JP6337055B2 - Absorption heat pump - Google Patents

Absorption heat pump Download PDF

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JP6337055B2
JP6337055B2 JP2016173978A JP2016173978A JP6337055B2 JP 6337055 B2 JP6337055 B2 JP 6337055B2 JP 2016173978 A JP2016173978 A JP 2016173978A JP 2016173978 A JP2016173978 A JP 2016173978A JP 6337055 B2 JP6337055 B2 JP 6337055B2
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liquid
temperature
heat transfer
absorber
heated
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JP2017072360A (en
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與四郎 竹村
與四郎 竹村
宏幸 山田
宏幸 山田
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荏原冷熱システム株式会社
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B37/00—Absorbers; Adsorbers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B30/00—Heat pumps
    • F25B30/04—Heat pumps of the sorption type
    • 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

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)

Description

本発明は吸収ヒートポンプに関し、特に伝熱管内の被加熱媒体が伝熱管から過剰に流出してしまうことを抑制する吸収ヒートポンプに関する。   The present invention relates to an absorption heat pump, and more particularly to an absorption heat pump that suppresses an excessively heated medium in a heat transfer tube from flowing out of the heat transfer tube.

駆動熱源温度より高い温度の被加熱媒体を取り出す熱源機械として、吸収ヒートポンプがある。吸収ヒートポンプは、冷媒液を蒸発させる蒸発器、冷媒蒸気を吸収液で吸収させる吸収器、吸収液から冷媒を離脱させる再生器、冷媒蒸気を凝縮させる凝縮器を主要構成として備えている。吸収ヒートポンプの一例として、吸収器内の伝熱管との間で被加熱媒体を循環させるように接続された気液分離器を備え、気液分離器内の液面の液位を所定レベルに確保するものがある（例えば、特許文献１参照。）。   There is an absorption heat pump as a heat source machine for taking out a heated medium having a temperature higher than the drive heat source temperature. The absorption heat pump mainly includes an evaporator for evaporating the refrigerant liquid, an absorber for absorbing the refrigerant vapor with the absorption liquid, a regenerator for removing the refrigerant from the absorption liquid, and a condenser for condensing the refrigerant vapor. As an example of an absorption heat pump, it is equipped with a gas-liquid separator connected to circulate the medium to be heated between the heat transfer tubes in the absorber, and the liquid level in the gas-liquid separator is kept at a predetermined level. (For example, refer to Patent Document 1).

特開２００６−１３８６１４号公報JP 2006-138614 A

しかしながら、気液分離器内の液面の液位を所定レベルに確保すると、伝熱管内の被加熱媒体の量が、定常運転中は適切になるとしても、起動時には多すぎる場合があり、伝熱管内で加熱された被加熱媒体が伝熱管から過剰に流出してしまう場合があった。   However, if the liquid level in the gas-liquid separator is maintained at a predetermined level, the amount of the medium to be heated in the heat transfer tube may be excessive during startup, even if appropriate during steady operation. In some cases, the heated medium heated in the heat pipe flows out of the heat transfer pipe excessively.

本発明は上述の課題に鑑み、伝熱管内の被加熱媒体が伝熱管から過剰に流出してしまうことを抑制する吸収ヒートポンプを提供することを目的とする。   In view of the above-described problems, an object of the present invention is to provide an absorption heat pump that suppresses an excessively heated medium in a heat transfer tube from flowing out of the heat transfer tube.

上記目的を達成するために、本発明の第１の態様に係る吸収ヒートポンプは、例えば図１に示すように、吸収液Ｓａ、Ｓｂが吸収対象冷媒の蒸気Ｖｂ、Ｖｅを吸収する際に発生する吸収熱で被加熱媒体Ｗｑ、Ｖｆを加熱する吸収ヒートポンプ１であって；内部に被加熱媒体Ｗｑ、Ｖｆを流す伝熱管１２Ａ、１２Ｂと、伝熱管１２Ａ、１２Ｂの外表面に向けて吸収液Ｓａ、Ｓｂを供給する吸収液供給器１３Ａ、１３Ｂと、吸収液Ｓａ、Ｓｂに吸収させる吸収対象冷媒の蒸気Ｖｂ、Ｖｅを導入する吸収対象冷媒蒸気導入部１９Ａ、１９Ｂと、を有する吸収器１０Ａ、１０Ｂと；吸収器１０Ａ、１０Ｂで吸収対象冷媒の蒸気Ｖｂ、Ｖｅを吸収して濃度が低下した吸収液Ｓｂ、Ｓｗを直接又は間接的に導入し、導入した吸収液Ｓｗから吸収対象冷媒Ｖｇを離脱させて吸収液Ｓｗの濃度を上昇させ、濃度が上昇した吸収液Ｓａを直接又は間接的に吸収器１０Ａ、１０Ｂに向けて流出させる再生器３０と；被加熱媒体Ｗｑ、Ｖｆを伝熱管１２Ａ、１２Ｂに向けて供給する被加熱媒体供給手段８６、４９と；再生器３０の出口における吸収液Ｓａの温度、再生器３０の出口における吸収液Ｓａの濃度、吸収器１０Ａ、１０Ｂの入口における吸収液Ｓａ、Ｓｂの温度、吸収器１０Ａ、１０Ｂの入口における吸収液Ｓａ、Ｓｂの濃度、吸収器１０Ａ、１０Ｂの出口における吸収液Ｓｂ、Ｓｗの温度、吸収器１０Ａ、１０Ｂの出口における吸収液Ｓｂ、Ｓｗの濃度、再生器３０の入口における吸収液Ｓｗの温度、再生器３０の入口における吸収液Ｓｗの濃度、伝熱管１２Ａ、１２Ｂ内の圧力、及び伝熱管１２Ａ、１２Ｂの出口における被加熱媒体Ｗｍ、Ｖｍの温度、の少なくとも１つの値又はこれと相関を有する値を取得する流体特性関連値取得手段５１Ａ、５１Ｂと；吸収ヒートポンプ１の起動時に、流体特性関連値取得手段５１Ａ、５１Ｂで取得された値に応じて伝熱管１２Ａ、１２Ｂに供給する被加熱媒体Ｗｑ、Ｖｆの流量を調節するように被加熱媒体供給手段８６、４９を制御する制御装置９０とを備える。ここで、被加熱媒体の流量を調節することには、被加熱媒体を流さないこと（流量ゼロ）を含む。   In order to achieve the above object, the absorption heat pump according to the first aspect of the present invention is generated when the absorbing liquids Sa and Sb absorb the vapors Vb and Ve of the refrigerant to be absorbed, for example, as shown in FIG. An absorption heat pump 1 that heats heated media Wq and Vf with absorbed heat; heat transfer tubes 12A and 12B through which heated media Wq and Vf flow and absorption liquid Sa toward the outer surfaces of the heat transfer tubes 12A and 12B Absorber 10A having absorption liquid supply devices 13A and 13B for supplying Sb and absorption target refrigerant vapor introduction portions 19A and 19B for introducing vapors Vb and Ve of the absorption target refrigerant to be absorbed by the absorption liquids Sa and Sb, 10B; Absorbing liquids Vb and Ve of the absorption target refrigerant are absorbed by the absorbers 10A and 10B, and the absorption liquids Sb and Sw having a reduced concentration are directly or indirectly introduced, and the absorption target refrigerant V is introduced from the introduced absorption liquid Sw. And the regenerator 30 for increasing the concentration of the absorbing solution Sw and causing the increased concentration of the absorbing solution Sa to flow out directly or indirectly toward the absorbers 10A and 10B; and the heated media Wq and Vf as heat transfer tubes Heated medium supply means 86 and 49 for supplying toward the 12A and 12B; the temperature of the absorbing liquid Sa at the outlet of the regenerator 30, the concentration of the absorbing liquid Sa at the outlet of the regenerator 30, and the inlets of the absorbers 10A and 10B Absorption liquid Sa, Sb temperature, absorption liquid Sa, Sb concentration at the inlets of the absorbers 10A, 10B, absorption liquid Sb, Sw temperature at the outlets of the absorbers 10A, 10B, absorption liquid at the outlets of the absorbers 10A, 10B The concentration of Sb, Sw, the temperature of the absorbent Sw at the inlet of the regenerator 30, the concentration of the absorbent Sw at the inlet of the regenerator 30, the pressure in the heat transfer tubes 12A and 12B, and the heat transfer tube Fluid characteristic related value acquisition means 51A, 51B for acquiring at least one value of the temperatures of the heated media Wm, Vm at the outlets of 2A, 12B or a value correlated therewith; A control device 90 that controls the heated medium supply means 86 and 49 so as to adjust the flow rates of the heated media Wq and Vf supplied to the heat transfer tubes 12A and 12B according to the values acquired by the related value acquisition means 51A and 51B. With. Here, adjusting the flow rate of the heated medium includes not flowing the heated medium (zero flow rate).

このように構成すると、吸収ヒートポンプの起動時に流体特性関連値取得手段で取得された値に応じて伝熱管に供給する被加熱媒体の流量を調節するので、伝熱管に被加熱媒体が過剰に導入されることを抑制することができ、被加熱媒体の蒸気に随伴して伝熱管から流出する被加熱媒体の液体が、伝熱管内の被加熱媒体が沸騰することによって伝熱管から過剰に流出してしまうことを抑制することができる。   If comprised in this way, since the flow volume of the to-be-heated medium supplied to a heat exchanger tube will be adjusted according to the value acquired by the fluid characteristic related value acquisition means at the time of starting of an absorption heat pump, the to-be-heated medium will be introduced excessively to a heat exchanger tube The liquid of the heated medium that flows out of the heat transfer tube accompanying the vapor of the heated medium excessively flows out of the heat transfer tube due to the boiling of the heated medium in the heat transfer tube. Can be suppressed.

また、本発明の第２の態様に係る吸収ヒートポンプは、例えば図１を参照して示すと、上記本発明の第１の態様に係る吸収ヒートポンプ１において、流体特性関連値取得手段５１Ａ、５１Ｂは、再生器３０の出口における吸収液Ｓａの温度、再生器３０の出口における吸収液Ｓａの濃度、吸収器１０Ａ、１０Ｂの入口における吸収液Ｓａ、Ｓｂの温度、吸収器１０Ａ、１０Ｂの入口における吸収液Ｓａ、Ｓｂの濃度、吸収器１０Ａ、１０Ｂの出口における吸収液Ｓｂ、Ｓｗの温度、及び吸収器１０Ａ、１０Ｂの出口における吸収液Ｓｂ、Ｓｗの濃度、再生器３０の入口における吸収液Ｓｗの温度、再生器３０の入口における吸収液Ｓｗの濃度、の少なくとも１つの値又はこれと相関を有する値である吸収液特性関連値を取得するように構成され；制御装置９０は、吸収ヒートポンプ１を起動する際、流体特性関連値取得手段５１Ａ、５１Ｂで取得された吸収液特性関連値が所定の値に到達したときに、被加熱媒体Ｗｑ、Ｖｆの伝熱管１２Ａ、１２Ｂへの供給を開始するように、被加熱媒体供給手段８６、４９を制御する。   Moreover, when the absorption heat pump according to the second aspect of the present invention is shown with reference to FIG. 1, for example, in the absorption heat pump 1 according to the first aspect of the present invention, the fluid characteristic related value acquisition means 51A and 51B include The temperature of the absorbent Sa at the outlet of the regenerator 30, the concentration of the absorbent Sa at the outlet of the regenerator 30, the temperature of the absorbents Sa and Sb at the inlets of the absorbers 10A and 10B, and the absorption at the inlets of the absorbers 10A and 10B. The concentration of the liquids Sa and Sb, the temperature of the absorption liquids Sb and Sw at the outlets of the absorbers 10A and 10B, the concentration of the absorption liquids Sb and Sw at the outlets of the absorbers 10A and 10B, and the concentration of the absorption liquid Sw at the inlet of the regenerator 30 It is configured to acquire at least one value of the temperature, the concentration of the absorbing liquid Sw at the inlet of the regenerator 30, or a value related to the absorbing liquid characteristic, which is a value correlated with the value. When the controller 90 starts up the absorption heat pump 1, when the absorption liquid characteristic related values acquired by the fluid characteristic related value acquisition means 51 </ b> A and 51 </ b> B reach a predetermined value, transmission of the heated media Wq and Vf is performed. The heated medium supply means 86 and 49 are controlled so as to start the supply to the heat tubes 12A and 12B.

このように構成すると、吸収器において十分な吸収熱が発生する前に伝熱管に被加熱媒体が供給されることを回避することができ、被加熱媒体が早期に導入された場合に生じ得る伝熱管の冷却で起動時間が延びることを回避することができる。   With this configuration, it is possible to prevent the heated medium from being supplied to the heat transfer tube before sufficient absorption heat is generated in the absorber, and transfer that may occur when the heated medium is introduced early. It is possible to avoid an increase in the start-up time due to the cooling of the heat pipe.

また、本発明の第３の態様に係る吸収ヒートポンプは、例えば図１を参照して示すと、上記本発明の第１の態様又は第２の態様に係る吸収ヒートポンプ１において、制御装置９０は、流体特性関連値取得手段５１Ａ、５１Ｂで取得された値が上昇するに連れて、被加熱媒体供給手段８６、４９から伝熱管１２Ａ、１２Ｂに供給される被加熱媒体Ｗｑ、Ｖｆの流量を増加させるように構成されている。   In addition, when the absorption heat pump according to the third aspect of the present invention is illustrated with reference to FIG. 1, for example, in the absorption heat pump 1 according to the first aspect or the second aspect of the present invention, the control device 90 includes: As the values acquired by the fluid characteristic related value acquisition means 51A and 51B increase, the flow rates of the heated media Wq and Vf supplied from the heated media supply means 86 and 49 to the heat transfer tubes 12A and 12B are increased. It is configured as follows.

このように構成すると、過剰な流量の被加熱媒体が伝熱管に供給されることに起因する伝熱管の冷却で起動時間が延びることを回避することができる。   If comprised in this way, it can avoid that starting time is extended by cooling of the heat exchanger tube resulting from the to-be-heated medium of an excessive flow volume being supplied to a heat exchanger tube.

また、本発明の第４の態様に係る吸収ヒートポンプは、例えば図１に示すように、上記本発明の第１の態様乃至第３の態様のいずれか１つの態様に係る吸収ヒートポンプ１において、伝熱管１２Ｂに供給される被加熱媒体Ｖｆを貯留する被加熱媒体貯留部４２と；伝熱管１２Ｂから流出した被加熱媒体の気体と液体との混合流体Ｖｍ、又は伝熱管１２Ｂから流出した後に発生した被加熱媒体の気体と液体との混合流体Ｖｍから、被加熱媒体の気体Ｖｂと液体Ｖｆとを分離する気液分離器６０と；気液分離器６０から伝熱管１２Ｂへ被加熱媒体Ｖｆを導く被加熱媒体流路６２と；被加熱媒体貯留部４２に貯留されている被加熱媒体Ｖｆを、気液分離器６０、被加熱媒体流路６２、又は伝熱管１２Ｂへ供給する被加熱媒体ポンプ４９とを備え；被加熱媒体貯留部４２は、被加熱媒体Ｖｆの液位を検知する被加熱媒体液位検知器４３を有し；制御装置９０は、被加熱媒体液位検知器４３が検知した値に応じて供給する被加熱媒体Ｖｆの流量を調節するように被加熱媒体ポンプ４９を制御する。   Further, the absorption heat pump according to the fourth aspect of the present invention is, for example, as shown in FIG. 1, in the absorption heat pump 1 according to any one of the first to third aspects of the present invention. Heated medium storage part 42 for storing the heated medium Vf supplied to the heat pipe 12B; generated after flowing out of the mixed fluid Vm of the gas and liquid of the heated medium flowing out of the heat transfer pipe 12B or the heat transfer pipe 12B A gas-liquid separator 60 for separating the gas Vb and the liquid Vf of the medium to be heated from the mixed fluid Vm of the gas and liquid of the medium to be heated; and the medium to be heated Vf is guided from the gas-liquid separator 60 to the heat transfer tube 12B. Heated medium flow path 62; Heated medium pump 49 for supplying heated medium Vf stored in heated medium storage section 42 to gas-liquid separator 60, heated medium flow path 62, or heat transfer pipe 12B. And equipped with The heat medium storage unit 42 includes a heated medium liquid level detector 43 that detects the liquid level of the heated medium Vf; the control device 90 supplies the heating medium according to the value detected by the heated medium liquid level detector 43. The heated medium pump 49 is controlled so as to adjust the flow rate of the heated medium Vf.

このように構成すると、被加熱媒体貯留部を大型化することなく、吸収ヒートポンプの効率的な起動を行うことができる。   If comprised in this way, an efficient starting of an absorption heat pump can be performed, without enlarging a to-be-heated medium storage part.

また、本発明の第５の態様に係る吸収ヒートポンプは、例えば図３に示すように、上記本発明の第１の態様乃至第４の態様のいずれか１つの態様に係る吸収ヒートポンプにおいて、伝熱管１２Ａが、被加熱媒体の液体Ｗｑを導入し加熱して蒸発させる蒸発管１２ｅを有し；吸収器１０Ａは、複数の蒸発管１２ｅへ被加熱媒体Ｗを分配する蒸発管分配部１４ｅｓにそれぞれの蒸発管１２ｅの一端が接続され、複数の蒸発管１２ｅから被加熱媒体Ｗを収集する蒸発管収集部１４ｅｃにそれぞれの蒸発管１２ｅの他端が接続され、蒸発管分配部１４ｅｓと蒸発管収集部１４ｅｃとがそれぞれ１個から構成されている。   Moreover, the absorption heat pump which concerns on the 5th aspect of this invention is the heat transfer tube in the absorption heat pump which concerns on any one aspect of the said 1st aspect thru | or 4th aspect of this invention, as shown, for example in FIG. 12A has an evaporation tube 12e that introduces and heats the liquid Wq to be heated and evaporates; the absorber 10A is provided in each of the evaporation tube distributors 14es that distribute the heated medium W to the plurality of evaporation tubes 12e. One end of the evaporation pipe 12e is connected, and the other end of each evaporation pipe 12e is connected to the evaporation pipe collection section 14ec that collects the heated medium W from the plurality of evaporation pipes 12e, and the evaporation pipe distribution section 14es and the evaporation pipe collection section 14ec is composed of one piece each.

このように構成すると、被加熱媒体の蒸気に随伴して伝熱管から流出する被加熱媒体の液体が伝熱管内の被加熱媒体が沸騰することによって伝熱管から過剰に流出してしまうことを抑制する効果を高めることができる。また、各蒸発管に流入する被加熱媒体の液体が各蒸発管に流入する前に蒸発してしまっていることを回避することができ、複数本の蒸発管のうち被加熱媒体の液体が流入せずに被加熱媒体の蒸気が流入してしまう蒸発管が生じることを防ぐことができて、被加熱媒体の液体への伝熱効率の低下を抑制することができる。   With this configuration, the liquid of the heated medium flowing out of the heat transfer tube accompanying the vapor of the heated medium is prevented from flowing out excessively from the heat transfer tube due to the boiling of the heated medium in the heat transfer tube. Can enhance the effect. In addition, it is possible to avoid the liquid of the heated medium flowing into each evaporation pipe from evaporating before flowing into each of the evaporation pipes, and the liquid of the heated medium flows into the plurality of evaporation pipes. Therefore, it is possible to prevent the occurrence of an evaporation tube in which the vapor of the heated medium flows in without reducing the heat transfer efficiency of the heated medium to the liquid.

本発明によれば、被加熱媒体の蒸気に随伴して伝熱管から流出する被加熱媒体の液体が、伝熱管内の被加熱媒体が沸騰することによって伝熱管から過剰に流出してしまうことを抑制することができる。   According to the present invention, the liquid of the heated medium flowing out of the heat transfer tube accompanying the vapor of the heated medium is excessively discharged from the heat transfer tube by boiling the heated medium in the heat transfer tube. Can be suppressed.

本発明の実施の形態に係る吸収ヒートポンプの模式的系統図である。1 is a schematic system diagram of an absorption heat pump according to an embodiment of the present invention. 本発明の実施の形態に係る吸収ヒートポンプの起動時の制御を説明するフローチャートである。It is a flowchart explaining the control at the time of starting of the absorption heat pump which concerns on embodiment of this invention. 本発明の実施の形態に係る吸収ヒートポンプの高温吸収器まわりの一例を示す断面図である。It is sectional drawing which shows an example around the high temperature absorber of the absorption heat pump which concerns on embodiment of this invention.

以下、図面を参照して本発明の実施の形態について説明する。なお、各図において互いに同一又は相当する部材には同一あるいは類似の符号を付し、重複した説明は省略する。   Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or similar members are denoted by the same or similar reference numerals, and redundant description is omitted.

まず図１を参照して、本発明の実施の形態に係る吸収ヒートポンプ１を説明する。図１は、吸収ヒートポンプ１の模式的系統図である。吸収ヒートポンプ１は、吸収液Ｓ（Ｓａ、Ｓｂ、Ｓｗ）と冷媒Ｖ（Ｖｂ、Ｖｅ、Ｖｇ、Ｖｆ）との吸収ヒートポンプサイクルが行われる主要機器を構成する吸収器、蒸発器２０、再生器３０、及び凝縮器４０を備えている。本実施の形態では、吸収器が、高温吸収器１０Ａ及び低温吸収器１０Ｂの２段構成になっている。吸収ヒートポンプ１は、さらに、低温気液分離器６０及び高温気液分離器８０と、制御装置９０とを備えている。   First, an absorption heat pump 1 according to an embodiment of the present invention will be described with reference to FIG. FIG. 1 is a schematic system diagram of the absorption heat pump 1. The absorption heat pump 1 includes an absorber, an evaporator 20, and a regenerator 30 that constitute main equipment in which an absorption heat pump cycle of the absorption liquid S (Sa, Sb, Sw) and the refrigerant V (Vb, Ve, Vg, Vf) is performed. , And a condenser 40. In the present embodiment, the absorber has a two-stage configuration of a high temperature absorber 10A and a low temperature absorber 10B. The absorption heat pump 1 further includes a low-temperature gas-liquid separator 60, a high-temperature gas-liquid separator 80, and a control device 90.

本明細書においては、吸収液に関し、ヒートポンプサイクル上における区別を容易にするために、性状やヒートポンプサイクル上の位置に応じて「希溶液Ｓｗ」や「高濃度溶液Ｓａ」等と呼称するが、性状等を不問にするときは総称して「吸収液Ｓ」ということとする。同様に、冷媒に関し、ヒートポンプサイクル上における区別を容易にするために、性状やヒートポンプサイクル上の位置に応じて「蒸発器冷媒蒸気Ｖｅ」、「再生器冷媒蒸気Ｖｇ」、「冷媒液Ｖｆ」等と呼称するが、性状等を不問にするときは総称して「冷媒Ｖ」ということとする。本実施の形態では、吸収液Ｓ（吸収剤と冷媒Ｖとの混合物）としてＬｉＢｒ水溶液が用いられており、冷媒Ｖとして水（Ｈ２Ｏ）が用いられている。また、吸収ヒートポンプ１から外部に生産物（目的物）として被加熱水蒸気Ｗｖを供給するように構成されている。被加熱水蒸気Ｗｖは、被加熱水液Ｗｑが蒸発したものであり、これらの性状を不問にするときは被加熱水Ｗということとする。本実施の形態では、被加熱水Ｗとして水（Ｈ２Ｏ）が用いられている。 In the present specification, the absorption liquid is referred to as “dilute solution Sw”, “high-concentration solution Sa” or the like in accordance with the properties and the position on the heat pump cycle in order to facilitate distinction on the heat pump cycle. When the property or the like is not asked, it is generally called “absorbing liquid S”. Similarly, regarding the refrigerant, in order to easily distinguish on the heat pump cycle, “evaporator refrigerant vapor Ve”, “regenerator refrigerant vapor Vg”, “refrigerant liquid Vf”, etc., depending on the properties and the position on the heat pump cycle. However, when the properties and the like are not asked, they are collectively referred to as “refrigerant V”. In the present embodiment, an LiBr aqueous solution is used as the absorbing liquid S (a mixture of the absorbent and the refrigerant V), and water (H 2 O) is used as the refrigerant V. Moreover, it is comprised so that the to-be-heated water vapor | steam Wv may be supplied from the absorption heat pump 1 to the exterior as a product (target object). The heated water vapor Wv is obtained by evaporating the heated water liquid Wq, and is referred to as heated water W when these properties are not questioned. In the present embodiment, water (H 2 O) is used as the heated water W.

高温吸収器１０Ａは、被加熱水Ｗの流路を構成する高温伝熱管１２Ａと、高濃度溶液Ｓａを散布する吸収液供給器としての高濃度溶液散布ノズル１３Ａとを内部に有している。また、高温吸収器１０Ａは、低温気液分離器６０から低温冷媒蒸気Ｖｂを導入する低温冷媒蒸気管６９が接続されている。高温吸収器１０Ａの、低温冷媒蒸気管６９が接続された部分である冷媒蒸気導入口１９Ａは、吸収対象冷媒蒸気導入部に相当する。高温吸収器１０Ａは、高濃度溶液散布ノズル１３Ａから高濃度溶液Ｓａが散布され、高濃度溶液Ｓａが低温冷媒蒸気Ｖｂを吸収する際に吸収熱を発生させる。この吸収熱を、高温伝熱管１２Ａを流れる被加熱水Ｗが受熱して、被加熱水Ｗが加熱されるように構成されている。高温吸収器１０Ａにおいて、高温伝熱管１２Ａの内部を流れる被加熱水Ｗは被加熱媒体に相当し、低温冷媒蒸気Ｖｂは吸収対象冷媒に相当する。   The high-temperature absorber 10A includes a high-temperature heat transfer tube 12A constituting a flow path of the water to be heated W and a high-concentration solution spray nozzle 13A as an absorbent supply device that sprays the high-concentration solution Sa. The high-temperature absorber 10A is connected to a low-temperature refrigerant vapor pipe 69 that introduces the low-temperature refrigerant vapor Vb from the low-temperature gas-liquid separator 60. The refrigerant vapor inlet 19A, which is the portion of the high-temperature absorber 10A to which the low-temperature refrigerant vapor pipe 69 is connected, corresponds to the absorption target refrigerant vapor introducing portion. The high temperature absorber 10A generates heat of absorption when the high concentration solution Sa is sprayed from the high concentration solution spray nozzle 13A and the high concentration solution Sa absorbs the low temperature refrigerant vapor Vb. This absorbed heat is received by the heated water W flowing through the high-temperature heat transfer tube 12A, and the heated water W is heated. In the high-temperature absorber 10A, the heated water W flowing inside the high-temperature heat transfer tube 12A corresponds to the heated medium, and the low-temperature refrigerant vapor Vb corresponds to the refrigerant to be absorbed.

低温吸収器１０Ｂは、冷媒液Ｖｆの流路を構成する低温伝熱管１２Ｂと、中間濃度溶液Ｓｂを散布する吸収液供給器としての中間濃度溶液散布ノズル１３Ｂとを内部に有している。また、低温吸収器１０Ｂには、蒸発器２０からの蒸発器冷媒蒸気Ｖｅを導入する冷媒蒸気導入口１９Ｂが形成されている。冷媒蒸気導入口１９Ｂは、吸収対象冷媒蒸気導入部に相当する。低温吸収器１０Ｂは、中間濃度溶液散布ノズル１３Ｂから中間濃度溶液Ｓｂが散布され、中間濃度溶液Ｓｂが蒸発器冷媒蒸気Ｖｅを吸収する際に吸収熱を発生させる。この吸収熱を、低温伝熱管１２Ｂを流れる冷媒液Ｖｆが受熱して、冷媒液Ｖｆが加熱されるように構成されている。低温吸収器１０Ｂにおいて、低温伝熱管１２Ｂの内部を流れる冷媒液Ｖｆは被加熱媒体に相当し、蒸発器冷媒蒸気Ｖｅは吸収対象冷媒に相当する。   The low-temperature absorber 10B includes therein a low-temperature heat transfer tube 12B that constitutes the flow path of the refrigerant liquid Vf and an intermediate-concentration solution spraying nozzle 13B as an absorbing liquid supplier that sprays the intermediate-concentration solution Sb. The low-temperature absorber 10B is formed with a refrigerant vapor inlet 19B for introducing the evaporator refrigerant vapor Ve from the evaporator 20. The refrigerant vapor inlet 19B corresponds to an absorption target refrigerant vapor inlet. The low temperature absorber 10B generates heat of absorption when the intermediate concentration solution Sb is sprayed from the intermediate concentration solution spray nozzle 13B and the intermediate concentration solution Sb absorbs the evaporator refrigerant vapor Ve. This absorbed heat is received by the refrigerant liquid Vf flowing through the low-temperature heat transfer tube 12B, and the refrigerant liquid Vf is heated. In the low-temperature absorber 10B, the refrigerant liquid Vf flowing inside the low-temperature heat transfer tube 12B corresponds to the medium to be heated, and the evaporator refrigerant vapor Ve corresponds to the refrigerant to be absorbed.

蒸発器２０は、熱源流体としての熱源温水ｈｅの流路を構成する熱源管２１と、冷媒液Ｖｆを熱源管２１に向けて散布する冷媒液散布ノズル２２とを内部に有している。また、蒸発器２０は、底部に貯留している冷媒液Ｖｆを冷媒液散布ノズル２２に導く冷媒液循環管２５と、冷媒液循環管２５に配設されて蒸発器２０底部の冷媒液Ｖｆを冷媒液散布ノズル２２に圧送する冷媒液循環ポンプ２６とを有している。蒸発器２０の熱源管２１から流出した熱源温水ｈｅを流す配管には、流路を開閉する蒸発器熱源弁２１ｖが配設されている。蒸発器２０は、冷媒液散布ノズル２２から冷媒液Ｖｆが散布され、散布された冷媒液Ｖｆが熱源管２１内を流れる熱源温水ｈｅの熱で蒸発して蒸発器冷媒蒸気Ｖｅが発生するように構成されている。低温吸収器１０Ｂと蒸発器２０とは、相互に連通するように構成されている。低温吸収器１０Ｂと蒸発器２０とが連通することにより、蒸発器２０で発生した蒸発器冷媒蒸気Ｖｅを高温吸収器１０Ｂに供給することができるように構成されている。   The evaporator 20 includes therein a heat source pipe 21 that forms a flow path of the heat source hot water he as a heat source fluid, and a refrigerant liquid spray nozzle 22 that sprays the refrigerant liquid Vf toward the heat source pipe 21. Further, the evaporator 20 is provided in the refrigerant liquid circulation pipe 25 that guides the refrigerant liquid Vf stored in the bottom to the refrigerant liquid spraying nozzle 22, and the refrigerant liquid Vf at the bottom of the evaporator 20 is provided in the refrigerant liquid circulation pipe 25. A refrigerant liquid circulation pump 26 that pumps the refrigerant liquid to the refrigerant liquid spray nozzle 22 is provided. An evaporator heat source valve 21v that opens and closes the flow path is disposed in a pipe through which the heat source hot water he flowing out from the heat source pipe 21 of the evaporator 20 flows. In the evaporator 20, the refrigerant liquid Vf is sprayed from the refrigerant liquid spray nozzle 22, and the sprayed refrigerant liquid Vf is evaporated by the heat of the heat source hot water he flowing in the heat source pipe 21 to generate the evaporator refrigerant vapor Ve. It is configured. The low-temperature absorber 10B and the evaporator 20 are configured to communicate with each other. The low-temperature absorber 10B and the evaporator 20 communicate with each other, so that the evaporator refrigerant vapor Ve generated in the evaporator 20 can be supplied to the high-temperature absorber 10B.

再生器３０は、希溶液Ｓｗを加熱する熱源流体としての熱源温水ｈｇを内部に流す熱源管３１と、希溶液Ｓｗを散布する希溶液散布ノズル３２とを有している。熱源管３１内を流れる熱源温水ｈｇは、熱源管２１内を流れる熱源温水ｈｅと同じ流体であっても異なる流体であってもよい。再生器３０の熱源管３１から流出した熱源温水ｈｇを流す配管には、流路を開閉する再生器熱源弁３１ｖが配設されている。再生器３０は、希溶液散布ノズル３２から散布された希溶液Ｓｗが熱源温水ｈｇに加熱されることにより、希溶液Ｓｗから冷媒Ｖが蒸発して濃度が上昇した高濃度溶液Ｓａが生成されるように構成されている。希溶液Ｓｗから蒸発した冷媒Ｖは再生器冷媒蒸気Ｖｇとして凝縮器４０に移動するように構成されている。   The regenerator 30 has a heat source pipe 31 for flowing heat source hot water hg as a heat source fluid for heating the dilute solution Sw, and a dilute solution spray nozzle 32 for spraying the dilute solution Sw. The heat source hot water hg flowing in the heat source pipe 31 may be the same fluid as the heat source hot water he flowing in the heat source pipe 21 or a different fluid. A regenerator heat source valve 31v that opens and closes the flow path is disposed in the pipe through which the heat source hot water hg flowing out from the heat source pipe 31 of the regenerator 30 flows. In the regenerator 30, when the dilute solution Sw sprayed from the dilute solution spray nozzle 32 is heated to the heat source hot water hg, the refrigerant V evaporates from the dilute solution Sw to generate a high-concentration solution Sa having an increased concentration. It is configured as follows. The refrigerant V evaporated from the dilute solution Sw is configured to move to the condenser 40 as a regenerator refrigerant vapor Vg.

凝縮器４０は、冷却媒体としての冷却水ｃが流れる冷却水管４１を有している。凝縮器４０の冷却水管４１から流出した冷却水ｃを流す配管には、流路を開閉する凝縮器冷却弁４１ｖが配設されている。凝縮器４０は、再生器３０で発生した再生器冷媒蒸気Ｖｇを導入し、これを冷却水ｃで冷却して凝縮させるように構成されている。凝縮器４０は、下部に、再生器冷媒蒸気Ｖｇが凝縮して生成された冷媒液Ｖｆが貯留される冷媒液貯留部４２が形成されている。冷媒液貯留部４２には、冷媒液Ｖｆの液位を検知する被加熱媒体液位検知器としての液位検知器４３が設けられている。再生器３０と凝縮器４０とは、相互に連通するように構成されている。再生器３０と凝縮器４０とが連通することにより、再生器３０で発生した再生器冷媒蒸気Ｖｇを凝縮器４０に供給することができるように構成されている。また、低温吸収器１０Ｂ及び蒸発器２０が再生器３０及び凝縮器４０よりも高所に配設されており、位置ヘッド及び内圧の差で低温吸収器１０Ｂ内の吸収液Ｓを再生器３０へ搬送可能に構成されている。   The condenser 40 has a cooling water pipe 41 through which cooling water c as a cooling medium flows. A condenser cooling valve 41v that opens and closes the flow path is disposed in the pipe through which the cooling water c flowing out from the cooling water pipe 41 of the condenser 40 flows. The condenser 40 is configured to introduce the regenerator refrigerant vapor Vg generated in the regenerator 30, cool it with the cooling water c, and condense it. In the lower part of the condenser 40, a refrigerant liquid storage part 42 is formed in which a refrigerant liquid Vf generated by condensing the regenerator refrigerant vapor Vg is stored. The refrigerant liquid storage section 42 is provided with a liquid level detector 43 as a heated medium liquid level detector that detects the liquid level of the refrigerant liquid Vf. The regenerator 30 and the condenser 40 are configured to communicate with each other. By connecting the regenerator 30 and the condenser 40, the regenerator refrigerant vapor Vg generated in the regenerator 30 can be supplied to the condenser 40. Further, the low-temperature absorber 10B and the evaporator 20 are disposed at a higher position than the regenerator 30 and the condenser 40, and the absorbing liquid S in the low-temperature absorber 10B is transferred to the regenerator 30 due to the difference in position head and internal pressure. It is configured to be transportable.

再生器３０の高濃度溶液Ｓａが貯留される部分と高温吸収器１０Ａの高濃度溶液散布ノズル１３Ａとは、高濃度溶液Ｓａを流す高濃度溶液管３５で接続されている。高濃度溶液管３５には、高濃度溶液Ｓａを圧送する高濃度溶液ポンプ３５ｐが配設されている。高温吸収器１０Ａの中間濃度溶液Ｓｂが貯留される部分と中間濃度溶液散布ノズル１３Ｂとは、中間濃度溶液Ｓｂを流す中間濃度溶液管１５Ａで接続されている。中間濃度溶液管１５Ａには、中間濃度溶液Ｓｂを圧送する中間濃度溶液ポンプ１６Ａが配設されている。低温吸収器１０Ｂの希溶液Ｓｗが貯留される部分と希溶液散布ノズル３２とは、希溶液Ｓｗを流す希溶液管１５Ｂで接続されている。高濃度溶液管３５及び中間濃度溶液管１５Ａには、高濃度溶液Ｓａと中間濃度溶液Ｓｂとの間で熱交換を行わせる高温溶液熱交換器３８Ａが配設されている。高濃度溶液管３５及び希溶液管１５Ｂには、高濃度溶液Ｓａと希溶液Ｓｗとの間で熱交換を行わせる低温溶液熱交換器３８Ｂが配設されている。   A portion of the regenerator 30 in which the high concentration solution Sa is stored and the high concentration solution spray nozzle 13A of the high temperature absorber 10A are connected by a high concentration solution pipe 35 through which the high concentration solution Sa flows. The high concentration solution pipe 35 is provided with a high concentration solution pump 35p for pumping the high concentration solution Sa. The portion of the high-temperature absorber 10A where the intermediate concentration solution Sb is stored and the intermediate concentration solution spray nozzle 13B are connected by an intermediate concentration solution tube 15A through which the intermediate concentration solution Sb flows. An intermediate concentration solution pump 16A that pumps the intermediate concentration solution Sb is disposed in the intermediate concentration solution tube 15A. The portion of the low temperature absorber 10B where the dilute solution Sw is stored and the dilute solution spray nozzle 32 are connected by a dilute solution tube 15B through which the dilute solution Sw flows. The high-concentration solution pipe 35 and the intermediate-concentration solution pipe 15A are provided with a high-temperature solution heat exchanger 38A that performs heat exchange between the high-concentration solution Sa and the intermediate-concentration solution Sb. The high concentration solution tube 35 and the dilute solution tube 15B are provided with a low temperature solution heat exchanger 38B that performs heat exchange between the high concentration solution Sa and the dilute solution Sw.

凝縮器４０の冷媒液貯留部４２には、冷媒液Ｖｆを流す冷媒液管４５の一端が接続されている。冷媒液管４５の他端は、冷媒液管４６と冷媒液管４８とに分岐している。換言すれば、冷媒液管４５の他端には、冷媒液管４６及び冷媒液管４８の一端がそれぞれ接続されている。冷媒液管４６の他端は蒸発器２０に接続されている。冷媒液管４６には冷媒液搬送ポンプ４７が配設されており、冷媒液Ｖｆを蒸発器２０内に流入させることができるように構成されている。冷媒液管４８の他端は低温気液分離器６０に接続されている。冷媒液管４８には、被加熱媒体供給手段としての冷媒液供給ポンプ４９が配設されており、冷媒液Ｖｆを低温気液分離器６０内に流入させることができるように構成されている。冷媒液供給ポンプ４９は、インバータにより回転速度を変化させることができ、これによって冷媒液管４８内を流れる冷媒液Ｖｆの流量を調節することができるように構成されている。   One end of a refrigerant liquid pipe 45 through which the refrigerant liquid Vf flows is connected to the refrigerant liquid storage part 42 of the condenser 40. The other end of the refrigerant liquid pipe 45 branches into a refrigerant liquid pipe 46 and a refrigerant liquid pipe 48. In other words, one end of each of the refrigerant liquid pipe 46 and the refrigerant liquid pipe 48 is connected to the other end of the refrigerant liquid pipe 45. The other end of the refrigerant liquid pipe 46 is connected to the evaporator 20. The refrigerant liquid pipe 46 is provided with a refrigerant liquid transport pump 47 so that the refrigerant liquid Vf can flow into the evaporator 20. The other end of the refrigerant liquid pipe 48 is connected to a low-temperature gas-liquid separator 60. The refrigerant liquid pipe 48 is provided with a refrigerant liquid supply pump 49 as a heated medium supply means, and is configured to allow the refrigerant liquid Vf to flow into the low temperature gas-liquid separator 60. The refrigerant liquid supply pump 49 is configured to be able to change the rotation speed by an inverter and thereby adjust the flow rate of the refrigerant liquid Vf flowing through the refrigerant liquid pipe 48.

低温気液分離器６０は、低温吸収器１０Ｂの低温伝熱管１２Ｂを流れて加熱された冷媒Ｖを導入し、低温冷媒蒸気Ｖｂと冷媒液Ｖｆとを分離する機器である。低温気液分離器６０と低温吸収器１０Ｂとは、低温気液分離器６０内の冷媒液Ｖｆを低温伝熱管１２Ｂに導く被加熱媒体流路としての冷媒液導入管６２及び加熱された冷媒Ｖを低温気液分離器６０に導く冷媒流出管６４で接続されている。また、低温気液分離器６０には、分離された低温冷媒蒸気Ｖｂを高温吸収器１０Ａに導く低温冷媒蒸気管６９が接続されている。また、低温気液分離器６０には、上述のように、凝縮器４０から冷媒液Ｖｆを導入するための冷媒液管４８の他端が接続されている。また、低温気液分離器６０には、内部の圧力を検知する低温圧力計６１が設けられている。   The low-temperature gas-liquid separator 60 is a device that introduces the refrigerant V heated by flowing through the low-temperature heat transfer tube 12B of the low-temperature absorber 10B and separates the low-temperature refrigerant vapor Vb and the refrigerant liquid Vf. The low-temperature gas-liquid separator 60 and the low-temperature absorber 10B are a refrigerant liquid introduction pipe 62 and a heated refrigerant V as a heated medium flow path that guides the refrigerant liquid Vf in the low-temperature gas-liquid separator 60 to the low-temperature heat transfer pipe 12B. Is connected by a refrigerant outflow pipe 64 that guides the gas to the low-temperature gas-liquid separator 60. The low-temperature gas-liquid separator 60 is connected to a low-temperature refrigerant vapor pipe 69 that guides the separated low-temperature refrigerant vapor Vb to the high-temperature absorber 10A. Moreover, the other end of the refrigerant liquid pipe 48 for introducing the refrigerant liquid Vf from the condenser 40 is connected to the low temperature gas-liquid separator 60 as described above. Further, the low temperature gas-liquid separator 60 is provided with a low temperature pressure gauge 61 for detecting the internal pressure.

高温気液分離器８０は、高温吸収器１０Ａの高温伝熱管１２Ａを流れて加熱された被加熱水Ｗを導入し、被加熱水蒸気Ｗｖと被加熱水液Ｗｑとに分離する機器である。高温気液分離器８０と高温吸収器１０Ａとは、高温気液分離器８０内の被加熱水液Ｗｑを高温伝熱管１２Ａに導く被加熱媒体流路としての被加熱水導入管８２及び加熱された被加熱水Ｗを高温気液分離器８０に導く被加熱水流出管８４で接続されている。本実施の形態では、吸収ヒートポンプ１の定常運転中は、被加熱水導入管８２と被加熱水流出管８４との気泡ヘッド差を駆動力とする自然循環作用で被加熱水Ｗｑが高温伝熱管１２Ａに供給されるように構成されている。したがって、被加熱水導入管８２には、被加熱水液Ｗｑを高温伝熱管１２Ａに送るポンプが設けられていない。しかしながら、高温気液分離器８０及び高温吸収器１０の配置や形状あるいは配管構成等により、高温伝熱管１２Ａに供給される被加熱水液Ｗｑの流量が充分に得られない場合は、被加熱水液Ｗｑを高温伝熱管１２Ａに送るポンプを設けるとよい。あるいは、被加熱水Ｗｑを高温伝熱管１２Ａに圧送する被加熱水ポンプを被加熱水導入管８２に設け、高温伝熱管１２Ａ内を加圧して高温伝熱管１２Ａの外で被加熱水蒸気Ｗｖが生じるようにしてもよい。なお、吸収ヒートポンプ１の起動時は、連通している高温伝熱管１２Ａと高温気液分離器８０とのそれぞれの液位は略同じになる。また、高温気液分離器８０には、分離された被加熱水蒸気Ｗｖを吸収ヒートポンプ１の外に導く被加熱水蒸気管８９が接続されている。また、主に蒸気として吸収ヒートポンプ１の外に供給された分の被加熱水Ｗを補うための補給水Ｗｓを吸収ヒートポンプ１の外から導入する補給水管８５が設けられている。補給水管８５は、被加熱水導入管８２に接続されており、被加熱水導入管８２を流れる被加熱水液Ｗｑに補給水Ｗｓを合流させるように構成されている。補給水管８５には、高温吸収器１０Ａに向けて補給水Ｗｓを圧送する被加熱媒体供給手段としての補給水ポンプ８６が配設されている。補給水ポンプ８６は、インバータにより回転速度を変化させることができ、これによって補給水管８５内を流れる補給水Ｗｓの流量を調節することができるように構成されている。   The high-temperature gas-liquid separator 80 is a device that introduces heated water W that has been heated by flowing through the high-temperature heat transfer pipe 12A of the high-temperature absorber 10A and separates it into heated water vapor Wv and heated water liquid Wq. The high-temperature gas-liquid separator 80 and the high-temperature absorber 10A are heated by a heated water introduction pipe 82 as a heated medium flow path that guides the heated water liquid Wq in the high-temperature gas-liquid separator 80 to the high-temperature heat transfer pipe 12A. The heated water outflow pipe 84 that guides the heated water W to the high-temperature gas-liquid separator 80 is connected. In the present embodiment, during the steady operation of the absorption heat pump 1, the heated water Wq is heated at high temperature by a natural circulation action using the bubble head difference between the heated water introduction pipe 82 and the heated water outflow pipe 84 as a driving force. 12A is configured to be supplied. Therefore, the heated water introduction pipe 82 is not provided with a pump for sending the heated water liquid Wq to the high temperature heat transfer pipe 12A. However, if the flow rate of the heated liquid Wq supplied to the high-temperature heat transfer tube 12A cannot be sufficiently obtained due to the arrangement, shape, piping configuration, or the like of the high-temperature gas-liquid separator 80 and the high-temperature absorber 10, heated water A pump for sending the liquid Wq to the high temperature heat transfer tube 12A may be provided. Alternatively, a heated water pump that pumps the heated water Wq to the high temperature heat transfer pipe 12A is provided in the heated water introduction pipe 82, and the high temperature heat transfer pipe 12A is pressurized to generate heated steam Wv outside the high temperature heat transfer pipe 12A. You may do it. When the absorption heat pump 1 is activated, the liquid levels of the high-temperature heat transfer tube 12A and the high-temperature gas-liquid separator 80 that are in communication are substantially the same. The high temperature gas-liquid separator 80 is connected to a heated steam pipe 89 that guides the separated heated steam Wv to the outside of the absorption heat pump 1. Further, a replenishment water pipe 85 for introducing replenishment water Ws for supplementing the heated water W supplied to the outside of the absorption heat pump 1 mainly as steam from the outside of the absorption heat pump 1 is provided. The makeup water pipe 85 is connected to the heated water introduction pipe 82 and is configured to merge the makeup water Ws with the heated water liquid Wq flowing through the heated water introduction pipe 82. The make-up water pipe 85 is provided with a make-up water pump 86 as heated medium supply means for pumping the make-up water Ws toward the high temperature absorber 10A. The makeup water pump 86 is configured to be able to change the rotation speed by an inverter and thereby adjust the flow rate of the makeup water Ws flowing through the makeup water pipe 85.

高温吸収器１０Ａの中間濃度溶液管１５Ａが接続された部分には、高温吸収器１０Ａから流出する中間濃度溶液Ｓｂの温度を検知する高温吸収器出口温度計５１Ａが設けられている。低温吸収器１０Ｂの希溶液管１５Ｂが接続された部分には、低温吸収器１０Ｂから流出する希溶液Ｓｗの温度を検知する低温吸収器出口温度計５１Ｂが設けられている。高温吸収器出口温度計５１Ａ及び低温吸収器出口温度計５１Ｂは、それぞれ流体特性関連値取得手段に相当し、高温吸収器出口温度計５１Ａで検知された値及び低温吸収器出口温度計５１Ｂで検知された値は、共に吸収液特性関連値に相当する。   A high-temperature absorber outlet thermometer 51A for detecting the temperature of the intermediate-concentration solution Sb flowing out from the high-temperature absorber 10A is provided at a portion where the intermediate-concentration solution tube 15A of the high-temperature absorber 10A is connected. A low temperature absorber outlet thermometer 51B for detecting the temperature of the dilute solution Sw flowing out from the low temperature absorber 10B is provided at a portion where the dilute solution tube 15B of the low temperature absorber 10B is connected. The high-temperature absorber outlet thermometer 51A and the low-temperature absorber outlet thermometer 51B correspond to fluid characteristic-related value acquisition means, respectively, and are detected by the high-temperature absorber outlet thermometer 51A and the low-temperature absorber outlet thermometer 51B. Both of these values correspond to the absorption liquid property related values.

制御装置９０は、吸収ヒートポンプ１の運転を制御する機器である。制御装置９０は、中間濃度溶液ポンプ１６Ａ、冷媒液循環ポンプ２６、高濃度溶液ポンプ３５ｐ、冷媒液搬送ポンプ４７、冷媒液供給ポンプ４９、補給水ポンプ８６と、それぞれ信号ケーブルで接続されており、各ポンプの発停及び必要に応じて吐出流量を制御することができるように構成されている。なお、少なくとも冷媒液供給ポンプ４９及び補給水ポンプ８６については、吐出流量を制御することができるように構成されている。また、制御装置９０は、液位検知器４３と信号ケーブルで接続されており、液位検知器４３が検知した液位を信号として受信することができるように構成されている。また、制御装置９０は、蒸発器熱源弁２１ｖ、再生器熱源弁３１ｖ、凝縮器冷却弁４１ｖとそれぞれ信号ケーブルで接続されており、各弁の開閉を制御することができるように構成されている。また、制御装置９０は、高温吸収器出口温度計５１Ａ及び低温吸収器出口温度計５１Ｂとそれぞれ信号ケーブルで接続されており、高温吸収器出口温度計５１Ａで検知された値及び低温吸収器出口温度計５１Ｂで検知された値をそれぞれ信号として受信することができるように構成されている。また、制御装置９０は、低温圧力計６１と信号ケーブルで接続されており、低温圧力計６１で検知された値を信号として受信することができるように構成されている。また、制御装置９０には、吸収ヒートポンプ１の起動時に適した、低温圧力計６１が検知した値と冷媒液供給ポンプ４９の回転速度との関係が、数表（テーブル）として記憶されている。なお、吸収ヒートポンプ１の起動時とは、定常運転に入るまでの運転状態である。   The control device 90 is a device that controls the operation of the absorption heat pump 1. The control device 90 is connected to the intermediate concentration solution pump 16A, the refrigerant liquid circulation pump 26, the high concentration solution pump 35p, the refrigerant liquid transport pump 47, the refrigerant liquid supply pump 49, and the makeup water pump 86 through signal cables, respectively. Each pump is configured to be able to control the discharge flow rate as required, and as required. Note that at least the refrigerant liquid supply pump 49 and the makeup water pump 86 are configured to control the discharge flow rate. The control device 90 is connected to the liquid level detector 43 through a signal cable, and is configured to receive the liquid level detected by the liquid level detector 43 as a signal. In addition, the control device 90 is connected to the evaporator heat source valve 21v, the regenerator heat source valve 31v, and the condenser cooling valve 41v by signal cables, respectively, and is configured to be able to control the opening and closing of each valve. . The control device 90 is connected to the high temperature absorber outlet thermometer 51A and the low temperature absorber outlet thermometer 51B via signal cables, respectively, and the value detected by the high temperature absorber outlet thermometer 51A and the low temperature absorber outlet temperature. Each of the values detected by the total 51B can be received as a signal. The control device 90 is connected to the cryogenic pressure gauge 61 through a signal cable, and is configured to receive a value detected by the cryogenic pressure gauge 61 as a signal. In addition, the control device 90 stores a relationship between a value detected by the low-temperature pressure gauge 61 and the rotation speed of the refrigerant liquid supply pump 49, which is suitable for starting the absorption heat pump 1, as a numerical table. In addition, the time of starting of the absorption heat pump 1 is an operation state until it enters into a steady operation.

引き続き図１を参照して、吸収ヒートポンプ１の作用を説明する。吸収ヒートポンプ１の停止中は、吸収液Ｓの結晶を回避するため、吸収液Ｓが冷媒Ｖで希釈された状態になっている。したがって、再生器３０に貯留されている吸収液Ｓの量が相対的に多く、凝縮器４０に貯留されている冷媒液Ｖｆの量が相対的に少なくなっている。また、各ポンプ１６Ａ、２６、３５ｐ、４７、４９、８６は停止しており、各弁２１ｖ、３１ｖ、４１ｖは閉になっている。吸収ヒートポンプ１を起動すると、吸収液Ｓ及び冷媒Ｖを循環させて吸収ヒートポンプサイクルを行わせることになるが、前述のように吸収ヒートポンプ１の停止中は凝縮器４０に貯留されている冷媒液Ｖｆの量が少ないため、低温伝熱管１２Ｂに供給することができる冷媒液Ｖｆが少ない。また、仮に低温伝熱管１２Ｂに供給することができる冷媒液Ｖｆが十分にあったとしても、起動初期から多量の冷媒液Ｖｆを低温伝熱管１２Ｂに供給すると、供給した冷媒液Ｖｆに吸収熱が奪われて、低温吸収器１０Ｂの昇温昇圧に時間がかかることとなり、定常運転に至るまでに要する時間が多くなる。このことは、高温吸収器１０Ａにおいて起動初期から被加熱水Ｗを高温伝熱管１２Ａに供給した場合にも生じ得る。また、起動当初に低温伝熱管１２Ｂ内の冷媒液Ｖｆの液が高液位にあると、加熱されて蒸発したときに、発生した蒸気が、流れの状況によっては液体を低温吸収器１０Ｂ出口に向けて吹き飛ばし、低温気液分離器６０に過剰な液体が流入して気液分離作用を劣化させる場合がある。このことは、高温吸収器１０Ａにおいて起動初期に高温伝熱管１２Ａ内の被加熱水Ｗの液位が高液位にある場合にも生じ得る。吸収ヒートポンプ１では、上述のような不都合を回避するため、以下のような手順で起動することとしている。   With continued reference to FIG. 1, the operation of the absorption heat pump 1 will be described. While the absorption heat pump 1 is stopped, the absorption liquid S is diluted with the refrigerant V in order to avoid crystals of the absorption liquid S. Therefore, the amount of the absorbing liquid S stored in the regenerator 30 is relatively large, and the amount of the refrigerant liquid Vf stored in the condenser 40 is relatively small. Also, each pump 16A, 26, 35p, 47, 49, 86 is stopped, and each valve 21v, 31v, 41v is closed. When the absorption heat pump 1 is started, the absorption liquid S and the refrigerant V are circulated to perform an absorption heat pump cycle. As described above, the refrigerant liquid Vf stored in the condenser 40 while the absorption heat pump 1 is stopped. Therefore, the refrigerant liquid Vf that can be supplied to the low-temperature heat transfer tube 12B is small. Even if there is sufficient refrigerant liquid Vf that can be supplied to the low-temperature heat transfer tube 12B, if a large amount of refrigerant liquid Vf is supplied to the low-temperature heat transfer pipe 12B from the beginning of startup, the supplied refrigerant liquid Vf has absorbed heat. As a result, it takes time to raise the temperature of the low-temperature absorber 10B, and the time required to reach steady operation increases. This can also occur when the heated water W is supplied to the high-temperature heat transfer tube 12A from the initial startup in the high-temperature absorber 10A. Further, when the refrigerant liquid Vf in the low-temperature heat transfer tube 12B is at a high liquid level at the beginning of startup, when the liquid is heated and evaporated, the generated steam may cause the liquid to flow to the low-temperature absorber 10B outlet depending on the flow situation. In some cases, excessive liquid flows into the low-temperature gas-liquid separator 60 and deteriorates the gas-liquid separation action. This can also occur when the liquid level of the heated water W in the high temperature heat transfer tube 12A is at a high liquid level in the high temperature absorber 10A at the initial start-up. In the absorption heat pump 1, in order to avoid the inconveniences as described above, the absorption heat pump 1 is started in the following procedure.

図２は、吸収ヒートポンプ１の起動時の制御を説明するフローチャートである。制御装置９０は、吸収ヒートポンプ１を起動する旨の指令を受けると、凝縮器冷却弁４１ｖを開にして、冷却水ｃを冷却水管４１に流す（Ｓ１）。これにより、凝縮器４０が冷却され、再生器３０で発生する再生器冷媒蒸気Ｖｇを凝縮する準備ができる。次に、高濃度溶液ポンプ３５ｐ及び中間濃度溶液ポンプ１６Ａを起動する（Ｓ２）。すると、吸収液Ｓが、再生器３０、高温吸収器１０Ａ、低温吸収器１０Ｂの間を循環することとなる。この吸収液Ｓの流れは、再生器３０から見て、高温吸収器１０Ａの吸収液Ｓを間接的に導入し、低温吸収器１０Ｂの吸収液Ｓを直接導入することとなり、高温吸収器１０Ａに吸収液Ｓを直接流出させ、低温吸収器１０Ｂに向けて吸収液Ｓを間接的に流出させることになる。また、制御装置９０は、蒸発器熱源弁２１ｖ及び再生器熱源弁３１ｖを開にして、熱源温水ｈｅを熱源管２１に流すと共に熱源温水ｈｇを熱源管３１に流す（Ｓ３）。これにより、希溶液散布ノズル３２から散布された吸収液Ｓは、熱源管３１を流れる熱源温水ｈｇによって加熱され、吸収液Ｓから冷媒Ｖが離脱して、離脱した冷媒Ｖが再生器冷媒蒸気Ｖｇとして凝縮器４０に流入する。再生器３０から凝縮器４０に流入してきた再生器冷媒蒸気Ｖｇは、冷却水管４１を流れる冷却水ｃによって凝縮して冷媒液Ｖｆとなり、冷媒液貯留部４２に落下する。他方、熱源管２１は、熱源温水ｈｅによって加熱され始める。また、制御装置９０は、冷媒液循環ポンプ２６及び冷媒液搬送ポンプ４７を起動する（Ｓ４）。冷媒液搬送ポンプ４７の起動により凝縮器４０内の冷媒液Ｖｆは蒸発器２０に搬送される。また、冷媒液循環ポンプ２６の起動により、蒸発器２０内に貯留されている冷媒液Ｖｆは冷媒液循環管２５を流れて冷媒液散布ノズル２２から蒸発器２０内に散布される。これにより、冷媒液散布ノズル２２から散布された冷媒液Ｖｆは、熱源管２１を流れる熱源温水ｈｅによって加熱されて蒸発し、蒸発器冷媒蒸気Ｖｅとして低温吸収器１０Ｂに流入する。なお、冷媒液貯留部４２に貯留されている冷媒液Ｖｆの量が多い場合は、工程（Ｓ４）を工程（Ｓ３）の前に行ってもよい。   FIG. 2 is a flowchart for explaining the control at the time of activation of the absorption heat pump 1. When receiving a command to activate the absorption heat pump 1, the control device 90 opens the condenser cooling valve 41v and causes the cooling water c to flow through the cooling water pipe 41 (S1). Thereby, the condenser 40 is cooled, and preparation for condensing the regenerator refrigerant vapor Vg generated in the regenerator 30 is completed. Next, the high concentration solution pump 35p and the intermediate concentration solution pump 16A are activated (S2). Then, the absorbing liquid S circulates between the regenerator 30, the high temperature absorber 10A, and the low temperature absorber 10B. When viewed from the regenerator 30, the flow of the absorption liquid S indirectly introduces the absorption liquid S of the high-temperature absorber 10A and directly introduces the absorption liquid S of the low-temperature absorber 10B, and enters the high-temperature absorber 10A. The absorption liquid S is directly discharged, and the absorption liquid S is indirectly discharged toward the low temperature absorber 10B. Further, the control device 90 opens the evaporator heat source valve 21v and the regenerator heat source valve 31v to flow the heat source hot water he to the heat source pipe 21 and flow the heat source hot water hg to the heat source pipe 31 (S3). As a result, the absorbing liquid S sprayed from the dilute solution spray nozzle 32 is heated by the heat source hot water hg flowing through the heat source pipe 31, and the refrigerant V is detached from the absorbing liquid S, and the separated refrigerant V becomes the regenerator refrigerant vapor Vg. Into the condenser 40. The regenerator refrigerant vapor Vg flowing into the condenser 40 from the regenerator 30 is condensed by the cooling water c flowing through the cooling water pipe 41 to become the refrigerant liquid Vf, and falls into the refrigerant liquid storage part 42. On the other hand, the heat source tube 21 starts to be heated by the heat source hot water he. Further, the control device 90 activates the refrigerant liquid circulation pump 26 and the refrigerant liquid conveyance pump 47 (S4). The refrigerant liquid Vf in the condenser 40 is conveyed to the evaporator 20 by the activation of the refrigerant liquid conveyance pump 47. Further, when the refrigerant liquid circulation pump 26 is activated, the refrigerant liquid Vf stored in the evaporator 20 flows through the refrigerant liquid circulation pipe 25 and is dispersed into the evaporator 20 from the refrigerant liquid spray nozzle 22. Thereby, the refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 22 is heated and evaporated by the heat source hot water he flowing through the heat source pipe 21, and flows into the low-temperature absorber 10B as the evaporator refrigerant vapor Ve. In addition, when there is much quantity of the refrigerant | coolant liquid Vf stored in the refrigerant | coolant liquid storage part 42, you may perform a process (S4) before a process (S3).

上述の各ポンプ３５ｐ、１６Ａ、２６、４７及び弁２１ｖ、３１ｖ、４１ｖの作動により、吸収ヒートポンプ１内の吸収液Ｓ及び冷媒Ｖが吸収ヒートポンプサイクルを開始する。再生器３０において、冷媒Ｖが離脱して濃度が上昇した吸収液Ｓは、高濃度溶液管３５を流れ、高濃度溶液散布ノズル１３Ａから高温吸収器１０Ａ内に散布される。この時点では、高温吸収器１０Ａに低温冷媒蒸気Ｖｂが供給されていないので、高温吸収器１０Ａに流入した吸収液Ｓはそのまま中間濃度溶液管１５Ａに流出する。中間濃度溶液管１５Ａを流れる吸収液Ｓは、中間濃度溶液散布ノズル１３Ｂから低温吸収器１０Ｂ内に散布され、蒸発器２０から流入してきた蒸発器冷媒蒸気Ｖｅを吸収することで吸収熱が発生する。この時点では、低温伝熱管１２Ｂ内に冷媒液Ｖｆが供給されていないので、低温伝熱管１２Ｂ内には、前回運転したときに残存した冷媒液Ｖｆが残っているが、冷媒液Ｖｆの残存量は定常運転時よりも少ない。また、冷媒液導入管６２と再生器３０とを連絡する連絡管（不図示）を設けると共にこの連絡管に止め弁を設けて、吸収ヒートポンプ１の起動前に、低温伝熱管１２Ｂ内に残存している冷媒液Ｖｆを再生器３０に流出させて、低温伝熱管１２Ｂ内の冷媒液Ｖｆの残存量を少なくするか又はなくし、低温伝熱管１２Ｂ内に残存している冷媒液Ｖｆの液位を定常運転時液位より下げてから吸収ヒートポンプ１を起動してもよい。吸収ヒートポンプ１の起動前の定常運転時液位からの液位の下げ幅は、起動時の冷媒液Ｖｆの液位の過度な上昇や、発生した低温冷媒蒸気Ｖｂが冷媒液Ｖｆを低温吸収器１０Ｂの出口に向けて吹き飛ばすことを抑制することができる所定の液位幅がよい。なお、このときの吸収熱による温度上昇は低温伝熱管１２Ｂを損傷させるほど高くないため、内部に流体が流れておらず、あらかじめ内部に溜まっている冷媒液Ｖｆの量が少なくて、低温伝熱管１２Ｂ内の冷媒液Ｖｆの液位が定常運転中の液位より低くても、低温伝熱管１２Ｂが損傷することはない。同様に、高温吸収器１０Ａにおいても、吸収ヒートポンプ１の起動時の高温伝熱管１２Ａ内は、前回運転したときに残存した被加熱水液Ｗｑが残っているが、被加熱水液Ｗｑの残存量は定常運転時よりも少なく、被加熱水液Ｗｑの液位が定常運転中の液位より低くても、高温伝熱管１２Ａが損傷することはない。また、吸収ヒートポンプ１の起動前に、高温伝熱管１２Ａ内に残存している被加熱水液Ｗｑをブロー管（不図示）からあらかじめ排出させて、高温伝熱管１２Ａ内の被加熱水液Ｗｑの残存量を少なくするか又はなくし、高温伝熱管１２Ａ内に残存している被加熱水液Ｗｑの液位を定常運転時液位より下げてから吸収ヒートポンプ１を起動してもよい。吸収ヒートポンプ１の起動前の定常運転時液位からの液位の下げ幅は、起動時の被加熱水液Ｗｑの液位の過度な上昇や、発生した被加熱水蒸気Ｗｖが被加熱水液Ｗｑを高温吸収器１０Ａの出口に向けて吹き飛ばすことを抑制することができる所定の液位幅がよい。低温吸収器１０Ｂで蒸発器冷媒蒸気Ｖｅを吸収して濃度が低下した吸収液Ｓは、希溶液管１５Ｂを流れ、希溶液散布ノズル３２から再生器３０内に散布され、前述のように熱源管３１を流れる熱源温水ｈｇによって加熱され、以降、上記の作用を繰り返す。   By the operation of each of the above-described pumps 35p, 16A, 26, 47 and valves 21v, 31v, 41v, the absorption liquid S and the refrigerant V in the absorption heat pump 1 start an absorption heat pump cycle. In the regenerator 30, the absorbing liquid S whose concentration has increased due to the separation of the refrigerant V flows through the high concentration solution pipe 35 and is sprayed into the high temperature absorber 10 </ b> A from the high concentration solution spray nozzle 13 </ b> A. At this time, since the low-temperature refrigerant vapor Vb is not supplied to the high-temperature absorber 10A, the absorbent S that has flowed into the high-temperature absorber 10A flows out to the intermediate concentration solution tube 15A as it is. The absorbing liquid S flowing through the intermediate concentration solution tube 15A is sprayed into the low temperature absorber 10B from the intermediate concentration solution spray nozzle 13B and absorbs the evaporator refrigerant vapor Ve flowing in from the evaporator 20 to generate absorption heat. . At this time, since the refrigerant liquid Vf is not supplied into the low-temperature heat transfer tube 12B, the refrigerant liquid Vf remaining in the previous operation remains in the low-temperature heat transfer tube 12B, but the remaining amount of the refrigerant liquid Vf Is less than in steady operation. In addition, a communication pipe (not shown) for connecting the refrigerant liquid introduction pipe 62 and the regenerator 30 is provided, and a stop valve is provided for the communication pipe, so that it remains in the low-temperature heat transfer pipe 12B before the absorption heat pump 1 is started. The refrigerant liquid Vf flowing out to the regenerator 30 is used to reduce or eliminate the remaining amount of the refrigerant liquid Vf in the low-temperature heat transfer pipe 12B, and to change the liquid level of the refrigerant liquid Vf remaining in the low-temperature heat transfer pipe 12B. The absorption heat pump 1 may be started after being lowered from the liquid level during steady operation. The amount of decrease in the liquid level from the liquid level during steady operation before startup of the absorption heat pump 1 is that the liquid level of the refrigerant liquid Vf during startup is excessively increased, or the generated low-temperature refrigerant vapor Vb causes the refrigerant liquid Vf to be cooled at low temperature. The predetermined liquid level width which can suppress blowing off toward the exit of 10B is good. Note that the temperature rise due to the absorbed heat at this time is not so high as to damage the low-temperature heat transfer tube 12B. Therefore, the fluid does not flow inside, and the amount of the refrigerant liquid Vf accumulated in the interior is small, so that the low-temperature heat transfer tube Even if the liquid level of the refrigerant liquid Vf in 12B is lower than the liquid level during steady operation, the low-temperature heat transfer tube 12B will not be damaged. Similarly, in the high-temperature absorber 10A, the heated water liquid Wq remaining in the previous operation is left in the high-temperature heat transfer tube 12A when the absorption heat pump 1 is started, but the remaining amount of the heated water liquid Wq remains. Is less than that during steady operation, and the high-temperature heat transfer tube 12A is not damaged even if the liquid level of the heated liquid Wq is lower than the liquid level during steady operation. Further, before the absorption heat pump 1 is started, the heated water liquid Wq remaining in the high temperature heat transfer pipe 12A is discharged in advance from a blow pipe (not shown), and the heated water liquid Wq in the high temperature heat transfer pipe 12A is discharged. The absorption heat pump 1 may be started after reducing or eliminating the remaining amount and lowering the liquid level of the heated water liquid Wq remaining in the high-temperature heat transfer tube 12A from the liquid level during steady operation. The amount of decrease in the liquid level from the liquid level during steady operation before the absorption heat pump 1 is activated is an excessive increase in the liquid level of the heated water liquid Wq at the time of activation, or the generated heated steam Wv is the heated water liquid Wq. Has a predetermined liquid level width that can suppress blowing off toward the outlet of the high-temperature absorber 10A. The absorbing liquid S whose concentration has been reduced by absorbing the evaporator refrigerant vapor Ve in the low temperature absorber 10B flows through the dilute solution pipe 15B, and is dispersed into the regenerator 30 from the dilute solution spray nozzle 32, and as described above, the heat source pipe. It is heated by the heat source hot water hg flowing through 31, and thereafter the above action is repeated.

上述のような部分的な吸収ヒートポンプサイクルを行っている間、制御装置９０は、低温吸収器出口温度計５１Ｂで検知された値が所定の値に到達したか否かを判断する（Ｓ５）。ここで、所定の値は、低温伝熱管１２Ｂ内への冷媒液供給ポンプ４９による冷媒液Ｖｆの供給を開始するのに適した温度であり、例えば、低温伝熱管１２Ｂ内へ冷媒液Ｖｆを供給した場合に冷媒液Ｖｆの少なくとも一部は蒸発する温度あるいは蒸発する温度に近い温度とすることが挙げられる。低温吸収器１０Ｂ内の温度が十分に上昇する前に低温伝熱管１２Ｂ内への冷媒液Ｖｆの供給を開始すると、供給した冷媒液Ｖｆに吸収熱が奪われて、低温吸収器１０Ｂの昇温昇圧に時間がかかることとなる。そこで、低温吸収器出口温度計５１Ｂで検知された値が所定の値に到達するまでは、低温伝熱管１２Ｂ内への冷媒液Ｖｆの供給を開始せず、低温吸収器１０Ｂの昇温昇圧を優先することとしている。低温吸収器出口温度計５１Ｂで検知された値が所定の値に到達したか否かを判断する工程（Ｓ５）において、所定の値に到達していない場合は、再び低温吸収器出口温度計５１Ｂで検知された値が所定の値に到達したか否かを判断する工程（Ｓ５）に戻る。他方、所定の値に到達した場合、制御装置９０は、冷媒液供給ポンプ４９を起動する（Ｓ６）。これにより、冷媒液貯留部４２の冷媒液Ｖｆを、冷媒液管４５、冷媒液管４８、低温気液分離器６０、冷媒液導入管６２を経て低温伝熱管１２Ｂに供給することができる。   While performing the partial absorption heat pump cycle as described above, the control device 90 determines whether or not the value detected by the low-temperature absorber outlet thermometer 51B has reached a predetermined value (S5). Here, the predetermined value is a temperature suitable for starting supply of the refrigerant liquid Vf by the refrigerant liquid supply pump 49 into the low-temperature heat transfer pipe 12B. For example, the refrigerant liquid Vf is supplied into the low-temperature heat transfer pipe 12B. In this case, at least a part of the refrigerant liquid Vf may be set to a temperature at which it evaporates or a temperature close to the evaporating temperature. If the supply of the refrigerant liquid Vf into the low-temperature heat transfer tube 12B is started before the temperature in the low-temperature absorber 10B sufficiently rises, the absorbed heat is deprived by the supplied refrigerant liquid Vf, and the temperature of the low-temperature absorber 10B is increased. It takes time to boost the voltage. Therefore, until the value detected by the low-temperature absorber outlet thermometer 51B reaches a predetermined value, the supply of the refrigerant liquid Vf into the low-temperature heat transfer tube 12B is not started, and the temperature rise and pressure increase of the low-temperature absorber 10B is started. Priority is given. In the step of determining whether or not the value detected by the low-temperature absorber outlet thermometer 51B has reached a predetermined value (S5), if the predetermined value has not been reached, the low-temperature absorber outlet thermometer 51B is again reached. The process returns to the step (S5) for determining whether or not the value detected in (1) has reached a predetermined value. On the other hand, when the predetermined value is reached, the control device 90 activates the refrigerant liquid supply pump 49 (S6). Thereby, the refrigerant liquid Vf in the refrigerant liquid storage part 42 can be supplied to the low-temperature heat transfer pipe 12B via the refrigerant liquid pipe 45, the refrigerant liquid pipe 48, the low-temperature gas-liquid separator 60, and the refrigerant liquid introduction pipe 62.

冷媒液供給ポンプ４９の起動当初は、初めから定格運転にするのではなく、当初は低い回転速度とする。仮に、冷媒液供給ポンプ４９の起動当初から多量の冷媒液Ｖｆを低温伝熱管１２Ｂ内に供給することとすると、低温伝熱管１２Ｂ内の冷媒液Ｖｆの温度上昇が阻害されて起動に時間を要すると共に、冷媒液Ｖｆが蒸発し始めて発生した低温冷媒蒸気Ｖｂの気泡が冷媒液Ｖｆの液位を押し上げ、低温伝熱管１２Ｂ内の液位が高くなりすぎる。低温伝熱管１２Ｂと低温気液分離器６０は、冷媒液導入管６２及び冷媒流出管６４を介して連通しているので、低温伝熱管１２Ｂ内の液位が高いと低温気液分離器６０内の液位も高くなり、低温気液分離器６０における気液分離作用を損なうおそれがある。また、冷媒液Ｖｆが加熱されて発生した低温冷媒蒸気Ｖｂが冷媒液Ｖｆを吹き飛ばし、低温気液分離器６０に過剰な冷媒液Ｖｆが流入して気液分離作用を損なうおそれがある。制御装置９０は、低温圧力計６１で検知した値を記憶されている数表に照らして冷媒液供給ポンプ４９の回転速度を決定している。このことで、低温伝熱管１２Ｂに供給される冷媒液Ｖｆの流量は、緩慢に少しずつ増大していく。さらに、本実施の形態では、液位検知器４３で検知した液位が低い場合は冷媒液供給ポンプ４９の回転速度を低くし、液位検知器４３で検知した液位が上昇するに連れて冷媒液供給ポンプ４９の回転速度を高くするように液位検知器４３で検知した液位に応じて冷媒液供給ポンプ４９の回転速度を調節する。前述のように、吸収ヒートポンプ１の停止時は、吸収液Ｓを希釈しているために冷媒液貯留部４２の液位が低くなっているため、液位検知器４３で検知した液位に応じて冷媒液供給ポンプ４９の回転速度を調節することにより、冷媒液貯留部４２の冷媒液Ｖｆが枯渇することなく、吸収ヒートポンプサイクルを継続することができる。また、液位検知器４３で検知した液位に応じて冷媒液供給ポンプ４９の回転速度を調節することにより、低温吸収器１０Ｂ内の温度上昇が、低温伝熱管１２Ｂ内に供給された冷媒液Ｖｆによって阻害されることを抑制することができる。このように、本実施の形態では、冷媒液供給ポンプ４９が被加熱媒体ポンプを兼ねている。冷媒液供給ポンプ４９を起動すると、低温伝熱管１２Ｂ内に供給された冷媒液Ｖｆは、低温吸収器１０Ｂ内で中間濃度溶液Ｓｂが蒸発器冷媒蒸気Ｖｅを吸収する際に発生する吸収熱によって加熱され、気液二相流（混合流体Ｖｍ）となって低温気液分離器６０に流入する。低温気液分離器６０に流入した混合流体Ｖｍは、気体と液体とに分離され、気体は低温冷媒蒸気Ｖｂとして低温冷媒蒸気管６９を流れて高温吸収器１０Ａに導かれ、液体は冷媒液Ｖｆとして冷媒液導入管６２に流入する。   When the refrigerant liquid supply pump 49 is started, the rated operation is not performed from the beginning, but initially the rotation speed is low. If a large amount of the refrigerant liquid Vf is supplied into the low-temperature heat transfer tube 12B from the beginning of the activation of the refrigerant liquid supply pump 49, the temperature rise of the refrigerant liquid Vf in the low-temperature heat transfer tube 12B is hindered and it takes time to start up. At the same time, the bubbles of the low-temperature refrigerant vapor Vb generated when the refrigerant liquid Vf starts to evaporate push up the liquid level of the refrigerant liquid Vf, and the liquid level in the low-temperature heat transfer tube 12B becomes too high. Since the low-temperature heat transfer tube 12B and the low-temperature gas-liquid separator 60 communicate with each other via the refrigerant liquid introduction tube 62 and the refrigerant outflow tube 64, if the liquid level in the low-temperature heat transfer tube 12B is high, the low-temperature gas-liquid separator 60 The liquid level of the gas becomes high, and the gas-liquid separation action in the low-temperature gas-liquid separator 60 may be impaired. Further, the low-temperature refrigerant vapor Vb generated by heating the refrigerant liquid Vf blows off the refrigerant liquid Vf, and there is a possibility that excessive refrigerant liquid Vf flows into the low-temperature gas-liquid separator 60 and impairs the gas-liquid separation action. The control device 90 determines the rotational speed of the refrigerant liquid supply pump 49 in light of the stored numerical table with the value detected by the low-temperature pressure gauge 61. As a result, the flow rate of the refrigerant liquid Vf supplied to the low-temperature heat transfer tube 12B gradually increases little by little. Furthermore, in the present embodiment, when the liquid level detected by the liquid level detector 43 is low, the rotational speed of the refrigerant liquid supply pump 49 is lowered, and as the liquid level detected by the liquid level detector 43 increases. The rotational speed of the refrigerant liquid supply pump 49 is adjusted according to the liquid level detected by the liquid level detector 43 so as to increase the rotational speed of the refrigerant liquid supply pump 49. As described above, when the absorption heat pump 1 is stopped, since the absorption liquid S is diluted, the liquid level in the refrigerant liquid storage unit 42 is low, so that the liquid level detector 43 detects the liquid level. By adjusting the rotational speed of the refrigerant liquid supply pump 49, the absorption heat pump cycle can be continued without the refrigerant liquid Vf in the refrigerant liquid storage section 42 being depleted. Further, by adjusting the rotational speed of the refrigerant liquid supply pump 49 in accordance with the liquid level detected by the liquid level detector 43, the temperature rise in the low temperature absorber 10B is caused by the refrigerant liquid supplied into the low temperature heat transfer pipe 12B. Inhibition by Vf can be suppressed. Thus, in the present embodiment, the refrigerant liquid supply pump 49 also serves as a heated medium pump. When the refrigerant liquid supply pump 49 is activated, the refrigerant liquid Vf supplied into the low-temperature heat transfer tube 12B is heated by absorption heat generated when the intermediate concentration solution Sb absorbs the evaporator refrigerant vapor Ve in the low-temperature absorber 10B. The gas-liquid two-phase flow (mixed fluid Vm) flows into the low-temperature gas-liquid separator 60. The mixed fluid Vm that has flowed into the low-temperature gas-liquid separator 60 is separated into a gas and a liquid. The gas flows as a low-temperature refrigerant vapor Vb through the low-temperature refrigerant vapor pipe 69 and is guided to the high-temperature absorber 10A, and the liquid is the refrigerant liquid Vf. As shown in FIG.

冷媒液供給ポンプ４９を起動したら（Ｓ６）、制御装置９０は、高温吸収器出口温度計５１Ａで検知された値が所定の値に到達したか否かを判断する（Ｓ７）。ここでの、所定の値は、高温伝熱管１２Ａ内への被加熱水液Ｗｑの供給を開始するのに適した温度であり、例えば、高温伝熱管１２Ａ内へ被加熱水液Ｗｑを供給した場合に被加熱水液Ｗｑの少なくとも一部は蒸発する温度あるいは蒸発する温度に近い温度とすることが挙げられる。高温伝熱管１２Ａ内の温度が十分に上昇する前に高温伝熱管１２Ａ内への被加熱水液Ｗｑの供給を開始すると、供給した被加熱水液Ｗｑに吸収熱が奪われて、高温伝熱管１２Ａの昇温昇圧に時間がかかることとなる。そこで、高温吸収器出口温度計５１Ａで検知された値が所定の値に到達するまでは、高温伝熱管１２Ａ内への被加熱水液Ｗｑの供給を開始せず、高温伝熱管１２Ａの昇温昇圧を優先することとしている。高温吸収器出口温度計５１Ａで検知された値が所定の値に到達したか否かを判断する工程（Ｓ７）において、所定の値に到達していない場合は、再び高温吸収器出口温度計５１Ａで検知された値が所定の値に到達したか否かを判断する工程（Ｓ７）に戻る。他方、所定の値に到達した場合、制御装置９０は、補給水ポンプ８６を起動して高温伝熱管１２Ａ内に被加熱水液Ｗｑを供給する（Ｓ８）。高温吸収器出口温度計５１Ａで検知された値が所定の値に到達していれば、被加熱水液Ｗｑを加熱する吸収熱量が旺盛だと判断できる。なお、高温伝熱管１２Ａへの被加熱水液Ｗｑの供給開始の判定精度を高めるために、以下のようにしてもよい。すなわち、高温伝熱管１２Ａ内に被加熱水Ｗが残存している場合は、高温吸収器出口温度計５１Ａで検知された値が所定の値に到達した場合であって、さらに、高温伝熱管１２Ａの出口における被加熱水Ｗの温度を検知して、この検知した温度が所定の値に到達した場合に、高温伝熱管１２Ａへの被加熱水液Ｗｑの供給開始と判断してもよい。ここで、高温伝熱管１２Ａの出口における被加熱水Ｗの温度に代えて、高温伝熱管１２Ａ内の圧力から算出される飽和温度、又は高温気液分離器８０における被加熱水Ｗの温度もしくは圧力から算出される飽和温度、又はこれらと相関を有する値を検知することとしてもよい。このことは、被加熱水Ｗを冷媒液Ｖｆと読み替え、高温吸収器１０Ａの各流体特性関連値を、対応する低温吸収器１０Ｂの各流体特性関連値に読み替えれば、低温吸収器１０Ｂにおいても同様に成り立つ。   When the refrigerant liquid supply pump 49 is activated (S6), the control device 90 determines whether or not the value detected by the high temperature absorber outlet thermometer 51A has reached a predetermined value (S7). Here, the predetermined value is a temperature suitable for starting the supply of the heated water liquid Wq into the high temperature heat transfer tube 12A. For example, the heated water liquid Wq is supplied into the high temperature heat transfer tube 12A. In this case, at least a part of the heated water liquid Wq is set to a temperature at which it evaporates or a temperature close to the evaporating temperature. If the supply of the heated water liquid Wq into the high temperature heat transfer tube 12A is started before the temperature in the high temperature heat transfer tube 12A sufficiently rises, the absorbed heat is deprived by the supplied heated water liquid Wq, and the high temperature heat transfer tube It takes time to raise the temperature of 12A. Therefore, until the value detected by the high-temperature absorber outlet thermometer 51A reaches a predetermined value, the supply of the heated liquid Wq into the high-temperature heat transfer tube 12A is not started, and the temperature of the high-temperature heat transfer tube 12A is increased. Boosting is given priority. In the step of determining whether or not the value detected by the high temperature absorber outlet thermometer 51A has reached a predetermined value (S7), if the predetermined value has not been reached, the high temperature absorber outlet thermometer 51A is again reached. The process returns to the step (S7) of determining whether or not the value detected in (1) has reached a predetermined value. On the other hand, when the predetermined value is reached, the controller 90 activates the makeup water pump 86 and supplies the heated liquid Wq into the high temperature heat transfer tube 12A (S8). If the value detected by the high-temperature absorber outlet thermometer 51A reaches a predetermined value, it can be determined that the amount of absorbed heat for heating the heated liquid Wq is vigorous. In addition, in order to raise the determination precision of the supply start of the to-be-heated water liquid Wq to the high temperature heat exchanger tube 12A, you may be as follows. That is, when the to-be-heated water W remains in the high-temperature heat transfer tube 12A, the value detected by the high-temperature absorber outlet thermometer 51A reaches a predetermined value, and further, the high-temperature heat transfer tube 12A. The temperature of the heated water W at the outlet of the water may be detected, and when the detected temperature reaches a predetermined value, it may be determined that the supply of the heated water liquid Wq to the high-temperature heat transfer tube 12A is started. Here, instead of the temperature of the heated water W at the outlet of the high temperature heat transfer tube 12A, the saturation temperature calculated from the pressure in the high temperature heat transfer tube 12A, or the temperature or pressure of the heated water W in the high temperature gas-liquid separator 80 It is good also as detecting the saturation temperature computed from these, or the value which has a correlation with these. This means that if the water to be heated W is read as the refrigerant liquid Vf and each fluid characteristic related value of the high temperature absorber 10A is read as each fluid characteristic related value of the corresponding low temperature absorber 10B, also in the low temperature absorber 10B. The same holds true.

補給水ポンプ８６の起動を開始した当初は、比較的少ない流量の被加熱水液Ｗｑを吐出するように補給水ポンプ８６の回転速度を調節するとよい。仮に、補給水ポンプ８６の起動当初から多量の被加熱水液Ｗｑを高温伝熱管１２Ａ内に供給することとすると、高温伝熱管１２Ａ内の被加熱水Ｗの温度上昇が阻害されて起動に時間を要すると共に、被加熱水液Ｗｑが蒸発し始めて発生した被加熱水蒸気Ｗｖの気泡が被加熱水液Ｗｑの液位を押し上げ、高温伝熱管１２Ａ内の液位が高くなりすぎる。高温伝熱管１２Ａと高温気液分離器８０は、被加熱水導入管８２及び被加熱水流出管８４を介して連通しているので、高温伝熱管１２Ａ内の液位が高いと高温気液分離器８０内の液位も高くなり、気液分離作用を損なうおそれがある。また、被加熱水液Ｗｑが加熱されて発生した被加熱水蒸気Ｗｖが被加熱水液Ｗｑを吹き飛ばし、高温気液分離器８０に過剰な被加熱水液Ｗｑが流入して気液分離作用を損なうおそれがある。そこで、補給水ポンプ８６の起動当初は比較的少ない流量の被加熱水液Ｗｑを吐出するようにすると、高温吸収器１０Ａ内の温度上昇が、高温伝熱管１２Ａ内に供給された被加熱水Ｗによって阻害されることを抑制することができると共に、起動中の高温伝熱管１２Ａ内の過度な液位上昇と被加熱水Ｗの吹き飛ばしを抑制して良好な気液分離を実現することができる。起動工程が進むと、高温伝熱管１２Ａ内に供給された被加熱水液Ｗｑは、高温吸収器１０Ａ内で高濃度溶液Ｓａが低温冷媒蒸気Ｖｂを吸収する際に発生する吸収熱によって加熱され、気液二相流（混合被加熱水Ｗｍ）となって高温気液分離器８０に流入する。高温気液分離器８０に流入した混合被加熱水Ｗｍは、気体と液体とに分離され、気体は被加熱水蒸気Ｗｖとして被加熱水蒸気管８９を流れて利用場所に導かれ、液体は被加熱水液Ｗｑとして被加熱水導入管８２に流入する。   When the start-up of the make-up water pump 86 is started, the rotational speed of the make-up water pump 86 may be adjusted so as to discharge the heated liquid Wq having a relatively small flow rate. If a large amount of heated liquid Wq is supplied into the high-temperature heat transfer pipe 12A from the beginning of the replenishment water pump 86, the temperature rise of the heated water W in the high-temperature heat transfer pipe 12A is hindered and it takes time to start up. In addition, bubbles of the heated water vapor Wv generated when the heated water liquid Wq starts to evaporate push up the liquid level of the heated water liquid Wq, and the liquid level in the high-temperature heat transfer tube 12A becomes too high. Since the high-temperature heat transfer tube 12A and the high-temperature gas-liquid separator 80 communicate with each other via the heated water introduction tube 82 and the heated water outflow tube 84, the high-temperature gas-liquid separation occurs when the liquid level in the high-temperature heat transfer tube 12A is high. The liquid level in the vessel 80 is also increased, and the gas-liquid separation action may be impaired. Further, the heated water vapor Wv generated by heating the heated water liquid Wq blows off the heated water liquid Wq, and the excessive heated water liquid Wq flows into the high-temperature gas-liquid separator 80 to impair the gas-liquid separation action. There is a fear. Therefore, if the heated water liquid Wq having a relatively small flow rate is discharged at the beginning of the makeup water pump 86, the temperature rise in the high-temperature absorber 10A is caused by the heated water W supplied into the high-temperature heat transfer pipe 12A. Can be suppressed, and an excessive rise in liquid level in the high-temperature heat transfer tube 12 </ b> A during startup and blowing off of the heated water W can be suppressed to achieve good gas-liquid separation. As the start-up process proceeds, the heated liquid Wq supplied into the high-temperature heat transfer tube 12A is heated by the absorbed heat generated when the high-concentration solution Sa absorbs the low-temperature refrigerant vapor Vb in the high-temperature absorber 10A. The gas-liquid two-phase flow (mixed heated water Wm) flows into the high-temperature gas-liquid separator 80. The mixed heated water Wm that has flowed into the high-temperature gas-liquid separator 80 is separated into a gas and a liquid, and the gas flows as a heated water vapor Wv through the heated water vapor pipe 89 and is guided to a use place, and the liquid is heated water. It flows into the heated water introduction pipe 82 as the liquid Wq.

制御装置９０は、補給水ポンプ８６を起動したら（Ｓ８）、高温気液分離器８０に過剰な被加熱水液Ｗｑが流入することを抑制するため、高温伝熱管１２Ａに供給される被加熱水液Ｗｑが、高温吸収器出口温度計５１Ａで検知した値が上昇するに連れて増加するように、補給水ポンプ８６の回転速度を徐々に上げるようにする。吸収ヒートポンプ１の起動後、高温吸収器１０Ａの温度は徐々に上昇するため、高温伝熱管１２Ａ内で蒸発する被加熱水液Ｗｑも徐々に増加するので、高温伝熱管１２Ａに供給される被加熱水液Ｗｑが徐々に増加することで、高温気液分離器８０に過剰な被加熱水液Ｗｑが流入することを抑制することができる。また、制御装置９０は、高温気液分離器８０内の被加熱水液Ｗｑの液位が徐々に上昇するように補給水ポンプ８６を制御している際に、高温気液分離器８０内の液位があらかじめ設定された定常運転時の液位になったか否か、及び高温気液分離器８０内の圧力があらかじめ設定された定常運転時の圧力になったか否かを判断する（Ｓ９）。高温気液分離器８０内が定常運転時の液位及び圧力になっていない場合は、再び高温気液分離器８０内が定常運転時の液位及び圧力になったか否かを判断する工程（Ｓ９）に戻る。他方、高温気液分離器８０内が定常運転時の液位及び圧力になった場合は、これまで説明した起動時の制御を終了し、定常運転時の制御に移行する。定常運転時は、被加熱水蒸気Ｗｖが利用場所に供給され、高温気液分離器８０内の被加熱水液Ｗｑが少なくなったら、制御装置９０は適宜補給水ポンプ８６を起動して、補給水Ｗｓを吸収ヒートポンプ１内に導入する。制御装置９０は、補給水Ｗｓの導入が完了したら、補給水ポンプ８６を停止する。   When the replenishing water pump 86 is activated (S8), the control device 90 controls the heated water supplied to the high-temperature heat transfer tube 12A in order to prevent the excessive heated liquid Wq from flowing into the high-temperature gas-liquid separator 80. The rotational speed of the makeup water pump 86 is gradually increased so that the liquid Wq increases as the value detected by the high-temperature absorber outlet thermometer 51A increases. Since the temperature of the high-temperature absorber 10A gradually rises after the absorption heat pump 1 is started, the heated liquid Wq that evaporates in the high-temperature heat transfer tube 12A also gradually increases, so the heated heat supplied to the high-temperature heat transfer tube 12A By gradually increasing the water liquid Wq, it is possible to suppress the excessive heated liquid Wq from flowing into the high-temperature gas-liquid separator 80. Further, the control device 90 controls the makeup water pump 86 so that the level of the heated water liquid Wq in the high temperature gas-liquid separator 80 gradually rises. It is determined whether or not the liquid level has reached a preset level for steady operation, and whether or not the pressure in the high-temperature gas-liquid separator 80 has reached a preset normal operation pressure (S9). . When the liquid level and pressure in the high-temperature gas-liquid separator 80 are not at the liquid level and pressure at the time of steady operation, the process of determining again whether the liquid level and pressure at the high-temperature gas-liquid separator 80 is at the normal operation ( Return to S9). On the other hand, when the temperature and pressure in the high-temperature gas-liquid separator 80 reach the liquid level and pressure during the steady operation, the control at the start-up described so far is terminated and the control proceeds to the control during the steady operation. At the time of steady operation, when the heated steam Wv is supplied to the place of use and the heated water liquid Wq in the high-temperature gas-liquid separator 80 decreases, the control device 90 activates the make-up water pump 86 as appropriate to make up the make-up water. Ws is introduced into the absorption heat pump 1. When the introduction of the makeup water Ws is completed, the control device 90 stops the makeup water pump 86.

以上で説明したように、本実施の形態に係る吸収ヒートポンプ１によれば、起動時に、低温吸収器出口温度計５１Ｂで検知した値が所定の値に到達したときに低温伝熱管１２Ｂ内への冷媒液Ｖｆの供給を開始し、高温吸収器出口温度計５１Ａで検知した値が所定の値に到達したときに高温伝熱管１２Ａ内への被加熱水Ｗの供給を開始すると共に、低温圧力計６１が検知した値及び液位検知器４３が検知した液位が上昇するに連れて低温伝熱管１２Ｂ内に供給する冷媒液Ｖｆの流量が増加し、高温吸収器出口温度計５１Ａで検知した値が増加するに連れて高温伝熱管１２Ａに供給する被加熱水Ｗの流量が増加するように制御するので、吸収ヒートポンプ１を緩慢に立ち上げることができ、低温気液分離器６０及び高温気液分離器８０に過剰な液体が流入して気液分離作用が損なわれることを抑制することができ、低温吸収器１０Ｂ及び高温吸収器１０Ａの昇温昇圧に要する時間が長くなることを抑制することができる。   As described above, according to the absorption heat pump 1 according to the present embodiment, when the value detected by the low-temperature absorber outlet thermometer 51B reaches a predetermined value during startup, The supply of the refrigerant liquid Vf is started, and when the value detected by the high temperature absorber outlet thermometer 51A reaches a predetermined value, the supply of the heated water W into the high temperature heat transfer tube 12A is started, and the low temperature pressure gauge As the liquid level detected by 61 and the liquid level detected by the liquid level detector 43 rise, the flow rate of the refrigerant liquid Vf supplied into the low-temperature heat transfer tube 12B increases, and the value detected by the high-temperature absorber outlet thermometer 51A. As the flow rate increases, the flow rate of the heated water W supplied to the high temperature heat transfer tube 12A is controlled to increase, so that the absorption heat pump 1 can be started up slowly, and the low temperature gas-liquid separator 60 and the high temperature gas liquid Excess liquid in separator 80 There can be suppressed that the gas-liquid separating effect and flows is impaired, it is possible to suppress the time required for raising the temperature and pressure of the cold absorber 10B and the high temperature absorber 10A becomes longer.

以上で説明した吸収ヒートポンプ１において、高温吸収器１０Ａ及び／又は低温吸収器１０Ｂの構造を以下のようにすると、伝熱管から気液分離器へ液体が過剰に流出してしまうことを抑制する効果をさらに高めることができる。   In the absorption heat pump 1 described above, when the structure of the high-temperature absorber 10A and / or the low-temperature absorber 10B is as follows, the effect of suppressing the liquid from flowing out excessively from the heat transfer tube to the gas-liquid separator. Can be further enhanced.

図３は、本発明の実施の形態に係る吸収ヒートポンプ１の高温吸収器１０Ａまわりの一例を示す断面図である。高温吸収器１０Ａは、高温伝熱管１２Ａと高濃度溶液散布ノズル１３Ａとが缶胴１１内に収容され、缶胴１１の外側に被加熱媒体室形成部材としての水室形成部材１４が設けられて構成されている。水室形成部材１４は、各高温伝熱管１２Ａに被加熱水Ｗを供給し、あるいは各高温伝熱管１２Ａから被加熱水Ｗを収集する被加熱媒体室としての水室を内部に形成する部材である。缶胴１１は、典型的には設置されたときに横長になるように形成されている。   FIG. 3 is a cross-sectional view showing an example around the high-temperature absorber 10A of the absorption heat pump 1 according to the embodiment of the present invention. The high-temperature absorber 10 </ b> A includes a high-temperature heat transfer tube 12 </ b> A and a high-concentration solution spray nozzle 13 </ b> A housed in a can body 11, and a water chamber forming member 14 as a heated medium chamber forming member is provided outside the can body 11. It is configured. The water chamber forming member 14 is a member that forms a water chamber as a heated medium chamber that supplies heated water W to each high temperature heat transfer tube 12A or collects heated water W from each high temperature heat transfer tube 12A. is there. The can body 11 is typically formed to be horizontally long when installed.

高温伝熱管１２Ａは、本実施の形態では、直線状に形成されたものの複数が缶胴１１内に設けられている。高温伝熱管１２Ａは、横長の缶胴１１の一端及びその反対側の他端に接合している。缶胴１１の、高温伝熱管１２Ａが接合する面は、高温伝熱管１２Ａを挿通することができる孔が形成された管板（伝熱管プレート）として形成されている。缶胴１１の両端の管板に接合した高温伝熱管１２Ａは、内部が缶胴１１の内部と連通しないようになっている。換言すれば、高温伝熱管１２Ａ内を流れる被加熱水Ｗと、缶胴１１内に流出入する吸収液Ｓ及び冷媒Ｖとが混合しないように構成されている。具体例を示すと、高温伝熱管１２Ａは、缶胴１１の管板に形成された孔に拡管され固定されている。   In the present embodiment, a plurality of high-temperature heat transfer tubes 12 </ b> A formed in a straight line are provided in the can body 11. The high-temperature heat transfer tube 12A is joined to one end of the horizontally long can body 11 and the other end on the opposite side. The surface of the can body 11 to which the high temperature heat transfer tube 12A is joined is formed as a tube plate (heat transfer tube plate) in which a hole through which the high temperature heat transfer tube 12A can be inserted is formed. The high-temperature heat transfer tube 12 </ b> A joined to the tube plates at both ends of the can body 11 does not communicate with the inside of the can body 11. In other words, the heated water W flowing in the high-temperature heat transfer tube 12 </ b> A is not mixed with the absorbing liquid S and the refrigerant V flowing into and out of the can body 11. As a specific example, the high temperature heat transfer tube 12 </ b> A is expanded and fixed in a hole formed in the tube plate of the can body 11.

高温伝熱管１２Ａは、本実施の形態では、その機能により、予熱管１２ｐと蒸発管１２ｅとに区別される。予熱管１２ｐは、被加熱水液Ｗｑを導入し、導入した被加熱水液Ｗｑを吸収熱で加熱して昇温させる管である。蒸発管１２ｅは、予熱管１２ｐにおいて加熱された被加熱水液Ｗｑを導入し、導入した被加熱水液Ｗｑを吸収熱で蒸発させる管である。蒸発管１２ｅでは、一端から流入した被加熱水液Ｗｑの少なくとも一部が、他端から流出するまでに蒸発して被加熱水蒸気Ｗｖとなる。蒸発管１２ｅは、予熱管１２ｐよりも上方に配置されている。各高温伝熱管１２Ａは、本実施の形態では、予熱管１２ｐ及び蒸発管１２ｅ共に、軸線が水平になるように配置されている。蒸発管１２ｅ内で被加熱水液Ｗｑを加熱沸騰させることを考慮すると、蒸発管１２ｅをその軸線が鉛直になるように配置することも考えられる。しかし、本実施の形態では、散布された吸収液Ｓを蒸発管１２ｅの外面に薄い液膜としてできるだけ多く接触させる観点から、蒸発管１２ｅを軸線が水平になるように配置することとしている。また、製造を簡便にする観点から、予熱管１２ｐも、蒸発管１２ｅと同様に、軸線が水平になるように配置することとしている。   In the present embodiment, the high temperature heat transfer tube 12A is classified into a preheating tube 12p and an evaporation tube 12e according to the function. The preheating pipe 12p is a pipe that introduces the heated water liquid Wq and heats the introduced heated water liquid Wq with absorption heat to raise the temperature. The evaporation pipe 12e is a pipe that introduces the heated water liquid Wq heated in the preheating pipe 12p and evaporates the introduced heated water liquid Wq with absorbed heat. In the evaporation pipe 12e, at least a part of the heated water liquid Wq flowing from one end evaporates until it flows out from the other end to become heated steam Wv. The evaporation pipe 12e is disposed above the preheating pipe 12p. In each of the high-temperature heat transfer tubes 12A, the preheating tube 12p and the evaporation tube 12e are arranged so that their axes are horizontal. In consideration of heating and boiling the heated water liquid Wq in the evaporation pipe 12e, it is conceivable to arrange the evaporation pipe 12e so that its axis is vertical. However, in the present embodiment, the evaporation pipe 12e is arranged so that the axis is horizontal from the viewpoint of bringing the dispersed absorbent S into contact with the outer surface of the evaporation pipe 12e as much as possible as a thin liquid film. Further, from the viewpoint of simplifying manufacturing, the preheating pipe 12p is also arranged so that the axis is horizontal, like the evaporation pipe 12e.

缶胴１１内に設けられる高温伝熱管１２Ａのうち、鉛直方向最下部に配置される予熱管１２ｐは、その下方に中間濃度溶液Ｓｂが貯留される部分（空間）が確保される位置に配置されている。このように構成されることで、定常運転時に高温伝熱管１２Ａが吸収液Ｓに没入することがなく、高温伝熱管１２Ａの表面に濡れ広がった高濃度溶液Ｓａに低温冷媒蒸気Ｖｂが吸収されるようになるため、高濃度溶液Ｓａと低温冷媒蒸気Ｖｂとの接触面積を大きくできると共に、発生した吸収熱が高温伝熱管１２Ａを流れる被加熱水Ｗに速やかに伝わり、吸収能力の回復を早めることができる。他方、缶胴１１の最上部に配置される蒸発管１２ｅは、高濃度溶液散布ノズル１３Ａが設置できる空間が確保される位置に配置されている。   Of the high-temperature heat transfer tubes 12A provided in the can body 11, the preheat tube 12p disposed at the lowest in the vertical direction is disposed at a position where a portion (space) in which the intermediate concentration solution Sb is stored is secured below. ing. With this configuration, the high-temperature heat transfer tube 12A is not immersed in the absorbing liquid S during steady operation, and the low-temperature refrigerant vapor Vb is absorbed by the high-concentration solution Sa that spreads wet on the surface of the high-temperature heat transfer tube 12A. As a result, the contact area between the high-concentration solution Sa and the low-temperature refrigerant vapor Vb can be increased, and the generated absorption heat is quickly transmitted to the heated water W flowing through the high-temperature heat transfer pipe 12A, thereby speeding up the recovery of the absorption capacity. Can do. On the other hand, the evaporation pipe 12e arranged at the uppermost part of the can body 11 is arranged at a position where a space in which the high concentration solution spray nozzle 13A can be installed is secured.

水室形成部材１４は、各高温伝熱管１２Ａの端部が接合している缶胴１１の両面（管板）に取り付けられている。水室形成部材１４は、一面が開口した直方体状の部材であり、その開口した面が、缶胴１１の管板に取り付けられている複数の高温伝熱管１２Ａの一端を覆うように、缶胴１１の管板に取り付けられている。水室形成部材１４が缶胴１１の管板に取り付けられることにより、水室形成部材１４と缶胴１１の管板とに囲まれた空間が水室となる。水室は、各高温伝熱管１２Ａの内部と連通している。つまり、水室には被加熱水Ｗが流出入するようになっている。水室形成部材１４の内部を区画して複数の水室を形成する場合は、水室形成部材１４の内部に仕切板１４ｗが設けられる。仕切板１４ｗによって区画された各水室には、その水室に流入する被加熱水Ｗを流す高温伝熱管１２Ａの一端、及び／又は、その水室から流出した被加熱水Ｗを流す高温伝熱管１２Ａの一端とが連通している。   The water chamber forming member 14 is attached to both surfaces (tube plates) of the can body 11 to which the end portions of the respective high temperature heat transfer tubes 12A are joined. The water chamber forming member 14 is a rectangular parallelepiped member whose one surface is open, and the open surface covers the one end of the plurality of high-temperature heat transfer tubes 12A attached to the tube plate of the can body 11. It is attached to 11 tube sheets. By attaching the water chamber forming member 14 to the tube plate of the can body 11, a space surrounded by the water chamber forming member 14 and the tube plate of the can body 11 becomes a water chamber. The water chamber communicates with the inside of each high-temperature heat transfer tube 12A. That is, the heated water W flows into and out of the water chamber. When the interior of the water chamber forming member 14 is partitioned to form a plurality of water chambers, a partition plate 14 w is provided inside the water chamber forming member 14. In each of the water chambers partitioned by the partition plate 14w, one end of the high-temperature heat transfer pipe 12A through which the heated water W flowing into the water chamber flows and / or the high-temperature transmission through which the heated water W flowing out of the water chamber flows. One end of the heat tube 12A is in communication.

仕切板１４ｗは、ある１つの水室に被加熱水Ｗを流出入させる１本又は２本以上の高温伝熱管１２Ａが、反対側の水室では異なる水室に連通するように設置されている。これにより、各高温伝熱管１２Ａ及び水室を流れる被加熱水Ｗは、最上流に位置する水室からこれに連通する高温伝熱管１２Ａを一方の向きに流れ、反対側の水室で流れの向きを変えてこれに連通する別の高温伝熱管１２Ａを一方の向きとは反対の向きに流れるというように、全体として蛇行する１つの流れとなって高温吸収器１０Ａ内を通過するように構成されている。また、仕切板１４ｗは、各高温伝熱管１２Ａ及び水室を全体として１つの流れとして流れる被加熱水Ｗが、高温吸収器１０Ａ内を全体として下方から上方に向かう流れとなるように水室を区画するべく設置されている。   The partition plate 14w is installed so that one or two or more high-temperature heat transfer tubes 12A that allow the heated water W to flow into and out of a certain water chamber communicate with different water chambers in the opposite water chamber. . As a result, the heated water W flowing through each of the high temperature heat transfer tubes 12A and the water chamber flows from the water chamber located at the uppermost stream to the high temperature heat transfer tube 12A communicating with the water chamber in one direction, and flows in the opposite water chamber. It is configured to pass through the high-temperature absorber 10A as a whole meandering flow, such that another high-temperature heat transfer tube 12A that changes its direction and communicates with the other high-temperature heat transfer tube 12A flows in a direction opposite to one direction. Has been. In addition, the partition plate 14w has a water chamber so that the heated water W that flows as a single flow through the high-temperature heat transfer tubes 12A and the water chamber as a whole flows from below to above in the high-temperature absorber 10A as a whole. It is installed to partition.

缶胴１１の両面にそれぞれ取り付けられている２つの水室形成部材１４のうち、一方の水室形成部材１４内の水室は、仕切板１４ｗで仕切られることによって、低温液室１４ｐｓと、混合流体室１４ｅｃとに区画されている。また、他方の水室形成部材１４内の水室は、仕切板１４ｗが設けられておらず、全体が高温液室１４ｅｓとなっている。   Of the two water chamber forming members 14 attached to both surfaces of the can body 11, the water chamber in one water chamber forming member 14 is partitioned by the partition plate 14w, thereby mixing with the low temperature liquid chamber 14ps. It is partitioned into a fluid chamber 14ec. Further, the water chamber in the other water chamber forming member 14 is not provided with the partition plate 14w, and the whole is a high temperature liquid chamber 14es.

低温液室１４ｐｓには、図３に示す側面断面図上において、１本又は２本以上の予熱管１２ｐの一端が接続されている。一端が低温液室１４ｐｓに接続されたすべての予熱管１２ｐの他端は、高温液室１４ｅｓに接続されている。このように、本実施の形態では、低温液室１４ｐｓと高温液室１４ｅｓとを連絡する予熱管１２ｐの、１種類の予熱管１２ｐが設けられている。ここで、低温液室１４ｐｓは、１種類の予熱管１２ｐに被加熱水液Ｗｑを供給する水室であり、予熱管供給部として機能する。高温液室１４ｅｓは、１種類の予熱管１２ｐで加熱された被加熱水液Ｗｑを回収する水室であり、予熱管回収部として機能する。本実施の形態では、予熱管１２ｐが１パスで構成されている。ここで、「パス」とは、ある高温伝熱管１２Ａ内を流れる流体が、他の高温伝熱管１２Ａ内の流体と合流することなく、かつ、流れ方向を１８０度変えることなく、流れる流路の単位である。パスは、高温伝熱管１２Ａ内を流れる流体が、流れ方向を１８０度変えず、途中で合流しない限り、高温伝熱管１２Ａの数を問わない。   One end of one or two or more preheating tubes 12p is connected to the low temperature liquid chamber 14ps in the side sectional view shown in FIG. The other ends of all the preheating pipes 12p whose one ends are connected to the low temperature liquid chamber 14ps are connected to the high temperature liquid chamber 14es. Thus, in the present embodiment, one kind of preheating pipe 12p is provided, which is the preheating pipe 12p that connects the low temperature liquid chamber 14ps and the high temperature liquid chamber 14es. Here, the low-temperature liquid chamber 14ps is a water chamber that supplies the heated liquid Wq to one kind of preheating pipe 12p, and functions as a preheating pipe supply unit. The high-temperature liquid chamber 14es is a water chamber that collects the heated water liquid Wq heated by one type of preheating pipe 12p, and functions as a preheating pipe collection unit. In the present embodiment, the preheating tube 12p is configured with one pass. Here, “pass” refers to a flow path in which a fluid flowing in a certain high-temperature heat transfer tube 12A does not merge with a fluid in another high-temperature heat transfer tube 12A and does not change the flow direction by 180 degrees. Unit. The number of the high-temperature heat transfer tubes 12A is not limited as long as the fluid flowing in the high-temperature heat transfer tubes 12A does not change the flow direction by 180 degrees and merges in the middle.

高温液室１４ｅｓには、上述した予熱管１２ｐの他に、複数の蒸発管１２ｅの一端が接続されている。一端が高温液室１４ｅｓに接続されたすべての蒸発管１２ｅの他端は、混合流体室１４ｅｃに接続されている。本実施の形態では、缶胴１１内に配設されたすべての蒸発管１２ｅについて、一端が高温液室１４ｅｓに接続され、他端が混合流体室１４ｅｃに接続されている。ここで、高温液室１４ｅｓは、複数の蒸発管１２ｅへ被加熱水液Ｗｑを分配する水室であり、蒸発管分配部に相当する。つまり、高温液室１４ｅｓは、予熱管回収部と蒸発管分配部とを兼ねている。また、混合流体室１４ｅｃは、複数の蒸発管１２ｅから被加熱水Ｗを回収する水室であり、蒸発管収集部に相当する。混合流体室１４ｅｃの上部（典型的には頂部）には、被加熱水流出管８４が接続されている。   In addition to the preheating pipe 12p described above, one end of a plurality of evaporation pipes 12e is connected to the high temperature liquid chamber 14es. The other ends of all the evaporation pipes 12e whose one ends are connected to the high temperature liquid chamber 14es are connected to the mixed fluid chamber 14ec. In the present embodiment, one end of each of the evaporation pipes 12e disposed in the can body 11 is connected to the high temperature liquid chamber 14es, and the other end is connected to the mixed fluid chamber 14ec. Here, the high temperature liquid chamber 14es is a water chamber that distributes the heated liquid Wq to the plurality of evaporation pipes 12e, and corresponds to an evaporation pipe distribution unit. That is, the high-temperature liquid chamber 14es serves as a preheating tube recovery unit and an evaporation tube distribution unit. The mixed fluid chamber 14ec is a water chamber that collects the heated water W from the plurality of evaporation tubes 12e, and corresponds to an evaporation tube collection unit. A heated water outlet pipe 84 is connected to the upper part (typically the top part) of the mixed fluid chamber 14ec.

缶胴１１内に収容されている高濃度溶液散布ノズル１３Ａは、高温伝熱管１２Ａに満遍なく高濃度溶液Ｓａを散布することができるように、鉛直上方から見て高温伝熱管１２Ａを覆う広範囲に広がって配置されている。高濃度溶液散布ノズル１３Ａに接続される高濃度溶液管３５は、缶胴１１の一面を貫通している。なお、上述のように、複数の高温伝熱管１２Ａは缶胴１１内に水平に配置されているが、水平に配置されているとは、厳密に水平であることを要求するものではなく、高温吸収器１０Ａ内を１つの流れとして蛇行して流れる被加熱水Ｗが蒸発管１２ｅ内で液から蒸気に変化しても被加熱水Ｗの流動を阻害しない程度に水平であればよい。しかしながら、高濃度溶液散布ノズル１３Ａから散布された高濃度溶液Ｓａが高温伝熱管１２Ａの外表面に接している量を増加させる観点から、水平に近づくほど好ましい。缶胴１１の底部に貯留されている中間濃度溶液Ｓｂを低温吸収器１０Ｂ（図１参照）に導く中間濃度溶液管１５Ａは、典型的には缶胴１１の底部に接続されている。   The high-concentration solution spray nozzle 13A accommodated in the can body 11 spreads over a wide range so as to cover the high-temperature heat transfer tube 12A as viewed from above vertically so that the high-concentration solution Sa can be uniformly sprayed on the high-temperature heat transfer tube 12A. Are arranged. The high concentration solution pipe 35 connected to the high concentration solution spray nozzle 13 </ b> A passes through one surface of the can body 11. As described above, the plurality of high-temperature heat transfer tubes 12A are arranged horizontally in the can body 11, but the horizontal arrangement does not require strictly horizontal, Even if the heated water W meandering as a single flow in the absorber 10A changes from a liquid to a vapor in the evaporation pipe 12e, it should be horizontal to the extent that the flow of the heated water W is not hindered. However, from the viewpoint of increasing the amount of the high-concentration solution Sa sprayed from the high-concentration solution spray nozzle 13A in contact with the outer surface of the high-temperature heat transfer tube 12A, the closer to the horizontal the better. An intermediate concentration solution tube 15 </ b> A that guides the intermediate concentration solution Sb stored at the bottom of the can body 11 to the low temperature absorber 10 </ b> B (see FIG. 1) is typically connected to the bottom of the can body 11.

高温気液分離器８０内の被加熱水液Ｗｑを高温吸収器１０Ａに導く被加熱水導入管８２は、被加熱水Ｗの流れの最上流の液室となる低温液室１４ｐｓに接続されている。補給水管８５は、被加熱水導入管８２に接続されている。この構成により、被加熱水Ｗを高温吸収器１０Ａに流入させる管の接続部が１箇所で済むこととなり、構成を簡便にすることができると共に、水室を開放する際の保守点検作業が容易になる。高温吸収器１０Ａで生成された湿り蒸気（混合被加熱水Ｗｍ）を高温気液分離器８０に導く被加熱水流出管８４は、混合流体室１４ｅｃに接続されている。   The heated water introduction pipe 82 that guides the heated water liquid Wq in the high temperature gas-liquid separator 80 to the high temperature absorber 10A is connected to the low temperature liquid chamber 14ps that is the most upstream liquid chamber in the flow of the heated water W. Yes. The makeup water pipe 85 is connected to the heated water introduction pipe 82. With this configuration, only one connecting portion of the pipe that allows the heated water W to flow into the high-temperature absorber 10A is required, so that the configuration can be simplified and the maintenance inspection work when opening the water chamber is easy. become. A heated water outflow pipe 84 that guides the wet steam (mixed heated water Wm) generated by the high temperature absorber 10A to the high temperature gas-liquid separator 80 is connected to the mixed fluid chamber 14ec.

上述のように構成された高温吸収器１０Ａは、典型的には以下のように作用する。高濃度溶液Ｓａは、高濃度溶液散布ノズル１３Ａから散布されると、重力によって落下し、まず蒸発管１２ｅに降りかかり、蒸発管１２ｅに接触しなかった分及び蒸発管１２ｅの表面を伝わって滴下してきた分が予熱管１２ｐに降りかかって、各蒸発管１２ｅ及び各予熱管１２ｐの表面に濡れ広がる。各蒸発管１２ｅ及び各予熱管１２ｐの表面に濡れ広がった高濃度溶液Ｓａは、低温気液分離器６０（図１参照）から供給された低温冷媒蒸気Ｖｂを吸収し、その際に発生する吸収熱で内部を流れる被加熱水Ｗを加熱する。低温冷媒蒸気Ｖｂを吸収した高濃度溶液Ｓａは、濃度が低下した中間濃度溶液Ｓｂとなって缶胴１１の下部に一旦貯留された後、中間濃度溶液管１５Ａを介して低温吸収器１０Ｂ（図１参照）に導かれる。   The high-temperature absorber 10A configured as described above typically operates as follows. When the high-concentration solution Sa is sprayed from the high-concentration solution spraying nozzle 13A, it falls by gravity, first descends on the evaporation pipe 12e, and drops by the amount not contacting the evaporation pipe 12e and the surface of the evaporation pipe 12e. The portion of the water reaches the preheating pipe 12p and spreads on the surfaces of the respective evaporation pipes 12e and the respective preheating pipes 12p. The high-concentration solution Sa wetted and spread on the surfaces of the respective evaporation tubes 12e and the respective preheating tubes 12p absorbs the low-temperature refrigerant vapor Vb supplied from the low-temperature gas-liquid separator 60 (see FIG. 1), and the absorption generated at that time. Heated water W flowing inside is heated by heat. The high-concentration solution Sa that has absorbed the low-temperature refrigerant vapor Vb becomes an intermediate-concentration solution Sb having a reduced concentration, and is temporarily stored in the lower portion of the can body 11, and then the low-temperature absorber 10B (see FIG. 1).

その一方で、高温吸収器１０Ａ内の低温液室１４ｐｓには、被加熱水導入管８２を介して高温気液分離器８０からの被加熱水液Ｗｑが流入する。低温液室１４ｐｓに流入する被加熱水液Ｗｑには、低温液室１４ｐｓに流入する前に、補給水ポンプ８６（図１参照）により補給水Ｗｓが混合される。なお、補給水管８５及び高温気液分離器８０から高温液室１４ｅｓに流入する被加熱水液Ｗｑの合計流量は、典型的には、高温吸収器１０Ａで生成される被加熱水蒸気Ｗｖの流量の２〜１０倍程度である。低温液室１４ｐｓに流入した被加熱水液Ｗｑは、予熱管１２ｐを流れて高温液室１４ｅｓに流入する。被加熱水液Ｗｑは、予熱管１２ｐ内を流れるとき、予熱管１２ｐの外表面に濡れ広がった高濃度溶液Ｓａが低温冷媒蒸気Ｖｂを吸収する際に発生する吸収熱で加熱される。このとき、予熱管１２ｐを流れる被加熱水液Ｗｑは、温度が上昇するが、蒸発はしない。   On the other hand, the heated liquid Wq from the high temperature gas-liquid separator 80 flows into the low temperature liquid chamber 14ps in the high temperature absorber 10A via the heated water introduction pipe 82. The heated water liquid Wq flowing into the low temperature liquid chamber 14ps is mixed with makeup water Ws by the makeup water pump 86 (see FIG. 1) before flowing into the low temperature liquid chamber 14ps. Note that the total flow rate of the heated water liquid Wq flowing into the high temperature liquid chamber 14es from the makeup water pipe 85 and the high temperature gas-liquid separator 80 is typically the flow rate of the heated water vapor Wv generated in the high temperature absorber 10A. It is about 2 to 10 times. The heated liquid Wq flowing into the low temperature liquid chamber 14ps flows through the preheating pipe 12p and flows into the high temperature liquid chamber 14es. When the heated liquid Wq flows through the preheating pipe 12p, it is heated by the absorbed heat generated when the high-concentration solution Sa wet and spreads on the outer surface of the preheating pipe 12p absorbs the low-temperature refrigerant vapor Vb. At this time, the heated liquid Wq flowing through the preheating pipe 12p rises in temperature but does not evaporate.

高温液室１４ｅｓ内の被加熱水液Ｗｑは、各蒸発管１２ｅに流入する。このとき、高温液室１４ｅｓには、実質的に被加熱水蒸気Ｗｖが存在しないので、すべての蒸発管１２ｅに被加熱水液Ｗｑが流入する。各蒸発管１２ｅを流れる被加熱水液Ｗｑは、蒸発管１２ｅの外表面に濡れ広がった高濃度溶液Ｓａが低温冷媒蒸気Ｖｂを吸収する際に発生する吸収熱で加熱され、混合流体室１４ｅｃに至るまでに一部又は全部が蒸発する。このとき、すべての蒸発管１２ｅに被加熱水液Ｗｑが流入することで、吸収熱が効率よく被加熱水液Ｗｑに伝わり、効率的に被加熱水蒸気Ｗｖを生成することができる。また、被加熱媒水液Ｗｑを蒸発管１２ｅに供給する前に予熱管１２ｐで予熱していたので、蒸発管１２ｅにおける被加熱水蒸気Ｗｖの生成を効率的に行うことができる。蒸発管１２ｅを流れる際に加熱された被加熱水Ｗは、混合被加熱水Ｗｍとなって混合流体室１４ｅｃに到達する。混合流体室１４ｅｃ内の混合被加熱水Ｗｍは、被加熱水流出管８４を流れて高温吸収器１０Ａから流出する。このように、１パスで構成された蒸発管１２ｅで生成された混合被加熱水Ｗｍは、その後は蒸発管を通過せずに高温吸収器１０Ａから流出する。蒸発管１２ｅ内で発生した被加熱水蒸気Ｗｖは、水平な伝熱管を流れた後に混合流体室１４ｅｃの上方から流出するだけのシンプルな流れになるので、高温吸収器１０Ａ内に滞留せずに流出しやすい。つまり、被加熱水蒸気Ｗｖが高温吸収器１０Ａ内に滞留せずに流れやすいので、発生した被加熱水蒸気Ｗｖが被加熱水液Ｗｑを高温吸収器１０Ａの出口に向けて吹き飛ばすことがない。また、発生した被加熱水蒸気Ｗｖが高温吸収器１０Ａ内に滞留しないので、吸収ヒートポンプ１の起動時の液位の過度な上昇を抑制することができ、気液分離作用を損なうことがない。このように、本実施の形態では、吸収ヒートポンプ１の起動中の被加熱水Ｗの吹き飛ばしと過度な液位上昇を抑制して、良好な気液分離を実現することができる。   The heated water liquid Wq in the high temperature liquid chamber 14es flows into each evaporation pipe 12e. At this time, since the heated water vapor Wv does not substantially exist in the high temperature liquid chamber 14es, the heated water liquid Wq flows into all the evaporation pipes 12e. The heated liquid Wq flowing through each evaporation pipe 12e is heated by the absorption heat generated when the high-concentration solution Sa that has spread on the outer surface of the evaporation pipe 12e absorbs the low-temperature refrigerant vapor Vb, and enters the mixed fluid chamber 14ec. Some or all of it evaporates. At this time, the heated water liquid Wq flows into all the evaporation pipes 12e, so that the absorbed heat is efficiently transmitted to the heated water liquid Wq, and the heated water vapor Wv can be efficiently generated. Further, since the heated medium water solution Wq is preheated by the preheating pipe 12p before being supplied to the evaporation pipe 12e, the heated water vapor Wv in the evaporation pipe 12e can be efficiently generated. The heated water W heated when flowing through the evaporation pipe 12e becomes the mixed heated water Wm and reaches the mixed fluid chamber 14ec. The mixed heated water Wm in the mixed fluid chamber 14ec flows through the heated water outflow pipe 84 and flows out from the high temperature absorber 10A. As described above, the mixed heated water Wm generated by the evaporation pipe 12e configured in one pass flows out from the high temperature absorber 10A without passing through the evaporation pipe. The heated steam Wv generated in the evaporation pipe 12e becomes a simple flow that flows out from the upper side of the mixed fluid chamber 14ec after flowing through the horizontal heat transfer pipe, and therefore flows out without staying in the high temperature absorber 10A. It's easy to do. That is, since the heated water vapor Wv easily flows without staying in the high temperature absorber 10A, the generated heated water vapor Wv does not blow the heated water liquid Wq toward the outlet of the high temperature absorber 10A. Moreover, since the generated steam Wv to be heated does not stay in the high-temperature absorber 10A, an excessive increase in the liquid level at the time of starting the absorption heat pump 1 can be suppressed, and the gas-liquid separation action is not impaired. As described above, in the present embodiment, it is possible to suppress the blowing off of the heated water W during the activation of the absorption heat pump 1 and the excessive increase in the liquid level, thereby realizing a good gas-liquid separation.

高温吸収器１０Ａから流出した混合被加熱水Ｗｍは、被加熱水流出管８４を介して高温気液分離器８０に流入する。高温気液分離器８０に流入した混合被加熱水Ｗｍは、バッフル板８０ａに衝突して気液分離され、被加熱水液Ｗｑと、被加熱水蒸気Ｗｖとに分かれる。分離された被加熱水蒸気Ｗｖは、吸収ヒートポンプ１外の蒸気利用場所に向かって被加熱水蒸気管８９を流れる。他方、高温気液分離器８０で分離された被加熱水液Ｗｑは、高温気液分離器８０下部の貯留部８１に貯留される。分離液体貯留部８１に貯留されている被加熱水液Ｗｑは、被加熱水導入管８２を流れる。被加熱水導入管８２を流れる被加熱水液Ｗｑは、補給水管８５からの補給水Ｗｓと合流して低温液室１４ｐｓに流入し、以降、上述の作用を繰り返す。   The mixed heated water Wm flowing out from the high-temperature absorber 10A flows into the high-temperature gas-liquid separator 80 via the heated water outflow pipe 84. The mixed heated water Wm that has flowed into the high-temperature gas-liquid separator 80 collides with the baffle plate 80a and undergoes gas-liquid separation, and is divided into heated water liquid Wq and heated steam Wv. The separated heated steam Wv flows through the heated steam pipe 89 toward the steam utilization place outside the absorption heat pump 1. On the other hand, the heated water liquid Wq separated by the high-temperature gas-liquid separator 80 is stored in the storage unit 81 below the high-temperature gas-liquid separator 80. The heated water liquid Wq stored in the separation liquid storage unit 81 flows through the heated water introduction pipe 82. The heated water liquid Wq flowing through the heated water introduction pipe 82 merges with the makeup water Ws from the makeup water pipe 85 and flows into the cryogenic liquid chamber 14ps, and thereafter repeats the above-described operation.

なお、図３に示す高温吸収器１０Ａでは、高温伝熱管１２Ａが予熱管１２ｐと蒸発管１２ｅとに区別されていることとしたが、予熱管１２ｐを省略してもよい。予熱管１２ｐを省略する場合、低温液室１４ｐｓも省略すると共に、被加熱水導入管８２を高温液室１４ｅｓに接続し、高温伝熱管１２Ａ全体が１パスの蒸発管１２ｅで構成されることとなる。   In the high temperature absorber 10A shown in FIG. 3, the high temperature heat transfer tube 12A is distinguished from the preheating tube 12p and the evaporation tube 12e, but the preheating tube 12p may be omitted. When the preheating pipe 12p is omitted, the low temperature liquid chamber 14ps is also omitted, the heated water introduction pipe 82 is connected to the high temperature liquid chamber 14es, and the entire high temperature heat transfer pipe 12A is constituted by a one-pass evaporation pipe 12e. Become.

以上の高温吸収器１０Ａの具体的な構成は、低温吸収器１０Ｂにも適用可能である。図３に示す構成を低温吸収器１０Ｂに適用する場合は、図３中の高濃度溶液散布ノズル１３Ａを中間濃度溶液散布ノズル１３Ｂに、低温冷媒蒸気Ｖｂが流れる低温冷媒蒸気管６９を蒸発器冷媒蒸気Ｖｅが流れる流路に、中間濃度溶液Ｓｂが流れる中間濃度溶液管１５Ａを希溶液Ｓｗが流れる希溶液管１５Ｂに、高温気液分離器８０まわりの構成を低温気液分離器６０まわりの構成に、予熱管１２ｐ（省略可）及び蒸発管１２ｅ内を流れる流体の被加熱水Ｗを冷媒Ｖに、それぞれ置き換えればよい。   The specific configuration of the high temperature absorber 10A described above can also be applied to the low temperature absorber 10B. When the configuration shown in FIG. 3 is applied to the low-temperature absorber 10B, the high-concentration solution spray nozzle 13A in FIG. 3 is used as the intermediate-concentration solution spray nozzle 13B, and the low-temperature refrigerant vapor pipe 69 through which the low-temperature refrigerant vapor Vb flows is the evaporator refrigerant. The configuration around the high-temperature gas-liquid separator 80 is changed from the intermediate concentration solution tube 15A through which the intermediate-concentration solution Sb flows into the flow path through which the vapor Ve flows to the dilute solution tube 15B through which the dilute solution Sw flows. In addition, the heated water W of the fluid flowing in the preheating pipe 12p (which may be omitted) and the evaporation pipe 12e may be replaced with the refrigerant V, respectively.

以上の説明では、高温吸収器１０Ａの高温伝熱管１２Ａに供給する被加熱水Ｗの流量を調節する（被加熱水Ｗの供給開始を調節することを含む）基となる流体特性関連値取得手段が、高温吸収器１０Ａの出口における中間濃度溶液Ｓｂの温度を検知する高温吸収器出口温度計５１Ａであるとしたが、このほか、高温吸収器１０Ａの出口における中間濃度溶液Ｓｂの濃度、高温吸収器１０Ａの入口における高濃度溶液Ｓａの温度又は濃度、再生器３０の出口における高濃度溶液Ｓａの温度又は濃度、再生器３０の入口における希溶液Ｓｗの温度又は濃度を検知するものであってもよく、あるいはこれらのいずれかと相関を有する値を検知して制御に用いられる値を算出することとしてもよい。相関を有する値としては、凝縮器４０の冷媒液貯留部４２における冷媒液Ｖｆの温度、冷媒液管４５内の冷媒液Ｖｆの温度、凝縮器４０内部又は再生器３０内部の圧力、低温伝熱管１２Ｂの出口における冷媒Ｖの温度、低温気液分離器６０の内部の冷媒Ｖの温度、低温冷媒蒸気管６９を流れる低温冷媒蒸気Ｖｂの温度、低温圧力計６１が検知する低温気液分離器６０の内部の圧力又はこれと連通する高温吸収器１０Ａ内部の圧力、などがある。特に、再生器３０の出口における高濃度溶液Ｓａの濃度又は高温吸収器１０Ａの入口における高濃度溶液Ｓａの濃度を検知することとすると、吸収ヒートポンプの起動からの濃度変化が最も大きく最も濃くなるので好ましい。吸収液の濃度を検知する場合、吸収液の温度とその吸収液が収容されている吸収器又は再生器の内圧とから、吸収液の濃度を算出することとしてもよい。また、高温伝熱管１２Ａ内に被加熱水Ｗの供給を開始した後に行う被加熱水Ｗの流量制御は、上記の各値を用いるほか、高温伝熱管１２Ａ内の圧力又は高温伝熱管１２Ａの出口における被加熱水Ｗの温度もしくは高温気液分離器８０における被加熱水Ｗの温度を検知するものであってもよく、あるいはこれらのいずれかと相関を有する値を検知して制御に用いられる値を算出することとしてもよい。相関を有する値としては、高温気液分離器８０から流出する被加熱水蒸気Ｗｖの温度、高温気液分離器８０又は被加熱水蒸気管８９又は被加熱水導入管８２又は被加熱水流出管８４のいずれかの表面温度、などがある。高温伝熱管１２Ａ内の圧力を検知することには、高温伝熱管１２Ａと連通する高温気液分離器８０の圧力を検知することも含まれる。また、高温伝熱管１２Ａの出口における被加熱水Ｗの温度は飽和温度であるから、高温気液分離器８０の圧力から高温伝熱管１２Ａの出口における被加熱水Ｗの温度を算出することとしてもよい。また、低温吸収器１０Ｂの低温伝熱管１２Ｂに供給する冷媒液Ｖｆの流量を調節する（冷媒液Ｖｆの供給開始を調節することを含む）基となる流体特性関連値取得手段が、低温吸収器１０Ｂの出口における希溶液Ｓｗの温度を検知する低温吸収器出口温度計５１Ｂであるとしたが、このほか、高温吸収器出口温度計５１Ａの場合に倣って、低温吸収器１０Ｂの出口における希溶液Ｓｗの濃度、低温吸収器１０Ｂの入口における中間濃度溶液Ｓｂの温度又は濃度、再生器３０の出口における高濃度溶液Ｓａの温度又は濃度、再生器３０の入口における希溶液Ｓｗの温度又は濃度を検知するものであってもよく、あるいはこれらのいずれかと相関を有する値を検知して制御に用いられる値を算出することとしてもよい。相関を有する値としては、凝縮器４０の冷媒液貯留部４２における冷媒液Ｖｆの温度、冷媒液管４５内の冷媒液Ｖｆの温度、凝縮器４０内部又は再生器３０内部の圧力、蒸発器２０内部の冷媒Ｖの温度、蒸発器２０内で発生する蒸発器冷媒蒸気Ｖｅの温度、蒸発器２０内部の圧力又はこれと連通する低温吸収器１０Ｂ内部の圧力、などがある。上述したように、再生器３０の出口における高濃度溶液Ｓａの濃度は、吸収ヒートポンプの起動からの濃度変化が最も大きく最も濃くなるので、これを検知することとすると好ましい。また、低温伝熱管１２Ｂ内に冷媒液Ｖｆの供給を開始した後に行う冷媒液Ｖｆの流量制御は、上記の各値を用いるほか、低温伝熱管１２Ｂ内の圧力（低温気液分離器６０の圧力を含む）又は低温伝熱管１２Ｂの出口における冷媒Ｖの温度又は低温気液分離器６０における冷媒Ｖの温度を検知するものであってもよく、あるいはこれらのいずれかと相関を有する値を検知して制御に用いられる値を算出することとしてもよい。相関を有する値としては、低温気液分離器６０から流出する低温冷媒蒸気Ｖｂの温度、低温気液分離器６０又は冷媒液導入管６２又は冷媒流出管６４又は低温冷媒蒸気管６９のいずれかの表面温度、などがある。   In the above description, the fluid characteristic related value acquisition means that is the basis for adjusting the flow rate of the heated water W supplied to the high temperature heat transfer tube 12A of the high temperature absorber 10A (including adjusting the supply start of the heated water W). Is the high temperature absorber outlet thermometer 51A for detecting the temperature of the intermediate concentration solution Sb at the outlet of the high temperature absorber 10A. In addition, the concentration of the intermediate concentration solution Sb at the outlet of the high temperature absorber 10A and the high temperature absorption The temperature or concentration of the high concentration solution Sa at the inlet of the regenerator 10A, the temperature or concentration of the high concentration solution Sa at the outlet of the regenerator 30, and the temperature or concentration of the dilute solution Sw at the inlet of the regenerator 30 may be detected. Alternatively, a value used for control may be calculated by detecting a value having a correlation with any of these. The correlated values include the temperature of the refrigerant liquid Vf in the refrigerant liquid storage section 42 of the condenser 40, the temperature of the refrigerant liquid Vf in the refrigerant liquid pipe 45, the pressure inside the condenser 40 or the regenerator 30, and the low-temperature heat transfer pipe. The temperature of the refrigerant V at the outlet of 12B, the temperature of the refrigerant V inside the low-temperature gas-liquid separator 60, the temperature of the low-temperature refrigerant vapor Vb flowing through the low-temperature refrigerant vapor pipe 69, and the low-temperature gas-liquid separator 60 detected by the low-temperature pressure gauge 61. Or the pressure inside the high-temperature absorber 10A communicating therewith. In particular, if the concentration of the high-concentration solution Sa at the outlet of the regenerator 30 or the concentration of the high-concentration solution Sa at the inlet of the high-temperature absorber 10A is detected, the concentration change from the start of the absorption heat pump is the largest and darkest. preferable. When detecting the concentration of the absorbing solution, the concentration of the absorbing solution may be calculated from the temperature of the absorbing solution and the internal pressure of the absorber or the regenerator in which the absorbing solution is stored. The flow rate control of the heated water W performed after the supply of the heated water W into the high temperature heat transfer tube 12A uses the above values, the pressure in the high temperature heat transfer tube 12A, or the outlet of the high temperature heat transfer tube 12A. The temperature of the water W to be heated or the temperature of the water W to be heated in the high-temperature gas-liquid separator 80 may be detected, or a value correlated with any of these may be detected and used for control. It may be calculated. The correlated values include the temperature of the heated steam Wv flowing out from the high-temperature gas-liquid separator 80, the high-temperature gas-liquid separator 80, the heated steam pipe 89, the heated water introduction pipe 82, or the heated water outflow pipe 84. Any surface temperature, etc. Detecting the pressure in the high-temperature heat transfer tube 12A includes detecting the pressure of the high-temperature gas-liquid separator 80 communicating with the high-temperature heat transfer tube 12A. Further, since the temperature of the heated water W at the outlet of the high temperature heat transfer tube 12A is the saturation temperature, the temperature of the heated water W at the outlet of the high temperature heat transfer tube 12A may be calculated from the pressure of the high temperature gas-liquid separator 80. Good. Further, the fluid characteristic related value acquisition means that is a base for adjusting the flow rate of the refrigerant liquid Vf supplied to the low-temperature heat transfer tube 12B of the low-temperature absorber 10B (including adjusting the supply start of the refrigerant liquid Vf) is a low-temperature absorber. The low temperature absorber outlet thermometer 51B detects the temperature of the dilute solution Sw at the outlet of 10B, but in addition to the case of the high temperature absorber outlet thermometer 51A, the dilute solution at the outlet of the low temperature absorber 10B is used. The concentration of Sw, the temperature or concentration of the intermediate concentration solution Sb at the inlet of the low temperature absorber 10B, the temperature or concentration of the high concentration solution Sa at the outlet of the regenerator 30, and the temperature or concentration of the dilute solution Sw at the inlet of the regenerator 30 are detected. It is also possible to calculate a value used for control by detecting a value having a correlation with any of these. The correlated values include the temperature of the refrigerant liquid Vf in the refrigerant liquid storage section 42 of the condenser 40, the temperature of the refrigerant liquid Vf in the refrigerant liquid pipe 45, the pressure inside the condenser 40 or the regenerator 30, and the evaporator 20 There are the temperature of the internal refrigerant V, the temperature of the evaporator refrigerant vapor Ve generated in the evaporator 20, the pressure inside the evaporator 20, or the pressure inside the low-temperature absorber 10B communicating with this. As described above, the concentration of the high-concentration solution Sa at the outlet of the regenerator 30 is preferably detected since the concentration change from the start of the absorption heat pump is the largest and the highest. The flow rate control of the refrigerant liquid Vf performed after the supply of the refrigerant liquid Vf into the low-temperature heat transfer tube 12B is performed using the above values, as well as the pressure in the low-temperature heat transfer pipe 12B (the pressure of the low-temperature gas-liquid separator 60). Or the temperature of the refrigerant V at the outlet of the low-temperature heat transfer tube 12B or the temperature of the refrigerant V in the low-temperature gas-liquid separator 60, or a value correlated with either of these may be detected. It is good also as calculating the value used for control. As a value having a correlation, the temperature of the low-temperature refrigerant vapor Vb flowing out from the low-temperature gas-liquid separator 60, any one of the low-temperature gas-liquid separator 60, the refrigerant liquid introduction pipe 62, the refrigerant outflow pipe 64, or the low-temperature refrigerant vapor pipe 69 is used. Surface temperature, etc.

以上の説明では、冷媒液供給ポンプ４９のインバータ制御によって低温伝熱管１２Ｂ内に供給される冷媒液Ｖｆの流量が可変に構成されていることとしたが、冷媒液供給ポンプ４９を複数台並列に設置して運転する台数を変えることで低温伝熱管１２Ｂ内に供給される冷媒液Ｖｆの流量を変化させることとしてもよい。また、補給水ポンプ８６のインバータ制御によって高温伝熱管１２Ａ内に供給される被加熱水Ｗの流量が可変に構成されていることとしたが、補給水ポンプ８６を複数台並列に設置して運転する台数を変えることで高温伝熱管１２Ａ内に供給される被加熱水Ｗの流量を変化させることとしてもよい。また、低温伝熱管１２Ｂ及び／又は高温伝熱管１２Ａに供給する流体の流量を変化させるに際し、ポンプのインバータ制御あるいは台数制御に代えて、開度が調節可能な流量調整弁を設け、流量調整弁の開度を変化させることにより、流量を変化させることとしてもよい。あるいは、ポンプをＯＮ／ＯＦＦ制御として、ＯＮ時間及びＯＦＦ時間の長さを各々制御してもよい。すなわち、ＯＮ時間を短くしＯＦＦ時間を長くして流量を少なくし、ＯＮ時間を長くしＯＦＦ時間を短くして流量を多くしてもよい。   In the above description, the flow rate of the refrigerant liquid Vf supplied into the low-temperature heat transfer tube 12B by the inverter control of the refrigerant liquid supply pump 49 is configured to be variable. However, a plurality of refrigerant liquid supply pumps 49 are arranged in parallel. It is good also as changing the flow volume of the refrigerant | coolant liquid Vf supplied in the low temperature heat exchanger tube 12B by changing the number to install and operate. In addition, the flow rate of the heated water W supplied into the high-temperature heat transfer pipe 12A by the inverter control of the makeup water pump 86 is configured to be variable. However, a plurality of makeup water pumps 86 are installed in parallel and operated. It is good also as changing the flow volume of the to-be-heated water W supplied in 12 A of high temperature heat exchanger tubes by changing the number to perform. Further, when changing the flow rate of the fluid supplied to the low temperature heat transfer tube 12B and / or the high temperature heat transfer tube 12A, a flow rate adjusting valve capable of adjusting the opening degree is provided instead of the inverter control or the number control of the pump. The flow rate may be changed by changing the degree of opening. Alternatively, the length of the ON time and the OFF time may be controlled by using the pump as ON / OFF control. That is, the ON time can be shortened and the OFF time can be lengthened to reduce the flow rate, and the ON time can be lengthened and the OFF time can be shortened to increase the flow rate.

以上の説明では、高温吸収器１０Ａで加熱される被加熱水Ｗが水であるとしたが、化学液体等の、蒸気として利用する要請のある流体であってもよい。   In the above description, the heated water W heated by the high-temperature absorber 10A is water, but it may be a fluid that is requested to be used as a vapor, such as a chemical liquid.

以上の説明では、冷媒液管４８が低温気液分離器６０に接続されていることとしたが、冷媒液導入管６２に接続されていてもよく、低温伝熱管１２Ｂに接続されていてもよい。   In the above description, the refrigerant liquid pipe 48 is connected to the low-temperature gas-liquid separator 60. However, the refrigerant liquid pipe 48 may be connected to the refrigerant liquid introduction pipe 62 or may be connected to the low-temperature heat transfer pipe 12B. .

以上の説明では、吸収ヒートポンプ１の起動時に、低温伝熱管１２Ｂに供給される冷媒液Ｖｆの流量と、高温伝熱管１２Ａに供給される被加熱水液Ｗｑの流量とが、共に流体特性関連値取得手段（低温吸収器出口温度計５１Ｂ、高温吸収器出口温度計５１Ａ）で取得された値に応じて調節されることとしたが、どちらか一方が調節されることとしてもよい。また、吸収器が高温吸収器１０Ａと低温吸収器１０Ｂとの２段に構成されているとしたが、例えば低温吸収器１０Ｂを省略して１段に構成されていてもよく、高温吸収器１０Ａと低温吸収器１０Ｂとの間に中温吸収器を設けて３段に構成されていてもよい。   In the above description, when the absorption heat pump 1 is started, the flow rate of the refrigerant liquid Vf supplied to the low temperature heat transfer tube 12B and the flow rate of the heated water liquid Wq supplied to the high temperature heat transfer tube 12A are both related to fluid characteristics. Although the adjustment is made according to the value acquired by the acquisition means (low temperature absorber outlet thermometer 51B, high temperature absorber outlet thermometer 51A), either one of them may be adjusted. Further, although the absorber is configured in two stages of the high temperature absorber 10A and the low temperature absorber 10B, for example, the low temperature absorber 10B may be omitted and may be configured in one stage. And a low temperature absorber 10B, an intermediate temperature absorber may be provided and configured in three stages.

１ 吸収ヒートポンプ
１０Ａ 高温吸収器
１０Ｂ 低温吸収器
１２Ａ 高温伝熱管
１２Ｂ 低温伝熱管
１３Ａ 高濃度溶液散布ノズル
１３Ｂ 中間濃度溶液散布ノズル
１６Ａ 中間濃度溶液ポンプ
１９Ａ 冷媒蒸気導入口
１９Ｂ 冷媒蒸気導入口
３０ 再生器
４２ 冷媒液貯留部
４３ 液位検知器
４９ 冷媒液供給ポンプ
５１Ａ 高温吸収器出口温度計
５１Ｂ 低温吸収器出口温度計
６０ 低温気液分離器
６２ 冷媒液導入管
８０ 高温気液分離器
８６ 補給水ポンプ
９０ 制御装置
Ｓａ 高濃度溶液
Ｓｂ 中間濃度溶液
Ｓｗ 希溶液
Ｖｂ 低温冷媒蒸気
Ｖｅ 蒸発器冷媒蒸気
Ｖｆ 冷媒液
Ｖｇ 再生器冷媒蒸気
Ｖｍ 混合流体
Ｗｍ 混合被加熱水
Ｗｑ 被加熱水液
DESCRIPTION OF SYMBOLS 1 Absorption heat pump 10A High temperature absorber 10B Low temperature absorber 12A High temperature heat transfer tube 12B Low temperature heat transfer tube 13A High concentration solution spray nozzle 13B Intermediate concentration solution spray nozzle 16A Intermediate concentration solution pump 19A Refrigerant vapor inlet 19B Refrigerant vapor inlet 30 Regenerator 42 Refrigerant liquid storage unit 43 Liquid level detector 49 Refrigerant liquid supply pump 51A High temperature absorber outlet thermometer 51B Low temperature absorber outlet thermometer 60 Low temperature gas / liquid separator 62 Refrigerant liquid introduction pipe 80 High temperature gas / liquid separator 86 Makeup water pump 90 Control device Sa High concentration solution Sb Intermediate concentration solution Sw Dilute solution Vb Low temperature refrigerant vapor Ve Evaporator refrigerant vapor Vf Refrigerant liquid Vg Regenerator refrigerant vapor Vm Mixed fluid Wm Mixed heated water Wq Heated water liquid

Claims (5)

吸収液が吸収対象冷媒の蒸気を吸収する際に発生する吸収熱で被加熱媒体を加熱する吸収ヒートポンプであって；
内部に前記被加熱媒体を流す伝熱管と、前記伝熱管の外表面に向けて前記吸収液を供給する吸収液供給器と、前記吸収液に吸収させる前記吸収対象冷媒の蒸気を導入する吸収対象冷媒蒸気導入部と、を有する吸収器と；
前記吸収器で前記吸収対象冷媒の蒸気を吸収して濃度が低下した前記吸収液を直接又は間接的に導入し、導入した前記吸収液から前記吸収対象冷媒を離脱させて前記吸収液の濃度を上昇させ、濃度が上昇した前記吸収液を直接又は間接的に前記吸収器に向けて流出させる再生器と；
前記被加熱媒体を前記伝熱管に向けて供給する被加熱媒体供給手段と；
前記再生器の出口における前記吸収液の温度、前記再生器の出口における前記吸収液の濃度、前記吸収器の入口における前記吸収液の温度、前記吸収器の入口における前記吸収液の濃度、前記吸収器の出口における前記吸収液の温度、前記吸収器の出口における前記吸収液の濃度、前記再生器の入口における前記吸収液の温度、前記再生器の入口における前記吸収液の濃度、前記伝熱管内の圧力、及び前記伝熱管の出口における前記被加熱媒体の温度、の少なくとも１つの値又はこれと相関を有する値を取得する流体特性関連値取得手段と；
前記吸収ヒートポンプの起動時に、前記流体特性関連値取得手段で取得された値に応じて前記伝熱管に供給する前記被加熱媒体の流量を調節するように前記被加熱媒体供給手段を制御する制御装置とを備え；
前記流体特性関連値取得手段は、前記再生器の出口における前記吸収液の温度、前記再生器の出口における前記吸収液の濃度、前記吸収器の入口における前記吸収液の温度、前記吸収器の入口における前記吸収液の濃度、前記吸収器の出口における前記吸収液の温度、及び前記吸収器の出口における前記吸収液の濃度、前記再生器の入口における前記吸収液の温度、前記再生器の入口における前記吸収液の濃度、の少なくとも１つの値又はこれと相関を有する値である吸収液特性関連値を取得するように構成され；
前記制御装置は、前記吸収ヒートポンプを起動する際、前記流体特性関連値取得手段で取得された前記吸収液特性関連値が、前記被加熱媒体の少なくとも一部は蒸発する温度と相関を有する所定の値に到達したときに、前記被加熱媒体の前記伝熱管への供給を開始するように、前記被加熱媒体供給手段を制御する；
吸収ヒートポンプ。 An absorption heat pump that heats the medium to be heated with absorption heat generated when the absorbing liquid absorbs the vapor of the refrigerant to be absorbed;
A heat transfer tube through which the heated medium flows, an absorption liquid supplier for supplying the absorption liquid toward the outer surface of the heat transfer tube, and an absorption target for introducing vapor of the absorption target refrigerant to be absorbed by the absorption liquid An absorber having a refrigerant vapor inlet;
The absorber absorbs the vapor of the refrigerant to be absorbed by the absorber and directly or indirectly introduces the absorption liquid, and the absorption refrigerant is desorbed from the introduced absorption liquid to reduce the concentration of the absorption liquid. A regenerator that raises and increases the concentration of the absorbent directly or indirectly toward the absorber;
Heated medium supply means for supplying the heated medium toward the heat transfer tube;
Temperature of the absorbent at the outlet of the regenerator, concentration of the absorbent at the outlet of the regenerator, temperature of the absorbent at the inlet of the absorber, concentration of the absorbent at the inlet of the absorber, absorption Temperature of the absorbing liquid at the outlet of the regenerator, concentration of the absorbing liquid at the outlet of the absorber, temperature of the absorbing liquid at the inlet of the regenerator, concentration of the absorbing liquid at the inlet of the regenerator, in the heat transfer tube Fluid characteristic related value acquisition means for acquiring at least one value of the pressure of the heat transfer tube and the temperature of the heated medium at the outlet of the heat transfer tube, or a value correlated therewith;
A control device that controls the heated medium supply means so as to adjust the flow rate of the heated medium supplied to the heat transfer tube according to the value acquired by the fluid characteristic related value acquisition means when the absorption heat pump is started. for example Bei the door;
The fluid characteristic related value acquisition means includes: the temperature of the absorbing liquid at the outlet of the regenerator; the concentration of the absorbing liquid at the outlet of the regenerator; the temperature of the absorbing liquid at the inlet of the absorber; the inlet of the absorber. The concentration of the absorbing liquid at the outlet of the absorber, the temperature of the absorbing liquid at the outlet of the absorber, the concentration of the absorbing liquid at the outlet of the absorber, the temperature of the absorbing liquid at the inlet of the regenerator, the inlet of the regenerator An absorption liquid property-related value that is at least one value of the concentration of the absorption liquid or a value correlated therewith;
When the control device starts up the absorption heat pump, the absorption liquid property related value acquired by the fluid property related value acquisition means has a predetermined correlation with a temperature at which at least a part of the heated medium evaporates . Controlling the heated medium supply means to start supplying the heated medium to the heat transfer tube when the value is reached;
Absorption heat pump. 前記吸収器が高温吸収器と低温吸収器とを含んで構成されると共に、前記低温吸収器の前記被加熱媒体が前記高温吸収器の前記吸収対象冷媒として構成され；
前記低温吸収器の前記伝熱管の内部の前記被加熱媒体を前記再生器に導く連絡管であって、前記連絡管の内部の流体の流れを止める止め弁が設けられた連絡管を備える；
請求項１に記載の吸収ヒートポンプ。 The absorber includes a high-temperature absorber and a low-temperature absorber, and the heated medium of the low-temperature absorber is configured as the absorption target refrigerant of the high-temperature absorber;
A communication pipe that guides the medium to be heated inside the heat transfer pipe of the low-temperature absorber to the regenerator, and includes a communication pipe provided with a stop valve that stops the flow of fluid inside the communication pipe;
The absorption heat pump according to claim 1. 前記制御装置は、前記流体特性関連値取得手段で取得された値が上昇するに連れて、前記被加熱媒体供給手段から前記伝熱管に供給される前記被加熱媒体の流量を増加させるように構成された；
請求項１又は請求項２に記載の吸収ヒートポンプ。 The controller is configured to increase the flow rate of the heated medium supplied from the heated medium supply unit to the heat transfer tube as the value acquired by the fluid characteristic related value acquisition unit increases. Was;
The absorption heat pump according to claim 1 or 2. 前記伝熱管に供給される前記被加熱媒体を貯留する被加熱媒体貯留部と；
前記伝熱管から流出した前記被加熱媒体の気体と液体との混合流体、又は前記伝熱管から流出した後に発生した前記被加熱媒体の気体と液体との混合流体から、前記被加熱媒体の気体と液体とを分離する気液分離器と；
前記気液分離器から前記伝熱管へ前記被加熱媒体を導く被加熱媒体流路と；
前記被加熱媒体貯留部に貯留されている前記被加熱媒体を、前記気液分離器、前記被加熱媒体流路、又は前記伝熱管へ供給する被加熱媒体ポンプとを備え；
前記被加熱媒体貯留部は、被加熱媒体の液位を検知する被加熱媒体液位検知器を有し；
前記制御装置は、前記被加熱媒体液位検知器が検知した値に応じて供給する前記被加熱媒体の流量を調節するように前記被加熱媒体ポンプを制御する；
請求項１乃至請求項３のいずれか１項に記載の吸収ヒートポンプ。 A heated medium storage section for storing the heated medium supplied to the heat transfer tube;
From the mixed fluid of gas and liquid of the heated medium flowing out from the heat transfer tube, or from the mixed fluid of gas and liquid of the heated medium generated after flowing out of the heat transfer tube, the gas of the heated medium A gas-liquid separator for separating the liquid;
A heated medium flow path for guiding the heated medium from the gas-liquid separator to the heat transfer tube;
A heated medium pump that supplies the heated medium stored in the heated medium storage section to the gas-liquid separator, the heated medium flow path, or the heat transfer pipe;
The heated medium storage unit includes a heated medium liquid level detector that detects a liquid level of the heated medium;
The control device controls the heated medium pump to adjust a flow rate of the heated medium to be supplied according to a value detected by the heated medium liquid level detector;
The absorption heat pump according to any one of claims 1 to 3. 前記伝熱管が、前記被加熱媒体の液体を導入し加熱して蒸発させる蒸発管を有し；
前記吸収器は、複数の前記蒸発管へ前記被加熱媒体を分配する蒸発管分配部にそれぞれの前記蒸発管の一端が接続され、複数の前記蒸発管から前記被加熱媒体を収集する蒸発管収集部にそれぞれの前記蒸発管の他端が接続され、前記蒸発管分配部と前記蒸発管収集部とがそれぞれ１個から構成された；
請求項１乃至請求項４のいずれか１項に記載の吸収ヒートポンプ。 The heat transfer pipe has an evaporation pipe for introducing and heating the liquid to be heated and evaporating;
The absorber is connected to an evaporating tube distribution unit that distributes the heated medium to the plurality of evaporating tubes, and one end of each evaporating tube is connected to collect the heated medium from the plurality of evaporating tubes. The other end of each of the evaporator tubes is connected to the unit, and the evaporator tube distributor and the evaporator tube collector are each composed of one piece;
The absorption heat pump according to any one of claims 1 to 4.
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JPH0686967B2 (en) * 1985-11-05 1994-11-02 三洋電機株式会社 Absorption refrigerator
JPH05248726A (en) * 1992-03-09 1993-09-24 Advance Koojienereeshiyon Syst Gijutsu Kenkyu Kumiai Absorption refrigerating machine
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JPH1130455A (en) * 1997-07-10 1999-02-02 Matsushita Electric Ind Co Ltd Absorption heat pump device
JP2004144394A (en) * 2002-10-24 2004-05-20 Ebara Corp Multi-stage absorption freezing machine and freezing system
US7464562B2 (en) * 2004-10-13 2008-12-16 Ebara Corporation Absorption heat pump
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JP2010164248A (en) * 2009-01-16 2010-07-29 Ebara Corp Absorption heat pump
JP6111094B2 (en) * 2012-04-06 2017-04-05 荏原冷熱システム株式会社 Absorption heat pump
JP2015025629A (en) * 2013-07-28 2015-02-05 井上　修行 Temperature rise type absorption heat pump
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