JP3791831B2 - Steam fired absorption chiller / heater - Google Patents

Steam fired absorption chiller / heater Download PDF

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JP3791831B2
JP3791831B2 JP2001090591A JP2001090591A JP3791831B2 JP 3791831 B2 JP3791831 B2 JP 3791831B2 JP 2001090591 A JP2001090591 A JP 2001090591A JP 2001090591 A JP2001090591 A JP 2001090591A JP 3791831 B2 JP3791831 B2 JP 3791831B2
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heat exchanger
temperature regenerator
line
high temperature
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JP2002286320A (en
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部 尚 樹 刑
前 和 則 松
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Tokyo Gas Co Ltd
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P80/00—Climate change mitigation technologies for sector-wide applications
    • Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
    • Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply

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Description

【０００１】
【発明の属する技術分野】
本発明は、吸収冷温水機に関し、特に、高温再生器、中温再生器、低温再生器を有する３重効用蒸気焚き吸収冷温水機に関する。
【０００２】
【従来の技術】
図９に典型的な一例を示す従来の３重効用蒸気焚き吸収冷温水機Ｊ１は、高温再生器２０２と、中温再生器２０４と、低温再生器２０６と、吸収器２０８と、凝縮器２１０と、蒸発器２１２とを有している。そして、高温再生器２０２には加熱源である蒸気が流過する加熱用蒸気ライン２１４が連通し、加熱用蒸気が保有する熱量が高温再生器２０２内の吸収溶液に投入されて冷媒蒸気が発生（再生）する。
【０００３】
高温再生器２０２で発生した蒸気は、蒸気ライン（第１の蒸気ライン）２１６を流れて、中温再生器２０４内の吸収溶液に対して、保有する熱量を投入する。これにより、中温再生器２０４で冷媒蒸気が発生（再生）する。
中温再生器２０４で発生した蒸気は、第２の冷媒蒸気ライン２１８を流れて、低温再生器２０６内の吸収溶液に対して、その保有する熱量を投入し、以って、低温再生器２０６から冷媒蒸気を発生せしめている。
【０００４】
従来の３重効用蒸気焚き吸収冷温水機Ｊ１では、高温再生器２０２で熱交換後の蒸気（蒸気ドレン）は、加熱用蒸気ライン２１４Ａを介してそのまま、系外へ排出される。加熱用蒸気ライン２１４Ａ内の蒸気ドレンは、未だに或程度の熱量を保有しているが、その熱量を保有したまま系外に排出されており、不経済でもったいない。
【０００５】
しかし、従来の３重効用蒸気焚き吸収冷温水機Ｊ１では、蒸気ドレンが保有している熱量の有効利用については、全く考えられていなかった。。
【０００６】
【発明が解決しようとする課題】
本発明は上述したような従来技術の問題点に鑑みて提案されたものであり、蒸気ドレンが保有している熱量の有効利用することが出来る３重効用蒸気焚き吸収冷温水機の提供を目的としている。
【０００７】
【課題を解決するための手段】
本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、吸収器（２０８）から出た吸収溶液が、高温再生器（２０２）、中温再生器（２０４）、低温再生器（２０６）の順に流過する様に構成され、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）に向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（１０６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（１０８）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第７の蒸気ドレン熱交換器（２２０、２２２、２２４、２２６、２２８、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２４）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と第１の分岐点（２４６Ｂ）との間の領域（２４６）に介装され、
第４の蒸気ドレン熱交換器（２２６）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第３の蒸気ドレン熱交換器（２２４）の間の第２の合流点（２４２Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第５の蒸気ドレン熱交換器（２２８）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と第２の分岐点（２４０Ｂ）との間の領域（２４０）に介装され、
第６の蒸気ドレン熱交換器（２３０）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２３４Ｂ）で分岐する第３の分岐ライン（２３８）に介装されており、該第３の分岐ライン（２３８）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第５の蒸気ドレン熱交換器（２２８）の間の第３の合流点（２３６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第７の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２３４Ｂ）との間の領域（２３５）に介装されており、
第１〜第７の蒸気ドレン熱交換器（２２０、２２２、２２４、２２６、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項１：図１）。
【０００８】
また、本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、吸収器（２０８）から出た吸収溶液が、高温再生器（２０２）、中温再生器（２０４）、低温再生器（２０６）の順に流過する様に構成され、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）に向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（１０６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（１０８）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１の蒸気ドレン熱交換器（２２０）と、第２の蒸気ドレン熱交換器（２３２）と、第３の蒸気ドレン熱交換器（２２５）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域に介装されており、
第３の蒸気ドレン熱交換器（２２５）は、高温再生器（２０２）に向う吸収溶液ラインの第７の蒸気ドレン熱交換器（２３２）と低温溶液熱交換器（３００）の間における分岐点（２３４Ｂ）で分岐する分岐ライン（２３６Ｑ）に介装されており、該分岐ライン（２３６Ｑ）は低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第１の蒸気ドレン熱交換器（２２０）と第２の蒸気ドレン熱交換器（２３２）と第３の蒸気ドレン熱交換器（２２５）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項２：図２）。
【０００９】
そして、本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、吸収器（２０８）から出た吸収溶液が、低温再生器（２０６）、中温再生器（２０４）、高温再生器（２０２）の順に流過する様に構成されており、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ライン（２３６）には低温溶液熱交換器（３００）が介装され、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（２４２）には中温溶液熱交換器（３０２）が介装され、中温溶液熱交換器（３０２）から高温再生器（２０２）に向う吸収溶液ライン（２４８）には高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）から吸収器（２０８）に向う吸収溶液ライン（１１０）を流れる吸収溶液が保有する熱量を投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの中温再生器（２０４）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２４Ａ）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの中温再生器（２０４）と第１の分岐点（２４６Ｂ）との間の領域（３８６）に介装され、
第４の蒸気ドレン熱交換器（２２４Ｂ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（３８４）の中温溶液熱交換器（３０２）と中温再生器（２０４）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの低温再生器（２０６）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４Ｂ）の間の第２の合流点（２４２Ｇ）で低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２８Ａ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの低温再生器（２０６）と第２の分岐点（２４０Ｂ）との間の領域（３８４）に介装され、
第７の蒸気ドレン熱交換器（２２８Ｂ）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの低温溶液熱交換器（３００）と低温再生器（２０６）との間の領域（３８２）に介装され、
第８の蒸気ドレン熱交換器（２３０）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２３４Ｂ）で分岐する第３の分岐ライン（２３８）に介装されており、該第３の分岐ライン（２３８）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８Ｂ）の間の第３の合流点（２３６Ｇ）で吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２３４Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項３：図３）。
【００１０】
さらに、本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）を出た吸収溶液が低温再生器（２０６）、中温再生器（２０４）、高温再生器（２０２）の順に流過する様に構成され且つ高温再生器（２０２）と吸収器（２０８）とを連通する吸収溶液ライン（２６０）を有し、低温再生器（２０６）と中温再生器（２０４）とを連通する吸収溶液ライン（２６２）から分岐（２６４）し且つ高温再生器（２０２）と吸収器（２０８）とを連通する前記吸収溶液ライン（２６０）と合流（２６６）する第１の分岐吸収溶液ライン（２６８）を有し、中温再生器（２０４）と高温再生器（２０２）とを連通する吸収溶液ライン（２７０）から分岐（２７２）し且つ高温再生器（２０２）と吸収器（２０８）とを連通する前記吸収溶液ライン（２６０）と合流（２７４）する第２の分岐吸収溶液ライン（２７６）を有し、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ライン（２３６）には低温溶液熱交換器（３００）が介装され、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（２４２）には中温溶液熱交換器（３０２）が介装され、中温溶液熱交換器（３０２）から高温再生器（２０２）に向う吸収溶液ライン（２４８）には高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）から吸収器（２０８）に向う吸収溶液ライン（１１０）を流れる吸収溶液が保有する熱量を投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（２７６）の分岐部（２７２）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２４）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（２７６）の分岐部（２７２）と第１の分岐点（２４６Ｂ）との間の領域に介装され、
第４の蒸気ドレン熱交換器（２２４Ｂ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（３８４）の中温溶液熱交換器（３０２）と中温再生器（２０４）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（２６８）の分岐部（２６４）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４Ｂ）の間の第２の合流点（２４２Ｇ）で低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２８Ａ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（２６８）の分岐部（２６４）と第２の分岐点（２４０Ｂ）との間の領域に介装され、
第７の蒸気ドレン熱交換器（２２８Ｂ）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの低温溶液熱交換器（３００）と低温再生器（２０６）との間の領域（３８２）に介装され、
第８の蒸気ドレン熱交換器（２３０）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２３４Ｂ）で分岐する第３の分岐ライン（２３８）に介装されており、該第３の分岐ライン（２３８）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８Ｂ）の間の第３の合流点（２３６Ｇ）で吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２３４Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項４：図４）。
【００１１】
或いは、本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から出た吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（３１４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（３１６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８４、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）から吸収器（２０８）に向かう吸収溶液ライン（３１２、３１４、３１６）には、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ライン（３１８）が合流（３２０）しており、且つ、低温再生器（２０６）で加熱された吸収溶液が流れる吸収溶液ライン（３２２）が合流（３２４）しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２３Ａ）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と第１の分岐点（２４６Ｂ）との間の領域（２８６）に介装され、
第４の蒸気ドレン熱交換器（２２４）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４）の間の第２の合流点（２４２Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２７）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と第２の分岐点（２４０Ｂ）との間の領域（２８４）に介装され、
第７の蒸気ドレン熱交換器（２２８）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）との間の領域に介装され、
第８の蒸気ドレン熱交換器（２３０）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２８２Ｂ）で分岐する第３の分岐ライン（２８３）に介装されており、該第３の分岐ライン（２８３）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８）の間の第３の合流点（２８３Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２８２Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項５：図５）。
【００１２】
本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から出た吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（３１４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（３１６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８４、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）から吸収器（２０８）に向かう吸収溶液ライン（３１２、３１４、３１６）には、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ライン（３１８）が合流（３２０）しており、且つ、低温再生器（２０６）で加熱された吸収溶液が流れる吸収溶液ライン（３２２）が合流（３２４）しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域（２８２）に介装されており、
第３の蒸気ドレン熱交換器（２２７Ｃ）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域（２８２）における分岐点（２８２Ｂ）で分岐する分岐ライン（２５１Ｓ）に介装されており、該分岐ライン（２５１Ｓ）は低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の合流点（２８７Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項６：図６）。
【００１３】
また、本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）へ向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（３１８）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（３２２）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）で加熱された吸収溶液が流れる吸収溶液ライン（３４０）は中温再生器（２０４）に連通しており、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ライン（３１８）は第１の分岐吸収溶液ライン（３０６）に合流して低温再生器（２０６）に連通しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２３Ａ）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と第１の分岐点（２４６Ｂ）との間の領域（２８６）に介装され、
第４の蒸気ドレン熱交換器（２２４）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４）の間の第２の合流点（２４２Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２７）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と第２の分岐点（２４０Ｂ）との間の領域に介装され、
第７の蒸気ドレン熱交換器（２２８）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）との間の領域に介装され、
第８の蒸気ドレン熱交換器（２３０）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２８２Ｂ）で分岐する第３の分岐ライン（２８３）に介装されており、該第３の分岐ライン（２８３）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８）の間の第３の合流点（２８３Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２８２Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項７：図７）。
【００１４】
そして本発明の蒸気焚き吸収冷温水機は、高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）へ向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ラインを流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ラインを流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）で加熱された吸収溶液が流れる吸収溶液ライン（３４０）は中温再生器（２０４）に連通しており、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ラインは第１の分岐吸収溶液ライン（３０６）に合流して低温再生器（２０６）に連通しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域に介装されており、
第３の蒸気ドレン熱交換器（２２７Ｃ）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域における分岐点（２８２Ｂ）で分岐する分岐ライン（２５１Ｓ）に介装されており、該分岐ライン（２５１Ｓ）は低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の合流点（２８７Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴としている（請求項８：図８）。
【００１５】
かかる構成を具備する本発明によれば、前記加熱用蒸気ライン（２１４、２１４Ａ）は高温再生器（２０２）に連通してから蒸気ドレン熱交換器（２２０、２２２、２２４、２２６、２２８、２３０、２３２）に連通しており、該蒸気ドレン熱交換器（２２０、２２２、２２４、２２６、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量が、吸収器（２０８）から出て再生器（２０２、２０４、２０６）に連通する吸収溶液ライン（２３４、２３８、２４０、２４４、２４６、２５０、２５２）を流過する吸収溶液（再生器に供給される吸収溶液）に投入される様に構成されている。
すなわち、従来技術では系外へ排出されていた蒸気ドレンが保有する熱量が、再生器（２０２、２０４、２０６）に向けて流れている吸収溶液（再生器に供給される吸収溶液）に投入されて、該吸収溶液の顕熱上昇に有効利用される。
【００１６】
そして、再生器（２０２、２０４、２０６）に供給される吸収溶液の液温が昇温する（顕熱上昇）結果として、再生器（２０２、２０４、２０６）で投入される熱量が同一であれば、冷媒蒸気（水蒸気）の再生量が増大し、吸収冷温水機の効率が向上するのである。
【００１７】
【発明の実施の形態】
以下、添付図面を参照して、本発明を３重効用蒸気焚き吸収冷温水機に適用した実施形態を説明する。なお、添付図面において、同様な部材には同様な符号を付して、部材名称と符号の重複説明を省略している。
【００１８】
図１は、第１の実施形態であるシリーズフロータイプ吸収冷温水機Ｓ１の構成を示している。
【００１９】
吸収器２０８と高温再生器２０２は、ポンプ１０２を介した吸収溶液ライン２３４で連通され、高温再生器２０２と中温再生器２０４とは吸収溶液ライン１０４と、第１の冷媒蒸気ライン２１６で連通されている。
第１の冷媒蒸気ライン２１６は、ライン内を通過する冷媒蒸気が保有する熱量が、中温再生器２０４内の吸収溶液に投入されて冷媒蒸気が再生されるよう構成されている。
【００２０】
中温再生器２０４と低温再生器２０６とは吸収溶液ライン１０６と第２の冷媒蒸気ライン２１８で連通されている。
第２の冷媒蒸気ライン２１８は、ライン内を通過する冷媒蒸気が保有する熱量が、低温再生器２０６内の吸収溶液に投入されて冷媒蒸気が再生されるよう構成されている。
【００２１】
低温再生器２０６と吸収器２０８は、吸収溶液ライン１０８で連通されている。
吸収溶液ライン１０４に高温溶液熱交換器３０４が介装され、吸収溶液ライン１０６に中温溶液熱交換器３０２が介装され、吸収溶液ライン１０８に低温溶液熱交換器３００が介装されている。
【００２２】
高温溶液熱交換器３０４、中温溶液熱交換器３０２及び低温溶液熱交換器３００は、いづれも吸収溶液ライン２３４と熱的に接触し、吸収溶液ライン２３４に伝熱させるよう構成されている。
【００２３】
高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン２１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する各蒸気ドレン熱交換器に接続されて蒸気供給源に戻るよう連通されている。
【００２４】
蒸気ドレン熱交換器２２０は、吸収溶液ライン２３４の高温溶液熱交換器３０４と高温再生器２０２との間の領域２５２に、ライン２１４Ａと熱的に接触して介装されている。
【００２５】
蒸気ドレン熱交換器２２２は、吸収溶液ライン２３４の高温溶液熱交換器３０４を分岐部２４６Ｂと合流部２４６Ｇでバイパスする領域２５０に、ライン２１４Ａと熱的に接触して介装されている。
【００２６】
蒸気ドレン熱交換器２２４は、吸収溶液ライン２３４の高温溶液熱交換器３０４と中温溶液熱交換器３０２との間の領域２４６に、ライン２１４Ａと熱的に接触して介装されている。
【００２７】
蒸気ドレン熱交換器２２６は、吸収溶液ライン２３４の中温溶液熱交換器３０２を分岐部２４０Ｂと合流部２４２Ｇでバイパスする領域２４４に、ライン２１４Ａと熱的に接触して介装されている。
【００２８】
蒸気ドレン熱交換器２２８は、吸収溶液ライン２３４の中温溶液熱交換器３０２と低温溶液熱交換器３００との間の領域２４０に、ライン２１４Ａと熱的に接触して介装されている。
【００２９】
蒸気ドレン熱交換器２３０は、吸収溶液ライン２３４の低温溶液熱交換器３００を分岐部２３４Ｂと合流部２３６Ｇでバイパスする領域２３８に、ライン２１４Ａと熱的に接触して介装されている。
【００３０】
蒸気ドレン熱交換器２３２は、吸収溶液ライン２３４の低温溶液熱交換器３００と吸収器２０８との間の領域２３５に、ライン２１４Ａと熱的に接触して介装されている。
【００３１】
上記各蒸気ドレン熱交換器２２０、２２２、２２４、２２６、２２８、２３０、２３２は、これらを経由するドレンの温度が、熱的に対となる吸収溶液ライン２３４の温度より高温であることが必要条件である。したがって、吸収冷温水機Ｓ１の温度状況、空調負荷、加熱蒸気の温度、外気条件等によって、各蒸気ドレン熱交換器２２０、２２２、２２４、２２６、２２８、２３０、２３２の何れか１つあるいは全数を含む何れか複数が介装されている。
【００３２】
上記吸収冷温水機Ｓ１の作用を、各蒸気ドレン熱交換器２２０、２２２、２２４、２２６、２２８、２３０、２３２の全てが介装されている例について説明する。
【００３３】
吸収器２０８からポンプ１０２で吸収溶液ライン２３４に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２３４Ｂで分岐して一方は領域２３８を通過して蒸気ドレン熱交換器２３０で加熱され昇温し、分岐部２３４で直行の他方の吸収溶液Ｌｉは低温溶液熱交換器３００を通過して加熱され昇温し、合流部２３６Ｇで合流する。
【００３４】
なお、分岐部２３４Ｂでの吸収溶液Ｌｉの分岐割合は、低温溶液熱交換器３００からの受熱と、蒸気ドレン熱交換器２３０からの受熱の合計熱量が最大となって合流部２３６Ｇでの吸収溶液Ｌｉ温度が最大になるように配分される。
【００３５】
合流部２３６Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２８を通過して加熱され昇温し、分岐部２４０Ｂで分岐して一方は領域２４４を通過して蒸気ドレン熱交換器２２６で加熱され昇温し、分岐部２４０Ｂで直行の他方の吸収溶液Ｌｉは中温溶液熱交換器３０２を通過して加熱され昇温し、合流部２４２Ｇで合流する。分岐部２４０Ｂでの吸収溶液Ｌｉの分岐割合は、分岐部２３４Ｂでの分岐と同じ要領である。
【００３６】
合流部２４２Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２４を通過して加熱され昇温し、分岐部２４６Ｂで分岐して一方は領域２５０を通過して蒸気ドレン熱交換器２２２で加熱され昇温し、分岐部２４６Ｂで直行の他方の吸収溶液Ｌｉは高温溶液熱交換器３０４を通過して加熱され昇温し、合流部２４６Ｇで合流する。分岐部２４６Ｂでの吸収溶液Ｌｉの分岐割合は、分岐部２３４Ｂでの分岐と同じ要領である。
【００３７】
合流部２４６Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０を通過して加熱され昇温し、高温再生器２０２に導入される。
【００３８】
冷媒溶液を含んだ稀釈吸収溶液Ｌｉは、高温再生器２０２で加熱用蒸気ライン２１４による蒸気Ｓｔにより加熱され、冷媒溶液を蒸気として分離され濃縮された濃縮吸収溶液Ｌｉは、吸収溶液ライン１０４によって高温溶液熱交換器３０４で放熱し中温再生器２０４に導入される。
【００３９】
濃縮吸収溶液Ｌｉは、中温再生器２０４で第１の冷媒蒸気ライン２１６からの冷媒蒸気によって加熱され、さらに冷媒溶液を蒸気として分離され濃縮された濃縮溶液Ｌｉは、吸収溶液ライン１０６に向かう。
吸収溶液ライン１０６に導かれた吸収溶液Ｌｉは、中温溶液熱交換器３０２で放熱し低温再生器２０６に導入される。
低温再生器２０６に導入された濃縮吸収溶液Ｌｉは冷媒溶液を蒸気として分離され一層濃縮されて、吸収溶液ライン１０８に導かれ低温溶液熱交換器３００で放熱し、吸収器２０８に戻る。
【００４０】
一方、高温再生器２０２で蒸発分離された冷媒ｈ２は、第１の冷媒蒸気ライン２１６を介して中温再生器２０４で放熱して濃縮吸収溶液Ｌｉをさらに加熱し、凝縮器２１０に向かう。また、中温再生器２０４で蒸発分離された冷媒ｈ３は、低温再生器２０６で放熱して濃縮吸収溶液Ｌｉを加熱し、第１の冷媒蒸気ライン２１６に合流して凝縮器２１０に向かう。
【００４１】
凝縮器２１０に導かれた冷媒ｈ２、ｈ３は、凝縮され、蒸発器２１２で蒸発して外部流体と熱交換する。また、吸収器２０８で冷媒が外部流体と熱交換する。
このようにして、加熱用蒸気ライン２１４を介した蒸気の熱量を余すところなく利用して吸収冷温水機Ｓ１の熱効率を向上させる。
【００４２】
図２は、第２の実施形態であるシリーズフロータイプの吸収冷温水機Ｓ４の構成を示している。図１の実施形態と異なる部分を主体に説明する。
高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン２１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する蒸気ドレン熱交換器に接続されて蒸気供給源に連通されている。
【００４３】
蒸気ドレン熱交換器２２５は、吸収溶液ライン２３４の蒸気ドレン熱交換器２２０と高温溶液熱交換器３０４との間と、低温溶液熱交換器３００と蒸気ドレン熱交換器２３２との間を、分岐部２３４Ｂと合流部２４６Ｇでバイパスする領域２３６Ｑに、ライン２１４Ａと熱的に接触して介装されている。
【００４４】
蒸気ドレン熱交換器２２５の前後に装着されている蒸気ドレン２３２と２２０への蒸気ドレン熱交換器２２５の連通関係は、実質的に前記図１の実施形態と同じである。即ち、図１における蒸気ドレン熱交換器２３０、２２８、２２６、２２２に代えて、蒸気ドレン熱交換器２２５を介装した状態である。
上記を除いては、前記図１の構成と同じである。
【００４５】
上記吸収冷温水機Ｓ４の作用を、蒸気ドレン熱交換器２２５が介装されている周辺を主体にして説明する。
吸収器２０８からポンプ１０２で吸収溶液ライン２３４に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２３４Ｂで分岐して、一方は領域２３６Ｑを通過して蒸気ドレン熱交換器２２５で加熱され昇温し、分岐部２３４Ｂで直行の他方の吸収溶液Ｌｉは低温溶液熱交換器３００、中低温溶液熱交換器３０２及び高温溶液熱交換器３０４を通過して加熱され昇温し、合流部２４６Ｇで合流する。
【００４６】
合流部２４６Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０を通過して加熱され昇温して高温再生器２０２方向に向かう。
上記のようにして、吸収冷温水器の配熱特性に応じて、蒸気ドレン熱交換器の個数を少数にして、かつ熱効率を向上させる。
【００４７】
図３は、第３の実施形態であるリバースフロータイプの吸収冷温水機ＲＳ５の構成を示している。図１の実施形態と異なる部分を主体に説明する。
稀釈吸収溶液の往路を構成する吸収器２０８と低温再生器２０６は、ポンプ１０２を介した吸収溶液ライン２３４、２３５、２３６、３８２で連通され、低温再生器２０６と中温再生器２０４とは吸収溶液ライン３８４、２４２、３８４で連通され、中温再生器２０４と高温再生器２０２とは吸収溶液ライン３８６、２４８、２５２でで連通されている。
【００４８】
濃縮吸収溶液の復路を構成する高温再生器２０２と吸収器２０８は、吸収溶液ライン１１０で連通されている。
吸収溶液ライン１１０には高温再生器２０２側から高温溶液熱交換器３０４、中温溶液熱交換器３０２、低温溶液熱交換器３００が介装されている。
【００４９】
吸収溶液ライン３８６と２５２間の領域２４８は、高温溶液熱交換器３０４を貫通して熱的に接触されている。領域２４８に、分岐部２４６Ｂと合流部２４６Ｇで高温溶液熱交換器３０４をバイパスする領域２５０が連通されている。
【００５０】
吸収溶液ライン３８４の中間部領域２４２は、中温溶液熱交換器３０２を貫通して熱的に接触されている。領域２４２に、分岐部２４０Ｂと合流部２４２Ｇで中温溶液熱交換器３０２をバイパスする領域２４４が連通されている。
【００５１】
吸収溶液ライン２３４と３８２の中間部領域２３６は、低温溶液熱交換器３００を貫通して熱的に接触されている。領域２３６に、分岐部２３４Ｂと合流部２３６Ｇで低温溶液熱交換器３００をバイパスする領域２３８が連通されている。
【００５２】
高温溶液熱交換器３０４、中温溶液熱交換器３０２及び低温溶液熱交換器３００は、それぞれ濃縮吸収溶液から稀釈吸収溶液に熱的に接触し、稀釈吸収溶液に伝熱させるよう構成されている。
【００５３】
高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン３１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する各蒸気ドレン熱交換器に接続されて蒸気供給源に連通されている。
【００５４】
蒸気ドレン熱交換器２２０は、高温溶液熱交換器３０４と高温再生器２０２との間の領域２５２に、ライン２１４Ａと熱的に接触して介装されている。
【００５５】
蒸気ドレン熱交換器２２２は、高温溶液熱交換器３０４をバイパスする領域２５０に、ライン２１４Ａと熱的に接触して介装されている。
蒸気ドレン熱交換器２２４Ａは、高温溶液熱交換器３０４と中温再生器２０４との間の領域３８６に、ライン２１４Ａと熱的に接触して介装されている。
【００５６】
蒸気ドレン熱交換器２２４Ｂは、中温再生器２０４と中温溶液熱交換器３０２との間の領域３８４に、ライン２１４Ａと熱的に接触して介装されている。
【００５７】
蒸気ドレン熱交換器２２６は、中温溶液熱交換器３０２をバイパスする領域２４４に、ライン２１４Ａと熱的に接触して介装されている。
【００５８】
蒸気ドレン熱交換器２２８Ａは、中温溶液熱交換器３０２と低温再生器２０６との間の領域３８４に、ライン２１４Ａと熱的に接触して介装されている。
【００５９】
蒸気ドレン熱交換器２２８Ｂは、低温再生器２０６と低温溶液熱交換器３００との間の領域３８２に、ライン２１４Ａと熱的に接触して介装されている。
蒸気ドレン熱交換器２３０は、低温溶液熱交換器３００をバイパスする領域２３８に、ライン２１４Ａと熱的に接触して介装されている。
【００６０】
蒸気ドレン熱交換器２３２は、吸収器２０８と低温溶液熱交換器３００との間の領域２３５に、ライン２１４Ａと熱的に接触して介装されている。
【００６１】
上記各蒸気ドレン熱交換器２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２は、これらを経由するドレンの温度が、熱的に対となる吸収溶液の温度より高温であることが必要条件である。したがって、吸収冷温水機ＲＳ５の温度状況、空調負荷、加熱蒸気の温度、外気条件等によって、各蒸気ドレン熱交換器２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２の何れか１つあるいは全数を含む何れか複数が介装されている。
上記以外の冷媒蒸気ライン等は、図１と同じである。
【００６２】
上記吸収冷温水機ＲＳ５の作用を、各蒸気ドレン熱交換器２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２の全てが介装されている例について説明する。
【００６３】
吸収器２０８からポンプ１０２で吸収溶液ライン２３４に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２３４Ｂで分岐して一方は領域２３８を通過して蒸気ドレン熱交換器２３０で加熱され昇温し、分岐部２３４Ｂで直行の他方の吸収溶液Ｌｉは低温溶液熱交換器３００を通過して加熱され昇温し、合流部２３６Ｇで合流する。
【００６４】
なお、分岐部２３４Ｂでの吸収溶液Ｌｉの分岐割合は、低温溶液熱交換器３００からの受熱と、蒸気ドレン熱交換器２３０からの受熱の合計熱量が最大となって合流部２３６Ｇでの吸収溶液Ｌｉ温度が最大になるように配分される。
【００６５】
合流部２３６Ｇを通過した稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２８Ｂを通過して加熱され昇温し、低温再生器２０６に導入される。
低温再生器２０６で加熱され昇温した稀釈吸収溶液Ｌｉは吸収溶液ライン３８４を介して蒸気ドレン熱交換器２２８Ａで加熱され昇温して分岐部２４０Ｂに向かう。そこで分岐した一方の稀釈吸収溶液Ｌｉは領域２４４を通過して蒸気ドレン熱交換器２２６で加熱され昇温し、分岐部２４０Ｂで直行の他方の稀釈吸収溶液Ｌｉは中温溶液熱交換器３０２を通過して加熱され昇温し、合流部２４２Ｇで合流する。
【００６６】
なお、分岐部２４０Ｂでの吸収溶液Ｌｉの分岐割合は、前記分岐部２３４Ｂにおける分岐要領と同様である
【００６７】
合流部２４２Ｇを通過した稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２４Ｂを通過して加熱され昇温し中温再生器２０４で冷媒蒸気に加熱され、冷媒の１部が蒸発分離されて濃縮される。
【００６８】
中温再生器２０４で濃縮された吸収溶液Ｌｉは、溶液ラインの領域３８６を介して蒸気ドレン熱交換器２２４Ａで加熱され昇温して、分岐部２４６Ｂに向かう。
分岐部２４６Ｂで分岐した吸収溶液Ｌｉの一方は領域２５０を通過して蒸気ドレン熱交換器２２２で加熱され昇温し、分岐部２４６Ｂで直行の他方の吸収溶液Ｌｉは高温溶液熱交換器３０４を通過して加熱され昇温し、合流部２４６Ｇで合流する。
【００６９】
なお、分岐部２４６Ｂでの吸収溶液Ｌｉの分岐割合は、前記分岐部２３４Ｂにおける分岐要領と同様である。
【００７０】
合流部２４６Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０を通過して加熱され昇温し、高温再生器２０２に導入される。
【００７１】
冷媒溶液を含んだ吸収溶液Ｌｉは、高温再生器２０２で加熱用蒸気ライン２１４による蒸気Ｓｔにより加熱され、冷媒溶液を蒸気として分離される。濃縮された濃縮吸収溶液Ｌｉは、吸収溶液ライン１１０を介して、高温溶液熱交換器３０４、中温溶液熱交換器３０２、低温溶液熱交換器３００で放熱し、吸収器２０８に導入される。
【００７２】
このようにして、加熱用蒸気ライン２１４を介した蒸気の熱量を余すところなく利用して吸収冷温水機ＲＳ５の熱効率を向上させる。
【００７３】
図４は、第４の実施形態であるリバースパラレルタイプの吸収冷温水機ＲＰ６の構成を示している。図５の実施形態と異なる部分を主体に説明する。
低温再生器２０６と中温再生器２０４を連通する吸収溶液ライン２６２の蒸気ドレン熱交換器２２８の手前に分岐部２６４が設けられ、分岐ライン２６８が取りつけられている。分岐ライン２６８は、高温再生器２０２と吸収器２０８を連通する吸収溶液ライン１１０の中温溶液熱交換器３０２と低温溶液熱交換器３００の間に連通されている。
【００７４】
また、中温再生器２０４と高温再生器２０２を連通する吸収溶液ライン２７０の蒸気ドレン２２４の手前に分岐部２７２が設られ、分岐ライン２７６が取りつけられている。分岐ライン２７６は、中温溶液熱交換器３０２と高温溶液熱交換器３０４との間に連通されている。
その他の構成は、図３の吸収冷温水機ＲＳ５と同じである。
【００７５】
上記吸収冷温水機ＲＰ６の作用を、分岐ライン２６８、２７６が取りつけられている周辺を主体にして説明する。
吸収器２０８からポンプ１０２で吸収溶液ライン２３４に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２、低温溶液熱交換器３００等を通過して加熱され昇温し、低温再生器２０６に導入される。
【００７６】
低温再生器２０６で加熱され少し濃縮された稀釈吸収溶液Ｌｉは吸収溶液ライン２６２の分岐部２６４に向かう。分岐部２６４で分岐された稀釈吸収溶液Ｌｉの一部は、分岐ライン２６８を介して合流部２６６で濃縮吸収溶液Ｌｉの流れる吸収溶液ライン１１０に入り、吸収器２０８に導入される。分岐部２６４を通過した稀釈吸収溶液Ｌｉは蒸気ドレン熱交換器２２８、中温溶液熱交換器３０２等を通過して加熱され昇温し中温再生器２０４に向かう。
【００７７】
中温再生器２０４で加熱され、さらに濃縮された稀釈吸収溶液Ｌｉは、吸収溶液ライン２７０の分岐部２７２に向かう。分岐部２７２で分岐された稀釈吸収溶液Ｌｉの一部は、分岐ライン２７４を介して合流部２７４で濃縮吸収溶液Ｌｉの流れる吸収溶液ライン１１０に入り、吸収器２０８に導入される。
【００７８】
分岐部２７６を通過した稀釈吸収溶液Ｌｉは蒸気ドレン熱交換器２２４、高温溶液熱交換器３０４等を通過して加熱され昇温し高温再生器２０２に向かう。
冷媒溶液を含んだ吸収溶液Ｌｉは、高温再生器２０２で加熱用蒸気ライン２１４による蒸気Ｓｔにより加熱され、冷媒溶液を蒸気として分離される。濃縮された濃縮吸収溶液Ｌｉは、吸収溶液ライン１１０を介して、高温溶液熱交換器３０４、中温溶液熱交換器３０２、低温溶液熱交換器３００で放熱し、吸収器２０８に導入される。
上記で省略した作用細部を含む作用全般は、すべて図５の吸収冷温水機ＲＳ５と同じである。
【００７９】
このようにして、低温再生器２０６、中温再生器２０４で加熱され濃縮された稀釈吸収溶液の一部を濃縮吸収溶液ライン１１０に導入して、系全体としての熱効率を向上させる。
【００８０】
図５は、第５の実施形態であるパラレルフロータイプの吸収冷温水機ＰＦ９の構成を示している。
吸収器２０８と高温再生器２０２とは、ポンプ１０２を介した吸収溶液ライン２８２で連通され、高温再生器２０２と中温再生器２０４とは、連続する吸収溶液ライン１０４、３１２、３１８で連通され、さらに第１の冷媒蒸気ライン２１６で連通されている。
【００８１】
第１の冷媒蒸気ライン２１６は、ライン内を通過する冷媒蒸気が保有する熱量が、中温再生器２０４内の吸収溶液に投入されて冷媒蒸気が再生されるよう構成されている。
【００８２】
中温再生器２０４と低温再生器２０６とは、連続する吸収溶液ライン３１８、３１４、３２２とで連通され、さらに並列に第２の冷媒蒸気ライン２１６Ａと第３の冷媒蒸気ライン２１８とで連通されている。
【００８３】
第３の冷媒蒸気ライン２１８は、ライン内を通過する冷媒蒸気が保有する熱量が、低温再生器２０６内の吸収溶液に投入されて冷媒蒸気が再生されるよう構成されている。
【００８４】
低温再生器２０６と吸収器２０８は、吸収溶液ライン１０８で連通されている。
吸収溶液ライン１０４に高温溶液熱交換器３０４が介装され、吸収溶液ライン３１４に中温溶液熱交換器３０２が介装され、吸収溶液ライン３１６に低温溶液熱交換器３００が介装されている。
【００８５】
高温溶液熱交換器３０４、中温溶液熱交換器３０２及び低温溶液熱交換器３００は、いづれも吸収溶液ライン２８２と熱的に接触し、吸収溶液ライン２８２に伝熱させるよう構成されている。
【００８６】 高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン２１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する各蒸気ドレン熱交換器に接続されて蒸気供給源戻るように連通されている。
【００８７】
蒸気ドレン熱交換器２２０は、吸収溶液ライン２８２の高温溶液熱交換器３０４と高温再生器２０２との間の領域２５２に、ライン２１４Ａと熱的に接触して介装されている。
【００８８】
蒸気ドレン熱交換器２２２は、吸収溶液ライン２８２の高温溶液熱交換器３０４を分岐部２６４Ｂと合流部２４６Ｇでバイパスする領域２５０に、ライン２１４Ａと熱的に接触して介装されている。
【００８９】
蒸気ドレン熱交換器２２３Ａは、吸収溶液ライン２８２の高温溶液熱交換器３０４と分岐部３１１との間の領域２８６に、ライン２１４Ａと熱的に接触して介装されている。
【００９０】
蒸気ドレン熱交換器２２４は、吸収溶液ライン２８２の分岐部３１１と中温溶液熱交換器３０２との間の領域２４６Ｂに、ライン２１４Ａと熱的に接触して介装されている。
【００９１】
蒸気ドレン熱交換器２２６は、吸収溶液ライン２８２の中温溶液熱交換器３０２を分岐部２４０Ｂと合流部２４２Ｇでバイパスする領域２４４に、ライン２１４Ａと熱的に接触して介装されている。
【００９２】
蒸気ドレン熱交換器２２７は、吸収溶液ライン２８２の分岐部３０８と分岐部２４０Ｂとの間の領域２８４に、ライン２１４Ａと熱的に接触して介装されている。
【００９３】
蒸気ドレン熱交換器２２８は、吸収溶液ライン２８２の分岐部３０８と合流部２８３Ｇとの間の領域２３８Ｈに、ライン２１４Ａと熱的に接触して介装されている。
【００９４】
蒸気ドレン熱交換器２３０は、吸収溶液ライン２８２の低温溶液熱交換器３００を分岐部２８２Ｂと合流部２８３Ｇでバイパスする領域２３８に、ライン２１４Ａと熱的に接触して介装されている。
【００９５】
蒸気ドレン熱交換器２３２は、吸収溶液ライン２８２の低温溶液熱交換器３００と吸収器２０８との間の領域２３５に、ライン２１４Ａと熱的に接触して介装されている。
【００９６】
上記各蒸気ドレン熱交換器２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２は、これらを経由するドレンの温度が、熱的に対となる吸収溶液ライン２３４の温度より高温であることが必要条件である。したがって、吸収冷温水機ＰＦ９の温度状況、空調負荷、加熱蒸気の温度、外気条件等によって、各蒸気ドレン熱交換器２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２の何れか１つあるいは全数を含む何れか複数が介装されている。
【００９７】
上記吸収冷温水機ＰＦ９の作用を、各蒸気ドレン熱交換器２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２の全てが介装されている例について説明する。
吸収器２０８からポンプ１０２で吸収溶液ライン２８２に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２８２Ｂで分岐して一方は領域２８３を通過して蒸気ドレン熱交換器２３０で加熱され昇温し、分岐部２８２Ｂで直行の他方の稀釈吸収溶液Ｌｉは低温溶液熱交換器３００を通過して加熱され昇温し、合流部２８３Ｇで合流する。
【００９８】
なお、分岐部２８２Ｂでの稀釈吸収溶液Ｌｉの分岐割合は、低温溶液熱交換器３００からの受熱と、蒸気ドレン熱交換器２３０からの受熱の合計熱量が最大となって合流部２８３Ｇでの稀釈吸収溶液Ｌｉ温度が最大になるように配分される。
【００９９】
合流部２８３Ｇを通過した稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２８を通過して加熱され昇温し、分岐部３０８で、一方は吸収溶液ライン３０６を介して低温再生器２０６に向かう。他方の吸収溶液ライン２８２を直行して蒸気ドレン熱交換器２２７で加熱され昇温して分岐部２４０Ｂに向かう。
【０１００】
分岐部２４０Ｂで分岐した稀釈吸収溶液Ｌｉの一方は領域２４４を通過して蒸気ドレン熱交換器２２６で加熱され昇温し、分岐部２４０Ｂで直行の他方の稀釈吸収溶液Ｌｉは中温溶液熱交換器３０２を通過して加熱され昇温し、合流部２４２Ｇで合流する。
【０１０１】
なお、分岐部２４０Ｂでの吸収溶液Ｌｉの分岐割合は、前記の分岐部２８２Ｂでの分岐要領と同じである。
【０１０２】
合流部２４２Ｇを通過した稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２４を通過して加熱され昇温し、分岐部３１１で分岐して一方は中温再生器２０４に、他方は高温再生器２０２に向かう。
【０１０３】
分岐部３１１で分岐された稀釈吸収溶液Ｌｉは、中温再生器２０４で第１の冷媒蒸気ライン２１６の加熱で濃縮される。
高温再生器２０２に向かった稀釈吸収溶液Ｌｉは蒸気ドレン熱交換器２２３Ａで加熱され昇温し、分岐部２４６Ｂに向かう。
【０１０４】
分岐部２４６Ｂで分岐した稀釈吸収溶液Ｌｉの一方は領域２５０を通過して蒸気ドレン熱交換器２２２で加熱され昇温し、分岐部２４６Ｂで直行の他方の稀釈吸収溶液Ｌｉは高温溶液熱交換器３０４を通過して加熱され昇温し、合流部２４６Ｇで合流する。
【０１０５】
なお、分岐部２４６Ｂでの吸収溶液Ｌｉの分岐割合は、前記の分岐部２８２Ｂ及び分岐部２４０Ｂでの分岐要領と同じである。
合流部２４６Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０を通過して加熱され昇温し、高温再生器２０２に導入される。
【０１０６】
冷媒溶液を含んだ稀釈吸収溶液Ｌｉは、高温再生器２０２で加熱用蒸気ライン２１４による蒸気Ｓｔにより加熱され、冷媒溶液を蒸気として分離され濃縮された濃縮吸収溶液Ｌｉは、吸収溶液ライン１０４によって高温溶液熱交換器３０４で放熱して吸収溶液ライン３１２の合流部３２０に向かう。
【０１０７】
合流部３２０に導かれた吸収溶液は、合流部３２０で、吸収溶液ライン３１８を介した吸収溶液と合流し、吸収溶液ライン３１４によって中温溶液熱交換器３０２で放熱して合流部３２４に向かう。
【０１０８】
合流部３２４に導かれた吸収溶液は、低温再生器２０６で濃縮された吸収溶液と合流して、低温溶液熱交換器３００で放熱して吸収器２０８に向かう。
冷媒の移動については、高温再生器２０２で稀釈吸収溶液Ｌｉから蒸発分離され、高熱量をもった蒸気として第１の冷媒蒸気ライン２１６を介して中温再生器２０４で吸収溶液を加熱させる。また、中温再生器２０４で蒸発分離された冷媒蒸気も、第２の冷媒蒸気ライン２１８を介して低温再生器２０６で熱量を放出する。
【０１０９】
低温再生器２０２で蒸発分離された冷媒蒸気は、中温再生器２０４からの蒸気とともに凝縮器２１０で凝縮され、蒸発器２１２で蒸発して外部流体と熱交換する。また、吸収器２０８で冷媒が外部流体と熱交換する。
【０１１０】
このようにして、加熱用蒸気ライン２１４を介した蒸気の熱量を余すところなく利用して吸収冷温水機ＰＦ９の熱効率を向上させる。
【０１１１】
図６は、第６の実施形態である別のパラレルフロータイプ吸収冷温水機ＰＦ１４の構成を示している。図５の実施形態と異なる部分を主体に説明する。
高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン２１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する蒸気ドレン熱交換器に接続されて蒸気供給源に連通されている。
【０１１２】
蒸気ドレン熱交換器２２７Ｃは、吸収溶液ライン２８２の高温溶液熱交換器３０４と中温溶液熱交換器３０２と低温溶液熱交換器３００と分岐部３０８と分岐部３１１を、分岐部２８２Ｂと合流部２８７Ｇでバイパスする領域２５１Ｓに、ライン２１４Ａと熱的に接触して介装されている。
【０１１３】
蒸気ドレン熱交換器２２７Ｃの前後に装着されている蒸気ドレン熱交換器２３２と２２０への蒸気ドレン熱交換器２２７Ｃの連通関係は、前記図５の実施形態と同じである。即ち、図５における蒸気ドレン熱交換器２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０に代えて、蒸気ドレン熱交換器２２７Ｃを介装した状態である。
上記を除いては、前記図５の構成と同じである。
【０１１４】
上記吸収冷温水機ＰＦ１４の作用を、蒸気ドレン熱交換器２２７Ｃが介装されている周辺を主体にして説明する。
吸収器２０８からポンプ１０２で吸収溶液ライン２８２に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２８２Ｂで分岐して、一方は蒸気ドレン熱交換器２２７Ｃで加熱され昇温して合流部２８７Ｇに向かう。
【０１１５】
分岐部２８２Ｂで直行の他方の稀釈吸収溶液Ｌｉは、低温溶液熱交換器３００を通過して加熱され昇温し、分岐部３０８で、一方は低温再生器２０６に向かい他方は直行して高温再生器２０２に向かう。
【０１１６】
高温再生器２０２に向かった稀釈吸収溶液Ｌｉは、中温溶液熱交換器３０２で加熱され昇温し分岐部３１１で一方は中温再生器２０４に向かい、他方は直行して高温再生器３０４で加熱され昇温し合流部２８７Ｇで蒸気ドレン熱交換器２２７Ｃを経由した稀釈吸収溶液Ｌｉと合流して高温再生器２０２に向かう。
【０１１７】
合流部２８７Ｇから高温再生器２０２に向かった吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０で加熱され昇温し高温再生器２０２に導入される。
高温再生器２０２、中温再生器２０４、低温再生器２０６等を経由する濃縮吸収溶液及び冷媒蒸気の作動は、図５と同じである。
【０１１８】
上記のようにして、吸収冷温水機の配熱特性に応じて、蒸気ドレン熱交換器の個数を少数にして、かつ熱効率を向上させる。
【０１１９】
図７は、第７の実施形態であるシリーズパラレルフロータイプ吸収冷温水機ＳＰ１５の構成を示している。
吸収器２０８と高温再生器２０２は、ポンプ１０２を介した稀釈吸収溶液ライン２８２で連通され、高温再生器２０２と中温再生器２０４とは吸収溶液ライン１０４と、第１の冷媒蒸気ライン２１６で連通されている。
【０１２０】
第１の冷媒蒸気ライン２１６は、ライン内を通過する冷媒蒸気が保有する熱量が、中温再生器２０４内の吸収溶液に投入されて冷媒蒸気が再生されるよう構成されている。
【０１２１】
中温再生器２０４と低温再生器２０６とは連続する吸収溶液ライン３１８、３０６と、並列な第１の冷媒蒸気ライン２１６と第２の冷媒蒸気ライン２１８とで連通されている。
【０１２２】
第２の冷媒蒸気ライン２１８は、ライン内を通過する冷媒蒸気が保有する熱量が、低温再生器２０６内の吸収溶液に投入されて冷媒蒸気が再生されるよう構成されている。
低温再生器２０６と吸収器２０８は、吸収溶液ライン３２２で連通されている。
【０１２３】
吸収溶液ライン３４０に高温溶液熱交換器３０４が介装され、吸収溶液ライン３１８に中温溶液熱交換器３０２が介装され、吸収溶液ライン３２２に低温溶液熱交換器３００が介装されている。
【０１２４】
高温溶液熱交換器３０４、中温溶液熱交換器３０２及び低温溶液熱交換器３００は、いづれも吸収溶液ライン２８２と熱的に接触し、吸収溶液ライン２８２に伝熱させるよう構成されている。
【０１２５】
高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン２１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する各蒸気ドレン熱交換器に接続されて蒸気供給源に戻るよう連通されている。
【０１２６】
蒸気ドレン熱交換器２２０は、吸収溶液ライン２８２の高温溶液熱交換器３０４と高温再生器２０２との間の領域２５２に、ライン２１４Ａと熱的に接触して介装されている。
【０１２７】
蒸気ドレン熱交換器２２２は、吸収溶液ライン２８２の高温溶液熱交換器３０４を分岐部２６４と合流部２４６Ｇでバイパスする領域２５０に、ライン２１４Ａと熱的に接触して介装されている。
【０１２８】
蒸気ドレン熱交換器２２３Ａは、吸収溶液ライン２８２の分岐部２４６Ｂと分岐部３１１との間の領域２８６に、ライン２１４Ａと熱的に接触して介装されている。
【０１２９】
蒸気ドレン熱交換器２２４は、吸収溶液ライン２８２の分岐部３１１と合流部２４２Ｇとの間の領域２４６Ｂに、ライン２１４Ａと熱的に接触して介装されている。
【０１３０】
蒸気ドレン熱交換器２２６は、吸収溶液ライン２８２の中温溶液熱交換器３０２を分岐部２４０Ｂと合流部２４２Ｇでバイパスする領域２４４に、ライン２１４Ａと熱的に接触して介装されている。
【０１３１】
蒸気ドレン熱交換器２２７は、吸収溶液ライン２８２の分岐部３０８と分岐部２４０Ｂとの間の領域２４３Ｐにライン２１４Ａと熱的に接触して介装されている。
【０１３２】
蒸気ドレン熱交換器２２８は、吸収溶液ライン２８２の合流部２８３Ｇと分岐部３０８との間の領域２８３Ｈに、ライン２１４Ａと熱的に接触して介装されている。
【０１３３】
蒸気ドレン熱交換器２３０は、吸収溶液ライン２８２の低温溶液熱交換器３００を分岐部２８２Ｂと合流部２８３Ｇでバイパスする領域２８３に、ライン２１４Ａと熱的に接触して介装されている。
【０１３４】
蒸気ドレン熱交換器２３２は、吸収溶液ライン２８２の吸収器２０８と分岐部２８２Ｂとの間の領域２３５に、ライン２１４Ａと熱的に接触して介装されている。
【０１３５】
上記各蒸気ドレン熱交換器２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２は、これらを経由するドレンの温度が、熱的に対となる吸収溶液ライン２３４の温度より高温であることが必要条件である。したがって、吸収冷温水機ＳＰ１５の温度状況、空調負荷、加熱蒸気の温度、外気条件等によって、各蒸気ドレン熱交換器２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２の何れか１つあるいは全数を含む何れか複数が介装されている。
【０１３６】
上記吸収冷温水機ＳＰ１５の作用を、各蒸気ドレン熱交換器２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２の全てが介装されている例について説明する。
吸収器２０８からポンプ１０２で吸収溶液ライン２８２に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２８２Ｂで分岐して一方は領域２８３を通過して蒸気ドレン熱交換器２３０で加熱され昇温し、分岐部２８２Ｂで直行の他方の稀釈吸収溶液Ｌｉは低温溶液熱交換器３００を通過して加熱され昇温し、合流部２８３Ｇで合流する。
【０１３７】
なお、分岐部２８２Ｂでの吸収溶液Ｌｉの分岐割合は、低温溶液熱交換器３００からの受熱と、蒸気ドレン熱交換器２３０からの受熱の合計熱量が最大となって合流部２８３Ｇでの吸収溶液Ｌｉ温度が最大になるように配分される。
【０１３８】
合流部２８３Ｇを通過した稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２８を通過して加熱され昇温し、分岐部３０８で、一方は吸収溶液ライン３０６を介して低温再生器２０６に向かう。他方は吸収溶液ライン２８２を直行して蒸気ドレン熱交換器２２７で加熱され昇温して分岐部２４０Ｂに向かう。
【０１３９】
分岐部２４０Ｂで分岐した稀釈吸収溶液Ｌｉの一方は領域２４４を通過して蒸気ドレン熱交換器２２６で加熱され昇温し、分岐部２４０Ｂで直行の他方の稀釈吸収溶液Ｌｉは中温溶液熱交換器３０２を通過して加熱され昇温し、合流部２４２Ｇで合流する。
【０１４０】
なお、分岐部２４０Ｂでの吸収溶液Ｌｉの分岐割合は、前記の分岐部２８２Ｂでの分岐要領と同じである。
合流部２４２Ｇを通過した稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２４を通過して加熱され昇温し、分岐部３１１で分岐して一方は中温再生器２０４に、他方は高温再生器２０２に向かう。
【０１４１】
分岐部３１１で分岐され吸収溶液ライン３１０に向かったた稀釈吸収溶液Ｌｉは、中温再生器２０４で第１の冷媒蒸気ライン２１６の加熱で濃縮される。
高温再生器２０２に向かった稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２２３Ａで加熱され昇温し、分岐部２４６Ｂに向かう。
【０１４２】
分岐部２４６Ｂで分岐した稀釈吸収溶液Ｌｉの一方は領域２５０を通過して蒸気ドレン熱交換器２２２で加熱され昇温し、分岐部２４６Ｂで直行の他方の稀釈吸収溶液Ｌｉは高温溶液熱交換器３０４を通過して加熱され昇温し、合流部２４６Ｇで合流する。
【０１４３】
なお、分岐部２４６Ｂでの吸収溶液Ｌｉの分岐割合は、前記の分岐部２８２Ｂ及び分岐部２４０Ｂでの分岐要領と同じである。
【０１４４】
合流部２４６Ｇを通過した吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０を通過して加熱され昇温し、高温再生器２０２に導入される。
【０１４５】
冷媒溶液を含んだ稀釈吸収溶液Ｌｉは、高温再生器２０２で加熱用蒸気ライン２１４による蒸気Ｓｔにより加熱され、冷媒溶液を蒸気として分離され濃縮された濃縮吸収溶液Ｌｉは、吸収溶液ライン３４０によって高温溶液熱交換器３０４で放熱して中温再生器２０４に向かう。
【０１４６】
中温再生器２０４で冷媒溶液を蒸気として分離され濃縮された濃縮吸収溶液Ｌｉは、吸収溶液ライン３１８によって中温溶液熱交換器３０２で放熱して吸収溶液ライン３０６に合流して低温再生器２０６に向かう。
低温再生器２０６で濃縮された吸収溶液は、低温溶液熱交換器３００で放熱して吸収器２０８に向かう。
【０１４７】
冷媒の移動については、高温再生器２０２で稀釈吸収溶液Ｌｉから蒸発分離され、高熱量をもった蒸気として第１の冷媒蒸気ライン２１６を介して中温再生器２０４で吸収溶液を加熱させる。また、中温再生器２０４で蒸発分離された冷媒蒸気も、第２の冷媒蒸気ライン２１８を介して低温再生器２０６で熱量を放出する。
【０１４８】
低温再生器２０２で蒸発分離された冷媒蒸気は、中温再生器２０４からの蒸気とともに凝縮器２１０で凝縮され、蒸発器２１２で蒸発して外部流体と熱交換する。また、吸収器２０８で冷媒が外部流体と熱交換する。
【０１４９】
このようにして、加熱用蒸気ライン２１４を介した蒸気の熱量を余すところなく利用して吸収冷温水機ＳＰ１５の熱効率を向上させる。
【０１５０】
図８は、第８の実施形態である別のシリーズパラレルフロータイプ吸収冷温水機ＳＰ２０の構成を示している。図７の実施形態と異なる部分を主体に説明する。
高温再生器２０２に、外部熱源に通じる加熱用蒸気ライン２１４が連通され、加熱用蒸気ライン２１４は高温再生器２０２を加熱経由してライン２１４Ａとなって次記する蒸気ドレン熱交換器に接続されて蒸気供給源に連通されている。
【０１５１】
蒸気ドレン熱交換器２２７Ｃは、吸収溶液ライン２８２の高温溶液熱交換器３０４と中温溶液熱交換器３０２と低温溶液熱交換器３００と分岐部３０８と分岐部３１１を、分岐部２８２Ｂと合流部２８７Ｇでバイパスする領域２５１Ｓに、ライン２１４Ａと熱的に接触して介装されている。
【０１５２】
蒸気ドレン熱交換器２２７Ｃの前後に装着されている蒸気ドレン熱交換器２３２と２２０への蒸気ドレン熱交換器２２７Ｃの連通関係は、前記図７の実施形態と同じである。即ち、図７における蒸気ドレン熱交換器２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０に代えて、蒸気ドレン熱交換器２２７Ｃを介装した状態である。
上記を除いては、前記図７の構成と同じである。
【０１５３】
上記吸収冷温水機ＳＰ２０の作用を、蒸気ドレン熱交換器２２７Ｃが介装されている周辺を主体にして説明する。
吸収器２０８からポンプ１０２で吸収溶液ライン２８２に吐出された冷媒を含む低温の稀釈吸収溶液Ｌｉは、蒸気ドレン熱交換器２３２で加熱され昇温し、分岐部２８２Ｂで分岐して、一方は蒸気ドレン熱交換器２２７Ｃで加熱され昇温して合流部２８７Ｇに向かう。
【０１５４】
分岐部２８２Ｂで直行の他方の稀釈吸収溶液Ｌｉは、低温溶液熱交換器３００を通過して加熱され昇温し、分岐部３０８で、一方は低温再生器２０６に向かい他方は直行して高温再生器２０２に向かう。
【０１５５】
高温再生器２０２に向かった稀釈吸収溶液Ｌｉは、中温溶液熱交換器３０２で加熱され昇温し、分岐部３１１で分岐して一方は中温再生器２０４に向かい、他方は直行して高温再生器３０４で加熱され昇温し、合流部２８７Ｇで蒸気ドレン熱交換器２２７Ｃを経由した稀釈吸収溶液Ｌｉと合流して高温再生器２０２に向かう。
【０１５６】
合流部２８７Ｇから高温再生器２０２に向かった吸収溶液Ｌｉは、蒸気ドレン熱交換器２２０で加熱され昇温し高温再生器２０２に導入される。
高温再生器２０２、中温再生器２０４、低温再生器２０６等を経由する濃縮吸収溶液及び冷媒蒸気の作動は、図７と同じである。
【０１５７】
上記のようにして、吸収冷温水機の配熱特性に応じて、蒸気ドレン熱交換器の個数を少数にして、かつ熱効率を向上させる。
【０１５８】
なお、図示８種の実施形態はあくまで例示であり、本発明の技術的範囲を限定する趣旨の記述ではない。
例えば、図示では各種のフロータイプ（例えば、シリーズフロー、パラレルフロー、リバースフロー、シリーズ・パラレルフロー、リバース・パラレルフロー）の代表的なもののみを示しているが、図示しないフローパターンにも本発明の利用が可能である。
また、冷媒ドレン熱交換器を配置し、下胴を複数段にし、溶液冷却吸収器を設けた実施形態も多数考えられる。
【０１５９】
【発明の効果】
本発明の作用効果を、以下に列記する。
（１） 本発明によれば、高温再生器で使用した加熱蒸気を複数の蒸気ドレン熱交換器で使用して稀釈吸収溶液を加熱させているので、熱の回収が大きい。
（２） 再生器で蒸発し発生した冷媒蒸気を低温再生器および低温の稀釈吸収溶液加熱に使用するので熱の回収がさらに大きくなる。
（３） 冷媒ドレンを冷媒ドレン熱交換器に通し、稀釈吸収冷媒を加熱させるので熱の回収が大きくなる。
（４） さらに、蒸発器と吸収器の下胴部分を複数段に分割すれば、機能が向上し熱効率がよくなる。
（５） 吸収器に溶液冷却吸収器を設ければ、再生器からの滴下吸収溶液の熱量を回収できる。
【図面の簡単な説明】
【図１】 本発明の第１の実施形態のシリーズフロータイプ吸収冷温水機を示す構成図。
【図２】 本発明の第２の実施形態の別のシリーズフロータイプ吸収冷温水機を示す構成図。
【図３】 本発明の第３の実施形態のリバースフロータイプ吸収冷温水機を示す構成図。
【図４】 本発明の第４の実施形態のリバースパラレルフロータイプ吸収冷温水機を示す構成図。
【図５】 本発明の第５の実施形態のパラレルフロータイプ吸収冷温水機を示す構成図。
【図６】 本発明の第６の実施形態の別のパラレルフロータイプ吸収冷温水機を示す構成図。
【図７】 本発明の第７の実施形態のシリーズパラレルフロータイプ吸収冷温水機を示す構成図。
【図８】 本発明の第８の実施形態の別のシリーズパラレルフロータイプ吸収冷温水機を示す構成図。
【図９】 従来のシリーズフロータイプ吸収冷温水機を示す構成図。
【符号の説明】
２０２・・・高温再生器
２０４・・・中温再生器
２０６・・・低温再生器
２０８・・・吸収器
２１０・・・凝縮器
２１２・・・蒸発器
２１４、２１４Ａ・・加熱用蒸気ライン
２２０、２２２、２２４、２２６、２２８、２３０、２３２・・蒸気ドレン熱交換器
２３４、２３８、２４０、２４４、２４６、２５０、２５２・・吸収溶液ライン[0001]
BACKGROUND OF THE INVENTION
The present invention relates to an absorption chiller / heater, and more particularly, to a triple effect steam-fired absorption chiller / heater having a high temperature regenerator, a medium temperature regenerator, and a low temperature regenerator.
[0002]
[Prior art]
A conventional triple-effect steam-fired absorption chiller / heater J1 shown in a typical example in FIG. 9 includes a high-temperature regenerator 202, a medium-temperature regenerator 204, a low-temperature regenerator 206, an absorber 208, and a condenser 210. , And an evaporator 212. The high temperature regenerator 202 is connected to a heating steam line 214 through which steam as a heating source flows, and the amount of heat held by the heating steam is input to the absorbing solution in the high temperature regenerator 202 to generate refrigerant vapor. (Reproduce.
[0003]
The steam generated in the high-temperature regenerator 202 flows through the steam line (first steam line) 216 and inputs the amount of heat held to the absorbing solution in the intermediate-temperature regenerator 204. Thereby, refrigerant vapor is generated (regenerated) in the intermediate temperature regenerator 204.
The steam generated in the intermediate temperature regenerator 204 flows through the second refrigerant vapor line 218 and inputs the amount of heat held in the absorption solution in the low temperature regenerator 206, and thus from the low temperature regenerator 206. Refrigerant vapor is generated.
[0004]
In the conventional triple effect steam-fired absorption chiller / heater J1, the steam (steam drain) after the heat exchange in the high-temperature regenerator 202 is directly discharged out of the system through the heating steam line 214A. Although the steam drain in the heating steam line 214A still retains a certain amount of heat, it is discharged out of the system while retaining the amount of heat, which is not economical.
[0005]
However, in the conventional triple effect steam-fired absorption chiller / heater J1, the effective use of the amount of heat held by the steam drain has not been considered at all. .
[0006]
[Problems to be solved by the invention]
The present invention has been proposed in view of the problems of the prior art as described above, and it is an object of the present invention to provide a triple-effect steam-fired absorption chiller / heater that can effectively use the amount of heat held by the steam drain. It is said.
[0007]
[Means for Solving the Problems]
The steam-fired absorption chiller / heater of the present invention includes a high-temperature regenerator (202), a medium-temperature regenerator (204), a low-temperature regenerator (206), an absorber (208), a condenser (210), and evaporation. The absorbent solution discharged from the absorber (208) flows through the high-temperature regenerator (202), the medium-temperature regenerator (204), and the low-temperature regenerator (206) in this order. The heating steam line (214, 214A) communicates with the high-temperature regenerator (202), and the amount of heat held by the steam flowing through the heating steam line (214) becomes the absorption solution in the high-temperature regenerator (202). It is configured to recycle the refrigerant vapor when it is thrown in,
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the intermediate temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The medium temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (302) converts the heat held by the absorption solution flowing through the absorption solution line (106) from the medium temperature regenerator (204) to the low temperature regenerator (206). 202), the low temperature solution heat exchanger (300) is held by the absorption solution flowing through the absorption solution line (108) from the low temperature regenerator (206) to the absorber (208). Is configured so as to be introduced into the absorbing solution towards the amount high temperature regenerator (202),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to seventh steam drain heat exchangers (220, 222, 224, 226, 228, 230, 232). )
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (222) is a first branch point between the intermediate solution heat exchanger (302) and the hot solution heat exchanger (304) of the absorption solution line toward the high temperature regenerator (202). (246B) is interposed in a first branch line (250) that bypasses the hot solution heat exchanger (304) and the hot solution heat exchanger (304). ) And the first steam drain heat exchanger (220) at the first junction (246G) and merged with the absorbent solution line toward the high temperature regenerator (202),
The third steam drain heat exchanger (224) is a region (246) between the intermediate solution heat exchanger (302) of the absorbing solution line and the first branch point (246B) toward the high temperature regenerator (202). Intervened in,
The fourth steam drain heat exchanger (226) is a second branch point between the cold solution heat exchanger (300) and the intermediate temperature solution heat exchanger (302) in the absorption solution line toward the high temperature regenerator (202). The second branch line (244) bypasses the intermediate temperature solution heat exchanger (302) and the intermediate temperature solution heat exchanger (302). ) And a third steam drain heat exchanger (224) at the second junction (242G) and merged with the absorbent solution line toward the high temperature regenerator (202),
The fifth steam drain heat exchanger (228) is a region (240) between the cold solution heat exchanger (300) and the second branch point (240B) of the absorption solution line toward the high temperature regenerator (202). Intervened in,
The sixth steam drain heat exchanger (230) is a third branch point (234B) between the absorbent solution pump (102) of the absorbent solution line and the cold solution heat exchanger (300) toward the high temperature regenerator (202). ) That is branched by a third branch line (238) that bypasses the low temperature solution heat exchanger (300) and is connected to the low temperature solution heat exchanger (300). Merging with the absorbent solution line towards the high temperature regenerator (202) at a third junction (236G) between the fifth steam drain heat exchanger (228);
The seventh steam drain heat exchanger (232) is interposed in a region (235) between the absorption solution pump (102) and the third branch point (234B) of the absorption solution line toward the high temperature regenerator (202). And
The first to seventh steam drain heat exchangers (220, 222, 224, 226, 228, 230, 232) are used for the heating steam or steam after the amount of heat is supplied to the absorbing solution in the high temperature regenerator (202). A feature is that the amount of heat held by the drain is introduced into the absorbing solution that leaves the absorber (208) and goes to the high-temperature regenerator (202) (Claim 1: FIG. 1).
[0008]
The steam-fired absorption chiller / heater of the present invention includes a high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), and a condenser (210). The absorption solution discharged from the absorber (208) flows in the order of the high temperature regenerator (202), the medium temperature regenerator (204), and the low temperature regenerator (206). The heating steam line (214, 214A) communicates with the high temperature regenerator (202), and the amount of heat held by the steam flowing through the heating steam line (214) is absorbed in the high temperature regenerator (202). It is configured to regenerate the refrigerant vapor when put into the solution,
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the intermediate temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The medium temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (302) converts the amount of heat held by the absorption solution flowing through the absorption solution line (106) from the medium temperature regenerator (204) to the low temperature regenerator (206). 202), the low temperature solution heat exchanger (300) is held by the absorption solution flowing through the absorption solution line (108) from the low temperature regenerator (206) to the absorber (208). Is configured so as to be introduced into the absorbing solution towards the amount high temperature regenerator (202),
A region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) includes a first steam drain heat exchanger (220) and a second steam drain heat exchanger (232). , Communicated with a third steam drain heat exchanger (225),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (232) is interposed in the region between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the high temperature regenerator (202). And
The third steam drain heat exchanger (225) is a branch point between the seventh steam drain heat exchanger (232) and the low temperature solution heat exchanger (300) in the absorption solution line toward the high temperature regenerator (202). (234B), the branch line (236Q) is interposed between the low temperature solution heat exchanger (300), the intermediate temperature solution heat exchanger (302), and the high temperature solution heat exchanger (304). ) And join the absorbing solution line toward the high temperature regenerator (202) at the confluence (246G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The first steam drain heat exchanger (220), the second steam drain heat exchanger (232), and the third steam drain heat exchanger (225) transfer heat to the absorbing solution in the high temperature regenerator (202). After the charging, the heating steam or the steam drainage is stored in the absorbing solution exiting from the absorber (208) toward the high-temperature regenerator (202). Item 2: FIG.
[0009]
The steam-fired absorption chiller / heater of the present invention includes a high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), and a condenser (210). And the evaporator (212), and the absorbent solution discharged from the absorber (208) flows through the low temperature regenerator (206), the medium temperature regenerator (204), and the high temperature regenerator (202) in this order. The heating steam line (214, 214A) communicates with the high temperature regenerator (202), and the amount of heat held by the steam flowing through the heating steam line (214) is within the high temperature regenerator (202). The refrigerant vapor is regenerated by being put into the absorption solution of
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
The absorption solution line (236) from the absorber (208) to the low temperature regenerator (206) is provided with a low temperature solution heat exchanger (300), and the low temperature regenerator (206) goes to the medium temperature regenerator (204). A medium temperature solution heat exchanger (302) is interposed in the absorption solution line (242), and a high temperature solution heat exchange is performed in the absorption solution line (248) from the medium temperature solution heat exchanger (302) to the high temperature regenerator (202). A heat exchanger (304) is interposed, and is configured to input the amount of heat held by the absorbent solution flowing through the absorbent solution line (110) from the high-temperature solution heat exchanger (304) toward the absorber (208),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 224A, 224B, 226, 228A, 228B). , 230, 232),
The first steam drain heat exchanger (220) is between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). Intervened in the region (252),
The second steam drain heat exchanger (222) is between the intermediate temperature regenerator (204) and the high temperature solution heat exchanger (304) of the absorbent solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). A first branch line (250) that branches at a first branch point (246B) is interposed between the first branch line (250) and the hot solution heat exchanger (304). Join the absorbent solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202) at a first junction (246G) between the heat exchanger (304) and the first steam drain heat exchanger (220). And
The third steam drain heat exchanger (224A) is located between the intermediate temperature regenerator (204) of the absorbing solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202) and the first branch point (246B). In the region (386) of
The fourth steam drain heat exchanger (224B) includes an intermediate solution heat exchanger (302) and an intermediate temperature regenerator (204) in the absorption solution line (384) from the low temperature regenerator (206) to the intermediate temperature regenerator (204). Intervened in the area between and
The fifth steam drain heat exchanger (226) is between the low temperature regenerator (206) and intermediate temperature solution heat exchanger (302) of the absorption solution line from the low temperature regenerator (206) to the medium temperature regenerator (204). A second branch line (244) that branches at the second branch point (240B) is interposed between the second branch line (244) and the intermediate temperature solution heat exchanger (302). Join the absorbent solution line from the low temperature regenerator (206) to the medium temperature regenerator (204) at the second confluence (242G) between the heat exchanger (302) and the fourth steam drain heat exchanger (224B). And
The sixth steam drain heat exchanger (228A) is located between the cold regenerator (206) of the absorbent solution line from the low temperature regenerator (206) to the medium temperature regenerator (204) and the second branch point (240B). In the region (384) of
The seventh steam drain heat exchanger (228B) is between the low temperature solution heat exchanger (300) and the low temperature regenerator (206) of the absorption solution line from the absorber (208) to the low temperature regenerator (206). In the region (382),
The eighth steam drain heat exchanger (230) is located between the absorbent solution pump (102) and the cold solution heat exchanger (300) in the absorbent solution line from the absorber (208) to the cold regenerator (206). Is interposed in a third branch line (238) that branches at the third branch point (234B), the third branch line (238) bypassing the low temperature solution heat exchanger (300) and the low temperature solution heat Joins the absorbent solution line from the absorber (208) to the cold regenerator (206) at a third junction (236G) between the exchanger (300) and the seventh steam drain heat exchanger (228B);
The ninth steam drain heat exchanger (232) is between the absorbent solution pump (102) and the third branch point (234B) of the absorbent solution line from the absorber (208) to the cold regenerator (206). Intervened in the region (235),
The first to ninth steam drain heat exchangers (220, 222, 224A, 224B, 226, 228A, 228B, 230, 232) are heated by supplying heat to the absorbing solution in the high temperature regenerator (202). It is configured that the amount of heat held by the steam for use or the steam drain is put into the absorbing solution that goes out of the absorber (208) and goes to the high-temperature regenerator (202) (Claim 3: FIG. 3). ).
[0010]
Furthermore, the steam-fired absorption chiller / heater of the present invention includes a high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), and a condenser (210). And the evaporator (212), the high-temperature regenerator (202) communicates with the heating steam lines (214, 214A), and the amount of heat held by the steam flowing through the heating steam line (214) is high. The refrigerant vapor is regenerated by being put into the absorbing solution in the regenerator (202),
The absorbent solution exiting the absorber (208) flows through the low temperature regenerator (206), the medium temperature regenerator (204), and the high temperature regenerator (202) in this order, and the high temperature regenerator (202) and the absorber. An absorbent solution line (260) that communicates with (208), branches (264) from the absorbent solution line (262) that communicates between the low temperature regenerator (206) and the intermediate temperature regenerator (204), and a high temperature regenerator The intermediate solution regenerator (204) and the high temperature regenerator have a first branched absorbent solution line (268) that merges (266) with the absorption solution line (260) that communicates between the (202) and the absorber (208). Branching (272) from the absorbing solution line (270) communicating with (202) and joining (274) the absorbing solution line (260) communicating with the high temperature regenerator (202) and the absorber (208). 2 branched absorption solution It has a line (276),
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
The absorption solution line (236) from the absorber (208) to the low temperature regenerator (206) is provided with a low temperature solution heat exchanger (300), and the low temperature regenerator (206) goes to the medium temperature regenerator (204). A medium temperature solution heat exchanger (302) is interposed in the absorption solution line (242), and a high temperature solution heat exchange is performed in the absorption solution line (248) from the medium temperature solution heat exchanger (302) to the high temperature regenerator (202). A heat exchanger (304) is interposed, and is configured to input the amount of heat held by the absorbent solution flowing through the absorbent solution line (110) from the high-temperature solution heat exchanger (304) toward the absorber (208),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 224, 224B, 226, 228A, 228B). , 230, 232),
The first steam drain heat exchanger (220) is between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). Intervened in the region (252),
The second steam drain heat exchanger (222) is connected to the branch (272) of the second branched absorbent solution line (276) of the absorbent solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202) and the high temperature. The first branch line (250) is branched at a first branch point (246B) between the solution heat exchangers (304), and the first branch line (250) The hot regenerator from the intermediate temperature regenerator (204) at the first junction (246G) bypassing the regenerator (304) and between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220) Merge with the absorbent solution line towards (202),
The third steam drain heat exchanger (224) includes a branch (272) and a second branch absorption solution line (276) of the absorption solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). Intervened in the area between 1 branch point (246B),
The fourth steam drain heat exchanger (224B) includes an intermediate solution heat exchanger (302) and an intermediate temperature regenerator (204) in the absorption solution line (384) from the low temperature regenerator (206) to the intermediate temperature regenerator (204). Intervened in the area between and
The fifth steam drain heat exchanger (226) is connected to the bifurcation (264) of the first branched absorbent solution line (268) and the intermediate temperature of the absorbent solution line from the low temperature regenerator (206) to the intermediate temperature regenerator (204). It is interposed in a second branch line (244) that branches at a second branch point (240B) between the solution heat exchangers (302), and the second branch line (244) is an intermediate temperature solution heat exchanger. From the low temperature regenerator (206) to the intermediate temperature regenerator at a second junction (242G) bypassing the regenerator (302) and between the intermediate temperature solution heat exchanger (302) and the fourth steam drain heat exchanger (224B) Merge with the absorbent solution line towards (204),
The sixth steam drain heat exchanger (228A) includes a first branch absorption solution line (268) branching portion (264) and an absorption solution line from the low temperature regenerator (206) to the medium temperature regenerator (204). Is interposed in the area between the two branch points (240B),
The seventh steam drain heat exchanger (228B) is between the low temperature solution heat exchanger (300) and the low temperature regenerator (206) of the absorption solution line from the absorber (208) to the low temperature regenerator (206). In the region (382),
The eighth steam drain heat exchanger (230) is located between the absorbent solution pump (102) and the cold solution heat exchanger (300) in the absorbent solution line from the absorber (208) to the cold regenerator (206). Is interposed in a third branch line (238) that branches at the third branch point (234B), the third branch line (238) bypassing the low temperature solution heat exchanger (300) and the low temperature solution heat Joins the absorbent solution line from the absorber (208) to the cold regenerator (206) at a third junction (236G) between the exchanger (300) and the seventh steam drain heat exchanger (228B);
The ninth steam drain heat exchanger (232) is between the absorbent solution pump (102) and the third branch point (234B) of the absorbent solution line from the absorber (208) to the cold regenerator (206). Intervened in the region (235),
The first to ninth steam drain heat exchangers (220, 222, 224, 224B, 226, 228A, 228B, 230, 232) are used to heat the absorption solution in the high-temperature regenerator (202) after the amount of heat is supplied thereto. The amount of heat possessed by the steam for use or the steam drain is introduced into an absorbing solution that exits from the absorber (208) and goes to the high-temperature regenerator (202) (Claim 4: FIG. 4). ).
[0011]
Alternatively, the steam-fired absorption chiller / heater of the present invention includes a high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), and a condenser (210). And the evaporator (212), the high-temperature regenerator (202) communicates with the heating steam lines (214, 214A), and the amount of heat held by the steam flowing through the heating steam line (214) is high. The refrigerant vapor is regenerated by being put into the absorbing solution in the regenerator (202),
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) is configured to input the amount of heat held by the absorption solution flowing through the absorption solution line (104) from the high temperature regenerator (202) into the absorption solution toward the high temperature regenerator (202). The intermediate temperature solution heat exchanger (302) absorbs the amount of heat held by the absorption solution flowing in the absorption solution line (314) from the intermediate temperature regenerator (204) toward the low temperature regenerator (206) toward the high temperature regenerator (202). The low-temperature solution heat exchanger (300) is configured to supply the amount of heat held by the absorption solution flowing through the absorption solution line (316) from the low-temperature regenerator (206) to the absorber (208). 20 Is configured so as to be introduced into the absorption solution toward the),
An absorbent solution line (282, 284, 286) communicating from the absorber (208) to the high temperature regenerator (202) is located in the region between the low temperature solution heat exchanger (300) and the medium temperature solution heat exchanger (302). A first branch absorption solution line (306) communicating with the low temperature regenerator (206) is branched (308), and a region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the intermediate temperature regenerator (204) is branched (311), and the absorption solution lines (312, 314) from the high temperature regenerator (202) to the absorber (208) are branched. 316), the absorption solution line (318) through which the absorption solution heated by the intermediate temperature regenerator (204) flows joins (320), and the absorption solution heated by the low temperature regenerator (206) Flowing absorbent solution Emissions (322) is joined (324),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228). , 230, 232),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (222) includes a branch (311) of the second branched absorbent solution line (310) and a high temperature solution heat exchanger (304) of the absorbent solution line toward the high temperature regenerator (202). The first branch line (250) branches at a first branch point (246B) between the first branch line (250B) and bypasses the hot solution heat exchanger (304). And merged with the absorption solution line toward the high temperature regenerator (202) at a first junction (246G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The third steam drain heat exchanger (223A) includes a branch (311) and a first branch point (246B) of the second branched absorbent solution line (310) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the area (286) between
The fourth steam drain heat exchanger (224) includes a middle temperature solution heat exchanger (302) of the absorption solution line toward the high temperature regenerator (202) and a branch (311) of the second branch absorption solution line (310). Intervened in the area between and
The fifth steam drain heat exchanger (226) includes a branch (308) of the first branched absorbent solution line (306) and an intermediate temperature solution heat exchanger (302) of the absorbent solution line toward the high temperature regenerator (202). Is interposed in a second branch line (244) that branches at a second branch point (240B) between the two, and the second branch line (244) bypasses the intermediate temperature solution heat exchanger (302). And at the second junction (242G) between the intermediate temperature solution heat exchanger (302) and the fourth steam drain heat exchanger (224), joins the absorption solution line toward the high temperature regenerator (202),
The sixth steam drain heat exchanger (227) includes a branch (308) and a second branch point (240B) of the first branched absorbent solution line (306) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the region (284) between
The seventh steam drain heat exchanger (228) includes a low temperature solution heat exchanger (300) of the absorption solution line toward the high temperature regenerator (202) and a branch (308) of the first branch absorption solution line (306). Intervened in the area between and
The eighth steam drain heat exchanger (230) has a third branch point (282B) between the absorbent solution pump (102) of the absorbent solution line and the cold solution heat exchanger (300) toward the high temperature regenerator (202). ) Is branched to a third branch line (283), which bypasses the low temperature solution heat exchanger (300) and is connected to the low temperature solution heat exchanger (300). Merging with the absorbent solution line towards the high temperature regenerator (202) at a third junction (283G) between the seventh steam drain heat exchanger (228);
The ninth steam drain heat exchanger (232) is interposed in the region (235) between the absorption solution pump (102) and the third branch point (282B) of the absorption solution line toward the high temperature regenerator (202). And
The first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228, 230, 232) are used to heat the absorbing solution in the high-temperature regenerator (202) after the amount of heat is supplied thereto. The amount of heat possessed by the steam for use or the steam drain is introduced into an absorbing solution that leaves the absorber (208) and goes to the high-temperature regenerator (202) (Claim 5: FIG. 5). ).
[0012]
The steam-fired absorption chiller / heater of the present invention includes a high-temperature regenerator (202), a medium-temperature regenerator (204), a low-temperature regenerator (206), an absorber (208), a condenser (210), and evaporation. The heating steam line (214, 214A) communicates with the high temperature regenerator (202), and the amount of heat held by the steam flowing through the heating steam line (214) is high temperature regenerator. The refrigerant vapor is regenerated by being charged into the absorbing solution in (202),
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) is configured to input the amount of heat held by the absorption solution flowing through the absorption solution line (104) from the high temperature regenerator (202) into the absorption solution toward the high temperature regenerator (202). The intermediate temperature solution heat exchanger (302) absorbs the amount of heat held by the absorption solution flowing in the absorption solution line (314) from the intermediate temperature regenerator (204) toward the low temperature regenerator (206) toward the high temperature regenerator (202). The low-temperature solution heat exchanger (300) is configured to supply the amount of heat held by the absorption solution flowing through the absorption solution line (316) from the low-temperature regenerator (206) to the absorber (208). 20 Is configured so as to be introduced into the absorption solution toward the),
An absorbent solution line (282, 284, 286) communicating from the absorber (208) to the high temperature regenerator (202) is located in the region between the low temperature solution heat exchanger (300) and the medium temperature solution heat exchanger (302). A first branch absorption solution line (306) communicating with the low temperature regenerator (206) is branched (308), and a region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the intermediate temperature regenerator (204) is branched (311), and the absorption solution lines (312, 314) from the high temperature regenerator (202) to the absorber (208) are branched. 316), the absorption solution line (318) through which the absorption solution heated by the intermediate temperature regenerator (204) flows joins (320), and the absorption solution heated by the low temperature regenerator (206) Flowing absorbent solution Emissions (322) is joined (324),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) communicates with the first to third steam drain heat exchangers (220, 232, 227C),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (232) is interposed in an area (282) between the absorbent solution pump (102) and the cold solution heat exchanger (300) of the absorbent solution line toward the high temperature regenerator (202). And
The third steam drain heat exchanger (227C) is a branch in the region (282) between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the hot regenerator (202). The branch line (251S) is branched at a point (282B), and the branch line (251S) includes a low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger ( 304) and joins the absorbent solution line toward the high temperature regenerator (202) at the junction (287G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The first to third steam drain heat exchangers (220, 232, 227C) absorb the amount of heat held by the heating steam or the steam drain after charging the amount of heat into the absorbing solution in the high temperature regenerator (202). It is characterized in that it is constructed so as to be put into the absorbing solution that leaves the vessel (208) and goes to the high temperature regenerator (202) (Claim 6: FIG. 6).
[0013]
The steam-fired absorption chiller / heater of the present invention includes a high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), and a condenser (210). And the evaporator (212), the high-temperature regenerator (202) communicates with the heating steam lines (214, 214A), and the amount of heat held by the steam flowing through the heating steam line (214) is high. The refrigerant vapor is regenerated by being put into the absorbing solution in the regenerator (202),
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202). The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the medium temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The intermediate temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (302) converts the amount of heat held by the absorption solution flowing through the absorption solution line (318) from the intermediate temperature regenerator (204) to the low temperature regenerator (206). 202), the low temperature solution heat exchanger (300) is held by the absorption solution flowing through the absorption solution line (322) from the low temperature regenerator (206) to the absorber (208). Is configured so as to be introduced into the absorbing solution towards the amount high temperature regenerator (202),
An absorbent solution line (282, 286) communicating from the absorber (208) to the high temperature regenerator (202) is regenerated at a low temperature in the region between the low temperature solution heat exchanger (300) and the intermediate temperature solution heat exchanger (302). A first branched absorbent solution line (306) communicating with the vessel (206) branches off (308) and has a medium temperature in the region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the regenerator (204) is branched (311), and the absorption solution line (340) through which the absorption solution heated by the high temperature regenerator (202) flows is regenerated at a medium temperature. The absorbent solution line (318) through which the absorbent solution heated by the intermediate temperature regenerator (204) flows joins the first branched absorbent solution line (306) and is connected to the low temperature regenerator (206). )
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228). , 230, 232),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (222) includes a branch (311) of the second branched absorbent solution line (310) and a high temperature solution heat exchanger (304) of the absorbent solution line toward the high temperature regenerator (202). The first branch line (250) branches at a first branch point (246B) between the first branch line (250B) and bypasses the hot solution heat exchanger (304). And merged with the absorption solution line toward the high temperature regenerator (202) at a first junction (246G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The third steam drain heat exchanger (223A) includes a branch (311) and a first branch point (246B) of the second branched absorbent solution line (310) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the area (286) between
The fourth steam drain heat exchanger (224) includes a middle temperature solution heat exchanger (302) of the absorption solution line toward the high temperature regenerator (202) and a branch (311) of the second branch absorption solution line (310). Intervened in the area between and
The fifth steam drain heat exchanger (226) includes a branch (308) of the first branched absorbent solution line (306) and an intermediate temperature solution heat exchanger (302) of the absorbent solution line toward the high temperature regenerator (202). Is interposed in a second branch line (244) that branches at a second branch point (240B) between the two, and the second branch line (244) bypasses the intermediate temperature solution heat exchanger (302). And at the second junction (242G) between the intermediate temperature solution heat exchanger (302) and the fourth steam drain heat exchanger (224), joins the absorption solution line toward the high temperature regenerator (202),
The sixth steam drain heat exchanger (227) includes a branch (308) and a second branch point (240B) of the first branched absorbent solution line (306) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the area between and
The seventh steam drain heat exchanger (228) includes a low temperature solution heat exchanger (300) of the absorption solution line toward the high temperature regenerator (202) and a branch (308) of the first branch absorption solution line (306). Intervened in the area between and
The eighth steam drain heat exchanger (230) has a third branch point (282B) between the absorbent solution pump (102) of the absorbent solution line and the cold solution heat exchanger (300) toward the high temperature regenerator (202). ) Is branched to a third branch line (283), which bypasses the low temperature solution heat exchanger (300) and is connected to the low temperature solution heat exchanger (300). Merging with the absorbent solution line towards the high temperature regenerator (202) at a third junction (283G) between the seventh steam drain heat exchanger (228);
The ninth steam drain heat exchanger (232) is interposed in the region (235) between the absorption solution pump (102) and the third branch point (282B) of the absorption solution line toward the high temperature regenerator (202). And
The first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228, 230, 232) are used to heat the absorbing solution in the high-temperature regenerator (202) after the amount of heat is supplied thereto. The amount of heat possessed by the steam for use or the steam drain is introduced into the absorbing solution that exits from the absorber (208) and goes to the high-temperature regenerator (202) (Claim 7: FIG. 7). ).
[0014]
The steam-fired absorption chiller / heater of the present invention includes a high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), An evaporator (212), a heating steam line (214, 214A) communicates with the high temperature regenerator (202), and the amount of heat held by the steam flowing through the heating steam line (214) is regenerated at a high temperature. The refrigerant vapor is regenerated by being put into the absorbing solution in the vessel (202),
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202). The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the medium temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The medium temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (202) stores the amount of heat held by the absorption solution flowing in the absorption solution line from the medium temperature regenerator (204) toward the low temperature regenerator (206). The low-temperature solution heat exchanger (300) is configured so as to be charged into the absorbent solution facing away, and the high-temperature regenerator (300 2 Is configured so as to be introduced into the absorption solution toward the 2),
An absorbent solution line (282, 286) communicating from the absorber (208) to the high temperature regenerator (202) is regenerated at a low temperature in the region between the low temperature solution heat exchanger (300) and the intermediate temperature solution heat exchanger (302). A first branched absorbent solution line (306) communicating with the vessel (206) branches off (308) and has a medium temperature in the region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the regenerator (204) is branched (311), and the absorption solution line (340) through which the absorption solution heated by the high temperature regenerator (202) flows is regenerated at a medium temperature. The absorbent solution line through which the absorbent solution heated by the intermediate temperature regenerator (204) flows joins the first branched absorbent solution line (306) and communicates with the low temperature regenerator (206). And
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) communicates with the first to third steam drain heat exchangers (220, 232, 227C),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (232) is interposed in the region between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the high temperature regenerator (202). And
The third steam drain heat exchanger (227C) is a branch point (282B) in the region between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the high temperature regenerator (202). ), And the branch line (251S) includes a low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304). Bypass and join the absorbent solution line towards the hot regenerator (202) at the junction (287G) between the hot solution heat exchanger (304) and the first steam drain heat exchanger (220);
The first to third steam drain heat exchangers (220, 232, 227C) absorb the amount of heat held by the heating steam or the steam drain after charging the amount of heat into the absorbing solution in the high temperature regenerator (202). It is characterized in that it is constituted so as to be put into the absorbing solution which goes out of the vessel (208) and goes to the high temperature regenerator (202) (Claim 8: FIG. 8).
[0015]
According to the present invention having such a configuration, the heating steam line (214, 214A) communicates with the high temperature regenerator (202) and then the steam drain heat exchanger (220, 222, 224, 226, 228, 230). 232), and the steam drain heat exchanger (220, 222, 224, 226, 228, 230, 232) heats the absorbing solution in the high-temperature regenerator (202) after the heat is input. The absorption solution line (234, 238, 240, 244, 246, 250, 252) where the amount of heat held by the steam or steam drain exits the absorber (208) and communicates with the regenerator (202, 204, 206). It is configured so as to be put into the flowing absorbent solution (the absorbent solution supplied to the regenerator).
That is, the amount of heat held by the steam drain that has been discharged out of the system in the prior art is input to the absorbing solution (the absorbing solution supplied to the regenerator) flowing toward the regenerator (202, 204, 206). Thus, it is effectively used for increasing the sensible heat of the absorbing solution.
[0016]
As a result of the temperature rise (sensible heat increase) of the absorbing solution supplied to the regenerator (202, 204, 206), the amount of heat input in the regenerator (202, 204, 206) is the same. For example, the regeneration amount of the refrigerant vapor (water vapor) is increased, and the efficiency of the absorption chiller / heater is improved.
[0017]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, an embodiment in which the present invention is applied to a triple effect steam-fired absorption chiller / heater will be described with reference to the accompanying drawings. In the accompanying drawings, similar members are denoted by the same reference numerals, and overlapping description of the member names and reference numerals is omitted.
[0018]
FIG. 1 shows a configuration of a series flow type absorption chiller / heater S1 according to the first embodiment.
[0019]
The absorber 208 and the high temperature regenerator 202 are communicated by an absorption solution line 234 via the pump 102, and the high temperature regenerator 202 and the medium temperature regenerator 204 are communicated by an absorption solution line 104 and a first refrigerant vapor line 216. ing.
The first refrigerant vapor line 216 is configured such that the amount of heat held by the refrigerant vapor passing through the line is input to the absorbing solution in the intermediate temperature regenerator 204 to regenerate the refrigerant vapor.
[0020]
The intermediate temperature regenerator 204 and the low temperature regenerator 206 are communicated with each other through an absorbing solution line 106 and a second refrigerant vapor line 218.
The second refrigerant vapor line 218 is configured such that the amount of heat held by the refrigerant vapor passing through the line is input to the absorbing solution in the low temperature regenerator 206 to regenerate the refrigerant vapor.
[0021]
The low temperature regenerator 206 and the absorber 208 are communicated with each other through the absorption solution line 108.
A high temperature solution heat exchanger 304 is interposed in the absorption solution line 104, a medium temperature solution heat exchanger 302 is interposed in the absorption solution line 106, and a low temperature solution heat exchanger 300 is interposed in the absorption solution line 108.
[0022]
The high temperature solution heat exchanger 304, the medium temperature solution heat exchanger 302, and the low temperature solution heat exchanger 300 are all configured to be in thermal contact with the absorbent solution line 234 and to conduct heat to the absorbent solution line 234.
[0023]
A heating steam line 214 communicating with an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 214 becomes a line 214A through heating the high-temperature regenerator 202 and is connected to each steam drain heat exchanger described below. And communicated back to the steam source.
[0024]
The steam drain heat exchanger 220 is interposed in a region 252 between the high temperature solution heat exchanger 304 and the high temperature regenerator 202 in the absorbent solution line 234 in thermal contact with the line 214A.
[0025]
The steam drain heat exchanger 222 is interposed in a region 250 that bypasses the high temperature solution heat exchanger 304 of the absorption solution line 234 at the branch portion 246B and the junction portion 246G, in thermal contact with the line 214A.
[0026]
The steam drain heat exchanger 224 is interposed in a region 246 between the hot solution heat exchanger 304 and the intermediate solution heat exchanger 302 in the absorbent solution line 234 in thermal contact with the line 214A.
[0027]
The steam drain heat exchanger 226 is interposed in a region 244 that bypasses the intermediate temperature solution heat exchanger 302 of the absorption solution line 234 at the branching portion 240B and the joining portion 242G in thermal contact with the line 214A.
[0028]
The steam drain heat exchanger 228 is interposed in a region 240 between the intermediate solution heat exchanger 302 and the low temperature solution heat exchanger 300 in the absorbent solution line 234 in thermal contact with the line 214A.
[0029]
The steam drain heat exchanger 230 is interposed in a region 238 that bypasses the low temperature solution heat exchanger 300 of the absorption solution line 234 at the branch portion 234B and the junction portion 236G in thermal contact with the line 214A.
[0030]
The steam drain heat exchanger 232 is interposed in a region 235 of the absorbent solution line 234 between the cold solution heat exchanger 300 and the absorber 208 in thermal contact with the line 214A.
[0031]
In each of the steam drain heat exchangers 220, 222, 224, 226, 228, 230, 232, it is necessary that the temperature of the drain passing through them is higher than the temperature of the absorbing solution line 234 that is thermally paired. It is a condition. Therefore, any one or all of the steam drain heat exchangers 220, 222, 224, 226, 228, 230, and 232 depending on the temperature condition of the absorption chiller / heater S1, the air conditioning load, the temperature of the heating steam, the outside air condition, and the like. Any one or more including
[0032]
The operation of the absorption chiller / heater S1 will be described with respect to an example in which all the steam drain heat exchangers 220, 222, 224, 226, 228, 230, and 232 are interposed.
[0033]
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 234 by the pump 102 is heated by the steam drain heat exchanger 232 to rise in temperature, branch at the branch portion 234B, and one of the regions 238 Is passed through the steam drain heat exchanger 230 and heated to increase the temperature, and the other absorption solution Li that is orthogonal to the branch portion 234 is heated and heated through the low-temperature solution heat exchanger 300 to be combined at the junction 236G. To do.
[0034]
The branching ratio of the absorbing solution Li at the branching portion 234B is such that the total amount of heat received from the low-temperature solution heat exchanger 300 and the heat received from the steam drain heat exchanger 230 is maximized, and the absorbing solution at the junction 236G. Distribution is performed so that the Li temperature becomes maximum.
[0035]
The absorbing solution Li that has passed through the merging portion 236G passes through the steam drain heat exchanger 228 and is heated to rise in temperature, branches at the branching portion 240B, and passes through the region 244 to be heated by the steam drain heat exchanger 226. Then, the other absorption solution Li, which is perpendicular to the branching section 240B, is heated by passing through the intermediate temperature solution heat exchanger 302, and is merged at the junction section 242G. The branching ratio of the absorbing solution Li in the branching part 240B is the same as that in the branching part 234B.
[0036]
The absorbing solution Li that has passed through the merging portion 242G passes through the steam drain heat exchanger 224 and is heated to rise in temperature, branches at the branching portion 246B, and passes through the region 250 and is heated by the steam drain heat exchanger 222. Then, the other absorbent solution Li that is perpendicular to the branching section 246B is heated by passing through the high-temperature solution heat exchanger 304, and is joined at the joining section 246G. The branching ratio of the absorbing solution Li at the branching part 246B is the same as that at the branching part 234B.
[0037]
The absorbing solution Li that has passed through the merging portion 246 </ b> G passes through the steam drain heat exchanger 220, is heated and heated, and is introduced into the high-temperature regenerator 202.
[0038]
The diluted absorbent solution Li containing the refrigerant solution is heated by the steam St in the heating steam line 214 in the high-temperature regenerator 202, and the concentrated absorbent solution Li separated and concentrated using the refrigerant solution as a vapor is heated by the absorbent solution line 104. The heat is dissipated by the solution heat exchanger 304 and introduced into the intermediate temperature regenerator 204.
[0039]
The concentrated absorbent Li is heated by the refrigerant vapor from the first refrigerant vapor line 216 in the intermediate temperature regenerator 204, and the concentrated solution Li separated and concentrated using the refrigerant solution as vapor is directed to the absorbent solution line 106.
The absorbing solution Li led to the absorbing solution line 106 dissipates heat in the intermediate temperature solution heat exchanger 302 and is introduced into the low temperature regenerator 206.
The concentrated absorbent solution Li introduced into the low-temperature regenerator 206 is separated and further concentrated as a refrigerant solution as a vapor, is led to the absorbent solution line 108, radiates heat in the low-temperature solution heat exchanger 300, and returns to the absorber 208.
[0040]
On the other hand, the refrigerant h2 evaporated and separated by the high-temperature regenerator 202 dissipates heat in the intermediate-temperature regenerator 204 via the first refrigerant vapor line 216, further heats the concentrated absorbent solution Li, and goes to the condenser 210. The refrigerant h3 evaporated and separated by the intermediate temperature regenerator 204 releases heat by the low temperature regenerator 206 to heat the concentrated absorbent solution Li, joins the first refrigerant vapor line 216, and goes to the condenser 210.
[0041]
The refrigerants h2 and h3 guided to the condenser 210 are condensed and evaporated by the evaporator 212 to exchange heat with an external fluid. In addition, the refrigerant exchanges heat with the external fluid in the absorber 208.
In this way, the heat efficiency of the absorption chiller / heater S1 is improved by making full use of the heat quantity of the steam through the heating steam line 214.
[0042]
FIG. 2 shows a configuration of a series flow type absorption chiller / heater S4 according to the second embodiment. A description will be given mainly of parts different from the embodiment of FIG.
A heating steam line 214 leading to an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 214 becomes a line 214A via the heating of the high-temperature regenerator 202 and is connected to a steam drain heat exchanger described below. Connected to the steam source.
[0043]
The steam drain heat exchanger 225 branches between the steam drain heat exchanger 220 and the hot solution heat exchanger 304 in the absorption solution line 234 and between the cold solution heat exchanger 300 and the steam drain heat exchanger 232. A region 236Q that is bypassed by the portion 234B and the junction 246G is interposed in thermal contact with the line 214A.
[0044]
The communication relationship of the steam drain heat exchanger 225 to the steam drains 232 and 220 mounted before and after the steam drain heat exchanger 225 is substantially the same as the embodiment of FIG. That is, the steam drain heat exchanger 225 is interposed instead of the steam drain heat exchangers 230, 228, 226, and 222 in FIG.
Except for the above, the configuration is the same as in FIG.
[0045]
The operation of the absorption chiller / heater S4 will be described with a focus on the vicinity where the steam drain heat exchanger 225 is interposed.
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 234 by the pump 102 is heated by the steam drain heat exchanger 232 to be heated and branched at the branch portion 234B, and one of the regions is a region. 236Q passes through 236Q and is heated by the steam drain heat exchanger 225 to increase the temperature, and the other absorption solution Li that goes straight at the branch portion 234B is the low-temperature solution heat exchanger 300, the medium-low temperature solution heat exchanger 302, and the high-temperature solution heat exchanger. It passes through 304, is heated and heated up, and merges at the junction 246G.
[0046]
The absorbing solution Li that has passed through the merging portion 246 </ b> G passes through the steam drain heat exchanger 220, is heated to rise in temperature, and travels toward the high-temperature regenerator 202.
As described above, according to the heat distribution characteristics of the absorption chiller / heater, the number of steam drain heat exchangers is reduced and the thermal efficiency is improved.
[0047]
FIG. 3 shows a configuration of a reverse flow type absorption chiller / heater RS5 according to the third embodiment. A description will be given mainly of parts different from the embodiment of FIG.
The absorber 208 and the low temperature regenerator 206 constituting the outgoing path of the diluted absorbent solution are communicated with each other through the absorption solution lines 234, 235, 236, and 382 via the pump 102. The low temperature regenerator 206 and the intermediate temperature regenerator 204 are connected to the absorbent solution. The medium temperature regenerator 204 and the high temperature regenerator 202 are communicated with each other through absorption solution lines 386, 248 and 252.
[0048]
The high-temperature regenerator 202 and the absorber 208 constituting the return path of the concentrated absorbent solution are communicated with each other through the absorbent solution line 110.
A high temperature solution heat exchanger 304, a medium temperature solution heat exchanger 302, and a low temperature solution heat exchanger 300 are interposed in the absorption solution line 110 from the high temperature regenerator 202 side.
[0049]
The region 248 between the absorbent solution lines 386 and 252 is in thermal contact with the hot solution heat exchanger 304. The region 248 communicates with a region 250 that bypasses the high-temperature solution heat exchanger 304 at the branching portion 246B and the joining portion 246G.
[0050]
The middle region 242 of the absorbent solution line 384 is in thermal contact with the intermediate solution heat exchanger 302. The region 242 communicates with a region 244 that bypasses the intermediate temperature solution heat exchanger 302 at the branching portion 240B and the joining portion 242G.
[0051]
The middle region 236 of the absorbent solution lines 234 and 382 passes through the cold solution heat exchanger 300 and is in thermal contact. The region 236 communicates with a region 238 that bypasses the low-temperature solution heat exchanger 300 at the branching portion 234B and the joining portion 236G.
[0052]
The high temperature solution heat exchanger 304, the medium temperature solution heat exchanger 302, and the low temperature solution heat exchanger 300 are each configured to thermally contact the diluted absorbent solution from the concentrated absorbent solution and transfer heat to the diluted absorbent solution.
[0053]
A heating steam line 214 leading to an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 314 becomes a line 214A via the high-temperature regenerator 202 via heating, and is connected to each steam drain heat exchanger described below. And communicated to a steam source.
[0054]
The steam drain heat exchanger 220 is interposed in a region 252 between the high temperature solution heat exchanger 304 and the high temperature regenerator 202 in thermal contact with the line 214A.
[0055]
The steam drain heat exchanger 222 is interposed in a region 250 that bypasses the high temperature solution heat exchanger 304 in thermal contact with the line 214A.
Steam drain heat exchanger 224A is interposed in a region 386 between hot solution heat exchanger 304 and intermediate temperature regenerator 204 in thermal contact with line 214A.
[0056]
The steam drain heat exchanger 224B is interposed in a region 384 between the intermediate temperature regenerator 204 and the intermediate temperature solution heat exchanger 302 in thermal contact with the line 214A.
[0057]
The steam drain heat exchanger 226 is interposed in a region 244 that bypasses the intermediate temperature solution heat exchanger 302 in thermal contact with the line 214A.
[0058]
The steam drain heat exchanger 228A is interposed in a region 384 between the medium temperature solution heat exchanger 302 and the low temperature regenerator 206 in thermal contact with the line 214A.
[0059]
The steam drain heat exchanger 228B is interposed in a region 382 between the low temperature regenerator 206 and the low temperature solution heat exchanger 300 in thermal contact with the line 214A.
The steam drain heat exchanger 230 is interposed in a region 238 that bypasses the low temperature solution heat exchanger 300 in thermal contact with the line 214A.
[0060]
The steam drain heat exchanger 232 is interposed in a region 235 between the absorber 208 and the cold solution heat exchanger 300 in thermal contact with the line 214A.
[0061]
In each of the steam drain heat exchangers 220, 222, 224A, 224B, 226, 228A, 228B, 230, 232, the temperature of the drain passing through them is higher than the temperature of the absorbing solution that is thermally paired. Is a necessary condition. Therefore, any one of the steam drain heat exchangers 220, 222, 224A, 224B, 226, 228A, 228B, 230, 232 depending on the temperature condition of the absorption chiller / heater RS5, the air conditioning load, the temperature of the heating steam, the outside air condition, etc. One or a plurality including one or all of the numbers are interposed.
Other refrigerant vapor lines and the like are the same as in FIG.
[0062]
The operation of the absorption chiller / heater RS5 will be described with respect to an example in which all the steam drain heat exchangers 220, 222, 224A, 224B, 226, 228A, 228B, 230, and 232 are interposed.
[0063]
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 234 by the pump 102 is heated by the steam drain heat exchanger 232 to rise in temperature, branch at the branch portion 234B, and one of the regions 238 And the other absorption solution Li direct in the branch part 234B is heated and heated through the low-temperature solution heat exchanger 300, and joins in the joining part 236G. To do.
[0064]
The branching ratio of the absorbing solution Li at the branching portion 234B is such that the total amount of heat received from the low-temperature solution heat exchanger 300 and the heat received from the steam drain heat exchanger 230 is maximized, and the absorbing solution at the junction 236G. Distribution is performed so that the Li temperature becomes maximum.
[0065]
The diluted absorbent solution Li that has passed through the merging portion 236G is heated and heated through the steam drain heat exchanger 228B, and is introduced into the low-temperature regenerator 206.
The diluted absorbent solution Li heated by the low-temperature regenerator 206 and heated is heated by the steam drain heat exchanger 228A via the absorbent solution line 384 and heated to the branching section 240B. One of the diluted absorbent solutions Li branched there passes through the region 244 and is heated by the steam drain heat exchanger 226, and the temperature of the other diluted absorbent solution Li passes through the branch 240B, and the other diluted absorbent solution Li passes through the intermediate temperature solution heat exchanger 302. Then, the temperature is raised and the temperature is raised, and the merging portion 242G joins.
[0066]
The branching ratio of the absorbing solution Li in the branching part 240B is the same as the branching procedure in the branching part 234B.
[0067]
The diluted absorbent solution Li that has passed through the junction 242G is heated and heated through the steam drain heat exchanger 224B, heated to the refrigerant vapor in the intermediate temperature regenerator 204, and part of the refrigerant is evaporated and separated to be concentrated. .
[0068]
The absorbing solution Li concentrated in the intermediate temperature regenerator 204 is heated by the steam drain heat exchanger 224A through the region 386 of the solution line and heated to the branch portion 246B.
One of the absorbing solutions Li branched at the branching portion 246B passes through the region 250 and is heated by the steam drain heat exchanger 222 to be heated, and the other absorbing solution Li at the branching portion 246B passes through the high-temperature solution heat exchanger 304. It passes through and is heated to rise in temperature, and merges at the junction 246G.
[0069]
The branching ratio of the absorbing solution Li at the branching portion 246B is the same as the branching procedure at the branching portion 234B.
[0070]
The absorbing solution Li that has passed through the merging portion 246 </ b> G passes through the steam drain heat exchanger 220, is heated and heated, and is introduced into the high-temperature regenerator 202.
[0071]
The absorbing solution Li containing the refrigerant solution is heated by the vapor St by the heating vapor line 214 in the high-temperature regenerator 202, and is separated using the refrigerant solution as vapor. The concentrated concentrated absorbent Li is radiated by the high temperature solution heat exchanger 304, the medium temperature solution heat exchanger 302, and the low temperature solution heat exchanger 300 via the absorption solution line 110 and introduced into the absorber 208.
[0072]
In this way, the heat efficiency of the absorption chiller / heater RS5 is improved by making full use of the amount of heat of the steam via the heating steam line 214.
[0073]
FIG. 4 shows the configuration of a reverse parallel type absorption chiller / heater RP6 according to the fourth embodiment. A description will be given mainly of parts different from the embodiment of FIG.
A branch portion 264 is provided in front of the steam drain heat exchanger 228 of the absorption solution line 262 communicating with the low temperature regenerator 206 and the intermediate temperature regenerator 204, and the branch line 268 is attached. The branch line 268 is communicated between the medium temperature solution heat exchanger 302 and the low temperature solution heat exchanger 300 that connect the high temperature regenerator 202 and the absorber 208 to each other.
[0074]
Further, a branch portion 272 is provided in front of the vapor drain 224 of the absorption solution line 270 that connects the intermediate temperature regenerator 204 and the high temperature regenerator 202, and a branch line 276 is attached. The branch line 276 is communicated between the medium temperature solution heat exchanger 302 and the high temperature solution heat exchanger 304.
Other configurations are the same as those of the absorption chiller / heater RS5 of FIG.
[0075]
The operation of the absorption chiller / heater RP6 will be described focusing on the periphery where the branch lines 268 and 276 are attached.
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 234 by the pump 102 passes through the steam drain heat exchanger 232, the low-temperature solution heat exchanger 300, etc. It is introduced into the low temperature regenerator 206.
[0076]
The diluted absorbent solution Li heated by the low-temperature regenerator 206 and slightly concentrated is directed to the branch 264 of the absorbent solution line 262. A part of the diluted absorbent solution Li branched at the branch part 264 enters the absorbent solution line 110 through which the concentrated absorbent solution Li flows at the junction part 266 via the branch line 268 and is introduced into the absorber 208. The diluted absorbent solution Li that has passed through the branching portion 264 is heated through the steam drain heat exchanger 228, the intermediate temperature solution heat exchanger 302, and the like, and is heated to the intermediate temperature regenerator 204.
[0077]
The diluted absorbent solution Li heated by the intermediate temperature regenerator 204 and further concentrated is directed to the branch 272 of the absorbent solution line 270. A part of the diluted absorbent solution Li branched at the branch part 272 enters the absorbent solution line 110 through which the concentrated absorbent solution Li flows at the junction part 274 via the branch line 274 and is introduced into the absorber 208.
[0078]
The diluted absorbent solution Li that has passed through the branching portion 276 passes through the steam drain heat exchanger 224, the high temperature solution heat exchanger 304, and the like, is heated and heated, and travels toward the high temperature regenerator 202.
The absorbing solution Li containing the refrigerant solution is heated by the vapor St by the heating vapor line 214 in the high-temperature regenerator 202, and is separated using the refrigerant solution as vapor. The concentrated concentrated absorbent Li is radiated by the high temperature solution heat exchanger 304, the medium temperature solution heat exchanger 302, and the low temperature solution heat exchanger 300 via the absorption solution line 110 and introduced into the absorber 208.
All the actions including the action details omitted above are all the same as the absorption chiller / heater RS5 of FIG.
[0079]
In this way, a part of the diluted absorbent solution heated and concentrated by the low temperature regenerator 206 and the intermediate temperature regenerator 204 is introduced into the concentrated absorbent solution line 110, thereby improving the thermal efficiency of the entire system.
[0080]
FIG. 5 shows a configuration of a parallel flow type absorption chiller / heater PF9 of the fifth embodiment.
The absorber 208 and the high temperature regenerator 202 are communicated with each other through an absorption solution line 282 via the pump 102, and the high temperature regenerator 202 and the medium temperature regenerator 204 are communicated with each other through continuous absorption solution lines 104, 312, 318, Further, the first refrigerant vapor line 216 communicates.
[0081]
The first refrigerant vapor line 216 is configured such that the amount of heat held by the refrigerant vapor passing through the line is input to the absorbing solution in the intermediate temperature regenerator 204 to regenerate the refrigerant vapor.
[0082]
The intermediate temperature regenerator 204 and the low temperature regenerator 206 are communicated with continuous absorption solution lines 318, 314, and 322, and are further communicated in parallel with the second refrigerant vapor line 216A and the third refrigerant vapor line 218. Yes.
[0083]
The third refrigerant vapor line 218 is configured such that the amount of heat held by the refrigerant vapor passing through the line is input to the absorbing solution in the low temperature regenerator 206 to regenerate the refrigerant vapor.
[0084]
The low temperature regenerator 206 and the absorber 208 are communicated with each other through the absorption solution line 108.
A high temperature solution heat exchanger 304 is interposed in the absorption solution line 104, a medium temperature solution heat exchanger 302 is interposed in the absorption solution line 314, and a low temperature solution heat exchanger 300 is interposed in the absorption solution line 316.
[0085]
The high temperature solution heat exchanger 304, the medium temperature solution heat exchanger 302, and the low temperature solution heat exchanger 300 are all configured to be in thermal contact with the absorbing solution line 282 and transfer heat to the absorbing solution line 282.
A heating steam line 214 communicating with an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 214 becomes a line 214 A via the heating of the high-temperature regenerator 202, and each steam drain heat exchange described below. Connected to the vessel and communicated back to the steam source.
[0087]
The steam drain heat exchanger 220 is interposed in a region 252 between the high temperature solution heat exchanger 304 and the high temperature regenerator 202 in the absorbent solution line 282 in thermal contact with the line 214A.
[0088]
The steam drain heat exchanger 222 is interposed in thermal contact with the line 214A in a region 250 that bypasses the high-temperature solution heat exchanger 304 of the absorption solution line 282 at the branch portion 264B and the junction portion 246G.
[0089]
The steam drain heat exchanger 223A is interposed in a region 286 between the high temperature solution heat exchanger 304 and the branch 311 of the absorption solution line 282 in thermal contact with the line 214A.
[0090]
The steam drain heat exchanger 224 is interposed in a region 246B between the branch portion 311 of the absorption solution line 282 and the intermediate temperature solution heat exchanger 302 in thermal contact with the line 214A.
[0091]
The steam drain heat exchanger 226 is interposed in a region 244 that bypasses the intermediate temperature solution heat exchanger 302 of the absorbing solution line 282 at the branching portion 240B and the joining portion 242G in thermal contact with the line 214A.
[0092]
The steam drain heat exchanger 227 is interposed in a region 284 between the branch 308 and the branch 240B of the absorption solution line 282 in thermal contact with the line 214A.
[0093]
The steam drain heat exchanger 228 is interposed in a region 238H between the branch portion 308 and the merge portion 283G of the absorbing solution line 282 in thermal contact with the line 214A.
[0094]
The steam drain heat exchanger 230 is interposed in a region 238 that bypasses the low-temperature solution heat exchanger 300 of the absorption solution line 282 at the branch portion 282B and the junction portion 283G in thermal contact with the line 214A.
[0095]
The steam drain heat exchanger 232 is interposed in a region 235 between the cold solution heat exchanger 300 and the absorber 208 of the absorbent solution line 282 in thermal contact with the line 214A.
[0096]
In each of the steam drain heat exchangers 220, 222, 223A, 224, 226, 227, 228, 230, 232, the temperature of the drain passing through these is higher than the temperature of the absorbing solution line 234 that is thermally paired. It is a necessary condition. Therefore, any one of the steam drain heat exchangers 220, 222, 223A, 224, 226, 227, 228, 230, 232 depending on the temperature condition of the absorption chiller / heater PF9, the air conditioning load, the temperature of the heating steam, the outside air condition, etc. One or a plurality including one or all of the numbers are interposed.
[0097]
The operation of the absorption chiller / heater PF9 will be described with respect to an example in which all the steam drain heat exchangers 220, 222, 223A, 224, 226, 227, 228, 230, and 232 are interposed.
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 282 by the pump 102 is heated by the steam drain heat exchanger 232 to rise in temperature, and is branched at the branching portion 282B. And the other diluted absorbent solution Li is directly passed through the low-temperature solution heat exchanger 300 and heated to rise in temperature at the junction 283G. Join.
[0098]
Note that the branching ratio of the diluted absorbent solution Li at the branching portion 282B is such that the total amount of heat received from the low temperature solution heat exchanger 300 and the heat received from the steam drain heat exchanger 230 is maximized, and the dilution at the junction 283G is performed. The absorption solution Li temperature is distributed so as to be maximized.
[0099]
The diluted absorbent solution Li that has passed through the merging portion 283G passes through the steam drain heat exchanger 228 and is heated to rise in temperature. At the branch portion 308, one is directed to the low-temperature regenerator 206 through the absorbent solution line 306. The other absorption solution line 282 goes straight, is heated by the steam drain heat exchanger 227, and is heated to the branching section 240B.
[0100]
One of the diluted absorbent solutions Li branched at the branch 240B passes through the region 244 and is heated by the steam drain heat exchanger 226 to increase the temperature, and the other diluted absorbent solution Li at the branch 240B is the intermediate temperature solution heat exchanger. It passes through 302 and is heated to rise in temperature, and merges at the junction 242G.
[0101]
The branching ratio of the absorbing solution Li at the branching portion 240B is the same as the branching procedure at the branching portion 282B.
[0102]
The diluted absorbent solution Li that has passed through the junction 242G passes through the steam drain heat exchanger 224 and is heated to rise in temperature, branching off at the branching section 311 and one into the medium temperature regenerator 204 and the other into the high temperature regenerator 202. Head.
[0103]
The diluted absorbent solution Li branched by the branch part 311 is concentrated by heating the first refrigerant vapor line 216 in the intermediate temperature regenerator 204.
The diluted absorbent solution Li toward the high-temperature regenerator 202 is heated by the steam drain heat exchanger 223A to increase the temperature, and proceeds to the branching section 246B.
[0104]
One of the diluted absorbent solutions Li branched at the branch portion 246B passes through the region 250 and is heated by the steam drain heat exchanger 222 to be heated, and the other diluted absorbent solution Li at the branch portion 246B is heated at the high temperature solution heat exchanger. It passes through 304, is heated and heated up, and merges at the junction 246G.
[0105]
The branching ratio of the absorbing solution Li at the branching portion 246B is the same as the branching procedure at the branching portion 282B and the branching portion 240B.
The absorbing solution Li that has passed through the merging portion 246 </ b> G passes through the steam drain heat exchanger 220, is heated and heated, and is introduced into the high-temperature regenerator 202.
[0106]
The diluted absorbent solution Li containing the refrigerant solution is heated by the steam St in the heating steam line 214 in the high-temperature regenerator 202, and the concentrated absorbent solution Li separated and concentrated using the refrigerant solution as a vapor is heated by the absorbent solution line 104. The heat is dissipated by the solution heat exchanger 304 and travels toward the junction 320 of the absorbing solution line 312.
[0107]
The absorbing solution guided to the merging unit 320 is merged with the absorbing solution via the absorbing solution line 318 in the merging unit 320, dissipates heat in the intermediate temperature solution heat exchanger 302 through the absorbing solution line 314, and travels to the merging unit 324.
[0108]
The absorption solution guided to the merge unit 324 merges with the absorption solution concentrated by the low temperature regenerator 206, dissipates heat in the low temperature solution heat exchanger 300, and travels toward the absorber 208.
As for the movement of the refrigerant, the absorption solution is heated by the intermediate temperature regenerator 204 through the first refrigerant vapor line 216 as a vapor having a high heat quantity after being evaporated and separated from the diluted absorption solution Li by the high temperature regenerator 202. In addition, the refrigerant vapor evaporated and separated by the intermediate temperature regenerator 204 also releases heat by the low temperature regenerator 206 through the second refrigerant vapor line 218.
[0109]
The refrigerant vapor evaporated and separated by the low temperature regenerator 202 is condensed by the condenser 210 together with the vapor from the intermediate temperature regenerator 204, and evaporated by the evaporator 212 to exchange heat with an external fluid. In addition, the refrigerant exchanges heat with the external fluid in the absorber 208.
[0110]
In this manner, the heat efficiency of the absorption chiller / heater PF9 is improved by making full use of the heat quantity of the steam through the heating steam line 214.
[0111]
FIG. 6 shows the configuration of another parallel flow type absorption chiller / heater PF14 according to the sixth embodiment. A description will be given mainly of parts different from the embodiment of FIG.
A heating steam line 214 leading to an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 214 becomes a line 214A via the heating of the high-temperature regenerator 202 and is connected to a steam drain heat exchanger described below. Connected to the steam source.
[0112]
The steam drain heat exchanger 227C includes a high temperature solution heat exchanger 304, a medium temperature solution heat exchanger 302, a low temperature solution heat exchanger 300, a branch portion 308, and a branch portion 311 of the absorption solution line 282, and a branch portion 282B and a junction portion 287G. In the region 251S to be bypassed, the line 214A is in thermal contact with the region 251S.
[0113]
The communication relationship of the steam drain heat exchanger 227C to the steam drain heat exchangers 232 and 220 mounted before and after the steam drain heat exchanger 227C is the same as that of the embodiment of FIG. In other words, the steam drain heat exchanger 227C is interposed instead of the steam drain heat exchangers 222, 223A, 224, 226, 227, 228, 230 in FIG.
Except for the above, the configuration is the same as that shown in FIG.
[0114]
The operation of the absorption chiller / heater PF14 will be described mainly with respect to the periphery where the steam drain heat exchanger 227C is interposed.
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 282 by the pump 102 is heated by the steam drain heat exchanger 232 to be heated and branched at the branch portion 282B. It is heated by the drain heat exchanger 227C and heated to the joining portion 287G.
[0115]
The other diluted absorption solution Li that goes straight at the branching portion 282B passes through the low-temperature solution heat exchanger 300 and is heated to rise in temperature, and at the branching portion 308, one goes to the low-temperature regenerator 206 and the other goes straight to the high-temperature regeneration. Head to vessel 202.
[0116]
The diluted absorption solution Li toward the high temperature regenerator 202 is heated by the intermediate temperature solution heat exchanger 302 and heated, and at the branching portion 311, one goes to the intermediate temperature regenerator 204 and the other goes straight and is heated by the high temperature regenerator 304. The temperature is raised and merged with the diluted absorbent solution Li via the steam drain heat exchanger 227C at the merge portion 287G and headed to the high temperature regenerator 202.
[0117]
The absorbing solution Li directed from the junction 287G to the high temperature regenerator 202 is heated by the steam drain heat exchanger 220, heated, and introduced into the high temperature regenerator 202.
The operation of the concentrated absorbent solution and the refrigerant vapor via the high temperature regenerator 202, the medium temperature regenerator 204, the low temperature regenerator 206, and the like is the same as in FIG.
[0118]
As described above, according to the heat distribution characteristics of the absorption chiller / heater, the number of steam drain heat exchangers is reduced and the thermal efficiency is improved.
[0119]
FIG. 7 shows a configuration of a series parallel flow type absorption chiller / heater SP15 according to the seventh embodiment.
The absorber 208 and the high temperature regenerator 202 are communicated with each other through a diluted absorption solution line 282 via the pump 102, and the high temperature regenerator 202 and the medium temperature regenerator 204 are communicated with each other through the absorption solution line 104 and the first refrigerant vapor line 216. Has been.
[0120]
The first refrigerant vapor line 216 is configured such that the amount of heat held by the refrigerant vapor passing through the line is input to the absorbing solution in the intermediate temperature regenerator 204 to regenerate the refrigerant vapor.
[0121]
The intermediate temperature regenerator 204 and the low temperature regenerator 206 are communicated with each other through continuous absorption solution lines 318 and 306, and a first refrigerant vapor line 216 and a second refrigerant vapor line 218 in parallel.
[0122]
The second refrigerant vapor line 218 is configured such that the amount of heat held by the refrigerant vapor passing through the line is input to the absorbing solution in the low temperature regenerator 206 to regenerate the refrigerant vapor.
The low temperature regenerator 206 and the absorber 208 are communicated with each other through an absorption solution line 322.
[0123]
A high temperature solution heat exchanger 304 is interposed in the absorption solution line 340, a medium temperature solution heat exchanger 302 is interposed in the absorption solution line 318, and a low temperature solution heat exchanger 300 is interposed in the absorption solution line 322.
[0124]
The high temperature solution heat exchanger 304, the medium temperature solution heat exchanger 302, and the low temperature solution heat exchanger 300 are all configured to be in thermal contact with the absorbing solution line 282 and transfer heat to the absorbing solution line 282.
[0125]
A heating steam line 214 communicating with an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 214 becomes a line 214A through heating the high-temperature regenerator 202 and is connected to each steam drain heat exchanger described below. And communicated back to the steam source.
[0126]
The steam drain heat exchanger 220 is interposed in a region 252 between the high temperature solution heat exchanger 304 and the high temperature regenerator 202 in the absorbent solution line 282 in thermal contact with the line 214A.
[0127]
The steam drain heat exchanger 222 is interposed in a region 250 that bypasses the high-temperature solution heat exchanger 304 of the absorption solution line 282 at the branch portion 264 and the junction portion 246G in thermal contact with the line 214A.
[0128]
The steam drain heat exchanger 223A is interposed in a region 286 between the branch portion 246B and the branch portion 311 of the absorption solution line 282 in thermal contact with the line 214A.
[0129]
The steam drain heat exchanger 224 is interposed in a region 246B between the branch portion 311 and the merge portion 242G of the absorbing solution line 282 in thermal contact with the line 214A.
[0130]
The steam drain heat exchanger 226 is interposed in a region 244 that bypasses the intermediate temperature solution heat exchanger 302 of the absorbing solution line 282 at the branching portion 240B and the joining portion 242G in thermal contact with the line 214A.
[0131]
The steam drain heat exchanger 227 is interposed in a region 243P between the branch 308 and the branch 240B of the absorption solution line 282 in thermal contact with the line 214A.
[0132]
The steam drain heat exchanger 228 is interposed in a region 283H between the joining portion 283G and the branching portion 308 of the absorbing solution line 282 in thermal contact with the line 214A.
[0133]
The steam drain heat exchanger 230 is interposed in a region 283 that bypasses the low-temperature solution heat exchanger 300 of the absorption solution line 282 at the branch portion 282B and the junction portion 283G in thermal contact with the line 214A.
[0134]
The steam drain heat exchanger 232 is interposed in a region 235 between the absorber 208 and the branch 282B of the absorption solution line 282 in thermal contact with the line 214A.
[0135]
In each of the steam drain heat exchangers 220, 222, 223A, 224, 226, 227, 228, 230, 232, the temperature of the drain passing through these is higher than the temperature of the absorbing solution line 234 that is thermally paired. It is a necessary condition. Therefore, one of the steam drain heat exchangers 220, 222, 223A, 224, 226, 227, 228, 230, 232 depending on the temperature condition of the absorption chiller / heater SP15, the air conditioning load, the temperature of the heated steam, the outside air conditions, and the like. Any one or more including one or all of the numbers are interposed.
[0136]
The operation of the absorption chiller / heater SP15 will be described with respect to an example in which all of the steam drain heat exchangers 220, 222, 223A, 224, 226, 227, 228, 230, and 232 are interposed.
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 282 by the pump 102 is heated by the steam drain heat exchanger 232 to rise in temperature, and is branched at the branching portion 282B. And the other diluted absorbent solution Li is directly passed through the low-temperature solution heat exchanger 300 and heated to rise in temperature at the junction 283G. Join.
[0137]
The branching ratio of the absorbing solution Li at the branching portion 282B is such that the total amount of heat received from the low-temperature solution heat exchanger 300 and the heat received from the steam drain heat exchanger 230 is maximized, and the absorbing solution at the junction 283G. Distribution is performed so that the Li temperature becomes maximum.
[0138]
The diluted absorbent solution Li that has passed through the merging portion 283G passes through the steam drain heat exchanger 228 and is heated to rise in temperature. At the branch portion 308, one is directed to the low-temperature regenerator 206 through the absorbent solution line 306. The other goes straight through the absorption solution line 282, is heated by the steam drain heat exchanger 227, rises in temperature, and goes to the branch 240B.
[0139]
One of the diluted absorbent solutions Li branched at the branch 240B passes through the region 244 and is heated by the steam drain heat exchanger 226 to increase the temperature, and the other diluted absorbent solution Li at the branch 240B is the intermediate temperature solution heat exchanger. It passes through 302 and is heated to rise in temperature, and merges at the junction 242G.
[0140]
The branching ratio of the absorbing solution Li at the branching portion 240B is the same as the branching procedure at the branching portion 282B.
The diluted absorbent solution Li that has passed through the junction 242G passes through the steam drain heat exchanger 224 and is heated to rise in temperature, branching off at the branching section 311 and one into the medium temperature regenerator 204 and the other into the high temperature regenerator 202. Head.
[0141]
The diluted absorbent solution Li branched from the branch section 311 and directed to the absorbent solution line 310 is concentrated by heating the first refrigerant vapor line 216 in the intermediate temperature regenerator 204.
The diluted absorbent solution Li toward the high-temperature regenerator 202 is heated by the steam drain heat exchanger 223A to increase the temperature, and proceeds to the branching portion 246B.
[0142]
One of the diluted absorbent solutions Li branched at the branch portion 246B passes through the region 250 and is heated by the steam drain heat exchanger 222 to be heated, and the other diluted absorbent solution Li at the branch portion 246B is heated at the high temperature solution heat exchanger. It passes through 304, is heated and heated up, and merges at the junction 246G.
[0143]
The branching ratio of the absorbing solution Li at the branching portion 246B is the same as the branching procedure at the branching portion 282B and the branching portion 240B.
[0144]
The absorbing solution Li that has passed through the merging portion 246 </ b> G passes through the steam drain heat exchanger 220, is heated and heated, and is introduced into the high-temperature regenerator 202.
[0145]
The diluted absorbent solution Li containing the refrigerant solution is heated by the steam St by the heating steam line 214 in the high-temperature regenerator 202, and the concentrated absorbent solution Li separated and concentrated using the refrigerant solution as the vapor is heated by the absorbent solution line 340. The solution heat exchanger 304 radiates heat toward the intermediate temperature regenerator 204.
[0146]
The concentrated absorbent solution Li separated and concentrated by the intermediate temperature regenerator 204 as a vapor is radiated by the intermediate solution heat exchanger 302 through the absorbent solution line 318 and merged with the absorbent solution line 306 toward the low temperature regenerator 206. .
The absorption solution concentrated by the low temperature regenerator 206 is radiated by the low temperature solution heat exchanger 300 and directed to the absorber 208.
[0147]
As for the movement of the refrigerant, the absorption solution is heated by the intermediate temperature regenerator 204 through the first refrigerant vapor line 216 as a vapor having a high heat quantity after being evaporated and separated from the diluted absorption solution Li by the high temperature regenerator 202. In addition, the refrigerant vapor evaporated and separated by the intermediate temperature regenerator 204 also releases heat by the low temperature regenerator 206 through the second refrigerant vapor line 218.
[0148]
The refrigerant vapor evaporated and separated by the low temperature regenerator 202 is condensed by the condenser 210 together with the vapor from the intermediate temperature regenerator 204, and evaporated by the evaporator 212 to exchange heat with an external fluid. In addition, the refrigerant exchanges heat with the external fluid in the absorber 208.
[0149]
In this way, the heat efficiency of the absorption chiller / heater SP15 is improved by making full use of the amount of heat of the steam through the heating steam line 214.
[0150]
FIG. 8 shows a configuration of another series parallel flow type absorption chiller / heater SP20 according to the eighth embodiment. A different part from the embodiment of FIG. 7 will be mainly described.
A heating steam line 214 leading to an external heat source is connected to the high-temperature regenerator 202, and the heating steam line 214 becomes a line 214A via the heating of the high-temperature regenerator 202 and is connected to a steam drain heat exchanger described below. Connected to the steam source.
[0151]
The steam drain heat exchanger 227C includes a high temperature solution heat exchanger 304, a medium temperature solution heat exchanger 302, a low temperature solution heat exchanger 300, a branch portion 308, and a branch portion 311 of the absorption solution line 282, and a branch portion 282B and a junction portion 287G. In the region 251S to be bypassed, the line 214A is in thermal contact with the region 251S.
[0152]
The communication relationship of the steam drain heat exchanger 227C to the steam drain heat exchangers 232 and 220 mounted before and after the steam drain heat exchanger 227C is the same as that of the embodiment of FIG. In other words, the steam drain heat exchanger 227C is interposed instead of the steam drain heat exchangers 222, 223A, 224, 226, 227, 228, 230 in FIG.
Except for the above, the configuration is the same as in FIG.
[0153]
The operation of the absorption chiller / heater SP20 will be described mainly in the vicinity where the steam drain heat exchanger 227C is interposed.
The low-temperature diluted absorbent solution Li containing the refrigerant discharged from the absorber 208 to the absorbent solution line 282 by the pump 102 is heated by the steam drain heat exchanger 232 to be heated and branched at the branch portion 282B. It is heated by the drain heat exchanger 227C and heated to the joining portion 287G.
[0154]
The other diluted absorption solution Li that goes straight at the branching portion 282B passes through the low-temperature solution heat exchanger 300 and is heated to rise in temperature, and at the branching portion 308, one goes to the low-temperature regenerator 206 and the other goes straight to the high-temperature regeneration. Head to vessel 202.
[0155]
The diluted absorbent solution Li toward the high temperature regenerator 202 is heated by the intermediate temperature solution heat exchanger 302 to be heated, branched at the branching section 311, one is directed to the intermediate temperature regenerator 204, and the other is directed to the high temperature regenerator. The temperature is increased by heating at 304, and the diluted absorption solution Li that has passed through the steam drain heat exchanger 227 </ b> C is merged at the junction 287 </ b> G and is directed to the high-temperature regenerator 202.
[0156]
The absorbing solution Li directed from the junction 287G to the high temperature regenerator 202 is heated by the steam drain heat exchanger 220, heated, and introduced into the high temperature regenerator 202.
The operation of the concentrated absorbent solution and the refrigerant vapor via the high temperature regenerator 202, the medium temperature regenerator 204, the low temperature regenerator 206, etc. is the same as in FIG.
[0157]
As described above, according to the heat distribution characteristics of the absorption chiller / heater, the number of steam drain heat exchangers is reduced and the thermal efficiency is improved.
[0158]
It should be noted that the eight illustrated embodiments are merely examples, and are not intended to limit the technical scope of the present invention.
For example, in the drawing, only representative ones of various flow types (for example, series flow, parallel flow, reverse flow, series / parallel flow, reverse / parallel flow) are shown, but the present invention also applies to a flow pattern (not shown). Can be used.
Further, many embodiments in which a refrigerant drain heat exchanger is arranged, the lower body is provided in a plurality of stages, and a solution cooling absorber is provided are also conceivable.
[0159]
【The invention's effect】
The effects of the present invention are listed below.
(1) According to the present invention, since the diluted absorption solution is heated using the heating steam used in the high-temperature regenerator in the plurality of steam drain heat exchangers, the heat recovery is large.
(2) Since the refrigerant vapor generated by evaporation in the regenerator is used for heating the low-temperature regenerator and the low-temperature diluted absorbent solution, heat recovery is further increased.
(3) Since the refrigerant drain is passed through the refrigerant drain heat exchanger and the diluted absorption refrigerant is heated, the heat recovery is increased.
(4) Further, if the lower body portion of the evaporator and the absorber is divided into a plurality of stages, the function is improved and the thermal efficiency is improved.
(5) If a solution cooling absorber is provided in the absorber, the amount of heat of the dripped absorbing solution from the regenerator can be recovered.
[Brief description of the drawings]
FIG. 1 is a configuration diagram showing a series flow type absorption chiller / heater according to a first embodiment of the present invention.
FIG. 2 is a configuration diagram showing another series flow type absorption chiller / heater according to the second embodiment of the present invention.
FIG. 3 is a configuration diagram showing a reverse flow type absorption chiller / heater according to a third embodiment of the present invention.
FIG. 4 is a configuration diagram showing a reverse parallel flow type absorption chiller / heater according to a fourth embodiment of the present invention.
FIG. 5 is a configuration diagram showing a parallel flow type absorption chiller / heater according to a fifth embodiment of the present invention.
FIG. 6 is a block diagram showing another parallel flow type absorption chiller / heater according to the sixth embodiment of the present invention.
FIG. 7 is a block diagram showing a series parallel flow type absorption chiller / heater according to a seventh embodiment of the present invention.
FIG. 8 is a configuration diagram showing another series parallel flow type absorption chiller / heater according to the eighth embodiment of the present invention.
FIG. 9 is a block diagram showing a conventional series flow type absorption chiller / heater.
[Explanation of symbols]
202 ... high temperature regenerator
204 ... Medium temperature regenerator
206 ... low temperature regenerator
208 ... Absorber
210 ... Condenser
212 ... Evaporator
214, 214A ... Steam line for heating
220, 222, 224, 226, 228, 230, 232... Steam drain heat exchanger
234, 238, 240, 244, 246, 250, 252... Absorbing solution line

Claims (8)

高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、吸収器（２０８）から出た吸収溶液が、高温再生器（２０２）、中温再生器（２０４）、低温再生器（２０６）の順に流過する様に構成され、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）に向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（１０６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（１０８）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第７の蒸気ドレン熱交換器（２２０、２２２、２２４、２２６、２２８、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２４）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と第１の分岐点（２４６Ｂ）との間の領域（２４６）に介装され、
第４の蒸気ドレン熱交換器（２２６）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第３の蒸気ドレン熱交換器（２２４）の間の第２の合流点（２４２Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第５の蒸気ドレン熱交換器（２２８）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と第２の分岐点（２４０Ｂ）との間の領域（２４０）に介装され、
第６の蒸気ドレン熱交換器（２３０）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２３４Ｂ）で分岐する第３の分岐ライン（２３８）に介装されており、該第３の分岐ライン（２３８）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第５の蒸気ドレン熱交換器（２２８）の間の第３の合流点（２３６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第７の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２３４Ｂ）との間の領域（２３５）に介装されており、
第１〜第７の蒸気ドレン熱交換器（２２０、２２２、２２４、２２６、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212). The absorbent solution discharged from (208) flows through the high-temperature regenerator (202), the medium-temperature regenerator (204), and the low-temperature regenerator (206) in this order. The steam lines (214, 214A) communicate with each other, and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high-temperature regenerator (202) to regenerate the refrigerant steam. Has been
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the intermediate temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The medium temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (302) converts the amount of heat held by the absorption solution flowing through the absorption solution line (106) from the medium temperature regenerator (204) to the low temperature regenerator (206). 202), the low temperature solution heat exchanger (300) is held by the absorption solution flowing through the absorption solution line (108) from the low temperature regenerator (206) to the absorber (208). Is configured so as to be introduced into the absorbing solution towards the amount high temperature regenerator (202),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to seventh steam drain heat exchangers (220, 222, 224, 226, 228, 230, 232). )
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (222) is a first branch point between the intermediate solution heat exchanger (302) and the hot solution heat exchanger (304) of the absorption solution line toward the high temperature regenerator (202). (246B) is interposed in a first branch line (250) that bypasses the hot solution heat exchanger (304) and the hot solution heat exchanger (304). ) And the first steam drain heat exchanger (220) at the first junction (246G) and merged with the absorbent solution line toward the high temperature regenerator (202),
The third steam drain heat exchanger (224) is a region (246) between the intermediate solution heat exchanger (302) of the absorbing solution line and the first branch point (246B) toward the high temperature regenerator (202). Intervened in,
The fourth steam drain heat exchanger (226) is a second branch point between the cold solution heat exchanger (300) and the intermediate temperature solution heat exchanger (302) in the absorption solution line toward the high temperature regenerator (202). The second branch line (244) bypasses the intermediate temperature solution heat exchanger (302) and the intermediate temperature solution heat exchanger (302). ) And a third steam drain heat exchanger (224) at the second junction (242G) and merged with the absorbent solution line toward the high temperature regenerator (202),
The fifth steam drain heat exchanger (228) is a region (240) between the cold solution heat exchanger (300) and the second branch point (240B) of the absorption solution line toward the high temperature regenerator (202). Intervened in,
The sixth steam drain heat exchanger (230) is a third branch point (234B) between the absorbent solution pump (102) of the absorbent solution line and the cold solution heat exchanger (300) toward the high temperature regenerator (202). ) That is branched by a third branch line (238) that bypasses the low temperature solution heat exchanger (300) and is connected to the low temperature solution heat exchanger (300). Merging with the absorbent solution line towards the high temperature regenerator (202) at a third junction (236G) between the fifth steam drain heat exchanger (228);
The seventh steam drain heat exchanger (232) is interposed in a region (235) between the absorption solution pump (102) and the third branch point (234B) of the absorption solution line toward the high temperature regenerator (202). And
The first to seventh steam drain heat exchangers (220, 222, 224, 226, 228, 230, 232) are used for the heating steam or steam after the amount of heat is supplied to the absorbing solution in the high temperature regenerator (202). A steam-fired absorption chiller / heater characterized by being configured to input the amount of heat held by the drain into an absorption solution that leaves the absorber (208) and goes to the high-temperature regenerator (202). 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、吸収器（２０８）から出た吸収溶液が、高温再生器（２０２）、中温再生器（２０４）、低温再生器（２０６）の順に流過する様に構成され、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）に向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（１０６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（１０８）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１の蒸気ドレン熱交換器（２２０）と、第２の蒸気ドレン熱交換器（２３２）と、第３の蒸気ドレン熱交換器（２２５）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域に介装されており、
第３の蒸気ドレン熱交換器（２２５）は、高温再生器（２０２）に向う吸収溶液ラインの第２の蒸気ドレン熱交換器（２３２）と低温溶液熱交換器（３００）の間における分岐点（２３４Ｂ）で分岐する分岐ライン（２３６Ｑ）に介装されており、該分岐ライン（２３６Ｑ）は低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第１の蒸気ドレン熱交換器（２２０）と第２の蒸気ドレン熱交換器（２３２）と第３の蒸気ドレン熱交換器（２２５）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212). The absorbent solution discharged from (208) flows through the high-temperature regenerator (202), the medium-temperature regenerator (204), and the low-temperature regenerator (206) in this order. The steam lines (214, 214A) communicate with each other, and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high-temperature regenerator (202) to regenerate the refrigerant steam. Has been
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the intermediate temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The medium temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (302) converts the amount of heat held by the absorption solution flowing through the absorption solution line (106) from the medium temperature regenerator (204) to the low temperature regenerator (206). 202), the low temperature solution heat exchanger (300) is held by the absorption solution flowing through the absorption solution line (108) from the low temperature regenerator (206) to the absorber (208). Is configured so as to be introduced into the absorbing solution towards the amount high temperature regenerator (202),
A region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) includes a first steam drain heat exchanger (220) and a second steam drain heat exchanger (232). , Communicated with a third steam drain heat exchanger (225),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (232) is interposed in the region between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the high temperature regenerator (202). And
The third steam drain heat exchanger (225) is a bifurcation point between the second steam drain heat exchanger (232) and the cold solution heat exchanger (300) in the absorption solution line toward the high temperature regenerator (202). (234B), the branch line (236Q) is interposed between the low temperature solution heat exchanger (300), the intermediate temperature solution heat exchanger (302), and the high temperature solution heat exchanger (304). ) And join the absorbing solution line toward the high temperature regenerator (202) at the confluence (246G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The first steam drain heat exchanger (220), the second steam drain heat exchanger (232), and the third steam drain heat exchanger (225) transfer heat to the absorbing solution in the high temperature regenerator (202). Steam heating characterized by being configured so that the amount of heat held by the heating steam or steam drain after charging is supplied to the absorbing solution exiting from the absorber (208) toward the high temperature regenerator (202). Absorption chiller / heater. 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、吸収器（２０８）から出た吸収溶液が、低温再生器（２０６）、中温再生器（２０４）、高温再生器（２０２）の順に流過する様に構成されており、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ライン（２３６）には低温溶液熱交換器（３００）が介装され、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（２４２）には中温溶液熱交換器（３０２）が介装され、中温溶液熱交換器（３０２）から高温再生器（２０２）に向う吸収溶液ライン（２４８）には高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）から吸収器（２０８）に向う吸収溶液ライン（１１０）を流れる吸収溶液が保有する熱量を投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの中温再生器（２０４）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２４Ａ）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの中温再生器（２０４）と第１の分岐点（２４６Ｂ）との間の領域（３８６）に介装され、
第４の蒸気ドレン熱交換器（２２４Ｂ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（３８４）の中温溶液熱交換器（３０２）と中温再生器（２０４）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの低温再生器（２０６）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４Ｂ）の間の第２の合流点（２４２Ｇ）で低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２８Ａ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの低温再生器（２０６）と第２の分岐点（２４０Ｂ）との間の領域（３８４）に介装され、
第７の蒸気ドレン熱交換器（２２８Ｂ）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの低温溶液熱交換器（３００）と低温再生器（２０６）との間の領域（３８２）に介装され、
第８の蒸気ドレン熱交換器（２３０）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２３４Ｂ）で分岐する第３の分岐ライン（２３８）に介装されており、該第３の分岐ライン（２３８）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８Ｂ）の間の第３の合流点（２３６Ｇ）で吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２３４Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４Ａ、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212). The absorbent solution discharged from (208) flows through the low-temperature regenerator (206), the medium-temperature regenerator (204), and the high-temperature regenerator (202) in this order. The heating steam lines (214, 214A) communicate with each other so that the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high-temperature regenerator (202) to regenerate the refrigerant steam. Is composed of
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
The absorption solution line (236) from the absorber (208) to the low temperature regenerator (206) is provided with a low temperature solution heat exchanger (300), and the low temperature regenerator (206) goes to the medium temperature regenerator (204). A medium temperature solution heat exchanger (302) is interposed in the absorption solution line (242), and a high temperature solution heat exchange is performed in the absorption solution line (248) from the medium temperature solution heat exchanger (302) to the high temperature regenerator (202). A heat exchanger (304) is interposed, and is configured to input the amount of heat held by the absorbent solution flowing through the absorbent solution line (110) from the high-temperature solution heat exchanger (304) toward the absorber (208),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 224A, 224B, 226, 228A, 228B). , 230, 232),
The first steam drain heat exchanger (220) is between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). Intervened in the region (252),
The second steam drain heat exchanger (222) is between the intermediate temperature regenerator (204) and the high temperature solution heat exchanger (304) of the absorbent solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). A first branch line (250) that branches at a first branch point (246B) is interposed between the first branch line (250) and the hot solution heat exchanger (304). Join the absorbent solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202) at a first junction (246G) between the heat exchanger (304) and the first steam drain heat exchanger (220). And
The third steam drain heat exchanger (224A) is located between the intermediate temperature regenerator (204) of the absorbing solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202) and the first branch point (246B). In the region (386) of
The fourth steam drain heat exchanger (224B) includes an intermediate solution heat exchanger (302) and an intermediate temperature regenerator (204) in the absorption solution line (384) from the low temperature regenerator (206) to the intermediate temperature regenerator (204). Intervened in the area between and
The fifth steam drain heat exchanger (226) is between the low temperature regenerator (206) and intermediate temperature solution heat exchanger (302) of the absorption solution line from the low temperature regenerator (206) to the medium temperature regenerator (204). A second branch line (244) that branches at the second branch point (240B) is interposed between the second branch line (244) and the intermediate temperature solution heat exchanger (302). Join the absorbent solution line from the low temperature regenerator (206) to the medium temperature regenerator (204) at the second confluence (242G) between the heat exchanger (302) and the fourth steam drain heat exchanger (224B). And
The sixth steam drain heat exchanger (228A) is located between the cold regenerator (206) of the absorbent solution line from the low temperature regenerator (206) to the medium temperature regenerator (204) and the second branch point (240B). In the region (384) of
The seventh steam drain heat exchanger (228B) is between the low temperature solution heat exchanger (300) and the low temperature regenerator (206) of the absorption solution line from the absorber (208) to the low temperature regenerator (206). In the region (382),
The eighth steam drain heat exchanger (230) is located between the absorbent solution pump (102) and the cold solution heat exchanger (300) in the absorbent solution line from the absorber (208) to the cold regenerator (206). Is interposed in a third branch line (238) that branches at the third branch point (234B), the third branch line (238) bypassing the low temperature solution heat exchanger (300) and the low temperature solution heat Joins the absorbent solution line from the absorber (208) to the cold regenerator (206) at a third junction (236G) between the exchanger (300) and the seventh steam drain heat exchanger (228B);
The ninth steam drain heat exchanger (232) is between the absorbent solution pump (102) and the third branch point (234B) of the absorbent solution line from the absorber (208) to the cold regenerator (206). Intervened in the region (235),
The first to ninth steam drain heat exchangers (220, 222, 224A, 224B, 226, 228A, 228B, 230, 232) are heated by supplying heat to the absorbing solution in the high temperature regenerator (202). A steam-fired absorption chiller / heater characterized by being configured so that the amount of heat held by the steam or steam drain is put into an absorbing solution that exits from the absorber (208) and goes to the high-temperature regenerator (202). 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）を出た吸収溶液が低温再生器（２０６）、中温再生器（２０４）、高温再生器（２０２）の順に流過する様に構成され且つ高温再生器（２０２）と吸収器（２０８）とを連通する吸収溶液ライン（２６０）を有し、低温再生器（２０６）と中温再生器（２０４）とを連通する吸収溶液ライン（２６２）から分岐（２６４）し且つ高温再生器（２０２）と吸収器（２０８）とを連通する前記吸収溶液ライン（２６０）と合流（２６６）する第１の分岐吸収溶液ライン（２６８）を有し、中温再生器（２０４）と高温再生器（２０２）とを連通する吸収溶液ライン（２７０）から分岐（２７２）し且つ高温再生器（２０２）と吸収器（２０８）とを連通する前記吸収溶液ライン（２６０）と合流（２７４）する第２の分岐吸収溶液ライン（２７６）を有し、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ライン（２３６）には低温溶液熱交換器（３００）が介装され、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（２４２）には中温溶液熱交換器（３０２）が介装され、中温溶液熱交換器（３０２）から高温再生器（２０２）に向う吸収溶液ライン（２４８）には高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）から吸収器（２０８）に向う吸収溶液ライン（１１０）を流れる吸収溶液が保有する熱量を投入する様に構成され、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（２７６）の分岐部（２７２）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２４）は、中温再生器（２０４）から高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（２７６）の分岐部（２７２）と第１の分岐点（２４６Ｂ）との間の領域に介装され、
第４の蒸気ドレン熱交換器（２２４Ｂ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ライン（３８４）の中温溶液熱交換器（３０２）と中温再生器（２０４）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（２６８）の分岐部（２６４）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４Ｂ）の間の第２の合流点（２４２Ｇ）で低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２８Ａ）は、低温再生器（２０６）から中温再生器（２０４）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（２６８）の分岐部（２６４）と第２の分岐点（２４０Ｂ）との間の領域に介装され、
第７の蒸気ドレン熱交換器（２２８Ｂ）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの低温溶液熱交換器（３００）と低温再生器（２０６）との間の領域（３８２）に介装され、
第８の蒸気ドレン熱交換器（２３０）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２３４Ｂ）で分岐する第３の分岐ライン（２３８）に介装されており、該第３の分岐ライン（２３８）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８Ｂ）の間の第３の合流点（２３６Ｇ）で吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、吸収器（２０８）から低温再生器（２０６）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２３４Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２４、２２４Ｂ、２２６、２２８Ａ、２２８Ｂ、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212) are provided. The heating steam line (214, 214A) communicates with the vessel (202), and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high temperature regenerator (202). It is configured to regenerate the refrigerant vapor,
The absorbent solution exiting the absorber (208) flows through the low temperature regenerator (206), the medium temperature regenerator (204), and the high temperature regenerator (202) in this order, and the high temperature regenerator (202) and the absorber. An absorbent solution line (260) that communicates with (208), branches (264) from the absorbent solution line (262) that communicates between the low temperature regenerator (206) and the intermediate temperature regenerator (204), and a high temperature regenerator The intermediate solution regenerator (204) and the high temperature regenerator have a first branched absorbent solution line (268) that merges (266) with the absorption solution line (260) that communicates between the (202) and the absorber (208). Branching (272) from the absorbing solution line (270) communicating with (202) and joining (274) the absorbing solution line (260) communicating with the high temperature regenerator (202) and the absorber (208). 2 branched absorption solution It has a line (276),
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
The absorption solution line (236) from the absorber (208) to the low temperature regenerator (206) is provided with a low temperature solution heat exchanger (300), and the low temperature regenerator (206) goes to the medium temperature regenerator (204). A medium temperature solution heat exchanger (302) is interposed in the absorption solution line (242), and a high temperature solution heat exchange is performed in the absorption solution line (248) from the medium temperature solution heat exchanger (302) to the high temperature regenerator (202). A heat exchanger (304) is interposed, and is configured to input the amount of heat held by the absorbent solution flowing through the absorbent solution line (110) from the high-temperature solution heat exchanger (304) toward the absorber (208),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 224, 224B, 226, 228A, 228B). , 230, 232),
The first steam drain heat exchanger (220) is between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). Intervened in the region (252),
The second steam drain heat exchanger (222) is connected to the branch (272) of the second branched absorbent solution line (276) of the absorbent solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202) and the high temperature. The first branch line (250) is branched at a first branch point (246B) between the solution heat exchangers (304), and the first branch line (250) The hot regenerator from the intermediate temperature regenerator (204) at the first junction (246G) bypassing the regenerator (304) and between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220) Merge with the absorbent solution line towards (202),
The third steam drain heat exchanger (224) includes a branch (272) and a second branch absorption solution line (276) of the absorption solution line from the intermediate temperature regenerator (204) to the high temperature regenerator (202). Intervened in the area between 1 branch point (246B),
The fourth steam drain heat exchanger (224B) includes an intermediate solution heat exchanger (302) and an intermediate temperature regenerator (204) in the absorption solution line (384) from the low temperature regenerator (206) to the intermediate temperature regenerator (204). Intervened in the area between and
The fifth steam drain heat exchanger (226) is connected to the bifurcation (264) of the first branched absorbent solution line (268) and the intermediate temperature of the absorbent solution line from the low temperature regenerator (206) to the intermediate temperature regenerator (204). It is interposed in a second branch line (244) that branches at a second branch point (240B) between the solution heat exchangers (302), and the second branch line (244) is an intermediate temperature solution heat exchanger. From the low temperature regenerator (206) to the intermediate temperature regenerator at a second junction (242G) bypassing the regenerator (302) and between the intermediate temperature solution heat exchanger (302) and the fourth steam drain heat exchanger (224B) Merge with the absorbent solution line towards (204),
The sixth steam drain heat exchanger (228A) includes a first branch absorption solution line (268) branching portion (264) and an absorption solution line from the low temperature regenerator (206) to the medium temperature regenerator (204). Is interposed in the area between the two branch points (240B),
The seventh steam drain heat exchanger (228B) is between the low temperature solution heat exchanger (300) and the low temperature regenerator (206) of the absorption solution line from the absorber (208) to the low temperature regenerator (206). In the region (382),
The eighth steam drain heat exchanger (230) is located between the absorbent solution pump (102) and the cold solution heat exchanger (300) in the absorbent solution line from the absorber (208) to the cold regenerator (206). Is interposed in a third branch line (238) that branches at the third branch point (234B), the third branch line (238) bypassing the low temperature solution heat exchanger (300) and the low temperature solution heat Joins the absorbent solution line from the absorber (208) to the cold regenerator (206) at a third junction (236G) between the exchanger (300) and the seventh steam drain heat exchanger (228B);
The ninth steam drain heat exchanger (232) is between the absorbent solution pump (102) and the third branch point (234B) of the absorbent solution line from the absorber (208) to the cold regenerator (206). Intervened in the region (235),
The first to ninth steam drain heat exchangers (220, 222, 224, 224B, 226, 228A, 228B, 230, 232) are used to heat the absorption solution in the high-temperature regenerator (202) after the amount of heat is supplied thereto. A steam-fired absorption chiller / heater characterized by being configured so that the amount of heat possessed by the steam or steam drain is put into an absorbing solution that exits from the absorber (208) and goes to the high-temperature regenerator (202). 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から出た吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（３１４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（３１６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８４、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）から吸収器（２０８）に向かう吸収溶液ライン（３１２、３１４、３１６）には、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ライン（３１８）が合流（３２０）しており、且つ、低温再生器（２０６）で加熱された吸収溶液が流れる吸収溶液ライン（３２２）が合流（３２４）しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２３Ａ）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と第１の分岐点（２４６Ｂ）との間の領域（２８６）に介装され、
第４の蒸気ドレン熱交換器（２２４）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４）の間の第２の合流点（２４２Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２７）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と第２の分岐点（２４０Ｂ）との間の領域（２８４）に介装され、
第７の蒸気ドレン熱交換器（２２８）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）との間の領域に介装され、
第８の蒸気ドレン熱交換器（２３０）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２８２Ｂ）で分岐する第３の分岐ライン（２８３）に介装されており、該第３の分岐ライン（２８３）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８）の間の第３の合流点（２８３Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２８２Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212) are provided. The heating steam line (214, 214A) communicates with the vessel (202), and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high temperature regenerator (202). It is configured to regenerate the refrigerant vapor,
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) is configured to input the amount of heat held by the absorption solution flowing through the absorption solution line (104) from the high temperature regenerator (202) into the absorption solution toward the high temperature regenerator (202). The intermediate temperature solution heat exchanger (302) absorbs the amount of heat held by the absorption solution flowing in the absorption solution line (314) from the intermediate temperature regenerator (204) toward the low temperature regenerator (206) toward the high temperature regenerator (202). The low-temperature solution heat exchanger (300) is configured to supply the amount of heat held by the absorption solution flowing through the absorption solution line (316) from the low-temperature regenerator (206) to the absorber (208). 20 Is configured so as to be introduced into the absorption solution toward the),
An absorbent solution line (282, 284, 286) communicating from the absorber (208) to the high temperature regenerator (202) is located in the region between the low temperature solution heat exchanger (300) and the medium temperature solution heat exchanger (302). A first branch absorption solution line (306) communicating with the low temperature regenerator (206) is branched (308), and a region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the intermediate temperature regenerator (204) is branched (311), and the absorption solution lines (312, 314) from the high temperature regenerator (202) to the absorber (208) are branched. 316), the absorption solution line (318) through which the absorption solution heated by the intermediate temperature regenerator (204) flows joins (320), and the absorption solution heated by the low temperature regenerator (206) Flowing absorbent solution Emissions (322) is joined (324),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228). , 230, 232),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (222) includes a branch (311) of the second branched absorbent solution line (310) and a high temperature solution heat exchanger (304) of the absorbent solution line toward the high temperature regenerator (202). The first branch line (250) branches at a first branch point (246B) between the first branch line (250B) and bypasses the hot solution heat exchanger (304). And merged with the absorption solution line toward the high temperature regenerator (202) at a first junction (246G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The third steam drain heat exchanger (223A) includes a branch (311) and a first branch point (246B) of the second branched absorbent solution line (310) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the area (286) between
The fourth steam drain heat exchanger (224) includes a middle temperature solution heat exchanger (302) of the absorption solution line toward the high temperature regenerator (202) and a branch (311) of the second branch absorption solution line (310). Intervened in the area between and
The fifth steam drain heat exchanger (226) includes a branch (308) of the first branched absorbent solution line (306) and an intermediate temperature solution heat exchanger (302) of the absorbent solution line toward the high temperature regenerator (202). Is interposed in a second branch line (244) that branches at a second branch point (240B) between the two, and the second branch line (244) bypasses the intermediate temperature solution heat exchanger (302). And at the second junction (242G) between the intermediate temperature solution heat exchanger (302) and the fourth steam drain heat exchanger (224), joins the absorption solution line toward the high temperature regenerator (202),
The sixth steam drain heat exchanger (227) includes a branch (308) and a second branch point (240B) of the first branched absorbent solution line (306) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the region (284) between
The seventh steam drain heat exchanger (228) includes a low temperature solution heat exchanger (300) of the absorption solution line toward the high temperature regenerator (202) and a branch (308) of the first branch absorption solution line (306). Intervened in the area between and
The eighth steam drain heat exchanger (230) has a third branch point (282B) between the absorbent solution pump (102) of the absorbent solution line and the cold solution heat exchanger (300) toward the high temperature regenerator (202). ) Is branched to a third branch line (283), which bypasses the low temperature solution heat exchanger (300) and is connected to the low temperature solution heat exchanger (300). Merging with the absorbent solution line towards the high temperature regenerator (202) at a third junction (283G) between the seventh steam drain heat exchanger (228);
The ninth steam drain heat exchanger (232) is interposed in the region (235) between the absorption solution pump (102) and the third branch point (282B) of the absorption solution line toward the high temperature regenerator (202). And
The first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228, 230, 232) are used to heat the absorbing solution in the high-temperature regenerator (202) after the amount of heat is supplied thereto. A steam-fired absorption chiller / heater characterized by being configured so that the amount of heat held by the steam or steam drain is put into an absorbing solution that exits from the absorber (208) and goes to the high-temperature regenerator (202). 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から出た吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（３１４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（３１６）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８４、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）から吸収器（２０８）に向かう吸収溶液ライン（３１２、３１４、３１６）には、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ライン（３１８）が合流（３２０）しており、且つ、低温再生器（２０６）で加熱された吸収溶液が流れる吸収溶液ライン（３２２）が合流（３２４）しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域（２８２）に介装されており、
第３の蒸気ドレン熱交換器（２２７Ｃ）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域（２８２）における分岐点（２８２Ｂ）で分岐する分岐ライン（２５１Ｓ）に介装されており、該分岐ライン（２５１Ｓ）は低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の合流点（２８７Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212) are provided. The heating steam line (214, 214A) communicates with the vessel (202), and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high temperature regenerator (202). It is configured to regenerate the refrigerant vapor,
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202), The high temperature solution heat exchanger (304) is configured to input the amount of heat held by the absorption solution flowing through the absorption solution line (104) from the high temperature regenerator (202) into the absorption solution toward the high temperature regenerator (202). The intermediate temperature solution heat exchanger (302) absorbs the amount of heat held by the absorption solution flowing in the absorption solution line (314) from the intermediate temperature regenerator (204) toward the low temperature regenerator (206) toward the high temperature regenerator (202). The low-temperature solution heat exchanger (300) is configured to supply the amount of heat held by the absorption solution flowing through the absorption solution line (316) from the low-temperature regenerator (206) to the absorber (208). 20 Is configured so as to be introduced into the absorption solution toward the),
An absorbent solution line (282, 284, 286) communicating from the absorber (208) to the high temperature regenerator (202) is located in the region between the low temperature solution heat exchanger (300) and the medium temperature solution heat exchanger (302). A first branch absorption solution line (306) communicating with the low temperature regenerator (206) is branched (308), and a region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the intermediate temperature regenerator (204) is branched (311), and the absorption solution lines (312, 314) from the high temperature regenerator (202) to the absorber (208) are branched. 316), the absorption solution line (318) through which the absorption solution heated by the intermediate temperature regenerator (204) flows joins (320), and the absorption solution heated by the low temperature regenerator (206) Flowing absorbent solution Emissions (322) is joined (324),
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) communicates with the first to third steam drain heat exchangers (220, 232, 227C),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (232) is interposed in an area (282) between the absorbent solution pump (102) and the cold solution heat exchanger (300) of the absorbent solution line toward the high temperature regenerator (202). And
The third steam drain heat exchanger (227C) is a branch in the region (282) between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the hot regenerator (202). The branch line (251S) is branched at a point (282B), and the branch line (251S) includes a low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger ( 304) and joins the absorbent solution line toward the high temperature regenerator (202) at the junction (287G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The first to third steam drain heat exchangers (220, 232, 227C) absorb the amount of heat held by the heating steam or the steam drain after charging the amount of heat into the absorbing solution in the high-temperature regenerator (202). A steam-fired absorption chiller / heater, characterized in that it is configured to enter the absorbent solution exiting from the vessel (208) toward the high temperature regenerator (202). 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）へ向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ライン（３１８）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ライン（３２２）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）で加熱された吸収溶液が流れる吸収溶液ライン（３４０）は中温再生器（２０４）に連通しており、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ライン（３１８）は第１の分岐吸収溶液ライン（３０６）に合流して低温再生器（２０６）に連通しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２２２）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と高温溶液熱交換器（３０４）の間における第１の分岐点（２４６Ｂ）で分岐する第１の分岐ライン（２５０）に介装されており、該第１の分岐ライン（２５０）は高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の第１の合流点（２４６Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第３の蒸気ドレン熱交換器（２２３Ａ）は、高温再生器（２０２）に向う吸収溶液ラインの第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）と第１の分岐点（２４６Ｂ）との間の領域（２８６）に介装され、
第４の蒸気ドレン熱交換器（２２４）は、高温再生器（２０２）に向う吸収溶液ラインの中温溶液熱交換器（３０２）と第２の分岐吸収溶液ライン（３１０）の分岐部（３１１）との間の領域に介装され、
第５の蒸気ドレン熱交換器（２２６）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と中温溶液熱交換器（３０２）の間における第２の分岐点（２４０Ｂ）で分岐する第２の分岐ライン（２４４）に介装されており、該第２の分岐ライン（２４４）は中温溶液熱交換器（３０２）をバイパスし且つ中温溶液熱交換器（３０２）と第４の蒸気ドレン熱交換器（２２４）の間の第２の合流点（２４２Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第６の蒸気ドレン熱交換器（２２７）は、高温再生器（２０２）に向う吸収溶液ラインの第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）と第２の分岐点（２４０Ｂ）との間の領域に介装され、
第７の蒸気ドレン熱交換器（２２８）は、高温再生器（２０２）に向う吸収溶液ラインの低温溶液熱交換器（３００）と第１の分岐吸収溶液ライン（３０６）の分岐部（３０８）との間の領域に介装され、
第８の蒸気ドレン熱交換器（２３０）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）の間における第３の分岐点（２８２Ｂ）で分岐する第３の分岐ライン（２８３）に介装されており、該第３の分岐ライン（２８３）は低温溶液熱交換器（３００）をバイパスし且つ低温溶液熱交換器（３００）と第７の蒸気ドレン熱交換器（２２８）の間の第３の合流点（２８３Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第９の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と第３の分岐点（２８２Ｂ）との間の領域（２３５）に介装されており、
第１〜第９の蒸気ドレン熱交換器（２２０、２２２、２２３Ａ、２２４、２２６、２２７、２２８、２３０、２３２）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212) are provided. The heating steam line (214, 214A) communicates with the vessel (202), and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high temperature regenerator (202). It is configured to regenerate the refrigerant vapor,
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202). The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the medium temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The intermediate temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (302) converts the amount of heat held by the absorption solution flowing through the absorption solution line (318) from the intermediate temperature regenerator (204) to the low temperature regenerator (206). 202), the low temperature solution heat exchanger (300) is held by the absorption solution flowing through the absorption solution line (322) from the low temperature regenerator (206) to the absorber (208). Is configured so as to be introduced into the absorbing solution towards the amount high temperature regenerator (202),
An absorbent solution line (282, 286) communicating from the absorber (208) to the high temperature regenerator (202) is regenerated at a low temperature in the region between the low temperature solution heat exchanger (300) and the intermediate temperature solution heat exchanger (302). A first branched absorbent solution line (306) communicating with the vessel (206) branches off (308) and has a medium temperature in the region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the regenerator (204) is branched (311), and the absorption solution line (340) through which the absorption solution heated by the high temperature regenerator (202) flows is regenerated at a medium temperature. The absorbent solution line (318) through which the absorbent solution heated by the intermediate temperature regenerator (204) flows joins the first branched absorbent solution line (306) and is connected to the low temperature regenerator (206). )
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) is the first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228). , 230, 232),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (222) includes a branch (311) of the second branched absorbent solution line (310) and a high temperature solution heat exchanger (304) of the absorbent solution line toward the high temperature regenerator (202). The first branch line (250) branches at a first branch point (246B) between the first branch line (250B) and bypasses the hot solution heat exchanger (304). And merged with the absorption solution line toward the high temperature regenerator (202) at a first junction (246G) between the high temperature solution heat exchanger (304) and the first steam drain heat exchanger (220),
The third steam drain heat exchanger (223A) includes a branch (311) and a first branch point (246B) of the second branched absorbent solution line (310) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the area (286) between
The fourth steam drain heat exchanger (224) includes a middle temperature solution heat exchanger (302) of the absorption solution line toward the high temperature regenerator (202) and a branch (311) of the second branch absorption solution line (310). Intervened in the area between and
The fifth steam drain heat exchanger (226) includes a branch (308) of the first branched absorbent solution line (306) and an intermediate temperature solution heat exchanger (302) of the absorbent solution line toward the high temperature regenerator (202). Is interposed in a second branch line (244) that branches at a second branch point (240B) between the two, and the second branch line (244) bypasses the intermediate temperature solution heat exchanger (302). And at the second junction (242G) between the intermediate temperature solution heat exchanger (302) and the fourth steam drain heat exchanger (224), joins the absorption solution line toward the high temperature regenerator (202),
The sixth steam drain heat exchanger (227) includes a branch (308) and a second branch point (240B) of the first branched absorbent solution line (306) of the absorbent solution line toward the high temperature regenerator (202). Intervened in the area between and
The seventh steam drain heat exchanger (228) includes a low temperature solution heat exchanger (300) of the absorption solution line toward the high temperature regenerator (202) and a branch (308) of the first branch absorption solution line (306). Intervened in the area between and
The eighth steam drain heat exchanger (230) has a third branch point (282B) between the absorbent solution pump (102) of the absorbent solution line and the cold solution heat exchanger (300) toward the high temperature regenerator (202). ) Is branched to a third branch line (283), which bypasses the low temperature solution heat exchanger (300) and is connected to the low temperature solution heat exchanger (300). Merging with the absorbent solution line towards the high temperature regenerator (202) at a third junction (283G) between the seventh steam drain heat exchanger (228);
The ninth steam drain heat exchanger (232) is interposed in the region (235) between the absorption solution pump (102) and the third branch point (282B) of the absorption solution line toward the high temperature regenerator (202). And
The first to ninth steam drain heat exchangers (220, 222, 223A, 224, 226, 227, 228, 230, 232) are used to heat the absorbing solution in the high-temperature regenerator (202) after the amount of heat is supplied thereto. A steam-fired absorption chiller / heater characterized by being configured so that the amount of heat held by the steam or steam drain is put into an absorbing solution that exits from the absorber (208) and goes to the high-temperature regenerator (202). 高温再生器（２０２）と、中温再生器（２０４）と、低温再生器（２０６）と、吸収器（２０８）と、凝縮器（２１０）と、蒸発器（２１２）とを有し、高温再生器（２０２）には加熱用蒸気ライン（２１４、２１４Ａ）が連通し、加熱用蒸気ライン（２１４）を流過する蒸気が保有する熱量が高温再生器（２０２）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
高温再生器（２０２）で再生した蒸気が流過する第１の冷媒蒸気ライン（２１６）が中温再生器（２０４）に連通し、第１の冷媒蒸気ライン（２１６）を流過する冷媒蒸気が保有する熱量が中温再生器（２０４）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、中温再生器（２０４）で再生した蒸気が流過する第２の冷媒蒸気ライン（２１８）が低温再生器（２０６）に連通し、第２の冷媒蒸気ライン（２１８）を流過する冷媒蒸気が保有する熱量が低温再生器（２０６）内の吸収溶液に投入されて冷媒蒸気が再生する様に構成されており、
吸収器（２０８）から高温再生器（２０２）に向う吸収溶液ラインには低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）が介装され、高温溶液熱交換器（３０４）は高温再生器（２０２）から中温再生器（２０４）へ向う吸収溶液ライン（１０４）を流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、中温溶液熱交換器（３０２）は中温再生器（２０４）から低温再生器（２０６）に向う吸収溶液ラインを流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、低温溶液熱交換器（３００）は低温再生器（２０６）から吸収器（２０８）に向う吸収溶液ラインを流れる吸収溶液が保有する熱量を高温再生器（２０２）に向う吸収溶液に投入する様に構成され、
吸収器（２０８）から高温再生器（２０２）に連通する吸収溶液ライン（２８２、２８６）が、低温溶液熱交換器（３００）と中温溶液熱交換器（３０２）との間の領域で低温再生器（２０６）に連通する第１の分岐吸収溶液ライン（３０６）が分岐（３０８）しており、中温溶液熱交換器（３０２）と高温溶液熱交換器（３０４）との間の領域で中温再生器（２０４）に連通する第２の分岐吸収溶液ライン（３１０）が分岐（３１１）しており、高温再生器（２０２）で加熱された吸収溶液が流れる吸収溶液ライン（３４０）は中温再生器（２０４）に連通しており、中温再生器（２０４）で加熱された吸収溶液が流れる吸収溶液ラインは第１の分岐吸収溶液ライン（３０６）に合流して低温再生器（２０６）に連通しており、
前記加熱用蒸気ライン（２１４、２１４Ａ）の高温再生器（２０２）を経由した領域（２１４Ａ）は第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）に連通しており、
第１の蒸気ドレン熱交換器（２２０）は、高温再生器（２０２）に向う吸収溶液ラインの高温溶液熱交換器（３０４）と高温再生器（２０２）の間の領域（２５２）に介装され、
第２の蒸気ドレン熱交換器（２３２）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域に介装されており、
第３の蒸気ドレン熱交換器（２２７Ｃ）は、高温再生器（２０２）に向う吸収溶液ラインの吸収溶液ポンプ（１０２）と低温溶液熱交換器（３００）との間の領域における分岐点（２８２Ｂ）で分岐する分岐ライン（２５１Ｓ）に介装されており、該分岐ライン（２５１Ｓ）は低温溶液熱交換器（３００）、中温溶液熱交換器（３０２）、高温溶液熱交換器（３０４）をバイパスし且つ高温溶液熱交換器（３０４）と第１の蒸気ドレン熱交換器（２２０）の間の合流点（２８７Ｇ）で高温再生器（２０２）に向う吸収溶液ラインと合流し、
第１〜第３の蒸気ドレン熱交換器（２２０、２３２、２２７Ｃ）は、高温再生器（２０２）内の吸収溶液に熱量を投入した後に前記加熱用蒸気或いは蒸気ドレンが保有する熱量を、吸収器（２０８）から出て高温再生器（２０２）に向う吸収溶液に投入する様に構成されていることを特徴とする蒸気焚き吸収冷温水機。A high temperature regenerator (202), a medium temperature regenerator (204), a low temperature regenerator (206), an absorber (208), a condenser (210), and an evaporator (212) are provided. The heating steam line (214, 214A) communicates with the vessel (202), and the amount of heat held by the steam flowing through the heating steam line (214) is input to the absorbing solution in the high temperature regenerator (202). It is configured to regenerate the refrigerant vapor,
The first refrigerant vapor line (216) through which the steam regenerated in the high temperature regenerator (202) flows is communicated with the intermediate temperature regenerator (204), and the refrigerant vapor flowing through the first refrigerant vapor line (216) The second refrigerant vapor line in which the amount of heat held is input to the absorbing solution in the intermediate temperature regenerator (204) to regenerate the refrigerant vapor, and the regenerated vapor flows in the intermediate temperature regenerator (204). (218) communicates with the low-temperature regenerator (206), and the amount of heat held by the refrigerant vapor flowing through the second refrigerant vapor line (218) is input to the absorbing solution in the low-temperature regenerator (206) to generate refrigerant vapor. Is configured to play,
A low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304) are interposed in the absorption solution line from the absorber (208) to the high temperature regenerator (202). The high temperature solution heat exchanger (304) converts the amount of heat held by the absorption solution flowing in the absorption solution line (104) from the high temperature regenerator (202) to the medium temperature regenerator (204) into the absorption solution toward the high temperature regenerator (202). The medium temperature solution heat exchanger (302) is configured to be charged, and the high temperature regenerator (202) stores the amount of heat held by the absorption solution flowing in the absorption solution line from the medium temperature regenerator (204) toward the low temperature regenerator (206). The low-temperature solution heat exchanger (300) is configured so as to be charged into the absorbent solution facing away, and the high-temperature regenerator (300 2 Is configured so as to be introduced into the absorption solution toward the 2),
An absorbent solution line (282, 286) communicating from the absorber (208) to the high temperature regenerator (202) is regenerated at a low temperature in the region between the low temperature solution heat exchanger (300) and the intermediate temperature solution heat exchanger (302). A first branched absorbent solution line (306) communicating with the vessel (206) branches off (308) and has a medium temperature in the region between the medium temperature solution heat exchanger (302) and the high temperature solution heat exchanger (304). The second branch absorption solution line (310) communicating with the regenerator (204) is branched (311), and the absorption solution line (340) through which the absorption solution heated by the high temperature regenerator (202) flows is regenerated at a medium temperature. The absorbent solution line through which the absorbent solution heated by the intermediate temperature regenerator (204) flows joins the first branched absorbent solution line (306) and communicates with the low temperature regenerator (206). And
The region (214A) of the heating steam line (214, 214A) through the high temperature regenerator (202) communicates with the first to third steam drain heat exchangers (220, 232, 227C),
The first steam drain heat exchanger (220) is interposed in a region (252) between the high temperature solution heat exchanger (304) and the high temperature regenerator (202) of the absorption solution line toward the high temperature regenerator (202). And
The second steam drain heat exchanger (232) is interposed in the region between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the high temperature regenerator (202). And
The third steam drain heat exchanger (227C) is a branch point (282B) in the region between the absorbing solution pump (102) and the cold solution heat exchanger (300) of the absorbing solution line toward the high temperature regenerator (202). ), And the branch line (251S) includes a low temperature solution heat exchanger (300), a medium temperature solution heat exchanger (302), and a high temperature solution heat exchanger (304). Bypass and join the absorbent solution line towards the hot regenerator (202) at the junction (287G) between the hot solution heat exchanger (304) and the first steam drain heat exchanger (220);
The first to third steam drain heat exchangers (220, 232, 227C) absorb the amount of heat held by the heating steam or the steam drain after charging the amount of heat into the absorbing solution in the high-temperature regenerator (202). A steam-fired absorption chiller / heater, characterized in that it is configured to enter the absorbent solution exiting from the vessel (208) toward the high temperature regenerator (202).
JP2001090591A 2001-03-27 2001-03-27 Steam fired absorption chiller / heater Expired - Fee Related JP3791831B2 (en)

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