JP3738955B2

JP3738955B2 - Absorption chiller / heater and control method

Info

Publication number: JP3738955B2
Application number: JP2000001432A
Authority: JP
Inventors: 部尚樹刑
Original assignee: Tokyo Gas Co Ltd
Current assignee: Tokyo Gas Co Ltd
Priority date: 2000-01-07
Filing date: 2000-01-07
Publication date: 2006-01-25
Anticipated expiration: 2020-01-07
Also published as: JP2001194021A

Description

【０００１】
【発明の属する技術分野】
本発明は、吸収器と、高温再生器と、低温再生器と、凝縮器と、蒸発器とを有する吸収冷温水機に関し、特に、所謂「一重二重効用」と呼ばれる吸収冷温水機に関する。
【０００２】
【従来の技術】
図２８は、所謂「パラレルフロー」タイプとして構成された従来の一重二重効用吸収冷温水機を示している。
図２８において、吸収器２２からポンプ２４により送出された稀溶液は、稀溶液ラインＬ１を流過し、低温溶液熱交換器２６を経て、分岐点Ｐ１で、高温再生器４４に連通するラインＬ１−１と、排熱焚再生器に連通するラインＬ１−２とに分岐する。
【０００３】
ラインＬ１−２を流れる稀溶液は、排熱焚再生器３０に供給される。排熱焚再生器３０においては、稀溶液に対して、排熱ラインＬ２を流れる排熱流体（例えば温排水等）が保有するエンタルピー（顕熱）が付加されて、加熱・一部再生される。
排熱焚再生器３０において再生された冷媒蒸気はラインＬ１３を流れて凝縮器５０へ流入する。
【０００４】
排熱焚再生器３０で加熱された吸収溶液は、ラインＬ１−２１を経由して低温再生器４８に供給される。
【０００５】
一方、分岐点Ｐ１で分岐した他方のラインＬ１−１は、高温溶液熱交換器４２を経由して、高温再生器４４に送られる。
高温再生器４４においては、例えばバーナ機構４５等の加熱手段により吸収溶液が加熱・濃縮され、これにより発生（再生）した冷媒蒸気（水蒸気）は蒸気ラインＬ１１を流れ、低温再生器４８を介して凝縮器５０（第１の凝縮器）に送られる。
【０００６】
そして、低温再生器４８において、蒸気が保有するエンタルピーにより、（ラインＬ１−２１を経由して排熱焚再生器３０から流入した）吸収溶液が再生される。そして再生した冷媒蒸気は、ラインＬ１５を介して凝縮器５０へ送られ、低温再生器４８で加熱した吸収溶液はラインＬ１−２２を流過する。
【０００７】
高温再生器４４で加熱・凝縮された吸収溶液（中間濃度溶液）は、溶液ラインＬ３を流れ、合流点Ｐ２で低温再生器４８からのラインＬ１−２２と合流する。ラインＬ３とラインＬ１−２２は、合流した後、低温溶液熱交換器２６を経由して、吸収器２２に戻る。
【０００８】
凝縮器５０で凝縮した液相冷媒は、ラインＬ５を流れて蒸発器５２へ供給される。蒸発器５２で冷水ライン（図示せず）を流れる冷水から気化熱を奪って蒸発した冷媒蒸気は、ラインＬ１７を流れて、吸収器２２へ流入する。
【０００９】
係る従来技術において、分岐点Ｐ１で分岐する２本のラインＬ１−１、Ｌ１−２を流れる吸収溶液の流量は、吸収冷温水機の圧力バランスに基いて、一定量に決定される。
これに対して、排熱ラインＬ２を経由して排熱焚再生器３０に供給される排熱（或いは、排熱ラインＬ２を流れる排熱流体が保有する熱量）は、図示しない排熱源の状態により変動する。
【００１０】
ここで、排熱ラインＬ２を流れる排熱流体の温度が、排熱焚再生器３０内の吸収溶液温度よりも十分に高温であれば、ラインＬ１−２を流れる吸収溶液流量を増加することにより、排熱焚再生器３０における再生量が増大し、高温再生器４４の加熱手段４５の高質燃料消費量を抑制して、吸収冷温水機の効率を向上出来る。
一方、排熱ラインＬ２を流れる排熱流体温度が、排熱焚再生器３０内の吸収溶液温度に対して十分に高温とは言い得ない場合には、排熱焚再生器３０における再生量は減少し、最悪の場合には、吸収溶液が保有する熱量が排熱流体へ（熱的に）逆流してしまう恐れがある。この様な場合には、ラインＬ１−１の流量を増加して、ラインＬ１−２の流量を減少する方が、吸収冷温水機の効率は良くなる。
従って、排熱流体の温度と、吸収溶液の温度とを比較して、ラインＬ１−１、Ｌ１−２を流れる吸収溶液流量を変更させることが、吸収冷温水機の効率を向上させるという見地からは好ましい。
【００１１】
しかし、排熱流体の温度と、吸収溶液の温度とを比較して、排熱焚再生器３０へ流入する吸収溶液流量を決定する様な吸収冷温水機は、現時点では存在しない。排熱流体の温度及び吸収溶液の温度には無関係に、吸収冷温水機内の溶液循環系における圧力バランスに基いて、排熱焚再生器３０へ流入する吸収溶液流量が無作為に決定されてしまうのが、現状である。
従って、排熱流体温度が高いのに排熱焚再生器３０へ流入する吸収溶液流量が少なかったり、或いは、排熱流体温度が低いのに排熱焚再生器３０へ流入する吸収溶液流量が多かったりして、吸収冷温水機の効率を向上するのに逆効してしまう、という問題点が存在する。
【００１２】
この様な問題点に対して、図２９で示す様に、吸収器（高圧側吸収器）２２Ｈから出る２本の稀溶液ラインＬ１−１１、Ｌ１−１２を設けることにより、対処することが考えられる。
すなわち、ラインＬ１−１１はポンプＰ１０−１によりヘッドが付加され高温溶液熱交換器４２を介して高温再生器４４に連通し、ラインＬ１−１２はポンプＰ１０−２によりヘッドが付加され低温溶液熱交換器２６を介して排熱焚再生器３０に連通する様に構成し、ポンプＰ１０−１、Ｐ１０−２の吐出流量を制御することにより、吸収溶液温度と排熱温度とに基いて、排熱再生器３０に流入する吸収溶液流量を調節し、以って、吸収冷温水機の効率を向上せしめることが可能である。
【００１３】
しかし、吸収器からラインを２本出して、各々のラインにポンプを介装し、各ポンプの吐出流量を（吸収溶液温度と排熱温度とに基いて）制御することは、構成を煩雑化して、吸収冷温水機製造コストを高騰化してしまう、という問題を生じてしまう。
【００１４】
【発明が解決しようとする課題】
本発明は上述した従来技術の問題点に鑑みて提案されたものであり、排熱焚再生器へ流入する吸収溶液流量を制御して、吸収冷温水機の効率を向上することが出来る様な吸収冷温水機及びその制御方法の提供を目的としている。
【００１５】
【課題を解決するための手段】
本発明の吸収冷温水機は、吸収器（２２）と、高温再生器（４４）と、低温再生器（４８）と、排熱焚再生器（３０）と、凝縮器（５０）と、蒸発器（５２）とを有する吸収冷温水機（２０）において、吸収器（２２）から送出された稀溶液が流過する稀溶液ライン（Ｌ１）は、第１の分岐点（ＢＰ）で、低温溶液熱交換器（２６）が介装されている第１の分岐ライン（Ｌ１−１）と、冷媒ドレン熱交換器（７０）が介装されている第２の分岐ライン（Ｌ１−２）とに分岐されており、高温再生器（４４）で再生した冷媒蒸気が流れるライン（Ｌ１１）の低温再生器（４８）と凝縮器（５０）の間の領域（Ｌ１１−７０）が前記冷媒ドレン熱交換器（７０）と熱的に連通しており、低温再生器（４８）を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されており、前記第１の分岐点（ＢＰ）に介装された三方弁（Ｖ１）と、排熱焚再生器（３０）と熱的に連通する排熱ライン（Ｌ２）と排熱源に連通するライン（Ｌ２Ｇ）との分岐箇所或いは合流箇所に介装された排熱投入用三方弁（ＶＥ）と、該排熱投入用三方弁（ＶＥ）が排熱ラインＬ２側を開放しているか閉鎖しているかを検出する開閉センサ（Ｓ１）と、該開閉センサ（Ｓ１）の検知信号により前記三方弁（Ｖ１）を開閉制御する制御手段（１５０）とを設け、該制御手段（１５０）は、排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を開放しているのであれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を所定量だけ増加し、排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を閉鎖しているのであれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を、所定量だけ減少する制御を行う様に構成されている。（図１、図２）
ここで、排熱源に連通するライン（Ｌ２Ｇ）を流れる排熱流体温度が低温であり、排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を閉鎖して、排熱ライン（Ｌ２）及び排熱焚再生器（３０）をバイパスしている場合には、吸収冷温水機の効率化という観点に着目すれば、排熱焚再生器（３０）に連通する第１分岐ライン（Ｌ１−１）に多量の稀溶液を流過させる必要は無い。
一方、排熱源に連通するライン（Ｌ２Ｇ）を流れる排熱流体が高温で、排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を開放して、大量の排熱を排熱焚再生器（３０）に対して投入出来る場合には、排熱焚再生器（３０）に連通する第１分岐ライン（Ｌ１−１）に多量の稀溶液が流過する方が、吸収冷温水機の効率化に寄与する。
上述した様な構成を具備する本発明によれば、排熱ライン（Ｌ２）側が開放されているか否か、換言すれば排熱焚再生器（３０）に排熱が投入されているか否かを判断し、排熱焚再生器（３０）に供給される稀溶液流量（第１分岐ラインＬ１−１を流れる吸収溶液流量）を制御しているので、排熱が有効利用されて、高温再生器（４４）で消費される高質燃料量を抑制して、吸収冷温水機の効率をさらに向上出来るのである。
【００１６】
また本発明の吸収冷温水機は、吸収器（２２）と、高温再生器（４４）と、低温再生器（４８）と、排熱焚再生器（３０）と、凝縮器（５０）と、蒸発器（５２）とを有する吸収冷温水機（２０）において、吸収器（２２）から送出された稀溶液が流過する稀溶液ライン（Ｌ１）は、第１の分岐点（ＢＰ）で、低温溶液熱交換器（２６）が介装されている第１の分岐ライン（Ｌ１−１）と、冷媒ドレン熱交換器（７０）が介装されている第２の分岐ライン（Ｌ１−２）とに分岐されており、高温再生器（４４）で再生した冷媒蒸気が流れるライン（Ｌ１１）の低温再生器（４８）と凝縮器（５０）の間の領域（Ｌ１１−７０）が前記冷媒ドレン熱交換器（７０）と熱的に連通しており、低温再生器（４８）を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されており、前記第１の分岐点（ＢＰ）に介装された三方弁（Ｖ１）と、排熱焚再生器（３０）と熱的に連通する排熱ライン（Ｌ２）を流れる流体の温度（Ｔｗ）を検出する温度センサ（Ｓ２）と、該温度センサ（Ｓ２）の検知信号により前記三方弁（Ｖ１）を開閉制御する制御手段（１５０）とを設け、該制御手段（１５０）は、排熱ライン（Ｌ２）側を流れる流体の温度（Ｔｗ）が上昇すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を増加し、排熱ライン（Ｌ２）側を流れる流体の温度（Ｔｗ）が下降すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を減少する制御を行う様に構成されている。（図３、図４）
上述した様な構成を具備する本発明によれば、排熱ライン（Ｌ２）を流れる温度（Ｔｗ）が上昇し、排熱焚再生器（３０）に排熱が有効に投入される状態であるかか否かを判断し、排熱焚再生器（３０）に供給される稀溶液流量（第１分岐ラインＬ１−１を流れる吸収溶液流量）を制御している。従って、排熱流体が保有する熱量（排熱）が投入可能か否かに基いて、第１分岐ライン（Ｌ１−１）を流れる吸収溶液流量を制御しているので、排熱の有効利用、高質燃料消費量の抑制を実現して、吸収冷温水機の効率をさらに向上している。
【００１７】
さらに本発明の吸収冷温水機は、吸収器（２２）と、高温再生器（４４）と、低温再生器（４８）と、排熱焚再生器（３０）と、凝縮器（５０）と、蒸発器（５２）とを有する吸収冷温水機（２０）において、吸収器（２２）から送出された稀溶液が流過する稀溶液ライン（Ｌ１）は、第１の分岐点（ＢＰ）で、低温溶液熱交換器（２６）が介装されている第１の分岐ライン（Ｌ１−１）と、冷媒ドレン熱交換器（７０）が介装されている第２の分岐ライン（Ｌ１−２）とに分岐されており、高温再生器（４４）で再生した冷媒蒸気が流れるライン（Ｌ１１）の低温再生器（４８）と凝縮器（５０）の間の領域（Ｌ１１−７０）が前記冷媒ドレン熱交換器（７０）と熱的に連通しており、低温再生器（４８）を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されており、前記第１の分岐点（ＢＰ）に介装された三方弁（Ｖ１）と、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）を検出する温度センサ（Ｓ３）と、該温度センサ（Ｓ３）の検知信号により前記三方弁（Ｖ１）を開閉制御する制御手段（１５０）とを設け、該制御手段（１５０）は、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）が上昇すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を減少し、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）が下降すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を増加する制御を行う様に構成されている。（図５、図６）。
上述した様な構成を具備する本発明によれば、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）が下降すれば、吸収溶液濃度が薄くなり、飽和温度が下がるため、同一熱量が投入されても排熱焚再生器（３０）における再生量が増加する。一方、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）が上昇すれば、吸収溶液濃度が濃くなり、飽和温度が上がるため、同一熱量が投入されても排熱焚再生器（３０）における再生量は減少する。
本発明では、吸収器出口温度（Ｔａ）を計測することにより、吸収溶液（或いは稀溶液）濃度が薄いか濃いか、換言すれば、飽和温度が低い（再生し易い）か高い（再生し難い）かを判断し、それに基いて、排熱焚再生器（３０）に供給される稀溶液流量（第１分岐ラインＬ１−１を流れる吸収溶液流量）を制御している。すなわち、排熱焚再生器に投入される排熱による再生量が増加するか否かに基いて、第１分岐ライン（Ｌ１−１）を流れる吸収溶液流量が制御され、排熱を有効利用し、高質燃料消費量を抑制して、吸収冷温水機の効率をさらに向上している。
【００１８】
本発明の実施に際して、排熱ライン（Ｌ２）に排熱流体が流過しているか否かを検出する開閉センサ（Ｓ１）と、排熱流体温度（Ｔｗ）を検出する温度センサ（Ｓ２）と、吸収器（２２）の出口における吸収溶液温度（Ｔａ：吸収器出口温度）を検出する温度センサ（Ｓ３）の内の何れか２つを設け、或いは３つ全てを設け、各センサで検出される各パラメータを全て参照して、制御行われる様に構成することが出来る（図７、図８）。
【００１９】
本発明において、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、該排熱焚再生器（３０）から高温再生器（４４）に向かうライン（Ｌ１−１４４）は、排熱焚再生器（３０）と高温溶液熱交換器（４２）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）に連通し（Ｌ１−４４）、高温再生器（４４）で加熱された吸収溶液は、中間濃度溶液ライン（Ｌ３）を流れて低温再生器（４８）へ流入し、低温再生器（４８）で加熱された後に高濃度溶液ライン（Ｌ４）を流れ、低温溶液熱交換器（２６）を経由して吸収器（２２）に戻る様に構成することが好ましい（図１−図８：シリーズフロータイプ）。
【００２０】
或いは、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、該排熱焚再生器（３０）から高温再生器（４４）に向かうライン（Ｌ１−１４４）は、高温溶液熱交換器（４２）と高温再生器（４４）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）に連通し、高温再生器（４４）で加熱された吸収溶液は中間濃度溶液ライン（Ｌ３）を流れて低温再生器（４８）へ流入し、低温再生器（４８）で加熱された後に高濃度溶液ライン（Ｌ４）を流れ、低温溶液熱交換器（２６）を経由して吸収器（２２）に戻る様に構成するのが好ましい（図９：シリーズフロータイプ）。
【００２１】
そして本発明は、前記第１及び第２の分岐ライン（Ｌ１−１、Ｌ１−２）は低温溶液熱交換器（２６）或いは冷媒ドレン熱交換器（７０）を経由してから直ちに第１の合流点（ＧＰ）で合流し、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−３）と排熱焚再生器（３０）に連通するライン（Ｌ１−４）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−３）を流れる稀溶液は高温溶液熱交換器（４２）を経由して高温再生器（４４）へ流入し、排熱焚再生器（３０）に連通するライン（Ｌ１−４）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−４２）は、高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し（Ｌ４）、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、前記三方弁（Ｖ１）は第１の分岐点（ＢＰ）ではなく、第２の分岐点（Ｐ１）に介装されているのが好ましい（図１０：パラレルフロータイプ）。
【００２２】
さらに本発明では、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−３）と排熱焚再生器（３０）に連通するライン（Ｌ１−４）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−３）を流れる稀溶液は高温溶液熱交換器（４２）を経由して高温再生器（４４）へ流入し、排熱焚再生器（３０）に連通するライン（Ｌ１−４）は第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流し、該ライン（合流後のＬ１−４）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−４２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し（Ｌ４）、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、第１の分岐点（ＢＰ）に介装された前記三方弁（Ｖ１）に代えて、第２の分岐点（Ｐ１）に介装された三方弁（Ｖ２）を設けているのが好ましい（図１１：パラレルフロータイプ）。
【００２３】
或いは、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−３）と排熱焚再生器（３０）に連通するライン（Ｌ１−４）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−３）を流れる稀溶液は高温溶液熱交換器（４２）を経由して高温再生器（４４）へ流入し、排熱焚再生器（３０）に連通するライン（Ｌ１−４）は第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流し、該ライン（合流後のＬ１−４）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−４２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し（Ｌ４）、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しているのが好ましい（図１２：パラレルフロータイプ）。
【００２４】
または、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−３）と排熱焚再生器（３０）に連通するライン（Ｌ１−４）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−３）を流れる稀溶液は高温溶液熱交換器（４２）を経由して高温再生器（４４）へ流入し、排熱焚再生器（３０）に連通するライン（Ｌ１−４）は第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流し、該ライン（合流後のＬ１−４）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−４２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し（Ｌ４）、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、第１の分岐点（ＢＰ）に介装された前記三方弁（Ｖ１）に加えて、第２の分岐点（Ｐ１）に介装された三方弁（Ｖ２）を設けているのが好ましい（図１３：パラレルフロータイプ）。
【００２５】
これに加えて本発明では、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−１１）と排熱焚再生器（３０）に連通するライン（Ｌ１−１２）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−１１）は第２の分岐点（Ｐ１）と高温溶液熱交換器（４２）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して（Ｌ１−４４）高温再生器（４４）へ連通し、排熱焚再生器（３０）に連通するライン（Ｌ１−１２）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−１２２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、第１の分岐点（ＢＰ）に介装された前記三方弁（Ｖ１）に代えて、第２の分岐点（Ｐ１）に介装された三方弁（Ｖ２）を設けているのが好ましい（図１４：パラレルフロータイプ）。
【００２６】
或いは本発明では、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−１１）と排熱焚再生器（３０）に連通するライン（Ｌ１−１２）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−１１）は第２の分岐点（Ｐ１）と高温溶液熱交換器（４２）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して（Ｌ１−４４）高温再生器（４４）へ連通し、排熱焚再生器（３０）に連通するライン（Ｌ１−１２）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−１２２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しているのが好ましい（図１５：パラレルフロータイプ）。
【００２７】
本発明は、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−１１）と排熱焚再生器（３０）に連通するライン（Ｌ１−１２）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−１１）は第２の分岐点（Ｐ１）と高温溶液熱交換器（４２）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して（Ｌ１−４４）高温再生器（４４）へ連通し、排熱焚再生器（３０）に連通するライン（Ｌ１−１２）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−１２２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、第１の分岐点（ＢＰ）に介装された前記三方弁（Ｖ１）に加えて、第２の分岐点（Ｐ１）に介装された三方弁（Ｖ２）を設けているのが好ましい（図１６：パラレルフロータイプ）。
【００２８】
本発明の実施に際して、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−１１）と排熱焚再生器（３０）に連通するライン（Ｌ１−１２）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−１１）は高温溶液熱交換器（４２）と高温再生器（４４）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）へ連通し、排熱焚再生器（３０）に連通するライン（Ｌ１−１２）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−１２２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、第１の分岐点（ＢＰ）に介装された前記三方弁（Ｖ１）に代えて、第２の分岐点（Ｐ１）に介装された三方弁（Ｖ２）を設けているのが好ましい（図１７：パラレルフロータイプ）。
【００２９】
本発明の実施に際して、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−１１）と排熱焚再生器（３０）に連通するライン（Ｌ１−１２）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−１１）は高温溶液熱交換器（４２）と高温再生器（４４）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）へ連通し、排熱焚再生器（３０）に連通するライン（Ｌ１−１２）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−１２２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しているのが好ましい（図１８：パラレルフロータイプ）。
【００３０】
本発明の実施に際して、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−１１）と排熱焚再生器（３０）に連通するライン（Ｌ１−１２）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−１１）は高温溶液熱交換器（４２）と高温再生器（４４）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）へ連通し、排熱焚再生器（３０）に連通するライン（Ｌ１−１２）を流れる稀溶液は排熱焚再生器（３０）で加熱されて低温再生器（４８）に流入し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−１２２）は高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通しており、第１の分岐点（ＢＰ）に介装された前記三方弁（Ｖ１）に加えて、第２の分岐点（Ｐ１）に介装された三方弁（Ｖ２）を設けているのが好ましい（図１９：パラレルフロータイプ）。
【００３１】
また本発明において、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、排熱焚再生器（３０）で加熱された吸収溶液が流れるライン（Ｌ１−３１）は、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−４４）と低温再生器（４８）に連通するライン（Ｌ１−４８）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−４４）を流れる稀溶液は高温溶液熱交換器（４２）を経由して高温再生器（４４）へ流入し、低温再生器（４８）に連通するライン（Ｌ１−４８）は第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流し、該ライン（合流後のＬ１−２）を流れる稀溶液は低温再生器（４８）に流入して加熱され、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−５１）は、高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し（Ｌ４）、低温溶液熱交換器（２６）を経由して吸収器（２２）へ連通するのが好ましい（図２０：パラレルフロータイプ）。
【００３２】
或いは、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、排熱焚再生器（３０）で加熱された吸収溶液が流れるライン（Ｌ１−３１）は、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−４４）と低温再生器（４８）に連通するライン（Ｌ１−４８）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−４４）は、第２の分岐点（Ｐ１）と高温溶液熱交換器（４２）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）へ連通し、低温再生器（４８）に連通するライン（Ｌ１−４８）を流れる稀溶液は低温再生器（４８）に流入して加熱され、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−４９）は、高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器を経由して吸収器へ連通するのが好ましい（図２１：パラレルフロータイプ）。
【００３３】
そして、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、排熱焚再生器（３０）で加熱された吸収溶液が流れるライン（Ｌ１−３１）は、第２の分岐点（Ｐ１）で高温再生器（４４）に連通するライン（Ｌ１−４４）と低温再生器（４８）に連通するライン（Ｌ１−４８）に分岐し、高温再生器（４４）に連通するライン（Ｌ１−４４）は、高温溶液熱交換器（４２）と高温再生器（４４）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して（Ｌ１−４６）高温再生器（４４）へ連通し、低温再生器（４８）に連通するライン（Ｌ１−４８）を流れる稀溶液は低温再生器（４８）に流入して加熱され、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ１−４９）は、高温再生器（４４）からの溶液ライン（Ｌ３）と第２の合流点（Ｐ２）で合流し、低温溶液熱交換器を経由して吸収器へ連通するのが好ましい（図２２：パラレルフロータイプ）。
【００３４】
本発明の実施に際して、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、排熱焚再生器（３０）で加熱された吸収溶液が流れるライン（Ｌ１−１３０）は低温再生器（４８）に連通し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ６）は、低温再生器（４８）と高温溶液熱交換器（４２）の間における第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して高温再生器（４４）へ連通し、高温再生器（４４）で加熱された吸収溶液は吸収器（２２）へ戻されるのが好ましい（図２３：リバースフロータイプ）。
【００３５】
そして、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、排熱焚再生器（３０）で加熱された吸収溶液が流れるライン（Ｌ１−１３０）は低温再生器（４８）に連通し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ６）は、高温溶液熱交換器（４２）と高温再生器（４４）の間の第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して（Ｌ６−４４）高温再生器（４４）へ連通し、高温再生器（４４）で加熱された吸収溶液は吸収器（２２）へ戻されるのが好ましい（図２４：リバースフロータイプ）。
【００３６】
これに加えて、前記第１の分岐ライン（Ｌ１−１）は、低温溶液熱交換器（２６）を経由した後に前記第２の分岐ライン（Ｌ１−２）とは合流せずに排熱焚再生器（３０）に連通し、排熱焚再生器（３０）で加熱された吸収溶液が流れるライン（Ｌ１−１３０）は、第１の合流点（ＧＰ）で前記第２の分岐ライン（Ｌ１−２）と合流して（Ｌ１−４８）低温再生器（４８）に連通し、低温再生器（４８）で加熱された吸収溶液が流れるライン（Ｌ６）は高温再生器（４４）へ連通し、高温再生器（４４）で加熱された吸収溶液は吸収器（２２）へ戻されるのが好ましい（図２５：リバースフロータイプ）。
【００３７】
本発明の実施に際しては、吸収器及び蒸発器（所謂「下胴」部分）が低圧側と高圧側の２段に構成されており、吸収冷温水機の効率化を企図しているのが好ましい（図２６、図２７）。
また、低圧側吸収器（２２Ｌ）には溶液冷却吸収器（７４）が設けられており、低圧側吸収器（２２Ｌ）内で滴下される濃縮された吸収溶液が保有するエンタルピーを稀溶液に投入し、以って、稀溶液温度を上昇せしめ、その分だけ再生し易くして、吸収冷温水機の効率を改善するのが好ましい（図２６、図２７）。
さらに、高温溶液熱交換器（４２）と高温再生器（４４）の間の領域に、高質燃料排熱投入用熱交換器（７６）が介装されており、該熱交換器（７６）を介して、当該領域を流れる吸収溶液に、高質燃料排熱ライン（Ｌ２０）を流れる高質燃料排熱（バーナ機構４５の加熱手段で吸収溶液を加熱した後に系外に廃棄される排熱）が投入されているのが好ましい（図２６、図２７）。
【００３８】
本発明によれば、低温再生器を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが、前記冷媒ドレン熱交換器（７０）を介して、前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されている。そして、前記第２の分岐ライン（Ｌ１−２）には前記冷媒ドレン熱交換器（７０）のみが介装されており、低温溶液熱交換器（２６）は介装されていない。従って、前記冷媒ドレン熱交換器（７０）を介して、低温再生器を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが、広い温度範囲に亘って、前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される。
【００３９】
低温溶液熱交換器（２６）で加熱された後の稀溶液（前記第１の分岐ラインＬ１−１を流れる稀溶液温度）の温度が、例えば６０℃−７５℃であり、低温再生器（４８）を加熱・再生した後の冷媒の温度が例えば９０℃であるとしても、前記第２の分岐ライン（Ｌ１−２）に流入する稀溶液温度は前記第１の分岐ライン（Ｌ１−１）を流れる稀溶液温度よりも遥かに低いので、７５℃−９０℃の温度範囲のエンタルピーは勿論、４０℃−７５℃の温度範囲のエンタルピー（顕熱）も、第２の分岐ライン（Ｌ１−２）を流れる稀溶液を昇温するのに用いられる。すなわち、上述した本発明によれば、高温再生器（４４）に供給される高質燃料が有効に利用されると共に、吸収溶液が効率的に昇温されるので、吸収冷温水機の効率が改善される。
【００４０】
本発明の吸収冷温水機の制御方法は、吸収器（２２）と、高温再生器（４４）と、低温再生器（４８）と、排熱焚再生器（３０）と、凝縮器（５０）と、蒸発器（５２）とを有し、吸収器（２２）から送出された稀溶液が流過する稀溶液ライン（Ｌ１）は、第１の分岐点（ＢＰ）で、低温溶液熱交換器（２６）が介装されている第１の分岐ライン（Ｌ１−１）と、冷媒ドレン熱交換器（７０）が介装されている第２の分岐ライン（Ｌ１−２）とに分岐されており、高温再生器（４４）で再生した冷媒蒸気が流れるライン（Ｌ１１）の低温再生器（４８）と凝縮器（５０）の間の領域（Ｌ１１−７０）が前記冷媒ドレン熱交換器（７０）と熱的に連通しており、低温再生器（４８）を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されており、前記第１の分岐点（ＢＰ）に介装された三方弁（Ｖ１）と、排熱焚再生器（３０）と熱的に連通する排熱ライン（Ｌ２）と排熱源に連通するライン（Ｌ２Ｇ）との分岐箇所或いは合流箇所に介装された排熱投入用三方弁（ＶＥ）と、該排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を開放しているか閉鎖しているかを検出する開閉センサ（Ｓ１）と、該開閉センサ（Ｓ１）の検知信号により前記三方弁（Ｖ１）を開閉制御する制御手段（１５０）とを有する吸収冷温水機の制御方法において、前記開閉センサ（Ｓ１）により前記排熱投入用三方弁（ＶＥ）が排熱ラインＬ２側を開放しているか閉鎖しているかを検出する工程と、排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を開放しているのであれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を所定量だけ増加し、排熱投入用三方弁（ＶＥ）が排熱ライン（Ｌ２）側を閉鎖しているのであれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を、所定量だけ減少する工程、とを含んでいる（図２）。
【００４１】
また本発明の吸収冷温水機の制御方法は、吸収器（２２）と、高温再生器（４４）と、低温再生器（４８）と、排熱焚再生器（３０）と、凝縮器（５０）と、蒸発器（５２）とを有し、吸収器（２２）から送出された稀溶液が流過する稀溶液ライン（Ｌ１）は、第１の分岐点（ＢＰ）で、低温溶液熱交換器（２６）が介装されている第１の分岐ライン（Ｌ１−１）と、冷媒ドレン熱交換器（７０）が介装されている第２の分岐ライン（Ｌ１−２）とに分岐されており、高温再生器（４４）で再生した冷媒蒸気が流れるライン（Ｌ１１）の低温再生器（４８）と凝縮器（５０）の間の領域（Ｌ１１−７０）が前記冷媒ドレン熱交換器（７０）と熱的に連通しており、低温再生器（４８）を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されており、前記第１の分岐点（ＢＰ）に介装された三方弁（Ｖ１）と、排熱焚再生器（３０）と熱的に連通する排熱ライン（Ｌ２）を流れる流体の温度（Ｔｗ）を検出する温度センサ（Ｓ２）と、該温度センサ（Ｓ２）の検知信号により前記三方弁（Ｖ１）を開閉制御する制御手段（１５０）とを有する吸収冷温水機の制御方法において、前記温度センサ（Ｓ２）により排熱ライン（Ｌ２）を流れる流体の温度（Ｔｗ）を検出する工程と、排熱ライン（Ｌ２）側を流れる流体の温度（Ｔｗ）が上昇すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を増加し、排熱ライン（Ｌ２）側を流れる流体の温度（Ｔｗ）が下降すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を減少する工程、とを含んでいる（図４）。
【００４２】
さらに本発明の吸収冷温水機の制御方法は、吸収器（２２）と、高温再生器（４４）と、低温再生器（４８）と、排熱焚再生器（３０）と、凝縮器（５０）と、蒸発器（５２）とを有し、吸収器（２２）から送出された稀溶液が流過する稀溶液ライン（Ｌ１）は、第１の分岐点（ＢＰ）で、低温溶液熱交換器（２６）が介装されている第１の分岐ライン（Ｌ１−１）と、冷媒ドレン熱交換器（７０）が介装されている第２の分岐ライン（Ｌ１−２）とに分岐されており、高温再生器（４４）で再生した冷媒蒸気が流れるライン（Ｌ１１）の低温再生器（４８）と凝縮器（５０）の間の領域（Ｌ１１−７０）が前記冷媒ドレン熱交換器（７０）と熱的に連通しており、低温再生器（４８）を経由した後の冷媒（Ｌ１１−７０を流れる冷媒）が保有するエンタルピーが前記第２の分岐ライン（Ｌ１−２）を流れる稀溶液へ投入される様に構成されており、前記第１の分岐点（ＢＰ）に介装された三方弁（Ｖ１）と、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）を検出する温度センサ（Ｓ３）と、該温度センサ（Ｓ３）の検知信号により前記三方弁（Ｖ１）を開閉制御する制御手段（１５０）とを有する吸収冷温水機の制御方法において、前記温度センサ（Ｓ３）により吸収器（２２）の出口における吸収溶液の温度（Ｔａ）を計測する工程と、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）が上昇すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を減少し、吸収器（２２）の出口における吸収溶液の温度（Ｔａ）が下降すれば、排熱焚再生器（３０）に連通する第１の分岐ライン（Ｌ１−１）を流過する稀溶液の流量を増加する工程、とを有している（図６）。
【００４３】
【発明の実施の形態】
以下、図１−図２７を参照して、本発明の実施の形態について説明する。
なお、図示の実施形態において、同様な部材については、同様な符号が付されている。
【００４４】
図１中、全体を符号２０で示す本発明の吸収式冷温水機は、所謂「シリーズフロー」タイプとして構成されている。
図１において、吸収器２２からポンプ２４により送出された稀溶液は、稀溶液ラインＬ１を流過し、分岐点ＢＰ（第１の分岐点）において、ラインＬ１−１（第１の分岐ライン）とラインＬ１−２（第２の分岐ライン）に分岐する。ラインＬ１−１には低温溶液熱交換器２６が介装されており、ラインＬ１−２には冷媒ドレン熱交換器７０が介装されている。
【００４５】
ここで、第１の分岐点ＢＰには三方弁Ｖ１が介装されており、該三方弁Ｖ１は、第１の分岐ラインＬ１−１と第２の分岐ラインＬ１−２の一方を開放し、他方を閉鎖する様に構成されている。なお符号１００は、三方弁Ｖ１の駆動手段を示している。
【００４６】
ラインＬ１−１を流れる稀溶液には、溶液ラインＬ４を流れる吸収溶液（高濃度溶液）が保有するエンタルピーが、低温溶液熱交換器２６を介して投入される。そして、ラインＬ１−２を流れる稀溶液には、冷媒ラインＬ１１の領域Ｌ１１−７０を流れる冷媒（吸収冷温水機の運転条件により、気相、液相、気液２相となる）が保有するエンタルピーが、冷媒ドレン熱交換器７０を介して投入される。
【００４７】
稀溶液ラインＬ１−１は、低温溶液熱交換器２６を経由した後、直ちに合流せずに、排熱焚再生器３０に連通する。その排熱焚再生器３０には、ラインＬ２を流れる排熱流体（例えば温排水）が供給されている。
【００４８】
ラインＬ２を流れる排熱流体は、その保有するエンタルピーを排熱焚再生器３０内の吸収溶液に対して投入し、当該吸収溶液を加熱・一部再生せしめる。そして、再生した冷媒蒸気は蒸気ラインＬ１３を介して凝縮器５０に流入する。
【００４９】
ここで、排熱ラインＬ２は、図示しない排熱源に連通するラインＬ２Ｇから分岐しており、その分岐箇所或いは合流箇所（図示の実施形態では合流箇所）には、排熱投入用三方弁ＶＥが介装されている。
【００５０】
排熱投入用三方弁ＶＥは、ラインＬ２Ｇを流れる排熱流体の温度（図示しない排熱流体温度検出手段により検出される）により、ラインＬ２を開放して排熱流体が排熱ラインＬ２を流過する様にせしめ、或いは、ラインＬ２を閉鎖して排熱流体がラインＬ２をバイパスする様にせしめるべく、開閉制御を行う様に構成されている。そして、排熱投入用三方弁ＶＥが、排熱ラインＬ２側を開放しているか、或いは閉鎖しているかは、開閉センサＳ１により検知される。
【００５１】
排熱ラインＬ２から投入されるエンタルピーにより排熱焚再生器３０内で加熱され、一部再生された後の吸収溶液は、ラインＬ１−１４４を流れ、ポンプ３２によりヘッドを付加される。
【００５２】
ポンプ３２によりヘッドを付加された吸収溶液は、合流点ＧＰで、第２の分岐ラインＬ１−２と合流する。そして、第２の分岐ラインＬ１−２とラインＬ１−１４４は、合流点ＧＰで合流した後、ラインＬ１−４４となり、高温溶液熱交換器４２を経由して高温再生器４４に連通する。
【００５３】
高温再生器４４において、吸収溶液はバーナ機構４５により加熱・濃縮され、冷媒蒸気（水蒸気）が再生される。
【００５４】
高温再生器４４で加熱・凝縮された吸収溶液（中間濃度溶液）は、中間濃度溶液ラインＬ３を流れて低温再生器４８へ流入する。この溶液が保有するエンタルピーは、高温溶液熱交換器４２により、ラインＬ１−４４（第１の合流点ＧＰと高温再生器４４とを連通するライン）を流れる吸収溶液に投入される。
低温再生器４８で加熱・再生された後の吸収溶液（高濃度溶液）は、高濃度溶液ラインＬ４を流れ、低温溶液熱交換器２６を経由して、吸収器２２に戻される。
【００５５】
一方、高温再生器４４で再生した冷媒蒸気（水蒸気：気相冷媒）は蒸気ラインＬ１１を流れ、低温再生器４８において冷媒蒸気が保有するエンタルピーを吸収溶液に供給して、低温再生器４８内の吸収溶液を再生する。
【００５６】
高温再生器４４で再生した冷媒蒸気は、低温再生器４８を出た後に、気相冷媒、液相冷媒、気液２相流のいずれかの形態でライン（或いは領域）Ｌ１１−７０を流過する。
【００５７】
このラインＬ１１−７０は、冷媒ドレン熱交換器７０を介して凝縮器５０に連通している。そして、ラインＬ１１−７０を流れる冷媒が保有するエンタルピーは、冷媒ドレン熱交換器７０を介して、第２の分岐ラインＬ１−２（稀溶液ライン）を流れる稀溶液に供給される。
【００５８】
ここで、ラインＬ１−２を流れる稀溶液に対しては、低温溶液熱交換器２６を介してラインＬ４を流れる高濃度溶液が保有する熱が投入されるのではない。そのため、従来技術においては廃棄されていた領域のエンタルピー、例えばラインＬ１１−７０を流れる冷媒における４０℃−７５℃の領域のエンタルピー（顕熱）が、ラインＬ１−２を流れる稀溶液に対して供給される。すなわち、高温再生器４４のバーナ機構４５により付加されたエンタルピーが、有効利用される。
【００５９】
図１において、ラインＬ５は凝縮器５０で凝縮した液相冷媒を蒸発器５２へ供給するための液相冷媒ラインである。また、ラインＬ１７は、蒸発器５２で冷水ライン（図示しない冷房負荷に連通しているライン：図示せず）を流れる冷水から気化熱を奪って蒸発した冷媒蒸気が流れる冷媒蒸気ラインであり、吸収器２２へ連通している。
【００６０】
ここで、ラインＬ２Ｇを流れる排熱流体温度が低温であり、排熱ラインＬ２及び排熱焚再生器３０をバイパスしている場合には、吸収冷温水機２０の効率化という観点に着目すれば、排熱焚再生器３０に連通する第１分岐ラインＬ１−１に多量の稀溶液を流過させる必要は無い。
一方、ラインＬ２Ｇを流れる排熱流体が高温で、排熱流体が（排熱ラインＬ２を介して）排熱焚再生器３０に対して保有する熱量を投入する場合には、排熱焚再生器３０に連通する第１分岐ラインＬ１−１に多量の稀溶液が流過すれば、吸収冷温水機２０の効率化に大いに寄与することとなる。
【００６１】
そのため、図１の実施形態においては、排熱投入用三方弁ＶＥの開閉状態に基いて、第１の分岐点ＢＰに介装された三方弁Ｖ１の開閉制御を行うべく、制御手段１５０を設けている。
【００６２】
以下、図２を主に参照しつつ、図１で示す実施形態における制御について説明する。
先ず、センサＳ１の検出信号が信号伝達ラインＣＬ−１を介して制御手段１５０に送出される（ステップＳＴ１）。そして、当該信号に基いて、排熱投入用三方弁ＶＥが排熱ラインＬ２側を開放しているのか、或いは閉鎖しているのかが判断される（ステップＳＴ２）。
【００６３】
排熱投入用三方弁ＶＥが排熱ラインＬ２側を開放しているのであれば（ステップＳＴ２がＹＥＳ）、制御手段１５０は、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００に対して制御信号を出力し、排熱焚再生器３０に連通する第１の分岐ラインＬ１−１（ＷＧ側）を流過する稀溶液の流量を、所定量だけ増加する（換言すれば、第１所定値までラインＬ１−１の流量を増加する）（ステップＳＴ３）。
【００６４】
一方、排熱投入用三方弁ＶＥが排熱ラインＬ２側を閉鎖しているのであれば（ステップＳＴ２がＮＯ）、排熱焚再生器３０に連通する第１の分岐ラインＬ１−１（ＷＧ側）を流過する稀溶液の流量を、所定量だけ減少する（換言すれば、第２所定値までラインＬ１−１の流量を減少する）（ステップＳＴ４）。
【００６５】
第１分岐ラインＬ１−１を流れる稀溶液流量を第１所定値或いは第２所定値に増減したならば（ステップＳＴ３、ＳＴ４を完了）、制御を続行するか否かを判断する（ステップＳＴ５）。
制御を続行するのであれば（ステップＳＴ５がＮＯ）、ステップＳＴ１に戻り、ステップＳＴ５がＹＥＳであれば、制御を終了する。
【００６６】
上述した様に、図１、図２の実施形態によれば、排熱焚再生器３０に排熱が投入されているか否かに基いて、排熱焚再生器３０に供給される稀溶液流量を制御しているので、排熱の有効利用、加熱手段４５で付加される熱量の有効利用を通じて、吸収冷温水機２０の効率をさらに向上出来るのである。
【００６７】
図３の実施形態は、溶液循環系、冷媒循環系の構成は図１、図２の実施形態と同一である。しかし、図１、図２の実施形態では、排熱投入用三方弁ＶＥ（図１）の開閉に基いて三方弁Ｖ１の制御を行っているが、図３の実施形態では、排熱ラインＬ２を流れる排熱流体温度に基いて三方弁Ｖ１を制御している。
【００６８】
図３において、排熱焚再生器３０と熱的に連通している排熱ラインＬ２には、温度センサＳ２が設置されている。そして温度センサＳ２の検出信号は、信号伝達ラインＣＬ−２を介して、制御手段１５０に送出される。
そして、制御手段１５０の制御信号は、信号伝達ラインＣＬ−Ｖ１を介して、三方弁Ｖ１の駆動手段１００へ出力される。
【００６９】
図３の実施形態における制御を、図４をも参照して説明する。
排熱ラインＬ２を流れる排熱流体の温度Ｔｗを温度センサＳ２で検出したならば（ステップＳＴ１１）、排熱流体温度が上昇したか否かを判断する（ステップＳＴ１２）。
【００７０】
排熱流体温度Ｔｗが上昇しているのであれば（ステップＳＴ１２がＹＥＳ）、制御手段１５０は、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００に制御信号を出力して、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を増加せしめる（ステップＳＴ１３）。
排熱流体温度Ｔｗが上昇し、排熱焚再生器３０に投入される熱量が増大するので、ラインＬ１−１の流量を増加すれば、排熱が有効利用されて、効率が向上するからである。
【００７１】
一方、排熱流体温度Ｔｗが下降している場合には（ステップＳＴ１２がＮＯ）、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を減少せしめる（ステップＳ１４）。排熱流体温度Ｔｗが下降すれば排熱焚再生器３０に投入される熱量も減少し、ラインＬ１−１を流れる稀溶液の再生量も減少してしまうことによる。
【００７２】
第１分岐ラインＬ１−１の流量を増減したならば（ステップＳＴ１３、ＳＴ１４の完了）、制御を終了するか否かを判断して（ステップＳＴ１５）、ステップＳＴ１５がＮＯであればステップＳＴ１１に戻る。
【００７３】
図５で示す実施形態は、溶液循環系、冷媒循環系については図１−図４の実施形態と同一であるが、温度センサの設置位置が異なっている。
図５において、稀溶液ラインＬ１の、吸収器２２とポンプ２４との間の領域に温度センサＳ３が介装されており、溶液の吸収器出口温度Ｔａを検出している。そして検出された溶液の吸収器出口温度Ｔａは、信号伝達ラインＣＬ−３を介して制御手段１５０に送られる。
【００７４】
制御手段１５０からの制御信号は、信号伝達ラインＣＬ−Ｖ１を介して、第１分岐点ＢＰの三方弁Ｖ１（の駆動手段１００）に対して出力されるのである。
その他の構成は、図１−図４と同様である。
【００７５】
次に、図６をも参照して、図５の実施形態の制御について説明する。
吸収溶液の吸収器出口温度Ｔａを温度センサＳ２で検出したならば（ステップＳＴ２１）、当該吸収器出口温度Ｔａが上昇したか否かを判断する（ステップＳＴ２２）。
【００７６】
吸収器出口温度Ｔａが上昇（ステップＳＴ２２がＹＥＳ）するということは、稀溶液濃度が濃くなったことを意味している。そして稀溶液濃度が濃くなれば、飽和温度が上昇する。従って、同一熱量の排熱が投入されても、再生蒸気量は減少してしまう。そのため、同一流量の稀溶液が排熱焚再生器３０に供給されても、再生量は減少する。従って、ステップＳＴ２２がＹＥＳの場合、制御手段１５０は、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００に制御信号を出力して、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を減少せしめる（ステップＳ２３）。
【００７７】
一方、吸収器出口温度Ｔａが下降している場合には（ステップＳＴ２２がＮＯ）、稀溶液濃度が薄くなっており、飽和温度が下降する。そのため、同一熱量の排熱が投入された際に排熱焚再生器３０における再生量は増加する（再生し易い状態となる）。従って、ステップＳＴ２２がＮＯの場合は、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を増加せしめ（ステップＳ２４）、排熱焚再生器３０の再生量を増加して、高温再生器４４における高質燃料消費量を抑制して、吸収冷温水機の効率を向上するのである。
【００７８】
第１分岐ラインＬ１−１の流量を減増したならば（ステップＳＴ２３、ＳＴ２４の完了）、制御を終了するか否かを判断して（ステップＳＴ２５）、ステップＳＴ２５がＮＯであればステップＳＴ２１に戻る。
【００７９】
図１、図２の実施形態、図３、図４の実施形態、図５、図６の実施形態は、それぞれ単一のセンサＳ１、Ｓ２、Ｓ３により、単一のパラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗの昇降、吸収器２２の出口における吸収溶液の液温Ｔａの昇降）に基いて、三方弁Ｖ１の開閉制御が行われている。
しかし、複数のセンサ及び複数のパラメータを組み合わせて制御することも可能である。
【００８０】
図７、図８の実施形態では、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出される各パラメータを全て参照して、制御が為されている。
その他の構成については、図７、図８の実施形態は、図１−図６の実施形態と同様である。
【００８１】
次に、図８を主として参照しつつ、図７の実施形態の制御について説明する。先ず、センサＳ１により排熱ラインＬ２に排熱流体が流過しているか否かを検出し、センサＳ２により排熱流体温度Ｔｗを検出し、センサＳ３により吸収器２２の出口温度Ｔａを検出する（ステップＳＴ３１）。
【００８２】
排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａを検出したならば（ステップＳＴ３１の完了）、ステップＳ１−Ｓ３で検出された各パラメータに基いて、各種数式、特性曲線、マップ、その他に基いて、その時点における排熱焚再生器３０への最適な稀溶液流量、換言すれば、第１分岐ラインＬ１−１における最適流量を決定する（ステップＳＴ３２）。
【００８３】
次に、ステップＳＴ３２で決定された最適流量Ｑｃと、その時点における第１分岐ラインＬ１−１における稀溶液流量Ｑｐとを比較する（ステップＳＴ３３）。
【００８４】
ステップＳＴ３２で決定された最適流量Ｑｃが、その時点における第１分岐ラインＬ１−１における稀溶液流量Ｑｐよりも少量である場合には（ステップＳＴ３３が「Ｑｃ＜Ｑｐ」）、制御手段１５０は、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００に制御信号を出力して、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を減少せしめる（ステップＳ３４）。
【００８５】
ステップＳＴ３２で決定された最適流量Ｑｃが、その時点における第１分岐ラインＬ１−１における稀溶液流量Ｑｐと等しい場合には（ステップＳＴ３３が「Ｑｃ＝Ｑｐ」）、三方弁Ｖ１の開度を変化せずに、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を維持する（ステップＳ３５）。
【００８６】
ステップＳＴ３２で決定された最適流量Ｑｃが、その時点における第１分岐ラインＬ１−１における稀溶液流量Ｑｐよりも多量である場合には（ステップＳＴ３３が「Ｑｃ＞Ｑｐ」）、制御手段１５０は、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００に制御信号を出力して、排熱焚再生器３０に連通する第１分岐ラインＬ１−１（ＷＧ側）の稀溶液流量を増加する（ステップＳ３６）。
【００８７】
第１分岐ラインＬ１−１の流量制御を完了（ステップＳＴ３４、ＳＴ３５、ＳＴ３６の完了）、制御を終了するか否かを判断する（ステップＳＴ３７）。ステップＳＴ３７がＮＯであればステップＳＴ３１に戻る。
【００８８】
図９の実施形態も、図１−図８の実施形態と同様に、所謂「シリーズフロータイプ」の吸収冷温水機にかかるものである。
【００８９】
この実施形態においても、分岐点ＢＰで分岐した稀溶液ラインＬ１−１は、低温溶液熱交換器２６を経由した後に直ちに合流せず、排熱焚再生器３０に連通する。しかし図９の実施形態は、図１−図８の実施形態と比較して、第１の分岐ラインＬ１−１と第２の分岐ラインＬ１−２との合流点（第１合流点ＧＰ）の位置が異なっている。
【００９０】
図９において、稀溶液ラインＬ１−１を介して排熱焚再生器３０に供給された稀溶液は、排熱ラインＬ２から投入されるエンタルピーにより加熱され、一部再生された後、ラインＬ１−１４４を流れ、ポンプ３２によりヘッドを負荷され、高温溶液熱交換器４２を経由する。
それから、高温溶液熱交換器４２と高温再生器４４との間の領域における第１合流点ＧＰにおいて、第１分岐ラインＬ１−２と第２分岐ラインＬ１−２とは合流し、ラインＬ１−４４となり、高温再生器４４に連通する。
【００９１】
図９の実施形態におけるその他の構成及び作用効果は、図１−図８の実施形態と同様である。そして、図９の実施形態の第１分岐点ＢＰにおける三方弁Ｖ１の開閉制御についても、図１−図８の実施形態と同様である。
【００９２】
図９においては、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号は信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００に送られている。
【００９３】
しかし、図９の実施形態においても、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１つのみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【００９４】
図１−図９は、所謂「シリーズフロー」タイプの吸収冷温水機について本発明を適用した実施形態である。これに対して、図１０の実施形態は、所謂「パラレルフロー」タイプの吸収冷温水機について本発明を適用したものである。
【００９５】
図１０において、吸収器２２から出た稀溶液は、ポンプ２４によりヘッドを付加されて稀溶液ラインＬ１を流れ、第１の分岐点ＢＰにおいて、ラインＬ１−１とラインＬ１−２に分岐する。ここで、ラインＬ１−１には低温溶液熱交換器２６が介装されており、ラインＬ１−２には冷媒ドレン熱交換器７０が介装されている。
【００９６】
ラインＬ１−１とラインＬ１−２とは、低温溶液熱交換器２６或いは冷媒ドレン熱交換器７０を経由してから、その近傍に設けられた第１の合流点ＧＰで合流してラインＬ１−Ｐ１となる。このラインＬ１−Ｐ１は、第２の分岐点Ｐ１において、高温再生器４４に連通するラインＬ１−３と、排熱焚再生器３０に連通するラインＬ１−４とに分岐する。
【００９７】
そして図１０の実施形態においては、この第２分岐点Ｐ１において三方弁Ｖ２が介装されており、三方弁Ｖ２の駆動手段１２０に対しては、信号伝達ラインＣＬ−Ｖ２を介して、制御手段１５０から制御信号が送られる様に構成されている。
なお、センサＳ１、Ｓ２、Ｓ３の設置位置については、図１−図９の実施形態と同様である。
【００９８】
ラインＬ１−３を流れる稀溶液は、高温溶液熱交換器４２を介して高温再生器４４へ流入し、バーナ機構４５により加熱・濃縮された後、溶液ラインＬ３を流れる。
高温再生器４４で再生した冷媒蒸気は、低温再生器４８に連通するラインＬ１１を流れ、低温再生器４８内の吸収溶液に保有するエンタルピーを供給して冷媒を再生した後、ラインＬ１１−７０を流れ、冷媒ドレン熱交換器７０を介してラインＬ１−２内の稀溶液にエンタルピーを供給し、凝縮器５０へ送られる。
【００９９】
ラインＬ１−４を流れる稀溶液は、排熱焚再生器３０において、排熱ラインＬ２を流れる排熱流体が保有するエンタルピーが投入され、加熱・再生・濃縮される。そして、排熱焚再生器３０で再生された冷媒蒸気は、ラインＬ１３を介して凝縮器５０に供給され、再生・濃縮後の吸収溶液は、溶液ラインＬ１−４１を流れて、低温再生器４８に流入する。
【０１００】
低温再生器４８で加熱・再生・濃縮された吸収溶液は溶液ラインＬ１−４２を流れ、溶液ラインＬ１−４２は、第２の合流点Ｐ２において、高温再生器４４からの溶液ラインＬ３と合流して溶液ラインＬ４となり、吸収器２２へ戻る。
【０１０１】
この実施形態においても、図１の実施形態で説明したのと同様に、ラインＬ１１−７０を流れる冷媒が保有するエンタルピーが、広い温度範囲に亘って、冷媒ドレン熱交換器７０を介して、稀溶液ラインＬ１−２内を流れる稀溶液に供給され、高温再生器４４（のバーナ機構４５）において付与されたエンタルピーが、冷媒蒸気発生のために有効に利用される。
また、排熱流体が保有するエンタルピーが、排熱焚再生器３０における再生で利用されるので、排熱流体の保有するエンタルピーの利用効率も向上する。
その結果、吸収冷温水機全体の効率が上昇する。
【０１０２】
図１０の実施形態におけるその他の構成及び作用効果は、図１−図９の実施形態と同様である。そして、図１０の実施形態の第２分岐点Ｐ１における三方弁Ｖ２の開閉制御は、図１−図９の実施形態の、第１分岐点ＢＰにおける三方弁Ｖ１の開閉制御と同様である。
【０１０３】
従って、排熱流体温度と吸収溶液との相対関係に基いて、三方弁Ｖ１を開閉制御することにより、排熱焚再生器３０に流入する吸収溶液の流量を制御し、以って、吸収冷温水機の効率を向上せしめることが出来る。
【０１０４】
図１０においては、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１０５】
しかし、図１０の実施形態においても、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１つのみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１０６】
図１１の実施形態も、「パラレルフロータイプ」の吸収冷温水機に係る実施形態である。
図１０で示す実施形態では、第１の分岐点ＢＰで分岐した２本のラインＬ１−１とＬ１−２は、低温溶液熱交換器２６或いは冷媒ドレン熱交換器７０を経由してから直ちに、その近傍に設けられた第１の合流点ＧＰで合流している。
【０１０７】
これに対して、図１１の実施形態では、第１の分岐点ＢＰで分岐した稀溶液ラインＬ１−１は、低温溶液熱交換器２６を経由した後、直ちに合流すること無く、第２の分岐点Ｐ１で、高温再生器４４に連通するラインＬ１−３と、ラインＬ１−４とに分岐する。そしてラインＬ１−４において、第１の合流点ＧＰで他方の分岐ラインＬ１−２と合流して、排熱焚再生器３０に連通するのである。
【０１０８】
換言すれば、図１１の実施形態では、第１の合流点ＧＰは、第２の分岐点Ｐ１と排熱焚再生器３０との間の領域に設けられている。
【０１０９】
図１１の実施形態におけるその他の構成は図１０で示す実施形態と同様である。そして、図１１の実施形態の第２分岐点Ｐ１における三方弁Ｖ２の開閉制御は（図１０の実施形態の第２分岐点Ｐ１における三方弁Ｖ２の開閉制御と略々等しく）、図１−図９の実施形態の、第１分岐点ＢＰにおける三方弁Ｖ１の開閉制御と同様である。
【０１１０】
図１１においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１１１】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１つのみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１１２】
図１２で示す実施形態は、図１１で示す実施形態と、溶液循環系、冷媒循環系、その他の構成が殆ど同一である。
しかし、図１１で示す実施形態では、第２の分岐点Ｐ１に三方弁Ｖ２を設け、当該三方弁Ｖ２の開閉制御をしているのに対して、図１２で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設け、当該三方弁Ｖ１に対して開閉制御を行っている。
【０１１３】
図１２の実施形態におけるその他の構成、作用効果は図１１の実施形態と同様であり、分岐点に設けた三方弁の開閉制御の態様も同様である。
【０１１４】
ここで、図１２においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１１５】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１１６】
図１３で示す実施形態も、図１１或いは図１２で示す実施形態と、溶液循環系、冷媒循環系、その他の構成が殆ど同一である。
図１１で示す実施形態では、第２の分岐点Ｐ１に三方弁Ｖ２を設け、当該三方弁Ｖ２の開閉制御をしており、図１２で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設け、当該三方弁Ｖ１に対して開閉制御を行っている。
【０１１７】
これに対して、図１３で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設けると共に、第２の分岐点Ｐ１にも三方弁Ｖ２を設け、制御手段１５０から、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００へ制御信号を出力し、且つ、伝達ラインＣＬ−Ｖ２を介して三方弁Ｖ２の駆動手段１２０へ制御信号を出力することにより、三方弁Ｖ１及びＶ２の双方を開閉制御している。
【０１１８】
図１３の実施形態におけるその他の構成、作用効果は図１１、図１２の実施形態と同様であり、第１分岐点ＢＰに設けた三方弁Ｖ１と、第２分岐点Ｐ１に設けた三方弁Ｖ２の開閉制御の態様も、図１−図１２の実施形態と同様である。
【０１１９】
ここで、図１３においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１２０】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１２１】
図１４で示す実施形態も「パラレルフロータイプ」の吸収冷温水機にかかるものである。
図１４において、分岐ラインＬ１−１は低温溶液熱交換器２６を経由した後に、他方の分岐ラインＬ１−２と直ちに合流せず、第２の分岐点Ｐ１で、高温再生器４４側に向かうラインＬ１−１１と、排熱焚再生器３０に連通するラインＬ１−１２とに分岐する。
【０１２２】
ここで、第２分岐点Ｐ１には三方弁Ｖ２が設けられており、三方弁Ｖ２の駆動手段１２０に対しては、信号伝達ラインＣＬ−Ｖ２を介して、制御手段１５０から制御信号が出力され、開閉制御が行われる。
【０１２３】
高温再生器４４側に向かうラインＬ１−１１は、第２分岐点Ｐ１と高温溶液熱交換器４２との間の領域における第１の合流点ＧＰで分岐ラインＬ１−２と合流してラインＬ１−４４となり、高温再生器４４へ連通する。
【０１２４】
一方、ラインＬ１−１２は排熱焚再生器３０に連通し、排熱焚再生器３０で加熱・一部再生された吸収溶液はラインＬ１−１２１を介して低温再生器４８に供給される。そして、低温再生器４８で加熱・一部再生された吸収溶液はラインＬ１−１２２を流れ、該ラインＬ１−１２２は第２の合流点ＰでラインＬ３と合流してラインＬ４となり、吸収器２２に戻る。
【０１２５】
図１４の実施形態におけるその他の構成は図１１−図１３で示す実施形態と同様である。また、作用効果については、図１−図１３で示す実施形態と同様である。
第２分岐点Ｐ１に設けた三方弁Ｖ２の開閉制御の態様も同様である。
【０１２６】
ここで、図１４においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１２７】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１２８】
図１５で示す実施形態は、図１４で示す実施形態と、溶液循環系、冷媒循環系、その他の構成が殆ど同一である。
しかし、図１４で示す実施形態では、第２の分岐点Ｐ１に三方弁Ｖ２を設け、当該三方弁Ｖ２の開閉制御をしているのに対して、図１５で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設け、当該三方弁Ｖ１に対して開閉制御を行っている。
【０１２９】
図１５の実施形態におけるその他の構成、作用効果は図１４の実施形態と同様であり、第１分岐点ＢＰに設けた三方弁Ｖ１の開閉制御の態様も同様である。
【０１３０】
ここで、図１５においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１３１】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１３２】
図１６で示す実施形態も、図１４或いは図１５で示す実施形態と、溶液循環系、冷媒循環系、その他の構成が殆ど同一である。
図１４で示す実施形態では、第２の分岐点Ｐ１に三方弁Ｖ２を設け、当該三方弁Ｖ２の開閉制御をしており、図１５で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設け、当該三方弁Ｖ１に対して開閉制御を行っている。
【０１３３】
これに対して、図１６で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設けると共に、第２の分岐点Ｐ１にも三方弁Ｖ２を設け、制御手段１５０から、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００へ制御信号を出力し、且つ、伝達ラインＣＬ−Ｖ２を介して三方弁Ｖ２の駆動手段１２０へ制御信号を出力することにより、三方弁Ｖ１及びＶ２の双方を開閉制御している。
【０１３４】
図１６の実施形態におけるその他の構成、作用効果は図１４、図１５の実施形態と同様であり、第１分岐点ＢＰに設けた三方弁Ｖ１と、第２分岐点Ｐ１に設けた三方弁Ｖ２の開閉制御の態様も、図１−図１５の実施形態と同様である。
【０１３５】
ここで、図１６においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１３６】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１３７】
図１７の実施形態も、「パラレルフロータイプ」の吸収冷温水機に係るものを示している。
図１７において、分岐ラインＬ１−１は低温溶液熱交換器２６を経由した後に、第２の分岐点Ｐ１で、高温再生器４４側に向かうラインＬ１−１１と、排熱焚再生器３０に連通するラインＬ１−１２とに分岐する。
【０１３８】
ここで、第２分岐点Ｐ１には三方弁Ｖ２が設けられており、三方弁Ｖ２の駆動手段１２０に対しては、信号伝達ラインＣＬ−Ｖ２を介して、制御手段１５０から制御信号が出力され、開閉制御が行われる。
【０１３９】
そしてラインＬ１−１１は高温溶液熱交換器４２を経由し、高温溶液熱交換器４２と高温再生器４４との間の領域における第１の合流点ＧＰで、分岐ラインＬ１−２と合流してラインＬ１−４４となり、高温再生器４４へ連通する。
【０１４０】
図１７の実施形態におけるその他の構成は図１０−図１６で示す実施形態と同様である。また、図１７の実施形態の作用効果については、図１−図１６で示す実施形態と同様である。また、第２分岐点Ｐ１における三方弁Ｖ２の開閉制御についても、図１−図１６の実施形態と同様である。
【０１４１】
図１８で示す実施形態は、図１７で示す実施形態と、溶液循環系、冷媒循環系、その他の構成が殆ど同一である。
しかし、図１７で示す実施形態では、第２の分岐点Ｐ１に三方弁Ｖ２を設け、当該三方弁Ｖ２の開閉制御をしているのに対して、図１８で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設け、当該三方弁Ｖ１に対して開閉制御を行っている。
【０１４２】
図１８の実施形態におけるその他の構成、作用効果は図１７の実施形態と同様であり、第１分岐点ＢＰに設けた三方弁Ｖ１の開閉制御の態様も同様である。
【０１４３】
ここで、図１８においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１４４】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１４５】
図１９で示す実施形態も、図１７或いは図１８で示す実施形態と、溶液循環系、冷媒循環系、その他の構成が殆ど同一である。
図１７で示す実施形態では、第２の分岐点Ｐ１に三方弁Ｖ２を設け、当該三方弁Ｖ２の開閉制御をしており、図１８で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設け、当該三方弁Ｖ１に対して開閉制御を行っている。
【０１４６】
これに対して、図１９で示す実施形態では、第１の分岐点ＢＰに三方弁Ｖ１を設けると共に、第２の分岐点Ｐ１にも三方弁Ｖ２を設け、制御手段１５０から、信号伝達ラインＣＬ−Ｖ１を介して三方弁Ｖ１の駆動手段１００へ制御信号を出力し、且つ、伝達ラインＣＬ−Ｖ２を介して三方弁Ｖ２の駆動手段１２０へ制御信号を出力することにより、三方弁Ｖ１及びＶ２の双方を開閉制御している。
【０１４７】
図１９の実施形態におけるその他の構成、作用効果は図１７、図１８の実施形態と同様であり、第１分岐点ＢＰに設けた三方弁Ｖ１と、第２分岐点Ｐ１に設けた三方弁Ｖ２の開閉制御の態様も、図１−図１８の実施形態と同様である。
【０１４８】
ここで、図１９においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１４９】
しかし、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１５０】
図２０の実施形態もパラレルフロータイプの吸収冷温水機に係るものを示している。
図２０において、稀溶液ラインＬ１は第１の分岐点ＢＰで第１分岐ラインＬ１−１と、第２分岐ラインＬ１−２とに分岐する。第１分岐ラインＬ１−１には低温溶液熱交換器２６が介装されており、第２分岐ラインＬ１−２は冷媒ドレン熱交換器７０を介装している。
【０１５１】
ここで、第１分岐点ＢＰには三方弁Ｖ１が介装されており、三方弁Ｖ１の駆動手段１００に対しては、信号伝達ラインＣＬ−Ｖ１を介して、制御手段１５０から制御信号が出力され、以って、三方弁Ｖ１の開閉制御が行われる。
【０１５２】
第１分岐ラインＬ１−１は低温溶液熱交換器２６を経由した後に、排熱焚再生器３０に連通する。そして、排熱焚再生器３０で加熱・一部再生された吸収溶液はラインＬ１−３１を流れ、該ラインＬ１−３１は、第２の分岐点Ｐ１で、高温再生器４４側に向かうラインＬ１−４４と、低温再生器４８側へ向かうラインＬ１−４８とに分岐する。
【０１５３】
ここでラインＬ１−４８は、第１の合流点ＧＰで分岐ラインＬ１−２と合流してラインＬ１−４９となり、低温再生器４８へ連通する。
低温再生器４８で加熱・一部再生された吸収溶液はラインＬ１−５１を流れ、該ラインＬ１−５１は第２の合流点Ｐ１でラインＬ３と合流して、ラインＬ４となる。
【０１５４】
図２０の実施形態におけるその他の構成は図１０−図１９で示す実施形態と同様である。また、図２０の実施形態の作用効果については、図１−図１９で示す実施形態と同様である。
さらに、図２０の実施形態における第１分岐点ＢＰに設置された三方弁Ｖ１の開閉制御の態様についても、図１−図１９の実施形態と同様である。
【０１５５】
図２０においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１５６】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１５７】
図２１の実施形態も、パラレルフロータイプの吸収冷温水機に係る。
図２１において、第１分岐点ＢＰで分岐した２本の分岐ラインＬ１−１、Ｌ１−２の内、低温溶液熱交換器２６を介装している分岐ラインＬ１−１は、排熱焚再生器３０に連通し、排熱焚再生器３０で加熱・一部再生された吸収溶液はラインＬ１−３１を流れ、該ラインＬ１−３１は、第２の分岐点Ｐ１で、高温再生器４４側に向かうラインＬ１−４４と、低温再生器４８側へ向かうラインＬ１−４８とに分岐する。
【０１５８】
第１分岐点ＢＰには三方弁Ｖ１が設けられ、三方弁Ｖ１の駆動手段１００に対しては、信号伝達ラインＣＬ−Ｖ１を介して、制御手段１５０から制御信号が出力され、以って、三方弁Ｖ１の開閉制御を行っている。
【０１５９】
図２１の実施形態では、高温再生器４４側に向かうラインＬ１−４４が、第２分岐点Ｐ１と高温溶液熱交換器４２との間の領域における第１の合流点ＧＰで、分岐ラインＬ１−２と合流してラインＬ１−４６となり、該ラインＬ１−４６は高温溶液熱交換器４２を経由して高温再生器４４へ連通する。
【０１６０】
一方、ラインＬ１−４８を介して低温再生器４８に供給され、加熱・一部再生された吸収溶液はラインＬ１−４９を流れ、第２の合流点Ｐ１でラインＬ３と合流して、ラインＬ４となる。
【０１６１】
図２１の実施形態におけるその他の構成は図２０で示す実施形態と同様である。また、図２１の実施形態の作用効果については、図１−図２０で示す実施形態と同様である。
そして、第１分岐点ＢＰに設けた三方弁Ｖ１の開閉制御の態様も、図１−図２０の実施形態と同様である。
【０１６２】
図２１においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１６３】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１６４】
図２２も、パラレルフロータイプの吸収冷温水機にかかる実施形態を示している。
図２２においても、稀溶液ラインＬ１は第１の分岐点ＢＰで、低温溶液熱交換器２６を介装した第１の分岐ラインＬ１−１と、冷媒ドレン熱交換器７０を介装した第２の分岐ラインＬ１−２とに分岐している。
【０１６５】
第１の分岐点ＢＰには三方弁Ｖ１が設けられ、三方弁Ｖ１の駆動手段１００に対しては、信号伝達ラインＣＬ−Ｖ１を介して、制御手段１５０から制御信号が出力される。これにより、三方弁Ｖ１の開閉制御が行われる。
【０１６６】
第１の分岐ラインＬ１−１を流れる吸収溶液は、低温溶液熱交換器２６、排熱焚再生器３０、ラインＬ１−３１、第２の分岐点Ｐ１を介して高温再生器４４側に向かうラインＬ１−４４を流れる。そしてラインＬ１−４４は、高温溶液熱交換器４２と高温再生器４４との間の領域における第１の合流点ＧＰで、分岐ラインＬ１−２と合流してラインＬ１−４６となり、高温再生器４４へ連通している。
【０１６７】
図２２の実施形態におけるその他の構成は図２１で示す実施形態と同様である。また、図２２の実施形態の作用効果については、図１−図２１で示す実施形態と同様である。
さらに、第１分岐点ＢＰに設けられた三方弁Ｖ１の開閉制御の態様についても、図１−図２１と同様である。
【０１６８】
図２２においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１６９】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１７０】
図２３−図２５は、本発明を所謂「リバースフロー」タイプの吸収冷温水機に適用した実施形態を示している。
【０１７１】
図２３で示す実施形態にかかる吸収冷温水機において、吸収器２２を出てポンプ２４でヘッドを付加された稀溶液は、稀溶液ラインＬ１を流れ、稀溶液ラインＬ１は、第１の分岐点ＢＰにおいて、低温溶液熱交換器２６が介装された第１の分岐ラインＬ１−１と、冷媒ドレン熱交換器７０が介装されている第２の分岐ラインＬ１−２とに分岐している。
【０１７２】
第１分岐点ＢＰには三方弁Ｖ１が設けられ、三方弁Ｖ１の駆動手段１００に対しては、信号伝達ラインＣＬ−Ｖ１を介して、制御手段１５０から制御信号が出力されており、以って、三方弁Ｖ１の開閉制御を行っている。
【０１７３】
第１の分岐点ＢＰで分岐した稀溶液ラインＬ１−１は、低温溶液熱交換器２６を経由した後、排熱焚再生器３０に連通し、その内部を流れる吸収溶液を排熱焚再生器３０へ供給する。
【０１７４】
排熱焚再生器３０で加熱・一部再生された吸収溶液は、ラインＬ１−１３０を流れて低温再生器４８に供給される。そして、低温再生器４８で加熱・一部再生された吸収溶液は、ラインＬ６を流れ、ポンプ６２でヘッドが負荷される。そして、ラインＬ６は、低温再生器４８と高温溶液熱交換器４２との間の領域における第１の合流点ＧＰで、第２の分岐ラインＬ１−２と合流してラインＬ６−４４となる。
【０１７５】
ラインＬ６−４４は高温溶液熱交換器４２を経由して、高温再生器４４に連通する。
高温再生器４４のバーナ機構４５で加熱・濃縮された吸収溶液は、溶液ラインＬ３を流れて吸収器２２へ戻される。
【０１７６】
高温再生器４４で再生した冷媒蒸気は、低温再生器４８に連通するラインＬ１１を流れ、低温再生器４８内の吸収溶液に保有するエンタルピーを供給して冷媒を再生した後、ラインＬ１１−７０を流れ、冷媒ドレン熱交換器７０を介してラインＬ１−２内の稀溶液にエンタルピーを供給し、凝縮器５０へ送られる。
【０１７７】
図２３の実施形態においても、図１−図２２の実施形態で説明したのと同様に、ラインＬ１１−７０を流れる冷媒が保有するエンタルピーが、広い温度範囲に亘って、冷媒ドレン熱交換器７０を介して、稀溶液ラインＬ１−２内を流れる稀溶液に供給され、高温再生器４４（のバーナ機構４５）において付与されたエンタルピーが、冷媒蒸気発生のために有効に利用される。
【０１７８】
また、排熱流体温度と吸収溶液との相対関係に基いて、三方弁Ｖ１を開閉制御することにより、排熱焚再生器３０に流入する吸収溶液の流量を制御し、以って、吸収冷温水機の効率を向上せしめることが出来る。
【０１７９】
図２３の実施形態における他の構成は、図１−図２２の実施形態と同様である。また図２３の実施形態におけるその他の作用効果については、図１−図２２の実施形態と同様である。
そして、第１分岐点ＢＰにおける三方弁Ｖ１の開閉制御の態様も、図１−図２２の実施形態と同様である。
【０１８０】
図２３においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１８１】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１８２】
図２３で示す実施形態では、ラインＬ１−２とラインＬ６とが合流する第１の合流点ＧＰは、低温再生器４８と高温溶液熱交換器４２との間の領域に設けられている。
これに対して、図２４の実施形態では、ラインＬ６とラインＬ１−２とが合流する第１の合流点ＧＰは、高温溶液熱交換器４２と高温再生器４４の間の領域に設けられている。
【０１８３】
換言すれば、低温再生器４８で加熱・濃縮され、ポンプ６２でヘッドが負荷された吸収溶液は、ラインＬ６を流れ、高温溶液熱交換器４２とを経由した後に、高温溶液熱交換器４２と高温再生器４４の間の領域における第１の合流点ＧＰで、第２分岐ラインＬ１−２と合流して、ラインＬ６−４４となる。そしてラインＬ６−４４は、高温再生器４４に連通する。
【０１８４】
図２４の実施形態におけるその他の構成は図２３で示す実施形態と同様である。また、図２４の実施形態の作用効果については、図１−図２３で示す実施形態と同様である。
そして、図２４の分岐点ＢＰにおける三方弁Ｖ１の開閉制御についても、図１−図２３で示す実施形態と同様である。
【０１８５】
図２４においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１８６】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１８７】
図２５で示す実施形態においても、第１の分岐点ＢＰで分岐した稀溶液ラインＬ１−１は、低温溶液熱交換器２６を経由した後、直ちに合流すること無く、排熱焚再生器３０に連通する。そして、ラインＬ１−１の内部を流れる吸収溶液は、排熱焚再生器３０へ供給される。
【０１８８】
排熱焚再生器３０で加熱・一部再生された吸収溶液は、低温再生器４８に連通するラインＬ１−１３０を流れ、排熱焚再生器３０と低温再生器４８の間の領域における第１の合流点ＧＰで、ラインＬ１−２に合流して、ラインＬ１−４８となる。ラインＬ１−４８は低温再生器４８に連通しており、その内部の吸収溶液は低温再生器４８へ供給される。
低温再生器４８で加熱・一部再生された吸収溶液は、ラインＬ６を流れポンプ６２でヘッドが負荷され、高温再生器４４へ供給される。
【０１８９】
図２５の実施形態におけるその他の構成は図２３、図２４で示す実施形態と同様である。また、図２５の実施形態の作用効果については、図１−図２４で示す実施形態と同様である。
さらに、図２５の分岐点ＢＰにおける三方弁Ｖ１の開閉制御については、図１−図２４で示す実施形態と同様である。
【０１９０】
図２５においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１９１】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１９２】
図２６は「パラレルフロー」タイプの吸収冷温水機を変形した実施形態にかかるものであり、吸収器及び蒸発器（所謂「下胴」部分）が低圧側と高圧側の２段に構成されており、吸収冷温水機の効率化を企図している。
また、低圧側吸収器２２Ｌには溶液冷却吸収器７４が設けられており、低圧側吸収器２２Ｌ内で滴下される濃縮された吸収溶液が保有するエンタルピーを稀溶液に投入し、稀溶液温度を上昇せしめるので、その分だけ再生し易くなり、吸収冷温水機の効率が改善される。
さらに、ラインＬ１−４４における高温溶液熱交換器４２と高温再生器４４の間の領域に、高質燃料排熱投入用熱交換器７６が介装されており、熱交換器７６を介して、当該領域を流れる吸収溶液に、高質燃料排熱ラインＬ２０を流れる高質燃料排熱（バーナ機構４５の加熱手段で吸収溶液を加熱した後に系外に廃棄される排熱流体が保有する熱量）が投入されている。
【０１９３】
図２６の実施形態におけるその他の構成及び作用効果については、図１０で示す実施形態と同様である。そして、第２の分岐点Ｐ１における三方弁Ｖ２の開閉制御についても、図１０と同様である。
【０１９４】
図２６においても、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１９５】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０１９６】
図２７の実施形態は、図２６の実施形態と概略同様な構成を具備しているが、第１合流点ＧＰと第２分岐点Ｐ１を連通するラインＬ１−３に排熱投入用熱交換器８０が介装されている。この排熱投入用熱交換器８０を介して、当該ラインＬ１−３内を流れる吸収溶液に、排熱ラインＬ２を流れる排熱流体が保有する熱量が投入される。
【０１９７】
図２７の実施形態におけるその他の構成及び作用効果については、図２６の実施形態と同様である。そして、第２の分岐点Ｐ１における三方弁Ｖ２の開閉制御についても、図２６（或いは図１０）と同様である。
【０１９８】
図２７において、排熱ラインＬ２に排熱流体が流過しているか否かを検出するセンサＳ１と、排熱流体温度Ｔｗを検出するセンサＳ２と、吸収器２２の出口温度Ｔａを検出するセンサＳ３を設け、各センサで検出されるパラメータは、それぞれ信号伝達ラインＣＬ−１、ＣＬ−２、ＣＬ−３を介して制御手段１５０に入力されており、制御信号１５０は、全ての制御パラメータに基いて制御信号を送出している。
【０１９９】
但し、センサＳ１、Ｓ２、Ｓ３のいずれか１つを設け、制御パラメータ（排熱ラインＬ２に排熱流体が流過しているか否か、排熱流体温度Ｔｗ、吸収器２２の出口における吸収溶液の液温Ｔａ）のいずれか１種類のみに基いて、三方弁Ｖ１の開閉制御を行うことも出来る。同様に、何れか２つのセンサを設け、上記した３種類の制御パラメータから２種類を選択して制御することも出来る。
【０２００】
【発明の効果】
以上説明した様に、本発明の吸収冷温水機では、排熱と吸収冷温水機内部の吸収溶液循環系との相対的な温度関係に基いて、分岐点における三方弁の開閉制御を行い、以って、排熱焚再生器に流入する吸収溶液量を制御することにより、高温再生器で消費される高質燃料を抑制し、排熱を有効利用して、吸収冷温水機の効率を改善することが出来る。
また、高温再生器で吸収溶液を再生した後の排熱流体が保有するエンタルピーであって、従来は利用されなかったエンタルピーが、冷媒ドレン熱交換器を介して稀溶液に投入されて、稀溶液の加熱に利用される。そのため、高質燃料が有効利用され、吸収冷温水機の熱効率が更に改善される。
さらに本発明によれば、排熱焚再生器において、冷媒蒸気の再生量を増加して、吸収冷温水機の熱効率を改善することが出来る。
【図面の簡単な説明】
【図１】本発明の第１実施形態を示す模式的に表現するブロック図。
【図２】図１の実施形態の制御フローチャートを示す図。
【図３】本発明の第２実施形態を示す模式的に表現するブロック図。
【図４】図３の実施形態の制御フローチャートを示す図。
【図５】本発明の第３実施形態を示す模式的に表現するブロック図。
【図６】図５の実施形態の制御フローチャートを示す図。
【図７】本発明の第４実施形態を示す模式的に表現するブロック図。
【図８】図７の実施形態の制御フローチャートを示す図。
【図９】本発明の第５実施形態を示す模式的に表現するブロック図。
【図１０】本発明の第６実施形態を示す模式的に表現するブロック図。
【図１１】本発明の第７実施形態を示す模式的に表現するブロック図。
【図１２】本発明の第８実施形態を示す模式的に表現するブロック図。
【図１３】本発明の第９実施形態を示す模式的に表現するブロック図。
【図１４】本発明の第１０実施形態を示す模式的に表現するブロック図。
【図１５】本発明の第１１実施形態を示す模式的に表現するブロック図。
【図１６】本発明の第１２実施形態を示す模式的に表現するブロック図。
【図１７】本発明の第１３実施形態を示す模式的に表現するブロック図。
【図１８】本発明の第１４実施形態を示す模式的に表現するブロック図。
【図１９】本発明の第１５実施形態を示す模式的に表現するブロック図。
【図２０】本発明の第１６実施形態を示す模式的に表現するブロック図。
【図２１】本発明の第１７実施形態を示す模式的に表現するブロック図。
【図２２】本発明の第１８実施形態を示す模式的に表現するブロック図。
【図２３】本発明の第１９実施形態を示す模式的に表現するブロック図。
【図２４】本発明の第２０実施形態を示す模式的に表現するブロック図。
【図２５】本発明の第２１実施形態を示す模式的に表現するブロック図。
【図２６】本発明の第２１実施形態を示す模式的に表現するブロック図。
【図２７】本発明の第２２実施形態を示す模式的に表現するブロック図。
【図２８】従来の吸収冷温水機の１例を模式的に表現するブロック図。
【図２９】その他の従来技術を模式的に表現するブロック図。
【符号の説明】
２０・・・吸収式冷温水機
２２・・・吸収器
２４、３２・・・ポンプ
２６・・・低温溶液熱交換器
３０・・・排熱焚再生器
Ｌ１、Ｌ１−１、Ｌ１−２、Ｌ１−２２、Ｌ１−２３、Ｌ３、Ｌ４、Ｌ５、Ｌ６、Ｌ６−１、Ｌ６−２、Ｌ８、Ｌ２２・・・溶液ライン
Ｌ１Ａ・・・溶液ラインの領域
Ｌ５、Ｌ１１、Ｌ１１−Ｄ、Ｌ１３、Ｌ１５、Ｌ１７、Ｌ１７Ｌ、Ｌ１７Ｈ、Ｌ５２、Ｌ７０・・・冷媒ライン
ＣＬ−１、ＣＬ−２、ＣＬ−３、ＣＬ−Ｖ１、ＣＬ−Ｖ２・・・信号伝達ライン４２・・・高温溶液熱交換器
４４・・・高温再生器
４８・・・低温再生器
５０・・・凝縮器
５２・・・蒸発器
７０・・・冷媒ドレン熱交換器
７４・・・溶液冷却吸収器
７６・・・高質燃料排熱投入用熱交換器
８０・・・排熱投入用熱交換器
Ｖ１、Ｖ２・・・三方弁
ＶＥ・・・排熱投入用三方弁
１００、１２０・・・三方弁駆動手段
Ｓ１、Ｓ２、Ｓ３・・・センサ
１５０・・・駆動手段[0001]
BACKGROUND OF THE INVENTION
The present invention relates to an absorption chiller / heater having an absorber, a high-temperature regenerator, a low-temperature regenerator, a condenser, and an evaporator, and more particularly, to an absorption chiller / heater called a “single double effect”.
[0002]
[Prior art]
FIG. 28 shows a conventional single double-effect absorption chiller / heater configured as a so-called “parallel flow” type.
In FIG. 28, the dilute solution sent from the absorber 22 by the pump 24 flows through the dilute solution line L1, passes through the low temperature solution heat exchanger 26, and is connected to the high temperature regenerator 44 at the branch point P1. -1 and a line L1-2 communicating with the exhaust heat soot regenerator.
[0003]
The dilute solution flowing through the line L1-2 is supplied to the exhaust heat soot regenerator 30. In the exhaust heat soot regenerator 30, the enthalpy (sensible heat) possessed by the exhaust heat fluid (for example, warm drainage) flowing through the exhaust heat line L2 is added to the rare solution to be heated and partially regenerated. .
The refrigerant vapor regenerated in the exhaust heat regenerator 30 flows through the line L13 and flows into the condenser 50.
[0004]
The absorption solution heated by the exhaust heat soot regenerator 30 is supplied to the low temperature regenerator 48 via the line L1-21.
[0005]
On the other hand, the other line L1-1 branched at the branch point P1 is sent to the high temperature regenerator 44 via the high temperature solution heat exchanger 42.
In the high temperature regenerator 44, for example, the absorbing solution is heated and concentrated by heating means such as a burner mechanism 45, and the generated (regenerated) refrigerant vapor (water vapor) flows through the vapor line L11 and passes through the low temperature regenerator 48. It is sent to the condenser 50 (first condenser).
[0006]
Then, in the low-temperature regenerator 48, the absorbing solution (flowed from the exhaust heat regenerator 30 via the line L1-21) is regenerated by the enthalpy held by the steam. And the regenerated refrigerant | coolant vapor | steam is sent to the condenser 50 via the line L15, and the absorption solution heated with the low temperature regenerator 48 flows through line L1-22.
[0007]
The absorbing solution (intermediate concentration solution) heated and condensed by the high temperature regenerator 44 flows through the solution line L3, and merges with the line L1-22 from the low temperature regenerator 48 at the junction P2. The line L3 and the line L1-22 join and then return to the absorber 22 via the low-temperature solution heat exchanger 26.
[0008]
The liquid-phase refrigerant condensed in the condenser 50 flows through the line L5 and is supplied to the evaporator 52. Refrigerant vapor evaporated by removing vaporization heat from cold water flowing through a cold water line (not shown) in the evaporator 52 flows through the line L 17 and flows into the absorber 22.
[0009]
In the related art, the flow rate of the absorbing solution flowing through the two lines L1-1 and L1-2 branched at the branch point P1 is determined to be a constant amount based on the pressure balance of the absorption chiller / heater.
In contrast, the exhaust heat supplied to the exhaust heat regenerator 30 via the exhaust heat line L2 (or the amount of heat held by the exhaust heat fluid flowing through the exhaust heat line L2) is a state of an exhaust heat source (not shown). Varies depending on
[0010]
Here, if the temperature of the exhaust heat fluid flowing through the exhaust heat line L2 is sufficiently higher than the absorption solution temperature in the exhaust heat soot regenerator 30, the flow rate of the absorption solution flowing through the line L1-2 is increased. The amount of regeneration in the exhaust heat regenerator 30 can be increased, the high-quality fuel consumption of the heating means 45 of the high-temperature regenerator 44 can be suppressed, and the efficiency of the absorption chiller / heater can be improved.
On the other hand, when the temperature of the exhaust heat fluid flowing through the exhaust heat line L2 cannot be said to be sufficiently high with respect to the absorption solution temperature in the exhaust heat soot regenerator 30, the amount of regeneration in the exhaust heat soot regenerator 30 is In the worst case, the amount of heat held by the absorbing solution may (thermally) flow back to the exhaust heat fluid. In such a case, the efficiency of the absorption chiller / heater is improved by increasing the flow rate of the line L1-1 and decreasing the flow rate of the line L1-2.
Therefore, comparing the temperature of the exhaust heat fluid and the temperature of the absorption solution and changing the flow rate of the absorption solution flowing through the lines L1-1 and L1-2 from the viewpoint of improving the efficiency of the absorption chiller / heater. Is preferred.
[0011]
However, there is currently no absorption chiller / heater that compares the temperature of the exhaust heat fluid with the temperature of the absorption solution to determine the flow rate of the absorption solution flowing into the exhaust heat regenerator 30. Regardless of the temperature of the exhaust heat fluid and the temperature of the absorption solution, the flow rate of the absorption solution flowing into the exhaust heat regenerator 30 is randomly determined based on the pressure balance in the solution circulation system in the absorption chiller / heater. is the current situation.
Accordingly, the flow rate of the absorbing solution flowing into the exhaust heat soot regenerator 30 is low even though the exhaust heat fluid temperature is high, or the flow rate of the absorbing solution flowing into the exhaust heat soot regenerator 30 is high even though the exhaust heat fluid temperature is low. In other words, there is a problem that it is counteracted to improve the efficiency of the absorption chiller / heater.
[0012]
As shown in FIG. 29, such a problem can be addressed by providing two dilute solution lines L1-11 and L1-12 that exit from the absorber (high-pressure side absorber) 22H. It is done.
That is, the line L1-11 is added with a head by a pump P10-1, and communicates with the high temperature regenerator 44 via the high temperature solution heat exchanger 42, and the line L1-12 is added with a head by the pump P10-2, and the low temperature solution heat is added. It is configured to communicate with the exhaust heat regenerator 30 via the exchanger 26, and by controlling the discharge flow rate of the pumps P10-1 and P10-2, the exhaust heat temperature is determined based on the absorption solution temperature and the exhaust heat temperature. It is possible to improve the efficiency of the absorption chiller / heater by adjusting the flow rate of the absorption solution flowing into the heat regenerator 30.
[0013]
However, taking out two lines from the absorber, installing a pump in each line, and controlling the discharge flow rate of each pump (based on the absorption solution temperature and exhaust heat temperature) complicates the configuration. As a result, the production cost of the absorption chiller / heater increases.
[0014]
[Problems to be solved by the invention]
The present invention has been proposed in view of the above-described problems of the prior art, and it is possible to control the absorption solution flow rate flowing into the exhaust heat regenerator to improve the efficiency of the absorption chiller / heater. The purpose is to provide an absorption chiller / heater and its control method.
[0015]
[Means for Solving the Problems]
The absorption chiller / heater of the present invention includes an absorber (22), a high temperature regenerator (44), a low temperature regenerator (48), a waste heat regenerator (30), a condenser (50), and evaporation. In the absorption chiller / heater (20) having the vessel (52), the rare solution line (L1) through which the rare solution sent out from the absorber (22) flows is the first branch point (BP) at a low temperature. The first branch line (L1-1) in which the solution heat exchanger (26) is interposed, and the second branch line (L1-2) in which the refrigerant drain heat exchanger (70) is interposed The region (L11-70) between the low temperature regenerator (48) and the condenser (50) of the line (L11) through which the refrigerant vapor regenerated by the high temperature regenerator (44) flows is the refrigerant drain heat. It is in thermal communication with the exchanger (70) and flows through the refrigerant (L11-70) after passing through the low temperature regenerator (48). The three-way valve is constructed so that the enthalpy possessed by the refrigerant) is introduced into the dilute solution flowing through the second branch line (L1-2), and is interposed at the first branch point (BP) (V1), exhaust heat input intercalated at a junction or junction of the exhaust heat line (L2) in thermal communication with the exhaust heat regenerator (30) and the line (L2G) in communication with the exhaust heat source A three-way valve (VE) for opening, an open / close sensor (S1) for detecting whether the three-way valve (VE) for exhaust heat input opens or closes the exhaust heat line L2, and the open / close sensor (S1) And a control means (150) for controlling opening and closing of the three-way valve (V1) by a detection signal. The control means (150) opens the exhaust heat line (L2) side of the exhaust heat input three-way valve (VE). If so, the first branch line ( If the flow rate of the dilute solution flowing through 1-1) is increased by a predetermined amount and the exhaust heat input three-way valve (VE) closes the exhaust heat line (L2) side, the exhaust heat soot regenerator The flow rate of the dilute solution flowing through the first branch line (L1-1) communicating with (30) is controlled to be reduced by a predetermined amount. (Fig. 1 and Fig. 2)
Here, the temperature of the exhaust heat fluid flowing through the line (L2G) communicating with the exhaust heat source is low, the exhaust heat input three-way valve (VE) closes the exhaust heat line (L2) side, and the exhaust heat line (L2 ) And the exhaust heat soot regenerator (30), the first branch line (L1) communicating with the exhaust heat soot regenerator (30) is focused on from the viewpoint of improving the efficiency of the absorption chiller / heater. It is not necessary to flow a large amount of dilute solution through -1).
On the other hand, the exhaust heat fluid flowing through the line (L2G) communicating with the exhaust heat source is hot, and the exhaust heat input three-way valve (VE) opens the exhaust heat line (L2) side to exhaust a large amount of exhaust heat. If the regenerator (30) can be charged, the absorption chiller / heater is more likely to allow a large amount of rare solution to flow through the first branch line (L1-1) communicating with the exhaust heat regenerator (30). Contribute to the efficiency improvement.
According to the present invention having the configuration as described above, whether or not the exhaust heat line (L2) side is opened, in other words, whether or not exhaust heat is input to the exhaust heat soot regenerator (30). Judgment and control of the dilute solution flow rate (absorbed solution flow rate flowing through the first branch line L1-1) supplied to the exhaust heat soot regenerator (30), the exhaust heat is effectively utilized, and the high temperature regenerator By suppressing the amount of high-quality fuel consumed in (44), the efficiency of the absorption chiller / heater can be further improved.
[0016]
Further, the absorption chiller / heater of the present invention includes an absorber (22), a high temperature regenerator (44), a low temperature regenerator (48), a waste heat soaker regenerator (30), a condenser (50), In the absorption chiller / heater (20) having the evaporator (52), the rare solution line (L1) through which the rare solution sent from the absorber (22) flows is the first branch point (BP). A first branch line (L1-1) in which a low-temperature solution heat exchanger (26) is interposed, and a second branch line (L1-2) in which a refrigerant drain heat exchanger (70) is interposed. The region (L11-70) between the low temperature regenerator (48) and the condenser (50) of the line (L11) through which the refrigerant vapor regenerated by the high temperature regenerator (44) flows is the refrigerant drain. The refrigerant (L11-70) is in thermal communication with the heat exchanger (70) and passes through the low temperature regenerator (48). A three-way valve arranged at the first branch point (BP) so that the enthalpy possessed by the refrigerant is flowing into the dilute solution flowing through the second branch line (L1-2). (V1), a temperature sensor (S2) for detecting the temperature (Tw) of the fluid flowing in the exhaust heat line (L2) in thermal communication with the exhaust heat soot regenerator (30), and the temperature sensor (S2) And a control means (150) for controlling the opening and closing of the three-way valve (V1) according to the detection signal, and the control means (150), if the temperature (Tw) of the fluid flowing through the exhaust heat line (L2) rises, The flow rate of the dilute solution flowing through the first branch line (L1-1) communicating with the exhaust heat soot regenerator (30) is increased, and the temperature (Tw) of the fluid flowing through the exhaust heat line (L2) is decreased. If so, the first branch line (L1- ) And is configured so as to perform control to decrease the flow rate of the diluted solution flowing past a. (Fig. 3, Fig. 4)
According to the present invention having the configuration as described above, the temperature (Tw) flowing through the exhaust heat line (L2) rises, and the exhaust heat is effectively input to the exhaust heat regenerator (30). Is determined, and the dilute solution flow rate (absorbing solution flow rate flowing through the first branch line L1-1) supplied to the exhaust heat soot regenerator (30) is controlled. Therefore, since the absorption solution flow rate flowing through the first branch line (L1-1) is controlled based on whether or not the amount of heat (exhaust heat) possessed by the exhaust heat fluid can be input, effective use of exhaust heat, The efficiency of the absorption chiller / heater is further improved by reducing the consumption of high-quality fuel.
[0017]
Furthermore, the absorption chiller / heater of the present invention includes an absorber (22), a high temperature regenerator (44), a low temperature regenerator (48), a waste heat soaker regenerator (30), a condenser (50), In the absorption chiller / heater (20) having the evaporator (52), the rare solution line (L1) through which the rare solution sent from the absorber (22) flows is the first branch point (BP). A first branch line (L1-1) in which a low-temperature solution heat exchanger (26) is interposed, and a second branch line (L1-2) in which a refrigerant drain heat exchanger (70) is interposed. The region (L11-70) between the low temperature regenerator (48) and the condenser (50) of the line (L11) through which the refrigerant vapor regenerated by the high temperature regenerator (44) flows is the refrigerant drain. The refrigerant (L11-7) is in thermal communication with the heat exchanger (70) and passes through the low temperature regenerator (48). The enthalpy possessed by the refrigerant flowing through the second branch line (L1-2) is introduced into the dilute solution, and the three sides interposed in the first branch point (BP) The valve (V1), a temperature sensor (S3) for detecting the temperature (Ta) of the absorbing solution at the outlet of the absorber (22), and the three-way valve (V1) are controlled to open and close by a detection signal of the temperature sensor (S3). Control means (150), and the control means (150) communicates with the exhaust heat regenerator (30) when the temperature (Ta) of the absorbent solution at the outlet of the absorber (22) rises. If the flow rate of the dilute solution flowing through the first branch line (L1-1) is decreased and the temperature (Ta) of the absorbing solution at the outlet of the absorber (22) decreases, the waste heat regenerator (30) A dilute solution flowing through the first branch line (L1-1) that communicates And it is configured so as to perform the control to increase the flow rate. (FIGS. 5 and 6).
According to the present invention having the above-described configuration, if the temperature (Ta) of the absorbing solution at the outlet of the absorber (22) decreases, the concentration of the absorbing solution decreases and the saturation temperature decreases. Even if it is charged, the amount of regeneration in the exhaust heat soot regenerator (30) increases. On the other hand, if the temperature (Ta) of the absorption solution at the outlet of the absorber (22) increases, the concentration of the absorption solution increases and the saturation temperature increases. Therefore, even if the same amount of heat is input, the exhaust heat soot regenerator (30) The amount of regeneration in decreases.
In the present invention, by measuring the absorber outlet temperature (Ta), the concentration of the absorbing solution (or rare solution) is low or high, in other words, the saturation temperature is low (easy to regenerate) or high (not easy to regenerate). Based on this, the dilute solution flow rate (absorbing solution flow rate flowing through the first branch line L1-1) supplied to the exhaust heat soot regenerator (30) is controlled. That is, based on whether or not the amount of regeneration due to exhaust heat input to the exhaust heat regenerator increases, the flow rate of the absorbing solution flowing through the first branch line (L1-1) is controlled to effectively use the exhaust heat. In addition, the consumption of high-quality fuel is suppressed and the efficiency of the absorption chiller / heater is further improved.
[0018]
In implementing the present invention, an open / close sensor (S1) for detecting whether or not the exhaust heat fluid is flowing through the exhaust heat line (L2), and a temperature sensor (S2) for detecting the exhaust heat fluid temperature (Tw) Any two or all three of the temperature sensors (S3) for detecting the absorbing solution temperature (Ta: absorber outlet temperature) at the outlet of the absorber (22) are provided and detected by each sensor. It can be configured such that control is performed with reference to all the parameters (FIGS. 7 and 8).
[0019]
In the present invention, the first branch line (L1-1) passes through the low temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2) to regenerate the exhaust heat soot. The line (L1-144) communicating with the regenerator (30) and going from the exhaust heat soot regenerator (30) to the high temperature regenerator (44) is connected to the exhaust heat soot regenerator (30) and the high temperature solution heat exchanger (42). ) At the first junction (GP) between the second branch line (L1-2) and communicate with the high temperature regenerator (44) (L1-44), and at the high temperature regenerator (44) The heated absorbent solution flows through the intermediate concentration solution line (L3) and flows into the low temperature regenerator (48). After being heated by the low temperature regenerator (48), it flows through the high concentration solution line (L4), It is preferable to configure so as to return to the absorber (22) via the heat exchanger (26) (FIGS. 1 to 8: Leeds flow type).
[0020]
Alternatively, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2), so that the exhaust heat soot regenerator ( 30), a line (L1-144) from the exhaust heat soot regenerator (30) to the high temperature regenerator (44) is connected between the high temperature solution heat exchanger (42) and the high temperature regenerator (44). The absorbing solution heated by the high temperature regenerator (44) is joined to the second branch line (L1-2) at the first confluence (GP) and communicated with the high temperature regenerator (44). It flows through the line (L3), flows into the low temperature regenerator (48), is heated by the low temperature regenerator (48), then flows through the high concentration solution line (L4), and passes through the low temperature solution heat exchanger (26). It is preferable to configure so as to return to the absorber (22) (FIG. 9: series flow type).
[0021]
In the present invention, the first and second branch lines (L1-1, L1-2) pass through the low-temperature solution heat exchanger (26) or the refrigerant drain heat exchanger (70) immediately after the first. A line (L1-3) that joins at the junction (GP) and communicates with the high-temperature regenerator (44) at the second branch point (P1) and a line (L1-4) that communicates with the exhaust heat regenerator (30) ) And the dilute solution flowing through the line (L1-3) communicating with the high temperature regenerator (44) flows into the high temperature regenerator (44) via the high temperature solution heat exchanger (42), and is exhausted. The dilute solution flowing through the line (L1-4) communicating with the regenerator (30) is heated by the exhaust heat regenerator (30), flows into the low temperature regenerator (48), and is heated by the low temperature regenerator (48). The line (L1-42) through which the absorbent solution flows is connected to the solution line (L3) from the high temperature regenerator (44). (L4), and communicates with the absorber (22) via the low-temperature solution heat exchanger (26). The three-way valve (V1) is connected to the first branch point (BP ), But preferably at the second branch point (P1) (FIG. 10: parallel flow type).
[0022]
Furthermore, in the present invention, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26), and the second branch line (L1-2) Branch line (L1-3) communicating with the high temperature regenerator (44) and a line (L1-4) communicating with the exhaust heat soot regenerator (30) at the branch point (P1) of the high temperature regenerator (44) The dilute solution flowing through the line (L1-3) communicating with the refrigerant flows into the high temperature regenerator (44) via the high temperature solution heat exchanger (42), and communicates with the exhaust heat regenerator (30) (L1). -4) joins the second branch line (L1-2) at the first joining point (GP), and the rare solution flowing through the line (L1-4 after joining) becomes the exhaust heat regenerator (30). ) To flow into the low-temperature regenerator (48) and the absorption solution heated by the low-temperature regenerator (48) flows (L -42) joins the solution line (L3) from the high temperature regenerator (44) at the second junction (P2) (L4), and passes through the low temperature solution heat exchanger (26) to the absorber (22). In place of the three-way valve (V1) interposed at the first branch point (BP), a three-way valve (V2) interposed at the second branch point (P1) is provided. (FIG. 11: parallel flow type).
[0023]
Alternatively, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26), and the second branch point. (P1) branches to a line (L1-3) that communicates with the high temperature regenerator (44) and a line (L1-4) that communicates with the exhaust heat soot regenerator (30), and communicates with the high temperature regenerator (44). The dilute solution flowing through the line (L1-3) flows into the high-temperature regenerator (44) via the high-temperature solution heat exchanger (42) and communicates with the exhaust heat regenerator (30) (L1-4). Joins the second branch line (L1-2) at the first joining point (GP), and the rare solution flowing through the line (L1-4 after joining) is heated by the exhaust heat regenerator (30). Into the low temperature regenerator (48), and the line (L1-42) through which the absorption solution heated by the low temperature regenerator (48) flows. The solution line (L3) from the high temperature regenerator (44) joins at the second junction (P2) (L4) and communicates with the absorber (22) via the low temperature solution heat exchanger (26). (FIG. 12: parallel flow type).
[0024]
Alternatively, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26), and the second branch point. (P1) branches to a line (L1-3) that communicates with the high temperature regenerator (44) and a line (L1-4) that communicates with the exhaust heat soot regenerator (30), and communicates with the high temperature regenerator (44). The dilute solution flowing through the line (L1-3) flows into the high-temperature regenerator (44) via the high-temperature solution heat exchanger (42) and communicates with the exhaust heat regenerator (30) (L1-4). Joins the second branch line (L1-2) at the first joining point (GP), and the rare solution flowing through the line (L1-4 after joining) is heated by the exhaust heat regenerator (30). Into the low temperature regenerator (48), and the line (L1-42) through which the absorption solution heated by the low temperature regenerator (48) flows. The solution line (L3) from the high temperature regenerator (44) joins at the second junction (P2) (L4) and communicates with the absorber (22) via the low temperature solution heat exchanger (26). In addition to the three-way valve (V1) interposed at the first branch point (BP), a three-way valve (V2) interposed at the second branch point (P1) is preferably provided. (FIG. 13: Parallel flow type).
[0025]
In addition, in the present invention, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26). The second branch point (P1) branches into a line (L1-11) communicating with the high temperature regenerator (44) and a line (L1-12) communicated with the exhaust heat soot regenerator (30). A line (L1-11) communicating with (44) is a first junction (GP) between the second branch point (P1) and the high-temperature solution heat exchanger (42), and the second branch line (L1). -2) (L1-44) communicates with the high temperature regenerator (44), and the rare solution flowing through the line (L1-12) communicating with the exhaust heat soot regenerator (30) 30) is a line in which the absorption solution heated by the low temperature regenerator (48) flows and flows into the low temperature regenerator (48). 1-122) joins at the solution line (L3) from the high temperature regenerator (44) and the second junction (P2), and communicates with the absorber (22) via the low temperature solution heat exchanger (26). In place of the three-way valve (V1) interposed at the first branch point (BP), a three-way valve (V2) interposed at the second branch point (P1) is provided. Is preferred (FIG. 14: parallel flow type).
[0026]
Alternatively, in the present invention, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2). Branch line (L1-11) communicating with the high temperature regenerator (44) and a line (L1-12) communicating with the exhaust heat soot regenerator (30) at the branch point (P1) of the high temperature regenerator (44) The line (L1-11) communicating with the second branch line (L1-2) is a first junction (GP) between the second branch point (P1) and the high temperature solution heat exchanger (42). (L1-44) is connected to the high-temperature regenerator (44), and the rare solution flowing through the line (L1-12) connected to the exhaust heat soot regenerator (30) is removed by the exhaust heat soot regenerator (30). A line (L1-) that is heated and flows into the low temperature regenerator (48) through which the absorption solution heated by the low temperature regenerator (48) flows. 22) joins at the solution line (L3) from the high temperature regenerator (44) and the second junction (P2), and communicates with the absorber (22) via the low temperature solution heat exchanger (26). (FIG. 15: parallel flow type).
[0027]
In the present invention, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26). At the branch point (P1), the line (L1-11) communicated with the high temperature regenerator (44) and the line (L1-12) communicated with the exhaust heat soot regenerator (30) are branched to the high temperature regenerator (44). The communicating line (L1-11) is a first junction (GP) between the second branch point (P1) and the high temperature solution heat exchanger (42) and the second branch line (L1-2). The dilute solution that joins (L1-44) and communicates with the high-temperature regenerator (44) and flows through the line (L1-12) that communicates with the exhaust heat regenerator (30) is heated by the exhaust heat regenerator (30). Line that flows into the low temperature regenerator (48) and through which the absorption solution heated by the low temperature regenerator (48) flows (L1-122) The solution line (L3) from the high temperature regenerator (44) joins at the second junction (P2) and communicates with the absorber (22) via the low temperature solution heat exchanger (26). In addition to the three-way valve (V1) interposed at one branch point (BP), it is preferable to provide a three-way valve (V2) interposed at the second branch point (P1) (FIG. 16). : Parallel flow type).
[0028]
In carrying out the present invention, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2). The bifurcation point (P1) branches to a line (L1-11) that communicates with the high temperature regenerator (44) and a line (L1-12) that communicates with the exhaust heat soaker regenerator (30), and the high temperature regenerator (44 ) Communicated with the second branch line (L1-2) at the first junction (GP) between the high temperature solution heat exchanger (42) and the high temperature regenerator (44). The dilute solution that joins and communicates with the high-temperature regenerator (44) and flows through the line (L1-12) that communicates with the exhaust heat soot regenerator (30) is heated by the exhaust heat soot regenerator (30) and is then supplied to the low-temperature regenerator. The line (L1-122) that flows into (48) and flows through the absorption solution heated by the low temperature regenerator (48) is high. The solution line (L3) from the regenerator (44) joins at the second junction (P2) and communicates with the absorber (22) via the low temperature solution heat exchanger (26). Instead of the three-way valve (V1) interposed at the branch point (BP), a three-way valve (V2) interposed at the second branch point (P1) is preferably provided (FIG. 17: Parallel flow type).
[0029]
In carrying out the present invention, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2). The bifurcation point (P1) branches to a line (L1-11) that communicates with the high temperature regenerator (44) and a line (L1-12) that communicates with the exhaust heat soaker regenerator (30), and the high temperature regenerator (44 ) Communicated with the second branch line (L1-2) at the first junction (GP) between the high temperature solution heat exchanger (42) and the high temperature regenerator (44). The dilute solution that joins and communicates with the high-temperature regenerator (44) and flows through the line (L1-12) that communicates with the exhaust heat soot regenerator (30) is heated by the exhaust heat soot regenerator (30) and is then supplied to the low-temperature regenerator. The line (L1-122) that flows into (48) and flows through the absorption solution heated by the low temperature regenerator (48) is high. It is preferable that the solution line (L3) from the regenerator (44) joins at the second junction (P2) and communicates with the absorber (22) via the low-temperature solution heat exchanger (26). (FIG. 18: Parallel flow type).
[0030]
In carrying out the present invention, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2). The bifurcation point (P1) branches to a line (L1-11) that communicates with the high temperature regenerator (44) and a line (L1-12) that communicates with the exhaust heat soaker regenerator (30), and the high temperature regenerator (44 ) Communicated with the second branch line (L1-2) at the first junction (GP) between the high temperature solution heat exchanger (42) and the high temperature regenerator (44). The dilute solution that joins and communicates with the high-temperature regenerator (44) and flows through the line (L1-12) that communicates with the exhaust heat soot regenerator (30) is heated by the exhaust heat soot regenerator (30) and is then supplied to the low-temperature regenerator. The line (L1-122) that flows into (48) and flows through the absorption solution heated by the low temperature regenerator (48) is high. The solution line (L3) from the regenerator (44) joins at the second junction (P2) and communicates with the absorber (22) via the low temperature solution heat exchanger (26). In addition to the three-way valve (V1) interposed at the branch point (BP), a three-way valve (V2) interposed at the second branch point (P1) is preferably provided (FIG. 19: Parallel flow type).
[0031]
In the present invention, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26), and is exhausted. The line (L1-31) that communicates with the regenerator (30) and through which the absorbent solution heated by the exhaust heat regenerator (30) flows communicates with the high temperature regenerator (44) at the second branch point (P1). The dilute solution that branches into the line (L1-48) communicating with the low temperature regenerator (48) and the line (L1-48) communicating with the low temperature regenerator (48) flows through the line (L1-44) communicated with the high temperature regenerator (44). A line (L1-48) that flows into the high-temperature regenerator (44) via the exchanger (42) and communicates with the low-temperature regenerator (48) is a second junction line at the first junction (GP). The dilute solution that joins (L1-2) and flows through the line (L1-2 after joining) is a low temperature regenerator. 48), the line (L1-51) through which the absorption solution heated by the low temperature regenerator (48) flows is connected to the solution line (L3) from the high temperature regenerator (44) and the second junction. It is preferable to join at (P2) (L4) and communicate with the absorber (22) via the low-temperature solution heat exchanger (26) (FIG. 20: parallel flow type).
[0032]
Alternatively, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2), so that the exhaust heat soot regenerator ( 30), the line (L1-31) through which the absorption solution heated in the exhaust heat regenerator (30) flows is a line (L1-31) that communicates with the high temperature regenerator (44) at the second branch point (P1). L1-44) branches to a line (L1-48) communicating with the low temperature regenerator (48), and a line (L1-44) communicating with the high temperature regenerator (44) is connected to the second branch point (P1). The first junction (GP) between the high temperature solution heat exchangers (42) joins the second branch line (L1-2) and communicates with the high temperature regenerator (44). ) The dilute solution flowing through the line (L1-48) communicating with the gas flows into the low-temperature regenerator (48) and is heated for low-temperature regeneration. The line (L1-49) through which the absorption solution heated in (48) flows joins at the solution line (L3) from the high temperature regenerator (44) and the second junction (P2), and the low temperature solution heat exchanger. It is preferable to communicate with the absorber via (FIG. 21: parallel flow type).
[0033]
The first branch line (L1-1) passes through the low temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2). 30), the line (L1-31) through which the absorption solution heated in the exhaust heat regenerator (30) flows is a line (L1-31) that communicates with the high temperature regenerator (44) at the second branch point (P1). L1-44) and a line (L1-48) branching to a line (L1-48) communicating with the low temperature regenerator (48) and a line (L1-44) communicating with the high temperature regenerator (44) are connected to the high temperature solution heat exchanger (42). The first junction (GP) between the high temperature regenerators (44) joins the second branch line (L1-2) (L1-46) and communicates with the high temperature regenerator (44) for low temperature regeneration. The dilute solution flowing through the line (L1-48) communicating with the regenerator (48) flows into the low temperature regenerator (48) and is heated. The line (L1-49) through which the absorption solution heated by the low temperature regenerator (48) flows joins the solution line (L3) from the high temperature regenerator (44) at the second junction (P2), and the low temperature It is preferable to communicate with the absorber via a solution heat exchanger (FIG. 22: parallel flow type).
[0034]
In carrying out the present invention, the first branch line (L1-1) passes through the low-temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2) to exhaust heat. A line (L1-130) that communicates with the regenerator (30) and through which the absorption solution heated by the exhaust heat regenerator (30) flows communicates with the low temperature regenerator (48) and is connected with the low temperature regenerator (48). The line (L6) through which the heated absorbent solution flows is the second branch line (L1-2) at the first junction (GP) between the low temperature regenerator (48) and the high temperature solution heat exchanger (42). ) And communicated with the high temperature regenerator (44), and the absorption solution heated by the high temperature regenerator (44) is preferably returned to the absorber (22) (FIG. 23: reverse flow type).
[0035]
The first branch line (L1-1) passes through the low temperature solution heat exchanger (26) and does not merge with the second branch line (L1-2). 30), the line (L1-130) through which the absorption solution heated by the exhaust heat regenerator (30) flows communicates with the low temperature regenerator (48) and is absorbed by the low temperature regenerator (48). The line (L6) through which the solution flows joins the second branch line (L1-2) at the first junction (GP) between the high temperature solution heat exchanger (42) and the high temperature regenerator (44). (L6-44) It is preferable that the absorbent solution communicated with the high temperature regenerator (44) and heated by the high temperature regenerator (44) is returned to the absorber (22) (FIG. 24: reverse flow type).
[0036]
In addition, the first branch line (L1-1) does not merge with the second branch line (L1-2) after passing through the low-temperature solution heat exchanger (26), and is exhausted. A line (L1-130) that communicates with the regenerator (30) and through which the absorption solution heated by the exhaust heat regenerator (30) flows is a second junction line (L1) at a first junction (GP). -2) (L1-48) communicates with the low temperature regenerator (48), and the line (L6) through which the absorption solution heated by the low temperature regenerator (48) flows communicates with the high temperature regenerator (44). The absorbing solution heated by the high-temperature regenerator (44) is preferably returned to the absorber (22) (FIG. 25: reverse flow type).
[0037]
In carrying out the present invention, it is preferable that the absorber and the evaporator (so-called “lower body” portion) are configured in two stages, a low-pressure side and a high-pressure side, to increase the efficiency of the absorption chiller / heater. (FIGS. 26 and 27).
In addition, the low pressure side absorber (22L) is provided with a solution cooling absorber (74), and the enthalpy held by the concentrated absorption solution dropped in the low pressure side absorber (22L) is added to the rare solution. Therefore, it is preferable to improve the efficiency of the absorption chiller / heater by increasing the temperature of the dilute solution and facilitating the regeneration by that amount (FIGS. 26 and 27).
Furthermore, a high-quality fuel exhaust heat input heat exchanger (76) is interposed in a region between the high-temperature solution heat exchanger (42) and the high-temperature regenerator (44), and the heat exchanger (76) The high-quality fuel exhaust heat flowing through the high-quality fuel exhaust heat line (L20) (exhaust heat discarded outside the system after the absorbent solution is heated by the heating means of the burner mechanism 45) ) Is preferably input (FIGS. 26 and 27).
[0038]
According to the present invention, the enthalpy held by the refrigerant (the refrigerant flowing through L11-70) after passing through the low-temperature regenerator is transferred to the second branch line (L1) via the refrigerant drain heat exchanger (70). -2). And only the said refrigerant | coolant drain heat exchanger (70) is interposed in the said 2nd branch line (L1-2), and the low temperature solution heat exchanger (26) is not interposed. Therefore, the enthalpy possessed by the refrigerant (refrigerant flowing through L11-70) after passing through the low-temperature regenerator via the refrigerant drain heat exchanger (70) is the second branch over a wide temperature range. The dilute solution flowing through the line (L1-2) is charged.
[0039]
The temperature of the dilute solution (the dilute solution temperature flowing through the first branch line L1-1) after being heated by the low temperature solution heat exchanger (26) is, for example, 60 ° C.-75 ° C., and the low temperature regenerator (48 Even if the temperature of the refrigerant after heating and regeneration is, for example, 90 ° C., the temperature of the dilute solution flowing into the second branch line (L1-2) is the same as that of the first branch line (L1-1). Since it is much lower than the flowing dilute solution temperature, not only the enthalpy in the temperature range of 75 ° C-90 ° C but also the enthalpy (sensible heat) in the temperature range of 40 ° C-75 ° C is the second branch line (L1-2) Is used to raise the temperature of a dilute solution flowing through That is, according to the present invention described above, the high-quality fuel supplied to the high-temperature regenerator (44) is effectively used, and the absorption solution is heated efficiently, so that the efficiency of the absorption chiller / heater is improved. Improved.
[0040]
The control method of the absorption chiller / heater of the present invention includes the absorber (22), the high temperature regenerator (44), the low temperature regenerator (48), the exhaust heat soot regenerator (30), and the condenser (50). And the evaporator (52), the rare solution line (L1) through which the rare solution sent from the absorber (22) flows is the first branch point (BP), and the low temperature solution heat exchanger (26) is branched into the first branch line (L1-1) in which the refrigerant drain heat exchanger (70) is interposed and the first branch line (L1-2) in which the refrigerant drain heat exchanger (70) is interposed. The region (L11-70) between the low temperature regenerator (48) and the condenser (50) of the line (L11) through which the refrigerant vapor regenerated by the high temperature regenerator (44) flows is the refrigerant drain heat exchanger (70). ) And is in thermal communication with the refrigerant (the refrigerant flowing through L11-70) after passing through the low temperature regenerator (48). It is configured so that the enthalpy is poured into a dilute solution flowing through the second branch line (L1-2), and a three-way valve (V1) interposed in the first branch point (BP), Waste heat input three-way valve (VE) interposed at a junction or junction between the exhaust heat line (L2) in thermal communication with the hot metal regenerator (30) and the line (L2G) in communication with the exhaust heat source An open / close sensor (S1) for detecting whether the exhaust heat input three-way valve (VE) opens or closes the exhaust heat line (L2), and a detection signal from the open / close sensor (S1). In the control method of the absorption chiller / heater having the control means (150) for controlling the opening and closing of the three-way valve (V1), the three-way valve for exhaust heat input (VE) is connected to the exhaust heat line L2 side by the opening / closing sensor (S1). A process to detect whether it is open or closed, If the three-way valve (VE) opens the exhaust heat line (L2) side, the rare solution that flows through the first branch line (L1-1) communicating with the exhaust heat soot regenerator (30) If the exhaust heat input three-way valve (VE) is closed on the exhaust heat line (L2) side, the first branch communicating with the exhaust heat regenerator (30) is increased. A step of reducing the flow rate of the dilute solution flowing through the line (L1-1) by a predetermined amount (FIG. 2).
[0041]
Moreover, the control method of the absorption chiller / heater of the present invention includes an absorber (22), a high temperature regenerator (44), a low temperature regenerator (48), a waste heat regenerator (30), and a condenser (50 ) And an evaporator (52), and the dilute solution line (L1) through which the dilute solution sent from the absorber (22) flows is a low temperature solution heat exchange at the first branch point (BP). The first branch line (L1-1) in which the condenser (26) is interposed, and the second branch line (L1-2) in which the refrigerant drain heat exchanger (70) is interposed. The region (L11-70) between the low temperature regenerator (48) and the condenser (50) of the line (L11) through which the refrigerant vapor regenerated by the high temperature regenerator (44) flows is the refrigerant drain heat exchanger ( 70) and is in thermal communication with the refrigerant (refrigerant flowing through L11-70) after passing through the low temperature regenerator (48). Enthalpy is introduced into a dilute solution flowing through the second branch line (L1-2), and a three-way valve (V1) interposed in the first branch point (BP); The temperature sensor (S2) for detecting the temperature (Tw) of the fluid flowing through the exhaust heat line (L2) that is in thermal communication with the exhaust heat soot regenerator (30), and the three-way detection by the detection signal of the temperature sensor (S2) In the control method of the absorption chiller / heater having control means (150) for controlling opening and closing of the valve (V1), a step of detecting the temperature (Tw) of the fluid flowing through the exhaust heat line (L2) by the temperature sensor (S2). When the temperature (Tw) of the fluid flowing through the exhaust heat line (L2) rises, the rare solution flowing through the first branch line (L1-1) communicating with the exhaust heat soot regenerator (30) Increase the flow rate and the temperature of the fluid flowing on the exhaust heat line (L2) side If (Tw) falls, it includes a step of reducing the flow rate of the rare solution flowing through the first branch line (L1-1) communicating with the exhaust heat regenerator (30) (FIG. 4). ).
[0042]
Furthermore, the control method of the absorption chiller / heater of the present invention includes an absorber (22), a high temperature regenerator (44), a low temperature regenerator (48), a waste heat regenerator (30), and a condenser (50 ) And an evaporator (52), and the dilute solution line (L1) through which the dilute solution sent from the absorber (22) flows is a low temperature solution heat exchange at the first branch point (BP). The first branch line (L1-1) in which the condenser (26) is interposed, and the second branch line (L1-2) in which the refrigerant drain heat exchanger (70) is interposed. The region (L11-70) between the low temperature regenerator (48) and the condenser (50) of the line (L11) through which the refrigerant vapor regenerated by the high temperature regenerator (44) flows is the refrigerant drain heat exchanger ( 70) is in thermal communication with the refrigerant (the refrigerant flowing through L11-70) after passing through the low-temperature regenerator (48). Enthalpy to be introduced into a dilute solution flowing through the second branch line (L1-2), a three-way valve (V1) interposed at the first branch point (BP), A temperature sensor (S3) for detecting the temperature (Ta) of the absorbing solution at the outlet of the absorber (22), and a control means (150) for controlling opening and closing of the three-way valve (V1) by a detection signal of the temperature sensor (S3). In the control method of the absorption chiller / heater having the above, the step of measuring the temperature (Ta) of the absorbing solution at the outlet of the absorber (22) by the temperature sensor (S3), and the absorbing solution at the outlet of the absorber (22) If the temperature (Ta) increases, the flow rate of the rare solution flowing through the first branch line (L1-1) communicating with the exhaust heat soot regenerator (30) is reduced, and the outlet of the absorber (22) The absorption solution temperature (Ta) at If the step of increasing the flow rate of the diluted solution flowing past the first branch line communicating with the exhaust heat 焚再 production unit (30) (L1-1), and a city (Figure 6).
[0043]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, an embodiment of the present invention will be described with reference to FIGS.
In the illustrated embodiment, similar members are denoted by the same reference numerals.
[0044]
In FIG. 1, the absorption chiller / heater of the present invention, indicated as a whole by reference numeral 20, is configured as a so-called “series flow” type.
In FIG. 1, the dilute solution sent from the absorber 22 by the pump 24 flows through the dilute solution line L1, and at the branch point BP (first branch point), the line L1-1 (first branch line). And branch to a line L1-2 (second branch line). A low temperature solution heat exchanger 26 is interposed in the line L1-1, and a refrigerant drain heat exchanger 70 is interposed in the line L1-2.
[0045]
Here, a three-way valve V1 is interposed at the first branch point BP, and the three-way valve V1 opens one of the first branch line L1-1 and the second branch line L1-2, It is configured to close the other. Reference numeral 100 indicates a driving means for the three-way valve V1.
[0046]
The enthalpy which the absorption solution (high concentration solution) which flows through the solution line L4 is input to the rare solution flowing through the line L1-1 through the low temperature solution heat exchanger 26. The dilute solution flowing in the line L1-2 holds the refrigerant flowing in the region L11-70 of the refrigerant line L11 (which becomes a gas phase, a liquid phase, and a gas-liquid two phase depending on the operating conditions of the absorption chiller / heater). Enthalpy is input through the refrigerant drain heat exchanger 70.
[0047]
The dilute solution line L1-1 passes through the low temperature solution heat exchanger 26 and then communicates with the exhaust heat soot regenerator 30 without immediately joining. The exhaust heat soot regenerator 30 is supplied with exhaust heat fluid (for example, warm waste water) flowing through the line L2.
[0048]
The exhaust heat fluid flowing through the line L2 inputs its enthalpy to the absorbing solution in the exhaust heat soot regenerator 30, and heats and partially regenerates the absorbing solution. Then, the regenerated refrigerant vapor flows into the condenser 50 via the vapor line L13.
[0049]
Here, the exhaust heat line L2 branches off from a line L2G communicating with an exhaust heat source (not shown), and the exhaust heat input three-way valve VE is provided at the branch point or the junction (the junction in the illustrated embodiment). It is intervened.
[0050]
The exhaust heat input three-way valve VE opens the line L2 according to the temperature of the exhaust heat fluid flowing through the line L2G (detected by an exhaust heat fluid temperature detecting means not shown), and the exhaust heat fluid flows through the exhaust heat line L2. Or open / close control is performed to close the line L2 and cause the exhaust heat fluid to bypass the line L2. The open / close sensor S1 detects whether the exhaust heat input three-way valve VE opens or closes the exhaust heat line L2.
[0051]
The absorbing solution after being heated and partially regenerated in the exhaust heat regenerator 30 by the enthalpy input from the exhaust heat line L2 flows through the line L1-144, and a head is added by the pump 32.
[0052]
The absorbing solution to which the head is added by the pump 32 joins the second branch line L1-2 at the joining point GP. The second branch line L1-2 and the line L1-144 join at the joining point GP, and then become the line L1-44. The second branch line L1-2 and the line L1-144 communicate with the high temperature regenerator 44 via the high temperature solution heat exchanger 42.
[0053]
In the high-temperature regenerator 44, the absorbing solution is heated and concentrated by the burner mechanism 45 to regenerate the refrigerant vapor (water vapor).
[0054]
The absorption solution (intermediate concentration solution) heated and condensed by the high temperature regenerator 44 flows through the intermediate concentration solution line L3 and flows into the low temperature regenerator 48. The enthalpy held by this solution is charged by the high-temperature solution heat exchanger 42 into the absorbing solution flowing through the line L1-44 (the line connecting the first junction GP and the high-temperature regenerator 44).
The absorption solution (high concentration solution) heated and regenerated by the low temperature regenerator 48 flows through the high concentration solution line L4 and is returned to the absorber 22 via the low temperature solution heat exchanger 26.
[0055]
On the other hand, the refrigerant vapor (water vapor: vapor phase refrigerant) regenerated by the high temperature regenerator 44 flows through the vapor line L11 and supplies the enthalpy held by the refrigerant vapor to the absorbing solution in the low temperature regenerator 48. Regenerate the absorbing solution.
[0056]
After the refrigerant vapor regenerated by the high temperature regenerator 44 exits the low temperature regenerator 48, it flows through the line (or region) L11-70 in the form of a gas phase refrigerant, a liquid phase refrigerant, or a gas-liquid two-phase flow. To do.
[0057]
The line L11-70 communicates with the condenser 50 via the refrigerant drain heat exchanger 70. And the enthalpy which the refrigerant | coolant which flows through line L11-70 holds is supplied to the rare solution which flows through the 2nd branch line L1-2 (rare solution line) via the refrigerant | coolant drain heat exchanger 70. FIG.
[0058]
Here, the heat held by the high-concentration solution flowing through the line L4 is not input to the dilute solution flowing through the line L1-2 via the low-temperature solution heat exchanger 26. Therefore, the enthalpy of the area discarded in the prior art, for example, the enthalpy (sensible heat) of the area of 40 ° C.-75 ° C. in the refrigerant flowing through the line L11-70 is supplied to the rare solution flowing through the line L1-2. Is done. That is, the enthalpy added by the burner mechanism 45 of the high temperature regenerator 44 is effectively used.
[0059]
In FIG. 1, a line L 5 is a liquid phase refrigerant line for supplying the liquid phase refrigerant condensed by the condenser 50 to the evaporator 52. The line L17 is a refrigerant vapor line in which the vaporized refrigerant vapor flows from the cold water flowing through the cold water line (a line communicating with a cooling load (not shown): not shown) flowing through the evaporator 52 and evaporated. It communicates with the vessel 22.
[0060]
Here, when the temperature of the exhaust heat fluid flowing through the line L2G is low and bypasses the exhaust heat line L2 and the exhaust heat regenerator 30, if attention is paid to the efficiency of the absorption chiller / heater 20 It is not necessary to flow a large amount of rare solution through the first branch line L1-1 communicating with the exhaust heat soot regenerator 30.
On the other hand, when the exhaust heat fluid flowing through the line L2G is hot and the exhaust heat fluid inputs the amount of heat retained by the exhaust heat fluid regenerator 30 (via the exhaust heat line L2), the exhaust heat residue regenerator If a large amount of a rare solution flows through the first branch line L 1-1 communicating with 30, it will greatly contribute to the efficiency of the absorption chiller / heater 20.
[0061]
Therefore, in the embodiment of FIG. 1, control means 150 is provided to perform opening / closing control of the three-way valve V1 interposed at the first branch point BP based on the opening / closing state of the exhaust heat input three-way valve VE. ing.
[0062]
Hereinafter, the control in the embodiment shown in FIG. 1 will be described with reference mainly to FIG.
First, the detection signal of the sensor S1 is sent to the control means 150 via the signal transmission line CL-1 (step ST1). Then, based on the signal, it is determined whether the exhaust heat input three-way valve VE opens or closes the exhaust heat line L2 side (step ST2).
[0063]
If the exhaust heat input three-way valve VE opens the exhaust heat line L2 side (YES in step ST2), the control means 150 is connected to the drive means 100 of the three-way valve V1 via the signal transmission line CL-V1. On the other hand, a control signal is output and the flow rate of the rare solution flowing through the first branch line L1-1 (WG side) communicating with the exhaust heat soot regenerator 30 is increased by a predetermined amount (in other words, the first 1) Increase the flow rate of the line L1-1 to a predetermined value) (step ST3).
[0064]
On the other hand, if the exhaust heat input three-way valve VE closes the exhaust heat line L2 side (step ST2 is NO), the first branch line L1-1 (WG side) communicating with the exhaust heat soot regenerator 30 ) Is decreased by a predetermined amount (in other words, the flow rate of the line L1-1 is decreased to the second predetermined value) (step ST4).
[0065]
If the dilute solution flow rate flowing through the first branch line L1-1 is increased or decreased to the first predetermined value or the second predetermined value (steps ST3 and ST4 are completed), it is determined whether or not the control is continued (step ST5). .
If the control is continued (NO in step ST5), the process returns to step ST1, and if step ST5 is YES, the control is terminated.
[0066]
As described above, according to the embodiment of FIGS. 1 and 2, the flow rate of the rare solution supplied to the exhaust heat soot regenerator 30 based on whether or not the exhaust heat is input to the exhaust heat soot regenerator 30. Therefore, the efficiency of the absorption chiller / heater 20 can be further improved through effective use of exhaust heat and effective use of the amount of heat added by the heating means 45.
[0067]
In the embodiment of FIG. 3, the configurations of the solution circulation system and the refrigerant circulation system are the same as those of the embodiment of FIGS. However, in the embodiment of FIGS. 1 and 2, the three-way valve V1 is controlled based on the opening and closing of the exhaust heat input three-way valve VE (FIG. 1), but in the embodiment of FIG. 3, the exhaust heat line L2 is controlled. The three-way valve V1 is controlled based on the temperature of the exhaust heat fluid flowing through the.
[0068]
In FIG. 3, a temperature sensor S 2 is installed in the exhaust heat line L 2 that is in thermal communication with the exhaust heat soot regenerator 30. The detection signal of the temperature sensor S2 is sent to the control means 150 via the signal transmission line CL-2.
And the control signal of the control means 150 is output to the drive means 100 of the three-way valve V1 via the signal transmission line CL-V1.
[0069]
The control in the embodiment of FIG. 3 will be described with reference to FIG.
If the temperature sensor S2 detects the temperature Tw of the exhaust heat fluid flowing through the exhaust heat line L2 (step ST11), it is determined whether or not the exhaust heat fluid temperature has increased (step ST12).
[0070]
If the exhaust heat fluid temperature Tw is rising (YES in step ST12), the control means 150 outputs a control signal to the drive means 100 of the three-way valve V1 via the signal transmission line CL-V1, The dilute solution flow rate of the first branch line L1-1 (WG side) communicating with the hot metal regenerator 30 is increased (step ST13).
Since the exhaust heat fluid temperature Tw rises and the amount of heat input to the exhaust heat trap regenerator 30 increases, if the flow rate of the line L1-1 is increased, the exhaust heat is effectively used and the efficiency is improved. is there.
[0071]
On the other hand, when the exhaust heat fluid temperature Tw is decreasing (NO in step ST12), the dilute solution flow rate of the first branch line L1-1 (WG side) communicating with the exhaust heat soot regenerator 30 is decreased ( Step S14). If the exhaust heat fluid temperature Tw falls, the amount of heat input to the exhaust heat trap regenerator 30 also decreases, and the regeneration amount of the rare solution flowing through the line L1-1 also decreases.
[0072]
If the flow rate of the first branch line L1-1 is increased or decreased (completion of steps ST13 and ST14), it is determined whether or not the control is terminated (step ST15). If step ST15 is NO, the process returns to step ST11. .
[0073]
The embodiment shown in FIG. 5 is the same as the embodiment of FIGS. 1 to 4 in terms of the solution circulation system and the refrigerant circulation system, but the installation position of the temperature sensor is different.
In FIG. 5, a temperature sensor S3 is interposed in a region of the rare solution line L1 between the absorber 22 and the pump 24, and detects the absorber outlet temperature Ta of the solution. The detected absorber outlet temperature Ta of the solution is sent to the control means 150 via the signal transmission line CL-3.
[0074]
The control signal from the control means 150 is output to the three-way valve V1 (the driving means 100) at the first branch point BP via the signal transmission line CL-V1.
Other configurations are the same as those in FIGS.
[0075]
Next, the control of the embodiment of FIG. 5 will be described with reference to FIG.
If the absorber outlet temperature Ta of the absorbing solution is detected by the temperature sensor S2 (step ST21), it is determined whether the absorber outlet temperature Ta has increased (step ST22).
[0076]
An increase in the absorber outlet temperature Ta (YES in step ST22) means that the diluted solution concentration has increased. And if a dilute solution density | concentration becomes deep, saturation temperature will rise. Therefore, even if the same amount of exhaust heat is input, the amount of regenerated steam is reduced. Therefore, even if a dilute solution having the same flow rate is supplied to the exhaust heat soot regenerator 30, the regeneration amount decreases. Therefore, when step ST22 is YES, the control unit 150 outputs a control signal to the driving unit 100 of the three-way valve V1 via the signal transmission line CL-V1 and communicates with the exhaust heat regenerator 30. The dilute solution flow rate in the line L1-1 (WG side) is decreased (step S23).
[0077]
On the other hand, when the absorber outlet temperature Ta is decreasing (NO in step ST22), the dilute solution concentration is low and the saturation temperature is decreasing. Therefore, when the same amount of exhaust heat is input, the amount of regeneration in the exhaust heat regenerator 30 increases (becomes easy to regenerate). Therefore, when step ST22 is NO, the flow rate of the rare solution in the first branch line L1-1 (WG side) communicating with the exhaust heat soot regenerator 30 is increased (step S24), and the regeneration of the exhaust heat soot regenerator 30 is performed. By increasing the amount, the consumption of high quality fuel in the high temperature regenerator 44 is suppressed, and the efficiency of the absorption chiller / heater is improved.
[0078]
If the flow rate of the first branch line L1-1 is decreased (steps ST23 and ST24 are completed), it is determined whether or not to end the control (step ST25). If step ST25 is NO, the process proceeds to step ST21. Return.
[0079]
The embodiment of FIGS. 1, 2, 3, 4, 5, 6, respectively, uses a single sensor (S 1, S 2, S 3) with a single parameter (in the exhaust heat line L 2). The open / close control of the three-way valve V1 is performed based on whether or not the exhaust heat fluid is flowing, whether the exhaust heat fluid temperature Tw is increased or decreased, and the temperature Ta of the absorbent solution is increased or decreased at the outlet of the absorber 22. .
However, it is also possible to control by combining a plurality of sensors and a plurality of parameters.
[0080]
7 and 8, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet of the absorber 22 A sensor S3 for detecting the temperature Ta is provided, and control is performed with reference to all parameters detected by each sensor.
For other configurations, the embodiment of FIGS. 7 and 8 is the same as the embodiment of FIGS.
[0081]
Next, the control of the embodiment of FIG. 7 will be described with reference mainly to FIG. First, the sensor S1 detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 detects the exhaust heat fluid temperature Tw, and the sensor S3 detects the outlet temperature Ta of the absorber 22. (Step ST31).
[0082]
If the exhaust heat fluid is flowing through the exhaust heat line L2, whether the exhaust heat fluid temperature Tw and the liquid temperature Ta of the absorption solution at the outlet of the absorber 22 are detected (completion of step ST31), step S1- Based on each parameter detected in S3, based on various mathematical formulas, characteristic curves, maps, etc., the optimal dilute solution flow rate to the exhaust heat soot regenerator 30 at that time, in other words, the first branch line L1 -1 is determined (step ST32).
[0083]
Next, the optimum flow rate Qc determined in step ST32 is compared with the dilute solution flow rate Qp in the first branch line L1-1 at that time (step ST33).
[0084]
When the optimum flow rate Qc determined in step ST32 is smaller than the dilute solution flow rate Qp in the first branch line L1-1 at that time (step ST33 is “Qc <Qp”), the control unit 150 A control signal is output to the driving means 100 of the three-way valve V1 via the signal transmission line CL-V1, and the flow rate of the dilute solution in the first branch line L1-1 (WG side) communicating with the exhaust heat soot regenerator 30 is reduced. (Step S34)
[0085]
When the optimum flow rate Qc determined in step ST32 is equal to the dilute solution flow rate Qp in the first branch line L1-1 at that time (step ST33 is “Qc = Qp”), the opening degree of the three-way valve V1 is changed. Without maintaining, the dilute solution flow rate of the first branch line L1-1 (WG side) communicating with the exhaust heat soot regenerator 30 is maintained (step S35).
[0086]
When the optimum flow rate Qc determined in step ST32 is larger than the dilute solution flow rate Qp in the first branch line L1-1 at that time (step ST33 is “Qc> Qp”), the control unit 150 A control signal is output to the driving means 100 of the three-way valve V1 via the signal transmission line CL-V1, and the flow rate of the rare solution in the first branch line L1-1 (WG side) communicating with the exhaust heat soaker regenerator 30 is increased. (Step S36).
[0087]
The flow control of the first branch line L1-1 is completed (steps ST34, ST35, ST36 are completed), and it is determined whether or not to end the control (step ST37). If step ST37 is NO, the process returns to step ST31.
[0088]
The embodiment of FIG. 9 is also related to a so-called “series flow type” absorption chiller / heater, similar to the embodiment of FIGS.
[0089]
Also in this embodiment, the dilute solution line L1-1 branched at the branch point BP does not immediately join after passing through the low-temperature solution heat exchanger 26, and communicates with the exhaust heat regenerator 30. However, the embodiment of FIG. 9 is compared with the embodiment of FIGS. 1 to 8 at the junction (first junction point GP) of the first branch line L1-1 and the second branch line L1-2. The position is different.
[0090]
In FIG. 9, the rare solution supplied to the exhaust heat soot regenerator 30 via the rare solution line L1-1 is heated by enthalpy supplied from the exhaust heat line L2, and partially regenerated, and then the line L1- 144, the head is loaded by the pump 32, and passes through the hot solution heat exchanger 42.
Then, at the first junction GP in the region between the high temperature solution heat exchanger 42 and the high temperature regenerator 44, the first branch line L1-2 and the second branch line L1-2 merge and the line L1-44. And communicates with the high temperature regenerator 44.
[0091]
Other configurations and operational effects in the embodiment of FIG. 9 are the same as those of the embodiment of FIGS. The opening / closing control of the three-way valve V1 at the first branch point BP of the embodiment of FIG. 9 is the same as that of the embodiment of FIGS.
[0092]
In FIG. 9, the sensor S1 that detects whether or not the exhaust heat fluid flows through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal is transmitted to the signal transmission line CL-V1. Is sent to the driving means 100 of the three-way valve V1.
[0093]
However, also in the embodiment of FIG. 9, any one of the sensors S1, S2, and S3 is provided, and control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, The opening / closing control of the three-way valve V1 can also be performed based on only one of the absorbing solution liquid temperature Ta) at the outlet of the absorber 22. Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0094]
1 to 9 show an embodiment in which the present invention is applied to a so-called “series flow” type absorption chiller / heater. On the other hand, in the embodiment of FIG. 10, the present invention is applied to a so-called “parallel flow” type absorption chiller / heater.
[0095]
In FIG. 10, the dilute solution coming out of the absorber 22 is added with a head by the pump 24 and flows through the dilute solution line L1, and branches to the lines L1-1 and L1-2 at the first branch point BP. Here, a low temperature solution heat exchanger 26 is interposed in the line L1-1, and a refrigerant drain heat exchanger 70 is interposed in the line L1-2.
[0096]
The line L1-1 and the line L1-2 pass through the low-temperature solution heat exchanger 26 or the refrigerant drain heat exchanger 70, and then merge at a first junction point GP provided in the vicinity thereof. P1. This line L1-P1 branches at a second branch point P1 into a line L1-3 communicating with the high temperature regenerator 44 and a line L1-4 communicating with the exhaust heat soot regenerator 30.
[0097]
In the embodiment of FIG. 10, the three-way valve V2 is interposed at the second branch point P1, and the control means is connected to the driving means 120 of the three-way valve V2 via the signal transmission line CL-V2. A control signal is sent from 150.
In addition, about the installation position of sensor S1, S2, S3, it is the same as that of embodiment of FIGS. 1-9.
[0098]
The dilute solution flowing through the line L1-3 flows into the high temperature regenerator 44 through the high temperature solution heat exchanger 42, and after being heated and concentrated by the burner mechanism 45, flows through the solution line L3.
The refrigerant vapor regenerated by the high temperature regenerator 44 flows through a line L11 communicating with the low temperature regenerator 48, supplies enthalpy held in the absorbing solution in the low temperature regenerator 48 to regenerate the refrigerant, and then regenerates the line L11-70. The enthalpy is supplied to the dilute solution in the line L 1-2 through the refrigerant drain heat exchanger 70, and sent to the condenser 50.
[0099]
The rare solution flowing through the line L1-4 is heated, regenerated, and concentrated in the exhaust heat regenerator 30 by adding the enthalpy held by the exhaust heat fluid flowing through the exhaust heat line L2. Then, the refrigerant vapor regenerated in the exhaust heat soot regenerator 30 is supplied to the condenser 50 via the line L13, and the regenerated / concentrated absorption solution flows through the solution line L1-41, and the low temperature regenerator 48. Flow into.
[0100]
The absorption solution heated, regenerated and concentrated by the low temperature regenerator 48 flows through the solution line L1-42, and the solution line L1-42 joins the solution line L3 from the high temperature regenerator 44 at the second junction P2. Then, the solution line L4 is obtained and the process returns to the absorber 22.
[0101]
In this embodiment as well, as described in the embodiment of FIG. 1, the enthalpy held by the refrigerant flowing through the line L11-70 is rarely passed through the refrigerant drain heat exchanger 70 over a wide temperature range. The enthalpy supplied to the dilute solution flowing in the solution line L1-2 and given in the high temperature regenerator 44 (the burner mechanism 45) is effectively used for generating the refrigerant vapor.
Moreover, since the enthalpy possessed by the exhaust heat fluid is used for regeneration in the exhaust heat soot regenerator 30, the use efficiency of the enthalpy possessed by the exhaust heat fluid is also improved.
As a result, the efficiency of the entire absorption chiller / heater increases.
[0102]
Other configurations and operational effects in the embodiment of FIG. 10 are the same as those of the embodiment of FIGS. The opening / closing control of the three-way valve V2 at the second branch point P1 in the embodiment of FIG. 10 is the same as the opening / closing control of the three-way valve V1 at the first branch point BP in the embodiment of FIGS.
[0103]
Therefore, based on the relative relationship between the exhaust heat fluid temperature and the absorption solution, the flow rate of the absorption solution flowing into the exhaust heat soot regenerator 30 is controlled by controlling the opening and closing of the three-way valve V1, and thus the absorption cold temperature The efficiency of the water machine can be improved.
[0104]
In FIG. 10, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0105]
However, also in the embodiment of FIG. 10, any one of the sensors S1, S2, and S3 is provided, and the control parameter (whether or not the exhaust heat fluid flows through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, The opening / closing control of the three-way valve V1 can also be performed based on only one of the absorbing solution liquid temperature Ta) at the outlet of the absorber 22. Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0106]
The embodiment of FIG. 11 is also an embodiment according to the “parallel flow type” absorption chiller / heater.
In the embodiment shown in FIG. 10, the two lines L 1-1 and L 1-2 branched at the first branch point BP are immediately passed through the low temperature solution heat exchanger 26 or the refrigerant drain heat exchanger 70. It merges at a first merge point GP provided in the vicinity thereof.
[0107]
On the other hand, in the embodiment of FIG. 11, the dilute solution line L1-1 branched at the first branch point BP passes through the low temperature solution heat exchanger 26 and then does not immediately join, but the second branch. At point P1, the line branches into a line L1-3 communicating with the high temperature regenerator 44 and a line L1-4. And in line L1-4, it joins with the other branch line L1-2 at the 1st confluence | merging point GP, and is connected to the exhaust-heat-steam regenerator 30. FIG.
[0108]
In other words, in the embodiment of FIG. 11, the first junction point GP is provided in a region between the second branch point P1 and the exhaust heat trap regenerator 30.
[0109]
Other configurations in the embodiment of FIG. 11 are the same as those of the embodiment shown in FIG. The opening / closing control of the three-way valve V2 at the second branch point P1 in the embodiment of FIG. 11 (substantially equal to the opening / closing control of the three-way valve V2 at the second branch point P1 of the embodiment of FIG. 10) is shown in FIG. This is the same as the open / close control of the three-way valve V1 at the first branch point BP in the ninth embodiment.
[0110]
Also in FIG. 11, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0111]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) The opening / closing control of the three-way valve V1 can be performed based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0112]
The embodiment shown in FIG. 12 is almost the same as the embodiment shown in FIG. 11 in the solution circulation system, the refrigerant circulation system, and other configurations.
However, in the embodiment shown in FIG. 11, the three-way valve V2 is provided at the second branch point P1, and the opening and closing control of the three-way valve V2 is performed, whereas in the embodiment shown in FIG. A three-way valve V1 is provided at the branch point BP, and opening / closing control is performed on the three-way valve V1.
[0113]
Other configurations and operational effects in the embodiment of FIG. 12 are the same as those of the embodiment of FIG.
[0114]
Here, also in FIG. 12, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0115]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0116]
The embodiment shown in FIG. 13 is almost the same as the embodiment shown in FIG. 11 or FIG. 12 in the solution circulation system, the refrigerant circulation system, and other configurations.
In the embodiment shown in FIG. 11, a three-way valve V2 is provided at the second branch point P1, and the opening and closing control of the three-way valve V2 is performed. In the embodiment shown in FIG. 12, the three-way valve is provided at the first branch point BP. V1 is provided to perform opening / closing control on the three-way valve V1.
[0117]
On the other hand, in the embodiment shown in FIG. 13, the three-way valve V1 is provided at the first branch point BP, and the three-way valve V2 is also provided at the second branch point P1. By outputting a control signal to the driving means 100 of the three-way valve V1 via -V1 and outputting a control signal to the driving means 120 of the three-way valve V2 via the transmission line CL-V2, the three-way valves V1 and V2 Both are controlled to open and close.
[0118]
Other configurations and effects in the embodiment of FIG. 13 are the same as those of the embodiment of FIGS. 11 and 12, and the three-way valve V1 provided at the first branch point BP and the three-way valve V2 provided at the second branch point P1. The mode of the opening / closing control is also the same as that of the embodiment of FIGS.
[0119]
Here, also in FIG. 13, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0120]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0121]
The embodiment shown in FIG. 14 also relates to a “parallel flow type” absorption chiller / heater.
In FIG. 14, the branch line L1-1 does not immediately merge with the other branch line L1-2 after passing through the low-temperature solution heat exchanger 26, and goes to the high-temperature regenerator 44 side at the second branch point P1. L1-11 branches to a line L1-12 that communicates with the exhaust heat regenerator 30.
[0122]
Here, a three-way valve V2 is provided at the second branch point P1, and a control signal is output from the control means 150 to the driving means 120 of the three-way valve V2 via the signal transmission line CL-V2. Opening / closing control is performed.
[0123]
The line L1-11 heading toward the high-temperature regenerator 44 joins the branch line L1-2 at the first junction GP in the region between the second branch point P1 and the high-temperature solution heat exchanger 42, so that the line L1- 44 and communicates with the high temperature regenerator 44.
[0124]
On the other hand, the line L1-12 communicates with the exhaust heat soot regenerator 30, and the absorption solution heated and partially regenerated by the exhaust heat soot regenerator 30 is supplied to the low temperature regenerator 48 via the line L1-121. The absorbent solution heated and partially regenerated by the low temperature regenerator 48 flows through the line L1-122, and the line L1-122 joins the line L3 at the second junction P to become the line L4. Return to.
[0125]
Other configurations in the embodiment of FIG. 14 are the same as those of the embodiment shown in FIGS. Moreover, about an effect, it is the same as that of embodiment shown in FIGS.
The same applies to the open / close control mode of the three-way valve V2 provided at the second branch point P1.
[0126]
Here, also in FIG. 14, the sensor S 1 that detects whether the exhaust heat fluid is flowing through the exhaust heat line L 2, the sensor S 2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22. Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0127]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0128]
The embodiment shown in FIG. 15 is almost the same as the embodiment shown in FIG. 14 in the solution circulation system, the refrigerant circulation system, and other configurations.
However, in the embodiment shown in FIG. 14, the three-way valve V2 is provided at the second branch point P1 and the three-way valve V2 is controlled to open and close, whereas in the embodiment shown in FIG. A three-way valve V1 is provided at the branch point BP, and opening / closing control is performed on the three-way valve V1.
[0129]
Other configurations and operational effects in the embodiment of FIG. 15 are the same as those of the embodiment of FIG. 14, and the mode of opening / closing control of the three-way valve V1 provided at the first branch point BP is also the same.
[0130]
Here, also in FIG. 15, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0131]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0132]
The embodiment shown in FIG. 16 is almost the same as the embodiment shown in FIG. 14 or FIG. 15 in the solution circulation system, the refrigerant circulation system, and other configurations.
In the embodiment shown in FIG. 14, a three-way valve V2 is provided at the second branch point P1, and the opening and closing control of the three-way valve V2 is performed. In the embodiment shown in FIG. 15, the three-way valve at the first branch point BP. V1 is provided to perform opening / closing control on the three-way valve V1.
[0133]
On the other hand, in the embodiment shown in FIG. 16, the three-way valve V1 is provided at the first branch point BP, and the three-way valve V2 is also provided at the second branch point P1. By outputting a control signal to the driving means 100 of the three-way valve V1 via -V1 and outputting a control signal to the driving means 120 of the three-way valve V2 via the transmission line CL-V2, the three-way valves V1 and V2 Both are controlled to open and close.
[0134]
Other configurations and operational effects in the embodiment of FIG. 16 are the same as those of the embodiment of FIGS. 14 and 15, and the three-way valve V1 provided at the first branch point BP and the three-way valve V2 provided at the second branch point P1. The mode of the opening / closing control is the same as that of the embodiment of FIGS.
[0135]
Here, also in FIG. 16, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0136]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0137]
The embodiment of FIG. 17 also shows a “parallel flow type” absorption chiller / heater.
In FIG. 17, the branch line L 1-1 communicates with the line L 1-11 toward the high temperature regenerator 44 side and the exhaust heat soaker regenerator 30 at the second branch point P 1 after passing through the low temperature solution heat exchanger 26. Branch to line L1-12.
[0138]
Here, a three-way valve V2 is provided at the second branch point P1, and a control signal is output from the control means 150 to the driving means 120 of the three-way valve V2 via the signal transmission line CL-V2. Opening / closing control is performed.
[0139]
The line L1-11 passes through the high temperature solution heat exchanger 42, and joins the branch line L1-2 at the first junction GP in the region between the high temperature solution heat exchanger 42 and the high temperature regenerator 44. The line becomes L1-44 and communicates with the high temperature regenerator 44.
[0140]
Other configurations in the embodiment of FIG. 17 are the same as those of the embodiment shown in FIGS. The operational effects of the embodiment of FIG. 17 are the same as those of the embodiment shown in FIGS. Also, the opening / closing control of the three-way valve V2 at the second branch point P1 is the same as in the embodiment of FIGS.
[0141]
The embodiment shown in FIG. 18 is almost the same as the embodiment shown in FIG. 17 in the solution circulation system, the refrigerant circulation system, and other configurations.
However, in the embodiment shown in FIG. 17, the three-way valve V2 is provided at the second branch point P1, and the opening and closing control of the three-way valve V2 is performed, whereas in the embodiment shown in FIG. A three-way valve V1 is provided at the branch point BP, and opening / closing control is performed on the three-way valve V1.
[0142]
The other configurations and operational effects in the embodiment of FIG. 18 are the same as those of the embodiment of FIG. 17, and the open / close control mode of the three-way valve V1 provided at the first branch point BP is also the same.
[0143]
Here, also in FIG. 18, the sensor S1 that detects whether or not the exhaust heat fluid flows through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0144]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0145]
The embodiment shown in FIG. 19 is almost the same as the embodiment shown in FIG. 17 or FIG. 18 in the solution circulation system, the refrigerant circulation system, and other configurations.
In the embodiment shown in FIG. 17, a three-way valve V2 is provided at the second branch point P1, and the opening and closing control of the three-way valve V2 is performed. In the embodiment shown in FIG. 18, the three-way valve at the first branch point BP. V1 is provided to perform opening / closing control on the three-way valve V1.
[0146]
On the other hand, in the embodiment shown in FIG. 19, the three-way valve V1 is provided at the first branch point BP, and the three-way valve V2 is provided at the second branch point P1. By outputting a control signal to the driving means 100 of the three-way valve V1 via -V1 and outputting a control signal to the driving means 120 of the three-way valve V2 via the transmission line CL-V2, the three-way valves V1 and V2 Both are controlled to open and close.
[0147]
Other configurations and operational effects in the embodiment of FIG. 19 are the same as those of the embodiment of FIGS. 17 and 18, and the three-way valve V1 provided at the first branch point BP and the three-way valve V2 provided at the second branch point P1. The mode of opening / closing control is also the same as that of the embodiment of FIGS.
[0148]
Here, also in FIG. 19, the sensor S1 that detects whether or not the exhaust heat fluid flows through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 Sensor S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, CL-3, respectively. A control signal is transmitted based on the control parameters.
[0149]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0150]
The embodiment of FIG. 20 also shows a parallel flow type absorption chiller / heater.
In FIG. 20, the dilute solution line L1 branches to a first branch line L1-1 and a second branch line L1-2 at a first branch point BP. The first branch line L1-1 is provided with a low-temperature solution heat exchanger 26, and the second branch line L1-2 is provided with a refrigerant drain heat exchanger 70.
[0151]
Here, a three-way valve V1 is interposed at the first branch point BP, and a control signal is output from the control means 150 to the driving means 100 of the three-way valve V1 via the signal transmission line CL-V1. Thus, opening / closing control of the three-way valve V1 is performed.
[0152]
The first branch line L 1-1 passes through the low temperature solution heat exchanger 26 and then communicates with the exhaust heat regenerator 30. Then, the absorbing solution heated and partially regenerated by the exhaust heat regenerator 30 flows through a line L1-31, and the line L1-31 is a line L1 toward the high temperature regenerator 44 side at the second branch point P1. -44 and a line L1-48 heading toward the low temperature regenerator 48 side.
[0153]
Here, the line L1-48 joins the branch line L1-2 at the first joining point GP to become a line L1-49, and communicates with the low temperature regenerator 48.
The absorbing solution heated and partially regenerated by the low temperature regenerator 48 flows through the line L1-51, and the line L1-51 merges with the line L3 at the second merge point P1 to become the line L4.
[0154]
Other configurations in the embodiment of FIG. 20 are the same as those of the embodiment shown in FIGS. The operational effects of the embodiment of FIG. 20 are the same as those of the embodiment shown in FIGS.
Furthermore, the mode of opening / closing control of the three-way valve V1 installed at the first branch point BP in the embodiment of FIG. 20 is the same as that of the embodiment of FIGS.
[0155]
Also in FIG. 20, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0156]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0157]
The embodiment of FIG. 21 also relates to a parallel flow type absorption chiller / heater.
In FIG. 21, of the two branch lines L1-1 and L1-2 branched at the first branch point BP, the branch line L1-1 interposing the low-temperature solution heat exchanger 26 The absorbent solution communicated with the regenerator 30 and heated / partially regenerated by the exhaust heat regenerator 30 flows through the line L1-31, and the line L1-31 is at the second branch point P1 on the high temperature regenerator 44 side. Branches to a line L1-44 heading to the line L1-48 and a line L1-48 heading to the low temperature regenerator 48 side.
[0158]
A three-way valve V1 is provided at the first branch point BP, and a control signal is output from the control means 150 to the driving means 100 of the three-way valve V1 via the signal transmission line CL-V1, Open / close control of the three-way valve V1 is performed.
[0159]
In the embodiment of FIG. 21, the line L1-44 toward the high temperature regenerator 44 is the first junction GP in the region between the second branch point P1 and the high temperature solution heat exchanger 42, and the branch line L1- 2 joins to become a line L1-46, and the line L1-46 communicates with the high-temperature regenerator 44 via the high-temperature solution heat exchanger 42.
[0160]
On the other hand, the absorption solution supplied to the low temperature regenerator 48 through the line L1-48, heated and partially regenerated flows through the line L1-49, and joins the line L3 at the second junction P1, and then the line L4. It becomes.
[0161]
Other configurations in the embodiment of FIG. 21 are the same as those of the embodiment shown in FIG. 21 is the same as that of the embodiment shown in FIGS. 1 to 20.
And the mode of opening and closing control of the three-way valve V1 provided at the first branch point BP is also the same as that of the embodiment of FIGS.
[0162]
Also in FIG. 21, the sensor S1 that detects whether or not the exhaust heat fluid flows through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0163]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0164]
FIG. 22 also shows an embodiment of a parallel flow type absorption chiller / heater.
Also in FIG. 22, the rare solution line L1 is the first branch point BP, and the first branch line L1-1 including the low-temperature solution heat exchanger 26 and the second branch line including the refrigerant drain heat exchanger 70 are provided. Branch to the branch line L1-2.
[0165]
A three-way valve V1 is provided at the first branch point BP, and a control signal is output from the control means 150 to the driving means 100 of the three-way valve V1 via the signal transmission line CL-V1. Thereby, opening / closing control of the three-way valve V1 is performed.
[0166]
The absorption solution flowing through the first branch line L1-1 is a line heading toward the high-temperature regenerator 44 via the low-temperature solution heat exchanger 26, the exhaust heat soot regenerator 30, the line L1-31, and the second branch point P1. It flows through L1-44. The line L1-44 is a first junction GP in the region between the high temperature solution heat exchanger 42 and the high temperature regenerator 44, and merges with the branch line L1-2 to become a line L1-46. 44.
[0167]
Other configurations in the embodiment of FIG. 22 are the same as those of the embodiment shown in FIG. The operational effects of the embodiment of FIG. 22 are the same as those of the embodiment shown in FIGS.
Furthermore, the manner of opening / closing control of the three-way valve V1 provided at the first branch point BP is also the same as in FIGS.
[0168]
Also in FIG. 22, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0169]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0170]
23 to 25 show an embodiment in which the present invention is applied to a so-called “reverse flow” type absorption chiller / heater.
[0171]
In the absorption chiller / heater according to the embodiment shown in FIG. 23, the dilute solution that has left the absorber 22 and the head is added by the pump 24 flows through the dilute solution line L1, and the dilute solution line L1 is the first branch point. In BP, it branches into the 1st branch line L1-1 in which the low temperature solution heat exchanger 26 was interposed, and the 2nd branch line L1-2 in which the refrigerant | coolant drain heat exchanger 70 was interposed. .
[0172]
A three-way valve V1 is provided at the first branch point BP, and a control signal is output from the control means 150 to the driving means 100 of the three-way valve V1 via the signal transmission line CL-V1. Thus, opening / closing control of the three-way valve V1 is performed.
[0173]
The dilute solution line L1-1 branched at the first branch point BP passes through the low-temperature solution heat exchanger 26 and then communicates with the exhaust heat soot regenerator 30 to remove the absorption solution flowing through the exhaust solution regenerator. 30.
[0174]
The absorbent solution heated and partially regenerated by the exhaust heat soaker regenerator 30 flows through the line L1-130 and is supplied to the low temperature regenerator 48. The absorbing solution heated and partially regenerated by the low temperature regenerator 48 flows through the line L6, and the head is loaded by the pump 62. And line L6 joins the 2nd branch line L1-2 at the 1st junction GP in the field between low temperature regenerator 48 and high temperature solution heat exchanger 42, and becomes line L6-44.
[0175]
The line L6-44 communicates with the high temperature regenerator 44 via the high temperature solution heat exchanger 42.
The absorbent solution heated and concentrated by the burner mechanism 45 of the high-temperature regenerator 44 flows through the solution line L3 and is returned to the absorber 22.
[0176]
The refrigerant vapor regenerated by the high temperature regenerator 44 flows through a line L11 communicating with the low temperature regenerator 48, supplies enthalpy held in the absorbing solution in the low temperature regenerator 48 to regenerate the refrigerant, and then regenerates the line L11-70. The enthalpy is supplied to the dilute solution in the line L 1-2 through the refrigerant drain heat exchanger 70, and sent to the condenser 50.
[0177]
In the embodiment of FIG. 23 as well, the enthalpy possessed by the refrigerant flowing through the line L11-70 is the refrigerant drain heat exchanger 70 over a wide temperature range, as described in the embodiment of FIGS. The enthalpy supplied to the dilute solution flowing in the dilute solution line L1-2 and applied in the high temperature regenerator 44 (the burner mechanism 45) is effectively used for generating the refrigerant vapor.
[0178]
Further, based on the relative relationship between the exhaust heat fluid temperature and the absorption solution, the flow rate of the absorption solution flowing into the exhaust heat soot regenerator 30 is controlled by controlling the opening and closing of the three-way valve V1, and thus the absorption cold temperature The efficiency of the water machine can be improved.
[0179]
Other configurations in the embodiment of FIG. 23 are the same as those of the embodiment of FIGS. Other operational effects in the embodiment of FIG. 23 are the same as those of the embodiment of FIGS.
And the mode of opening and closing control of the three-way valve V1 at the first branch point BP is also the same as that of the embodiment of FIGS.
[0180]
23, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0181]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0182]
In the embodiment shown in FIG. 23, the first junction point GP where the line L1-2 and the line L6 merge is provided in a region between the low temperature regenerator 48 and the high temperature solution heat exchanger 42.
On the other hand, in the embodiment of FIG. 24, the first junction point GP where the line L6 and the line L1-2 join is provided in a region between the high temperature solution heat exchanger 42 and the high temperature regenerator 44. Yes.
[0183]
In other words, the absorbing solution heated and concentrated by the low temperature regenerator 48 and loaded with the head by the pump 62 flows through the line L6, passes through the high temperature solution heat exchanger 42, and then passes through the high temperature solution heat exchanger 42. At the first junction GP in the region between the high-temperature regenerators 44, the second junction line L1-2 is merged to become a line L6-44. The line L6-44 communicates with the high temperature regenerator 44.
[0184]
Other configurations in the embodiment of FIG. 24 are the same as those of the embodiment shown in FIG. The operational effects of the embodiment of FIG. 24 are the same as those of the embodiment shown in FIGS.
The opening / closing control of the three-way valve V1 at the branch point BP in FIG. 24 is the same as that in the embodiment shown in FIGS.
[0185]
Also in FIG. 24, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0186]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0187]
Also in the embodiment shown in FIG. 25, the dilute solution line L1-1 branched at the first branch point BP passes through the low temperature solution heat exchanger 26 and then immediately joins the exhaust heat soot regenerator 30 without joining. Communicate. Then, the absorbing solution flowing inside the line L 1-1 is supplied to the exhaust heat soot regenerator 30.
[0188]
The absorbent solution heated and partially regenerated by the exhaust heat soot regenerator 30 flows through a line L1-130 communicating with the low temperature regenerator 48, and the first solution in the region between the exhaust heat soot regenerator 30 and the low temperature regenerator 48. At the confluence point GP, the line L1-2 is merged to become a line L1-48. The line L1-48 communicates with the low temperature regenerator 48, and the absorption solution therein is supplied to the low temperature regenerator 48.
The absorbing solution heated and partially regenerated by the low temperature regenerator 48 flows through the line L6, is loaded with the head by the pump 62, and is supplied to the high temperature regenerator 44.
[0189]
Other configurations in the embodiment of FIG. 25 are the same as those of the embodiment shown in FIGS. The operational effects of the embodiment of FIG. 25 are the same as those of the embodiment shown in FIGS.
Furthermore, the opening / closing control of the three-way valve V1 at the branch point BP in FIG. 25 is the same as that in the embodiment shown in FIGS.
[0190]
Also in FIG. 25, the sensor S1 that detects whether or not the exhaust heat fluid flows through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0191]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0192]
FIG. 26 relates to a modified embodiment of the “parallel flow” type absorption chiller / heater, in which the absorber and the evaporator (so-called “lower body” portion) are configured in two stages, a low pressure side and a high pressure side. The company intends to improve the efficiency of the absorption chiller / heater.
Further, the low pressure side absorber 22L is provided with a solution cooling absorber 74, and the enthalpy held by the concentrated absorption solution dropped in the low pressure side absorber 22L is introduced into the rare solution, and the rare solution temperature is set. Since it raises, it becomes easy to reproduce | regenerate that much and the efficiency of an absorption cold / hot water machine is improved.
Furthermore, a high quality fuel exhaust heat input heat exchanger 76 is interposed in the region between the high temperature solution heat exchanger 42 and the high temperature regenerator 44 in the line L1-44. High quality fuel exhaust heat flowing through the high quality fuel exhaust heat line L20 (the amount of heat held by the exhaust heat fluid discarded outside the system after the absorbent solution is heated by the heating means of the burner mechanism 45) Has been introduced.
[0193]
Other configurations and operational effects in the embodiment of FIG. 26 are the same as those of the embodiment shown in FIG. And the open / close control of the three-way valve V2 at the second branch point P1 is the same as in FIG.
[0194]
Also in FIG. 26, the sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, the sensor S2 that detects the exhaust heat fluid temperature Tw, and the outlet temperature Ta of the absorber 22 are detected. A sensor S3 is provided, and parameters detected by each sensor are input to the control means 150 via signal transmission lines CL-1, CL-2, and CL-3, respectively, and the control signal 150 includes all control parameters. The control signal is sent based on
[0195]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0196]
The embodiment of FIG. 27 has a configuration substantially similar to that of the embodiment of FIG. 26, but is connected to a line L1-3 connecting the first junction point GP and the second branch point P1 to the heat exchanger for exhaust heat input. 80 is interposed. Through this heat exchanger 80 for exhaust heat input, the amount of heat held by the exhaust heat fluid flowing in the exhaust heat line L2 is input to the absorbing solution flowing in the line L1-3.
[0197]
Other configurations and operational effects in the embodiment of FIG. 27 are the same as those of the embodiment of FIG. The opening / closing control of the three-way valve V2 at the second branch point P1 is the same as that in FIG. 26 (or FIG. 10).
[0198]
In FIG. 27, a sensor S1 that detects whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, a sensor S2 that detects the exhaust heat fluid temperature Tw, and a sensor that detects the outlet temperature Ta of the absorber 22. S3 is provided, and the parameters detected by each sensor are input to the control means 150 via the signal transmission lines CL-1, CL-2, and CL-3, respectively. The control signal 150 includes all the control parameters. A control signal is sent based on this.
[0199]
However, any one of the sensors S1, S2, S3 is provided, and the control parameters (whether or not the exhaust heat fluid is flowing through the exhaust heat line L2, whether or not the exhaust heat fluid temperature Tw, the absorption solution at the outlet of the absorber 22) It is also possible to control the opening / closing of the three-way valve V1 based on only one of the liquid temperatures Ta). Similarly, any two sensors can be provided, and control can be performed by selecting two types from the above three types of control parameters.
[0200]
【The invention's effect】
As described above, in the absorption chiller / heater of the present invention, based on the relative temperature relationship between the exhaust heat and the absorption solution circulation system inside the absorption chiller / heater, the opening / closing control of the three-way valve at the branch point is performed, Therefore, by controlling the amount of absorbed solution flowing into the exhaust heat regenerator, the high-quality fuel consumed in the high-temperature regenerator is suppressed, and the exhaust heat is effectively used to improve the efficiency of the absorption chiller / heater. It can be improved.
In addition, the enthalpy held by the exhaust heat fluid after regenerating the absorbing solution with the high temperature regenerator, which has not been used conventionally, is introduced into the rare solution via the refrigerant drain heat exchanger, and the rare solution It is used for heating. Therefore, high quality fuel is effectively used, and the thermal efficiency of the absorption chiller / heater is further improved.
Furthermore, according to the present invention, in the exhaust heat regenerator, the amount of refrigerant vapor regenerated can be increased, and the thermal efficiency of the absorption chiller / heater can be improved.
[Brief description of the drawings]
FIG. 1 is a block diagram schematically illustrating a first embodiment of the present invention.
FIG. 2 is a view showing a control flowchart of the embodiment of FIG. 1;
FIG. 3 is a block diagram schematically illustrating a second embodiment of the present invention.
FIG. 4 is a view showing a control flowchart of the embodiment of FIG. 3;
FIG. 5 is a block diagram schematically illustrating a third embodiment of the present invention.
6 is a diagram showing a control flowchart of the embodiment of FIG. 5;
FIG. 7 is a block diagram schematically illustrating a fourth embodiment of the present invention.
FIG. 8 is a view showing a control flowchart of the embodiment of FIG. 7;
FIG. 9 is a block diagram schematically illustrating a fifth embodiment of the present invention.
FIG. 10 is a block diagram schematically illustrating a sixth embodiment of the present invention.
FIG. 11 is a block diagram schematically illustrating a seventh embodiment of the present invention.
FIG. 12 is a block diagram schematically illustrating an eighth embodiment of the present invention.
FIG. 13 is a block diagram schematically illustrating a ninth embodiment of the present invention.
FIG. 14 is a block diagram schematically illustrating a tenth embodiment of the present invention.
FIG. 15 is a block diagram schematically illustrating an eleventh embodiment of the present invention.
FIG. 16 is a block diagram schematically illustrating a twelfth embodiment of the present invention.
FIG. 17 is a block diagram schematically illustrating a thirteenth embodiment of the present invention.
FIG. 18 is a block diagram schematically illustrating a fourteenth embodiment of the present invention.
FIG. 19 is a block diagram schematically illustrating a fifteenth embodiment of the present invention.
FIG. 20 is a block diagram schematically illustrating a sixteenth embodiment of the present invention.
FIG. 21 is a block diagram schematically illustrating a seventeenth embodiment of the present invention.
FIG. 22 is a block diagram schematically illustrating an eighteenth embodiment of the present invention.
FIG. 23 is a block diagram schematically illustrating a nineteenth embodiment of the present invention.
FIG. 24 is a block diagram schematically illustrating a twentieth embodiment of the present invention.
FIG. 25 is a block diagram schematically illustrating a twenty-first embodiment of the present invention.
FIG. 26 is a block diagram schematically illustrating a twenty-first embodiment of the present invention.
FIG. 27 is a block diagram schematically illustrating a twenty-second embodiment of the present invention.
FIG. 28 is a block diagram schematically illustrating an example of a conventional absorption chiller / heater.
FIG. 29 is a block diagram schematically illustrating another conventional technique.
[Explanation of symbols]
20 ... Absorption type water heater
22 ... Absorber
24, 32 ... Pump
26 ... Low temperature solution heat exchanger
30 ... Waste heat regenerator
L1, L1-1, L1-2, L1-22, L1-23, L3, L4, L5, L6, L6-1, L6-2, L8, L22 ... Solution line
L1A: Solution line area
L5, L11, L11-D, L13, L15, L17, L17L, L17H, L52, L70 ... Refrigerant line
CL-1, CL-2, CL-3, CL-V1, CL-V2 ... Signal transmission line 42 ... High temperature solution heat exchanger
44 ... High temperature regenerator
48 ... Low temperature regenerator
50 ... Condenser
52 ... Evaporator
70 ... Refrigerant drain heat exchanger
74 ... Solution cooling absorber
76 ... Heat exchanger for high-quality fuel exhaust heat input
80 ... Heat exchanger for exhaust heat input
V1, V2 three-way valve
VE: Three-way valve for exhaust heat input
100, 120 ... three-way valve drive means
S1, S2, S3 ... Sensor
150 ... Driving means

Claims

In an absorption chiller / heater having an absorber, a high-temperature regenerator, a low-temperature regenerator, a waste heat trap regenerator, a condenser, and an evaporator, the rare solution sent from the absorber flows through. The line is branched at a first branch point into a first branch line in which a low-temperature solution heat exchanger is interposed and a second branch line in which a refrigerant drain heat exchanger is interposed. The region between the low-temperature regenerator and the condenser in the line through which the refrigerant vapor regenerated by the high-temperature regenerator flows is in thermal communication with the refrigerant drain heat exchanger, and the refrigerant after passing through the low-temperature regenerator holds The enthalpy is injected into the dilute solution flowing through the second branch line, and is in thermal communication with the three-way valve interposed at the first branch point and the exhaust heat regenerator. It is installed at the junction or junction of the exhaust heat line and the line communicating with the exhaust heat source. A heat input three-way valve, an open / close sensor that detects whether the exhaust heat input three-way valve opens or closes the exhaust heat line L2, and controls the opening / closing of the three-way valve by a detection signal of the open / close sensor A control means, and if the three-way valve for exhaust heat input opens the exhaust heat line side, the control means passes through the first branch line communicating with the exhaust heat soot regenerator. If the exhaust heat input three-way valve closes the exhaust heat line side, the flow rate of the rare solution flowing through the first branch line communicating with the exhaust heat soot regenerator is increased. The absorption chiller / heater is configured to perform control to reduce the amount by a predetermined amount.

In an absorption chiller / heater having an absorber, a high-temperature regenerator, a low-temperature regenerator, a waste heat trap regenerator, a condenser, and an evaporator, the rare solution sent from the absorber flows through. The line is branched at a first branch point into a first branch line in which a low-temperature solution heat exchanger is interposed and a second branch line in which a refrigerant drain heat exchanger is interposed. The region between the low-temperature regenerator and the condenser in the line through which the refrigerant vapor regenerated by the high-temperature regenerator flows is in thermal communication with the refrigerant drain heat exchanger, and the refrigerant after passing through the low-temperature regenerator holds The enthalpy is injected into the dilute solution flowing through the second branch line, and is in thermal communication with the three-way valve interposed at the first branch point and the exhaust heat regenerator. A temperature sensor for detecting the temperature of the fluid flowing through the exhaust heat line, and a detection signal of the temperature sensor; And a control means for controlling opening and closing of the three-way valve, and when the temperature of the fluid flowing through the exhaust heat line rises, the control means flows through the first branch line communicating with the exhaust heat soot regenerator. When the flow rate of the dilute solution is increased and the temperature of the fluid flowing on the exhaust heat line side decreases, the flow rate of the dilute solution flowing through the first branch line communicating with the exhaust heat soot regenerator is reduced. Absorption chiller / heater characterized in that it is configured to.

In an absorption chiller / heater having an absorber, a high-temperature regenerator, a low-temperature regenerator, a waste heat trap regenerator, a condenser, and an evaporator, the rare solution sent from the absorber flows through. The line is branched at a first branch point into a first branch line in which a low-temperature solution heat exchanger is interposed and a second branch line in which a refrigerant drain heat exchanger is interposed. The region between the low-temperature regenerator and the condenser in the line through which the refrigerant vapor regenerated by the high-temperature regenerator flows is in thermal communication with the refrigerant drain heat exchanger, and the refrigerant after passing through the low-temperature regenerator holds The enthalpy is applied to the dilute solution flowing through the second branch line, and the temperature of the absorbing solution at the outlet of the absorber is detected by the three-way valve interposed at the first branch point. And the three-way valve is opened by the detection signal of the temperature sensor. Control means for controlling, and if the temperature of the absorbent solution at the outlet of the absorber rises, the control means reduces the flow rate of the rare solution flowing through the first branch line communicating with the exhaust heat soot regenerator When the temperature of the absorbing solution at the outlet of the absorber is lowered, control is performed so as to increase the flow rate of the rare solution flowing through the first branch line communicating with the exhaust heat regenerator. Absorption chiller / heater characterized by

The first branch line passes through the low temperature solution heat exchanger and then communicates with the exhaust heat soot regenerator without joining the second branch line, and is directed from the exhaust heat soot regenerator to the high temperature regenerator. The line joins the second branch line at the first junction between the exhaust heat regenerator and the high temperature solution heat exchanger and communicates with the high temperature regenerator, and the absorption solution heated by the high temperature regenerator is The intermediate concentration solution line flows into the low temperature regenerator, is heated by the low temperature regenerator, and then flows through the high concentration solution line and returns to the absorber via the low temperature solution heat exchanger. The absorption cold / hot water machine of any one of claim | item 1-3.

The first branch line passes through the low temperature solution heat exchanger and then communicates with the exhaust heat soot regenerator without joining the second branch line, and is directed from the exhaust heat soot regenerator to the high temperature regenerator. The line joins the second branch line at the first junction between the high temperature solution heat exchanger and the high temperature regenerator, communicates with the high temperature regenerator, and the absorbing solution heated by the high temperature regenerator has an intermediate concentration. A flow through a solution line, into a low-temperature regenerator, heated in a low-temperature regenerator, then flowed through a high-concentration solution line, and returned to an absorber via a low-temperature solution heat exchanger. 4. The absorption chiller / heater according to any one of 3 above.

The first and second branch lines join at the first junction immediately after passing through the low temperature solution heat exchanger or the refrigerant drain heat exchanger, and communicate with the high temperature regenerator at the second branch point. A dilute solution that branches to a line that communicates with the exhaust heat soot regenerator and flows through the line that communicates with the high temperature regenerator flows into the high temperature regenerator via the high temperature solution heat exchanger and communicates with the exhaust heat soot regenerator. The dilute solution flowing through is heated by the waste heat regenerator and flows into the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows joins the solution line from the high temperature regenerator and the second junction. Any one of claims 1-3, wherein the three-way valve is connected not to the first branch point but to the second branch point through a low-temperature solution heat exchanger. Absorption chiller / heater of item 1.

The first branch line does not merge with the second branch line after passing through the low-temperature solution heat exchanger, and is connected to a line communicating with the high-temperature regenerator at the second branch point and the exhaust heat regenerator. The dilute solution that branches to the communicating line and flows through the line communicating with the high temperature regenerator flows into the high temperature regenerator via the high temperature solution heat exchanger, and the line communicating with the exhaust heat regenerator is the first junction. The rare solution flowing through the second branch line is heated by the exhaust heat regenerator and flows into the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows is the high temperature regenerator. From the solution line to the second junction, communicates with the absorber via the low-temperature solution heat exchanger, and instead of the three-way valve interposed at the first branch point, The absorption cold / hot water of any one of Claims 1-3 which has provided the three-way valve intervened in the branch point of .

The first branch line does not merge with the second branch line after passing through the low-temperature solution heat exchanger, and is connected to a line communicating with the high-temperature regenerator at the second branch point and the exhaust heat regenerator. The dilute solution that branches to the communicating line and flows through the line communicating with the high temperature regenerator flows into the high temperature regenerator via the high temperature solution heat exchanger, and the line communicating with the exhaust heat regenerator is the first junction. The rare solution flowing through the second branch line is heated by the exhaust heat regenerator and flows into the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows is the high temperature regenerator. The absorption chiller / heater according to any one of claims 1 to 3, which joins at a second merging point with a solution line from the chiller and communicates with an absorber via a low-temperature solution heat exchanger.

The first branch line does not merge with the second branch line after passing through the low-temperature solution heat exchanger, and is connected to a line communicating with the high-temperature regenerator at the second branch point and the exhaust heat regenerator. The line that branches into the communicating line and communicates with the high temperature regenerator joins the second branch line at the first junction between the second branch point and the high temperature solution heat exchanger and communicates with the high temperature regenerator. However, the dilute solution flowing through the line communicating with the exhaust heat regenerator is heated by the exhaust heat regenerator and flows into the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows is from the high temperature regenerator. It joins at the solution line and the second junction, communicates with the absorber via the low-temperature solution heat exchanger, and instead of the three-way valve interposed at the first branch point, the second branch The absorption chiller-heater according to any one of claims 1 to 3, further comprising a three-way valve interposed at a point.

The first branch line does not merge with the second branch line after passing through the low-temperature solution heat exchanger, and is connected to a line communicating with the high-temperature regenerator at the second branch point and the exhaust heat regenerator. The line that branches into the communicating line and communicates with the high temperature regenerator joins the second branch line at the first junction between the second branch point and the high temperature solution heat exchanger and communicates with the high temperature regenerator. However, the dilute solution flowing through the line communicating with the exhaust heat regenerator is heated by the exhaust heat regenerator and flows into the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows is from the high temperature regenerator. The absorption chiller / heater according to any one of claims 1 to 3, wherein the absorption chiller / heater joins at the solution line and the second merging point and communicates with the absorber via a low-temperature solution heat exchanger.

The first branch line does not merge with the second branch line after passing through the low-temperature solution heat exchanger, and is connected to a line communicating with the high-temperature regenerator at the second branch point and the exhaust heat regenerator. Branching into a communicating line, the line communicating with the high temperature regenerator joins the second branch line at the first junction between the high temperature solution heat exchanger and the high temperature regenerator and communicates with the high temperature regenerator, The dilute solution flowing through the line communicating with the exhaust heat soot regenerator is heated by the exhaust heat soot regenerator and flows into the low temperature regenerator. The line through which the absorption solution heated by the low temperature regenerator flows is the solution line from the high temperature regenerator. At the second junction, and communicates with the absorber via a low-temperature solution heat exchanger. Instead of the three-way valve interposed at the first junction, the second junction The absorption chiller / heater according to any one of claims 1 to 3, further comprising an interposed three-way valve.

The first branch line does not merge with the second branch line after passing through the low-temperature solution heat exchanger, and is connected to a line communicating with the high-temperature regenerator at the second branch point and the exhaust heat regenerator. Branching into a communicating line, the line communicating with the high temperature regenerator joins the second branch line at the first junction between the high temperature solution heat exchanger and the high temperature regenerator and communicates with the high temperature regenerator, The dilute solution flowing through the line communicating with the exhaust heat soot regenerator is heated by the exhaust heat soot regenerator and flows into the low temperature regenerator. The line through which the absorption solution heated by the low temperature regenerator flows is the solution line from the high temperature regenerator. The absorption chiller / heater according to any one of claims 1 to 3, wherein the chiller and the second merging point are joined to each other and communicated with the absorber via a low-temperature solution heat exchanger.

The first branch line passes through the low-temperature solution heat exchanger and then does not merge with the second branch line, communicates with the exhaust heat soot regenerator, and the absorbed solution heated by the exhaust heat soot regenerator The flowing line branches into a line communicating with the high temperature regenerator and a line communicating with the low temperature regenerator at the second branch point, and the rare solution flowing through the line communicating with the high temperature regenerator passes through the high temperature solution heat exchanger. The line that flows into the high temperature regenerator and communicates with the low temperature regenerator joins the second branch line at the first junction, and the dilute solution flowing through the line flows into the low temperature regenerator and is heated for low temperature regeneration. The line through which the absorption solution heated by the vessel flows joins the solution line from the high-temperature regenerator at the second junction, and communicates with the absorber via the low-temperature solution heat exchanger. The absorption cold / hot water machine of item 1.

The first branch line passes through the low-temperature solution heat exchanger and then does not merge with the second branch line, communicates with the exhaust heat soot regenerator, and the absorbed solution heated by the exhaust heat soot regenerator The flowing line branches into a line communicating with the high temperature regenerator and a line communicating with the low temperature regenerator at the second branch point, and the line communicating with the high temperature regenerator is connected to the second branch point and the high temperature solution heat exchanger. The dilute solution that flows through the line that joins the second branch line at the first junction in between and communicates with the high temperature regenerator and that communicates with the low temperature regenerator flows into the low temperature regenerator and is heated. The line through which the absorption solution heated in step flows joins with the solution line from the high-temperature regenerator at the second junction, and communicates with the absorber via the low-temperature solution heat exchanger. Absorption chiller / heater of item 1.

The first branch line passes through the low-temperature solution heat exchanger and then does not merge with the second branch line, communicates with the exhaust heat soot regenerator, and the absorbed solution heated by the exhaust heat soot regenerator The flowing line branches into a line communicating with the high temperature regenerator and a line communicating with the low temperature regenerator at the second branch point, and the line communicating with the high temperature regenerator is between the high temperature solution heat exchanger and the high temperature regenerator. The dilute solution that joins the second branch line at the first junction and communicates with the high-temperature regenerator and flows through the line that communicates with the low-temperature regenerator flows into the low-temperature regenerator and is heated and heated by the low-temperature regenerator. The line through which the absorbed solution flows joins the solution line from the high-temperature regenerator at the second junction, and communicates with the absorber via the low-temperature solution heat exchanger. Absorption cold and hot water machine.

The first branch line passes through the low-temperature solution heat exchanger and then does not merge with the second branch line, communicates with the exhaust heat soot regenerator, and the absorption solution heated by the exhaust heat soot regenerator The flowing line communicates with the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows joins the second branch line at the first junction between the low temperature regenerator and the high temperature solution heat exchanger. The absorption chiller / heater according to any one of claims 1 to 3, wherein the absorbing solution heated to the high temperature regenerator is returned to the absorber.

The first branch line passes through the low-temperature solution heat exchanger and then does not merge with the second branch line, communicates with the exhaust heat soot regenerator, and the absorbed solution heated by the exhaust heat soot regenerator The flowing line communicates with the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows joins the second branch line at the first junction between the high temperature solution heat exchanger and the high temperature regenerator. The absorption chiller / heater according to any one of claims 1 to 3, wherein the absorbing solution heated to the high temperature regenerator is returned to the absorber (22).

The first branch line passes through the low-temperature solution heat exchanger and then does not merge with the second branch line, communicates with the exhaust heat soot regenerator, and the absorbed solution heated by the exhaust heat soot regenerator The flowing line merges with the second branch line at the first junction and communicates with the low temperature regenerator, and the line through which the absorption solution heated by the low temperature regenerator flows communicates with the high temperature regenerator. The absorption chiller / heater according to any one of claims 1 to 3, wherein the absorption solution heated in step 1 is returned to the absorber.

The rare solution line, which includes an absorber, a high temperature regenerator, a low temperature regenerator, a waste heat trap regenerator, a condenser, and an evaporator, through which the rare solution sent from the absorber flows, 1 is branched into a first branch line in which a low-temperature solution heat exchanger is interposed and a second branch line in which a refrigerant drain heat exchanger is interposed. The region between the low-temperature regenerator and the condenser in the line through which the refrigerant vapor regenerated in the flow flows is in thermal communication with the refrigerant drain heat exchanger, and the enthalpy possessed by the refrigerant after passing through the low-temperature regenerator is A three-way valve interposed at the first branch point, and a waste heat line in thermal communication with the waste heat trap regenerator, configured to be poured into a dilute solution flowing through the second branch line A three-way valve for exhaust heat input interposed at a branch point or junction with the line communicating with the exhaust heat source, Absorption chiller / heater having an open / close sensor for detecting whether the heat input three-way valve opens or closes the exhaust heat line L2 side, and a control means for controlling the open / close of the three-way valve by a detection signal of the open / close sensor In the control method, the open / close sensor detects whether the exhaust heat input three-way valve opens or closes the exhaust heat line side, and the exhaust heat input three-way valve opens the exhaust heat line side. If so, the flow rate of the dilute solution flowing through the first branch line communicating with the exhaust heat regenerator is increased by a predetermined amount, and the exhaust heat input three-way valve closes the exhaust heat line side. If it is, the control method of the absorption cold / hot water machine characterized by including the process of reducing only the predetermined amount the flow volume of the dilute solution which flows through the 1st branch line connected to an exhaust-heat-steam regenerator.

The rare solution line, which includes an absorber, a high temperature regenerator, a low temperature regenerator, a waste heat trap regenerator, a condenser, and an evaporator, through which the rare solution sent from the absorber flows, 1 is branched into a first branch line in which a low-temperature solution heat exchanger is interposed and a second branch line in which a refrigerant drain heat exchanger is interposed. The region between the low-temperature regenerator and the condenser in the line through which the refrigerant vapor regenerated in the flow flows is in thermal communication with the refrigerant drain heat exchanger, and the enthalpy possessed by the refrigerant after passing through the low-temperature regenerator is A three-way valve interposed at the first branch point and a waste heat line that is in thermal communication with the waste heat regenerator are configured to be poured into a dilute solution flowing through the second branch line. A temperature sensor for detecting the temperature of the flowing fluid, and the three-way valve is opened by a detection signal of the temperature sensor. In the control method of the absorption chiller / heater having control means for controlling, if the temperature of the fluid flowing through the exhaust heat line is detected by the temperature sensor and the temperature of the fluid flowing through the exhaust heat line rises, the exhaust heat If the flow rate of the dilute solution flowing through the first branch line communicating with the soot regenerator is increased and the temperature of the fluid flowing through the exhaust heat line decreases, the first branch line communicating with the exhaust heat soot regenerator And a step of reducing the flow rate of the dilute solution flowing through the absorption chiller / heater.

The rare solution line, which includes an absorber, a high temperature regenerator, a low temperature regenerator, a waste heat trap regenerator, a condenser, and an evaporator, through which the rare solution sent from the absorber flows, 1 is branched into a first branch line in which a low-temperature solution heat exchanger is interposed and a second branch line in which a refrigerant drain heat exchanger is interposed. The region between the low-temperature regenerator and the condenser in the line through which the refrigerant vapor regenerated in the flow flows is in thermal communication with the refrigerant drain heat exchanger, and the enthalpy possessed by the refrigerant after passing through the low-temperature regenerator is A three-way valve interposed at the first branch point; a temperature sensor for detecting the temperature of the absorbent solution at the outlet of the absorber; and a temperature sensor configured to be poured into a dilute solution flowing through the second branch line And a control means for controlling opening and closing of the three-way valve according to a detection signal of the temperature sensor. In the control method of the absorption chiller / heater, the step of measuring the temperature of the absorbing solution at the outlet of the absorber by the temperature sensor, and the temperature of the absorbing solution at the outlet of the absorber rises, communicate with the exhaust heat regenerator If the flow rate of the dilute solution flowing through the first branch line is decreased and the temperature of the absorbent solution at the outlet of the absorber is decreased, the rare solution flowing through the first branch line communicating with the exhaust heat regenerator And a method of increasing the flow rate of the solution.