JP6971340B2

JP6971340B2 - Absorption chiller

Info

Publication number: JP6971340B2
Application number: JP2020010876A
Authority: JP
Inventors: 達郎藤居; 茂裕土井; 稔宮内; 健太郎蛭田
Original assignee: ジョンソンコントロールズビルディングエフィシェンシージャパン合同会社
Priority date: 2020-01-27
Filing date: 2020-01-27
Publication date: 2021-11-24
Anticipated expiration: 2040-01-27
Also published as: JP2021116972A

Description

本発明は、吸収式冷凍機に関するものである。 The present invention relates to an absorption chiller.

吸収式冷凍機の機内から不凝縮ガスを吸引して外部に排出する抽気エゼクタでは、駆動液（溶液）をノズルから噴出させて周囲の不凝縮ガスを駆動液に随伴させる原理であることから、駆動液（溶液）を供給するポンプはこのノズルの抵抗に対応した高揚程ポンプとする必要がある。
特許文献１には、２つの吸収溶液が独立した２つの吸収溶液サイクルを構成する吸収式冷凍機であって、２つの吸収溶液サイクルのそれぞれの吸収器の内部には、エゼクタが設けられ、エゼクタのそれぞれの駆動液は、吸収器のそれぞれの吸収溶液の一部であり、吸収器のそれぞれに接続された溶液ポンプから供給される構成を開示している。 In the bleeding ejector that sucks the non-condensable gas from the inside of the absorption chiller and discharges it to the outside, the driving liquid (solution) is ejected from the nozzle and the surrounding non-condensed gas is accompanied by the driving liquid. The pump that supplies the driving liquid (solution) needs to be a high-lift pump that corresponds to the resistance of this nozzle.
Patent Document 1 is an absorption chiller in which two absorption solutions constitute two independent absorption solution cycles, and an ejector is provided inside each absorber of the two absorption solution cycles. Each drive fluid is part of each absorption solution in the absorber and discloses a configuration supplied from a solution pump connected to each of the absorbers.

特開２０１７−５３４９９号公報JP-A-2017-53499

しかしながら、特許文献１では、低温吸収器の抽気エゼクタを低温吸収器の溶液で、補助吸収器の抽気エゼクタを補助吸収器の溶液で駆動する構成であったため、それぞれの吸収器に高揚程ポンプを設置する必要があり、消費電力とコストの増大を招いていた。
さらに特許文献１では、補助吸収器の抽気エゼクタの駆動液として、濃度が低く飽和圧力が高い補助吸収器の溶液を用いていたことから、抽気エゼクタの吸引力が低く、不凝縮ガスを十分に吸引、除去できないという課題もあった。 However, in Patent Document 1, since the bleeding ejector of the low temperature absorber is driven by the solution of the low temperature absorber and the bleeding ejector of the auxiliary absorber is driven by the solution of the auxiliary absorber, a high lift pump is provided for each absorber. It had to be installed, which led to increased power consumption and cost.
Further, in Patent Document 1, since the solution of the auxiliary absorber having a low concentration and a high saturation pressure is used as the driving liquid of the bleed air ejector of the auxiliary absorber, the suction power of the bleed air ejector is low and the non-condensable gas is sufficiently used. There was also the problem that it could not be sucked or removed.

そこで、本発明は、補助吸収器の抽気エゼクタの駆動液として、低温吸収器の溶液を用いることにより、補助吸収器のポンプを低揚程とすることができ、省電力で安価なポンプを使用することができる、吸収式冷凍機を提供することを目的とする。 Therefore, in the present invention, by using the solution of the low temperature absorber as the driving liquid of the bleed air ejector of the auxiliary absorber, the pump of the auxiliary absorber can have a low lift, and a power-saving and inexpensive pump is used. It is an object of the present invention to provide an absorption chiller that can be used.

本発明は、濃度が異なる２つの吸収溶液が独立した２つの吸収溶液サイクルを構成する吸収式冷凍機であって、前記２つの吸収溶液サイクルはそれぞれ、吸収器を有し、前記吸収器のそれぞれの気相部は、分離され、前記吸収器のそれぞれの気相部は、それぞれ設けられたエゼクタの吸引側に接続され、前記エゼクタのそれぞれの駆動液は、いずれも前記２つの吸収溶液サイクルのうち、濃度が高い方の吸収溶液サイクルの前記吸収溶液の一部である。 The present invention is an absorption type refrigerating machine in which two absorption solutions having different concentrations constitute two independent absorption solution cycles, each of the two absorption solution cycles having an absorber, and each of the above absorbers. The gas phase part of the absorber is separated, each gas phase part of the absorber is connected to the suction side of the ejector provided, and each driving liquid of the ejector is of the two absorption solution cycles. Of these, it is a part of the absorption solution of the absorption solution cycle having the higher concentration.

本発明によれば、補助吸収器の抽気エゼクタの駆動液として、低温吸収器の溶液を用いることにより、補助吸収器のポンプを低揚程とすることができ、省電力で安価なポンプを使用することができる。
また、補助吸収器の抽気エゼクタの駆動液として、補助吸収器に比べて濃度が高い低温吸収器の溶液を用いることにより、補助吸収器の抽気エゼクタの吸引力を向上できる。 According to the present invention, by using the solution of the low temperature absorber as the driving liquid of the bleed air ejector of the auxiliary absorber, the pump of the auxiliary absorber can have a low head, and a power-saving and inexpensive pump is used. be able to.
Further, by using a solution of a low temperature absorber having a higher concentration than that of the auxiliary absorber as the driving liquid of the bleed air ejector of the auxiliary absorber, the suction power of the bleed air ejector of the auxiliary absorber can be improved.

第１の実施形態に係わる吸収式冷凍機を概略的に示す全体構成図である。It is an overall block diagram which shows schematically the absorption chiller which concerns on 1st Embodiment. 第２の実施形態に係わる吸収式冷凍機の要部を示す構成図である。It is a block diagram which shows the main part of the absorption chiller which concerns on 2nd Embodiment. 第３の実施形態に係わる吸収式冷凍機の要部を示す構成図である。It is a block diagram which shows the main part of the absorption chiller which concerns on 3rd Embodiment. 第４の実施形態に係わる吸収式冷凍機を概略的に示す全体構成図であるIt is an overall block diagram which shows schematically the absorption chiller which concerns on 4th Embodiment. 第５の実施形態に係わる吸収式冷凍機を概略的に示す全体構成図である。It is an overall block diagram which shows schematically the absorption chiller which concerns on 5th Embodiment. 第６の実施形態に係わる吸収式冷凍機の要部を示す構成図である。It is a block diagram which shows the main part of the absorption chiller which concerns on 6th Embodiment.

本発明における主要な装置構成について説明する。 The main device configuration in the present invention will be described.

本発明の吸収式冷凍機は、蒸発器、吸収器、高圧再生器、低圧再生器、凝縮器、補助吸収器、補助再生器、熱交換器（低温、中温、高温）、冷媒ポンプ、溶液ポンプ、冷却水ポンプ及び冷却塔、並びにこれらを機能的に接続する配管系から概ね構成されている。冷媒蒸気を吸収する溶液のフローは、吸収器、高圧再生器、低圧再生器などを備えているメインサイクルフローと、補助吸収器、補助再生器などを備えている補助サイクルフローの２系統で構成されている。冷凍能力を維持するために、各サイクルフローに必要な溶液循環量は、それぞれ定まっており、お互いの溶液が混合または分配されないようにそれぞれが独立した配管系を成している。上記のようにメインサイクルフローと補助サイクルフローとから構成されている吸収式冷凍機を、ここではダブルリフトサイクル吸収式冷凍機と呼ぶ。 The absorption chiller of the present invention includes an evaporator, an absorber, a high-pressure regenerator, a low-pressure regenerator, a condenser, an auxiliary absorber, an auxiliary regenerator, a heat exchanger (low temperature, medium temperature, high temperature), a refrigerant pump, and a solution pump. It generally consists of a cooling water pump and a cooling tower, and a piping system that functionally connects them. The flow of the solution that absorbs the refrigerant vapor consists of two systems: a main cycle flow equipped with an absorber, high-pressure regenerator, low-pressure regenerator, etc., and an auxiliary cycle flow equipped with an auxiliary absorber, auxiliary regenerator, etc. Has been done. In order to maintain the refrigerating capacity, the amount of solution circulation required for each cycle flow is fixed, and each forms an independent piping system so that the solutions of each other are not mixed or distributed. The absorption chiller composed of the main cycle flow and the auxiliary cycle flow as described above is referred to as a double lift cycle absorption chiller here.

以下、本発明の実施の態様について４つに分けて説明する。 Hereinafter, embodiments of the present invention will be described in four parts.

まず、第１の実施の態様(図１Ａ参照)について説明する。 First, the first embodiment (see FIG. 1A) will be described.

メインサイクルフローにおいて、溶液ポンプの下流側配管（吐出側配管）を低温溶液熱交換器の手前で分岐し、吸収器内部へ導く。その分岐配管を吸収器から取り出し、吸収器と溶液ポンプとをつなぐ配管の途中に接続する。さらに、吸収器内を通過する分岐配管の途中にエゼクタを設ける。そのエゼクタによって吸収器内部に溜まった不凝縮ガスを抽気する。なお、エゼクタの駆動液は、溶液ポンプの下流側（吐出側）を流れる溶液（メインサイクルフロー側）の一部とする。エゼクタの駆動液は、溶液ポンプの吐出側からエゼクタに流入し、エゼクタから溶液ポンプの吸込側に流出する。 In the main cycle flow, the downstream pipe (discharge side pipe) of the solution pump is branched in front of the low temperature solution heat exchanger and guided to the inside of the absorber. The branch pipe is taken out from the absorber and connected in the middle of the pipe connecting the absorber and the solution pump. Further, an ejector is provided in the middle of the branch pipe passing through the absorber. The ejector draws out the non-condensable gas accumulated inside the absorber. The driving liquid of the ejector is a part of the solution (main cycle flow side) flowing on the downstream side (discharge side) of the solution pump. The driving liquid of the ejector flows into the ejector from the discharge side of the solution pump, and flows out from the ejector to the suction side of the solution pump.

また、補助サイクルフローにおいては、上記メインサイクルフローの溶液ポンプの下流側配管（吐出側配管）を低温溶液熱交換器の手前で分岐し、補助吸収器内部へ導く。その分岐配管を補助吸収器から取り出し、吸収器と溶液ポンプとをつなぐ配管の途中に接続する。さらに、補助吸収器内を通過する分岐配管の途中にエゼクタを設ける。そのエゼクタによって補助吸収器内部に溜まった不凝縮ガスを抽気する。上記と同様に、エゼクタの駆動液は、溶液ポンプの下流側（吐出側）を流れる溶液（メインサイクルフロー側）の一部とする。エゼクタの駆動液は、溶液ポンプの吐出側からエゼクタに流入し、エゼクタから溶液ポンプの吸込側に流出する。 Further, in the auxiliary cycle flow, the downstream side pipe (discharge side pipe) of the solution pump of the main cycle flow is branched in front of the low temperature solution heat exchanger and guided to the inside of the auxiliary absorber. The branch pipe is taken out from the auxiliary absorber and connected in the middle of the pipe connecting the absorber and the solution pump. Further, an ejector is provided in the middle of the branch pipe passing through the auxiliary absorber. The ejector draws out the non-condensable gas accumulated inside the auxiliary absorber. Similar to the above, the driving liquid of the ejector is a part of the solution (main cycle flow side) flowing on the downstream side (discharge side) of the solution pump. The driving liquid of the ejector flows into the ejector from the discharge side of the solution pump, and flows out from the ejector to the suction side of the solution pump.

各フローで抽気された不凝縮ガスは、溶液の流れに乗って高圧再生器（メインサイクルフロー側）に送られる。そして、高圧再生器で生成された冷媒蒸気と送られてきた不凝縮ガスとが凝縮器に流れ込む。 The non-condensable gas extracted in each flow is sent to the high-pressure regenerator (main cycle flow side) on the flow of the solution. Then, the refrigerant vapor generated by the high-pressure regenerator and the sent non-condensable gas flow into the condenser.

加えて、凝縮器内部には、次の構造を備える。すなわち、メインサイクルフロー側の溶液ポンプの下流側配管を低温溶液熱交換器の手前で分岐し、凝縮器内部へ導く。その分岐配管を凝縮器から取り出し、気液分離器に接続する。さらに、凝縮器内部を通過する分岐配管の途中にエゼクタを設ける。そして、そのエゼクタによって、上記の各サイクルフローから集められた不凝縮ガスをまとめて抽気する。なお、エゼクタの駆動液は、メインサイクルフローを循環する溶液の一部とする。 In addition, the inside of the condenser has the following structure. That is, the piping on the downstream side of the solution pump on the main cycle flow side is branched in front of the low temperature solution heat exchanger and led to the inside of the condenser. Remove the branch pipe from the condenser and connect it to the gas-liquid separator. Further, an ejector is provided in the middle of the branch pipe passing through the inside of the condenser. Then, the non-condensable gas collected from each of the above cycle flows is collectively extracted by the ejector. The driving liquid of the ejector is a part of the solution circulating in the main cycle flow.

次に、気液分離器内部で溶液と不凝縮ガスに分離して、溶液は、メインサイクルフローに戻される。一方、不凝縮ガスは、貯気タンクに一時的に保持されて、排出用のエゼクタによって不凝縮ガスを機外へ排出する。 The solution is then separated into a solution and a non-condensable gas inside the gas-liquid separator and the solution is returned to the main cycle flow. On the other hand, the non-condensable gas is temporarily held in the air storage tank, and the non-condensable gas is discharged to the outside of the machine by the ejector for discharge.

次に、第２の実施の態様(図１Ｂ参照)について説明する。 Next, a second embodiment (see FIG. 1B) will be described.

第１の実施の態様において、駆動液となる吸収溶液の一部は、メインサイクルフローの分岐配管を吸収器に導く前に蒸発器の内部を経由するように配置することにより、蒸発器の内部にて熱交換を行い、蒸発器から取り出した分岐配管を吸収器に導くものである。 In the first embodiment, a part of the absorbing solution serving as a driving liquid is arranged inside the evaporator so as to pass through the inside of the evaporator before guiding the branch pipe of the main cycle flow to the absorber. The branch pipe taken out from the evaporator is guided to the absorber by exchanging heat at.

次に、第３の実施の態様（図１Ｃ参照）について説明する。 Next, a third embodiment (see FIG. 1C) will be described.

第１又は第２の実施の態様において、吸収式冷凍機の運転中に、冷凍能力を取得して能力低下が認められた場合にのみ抽気動作を実施するものである。つまり、各サイクルフローの抽気用分岐配管の途中に電磁弁を設置し、冷凍能力の低下に応じて電磁弁を開き、抽気を行うものである。なお、冷凍能力の判定は、蒸発器からの冷水出口の温度データなどを参照する。 In the first or second embodiment, the bleeding operation is performed only when the refrigerating capacity is acquired and a decrease in the capacity is recognized during the operation of the absorption chiller. That is, an electromagnetic valve is installed in the middle of the bleeding branch pipe of each cycle flow, and the solenoid valve is opened according to the decrease in the refrigerating capacity to perform bleeding. For the determination of the refrigerating capacity, refer to the temperature data of the cold water outlet from the evaporator.

＜実施形態１＞
図１Ａは、ダブルリフトサイクル吸収式冷凍機を概略的に示す全体構成図である。 <Embodiment 1>
FIG. 1A is an overall configuration diagram schematically showing a double lift cycle absorption chiller.

吸収式冷凍機１００は、メインサイクルと補助サイクルとから構成されており、それぞれのサイクルで吸収溶液（単に「溶液」ともいう。）が独立して循環する。メインサイクルは、蒸発器１０１、吸収器１０２、高圧再生器１０３、低圧再生器１０４、凝縮器１０５、低温溶液熱交換器１０６、高温溶液熱交換器１０７、冷媒ポンプ１０８、溶液ポンプ１０９、１１０などを備えている。補助サイクルは、補助吸収器１１１、補助再生器１１２、中温溶液熱交換器１１３、溶液ポンプ１１４、１１５などを備えている。蒸発器１０１、吸収器１０２、高圧再生器１０３、低圧再生器１０４、補助吸収器１１１及び補助再生器１１２は、流下液膜式の熱交換器を有する。低圧再生器１０４と補助吸収器１１１とは、連通する気相部を有し、高圧再生器１０３及び補助再生器１１２は、共通の凝縮器１０５に接続され、高圧再生器１０３と補助再生器１１２と凝縮器１０５とは、連通する気相部を有する。 The absorption chiller 100 is composed of a main cycle and an auxiliary cycle, and an absorption solution (also simply referred to as "solution") circulates independently in each cycle. The main cycle includes an evaporator 101, an absorber 102, a high-pressure regenerator 103, a low-pressure regenerator 104, a condenser 105, a low-temperature solution heat exchanger 106, a high-temperature solution heat exchanger 107, a refrigerant pump 108, a solution pump 109, 110, and the like. It is equipped with. The auxiliary cycle includes an auxiliary absorber 111, an auxiliary regenerator 112, a medium temperature solution heat exchanger 113, solution pumps 114, 115 and the like. The evaporator 101, the absorber 102, the high-pressure regenerator 103, the low-pressure regenerator 104, the auxiliary absorber 111, and the auxiliary regenerator 112 have a flow-down liquid film type heat exchanger. The low-pressure regenerator 104 and the auxiliary absorber 111 have a gas phase portion that communicates with each other, and the high-pressure regenerator 103 and the auxiliary regenerator 112 are connected to a common condenser 105, and the high-pressure regenerator 103 and the auxiliary regenerator 112 are connected to each other. And the condenser 105 have a gas phase portion that communicates with each other.

メインサイクルフローについて説明する。 The main cycle flow will be described.

高い真空圧力に維持された蒸発器１０１では、冷媒ポンプ１０８で蒸発器１０１底部に溜められた冷媒を冷媒配管１１６に通して散布装置１０１ａに導き、伝熱管群１０１ｂの外面に散布する。散布した冷媒は、その伝熱管内を流れる冷水に加熱され、その一部が冷媒蒸気となり、エリミネータ１１７を介して吸収器１０２に導かれる。このときに冷媒が蒸発する際の蒸発潜熱が、その伝熱管内を流れる冷水を冷却する。 In the evaporator 101 maintained at a high vacuum pressure, the refrigerant stored in the bottom of the evaporator 101 is guided to the spraying device 101a by the refrigerant pump 108 through the refrigerant pipe 116, and is sprayed on the outer surface of the heat transfer tube group 101b. The sprayed refrigerant is heated by the cold water flowing in the heat transfer tube, and a part of the sprayed refrigerant becomes refrigerant vapor and is guided to the absorber 102 via the eliminator 117. At this time, the latent heat of vaporization when the refrigerant evaporates cools the cold water flowing in the heat transfer tube.

吸収器１０２では、後述の低圧再生器１０４及び高圧再生器１０３で濃縮された溶液が、散布装置１０２ａから伝熱管群１０２ｂの外面に散布される。その散布された溶液は、蒸発器１０１から流入した冷媒蒸気を吸収し、濃度の薄い溶液（以下、「稀溶液」という。）となり、吸収器１０２底部に溜まる。吸収器１０２底部に溜まった稀溶液は、溶液ポンプ１０９によって、稀溶液配管１１８を通して高圧再生器１０３へ送液される。吸収器１０２から高圧再生器１０３までの稀溶液配管１１８の途中には、低温溶液熱交換器１０６及び高温溶液熱交換器１０７が設置されており、その稀溶液は、高圧再生器１０３に到達するまでに順次、昇温される。 In the absorber 102, the solution concentrated by the low-pressure regenerator 104 and the high-pressure regenerator 103, which will be described later, is sprayed from the spraying device 102a to the outer surface of the heat transfer tube group 102b. The sprayed solution absorbs the refrigerant vapor flowing from the evaporator 101, becomes a low-concentration solution (hereinafter referred to as "rare solution"), and accumulates at the bottom of the absorber 102. The rare solution collected at the bottom of the absorber 102 is sent to the high-pressure regenerator 103 through the rare solution pipe 118 by the solution pump 109. A low-temperature solution heat exchanger 106 and a high-temperature solution heat exchanger 107 are installed in the middle of the rare solution pipe 118 from the absorber 102 to the high-pressure regenerator 103, and the rare solution reaches the high-pressure regenerator 103. The temperature is gradually raised by.

また、低温溶液熱交換器１０６と高温溶液熱交換器１０７とをつなぐ稀溶液配管１１８の途中に分岐部ｆを設け、分岐部ｆから低圧再生器１０４までを分岐配管１３６で接続する。その分岐配管１３６の流路途中には、流量調整弁１３７を備える。その流量調整弁１３７によって低圧再生器１０４及び高圧再生器１０３への溶液散布量を制御できる。 Further, a branch portion f is provided in the middle of the rare solution pipe 118 connecting the low temperature solution heat exchanger 106 and the high temperature solution heat exchanger 107, and the branch portion f to the low pressure regenerator 104 are connected by the branch pipe 136. A flow rate adjusting valve 137 is provided in the middle of the flow path of the branch pipe 136. The flow rate adjusting valve 137 can control the amount of solution sprayed on the low pressure regenerator 104 and the high pressure regenerator 103.

高圧再生器１０３では、外部から投入した伝熱管群１０３ｂの内部を通る熱媒体（図示なし）によって、稀溶液が加熱濃縮されて冷媒蒸気と濃度の濃い溶液（濃溶液）に分離される。分離された冷媒蒸気は、通路１１９を通って凝縮器１０５へ送られる。一方、濃溶液は、溶液ポンプ１１０の駆動力によって、濃溶液配管１３８へ導かれ、高温溶液熱交換器１０７を通過したのち、濃溶液配管１３８の途中の合流部ｇで、後述する低圧再生器１０４から送られてきた濃溶液と合流し、低温溶液熱交換器１０６を通過して、吸収器１０２の上部に設置されている散布装置１０２ａへ送液される。 In the high-pressure regenerator 103, the rare solution is heated and concentrated by a heat medium (not shown) passing through the inside of the heat transfer tube group 103b input from the outside, and separated into a refrigerant vapor and a concentrated solution (concentrated solution). The separated refrigerant vapor is sent to the condenser 105 through the passage 119. On the other hand, the concentrated solution is guided to the concentrated solution pipe 138 by the driving force of the solution pump 110, passes through the high temperature solution heat exchanger 107, and then at the confluence g in the middle of the concentrated solution pipe 138, the low pressure regenerator described later. It merges with the concentrated solution sent from 104, passes through the low temperature solution heat exchanger 106, and is sent to the spraying device 102a installed on the upper part of the absorber 102.

低圧再生器１０４では、分岐部ｆから送られた稀溶液が、低圧再生器１０４の上部にある散布装置１０４ａから伝熱管群１０４ｂに散布され、管群内を通る熱媒体によって加熱濃縮され、濃度の濃い溶液（濃溶液）になる。その濃溶液は、低圧再生器１０４の底部に溜まり、溶液ポンプ１１０の駆動力によって濃溶液配管１２０を通って、高圧再生器１０３から送られてくる濃溶液と合流部ｇで合流して、低温溶液熱交換器１０６を通過したのち、吸収器１０２へ送液される。 In the low-pressure regenerator 104, the rare solution sent from the branch portion f is sprayed from the spraying device 104a on the upper part of the low-pressure regenerator 104 to the heat transfer tube group 104b, heated and concentrated by the heat medium passing through the tube group, and concentrated. It becomes a concentrated solution (concentrated solution). The concentrated solution collects at the bottom of the low-pressure regenerator 104, passes through the concentrated solution pipe 120 by the driving force of the solution pump 110, merges with the concentrated solution sent from the high-pressure regenerator 103 at the confluence portion g, and has a low temperature. After passing through the solution heat exchanger 106, the liquid is sent to the absorber 102.

凝縮器１０５では、高圧再生器１０３から送られてきた冷媒蒸気と、後述の補助再生器１１２からの冷媒蒸気とが合流して、それらの冷媒が凝縮液化したのち、蒸発器１０１底部へ送液される。 In the condenser 105, the refrigerant vapor sent from the high-pressure regenerator 103 and the refrigerant vapor from the auxiliary regenerator 112 described later merge to form a condensed liquid, and then the liquid is sent to the bottom of the evaporator 101. Will be done.

以下、上記フローが繰り返し循環する。また、このように吸収器１０２から出た稀溶液が、高圧再生器１０３と低圧再生器１０４に分配送液され、並行してそれらの溶液を加熱濃縮するフローをパラレルフローと呼ぶ。 Hereinafter, the above flow circulates repeatedly. Further, the flow in which the rare solution discharged from the absorber 102 is separately delivered to the high-pressure regenerator 103 and the low-pressure regenerator 104 and the solutions are heated and concentrated in parallel is called a parallel flow.

補助サイクルフローについて説明する。 The auxiliary cycle flow will be described.

補助吸収器１１１では、後述の補助再生器１１２で濃縮された濃溶液が、散布装置１１１ａから伝熱管群１１１ｂの外面に散布される。その散布された濃溶液は、低圧再生器１０４から流入した冷媒蒸気を吸収し、稀溶液となる。その稀溶液は、補助吸収器１１１の底部に溜まり、溶液ポンプ１１４によって、稀溶液配管１２１を通過して、補助再生器１１２へ送られる。補助吸収器１１１と補助再生器１１２とをつなぐ稀溶液配管１２１の途中には中温溶液熱交換器１１３が設置されており、その稀溶液は補助再生器１１２に到達するまでに昇温される。 In the auxiliary absorber 111, the concentrated solution concentrated by the auxiliary regenerator 112 described later is sprayed from the spraying device 111a to the outer surface of the heat transfer tube group 111b. The sprayed concentrated solution absorbs the refrigerant vapor flowing from the low-pressure regenerator 104 and becomes a rare solution. The rare solution collects at the bottom of the auxiliary absorber 111, passes through the rare solution pipe 121 by the solution pump 114, and is sent to the auxiliary regenerator 112. A medium temperature solution heat exchanger 113 is installed in the middle of the rare solution pipe 121 connecting the auxiliary absorber 111 and the auxiliary regenerator 112, and the temperature of the rare solution is raised by the time it reaches the auxiliary regenerator 112.

補助再生器１１２では、補助吸収器１１１から送液された稀溶液が、散布装置１１２ａによって伝熱管群１１２ｂの外面に散布される。散布された稀溶液は、外部から投入した伝熱管群１１２ｂの内部を流れる熱媒体によって、加熱濃縮されて冷媒蒸気と濃溶液に分離される。その濃溶液は、補助再生器１１２の底部に溜まり、溶液ポンプ１１５によって濃溶液配管１２２を通って、補助吸収器１１１に送られる。補助再生器１１２から補助吸収器１１１への濃溶液配管１２２の途中には中温溶液熱交換器１１３が設置され、補助吸収器１１１から補助再生器１１２へ向かう稀溶液と熱交換する。 In the auxiliary regenerator 112, the rare solution sent from the auxiliary absorber 111 is sprayed on the outer surface of the heat transfer tube group 112b by the spraying device 112a. The sprayed rare solution is heated and concentrated by a heat medium flowing inside the heat transfer tube group 112b input from the outside, and is separated into a refrigerant vapor and a concentrated solution. The concentrated solution collects at the bottom of the auxiliary regenerator 112 and is sent to the auxiliary absorber 111 by the solution pump 115 through the concentrated solution pipe 122. A medium temperature solution heat exchanger 113 is installed in the middle of the concentrated solution pipe 122 from the auxiliary absorber 112 to the auxiliary absorber 111, and exchanges heat with the rare solution from the auxiliary absorber 111 to the auxiliary absorber 112.

凝縮器１０５では、補助再生器１１２で発生した冷媒蒸気が通路１２３を通って送られてきて、前述の高圧再生器１０３からの冷媒蒸気と合流して、それらの冷媒が凝縮液化したのち、蒸発器１０１底部へ送液される。 In the condenser 105, the refrigerant vapor generated in the auxiliary regenerator 112 is sent through the passage 123, merges with the refrigerant vapor from the high-pressure regenerator 103 described above, and the refrigerants are condensed and liquefied, and then evaporated. The liquid is sent to the bottom of the vessel 101.

また、ダブルリフトサイクル吸収式冷凍機の駆動力である熱媒体は、高圧再生器１０３、低圧再生器１０４、補助再生器１１２の伝熱管群（１０３ｂ、１０４ｂ、１１２ｂ）内に投入して、熱を回収する。 Further, the heat medium that is the driving force of the double lift cycle absorption chiller is put into the heat transfer tube group (103b, 104b, 112b) of the high pressure regenerator 103, the low pressure regenerator 104, and the auxiliary regenerator 112 to generate heat. To collect.

吸収器１０２、補助吸収器１１１、凝縮器１０５には、熱回収用の冷却水が、伝熱管群（１０２ｂ、１１１ｂ、１０５ｂ）内を通して送液されている。熱を回収した冷却水は、図示していない冷却塔によって冷却され、再度冷却水として循環される。
以上の構成をもとに、メインサイクルと補助サイクルの溶液濃度の高低関係について説明する。メインサイクルにおける低圧再生器１０４で発生した冷媒蒸気は補助サイクルの補助吸収器１１１によって吸収されるのに対して、補助サイクルにおける補助再生器１１２で発生した冷媒蒸気は凝縮器１０５によって吸引され、凝縮する。ここで、補助吸収器１１１の伝熱管群１１１ｂと、凝縮器１０５に伝熱管群１０５ｂに供給される冷却水の温度はほぼ同等である。しかしながら、これらの器内の蒸気圧力は、凝縮器１１５においては冷却水の温度に対応した凝縮圧力となるのに対して、補助吸収器１１１においては、冷却水の温度と補助再生器１１２から供給された吸収溶液濃度に対する平衡圧力となり、凝縮器内の圧力よりも低圧となる。
したがって、低圧再生器１０４と補助再生器１１２の溶液濃度は、より低い圧力の下で濃縮される低圧再生器の方が高濃度となり、この低圧再生器１０４を有するメインサイクルの方が、吸収溶液が補助再生器１１２のみによって濃縮される補助サイクルに対して濃度が高くなる。すなわち、濃度が高い方の吸収溶液サイクルは、メインサイクルとなる。
また、本実施形態の構造的な特徴は、濃度が高い方、すなわち吸収器における吸収力が高いメインサイクルの吸収器１０２の気相部が、冷水を冷却する蒸発器１０１の気相部に連通している点にある。 Cooling water for heat recovery is sent to the absorber 102, the auxiliary absorber 111, and the condenser 105 through the heat transfer tube group (102b, 111b, 105b). The cooling water from which the heat has been recovered is cooled by a cooling tower (not shown) and circulated again as cooling water.
Based on the above configuration, the relationship between the high and low solution concentrations of the main cycle and the auxiliary cycle will be described. The refrigerant vapor generated in the low pressure regenerator 104 in the main cycle is absorbed by the auxiliary absorber 111 in the auxiliary cycle, whereas the refrigerant vapor generated in the auxiliary regenerator 112 in the auxiliary cycle is sucked by the condenser 105 and condensed. do. Here, the temperatures of the heat transfer tube group 111b of the auxiliary absorber 111 and the cooling water supplied to the heat transfer tube group 105b to the condenser 105 are substantially the same. However, the steam pressure in these vessels is a condensation pressure corresponding to the temperature of the cooling water in the condenser 115, whereas in the auxiliary absorber 111, it is supplied from the temperature of the cooling water and the auxiliary regenerator 112. It becomes the equilibrium pressure with respect to the absorbed solution concentration, and becomes lower than the pressure in the condenser.
Therefore, the solution concentrations of the low pressure regenerator 104 and the auxiliary regenerator 112 are higher in the low pressure regenerator that is concentrated under lower pressure, and the absorption solution in the main cycle having the low pressure regenerator 104. Is concentrated with respect to the auxiliary cycle enriched only by the auxiliary regenerator 112. That is, the absorption solution cycle having the higher concentration becomes the main cycle.
Further, the structural feature of the present embodiment is that the gas phase portion of the absorber 102 of the main cycle having a higher concentration, that is, the absorbent capacity of the absorber, communicates with the gas phase portion of the evaporator 101 that cools the cold water. It is in the point of doing.

本発明が提案する不凝縮ガスの抽気、排出動作について説明する。 The bleeding and discharging operations of the non-condensable gas proposed by the present invention will be described.

吸収式冷凍機内部で発生した不凝縮ガスは、機内で最も低圧となる吸収器１０２（メインサイクル側）と補助吸収器１１１（補助サイクル側）に溜まる。 The non-condensable gas generated inside the absorption chiller accumulates in the absorber 102 (main cycle side) and the auxiliary absorber 111 (auxiliary cycle side), which have the lowest pressure in the machine.

まず、吸収器１０２内部（メインサイクル側）に溜まる不凝縮ガス１２４の抽気手段について説明する。 First, the bleeding means of the non-condensable gas 124 accumulated inside the absorber 102 (main cycle side) will be described.

抽気構造について説明する。溶液ポンプ１０９下流に接続されている稀溶液配管１１８の分岐部ａから分岐配管１２５を接続し、吸収器１０２内部を通過させるように配置する。吸収器１０２通過後の分岐配管１２５は、吸収器１０２と溶液ポンプ１０９をつなぐ稀溶液配管１１８の途中（合流部ｂ）に接続し、合流させる。また、吸収器１０２内部を通過する分岐配管１２５の途中には、エゼクタ１２６を設置する。 The bleed air structure will be described. The branch pipe 125 is connected from the branch portion a of the rare solution pipe 118 connected downstream of the solution pump 109, and is arranged so as to pass through the inside of the absorber 102. The branch pipe 125 after passing through the absorber 102 is connected to the middle of the rare solution pipe 118 (merging portion b) connecting the absorber 102 and the solution pump 109 to merge. Further, an ejector 126 is installed in the middle of the branch pipe 125 passing through the inside of the absorber 102.

抽気動作について説明する。分岐部ａで稀溶液の一部が、分岐配管１２５を通って吸収器１０２内部のエゼクタ１２６に送液される。そして、エゼクタ効果により吸収器１０２内部の不凝縮ガス１２４を抽気し、送液された稀溶液に回収後、分岐配管１２５を通って稀溶液配管１１８の合流部ｂに送液される。合流部ｂでは吸収器１０２から出た稀溶液と、抽気による不凝縮ガス１２４を含んだ稀溶液とが合流する。 The bleeding operation will be described. At the branch portion a, a part of the rare solution is sent to the ejector 126 inside the absorber 102 through the branch pipe 125. Then, the non-condensable gas 124 inside the absorber 102 is extracted by the ejector effect, collected in the sent rare solution, and then sent to the confluence portion b of the rare solution pipe 118 through the branch pipe 125. At the merging portion b, the rare solution discharged from the absorber 102 and the rare solution containing the non-condensable gas 124 by bleed air merge.

次に、補助吸収器１１１（補助サイクル側）に溜まる不凝縮ガス１２７の抽気手段について説明する。 Next, the bleeding means of the non-condensable gas 127 accumulated in the auxiliary absorber 111 (auxiliary cycle side) will be described.

抽気構造について説明する。溶液ポンプ１０９下流に接続されている稀溶液配管１１８の分岐部ｃから分岐配管５０１を接続し、補助吸収器１１１内部を通過させるように配置する。補助吸収器１１１通過後の分岐配管５０１は、吸収器１０２と溶液ポンプ１０９をつなぐ稀溶液配管１１８の途中（合流部ｄ）に接続し、合流させる。また、補助吸収器１１１内部を通過する分岐配管５０１の途中にはエゼクタ１２９を設置する。 The bleed air structure will be described. The branch pipe 501 is connected from the branch portion c of the rare solution pipe 118 connected downstream of the solution pump 109, and is arranged so as to pass through the inside of the auxiliary absorber 111. The branch pipe 501 after passing through the auxiliary absorber 111 is connected to the middle of the rare solution pipe 118 (merging portion d) connecting the absorber 102 and the solution pump 109 to merge. Further, an ejector 129 is installed in the middle of the branch pipe 501 passing through the inside of the auxiliary absorber 111.

抽気動作について説明する。分岐部ｃで稀溶液の一部が、分岐配管５０１を通って補助吸収器１１１内部のエゼクタ１２９に送液される。そして、エゼクタ効果により補助吸収器１１１内部の不凝縮ガス１２７を抽気し、送液された稀溶液に回収後、分岐配管５０１を通って稀溶液配管１１８の合流部ｄに送液される。合流部ｄでは、吸収器１０２から出た稀溶液と、抽気による不凝縮ガス１２７を含んだ稀溶液とが合流し、さらに、上述した通り、抽気による不凝縮ガス１２４を含んだ稀溶液とが合流する。
抽気されたメインサイクル側と補助サイクル側の不凝縮ガス（１２４、１２７）は、稀溶液に含まれた状態で高圧再生器１０３へ送られる。高圧再生器１０３に送られた不凝縮ガス（１２４、１２７）を含む稀溶液は、加熱濃縮されて冷媒蒸気と、不凝縮ガス（１２４、１２７）と、濃溶液に分離される。その内、冷媒蒸気と不凝縮ガス（１２４、１２７）は、通路１１９を通って凝縮器１０５に送られる。上記の抽気動作によって、吸収器１０２に溜まった不凝縮ガス１２４および補助吸収器１１１に溜まった不凝縮ガス１２７が凝縮器１０５に送られる。凝縮器１０５の内部にもエゼクタ１３９が設けられている。 The bleeding operation will be described. At the branch portion c, a part of the rare solution is sent to the ejector 129 inside the auxiliary absorber 111 through the branch pipe 501. Then, the non-condensable gas 127 inside the auxiliary absorber 111 is extracted by the ejector effect, collected in the sent rare solution, and then sent to the confluence portion d of the rare solution pipe 118 through the branch pipe 501. At the merging portion d, the rare solution discharged from the absorber 102 and the rare solution containing the non-condensable gas 127 by bleed air are merged, and further, as described above, the rare solution containing the non-condensable gas 124 by bleed air is formed. Meet.
The extracted non-condensable gas (124, 127) on the main cycle side and the auxiliary cycle side is sent to the high pressure regenerator 103 in a state of being contained in the rare solution. The rare solution containing the non-condensable gas (124, 127) sent to the high-pressure regenerator 103 is heated and concentrated and separated into a refrigerant vapor, a non-condensable gas (124, 127), and a concentrated solution. Among them, the refrigerant vapor and the non-condensable gas (124, 127) are sent to the condenser 105 through the passage 119. By the above bleeding operation, the non-condensable gas 124 accumulated in the absorber 102 and the non-condensable gas 127 accumulated in the auxiliary absorber 111 are sent to the condenser 105. An ejector 139 is also provided inside the condenser 105.

また、吸収器１０２と補助吸収器１１１のそれぞれの内部には、不凝縮ガスを吸引して排出する抽気ダクト（不図示）が設けられ、それぞれの抽気ダクトは、それぞれ設けられたエゼクタ１２６、１２９の吸引側に接続されていてもよい。 Further, inside each of the absorber 102 and the auxiliary absorber 111, bleed air ducts (not shown) for sucking and discharging non-condensable gas are provided, and each bleed air duct is provided with ejectors 126 and 129, respectively. It may be connected to the suction side of.

次に、凝縮器１０５に集められたメインサイクル側と補助サイクル側の不凝縮ガス（１２４、１２７）の排出方法について説明する。 Next, a method of discharging the non-condensable gas (124, 127) collected in the condenser 105 on the main cycle side and the auxiliary cycle side will be described.

不凝縮ガス（１２４、１２７）の排出を行う構造について説明する。 The structure for discharging the non-condensable gas (124, 127) will be described.

メインサイクル側の稀溶液配管１１８で、溶液ポンプ１０９と低温溶液熱交換器１０６をつなぐ稀溶液配管１１８の途中に分岐部ｅを設け、稀溶液が分岐部ｅから分岐配管１３０を接続し、凝縮器１０５の内部を通過するように配置する。分岐配管１３０により送られた稀溶液は、凝縮器１０５の内部に設けたエゼクタ１３９の駆動液となる。そして、凝縮器１０５通過後の分岐配管１３０は、気液分離器１３１に接続される。凝縮器１０５の内部の不凝縮ガスは、凝縮器１０５の内部に設けたエゼクタ１３９により気液分離器１３１に導かれる。 In the rare solution pipe 118 on the main cycle side, a branch portion e is provided in the middle of the rare solution pipe 118 connecting the solution pump 109 and the low temperature solution heat exchanger 106, and the rare solution connects the branch pipe 130 from the branch portion e and condenses. Arrange so as to pass through the inside of the vessel 105. The rare solution sent by the branch pipe 130 serves as a driving liquid for the ejector 139 provided inside the condenser 105. Then, the branch pipe 130 after passing through the condenser 105 is connected to the gas-liquid separator 131. The non-condensable gas inside the condenser 105 is guided to the gas-liquid separator 131 by the ejector 139 provided inside the condenser 105.

気液分離器１３１で分離された不凝縮ガスは、貯気タンク１３２に一定期間保持される。一方、稀溶液は配管１３３によって吸収器１０２へ戻される。そして、貯気タンク１３２内部の圧力値の変化をモニターし、設定値よりも圧力が上がった場合は、不凝縮ガスは、エゼクタ１３４によって配管１３５に吸引され、エゼクタ駆動液とともに機外（大気中）へ排出される。このときのエゼクタ駆動液は、上記の冷却水などを利用すればよい。 The non-condensable gas separated by the gas-liquid separator 131 is held in the air storage tank 132 for a certain period of time. On the other hand, the rare solution is returned to the absorber 102 by the pipe 133. Then, the change in the pressure value inside the air storage tank 132 is monitored, and when the pressure rises above the set value, the non-condensable gas is sucked into the pipe 135 by the ejector 134, and is outside the machine (in the atmosphere) together with the ejector drive liquid. ) Is discharged. As the ejector driving liquid at this time, the above-mentioned cooling water or the like may be used.

本実施形態では、高圧再生器１０３と低圧再生器１０４に分配送液され、並行してそれらの溶液を加熱濃縮するパラレルフローの場合での不凝縮ガス抽気、排出方法を説明したが、高圧再生器１０３と低圧再生器１０４の順にそれらの溶液を加熱濃縮するシリーズフローの場合でも同様の効果が得られる。 In the present embodiment, the non-condensable gas extraction and discharge methods in the case of a parallel flow in which liquids are separately delivered to the high-pressure regenerator 103 and the low-pressure regenerator 104 and the solutions are heated and concentrated in parallel have been described. The same effect can be obtained in the case of a series flow in which the solutions are heated and concentrated in the order of the device 103 and the low pressure regenerator 104.

＜実施形態２＞
図１Ｂは、吸収式冷凍機の要部の構成を示したものである。 <Embodiment 2>
FIG. 1B shows the configuration of a main part of the absorption chiller.

本実施形態は、実施形態１の不凝縮ガス１２４の抽出性能を向上させるものである。 This embodiment improves the extraction performance of the non-condensable gas 124 of the first embodiment.

すなわち、溶液ポンプ１０９下流の稀溶液配管１１８の途中の分岐部ａから分岐接続された分岐配管２０１を蒸発器１０１内部に通し（図１Ｂ中、Ａ１で示す。）、蒸発器１０１から出た分岐配管２０１を吸収器１０２に導く配管構造にしたものである（図１Ｂ中、Ａ２で示す。）。この配管構造により、分岐部ａで分岐された稀溶液の一部を蒸発器１０１に導き、その稀溶液を蒸発器１０１内の温度で冷却し、その後、吸収器１０２内部のエゼクタ１２６に送ることができる。稀溶液を蒸発器１０１内部で冷却したことによりエゼクタ１２６の駆動液となる稀溶液の圧力が下がり、エゼクタの抽気性能が向上する。 That is, the branch pipe 201 branched and connected from the branch portion a in the middle of the rare solution pipe 118 downstream of the solution pump 109 is passed through the inside of the evaporator 101 (indicated by A1 in FIG. 1B), and the branch exits from the evaporator 101. The pipe 201 has a pipe structure that leads to the absorber 102 (indicated by A2 in FIG. 1B). With this piping structure, a part of the rare solution branched at the branch portion a is guided to the evaporator 101, the rare solution is cooled at the temperature inside the evaporator 101, and then sent to the ejector 126 inside the absorber 102. Can be done. By cooling the rare solution inside the evaporator 101, the pressure of the rare solution serving as the driving liquid of the ejector 126 is lowered, and the bleeding performance of the ejector is improved.

＜実施形態３＞
図１Ｃは、吸収式冷凍機の要部の構成を示したものである。 <Embodiment 3>
FIG. 1C shows the configuration of a main part of the absorption chiller.

本実施形態は、上記実施形態１、２において、必要に応じて不凝縮ガス１２４の抽気動作を実施させるものである。 In this embodiment, in the first and second embodiments, the bleeding operation of the non-condensable gas 124 is performed as needed.

すなわち、メインサイクル側で、稀溶液の分岐配管３０１の途中（分岐部ａからエゼクタ１２６の間）に電磁弁３０２を設ける。また、蒸発器１０１から出る冷水配管３０３には、冷水の温度をモニターする温度検知部３０４（温度検知手段）を設ける。そして、冷水温度測定値を制御ユニット３０５で取得し、冷水が設定温度に到達しない場合は、不凝縮ガスが発生したものと判定し、電磁弁３０２を開けてエゼクタ１２６を駆動する。
なお、冷水温度の異常は、不凝縮ガス１２４の発生に限ったものではないが、性能低下の一因であるため、これを排除するために上記の制御を行う。 That is, on the main cycle side, the solenoid valve 302 is provided in the middle of the branch pipe 301 for the rare solution (between the branch portion a and the ejector 126). Further, the cold water pipe 303 coming out of the evaporator 101 is provided with a temperature detecting unit 304 (temperature detecting means) for monitoring the temperature of the cold water. Then, the cold water temperature measurement value is acquired by the control unit 305, and if the cold water does not reach the set temperature, it is determined that non-condensable gas has been generated, and the solenoid valve 302 is opened to drive the ejector 126.
The abnormality of the cold water temperature is not limited to the generation of the non-condensable gas 124, but it is one of the causes of the performance deterioration, so the above control is performed to eliminate it.

＜実施形態４＞
図１Ｄは、実施形態４のダブルリフト吸収式冷凍機を概略的に示す全体構成図である。本実施形態は、実施形態１の不凝縮ガス１２７の抽出性能を向上させるものである。すなわち、補助吸収器１１１内部の不凝縮ガス１２７を抽気した稀溶液の配管５０１を、凝縮器１０５通過後の分岐配管１３０と同様に、気液分離器１３１に直接接続したものである。この配管構造により、気液分離器１３１が大型化する代わりに、不凝縮ガス１２７が分岐配管５０１、合流点ｄ、溶液ポンプ１０９、分岐点ｆおよび分岐配管１３６を経て低圧再生器１０４および補助吸収器１１１に再循環することを防止できる。従って、不凝縮ガス１２７を抽気して機外へ排出する性能が向上する。 <Embodiment 4>
FIG. 1D is an overall configuration diagram schematically showing the double lift absorption chiller of the fourth embodiment. This embodiment improves the extraction performance of the non-condensable gas 127 of the first embodiment. That is, the pipe 501 of the rare solution from which the non-condensable gas 127 inside the auxiliary absorber 111 is extracted is directly connected to the gas-liquid separator 131, similarly to the branch pipe 130 after passing through the condenser 105. Due to this piping structure, instead of increasing the size of the gas-liquid separator 131, the non-condensable gas 127 passes through the branch pipe 501, the merging point d, the solution pump 109, the branch point f and the branch pipe 136, and then the low pressure regenerator 104 and the auxiliary absorption. It is possible to prevent recirculation to the vessel 111. Therefore, the performance of extracting the non-condensable gas 127 and discharging it to the outside of the machine is improved.

以上の実施形態においては、メインサイクルと補助サイクルの溶液循環サイクルとが独立して循環し、メインサイクルにおいて高温再生器と低温再生器に並列に溶液が供給されているパラレルフローのダブルリフト吸収式冷凍機について説明したが、本発明はこれに限定されるものではなく、シリーズフロー、二重効用、三重効用等のサイクルにも適用可能である。 In the above embodiment, the solution circulation cycle of the main cycle and the auxiliary cycle circulates independently, and the solution is supplied in parallel to the high temperature regenerator and the low temperature regenerator in the main cycle. Although the refrigerator has been described, the present invention is not limited to this, and can be applied to cycles such as series flow, double-effect, triple-effect, and the like.

＜実施形態５＞
図２の実施形態５は、実施形態１から４において、高圧再生器１０３、分岐部ｆ、合流部ｇおよび高温溶液熱交換器１０７がない構成である。実施形態１と異なる構成について説明し、同じ構成は説明を省略する。
吸収器１０２内部（メインサイクル側）に溜まる不凝縮ガス１２４の抽気手段と補助吸収器１１１（補助サイクル側）に溜まる不凝縮ガス１２７の抽気手段は、実施形態１と同様である。ただし、不凝縮ガス１２７を抽気するエゼクタ１２９を設置した分岐配管５０１の出口は、実施形態４と同様に気液分離器１３１に接続する。
抽気されたメインサイクル側の不凝縮ガス（１２４）は、稀溶液に含まれた状態で、低圧再生器１０４へ送られる。一方、補助サイクル側の不凝縮ガス（１２７）は、稀溶液に含まれた状態（図２中、Ｂで示す。）で、気液分離器１３１へ送られる。
低圧再生器１０４へ送られた不凝縮ガス（１２４）を含む稀溶液は、低圧再生器１０４の上部にある散布装置１０４ａから伝熱管群１０４ｂに散布され、管群内を通る熱媒体によって加熱濃縮され、冷媒蒸気と、不凝縮ガス（１２４）と、濃度の濃い溶液（濃溶液）に分離される。その内、冷媒蒸気と不凝縮ガス（１２４）は、補助吸収器１１１に送られ、冷媒蒸気は補助吸収器内の溶液に吸収され、濃溶液は、低圧再生器１０４の底部に溜まり、溶液ポンプ１１０の駆動力によって濃溶液配管１２０を通って、低温溶液熱交換器１０６を通過したのち、吸収器１０２へ送液される。
一方、不凝縮ガス（１２４）は補助吸収器内の不凝縮ガス（１２７）とともにエゼクタ１２９によって抽気され、稀溶液に含まれた状態（図２中、Ｂで示す。）で、気液分離器１３１へ送られる。気液分離器１３１へ送られた不凝縮ガス（１２４、１２７）を含む稀溶液は、凝縮器１０５の内部からエゼクタ１３９により気液分離器１３１に導かれた稀溶液と同様、気液分離器１３１内で稀溶液と不凝縮ガスとに分離され、分離された不凝縮ガスは貯気タンク１３２に一定期間保持される。そして、エゼクタ１３４によって機外へ排出される。 <Embodiment 5>
The fifth embodiment of FIG. 2 has a configuration in which the high-pressure regenerator 103, the branch portion f, the confluence portion g, and the high-temperature solution heat exchanger 107 are not provided in the first to fourth embodiments. A configuration different from that of the first embodiment will be described, and the same configuration will be omitted.
The bleeding means of the non-condensable gas 124 collected inside the absorber 102 (main cycle side) and the bleeding means of the non-condensed gas 127 collected in the auxiliary absorber 111 (auxiliary cycle side) are the same as those in the first embodiment. However, the outlet of the branch pipe 501 in which the ejector 129 for extracting the non-condensable gas 127 is installed is connected to the gas-liquid separator 131 as in the fourth embodiment.
The extracted non-condensable gas (124) on the main cycle side is sent to the low pressure regenerator 104 in a state of being contained in the rare solution. On the other hand, the non-condensable gas (127) on the auxiliary cycle side is sent to the gas-liquid separator 131 in a state of being contained in the rare solution (indicated by B in FIG. 2).
The rare solution containing the non-condensable gas (124) sent to the low-pressure regenerator 104 is sprayed from the spraying device 104a on the upper part of the low-pressure regenerator 104 to the heat transfer tube group 104b, and is heated and concentrated by a heat medium passing through the tube group. Then, it is separated into a refrigerant steam, a non-condensable gas (124), and a concentrated solution (concentrated solution). Among them, the refrigerant steam and the non-condensable gas (124) are sent to the auxiliary absorber 111, the refrigerant steam is absorbed by the solution in the auxiliary absorber, and the concentrated solution collects at the bottom of the low pressure regenerator 104 and is a solution pump. After passing through the low-temperature solution heat exchanger 106 through the concentrated solution pipe 120 by the driving force of 110, the liquid is sent to the absorber 102.
On the other hand, the non-condensable gas (124) is extracted by the ejector 129 together with the non-condensable gas (127) in the auxiliary absorber, and is contained in the rare solution (indicated by B in FIG. 2). It is sent to 131. The rare solution containing the non-condensable gas (124, 127) sent to the gas-liquid separator 131 is the same as the rare solution guided from the inside of the condenser 105 to the gas-liquid separator 131 by the ejector 139. It is separated into a rare solution and a non-condensable gas in 131, and the separated non-condensable gas is held in the air storage tank 132 for a certain period of time. Then, it is discharged to the outside of the machine by the ejector 134.

なお、実施形態５は、実施形態２(図１Ｂ)および３（図１Ｃ）の態様を適用することができる。 In addition, the embodiment 2 (FIG. 1B) and 3 (FIG. 1C) can be applied to the fifth embodiment.

＜実施形態６＞
図３の実施形態６は、実施形態１において、メインサイクル側の蒸発器１０１と吸収器１０２とがそれぞれ低圧部（１０１１、１０２１）と高圧部（１０１２、１０２２）に分離されている構成である。低圧部吸収器１０２１に第一エゼクタ１２６１が、高圧部吸収器１０２２に第二エゼクタ１２６２が設けられている。実施形態１と異なる構成について説明し、同じ構成は説明を省略する。
溶液ポンプ１０９下流に接続されている稀溶液配管１１８の分岐部ａから分岐配管１２５を接続し、この分岐配管１２５から分岐された第一分岐配管１２５１が低圧吸収器１０２１内部を通過させるように配置する。低圧吸収器１０２１通過後の分岐配管１２５１は、高圧吸収器１０２２と溶液ポンプ１０９をつなぐ稀溶液配管１１８の途中（合流部ｂ１）に接続し、合流させる。低圧吸収器１０２１内部を通過する第一分岐配管１２５１の途中には、第一エゼクタ１２６１を設置する。
また、分岐配管１２５から分岐された第二分岐配管１２５２が高圧吸収器１０２２内部を通過させるように配置する。高圧吸収器１０２２通過後の分岐配管１２５２は、高圧吸収器１０２２と溶液ポンプ１０９をつなぐ稀溶液配管１１８の途中（合流部ｂ２）に接続し、合流させる。高圧吸収器１０２２内部を通過する第二分岐配管１２５２の途中には、第二エゼクタ１２６２を設置する。 <Embodiment 6>
In the sixth embodiment of FIG. 3, in the first embodiment, the evaporator 101 and the absorber 102 on the main cycle side are separated into a low pressure portion (1011, 1021) and a high pressure portion (1012, 1022), respectively. .. The low-pressure section absorber 1021 is provided with a first ejector 1261, and the high-pressure section absorber 1022 is provided with a second ejector 1262. A configuration different from that of the first embodiment will be described, and the same configuration will be omitted.
The branch pipe 125 is connected from the branch a of the rare solution pipe 118 connected downstream of the solution pump 109, and the first branch pipe 1251 branched from the branch pipe 125 is arranged so as to pass through the inside of the low pressure absorber 1021. do. The branch pipe 1251 after passing through the low pressure absorber 1021 is connected to the middle of the rare solution pipe 118 (merging portion b1) connecting the high pressure absorber 1022 and the solution pump 109, and merges. The first ejector 1261 is installed in the middle of the first branch pipe 1251 passing through the inside of the low pressure absorber 1021.
Further, the second branch pipe 1252 branched from the branch pipe 125 is arranged so as to pass through the inside of the high voltage absorber 1022. The branch pipe 1252 after passing through the high pressure absorber 1022 is connected to the middle of the rare solution pipe 118 (merging portion b2) connecting the high pressure absorber 1022 and the solution pump 109, and merges. A second ejector 1262 is installed in the middle of the second branch pipe 1252 passing through the inside of the high voltage absorber 1022.

抽気動作について説明する。分岐部ａで稀溶液の一部が、分岐配管１２５及び第一分岐配管１２５１を通って低圧吸収器１０２１内部の第一エゼクタ１２６１に送液される。そして、エゼクタ効果により低圧吸収器１０２１内部の不凝縮ガスを抽気し、送液された稀溶液に回収後、第一分岐配管１２５１を通って稀溶液配管１１８の合流部ｂ１に送液される。合流部ｂ１では低圧吸収器１０２１から出た稀溶液と、抽気による不凝縮ガスを含んだ稀溶液とが合流する。
また、分岐部ａで稀溶液の一部が、分岐配管１２５及び第二分岐配管１２５２を通って高圧吸収器１０２２内部の第二エゼクタ１２６２に送液される。そして、エゼクタ効果により高圧吸収器１０２２内部の不凝縮ガスを抽気し、送液された稀溶液に回収後、第二分岐配管１２５２を通って稀溶液配管１１８の合流部ｂ２に送液される。合流部ｂ２では高圧吸収器１０２２から出た稀溶液と、抽気による不凝縮ガスを含んだ稀溶液とが合流する。 The bleeding operation will be described. At the branch portion a, a part of the rare solution is sent to the first ejector 1261 inside the low pressure absorber 1021 through the branch pipe 125 and the first branch pipe 1251. Then, the non-condensable gas inside the low-pressure absorber 1021 is extracted by the ejector effect, collected in the sent rare solution, and then sent to the confluence portion b1 of the rare solution pipe 118 through the first branch pipe 1251. At the merging portion b1, the rare solution discharged from the low-pressure absorber 1021 and the rare solution containing the non-condensable gas produced by bleed air merge.
Further, a part of the rare solution at the branch portion a is sent to the second ejector 1262 inside the high pressure absorber 1022 through the branch pipe 125 and the second branch pipe 1252. Then, the non-condensable gas inside the high-pressure absorber 1022 is extracted by the ejector effect, collected in the sent rare solution, and then sent to the confluence portion b2 of the rare solution pipe 118 through the second branch pipe 1252. At the merging portion b2, the rare solution discharged from the high-pressure absorber 1022 and the rare solution containing the non-condensable gas produced by bleed air merge.

以上の構成によれば、蒸発器と吸収器を２段に分離して高性能化を図ったダブルリフトサイクル吸収冷凍機に対して、分離された各段にそれぞれ不凝縮ガスを抽気するエゼクタを設けることにより、吸収冷凍機の性能低下をより効果的に防止することができる。 According to the above configuration, for a double lift cycle absorption chiller that separates the evaporator and absorber into two stages to improve performance, an ejector that extracts non-condensable gas into each separated stage is provided. By providing it, it is possible to more effectively prevent the performance deterioration of the absorption chiller.

補助吸収器１１１（補助サイクル側）に溜まる不凝縮ガスの抽気手段である、第三エゼクタ１２９１は、駆動液が通液されるエゼクタ本体を補助吸収器１１１の筐体外部に設け、吸引部分を補助吸収器１１１の気相部に連通させた構成である。
溶液ポンプ１０９下流に接続されている稀溶液配管１１８の分岐部ｃから分岐配管５０１を接続し、分岐配管５０１を補助吸収器１１１の筐体外部に設けられたエゼクタ本体を通過させ、吸収器１０２と溶液ポンプ１０９をつなぐ稀溶液配管１１８の途中（合流部ｄ）に接続し、合流させる。
分岐部ｃで稀溶液の一部が、分岐配管５０１を通って第三エゼクタ１２９１に送液される。そして、エゼクタ効果により補助吸収器１１１内部の不凝縮ガスを抽気し、送液された稀溶液に回収後、分岐配管５０１を通って稀溶液配管１１８の合流部ｄに送液される。合流部ｄでは、低圧吸収器１０２２から出た稀溶液と、抽気による不凝縮ガスを含んだ稀溶液とが合流し、さらに、上述した通り、抽気による不凝縮ガスを含んだ稀溶液とが合流する。 The third ejector 1291, which is a means for extracting non-condensable gas accumulated in the auxiliary absorber 111 (auxiliary cycle side), has an ejector body through which the driving liquid is passed, provided outside the housing of the auxiliary absorber 111, and a suction portion is provided. It is configured to communicate with the gas phase portion of the auxiliary absorber 111.
The branch pipe 501 is connected from the branch portion c of the rare solution pipe 118 connected downstream of the solution pump 109, and the branch pipe 501 is passed through the ejector main body provided outside the housing of the auxiliary absorber 111 to pass the absorber 102. And the solution pump 109 are connected to the middle of the rare solution pipe 118 (merging portion d) to be connected and merged.
At the branch portion c, a part of the rare solution is sent to the third ejector 1291 through the branch pipe 501. Then, the non-condensable gas inside the auxiliary absorber 111 is extracted by the ejector effect, collected in the sent rare solution, and then sent to the confluence portion d of the rare solution pipe 118 through the branch pipe 501. At the merging portion d, the rare solution discharged from the low-pressure absorber 1022 and the rare solution containing the non-condensable gas due to bleed air merge, and further, as described above, the rare solution containing the non-condensable gas produced by bleed air merges. do.

以上の構成によれば、運転中や停止直後に、濃度が高い方の吸収溶液サイクルの吸収溶液が濃度の低い方の吸収溶液サイクルに移動することによる、各吸収溶液サイクル間の吸収溶液量の配分の変化を防ぐことができる。 According to the above configuration, the absorption solution amount between each absorption solution cycle is increased by moving the absorption solution of the absorption solution cycle having the higher concentration to the absorption solution cycle of the lower concentration during operation or immediately after stopping. It is possible to prevent changes in distribution.

１００：吸収式冷凍機、１０１：蒸発器、１０２：吸収器、１０３：高圧再生器、１０４：低圧再生器、１０５：凝縮器、１０６：低温溶液熱交換器、１０７：高温溶液熱交換器、１０８：冷媒ポンプ、１０９：溶液ポンプ、１１０：溶液ポンプ、１１１：補助吸収器、１１２：補助再生器、１１３：中温溶液熱交換器、１１４：溶液ポンプ、１１５：溶液ポンプ、１１６：冷媒配管、１１７：エリミネータ、１１８：稀溶液配管、１１９：通路、１２０：濃溶液配管、１２１：稀溶液配管、１２２：濃溶液配管、１２３：通路、１２４：不凝縮ガス、１２５：分岐配管、１２６：エゼクタ、１２７：不凝縮ガス、１２９：エゼクタ、１３０：分岐配管、１３１：気液分離器、１３２：貯気タンク、１３３：配管、１３４：エゼクタ、１３５：配管、１３６：分岐配管、１３７：流量調整弁、１３８：濃溶液配管、１３９：エゼクタ、２０１：分岐配管、３０１：分岐配管、３０２：電磁弁、３０３：冷水配管、３０４：温度検知部、３０５：制御ユニット、５０１：分岐配管、第一分岐配管１２５１、第二分岐配管１２５２、第一エゼクタ１２６１、第二エゼクタ１２６２、第三エゼクタ１２６３。 100: Absorption type refrigerator, 101: Evaporator, 102: Absorber, 103: High pressure regenerator, 104: Low pressure regenerator, 105: Condenser, 106: Low temperature solution heat exchanger, 107: High temperature solution heat exchanger, 108: Refrigerator pump, 109: Solution pump, 110: Solution pump, 111: Auxiliary absorber, 112: Auxiliary regenerator, 113: Medium temperature solution heat exchanger, 114: Solution pump, 115: Solution pump, 116: Refrigerator piping, 117: Eliminator, 118: Rare solution piping 119: Passage, 120: Concentrated solution piping, 121: Rare solution piping, 122: Concentrated solution piping, 123: Passage, 124: Non-condensable gas, 125: Branch piping, 126: Ejector , 127: Non-condensable gas, 129: Ejector, 130: Branch piping, 131: Gas-liquid separator, 132: Air storage tank, 133: Piping, 134: Ejector, 135: Piping, 136: Branch piping, 137: Flow adjustment Valve, 138: concentrated solution pipe, 139: ejector, 201: branch pipe, 301: branch pipe, 302: electromagnetic valve, 303: cold water pipe, 304: temperature detector, 305: control unit, 501: branch pipe, first Branch pipe 1251, second branch pipe 1252, first ejector 1261, second ejector 1262, third ejector 1263.

ただし、添え字ａ：器内の散布装置、添え字ｂ：器内の伝熱管群。 However, the subscript a: the spraying device in the vessel, and the subscript b: the heat transfer tube group in the vessel.

Claims

An absorption chiller in which two absorption solutions with different concentrations constitute two independent absorption solution cycles.
Each of the two absorption solution cycles has an absorber.
Each gas phase portion of the absorber is separated and separated.
Each gas phase portion of the absorber is connected to the suction side of the ejector provided.
An absorption chiller in which each driving liquid of the ejector is a part of the absorption solution of the absorption solution cycle having the higher concentration of the two absorption solution cycles.

The absorption chiller according to claim 1, wherein the driving liquid is supplied from a solution pump connected to the absorber provided in the absorption solution cycle having the higher concentration of the two absorption solution cycles.

The driving liquid is supplied to the ejector from the discharge side of the solution pump, sucks the non-condensable gas from the absorber to which each ejector is connected, and then is guided to the suction side of the solution pump. Absorption chiller.

A gas-liquid separator that separates the drive liquid of the ejector that has sucked the non-condensable gas into an absorption solution and a non-condensable gas is provided, and the gas phase portion of the absorber provided in the absorption solution cycle having the lower concentration is provided. The absorption chiller according to claim 1 or 2, wherein the driving liquid sucking the non-condensable gas by the provided ejector is guided to the gas-liquid separator.

Inside each of the absorbers, bleed air ducts for sucking and discharging non-condensable gas are provided.
Each of the bleed ducts is connected to the suction side of the ejector provided.
The absorption chiller according to claim 1, wherein each driving liquid of the ejector is a part of the absorption solution of the absorption solution cycle having the higher concentration of the two absorption solution cycles.

The absorption chiller according to claim 5, wherein the driving liquid is supplied from a solution pump connected to the absorber provided in the absorption solution cycle having the higher concentration of the two absorption solution cycles. ..

The first solution cycle, which connects a low temperature absorber, a low temperature regenerator, a solution heat exchanger, etc.
A second solution cycle connecting an auxiliary absorber, an auxiliary regenerator, an auxiliary solution heat exchanger, etc.
Consists of an evaporator and a condenser,
The gas phase part of each of the low temperature absorber and the auxiliary absorber is separated.
Each gas phase portion of the low temperature absorber and the auxiliary absorber is connected to the suction side of the ejector provided respectively.
An absorption chiller in which each driving liquid of the ejector is supplied from a solution pump connected to the low temperature absorber.

The absorption chiller according to claim 7, wherein the high temperature regenerator is connected to the first solution cycle.

The absorption chiller according to claim 7 or 8, wherein the driving liquid of the ejector connected to the low temperature absorber is guided to the suction side of the solution pump connected to the low temperature absorber.

Of the two absorption solution cycles, the absorber of the absorption solution cycle having the higher concentration is separated into a low pressure part and a high pressure part, and the ejector is provided corresponding to each region of the low pressure part and the high pressure part, respectively. , The absorption chiller according to any one of claims 1 to 6.

Of the two absorption solution cycles, the ejector provided in the absorber of the absorption solution cycle having the lower concentration has an ejector body through which the driving liquid is passed, which is provided outside the housing of the absorber, and is a suction portion. The absorption chiller according to any one of claims 1 to 6, wherein the chiller is communicated with the gas phase portion of the absorber.