JP5513981B2 - Absorption heat pump - Google Patents

Absorption heat pump Download PDF

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JP5513981B2
JP5513981B2 JP2010112595A JP2010112595A JP5513981B2 JP 5513981 B2 JP5513981 B2 JP 5513981B2 JP 2010112595 A JP2010112595 A JP 2010112595A JP 2010112595 A JP2010112595 A JP 2010112595A JP 5513981 B2 JP5513981 B2 JP 5513981B2
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refrigerant
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JP2011242016A (en
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修行 井上
智芳 入江
幸大 福住
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荏原冷熱システム株式会社
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems

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Description

本発明は吸収ヒートポンプに関し、特に昇温能力の向上を可能にしつつ適切なＣＯＰで運転可能な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 can be operated with an appropriate COP while allowing an increase in heating capability.

駆動熱源温度より高い温度の被加熱媒体を取り出す昇温型のヒートポンプである第二種吸収ヒートポンプには、被加熱媒体を利用価値の高い高温水又は高温蒸気として取り出すため、被加熱媒体の昇温幅を大きくするべく、吸収器を多段に構成した多段昇温型吸収ヒートポンプがある。多段昇温型吸収ヒートポンプの一例として、高温側吸収器及び低温側吸収器へ供給する冷媒蒸気を発生させる蒸発器を共通にし、高温側吸収器及び低温側吸収器の作動圧力を等しい圧力にして内圧の上昇を抑制した二段昇温型吸収ヒートポンプ（例えば、特許文献１参照。）や、高温側吸収器へ供給する冷媒蒸気を発生させる高温側蒸発器と、低温側吸収器へ供給する冷媒蒸気を発生させる低温側蒸発器とを個別に設け、高温側吸収器を低温側吸収器よりも高い圧力で作動させて、吸収液の結晶ライン付近への濃度上昇を抑制した二段昇温型吸収ヒートポンプ（例えば、特許文献２参照。）がある。   In the type 2 absorption heat pump, which is a temperature rising type heat pump that takes out a heated medium having a temperature higher than the driving heat source temperature, the temperature of the heated medium is increased because the heated medium is taken out as high-temperature water or high-temperature steam having high utility value. In order to increase the width, there is a multistage temperature rising type absorption heat pump in which absorbers are configured in multiple stages. As an example of a multi-stage temperature rising type absorption heat pump, a common evaporator is used to generate refrigerant vapor to be supplied to the high temperature side absorber and the low temperature side absorber, and the operating pressures of the high temperature side absorber and the low temperature side absorber are made equal. A two-stage temperature rising absorption heat pump (for example, refer to Patent Document 1) that suppresses an increase in internal pressure, a high temperature side evaporator that generates refrigerant vapor to be supplied to the high temperature side absorber, and a refrigerant to be supplied to the low temperature side absorber. A two-stage temperature rise type that separately installs a low-temperature side evaporator that generates steam and operates the high-temperature side absorber at a higher pressure than the low-temperature side absorber to suppress the concentration rise near the crystal line of the absorbent There exists an absorption heat pump (for example, refer patent document 2).

特開昭５９−１１５９５２号公報（図２等）JP 59-115952 (FIG. 2 etc.) 特開２００６−１１２６８６号公報（図６等）JP 2006-112686 A (FIG. 6 etc.)

しかしながら、特許文献１及び特許文献２に記載の二段昇温型吸収ヒートポンプでは、被加熱媒体を昇温できる幅が限定的であり、昇温能力が不足する場合があった。昇温能力を向上させるためには吸収器をさらに多段に構成することが考えられるが、吸収器を多段にするほど内圧又は結晶の問題が生ずるだけでなく、ＣＯＰ（成績係数）が低下してしまうという問題があった。   However, in the two-stage temperature rising type absorption heat pump described in Patent Document 1 and Patent Document 2, the range in which the medium to be heated can be raised is limited, and the temperature raising ability may be insufficient. In order to improve the temperature raising capability, it is conceivable to configure the absorber in multiple stages. However, as the number of absorbers is increased, not only the problem of internal pressure or crystals occurs, but also the COP (coefficient of performance) decreases. There was a problem that.

本発明は上述の課題に鑑み、昇温能力の向上を可能にしつつ適切なＣＯＰで運転可能な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 can be operated with an appropriate COP while enabling an increase in heating capability.

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、被加熱媒体Ｗの流路１１を内部に有し、第１の吸収液Ｓａが第１の冷媒蒸気Ｖｒを吸収する際に発生する吸収熱で被加熱媒体Ｗを加熱する第１の吸収器１０と；第１の吸収器１０に第１の冷媒蒸気Ｖｒを供給する蒸発器２０と；第２の吸収液Ｓｂが第２の冷媒蒸気Ｖｓを吸収する際に発生する吸収熱で蒸発器２０内の冷媒液Ｖｆを加熱して第１の冷媒蒸気Ｖｒを生成する、第１の吸収器１０よりも作動温度が低い第２の吸収器３０と；第１の吸収器１０で第１の吸収液Ｓａが第１の冷媒蒸気Ｖｒを吸収して濃度が低下した第１の希溶液Ｓｗを導入し加熱して、第１の希溶液Ｓｗから冷媒を蒸発させて第１の吸収液Ｓａを生成する高温再生器５０と；第２の吸収器３０で第２の吸収液Ｓｂが第２の冷媒蒸気Ｖｓを吸収して濃度が低下した第２の希溶液Ｓｖを導入し加熱して、第２の希溶液Ｓｖから冷媒を蒸発させて第２の吸収液Ｓｂを生成する低温再生器６０と；第１の吸収器１０内の第１の希溶液Ｓｗを高温再生器５０に導く第１の希溶液管１６と；第１の希溶液管１６に接続され、第１の希溶液管１６を流れる第１の希溶液Ｓｗを直接的又は間接的に低温再生器６０へ導く分岐管１７と；第１の希溶液管１６を流れる第１の希溶液Ｓｗを、高温再生器５０へ流入させるのと、低温再生器６０へ流入させるのとを切り替える切替弁１８とを備える。低温再生器において第２の希溶液を加熱する加熱源は、典型的には、排熱が用いられる。   In order to achieve the above object, the absorption heat pump according to the first aspect of the present invention has a flow path 11 of the medium to be heated W inside, for example, as shown in FIG. A first absorber 10 that heats the medium W to be heated with absorption heat generated when absorbing the first refrigerant vapor Vr; and an evaporator 20 that supplies the first refrigerant vapor Vr to the first absorber 10. And the second absorbing liquid Sb heats the refrigerant liquid Vf in the evaporator 20 with the absorption heat generated when the second refrigerant vapor Vs absorbs the second refrigerant vapor Vs, thereby generating the first refrigerant vapor Vr. A second absorber 30 having an operating temperature lower than that of the absorber 10; a first dilute solution in which the first absorber Sa absorbs the first refrigerant vapor Vr in the first absorber 10 to reduce its concentration. High temperature regeneration in which Sw is introduced and heated to evaporate the refrigerant from the first dilute solution Sw to produce the first absorbent Sa 50; the second absorber Sb absorbs the second refrigerant vapor Vs in the second absorber 30 and the second dilute solution Sv having a reduced concentration is introduced and heated to heat the second dilute solution Sv. A low-temperature regenerator 60 that evaporates the refrigerant from the low-pressure regenerator 60 to generate the second absorbent Sb; a first dilute solution pipe 16 that guides the first dilute solution Sw in the first absorber 10 to the high-temperature regenerator 50; A branch pipe 17 connected to the first dilute solution pipe 16 and directing the first dilute solution Sw flowing through the first dilute solution pipe 16 directly or indirectly to the low-temperature regenerator 60; There is provided a switching valve 18 for switching between flowing the first dilute solution Sw flowing through the pipe 16 into the high temperature regenerator 50 and flowing into the low temperature regenerator 60. Exhaust heat is typically used as a heating source for heating the second dilute solution in the low-temperature regenerator.

このように構成すると、第１の希溶液を高温再生器へ流入させるのと低温再生器へ流入させるのとを切り替えることができ、ヒートポンプサイクルの状況に応じて昇温を重視する運転とＣＯＰを重視する運転とを切り替えることができる。   If comprised in this way, it can switch between making a 1st dilute solution flow in into a high temperature regenerator, and letting it flow into a low temperature regenerator, and operation and COP which attach importance to temperature rising according to the situation of a heat pump cycle. It is possible to switch between important driving.

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に示すように、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、第１の吸収器１０から導出される第１の希溶液Ｓｗの濃度を検出する第１の希溶液濃度検出手段９５と；低温再生器６０で生成された第２の吸収液Ｓｂの濃度を検出する第２の吸収液濃度検出手段９６と；第１の希溶液濃度検出手段９５で検出された値が第２の吸収液濃度検出手段９６で検出された値よりも小さいときに第１の希溶液Ｓｗの少なくとも一部を低温再生器６０に導き、第１の希溶液濃度検出手段９５で検出された値が第２の吸収液濃度検出手段９６で検出された値以上のときに第１の希溶液Ｓｗの全部を高温再生器５０に導くように、切替弁１８を制御する制御装置９９とを備える。   Further, the absorption heat pump according to the second aspect of the present invention is a first derived from the first absorber 10 in the absorption heat pump 1 according to the first aspect of the present invention as shown in FIG. First dilute solution concentration detecting means 95 for detecting the concentration of the dilute solution Sw; and second absorbing solution concentration detecting means 96 for detecting the concentration of the second absorbing solution Sb generated by the low temperature regenerator 60; When the value detected by the first dilute solution concentration detecting means 95 is smaller than the value detected by the second absorbing liquid concentration detecting means 96, at least a part of the first dilute solution Sw is transferred to the low temperature regenerator 60. Then, when the value detected by the first dilute solution concentration detecting means 95 is equal to or greater than the value detected by the second absorbing liquid concentration detecting means 96, all of the first dilute solution Sw is guided to the high temperature regenerator 50. And a control device 99 for controlling the switching valve 18.

このように構成すると、ヒートポンプサイクルの状況に応じた運転の切り替えを適切なタイミングで行うことが可能になる。   If comprised in this way, it will become possible to perform the switching of the operation | movement according to the condition of the heat pump cycle at an appropriate timing.

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に示すように、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、第２の吸収器３０で発生した吸収熱を、直接的又は間接的に高温再生器５０内に搬送する吸収熱搬送手段５１を備える。   Moreover, the absorption heat pump which concerns on the 3rd aspect of this invention is a 2nd absorber 30 in the absorption heat pump 1 which concerns on the said 1st aspect or this 2nd aspect of this invention, for example, as shown in FIG. Absorbing heat transfer means 51 for transferring the generated absorbed heat directly or indirectly into the high temperature regenerator 50 is provided.

このように構成すると、昇温の幅を大きくすることができる。   If comprised in this way, the range of temperature rise can be enlarged.

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、第２の吸収器３０に導入される第２の吸収液Ｓｂのうち、第２の冷媒蒸気Ｖｓを吸収する第２の吸収液Ｓｂの流量を調節する吸収液流量調節手段３５、３５ｖを備える。   Moreover, the absorption heat pump according to the fourth aspect of the present invention includes an absorption heat pump 1 according to any one of the first to third aspects of the present invention, as shown in FIG. Among the second absorbing liquid Sb introduced into the second absorber 30, absorbing liquid flow rate adjusting means 35, 35v for adjusting the flow rate of the second absorbing liquid Sb that absorbs the second refrigerant vapor Vs are provided.

このように構成すると、第１の冷媒蒸気の生成量に関係する第２の吸収器で発生する吸収熱の量を調節することができ、ひいては高温再生器に投入される熱量を調節することができ、高温再生器における吸収液の結晶を回避することが可能になる。   With this configuration, it is possible to adjust the amount of heat absorbed by the second absorber related to the amount of first refrigerant vapor generated, and thus to adjust the amount of heat input to the high-temperature regenerator. This makes it possible to avoid crystallization of the absorbing solution in the high-temperature regenerator.

本発明によれば、第１の希溶液を高温再生器へ流入させるのと低温再生器へ流入させるのとを切り替えることができ、ヒートポンプサイクルの状況に応じて昇温を重視する運転とＣＯＰを重視する運転とを切り替えることができる。   According to the present invention, the first dilute solution can be switched between flowing into the high-temperature regenerator and flowing into the low-temperature regenerator, and the operation and COP that place importance on the temperature rise according to the state of the heat pump cycle. It is possible to switch between important driving.

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デューリング線図である。It is a Duhring diagram of the absorption heat pump concerning an embodiment of the invention. 参考例に係る三段昇温型吸収ヒートポンプのデューリング線図である。（ａ）はシリーズフローのもの、（ｂ）はパラレルフローのものを示す。It is a Duhring diagram of the three-step temperature rising type absorption heat pump which concerns on a reference example. (A) shows a series flow, and (b) shows a parallel flow. 本発明の実施の形態に係る吸収ヒートポンプの別の状態におけるデューリング線図である。（ａ）は高温希溶液を低温再生器へ流入させつつ高温再生器へ熱を投入した状態のもの、（ｂ）高温希溶液を低温再生器へ流入させつつ高温再生器へ熱を投入しない状態のものの図である。It is a Duhring diagram in another state of an absorption heat pump concerning an embodiment of the invention. (A) is a state where heat is supplied to the high temperature regenerator while flowing the high temperature dilute solution into the low temperature regenerator, and (b) is a state where heat is not input to the high temperature regenerator while flowing the high temperature dilute solution into the low temperature regenerator. FIG. 本発明の実施の形態の変形例に係る吸収ヒートポンプの模式的系統図である。（ａ）は第１の変形例、（ｂ）は第２の変形例の図である。It is a typical systematic diagram of the absorption heat pump which concerns on the modification of embodiment of this invention. (A) is a 1st modification, (b) is a figure of a 2nd modification.

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、濃度方向及び圧力方向にそれぞれ昇温する三段昇温型の吸収ヒートポンプである。吸収ヒートポンプ１は、主要構成機器として、第１の吸収液としての高温濃溶液Ｓａが第１の冷媒蒸気としての高温冷媒蒸気Ｖｒを吸収する際の吸収熱で被加熱媒体Ｗを加熱する第１の吸収器としての高温吸収器１０と、高温冷媒蒸気Ｖｒを高温吸収器１０に供給する蒸発器としての高温蒸発器２０と、高温吸収器１０よりも作動温度が低い第２の吸収器としての低温吸収器３０と、第２の冷媒蒸気としての低温冷媒蒸気Ｖｓを低温吸収器３０に供給する低温蒸発器４０と、高温濃溶液Ｓａが高温冷媒蒸気Ｖｒを吸収して濃度が低下した第１の希溶液としての高温希溶液Ｓｗを加熱濃縮して高温濃溶液Ｓａを生成する高温再生器５０と、低温吸収器３０において第２の吸収液としての低温濃溶液Ｓｂが低温冷媒蒸気Ｖｓを吸収して濃度が低下した第２の希溶液としての低温希溶液Ｓｖを加熱濃縮して低温濃溶液Ｓｂを生成する低温再生器６０と、高温再生器５０で高温希溶液Ｓｗから蒸発した冷媒と低温再生器６０で低温希溶液Ｓｖから蒸発した冷媒とが混合した再生器冷媒蒸気Ｖｇを冷却して凝縮させる凝縮器７０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 is a three-stage temperature rising type absorption heat pump that raises the temperature in the concentration direction and the pressure direction, respectively. The absorption heat pump 1 is a first component that heats the heated medium W with heat absorbed when the high-temperature concentrated solution Sa as the first absorption liquid absorbs the high-temperature refrigerant vapor Vr as the first refrigerant vapor. A high-temperature absorber 10 as an absorber, a high-temperature evaporator 20 as an evaporator for supplying the high-temperature refrigerant vapor Vr to the high-temperature absorber 10, and a second absorber having a lower operating temperature than the high-temperature absorber 10. The low temperature absorber 30, the low temperature evaporator 40 that supplies the low temperature refrigerant vapor Vs as the second refrigerant vapor to the low temperature absorber 30, and the high temperature concentrated solution Sa absorbs the high temperature refrigerant vapor Vr and the first concentration is lowered. The high-temperature regenerator 50 that heat-concentrates the high-temperature dilute solution Sw as a dilute solution to produce a high-temperature concentrated solution Sa, and the low-temperature concentrated solution Sb as the second absorbent in the low-temperature absorber 30 absorbs the low-temperature refrigerant vapor Vs. The concentration drops The low temperature regenerator 60 that heat-concentrates the low temperature dilute solution Sv as the second dilute solution to generate the low temperature concentrated solution Sb, the refrigerant evaporated from the high temperature dilute solution Sw in the high temperature regenerator 50, and the low temperature regenerator 60 at low temperature. And a condenser 70 for cooling and condensing the regenerator refrigerant vapor Vg mixed with the refrigerant evaporated from the dilute solution Sv.

さらに、吸収ヒートポンプ１は、高温再生器５０の内部を通過するように配設された吸収熱搬送手段としての冷媒蒸気熱源管５１と、高温吸収器１０で加熱された被加熱媒体Ｗを導入して気体の被加熱媒体Ｗである被加熱媒体蒸気Ｗｖと液体の被加熱媒体Ｗである被加熱媒体液Ｗｑとを分離する気液分離器８０と、制御装置９９とを備えている。吸収ヒートポンプ１は、本実施の形態では、比較的利用価値の低い低温（例えば８０℃〜９０℃程度）の排温水ｈを熱源媒体として低温再生器６０及び低温蒸発器４０に供給して、利用価値の高い蒸気Ｗｖ（例えば、圧力が約０．２ＭＰａ（ゲージ圧）を超え、望ましくは０．８ＭＰａ（ゲージ圧）程度）を気液分離器８０から取り出すことができるものである。   Further, the absorption heat pump 1 introduces a refrigerant vapor heat source pipe 51 as absorption heat transfer means disposed so as to pass through the inside of the high-temperature regenerator 50 and the heated medium W heated by the high-temperature absorber 10. A gas-liquid separator 80 that separates a heated medium vapor Wv, which is a gaseous heated medium W, and a heated medium liquid Wq, which is a liquid heated medium W, and a control device 99. In the present embodiment, the absorption heat pump 1 supplies the low-temperature regenerator 60 and the low-temperature evaporator 40 with the low-temperature (for example, about 80 ° C. to 90 ° C.) waste water h having a relatively low utility value as a heat source medium. High-value steam Wv (for example, the pressure exceeds about 0.2 MPa (gauge pressure), desirably about 0.8 MPa (gauge pressure)) can be taken out from the gas-liquid separator 80.

なお、以下の説明においては、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「高温希溶液Ｓｗ」、「低温希溶液Ｓｖ」、「高温濃溶液Ｓａ」、「低温濃溶液Ｓｂ」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「高温冷媒蒸気Ｖｒ」、「低温冷媒蒸気Ｖｓ」、「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、被加熱媒体Ｗは、液体の被加熱媒体Ｗである被加熱媒体液Ｗｑ、気体の被加熱媒体である被加熱媒体蒸気Ｗｖ、被加熱媒体液Ｗｑと被加熱媒体蒸気Ｗｖとが混合した混合被加熱媒体Ｗｍの総称である。本実施の形態では、被加熱媒体Ｗとして水（Ｈ２Ｏ）が用いられている。 In the following description, in order to facilitate the distinction on the heat pump cycle with respect to the absorbing liquid, “high temperature dilute solution Sw”, “low temperature dilute solution Sv”, “high temperature dilute” depending on properties and positions on the heat pump cycle. Although they are referred to as “concentrated solution Sa”, “low temperature concentrated solution Sb”, etc., they are collectively referred to as “absorbing liquid S” when the properties are not questioned. Similarly, regarding the refrigerant, in order to facilitate the distinction on the heat pump cycle, “high temperature refrigerant vapor Vr”, “low temperature refrigerant vapor Vs”, “regenerator refrigerant vapor Vg”, depending on properties and positions on the heat pump cycle, Although it is referred to as “refrigerant liquid Vf” or the like, it is generally referred to as “refrigerant V” when the property or the like is not questioned. 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. The heated medium W is a heated medium liquid Wq which is a liquid heated medium W, a heated medium vapor Wv which is a gaseous heated medium, and the heated medium liquid Wq and the heated medium vapor Wv are mixed. A general term for the mixed medium Wm to be heated. In the present embodiment, water (H 2 O) is used as the heating medium W.

高温吸収器１０は、被加熱媒体Ｗの流路を構成する加熱管１１と、高温濃溶液Ｓａを散布する高温濃溶液散布ノズル１２を内部に有している。高温濃溶液散布ノズル１２は、散布した高温濃溶液Ｓａが加熱管１１に降りかかるように、加熱管１１の上方に配設されている。高温吸収器１０は、高温濃溶液散布ノズル１２から高温濃溶液Ｓａが散布され、高温濃溶液Ｓａが高温冷媒蒸気Ｖｒを吸収する際に吸収熱を発生させる。この吸収熱を、加熱管１１を流れる被加熱媒体Ｗが受熱して、被加熱媒体Ｗが加熱されるように構成されている。高温吸収器１０の下部には、散布された高温濃溶液Ｓａが高温冷媒蒸気Ｖｒを吸収して濃度が低下した高温希溶液Ｓｗが貯留される貯留部１３が形成されている。加熱管１１は、高温希溶液Ｓｗに没入しないように、貯留部１３よりも上方に配設されている。このようにすると、発生した吸収熱が加熱管１１を流れる被加熱媒体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。貯留部１３には、貯留された高温希溶液Ｓｗの液位を検出する高温吸収器液位検出器１４が配設されていると共に、高温希溶液Ｓｗを高温再生器５０又は低温再生器６０へ向けて導出する高温希溶液管１６の一端が接続されている。高温希溶液管１６には、高温吸収器１０から導出される高温希溶液Ｓｗの濃度を検出する第１の希溶液濃度検出手段としての高温希溶液濃度検出器９５が設けられている。なお、高温希溶液濃度検出器９５は、貯留部１３に設けられていてもよい。   The high-temperature absorber 10 includes a heating tube 11 that forms a flow path of the medium to be heated W and a high-temperature concentrated solution spray nozzle 12 that sprays the high-temperature concentrated solution Sa. The hot concentrated solution spray nozzle 12 is disposed above the heating tube 11 so that the sprayed hot concentrated solution Sa falls on the heating tube 11. The high temperature absorber 10 sprays the high temperature concentrated solution Sa from the high temperature concentrated solution spray nozzle 12 and generates heat of absorption when the high temperature concentrated solution Sa absorbs the high temperature refrigerant vapor Vr. The heated medium W flowing through the heating tube 11 receives this absorbed heat so that the heated medium W is heated. In the lower part of the high-temperature absorber 10, a storage part 13 is formed in which the high-temperature dilute solution Sw that has been dispersed by the dispersed high-temperature concentrated solution Sa absorbing the high-temperature refrigerant vapor Vr is stored. The heating tube 11 is disposed above the storage unit 13 so as not to be immersed in the hot dilute solution Sw. If it does in this way, generated absorbed heat will be quickly transmitted to the to-be-heated medium W which flows through the heating pipe | tube 11, and recovery | restoration of absorption capability can be accelerated. The storage unit 13 is provided with a high-temperature absorber liquid level detector 14 that detects the liquid level of the stored high-temperature dilute solution Sw, and the high-temperature dilute solution Sw is supplied to the high-temperature regenerator 50 or the low-temperature regenerator 60. One end of the hot dilute solution pipe 16 leading out is connected. The high temperature dilute solution tube 16 is provided with a high temperature dilute solution concentration detector 95 as a first dilute solution concentration detecting means for detecting the concentration of the high temperature dilute solution Sw derived from the high temperature absorber 10. The high-temperature dilute solution concentration detector 95 may be provided in the storage unit 13.

高温蒸発器２０は、高温吸収器１０に高温冷媒蒸気Ｖｒを供給する構成部材である。高温蒸発器２０は、冷媒液Ｖｆ及び高温冷媒蒸気Ｖｒを収容する冷媒気液分離胴２１と、冷媒液Ｖｆを低温吸収器３０の加熱管３１に導く冷媒液供給管２２と、加熱管３１で冷媒液Ｖｆが加熱されて生成された高温冷媒蒸気Ｖｒあるいは高温冷媒蒸気Ｖｒと冷媒液Ｖｆとの冷媒気液混相を冷媒気液分離胴２１まで案内する高温冷媒蒸気受入管２４と、冷媒気液分離胴２１内にて高温冷媒蒸気Ｖｒ中に含まれる冷媒Ｖの液滴を衝突分離させるバッフル板２５と、冷媒気液分離胴２１内の冷媒液Ｖｆの液位を検出する高温蒸発器液位検出器２６とを有し、加熱管３１の内面を高温蒸発器２０の伝熱面としている。また、高温蒸発器２０には冷媒液Ｖｆを導入する冷媒液管２９が接続されている。冷媒液供給管２２は、冷媒気液分離胴２１の冷媒液Ｖｆが貯留されている部分に一端が接続され、他端が加熱管３１の一端に接続されている。高温冷媒蒸気受入管２４は、冷媒気液分離胴２１内の冷媒液Ｖｆの最高液位とバッフル板２５との間の高さに一端が位置するように配設され、他端が加熱管３１の他端に接続されている。高温蒸発器液位検出器２６は、冷媒液管２９に配設された二方弁２９ｖと信号ケーブルで接続されており、検出した冷媒液Ｖｆの液位に応じて冷媒気液分離胴２１内に導入する冷媒液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。なお、加熱管３１の内部で冷媒液Ｖｆが蒸気に変化して密度が大幅に減少するので、加熱管３１を気泡ポンプとして機能させることで、冷媒液供給管２２内で冷媒液Ｖｆを圧送するポンプを省略することが可能となる。なお、冷媒液供給管２２内に冷媒液Ｖｆを圧送するポンプを設けてもよく、この場合、管内流量を最適化（管内二相流のかわき度の最適化）することで伝熱を改良することも可能となる。   The high temperature evaporator 20 is a component that supplies the high temperature refrigerant vapor Vr to the high temperature absorber 10. The high-temperature evaporator 20 includes a refrigerant gas-liquid separation cylinder 21 that stores the refrigerant liquid Vf and the high-temperature refrigerant vapor Vr, a refrigerant liquid supply pipe 22 that guides the refrigerant liquid Vf to the heating pipe 31 of the low-temperature absorber 30, and the heating pipe 31. A high-temperature refrigerant vapor receiving pipe 24 that guides the high-temperature refrigerant vapor Vr generated by heating the refrigerant liquid Vf or a refrigerant gas-liquid mixed phase of the high-temperature refrigerant vapor Vr and the refrigerant liquid Vf to the refrigerant gas-liquid separation cylinder 21; A baffle plate 25 that collides and separates the droplets of the refrigerant V contained in the high-temperature refrigerant vapor Vr in the separation cylinder 21, and a high-temperature evaporator liquid level that detects the liquid level of the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 21. The inner surface of the heating tube 31 is used as the heat transfer surface of the high-temperature evaporator 20. The high-temperature evaporator 20 is connected to a refrigerant liquid pipe 29 for introducing the refrigerant liquid Vf. One end of the refrigerant liquid supply pipe 22 is connected to the portion of the refrigerant gas-liquid separation cylinder 21 where the refrigerant liquid Vf is stored, and the other end is connected to one end of the heating pipe 31. The high-temperature refrigerant vapor receiving pipe 24 is disposed so that one end is located at a height between the highest liquid level of the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 21 and the baffle plate 25, and the other end is the heating pipe 31. Is connected to the other end. The high-temperature evaporator liquid level detector 26 is connected to a two-way valve 29v disposed in the refrigerant liquid pipe 29 by a signal cable, and the refrigerant gas-liquid separation cylinder 21 is provided in accordance with the detected liquid level of the refrigerant liquid Vf. It is comprised so that the flow volume of the refrigerant | coolant liquid Vf introduce | transduced into can be adjusted. Since the refrigerant liquid Vf changes to steam inside the heating pipe 31 and the density is significantly reduced, the refrigerant liquid Vf is pumped in the refrigerant liquid supply pipe 22 by causing the heating pipe 31 to function as a bubble pump. The pump can be omitted. A pump for pumping the refrigerant liquid Vf may be provided in the refrigerant liquid supply pipe 22, and in this case, the heat transfer is improved by optimizing the flow rate in the pipe (optimizing the degree of the two-phase flow in the pipe). It is also possible.

高温吸収器１０と高温蒸発器２０とは、相互に連通するように１つの缶胴内に形成されている。高温吸収器１０と高温蒸発器２０とが連通することにより、高温蒸発器２０内の高温冷媒蒸気Ｖｒを高温吸収器１０に供給することができるように構成されている。高温吸収器１０と高温蒸発器２０とは、典型的には、高温濃溶液散布ノズル１２より上方及びバッフル板２５より上方で連通している。   The high temperature absorber 10 and the high temperature evaporator 20 are formed in one can body so as to communicate with each other. The high temperature absorber 10 and the high temperature evaporator 20 communicate with each other so that the high temperature refrigerant vapor Vr in the high temperature evaporator 20 can be supplied to the high temperature absorber 10. The high-temperature absorber 10 and the high-temperature evaporator 20 typically communicate with each other above the high-temperature concentrated solution spray nozzle 12 and above the baffle plate 25.

低温吸収器３０は、冷媒液Ｖｆ及び高温冷媒蒸気Ｖｒの流路を構成する加熱管３１と、低温濃溶液Ｓｂを散布する低温濃溶液散布ノズル３２を内部に有している。加熱管３１は、上述のように、一端に冷媒液供給管２２が、他端に高温冷媒蒸気受入管２４が、それぞれ接続されている。低温濃溶液散布ノズル３２は、散布した低温濃溶液Ｓｂが加熱管３１に降りかかるように、加熱管３１の上方に配設されている。低温濃溶液散布ノズル３２には、低温濃溶液Ｓｂを内部に流す低温濃溶液管３８の一端が接続されている。低温吸収器３０は、低温濃溶液散布ノズル３２から低温濃溶液Ｓｂが散布され、低温濃溶液Ｓｂが低温冷媒蒸気Ｖｓを吸収する際に生じる吸収熱により、加熱管３１を流れる冷媒液Ｖｆを加熱して高温冷媒蒸気Ｖｒを生成することができるように構成されている。低温吸収器３０は、高温吸収器１０よりも低い圧力（露点温度）で作動するように構成されており、高温吸収器１０よりも作動温度が低くなっている。低温吸収器３０の下部には、散布された低温濃溶液Ｓｂが低温冷媒蒸気Ｖｓを吸収して濃度が低下した低温希溶液Ｓｖが貯留される貯留部３３が形成されている。加熱管３１は、貯留部３３よりも上方に配設されている。貯留部３３には、貯留された低温希溶液Ｓｖの液位を検出する低温吸収器液位検出器３４が配設されていると共に、低温希溶液Ｓｖを低温再生器６０へ向けて導出する低温希溶液管３６の一端が接続されている。また、低温濃溶液管３８には、内部を流れる低温濃溶液Ｓｂを、低温濃溶液散布ノズル３２をバイパスして加熱管３１の下方に導くバイパス管３５が接続されている。バイパス管３５には、内部を流れる低温濃溶液Ｓｂの流量を調節する流量調節弁３５ｖが配設されている。バイパス管３５及び流量調節弁３５ｖは、吸収液流量調節手段の一形態である。   The low-temperature absorber 30 includes a heating pipe 31 that forms a flow path for the refrigerant liquid Vf and the high-temperature refrigerant vapor Vr, and a low-temperature concentrated solution spray nozzle 32 that sprays the low-temperature concentrated solution Sb. As described above, the heating pipe 31 has one end connected to the refrigerant liquid supply pipe 22 and the other end connected to the high-temperature refrigerant vapor receiving pipe 24. The low temperature concentrated solution spray nozzle 32 is disposed above the heating tube 31 so that the sprayed low temperature concentrated solution Sb falls on the heating tube 31. One end of a low-temperature concentrated solution tube 38 that allows the low-temperature concentrated solution Sb to flow inside is connected to the low-temperature concentrated solution spray nozzle 32. The low-temperature absorber 30 sprays the low-temperature concentrated solution Sb from the low-temperature concentrated solution spray nozzle 32, and heats the refrigerant liquid Vf flowing through the heating pipe 31 by heat absorbed when the low-temperature concentrated solution Sb absorbs the low-temperature refrigerant vapor Vs. Thus, the high-temperature refrigerant vapor Vr can be generated. The low temperature absorber 30 is configured to operate at a pressure (dew point temperature) lower than that of the high temperature absorber 10, and the operating temperature is lower than that of the high temperature absorber 10. In the lower part of the low-temperature absorber 30, a storage part 33 is formed in which the sprayed low-temperature concentrated solution Sb absorbs the low-temperature refrigerant vapor Vs to store the low-temperature dilute solution Sv having a reduced concentration. The heating tube 31 is disposed above the storage unit 33. The storage unit 33 is provided with a low-temperature absorber liquid level detector 34 for detecting the liquid level of the stored low-temperature dilute solution Sv, and a low temperature for deriving the low-temperature dilute solution Sv toward the low-temperature regenerator 60. One end of the dilute solution pipe 36 is connected. The low-temperature concentrated solution pipe 38 is connected to a bypass pipe 35 that guides the low-temperature concentrated solution Sb flowing through the low-temperature concentrated solution pipe 38 to the lower side of the heating pipe 31 by bypassing the low-temperature concentrated solution spray nozzle 32. The bypass pipe 35 is provided with a flow rate adjustment valve 35v for adjusting the flow rate of the low-temperature concentrated solution Sb flowing inside. The bypass pipe 35 and the flow rate adjusting valve 35v are one form of the absorbing liquid flow rate adjusting means.

低温蒸発器４０は、熱源媒体としての排温水ｈの流路を構成する第１の熱源媒体管としての熱源管４１と、冷媒液Ｖｆを散布する冷媒液散布ノズル４２とを内部に有している。冷媒液散布ノズル４２は、散布した冷媒液Ｖｆが熱源管４１に降りかかるように、熱源管４１の上方に配設されている。冷媒液散布ノズル４２には、冷媒液Ｖｆを内部に流す冷媒液管４８の一端が接続されている。冷媒液管４８には、冷媒液散布ノズル４２に供給する冷媒液Ｖｆの流量を調節する流量調節弁４８ｖが配設されている。低温蒸発器４０は、冷媒液散布ノズル４２から冷媒液Ｖｆが散布され、散布された冷媒液Ｖｆが熱源管４１内を流れる排温水ｈの熱で蒸発して低温冷媒蒸気Ｖｓが発生するように構成されている。低温蒸発器４０は、高温蒸発器２０よりも低い圧力（露点温度）で作動するように構成されており、高温蒸発器２０よりも作動温度が低くなっている。低温蒸発器４０の下部には、凝縮器７０から導入し散布された冷媒液Ｖｆのうち蒸発しなかった冷媒液Ｖｆが貯留される貯留部４３が形成されている。貯留部４３には、貯留されている冷媒液Ｖｆを凝縮器７０へと導く冷媒液管４５が接続されている。熱源管４１は、貯留部４３よりも上方に配設されている。貯留部４３には、貯留された冷媒液Ｖｆの液位を検出する低温蒸発器液位検出器４４が配設されている。低温蒸発器液位検出器４４は、冷媒液管４８に配設された流量調節弁４８ｖと信号ケーブルで接続されており、検出した冷媒液Ｖｆの液位に応じて低温蒸発器４０に導入する冷媒液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。   The low-temperature evaporator 40 includes a heat source pipe 41 as a first heat source medium pipe that constitutes a flow path of the exhaust hot water h as a heat source medium, and a refrigerant liquid spray nozzle 42 that sprays the refrigerant liquid Vf. Yes. The refrigerant liquid spray nozzle 42 is disposed above the heat source pipe 41 so that the sprayed refrigerant liquid Vf falls on the heat source pipe 41. One end of a refrigerant liquid pipe 48 through which the refrigerant liquid Vf flows is connected to the refrigerant liquid spray nozzle 42. The refrigerant liquid pipe 48 is provided with a flow rate adjusting valve 48v for adjusting the flow rate of the refrigerant liquid Vf supplied to the refrigerant liquid spraying nozzle 42. In the low-temperature evaporator 40, the refrigerant liquid Vf is sprayed from the refrigerant liquid spray nozzle 42, and the sprayed refrigerant liquid Vf is evaporated by the heat of the exhausted hot water h flowing in the heat source pipe 41 to generate the low-temperature refrigerant vapor Vs. It is configured. The low temperature evaporator 40 is configured to operate at a pressure (dew point temperature) lower than that of the high temperature evaporator 20, and the operating temperature is lower than that of the high temperature evaporator 20. In the lower part of the low-temperature evaporator 40, a storage part 43 is formed in which the refrigerant liquid Vf that has not evaporated out of the refrigerant liquid Vf introduced and dispersed from the condenser 70 is stored. A refrigerant liquid pipe 45 that guides the stored refrigerant liquid Vf to the condenser 70 is connected to the storage unit 43. The heat source tube 41 is disposed above the storage unit 43. The storage unit 43 is provided with a low-temperature evaporator liquid level detector 44 that detects the liquid level of the stored refrigerant liquid Vf. The low-temperature evaporator liquid level detector 44 is connected to the flow rate adjusting valve 48v disposed in the refrigerant liquid pipe 48 by a signal cable, and is introduced into the low-temperature evaporator 40 according to the detected liquid level of the refrigerant liquid Vf. The flow rate of the refrigerant liquid Vf can be adjusted.

低温吸収器３０と低温蒸発器４０とは、相互に連通するように１つの缶胴内に形成されている。低温吸収器３０と低温蒸発器４０とが連通することにより、低温蒸発器４０で発生した低温冷媒蒸気Ｖｓを低温吸収器３０に供給することができるように構成されている。低温吸収器３０と低温蒸発器４０とは、典型的には、低温濃溶液散布ノズル３２より上方及び冷媒液散布ノズル４２より上方で連通している。   The low temperature absorber 30 and the low temperature evaporator 40 are formed in one can body so as to communicate with each other. The low temperature absorber 30 and the low temperature evaporator 40 communicate with each other so that the low temperature refrigerant vapor Vs generated in the low temperature evaporator 40 can be supplied to the low temperature absorber 30. The low-temperature absorber 30 and the low-temperature evaporator 40 typically communicate with each other above the low-temperature concentrated solution spray nozzle 32 and above the refrigerant liquid spray nozzle 42.

高温再生器５０は、冷媒蒸気熱源管５１の一部が内部に配設されている。冷媒蒸気熱源管５１は、高温再生器５０内で開放されておらず、一端が高温蒸発器２０の気相部に接続され、他端が凝縮器７０に接続されており、高温蒸発器２０内で高温冷媒蒸気Ｖｒの形態の冷媒Ｖを受け入れ、高温再生器５０で冷媒液Ｖｆに形を変えたうえで凝縮器７０内へと導くことができるように構成されている。冷媒蒸気熱源管５１には、高温再生器５０の外側で、内部を流れる高温冷媒蒸気Ｖｒの流量を調節する冷媒蒸気熱源流量調節弁としての熱源流量調節弁５１ｖが配設されている。高温再生器５０は、高温希溶液Ｓｗ、あるいは低温再生器６０で生成された低温濃溶液Ｓｂを導入して散布する中間濃溶液散布ノズル５２を有している。中間濃溶液散布ノズル５２は、散布した高温希溶液Ｓｗ又は低温濃溶液Ｓｂが冷媒蒸気熱源管５１に降りかかるように、冷媒蒸気熱源管５１の上方に配設されている。高温再生器５０は、散布された高温希溶液Ｓｗ又は低温濃溶液Ｓｂが冷媒蒸気熱源管５１内を流れる高温冷媒蒸気Ｖｒに加熱されることにより、吸収液Ｓから冷媒Ｖが蒸発して濃度が上昇した高温濃溶液Ｓａが生成され、生成された高温濃溶液Ｓａが下部に貯留されるように構成されている。   In the high temperature regenerator 50, a part of the refrigerant vapor heat source pipe 51 is disposed inside. The refrigerant vapor heat source pipe 51 is not opened in the high temperature regenerator 50, one end is connected to the gas phase part of the high temperature evaporator 20, and the other end is connected to the condenser 70. Then, the refrigerant V in the form of the high-temperature refrigerant vapor Vr is received, changed into the refrigerant liquid Vf by the high-temperature regenerator 50, and then introduced into the condenser 70. The refrigerant vapor heat source pipe 51 is provided with a heat source flow rate adjustment valve 51v as a refrigerant vapor heat source flow rate adjustment valve that adjusts the flow rate of the high temperature refrigerant vapor Vr flowing inside the high temperature regenerator 50 outside. The high temperature regenerator 50 has an intermediate concentrated solution spray nozzle 52 for introducing and spraying the high temperature dilute solution Sw or the low temperature concentrated solution Sb generated by the low temperature regenerator 60. The intermediate concentrated solution spray nozzle 52 is disposed above the refrigerant vapor heat source pipe 51 so that the sprayed hot dilute solution Sw or low temperature concentrated solution Sb falls on the refrigerant vapor heat source pipe 51. In the high-temperature regenerator 50, the sprayed high-temperature dilute solution Sw or low-temperature concentrated solution Sb is heated by the high-temperature refrigerant vapor Vr flowing in the refrigerant vapor heat source pipe 51, whereby the refrigerant V evaporates from the absorbent S and the concentration is increased. The elevated high temperature concentrated solution Sa is generated, and the generated high temperature concentrated solution Sa is stored in the lower part.

高温再生器５０の高温濃溶液Ｓａが貯留される部分と高温吸収器１０の高温濃溶液散布ノズル１２とは、高温濃溶液Ｓａを流す高温濃溶液管５５で接続されている。高温濃溶液管５５には、高温再生器５０の高温濃溶液Ｓａを高温吸収器１０に圧送する高温溶液ポンプ５６が配設されている。高温溶液ポンプ５６は、高温吸収器液位検出器１４と信号ケーブルで接続されたインバータ５６ｖを有しており、高温吸収器液位検出器１４が検出する液位に応じて回転速度が調節されて高温吸収器１０に圧送する高温濃溶液Ｓａの流量を調節することができるように構成されている。中間濃溶液散布ノズル５２と高温吸収器１０の貯留部１３とは、高温希溶液Ｓｗを流す高温希溶液管１６で接続されている。高温濃溶液管５５及び高温希溶液管１６には、高温濃溶液Ｓａと高温希溶液Ｓｗとの間で熱交換を行わせる高温溶液熱交換器５８が配設されている。   The portion of the high temperature regenerator 50 in which the high temperature concentrated solution Sa is stored and the high temperature concentrated solution spray nozzle 12 of the high temperature absorber 10 are connected by a high temperature concentrated solution tube 55 through which the high temperature concentrated solution Sa flows. The high temperature concentrated solution tube 55 is provided with a high temperature solution pump 56 that pumps the high temperature concentrated solution Sa of the high temperature regenerator 50 to the high temperature absorber 10. The high temperature solution pump 56 has an inverter 56v connected to the high temperature absorber liquid level detector 14 by a signal cable, and the rotation speed is adjusted according to the liquid level detected by the high temperature absorber liquid level detector 14. Thus, the flow rate of the hot concentrated solution Sa pumped to the high temperature absorber 10 can be adjusted. The intermediate concentrated solution spray nozzle 52 and the storage unit 13 of the high-temperature absorber 10 are connected by a high-temperature dilute solution pipe 16 through which the high-temperature dilute solution Sw flows. The high temperature concentrated solution tube 55 and the high temperature diluted solution tube 16 are provided with a high temperature solution heat exchanger 58 that performs heat exchange between the high temperature concentrated solution Sa and the high temperature diluted solution Sw.

低温再生器６０は、熱源媒体としての排温水ｈの流路を構成する第２の熱源媒体管としての熱源管６１と、低温希溶液Ｓｖ又は混合希溶液Ｓｘを散布する低混希溶液散布ノズル６２とを有している。混合希溶液Ｓｘは、高温希溶液Ｓｗと低温希溶液Ｓｖとが混合した吸収液である。本実施の形態では、低温蒸発器４０の熱源管４１を流れる排温水ｈと、低温再生器６０の熱源管６１を流れる排温水ｈとは同じ温水であり、熱源管４１を流れた排温水ｈがその後熱源管６１を流れるように配管（不図示）で接続されているが、各熱源管４１、６１に異なる熱源媒体が流れることとしてもよい。低混希溶液散布ノズル６２は、散布した低温希溶液Ｓｖ又は混合希溶液Ｓｘが熱源管６１に降りかかるように、熱源管６１の上方に配設されている。低温再生器６０は、散布された低温希溶液Ｓｖ又は混合希溶液Ｓｘが排温水ｈで加熱されることにより、吸収液Ｓから冷媒Ｖが蒸発して濃度が上昇した低温濃溶液Ｓｂが生成され、生成された低温濃溶液Ｓｂが下部に貯留されるように構成されている。低温再生器６０の下部には、生成された低温濃溶液Ｓｂを貯留する貯留部６３が形成されている。貯留部６３は、堰６３ｓによって落下貯留部６３ａと越流貯留部６３ｂとに分割されており、排温水ｈで加熱されることによって生成された低温濃溶液Ｓｂが落下してまず落下貯留部６３ａに貯留され、落下貯留部６３ａに溜まって堰６３ｓを超えた低温濃溶液Ｓｂが越流貯留部６３ｂに流入するように構成されている。   The low-temperature regenerator 60 includes a heat source pipe 61 as a second heat source medium pipe that constitutes a flow path of the exhaust hot water h as a heat source medium, and a low-mix dilute solution spray nozzle that sprays the low-temperature dilute solution Sv or the mixed dilute solution Sx. 62. The mixed dilute solution Sx is an absorbing solution in which the high temperature dilute solution Sw and the low temperature dilute solution Sv are mixed. In the present embodiment, the exhaust warm water h flowing through the heat source pipe 41 of the low temperature evaporator 40 and the exhaust warm water h flowing through the heat source pipe 61 of the low temperature regenerator 60 are the same hot water, and the exhaust warm water h flowing through the heat source pipe 41 is the same. Are connected by piping (not shown) so as to flow through the heat source pipe 61 thereafter, but different heat source media may flow through the heat source pipes 41 and 61. The low-mixed dilute solution spray nozzle 62 is disposed above the heat source pipe 61 so that the sprayed low-temperature dilute solution Sv or mixed dilute solution Sx falls on the heat source pipe 61. The low-temperature regenerator 60 generates a low-temperature concentrated solution Sb whose concentration has been increased by evaporating the refrigerant V from the absorbing solution S by heating the sprayed low-temperature diluted solution Sv or mixed diluted solution Sx with the exhaust hot water h. The generated low-temperature concentrated solution Sb is stored in the lower part. A storage part 63 for storing the generated low-temperature concentrated solution Sb is formed in the lower part of the low-temperature regenerator 60. The storage part 63 is divided into a drop storage part 63a and an overflow storage part 63b by a weir 63s, and the low temperature concentrated solution Sb generated by being heated by the exhausted hot water h falls and first falls storage part 63a. The low temperature concentrated solution Sb stored in the fall storage part 63a and exceeding the weir 63s is configured to flow into the overflow storage part 63b.

低温再生器６０は、高温再生器５０と同じ缶胴内に収容されている。本実施の形態では、缶胴の下部に高温再生器５０が、上部に低温再生器６０が配設されており、両者の間には熱源管６１の下方及び側方を囲うように設けられた区画板６４が配置されている。区画板６４は、高温再生器５０と低温再生器６０とを完全に隔離するものではなく、両者は互いに連通していて概ね等しい圧力（露点温度）で作動するように構成されている。また、高温再生器５０の気相部と低温再生器６０の気相部とを連通する連通管６７が設けられている。低温再生器６０の落下貯留部６３ａと低温吸収器３０の低温濃溶液散布ノズル３２とは、低温濃溶液Ｓｂを流す低温濃溶液管３８で接続されている。低温濃溶液管３８には、低温再生器６０で生成された低温濃溶液Ｓｂの濃度を検出する第２の吸収液濃度検出手段としての低温濃溶液濃度検出器９６が設けられている。低温濃溶液濃度検出器９６は、貯留部６３に設けられていてもよい。また、低温濃溶液管３８には、バイパス管３５の接続部よりも上流側に、低温再生器６０の低温濃溶液Ｓｂを低温吸収器３０に圧送する低温溶液ポンプ６６が配設されている。低温溶液ポンプ６６は、低温吸収器液位検出器３４と信号ケーブルで接続されたインバータ６６ｖを有しており、低温吸収器液位検出器３４が検出する液位に応じて回転速度が調節され、低温吸収器３０に向けて圧送される低温濃溶液Ｓｂの流量を調節することができるように構成されている。低温再生器６０の越流貯留部６３ｂと、高温溶液熱交換器５８の下流側の高温希溶液管１６とは、中間濃溶液管５７で接続されている。中間濃溶液管５７には、流路を遮断可能な開閉弁５７ｖが配設されている。   The low temperature regenerator 60 is accommodated in the same can body as the high temperature regenerator 50. In the present embodiment, a high-temperature regenerator 50 is disposed at the lower portion of the can body, and a low-temperature regenerator 60 is disposed at the upper portion, and is provided so as to surround the lower side and the side of the heat source pipe 61 therebetween. A partition plate 64 is disposed. The partition plate 64 does not completely separate the high-temperature regenerator 50 and the low-temperature regenerator 60, and both are in communication with each other and are configured to operate at substantially the same pressure (dew point temperature). In addition, a communication pipe 67 that communicates the gas phase portion of the high temperature regenerator 50 and the gas phase portion of the low temperature regenerator 60 is provided. The drop storage part 63a of the low temperature regenerator 60 and the low temperature concentrated solution spray nozzle 32 of the low temperature absorber 30 are connected by a low temperature concentrated solution pipe 38 through which the low temperature concentrated solution Sb flows. The low temperature concentrated solution tube 38 is provided with a low temperature concentrated solution concentration detector 96 as a second absorbent concentration detecting means for detecting the concentration of the low temperature concentrated solution Sb produced by the low temperature regenerator 60. The low-temperature concentrated solution concentration detector 96 may be provided in the storage unit 63. The low temperature concentrated solution pipe 38 is provided with a low temperature solution pump 66 that pumps the low temperature concentrated solution Sb of the low temperature regenerator 60 to the low temperature absorber 30 upstream of the connection portion of the bypass pipe 35. The low temperature solution pump 66 has an inverter 66v connected to the low temperature absorber liquid level detector 34 by a signal cable, and the rotation speed is adjusted according to the liquid level detected by the low temperature absorber liquid level detector 34. The flow rate of the low-temperature concentrated solution Sb pumped toward the low-temperature absorber 30 can be adjusted. The overflow reservoir 63 b of the low temperature regenerator 60 and the high temperature dilute solution pipe 16 on the downstream side of the high temperature solution heat exchanger 58 are connected by an intermediate concentrated solution pipe 57. The intermediate concentrated solution tube 57 is provided with an open / close valve 57v that can shut off the flow path.

低混希溶液散布ノズル６２には、低温希溶液Ｓｖ又は混合希溶液Ｓｘを内部に流す低混希溶液管３７の一端が接続されており、低混希溶液管３７の他端には、低温希溶液管３６と分岐管１７とが接続されている。分岐管１７は、高温希溶液管１６を流れる高温希溶液Ｓｗを、低温再生器６０へ向かわせるように、中間濃溶液管５７の接続部と高温溶液熱交換器５８との間で高温希溶液管１６から分岐した管である。高温希溶液管１６及び分岐管１７には、高温希溶液Ｓｗを高温再生器５０へ向かわせるのと低温再生器６０へ向かわせるのとを切り替える切替弁１８が配設されている。本実施の形態では、切替弁１８が、高温希溶液管１６と分岐管１７との接続部に配設された三方弁であるが、高温希溶液管１６と分岐管１７との接続部より下流側にそれぞれ二方弁を設けることとしてもよい。バイパス管３５の接続部よりも上流側の低温濃溶液管３８及び低温希溶液管３６には、低温濃溶液Ｓｂと低温希溶液Ｓｖとの間で熱交換を行わせる低温溶液熱交換器６８が配設されている。   One end of a low-mixed dilute solution pipe 37 for flowing the low-temperature dilute solution Sv or the mixed dilute solution Sx is connected to the low-mixed dilute solution spray nozzle 62. The dilute solution pipe 36 and the branch pipe 17 are connected. The branch pipe 17 is a high-temperature dilute solution between the connection portion of the intermediate concentrated solution pipe 57 and the high-temperature solution heat exchanger 58 so that the high-temperature dilute solution Sw flowing in the high-temperature dilute solution pipe 16 is directed to the low-temperature regenerator 60. This is a pipe branched from the pipe 16. The high-temperature dilute solution pipe 16 and the branch pipe 17 are provided with a switching valve 18 for switching between directing the high-temperature dilute solution Sw toward the high-temperature regenerator 50 and the low-temperature regenerator 60. In the present embodiment, the switching valve 18 is a three-way valve disposed at the connection portion between the high temperature dilute solution pipe 16 and the branch pipe 17, but is downstream from the connection portion between the high temperature dilute solution pipe 16 and the branch pipe 17. A two-way valve may be provided on each side. The low temperature concentrated solution pipe 38 and the low temperature diluted solution pipe 36 upstream of the connection portion of the bypass pipe 35 are provided with a low temperature solution heat exchanger 68 that performs heat exchange between the low temperature concentrated solution Sb and the low temperature diluted solution Sv. It is arranged.

凝縮器７０は、冷却媒体流路を形成する冷却水管７１を有している。冷却水管７１には、冷却媒体としての冷却水ｃが流れる。凝縮器７０は、高温再生器５０で発生した冷媒Ｖの蒸気と低温再生器６０で発生した冷媒Ｖの蒸気とが混合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。冷却水管７１は、再生器冷媒蒸気Ｖｇを直接冷却することができるように、再生器冷媒蒸気Ｖｇが凝縮した冷媒液Ｖｆに浸らないように配設されている。凝縮器７０には、凝縮した冷媒液Ｖｆを高温蒸発器２０及び低温蒸発器４０に向けて送る冷媒液管７５が接続されている。冷媒液管７５は、高温蒸発器２０に接続された冷媒液管２９及び低温蒸発器４０に接続された冷媒液管４８に接続されており、凝縮器７０内の冷媒液Ｖｆを高温蒸発器２０と低温蒸発器４０とに分配することができるように構成されている。冷媒液管７５には、冷媒液Ｖｆを圧送するための凝縮器冷媒ポンプ７６が配設されている。冷媒液管７５と、冷媒液Ｖｆを低温蒸発器４０の貯留部４３から凝縮器７０へと導く冷媒液管４５とには、凝縮器７０に流入する冷媒液Ｖｆと凝縮器７０から流出した冷媒液Ｖｆとの間で熱交換を行わせる冷媒液熱交換器７８が配設されている。   The condenser 70 has a cooling water pipe 71 that forms a cooling medium flow path. The cooling water c as a cooling medium flows through the cooling water pipe 71. The condenser 70 introduces the regenerator refrigerant vapor Vg in which the vapor of the refrigerant V generated in the high temperature regenerator 50 and the vapor of the refrigerant V generated in the low temperature regenerator 60 are mixed, and cools it with the cooling water c. It is configured to condense. The cooling water pipe 71 is disposed so that the regenerator refrigerant vapor Vg is not immersed in the condensed refrigerant liquid Vf so that the regenerator refrigerant vapor Vg can be directly cooled. The condenser 70 is connected to a refrigerant liquid pipe 75 that sends the condensed refrigerant liquid Vf toward the high temperature evaporator 20 and the low temperature evaporator 40. The refrigerant liquid pipe 75 is connected to the refrigerant liquid pipe 29 connected to the high temperature evaporator 20 and the refrigerant liquid pipe 48 connected to the low temperature evaporator 40, and the refrigerant liquid Vf in the condenser 70 is transferred to the high temperature evaporator 20. And the low-temperature evaporator 40 can be distributed. The refrigerant liquid pipe 75 is provided with a condenser refrigerant pump 76 for pumping the refrigerant liquid Vf. A refrigerant liquid pipe 75 and a refrigerant liquid pipe 45 that guides the refrigerant liquid Vf from the storage portion 43 of the low-temperature evaporator 40 to the condenser 70 are connected to the refrigerant liquid Vf that flows into the condenser 70 and the refrigerant that flows out of the condenser 70. A refrigerant liquid heat exchanger 78 that performs heat exchange with the liquid Vf is disposed.

高温再生器５０及び低温再生器６０と凝縮器７０とは、相互に連通するように１つの缶胴内に形成されている。高温再生器５０及び低温再生器６０と凝縮器７０とが連通することにより、高温再生器５０及び低温再生器６０で発生した再生器冷媒蒸気Ｖｇを凝縮器７０に供給することができるように構成されている。高温再生器５０及び低温再生器６０と凝縮器７０とは、上部の気相部で連通している。また、本実施の形態では、高温再生器５０及び低温再生器６０並びに凝縮器７０が、高温吸収器１０、高温蒸発器２０、低温吸収器３０、低温蒸発器４０の下方に設けられている。   The high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 are formed in one can body so as to communicate with each other. The high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 communicate with each other, so that the regenerator refrigerant vapor Vg generated in the high temperature regenerator 50 and the low temperature regenerator 60 can be supplied to the condenser 70. Has been. The high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 communicate with each other in the upper gas phase portion. In the present embodiment, the high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 are provided below the high temperature absorber 10, the high temperature evaporator 20, the low temperature absorber 30, and the low temperature evaporator 40.

気液分離器８０は、高温吸収器１０の加熱管１１を流れて加熱された被加熱媒体Ｗを導入し、被加熱媒体蒸気Ｗｖと被加熱媒体液Ｗｑとを分離する機器である。気液分離器８０には、内部に貯留する被加熱媒体液Ｗｑの液位を検出する気液分離器液位検出器８１が設けられている。気液分離器８０の下部と高温吸収器１０の加熱管１１の一端とは、被加熱媒体液Ｗｑを加熱管１１に導く被加熱媒体液管８２で接続されている。被加熱媒体液管８２には、被加熱媒体液Ｗｑを加熱管１１に向けて圧送する被加熱媒体ポンプ８３が配設されている。内部が気相部となる気液分離器８０の側面と加熱管１１の他端とは、加熱された被加熱媒体Ｗを気液分離器８０に導く加熱後被加熱媒体管８４で接続されている。   The gas-liquid separator 80 is a device that introduces the heated medium W that flows through the heating tube 11 of the high-temperature absorber 10 and separates the heated medium vapor Wv and the heated medium liquid Wq. The gas-liquid separator 80 is provided with a gas-liquid separator liquid level detector 81 that detects the liquid level of the heated medium liquid Wq stored inside. The lower part of the gas-liquid separator 80 and one end of the heating pipe 11 of the high-temperature absorber 10 are connected by a heated medium liquid pipe 82 that guides the heated medium liquid Wq to the heating pipe 11. The heated medium liquid pipe 82 is provided with a heated medium pump 83 that pumps the heated medium liquid Wq toward the heated pipe 11. The side surface of the gas-liquid separator 80 whose inside is a gas phase portion and the other end of the heating tube 11 are connected by a heated medium tube 84 after heating that guides the heated medium W to the gas-liquid separator 80. Yes.

また、気液分離器８０には、蒸気として系外に供給された分の被加熱媒体Ｗを補うための補給水Ｗｓを系外から導入する補給水管８５が接続されている。補給水管８５には、気液分離器８０に向けて補給水Ｗｓを圧送する補給水ポンプ８６と、逆止弁８５ｃと、補給水Ｗｓを温水で予熱する補給水熱交換器８７とが、補給水Ｗｓの流れ方向に向かってこの順に配設されている。補給水ポンプ８６は、気液分離器液位検出器８１と信号ケーブルで接続されており、気液分離器８０内の被加熱媒体液Ｗｑの液位に応じて発停が制御されるように構成されている。また、気液分離器８０には、被加熱媒体蒸気Ｗｖを系外に供給する被加熱媒体蒸気供給管８９が上部（典型的には頂部）に接続されている。被加熱媒体蒸気供給管８９には、系外に供給する被加熱媒体蒸気Ｗｖの流量を調節することで気液分離器８０内の圧力を調節する圧力調節弁８９ｖが配設されている。気液分離器８０には、内部の静圧を検出する気液分離器圧力センサ９２が設けられている。圧力調節弁８９ｖは、気液分離器圧力センサ９２と信号ケーブルで接続されており、気液分離器圧力センサ９２で検出された圧力に応じて開度を調節することができるように構成されている。   The gas-liquid separator 80 is connected to a makeup water pipe 85 that introduces makeup water Ws for supplementing the heated medium W supplied to the outside of the system as steam from outside the system. The make-up water pipe 85 is supplied with a make-up water pump 86 for pumping make-up water Ws toward the gas-liquid separator 80, a check valve 85c, and a make-up water heat exchanger 87 for preheating the make-up water Ws with warm water. It arrange | positions in this order toward the flow direction of water Ws. The make-up water pump 86 is connected to the gas-liquid separator liquid level detector 81 through a signal cable so that the start / stop is controlled according to the liquid level of the heated medium liquid Wq in the gas-liquid separator 80. It is configured. Further, the heated liquid vapor supply pipe 89 for supplying the heated medium vapor Wv to the outside of the system is connected to the upper part (typically the top) of the gas-liquid separator 80. The heated medium vapor supply pipe 89 is provided with a pressure adjustment valve 89v that adjusts the pressure in the gas-liquid separator 80 by adjusting the flow rate of the heated medium vapor Wv supplied outside the system. The gas-liquid separator 80 is provided with a gas-liquid separator pressure sensor 92 that detects an internal static pressure. The pressure control valve 89v is connected to the gas-liquid separator pressure sensor 92 through a signal cable, and is configured to be able to adjust the opening according to the pressure detected by the gas-liquid separator pressure sensor 92. Yes.

気液分離器８０は、加熱管１１内で被加熱媒体液Ｗｑの一部が蒸発して被加熱媒体液Ｗｑと被加熱媒体蒸気Ｗｖとが混合した混合被加熱媒体Ｗｍを導入してもよく、被加熱媒体液Ｗｑのまま気液分離器８０に導いて減圧し一部を気化させて混合被加熱媒体Ｗｍとしたものを気液分離させるようにしてもよい。被加熱媒体液Ｗｑを減圧気化するには、オリフィス等の絞り手段を用いることができる。加熱管１１内で被加熱媒体液Ｗｑの一部を蒸発させるか否かは、典型的には、被加熱媒体ポンプ８３及び／又は補給水ポンプ８６の吐出圧力を調節することにより、加熱管１１内の圧力を被加熱媒体液Ｗｑの温度に相当する飽和圧力よりも高くするか否かによって調節することができる。   The gas-liquid separator 80 may introduce a mixed heated medium Wm in which part of the heated medium liquid Wq is evaporated in the heating tube 11 and the heated medium liquid Wq and the heated medium vapor Wv are mixed. Alternatively, the heated medium liquid Wq may be guided to the gas-liquid separator 80, and the pressure may be reduced to partially vaporize the mixed heated medium Wm for gas-liquid separation. In order to vaporize the medium to be heated Wq under reduced pressure, a throttle means such as an orifice can be used. Whether or not a part of the heated medium liquid Wq is evaporated in the heating pipe 11 is typically determined by adjusting the discharge pressure of the heated medium pump 83 and / or the make-up water pump 86. The internal pressure can be adjusted by whether or not the internal pressure is higher than a saturation pressure corresponding to the temperature of the heated medium liquid Wq.

制御装置９９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９９は、凝縮器冷媒ポンプ７６、被加熱媒体ポンプ８３とそれぞれ信号ケーブルで接続されており、これらの発停や回転速度の調節を行うことができるように構成されている。これまでの説明では高温吸収器液位検出器１４の出力を直接入力して制御されることとした高温溶液ポンプ５６、低温吸収器液位検出器３４の出力を直接入力して制御されることとした低温溶液ポンプ６６、及び気液分離器液位検出器８１の出力を直接入力して制御されることとした補給水ポンプ８６も、制御装置９９を介して（検出器の出力信号を一旦制御装置９９に入力して）制御されることとしてもよい。また、制御装置９９は、切替弁１８、流量調節弁３５ｖ、開閉弁５７ｖ、熱源流量調節弁５１ｖとそれぞれ信号ケーブルで接続されており、各弁の切り替え又は開閉動作あるいは開度を調節することができるように構成されている。これまでの説明では高温蒸発器液位検出器２６の出力を直接入力して制御されることとした二方弁２９ｖ、低温蒸発器液位検出器４４の出力を直接入力して制御されることとした流量調節弁４８ｖ、及び気液分離器圧力センサ９２の出力を直接入力して制御されることとした圧力調節弁８９ｖも、制御装置９９を介して（検出器の出力信号を一旦制御装置９９に入力して）制御されることとしてもよい。また、制御装置９９は、高温希溶液濃度検出器９５及び低温濃溶液濃度検出器９６とそれぞれ信号ケーブルで接続されており、検出値のデータを受信することができるように構成されている。   The control device 99 is a device that controls the operation of the absorption heat pump 1. The control device 99 is connected to the condenser refrigerant pump 76 and the heated medium pump 83 via signal cables, respectively, and is configured to be able to start / stop and adjust the rotation speed. In the description so far, the output of the high-temperature absorber liquid level detector 14 is directly input and controlled, and the output of the high-temperature solution pump 56 and the low-temperature absorber liquid level detector 34 is directly input and controlled. The replenishing water pump 86 that is controlled by directly inputting the output of the low-temperature solution pump 66 and the gas-liquid separator liquid level detector 81 are also connected via the control device 99 (the output signal of the detector is temporarily set). It is good also as being controlled by inputting into the control apparatus 99. FIG. Further, the control device 99 is connected to the switching valve 18, the flow rate adjusting valve 35v, the on-off valve 57v, and the heat source flow rate adjusting valve 51v through signal cables, respectively, and can adjust the switching or opening / closing operation or opening degree of each valve. It is configured to be able to. In the description so far, the output of the high-temperature evaporator liquid level detector 26 is directly input and controlled. The two-way valve 29v and the output of the low-temperature evaporator liquid level detector 44 are directly input and controlled. The flow rate control valve 48v and the pressure control valve 89v that are controlled by directly inputting the output of the gas-liquid separator pressure sensor 92 are also connected via the control device 99 (the output signal of the detector is once controlled by the control device). It is also possible to be controlled (by inputting to 99). The control device 99 is connected to the high-temperature dilute solution concentration detector 95 and the low-temperature concentrated solution concentration detector 96 via signal cables, respectively, and is configured to receive detection value data.

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。はじめに、切替弁１８が高温希溶液Ｓｗを高温再生器５０へ導くように設定され、開閉弁５７ｖが閉じられており、熱源流量調節弁５１ｖが開となっている状態の作用を説明する。まず、冷媒側のサイクルを説明する。凝縮器７０では、高温再生器５０及び低温再生器６０で発生した再生器冷媒蒸気Ｖｇを受け入れて、冷却水管７１を流れる冷却水ｃで冷却して凝縮し、冷媒液Ｖｆとする。凝縮した冷媒液Ｖｆは、凝縮器冷媒ポンプ７６で高温蒸発器２０及び低温蒸発器４０に向けて圧送される。凝縮器冷媒ポンプ７６で圧送された冷媒液Ｖｆは、冷媒液管７５を流れた後、冷媒液管２９と冷媒液管４８とに分流され、冷媒液管２９を流れる冷媒液Ｖｆは冷媒気液分離胴２１に導入され、冷媒液管４８を流れる冷媒液Ｖｆは冷媒液散布ノズル４２から散布される。このとき、高温蒸発器２０の冷媒気液分離胴２１の下部に溜まった冷媒液Ｖｆが所定の液位になるように、高温蒸発器液位検出器２６の検出液位に応じて二方弁２９ｖが制御され、低温蒸発器４０の貯留部４３内の冷媒液Ｖｆが所定の液位になるように、低温蒸発器液位検出器４４の検出液位に応じて流量調節弁４８ｖが制御される。   With continued reference to FIG. 1, the operation of the absorption heat pump 1 will be described. First, the operation in a state in which the switching valve 18 is set to guide the hot dilute solution Sw to the high temperature regenerator 50, the on-off valve 57v is closed, and the heat source flow rate adjustment valve 51v is opened will be described. First, the refrigerant side cycle will be described. In the condenser 70, the regenerator refrigerant vapor Vg generated in the high temperature regenerator 50 and the low temperature regenerator 60 is received, cooled and condensed with the cooling water c flowing through the cooling water pipe 71, and the refrigerant liquid Vf is obtained. The condensed refrigerant liquid Vf is pumped by the condenser refrigerant pump 76 toward the high temperature evaporator 20 and the low temperature evaporator 40. The refrigerant liquid Vf pumped by the condenser refrigerant pump 76 flows through the refrigerant liquid pipe 75, and then is divided into the refrigerant liquid pipe 29 and the refrigerant liquid pipe 48. The refrigerant liquid Vf flowing through the refrigerant liquid pipe 29 is the refrigerant gas-liquid. The refrigerant liquid Vf introduced into the separation cylinder 21 and flowing through the refrigerant liquid pipe 48 is sprayed from the refrigerant liquid spray nozzle 42. At this time, the two-way valve according to the detected liquid level of the high-temperature evaporator liquid level detector 26 so that the refrigerant liquid Vf accumulated in the lower part of the refrigerant gas-liquid separation cylinder 21 of the high-temperature evaporator 20 becomes a predetermined liquid level. 29v is controlled, and the flow rate adjustment valve 48v is controlled according to the detected liquid level of the low temperature evaporator liquid level detector 44 so that the refrigerant liquid Vf in the storage unit 43 of the low temperature evaporator 40 becomes a predetermined liquid level. The

冷媒液散布ノズル４２から散布された冷媒液Ｖｆは、熱源管４１内を流れる排温水ｈによって加熱され蒸発して低温冷媒蒸気Ｖｓとなる。低温蒸発器４０で発生した低温冷媒蒸気Ｖｓは、低温蒸発器４０と連通する低温吸収器３０へと移動する。他方、冷媒気液分離胴２１に導入された冷媒液Ｖｆは、重力によって低温吸収器３０の加熱管３１に送られる。加熱管３１に送られた冷媒液Ｖｆは、低温吸収器３０において、低温蒸発器４０で発生して低温吸収器３０に移動してきた低温冷媒蒸気Ｖｓが低温濃溶液Ｓｂに吸収される際に発生する吸収熱により加熱され、この加熱により蒸発して高温冷媒蒸気Ｖｒとなる。加熱管３１内で発生した高温冷媒蒸気Ｖｒは、冷媒液Ｖｆよりも密度が小さいために高温蒸発器２０に向かって上昇し、高温冷媒蒸気受入管２４を流れて冷媒気液分離胴２１に至り、高温蒸発器２０と連通する高温吸収器１０へと移動する。さらに、冷媒気液分離胴２１に到達した高温冷媒蒸気Ｖｒの一部は冷媒蒸気熱源管５１内に入り、高温再生器５０内で、中間濃溶液散布ノズル５２から散布された低温濃溶液Ｓｂに熱を奪われて凝縮し、凝縮した冷媒液Ｖｆは凝縮器７０内に流入する。このように、冷媒蒸気熱源管５１内の高温冷媒蒸気Ｖｒは、特別な動力を要しないで凝縮器７０へ向けて流れる。   The refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 42 is heated and evaporated by the exhausted hot water h flowing in the heat source pipe 41 to become a low-temperature refrigerant vapor Vs. The low-temperature refrigerant vapor Vs generated in the low-temperature evaporator 40 moves to the low-temperature absorber 30 that communicates with the low-temperature evaporator 40. On the other hand, the refrigerant liquid Vf introduced into the refrigerant gas-liquid separation cylinder 21 is sent to the heating pipe 31 of the low-temperature absorber 30 by gravity. The refrigerant liquid Vf sent to the heating pipe 31 is generated in the low temperature absorber 30 when the low temperature refrigerant vapor Vs generated in the low temperature evaporator 40 and moved to the low temperature absorber 30 is absorbed by the low temperature concentrated solution Sb. It is heated by the absorbed heat, and evaporates by this heating to become high-temperature refrigerant vapor Vr. Since the high-temperature refrigerant vapor Vr generated in the heating pipe 31 has a lower density than the refrigerant liquid Vf, the high-temperature refrigerant vapor Vr rises toward the high-temperature evaporator 20 and flows through the high-temperature refrigerant vapor receiving pipe 24 to reach the refrigerant gas-liquid separation cylinder 21. Then, it moves to the high-temperature absorber 10 that communicates with the high-temperature evaporator 20. Further, part of the high-temperature refrigerant vapor Vr that has reached the refrigerant gas-liquid separation cylinder 21 enters the refrigerant vapor heat source pipe 51, and in the high-temperature regenerator 50, the low-temperature concentrated solution Sb sprayed from the intermediate concentrated solution spray nozzle 52. The condensed refrigerant liquid Vf is deprived of heat and flows into the condenser 70. Thus, the high-temperature refrigerant vapor Vr in the refrigerant vapor heat source pipe 51 flows toward the condenser 70 without requiring special power.

次に吸収ヒートポンプ１の吸収液側のサイクルを説明する。高温吸収器１０では、高温濃溶液Ｓａが高温濃溶液散布ノズル１２から散布され、この散布された高温濃溶液Ｓａが高温蒸発器２０から移動してきた高温冷媒蒸気Ｖｒを吸収する。高温冷媒蒸気Ｖｒを吸収した高温濃溶液Ｓａは、濃度が低下して高温希溶液Ｓｗとなる。高温吸収器１０では、高温濃溶液Ｓａが高温冷媒蒸気Ｖｒを吸収する際に吸収熱が発生する。この吸収熱により、加熱管１１を流れる被加熱媒体液Ｗｑが加熱される。ここで、被加熱媒体蒸気Ｗｖを取り出すための気液分離器８０まわりの作用について説明する。   Next, the cycle on the absorption liquid side of the absorption heat pump 1 will be described. In the high-temperature absorber 10, the hot concentrated solution Sa is sprayed from the hot concentrated solution spray nozzle 12, and the sprayed hot concentrated solution Sa absorbs the high-temperature refrigerant vapor Vr that has moved from the high-temperature evaporator 20. The high temperature concentrated solution Sa that has absorbed the high temperature refrigerant vapor Vr is reduced in concentration to become a high temperature diluted solution Sw. In the high-temperature absorber 10, heat of absorption is generated when the high-temperature concentrated solution Sa absorbs the high-temperature refrigerant vapor Vr. The absorbed medium liquid Wq flowing through the heating tube 11 is heated by the absorbed heat. Here, the operation around the gas-liquid separator 80 for taking out the heated medium vapor Wv will be described.

気液分離器８０には、系外から補給水Ｗｓが補給水管８５を介して導入される。補給水Ｗｓは、補給水ポンプ８６により補給水管８５を圧送され、補給水熱交換器８７で温度が上昇した後に気液分離器８０に導入される。気液分離器８０に導入された補給水Ｗｓは、被加熱媒体液Ｗｑとして気液分離器８０の下部に貯留される。気液分離器８０の下部に貯留される被加熱媒体液Ｗｑが所定の液位になるように、補給水ポンプ８６が制御される。気液分離器８０の下部に貯留されている被加熱媒体液Ｗｑは、被加熱媒体ポンプ８３で高温吸収器１０の加熱管１１に送られる。加熱管１１に送られた被加熱媒体液Ｗｑは、高温吸収器１０における上述の吸収熱により加熱される。加熱管１１で加熱された被加熱媒体液Ｗｑは、一部が蒸発して被加熱媒体蒸気Ｗｖとなった混合被加熱媒体Ｗｍとして、あるいは温度が上昇した被加熱媒体液Ｗｑとして、気液分離器８０に向けて加熱後被加熱媒体管８４を流れる。加熱後被加熱媒体管８４を、温度が上昇した被加熱媒体液Ｗｑが流れる場合、被加熱媒体液Ｗｑは、気液分離器８０に導入される際に減圧され、一部が蒸発して被加熱媒体蒸気Ｗｖとなった混合被加熱媒体Ｗｍとして気液分離器８０に導入される。気液分離器８０に導入された混合被加熱媒体Ｗｍは、被加熱媒体液Ｗｑと被加熱媒体蒸気Ｗｖとが分離される。分離された被加熱媒体液Ｗｑは、気液分離器８０の下部に貯留され、再び高温吸収器１０の加熱管１１に送られる。他方、分離された被加熱媒体蒸気Ｗｖは、被加熱媒体蒸気供給管８９に導出され、蒸気利用場所に供給される。本実施の形態では、０．２〜０．４ＭＰａ（ゲージ圧）を超える被加熱媒体蒸気Ｗｖが気液分離器８０から導出され、また、排温水ｈの温度を上昇させることで０．８ＭＰａ（ゲージ圧）程度の、あるいはこれらの間の任意の圧力の被加熱媒体蒸気Ｗｖが導出される。   The gas-liquid separator 80 is introduced with makeup water Ws from outside the system via a makeup water pipe 85. The makeup water Ws is pumped through the makeup water pipe 85 by the makeup water pump 86 and is introduced into the gas-liquid separator 80 after the temperature rises by the makeup water heat exchanger 87. The makeup water Ws introduced into the gas-liquid separator 80 is stored in the lower part of the gas-liquid separator 80 as the heated medium liquid Wq. The makeup water pump 86 is controlled so that the heated medium liquid Wq stored in the lower part of the gas-liquid separator 80 becomes a predetermined liquid level. The heated medium liquid Wq stored in the lower part of the gas-liquid separator 80 is sent to the heating tube 11 of the high-temperature absorber 10 by the heated medium pump 83. The heated medium liquid Wq sent to the heating tube 11 is heated by the above-described absorption heat in the high-temperature absorber 10. The heated medium liquid Wq heated by the heating tube 11 is gas-liquid separated as a mixed heated medium Wm partially evaporated to become a heated medium vapor Wv, or as a heated medium liquid Wq whose temperature has increased. Flows through the heated medium tube 84 after heating toward the vessel 80. When the heated medium liquid Wq whose temperature has risen flows through the heated medium pipe 84 after heating, the heated medium liquid Wq is depressurized when being introduced into the gas-liquid separator 80, and a part of the heated medium liquid Wq is evaporated and covered. The mixed medium to be heated Wm that has become the heating medium vapor Wv is introduced into the gas-liquid separator 80. In the mixed heated medium Wm introduced into the gas-liquid separator 80, the heated medium liquid Wq and the heated medium vapor Wv are separated. The separated heated medium liquid Wq is stored in the lower part of the gas-liquid separator 80 and sent again to the heating tube 11 of the high-temperature absorber 10. On the other hand, the separated heated medium vapor Wv is led out to the heated medium vapor supply pipe 89 and supplied to the vapor use place. In the present embodiment, the heated medium vapor Wv exceeding 0.2 to 0.4 MPa (gauge pressure) is led out from the gas-liquid separator 80, and the temperature of the exhaust hot water h is raised to 0.8 MPa ( The heated medium vapor Wv having a pressure of about the gauge pressure) or an arbitrary pressure therebetween is derived.

再び吸収ヒートポンプ１の吸収液側のサイクルの説明に戻る。高温吸収器１０で高温冷媒蒸気Ｖｒを吸収した高温濃溶液Ｓａは、濃度が低下して高温希溶液Ｓｗとなり、貯留部１３に貯留される。貯留部１３内の高温希溶液Ｓｗは、重力及び内圧の差により高温再生器５０に向かって高温希溶液管１６を流れ、高温溶液熱交換器５８で高温濃溶液Ｓａと熱交換して温度が低下した後に、中間濃溶液散布ノズル５２に至る。その後、高温希溶液Ｓｗは、冷媒蒸気熱源管５１に向けて散布され、冷媒蒸気熱源管５１内を流れる高温冷媒蒸気Ｖｒによって加熱濃縮されて、冷媒Ｖの一部が蒸発して濃度が上昇し、高温濃溶液Ｓａとなって、高温再生器５０の下部に貯留される。高温再生器５０の下部に貯留された高温濃溶液Ｓａは、高温溶液ポンプ５６により、高温濃溶液管５５を介して吸収器１０の高温濃溶液散布ノズル１２に向けて圧送され、高温溶液熱交換器５８で高温希溶液Ｓｗと熱交換して温度が上昇した後に、高温濃溶液散布ノズル１２に至る。このとき、高温吸収器１０の貯留部１３に貯留された高温希溶液Ｓｗが所定の液位になるように、高温吸収器液位検出器１４の検出液位に応じてインバータ５６ｖにより高温溶液ポンプ５６の回転速度（ひいては吐出流量）が調節される。高温濃溶液散布ノズル１２に到達した高温濃溶液Ｓａは、高温濃溶液散布ノズル１２から散布され、以降、同様のサイクルを繰り返す。   Returning to the description of the cycle on the absorption liquid side of the absorption heat pump 1 again. The high-temperature concentrated solution Sa that has absorbed the high-temperature refrigerant vapor Vr by the high-temperature absorber 10 is reduced in concentration to become a high-temperature dilute solution Sw, and is stored in the storage unit 13. The high-temperature dilute solution Sw in the reservoir 13 flows through the high-temperature dilute solution pipe 16 toward the high-temperature regenerator 50 due to the difference between gravity and internal pressure, and exchanges heat with the high-temperature concentrated solution Sa in the high-temperature solution heat exchanger 58 to have a temperature. After the decrease, the intermediate concentrated solution spray nozzle 52 is reached. Thereafter, the high-temperature dilute solution Sw is sprayed toward the refrigerant vapor heat source pipe 51 and is heated and concentrated by the high-temperature refrigerant vapor Vr flowing in the refrigerant vapor heat source pipe 51, and a part of the refrigerant V evaporates to increase the concentration. The high-temperature concentrated solution Sa is stored in the lower part of the high-temperature regenerator 50. The high temperature concentrated solution Sa stored in the lower part of the high temperature regenerator 50 is pumped by the high temperature solution pump 56 toward the high temperature concentrated solution spray nozzle 12 of the absorber 10 via the high temperature concentrated solution tube 55, and high temperature solution heat exchange is performed. After the temperature rises due to heat exchange with the hot dilute solution Sw in the vessel 58, the hot melt solution spray nozzle 12 is reached. At this time, the high temperature solution pump is driven by the inverter 56v according to the detected liquid level of the high temperature absorber liquid level detector 14 so that the high temperature dilute solution Sw stored in the storage unit 13 of the high temperature absorber 10 becomes a predetermined liquid level. The rotational speed 56 (and thus the discharge flow rate) is adjusted. The hot concentrated solution Sa that has reached the hot concentrated solution spray nozzle 12 is sprayed from the hot concentrated solution spray nozzle 12, and thereafter the same cycle is repeated.

他方、低温吸収器３０では、低温濃溶液Ｓｂが、低温濃溶液散布ノズル３２から加熱管３１に向けて散布され、低温蒸発器４０から移動してきた低温冷媒蒸気Ｖｓを吸収し、その際に発生する吸収熱で加熱管３１内を流れる冷媒液Ｖｆを加熱して高温冷媒蒸気Ｖｒとする。低温冷媒蒸気Ｖｓを吸収した低温濃溶液Ｓｂは、濃度が低下して低温希溶液Ｓｖとなり、貯留部３３に貯留される。貯留部３３の低温希溶液Ｓｖは、重力及び内圧の差により低温再生器６０へ送られる。低温希溶液Ｓｖは、低温吸収器３０から低温再生器６０に向かって低温希溶液管３６を流れる際、低温溶液熱交換器６８で落下貯留部６３ａから導出された低温濃溶液Ｓｂと熱交換して温度が低下した後に、低混希溶液管３７を介して低温再生器６０に送られて、低混希溶液散布ノズル６２から散布される。低混希溶液散布ノズル６２から散布された低温希溶液Ｓｖは、熱源管６１を流れる排温水ｈ（本実施の形態では約８０℃前後）によって加熱され、散布された低温希溶液Ｓｖ中の冷媒Ｖの一部が蒸発し濃度が上昇して低温濃溶液Ｓｂとなり、まず低温再生器６０の落下貯留部６３ａに貯留され、落下貯留部６３ａの液位が上昇して堰６３ｓを越えた分が越流貯留部６３ｂに貯留される。ここでは、開閉弁５７ｖが閉じているので、低温濃溶液Ｓｂは越流貯留部６３ｂから流出せずに貯留される。なお、貯留部６３の低温濃溶液Ｓｂの液位が連通管６７の上端開口よりも上昇した場合は、連通管６７を通して高温再生器５０に流入する。   On the other hand, in the low-temperature absorber 30, the low-temperature concentrated solution Sb is sprayed from the low-temperature concentrated solution spray nozzle 32 toward the heating pipe 31, absorbs the low-temperature refrigerant vapor Vs that has moved from the low-temperature evaporator 40, and is generated at that time. The refrigerant liquid Vf flowing in the heating pipe 31 is heated by the absorbed heat to be converted into a high-temperature refrigerant vapor Vr. The low-temperature concentrated solution Sb that has absorbed the low-temperature refrigerant vapor Vs decreases in concentration to become a low-temperature dilute solution Sv and is stored in the storage unit 33. The low temperature dilute solution Sv in the reservoir 33 is sent to the low temperature regenerator 60 due to the difference between gravity and internal pressure. When the low-temperature dilute solution Sv flows through the low-temperature dilute solution tube 36 from the low-temperature absorber 30 toward the low-temperature regenerator 60, the low-temperature dilute solution Sv exchanges heat with the low-temperature concentrated solution Sb derived from the drop storage unit 63a by the low-temperature solution heat exchanger 68. Then, after the temperature is lowered, it is sent to the low-temperature regenerator 60 through the low-mixed dilute solution pipe 37 and sprayed from the low-mixed dilute solution spray nozzle 62. The low temperature dilute solution Sv sprayed from the low dilute solution spray nozzle 62 is heated by the exhausted hot water h (about 80 ° C. in the present embodiment) flowing through the heat source pipe 61, and the refrigerant in the sprayed low temperature dilute solution Sv. A part of V evaporates and the concentration rises to become a low-temperature concentrated solution Sb, which is first stored in the drop reservoir 63a of the low-temperature regenerator 60, and the liquid level in the drop reservoir 63a rises and exceeds the weir 63s. It is stored in the overflow storage part 63b. Here, since the on-off valve 57v is closed, the low-temperature concentrated solution Sb is stored without flowing out of the overflow storage portion 63b. When the liquid level of the low-temperature concentrated solution Sb in the storage unit 63 rises from the upper end opening of the communication pipe 67, it flows into the high-temperature regenerator 50 through the communication pipe 67.

他方、低温希溶液Ｓｖから蒸発した冷媒Ｖは、高温再生器５０で発生した冷媒Ｖの蒸気と合流し、再生器冷媒蒸気Ｖｇとして凝縮器７０へと移動する。低温再生器６０の落下貯留部６３ａに貯留された低温濃溶液Ｓｂは、低温溶液ポンプ６６により、低温濃溶液管３８を介して低温吸収器３０の低温濃溶液散布ノズル３２に圧送される。このとき、低温吸収器３０の貯留部３３に貯留される低温希溶液Ｓｖの液位が所定の液位になるように、低温吸収器液位検出器３４の検出液位に応じてインバータ６６ｖにより低温溶液ポンプ６６の回転速度（ひいては吐出流量）が調節される。低温濃溶液管３８を流れる低温濃溶液Ｓｂは、低温溶液熱交換器６８で低温希溶液Ｓｖと熱交換して温度が上昇してから低温吸収器３０に流入し、低温濃溶液散布ノズル３２から散布される。以降、同様のサイクルを繰り返す。このように、これまで説明した状態の吸収ヒートポンプ１では、吸収液Ｓ側のサイクルが、高温吸収器１０及び高温再生器５０の系統と、低温吸収器３０及び低温再生器６０の系統とに分かれている。   On the other hand, the refrigerant V evaporated from the low temperature dilute solution Sv merges with the vapor of the refrigerant V generated in the high temperature regenerator 50 and moves to the condenser 70 as the regenerator refrigerant vapor Vg. The low temperature concentrated solution Sb stored in the drop storage unit 63a of the low temperature regenerator 60 is pumped by the low temperature solution pump 66 to the low temperature concentrated solution spray nozzle 32 of the low temperature absorber 30 via the low temperature concentrated solution pipe 38. At this time, the inverter 66v according to the detected liquid level of the low temperature absorber liquid level detector 34 so that the liquid level of the low temperature diluted solution Sv stored in the storage unit 33 of the low temperature absorber 30 becomes a predetermined liquid level. The rotational speed (and hence the discharge flow rate) of the low temperature solution pump 66 is adjusted. The low-temperature concentrated solution Sb flowing through the low-temperature concentrated solution pipe 38 heat-exchanges with the low-temperature dilute solution Sv in the low-temperature solution heat exchanger 68 and rises in temperature, and then flows into the low-temperature absorber 30. Be sprayed. Thereafter, the same cycle is repeated. Thus, in the absorption heat pump 1 in the state described so far, the cycle on the side of the absorbent S is divided into a system of the high temperature absorber 10 and the high temperature regenerator 50 and a system of the low temperature absorber 30 and the low temperature regenerator 60. ing.

図２のデューリング線図をも参照して、上述した状態の吸収ヒートポンプ１の作用の説明を補足する。図２のデューリング線図は、縦軸に冷媒Ｖ（本実施の形態では水）の露点温度を、横軸に吸収液Ｓ（本実施の形態ではＬｉＢｒ水溶液）の温度をとっている。右上がりの線は吸収液Ｓの等濃度線を表し、右に行くほど高濃度、左に行くほど低濃度となり、図中の原点を通る右上がりの線は溶液濃度０％（すなわち冷媒のみ）の線である。なお、縦軸が示す露点温度は飽和圧力と対応関係にあるため、冷媒蒸気Ｖｒ、Ｖｓ、Ｖｇが飽和蒸気である本実施の形態のヒートポンプサイクルでは、縦軸は主要構成部材１０、２０、３０、４０、５０、６０、７０の内部圧力を表していると見ることもできる。   The explanation of the operation of the absorption heat pump 1 in the above-described state will be supplemented also with reference to the Duhring diagram of FIG. In the Dueling diagram of FIG. 2, the vertical axis represents the dew point temperature of the refrigerant V (water in the present embodiment), and the horizontal axis represents the temperature of the absorbing liquid S (LiBr aqueous solution in the present embodiment). The line rising to the right represents the isoconcentration line of the absorbent S, and the concentration increases toward the right and decreases toward the left. The line rising toward the right passing through the origin in the figure has a solution concentration of 0% (that is, only the refrigerant). It is a line. Since the dew point temperature indicated by the vertical axis has a corresponding relationship with the saturation pressure, in the heat pump cycle of the present embodiment in which the refrigerant vapors Vr, Vs, and Vg are saturated vapors, the vertical axis indicates the main constituent members 10, 20, 30. , 40, 50, 60, 70 can be viewed as representing the internal pressure.

図２中、吸収ヒートポンプ１の定格運転における吸収液Ｓの状態は、高温吸収器１０及び高温再生器５０の系統が高温溶液線ＳＨＤで、低温吸収器３０及び低温再生器６０の系統が低温溶液線ＳＬＤで表され、定格運転における冷媒Ｖの状態は冷媒線ＶＤで表されている。図２中、状態Ｐ１２、Ｐ１３、Ｐ５２、Ｐ５３は、それぞれ高温濃溶液散布ノズル１２、貯留部１３、中間濃溶液散布ノズル５２、高温再生器５０の下部における吸収液Ｓの状態を表しており、状態Ｐ３２、Ｐ３３、Ｐ６２、Ｐ６３は、それぞれ低温濃溶液散布ノズル３２、貯留部３３、低混希溶液散布ノズル６２、貯留部６３、における吸収液Ｓの状態を表している。状態Ｐ１２〜Ｐ１３、状態Ｐ３２〜Ｐ３３、状態Ｐ６２〜Ｐ６３、Ｐ５２〜Ｐ５３が水平方向に伸びているのは、等圧下で吸収液Ｓの濃度が変化していることを表している。また、状態Ｐ２０は高温蒸発器２０の状態を、状態Ｐ４０は低温蒸発器４０の状態を、状態Ｐ７０は凝縮器７０の状態をそれぞれ表している。図２から明らかなように、本実施の形態では、高温吸収器１０と高温蒸発器２０、低温吸収器３０と低温蒸発器４０、高温再生器５０及び低温再生器６０と凝縮器７０の圧力が、それぞれ等しくなっている。なお、冷媒Ｖの蒸気を移動させるために互いに連通している高温吸収器１０と高温蒸発器２０、低温吸収器３０と低温蒸発器４０、高温再生器５０及び低温再生器６０と凝縮器７０の内部圧力は、厳密に言えば冷媒Ｖの蒸気の下流側となる方が冷媒Ｖの蒸気の流動による圧力損失分だけ低くなるが、ほぼ同じ圧力である。   In FIG. 2, the state of the absorbent S in the rated operation of the absorption heat pump 1 is that the system of the high temperature absorber 10 and the high temperature regenerator 50 is the high temperature solution line SHD, and the system of the low temperature absorber 30 and the low temperature regenerator 60 is the low temperature solution. It is represented by a line SLD, and the state of the refrigerant V in the rated operation is represented by a refrigerant line VD. In FIG. 2, states P12, P13, P52, and P53 represent the states of the absorbing liquid S at the lower part of the high temperature concentrated solution spray nozzle 12, the storage unit 13, the intermediate concentrated solution spray nozzle 52, and the high temperature regenerator 50, respectively. The states P32, P33, P62, and P63 represent the states of the absorbing liquid S in the low-temperature concentrated solution spray nozzle 32, the storage unit 33, the low-mixed dilute solution spray nozzle 62, and the storage unit 63, respectively. The states P12 to P13, states P32 to P33, states P62 to P63, and P52 to P53 extending in the horizontal direction indicate that the concentration of the absorbing liquid S changes under the same pressure. Further, the state P20 represents the state of the high temperature evaporator 20, the state P40 represents the state of the low temperature evaporator 40, and the state P70 represents the state of the condenser 70. As apparent from FIG. 2, in this embodiment, the pressures of the high temperature absorber 10 and the high temperature evaporator 20, the low temperature absorber 30 and the low temperature evaporator 40, the high temperature regenerator 50, the low temperature regenerator 60 and the condenser 70 are as follows. Are equal. Note that the high-temperature absorber 10 and the high-temperature evaporator 20, the low-temperature absorber 30 and the low-temperature evaporator 40, the high-temperature regenerator 50, the low-temperature regenerator 60, and the condenser 70 that are in communication with each other to move the vapor of the refrigerant V. Strictly speaking, the internal pressure is lower on the downstream side of the vapor of the refrigerant V by a pressure loss due to the flow of the vapor of the refrigerant V, but is almost the same pressure.

低温吸収器３０及び低温再生器６０の系統は、吸収液Ｓが、低温溶液線ＳＬＤ上を反時計回りに循環する。状態Ｐ６２〜Ｐ６３に示すように、低温再生器６０では、排温水ｈから排熱を受けて吸収液Ｓの温度が上昇すると共に濃度が上昇し、低温希溶液Ｓｖが低温濃溶液Ｓｂとなる。低温再生器６０において吸収液Ｓの濃度の上昇に伴い発生した冷媒Ｖの蒸気は、高温再生器５０で発生した冷媒Ｖの蒸気と共に再生器冷媒蒸気Ｖｇとして凝縮器７０に流入して冷却される（状態Ｐ７０）。状態Ｐ４０にある低温蒸発器４０の冷媒Ｖは、排温水ｈから排熱を受けて低温冷媒蒸気Ｖｓとなり、これを低温吸収器３０の低温濃溶液Ｓｂに吸収させて、状態Ｐ３２〜Ｐ３３に示すように低温濃溶液Ｓｂの濃度を低下させる。状態Ｐ３２〜Ｐ３３における低温濃溶液Ｓｂが低温冷媒蒸気Ｖｓを吸収して発生する吸収熱Ｈ２０は、状態Ｐ２０にある高温蒸発器２０の冷媒Ｖを加熱して、これを高温冷媒蒸気Ｖｒとする。そして、吸収熱Ｈ２０によって発生した高温冷媒蒸気Ｖｒを高温吸収器１０の高温濃溶液Ｓａに吸収させて、状態Ｐ１２〜Ｐ１３に示すように高温濃溶液Ｓａの濃度を低下させる。   In the system of the low-temperature absorber 30 and the low-temperature regenerator 60, the absorbing liquid S circulates counterclockwise on the low-temperature solution line SLD. As shown in states P62 to P63, in the low-temperature regenerator 60, the temperature of the absorbing liquid S rises as it receives exhaust heat from the exhausted hot water h, and the concentration increases, and the low-temperature dilute solution Sv becomes the low-temperature concentrated solution Sb. The refrigerant V generated in the low temperature regenerator 60 with the increase in the concentration of the absorbent S flows into the condenser 70 as the regenerator refrigerant vapor Vg together with the refrigerant V generated in the high temperature regenerator 50 and is cooled. (State P70). The refrigerant V of the low-temperature evaporator 40 in the state P40 receives the exhaust heat from the exhaust hot water h to become the low-temperature refrigerant vapor Vs, which is absorbed by the low-temperature concentrated solution Sb of the low-temperature absorber 30 and shown in the states P32 to P33. As such, the concentration of the low temperature concentrated solution Sb is lowered. Absorption heat H20 generated by the low-temperature concentrated solution Sb absorbing the low-temperature refrigerant vapor Vs in the states P32 to P33 heats the refrigerant V of the high-temperature evaporator 20 in the state P20, and makes this the high-temperature refrigerant vapor Vr. Then, the high-temperature refrigerant vapor Vr generated by the absorption heat H20 is absorbed by the high-temperature concentrated solution Sa of the high-temperature absorber 10 to reduce the concentration of the high-temperature concentrated solution Sa as shown in the states P12 to P13.

高温吸収器１０及び高温再生器５０の系統は、吸収液Ｓが、高温溶液線ＳＨＤ上を反時計回りに循環する。状態Ｐ１２〜Ｐ１３における高温濃溶液Ｓａが高温冷媒蒸気Ｖｒを吸収して発生する吸収熱Ｈｗは、被加熱媒体Ｗを加熱する。これにより、被加熱媒体Ｗを、状態Ｐ１３における吸収液Ｓの温度付近まで温度上昇させることが可能となる。この、被加熱媒体Ｗの温度が上昇する過程で、加熱されている被加熱媒体液Ｗｑの圧力における沸点を超えると、被加熱媒体蒸気Ｗｖの生成が可能となる。高温溶液線ＳＨＤの下部に相当する高温再生器５０では、状態Ｐ５２〜Ｐ５３に示すように、高温冷媒蒸気Ｖｒの保有熱Ｈ５０を受けて吸収液Ｓの温度が上昇すると共に濃度が上昇し、高温希溶液Ｓｗが高温濃溶液Ｓａとなる。図２中、高温冷媒蒸気Ｖｒの保有熱Ｈ５０の移動を示す線図の傾きが大きく、温度変化が小さいように見えるが、高温冷媒蒸気Ｖｒは状態Ｐ５２〜Ｐ５３において吸収液Ｓを加熱する際に気相から液相に状態変化をしており、すなわち潜熱を高温再生器５０の吸収液Ｓに与えている。したがって、高温再生器５０の吸収液Ｓに与えられる保有熱Ｈ５０は、温度変化に伴う顕熱を与える場合に比べて極めて大きな熱量となり、効果的に高温希溶液Ｓｗを高温濃溶液Ｓａに再生することができる。   In the system of the high temperature absorber 10 and the high temperature regenerator 50, the absorbing liquid S circulates counterclockwise on the high temperature solution line SHD. The absorption heat Hw generated by the high temperature concentrated solution Sa in the states P12 to P13 absorbing the high temperature refrigerant vapor Vr heats the medium W to be heated. Thereby, it becomes possible to raise the temperature of the to-be-heated medium W to the temperature vicinity of the absorption liquid S in the state P13. If the boiling point of the heated medium liquid Wq exceeds the boiling point in the process of increasing the temperature of the heated medium W, the heated medium vapor Wv can be generated. In the high-temperature regenerator 50 corresponding to the lower part of the high-temperature solution line SHD, as shown in the states P52 to P53, the temperature of the absorbing liquid S increases and the concentration increases due to the retained heat H50 of the high-temperature refrigerant vapor Vr. The dilute solution Sw becomes the high temperature concentrated solution Sa. In FIG. 2, the slope of the diagram showing the movement of the retained heat H50 of the high-temperature refrigerant vapor Vr is large and the temperature change seems to be small. However, the high-temperature refrigerant vapor Vr is heated when the absorbing liquid S is heated in the states P52 to P53. The state is changed from the gas phase to the liquid phase, that is, latent heat is given to the absorbing liquid S of the high temperature regenerator 50. Therefore, the retained heat H50 given to the absorbing liquid S of the high-temperature regenerator 50 becomes an extremely large amount of heat compared to the case where sensible heat accompanying temperature change is given, and the high-temperature dilute solution Sw is effectively regenerated into the high-temperature concentrated solution Sa. be able to.

図３に、参考例に係る三段昇温型吸収ヒートポンプのデューリング線図を示す。（ａ）は吸収液をシリーズフローとしたもの、（ｂ）は吸収液をパラレルフローとしたものである。図３（ａ）に示すものは、吸収器と蒸発器との組み合わせを三段設けたものであり、低温吸収器ＡＬにおける吸収熱を中温蒸発器ＥＭの冷媒を蒸発させるために用い、中温吸収器ＡＭにおける吸収熱を高温蒸発器ＥＨの冷媒を蒸発させるために用いており、高温吸収器ＡＨは高温蒸発器ＥＨと同圧に、低温蒸発器ＥＬは低温吸収器ＡＬと同圧に、凝縮器Ｃと再生器Ｇとが同圧になっている。これは、圧力方向に三段昇圧したもので、理論ＣＯＰは０．２５０である。他方、図３（ｂ）に示すものは、吸収器と再生器との組み合わせを三段設けたものであり、低温吸収器ＡＬにおける吸収熱を中温再生器ＧＭの吸収液を再生させるために用い、中温吸収器ＡＭにおける吸収熱を高温再生器ＧＨの吸収液を再生させるために用いており、高温吸収器ＡＨ及び蒸発器Ｅは低温吸収器ＡＬ及び中温吸収器ＡＭと同圧に、低温再生器ＧＬ及び凝縮器Ｃは高温再生器ＧＨ及び中温再生器ＧＭと同圧になっている。これは、温度方向に三段昇温したもので、理論ＣＯＰは０．２５０である。   FIG. 3 shows a Duhring diagram of a three-stage temperature rising type absorption heat pump according to a reference example. (A) is a series flow of the absorbent, and (b) is a parallel flow of the absorbent. In FIG. 3A, the combination of the absorber and the evaporator is provided in three stages. The absorption heat in the low temperature absorber AL is used to evaporate the refrigerant of the intermediate temperature evaporator EM, and the intermediate temperature absorption is performed. The absorption heat in the evaporator AM is used to evaporate the refrigerant in the high temperature evaporator EH. The high temperature absorber AH is condensed to the same pressure as the high temperature evaporator EH, and the low temperature evaporator EL is condensed to the same pressure as the low temperature absorber AL. The vessel C and the regenerator G are at the same pressure. This is a three-step pressure increase in the pressure direction, and the theoretical COP is 0.250. On the other hand, what is shown in FIG. 3B is a three-stage combination of an absorber and a regenerator, and is used to regenerate the absorption heat of the intermediate temperature regenerator GM using the absorption heat in the low temperature absorber AL. The heat absorbed in the intermediate temperature absorber AM is used to regenerate the absorption liquid of the high temperature regenerator GH. The high temperature absorber AH and the evaporator E are at the same pressure as the low temperature absorber AL and the intermediate temperature absorber AM, and the low temperature regeneration. The condenser GL and the condenser C are at the same pressure as the high temperature regenerator GH and the medium temperature regenerator GM. This is a three-stage temperature rise in the temperature direction, and the theoretical COP is 0.250.

本実施の形態に係る吸収ヒートポンプ１のデューリング線図（図２参照）を見ると、２つのサイクルを示す高温溶液線ＳＨＤ及び低温溶液線ＳＬＤは、低圧側は等しいものの、高温溶液線ＳＨＤでは、低温溶液線ＳＬＤよりも最高圧力が高い。このように構成されていることで、導入される排温水ｈから被加熱媒体蒸気Ｗｖを生成する昇温幅を大きくすることができる。そして、本実施の形態に係る吸収ヒートポンプ１を、参考例に係る三段昇温型吸収ヒートポンプと、デューリング線図において比較してみると、図３（ａ）に示すものに対して最高圧力が低くなっており、図３（ｂ）に示すものに対して吸収液Ｓの最高濃度が低くなっている。本実施の形態に係る吸収ヒートポンプ１は、温度方向に二段昇温したうえで圧力方向に二段昇圧したものといえ、理論ＣＯＰは０．２５０である。本実施の形態に係る吸収ヒートポンプ１は、図３（ａ）に示す三段昇温型吸収ヒートポンプに対して、最高圧力が低いので内圧の上昇を抑制することができて缶胴の強度の観点からの条件が緩和されると共に、吸収液Ｓ及び冷媒Ｖの循環のためのポンプの必要ヘッドを抑制することができることに伴い動力の増加を防ぐことができ、また、図３（ｂ）に示す三段昇温型吸収ヒートポンプに対して、最高濃度が低いので吸収液Ｓの濃度の過度の上昇を抑制することができて吸収液Ｓの結晶を回避した安定的な運転が可能となる。   Looking at the dueling diagram (see FIG. 2) of the absorption heat pump 1 according to the present embodiment, the high temperature solution line SHD and the low temperature solution line SLD showing two cycles are equal on the low pressure side, but in the high temperature solution line SHD, The maximum pressure is higher than that of the low temperature solution line SLD. By being comprised in this way, the temperature increase range which produces | generates the to-be-heated medium vapor | steam Wv from the exhausted hot water h introduce | transduced can be enlarged. Then, when the absorption heat pump 1 according to the present embodiment is compared with the three-stage temperature rising absorption heat pump according to the reference example in the Duering diagram, the maximum pressure with respect to that shown in FIG. Is lower, and the maximum concentration of the absorbing liquid S is lower than that shown in FIG. It can be said that the absorption heat pump 1 according to the present embodiment has a two-step temperature increase in the temperature direction and a two-step pressure increase in the pressure direction, and the theoretical COP is 0.250. The absorption heat pump 1 according to the present embodiment has a lower maximum pressure than the three-stage temperature increase type absorption heat pump shown in FIG. 3 is relaxed, and it is possible to prevent an increase in power due to the suppression of the necessary head of the pump for circulating the absorbing liquid S and the refrigerant V, as shown in FIG. Since the maximum concentration is low with respect to the three-stage temperature rising type absorption heat pump, an excessive increase in the concentration of the absorbing solution S can be suppressed, and a stable operation that avoids the crystals of the absorbing solution S is possible.

上述のように、本実施の形態に係る吸収ヒートポンプ１は、参考例に係る三段昇温型吸収ヒートポンプ（図３参照）と比較して、最高内圧及び最高濃度が抑制されるので、安定した運転を可能にしつつ、導入される排温水ｈから被加熱媒体蒸気Ｗｖを生成する昇温幅を図３に示す参考例と同等にすることができる。しかしながら、これまで説明した状態の吸収ヒートポンプ１の理論ＣＯＰは、図３に示す参考例と同じである。そこで、本実施の形態に係る吸収ヒートポンプ１は、排温水ｈの温度や冷却水ｃの温度等の、変化する運転条件に応じた適切なＣＯＰで運転するべく、次のような制御を行う。すなわち、制御装置９９は、高温希溶液濃度検出器９５で検出された値（以下「検出値Ｎ９５」ともいう。）及び低温濃溶液濃度検出器９６で検出された値（以下「検出値Ｎ９６」ともいう。）を比較して、検出値Ｎ９５が検出値Ｎ９６以上のときは、上述のように、高温希溶液管１６を流れる高温希溶液Ｓｗの全部が高温再生器５０へ流入するように、切替弁１８を設定する。他方、検出値Ｎ９５が検出値Ｎ９６よりも小さいときは、高温希溶液管１６を流れる高温希溶液Ｓｗが分岐管１７及び低混希溶液管３７を介して低温再生器６０へ流入するように切替弁１８を設定すると共に、開閉弁５７ｖを開にする。   As described above, the absorption heat pump 1 according to the present embodiment is stable because the maximum internal pressure and the maximum concentration are suppressed as compared with the three-stage temperature rising absorption heat pump according to the reference example (see FIG. 3). While enabling operation, the temperature rise width for generating the heated medium vapor Wv from the introduced waste water h can be made equal to the reference example shown in FIG. However, the theoretical COP of the absorption heat pump 1 in the state described so far is the same as the reference example shown in FIG. Therefore, the absorption heat pump 1 according to the present embodiment performs the following control in order to operate with an appropriate COP according to changing operating conditions such as the temperature of the exhaust water h and the temperature of the cooling water c. That is, the control device 99 detects a value detected by the high temperature diluted solution concentration detector 95 (hereinafter also referred to as “detected value N95”) and a value detected by the low temperature concentrated solution concentration detector 96 (hereinafter “detected value N96”). When the detection value N95 is equal to or higher than the detection value N96, the high-temperature dilute solution Sw flowing through the high-temperature dilute solution pipe 16 flows into the high-temperature regenerator 50 as described above. The switching valve 18 is set. On the other hand, when the detection value N95 is smaller than the detection value N96, the high-temperature dilute solution Sw flowing through the high-temperature dilute solution pipe 16 is switched to flow into the low-temperature regenerator 60 via the branch pipe 17 and the low-mixed dilute solution pipe 37. The valve 18 is set and the on-off valve 57v is opened.

このようにすることで、運転条件によって高温溶液線ＳＨＤと低温溶液線ＳＬＤとに重なる部分が生じるときに、低温再生器６０に投入される排温水ｈの排熱によって高温希溶液Ｓｗの一部又は全部の加熱濃縮を行うことで、高温冷媒蒸気Ｖｒの熱（低温吸収器３０で発生した吸収熱）の利用を抑制して、ＣＯＰの向上を図ることができる。特に、凝縮器７０に導入される冷却水ｃの温度が低下した状態では、高温再生器５０から導出される吸収液Ｓの濃度が上昇しやすく過濃縮による結晶のおそれが生じ得る。過濃縮を抑制するためには、高温再生器５０における加熱能力を制限するとよく、例えば熱源流量調節弁５１ｖで冷媒蒸気熱源管５１を流れる高温冷媒蒸気Ｖｒの流量を制限することで過濃縮を防ぐことができる。このとき、高温冷媒蒸気Ｖｒの使用量が減るので、低温吸収器３０における加熱管３１内での蒸気発生量を減らしてもよい。例えば、流量調節弁３５ｖを調節してバイパス管３５を流れる低温濃溶液Ｓｂの流量を多くすると、低温吸収器３０内における吸収熱の発生が抑制され、加熱管３１内で発生する高温冷媒蒸気Ｖｒの量が減少し、低温吸収器３０から導出される低温希溶液Ｓｖの濃度はバイパスさせないときよりも上昇して、低温溶液線ＳＬＤが高温溶液線ＳＨＤに重なりやすくなる。つまり、流量調節弁３５ｖを用いることで低温溶液線ＳＬＤと高温溶液線ＳＨＤとの重なりが早く生じ、ＣＯＰの改善を図ることができる。   In this way, when a portion overlapping the high-temperature solution line SHD and the low-temperature solution line SLD occurs depending on the operating conditions, a part of the high-temperature dilute solution Sw is discharged by the exhaust heat of the exhaust water h that is input to the low-temperature regenerator 60. Alternatively, by performing all the heating and concentration, the utilization of the heat of the high-temperature refrigerant vapor Vr (absorption heat generated in the low-temperature absorber 30) can be suppressed, and the COP can be improved. In particular, in a state where the temperature of the cooling water c introduced into the condenser 70 is lowered, the concentration of the absorbing liquid S led out from the high-temperature regenerator 50 is likely to increase, and there is a risk of crystals due to overconcentration. In order to suppress overconcentration, the heating capacity in the high-temperature regenerator 50 may be limited. For example, by limiting the flow rate of the high-temperature refrigerant vapor Vr flowing through the refrigerant vapor heat source pipe 51 with the heat source flow rate adjustment valve 51v, overconcentration is prevented. be able to. At this time, since the amount of use of the high-temperature refrigerant vapor Vr is reduced, the amount of vapor generated in the heating pipe 31 in the low-temperature absorber 30 may be reduced. For example, when the flow rate of the low-temperature concentrated solution Sb flowing through the bypass pipe 35 is increased by adjusting the flow rate control valve 35v, the generation of absorbed heat in the low-temperature absorber 30 is suppressed, and the high-temperature refrigerant vapor Vr generated in the heating pipe 31 is suppressed. And the concentration of the low-temperature dilute solution Sv derived from the low-temperature absorber 30 is higher than when the bypass is not bypassed, and the low-temperature solution line SLD is likely to overlap the high-temperature solution line SHD. That is, by using the flow rate control valve 35v, the low temperature solution line SLD and the high temperature solution line SHD are quickly overlapped, and the COP can be improved.

ここで図１を参照して、高温希溶液Ｓｗを低温再生器６０へ流入させた状態における吸収ヒートポンプ１の作用について、高温希溶液Ｓｗを高温再生器５０へ流入させた状態との相違点を説明する。高温吸収器１０の貯留部１３内の高温希溶液Ｓｗは、重力及び内圧の差により低温再生器６０に向かって高温希溶液管１６を流れ、高温溶液熱交換器５８で高温濃溶液Ｓａと熱交換して温度が低下した後に、低混希溶液管３７に流入する。低混希溶液管３７に流入した高温希溶液Ｓｗは、低混希溶液管３７に流入した低温希溶液Ｓｖと混合して混合希溶液Ｓｘとなり、低温再生器６０に送られる。低温再生器６０に送られた混合希溶液Ｓｘは、低混希溶液散布ノズル６２から散布される。低混希溶液散布ノズル６２から散布された混合希溶液Ｓｘは、熱源管６１を流れる排温水ｈ（本実施の形態では約８０℃前後）によって加熱され、散布された混合希溶液Ｓｘ中の冷媒Ｖの一部が蒸発し濃度が上昇して低温濃溶液Ｓｂとなり、まず低温再生器６０の落下貯留部６３ａに貯留され、落下貯留部６３ａの液位が上昇して堰６３ｓを越えた分が越流貯留部６３ｂに貯留される。   Here, referring to FIG. 1, the difference between the action of the absorption heat pump 1 in the state where the high temperature dilute solution Sw is flowed into the low temperature regenerator 60 and the state where the high temperature dilute solution Sw is flowed into the high temperature regenerator 50 will be described. explain. The high-temperature dilute solution Sw in the reservoir 13 of the high-temperature absorber 10 flows through the high-temperature dilute solution tube 16 toward the low-temperature regenerator 60 due to the difference between gravity and internal pressure, and the high-temperature solution heat exchanger 58 and the high-temperature concentrated solution Sa are heated. After the exchange and the temperature is lowered, it flows into the low dilute solution tube 37. The high-temperature dilute solution Sw that has flowed into the low-mixed dilute solution tube 37 is mixed with the low-temperature dilute solution Sv that has flowed into the low-mixed dilute solution tube 37 to form a mixed dilute solution Sx, which is sent to the low-temperature regenerator 60. The mixed dilute solution Sx sent to the low temperature regenerator 60 is sprayed from the low dilute solution spray nozzle 62. The mixed dilute solution Sx sprayed from the low dilute solution spray nozzle 62 is heated by the exhaust hot water h (about 80 ° C. in the present embodiment) flowing through the heat source pipe 61, and the refrigerant in the sprayed mixed dilute solution Sx. A part of V evaporates and the concentration rises to become a low-temperature concentrated solution Sb, which is first stored in the drop reservoir 63a of the low-temperature regenerator 60, and the liquid level in the drop reservoir 63a rises and exceeds the weir 63s. It is stored in the overflow storage part 63b.

低温再生器６０の落下貯留部６３ａに貯留された低温濃溶液Ｓｂは、高温希溶液Ｓｗを高温再生器５０へ流入させた状態のときと同様に、低温溶液ポンプ６６で低温濃溶液管３８を介して低温吸収器３０の低温濃溶液散布ノズル３２に圧送される。他方、越流貯留部６３ｂに貯留された低温濃溶液Ｓｂは、中間濃溶液管５７を介して高温希溶液管１６に流入した後に高温再生器５０に導入されて、中間濃溶液散布ノズル５２から散布される。中間濃溶液散布ノズル５２から散布された低温濃溶液Ｓｂは、冷媒蒸気熱源管５１内を流れる高温冷媒蒸気Ｖｒによって加熱濃縮されて、冷媒Ｖの一部が蒸発して濃度が上昇し、高温濃溶液Ｓａとなって、高温再生器５０の下部に貯留され、高温溶液ポンプ５６によって高温濃溶液散布ノズル１２に圧送される。   The low temperature concentrated solution Sb stored in the drop storage unit 63a of the low temperature regenerator 60 is supplied to the low temperature concentrated solution tube 38 by the low temperature solution pump 66 in the same manner as when the high temperature dilute solution Sw is introduced into the high temperature regenerator 50. To the low-temperature concentrated solution spray nozzle 32 of the low-temperature absorber 30. On the other hand, the low-temperature concentrated solution Sb stored in the overflow storage section 63 b flows into the high-temperature dilute solution pipe 16 via the intermediate concentrated solution pipe 57 and is then introduced into the high-temperature regenerator 50, from the intermediate concentrated solution spray nozzle 52. Be sprayed. The low-temperature concentrated solution Sb sprayed from the intermediate concentrated solution spray nozzle 52 is heated and concentrated by the high-temperature refrigerant vapor Vr flowing in the refrigerant vapor heat source pipe 51, and a part of the refrigerant V evaporates to increase the concentration. The solution Sa is stored in the lower portion of the high temperature regenerator 50 and is pumped to the high temperature concentrated solution spray nozzle 12 by the high temperature solution pump 56.

図４は、高温希溶液Ｓｗを低温再生器６０へ流入させた状態の吸収ヒートポンプ１のデューリング線図であり、上述した吸収液Ｓのサイクルを（ａ）に示している。図４（ａ）に示すように、検出値Ｎ９５が検出値Ｎ９６よりも小さいときは、高温溶液線ＳＨＤと低温溶液線ＳＬＤとに重なる部分が生じている。このときも、吸収液Ｓは、高温溶液線ＳＨＤ及び低温溶液線ＳＬＤを反時計回りに循環する。低温吸収器３０の貯留部３３に貯留された状態Ｐ３３の低温希溶液Ｓｖは分岐管１７に向かって流れ、高温吸収器１０の貯留部１３に貯留された状態Ｐ１３の高温希溶液Ｓｗは低混希溶液管３７に向かって流れる。低混希溶液管３７内に流入した低温希溶液Ｓｖ及び高温希溶液Ｓｗは混合されて混合希溶液Ｓｘとなる。このときの混合希溶液Ｓｘ状態は、図４（ａ）のデューリング線図上における状態Ｐ１７Ｌと状態Ｐ１７Ｈとの間の混合割合に応じた状態となる。   FIG. 4 is a Duhring diagram of the absorption heat pump 1 in a state where the high-temperature dilute solution Sw is flowed into the low-temperature regenerator 60, and the cycle of the absorption liquid S described above is shown in (a). As shown in FIG. 4A, when the detection value N95 is smaller than the detection value N96, a portion overlapping the high temperature solution line SHD and the low temperature solution line SLD occurs. Also at this time, the absorbing liquid S circulates through the high temperature solution line SHD and the low temperature solution line SLD counterclockwise. The low-temperature dilute solution Sv in the state P33 stored in the storage unit 33 of the low-temperature absorber 30 flows toward the branch pipe 17, and the high-temperature dilute solution Sw in the state P13 stored in the storage unit 13 of the high-temperature absorber 10 is low mixed. It flows toward the dilute solution tube 37. The low temperature dilute solution Sv and the high temperature dilute solution Sw flowing into the low dilute solution tube 37 are mixed to form a mixed dilute solution Sx. The mixed dilute solution Sx state at this time becomes a state corresponding to the mixing ratio between the state P17L and the state P17H on the Dueling diagram of FIG.

低混希溶液管３７から低温再生器６０に流入した混合希溶液Ｓｘは、排温水ｈから排熱を受けて吸収液Ｓの温度が上昇すると共に濃度が上昇し、状態Ｐ６３に示すような低温濃溶液Ｓｂとなる。低温再生器６０で生成された低温濃溶液Ｓｂのうち、落下貯留部６３ａのものは状態Ｐ６３〜Ｐ３２に示すように低温吸収器３０に圧送されて低温冷媒蒸気Ｖｓを吸収して吸収熱を発生させるのに用いられ、越流貯留部６３ｂのものは高温再生器５０に流入されて状態Ｐ６３〜Ｐ５３に示すように高温冷媒蒸気Ｖｒの保有熱Ｈ５０を受けて吸収液Ｓの温度が上昇すると共に濃度が上昇して高温濃溶液Ｓａとなる。このように、高温希溶液Ｓｗを一旦低温再生器６０に流入させて排温水ｈの排熱で一部を加熱濃縮させるので、排熱を最大限利用することにより高温冷媒蒸気Ｖｒの保有熱Ｈ５０の利用分を小さくすることができ、ＣＯＰを向上させることができる。   The mixed dilute solution Sx flowing into the low temperature regenerator 60 from the low dilute solution tube 37 receives the exhaust heat from the exhaust hot water h, the temperature of the absorbing solution S rises and the concentration rises, and the low temperature as shown in the state P63. It becomes the concentrated solution Sb. Of the low-temperature concentrated solution Sb generated by the low-temperature regenerator 60, the drop storage part 63a is pumped to the low-temperature absorber 30 as shown in states P63 to P32 to absorb the low-temperature refrigerant vapor Vs and generate absorbed heat. As shown in states P63 to P53, the overflow reservoir 63b in the overflow reservoir 63b receives the retained heat H50 of the high-temperature refrigerant vapor Vr and rises in the temperature of the absorbent S. The concentration increases to become a hot concentrated solution Sa. In this way, the high-temperature dilute solution Sw once flows into the low-temperature regenerator 60 and is partially heated and concentrated by the exhaust heat of the exhaust hot water h. Therefore, the retained heat H50 of the high-temperature refrigerant vapor Vr can be obtained by making maximum use of the exhaust heat. Can be reduced and COP can be improved.

図４（ｂ）に示すデューリング線図は、上述した高温希溶液Ｓｗを低温再生器６０へ流入させた状態と同様の吸収液Ｓのサイクルにおいて、熱源流量調節弁５１ｖを閉じて高温再生器５０に熱を投入していない状態のものである。この場合、低温再生器６０の落下貯留部６３ａから低温吸収器３０へ圧送される吸収液Ｓ（状態Ｐ６３、５３〜Ｐ３２）と、高温再生器５０の下部から高温吸収器１０へ圧送される吸収液Ｓ（状態Ｐ６３、５３〜Ｐ１２）とは、同じ濃度となる。この図４（ｂ）に示す吸収液Ｓのサイクルの場合は二段昇温サイクルとなり、このときの理論ＣＯＰは０．３３３である。他方、図４（ａ）に示す吸収液Ｓのサイクルの場合は二〜三段昇温サイクルとなり、このときの理論ＣＯＰは０．２５０を超え、０．３３３未満となる。このように、本実施の形態に係る吸収ヒートポンプ１は、切替弁１８によって高温希溶液Ｓｗの導入先を高温再生器５０と低温再生器６０とで切り替えると共に、熱源流量調節弁５１ｖによって高温再生器５０への投入熱量を調節することにより、運転条件に応じた最適なＣＯＰで運転することが可能となる。   The Duhring diagram shown in FIG. 4B is a high temperature regenerator in which the heat source flow rate adjustment valve 51v is closed in the same cycle of the absorbing liquid S as in the state where the high temperature dilute solution Sw is introduced into the low temperature regenerator 60. 50 is a state in which no heat is applied. In this case, the absorption liquid S (states P63, 53 to P32) pumped from the drop reservoir 63a of the low temperature regenerator 60 to the low temperature absorber 30 and the absorption pumped from the lower part of the high temperature regenerator 50 to the high temperature absorber 10. The liquid S (states P63, 53 to P12) has the same concentration. In the case of the cycle of the absorbing liquid S shown in FIG. 4B, a two-stage temperature increase cycle is obtained, and the theoretical COP at this time is 0.333. On the other hand, in the case of the cycle of the absorbing liquid S shown in FIG. 4 (a), it becomes a two- to three-stage heating cycle, and the theoretical COP at this time exceeds 0.250 and is less than 0.333. As described above, the absorption heat pump 1 according to the present embodiment switches the introduction destination of the high-temperature dilute solution Sw between the high-temperature regenerator 50 and the low-temperature regenerator 60 by the switching valve 18 and at the high-temperature regenerator by the heat source flow rate adjustment valve 51v. By adjusting the amount of heat input to 50, it is possible to operate with the optimum COP according to the operating conditions.

以上の説明では、分岐管１７が低混希溶液管３７に接続されていて、高温希溶液Ｓｗが低温再生器６０に導入される際に低温希溶液Ｓｖと混合されることとしたが、分岐管１７が低温希溶液Ｓｖの系統とは別に独立して低温再生器６０まで配設され、低温再生器６０内で低温希溶液Ｓｖを散布するノズルとは別の高温希溶液Ｓｗを散布するノズルに接続されるように構成され、つまり、高温希溶液Ｓｗを直接的に低温再生器６０へ導くこととしてもよい。   In the above description, the branch pipe 17 is connected to the low-mix dilute solution pipe 37, and when the high-temperature dilute solution Sw is introduced into the low-temperature regenerator 60, it is mixed with the low-temperature dilute solution Sv. The nozzle 17 is provided up to the low temperature regenerator 60 independently of the system of the low temperature dilute solution Sv and sprays the high temperature dilute solution Sw different from the nozzle that sprays the low temperature dilute solution Sv in the low temperature regenerator 60. In other words, the high-temperature dilute solution Sw may be directly guided to the low-temperature regenerator 60.

以上の説明では、第１の希溶液濃度検出手段及び第２の吸収液濃度検出手段が、吸収液Ｓの濃度を直接検出する濃度計である高温希溶液濃度検出器９５及び低温濃溶液濃度検出器９６であるとしたが、吸収液Ｓの濃度に関連する物理量を検出して間接的に吸収液Ｓの濃度を検出することとしてもよい。間接的に検出する例として、吸収液Ｓの密度と温度とから濃度を算出する（温度の影響が小さい場合は密度だけで判断してもよい）、吸収液Ｓの温度と蒸気圧とから気液平衡状態と推定して濃度を算出する、吸収液Ｓの温度と露点とからデューリング線図に基づいて濃度を算出することが挙げられる。また、濃度に換算せずに沸点上昇の比較で行ってもよい。沸点上昇は吸収液Ｓの温度と露点との差であり、沸点上昇の大きい方が吸収液Ｓの濃度の濃い方として差し支えない。   In the above description, the first diluted solution concentration detecting means and the second absorbing solution concentration detecting means are a high temperature diluted solution concentration detector 95 and a low temperature concentrated solution concentration detection which are concentration meters that directly detect the concentration of the absorbing solution S. However, the concentration of the absorbing liquid S may be detected indirectly by detecting a physical quantity related to the concentration of the absorbing liquid S. As an indirect detection example, the concentration is calculated from the density and temperature of the absorbing liquid S (if the influence of temperature is small, it may be determined only by the density). The concentration is calculated based on the temperature and dew point of the absorbing liquid S, which is estimated as a liquid equilibrium state, and is calculated based on the Düring diagram. Moreover, you may carry out by the comparison of a boiling point rise, without converting into a density | concentration. The increase in boiling point is the difference between the temperature of the absorbing liquid S and the dew point, and the higher boiling point may be the higher concentration of the absorbing liquid S.

以上の説明では、高温再生器５０と低温再生器６０とが同じ缶胴内に収容されていて、缶胴の下部に高温再生器５０が、上部に低温再生器６０が配設されていることとしたが、上部に高温再生器５０が、下部に低温再生器６０が配設されていることとしてもよく、高温再生器５０と低温再生器６０とが横並びに配設されていることとしてもよい（このように構成する場合は、必要に応じて、低温再生器６０から高温再生器５０へ吸収液Ｓを搬送するポンプを設ける。）。また、高温再生器５０で蒸発した冷媒Ｖの蒸気と低温再生器６０で蒸発した冷媒Ｖの蒸気とが共通の凝縮器７０で凝縮されることとしたが、高温再生器５０で蒸発した冷媒Ｖの蒸気を凝縮させる凝縮器と、低温再生器６０で蒸発した冷媒Ｖの蒸気を凝縮させる凝縮器とを個別に設けてもよい。この場合は、高温再生器５０及び高温再生器５０用の凝縮器と、低温再生器６０及び低温再生器６０用の凝縮器との組み合わせで、それぞれ別の缶胴に収容される構成とするのが好ましい。   In the above description, the high temperature regenerator 50 and the low temperature regenerator 60 are accommodated in the same can body, and the high temperature regenerator 50 is disposed in the lower portion of the can body, and the low temperature regenerator 60 is disposed in the upper portion. However, the high temperature regenerator 50 may be disposed at the top and the low temperature regenerator 60 may be disposed at the bottom, and the high temperature regenerator 50 and the low temperature regenerator 60 may be disposed side by side. (In the case of such a configuration, a pump for transporting the absorbing liquid S from the low temperature regenerator 60 to the high temperature regenerator 50 is provided if necessary). Further, the vapor of the refrigerant V evaporated in the high temperature regenerator 50 and the vapor of the refrigerant V evaporated in the low temperature regenerator 60 are condensed in the common condenser 70, but the refrigerant V evaporated in the high temperature regenerator 50 is used. You may provide separately the condenser which condenses this vapor | steam, and the condenser which condenses the vapor | steam of the refrigerant | coolant V evaporated by the low temperature regenerator 60 separately. In this case, the high-temperature regenerator 50 and the condenser for the high-temperature regenerator 50 are combined with the condenser for the low-temperature regenerator 60 and the low-temperature regenerator 60 so that they are accommodated in different can bodies. Is preferred.

以上の説明では、高温再生器５０で発生した冷媒Ｖの蒸気を、特に他の流体と熱交換させずに凝縮器７０へ導くこととしたが、低温再生器６０の熱源管６１の周辺を通すことによって低温希溶液散布ノズル６２から散布された低温希溶液Ｓｖを加熱した後に凝縮器７０へ導くこととしてもよい。このようにすると、高温再生器５０で発生した高温の冷媒Ｖの蒸気が持つエネルギーを低温再生器６０で加熱濃縮される低温希溶液Ｓｖに与えることができ、低温再生器６０での外部熱源（排温水ｈ）の必要量を低減することができ、ＣＯＰの向上につながることとなる。   In the above description, the vapor of the refrigerant V generated in the high temperature regenerator 50 is guided to the condenser 70 without particularly exchanging heat with other fluids. However, it passes through the periphery of the heat source pipe 61 of the low temperature regenerator 60. Thus, the low-temperature dilute solution Sv sprayed from the low-temperature dilute solution spray nozzle 62 may be heated and then guided to the condenser 70. In this way, the energy of the vapor of the high-temperature refrigerant V generated in the high-temperature regenerator 50 can be given to the low-temperature dilute solution Sv heated and concentrated in the low-temperature regenerator 60, and the external heat source ( The required amount of the waste water h) can be reduced, leading to an improvement in COP.

以上の説明では、吸収熱搬送手段が、低温吸収器３０で発生した吸収熱を保有する高温冷媒蒸気Ｖｒを高温蒸発器２０から高温再生器５０へ導くことによって低温吸収器３０で発生した吸収熱を間接的に高温再生器５０内に搬送する冷媒蒸気熱源管５１であることとしたが、冷媒蒸気熱源管５１に代えて、以下のように構成してもよい。
図５は、本実施の形態の変形例に係る吸収ヒートポンプの模式的系統図であり、（ａ）は第１の変形例を、（ｂ）は第２の変形例を示している。図５（ａ）に示す第１の変形例では、低温吸収器３０と高温再生器５０との間で液体の熱媒体ｔを循環させるクローズド配管の循環熱媒体管２５１を設け、循環熱媒体管２５１に配設された循環熱媒体ポンプ２５９で熱媒体ｔを循環させることにより、低温吸収器３０で発生した吸収熱を直接的に高温再生器５０内に搬送することとしている。図５（ｂ）に示す第２の変形例では、冷媒蒸気熱源管５１に代えて、低温吸収器の役割を果たす加熱用吸収装置３５１を高温再生器５０内に設けている。ここで例示する加熱用吸収装置３５１は、複数の伝熱管が鉛直に延びるように配設され、複数の伝熱管の各上端が上部ヘッダーで、各下端が下部ヘッダーでそれぞれ接続され、上部ヘッダーに、配管３５７を介して低温蒸発器４０内の低温冷媒蒸気Ｖｓを、及び配管３５８を介して低温濃溶液管３８を流れる低温濃溶液Ｓｂを導入するように構成して、加熱用吸収装置３５１の内部に低温濃溶液Ｓｂ及び低温冷媒蒸気Ｖｓを導入し、加熱用吸収装置３５１の伝熱管内で低温濃溶液Ｓｂに低温冷媒蒸気Ｖｓを吸収させて吸収熱を発生させ、中間濃溶液散布ノズル５２から加熱用吸収装置の外部に散布された高温希溶液Ｓｗ又は低温濃溶液Ｓｂを加熱することとしている。加熱用吸収装置３５１の下部ヘッダーは、配管３５９を介して低温希溶液管３６に接続されており、加熱用吸収装置３５１で濃度が低下した吸収液Ｓを低温希溶液管３６に導入することができるように構成されている。 In the above description, the absorption heat generated in the low-temperature absorber 30 by the absorption heat transfer means guiding the high-temperature refrigerant vapor Vr having the absorption heat generated in the low-temperature absorber 30 from the high-temperature evaporator 20 to the high-temperature regenerator 50. However, the refrigerant vapor heat source pipe 51 may be configured as follows in place of the refrigerant vapor heat source pipe 51.
FIG. 5 is a schematic system diagram of an absorption heat pump according to a modification of the present embodiment, where (a) shows a first modification and (b) shows a second modification. In the first modification shown in FIG. 5 (a), a circulating heat medium pipe 251 of a closed pipe that circulates a liquid heat medium t between the low temperature absorber 30 and the high temperature regenerator 50 is provided. The heat generated by the low-temperature absorber 30 is directly conveyed into the high-temperature regenerator 50 by circulating the heat medium t with a circulating heat medium pump 259 disposed at 251. In the second modification shown in FIG. 5B, a heating absorber 351 that functions as a low-temperature absorber is provided in the high-temperature regenerator 50 instead of the refrigerant vapor heat source pipe 51. The heating absorption device 351 exemplified here is arranged so that a plurality of heat transfer tubes extend vertically, and each upper end of the plurality of heat transfer tubes is connected to the upper header and each lower end is connected to the lower header. The low-temperature refrigerant vapor Vs in the low-temperature evaporator 40 is introduced via the pipe 357, and the low-temperature concentrated solution Sb flowing through the low-temperature concentrated solution pipe 38 is introduced via the pipe 358. The low-temperature concentrated solution Sb and the low-temperature refrigerant vapor Vs are introduced therein, and the low-temperature concentrated solution Sb absorbs the low-temperature concentrated solution Sb in the heat transfer tube of the heating absorption device 351 to generate heat of absorption. The high-temperature dilute solution Sw or the low-temperature concentrated solution Sb sprayed to the outside of the heating absorber is heated. The lower header of the heating absorber 351 is connected to the low temperature dilute solution pipe 36 via a pipe 359, and the absorbing solution S whose concentration has been reduced by the heating absorber 351 can be introduced into the low temperature dilute solution pipe 36. It is configured to be able to.

１ 吸収ヒートポンプ
１０ 高温吸収器
１１ 加熱管
１７ 分岐管
１８ 切替弁
２０ 高温蒸発器
３０ 低温吸収器
３５ バイパス管
３５ｖ 流量調節弁
４０ 低温蒸発器
５０ 高温再生器
５１ 冷媒蒸気熱源管
５１ｖ 熱源流量調節弁
６０ 低温再生器
７０ 凝縮器
９５ 高温希溶液濃度検出器
９６ 低温濃溶液濃度検出器
９９ 制御装置
Ｓａ 高温濃溶液
Ｓｂ 低温濃溶液
Ｓｖ 低温希溶液
Ｓｗ 高温希溶液
Ｓｘ 混合希溶液
Ｖｆ 冷媒液
Ｖｇ 再生器冷媒蒸気
Ｖｒ 高温冷媒蒸気
Ｖｓ 低温冷媒蒸気
Ｗ 被加熱媒体

DESCRIPTION OF SYMBOLS 1 Absorption heat pump 10 High temperature absorber 11 Heating pipe 17 Branch pipe 18 Switching valve 20 High temperature evaporator 30 Low temperature absorber 35 Bypass pipe 35v Flow control valve 40 Low temperature evaporator 50 High temperature regenerator 51 Refrigerant vapor heat source pipe 51v Heat source flow control valve 60 Low temperature regenerator 70 Condenser 95 High temperature dilute solution concentration detector 96 Low temperature concentrated solution concentration detector 99 Control device Sa High temperature concentrated solution Sb Low temperature concentrated solution Sv Low temperature dilute solution Sw High temperature dilute solution Sx Mixed dilute solution Vf Refrigerant liquid Vg Regenerator refrigerant Steam Vr High-temperature refrigerant vapor Vs Low-temperature refrigerant vapor W Heated medium

Claims (4)

被加熱媒体の流路を内部に有し、第１の吸収液が第１の冷媒蒸気を吸収する際に発生する吸収熱で前記被加熱媒体を加熱する第１の吸収器と；
前記第１の吸収器に前記第１の冷媒蒸気を供給する蒸発器と；
第２の吸収液が第２の冷媒蒸気を吸収する際に発生する吸収熱で前記蒸発器内の冷媒液を加熱して前記第１の冷媒蒸気を生成する、前記第１の吸収器よりも作動温度が低い第２の吸収器と；
前記第１の吸収器で前記第１の吸収液が前記第１の冷媒蒸気を吸収して濃度が低下した第１の希溶液を導入し加熱して、前記第１の希溶液から冷媒を蒸発させて前記第１の吸収液を生成する高温再生器と；
前記第２の吸収器で前記第２の吸収液が前記第２の冷媒蒸気を吸収して濃度が低下した第２の希溶液を導入し加熱して、前記第２の希溶液から冷媒を蒸発させて前記第２の吸収液を生成する低温再生器と；
前記第１の吸収器内の前記第１の希溶液を前記高温再生器に導く第１の希溶液管と；
前記第１の希溶液管に接続され、前記第１の希溶液管を流れる第１の希溶液を直接的又は間接的に前記低温再生器へ導く分岐管と；
前記第１の希溶液管を流れる前記第１の希溶液を、前記高温再生器へ流入させるのと、前記低温再生器へ流入させるのとを切り替える切替弁とを備え；
前記第１の希溶液管を流れる前記第１の希溶液が前記低温再生器に流入したときに、前記低温再生器は前記第１の希溶液及び前記第２の希溶液から冷媒を蒸発させるように構成され；
前記低温再生器で生成された前記第２の吸収液の一部を前記高温再生器に導く中間濃溶液管であって、流路を遮断可能な開閉弁を有する中間濃溶液管をさらに備え；
前記第１の希溶液管を流れる前記第１の希溶液を前記高温再生器へ流入させたときは前記開閉弁を閉にし、前記第１の希溶液管を流れる前記第１の希溶液を前記低温再生器へ流入させたときは前記開閉弁を開にして前記低温再生器で生成された前記第２の吸収液の一部を前記高温再生器に導くように構成された；
吸収ヒートポンプ。 A first absorber that has a flow path for the medium to be heated, and that heats the medium to be heated with absorption heat generated when the first absorption liquid absorbs the first refrigerant vapor;
An evaporator for supplying the first refrigerant vapor to the first absorber;
More than the first absorber, wherein the first refrigerant vapor is generated by heating the refrigerant liquid in the evaporator with absorption heat generated when the second absorption liquid absorbs the second refrigerant vapor. A second absorber with a low operating temperature;
In the first absorber, the first absorbing liquid absorbs the first refrigerant vapor and introduces and heats the first dilute solution having a reduced concentration to evaporate the refrigerant from the first dilute solution. A high temperature regenerator for producing the first absorbent;
In the second absorber, the second absorbing liquid absorbs the second refrigerant vapor and introduces and heats the second dilute solution having a reduced concentration to evaporate the refrigerant from the second dilute solution. A low temperature regenerator for producing the second absorbent;
A first dilute solution tube that guides the first dilute solution in the first absorber to the high temperature regenerator;
A branch pipe connected to the first dilute solution pipe and leading the first dilute solution flowing through the first dilute solution pipe directly or indirectly to the low temperature regenerator;
Said first dilute solution flowing through the first dilute solution tube, and cause to flow into the high-temperature regenerator, Bei example a switching valve for switching between cause to flow into the low-temperature regenerator;
When the first dilute solution flowing through the first dilute solution tube flows into the low temperature regenerator, the low temperature regenerator evaporates refrigerant from the first dilute solution and the second dilute solution. Composed of;
An intermediate concentrated solution pipe for guiding a part of the second absorption liquid generated by the low temperature regenerator to the high temperature regenerator, further comprising an intermediate concentrated solution pipe having an on-off valve capable of blocking the flow path;
When the first dilute solution flowing through the first dilute solution pipe flows into the high-temperature regenerator, the on-off valve is closed, and the first dilute solution flowing through the first dilute solution pipe is When the refrigerant is flowed into the low temperature regenerator, the on-off valve is opened so that a part of the second absorbing liquid generated in the low temperature regenerator is guided to the high temperature regenerator;
Absorption heat pump. 被加熱媒体の流路を内部に有し、第１の吸収液が第１の冷媒蒸気を吸収する際に発生する吸収熱で前記被加熱媒体を加熱する第１の吸収器と；
前記第１の吸収器に前記第１の冷媒蒸気を供給する蒸発器と；
第２の吸収液が第２の冷媒蒸気を吸収する際に発生する吸収熱で前記蒸発器内の冷媒液を加熱して前記第１の冷媒蒸気を生成する、前記第１の吸収器よりも作動温度が低い第２の吸収器と；
前記第１の吸収器で前記第１の吸収液が前記第１の冷媒蒸気を吸収して濃度が低下した第１の希溶液を導入し加熱して、前記第１の希溶液から冷媒を蒸発させて前記第１の吸収液を生成する高温再生器と；
前記第２の吸収器で前記第２の吸収液が前記第２の冷媒蒸気を吸収して濃度が低下した第２の希溶液を導入し加熱して、前記第２の希溶液から冷媒を蒸発させて前記第２の吸収液を生成する低温再生器と；
前記第１の吸収器内の前記第１の希溶液を前記高温再生器に導く第１の希溶液管と；
前記第１の希溶液管に接続され、前記第１の希溶液管を流れる第１の希溶液を直接的又は間接的に前記低温再生器へ導く分岐管と；
前記第１の希溶液管を流れる前記第１の希溶液を、前記高温再生器へ流入させるのと、前記低温再生器へ流入させるのとを切り替える切替弁と；
前記第１の吸収器から導出される前記第１の希溶液の濃度を検出する第１の希溶液濃度検出手段と；
前記低温再生器で生成された第２の吸収液の濃度を検出する第２の吸収液濃度検出手段と；
前記第１の希溶液濃度検出手段で検出された値が前記第２の吸収液濃度検出手段で検出された値よりも小さいときに前記第１の希溶液の少なくとも一部を前記低温再生器に導き、前記第１の希溶液濃度検出手段で検出された値が前記第２の吸収液濃度検出手段で検出された値以上のときに前記第１の希溶液の全部を前記高温再生器に導くように、前記切替弁を制御する制御装置とを備える；
吸収ヒートポンプ。 A first absorber that has a flow path for the medium to be heated, and that heats the medium to be heated with absorption heat generated when the first absorption liquid absorbs the first refrigerant vapor;
An evaporator for supplying the first refrigerant vapor to the first absorber;
More than the first absorber, wherein the first refrigerant vapor is generated by heating the refrigerant liquid in the evaporator with absorption heat generated when the second absorption liquid absorbs the second refrigerant vapor. A second absorber with a low operating temperature;
In the first absorber, the first absorbing liquid absorbs the first refrigerant vapor and introduces and heats the first dilute solution having a reduced concentration to evaporate the refrigerant from the first dilute solution. A high temperature regenerator for producing the first absorbent;
In the second absorber, the second absorbing liquid absorbs the second refrigerant vapor and introduces and heats the second dilute solution having a reduced concentration to evaporate the refrigerant from the second dilute solution. A low temperature regenerator for producing the second absorbent;
A first dilute solution tube that guides the first dilute solution in the first absorber to the high temperature regenerator;
A branch pipe connected to the first dilute solution pipe and leading the first dilute solution flowing through the first dilute solution pipe directly or indirectly to the low temperature regenerator;
A switching valve for switching between flowing the first dilute solution flowing through the first dilute solution pipe into the high temperature regenerator and flowing into the low temperature regenerator ;
First dilute solution concentration detecting means for detecting the concentration of the first dilute solution derived from the first absorber;
Second absorbing liquid concentration detecting means for detecting the concentration of the second absorbing liquid generated by the low temperature regenerator;
When the value detected by the first dilute solution concentration detecting means is smaller than the value detected by the second absorbing solution concentration detecting means, at least a part of the first dilute solution is transferred to the low temperature regenerator. When the value detected by the first dilute solution concentration detecting means is greater than or equal to the value detected by the second absorbing solution concentration detecting means, all of the first dilute solution is led to the high temperature regenerator. And a control device for controlling the switching valve;
Absorption heat pump. 前記第２の吸収器で発生した吸収熱を、直接的又は間接的に前記高温再生器内に搬送する吸収熱搬送手段を備える；
請求項１又は請求項２に記載の吸収ヒートポンプ。 An absorption heat transfer means for transferring absorbed heat generated in the second absorber directly or indirectly into the high temperature regenerator;
The absorption heat pump according to claim 1 or 2. 前記第２の吸収器に導入される前記第２の吸収液のうち、前記第２の冷媒蒸気を吸収する前記第２の吸収液の流量を調節する吸収液流量調節手段を備える；
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。 An absorption liquid flow rate adjusting means for adjusting a flow rate of the second absorption liquid that absorbs the second refrigerant vapor among the second absorption liquid introduced into the second absorber;
The absorption heat pump according to any one of claims 1 to 3.
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JP2007127342A (en) * 2005-11-04 2007-05-24 Ebara Corp Absorption heat pump and steam supply system
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