JP2013036666A - Heat exchanger - Google Patents
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- JP2013036666A JP2013036666A JP2011172627A JP2011172627A JP2013036666A JP 2013036666 A JP2013036666 A JP 2013036666A JP 2011172627 A JP2011172627 A JP 2011172627A JP 2011172627 A JP2011172627 A JP 2011172627A JP 2013036666 A JP2013036666 A JP 2013036666A
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本発明は、流路内を流れる熱交換流体と流路外の熱交換対象物との間で熱交換を行わせる熱交換器に関する。 The present invention relates to a heat exchanger that exchanges heat between a heat exchange fluid flowing in a flow path and a heat exchange object outside the flow path.
ステンレス鋼板やアルミニウム板等の薄板金属の表面に、エッチング技術等を用いて熱交換流体を流通させるための流路を形成した熱交換器が開発されている。このような熱交換器として、特許文献１には、金属薄板状プレートに複数の伝熱フィンを設け、この金属薄板状プレートを交互に積み重ねることにより、対向する２つの金属薄板状プレート間に熱交換流体の流路を形成した熱交換器が開示されている。伝熱フィンを、先端から後端に向かって曲線状の断面形状に形成し、伝熱フィンの間を流れる流体の流路面積を略一定とすることにより、流路を流れる熱交換流体の縮流や拡流による圧力損失を小さくすることができ、熱交換器のコンパクト化と低コスト化とを維持しつつ、熱交換器の伝熱性能を損なうことなく、熱交換流体の圧力損失を小さく抑えることができる。 2. Description of the Related Art A heat exchanger has been developed in which a flow path for circulating a heat exchange fluid is formed on the surface of a thin metal plate such as a stainless steel plate or an aluminum plate using an etching technique or the like. As such a heat exchanger, in Patent Document 1, a plurality of heat transfer fins are provided on a metal thin plate plate, and the metal thin plate plates are alternately stacked, so that heat is generated between two opposing metal thin plate plates. A heat exchanger having a flow path for exchange fluid is disclosed. The heat transfer fins are formed in a curved cross-sectional shape from the front end to the rear end, and the flow path area of the fluid flowing between the heat transfer fins is made substantially constant, so that the heat exchange fluid flowing in the flow path is reduced. The pressure loss due to flow and expansion can be reduced, and the pressure loss of the heat exchange fluid can be reduced without compromising the heat transfer performance of the heat exchanger while maintaining a compact and low cost heat exchanger. Can be suppressed.
しかしながら、特許文献１の熱交換器のように、流路の側面が屈曲していると、流路内において主流に逆行するような流れ（渦）が発生し易くなり、この渦によって圧力損失が増大し、熱交換が妨げられる結果、熱交換性能が低下するという問題がある。なお、特許文献１において流体の流路面積を略一定としているように、流路面積を減少させると圧力損失が大きくなるので、通常、流路面積を減少させるようなことはしない。 However, if the side surface of the flow path is bent as in the heat exchanger of Patent Document 1, a flow (vortex) that goes back to the main flow easily occurs in the flow path, and pressure loss is caused by this vortex. As a result, the heat exchange performance is deteriorated as a result of increasing the heat exchange. In addition, since the pressure loss increases when the flow path area is reduced as in the case of Patent Document 1 where the flow path area of the fluid is substantially constant, the flow path area is not normally reduced.
本発明の目的は、熱交換性能を向上させることが可能な熱交換器を提供することである。 The objective of this invention is providing the heat exchanger which can improve heat exchange performance.
本発明における熱交換器は、流路内を流れる熱交換流体と、前記流路外の熱交換対象物との間で熱交換を行わせる熱交換器であって、前記流路の側面には、前記流路が蛇行するように屈曲された屈曲部が複数形成されているとともに、前記流路の底面には、前記熱交換流体の進行方向に沿って波状に起伏された起伏部が複数形成されており、隣り合う前記屈曲部間の間隔が、隣り合う前記起伏部間の間隔よりも大きいことを特徴とする。 The heat exchanger according to the present invention is a heat exchanger that exchanges heat between a heat exchange fluid flowing in a flow path and a heat exchange object outside the flow path, and is provided on a side surface of the flow path. A plurality of bent portions that are bent so that the flow path meanders, and a plurality of undulated portions that are undulated along the traveling direction of the heat exchange fluid are formed on the bottom surface of the flow path. The interval between the adjacent bent portions is larger than the interval between the adjacent undulating portions.
上記の構成によれば、流路の側面が屈曲していると、流路内において主流に逆行するような流れ（渦）が発生し易くなり、この渦によって圧力損失が増大し、熱交換が妨げられる結果、熱交換性能が低下するという問題がある。そこで、流路の底面に複数の起伏部を形成することで、流路の底面を熱交換流体の進行方向に沿って波状に起伏させる。すると、起伏部が流路面積を減少させるので、圧力損失が大きくなる傾向となるが、起伏部が渦の発達を抑制し、隣り合う屈曲部間において渦が広範囲に生じ難くなるので、圧力損失が減少するとともに熱伝達特性が向上する。また、流路の内面において境界層が形成され難くなるので、境界層の発達が抑制される。これにより、熱交換性能を向上させることができる。なお、境界層とは、流路の内面に形成される温度の遷移域のことであり、熱抵抗として作用することで熱交換性能を低下させるものである。 According to the above configuration, when the side surface of the flow path is bent, a flow (vortex) that goes back to the main flow easily occurs in the flow path, and this vortex increases pressure loss and heat exchange. As a result, the heat exchange performance is degraded. Therefore, by forming a plurality of undulating portions on the bottom surface of the flow path, the bottom surface of the flow path is undulated along the traveling direction of the heat exchange fluid. Then, since the undulations reduce the flow path area, the pressure loss tends to increase, but the undulations suppress the development of vortices, and it is difficult for vortices to occur in a wide range between adjacent bends. As heat decreases, heat transfer characteristics improve. Moreover, since it becomes difficult to form a boundary layer on the inner surface of the flow path, the development of the boundary layer is suppressed. Thereby, heat exchange performance can be improved. The boundary layer is a temperature transition region formed on the inner surface of the flow path, and reduces heat exchange performance by acting as a thermal resistance.
また、本発明における熱交換器において、前記起伏部は、仰角と俯角とが同じであってよい。上記の構成によれば、起伏部の仰角と俯角とを同じにして、熱交換流体の流れをスムーズにすることで、渦の発達を抑制することができる。ここで、仰角とは水平を基準とした上向きの角度であり、俯角とは水平を基準とした下向きの角度である。 In the heat exchanger according to the present invention, the undulating portion may have the same elevation angle and depression angle. According to said structure, development of a vortex can be suppressed by making the elevation angle and depression angle of a undulation part the same, and making the flow of a heat exchange fluid smooth. Here, the elevation angle is an upward angle based on the horizontal, and the depression angle is a downward angle based on the horizontal.
また、本発明における熱交換器において、前記流路の最下部から前記流路の上面までの高さをＡとし、前記起伏部の頂点から前記流路の上面までの高さをａとし、前記起伏部の仰角をθとすると、０．７２＜ａ／Ａ≦０．８５、且つ、５°≦θ≦２５°の条件を満足してよい。上記の構成によれば、０．７２＜ａ／Ａ≦０．８５、且つ、５°≦θ≦２５°の条件を満足すると、熱伝達特性因子ｊの値を摩擦係数ｆの値で除した値が、起伏部を有しない蛇行した流路に対して、１．１５よりも大きい割合で上昇する。このことから、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 Further, in the heat exchanger according to the present invention, the height from the lowest part of the flow path to the upper surface of the flow path is A, the height from the top of the undulating portion to the upper surface of the flow path is a, If the elevation angle of the undulating portion is θ, the conditions of 0.72 <a / A ≦ 0.85 and 5 ° ≦ θ ≦ 25 ° may be satisfied. According to the above configuration, when the conditions of 0.72 <a / A ≦ 0.85 and 5 ° ≦ θ ≦ 25 ° are satisfied, the value of the heat transfer characteristic factor j is divided by the value of the friction coefficient f. The value rises at a rate greater than 1.15 for a serpentine channel having no undulations. From this, the heat exchange performance can be suitably improved by satisfying the above conditions.
また、本発明における熱交換器において、前記流路の最下部から前記流路の上面までの高さをＡとし、前記起伏部の頂点から前記流路の上面までの高さをａとし、前記起伏部の仰角をθとすると、０．５８＜ａ／Ａ≦０．７２、且つ、５°≦θ≦３０°の条件を満足してよい。上記の構成によれば、０．５８＜ａ／Ａ≦０．７２、且つ、５°≦θ≦３０°の条件を満足すると、熱伝達特性因子ｊの値を摩擦係数ｆの値で除した値が、起伏部を有しない蛇行した流路に対して、１．１５よりも大きい割合で上昇する。このことから、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 Further, in the heat exchanger according to the present invention, the height from the lowest part of the flow path to the upper surface of the flow path is A, the height from the top of the undulating portion to the upper surface of the flow path is a, If the elevation angle of the undulating portion is θ, the conditions of 0.58 <a / A ≦ 0.72 and 5 ° ≦ θ ≦ 30 ° may be satisfied. According to the above configuration, when the conditions of 0.58 <a / A ≦ 0.72 and 5 ° ≦ θ ≦ 30 ° are satisfied, the value of the heat transfer characteristic factor j is divided by the value of the friction coefficient f. The value rises at a rate greater than 1.15 for a serpentine channel having no undulations. From this, the heat exchange performance can be suitably improved by satisfying the above conditions.
また、本発明における熱交換器において、前記流路の最下部から前記流路の上面までの高さをＡとし、前記起伏部の頂点から前記流路の上面までの高さをａとし、前記起伏部の仰角をθとすると、ａ／Ａ＝０．５８、且つ、５°≦θ≦４５°の条件を満足してよい。上記の構成によれば、ａ／Ａ＝０．５８、且つ、５°≦θ≦４５°の条件を満足すると、レイノルズ数が５００未満のときに、熱伝達特性因子ｊの値を摩擦係数ｆの値で除した値が、起伏部を有しない蛇行した流路に対して、１．１５よりも大きい割合で上昇する。このことから、レイノルズ数が５００未満のときに、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 Further, in the heat exchanger according to the present invention, the height from the lowest part of the flow path to the upper surface of the flow path is A, the height from the top of the undulating portion to the upper surface of the flow path is a, When the elevation angle of the undulating portion is θ, the conditions of a / A = 0.58 and 5 ° ≦ θ ≦ 45 ° may be satisfied. According to the above configuration, when the condition of a / A = 0.58 and 5 ° ≦ θ ≦ 45 ° is satisfied, the value of the heat transfer characteristic factor j is set to the friction coefficient f when the Reynolds number is less than 500. The value divided by this value rises at a rate larger than 1.15 with respect to the meandering flow path having no undulations. From this, when the Reynolds number is less than 500, the heat exchange performance can be suitably improved by satisfying the above condition.
本発明の熱交換器によると、流路の底面に複数の起伏部を形成することで、流路の底面を熱交換流体の進行方向に沿って波状に起伏させる。すると、起伏部が流路面積を減少させるので、圧力損失が大きくなる傾向となるが、起伏部が渦の発達を抑制し、隣り合う屈曲部間において渦が広範囲に生じ難くなるので、圧力損失が減少するとともに熱伝達特性が向上する。また、流路の内面において境界層が形成され難くなるので、境界層の発達が抑制される。これにより、熱交換性能を向上させることができる。 According to the heat exchanger of the present invention, by forming a plurality of undulating portions on the bottom surface of the flow path, the bottom surface of the flow path is undulated along the traveling direction of the heat exchange fluid. Then, since the undulations reduce the flow path area, the pressure loss tends to increase, but the undulations suppress the development of vortices, and it is difficult for vortices to occur in a wide range between adjacent bends. As heat decreases, heat transfer characteristics improve. Moreover, since it becomes difficult to form a boundary layer on the inner surface of the flow path, the development of the boundary layer is suppressed. Thereby, heat exchange performance can be improved.
以下、本発明を実施するための形態について図面を参照しつつ説明する。 Hereinafter, embodiments for carrying out the present invention will be described with reference to the drawings.
（熱交換器の構成）
本実施形態に係る熱交換器１は、図１に示すように、概ね長方体状の箱型に形成された本体２を有している。本体２の内部には、流路構成部材１０が設けられている。
(Configuration of heat exchanger)
As shown in FIG. 1, the heat exchanger 1 according to the present embodiment has a main body 2 formed in a substantially rectangular box shape. A flow path component 10 is provided inside the main body 2.
流路構成部材１０は、図２に示すように、第１金属薄板１１及び第２金属薄板１２を交互に複数積層して形成されている。なお、第１金属薄板１１、第２金属薄板１２としては、例えば、ステンレス鋼板を用いることができるが、鉄、銅、アルミニウム、アルミニウム合金などを用いてもよい。 As shown in FIG. 2, the flow path component member 10 is formed by alternately laminating a plurality of first metal thin plates 11 and second metal thin plates 12. In addition, as the 1st metal thin plate 11 and the 2nd metal thin plate 12, although a stainless steel plate can be used, for example, iron, copper, aluminum, an aluminum alloy, etc. may be used.
第１金属薄板１１は、表面に複数の流路（溝）Ｒ１が形成された長方形状の薄板である。複数の流路Ｒ１は、長方形状の薄板の長手方向に延びるように形成されている。各流路Ｒ１の水平幅は、例えば２ｍｍである。また、各流路Ｒ１の底面から上面までの高さは、後述する起伏部２２によって高低するが、最大高さは例えば１ｍｍである。 The first metal thin plate 11 is a rectangular thin plate having a plurality of flow paths (grooves) R1 formed on the surface thereof. The plurality of flow paths R1 are formed so as to extend in the longitudinal direction of the rectangular thin plate. The horizontal width of each flow path R1 is 2 mm, for example. In addition, the height from the bottom surface to the top surface of each flow path R1 is raised and lowered by the undulating portion 22 described later, but the maximum height is, for example, 1 mm.
第２金属薄板１２は、第１金属薄板１１と同じ大きさの長方形状の薄板である。第２金属薄板１２の表面には、第１金属薄板１１に形成された流路Ｒ１とは直交する方向（長方形状の薄板の短手方向）に延びる複数の流路（溝）Ｒ２が形成されている。各流路Ｒ２の水平幅は、例えば２ｍｍである。また、各流路Ｒ２の底面から上面までの高さは、後述する起伏部２２によって高低するが、最大高さは例えば１ｍｍである。 The second metal thin plate 12 is a rectangular thin plate having the same size as the first metal thin plate 11. On the surface of the second metal thin plate 12, a plurality of flow channels (grooves) R2 extending in a direction perpendicular to the flow channel R1 formed in the first metal thin plate 11 (short direction of the rectangular thin plate) are formed. ing. The horizontal width of each flow path R2 is 2 mm, for example. Moreover, although the height from the bottom face of each flow path R2 to the upper surface is raised and lowered by the undulating portion 22 described later, the maximum height is, for example, 1 mm.
ここで、流路Ｒ１および流路Ｒ２は、一の金属薄板に形成された溝の側面及び底面と、その上に積層される他の金属薄板の下面とで、流れ方向に対して直交する方向を全て覆われている。 Here, the flow path R1 and the flow path R2 are directions perpendicular to the flow direction between the side surface and the bottom surface of the groove formed in one thin metal plate and the lower surface of another thin metal plate laminated thereon. All covered.
図１に示すように、熱交換器１の本体２には、本体２の側面を形成するように、第１供給ヘッダー３、第１排出ヘッダー４、第２供給ヘッダー５、および、第２排出ヘッダー６が設けられている。 As shown in FIG. 1, the main body 2 of the heat exchanger 1 has a first supply header 3, a first discharge header 4, a second supply header 5, and a second discharge so as to form a side surface of the main body 2. A header 6 is provided.
第１供給ヘッダー３には供給管３ａから、例えば冷水等の熱交換流体が供給される。そして、この熱交換流体は、第１供給ヘッダー３を介して、複数の第１金属薄板１１に形成された複数の流路Ｒ１に分配される。 A heat exchange fluid such as cold water is supplied to the first supply header 3 from the supply pipe 3a. The heat exchange fluid is distributed to the plurality of flow paths R1 formed in the plurality of first metal thin plates 11 via the first supply header 3.
第１供給ヘッダー３から供給された熱交換流体は、第１金属薄板１１に形成された複数の流路Ｒ１を通過して第１排出ヘッダー４に流れ込む。第１排出ヘッダー４は、第１供給ヘッダー３に対向する側面を形成するように本体２に設けられている。第１排出ヘッダー４には、第１金属薄板１１に形成された複数の流路Ｒ１から排出された熱交換流体が供給される。そして、熱交換流体は、第１排出ヘッダー４に設けられた排出管４ａを通じて排出される。 The heat exchange fluid supplied from the first supply header 3 passes through the plurality of flow paths R <b> 1 formed in the first metal thin plate 11 and flows into the first discharge header 4. The first discharge header 4 is provided on the main body 2 so as to form a side surface facing the first supply header 3. The first discharge header 4 is supplied with the heat exchange fluid discharged from the plurality of flow paths R1 formed in the first metal thin plate 11. Then, the heat exchange fluid is discharged through a discharge pipe 4 a provided in the first discharge header 4.
第２供給ヘッダー５には供給管５ａから、熱交換流体との熱交換の対象となる熱交換対象物である流体（以下、対象流体）が供給される。そして、この対象流体は、第２供給ヘッダー５を介して、第２金属薄板１２に形成された複数の流路Ｒ２に分配される。 The second supply header 5 is supplied from a supply pipe 5a with a fluid (hereinafter, a target fluid) that is a heat exchange target that is a target of heat exchange with the heat exchange fluid. The target fluid is distributed to the plurality of flow paths R2 formed in the second metal thin plate 12 via the second supply header 5.
第２供給ヘッダー５から供給された対象流体は、第２金属薄板１２に形成された複数の流路Ｒ２を通過して第２排出ヘッダー６に流れ込む。これにより、第２金属薄板１２に形成された流路Ｒ２を流れる対象流体と、第１金属薄板１１に形成された流路Ｒ１を流れる熱交換流体との間で、流路構成部材１０を介しての熱交換が行われることとなる。 The target fluid supplied from the second supply header 5 flows into the second discharge header 6 through the plurality of flow paths R2 formed in the second metal thin plate 12. Thus, the target fluid flowing in the flow path R2 formed in the second metal thin plate 12 and the heat exchange fluid flowing in the flow path R1 formed in the first metal thin plate 11 are interposed via the flow path constituting member 10. All heat exchanges will be performed.
第２排出ヘッダー６は、第２供給ヘッダー５に対向する側面を形成するように本体２に設けられている。第２排出ヘッダー６には、第２金属薄板１２に形成された複数の流路Ｒ２から排出された対象流体が供給される。そして、対象流体は、第２排出ヘッダー６に設けられた排出管６ａを通じて排出される。 The second discharge header 6 is provided on the main body 2 so as to form a side surface facing the second supply header 5. The target fluid discharged from the plurality of flow paths R2 formed in the second metal thin plate 12 is supplied to the second discharge header 6. Then, the target fluid is discharged through the discharge pipe 6 a provided in the second discharge header 6.
（流路の詳細）
第１金属薄板１１に形成された流路Ｒ１は、図２に示すように、第１金属薄板１１の長手方向に沿って蛇行している。即ち、流路Ｒ１の側面には、流路Ｒ１が蛇行するように屈曲された屈曲部２１が複数形成されている（図３参照）。また、第２金属薄板１２に形成された流路Ｒ２は、第２金属薄板１２の短手方向に沿って蛇行している。即ち、流路Ｒ２の側面には、流路Ｒ２が蛇行するように屈曲された屈曲部２１が複数形成されている（図３参照）。流路Ｒ１および流路Ｒ２に形成された各屈曲部２１の屈曲角度は、例えば１２０°である。また、流体の進行方向に隣り合う屈曲部２１・２１間の距離は、例えば５ｍｍである。
(Details of channel)
The flow path R1 formed in the first metal thin plate 11 meanders along the longitudinal direction of the first metal thin plate 11 as shown in FIG. That is, a plurality of bent portions 21 that are bent so that the flow path R1 meanders are formed on the side surface of the flow path R1 (see FIG. 3). Further, the flow path R <b> 2 formed in the second metal thin plate 12 meanders along the short direction of the second metal thin plate 12. That is, a plurality of bent portions 21 that are bent so that the flow path R2 meanders are formed on the side surface of the flow path R2 (see FIG. 3). The bending angle of each bent portion 21 formed in the flow path R1 and the flow path R2 is, for example, 120 °. Moreover, the distance between the bending parts 21 * 21 adjacent to the advancing direction of a fluid is 5 mm, for example.
流路Ｒ１の斜視図を図３（ａ）に示す。流路Ｒ１の底面には、熱交換流体の進行方向に沿って波状に起伏された起伏部２２が複数形成されている。なお、流路Ｒ２の底面にも、流路Ｒ１と同様の起伏部２２が複数形成されている。比較例として、流路Ｒ１とは起伏部２２を設けていない点で異なる、底面がフラットな流路Ｃ１の斜視図を図３（ｂ）に示す。複数の起伏部２２により、流路Ｒ１の伝熱面積は流路Ｃ１の伝熱面積よりも広くなっている。 A perspective view of the flow path R1 is shown in FIG. On the bottom surface of the flow path R1, a plurality of undulating portions 22 that are undulated along the traveling direction of the heat exchange fluid are formed. A plurality of undulations 22 similar to the flow path R1 are formed on the bottom surface of the flow path R2. As a comparative example, FIG. 3B shows a perspective view of a channel C1 having a flat bottom surface, which is different from the channel R1 in that the undulating portion 22 is not provided. Due to the plurality of undulating portions 22, the heat transfer area of the flow path R1 is wider than the heat transfer area of the flow path C1.
ここで、各起伏部２２は、流路Ｒ１の底面から流体の進行方向に所定の角度で隆起していき、頂点を境に流体の進行方向に所定の角度で流路Ｒ１の最下部まで沈降していく形状にされている。即ち、各起伏部２２の仰角と俯角とは同じである。ここで、仰角とは水平を基準とした上向きの角度であり、俯角とは水平を基準とした下向きの角度である。これにより、流体の進行方向に沿った起伏部２２の断面形状は、二等辺三角形になっている。なお、起伏部２２の頂点はとがっていてもよいし、丸みを帯びていてもよい。 Here, each undulation portion 22 rises from the bottom surface of the flow path R1 at a predetermined angle in the fluid traveling direction, and sinks to the lowest part of the flow path R1 at a predetermined angle in the fluid traveling direction from the apex. It is made into a shape to do. That is, the elevation angle and depression angle of each undulating portion 22 are the same. Here, the elevation angle is an upward angle based on the horizontal, and the depression angle is a downward angle based on the horizontal. Thereby, the cross-sectional shape of the undulating portion 22 along the fluid traveling direction is an isosceles triangle. In addition, the peak of the undulating portion 22 may be sharp or rounded.
また、流体の進行方向に隣り合う屈曲部２１・２１間には、起伏部２２が４つずつ設けられている。即ち、流体の進行方向に隣り合う屈曲部２１・２１間の間隔は、流体の進行方向に隣り合う起伏部２２・２２間の間隔よりも大きい。なお、流体の進行方向に隣り合う屈曲部２１・２１間に設けられる起伏部２２の数は４つに限定されず、５つ以上であっても３つ以下であってもよい。 In addition, four undulating portions 22 are provided between the bent portions 21 and 21 adjacent to each other in the fluid traveling direction. That is, the interval between the bent portions 21 and 21 adjacent to each other in the fluid traveling direction is larger than the interval between the undulating portions 22 and 22 adjacent to each other in the fluid traveling direction. The number of the undulating portions 22 provided between the bent portions 21 and 21 adjacent to each other in the fluid traveling direction is not limited to four, and may be five or more or three or less.
このような起伏部２２は、エッチングで流路Ｒ１，Ｒ２を形成する際に、マスク等を用いて場所により腐食時間を変化させることで形成されている。なお、起伏部２２は、流路Ｒ１，Ｒ２の底面に転写により形成されてもよい。 Such undulations 22 are formed by changing the corrosion time depending on the location using a mask or the like when the flow paths R1 and R2 are formed by etching. Note that the undulating portion 22 may be formed on the bottom surfaces of the flow paths R1, R2 by transfer.
（流路内の流れ解析）
次に、図３（ａ）に示した流路Ｒ１内における流体の流れを解析した解析結果（速度ベクトル図）を図４（ａ）に示す。尚、図４は、流路Ｒ１内を流れる熱交換流体のレイノルズ数Ｒｅを５００としたときの速度ベクトル図である。
(Flow analysis in the flow path)
Next, FIG. 4A shows an analysis result (speed vector diagram) obtained by analyzing the flow of the fluid in the flow path R1 shown in FIG. FIG. 4 is a velocity vector diagram when the Reynolds number Re of the heat exchange fluid flowing in the flow path R1 is 500.
レイノルズ数Ｒｅは式（１）で定義される。
Ｒｅ＝ｕＤ／ν ・・・式（１）
The Reynolds number Re is defined by the formula (1).
Re = uD / ν Expression (1)
ここで、式（１）において、ｕ：熱交換流体の流速、Ｄ：狭流路幅基準の水力直径、ν：熱交換流体の動粘性係数、である。 Here, in Equation (1), u is the flow velocity of the heat exchange fluid, D is the hydraulic diameter based on the narrow channel width, and ν is the kinematic viscosity coefficient of the heat exchange fluid.
比較のため、流路Ｒ１とは起伏部２２を設けていない点で異なる流路Ｃ１内における流体の流れを同じ条件で解析した解析結果（速度ベクトル図）を図４（ｂ）に示す。ここで、隣り合う屈曲部２１・２１間の一方の壁面側において、上流側の屈曲部２１の位置にＡ点、下流側の屈曲部２１の位置にＢ点をそれぞれ設定し、Ａ点とＢ点との間の壁面をＡ−Ｂ壁面とする。 For comparison, FIG. 4B shows an analysis result (velocity vector diagram) obtained by analyzing the flow of the fluid in the flow channel C1, which is different from the flow channel R1 in that the undulating portion 22 is not provided. Here, on one wall surface side between adjacent bent portions 21 and 21, point A is set at the position of the bent portion 21 on the upstream side, and point B is set at the position of the bent portion 21 on the downstream side. The wall surface between the points is defined as the A-B wall surface.
図４（ｂ）に示すように、比較例の流路Ｃ１においては、Ａ点とＢ点との間にわたって循環するような渦がＡ−Ｂ壁面に沿って発生している。この場合、Ａ−Ｂ壁面側において、熱交換流体と流路構成部材１０との間の熱交換効率が大きく悪化してしまう。 As shown in FIG. 4B, in the flow path C1 of the comparative example, a vortex that circulates between the point A and the point B is generated along the AB wall surface. In this case, the heat exchange efficiency between the heat exchange fluid and the flow path component 10 is greatly deteriorated on the A-B wall surface side.
一方、図４（ａ）に示すように、本実施形態の流路Ｒ１においては、渦は、Ａ−Ｂ壁面側のＡ点近傍にのみ発生している。この場合、Ａ−Ｂ壁面に沿った逆向きの流れが少なくなるため、熱交換流体と流路構成部材１０との間の熱交換効率が向上する。 On the other hand, as shown to Fig.4 (a), in flow path R1 of this embodiment, the vortex has generate | occur | produced only in the vicinity of A point on the AB wall surface side. In this case, since the reverse flow along the AB wall surface is reduced, the heat exchange efficiency between the heat exchange fluid and the flow path component 10 is improved.
図４に示すＡ点からＢ点までのＡ−Ｂ壁面のＮｕ数（熱伝達率）を本実施形態と比較例とで比較したグラフを図５に示す。本実施形態の複数の起伏部２２を備えた流路Ｒ１では、比較例の起伏部２２を備えない流路Ｃ１と比べて、Ｂ点側におけるＮｕ数（熱伝達率）が大きく向上していることがわかる。 FIG. 5 shows a graph comparing the Nu number (heat transfer coefficient) of the AB wall surface from point A to point B shown in FIG. 4 between this embodiment and the comparative example. In the flow path R1 including the plurality of undulations 22 of the present embodiment, the Nu number (heat transfer coefficient) on the B point side is greatly improved as compared with the flow path C1 not including the undulations 22 of the comparative example. I understand that.
このように、側面が屈曲しているだけの流路Ｃ１においては、流路Ｃ１内において主流に逆行するような流れ（渦）が発生し易くなり、この渦によって圧力損失が増大し、熱交換が妨げられる結果、熱交換性能が低下するという問題がある。そこで、本実施形態の流路Ｒ１では、底面に複数の起伏部２２を形成することで、底面を熱交換流体の進行方向に沿って波状に起伏させている。すると、起伏部２２が流路面積を減少させるので、圧力損失が大きくなる傾向となるが、起伏部２２が渦の発達を抑制し、隣り合う屈曲部２１・２１間において渦が広範囲に生じ難くなるので、圧力損失が減少するとともに熱伝達特性が向上する。また、流路Ｒ１の内面において境界層が形成され難くなるので、境界層の発達が抑制される。これにより、熱交換性能を向上させることができる。なお、境界層とは、流路の内面に形成される温度の遷移域のことであり、熱抵抗として作用することで熱交換性能を低下させるものである。 In this way, in the flow path C1 whose side surfaces are only bent, a flow (vortex) that goes back to the main flow easily occurs in the flow path C1, and this vortex increases pressure loss and heat exchange. As a result, the heat exchange performance is degraded. Therefore, in the flow path R1 of this embodiment, the bottom surface is undulated along the traveling direction of the heat exchange fluid by forming a plurality of undulating portions 22 on the bottom surface. Then, since the undulating portion 22 reduces the flow path area, the pressure loss tends to increase. However, the undulating portion 22 suppresses the development of the vortex, and the vortex is not easily generated in a wide range between the adjacent bent portions 21 and 21. As a result, pressure loss is reduced and heat transfer characteristics are improved. Moreover, since it becomes difficult to form a boundary layer on the inner surface of the flow path R1, the development of the boundary layer is suppressed. Thereby, heat exchange performance can be improved. The boundary layer is a temperature transition region formed on the inner surface of the flow path, and reduces heat exchange performance by acting as a thermal resistance.
また、起伏部２２の仰角と俯角とを同じにして、熱交換流体の流れをスムーズにすることで、渦の発達を抑制することができる。 Further, by making the elevation angle and the depression angle of the undulating portion 22 the same and smoothening the flow of the heat exchange fluid, the development of vortices can be suppressed.
（熱伝達特性等に関する解析結果）
次に、本実施形態の熱交換器１における流路Ｒ１（図３（ａ）参照）、及び比較例の流路Ｃ１（図３（ｂ）参照）について、流路を流れる流体のレイノルズ数Ｒｅと熱伝達特性因子ｊとの関係の解析結果を図６に示す。また、流路を流れる流体のレイノルズ数Ｒｅと摩擦係数ｆとの関係の解析結果を図７に示す。また、流路を流れる流体のレイノルズ数Ｒｅとｊ／ｆ値との関係の解析結果を図８に示す。
(Analysis results on heat transfer characteristics, etc.)
Next, with respect to the flow path R1 (see FIG. 3A) in the heat exchanger 1 of the present embodiment and the flow path C1 of the comparative example (see FIG. 3B), the Reynolds number Re of the fluid flowing through the flow path. FIG. 6 shows the analysis result of the relationship between the temperature and the heat transfer characteristic factor j. FIG. 7 shows an analysis result of the relationship between the Reynolds number Re of the fluid flowing through the flow path and the friction coefficient f. Moreover, the analysis result of the relationship between the Reynolds number Re of the fluid which flows through a flow path and j / f value is shown in FIG.
熱伝達特性因子ｊは、以下の式（２）、式（３）に基づいて解析により求められる。熱伝達特性因子ｊは、熱伝達特性を表す因子であり、流路を流れる流体から流路構成部材１０への熱伝達特性が高いほど、大きい値となる。 The heat transfer characteristic factor j is obtained by analysis based on the following formulas (2) and (3). The heat transfer characteristic factor j is a factor representing the heat transfer characteristic. The higher the heat transfer characteristic from the fluid flowing through the flow path to the flow path constituting member 10, the larger the value.
ここで、式（２）、式（３）において、Ｎｕ：ヌセルト数、Ｒｅ：レイノルズ数、Ｐｒ：プラントル数、ｈ：流体と流路構成部材との間の熱伝達率、ｋ：流体の熱伝導率、ｄ：水力直径、である。 Here, in Expressions (2) and (3), Nu: Nusselt number, Re: Reynolds number, Pr: Prandtl number, h: Heat transfer coefficient between fluid and flow path component, k: Heat of fluid Conductivity, d: hydraulic diameter.
摩擦係数ｆは、以下に示す式（４）に基づいて求めた値であり、流路内を通過する流体の圧力損失が大きいほど、大きい値となる。 The friction coefficient f is a value obtained based on the following equation (4), and becomes a larger value as the pressure loss of the fluid passing through the flow path is larger.
ここで、式（４）において、ΔＰ：圧力損失、ｕ：流速、ｄ：水力直径、ρ：流体の密度、Ｌ：流路長、である。 Here, in Expression (4), ΔP: pressure loss, u: flow velocity, d: hydraulic diameter, ρ: fluid density, L: flow path length.
図６に示すように、熱伝達特性因子ｊの値は、レイノルズ数Ｒｅの値によらず、比較例よりも本実施形態の方が大きくなっている。このことから、本実施形態の流路Ｒ１の方が、比較例の流路Ｃ１よりも熱伝達特性が優れていることがわかる。 As shown in FIG. 6, the value of the heat transfer characteristic factor j is larger in the present embodiment than in the comparative example, regardless of the value of the Reynolds number Re. From this, it can be seen that the flow path R1 of the present embodiment has better heat transfer characteristics than the flow path C1 of the comparative example.
また、図７に示すように、摩擦係数ｆの値は、レイノルズ数Ｒｅの値によらず、比較例よりも本実施形態の方が小さくなっている。このことから、本実施形態の流路Ｒ１の方が、比較例の流路Ｃ１よりも圧力損失が小さいことがわかる。 Further, as shown in FIG. 7, the value of the friction coefficient f is smaller in the present embodiment than in the comparative example, regardless of the value of the Reynolds number Re. From this, it can be understood that the flow path R1 of the present embodiment has a smaller pressure loss than the flow path C1 of the comparative example.
その結果、図８に示すように、熱伝達特性因子ｊの値を摩擦係数ｆの値で除したｊ／ｆ値は、レイノルズ数Ｒｅの値によらず、比較例よりも本実施形態の方が大きくなっている。 As a result, as shown in FIG. 8, the j / f value obtained by dividing the value of the heat transfer characteristic factor j by the value of the friction coefficient f is greater than that of the comparative example regardless of the value of the Reynolds number Re. Is getting bigger.
このように、本実施形態の流路Ｒ１は、底面に形成された複数の起伏部２２が流路面積を減少させるので、圧力損失が大きくなる傾向となるが、起伏部２２が渦の発達を抑制し、隣り合う屈曲部２１・２１間において渦が広範囲に生じ難くなるので、圧力損失が減少するとともに熱伝達特性が向上する。また、複数の起伏部２２により流路Ｒ１の内面において境界層が形成され難くなっている。よって、比較例の流路Ｃ１に比べて本実施形態の流路Ｒ１の熱交換性能を向上させることができる。 As described above, in the flow path R1 of the present embodiment, the plurality of undulations 22 formed on the bottom surface reduce the flow path area, and thus the pressure loss tends to increase. Suppressing and making it difficult for vortices to be generated in a wide range between the adjacent bent portions 21 and 21, thereby reducing pressure loss and improving heat transfer characteristics. Moreover, it is difficult for the plurality of undulating portions 22 to form a boundary layer on the inner surface of the flow path R1. Therefore, the heat exchange performance of the flow path R1 of the present embodiment can be improved compared to the flow path C1 of the comparative example.
なお、複数の起伏部２２で流路の底面を波状に起伏させる代わりに、複数の凸部で流路の底面を凹凸状に起伏させることが考えられる。しかし、両者を比較した結果、図８に示すように、底面を波状に起伏させた比較例の方が、底面を凹凸状に起伏させた比較例２よりも、ｊ／ｆの値が大きくなった。このことから、底面を凹凸状に起伏させるよりも、底面を波状に起伏させた方が熱交換性能がより向上することがわかる。 In addition, instead of causing the plurality of undulating portions 22 to undulate the bottom surface of the channel, it is conceivable that the bottom surface of the channel is undulated with a plurality of convex portions. However, as a result of comparing the two, as shown in FIG. 8, the value of j / f is larger in the comparative example in which the bottom surface is undulated as compared to Comparative Example 2 in which the bottom surface is undulated. It was. From this, it can be seen that the heat exchanging performance is more improved when the bottom surface is undulated than when the bottom surface is undulated.
（ｊ／ｆ値の評価結果）
次に、図３において、流路Ｒ１の最下部から流路Ｒ１の上面（他の金属薄板の下面）までの高さ（流路Ｃ１の底面から流路Ｃ１の上面までの高さ）をＡとし、起伏部２２の頂点から流路Ｒ１の上面（他の金属薄板の下面）までの高さをａとし、起伏部２２の仰角をθとしたときに、流路Ｃ１に対する流路Ｒ１のｊ／ｆ値の上昇割合を表１、表２に示す。ａ／Ａは起伏部２２の頂点の高さを表し、値が小さいほど頂点は高い。ここで、起伏部２２の頂点の高さをａ／Ａ＝０．５８よりも高くすると、流路面積が減少しすぎるので、ａ／Ａ≧０．５８とした。また、起伏部２２の仰角θを４５°よりも大きくすると、起伏部２２間のピッチ（間隔）が狭くなりすぎるので、θ≦４５°とした。
(J / f value evaluation result)
Next, in FIG. 3, the height (the height from the bottom surface of the flow channel C1 to the upper surface of the flow channel C1) from the bottom of the flow channel R1 to the upper surface of the flow channel R1 (the lower surface of the other metal thin plate) is defined as A. Where the height from the apex of the undulating portion 22 to the upper surface of the flow path R1 (the lower surface of another thin metal plate) is a, and the elevation angle of the undulating portion 22 is θ, j of the flow path R1 with respect to the flow path C1. Tables 1 and 2 show the rate of increase in the / f value. a / A represents the height of the vertex of the undulating portion 22, and the smaller the value, the higher the vertex. Here, if the height of the apex of the undulating portion 22 is higher than a / A = 0.58, the flow path area is excessively reduced, so a / A ≧ 0.58. Further, if the elevation angle θ of the undulating portion 22 is larger than 45 °, the pitch (interval) between the undulating portions 22 becomes too narrow, so θ ≦ 45 °.
表１、表２から、起伏部２２の頂点の高さが一定であれば、仰角θが大きくなるにつれて上昇割合が減少していく傾向にあることがわかる。これは、頂点の高さを一定として仰角θを大きくするほど起伏部２２・２２間のピッチが狭くなっていき、ピッチが狭くなるにつれて、頂点間の距離が短くなり、起伏部２２の起伏に沿って流れる流体の量が減少することで、起伏部２２が渦の発達を抑制する作用が弱まっていくためと考えられる。この傾向を踏まえて、０．７２＜ａ／Ａ≦０．８５、且つ、５°≦θ≦２５°の条件を満足すると、レイノルズ数Ｒｅの値によらず、ｊ／ｆ値の上昇割合は１．１５よりも大きくなる。このことから、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 From Tables 1 and 2, it can be seen that if the height of the apex of the undulating portion 22 is constant, the increasing rate tends to decrease as the elevation angle θ increases. This is because the pitch between the undulating portions 22 and 22 becomes narrower as the elevation angle θ is increased with the height of the vertex being constant, and as the pitch is reduced, the distance between the vertices is shortened. It is considered that the action of the undulations 22 to suppress the development of vortices is weakened by reducing the amount of fluid flowing along. Based on this tendency, when the conditions of 0.72 <a / A ≦ 0.85 and 5 ° ≦ θ ≦ 25 ° are satisfied, the increase rate of the j / f value is independent of the Reynolds number Re. Greater than 1.15. From this, the heat exchange performance can be suitably improved by satisfying the above conditions.
また、０．５８＜ａ／Ａ≦０．７２、且つ、５°≦θ≦３０°の条件を満足すると、レイノルズ数Ｒｅの値によらず、ｊ／ｆ値の上昇割合は１．１５よりも大きくなる。このことから、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 Further, when the conditions of 0.58 <a / A ≦ 0.72 and 5 ° ≦ θ ≦ 30 ° are satisfied, the increase rate of the j / f value is 1.15 regardless of the value of the Reynolds number Re. Also grows. From this, the heat exchange performance can be suitably improved by satisfying the above conditions.
また、ａ／Ａ＝０．５８、且つ、５°≦θ≦４５°の条件を満足すると、レイノルズ数Ｒｅが５００未満のときに、ｊ／ｆ値の上昇割合は１．１５よりも大きくなる。このことから、レイノルズ数Ｒｅが５００未満のときに、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 Further, when the condition of a / A = 0.58 and 5 ° ≦ θ ≦ 45 ° is satisfied, when the Reynolds number Re is less than 500, the increase rate of the j / f value becomes larger than 1.15. . Therefore, when the Reynolds number Re is less than 500, the heat exchange performance can be suitably improved by satisfying the above condition.
（効果）
以上に述べたように、流路の側面が屈曲していると、流路内において主流に逆行するような流れ（渦）が発生し易くなり、この渦によって圧力損失が増大し、熱交換が妨げられる結果、熱交換性能が低下するという問題がある。そこで、本実施形態に係る熱交換器１においては、流路Ｒ１，Ｒ２の底面に複数の起伏部２２を形成することで、流路Ｒ１，Ｒ２の底面を流体の進行方向に沿って波状に起伏させている。すると、起伏部２２が流路面積を減少させるので、圧力損失が大きくなる傾向となるが、起伏部２２が渦の発達を抑制し、隣り合う屈曲部２１・２１間において渦が広範囲に生じ難くなるので、圧力損失が減少するとともに熱伝達特性が向上する。また、流路Ｒ１，Ｒ２の内面において境界層が形成され難くなるので、境界層の発達が抑制される。これにより、熱交換性能を向上させることができる。
(effect)
As described above, when the side surface of the flow path is bent, a flow (vortex) reverse to the main flow is likely to occur in the flow path, and this vortex increases pressure loss and heat exchange. As a result, the heat exchange performance is degraded. Therefore, in the heat exchanger 1 according to the present embodiment, by forming a plurality of undulating portions 22 on the bottom surfaces of the flow paths R1 and R2, the bottom surfaces of the flow paths R1 and R2 are waved along the fluid traveling direction. It is undulating. Then, since the undulating portion 22 reduces the flow path area, the pressure loss tends to increase. However, the undulating portion 22 suppresses the development of the vortex, and the vortex is not easily generated in a wide range between the adjacent bent portions 21 and 21. As a result, pressure loss is reduced and heat transfer characteristics are improved. Moreover, since it becomes difficult to form a boundary layer on the inner surfaces of the flow paths R1 and R2, the development of the boundary layer is suppressed. Thereby, heat exchange performance can be improved.
また、、起伏部２２の仰角と俯角とを同じにして、流体の流れをスムーズにすることで、渦の発達を抑制することができる。 Further, by making the elevation angle and depression angle of the undulating portion 22 the same and smoothing the flow of fluid, the development of vortices can be suppressed.
また、０．７２＜ａ／Ａ≦０．８５、且つ、５°≦θ≦２５°の条件を満足すると、熱伝達特性因子ｊの値を摩擦係数ｆの値で除した値が、起伏部を有しない蛇行した流路に対して、１．１５よりも大きい割合で上昇する。このことから、上記条件を満足させることで、熱交換性能を好適に向上させることができる。なお、上述したように、Ａは流路Ｒ１，Ｒ２の最下部から流路Ｒ１，Ｒ２の上面までの高さであり、ａは起伏部２２の頂点から流路Ｒ１，Ｒ２の上面までの高さであり、θは起伏部２２の仰角である。 When the conditions of 0.72 <a / A ≦ 0.85 and 5 ° ≦ θ ≦ 25 ° are satisfied, the value obtained by dividing the value of the heat transfer characteristic factor j by the value of the friction coefficient f is It rises at a rate larger than 1.15 with respect to the meandering flow path not having. From this, the heat exchange performance can be suitably improved by satisfying the above conditions. As described above, A is the height from the lowest part of the flow paths R1 and R2 to the upper surfaces of the flow paths R1 and R2, and a is the height from the top of the undulating portion 22 to the upper surfaces of the flow paths R1 and R2. And θ is the elevation angle of the undulating portion 22.
また、０．５８＜ａ／Ａ≦０．７２、且つ、５°≦θ≦３０°の条件を満足すると、熱伝達特性因子ｊの値を摩擦係数ｆの値で除した値が、起伏部を有しない蛇行した流路に対して、１．１５よりも大きい割合で上昇する。このことから、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 When the conditions of 0.58 <a / A ≦ 0.72 and 5 ° ≦ θ ≦ 30 ° are satisfied, the value obtained by dividing the value of the heat transfer characteristic factor j by the value of the friction coefficient f is It rises at a rate larger than 1.15 with respect to the meandering flow path not having. From this, the heat exchange performance can be suitably improved by satisfying the above conditions.
また、ａ／Ａ＝０．５８、且つ、５°≦θ≦４５°の条件を満足すると、レイノルズ数が５００未満のときに、熱伝達特性因子ｊの値を摩擦係数ｆの値で除した値が、起伏部を有しない蛇行した流路に対して、１．１５よりも大きい割合で上昇する。このことから、レイノルズ数が５００未満のときに、上記条件を満足させることで、熱交換性能を好適に向上させることができる。 When the condition of a / A = 0.58 and 5 ° ≦ θ ≦ 45 ° is satisfied, the value of the heat transfer characteristic factor j is divided by the value of the friction coefficient f when the Reynolds number is less than 500. The value rises at a rate greater than 1.15 for a serpentine channel having no undulations. From this, when the Reynolds number is less than 500, the heat exchange performance can be suitably improved by satisfying the above condition.
（本実施形態の変形例）
以上、本発明の実施形態を説明したが、具体例を例示したに過ぎず、特に本発明を限定するものではなく、具体的構成などは、適宜設計変更可能である。また、発明の実施の形態に記載された、作用及び効果は、本発明から生じる最も好適な作用及び効果を列挙したに過ぎず、本発明による作用及び効果は、本発明の実施の形態に記載されたものに限定されるものではない。
(Modification of this embodiment)
The embodiment of the present invention has been described above, but only specific examples are illustrated, and the present invention is not particularly limited, and the specific configuration and the like can be appropriately changed in design. Further, the actions and effects described in the embodiments of the invention only list the most preferable actions and effects resulting from the present invention, and the actions and effects according to the present invention are described in the embodiments of the present invention. It is not limited to what was done.
例えば、流路Ｒ１，Ｒ２の底面だけでなく、流路Ｒ１，Ｒ２の上面、即ち、一の金属薄板の上に積層された他の金属薄板の下面に複数の起伏部２２が形成されていてもよい。 For example, a plurality of undulations 22 are formed not only on the bottom surfaces of the flow paths R1 and R2, but also on the top surfaces of the flow paths R1 and R2, that is, the lower surfaces of other thin metal plates stacked on one thin metal plate. Also good.
１ 熱交換器
２ 本体
３ 第１供給ヘッダー
３ａ 供給管
４ 第１排出ヘッダー
４ａ 排出管
５ 第２供給ヘッダー
５ａ 供給管
６ 第２排出ヘッダー
６ａ 排出管
１０ 流路構成部材
１１ 第１金属薄板
１２ 第２金属薄板
２１ 屈曲部
２２ 起伏部
Ｒ１，Ｒ２ 流路
DESCRIPTION OF SYMBOLS 1 Heat exchanger 2 Main body 3 1st supply header 3a Supply pipe 4 1st discharge header 4a Discharge pipe 5 2nd supply header 5a Supply pipe 6 2nd discharge header 6a Discharge pipe 10 Flow path component 11 1st metal thin plate 12 1st 2 Metal thin plate 21 Bent part 22 Undulating part R1, R2 Flow path
Claims (5)
前記流路の側面には、前記流路が蛇行するように屈曲された屈曲部が複数形成されているとともに、前記流路の底面には、前記熱交換流体の進行方向に沿って波状に起伏された起伏部が複数形成されており、
隣り合う前記屈曲部間の間隔が、隣り合う前記起伏部間の間隔よりも大きいことを特徴とする熱交換器。 A heat exchanger that exchanges heat between a heat exchange fluid flowing in a flow path and a heat exchange target outside the flow path,
A plurality of bent portions that are bent so that the flow path meanders are formed on the side surface of the flow path, and the bottom surface of the flow path undulates along the traveling direction of the heat exchange fluid. A plurality of undulated portions formed,
A heat exchanger characterized in that an interval between adjacent bent portions is larger than an interval between adjacent undulating portions.
０．７２＜ａ／Ａ≦０．８５、且つ、５°≦θ≦２５°の条件を満足することを特徴とする請求項２に記載の熱交換器。 When the height from the lowest part of the flow path to the upper surface of the flow path is A, the height from the top of the undulation part to the upper surface of the flow path is a, and the elevation angle of the undulation part is θ,
The heat exchanger according to claim 2, wherein the conditions of 0.72 <a / A ≦ 0.85 and 5 ° ≦ θ ≦ 25 ° are satisfied.
０．５８＜ａ／Ａ≦０．７２、且つ、５°≦θ≦３０°の条件を満足することを特徴とする請求項２に記載の熱交換器。 When the height from the lowest part of the flow path to the upper surface of the flow path is A, the height from the top of the undulation part to the upper surface of the flow path is a, and the elevation angle of the undulation part is θ,
3. The heat exchanger according to claim 2, wherein the conditions of 0.58 <a / A ≦ 0.72 and 5 ° ≦ θ ≦ 30 ° are satisfied.
ａ／Ａ＝０．５８、且つ、５°≦θ≦４５°の条件を満足することを特徴とする請求項２に記載の熱交換器。
When the height from the lowest part of the flow path to the upper surface of the flow path is A, the height from the top of the undulation part to the upper surface of the flow path is a, and the elevation angle of the undulation part is θ,
The heat exchanger according to claim 2, wherein a / A = 0.58 and 5 ° ≦ θ ≦ 45 ° are satisfied.
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