JP3849965B2

JP3849965B2 - Heat exchanger, regenerator and absorption chiller / heater

Info

Publication number: JP3849965B2
Application number: JP35268599A
Authority: JP
Inventors: 楽敦設; 部尚樹刑
Original assignee: Tokyo Gas Co Ltd
Current assignee: Tokyo Gas Co Ltd
Priority date: 1999-12-13
Filing date: 1999-12-13
Publication date: 2006-11-22
Anticipated expiration: 2019-12-13
Also published as: JP2001174099A

Description

【０００１】
【発明の属する技術分野】
本発明は、熱交換器（本明細書において、「熱交換器」なる文言は、蒸発、再生等の相変化を伴う熱交換を行うタイプの熱交換器を意味しており、顕熱（液−液）熱交換器は含まれない）と、再生器と、吸収冷温水機に関し、特に、熱交換器、再生器の小型化を図る技術に関する。
【０００２】
【従来の技術】
従来の吸収冷温水機Ｊ１における高温および低温の２重効用の再生器を有する一般的なブロック構成を図１３に示す。符号ＨＧｅは高温再生器、ＬＧｅは低温再生器、Ｃｎは凝縮器、Ｅｖは蒸発器、Ａｂは吸収器、ＨＥｘは高温側熱交換器、ＬＨｘは低温側熱交換器をそれぞれ示している。このような２重効用の再生器による効率向上を図った構成であっても、まだ効率向上の余地がある。
【０００３】
図１４および図１５は、従来の熱交換器（蒸気発生器或いは再生器）の構成を示している。
図１４において、ラインＡ１９から供給され、ラインＡ２０から流出する被加熱流体Ｌ中に、内部に加熱流体が流れる加熱ラインＡ１５を配置して、当該加熱ラインＡ１５を流れる加熱流体が保有する熱量により被加熱流体を加熱する満液式熱交換器が示されている。この満液式熱交換器における総括伝熱係数Ｋと温度差△Ｔとの特性は、加熱ラインＡ１５内の温度と、被加熱流体Ｌとの温度差を横軸、総括伝熱係数Ｋを縦軸に取った伝熱特性線図１６においては、実線で示す特性線ＡＬとなる。
【０００４】
この満液式熱交換の伝熱特性ＡＬは、蒸気を発生して沸騰が起きる場合の特性として、温度差△Ｔに比例して総括伝熱係数Ｋが大になる。したがって、温度差△Ｔが高い領域では総括伝熱係数Ｋが大きいが、温度差△Ｔが低い領域では総括伝熱係数Ｋが小さくなってしまう、という欠点がある。従って、再生器における溶液濃度幅を大きくとるためには、大きな再生器を使用しなければならない。即ち、満液式熱交換器を使用する吸収冷温水機では上記による温度差△Ｔが低い領域での総括伝熱係数Ｋの改善が必要である。
【０００５】
一方、図１５においては、流下液膜式熱交換器が示されている。この流下液膜式熱交換器によれば、ラインＢ１９を介して供給され、ラインＢ２０から流出する被加熱流体は、符号Ｄで示す様に液滴として滴下されており、被加熱流体の液滴が滴下する空間内に配置された加熱ラインＢ１５は、その表面に被加熱流体の液膜が形成され、加熱ラインＢ１５内を流れる加熱流体が保有する熱量が当該液膜に対して伝熱される。
この流下液膜式熱交換器において、加熱ラインＢ１５内の温度と被加熱流体Ｄとの温度差△Ｔを横軸、総括伝熱係数Ｋを縦軸にした場合の伝熱特性線は、図１６の符号ＢＬで示されている。
【０００６】
この液膜式熱交換の伝熱特性ＢＬは、温度差△Ｔに対して総括伝熱係数Ｋがあまり変わらない特性を有している。したがって、温度差△Ｔが低い領域でも総括伝熱係数Ｋが小にならない代わりに、温度差△Ｔが高い領域でも総括伝熱係数Ｋが大きくならない欠点がある。そのため、再生器における溶液濃度幅を大きくとるためには大きな再生器を使用しなければならない。即ち、液膜式熱交換器を使用する吸収冷温水機では、温度差△Ｔが高い領域での総括伝熱係数Ｋの改善が必要である。
【０００７】
【発明が解決しようとする課題】
本発明は上記した従来技術の問題点に鑑みて提案されたものであり、温度差△Ｔとは無関係に常に良好な総括伝熱係数Ｋを維持するという特性を備えている熱交換器、再生器、或いはその様な再生器を具備する吸収冷温水機の提供を目的としている。
【０００８】
【課題を解決するための手段】
本発明の熱交換器は、第１の熱交換部と第２の熱交換部とを有し、第１の熱交換部は第１の液槽を備え、第１の液槽内に貯留している被加熱流体の中には加熱流体が流れる第１の加熱ラインが配置されており（従って、満液式熱交換器としての構成を具備しており）、前記第２の熱交換部は、第２の液槽を備え、第２の液槽の上方には前記第１の熱交換部を経由した被加熱流体を液滴として滴下する滴下機構が設けられ、該滴下機構から被加熱流体の液滴が滴下される空間内に第２の加熱ラインが配置され（従って、流下液膜式熱交換器としての構成を具備しており）、前記第１の加熱ラインの出口と前記第２の加熱ラインの入口が接続され、前記第１の液槽の底部と前記滴下機構とが接続されている。
ここで、本明細書において、「熱交換器」なる文言は、満液式熱交換器や流下液膜式熱交換器の様に、蒸発、再生等の相変化を伴う熱交換を行うタイプを意味しており、顕熱（液−液）熱交換器は含まれない。
【０００９】
本発明の熱交換器によれば、第１の加熱ラインと被加熱流体との温度差が大きい領域では総括伝熱係数の大きい満液式熱交換とし、第２の加熱ラインと被加熱流体との温度差が小さい領域で総括伝熱係数の大きい流下液膜式熱交換をして、総熱伝達量を大にしている。これにより熱交換器を小型にできる。
【００１０】
また本発明の再生器は、第１の熱交換部と第２の熱交換部とを有し、第１の熱交換部は第１の液槽を備え、第１の液槽内に貯留している吸収溶液の中には加熱流体が流れる第１の加熱ラインが配置されており（従って、満液式熱交換器としての構成を具備しており）、前記第２の熱交換部は、第２の液槽を備え、第２の液槽の上方には前記第１の熱交換部を経由した吸収溶液を液滴として滴下する滴下機構が設けられ、該滴下機構から吸収溶液の液滴が滴下される空間内に第２の加熱ラインが配置され（従って、流下液膜式熱交換器としての構成を具備しており）、前記第１の加熱ラインの出口と前記第２の加熱ラインの入口が接続され、前記第１の液槽の底部と前記滴下機構とが接続されている。
【００１１】
かかる構成を具備する本発明の再生器によれば、第１の熱交換部では満液式熱交換、第２の熱交換部では流下液膜式熱交換を行い、全領域において総括伝熱係数を大きくとることが出来るので、再生器における熱伝達効率を向上して、小型化することが出来る。
再生器の効率を向上するためには、吸収溶液の濃度幅を広げなければならない。そして濃度幅を広げることにより、再生器における稀溶液と濃溶液の飽和温度の差が大きくなる。その結果、被加熱側（吸収溶液）と加熱源（一定温度）との温度差ΔＴは、再生器の吸収溶液入口では大きくなるが、吸収溶液出口では小さくなる。すなわち、再生器の吸収溶液入口の温度差ΔＴは、吸収溶液出口のΔＴよりも大きくなる。
本発明によれば、温度差が大きい領域と、温度差が小さい領域に、それぞれ適した熱交換方式を用いることにより、再生器をコンパクトにすることが出来るのである。換言すれば、同一伝熱面積で、再生量を増加することが出来る。
【００１２】
また、本発明の吸収冷温水機は、高温再生器と、低温再生器と、凝縮器と、蒸発器と、吸収器とを有し、前記低温再生器は、第１の熱交換部と第２の熱交換部とを有し、第１の熱交換部は第１の液槽を備え、第１の液槽内に貯留している吸収溶液の中には、高温再生器で再生した冷媒蒸気が流れる第１の加熱ラインが配置されており、前記第２の熱交換部は、第２の液槽を備え、第２の液槽の上方には前記第１の熱交換部を経由した吸収溶液を液滴として滴下する滴下機構が設けられ、該滴下機構から吸収溶液の液滴が滴下される空間内に第２の加熱ラインが配置され、前記第１の加熱ラインの出口と前記第２の加熱ラインの入口が接続され、前記第１の液槽の底部と前記滴下機構とが接続されている。
【００１３】
かかる構成を有する本発明によれば、吸収溶液を昇温して再生し易い状態とせしめ、再生器における熱伝達効率を向上して、小型化することが出来る。換言すれば、同一伝熱面積で、再生量を増加することが出来るのである。
【００１４】
また、本発明の吸収冷温水機は、高温再生器と、低温再生器と、凝縮器と、蒸発器と、吸収器とを有し、前記吸収器と前記高温再生器とを接続する稀溶液ラインに排熱焚再生器を介装し、その排熱焚再生器は、第１の熱交換部と第２の熱交換部とを有し、第１の熱交換部は第１の液槽を備え、第１の液槽内に貯留している吸収溶液の中には、外部熱源から供給される加熱流体（例えば高温水等）が流れる第１の加熱ラインが配置されており、前記第２の熱交換部は、第２の液槽を備え、第２の液槽の上方には前記第１の熱交換部を経由した吸収溶液を液滴として滴下する滴下機構が設けられ、該滴下機構から吸収溶液の液滴が滴下される空間内に第２の加熱ラインが配置され、前記第１の加熱ラインの出口と前記第２の加熱ラインの入口が接続され、前記第１の液槽の底部と前記滴下機構とが接続されている。
かかる構成を有する本発明によれば、再生器を小型化することが出来る。すなわち、同一伝熱面積で、再生量を増加することが出来るのである。
【００１５】
本発明の吸収冷温水機は、高温再生器と、低温再生器と、凝縮器と、蒸発器と、吸収器とを有し、前記高温再生器は、第１の熱交換部と第２の熱交換部とを有し、第１の熱交換部は第１の液槽を備え、第１の液槽内に貯留している吸収溶液の中には、外部熱源から供給される加熱流体（例えば高圧蒸気等）が流れる第１の加熱ラインが配置されており、前記第２の熱交換部は、第２の液槽を備え、第２の液槽の上方には前記第１の熱交換部を経由した吸収溶液を液滴として滴下する滴下機構が設けられ、該滴下機構から吸収溶液の液滴が滴下される空間内に第２の加熱ラインが配置され、前記第１の加熱ラインの出口と前記第２の加熱ラインの入口が接続され、前記第１の液槽の底部と前記滴下機構とが接続されている。
【００１６】
【発明の実施の形態】
以下図面を参照して本発明の実施の形態を説明する。
図１および図２に、本発明の第１の実施形態である熱交換器１０を示す。
熱交換器１０は、第１の熱交換部１１（満液式の構成を有する部分）と、第２の熱交換部２１（流下液膜式の構成を有する部分）とで構成されている。
第１の熱交換部１１は、その内部を加熱流体（温水、蒸気等）が流れる第１の加熱ライン１５が、被加熱流体Ｌ１中に配置された構造となっている。そして第２の熱交換部２１は、第２の加熱ライン１８が、被加熱流体の液滴Ｄ１が滴下する領域中に配置された構造を有している。
【００１７】
満液式熱交換器の構成を具備する第１の熱交換部１１は、第１の液槽１３と、被加熱流体Ｌ１が導入される流入ライン１９と、被加熱流体Ｌ１中に配置され且つ内部に加熱流体（蒸気、熱水等）が流れている複数の第１の加熱ライン１５、とを備えている。
第１の液槽１３は、被加熱流体Ｌ１が極めて低速で流過する様に複数の邪魔板１３ｂを有しており、加熱された被加熱流体Ｌ１を第２の熱交換部２１に導く出口部１３ｃが設けられている。
ここで、第１の加熱ライン１５は、図示しない熱源から加熱流体（例えば熱水或いは高圧蒸気、その他）が供給されている。
【００１８】
流下液膜式熱交換器の構成を具備する第２の熱交換部２１は、第２の液槽２３と、出口部１３ｃからの被加熱流体Ｌ１が導入される皿体１６と、皿体１６から流下する（被加熱流体Ｌ１の）液滴Ｄ１中に配置され且つ内部に加熱流体が流れている複数の第２の加熱ライン１８と、加熱後に貯留された被加熱流体Ｌ１を外部に導く流出ライン２０、とを備えている。
第２の液槽２３は、その上端部が第１の液槽１３の底部と接続され、上部に皿体１６を支持し、皿体１６の下方に流下液滴Ｄ１が放散される空間を有し（すなわち、被加熱流体の液滴を滴下する滴下機構を備えており）、第２の加熱ライン１８の下方に加熱された被加熱流体Ｌ１が収納される空間を有している。
皿体１６の底部には複数の小孔１６ａが穿孔されており、被加熱流体Ｌ１が液滴となって流下するよう構成されている。
そして、第１の加熱ライン１５の出口と、第２の加熱ライン１８の入口は接続部１７によって接続されている。
【００１９】
次に、上記構成による熱交換器１０の作用を説明する。
図１および図２において、熱交換器１０の第１の液槽１３上部からライン１９を介して被加熱流体Ｌ１が導入され、第１の加熱ライン１５を介して加熱流体が側方から導入される。被加熱流体Ｌ１は、液槽１３内を非常に遅い速度で流過する。
一方、貯留された被加熱流体Ｌ１内に配置された第１の加熱ライン１５は、そのライン壁を介して、温度差△Ｔによる伝熱により、その保有する熱量を被加熱流体Ｌ１に投入して、加熱・昇温させる。
第１の熱交換部１１における伝熱の形態は、被加熱流体中に加熱ラインがあるので、上述した様にとなる。即ち、図３において、折線Ａ０で示される総括伝熱係数Ｋの特性において、符号「Ａ１」で示す領域の特性となる。すなわち、第１の熱交換部１１においては、効率の良い満液式熱交換（伝熱による熱交換）で、被加熱流体Ｌ１は加熱される。
ちなみに、点線ＢＬは、流下液膜式の場合の総括伝熱係数Ｋで、こちらの形態を採用すれば熱交換の効率は低くなる。
【００２０】
このようにして、第１の熱交換部１１で加熱された被加熱流体Ｌ１の温度は上昇すると共に、第１の加熱ライン１５との温度差△Ｔは小さくなる。そして被加熱流体Ｌ１は、出口部１３ｃを介して、第２の熱交換部２１の上部に流入する。
一方、第１の加熱ライン１５内を流れる加熱流体の温度は降下して（後記のように、加熱流体が蒸気であれば温度降下は小さく、加熱流体が液体であれば温度降下は大きい）、接続部１７を介して第２の加熱ライン１８に導かれる。
【００２１】
第２の熱交換部２１に流入した被加熱流体Ｌ１は、皿体１６の複数の小孔１６ａから液滴Ｄ１となって流下し、第２の加熱ライン１８のライン壁外周に液膜となって付着し加熱される。この時の伝熱の形態は、被加熱流体Ｌ１が液膜なので流下液膜式熱交換となる。即ち、図３において、折線Ａ０で示される総括伝熱係数Ｋの特性において、符号「Ａ２」で示す領域の特性となるので、効率の良好な伝熱による熱交換により、被加熱流体Ｌ１は加熱される。
ちなみに、点線ＡＬは、満液式の場合の総括伝熱係数Ｋで、こちらの形態を採用すれば熱交換の効率は低くなる。
【００２２】
このように、加熱側と被加熱側との特定の温度差△Ｔ０（図３）を分岐点として、温度差△Ｔが大きい場合は満液式熱交換とし、温度差△Ｔが小さい場合に流下液膜式熱交換として、総括伝熱係数Ｋを常に良好となる様にしている。
【００２３】
図５は、本発明を低温再生器に適用した実施形態である第２実施形態にかかる吸収冷温水機２を示している。
以下、図１３に示した従来の吸収冷温水機Ｊ１と異なる装置、部分を主体に説明する。なお、図１３の吸収冷温水機Ｊ１と同様な機器については、同様な符号を重複して使用する。
図５および図６において、吸収冷温水機２は所謂「シリーズフロータイプ」の吸収冷温水機として構成されており、低温再生器２ＬＧｅは、第１の熱交換部Ａ１１と、第２の熱交換部Ａ２１、とで構成されている。
第１の熱交換部Ａ１１は、満液式熱交換器としての構成を具備しており、第１の加熱ライン３２が、高温再生器ＨＧｅで発生した冷媒蒸気が流れるライン３１に接続しており、被加熱流体である吸収溶液Ｌ１中に配置されている。
一方、第２の熱交換部Ａ２１は流下液膜式熱交換器としての構成を具備しており、第２の加熱ライン３４が吸収溶液Ｌ１の液滴Ｄ１中に配置されている。
以下の細部については、図２をも参考にして説明する。
【００２４】
第１の熱交換部Ａ１１は、第１の液槽１３と、吸収溶液Ｌ１中に配置された複数の第１の加熱ライン３２、とを備えている。
第１の液槽１３は、高温再生器ＨＧｅから導かれた吸収溶液Ｌ１が非常に遅い流速で流れる様に、複数の邪魔板１３ｂを有し、加熱された吸収溶液Ｌ１を第２の熱交換部Ａ２１に導く出口部１３ｃが設けられている。
第１の加熱ライン３２は、複数の直ライン（その内部を、高温再生器ＨＧｅから導かれた冷媒蒸気が加熱流体として流れている）となって、吸収溶液Ｌ１を加熱するよう構成されている。
【００２５】
第２の熱交換部Ａ２１は、第２の液槽２３と、第１の熱交換部Ａ１１から導かれた吸収溶液Ｌ１が導入される皿体１６と、皿体１６から流下する液滴Ｄ１中に配置された複数の第２の加熱ライン３４と、加熱後に貯留された吸収溶液Ｌ１を外部に導く流出ライン４２、とを備えている。
第２の液槽２３は、その上端部で第１の液槽１３の底部と接続され、上部に皿体１６を支持し、皿体１６の下方に流下液滴Ｄ１が放散される空間を有し（すなわち、被加熱流体の液滴を滴下する滴下機構を備えており）、第２の加熱ライン３４の下方に加熱された吸収溶液Ｌ１が貯留される空間を有している。
皿体１６には、底部に複数の小孔１６ａが設けられ、吸収溶液Ｌ１が液滴となって流下するよう構成されている。
第２の加熱ライン３４は、第１の加熱ライン３２の出口に接続部３３で接続されて、複数の直ラインとなって液滴Ｄ１中に配置されている。
【００２６】
上記構成による低温再生器２ＬＧｅは、高温再生器ＨＧｅ、凝縮器Ｃｎ、吸収器Ａｂは、以下の様に接続されている。
第１の液槽１３の上部に吸収溶液Ｌ１を導くライン４１は高温再生器ＨＧｅに接続され、第１の液槽１３下部の吸収溶液Ｌ１中に配置されている第１の加熱ライン３２は、上述した様に、高温再生器ＨＧｅで発生した冷媒蒸気が流れる冷媒蒸気ライン３１に接続されている。
第１の液槽１３の上部には、凝縮器Ｃｎに連通するライン３８が接続されており、第１の液槽１３で発生（再生）した冷媒蒸気を導くよう接続されている。
第２の液槽２３に配置された第２の加熱ライン３４は、ライン３５を介して凝縮器Ｃｎに連通する。第２の液槽２３の底部２３ａと吸収器Ａｂとは、ライン４２を介して接続されている。そして、第２の液槽２３の上部はライン３８ａ（第２の液槽２３で発生・再生した冷媒蒸気が流れる冷媒蒸気ライン）及びライン３８を介して凝縮器Ｃｎに接続されている。
【００２７】
上記構成による吸収冷温水機２の作用を、低温再生器２ＬＧｅまわりに限定して説明する。
高温再生器ＨＧｅで加熱・濃縮された吸収溶液はライン４１を介して、低温再生器２ＬＧｅの第１の熱交換部Ａ１１に導かれる。そして、高温再生器ＨＧｅで発生・再生した冷媒蒸気はライン３１を介して冷媒蒸気が、低温再生器２ＬＧｅの第１の熱交換部Ａ１１に導かれる。
吸収溶液Ｌ１は、第１の液槽１３内で冷媒蒸気による加熱ライン３２で加熱され昇温し、蒸発した冷媒蒸気はライン３８を介して凝縮器Ｃｎに導かれる。この時の加熱ライン３２と吸収溶液Ｌ１との熱交換の形態は、満液式の熱交換である。
【００２８】
第１の液槽１３で加熱され再生された吸収溶液Ｌ１は、第２の熱交換部Ａ２１における第２の液槽２３に入り、皿体１６の小孔１６ａから、液滴Ｄ１となって流下する。
この液滴Ｄ１が第２の加熱ライン３４に液膜となって接触し、第２の加熱ライン３４内を流れる加熱流体が保有する熱量により加熱され、昇温して、冷媒蒸気を発生（再生）させる。この時の加熱ライン３４と液滴Ｄ１（即ち吸収溶液Ｌ１）との熱交換の形態は、流下液膜式熱交換である。
【００２９】
図７は、上記の伝熱形態を図式的に説明するもので、第１の加熱ライン３２および第２の加熱ライン３４内を流れる冷媒蒸気の温度と、それに対する被加熱流体Ｌ１の温度状態を示している。
図７の左側の領域（満液式）は、第１の熱交換部Ａ１１に対応しており、温度差△Ｔが大きいので、満液式熱交換により吸収溶液Ｌ１を加熱再生している。一方、図７の右側の領域（流下液膜式）は、第２の熱交換部Ａ２１に対応しており、温度差△Ｔが小さいので、流下液膜式熱交換により吸収溶液Ｌ１を加熱再生させている。
その結果、温度差△Ｔの大小に関り無く、総括伝熱係数Ｋが常に大きい状態で低温再生器ＬＧｅで吸収溶液を加熱しているので、従来の満液式熱交換のみに比べて、高い再生効率を維持することが出来る。
図４は、図５−図７で説明した吸収冷温水機の作動を示すデューリング線図であり、満液式の低温再生器の作動である点線で示す特性に対して、総括伝熱係数Ｋを最良に選択した満液および流下液膜式の合成では、熱伝達がＱＬｇとなって大きくなることがわかる。
【００３０】
図８に、本発明の第３の実施形態である吸収冷温水機３を示す。図１３に示した従来の吸収冷温水機Ｊ１と異なる装置、部分を主として説明する。なお、同様な機器については同様な符号を重複して使用する。
図８および図９において、吸収冷温水器３を構成する排熱焚再生器ＭＧｅが稀溶液ラインである稀溶液ライン５４に介装されている。その排熱焚再生器ＭＧｅは、第１の熱交換部Ｂ１１と、第２の熱交換部Ｂ２１、とで構成されている。
第１の熱交換部Ｂ１１は満液式熱交換器としての構成を具備しており、加熱流体が内部を流れる第１の加熱ライン１５が、被加熱流体である稀溶液Ｋ中に配置されている。一方、第２の熱交換部Ｂ２１は流下液膜式熱交換器としての構成を具備しており、第２の加熱ライン１８が稀溶液Ｋの液滴Ｄ１中に配置されて、構成されている。
以下の細部については、図２をも参照しつつ説明する。
【００３１】
第１の熱交換部Ｂ１１は、第１の液槽１３と、稀溶液Ｋ中に配置された複数の第１の加熱ライン１５、とを備えている。
第１の液槽１３は、吸収器Ａｂから導かれる稀溶液Ｋが非常に遅い流速で流過するための複数の邪魔板１３ｂを有し、加熱された稀溶液Ｋを第２の熱交換部Ｂ２１に導く出口部１３ｃが設けられている。
第１の加熱ライン１５は、外部から供給される（加熱流体である）高温水がその内部を流れており、複数の直ラインとなって稀溶液Ｋを加熱する。
【００３２】
第２の熱交換部Ｂ２１は、第２の液槽２３と、第１の熱交換部Ｂ１１から流入した稀溶液Ｋが導入される皿体１６と、皿体１６から流下する液滴Ｄ１中に配置された複数の第２の加熱ライン１８と、加熱後に貯留された稀溶液Ｋを外部に導く流出ライン５５、とを有している。
第２の液槽２３は、その上端部で第１の液槽１３の底部と接続され、上部に皿体１６を支持しており、皿体１６の下方に流下液滴Ｄ１が滴下する空間を有し、そして、第２の加熱ライン１８の下方には、加熱された稀溶液Ｋが貯留される空間を有している。
皿体１６の底部には複数の小孔１６ａが形成されており、稀溶液Ｋが液滴となって流下するよう構成されている。
第２の加熱ライン１８は、接続部１７を介して、第１の加熱ライン１５の出口に接続された複数の直ラインとなって、液滴Ｄ１が滴下する空間中に配置されている。
【００３３】
上記構成による排熱焚再生器ＭＧｅは、高温再生器ＨＧｅ、凝縮器Ｃｎ、吸収器Ａｂは、つぎの様に構成されている。
第１の液槽１３に稀溶液Ｋを供給するライン５４は、吸収器Ａｂに接続され、第１の液槽１３の稀溶液Ｋ中に配置されている第１の加熱ライン１５は、外部の熱源である燃焼排熱源（図示せず）に接続されている。また、第１の液槽１３から発生（再生）した冷媒蒸気は、ライン５７を介して、凝縮器Ｃｎに供給されている。
【００３４】
第２の液槽２３に配置された第２の加熱ライン１８（の出口側）は、図示しない燃焼排熱源に連通している。排熱焚再生器ＭＧｅ或いは第２の液槽２３の底部２３ａと、高温再生器ＨＧｅとは、第２の稀溶液ライン５５を介して接続されている。
また、第２の液槽２３で発生（再生）した蒸気は、ライン５７ａを介してライン５７に接続されて、凝縮器Ｃｎに連通している。
【００３５】
上記構成による吸収冷温水機３の作用を、排熱焚再生器ＭＧｅに関連する部分を主として説明する。
吸収器Ａｂで冷媒蒸気を吸収して稀釈された吸収溶液（稀溶液）Ｋは、第１の稀溶液ライン５４を介して、排熱焚再生器ＭＧｅの第１の熱交換部Ｂ１１に流入する。また、外部の排熱焚熱源（図示せず）からは、加熱流体（例えば高温水）が、第１の加熱ライン１５に導かれる。
稀溶液Ｋは、第１の液槽１３内で、加熱ライン１５内を流れる加熱流体（例えば高温水）が保有する熱量により加熱され昇温し、発生（再生）した冷媒蒸気はライン５７を介して凝縮器Ｃｎに送出される。この時の加熱ライン１５を流れる加熱流体（例えば高温水）と稀溶液Ｋとの熱交換の形態は、満液式熱交換である。
第１の液槽１３で加熱された稀溶液Ｋは、第２の熱交換部Ｂ２１における第２の液槽２３に入り、皿体１６の小孔１６ａから液滴Ｄ１となって滴下される（すなわち、被加熱流体の液滴を滴下する滴下機構を備えている）。この液滴Ｄ１が第２の加熱ライン１８に液膜となって接触し、第２の加熱ライン１８内を流れる加熱流体が保有する熱量により加熱され、昇温して、冷媒蒸気が再生される。この時の加熱ライン１８と液滴Ｄ１即ち稀溶液Ｋとの熱交換の形態は、流下液膜式熱交換である。
【００３６】
図１０は、上記の伝熱形態を図式的に説明するもので、第１の加熱ライン１５および第２の加熱ライン１８内を流れる高温水の温度変化と、被加熱流体である稀溶液Ｋの温度変化とを比較して、温度差△Ｔと共に示している。
第１の熱交換部Ｂ１１においては、温度差△Ｔが大きいので、満液式熱交換により稀溶液Ｋを加熱再生させている。一方、第２の熱交換部Ｂ２１では温度差△Ｔが小さいので、流下液膜式熱交換により稀溶液Ｋを加熱再生させている。なお、加熱流体が温水の場合は、蒸気の場合とは異なり、熱交換によって加熱流体の温度が低下している。
【００３７】
上記のようにして、高温再生器ＨＧｅにおける稀溶液Ｋの再生前に、予め稀溶液Ｋを外部熱源の高温水により満液式および流下液膜式を併用して、加熱し再生している。そのため、高温再生器ＨＧｅにおける加熱量を節約することが出来、しかも、冷媒蒸気の再生量も増加するので、吸収冷温水機の効率が向上するのである。
【００３８】
図１１は、本発明の第４の実施形態にかかる吸収冷温水機４を示す。
以下、図１１の実施形態にかかる吸収冷温水機４について、図１３に示した従来の吸収冷温水機Ｊ１と異なる装置、部分を主体に説明する。なお、同様な機器については、同様な符号を重複して使用する。
図１１および図１２において、吸収冷温水機２を構成する高温再生器４ＨＧｅは、第１の熱交換部Ｃ１１と、第２の熱交換部Ｃ２１、とで構成されている。そして第１の熱交換部Ｃ１１は、満液式熱交換器として構成されており、その内部に加熱流体が流れる第１の加熱ライン１５が、被加熱流体である稀溶液Ｋ１中に配置されている。一方、第２の熱交換部Ｃ２１は流下液膜式熱交換器として構成されており、第１の熱交換部Ｃ１１を経由した吸収溶液Ｌ２の液滴Ｄ１が滴下する空間中に、第２の加熱ライン１８が配置された構成を具備している。
以下の細部については、図２をも参考にして説明する。
【００３９】
第１の熱交換部Ｃ１１は、第１の液槽１３と、稀溶液Ｋ１中に配置された複数の第１の加熱ライン１５、とで主要構成がされている。
第１の液槽１３には、稀溶液Ｋ１が非常に遅い流速にて流過するための複数の邪魔板１３ｂと、加熱された稀溶液Ｋ１を第２の熱交換部Ｃ２１に導く出口部１３ｃ、とが設けられている。
第２の熱交換部Ｃ２１は、第２の液槽２３と、第１の熱交換部Ｃ１１から導かれた吸収溶液Ｌ２が導入される皿体１６と、皿体１６から流下する液滴Ｄ１中に配置された複数の第２の加熱ライン１８と、加熱後に貯留された吸収溶液Ｌ２を外部に導く流出ライン４１、とを有している。
第２の液槽２３は、その上端部で第１の液槽１３の底部と接続され、上部に皿体１６を支持し、皿体１６の下方に流下液滴Ｄ１が滴下される空間を有し、第２の加熱ライン１８の下方には、加熱された後の吸収溶液Ｌ２が貯留される空間を有している。
皿体１６には、底部に複数の小孔１６ａが設けられ、吸収溶液Ｌ１が液滴となって滴下するよう構成されている。
第２の加熱ライン１８は、接続部１７を介して第１の加熱ライン１５に接続されており、複数の直ラインの形態で、液滴Ｄ１が滴下する空間中に配置されている（すなわち、被加熱流体の液滴を滴下する滴下機構を備えている）。
【００４０】
上記構成による高温再生器４ＨＧｅ、低温再生器ＬＧｅ、凝縮器Ｃｎ、吸収器Ａｂを有する吸収冷温水機４は、次の様に接続されて、冷媒蒸気、吸収溶液が循環している。
第１の液槽１３には、吸収器Ａｂから第１の稀溶液ライン５４を介して稀溶液Ｋ１が供給される。そして、第１の液槽１３の稀溶液Ｋ１中に配置されている第１の加熱ライン１５には、外部の図示しない熱源より、加熱流体である高圧蒸気が供給されている。
第１の液槽１３で発生（再生）した冷媒蒸気は、ライン３１を介して、凝縮器Ｃｎに供給されている。
【００４１】
第２の液槽２３に配置された第２の加熱ライン１８は、図示しない高圧蒸気源に戻されるよう接続されている。第２の液槽２３の底部２３ａ（或いは高温再生器４ＨＧｅ）と低温再生器ＬＧｅとは、吸収溶液ライン４１により連通されている。
また、第２の液槽２３の上部はライン３１ａによってライン３１に接続されており、第２の液槽２３で発生（再生）した冷媒蒸気が、ライン３１ａ、ライン３１を介して、低温再生器ＬＧｅを経由して、凝縮器Ｃｎに連通する様に構成されている。
【００４２】
上記構成による吸収冷温水機４の作用を、高温再生器４ＨＧｅに関連する構成を主として説明する。
吸収器Ａｂで冷媒蒸気を吸収して稀釈された稀溶液Ｋ１は、第１の稀溶液ライン５４を介して、高温再生器４ＨＧｅの第１の熱交換部Ｃ１１に導かれる。また、外部の高圧蒸気源から、第１の加熱ライン１５に高圧蒸気が導かれる。
稀溶液Ｋ１は第１の液槽１３内で、加熱ライン１５を流れる高圧蒸気が保有する熱量により、加熱され昇温し、再生される。再生した冷媒蒸気は、ライン３１を介して凝縮器Ｃｎに供給される。この時の加熱ライン１５と稀溶液Ｋ１との熱交換の形態は、満液式熱交換である。
第１の液槽１３で加熱され濃縮された稀溶液Ｋ１は、第２の熱交換部Ｃ２１における第２の液槽２３に入り、皿体１６の小孔１６ａから液滴Ｄ１となって滴下する。この液滴Ｄ１が第２の加熱ライン１８に液膜となって接触し、第２の加熱ライン１８内を流れる加熱流体により加熱されて、昇温し、再生される。この時の加熱ライン１８と液滴Ｄ１即ち稀溶液Ｋ１との熱交換の形態は、流下液膜式熱交換である。
【００４３】
上記の伝熱形態を図式的に示すと図７と同様になり、第１および第２の加熱ライン１５および１８内の高圧蒸気は温度が一定どあるのに対し、被加熱流体である稀溶液Ｋ１の温度は徐々に上昇する。
図３で示すのと同様に、第１の熱交換部Ｃ１１では温度差△Ｔが大きいので、満液式熱交換により稀溶液Ｋ１を加熱再生させる。一方、第２の熱交換部Ｃ２１では温度差△Ｔが小さいので、流下液膜式熱交換により吸収溶液Ｌ２を加熱再生させている。
上記のようにして、高温再生器４ＨＧｅでの稀溶液Ｋ１の再生を、従来の満液式熱交換のみに比べて高い再生をさせている。
【００４４】
【発明の効果】
本発明の作用効果を、以下に列記する。
（１）第１の加熱ラインと被加熱流体との熱交換、すなわち加熱流体と被加熱流体との温度差が大きい領域では満液式熱交換とし、第２の加熱ラインと被加熱流体との熱交換、すなわち加熱流体と被加熱流体との温度差が小さい領域では流下液膜式熱交換をしているので、熱伝達量が非常に大きい。
（２）熱交換器を小型にできる。
（３）再生器に利用すれば、被加熱側の吸収溶液と加熱源との温度差が小さい領域まで熱交換を行うことが出来るので、吸収溶液の濃度幅を大きく取ることができる。そのため、高効率となる。
（４）低温再生器、排熱焚再生器に本発明を適用すれば、加熱流体が保有する熱量が吸収溶液に対して効率的に投入され、吸収溶液温度が上昇するので、高温再生器で付加される熱量を減少することが出来るので、吸収冷温水機の効率が向上する。
（５）低温再生器、排熱焚再生器、高温再生器に本発明を適用すれば、加熱流体が保有する熱量が効率的に吸収溶液に投入される結果、冷媒蒸気の再生量が増加し、吸収冷温水機の効率が向上する。
【図面の簡単な説明】
【図１】本発明の第１の実施形態にかかる熱交換器の構成図。
【図２】図１の熱交換器の斜視内部詳細図。
【図３】図１および図２に示す熱交換器の伝熱特性線図。
【図４】従来の満液式と本発明とを比較して示すデューリング線図。
【図５】本発明の第２の実施形態にかかる吸収冷温水機を示すブロック構成図。
【図６】図５で使用する低温再生器の構成図。
【図７】本発明で加熱源として蒸気を使用する場合の熱交換器の特性線図。
【図８】本発明の第３の実施形態にかかる吸収冷温水機を示すブロック構成図。
【図９】図８で使用する再生器の構成図。
【図１０】本発明で、加熱源として温水を使用する場合の熱交換器の特性線図。
【図１１】本発明の第４の実施形態にかかる吸収冷温水機を示すブロック構成図。
【図１２】図１１で使用する高温再生器の構成図。
【図１３】従来の吸収冷温水機を示すブロック構成図。
【図１４】満液式再生器の構成説明図。
【図１５】流下液膜式再生器の構成説明図。
【図１６】満液式再生器と流下液膜式再生器の総括伝熱係数の比較線図。
【符号の説明】
Ａｂ・・・吸収器
Ｃｎ・・・凝縮器
Ｅｖ・・・蒸発器
ＨＧｅ・・高温再生器
ＬＧｅ・・低温再生器
Ｌ１・・・被加熱流体
Ｄ１・・・液滴
１、２、３、４・・吸収冷温水機
１０・・熱交換器
１１・・第１の熱交換器
１３・・第１の液槽
１５・・第１の加熱ライン
１７・・接続部
１８・・第２の加熱ライン
１９・・ライン
２０・・流出ライン
２１・・第２の熱交換部
２３・・第２の液槽[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a heat exchanger (in this specification, the term “heat exchanger” means a heat exchanger of a type that performs heat exchange accompanied by phase change such as evaporation and regeneration, -Liquid) heat exchanger is not included), a regenerator, and an absorption chiller / heater, and more particularly, a technology for miniaturizing a heat exchanger and a regenerator.
[0002]
[Prior art]
FIG. 13 shows a general block configuration having a high-temperature and low-temperature double-effect regenerator in the conventional absorption chiller / heater J1. Reference numeral HGe denotes a high temperature regenerator, LGe denotes a low temperature regenerator, Cn denotes a condenser, Ev denotes an evaporator, Ab denotes an absorber, HEx denotes a high temperature side heat exchanger, and LHx denotes a low temperature side heat exchanger. Even with such a configuration in which efficiency is improved by the double effect regenerator, there is still room for improvement in efficiency.
[0003]
14 and 15 show the configuration of a conventional heat exchanger (steam generator or regenerator).
In FIG. 14, a heating line A15 through which the heating fluid flows is arranged in the heated fluid L supplied from the line A19 and flowing out from the line A20, and the amount of heat held by the heating fluid flowing through the heating line A15 is determined. A full heat exchanger for heating a heated fluid is shown. The characteristics of the overall heat transfer coefficient K and the temperature difference ΔT in this liquid heat exchanger are as follows: the temperature difference between the temperature in the heating line A15 and the fluid L to be heated is the horizontal axis, and the overall heat transfer coefficient K is vertical. In the heat transfer characteristic diagram 16 taken on the shaft, the characteristic line AL is indicated by a solid line.
[0004]
The heat transfer characteristic AL of this full liquid heat exchange has a large overall heat transfer coefficient K in proportion to the temperature difference ΔT as a characteristic when boiling occurs due to generation of steam. Therefore, the overall heat transfer coefficient K is large in the region where the temperature difference ΔT is high, but the overall heat transfer coefficient K is small in the region where the temperature difference ΔT is low. Therefore, in order to increase the solution concentration range in the regenerator, a large regenerator must be used. In other words, in the absorption chiller / heater using the full liquid heat exchanger, it is necessary to improve the overall heat transfer coefficient K in the region where the temperature difference ΔT is low.
[0005]
On the other hand, in FIG. 15, a falling liquid film heat exchanger is shown. According to this falling liquid film type heat exchanger, the heated fluid supplied through the line B19 and flowing out from the line B20 is dropped as a droplet as indicated by the symbol D. As for heating line B15 arrange | positioned in the space where dripping falls, the liquid film of the to-be-heated fluid is formed in the surface, and the calorie | heat amount which the heating fluid which flows through the inside of heating line B15 has transferred to the said liquid film.
In this falling liquid film heat exchanger, the heat transfer characteristic line when the temperature difference ΔT between the temperature in the heating line B15 and the fluid D to be heated is on the horizontal axis and the overall heat transfer coefficient K is on the vertical axis is shown in FIG. It is indicated by 16 code BL.
[0006]
The heat transfer characteristic BL of this liquid film type heat exchange has a characteristic that the overall heat transfer coefficient K does not change much with respect to the temperature difference ΔT. Therefore, the overall heat transfer coefficient K does not decrease even in a region where the temperature difference ΔT is low, but the overall heat transfer coefficient K does not increase even in a region where the temperature difference ΔT is high. Therefore, a large regenerator must be used to increase the solution concentration range in the regenerator. That is, in the absorption chiller / heater using the liquid film heat exchanger, it is necessary to improve the overall heat transfer coefficient K in a region where the temperature difference ΔT is high.
[0007]
[Problems to be solved by the invention]
The present invention has been proposed in view of the above-mentioned problems of the prior art, and is a heat exchanger having the characteristic of always maintaining a good overall heat transfer coefficient K irrespective of the temperature difference ΔT, and regeneration. Or an absorption chiller / heater equipped with such a regenerator.
[0008]
[Means for Solving the Problems]
The heat exchanger according to the present invention includes a first heat exchange unit and a second heat exchange unit, and the first heat exchange unit includes a first liquid tank and is stored in the first liquid tank. In the heated fluid, a first heating line through which the heating fluid flows is arranged (therefore, a configuration as a full liquid heat exchanger is provided), and the second heat exchanging portion is A dropping mechanism that drops the heated fluid that has passed through the first heat exchange section as droplets is provided above the second liquid tank, and the heated fluid from the dropping mechanism The second heating line is arranged in the space where the droplets of the liquid are dropped (thus having a configuration as a falling liquid film heat exchanger), the outlet of the first heating line and the second The inlet of the heating line is connected, and the bottom of the first liquid tank and the dropping mechanism are connected.
Here, in this specification, the term “heat exchanger” refers to a type that performs heat exchange with phase change such as evaporation and regeneration, such as a full liquid heat exchanger and a falling film heat exchanger. It does not include sensible heat (liquid-liquid) heat exchangers.
[0009]
According to the heat exchanger of the present invention, in a region where the temperature difference between the first heating line and the fluid to be heated is large, liquid heat exchange with a large overall heat transfer coefficient is performed, and the second heating line and the fluid to be heated are In the region where the temperature difference is small, the falling film type heat exchange with a large overall heat transfer coefficient is performed to increase the total heat transfer amount. Thereby, a heat exchanger can be reduced in size.
[0010]
The regenerator of the present invention includes a first heat exchange unit and a second heat exchange unit, and the first heat exchange unit includes a first liquid tank and is stored in the first liquid tank. A first heating line through which a heating fluid flows is arranged in the absorbing solution (which has a configuration as a full liquid heat exchanger), and the second heat exchange unit includes A second liquid tank is provided, and a dropping mechanism is provided above the second liquid tank to drop the absorbing solution that has passed through the first heat exchange unit as a droplet. The second heating line is disposed in the space where the liquid is dropped (thus, the second heating line has a configuration as a falling liquid film heat exchanger), and the outlet of the first heating line and the second heating line Is connected, and the bottom of the first liquid tank and the dropping mechanism are connected.
[0011]
According to the regenerator of the present invention having such a configuration, the first heat exchange section performs full liquid heat exchange, the second heat exchange section performs falling liquid film heat exchange, and the overall heat transfer coefficient in the entire region. Since the heat transfer efficiency in the regenerator can be improved, the size can be reduced.
In order to improve the efficiency of the regenerator, the concentration range of the absorbing solution must be widened. By widening the concentration range, the difference in saturation temperature between the dilute solution and the concentrated solution in the regenerator increases. As a result, the temperature difference ΔT between the heated side (absorbing solution) and the heating source (constant temperature) increases at the absorbing solution inlet of the regenerator, but decreases at the absorbing solution outlet. That is, the temperature difference ΔT at the absorption solution inlet of the regenerator is larger than ΔT at the absorption solution outlet.
According to the present invention, the regenerator can be made compact by using a heat exchange method suitable for a region where the temperature difference is large and a region where the temperature difference is small. In other words, the amount of regeneration can be increased with the same heat transfer area.
[0012]
The absorption chiller / heater according to the present invention includes a high-temperature regenerator, a low-temperature regenerator, a condenser, an evaporator, and an absorber. The low-temperature regenerator includes a first heat exchange unit and a first heat exchanger. The first heat exchanging unit includes a first liquid tank, and in the absorbing solution stored in the first liquid tank, the refrigerant regenerated by the high temperature regenerator A first heating line through which steam flows is disposed, and the second heat exchange unit includes a second liquid tank, and the second liquid tank is routed above the first heat exchange unit. A dropping mechanism for dropping the absorbing solution as a droplet is provided, and a second heating line is disposed in a space in which the droplet of the absorbing solution is dropped from the dropping mechanism, and the outlet of the first heating line and the first heating line are disposed. The inlet of 2 heating lines is connected, and the bottom of the first liquid tank and the dropping mechanism are connected.
[0013]
According to the present invention having such a configuration, it is possible to make the absorbing solution into a state where it can be easily regenerated by increasing the temperature, thereby improving the heat transfer efficiency in the regenerator and reducing the size. In other words, the amount of regeneration can be increased with the same heat transfer area.
[0014]
The absorption chiller / heater of the present invention includes a high-temperature regenerator, a low-temperature regenerator, a condenser, an evaporator, and an absorber, and a rare solution that connects the absorber and the high-temperature regenerator. An exhaust heat soot regenerator is interposed in the line, and the exhaust heat soot regenerator has a first heat exchange part and a second heat exchange part, and the first heat exchange part is a first liquid tank. A first heating line through which a heating fluid (for example, high-temperature water) supplied from an external heat source flows is disposed in the absorbing solution stored in the first liquid tank, The second heat exchange section includes a second liquid tank, and a dropping mechanism for dropping the absorbing solution via the first heat exchange section as a droplet is provided above the second liquid tank. A second heating line is disposed in a space where the absorbing solution droplets are dropped from the mechanism, and the outlet of the first heating line and the inlet of the second heating line are in contact with each other. It is, with the bottom portion of the first liquid tank and the dropping mechanism is connected.
According to the present invention having such a configuration, the regenerator can be reduced in size. That is, the amount of regeneration can be increased with the same heat transfer area.
[0015]
The absorption chiller / heater of the present invention includes a high temperature regenerator, a low temperature regenerator, a condenser, an evaporator, and an absorber. The high temperature regenerator includes a first heat exchange unit and a second heat exchanger. A heat exchange section, the first heat exchange section includes a first liquid tank, and in the absorbing solution stored in the first liquid tank, a heating fluid (from an external heat source ( For example, a first heating line through which high-pressure steam or the like flows is disposed, and the second heat exchange unit includes a second liquid tank, and the first heat exchange is provided above the second liquid tank. A dropping mechanism for dropping the absorbing solution via the section as a droplet, a second heating line is disposed in a space where the absorbing solution droplet is dropped from the dropping mechanism, and the first heating line An outlet and an inlet of the second heating line are connected, and a bottom of the first liquid tank and the dropping mechanism are connected.
[0016]
DETAILED DESCRIPTION OF THE INVENTION
Embodiments of the present invention will be described below with reference to the drawings.
1 and 2 show a heat exchanger 10 according to a first embodiment of the present invention.
The heat exchanger 10 includes a first heat exchange unit 11 (a portion having a full liquid type configuration) and a second heat exchange unit 21 (a portion having a falling liquid film type configuration).
The first heat exchange unit 11 has a structure in which a first heating line 15 through which a heating fluid (hot water, steam, etc.) flows is disposed in the heated fluid L1. And the 2nd heat exchange part 21 has the structure where the 2nd heating line 18 was arrange | positioned in the area | region where the droplet D1 of the to-be-heated fluid drops.
[0017]
The first heat exchanging unit 11 having the configuration of a full liquid heat exchanger is disposed in the first liquid tank 13, the inflow line 19 into which the heated fluid L1 is introduced, the heated fluid L1, and And a plurality of first heating lines 15 through which heating fluid (steam, hot water, etc.) flows.
The first liquid tank 13 has a plurality of baffle plates 13b so that the heated fluid L1 flows at a very low speed, and an outlet for guiding the heated heated fluid L1 to the second heat exchange unit 21. A portion 13c is provided.
Here, the first heating line 15 is supplied with a heating fluid (for example, hot water, high-pressure steam, or the like) from a heat source (not shown).
[0018]
The second heat exchanging part 21 having the configuration of a falling liquid film heat exchanger includes a second liquid tank 23, a dish body 16 into which the fluid L1 to be heated from the outlet part 13c is introduced, and the dish body 16 A plurality of second heating lines 18 arranged in the droplet D1 flowing down from (the heated fluid L1) and flowing the heated fluid therein, and an outflow for guiding the heated fluid L1 stored after the heating to the outside Line 20.
The upper end of the second liquid tank 23 is connected to the bottom of the first liquid tank 13, supports the dish body 16 at the top, and has a space where the falling liquid droplet D <b> 1 is diffused below the dish body 16. (I.e., provided with a dropping mechanism for dropping droplets of the heated fluid), and has a space for storing the heated fluid L <b> 1 below the second heating line 18.
A plurality of small holes 16a are perforated at the bottom of the plate body 16, and the heated fluid L1 flows as droplets.
Then, the outlet of the first heating line 15 and the inlet of the second heating line 18 are connected by a connecting portion 17.
[0019]
Next, the operation of the heat exchanger 10 having the above configuration will be described.
1 and 2, the heated fluid L1 is introduced from the upper part of the first liquid tank 13 of the heat exchanger 10 through the line 19, and the heated fluid is introduced from the side through the first heating line 15. The The heated fluid L1 flows through the liquid tank 13 at a very low speed.
On the other hand, the 1st heating line 15 arrange | positioned in the stored to-be-heated fluid L1 throws in the amount of heat which it holds to the to-be-heated fluid L1 by the heat transfer by temperature difference (DELTA) T through the line wall. Then heat and raise the temperature.
The form of heat transfer in the first heat exchange unit 11 is as described above because there is a heating line in the fluid to be heated. That is, in FIG. 3, the characteristic of the overall heat transfer coefficient K indicated by the broken line A0 is the characteristic of the region indicated by the reference numeral “A1”. That is, in the first heat exchange unit 11, the fluid L1 to be heated is heated by efficient full liquid heat exchange (heat exchange by heat transfer).
Incidentally, the dotted line BL is the overall heat transfer coefficient K in the case of the falling liquid film type, and if this form is adopted, the efficiency of heat exchange becomes low.
[0020]
In this manner, the temperature of the heated fluid L1 heated by the first heat exchange unit 11 rises, and the temperature difference ΔT with the first heating line 15 becomes small. And the to-be-heated fluid L1 flows into the upper part of the 2nd heat exchange part 21 via the exit part 13c.
On the other hand, the temperature of the heating fluid flowing in the first heating line 15 drops (as will be described later, the temperature drop is small if the heating fluid is steam, and the temperature drop is large if the heating fluid is liquid). It is led to the second heating line 18 through the connection part 17.
[0021]
The heated fluid L1 that has flowed into the second heat exchanging portion 21 flows as droplets D1 from the plurality of small holes 16a of the dish body 16, and forms a liquid film on the outer periphery of the line wall of the second heating line 18. It adheres and is heated. The form of heat transfer at this time is a falling film type heat exchange because the fluid L1 to be heated is a liquid film. That is, in the characteristic of the overall heat transfer coefficient K indicated by the broken line A0 in FIG. 3, the characteristic of the region indicated by the symbol “A2” is obtained, so that the heated fluid L1 is heated by heat exchange by heat transfer with good efficiency. Is done.
Incidentally, the dotted line AL is the overall heat transfer coefficient K in the case of the full liquid type, and if this form is adopted, the efficiency of heat exchange becomes low.
[0022]
In this way, with a specific temperature difference ΔT0 (FIG. 3) between the heating side and the heated side as a branch point, when the temperature difference ΔT is large, full-liquid heat exchange is performed, and when the temperature difference ΔT is small. As the falling film heat exchange, the overall heat transfer coefficient K is always good.
[0023]
FIG. 5 shows an absorption chiller / heater 2 according to a second embodiment which is an embodiment in which the present invention is applied to a low-temperature regenerator.
Hereinafter, a description will be given mainly of devices and parts different from the conventional absorption chiller / heater J1 shown in FIG. In addition, about the apparatus similar to the absorption cold / hot water machine J1 of FIG. 13, the same code | symbol is used repeatedly.
5 and 6, the absorption chiller / heater 2 is configured as a so-called “series flow type” absorption chiller / heater, and the low-temperature regenerator 2LGe includes a first heat exchange unit A11 and a second heat exchange unit. Part A21.
The first heat exchanging part A11 has a configuration as a full liquid heat exchanger, and the first heating line 32 is connected to a line 31 through which refrigerant vapor generated in the high temperature regenerator HGe flows. These are disposed in the absorbing solution L1 that is a fluid to be heated.
On the other hand, the second heat exchange section A21 has a configuration as a falling liquid film heat exchanger, and the second heating line 34 is disposed in the droplet D1 of the absorbing solution L1.
The following details will be described with reference to FIG.
[0024]
The first heat exchange unit A11 includes a first liquid tank 13 and a plurality of first heating lines 32 arranged in the absorbing solution L1.
The first liquid tank 13 has a plurality of baffle plates 13b so that the absorbing solution L1 guided from the high temperature regenerator HGe flows at a very slow flow rate, and the heated absorbing solution L1 is subjected to the second heat exchange. An outlet portion 13c leading to the portion A21 is provided.
The first heating line 32 becomes a plurality of straight lines (in which the refrigerant vapor guided from the high temperature regenerator HGe flows as a heating fluid) and is configured to heat the absorbing solution L1. .
[0025]
The second heat exchanging part A21 is in the second liquid tank 23, the dish body 16 into which the absorbing solution L1 introduced from the first heat exchanging part A11 is introduced, and the droplet D1 flowing down from the dish body 16 And a plurality of second heating lines 34, and an outflow line 42 that guides the absorbing solution L1 stored after the heating to the outside.
The second liquid tank 23 is connected to the bottom of the first liquid tank 13 at its upper end, supports the dish body 16 at the top, and has a space where the falling liquid droplet D1 is diffused below the dish body 16. However, it has a space for storing the heated absorbent solution L1 below the second heating line 34 (that is, provided with a dropping mechanism for dropping a droplet of the fluid to be heated).
The dish body 16 is provided with a plurality of small holes 16a at the bottom so that the absorbing solution L1 flows as droplets.
The second heating line 34 is connected to the outlet of the first heating line 32 by the connection portion 33 and is arranged in the droplet D1 as a plurality of straight lines.
[0026]
In the low-temperature regenerator 2LGe having the above configuration, the high-temperature regenerator HGe, the condenser Cn, and the absorber Ab are connected as follows.
A line 41 for guiding the absorbing solution L1 to the upper part of the first liquid tank 13 is connected to the high temperature regenerator HGe, and a first heating line 32 arranged in the absorbing solution L1 at the lower part of the first liquid tank 13 is As described above, the refrigerant vapor line 31 through which refrigerant vapor generated in the high-temperature regenerator HGe flows is connected.
A line 38 communicating with the condenser Cn is connected to the upper part of the first liquid tank 13 so as to guide the refrigerant vapor generated (regenerated) in the first liquid tank 13.
The second heating line 34 disposed in the second liquid tank 23 communicates with the condenser Cn via the line 35. The bottom 23 a of the second liquid tank 23 and the absorber Ab are connected via a line 42. The upper part of the second liquid tank 23 is connected to the condenser Cn via a line 38a (a refrigerant vapor line through which refrigerant vapor generated and regenerated in the second liquid tank 23 flows) and the line 38.
[0027]
The operation of the absorption chiller / heater 2 having the above-described configuration will be described limited to the low temperature regenerator 2LGe.
The absorption solution heated and concentrated by the high temperature regenerator HGe is guided to the first heat exchange part A11 of the low temperature regenerator 2LGe via the line 41. The refrigerant vapor generated and regenerated by the high temperature regenerator HGe is led to the first heat exchange part A11 of the low temperature regenerator 2LGe via the line 31.
The absorption solution L1 is heated in the first liquid tank 13 by the heating line 32 using the refrigerant vapor and heated up, and the evaporated refrigerant vapor is guided to the condenser Cn via the line 38. The form of heat exchange between the heating line 32 and the absorbing solution L1 at this time is full liquid heat exchange.
[0028]
The absorption solution L1 heated and regenerated in the first liquid tank 13 enters the second liquid tank 23 in the second heat exchange part A21, and flows down as a droplet D1 from the small hole 16a of the dish body 16. To do.
The droplet D1 comes into contact with the second heating line 34 as a liquid film, is heated by the amount of heat held by the heating fluid flowing in the second heating line 34, and is heated to generate refrigerant vapor (regeneration). ) The form of heat exchange between the heating line 34 and the droplet D1 (that is, the absorbing solution L1) at this time is a falling liquid film type heat exchange.
[0029]
FIG. 7 schematically illustrates the above heat transfer mode. The temperature of the refrigerant vapor flowing in the first heating line 32 and the second heating line 34 and the temperature state of the fluid L1 to be heated are shown. Show.
The left region (full liquid type) in FIG. 7 corresponds to the first heat exchanging part A11, and the temperature difference ΔT is large, so that the absorbing solution L1 is heated and regenerated by the full liquid heat exchange. On the other hand, the area on the right side of FIG. 7 (falling liquid film type) corresponds to the second heat exchanging part A21 and has a small temperature difference ΔT, so that the absorbing solution L1 is heated and regenerated by flowing down liquid film type heat exchange. I am letting.
As a result, regardless of the magnitude of the temperature difference ΔT, the absorption solution is heated by the low-temperature regenerator LGe while the overall heat transfer coefficient K is always large. Therefore, compared to the conventional full liquid heat exchange alone, High regeneration efficiency can be maintained.
FIG. 4 is a Düring diagram showing the operation of the absorption chiller / heater described in FIGS. It can be seen that heat transfer is increased to QLg in the full and falling film type synthesis in which K is best selected.
[0030]
In FIG. 8, the absorption cold / hot water machine 3 which is the 3rd Embodiment of this invention is shown. The apparatus and parts different from the conventional absorption chiller / heater J1 shown in FIG. 13 will be mainly described. In addition, about the same apparatus, the same code | symbol is duplicated and used.
8 and 9, the exhaust heat soot regenerator MGe constituting the absorption chiller / heater 3 is interposed in a dilute solution line 54 which is a dilute solution line. The exhaust heat soot regenerator MGe includes a first heat exchange part B11 and a second heat exchange part B21.
The first heat exchanging part B11 has a configuration as a full liquid heat exchanger, and the first heating line 15 through which the heating fluid flows is arranged in the rare solution K that is the fluid to be heated. Yes. On the other hand, the second heat exchanging part B21 has a configuration as a falling liquid film type heat exchanger, and the second heating line 18 is arranged in the droplet D1 of the dilute solution K. .
The following details will be described with reference to FIG.
[0031]
The first heat exchange unit B11 includes a first liquid tank 13 and a plurality of first heating lines 15 disposed in the dilute solution K.
The first liquid tank 13 has a plurality of baffle plates 13b for allowing the dilute solution K guided from the absorber Ab to flow at a very slow flow rate, and the heated dilute solution K is supplied to the second heat exchange unit. An outlet portion 13c leading to B21 is provided.
In the first heating line 15, high temperature water (which is a heating fluid) supplied from the outside flows in the first heating line 15, and heats the rare solution K as a plurality of straight lines.
[0032]
The second heat exchanging part B21 is in the second liquid tank 23, the dish body 16 into which the dilute solution K that has flowed in from the first heat exchanging part B11 is introduced, and the droplet D1 that flows down from the dish body 16. It has the some 2nd heating line 18 arrange | positioned, and the outflow line 55 which guides the dilute solution K stored after the heating outside.
The second liquid tank 23 is connected to the bottom of the first liquid tank 13 at its upper end, supports the dish body 16 at the top, and has a space where the falling liquid droplet D1 drops below the dish body 16. In addition, below the second heating line 18, there is a space for storing the heated diluted solution K.
A plurality of small holes 16a are formed in the bottom of the dish body 16, and the dilute solution K is configured to flow down as droplets.
The second heating line 18 becomes a plurality of straight lines connected to the outlet of the first heating line 15 via the connection portion 17 and is disposed in the space where the droplet D1 drops.
[0033]
The exhaust heat soot regenerator MGe having the above-described configuration has the high temperature regenerator HGe, the condenser Cn, and the absorber Ab configured as follows.
The line 54 for supplying the dilute solution K to the first liquid tank 13 is connected to the absorber Ab, and the first heating line 15 disposed in the dilute solution K of the first liquid tank 13 is connected to the outside. It is connected to a combustion exhaust heat source (not shown) which is a heat source. The refrigerant vapor generated (regenerated) from the first liquid tank 13 is supplied to the condenser Cn via the line 57.
[0034]
The 2nd heating line 18 (outlet side) arrange | positioned at the 2nd liquid tank 23 is connected to the combustion exhaust heat source which is not shown in figure. The exhaust heat soot regenerator MGe or the bottom 23 a of the second liquid tank 23 and the high temperature regenerator HGe are connected via a second dilute solution line 55.
The steam generated (regenerated) in the second liquid tank 23 is connected to the line 57 via the line 57a and communicates with the condenser Cn.
[0035]
The operation of the absorption chiller / heater 3 having the above-described configuration will be mainly described with respect to the portion related to the exhaust heat regenerator MGe.
The absorbing solution (dilute solution) K diluted by absorbing the refrigerant vapor in the absorber Ab flows into the first heat exchange part B11 of the exhaust heat regenerator MGe through the first diluted solution line 54. . In addition, a heating fluid (for example, high-temperature water) is guided to the first heating line 15 from an external exhaust heat / heat source (not shown).
The diluted solution K is heated in the first liquid tank 13 by the amount of heat held by the heating fluid (for example, high-temperature water) flowing in the heating line 15, and the generated (regenerated) refrigerant vapor passes through the line 57. To the condenser Cn. The form of heat exchange between the heating fluid (for example, high-temperature water) flowing through the heating line 15 and the rare solution K at this time is full liquid heat exchange.
The dilute solution K heated in the first liquid tank 13 enters the second liquid tank 23 in the second heat exchange section B21 and is dropped as a droplet D1 from the small hole 16a of the dish body 16 ( That is, a dropping mechanism for dropping a droplet of the fluid to be heated is provided. The droplet D1 comes into contact with the second heating line 18 as a liquid film, is heated by the amount of heat held by the heating fluid flowing in the second heating line 18, and is heated to regenerate the refrigerant vapor. . At this time, the form of heat exchange between the heating line 18 and the droplets D1, that is, the dilute solution K is a falling liquid film type heat exchange.
[0036]
FIG. 10 schematically illustrates the above heat transfer mode. The temperature change of the high-temperature water flowing in the first heating line 15 and the second heating line 18 and the diluted solution K, which is a fluid to be heated, are illustrated. The temperature change is compared with the temperature difference ΔT.
In the first heat exchange part B11, since the temperature difference ΔT is large, the dilute solution K is heated and regenerated by full liquid heat exchange. On the other hand, since the temperature difference ΔT is small in the second heat exchange part B21, the dilute solution K is heated and regenerated by the falling film heat exchange. In addition, when the heating fluid is hot water, unlike the case of steam, the temperature of the heating fluid is reduced by heat exchange.
[0037]
As described above, before the dilute solution K is regenerated in the high temperature regenerator HGe, the dilute solution K is preliminarily heated and regenerated using high temperature water of an external heat source in combination with a full liquid type and a falling liquid film type. Therefore, the heating amount in the high-temperature regenerator HGe can be saved, and the regeneration amount of the refrigerant vapor is also increased, so that the efficiency of the absorption chiller / heater is improved.
[0038]
FIG. 11 shows an absorption chiller / heater 4 according to a fourth embodiment of the present invention.
Hereinafter, the absorption chiller / heater 4 according to the embodiment of FIG. 11 will be described mainly with respect to devices and portions different from those of the conventional absorption chiller / heater J1 shown in FIG. In addition, about the same apparatus, the same code | symbol is duplicated and used.
In FIG. 11 and FIG. 12, the high temperature regenerator 4HGe constituting the absorption chiller / heater 2 is composed of a first heat exchange part C11 and a second heat exchange part C21. And the 1st heat exchange part C11 is comprised as a full liquid type heat exchanger, and the 1st heating line 15 into which a heating fluid flows into the inside is arrange | positioned in the rare solution K1 which is a to-be-heated fluid. Yes. On the other hand, the second heat exchanging part C21 is configured as a falling liquid film type heat exchanger, and the second heat exchanging part C21 is in the space where the droplet D1 of the absorbing solution L2 drops via the first heat exchanging part C11. The heating line 18 is arranged.
The following details will be described with reference to FIG.
[0039]
The first heat exchange section C11 is mainly configured by a first liquid tank 13 and a plurality of first heating lines 15 arranged in the dilute solution K1.
In the first liquid tank 13, a plurality of baffle plates 13b for allowing the dilute solution K1 to flow at a very slow flow rate, and an outlet portion 13c for guiding the heated dilute solution K1 to the second heat exchange unit C21. , And are provided.
The second heat exchanging unit C21 includes the second liquid tank 23, the dish body 16 into which the absorbing solution L2 introduced from the first heat exchanging part C11 is introduced, and the droplet D1 flowing down from the dish body 16 And a plurality of second heating lines 18 and an outflow line 41 for guiding the absorbent solution L2 stored after the heating to the outside.
The second liquid tank 23 is connected to the bottom of the first liquid tank 13 at its upper end, supports the dish body 16 at the top, and has a space where the falling liquid droplet D1 is dropped below the dish body 16. In addition, below the second heating line 18, there is a space for storing the heated absorption solution L2.
The dish body 16 is provided with a plurality of small holes 16a at the bottom so that the absorbing solution L1 is dropped as droplets.
The second heating line 18 is connected to the first heating line 15 via the connecting portion 17, and is arranged in a space where the droplet D1 drops in the form of a plurality of straight lines (that is, A dropping mechanism for dropping a droplet of the fluid to be heated is provided).
[0040]
The absorption chiller / heater 4 having the high-temperature regenerator 4HGe, the low-temperature regenerator LGe, the condenser Cn, and the absorber Ab having the above-described configuration is connected as follows, and the refrigerant vapor and the absorption solution are circulated.
The dilute solution K1 is supplied to the first liquid tank 13 from the absorber Ab via the first dilute solution line 54. And the high pressure steam which is a heating fluid is supplied to the 1st heating line 15 arrange | positioned in the dilute solution K1 of the 1st liquid tank 13 from the heat source which is not shown outside.
The refrigerant vapor generated (regenerated) in the first liquid tank 13 is supplied to the condenser Cn via the line 31.
[0041]
The 2nd heating line 18 arrange | positioned at the 2nd liquid tank 23 is connected so that it may return to the high pressure steam source which is not shown in figure. The bottom 23a (or the high temperature regenerator 4HGe) of the second liquid tank 23 and the low temperature regenerator LGe are communicated with each other through an absorbing solution line 41.
The upper part of the second liquid tank 23 is connected to the line 31 by a line 31a, and the refrigerant vapor generated (regenerated) in the second liquid tank 23 passes through the line 31a and the line 31 and is a low temperature regenerator. It is configured to communicate with the condenser Cn via LGe.
[0042]
The operation of the absorption chiller / heater 4 with the above configuration will be mainly described with respect to the configuration related to the high temperature regenerator 4HGe.
The diluted solution K1 diluted by absorbing the refrigerant vapor by the absorber Ab is guided to the first heat exchange part C11 of the high-temperature regenerator 4HGe via the first diluted solution line. Further, high-pressure steam is guided to the first heating line 15 from an external high-pressure steam source.
The dilute solution K1 is heated and heated in the first liquid tank 13 by the amount of heat held by the high-pressure steam flowing through the heating line 15, and is regenerated. The regenerated refrigerant vapor is supplied to the condenser Cn via the line 31. The form of heat exchange between the heating line 15 and the dilute solution K1 at this time is full liquid heat exchange.
The diluted solution K1 heated and concentrated in the first liquid tank 13 enters the second liquid tank 23 in the second heat exchange section C21, and is dropped as a droplet D1 from the small hole 16a of the dish body 16. . The droplet D1 comes into contact with the second heating line 18 as a liquid film, is heated by the heating fluid flowing in the second heating line 18, is heated, and is regenerated. The form of heat exchange between the heating line 18 and the droplet D1, that is, the dilute solution K1 at this time is a falling liquid film type heat exchange.
[0043]
The above heat transfer form is schematically shown in FIG. 7, and the high-pressure steam in the first and second heating lines 15 and 18 has a constant temperature, whereas the diluted solution that is a fluid to be heated. The temperature of K1 gradually increases.
As shown in FIG. 3, since the temperature difference ΔT is large in the first heat exchange section C11, the dilute solution K1 is heated and regenerated by the full liquid heat exchange. On the other hand, since the temperature difference ΔT is small in the second heat exchange section C21, the absorbing solution L2 is heated and regenerated by the falling film heat exchange.
As described above, the regeneration of the dilute solution K1 in the high-temperature regenerator 4HGe is made higher than that in the conventional full liquid heat exchange alone.
[0044]
【The invention's effect】
The effects of the present invention are listed below.
(1) Heat exchange between the first heating line and the fluid to be heated, that is, in a region where the temperature difference between the heating fluid and the fluid to be heated is large, full heat exchange is performed. In the region where the heat exchange, that is, the temperature difference between the heated fluid and the fluid to be heated is small, the falling liquid film type heat exchange is performed, so the amount of heat transfer is very large.
(2) The heat exchanger can be made small.
(3) If used in the regenerator, heat exchange can be performed up to a region where the temperature difference between the absorption solution on the heated side and the heating source is small, so that the concentration range of the absorption solution can be increased. Therefore, it becomes highly efficient.
(4) If the present invention is applied to a low-temperature regenerator and a waste heat regenerator, the amount of heat held by the heating fluid is efficiently input to the absorbing solution, and the absorbing solution temperature rises. Since the amount of added heat can be reduced, the efficiency of the absorption chiller / heater is improved.
(5) If the present invention is applied to a low-temperature regenerator, a waste heat regenerator, and a high-temperature regenerator, the amount of heat held by the heating fluid is efficiently input to the absorbing solution, resulting in an increase in the amount of refrigerant vapor regenerated. The efficiency of the absorption chiller / heater is improved.
[Brief description of the drawings]
FIG. 1 is a configuration diagram of a heat exchanger according to a first embodiment of the present invention.
2 is a detailed perspective internal view of the heat exchanger of FIG. 1. FIG.
3 is a heat transfer characteristic diagram of the heat exchanger shown in FIGS. 1 and 2. FIG.
FIG. 4 is a Duling diagram showing a comparison between a conventional full liquid type and the present invention.
FIG. 5 is a block diagram showing an absorption chiller / heater according to a second embodiment of the present invention.
6 is a configuration diagram of a low-temperature regenerator used in FIG.
FIG. 7 is a characteristic diagram of a heat exchanger when steam is used as a heating source in the present invention.
FIG. 8 is a block configuration diagram showing an absorption chiller / heater according to a third embodiment of the present invention.
9 is a configuration diagram of a regenerator used in FIG.
FIG. 10 is a characteristic diagram of a heat exchanger when hot water is used as a heating source in the present invention.
FIG. 11 is a block configuration diagram showing an absorption chiller / heater according to a fourth embodiment of the present invention.
12 is a configuration diagram of a high-temperature regenerator used in FIG.
FIG. 13 is a block diagram showing a conventional absorption chiller / heater.
FIG. 14 is a diagram illustrating the configuration of a full liquid regenerator.
FIG. 15 is a configuration explanatory view of a falling liquid film type regenerator.
FIG. 16 is a comparison diagram of the overall heat transfer coefficient of the full liquid regenerator and the falling liquid film regenerator.
[Explanation of symbols]
Ab ... Absorber
Cn: Condenser
Ev ... Evaporator
HGe ・・ High temperature regenerator
LGe ... Low temperature regenerator
L1 ... Heated fluid
D1 droplet
1, 2, 3, 4, ... Absorption chiller / heater
10. Heat exchanger
11. First heat exchanger
13. First liquid tank
15. First heating line
17. Connection part
18. Second heating line
19. Line
20. ・ Outflow line
21 .. Second heat exchange section
23 .. Second liquid tank

Claims

It has a 1st heat exchange part and a 2nd heat exchange part, and the 1st heat exchange part is provided with the 1st liquid tank, in the to-be-heated fluid stored in the 1st liquid tank Has a first heating line through which a heating fluid flows, and the second heat exchange section includes a second liquid tank, and the first heat exchange section is disposed above the second liquid tank. There is provided a dropping mechanism for dropping the fluid to be heated as a droplet, a second heating line is disposed in a space where the droplet of the fluid to be heated is dropped from the dropping mechanism, and the first heating line The heat exchanger, wherein an outlet and an inlet of the second heating line are connected, and a bottom portion of the first liquid tank and the dropping mechanism are connected.

It has a first heat exchange part and a second heat exchange part, the first heat exchange part is provided with a first liquid tank, and in the absorbing solution stored in the first liquid tank, A first heating line through which a heating fluid flows is disposed, and the second heat exchange unit includes a second liquid tank, and the second liquid tank is disposed above the first heat exchange unit. A dropping mechanism for dropping the absorbed solution as droplets is provided, a second heating line is disposed in a space in which the droplets of the absorbing solution are dropped from the dropping mechanism, and an outlet of the first heating line and the An inlet of a second heating line is connected, and the regenerator is connected to the bottom of the first liquid tank and the dropping mechanism.

A high temperature regenerator, a low temperature regenerator, a condenser, an evaporator, and an absorber; the low temperature regenerator includes a first heat exchange unit and a second heat exchange unit; 1 heat exchange part is provided with the 1st liquid tank, and the 1st heating line through which the refrigerant vapor regenerated with the high temperature regenerator flows is arranged in the absorption solution currently stored in the 1st liquid tank. The second heat exchanging unit includes a second liquid tank, and a dropping mechanism for dropping the absorbing solution passing through the first heat exchanging part as droplets is provided above the second liquid tank. Provided, a second heating line is disposed in a space in which droplets of the absorbing solution are dropped from the dropping mechanism, an outlet of the first heating line and an inlet of the second heating line are connected, and The absorption cold / hot water machine characterized by the bottom part of a 1st liquid tank, and the said dripping mechanism being connected.

It has a high temperature regenerator, a low temperature regenerator, a condenser, an evaporator, and an absorber, and an exhaust heat regenerator is installed in a rare solution line connecting the absorber and the high temperature regenerator. The exhaust heat regenerator has a first heat exchange part and a second heat exchange part, and the first heat exchange part includes a first liquid tank and is stored in the first liquid tank. A first heating line through which a heating fluid supplied from an external heat source flows is disposed in the absorbing solution, and the second heat exchange unit includes a second liquid tank, A dropping mechanism for dropping the absorbing solution via the first heat exchange section as a droplet is provided above the liquid tank, and the second is placed in the space where the absorbing solution droplet is dropped from the dropping mechanism. A heating line is disposed, the outlet of the first heating line and the inlet of the second heating line are connected, and the bottom of the first liquid tank and the dropping mechanism are in contact with each other; Absorption chiller which is characterized in that it is.

A high-temperature regenerator, a low-temperature regenerator, a condenser, an evaporator, and an absorber; the high-temperature regenerator includes a first heat exchange unit and a second heat exchange unit; 1 heat exchange part is provided with the 1st liquid tank, and the 1st heating line through which the heating fluid supplied from an external heat source flows is arranged in the absorption solution currently stored in the 1st liquid tank. The second heat exchanging unit includes a second liquid tank, and a dropping mechanism for dropping the absorbing solution passing through the first heat exchanging part as droplets is provided above the second liquid tank. Provided, a second heating line is disposed in a space in which droplets of the absorbing solution are dropped from the dropping mechanism, an outlet of the first heating line and an inlet of the second heating line are connected, and The absorption cold / hot water machine characterized by the bottom part of a 1st liquid tank, and the said dripping mechanism being connected.