EP0802383A2 - Echangeur de chaleur multitubulaire avec disposition particulière des tubes - Google Patents

Echangeur de chaleur multitubulaire avec disposition particulière des tubes Download PDF

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Publication number
EP0802383A2
EP0802383A2 EP97302586A EP97302586A EP0802383A2 EP 0802383 A2 EP0802383 A2 EP 0802383A2 EP 97302586 A EP97302586 A EP 97302586A EP 97302586 A EP97302586 A EP 97302586A EP 0802383 A2 EP0802383 A2 EP 0802383A2
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EP
European Patent Office
Prior art keywords
microtubes
heat exchanger
heat exchange
exchange medium
multitubular
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Withdrawn
Application number
EP97302586A
Other languages
German (de)
English (en)
Other versions
EP0802383A3 (fr
Inventor
Tomohiro Yamaguchi
Tomonari Morita
Kenichi Sasaki
Masataka Tsunoda
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sanden Corp
Original Assignee
Sanden Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sanden Corp filed Critical Sanden Corp
Publication of EP0802383A2 publication Critical patent/EP0802383A2/fr
Publication of EP0802383A3 publication Critical patent/EP0802383A3/fr
Withdrawn legal-status Critical Current

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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
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/04—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by preventing the formation of continuous films of condensate on heat-exchange surfaces, e.g. by promoting droplet formation
    • 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
    • F28D1/05316—Assemblies of conduits connected to common headers, e.g. core type radiators
    • F28D1/05341—Assemblies of conduits connected to common headers, e.g. core type radiators with multiple rows of conduits or with multi-channel conduits combined with a particular flow pattern, e.g. multi-row multi-stage radiators
    • 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
    • F25B39/02—Evaporators
    • 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

Definitions

  • This invention relates to a heat exchanger for use in an air-conditioner and, in particular, to a multitubular or shell-and-tube heat exchanger comprising a tube bundle array.
  • a general heat exchanger for use in an air conditioner is required to have a low draft resistance (pressure loss) and a high heat transfer power (cooling capacity or heat radiation capacity).
  • the outside heat transfer coefficient and the ventilating resistance are related to a tube arrangement pattern and an air velocity.
  • a multitubular heat exchanger of the type is disclosed in Japanese Unexamined Patent Publication (JP-A) No. 190287/1986 corresponding to United States Patent No. 4,676,305.
  • the heat exchanger comprises a plurality of heat exchange modules each of which contains an array of a plurality of microtubes (may simply be referred to as tubes) arranged in parallel to one another and a shell surrounding the tubes. Each tube has an outside diameter not greater than 3mm.
  • the heat exchange module is of a so-called counterflow type. Specifically, an outer fluid outside of the tubes flows within the shell in one direction parallel to an axial direction of each tube while an inner fluid inside of the tubes flows in a reverse direction reverse to the one direction.
  • the tubes are arranged in a staggered pattern. Specifically, the tubes have a hexagonal-close-pack pattern with an angle of 60°.
  • the row distance between rows of the tubes is equal to 0.866 times the tube center distance (TC) between tube centers.
  • the tube center distance (TC) is generally equal to 1.3 to 2.8 times the outside diameter of the tubes.
  • a multitubular heat exchanger to which this invention is applicable is for carrying out heat exchange between a first heat exchange medium flowing substantially in a first direction and a second heat exchange medium flowing in a second direction intersecting the first direction.
  • the heat exchanger comprises a plurality of microtubes each guiding the second heat exchange medium in the second direction.
  • the microtubes are staggered to have a pitch X in the first direction and aligned to have a pitch Y in a third direction perpendicular to the first and the second directions.
  • Each of the microtubes has an outer diameter not greater than 3mm.
  • Each of the microtubes containes, as the second heat exchange medium, a refrigerant which is evaporated within each of the microtubes to make water be condensed as condensed water on an outer peripheral surface of each of the microtubes.
  • the second direction is the vertical direction. The condensed water flows downward along the outer peripheral surface of each of the microtubes.
  • the heat exchanger comprises a plurality of microtubes each having an outer diameter D and guiding the second heat exchange medium in the second direction.
  • the microtubes are staggered to have a pitch X in the first direction and aligned to have a pitch Y in a third direction perpendicular to the first and the second directions.
  • the pitch X satisfies the relationship expressed by: 1 .12 ⁇ X/D ⁇ 1.8.
  • the heat exchanger comprises a plurality of microtubes each having an outer diameter D and guiding the second heat exchange medium in the second direction.
  • the microtubes are staggered to have a pitch X in the first direction and aligned to have a pitch Y in a third direction perpendicular to the first and the second directions.
  • the pitch Y satisfies the relationship expressed by: 1.8 ⁇ Y/D ⁇ 2.4.
  • a multitubular heat exchanger is a multitubular evaporator.
  • the evaporator comprises a large number of microtubes 1 each having an outer diameter not greater than 3.0mm.
  • Each of the microtubes 1 has opposite ends bonded by brazing to upper and lower tanks 2 and 3 so as to allow fluid communication between the microtubes 1 and the upper and the lower tanks 2 and 3.
  • the microtubes 1 may collectively be called a tube bundle.
  • the upper tank 2 is connected to an inlet tube 4 and an outlet tube 5.
  • the upper tank 2 is provided with partition plates 7 and 8 partitioning an internal space of the upper tank 2, as depicted by dotted lines in the figure.
  • the lower tank 3 is provided with similar partition plates 7' and 8'.
  • Each of the upper and the lower tanks 2 and 3 is thus divided into four chambers.
  • the partition plate 8 in the upper tank 2 is partially provided with communication holes to allow fluid communication between the rear-side two chambers.
  • the partition plate 7' in the lower tank 3 is provided with communication holes to allow fluid communication between the right-side two chambers and between the left-side two chambers.
  • a pair of side plates 6 are attached to both lateral sides of the evaporator. Furthermore, a horizontal center plate 10 is fixed to the side plates 6 to support the tube bundle.
  • a refrigerant flows through the inlet tube 4 into the upper tank 2, travels through a refrigerant path formed by the microtubes 1 and the upper and the lower tanks 2 and 3, and flows out from the upper tank 2 through the outlet tube 5, as depicted at thick solid lines with arrowheads.
  • the refrigerant path comprises four parts, namely, a front-side downward path, a rear-side upward path, a rear-side downward path, and a front-side upward path.
  • the partition plates in the upper and the lower tanks 2 and 3 serve as an inner fluid guiding arrangement to define the above-mentioned four-part refrigerant path.
  • a first heat exchange medium As an outer fluid or a first heat exchange medium, air flows into the evaporator from a front side thereof in a first direction depicted by a white arrow in the figure, namely, in the horizontal direction.
  • the first heat exchange medium flows through a space in the tube bundle in the first direction which may be referred to as the airstream direction.
  • a combination of the upper and the lower tanks 2 and 3, the side plates 6, and the center plate 10 serves as a guiding arrangement for guiding the first heat exchange medium in the first direction.
  • each microtube extends in a second direction intersecting or perpendicular to the first direction, namely, in the vertical direction.
  • the refrigerant flows upward or downward as a second heat exchange medium within the microtubes 1 for heat exchange with the first heat exchange medium.
  • the illustrated multitubular evaporator is a multitubular heat exchanger of an orthogonal flow type.
  • a multitubular heat exchanger is also a multitubular evaporator.
  • the evaporator comprises a large number of microtubes 1 each having an outer diameter not greater than 3.0mm.
  • Each of the microtubes 1 has opposite ends bonded by brazing to upper and lower tanks 11 and 12 so as to allow fluid communication between the microtubes 1 and the upper and the lower tanks 11 and 12.
  • the upper tank 11 is connected to an inlet tube 16 and an outlet tube 17.
  • the upper tank 11 is provided with partition plates 13, 14, and 15 partitioning an internal space of the upper tank 11, as depicted by dotted lines in the figure.
  • the lower tank 12 is provided with similar partition plates 13', 14', and 15'.
  • Each of the upper and the lower tanks 11 and 12 is thus divided into six chambers.
  • the partition plate 15 in the upper tank 11 is provided with communication holes to allow fluid communication between the rear-side center and left chambers and between the front-side left and center chambers.
  • the partition plates 13' and 14' in the lower tank 12 are provided with communication holes to allow fluid communication between the rear-side right and center chambers, between the left-side two chambers, between the front-side center and right chambers, and between the rear-side center and right chambers.
  • a pair of side plates 6 are attached to both lateral sides of the evaporator. Furthermore, a horizontal center plate 10 is fixed to the side plates 6 to support the tube bundle.
  • a refrigerant flows through the inlet tube 16 into the upper tank 11, travels through a refrigerant path formed by the microtubes 1 and the upper and the lower tanks 11 and 12, and flows out from the upper tank 11 through the outlet tube 17, as depicted at thick solid lines with arrowheads.
  • the refrigerant path comprises six parts, namely, a rear-side right downward path, a rear-side center upward path, a rear-side left downward path, a front-side left upward path, a front-side center downward path, and a front-side right upward path.
  • the partition plates in the upper and the lower tanks 11 and 12 serve as an inner fluid guiding arrangement to define the above-mentioned six-part refrigerant path.
  • a combination of the upper and the lower tanks 11 and 12, the side plates 6, and the center plate 10 serves as a guiding arrangement for guiding the first heat exchange medium in the first direction.
  • the microtubes 1 of the tube bundle are arranged in a staggered pattern, which will hereafter be described, so as to obtain an optimum ratio of an overall heat transfer coefficient to a ventilating resistance.
  • measurement has been made of the overall heat transfer coefficient and the ventilating resistance of the tube bundle for various arrangement pitches.
  • FIG. 3 description will be made about an arrangement of the microtubes 1 in each of the multitubular evaporators shown in Figs. 1 and 2.
  • the first direction along which the outer fluid or the first heat exchange medium flows is depicted by a white arrow.
  • the second direction along which the inner fluid or the second heat exchange medium flows is perpendicular to a drawing sheet.
  • a third direction is perpendicular to the first and the second directions.
  • Each of the microtubes 1 has an outer diameter D.
  • the microtubes 1 are staggered or offset in each of the first and the second directions. In other words, the microtubes 1 are staggered to have a pitch X in the first direction while they are aligned to have a pitch Y in the third direction.
  • the microtubes 1 are classified into three groups, namely, first microtubes la, second microtubes 1b adjacent to the first microtubes la in the third direction, and third microtubes 1c adjacent to the first and the second microtubes 1a and 1b in a fourth direction obliquely intersecting the first and the third directions.
  • a plurality of samples of heat exchangers were manufactured with the structure illustrated in Fig. 1 or 2. These samples had different arrangement patterns with different X/D and Y/D ratios of the pitches X and Y to the outer diameter D of the microtubes.
  • a test apparatus use was made of a cyclometric calorimeter including a refrigerant circuit using fluorocarbon as a refrigerant. Each sample was used as an evaporator in the refrigerant circuit.
  • test conditions were as follows:
  • An air volume (outlet air volume) passing through the evaporator was controlled to several predetermined air volumes between 300 and 450 m 3 /h. Then, measurement was made of a cooling capacity and a ventilating resistance of the evaporator.
  • An air velocity in each sample for these air volumes is about 6 to 7m/s or less in terms of a peak velocity, namely, a velocity during passage through a minimum spacing or gap between adjacent tubes.
  • a Reynolds number Re max is not greater than 1200 for the peak velocity and the tube diameter of a characteristic size.
  • a heat transfer characteristic of the tube bundle is represented as the overall heat transfer coefficient based on enthalpy difference.
  • K i Q/(A ⁇ dI), where K i represents the overall heat transfer coefficient based on enthalpy difference, A, the outside total heating surface area, and dI, the logarithmic mean enthalpy difference.
  • dI [(Ia1 - Ia2)] /In[Ia1 - Ir) - (Ia2 - Ir)], where Ir represents the enthalpy of saturated air corresponding to the refrigerant saturation temperature at the mean evaporator pressure.
  • the heat exchanger efficiency of the evaporator is defined as a ratio (K i /f) of the overall heat transfer coefficient based on enthalpy difference to the pressure loss.
  • Fig. 4 schematically shows the arrangement of the tube bundle in the multitubular evaporators shown in Fig. 1. Gaps are present between lateral sides of the tube bundle and the side plates 6. In addition, another gap is present at the center of the tube bundle in correspondence to the partition plate within the tank described above. These gaps may possibly form bypassing paths of the airstream. In order to more accurately measure the ventilating resistance and the overall heat transfer coefficient of the tube bundle, such unexpected bypassing of the airstream in the tube bundle must be inhibited. For this purpose, sealing members 21, 22, and 23 are fitted in these gaps, as illustrated in Fig. 4.
  • Fig. 5 shows the K i/ f ratio as the heat exchanger efficiency with respect to the X/D ratio.
  • the minimum X/D ratio is equal to 1.04, in which case the portion b in Fig. 3 gives a minimum path sectional area corresponding to the above-mentioned minimum spacing or gap.
  • the second minimum X/D ratio is equal to 1.12, in which case the portions a and b have the same size.
  • the minimum path sectional area is given by the portion a.
  • the relationship between the K i /f ratio and the air velocity is shown in Fig. 5 for all of the samples.
  • the air velocity is calculated from a predetermined air volume and the path sectional area based on the portion a.
  • the number of rows of tubes in the first direction is equal to 12 in the 3-mm diameter samples.
  • the four kinds of 2.2mm-diameter samples have the constant Y/D ratio of 1.82 and the different X/D ratios.
  • the number of rows of tubes is equal to 11.
  • the K i /f ratio slightly increases with an increase of the X/D ratio until it is saturated at the X/D ratio of about 1.6.
  • the condensed water forms a water film on the surface of each tube.
  • the heat exchanger is made compact by reducing the X/D ratio, the X/D ratio must be selected to be an optimum value such that the above-mentioned disadvantages are avoided.
  • the K i /f ratio shows the gradient substantially equal to that of the 3mm-diameter samples. It is noted here that, with the decrease in air velocity, the saturation tendency is slightly suppressed in the 2.2mm-diameter samples as compared with the 3mm-diameter samples.
  • the X/D ratio must be equal to 1.12 or more, preferably, 1.2 or more in order to obtain the effective value of the heat exchange efficiency, namely, the ratio (K i /f) of the overall heat transfer coefficient based on enthalpy difference to the pressure loss.
  • the increase in X/D ratio results in a disadvantage that the tube bundle array is greater in size in the first or the airstream direction. Accordingly, taking the saturation of the K i /f ratio into consideration, the X/D ratio must have an upper limit value on the order of 1.8, preferably, 1.7.
  • Fig. 6 shows the K i /f ratio as the heat exchanger efficiency with respect to the Y/D ratio.
  • the six kinds of 3mm-diameter samples have the constant X/D ratio of 1.33 and the different Y/D ratios.
  • the three kinds of 2.2mm-diameter samples have the constant X/D value of 1.27 and the different Y/D ratios.
  • the K i /f ratio tends to increase for each air velocity until the Y/D ratio reaches 2.2. Beyond the value, the K i /f ratio is saturated.
  • the K i /f ratio exhibits the gradient substantially equal to that of the 3mm-diameter samples. It is noted here that the K i /f ratios in the 2.2mm-diameter samples are slightly lower than those in the 3mm-diameter samples. The reason will presently be described in conjunction with a specific example. As described in the foregoing, the 3mm-diameter samples and the 2.2mm-diameter samples have the X/D ratios of 1.33 and 1.27, respectively, in Fig. 6.
  • the difference in K i /f ratio resulting from the above-mentioned difference in X/D ratio is about 3% as seen from the gradient at the air velocity of 4m/s in Fig. 6 for example.
  • the K i /f ratios of the 2.2mm-diameter samples in Fig. 6 are lower than those of the 3.0mm-diameter samples in correspondence to the above-mentioned difference in X/D ratio.
  • the 2.2mm-diameter sample having the Y/D value of 2.0 shows the K i /f ratio of about 88.
  • the K i /f ratio of about 88 is modified into about 90.6 which is nearer to the K i /f value of the corresponding 3.0mm-diameter sample.
  • the Y/D ratio in order to obtain the effective value of the heat exchanger efficiency, namely, the ratio (K i /f) of the overall heat transfer coefficient based on enthalpy difference to the pressure loss, the Y/D ratio must be equal to about 2.2.
  • the increase in Y/D ratio requires a reduced number of tubes to be arranged in the third or widthwise direction if the width of the heat exchanger is unchanged. This results in decrease in cooling capacity. In order to assure a sufficient cooling capacity, the number of the tubes must not be reduced. In this event, the increase in Y/D ratio results in an increase in size of the heat exchanger in the third direction and is therefore unfavorable.
  • the Y/D ratio within a range between about 1.8 and 2.4 is preferable to provide an effective K i /f ratio.
  • Fig. 7 shows the K i /f ratio as the heat exchanger efficiency with respect to the number N of rows of tubes.
  • all samples have the tube diameter of 3mm and the X/D ratio of 1.33.
  • the numbers of rows of tubes are equal to 10, 12, and 14.
  • the K i /f ratio slightly increases in a linear fashion with respect to the increase of the number of rows of tubes.
  • the evaporator is divided into four or six sections. It will be understood that the number of sections may be any appropriate number as far as the inner circuit pressure loss caused by the refrigerant flowing inside of the tubes can be suppressed within an allowable range and the refrigerant is substantially uniformly distributed in the respective tubes. At any rate, the refrigerant or the inner fluid flows into one of the tanks and flows out from the other tank.
  • a multitubular heat exchanger according to a third embodiment of this invention has upper and lower tanks 11 and 12 each of which has no partition plate.
  • the inner fluid travels through a single path from the lower tank 12 through the microtubes 1 to the upper tank 11.
  • a multitubular heat exchanger according to a fourth embodiment of this invention has upper and lower tanks 11 and 12 each of which has two chambers divided by a single partition plate.
  • the inner fluid travels through a two-part fluid path from the upper tank 11 through the microtubes 1, the lower tank 12, and the microtubes 1 to the upper tank 11.
  • the heat exchanger has a pair of tanks arranged in parallel to each other in a vertical direction.
  • the tanks may be arranged in parallel to each other in the horizontal direction with the axial direction of the tubes in parallel to the horizontal direction. In this case, however, additional means is required to assure substantially uniform flow of the inner heat exchange medium within the respective tubes.
  • a multitubular heat exchanger has a single-sided tank structure.
  • the upper and the lower tanks (2, 3 or 11, 12) are arranged opposite to each other with the tube bundle interposed therebetween.
  • the heat exchanger comprises upper and lower tanks 11 and 12 arranged at one side (at the top in Fig. 10) of a tube bundle array.
  • the upper and the lower tanks 11 and 12 are formed by partitioning a single tank at a center plane in the vertical direction to obtain a two-layer structure.
  • Each microtube 1 is bent at the bottom of the heat exchanger to form a U shape and has one tube end communicating with the lower tank 12 and the other tube end communicating with the upper tank 11 after penetrating through the lower tank 12. With this structure, an inner heat exchange medium flows from the lower tank 12 through the tubes 1 into the upper tank 11.
  • This invention is preferably applicable to a tube bundle array including ten or more rows of tubes with the tube diameter of 3mm or more in case where an air stream has the Raynolds number Re max far smaller than 2000 for the peak velocity and the tube diameter of a characteristic size.
  • the multitubular heat exchanger according to this invention is capable of achieving the effective value of the heat exchanger efficiency as the ratio of the outside heat transfer coefficient to the ventilating resistance by selecting an appropriate tube arrangement pattern taking condensation of moisture contained in air into consideration.
EP97302586A 1996-04-18 1997-04-16 Echangeur de chaleur multitubulaire avec disposition particulière des tubes Withdrawn EP0802383A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP96394/96 1996-04-18
JP9639496A JPH09280755A (ja) 1996-04-18 1996-04-18 多管式熱交換器

Publications (2)

Publication Number Publication Date
EP0802383A2 true EP0802383A2 (fr) 1997-10-22
EP0802383A3 EP0802383A3 (fr) 1998-10-07

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EP97302586A Withdrawn EP0802383A3 (fr) 1996-04-18 1997-04-16 Echangeur de chaleur multitubulaire avec disposition particulière des tubes

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JP (1) JPH09280755A (fr)

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0947792A2 (fr) * 1998-04-03 1999-10-06 Denso Corporation Evaporateur pour réfrigérant et sa méthode de fabrication
DE10158436A1 (de) * 2001-11-29 2003-06-12 Behr Gmbh & Co Wärmetauscher
DE10257767A1 (de) * 2002-12-10 2004-06-24 Behr Gmbh & Co. Kg Wärmeübertrager
FR2855599A1 (fr) * 2003-04-21 2004-12-03 Denso Corp Echangeur de chaleur
EP1571534A2 (fr) * 2004-02-16 2005-09-07 Hitachi, Ltd. Appareil électronique, radiateur d'un tel système et procédé de fabrication
EP1298401A3 (fr) * 2001-09-29 2005-12-28 Halla Climate Control Corporation Echangeur de chaleur
WO2007093590A1 (fr) * 2006-02-15 2007-08-23 Corporacion Capricornio Technologies, S.L. Echangeur thermique et climatiseur associe
WO2009022020A1 (fr) * 2007-08-16 2009-02-19 Valeo Systemes Thermiques Evaporateur à nappes multiples, en particulier pour un circuit de climatisation de véhicule automobile
CN101975493A (zh) * 2010-11-01 2011-02-16 芜湖博耐尔汽车电气系统有限公司 一种汽车空调平行流蒸发器
US8177932B2 (en) 2009-02-27 2012-05-15 International Mezzo Technologies, Inc. Method for manufacturing a micro tube heat exchanger
US8695689B2 (en) 2007-12-10 2014-04-15 Behr Gmbh & Co. Kg Heat exchanger, in particular heater for motor vehicles
CN103968681A (zh) * 2014-05-22 2014-08-06 苏州意玛斯砂光设备有限公司 一种分级散热装置
EP2447657A3 (fr) * 2010-10-28 2015-03-04 Samsung Electronics Co., Ltd. Échangeur multicircuit avec des collecteurs sectionnels
CN104428611A (zh) * 2012-07-04 2015-03-18 株式会社电装 冷媒蒸发器
EP2930455A1 (fr) * 2014-04-10 2015-10-14 MAHLE International GmbH Fluide caloporteur
DE102015211606A1 (de) * 2015-06-23 2016-12-29 Mahle International Gmbh Verdampfereinheit für eine Aufdachklimaanlage eines Straßenfahrzeugs
US10330398B2 (en) * 2014-02-27 2019-06-25 Hangzhou Sanhua Research Institute Co., Ltd. Heat exchanger
US10670349B2 (en) 2017-07-18 2020-06-02 General Electric Company Additively manufactured heat exchanger

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KR100825708B1 (ko) * 2001-09-29 2008-04-29 한라공조주식회사 이산화탄소용 열교환기

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JPH01169295A (ja) * 1987-12-24 1989-07-04 Kawasaki Steel Corp 熱交換器
JPH04113176A (ja) * 1990-08-31 1992-04-14 Nippondenso Co Ltd 積層型熱交換器
EP0640804A1 (fr) * 1993-08-30 1995-03-01 Sanden Corporation Echangeur de chaleur et arrangement de tubes pour cela

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US4676305A (en) * 1985-02-11 1987-06-30 Doty F David Microtube-strip heat exchanger
JPH01169295A (ja) * 1987-12-24 1989-07-04 Kawasaki Steel Corp 熱交換器
JPH04113176A (ja) * 1990-08-31 1992-04-14 Nippondenso Co Ltd 積層型熱交換器
EP0640804A1 (fr) * 1993-08-30 1995-03-01 Sanden Corporation Echangeur de chaleur et arrangement de tubes pour cela

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PATENT ABSTRACTS OF JAPAN vol. 016, no. 363 (M-1290), 5 August 1992 & JP 04 113176 A (NIPPONDENSO CO LTD), 14 April 1992 *

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0947792A2 (fr) * 1998-04-03 1999-10-06 Denso Corporation Evaporateur pour réfrigérant et sa méthode de fabrication
EP0947792A3 (fr) * 1998-04-03 2000-03-29 Denso Corporation Evaporateur pour réfrigérant et sa méthode de fabrication
US6272881B1 (en) 1998-04-03 2001-08-14 Denso Corporation Refrigerant evaporator and manufacturing method for the same
EP1298401A3 (fr) * 2001-09-29 2005-12-28 Halla Climate Control Corporation Echangeur de chaleur
DE10158436A1 (de) * 2001-11-29 2003-06-12 Behr Gmbh & Co Wärmetauscher
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Also Published As

Publication number Publication date
EP0802383A3 (fr) 1998-10-07
JPH09280755A (ja) 1997-10-31

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