio of thermal boundary thickness to momentum boundary layer thickness can be greater than 1.
- These and other features of the systems and methods of the subject disclosure will become more readily apparent to those skilled in the art from the following detailed description of the preferred embodiments taken in conjunction with the drawings.
- So that those skilled in the art to which the subject invention appertains will readily understand how to make and use the devices and methods of the subject invention without undue experimentation, preferred embodiments thereof will be described in detail herein below with reference to certain figures, wherein:
-
Fig. 1 is a perspective view of a heat exchanger; -
Fig. 2 is a perspective view of a heat exchanger plane ofFig. 1 , showing a channel for transporting a fluid; -
Fig. 3 is a perspective view of an alternate embodiment ofFig. 1 , showing a second type of flow disruptor; and -
Fig. 4 is a perspective view of an alternate embodiment ofFig. 1 , showing a third type of flow disruptor. - Reference will now be made to the drawings wherein like reference numerals identify similar structural features or aspects of the subject invention. For purposes of explanation and illustration, and not limitation, a partial view of an exemplary embodiment of a heat exchanger channel in accordance with the invention is shown in
Fig. 1 and is designated generally byreference character 100. Other embodiments of heat exchanger channel in accordance with the invention, or aspects thereof, are provided inFigs. 2-4 , as will be described. The methods and systems of the invention can be used to improve heat transfer using fluids with a high Prandtl number. - Referring to
Fig. 1 , aheat exchanger 100 having multiple channels for passing fluids therethough is shown. Theheat exchanger 100 includes ahot fluid inlet 102, acold fluid inlet 104, and aheader 106. The disclosure focuses on the structure of the individual channels for the hot fluid and the cold fluid. - Referring to
Figs. 2-4 , achannel 108 for passing a first fluid therethrough is arranged along aprimary axis 110 including at least twosegments first segment 112 defines a length L1 that may be different from a length L2 of asecond segment 114, and a firstpattern flow disruptor 116 is interspersed between each of the segments of the first flow pattern to enhance heat transfer of the fluid flow along thechannel 108. Thechannel 108 can include multiple segments of the first flow pattern, andmultiple disruptors 116. The length of the first segment L1 is defined by the equation 5Dh < L1 < 4DhPr wherein L1 is the length of the first segment, Dh is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along thefirst segment 112, and the length of the second segment is defined by the equation 5Dh < L2 < 4DhPr wherein L2 is the length of the second segment, Dh is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along thesecond segment 114. The Prandtl number can be calculated at the midpoint of each segment. However, an average Prandtl number can be used, as the number is not expected to vary substantially within each segment. The Prandtl number is a dimensionless number defined as the ratio of momentum diffusivity to thermal diffusivity. Wherein the momentum diffusion rate is dependent of the dynamic viscosity and density of the fluid along a heat exchange channel, and the thermal diffusivity is dependent of the thermal conductivity and density of the fluid, which again varies along the flow path. Using an expected steady state Prandtl number of fluid flowing through a heat exchanger, the heat exchanger channel is sized accordingly. - The
segments segments Fig. 2 , theflow disruptor 116 can be a sinusoidal path attached to the straight first flow pattern. As shown inFig. 3 , theflow disruptor 116 can be straight flow and set-off from the first flow pattern. As shown inFig. 4 , the firstpattern flow disruptor 116 can narrow the flow channel or change a direction of flow of the first fluid. It is further contemplated that the firstpattern flow disruptor 116 can include multiple disruptors between each of the firstflow pattern portions - A method of transferring heat between fluids using a heat exchanger is also disclosed. The method includes directing a first fluid through a heat exchanger channel and developing a thermal boundary layer between the first fluid and a surface of the channel and a momentum boundary layer between the first fluid and the surface of the channel, wherein the thermal boundary layer of the first fluid includes a different thickness than a thickness of the momentum boundary layer. Directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid. The first fluid includes a Pradntl number greater than 1, or more specifically a Prandtl number greater than 7.
- For fluids with a Prandtl number above 1, the thermal boundary layer of the first fluid is thinner than the momentum boundary layer. A ratio of thermal boundary thickness to momentum boundary layer thickness decreases along with the flow of the fluid and the ratio is always greater than 1.
- The method described above is leveraged to augment heat transfer while reducing pressure drop penalty by intermittently disturbing the flow at desired intervals, where the momentum profile is allowed to recover while the thermal profile remains augmented. For fluids having a high Prandtl number the flow through the first segement (L1) result in lower pressure drop with little degradation to the enhancement in heat transfer caused by the disruptor. The optimal length the disruptors can be selected based on expected steady state conditions and fluid properties. The implementation of this method has shown an improvement of approximately 30% more heat transfer with respect to conventional methods, while keeping the pressure drop penalty unchanged.
- The methods and systems of the present disclosure, as described above and shown in the drawings, provide for a heat exchanger with superior properties heat transfer. While the apparatus and methods of the subject disclosure have been showing and described with reference to embodiments, those skilled in the art will readily appreciate that changes and/or modifications may be made thereto without departing from the scope of the subject disclosure.
Claims (15)
- A fluid heat exchanger comprising:a channel (108) for passing a first fluid therethrough arranged along a primary axis including at least two segments of a first flow pattern, wherein a length of at least one segment being set in relation to a hydraulic diameter and a Prandtl number of the first fluid; anda first pattern flow disruptor (116) interspersed between each of the segments of the first flow pattern configured to reduce a pressure loss of the fluid flow along the channel.
- The heat exchanger of claim 1, wherein at least one segment of the at least two segments defines a length greater than five times a hydraulic diameter of the channel.
- The heat exchanger of claims 1 or 2, wherein a first segment of the at least two segments defines a length different from a length of a second segment of the at least two segments.
- The heat exchanger of claim 3, wherein the length of the first segment is defined by the equation 5Dh < L < 4DhPr wherein L is the length of the first segment, Dh is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment; and/or wherein the length of the second segment is defined by the equation 5Dh < L < 4DhPr wherein L is the length of the second segment, Dh is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment.
- The heat exchanger of any preceding claim, wherein the segments of the first flow pattern are aligned in the same direction, and/or wherein the segments of the first flow pattern are straight.
- The heat exchanger of claim 1, wherein the first pattern flow disruptor narrows the flow channel.
- The heat exchanger of any preceding claim, wherein the first pattern flow disruptor changes a direction of flow of the first fluid.
- The heat exchanger of any preceding claim, wherein the first pattern flow disruptor includes multiple disruptors, and preferably wherein at least one of the flow disruptors includes a longer length than another disruptor.
- The heat exchanger of any preceding claim, further comprising a second series of channels for passing a second fluid therethrough for transferring energy to the first fluid.
- A method of transferring heat between fluids comprising:directing a fluid through a heat exchanger channel; anddeveloping a thermal boundary layer between the fluid and a surface of the channel and a momentum boundary layer between the fluid and the surface of the channel, wherein the thermal boundary layer of the fluid includes a different thickness than a thickness of the momentum boundary layer.
- The method of claim 10, wherein the fluid includes a Pradntl number greater than 1.
- The method of claims 10 or 11, wherein the fluid includes a Prandtl number greater than 7.
- The method of any of claims 10 to 12, wherein the thermal boundary layer of the fluid is thinner than the momentum boundary layer.
- The method of any of claims 10 to 13, wherein a ratio of thermal boundary thickness to momentum boundary layer thickness decreases along a flow direction of the fluid, and preferably wherein the ratio of thermal boundary thickness to momentum boundary layer thickness is greater than 1.
- The method of any of claims 10 to 14, further comprising directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US16/396,124 US20200340765A1 (en) | 2019-04-26 | 2019-04-26 | Heat exchanger for high prandtl number fluids |
Publications (1)
Publication Number | Publication Date |
---|---|
EP3730891A1 true EP3730891A1 (en) | 2020-10-28 |
Family
ID=68732784
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19212330.5A Withdrawn EP3730891A1 (en) | 2019-04-26 | 2019-11-28 | Heat exchanger for high prandtl number fluids |
Country Status (2)
Country | Link |
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US (1) | US20200340765A1 (en) |
EP (1) | EP3730891A1 (en) |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3111982A (en) * | 1958-05-24 | 1963-11-26 | Gutehoffnungshuette Sterkrade | Corrugated heat exchange structures |
DE3521914A1 (en) * | 1984-06-20 | 1986-01-02 | Showa Aluminum Corp., Sakai, Osaka | HEAT EXCHANGER IN WING PANEL DESIGN |
CA2290230A1 (en) * | 1998-11-20 | 2000-05-20 | Eberhard Paul | Heat transfer plate and method of producing heat transfer plates |
US20160327346A1 (en) * | 2015-05-06 | 2016-11-10 | Halla Visteon Climate Control Corp. | Heat exchanger with mechanically offset tubes and method of manufacturing |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4230179A (en) * | 1979-07-09 | 1980-10-28 | Haruo Uehara | Plate type condensers |
FR2695326B1 (en) * | 1992-09-08 | 1994-12-02 | Strasbourg Ecole Nale Sup Arts | Metallic matrix of catalytic reactor for the treatment of combustion gases. |
EP0869844B1 (en) * | 1995-12-13 | 2002-03-20 | Kemira Metalkat Oy | Turbulence inducer in chemical reactor |
DE19922356C2 (en) * | 1999-05-14 | 2001-06-13 | Helmut Swars | Honeycomb body |
KR101534497B1 (en) * | 2013-10-17 | 2015-07-09 | 한국원자력연구원 | Heat exchanger for steam generator and steam generator having the same |
-
2019
- 2019-04-26 US US16/396,124 patent/US20200340765A1/en not_active Abandoned
- 2019-11-28 EP EP19212330.5A patent/EP3730891A1/en not_active Withdrawn
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3111982A (en) * | 1958-05-24 | 1963-11-26 | Gutehoffnungshuette Sterkrade | Corrugated heat exchange structures |
DE3521914A1 (en) * | 1984-06-20 | 1986-01-02 | Showa Aluminum Corp., Sakai, Osaka | HEAT EXCHANGER IN WING PANEL DESIGN |
CA2290230A1 (en) * | 1998-11-20 | 2000-05-20 | Eberhard Paul | Heat transfer plate and method of producing heat transfer plates |
US20160327346A1 (en) * | 2015-05-06 | 2016-11-10 | Halla Visteon Climate Control Corp. | Heat exchanger with mechanically offset tubes and method of manufacturing |
Also Published As
Publication number | Publication date |
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US20200340765A1 (en) | 2020-10-29 |
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