JP2008064457A - Heat exchanger - Google Patents

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JP2008064457A
JP2008064457A JP2007307601A JP2007307601A JP2008064457A JP 2008064457 A JP2008064457 A JP 2008064457A JP 2007307601 A JP2007307601 A JP 2007307601A JP 2007307601 A JP2007307601 A JP 2007307601A JP 2008064457 A JP2008064457 A JP 2008064457A
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heat exchanger
heat transfer
transfer tube
fins
heat
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Ryuta Onishi
竜太 大西
Kazuhisa Mishiro
一寿 三代
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Sharp Corp
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Sharp Corp
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Abstract

<P>PROBLEM TO BE SOLVED: To provide a heat exchanger provided with an auxiliary heat exchanger and a main heat exchanger and capable of improving efficiency in heat exchange. <P>SOLUTION: This heat exchanger is provided with heat transfer tubes 2a-2f for flowing refrigerant therein, and diameter D<SB>1</SB>of each of the heat transfer tubes 2a, 2b of the auxiliary heat exchanger 10a is larger than diameter D<SB>2</SB>of each of the heat transfer tubes 2c-2f of the main heat exchanger 10b when using the heat exchanger as a condenser. The heat exchanger is further provided with a plurality of fins 1a coming into contact with the heat transfer tubes 2a, 2b and a plurality of fins 1b coming into contact with the heat transfer tubes 2c-2f. An interval E<SB>1</SB>between the fins 1a is larger than an interval E<SB>2</SB>between the fins 1b. The auxiliary heat exchanger 10a is in an excessively cooled region being the downstream side, mainly, in a region where refrigerant being a liquid flows when using the heat exchanger 1 as the condenser. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

本発明は、熱交換器に関し、より特定的には補助熱交換器と主熱交換器とを備えた熱交換器に関する。   The present invention relates to a heat exchanger, and more particularly to a heat exchanger including an auxiliary heat exchanger and a main heat exchanger.

近年、空気調和機の省エネルギ化の進行とともに、空気調和機に使用される熱交換器の高効率化が要求されている。熱交換器の高効率化を実現する構成として、過冷却用の補助熱交換器と主熱交換器とを備えた熱交換器がある。従来の補助熱交換器と主熱交換器とを備えた熱交換器が、たとえば特公昭６２−１３５７４号公報（特許文献１）に開示されている。特許文献１に開示された熱交換器は、たとえば以下のような構成を備えている。   In recent years, with the progress of energy saving in air conditioners, there has been a demand for higher efficiency of heat exchangers used in air conditioners. As a configuration for realizing high efficiency of the heat exchanger, there is a heat exchanger provided with an auxiliary heat exchanger for supercooling and a main heat exchanger. A heat exchanger provided with a conventional auxiliary heat exchanger and a main heat exchanger is disclosed in, for example, Japanese Patent Publication No. 62-13574 (Patent Document 1). The heat exchanger disclosed in Patent Document 1 has the following configuration, for example.

図１１は、従来の熱交換器の一の構成を示す側面図である。図１２は、従来の熱交換器の一の構成を示す斜視図である。   FIG. 11 is a side view showing one configuration of a conventional heat exchanger. FIG. 12 is a perspective view showing one configuration of a conventional heat exchanger.

図１１および図１２を参照して、熱交換器１１０は、補助熱交換器１１０ａと主熱交換器１１０ｂとを備えている。そして、矢印で示された空気の流れ方向１０６から空気が熱交換器１１０に送り込まれる。空気の流れ方向１０６に対して、補助熱交換器１１０ａは上流側（図１１中左側）に、主熱交換器１１０ｂは下流側（図１１中右側）に、互いに並列して配置されている。補助熱交換器１１０ａは、伝熱管１０２ａと、放熱のための複数のフィン１０１ａとを有している。伝熱管１０２ａは、直線部分１０９を含む蛇行状に延びるように形成されている。複数のフィン１０１ａは、この伝熱管１０２ａの直線部分１０９とほぼ直角になるように接触して配置されている。主熱交換器１１０ｂは、伝熱管１０２ｂ、１０２ｃと、放熱のための複数のフィン１０１ｂとを有しており、補助熱交換器１１０ａとほぼ同様の構成となっている。ここで、伝熱管１０２ａの直径は、伝熱管１０２ｂ、１０２ｃの直径よりも小さい。   Referring to FIGS. 11 and 12, the heat exchanger 110 includes an auxiliary heat exchanger 110a and a main heat exchanger 110b. Then, air is fed into the heat exchanger 110 from the air flow direction 106 indicated by the arrow. With respect to the air flow direction 106, the auxiliary heat exchanger 110a is arranged in parallel with each other on the upstream side (left side in FIG. 11) and the main heat exchanger 110b is arranged on the downstream side (right side in FIG. 11). The auxiliary heat exchanger 110a includes a heat transfer tube 102a and a plurality of fins 101a for heat dissipation. The heat transfer tube 102 a is formed to extend in a meandering manner including the straight portion 109. The plurality of fins 101a are arranged in contact with the straight portion 109 of the heat transfer tube 102a so as to be substantially perpendicular. The main heat exchanger 110b has heat transfer tubes 102b and 102c and a plurality of fins 101b for heat dissipation, and has substantially the same configuration as the auxiliary heat exchanger 110a. Here, the diameter of the heat transfer tube 102a is smaller than the diameter of the heat transfer tubes 102b and 102c.

このような熱交換器１１０に空気が送り込まれると、この空気と、伝熱管１０２ａ〜１０２ｃを流れる冷媒との間で熱交換が行われる。たとえば高温の気体となっている冷媒を冷却することにより液化する場合（凝縮器として使用する場合）を考える。この場合には、冷媒よりも相対的に温度の低い空気が流れ方向１０６に送り込まれている状態で、高温の気体となっている冷媒が出入り口１０７より流入する。流入した冷媒は、分岐部分１０４で伝熱管１０２ｂと伝熱管１０２ｃとの２方向に分流し、空気と熱交換して徐々に液化する。伝熱管１０２ｂ、１０２ｃの各々を流れる冷媒が液化して気液２相状態（気体と液体とが混ざった状態）となっているときには、冷媒の温度および圧力は一定に保たれている。そして、気液２相状態の冷媒は、分岐部分１０３で合流し、補助熱交換器１１０ａの伝熱管１０２ａを流れながら圧力一定の下で過冷却される。その結果、低温の液体の冷媒が出入り口１０５から流出する。   When air is sent into such a heat exchanger 110, heat exchange is performed between the air and the refrigerant flowing through the heat transfer tubes 102a to 102c. For example, consider a case where a refrigerant that is a high-temperature gas is liquefied by cooling (when used as a condenser). In this case, in a state where air having a temperature lower than that of the refrigerant is sent in the flow direction 106, the refrigerant that is a high-temperature gas flows in through the inlet / outlet 107. The refrigerant that has flowed in is branched into two directions, the heat transfer tube 102b and the heat transfer tube 102c, at the branch portion 104, and is gradually liquefied by exchanging heat with air. When the refrigerant flowing through each of the heat transfer tubes 102b and 102c is liquefied and is in a gas-liquid two-phase state (a state where gas and liquid are mixed), the temperature and pressure of the refrigerant are kept constant. The gas-liquid two-phase refrigerant merges at the branch portion 103 and is supercooled under a constant pressure while flowing through the heat transfer tube 102a of the auxiliary heat exchanger 110a. As a result, a low-temperature liquid refrigerant flows out from the doorway 105.

図１１および図１２に示す従来の熱交換器１１０においては、補助熱交換器１１０ａと主熱交換器１１０ｂとが分離されている。このため、熱交換器１１０を凝縮器として使用したとき、低温の液体冷媒で満たされる補助熱交換器１１０ａは主熱交換器１１０ｂと分離されているため、主熱交換器１１０ｂを高い温度に保つことができる。その結果、空気と熱交換器との温度差が大きくなるので、補助熱交換器１１０ａの熱交換効率（凝縮効率および蒸発効率）が向上する。また、補助熱交換器１１０ａの伝熱管１０２ａが細管（直径の小さい伝熱管）で構成されている。これにより、伝熱管１０２ａを流れる液体の冷媒の流速が増加し、液体の冷媒が伝熱管１０２ａの内壁全体に貼りついた状態で流れるようになる。その結果、補助熱交換器１１０ａの凝縮効率が向上されている。このように、伝熱管が細管で構成された熱交換器が、たとえば特開２００２−２５７４８３号公報（特許文献２）にも開示されている。特許文献２に開示された熱交換器は、たとえば以下のような構成を備えている。   In the conventional heat exchanger 110 shown in FIGS. 11 and 12, the auxiliary heat exchanger 110a and the main heat exchanger 110b are separated. For this reason, when the heat exchanger 110 is used as a condenser, the auxiliary heat exchanger 110a filled with the low-temperature liquid refrigerant is separated from the main heat exchanger 110b, so the main heat exchanger 110b is kept at a high temperature. be able to. As a result, the temperature difference between the air and the heat exchanger increases, so that the heat exchange efficiency (condensation efficiency and evaporation efficiency) of the auxiliary heat exchanger 110a is improved. Further, the heat transfer tube 102a of the auxiliary heat exchanger 110a is constituted by a thin tube (a heat transfer tube having a small diameter). As a result, the flow rate of the liquid refrigerant flowing through the heat transfer tube 102a increases, and the liquid refrigerant flows in a state of being attached to the entire inner wall of the heat transfer tube 102a. As a result, the condensation efficiency of the auxiliary heat exchanger 110a is improved. Thus, the heat exchanger with which the heat exchanger tube was comprised by the thin tube is also disclosed by Unexamined-Japanese-Patent No. 2002-257383 (patent document 2), for example. The heat exchanger disclosed in Patent Document 2 has the following configuration, for example.

図１３は、従来の熱交換器の他の構成を示す側面図である。
図１３を参照して、熱交換器１２０は、補助熱交換器１１０ａと主熱交換器１１０ｂとを備えている。主熱交換器１１０ｂは伝熱管１０２ｄ、１０２ｅを有している。伝熱管１０２ｄ、１０２ｅの各々は、補助熱交換器１１０ａの伝熱管１０２ｂ、１０２ｃと同様に細管で構成されている。 FIG. 13 is a side view showing another configuration of the conventional heat exchanger.
With reference to FIG. 13, the heat exchanger 120 includes an auxiliary heat exchanger 110a and a main heat exchanger 110b. The main heat exchanger 110b has heat transfer tubes 102d and 102e. Each of the heat transfer tubes 102d and 102e is configured by a thin tube, similar to the heat transfer tubes 102b and 102c of the auxiliary heat exchanger 110a.

なお、これ以外の構成は、図１１および図１２に示す従来の熱交換器の一の構成とほぼ同じであるため、同一の構成要素については同一の符号を付し、その説明を省略する。   In addition, since the structure of those other than this is as substantially the same as the structure of one of the conventional heat exchangers shown in FIG. 11 and FIG. 12, the same code | symbol is attached | subjected about the same component and the description is abbreviate | omitted.

図１３に示す従来の熱交換器１２０においては、主熱交換器１１０ｂの伝熱管１０２ｄ、１０２ｅも細管で構成されている。これにより、伝熱管１０２ｄ、１０２ｅを流れる気液２相流の冷媒の流速が増加し、液体の冷媒が攪拌されながら流れるようになる。その結果、さらに主熱交換器１１０ｂの熱交換効率が向上する。
特公昭６２−１３５７４号公報 特開２００２−２５７４８３号公報 In the conventional heat exchanger 120 shown in FIG. 13, the heat transfer tubes 102d and 102e of the main heat exchanger 110b are also constituted by thin tubes. As a result, the flow rate of the gas-liquid two-phase refrigerant flowing through the heat transfer tubes 102d and 102e increases, and the liquid refrigerant flows while being stirred. As a result, the heat exchange efficiency of the main heat exchanger 110b is further improved.
Japanese Examined Patent Publication No. 62-13574 JP 2002-257383 A

しかしながら、特許文献１に開示された熱交換器１１０および特許文献２に開示された熱交換器１２０においては、伝熱管１０２ａを流れる冷媒に生じる圧力損失が大きいという問題があった。ここで、圧力損失とは、流体が管内を流れる際に上流側と比較して下流側の圧力が低下するという現象である。圧力損失は、流体が流れる管の直径の大きさに反比例し、流体が流れる距離、すなわち流体が流れる管の長さに比例する。熱交換器１１０および熱交換器１２０において、補助熱交換器１１０ａの伝熱管１０２ａは１本の伝熱管により構成されており、分岐部分を有していない（小流路化している）。したがって、冷媒が流れる伝熱管の長さが長くなっている。また、補助熱交換器１１０ａの伝熱管１０２ａは細管であるので、管の直径が小さい。したがって、伝熱管１０２ａを流れる冷媒に生じる圧力損失は大きい。   However, the heat exchanger 110 disclosed in Patent Document 1 and the heat exchanger 120 disclosed in Patent Document 2 have a problem that the pressure loss generated in the refrigerant flowing through the heat transfer tube 102a is large. Here, the pressure loss is a phenomenon in which the pressure on the downstream side decreases as compared with the upstream side when the fluid flows in the pipe. The pressure loss is inversely proportional to the size of the diameter of the tube through which the fluid flows, and is proportional to the distance through which the fluid flows, that is, the length of the tube through which the fluid flows. In the heat exchanger 110 and the heat exchanger 120, the heat transfer tube 102a of the auxiliary heat exchanger 110a is configured by a single heat transfer tube, and does not have a branch portion (the flow path is reduced). Therefore, the length of the heat transfer tube through which the refrigerant flows is long. Further, since the heat transfer tube 102a of the auxiliary heat exchanger 110a is a thin tube, the diameter of the tube is small. Therefore, the pressure loss generated in the refrigerant flowing through the heat transfer tube 102a is large.

伝熱管１０２ａを流れる冷媒に生じる圧力損失が大きいと、特に、熱交換器１１０および熱交換器１２０を蒸発器として使用する場合に問題が生じる。すなわち、伝熱管１０２ａを流れる冷媒に生じる圧力損失が大きいと、冷媒の流れにおける上流側の圧力が上昇する。その結果、熱交換器１１０の平均温度が上昇し、空気と熱交換器１１０との温度差が小さくなるため、熱交換器１１０の蒸発効率（熱交換効率）が低下するという問題があった。   When the pressure loss generated in the refrigerant flowing through the heat transfer tube 102a is large, a problem arises particularly when the heat exchanger 110 and the heat exchanger 120 are used as an evaporator. That is, when the pressure loss generated in the refrigerant flowing through the heat transfer tube 102a is large, the upstream pressure in the refrigerant flow increases. As a result, the average temperature of the heat exchanger 110 is increased, and the temperature difference between the air and the heat exchanger 110 is reduced, so that the evaporation efficiency (heat exchange efficiency) of the heat exchanger 110 is reduced.

したがって、本発明の目的は、熱交換効率が高い熱交換器を提供することである。   Accordingly, an object of the present invention is to provide a heat exchanger with high heat exchange efficiency.

本発明の一の局面に従う熱交換器は、冷媒を流すための伝熱管を備える熱交換器であって、熱交換器を凝縮器として使用した場合に、下流側となる過冷却領域にある主に液体の前記冷媒が流れる領域の第１の伝熱管の直径は、前記熱交換器内の他の伝熱管である第２の伝熱管の直径より大きい。また熱交換器は、第１の伝熱管と接触する複数の第１のフィンと、第２の伝熱管と接触する複数の第２のフィンとをさらに備えている。第１のフィンの各々の間隔は、第２のフィンの各々の間隔よりも大きい。   A heat exchanger according to one aspect of the present invention is a heat exchanger that includes a heat transfer tube for flowing a refrigerant, and when the heat exchanger is used as a condenser, the heat exchanger is located in a subcooling region on the downstream side. The diameter of the first heat transfer tube in the region where the liquid refrigerant flows is larger than the diameter of the second heat transfer tube, which is another heat transfer tube in the heat exchanger. The heat exchanger further includes a plurality of first fins that contact the first heat transfer tube and a plurality of second fins that contact the second heat transfer tube. The distance between the first fins is greater than the distance between the second fins.

本発明の熱交換器によれば、過冷却領域にある主に液体の冷媒が流れる領域の伝熱管の直径が大きいので、過冷却領域にある主に液体の冷媒が流れる領域の伝熱管を流れる冷媒の圧力損失が抑止される。これにより、過冷却領域にある主に液体の冷媒が流れる領域の伝熱管および熱交換器内の他の伝熱管を流れる冷媒の圧力を一定に保つことができるので、熱交換器内の他の伝熱管における気液２層状態の冷媒が流れる部分の温度を一定に保つことができる。したがって、外気と、気液２層状態の冷媒が流れる伝熱管との温度差を大きく保つことができ、熱交換器を蒸発器として使用した場合の蒸発効率が高くなる。一方、熱交換器内の他の伝熱管の直径が小さいので、熱交換器を蒸発器および凝縮器として使用した場合に、熱交換器内の他の伝熱管を流れる気液２相状態の冷媒の流速が増加し、液体の冷媒が攪拌されながら流れるようになる。その結果、熱交換器内の他の伝熱管の蒸発効率および凝縮効率が高くなる。以上の理由により、熱交換器の熱交換効率が高くなる。   According to the heat exchanger of the present invention, since the diameter of the heat transfer tube in the region where mainly the liquid refrigerant flows in the supercooling region is large, it flows through the heat transfer tube in the region where mainly the liquid refrigerant flows in the supercooling region. The pressure loss of the refrigerant is suppressed. As a result, the pressure of the refrigerant flowing through the heat transfer tubes in the supercooling region where the liquid refrigerant mainly flows and the other heat transfer tubes in the heat exchanger can be kept constant. The temperature of the portion where the refrigerant in the gas-liquid two-layer state in the heat transfer tube flows can be kept constant. Therefore, a large temperature difference between the outside air and the heat transfer tube through which the gas-liquid two-layer refrigerant flows can be maintained, and the evaporation efficiency when the heat exchanger is used as an evaporator is increased. On the other hand, since the diameter of the other heat transfer tubes in the heat exchanger is small, when the heat exchanger is used as an evaporator and a condenser, a refrigerant in a gas-liquid two-phase state that flows through the other heat transfer tubes in the heat exchanger And the liquid refrigerant flows while being stirred. As a result, the evaporation efficiency and the condensation efficiency of the other heat transfer tubes in the heat exchanger are increased. For the above reasons, the heat exchange efficiency of the heat exchanger is increased.

加えて、複数の第１のフィンおよび複数の第２のフィンの各々により、第１の伝熱管および第２の伝熱管の各々の伝熱面積を大きくすることができる。したがって、熱交換器の熱交換効率を一層向上することができる。また、第１の伝熱管の複数の第１のフィンの間隔が広くなるので、外気の流れ方向からの気流が第１の伝熱管の複数の第１のフィンの隙間を通って第２の伝熱管の複数の第２のフィンに当たりやすくなる。すなわち、第１の伝熱管側の通風抵抗が減少する。したがって、第２の伝熱管側の熱交換効率を一層向上することができる。   In addition, the heat transfer area of each of the first heat transfer tube and the second heat transfer tube can be increased by each of the plurality of first fins and the plurality of second fins. Therefore, the heat exchange efficiency of the heat exchanger can be further improved. Moreover, since the space | interval of the several 1st fin of a 1st heat exchanger tube becomes wide, the airflow from the flow direction of external air passes through the clearance gap between the 1st fins of a 1st heat exchanger tube, and 2nd heat transfer. It becomes easy to hit the several 2nd fin of a heat tube. That is, the ventilation resistance on the first heat transfer tube side is reduced. Therefore, the heat exchange efficiency on the second heat transfer tube side can be further improved.

本発明の他の局面に従う熱交換器は、冷媒を流すための伝熱管を有する熱交換器であって、補助熱交換器と、空気の流れ方向に対して前記補助熱交換器よりも下流側に配置される主熱交換器とを備えている。補助熱交換器は、冷媒を流すための第１の伝熱管と、第１の伝熱管と接触する複数の第１のフィンとを有している。主熱交換器は、第１の伝熱管と接続された第２の伝熱管と、第２の伝熱管と接触する複数の第２のフィンとを有している。第１の伝熱管の直径は、第２の伝熱管の直径よりも大きく、かつ第１のフィンの各々の間隔は、第２のフィンの各々の間隔よりも大きい。   A heat exchanger according to another aspect of the present invention is a heat exchanger having a heat transfer tube for flowing a refrigerant, and is downstream of the auxiliary heat exchanger and the auxiliary heat exchanger with respect to the air flow direction. And a main heat exchanger. The auxiliary heat exchanger has a first heat transfer tube for flowing the refrigerant, and a plurality of first fins in contact with the first heat transfer tube. The main heat exchanger has a second heat transfer tube connected to the first heat transfer tube, and a plurality of second fins in contact with the second heat transfer tube. The diameter of the first heat transfer tube is larger than the diameter of the second heat transfer tube, and the distance between the first fins is larger than the distance between the second fins.

本発明の他の局面に従う熱交換器によれば、第１の伝熱管の直径が大きいので、第１の伝熱管を流れる冷媒の圧力損失が抑止される。その結果、第１の伝熱管および第２の伝熱管を流れる冷媒の圧力を一定に保つことができるので、主熱交換器の温度を一定に保つことができる。したがって、外気と主熱交換器との温度差を大きく保つことができ、熱交換器を蒸発器として使用した場合の蒸発効率が高くなる。一方、第２の伝熱管の直径が小さいので、熱交換器を蒸発器および凝縮器として使用した場合に、第２の伝熱管を流れる気液２相状態の冷媒の流速が増加し、液体の冷媒が攪拌されながら流れるようになる。その結果、主熱交換器の蒸発効率および凝縮効率が高くなる。以上の理由により、熱交換器の熱交換効率が高くなる。   According to the heat exchanger according to another aspect of the present invention, since the diameter of the first heat transfer tube is large, pressure loss of the refrigerant flowing through the first heat transfer tube is suppressed. As a result, since the pressure of the refrigerant flowing through the first heat transfer tube and the second heat transfer tube can be kept constant, the temperature of the main heat exchanger can be kept constant. Therefore, the temperature difference between the outside air and the main heat exchanger can be kept large, and the evaporation efficiency when the heat exchanger is used as an evaporator is increased. On the other hand, since the diameter of the second heat transfer tube is small, when the heat exchanger is used as an evaporator and a condenser, the flow rate of the gas-liquid two-phase refrigerant flowing through the second heat transfer tube increases, The refrigerant flows while being stirred. As a result, the evaporation efficiency and the condensation efficiency of the main heat exchanger are increased. For the above reasons, the heat exchange efficiency of the heat exchanger is increased.

加えて、複数の第１のフィンおよび複数の第２のフィンの各々により、第１の伝熱管および第２の伝熱管の各々の伝熱面積を大きくすることができる。したがって、熱交換器の熱交換効率を一層向上することができる。また、補助熱交換器の複数の第１のフィンの間隔が広くなるので、外気の流れ方向からの気流が補助熱交換器の複数の第１のフィンの隙間を通って主熱交換器の複数の第２のフィンに当たりやすくなる。すなわち、補助熱交換器の通風抵抗が減少する。したがって、主熱交換器の熱交換効率を一層向上することができる。   In addition, the heat transfer area of each of the first heat transfer tube and the second heat transfer tube can be increased by each of the plurality of first fins and the plurality of second fins. Therefore, the heat exchange efficiency of the heat exchanger can be further improved. Moreover, since the space | interval of the some 1st fin of an auxiliary heat exchanger becomes wide, the airflow from the flow direction of external air passes through the clearance gap between the some 1st fin of an auxiliary heat exchanger, and the plurality of main heat exchangers. It becomes easy to hit the second fin. That is, the ventilation resistance of the auxiliary heat exchanger is reduced. Therefore, the heat exchange efficiency of the main heat exchanger can be further improved.

なお、本明細書中において「補助熱交換器」とは、熱交換器を凝縮器として使用した場合に、過冷却領域にある液体の冷媒が流れる部分の熱交換器を意味しており、「主熱交換器」とは、熱交換器を凝縮器として使用した場合に、気液２相状態の冷媒および気体の冷媒が流れる部分の熱交換器を意味している。   In the present specification, the term “auxiliary heat exchanger” means a heat exchanger in a portion where a liquid refrigerant in the supercooling region flows when the heat exchanger is used as a condenser. The “main heat exchanger” means a heat exchanger in a portion where a gas-liquid two-phase refrigerant and a gas refrigerant flow when the heat exchanger is used as a condenser.

本発明の熱交換器において好ましくは、第１の伝熱管および第２の伝熱管の各々は、直線部分を含む蛇行状に延びるように形成され、第１の伝熱管における直線部分の各々の間隔は、第２の伝熱管における直線部分の各々の間隔よりも大きい。   Preferably, in the heat exchanger according to the present invention, each of the first heat transfer tube and the second heat transfer tube is formed to extend in a meandering manner including a straight portion, and a distance between each of the straight portions in the first heat transfer tube. Is larger than the interval between the straight portions of the second heat transfer tube.

これにより、第１の伝熱管の間隔が広くなるので、外気の流れ方向からの気流が蛇行した第１の伝熱管の隙間を通って第２の伝熱管に当たりやすくなる。すなわち、第１の伝熱管側（補助熱交換器）の通風抵抗が減少する。したがって、第２の伝熱管側（補助熱交換器）の熱交換効率を一層向上することができる。   Thereby, since the space | interval of a 1st heat exchanger tube becomes wide, it becomes easy to hit a 2nd heat exchanger tube through the clearance gap between the 1st heat exchanger tube where the airflow from the flow direction of external air meandered. That is, the ventilation resistance on the first heat transfer tube side (auxiliary heat exchanger) is reduced. Therefore, the heat exchange efficiency on the second heat transfer tube side (auxiliary heat exchanger) can be further improved.

本発明の熱交換器において好ましくは、第１のフィンの各々の厚さは、第２のフィンの各々の厚さよりも薄い。   In the heat exchanger according to the present invention, preferably, the thickness of each of the first fins is smaller than the thickness of each of the second fins.

これにより、第１の伝熱管（補助熱交換器）の複数の第１のフィンの間隔を広くしやすくなるので、外気の流れ方向からの気流が第１の伝熱管（補助熱交換器）の複数の第１のフィンの隙間を通って第２の伝熱管（主熱交換器）の複数の第２のフィンに当たりやすくなる。すなわち、第１の伝熱管側（補助熱交換器）の通風抵抗が減少する。したがって、第２の伝熱管側（主熱交換器）の熱交換効率を一層向上することができる。   Thereby, since it becomes easy to widen the space | interval of the several 1st fin of a 1st heat exchanger tube (auxiliary heat exchanger), the airflow from the flow direction of external air is a 1st heat exchanger tube (auxiliary heat exchanger). It becomes easy to hit the plurality of second fins of the second heat transfer tube (main heat exchanger) through the gaps of the plurality of first fins. That is, the ventilation resistance on the first heat transfer tube side (auxiliary heat exchanger) is reduced. Therefore, the heat exchange efficiency on the second heat transfer tube side (main heat exchanger) can be further improved.

本発明の熱交換器において好ましくは、第１のフィンの各々の幅は、第２のフィンの各々の幅よりも大きい。   In the heat exchanger according to the present invention, preferably, the width of each of the first fins is larger than the width of each of the second fins.

これにより、補助熱交換器における第１のフィンの伝熱面積が大きくなるので、より多くの外気と熱交換することができる。その結果、補助熱交換器の熱交換効率を改善することができる。特に熱交換器を凝縮器として使用する場合、補助熱交換器の第１の伝熱管には液体の冷媒が流れる。このため、補助熱交換器は、気液２相状態の冷媒が流れる主熱交換器と比較して、熱交換効率が低くなっている。したがって、特に熱交換器を凝縮器として使用する場合に、補助熱交換器の熱交換効率を大きく改善することができる。   Thereby, since the heat transfer area of the 1st fin in an auxiliary heat exchanger becomes large, it can exchange heat with more outside air. As a result, the heat exchange efficiency of the auxiliary heat exchanger can be improved. In particular, when the heat exchanger is used as a condenser, a liquid refrigerant flows through the first heat transfer tube of the auxiliary heat exchanger. For this reason, the auxiliary heat exchanger has a lower heat exchange efficiency than the main heat exchanger in which the gas-liquid two-phase refrigerant flows. Therefore, particularly when the heat exchanger is used as a condenser, the heat exchange efficiency of the auxiliary heat exchanger can be greatly improved.

本発明の熱交換器において好ましくは、第１の伝熱管を流れる冷媒が乱流化するように、第１の伝熱管は構成されている。   In the heat exchanger of the present invention, preferably, the first heat transfer tube is configured so that the refrigerant flowing through the first heat transfer tube is turbulent.

これにより、第１の伝熱管を流れる冷媒が攪拌され、冷媒の対流が促進される。したがって、補助熱交換器の熱交換効率が一層向上する。ここで、本発明の形態の熱交換器においては、第１の伝熱管の直径は第２の伝熱管の直径よりも大きいので、第１の伝熱管の直径を小さくし冷媒の流速を速くするという方法で、第１の伝熱管を流れる冷媒を攪拌することは難しい。したがって、冷媒の流速を速くするという方法の代わりに、第１の伝熱管を流れる冷媒が乱流化するように第１の伝熱管を構成することで、補助熱交換器の熱交換効率を高めることができる点で特に有効である。   Thereby, the refrigerant | coolant which flows through a 1st heat exchanger tube is stirred, and the convection of a refrigerant | coolant is accelerated | stimulated. Therefore, the heat exchange efficiency of the auxiliary heat exchanger is further improved. Here, in the heat exchanger according to the embodiment of the present invention, the diameter of the first heat transfer tube is larger than the diameter of the second heat transfer tube, so the diameter of the first heat transfer tube is reduced and the flow rate of the refrigerant is increased. Thus, it is difficult to stir the refrigerant flowing through the first heat transfer tube. Therefore, instead of the method of increasing the flow rate of the refrigerant, the heat exchange efficiency of the auxiliary heat exchanger is increased by configuring the first heat transfer tube so that the refrigerant flowing through the first heat transfer tube is turbulent. It is particularly effective in that it can be used.

本発明の熱交換器において好ましくは、第１のフィンの各々および第２のフィンの各々には起伏部が設けられており、第１のフィンの各々における単位面積当たりの起伏部の数は、第２のフィンの各々における単位面積当たりの起伏部の数よりも多い。   In the heat exchanger of the present invention, preferably, each of the first fins and each of the second fins is provided with undulations, and the number of undulations per unit area in each of the first fins is: More than the number of undulations per unit area in each of the second fins.

これにより、第１のフィンにおける起伏部の数が多くなるので、第１のフィンの各々の表面を通過する外気の気流が起伏部で乱されるようになり、第１のフィンの各々の表面から離れた部分に存在する外気を巻き込みながら外気が流れるようになる。その結果、第１のフィンの各々の表面を通過する外気と、第１のフィンの各々との温度差をより大きく保つことができる。また、起伏部の数が多くなることで第１のフィンの伝熱面積が増加する。したがって、補助熱交換器の熱交換効率を一層向上することができる。   Accordingly, since the number of undulations in the first fin increases, the airflow of the outside air passing through the surface of each of the first fins is disturbed by the undulations, and the surface of each of the first fins The outside air flows while entraining the outside air that exists in the part away from. As a result, the temperature difference between the outside air passing through the surface of each of the first fins and each of the first fins can be kept larger. Moreover, the heat-transfer area of a 1st fin increases because the number of undulation parts increases. Therefore, the heat exchange efficiency of the auxiliary heat exchanger can be further improved.

本発明の熱交換器において好ましくは、第１の伝熱管における冷媒が流れる経路の数は、第２の伝熱管における冷媒が流れる経路の数よりも少ない。   Preferably, in the heat exchanger of the present invention, the number of paths through which the refrigerant flows in the first heat transfer tube is smaller than the number of paths through which the refrigerant flows in the second heat transfer tube.

これにより、第１の伝熱管の分岐部分が少なくなるので、分岐した伝熱管ごとの冷媒の流量が不均一になる（偏流が生じる）ことが抑止される。なお、第１の伝熱管の分岐部分が少なくなれば、第１の伝熱管の長さが長くなるが、第１の伝熱管の直径は大きいので、第１の伝熱管を流れる冷媒の圧力損失は大きくならない。以上の理由から、第１の伝熱管における冷媒の圧力損失を抑止しながら、分岐した伝熱管ごとの冷媒の流量が不均一になることが抑止される。   Thereby, since the branch part of the 1st heat exchanger tube decreases, it is suppressed that the flow rate of the refrigerant | coolant for every branched heat exchanger tube becomes uneven (it produces a drift). If the first heat transfer tube has fewer branches, the length of the first heat transfer tube becomes longer. However, since the diameter of the first heat transfer tube is large, the pressure loss of the refrigerant flowing through the first heat transfer tube Will not grow. For the above reasons, the refrigerant flow rate for each branched heat transfer tube is suppressed from becoming non-uniform while suppressing the pressure loss of the refrigerant in the first heat transfer tube.

本発明の熱交換器によれば、過冷却領域にある主に液体の冷媒が流れる領域の伝熱管の直径が大きいので、過冷却領域にある主に液体の冷媒が流れる領域の伝熱管を流れる冷媒の圧力損失が抑止される。これにより、過冷却領域にある主に液体の冷媒が流れる領域の伝熱管および熱交換器内の他の伝熱管を流れる冷媒の圧力を一定に保つことができるので、熱交換器内の他の伝熱管における気液２層状態の冷媒が流れる部分の温度を一定に保つことができる。したがって、外気と、気液２層状態の冷媒が流れる伝熱管との温度差を大きく保つことができ、熱交換器を蒸発器として使用した場合の蒸発効率が高くなる。一方、熱交換器内の他の伝熱管の直径が小さいので、熱交換器を蒸発器および凝縮器として使用した場合に、熱交換器内の他の伝熱管を流れる気液２相状態の冷媒の流速が増加し、液体の冷媒が攪拌されながら流れるようになる。その結果、熱交換器内の他の伝熱管の蒸発効率および凝縮効率が高くなる。以上の理由により、熱交換器の熱交換効率が高くなる。   According to the heat exchanger of the present invention, since the diameter of the heat transfer tube in the region where mainly the liquid refrigerant flows in the supercooling region is large, it flows through the heat transfer tube in the region where mainly the liquid refrigerant flows in the supercooling region. The pressure loss of the refrigerant is suppressed. As a result, the pressure of the refrigerant flowing through the heat transfer tubes in the supercooling region where the liquid refrigerant mainly flows and the other heat transfer tubes in the heat exchanger can be kept constant. The temperature of the portion where the refrigerant in the gas-liquid two-layer state in the heat transfer tube flows can be kept constant. Therefore, a large temperature difference between the outside air and the heat transfer tube through which the gas-liquid two-layer refrigerant flows can be maintained, and the evaporation efficiency when the heat exchanger is used as an evaporator is increased. On the other hand, since the diameter of the other heat transfer tubes in the heat exchanger is small, when the heat exchanger is used as an evaporator and a condenser, a refrigerant in a gas-liquid two-phase state that flows through the other heat transfer tubes in the heat exchanger And the liquid refrigerant flows while being stirred. As a result, the evaporation efficiency and the condensation efficiency of the other heat transfer tubes in the heat exchanger are increased. For the above reasons, the heat exchange efficiency of the heat exchanger is increased.

加えて、複数の第１のフィンおよび複数の第２のフィンの各々により、第１の伝熱管および第２の伝熱管の各々の伝熱面積を大きくすることができる。したがって、熱交換器の熱交換効率を一層向上することができる。また、第１の伝熱管側（補助熱交換器）の複数の第１のフィンの間隔が広くなるので、外気の流れ方向からの気流が第１の伝熱管側（補助熱交換器）の複数の第１のフィンの隙間を通って第２の伝熱管側（主熱交換器）の複数の第２のフィンに当たりやすくなる。すなわち、第１の伝熱管側（補助熱交換器）の通風抵抗が減少する。したがって、第２の伝熱管側（主熱交換器）の熱交換効率を一層向上することができる。   In addition, the heat transfer area of each of the first heat transfer tube and the second heat transfer tube can be increased by each of the plurality of first fins and the plurality of second fins. Therefore, the heat exchange efficiency of the heat exchanger can be further improved. Moreover, since the space | interval of the some 1st fin on the 1st heat exchanger tube side (auxiliary heat exchanger) becomes wide, the airflow from the flow direction of external air is the plurality on the 1st heat exchanger tube side (auxiliary heat exchanger). It becomes easy to hit the 2nd fin of the 2nd heat exchanger tube side (main heat exchanger) through the crevice of the 1st fin. That is, the ventilation resistance on the first heat transfer tube side (auxiliary heat exchanger) is reduced. Therefore, the heat exchange efficiency on the second heat transfer tube side (main heat exchanger) can be further improved.

以下、本発明の実施の形態について、図に基づいて説明する。
（実施の形態１）
図１は、本発明の実施の形態１における熱交換器の構成を示す正面図である。図２は本発明の実施の形態１における熱交換器の構成を示す斜視図である。 Hereinafter, embodiments of the present invention will be described with reference to the drawings.
(Embodiment 1)
FIG. 1 is a front view showing the configuration of the heat exchanger according to Embodiment 1 of the present invention. FIG. 2 is a perspective view showing the configuration of the heat exchanger according to Embodiment 1 of the present invention.

図１および図２を参照して、本実施の形態における熱交換器１０は、補助熱交換器１０ａと主熱交換器１０ｂとを備えている。そして、矢印で示された空気の流れ方向６から空気が熱交換器１０に送り込まれる。空気の流れ方向６に対して、補助熱交換器１０ａは上流側（図１中左側）に、主熱交換器１０ｂは下流側（図１中右側）に、互いに並列して配置されている。   With reference to FIG. 1 and FIG. 2, the heat exchanger 10 in this Embodiment is provided with the auxiliary | assistant heat exchanger 10a and the main heat exchanger 10b. Then, air is fed into the heat exchanger 10 from the air flow direction 6 indicated by the arrow. With respect to the air flow direction 6, the auxiliary heat exchanger 10a is arranged in parallel with each other on the upstream side (left side in FIG. 1) and the main heat exchanger 10b is arranged on the downstream side (right side in FIG. 1).

補助熱交換器１０ａは、伝熱管２ａ、２ｂ（第１の伝熱管）と、複数のフィン１ａ（第１のフィン）とを有している。伝熱管２ａ、２ｂの各々は直線部分１３ａ、１３ｂを含む蛇行状に延びるように形成されていて、複数のフィン１ａは等間隔に配置されている。伝熱管２ａ、２ｂの各々の直線部分が複数のフィン１ａを略直角に貫通することにより、伝熱管２ａ、２ｂと複数のフィン１ａとが接触している。伝熱管２ａ、２ｂは、分岐部分３ａで結合して出入り口５に接続されている。   The auxiliary heat exchanger 10a includes heat transfer tubes 2a and 2b (first heat transfer tubes) and a plurality of fins 1a (first fins). Each of the heat transfer tubes 2a, 2b is formed to extend in a meandering manner including the straight portions 13a, 13b, and the plurality of fins 1a are arranged at equal intervals. The respective straight portions of the heat transfer tubes 2a and 2b penetrate the plurality of fins 1a at substantially right angles, so that the heat transfer tubes 2a and 2b and the plurality of fins 1a are in contact with each other. The heat transfer tubes 2 a and 2 b are connected to the entrance / exit 5 by being joined at the branch portion 3 a.

主熱交換器１０ｂは、伝熱管２ｃ〜２ｆ（第２の伝熱管）と、複数のフィン１ｂ（第２のフィン）とを有している。伝熱管２ｃ〜２ｆの各々は直線部分を含む蛇行状に延びるように形成されていて、複数のフィン１ｂは等間隔に配置されている。伝熱管２ｃ〜２ｆの各々の直線部分が複数のフィン１ｂを略直角に貫通することにより、伝熱管２ｃ〜２ｆと複数のフィン１ｂとが接触している。伝熱管２ｃ、２ｄは、分岐部分３ｂで結合して伝熱管２ａと接続されている。また、伝熱管２ｃ、２ｄは、分岐部分４ａで結合して接続管９ａと接続されている。伝熱管２ｅ、２ｆは、分岐部分３ｃで結合して伝熱管２ｂと接続されている。また、伝熱管２ｅ、２ｆは、分岐部分４ｂで結合して接続管９ｂと接続されている。接続管９ａ、９ｂは、分岐部分４ｃで結合して出入り口７に接続されている。   The main heat exchanger 10b has heat transfer tubes 2c to 2f (second heat transfer tubes) and a plurality of fins 1b (second fins). Each of the heat transfer tubes 2c to 2f is formed to extend in a meandering manner including a straight portion, and the plurality of fins 1b are arranged at equal intervals. Each of the straight portions of the heat transfer tubes 2c to 2f penetrates the plurality of fins 1b substantially at right angles, so that the heat transfer tubes 2c to 2f and the plurality of fins 1b are in contact with each other. The heat transfer tubes 2c and 2d are connected at the branch portion 3b and connected to the heat transfer tube 2a. Further, the heat transfer tubes 2c and 2d are joined at the branch portion 4a and connected to the connection tube 9a. The heat transfer tubes 2e and 2f are connected at the branch portion 3c and connected to the heat transfer tube 2b. Further, the heat transfer tubes 2e and 2f are coupled to each other at the branch portion 4b and connected to the connection tube 9b. The connecting pipes 9a and 9b are connected to the entrance / exit 7 by being joined at the branch portion 4c.

本実施の形態の熱交換器１０においては、補助熱交換器１０ａの伝熱管２ａ、２ｂの各々の直径Ｄ1は、主熱交換器１０ｂの伝熱管２ｃ〜２ｆの各々の直径Ｄ2よりも大きい。具体的には、伝熱管２ａ、２ｂの各々の直径Ｄ1はたとえば７ｍｍであり、伝熱管２ｃ〜２ｆの各々の直径Ｄ2はたとえば５ｍｍである。 In the heat exchanger 10 of the present embodiment, the heat transfer tube 2a of the auxiliary heat exchanger 10a, each of the diameter D 1 of the 2b, rather than each diameter D 2 of the heat transfer tube 2c~2f of the main heat exchanger 10b large. Specifically, the heat transfer tube 2a, each of the diameter D 1 of the 2b is 7mm for example, the diameter D 2 of each of the heat transfer tube 2c~2f is 5mm example.

続いて、本実施の形態の熱交換器１０における冷媒の流れについて説明する。
熱交換器１０が空気調和機の蒸発器として使用される場合には、まず、低温の液体の冷媒が出入り口５より流入し、分岐部分３ａで伝熱管２ａと伝熱管２ｂとの２方向に分流する。液体の冷媒は、伝熱管２ａ、２ｂの各々を流れながら、空気の流れ方向６から送り込まれる空気と熱交換を行なう。その結果、冷媒の温度が上昇し、冷媒は蒸発し始める。ここで、本実施の形態の伝熱管２ａ、２ｂの各々の直径Ｄ1は大きいので、伝熱管２ａ、２ｂを流れる冷媒に生じる圧力損失は抑止される。次に、気液２相状態の冷媒が伝熱管２ａ、２ｂの各々を経て、主熱交換器１０ｂの分岐部分３ｂ、３ｃの各々へ流れ込む。伝熱管２ａを流れる冷媒は分岐部分３ｂでさらに２方向に分流し、主熱交換器１０ｂの伝熱管２ｃ、２ｄの各々を流れる。また、伝熱管２ｂを流れる冷媒は分岐部分３ｃでさらに２方向に分流し、主熱交換器１０ｂの伝熱管２ｅ、２ｆの各々を流れる。冷媒は、伝熱管２ｃ〜２ｆの各々を流れながら、空気の流れ方向６から送り込まれる空気と熱交換を行ない、気体の割合を増加させる（乾き度を進行させる）。ここで、伝熱管２ｃ〜２ｆの各々を流れる冷媒が気液２相状態となっているときには、冷媒の温度および圧力は一定に保たれている。その後、伝熱管２ｃ、２ｄを流れる冷媒は、主熱交換器１０ｂの分岐部分４ａで合流し、接続管９ａ内を流れる。また、伝熱管２ｅ、２ｆを流れる冷媒は、主熱交換器１０ｂの分岐部分４ｂで合流し、接続管９ｂ内を流れる。そして、接続管９ａ、９ｂの各々を流れる冷媒は、分岐部分４ｃで合流し、出入り口７から高温の気体となって流出する。 Subsequently, the flow of the refrigerant in the heat exchanger 10 of the present embodiment will be described.
When the heat exchanger 10 is used as an evaporator of an air conditioner, first, a low-temperature liquid refrigerant flows in from the inlet / outlet 5 and splits in two directions of the heat transfer tube 2a and the heat transfer tube 2b at the branch portion 3a. To do. The liquid refrigerant exchanges heat with the air fed from the air flow direction 6 while flowing through each of the heat transfer tubes 2a and 2b. As a result, the temperature of the refrigerant rises and the refrigerant starts to evaporate. Here, the heat transfer tube 2a of the present embodiment, since each of the diameter D 1 of the 2b is large, the pressure loss generated in the refrigerant flowing through the heat transfer tubes 2a, 2b is suppressed. Next, the gas-liquid two-phase refrigerant flows into each of the branch portions 3b and 3c of the main heat exchanger 10b through each of the heat transfer tubes 2a and 2b. The refrigerant flowing through the heat transfer tube 2a is further divided into two directions at the branch portion 3b, and flows through each of the heat transfer tubes 2c and 2d of the main heat exchanger 10b. Further, the refrigerant flowing through the heat transfer tube 2b is further divided into two directions at the branch portion 3c, and flows through each of the heat transfer tubes 2e and 2f of the main heat exchanger 10b. While flowing through each of the heat transfer tubes 2c to 2f, the refrigerant exchanges heat with the air fed from the air flow direction 6 to increase the gas ratio (advance the dryness). Here, when the refrigerant flowing through each of the heat transfer tubes 2c to 2f is in a gas-liquid two-phase state, the temperature and pressure of the refrigerant are kept constant. Thereafter, the refrigerant flowing through the heat transfer tubes 2c and 2d joins at the branch portion 4a of the main heat exchanger 10b and flows through the connection tube 9a. Moreover, the refrigerant | coolant which flows through the heat exchanger tubes 2e and 2f merges in the branch part 4b of the main heat exchanger 10b, and flows through the inside of the connection pipe 9b. And the refrigerant | coolant which flows through each of the connecting pipes 9a and 9b merges in the branch part 4c, and flows out from the entrance / exit 7 as high temperature gas.

一方、熱交換器１０が空気調和機の凝縮器として使用される場合には、まず、高温の気体の冷媒が出入り口７より流入し、分岐部分４ｃで接続管９ａと接続管９ｂとの２方向に分流する。そして、冷媒は接続管９ａ、９ｂの各々を経て、主熱交換器１０ｂの分岐部分４ａ、４ｂの各々へ流れ込む。接続管９ａを流れる冷媒は、分岐部分４ａでさらに２方向に分流し、主熱交換器１０ｂの伝熱管２ｃ、２ｄの各々を流れる。また、接続管９ｂを流れる冷媒は、分岐部分４ｂでさらに２方向に分流し、主熱交換器１０ｂの伝熱管２ｅ、２ｆの各々を流れる。冷媒は、伝熱管２ｃ〜２ｆの各々を流れながら、空気の流れ方向６から送り込まれる空気と熱交換を行なう。その結果、冷媒の温度が低下し、冷媒は徐々に液化する。ここで、冷媒が液化し始めてからが全て液化するまでの気液２相状態の間、冷媒の温度および圧力は一定に保たれている。また、伝熱管２ｃ〜２ｆの直径Ｄ2は小さい（細管で構成されている）ので、伝熱管２ｃ〜２ｆの各々を流れる冷媒の流速が増加し、液体の冷媒が攪拌されながら流れるようになる。その結果、主熱交換器１１０ｂの熱交換効率は高くなっている。その後、伝熱管２ｃ、２ｄの各々を流れる冷媒は、分岐部分３ｂで合流し、補助熱交換器１０ａの伝熱管２ａへ流れ込む。また、伝熱管２ｅ、２ｆの各々を流れる冷媒は、分岐部分３ｃで合流し、補助熱交換器１０ａの伝熱管２ｂへ流れ込む。このとき、冷媒はほぼ液体となっている。補助熱交換器１０ａの伝熱管２ａ、２ｂの各々を流れる冷媒は、空気の流れ方向６から送り込まれる空気と熱交換を行なうことにより過冷却される。そして、伝熱管２ａ、２ｂの各々を流れる冷媒は、分岐部分３ａで合流し、低温の液体の冷媒が出入り口５から流出する。 On the other hand, when the heat exchanger 10 is used as a condenser of an air conditioner, first, a high-temperature gaseous refrigerant flows in from the inlet / outlet 7, and in two directions of the connecting pipe 9a and the connecting pipe 9b at the branching portion 4c. Divide into And a refrigerant | coolant flows in each of the branch parts 4a and 4b of the main heat exchanger 10b through each of the connection pipes 9a and 9b. The refrigerant flowing through the connection pipe 9a is further divided into two directions at the branch portion 4a, and flows through each of the heat transfer pipes 2c and 2d of the main heat exchanger 10b. The refrigerant flowing through the connection pipe 9b is further divided into two directions at the branch portion 4b and flows through the heat transfer pipes 2e and 2f of the main heat exchanger 10b. The refrigerant exchanges heat with air fed from the air flow direction 6 while flowing through each of the heat transfer tubes 2c to 2f. As a result, the temperature of the refrigerant decreases and the refrigerant gradually liquefies. Here, the temperature and the pressure of the refrigerant are kept constant during the gas-liquid two-phase state from when the refrigerant starts to liquefy until it completely liquefies. Further, since the diameter D 2 of the heat transfer tube 2C～2f is small (consisting of tubules), increases the flow velocity of the refrigerant flowing through each of the heat transfer tube 2C～2f, refrigerant liquid to flow while being stirred . As a result, the heat exchange efficiency of the main heat exchanger 110b is high. Thereafter, the refrigerant flowing through each of the heat transfer tubes 2c and 2d merges at the branch portion 3b and flows into the heat transfer tube 2a of the auxiliary heat exchanger 10a. Moreover, the refrigerant | coolant which flows through each of the heat exchanger tubes 2e and 2f merges in the branch part 3c, and flows into the heat exchanger tube 2b of the auxiliary heat exchanger 10a. At this time, the refrigerant is almost liquid. The refrigerant flowing through each of the heat transfer tubes 2a and 2b of the auxiliary heat exchanger 10a is supercooled by exchanging heat with air fed from the air flow direction 6. The refrigerant flowing through each of the heat transfer tubes 2 a and 2 b merges at the branch portion 3 a, and a low-temperature liquid refrigerant flows out from the entrance / exit 5.

本実施の形態の熱交換器１０によれば、伝熱管２ａ、２ｂの直径Ｄ1が大きいので、伝熱管２ａ、２ｂを流れる冷媒の圧力損失が抑止される。これにより、伝熱管２ａ、２ｂおよび伝熱管２ｃ〜２ｆを流れる冷媒の圧力を一定に保つことができるので、主熱交換器１０ｂの温度を一定に保つことができる。したがって、空気と主熱交換器１０ｂとの温度差を大きく保つことができ、熱交換器１０を蒸発器として使用した場合の蒸発効率が高くなる。一方、伝熱管２ｃ〜２ｆの直径Ｄ2が小さいので、熱交換器１０を蒸発器および凝縮器として使用した場合に、伝熱管２ｃ〜２ｆを流れる気液２相流の冷媒の流速が増加し、液体の冷媒が攪拌されながら流れるようになる。その結果、主熱交換器１０ｂの蒸発効率および凝縮効率が高くなる。以上の理由により、熱交換器の熱交換効率が高くなる。 According to the heat exchanger 10 of the present embodiment, since the heat transfer tube 2a, a large diameter D 1 of the 2b, the pressure loss of the refrigerant flowing through the heat transfer tubes 2a, 2b is suppressed. Thereby, since the pressure of the refrigerant flowing through the heat transfer tubes 2a and 2b and the heat transfer tubes 2c to 2f can be kept constant, the temperature of the main heat exchanger 10b can be kept constant. Accordingly, the temperature difference between the air and the main heat exchanger 10b can be kept large, and the evaporation efficiency when the heat exchanger 10 is used as an evaporator is increased. On the other hand, the diameter D 2 of the heat transfer tube 2c~2f small, when using a heat exchanger 10 as an evaporator and condenser, the flow rate of refrigerant in the gas-liquid two-phase flow flowing in the heat transfer tube 2c~2f increased The liquid refrigerant flows while being stirred. As a result, the evaporation efficiency and the condensation efficiency of the main heat exchanger 10b are increased. For the above reasons, the heat exchange efficiency of the heat exchanger is increased.

なお、本実施の形態においては、熱交換器の構成が図１に示す構成である場合について示したが、本発明はこのような場合に限定されるものではなく、補助熱交換器の第１の伝熱管の直径が主熱交換器の第２の熱交換器の直径よりも大きければよい。さらに、熱交換器を凝縮器として使用した場合に下流側となる過冷却領域にある主に液体の冷媒が流れる領域の伝熱管の直径が、熱交換器内の他の伝熱管の直径より大きければよい。すなわち、分岐部分の数や位置、伝熱管の管路やフィンの形状などについてはどのような構成であってもよい。   In the present embodiment, the case where the configuration of the heat exchanger is the configuration shown in FIG. 1 is shown, but the present invention is not limited to such a case, and the first of the auxiliary heat exchangers The diameter of the heat transfer tube should be larger than the diameter of the second heat exchanger of the main heat exchanger. Furthermore, when the heat exchanger is used as a condenser, the diameter of the heat transfer tube in the region where the liquid refrigerant mainly flows in the supercooling region on the downstream side should be larger than the diameter of the other heat transfer tubes in the heat exchanger. That's fine. In other words, any configuration may be used for the number and position of the branch portions, the shape of the pipes and fins of the heat transfer tubes, and the like.

（実施の形態２）
図３は、本発明の実施の形態２における熱交換器の構成を示す正面図である。図４（ａ）は、本発明の実施の形態２における補助熱交換器の構成を示す側面図であり、図４（ｂ）は、本発明の実施の形態２における主熱交換器の構成を示す側面図である。 (Embodiment 2)
FIG. 3 is a front view showing the configuration of the heat exchanger according to Embodiment 2 of the present invention. FIG. 4 (a) is a side view showing the configuration of the auxiliary heat exchanger according to Embodiment 2 of the present invention, and FIG. 4 (b) shows the configuration of the main heat exchanger according to Embodiment 2 of the present invention. FIG.

図３および図４（ａ）、（ｂ）を参照して、本実施の形態における熱交換器１０において、蛇行状に延びた伝熱管２ａ、２ｂの直線部分１３ａの各々は、距離Ｌ1の間隔で配置されている。また、蛇行状に延びた伝熱管２ｃ〜２ｆの直線部分１３ｂの各々は、距離Ｌ2の間隔で配置されている。ここで、直線部分１３ａ、１３ｂの各々の間隔（距離Ｌ1および距離Ｌ2）は、空気の流れ方向６に対して垂直な方向の距離で規定されている。すなわち、図４（ａ）、（ｂ）において、空気の流れ方向６は紙面に垂直な方向となっているので、直線部分１３ａの各々の間隔（距離Ｌ1）および直線部分１３ｂの各々の間隔（距離Ｌ2）は、直線部分１３ａおよび直線部分１３ｂの各々における紙面上での間隔で規定されている。直線部分１３ａの各々の間隔（距離Ｌ1）は、直線部分１３ｂの各々の間隔（距離Ｌ2）よりも大きい。すなわち、距離Ｌ1はたとえば１９ｍｍであり、距離Ｌ2はたとえば１７ｍｍである。 3 and 4 (a) and 4 (b), in heat exchanger 10 in the present embodiment, each of straight portions 13a of heat transfer tubes 2a and 2b extending in a meandering manner has a distance L 1 . Arranged at intervals. Also, each of the straight portions 13b of the heat transfer tube 2c~2f extending in meandering shape, are arranged at intervals of a distance L 2. Here, the distance (distance L 1 and distance L 2 ) between the straight portions 13 a and 13 b is defined by a distance in a direction perpendicular to the air flow direction 6. That is, in FIGS. 4A and 4B, since the air flow direction 6 is a direction perpendicular to the paper surface, the distance between the straight portions 13a (distance L 1 ) and the distance between the straight portions 13b. (Distance L 2 ) is defined by the interval on the paper surface in each of the straight line portion 13a and the straight line portion 13b. Each interval (distance L 1 ) of the straight line portions 13a is larger than each interval (distance L 2 ) of the straight line portions 13b. That is, the distance L 1 is 19 mm, for example, and the distance L 2 is 17 mm, for example.

なお、これ以外の構成は、図１および図２に示す実施の形態１の構成とほぼ同じであるため、同一の構成要素については同一の符号を付し、その説明を省略する。   Since the other configuration is substantially the same as the configuration of the first embodiment shown in FIGS. 1 and 2, the same components are denoted by the same reference numerals and the description thereof is omitted.

本実施の形態の熱交換器１０において、伝熱管２ａ、２ｂおよび伝熱管２ｃ〜２ｆの各々は、直線部分１３ａ、１３ｂを含む蛇行状に延びるように形成されていて、伝熱管２ａ、２ｂにおける直線部分１３ａの各々の間隔（距離Ｌ1）は、伝熱管２ｃ〜２ｆにおける直線部分１３ｂの各々の間隔（距離Ｌ2）よりも大きい。 In heat exchanger 10 of the present embodiment, each of heat transfer tubes 2a and 2b and heat transfer tubes 2c to 2f is formed to extend in a meandering manner including straight portions 13a and 13b, and in heat transfer tubes 2a and 2b, Each interval (distance L 1 ) of the linear portions 13a is larger than each interval (distance L 2 ) of the linear portions 13b in the heat transfer tubes 2c to 2f.

これにより、補助熱交換器１０ａの伝熱管２ａ、２ｂの間隔が広くなるので、空気の流れ方向６からの気流が補助熱交換器１０ａの伝熱管２ａ、２ｂの隙間を通って主熱交換器１０ｂの伝熱管２ｃ〜２ｆに当たりやすくなる。すなわち、補助熱交換器１０ａの通風抵抗が減少する。したがって、主熱交換器１０ｂの熱交換効率を一層向上することができる。   Thereby, since the space | interval of the heat exchanger tubes 2a and 2b of the auxiliary heat exchanger 10a becomes wide, the airflow from the air flow direction 6 passes through the clearance between the heat exchanger tubes 2a and 2b of the auxiliary heat exchanger 10a, and the main heat exchanger It becomes easy to hit the heat transfer tubes 2c to 2f of 10b. That is, the ventilation resistance of the auxiliary heat exchanger 10a is reduced. Therefore, the heat exchange efficiency of the main heat exchanger 10b can be further improved.

なお、本実施の形態においては、伝熱管２ａ、２ｂの直線部分１３ａおよび伝熱管２ｃ〜２ｆの直線部分１３ｂが全て等間隔で配置されている場合について示した。しかしながら、本発明はこのような場合に限定されるものではなく、直線部分１３ａおよび直線部分１３ｂの各々の間隔が部分的に異なっていてもよい。この場合には、直線部分１３ａの各々のうち最も間隔が狭い部分の距離Ｌ1が、直線部分１３ｂの各々のうち最も間隔が広い部分の距離Ｌ2よりも大きければよい。 In addition, in this Embodiment, it showed about the case where the linear part 13a of the heat exchanger tubes 2a and 2b and the linear part 13b of the heat exchanger tubes 2c-2f are all arrange | positioned at equal intervals. However, the present invention is not limited to such a case, and the intervals between the straight portion 13a and the straight portion 13b may be partially different. In this case, it is only necessary that the distance L 1 of the portion with the narrowest interval among the straight portions 13a is larger than the distance L 2 of the portion with the widest intervals among the straight portions 13b.

（実施の形態３）
図５は、本発明の実施の形態３における熱交換器の一部の構成を示す上部平面図である。図６（ａ）は、図５におけるＡ部の拡大図、図６（ｂ）は、図５におけるＢ部の拡大図である。 (Embodiment 3)
FIG. 5 is a top plan view showing a partial configuration of the heat exchanger according to Embodiment 3 of the present invention. 6A is an enlarged view of a portion A in FIG. 5, and FIG. 6B is an enlarged view of a portion B in FIG.

図５を参照して、補助熱交換器１０ａにおける複数のフィン１ａの各々は、距離Ｅ1の間隔で等間隔に配置されている。主熱交換器１０ｂにおける複数のフィン１ｂの各々は、距離Ｅ2の間隔で等間隔に配置されている。複数のフィン１ａの各々の間隔（距離Ｅ1）は、複数のフィン１ｂの各々の間隔（距離Ｅ2）よりも大きい。すなわち、距離Ｅ1はたとえば１．４９ｍｍであり、距離Ｅ2はたとえば１．１５ｍｍである。 Referring to FIG. 5, each of the plurality of fins 1 a in the auxiliary heat exchanger 10 a is arranged at equal intervals with a distance E 1 . Each of the plurality of fins 1b in the main heat exchanger 10b is arranged at equal intervals of a distance E 2. The intervals (distance E 1 ) between the plurality of fins 1a are larger than the intervals (distance E 2 ) between the plurality of fins 1b. That is, the distance E 1 is 1.49mm for example, the distance E 2 is 1.15mm, for example.

また、補助熱交換器１０ａにおける複数のフィン１ａの各々は、幅Ｐ1を有している。主熱交換器１０ｂにおける複数のフィン１ｂの各々は、幅Ｐ2を有している。ここで、本明細書中において、複数のフィン１ａの幅（長さＰ1）および複数のフィン１ｂの幅（長さＰ2）は、伝熱管１本当たりが有するフィンの幅（図中縦方向の長さ）として規定されている。すなわち、複数のフィン１ｂの各々は、元々幅Ｐ3を有している。また、複数のフィン１ｂにおいては、幅方向に２本の伝熱管が配置されている。以上のことから、複数のフィン１ｂにおいて、伝熱管２ｃ〜２ｆの各々は幅Ｐ3の２分の１の幅、すなわち幅Ｐ2を有していると規定されている。複数のフィン１ａの各々の幅Ｐ1は、複数のフィン１ｂの各々の幅Ｐ2よりも長い。すなわち、幅Ｐ1はたとえば１１ｍｍであり、幅Ｐ2はたとえば１０ｍｍである。 Further, each of the plurality of fins 1a in the auxiliary heat exchanger 10a has a width P 1. Each of the plurality of fins 1b in the main heat exchanger 10b has a width P 2. Here, in the present specification, the width (length P 1 ) of the plurality of fins 1 a and the width (length P 2 ) of the plurality of fins 1 b are the widths of the fins per one heat transfer tube (vertical in the figure). Length of direction). That is, each of the plurality of fins 1b are originally has a width P 3. In the plurality of fins 1b, two heat transfer tubes are arranged in the width direction. From the above, a plurality of fins 1b, each of the heat transfer tube 2c~2f is defined to have one-half width of P3, i.e., the width P 2. The width P 1 of each of the plurality of fins 1a is longer than the width P 2 of each of the plurality of fins 1b. That is, the width P 1 is, for example, 11 mm, and the width P 2 is, for example, 10 mm.

図６（ａ）、（ｂ）を参照して、複数のフィン１ａの各々の厚さ（厚さＦ1）は、複数のフィン１ｂの各々の厚さ（厚さＦ2）よりも薄い。すなわち、厚さＦ1はたとえば０．１ｍｍであり、厚さＦ2はたとえば０．１１ｍｍである。 Referring to FIGS. 6A and 6B, the thickness (thickness F 1 ) of each of the plurality of fins 1a is smaller than the thickness (thickness F 2 ) of each of the plurality of fins 1b. That is, the thickness F 1 is 0.1 mm, for example, and the thickness F 2 is 0.11 mm, for example.

なお、これ以外の構成は、図１および図２に示す実施の形態１の構成とほぼ同じであるため、同一の構成要素については同一の符号を付し、その説明を省略する。   Since the other configuration is substantially the same as the configuration of the first embodiment shown in FIGS. 1 and 2, the same components are denoted by the same reference numerals and the description thereof is omitted.

本実施の形態の熱交換器１０において、補助熱交換器１０ａは複数のフィン１ａをさらに有していて、かつ主熱交換器１０ｂは複数のフィン１ｂをさらに有している。複数のフィン１ａの各々の間隔（距離Ｅ1）は、フィン１ｂの各々の間隔（距離Ｅ2）よりも大きい。 In the heat exchanger 10 of the present embodiment, the auxiliary heat exchanger 10a further includes a plurality of fins 1a, and the main heat exchanger 10b further includes a plurality of fins 1b. The interval (distance E 1 ) between each of the plurality of fins 1a is larger than the interval (distance E 2 ) between each fin 1b.

これにより、複数のフィン１ａおよび複数のフィン１ｂの各々により、伝熱管２ａ、２ｂおよび伝熱管２ｃ〜２ｆの各々の伝熱面積を大きくすることができる。したがって、熱交換器１０の熱交換効率を一層向上することができる。また、補助熱交換器１０ａの複数のフィン１ａの間隔が広くなるので、空気の流れ方向６からの気流が補助熱交換器１０ａの複数のフィン１ａの隙間を通って主熱交換器１０ｂの複数のフィンに当たりやすくなる。すなわち、補助熱交換器１０ａの通風抵抗が減少する。したがって、主熱交換器１０ｂの熱交換効率を一層向上することができる。   Thereby, the heat transfer area of each of the heat transfer tubes 2a and 2b and the heat transfer tubes 2c to 2f can be increased by each of the plurality of fins 1a and the plurality of fins 1b. Therefore, the heat exchange efficiency of the heat exchanger 10 can be further improved. Moreover, since the space | interval of the several fin 1a of the auxiliary heat exchanger 10a becomes wide, the airflow from the air flow direction 6 passes through the clearance gap between the several fin 1a of the auxiliary heat exchanger 10a, and the plurality of main heat exchangers 10b. It will be easier to hit the fins. That is, the ventilation resistance of the auxiliary heat exchanger 10a is reduced. Therefore, the heat exchange efficiency of the main heat exchanger 10b can be further improved.

本実施の形態の熱交換器１０において、複数のフィン１ａの各々の厚さＦ1は、フィン１ｂの各々の厚さＦ2よりも薄い。 In the heat exchanger 10 of the present embodiment, the thickness F 1 of each of the plurality of fins 1a is thinner than the thickness F 2 of each of the fins 1b.

これにより、補助熱交換器１０ａの複数のフィン１ａの間隔を広くしやすくなるので、空気の流れ方向６からの気流が補助熱交換器１０ａの複数のフィン１ａの隙間を通って主熱交換器１０ｂの複数のフィンに当たりやすくなる。すなわち、補助熱交換器１０ａの通風抵抗が減少する。したがって、主熱交換器１０ｂの熱交換効率を一層向上することができる。   Thereby, since it becomes easy to widen the space | interval of the several fin 1a of the auxiliary heat exchanger 10a, the airflow from the air flow direction 6 passes through the clearance gap between the several fin 1a of the auxiliary heat exchanger 10a, and the main heat exchanger It becomes easy to hit the plurality of fins 10b. That is, the ventilation resistance of the auxiliary heat exchanger 10a is reduced. Therefore, the heat exchange efficiency of the main heat exchanger 10b can be further improved.

本実施の形態の熱交換器１０において、複数のフィン１ａの各々の幅Ｐ1は、フィン１ｂの各々の幅Ｐ2よりも長い。 In the heat exchanger 10 of the present embodiment, the width P 1 of each of the plurality of fins 1a is longer than the width P 2 of each of the fins 1b.

これにより、補助熱交換器１０ａにおけるフィン１ａの伝熱面積が大きくなるので、より多くの空気と熱交換することができる。その結果、補助熱交換器１０ａの熱交換効率を改善することができる。特に熱交換器１０を凝縮器として使用する場合、補助熱交換器１０ａの伝熱管２ａ、２ｂには液体の冷媒が流れる。このため、補助熱交換器１０ａは、気液二相状態の冷媒が流れる主熱交換器１０ｂと比較して、熱交換効率が低くなっている。したがって、特に熱交換器１０を凝縮器として使用する場合に、補助熱交換器１０ａの熱交換効率を大きく改善することができる。   Thereby, since the heat transfer area of the fin 1a in the auxiliary heat exchanger 10a is increased, heat can be exchanged with more air. As a result, the heat exchange efficiency of the auxiliary heat exchanger 10a can be improved. In particular, when the heat exchanger 10 is used as a condenser, a liquid refrigerant flows through the heat transfer tubes 2a and 2b of the auxiliary heat exchanger 10a. For this reason, the heat exchange efficiency of the auxiliary heat exchanger 10a is lower than that of the main heat exchanger 10b in which the gas-liquid two-phase refrigerant flows. Therefore, particularly when the heat exchanger 10 is used as a condenser, the heat exchange efficiency of the auxiliary heat exchanger 10a can be greatly improved.

（実施の形態４）
図７（ａ）は、本発明の実施の形態４における補助熱交換器の伝熱管の断面図である。図７（ｂ）は、本発明の実施の形態４における主熱交換器の伝熱管の断面図である。 (Embodiment 4)
Fig.7 (a) is sectional drawing of the heat exchanger tube of the auxiliary heat exchanger in Embodiment 4 of this invention. FIG.7 (b) is sectional drawing of the heat exchanger tube of the main heat exchanger in Embodiment 4 of this invention.

図７（ａ）、（ｂ）を参照して、本実施の形態の熱交換器１０において、伝熱管２ａ、２ｂの各々の管内には複数の溝８ａが形成されている。溝８ａは深さＨ1を有している。また、伝熱管２ｃ〜２ｆの各々の管内には複数の溝８ｂが形成されている。溝８ｂは深さＨ2を有している。深さＨ1はたとえば０．２５ｍｍであり、深さＨ2はたとえば０．１５ｍｍである。また、溝８ａは円周方向にたとえば１８個形成されており、溝８ａは円周方向にたとえば９個形成されている。以上のように、伝熱管２ａ〜２ｆの各々の管内に適当な深さ、数および形状を有する溝８ａ、８ｂを設けると、溝８ａ、８ｂの各々によって冷媒の流れが乱され、伝熱管２ａ、２ｂおよび伝熱管２ｃ〜２ｆの各々を流れる冷媒は乱流化される。 7 (a) and 7 (b), in heat exchanger 10 of the present embodiment, a plurality of grooves 8a are formed in each of heat transfer tubes 2a and 2b. Groove 8a has a depth H 1. A plurality of grooves 8b are formed in each of the heat transfer tubes 2c to 2f. Groove 8b has a depth H 2. The depth H 1 is 0.25 mm, for example, and the depth H 2 is 0.15 mm, for example. Further, for example, 18 grooves 8a are formed in the circumferential direction, and 9 grooves 8a are formed in the circumferential direction, for example. As described above, when the grooves 8a and 8b having an appropriate depth, number, and shape are provided in each of the heat transfer tubes 2a to 2f, the flow of the refrigerant is disturbed by each of the grooves 8a and 8b, and the heat transfer tube 2a. 2b and the refrigerant flowing through each of the heat transfer tubes 2c to 2f are turbulent.

なお、これ以外の構成は、図１および図２に示す実施の形態１の構成とほぼ同じであるため、同一の構成要素については同一の符号を付し、その説明を省略する。   Since the other configuration is substantially the same as the configuration of the first embodiment shown in FIGS. 1 and 2, the same components are denoted by the same reference numerals and the description thereof is omitted.

本発明の熱交換器において好ましくは、第１の伝熱管を流れる冷媒が乱流化するように、第１の伝熱管は構成されている。   In the heat exchanger of the present invention, preferably, the first heat transfer tube is configured so that the refrigerant flowing through the first heat transfer tube is turbulent.

これにより、伝熱管２ａ、２ｃを流れる冷媒が攪拌され、冷媒の対流が促進される。したがって、補助熱交換器１０ａの熱交換効率が一層向上する。ここで、本実施の形態の熱交換器においては、伝熱管２ａ、２ｂの直径Ｄ1は伝熱管２ｃ〜２ｆの直径Ｄ2よりも大きいので、伝熱管２ａ、２ｂの直径Ｄ1を小さくし冷媒の流速を速くするという方法で、伝熱管２ａ、２ｂを流れる冷媒を攪拌することは難しい。したがって、冷媒の流速を速くするという方法の代わりに、伝熱管２ａ、２ｂを流れる冷媒が乱流化するように伝熱管２ａ、２ｂを構成することで、補助熱交換器１０ａの熱交換効率を高めることができる点で特に有効である。 Thereby, the refrigerant | coolant which flows through the heat exchanger tubes 2a and 2c is stirred, and the convection of a refrigerant | coolant is accelerated | stimulated. Therefore, the heat exchange efficiency of the auxiliary heat exchanger 10a is further improved. Here, in the heat exchanger of the present embodiment, the diameter D 1 of the heat transfer tube 2a, 2b so larger than the diameter D 2 of the heat transfer tube 2C～2f, reduced heat transfer tube 2a, the diameter D 1 of the 2b It is difficult to stir the refrigerant flowing through the heat transfer tubes 2a and 2b by increasing the flow rate of the refrigerant. Therefore, instead of the method of increasing the flow rate of the refrigerant, the heat transfer tubes 2a and 2b are configured so that the refrigerant flowing through the heat transfer tubes 2a and 2b is turbulent, thereby improving the heat exchange efficiency of the auxiliary heat exchanger 10a. This is particularly effective in that it can be increased.

なお、本実施の形態の熱交換器１０においては、溝８ａの深さＨ1、数、および形状の一例が示されたが、本発明はこのような溝の深さ、数および形状に限定されるものではなく、伝熱管２ａ、２ｂを流れる冷媒が乱流化されるように伝熱管２ａ、２ｂが構成されていればよい。したがって、溝８ａはたとえば三角形や半円形などの断面形状でもよい。また、伝熱管２ｃ〜２ｆを流れる冷媒は乱流化していなくてもよい。 In the heat exchanger 10 of the present embodiment, an example of the depth H 1 , number, and shape of the groove 8a is shown, but the present invention is limited to the depth, number, and shape of such a groove. The heat transfer tubes 2a and 2b may be configured so that the refrigerant flowing through the heat transfer tubes 2a and 2b is turbulent. Therefore, the groove 8a may have a cross-sectional shape such as a triangle or a semicircle. Moreover, the refrigerant | coolant which flows through the heat exchanger tubes 2c-2f does not need to be turbulent.

（実施の形態５）
図８は、本発明の実施の形態５におけるフィンの構成を模式的に示す正面拡大図である。図９は図８のＩＸ−ＩＸの線に沿った断面図である。なお、図９においては複数のフィンのうち、１枚のフィンのみを示している。 (Embodiment 5)
FIG. 8 is an enlarged front view schematically showing the configuration of the fin in the fifth embodiment of the present invention. FIG. 9 is a cross-sectional view taken along the line IX-IX in FIG. FIG. 9 shows only one fin among the plurality of fins.

図８および図９を参照して、補助熱交換器１０ａの複数のフィン１ａの各々には、矩形に近い平面形状の凸部１１および凹部１２（起伏部）が形成されている。凸部１１および凹部１２は、伝熱管２ａ、２ｂの各々の周囲を取り囲むように、フィン１ａの幅方向（図８中横方向）に４つ並んで形成されている。また、主熱交換器１０ｂの複数のフィン１ｂの各々にも、凸部１１および凹部１２が形成されている。凸部１１および凹部１２は、伝熱管２ｃ〜２ｆの各々の周囲を取り囲むように、フィン１ｂの幅方向（図８中横方向）に４つ並んで形成されている。フィン１ａの各々における単位面積当たりの凸部１１および凹部１２の数は、フィン１ｂの各々における単位面積当たりの凸部１１および凹部１２の数の数よりも多くなっている。   Referring to FIGS. 8 and 9, each of the plurality of fins 1 a of the auxiliary heat exchanger 10 a is formed with a convex portion 11 and a concave portion 12 (an undulating portion) having a planar shape close to a rectangle. The four convex portions 11 and the concave portions 12 are formed side by side in the width direction of the fin 1a (lateral direction in FIG. 8) so as to surround each of the heat transfer tubes 2a and 2b. Moreover, the convex part 11 and the recessed part 12 are formed also in each of the several fin 1b of the main heat exchanger 10b. The four protrusions 11 and the recesses 12 are formed side by side in the width direction of the fin 1b (lateral direction in FIG. 8) so as to surround each of the heat transfer tubes 2c to 2f. The number of protrusions 11 and recesses 12 per unit area in each fin 1a is larger than the number of protrusions 11 and recesses 12 per unit area in each fin 1b.

なお、これ以外の構成は、図１および図２に示す実施の形態１の構成とほぼ同じであるため、同一の構成要素については同一の符号を付し、その説明を省略する。   Since the other configuration is substantially the same as the configuration of the first embodiment shown in FIGS. 1 and 2, the same components are denoted by the same reference numerals and the description thereof is omitted.

本実施の形態における熱交換器１０においては、フィン１ａの各々およびフィン１ｂの各々には凸部１１および凹部１２が設けられており、フィン１ａの各々における単位面積当たりの凸部１１および凹部１２の数は、フィン１ｂの各々における単位面積当たりの凸部１１および凹部１２の数よりも多い。   In the heat exchanger 10 according to the present embodiment, each of the fins 1a and each of the fins 1b is provided with a convex part 11 and a concave part 12, and the convex part 11 and the concave part 12 per unit area in each of the fins 1a. Is greater than the number of convex portions 11 and concave portions 12 per unit area in each of the fins 1b.

これにより、フィン１ａの各々における凸部１１および凹部１２の数が多くなるので、フィン１ａの各々の表面を通過する外気の気流が凸部１１および凹部１２で乱されるようになり、フィン１ａの各々の表面から離れた部分に存在する外気を巻き込みながら外気が流れるようになる。その結果、フィン１ａの各々の表面を通過する外気とフィン１ａの各々との温度差をより大きく保つことができる。また、凸部１１および凹部１２の数が多くなることでフィン１ａの伝熱面積が増加する。したがって、補助熱交換器１０ａの熱交換効率を一層向上することができる。   Thereby, since the number of the convex part 11 and the recessed part 12 in each of the fin 1a increases, the airflow of the external air which passes each surface of the fin 1a comes to be disturbed by the convex part 11 and the recessed part 12, and fin 1a The outside air flows while entraining the outside air existing in the part away from the surface of each. As a result, the temperature difference between the outside air passing through each surface of the fin 1a and each of the fins 1a can be kept larger. Moreover, the heat-transfer area of the fin 1a increases because the number of the convex parts 11 and the recessed parts 12 increases. Therefore, the heat exchange efficiency of the auxiliary heat exchanger 10a can be further improved.

なお、本実施の形態においては、起伏部が図８および図９に示す凸部１１および凹部１２のような形状である場合について示したが、本発明はこのような場合に限定されるものではなく、第１のフィンおよび第２のフィンに設けられた起伏部であればよい。   In the present embodiment, the case where the undulating portion has a shape such as the convex portion 11 and the concave portion 12 shown in FIGS. 8 and 9 is shown, but the present invention is not limited to such a case. The undulations provided on the first fin and the second fin may be used.

（実施の形態６）
図１０は、本発明の実施の形態６における熱交換器の構成を示す側面図である。 (Embodiment 6)
FIG. 10 is a side view showing the configuration of the heat exchanger according to Embodiment 6 of the present invention.

図１０を参照して、本実施の形態における熱交換器３０は、補助熱交換器３０ａと主熱交換器１０ｂとを備えている。本実施の形態においては、補助熱交換器３０ａの構成が、実施の形態１の補助熱交換器１０ａの構成と異なっている。すなわち、補助熱交換器３０ａは、伝熱管３２（第１の伝熱管）と、複数のフィン１ａとを有している。伝熱管３２は直線部分を含む蛇行状に延びるように形成されている。伝熱管３２の直線部分が複数のフィン１ａを略直角に貫通することにより、伝熱管３２と複数のフィン１ａとが接触している。伝熱管３２は分岐部分を有しておらず、伝熱管３２の一端は出入り口５に接続されており、伝熱管３２の他端は分岐部分３３に接続されている。また、補助熱交換器３０ａと主熱交換器１０ｂとは接続管９ｃ、９ｄにより接続されている。接続管９ｃは、分岐部分３３と主熱交換器１０ｂの分岐部分３ｂとに接続されている。接続管９ｄは、分岐部分３３と主熱交換器１０ｂの分岐部分３ｃとに接続されている。   Referring to FIG. 10, heat exchanger 30 in the present embodiment includes auxiliary heat exchanger 30a and main heat exchanger 10b. In the present embodiment, the configuration of the auxiliary heat exchanger 30a is different from the configuration of the auxiliary heat exchanger 10a of the first embodiment. That is, the auxiliary heat exchanger 30a includes a heat transfer tube 32 (first heat transfer tube) and a plurality of fins 1a. The heat transfer tube 32 is formed to extend in a meandering manner including a straight portion. The heat transfer tube 32 and the plurality of fins 1a are in contact with each other when the straight portion of the heat transfer tube 32 penetrates the plurality of fins 1a at a substantially right angle. The heat transfer tube 32 does not have a branch portion, one end of the heat transfer tube 32 is connected to the entrance / exit 5, and the other end of the heat transfer tube 32 is connected to the branch portion 33. The auxiliary heat exchanger 30a and the main heat exchanger 10b are connected by connecting pipes 9c and 9d. The connecting pipe 9c is connected to the branch portion 33 and the branch portion 3b of the main heat exchanger 10b. The connecting pipe 9d is connected to the branch portion 33 and the branch portion 3c of the main heat exchanger 10b.

なお、これ以外の構成は、図１および図２に示す実施の形態１の構成とほぼ同じであるため、同一の構成要素については同一の符号を付し、その説明を省略する。   Since the other configuration is substantially the same as the configuration of the first embodiment shown in FIGS. 1 and 2, the same components are denoted by the same reference numerals and the description thereof is omitted.

続いて、本実施の形態の熱交換器３０における冷媒の流れについて説明する。
熱交換器３０が空気調和機の蒸発器として使用される場合には、まず、低温の液体もしくは気液２層状態の冷媒が出入り口５より流入し、伝熱管３２を流れる。伝熱管３２は分岐部分を有していないので、冷媒は分流することなく１つの経路を流れる。冷媒は伝熱管３２を流れながら、空気の流れ方向６から送り込まれる空気と熱交換を行なう。その結果、冷媒の温度が上昇し、冷媒は蒸発し始める。そして、気液２相状態の冷媒が伝熱管３２を経て分岐部分３３へ流れ込む。冷媒は分岐部分３ｂでさらに２方向に分流し、接続管９ｃ、９ｄの各々を介して主熱交換器１０ｂ内の分岐部分３ｂ、３ｃへ流れ込む。その後、冷媒は主熱交換器１０ｂ内において、伝熱管２ｃ〜２ｆの４つの経路を流れる。そして、低温の気体もしくは気液２層状態の冷媒が出入り口７から流出する。 Subsequently, the flow of the refrigerant in the heat exchanger 30 of the present embodiment will be described.
When the heat exchanger 30 is used as an evaporator of an air conditioner, first, a low-temperature liquid or a gas-liquid two-layer refrigerant flows from the inlet / outlet 5 and flows through the heat transfer tube 32. Since the heat transfer tube 32 does not have a branch portion, the refrigerant flows through one path without being divided. While the refrigerant flows through the heat transfer tube 32, the refrigerant exchanges heat with the air fed from the air flow direction 6. As a result, the temperature of the refrigerant rises and the refrigerant starts to evaporate. Then, the gas-liquid two-phase refrigerant flows into the branch portion 33 through the heat transfer tube 32. The refrigerant further splits in two directions at the branch portion 3b and flows into the branch portions 3b and 3c in the main heat exchanger 10b through the connection pipes 9c and 9d. Thereafter, the refrigerant flows through four paths of the heat transfer tubes 2c to 2f in the main heat exchanger 10b. Then, a low-temperature gas or a gas-liquid two-layer refrigerant flows out from the doorway 7.

一方、熱交換器１０が空気調和機の凝縮器として使用される場合には、まず、高温の気体の冷媒が出入り口７より流入する。流入した冷媒は、主熱交換器１０ｂ内の伝熱管２ｃ〜２ｆの４つの経路を介して、分岐部分３ｂ、３ｃの各々で合流する。このとき、冷媒はほぼ液体となっている。分岐部分３ｂで合流した冷媒は接続管９ｃを流れ、分岐部分３ｃで合流した冷媒は接続管９ｄを流れる。そして、接続管９ｃ、９ｄの各々を流れる冷媒は、分岐部分３３で合流し、補助熱交換器１０ａの伝熱管３２を流れる。伝熱管３２を流れる冷媒は、空気の流れ方向６から送り込まれる空気と熱交換を行なうことにより過冷却される。その後、過冷却された冷媒は出入り口５から流出する。   On the other hand, when the heat exchanger 10 is used as a condenser of an air conditioner, first, a high-temperature gaseous refrigerant flows from the inlet / outlet 7. The refrigerant that has flowed in joins at each of the branch portions 3b and 3c via the four paths of the heat transfer tubes 2c to 2f in the main heat exchanger 10b. At this time, the refrigerant is almost liquid. The refrigerant joined at the branch portion 3b flows through the connecting pipe 9c, and the refrigerant joined at the branch portion 3c flows through the connecting pipe 9d. And the refrigerant | coolant which flows through each of the connection pipes 9c and 9d merges in the branch part 33, and flows through the heat exchanger tube 32 of the auxiliary heat exchanger 10a. The refrigerant flowing through the heat transfer tubes 32 is supercooled by exchanging heat with the air fed from the air flow direction 6. Thereafter, the supercooled refrigerant flows out from the entrance 5.

本実施の形態においては、補助熱交換器３０ａの伝熱管３２における冷媒の流れる経路は１つとなっている。一方、実施の形態１の補助熱交換器１０ａの伝熱管２ａ、２ｂは、分岐部分３ａで伝熱管２ａおよび伝熱管２ｂに分岐しているため、冷媒の流れる経路は２つとなっている。このように、冷媒の流れる経路の数が減少すれば、冷媒が流れる伝熱管の長さ（冷媒が流れる距離）が長くなる。しかしながら、本実施の形態の熱交換器３０においては、伝熱管３２の直径Ｄ1が伝熱管２ｃ〜２ｆの直径Ｄ2よりも大きいので、圧力損失は大きくならない。一方、冷媒の流れる経路の数が減少するということは、分岐部分が減少ということである。分岐部分が減少すれば、冷媒が分岐部分で分流する際に、分岐した冷媒の流量が不均一になることが抑止される。ここで、分岐した冷媒の流量を均一にするために分流器を用いる方法も考えられる。しかしながら、分流器を用いれば、装置構成が複雑するという問題が生じる。また、分流器を冷媒が流れる際に冷媒に圧力損失が生じるという問題も生じる。 In the present embodiment, there is only one path through which the refrigerant flows in the heat transfer tube 32 of the auxiliary heat exchanger 30a. On the other hand, the heat transfer tubes 2a and 2b of the auxiliary heat exchanger 10a of Embodiment 1 are branched into the heat transfer tube 2a and the heat transfer tube 2b at the branch portion 3a, so that there are two paths through which the refrigerant flows. Thus, if the number of paths through which the refrigerant flows decreases, the length of the heat transfer tube through which the refrigerant flows (distance through which the refrigerant flows) increases. However, in the heat exchanger 30 of this embodiment, the diameter D 1 of the heat transfer tube 32 is greater than the diameter D 2 of the heat transfer tube 2C～2f, pressure loss is not increased. On the other hand, a decrease in the number of paths through which the refrigerant flows means that the branching portion is reduced. If the branching portion is reduced, it is possible to prevent the flow rate of the branched refrigerant from becoming uneven when the refrigerant is diverted at the branching portion. Here, in order to make the flow rate of the branched refrigerant uniform, a method using a flow divider is also conceivable. However, the use of a shunt causes a problem that the device configuration is complicated. There is also a problem that pressure loss occurs in the refrigerant when the refrigerant flows through the shunt.

本実施の形態の熱交換器３０においては、伝熱管３２における冷媒が流れる経路の数は、伝熱管２ｃ〜２ｆにおける冷媒が流れる経路の数よりも少ない。   In the heat exchanger 30 of the present embodiment, the number of paths through which the refrigerant flows in the heat transfer tubes 32 is smaller than the number of paths through which the refrigerant flows in the heat transfer tubes 2c to 2f.

これにより、伝熱管３２の分岐部分がなくなるので、分岐した伝熱管ごとの冷媒の流量が不均一になる（偏流が生じる）ことが防止される。なお、伝熱管３２の分岐部分がなくなれば、伝熱管３２の長さが長くなるが、伝熱管３２の直径Ｄ1は大きいので、伝熱管３２を流れる冷媒の圧力損失は大きくならない。以上の理由から、伝熱管３２における冷媒の圧力損失を抑止しながら、伝熱管３２の冷媒の流量が不均一になることが抑止される。 Thereby, since the branched portion of the heat transfer tube 32 is eliminated, it is prevented that the flow rate of the refrigerant for each branched heat transfer tube becomes non-uniform (the occurrence of drift). If the branch portion of the heat transfer tube 32 is eliminated, the length of the heat transfer tube 32 is increased, but the diameter D 1 of the heat transfer tube 32 is large, so that the pressure loss of the refrigerant flowing through the heat transfer tube 32 does not increase. For the above reasons, the refrigerant flow rate in the heat transfer tube 32 is prevented from becoming uneven while suppressing the pressure loss of the refrigerant in the heat transfer tube 32.

なお、本実施の形態においては、補助熱交換器３０ａの伝熱管３２における冷媒が流れる経路が１本であり、主熱交換器１０ｂの伝熱管２ｃ〜２ｆにおける冷媒が流れる経路が４本である場合について示したが、本実施の形態はこのような場合に限定されるものではなく、補助熱交換器の第１の伝熱管における冷媒が流れる経路の数が主熱交換器の第２の伝熱管における冷媒が流れる経路の数よりも少なければよい。   In the present embodiment, there is one path through which refrigerant flows in the heat transfer tubes 32 of the auxiliary heat exchanger 30a, and there are four paths through which refrigerant flows in the heat transfer tubes 2c to 2f of the main heat exchanger 10b. Although the case has been shown, the present embodiment is not limited to such a case, and the number of paths through which the refrigerant flows in the first heat transfer tube of the auxiliary heat exchanger is the second heat transfer of the main heat exchanger. The number should be smaller than the number of paths through which the refrigerant flows in the heat pipe.

また、本実施の形態においては、１本の伝熱管３２から分岐部分３３で接続管９ｃ、９ｄに分岐し、さらに接続管９ｃ、９ｄから分岐部分３ｂ、３ｃで４本の伝熱管２ｃ〜２ｆに分岐する場合について示した。しかしながら、本実施の形態はこのような場合の他、たとえば１本の伝熱管３２から１つの分岐部分によって４本の伝熱管２ｃ〜２ｆに分岐してもよい。   Moreover, in this Embodiment, it branches to the connection pipes 9c and 9d by the branch part 33 from the one heat transfer pipe 32, and also the four heat transfer pipes 2c-2f by the branch parts 3b and 3c from the connection pipes 9c and 9d. The case of branching is shown. However, in this embodiment, in addition to such a case, for example, one heat transfer tube 32 may be branched into four heat transfer tubes 2c to 2f by one branch portion.

以上に開示された実施の形態はすべての点で例示であって制限的なものではないと考慮されるべきである。本発明の範囲は、以上の実施の形態ではなく、特許請求の範囲によって示され、特許請求の範囲と均等の意味および範囲内でのすべての修正や変形を含むものと意図される。   The embodiment disclosed above should be considered as illustrative in all points and not restrictive. The scope of the present invention is shown not by the above embodiments but by the scope of claims, and is intended to include all modifications and variations within the scope and meaning equivalent to the scope of claims.

本発明の実施の形態１における熱交換器の構成を示す正面図である。It is a front view which shows the structure of the heat exchanger in Embodiment 1 of this invention. 本発明の実施の形態１における熱交換器の構成を示す斜視図である。It is a perspective view which shows the structure of the heat exchanger in Embodiment 1 of this invention. 本発明の実施の形態２における熱交換器の構成を示す正面図である。It is a front view which shows the structure of the heat exchanger in Embodiment 2 of this invention. （ａ）本発明の実施の形態２における補助熱交換器の構成を示す側面図である。（ｂ）本発明の実施の形態２における主熱交換器の構成を示す側面図である。(A) It is a side view which shows the structure of the auxiliary heat exchanger in Embodiment 2 of this invention. (B) It is a side view which shows the structure of the main heat exchanger in Embodiment 2 of this invention. 本発明の実施の形態３における熱交換器の一部の構成を示す上部平面図である。It is an upper top view which shows the structure of a part of heat exchanger in Embodiment 3 of this invention. （ａ）図５におけるＡ部の拡大図である。（ｂ）図５におけるＢ部の拡大図である。(A) It is an enlarged view of the A section in FIG. (B) It is an enlarged view of the B section in FIG. （ａ）本発明の実施の形態４における補助熱交換器の伝熱管の断面図である。（ｂ）本発明の実施の形態４における主熱交換器の伝熱管の断面図である。(A) It is sectional drawing of the heat exchanger tube of the auxiliary heat exchanger in Embodiment 4 of this invention. (B) It is sectional drawing of the heat exchanger tube of the main heat exchanger in Embodiment 4 of this invention. 本発明の実施の形態５におけるフィンの構成を模式的に示す正面拡大図である。It is a front enlarged view which shows typically the structure of the fin in Embodiment 5 of this invention. 図８のＩＸ−ＩＸの線に沿った断面図である。FIG. 9 is a cross-sectional view taken along line IX-IX in FIG. 8. 本発明の実施の形態６における熱交換器の構成を示す側面図である。It is a side view which shows the structure of the heat exchanger in Embodiment 6 of this invention. 従来の熱交換器の一の構成を示す側面図である。It is a side view which shows one structure of the conventional heat exchanger. 従来の熱交換器の一の構成を示す斜視図である。It is a perspective view which shows one structure of the conventional heat exchanger. 従来の熱交換器の他の構成を示す側面図である。It is a side view which shows the other structure of the conventional heat exchanger.

符号の説明Explanation of symbols

１ａ，１ｂ，１０１ａ，１０１ｂ フィン、２ａ〜２ｆ，３２，１０２ａ〜１０２ｅ 伝熱管、３ａ〜３ｃ，４ａ〜４ｃ，３３，１０３，１０４ 分岐部分、５，７，１０５，１０７ 出入り口、６，１０６ 流れ方向、８ａ，８ｂ 溝、９ａ，９ｂ，９ｃ，９ｄ 接続管、１０，３０，１１０，１２０ 熱交換器、１０ａ，３０ａ，１１０ａ 補助熱交換器、１０ｂ，１１０ｂ 主熱交換器、１１ 凸部、１２ 凹部、１３ａ，１３ｂ，１０９ 直線部分。   1a, 1b, 101a, 101b Fin, 2a-2f, 32, 102a-102e Heat transfer tube, 3a-3c, 4a-4c, 33, 103, 104 Branch part, 5, 7, 105, 107 Entrance / exit, 6,106 flow Direction, 8a, 8b groove, 9a, 9b, 9c, 9d connecting pipe, 10, 30, 110, 120 heat exchanger, 10a, 30a, 110a auxiliary heat exchanger, 10b, 110b main heat exchanger, 11 convex part, 12 Recess, 13a, 13b, 109 Straight line part.

Claims (4)

冷媒を流すための伝熱管を備える熱交換器であって、
前記熱交換器を凝縮器として使用した場合に、下流側となる過冷却領域にある主に液体の前記冷媒が流れる領域の第１の伝熱管の直径は、前記熱交換器内の他の伝熱管である第２の伝熱管の直径より大きく、
前記第１の伝熱管と接触する複数の第１のフィンと、
前記第２の伝熱管と接触する複数の第２のフィンとをさらに備え、
前記第１のフィンの各々の間隔は、前記第２のフィンの各々の間隔よりも大きいことを特徴とする、熱交換器。 A heat exchanger comprising a heat transfer tube for flowing a refrigerant,
When the heat exchanger is used as a condenser, the diameter of the first heat transfer tube in the region where the mainly liquid refrigerant flows in the subcooling region on the downstream side is the other heat transfer tube in the heat exchanger. Larger than the diameter of the second heat transfer tube, which is a heat tube,
A plurality of first fins in contact with the first heat transfer tube;
A plurality of second fins in contact with the second heat transfer tubes;
The heat exchanger according to claim 1, wherein a distance between each of the first fins is larger than a distance between each of the second fins. 冷媒を流すための伝熱管を有する熱交換器であって、
補助熱交換器と、空気の流れ方向に対して前記補助熱交換器よりも下流側に配置される主熱交換器とを備え、
前記補助熱交換器は、前記冷媒を流すための第１の伝熱管と、前記第１の伝熱管と接触する複数の第１のフィンとを有し、
前記主熱交換器は、前記第１の伝熱管と接続された第２の伝熱管と、前記第２の伝熱管と接触する複数の第２のフィンとを有し、
前記第１の伝熱管の直径は、前記第２の伝熱管の直径よりも大きく、かつ前記第１のフィンの各々の間隔は、前記第２のフィンの各々の間隔よりも大きいことを特徴とする、熱交換器。 A heat exchanger having a heat transfer tube for flowing refrigerant,
An auxiliary heat exchanger, and a main heat exchanger disposed downstream of the auxiliary heat exchanger with respect to the air flow direction,
The auxiliary heat exchanger has a first heat transfer tube for flowing the refrigerant, and a plurality of first fins in contact with the first heat transfer tube,
The main heat exchanger has a second heat transfer tube connected to the first heat transfer tube, and a plurality of second fins in contact with the second heat transfer tube,
The diameter of the first heat transfer tube is larger than the diameter of the second heat transfer tube, and the interval between the first fins is larger than the interval between the second fins. Heat exchanger. 前記第１の伝熱管および前記第２の伝熱管の各々は、直線部分を含む蛇行状に延びるように形成され、
前記第１の伝熱管における前記直線部分の各々の間隔は、前記第２の伝熱管における前記直線部分の各々の間隔よりも大きいことを特徴とする、請求項１または２に記載の熱交換器。 Each of the first heat transfer tube and the second heat transfer tube is formed to extend in a meandering manner including a straight portion,
3. The heat exchanger according to claim 1, wherein an interval between the linear portions in the first heat transfer tube is larger than an interval between the linear portions in the second heat transfer tube. . 前記第１のフィンの各々の厚さは、前記第２のフィンの各々の厚さよりも薄いことを特徴とする、請求項１〜３のいずれかに記載の熱交換器。   4. The heat exchanger according to claim 1, wherein a thickness of each of the first fins is thinner than a thickness of each of the second fins.
JP2007307601A 2007-11-28 2007-11-28 Heat exchanger Pending JP2008064457A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009013076A1 (en) 2008-03-13 2009-12-03 Hoya Corp. imaging device
CN106871664A (en) * 2017-01-09 2017-06-20 青岛海尔空调电子有限公司 A kind of heat exchanger, air-conditioning and design of heat exchanger method
WO2019176803A1 (en) * 2018-03-12 2019-09-19 株式会社Uacj Heat exchanger for freezer refrigerator

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009013076A1 (en) 2008-03-13 2009-12-03 Hoya Corp. imaging device
CN106871664A (en) * 2017-01-09 2017-06-20 青岛海尔空调电子有限公司 A kind of heat exchanger, air-conditioning and design of heat exchanger method
WO2019176803A1 (en) * 2018-03-12 2019-09-19 株式会社Uacj Heat exchanger for freezer refrigerator
JPWO2019176803A1 (en) * 2018-03-12 2021-03-11 株式会社Uacj Heat exchanger for refrigerator / freezer

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