WO2018150516A1

WO2018150516A1 - Absorption refrigerator

Info

Publication number: WO2018150516A1
Application number: PCT/JP2017/005716
Authority: WO
Inventors: 浩伸川村; 藤居　達郎; 博敏石丸; 武田　伸之
Original assignee: 日立ジョンソンコントロールズ空調株式会社
Priority date: 2017-02-16
Filing date: 2017-02-16
Publication date: 2018-08-23
Also published as: DE112017006707B4; CN110234941B; KR20190089997A; CN110234941A; KR102206209B1; DE112017006707T5

Abstract

This absorption refrigerator is provided with: an evaporator; an absorber; a low-pressure regenerator; a high-pressure regenerator; an auxiliary absorber; an auxiliary regenerator; a condenser; and a solution pump, wherein the evaporator and the absorber are connected with each other at respective gas phase parts, the low-pressure regenerator and the auxiliary absorber are connected with each other at respective gas phase parts, the high-pressure regenerator, the auxiliary regenerator, and the condenser are connected with one another at respective gas phase parts, solution piping laid from the absorber toward the high-pressure regenerator has a branch part, solution piping laid toward the low-pressure regenerator is connected to the branch part, the solution pump is provided to solution piping laid from the absorber to the branch part, and solution piping laid from the high-pressure regenerator toward the absorber has a confluence part connected to solution piping from the low-pressure regenerator. Thus, in the absorption refrigerator that combines a two-stage absorption cycle with a single-effect cycle, cold can be supplied by recovering heat from one exhaust heat source of about 90°C until a low temperature is reached, the low-pressure regenerator can be downsized, each heat exchanger can be freely arranged, the solution pump can be made smaller, and power consumption can be reduced.

Description

吸収式冷凍機Absorption refrigerator

　本発明は、吸収式冷凍機に関する。 The present invention relates to an absorption refrigerator.

　吸収式冷凍機は、熱駆動できることから、排熱として出た温水を駆動熱源として冷熱を供給することができる。再生器が１つの単効用サイクルでは、９０℃程度の温水を駆動熱源として７℃程度の冷熱を供給できる。 Since the absorption refrigerator can be driven by heat, cold water can be supplied using hot water generated as exhaust heat as a driving heat source. In a single effect cycle with one regenerator, cold water of about 7 ° C. can be supplied using hot water of about 90 ° C. as a driving heat source.

　特許文献１には、再生器が２つの２段吸収サイクルとし、単効用サイクルより低い温度の温水を駆動熱源として冷熱を供給できることが記載されている。 Patent Document 1 describes that the regenerator has two two-stage absorption cycles, and cold water can be supplied using hot water having a temperature lower than that of the single effect cycle as a driving heat source.

　また、特許文献２には、単効用サイクルと２段吸収サイクルを組合せた吸収式冷凍機が記載されている。これは、単効用サイクルと補助サイクルからなり、単効用サイクル側に高圧再生器と低圧再生器を設け、溶液の全量を吸収器、高圧再生器、低圧再生器、吸収器の順で循環させるシリーズフローとなっている。また、補助サイクル側は、補助吸収器と補助再生器からなり、補助吸収器の気相部が低圧再生器と連通し、補助再生器の気相部が高圧再生器と凝縮器の気相部と連通した構成が記載されている。特許文献２では、駆動熱源の温水を単効用サイクルに必要な温度から、２段吸収サイクルに必要な温度まで利用できるとしている。 Also, Patent Document 2 describes an absorption refrigerator that combines a single effect cycle and a two-stage absorption cycle. This series consists of a single-effect cycle and an auxiliary cycle. A high-pressure regenerator and a low-pressure regenerator are provided on the single-effect cycle side, and the entire amount of the solution is circulated in the order of absorber, high-pressure regenerator, low-pressure regenerator, and absorber. It is a flow. The auxiliary cycle side is composed of an auxiliary absorber and an auxiliary regenerator. The gas phase part of the auxiliary absorber communicates with the low pressure regenerator, and the gas phase part of the auxiliary regenerator is the gas phase part of the high pressure regenerator and the condenser. The structure communicated with is described. In Patent Document 2, the hot water of the driving heat source can be used from the temperature required for the single effect cycle to the temperature required for the two-stage absorption cycle.

特開２００４－２１１９７９号公報（図６）JP 2004-211979 A (FIG. 6) 韓国公開特許第１０－２０１１－００１４３７６号公報（図２）Korean Published Patent No. 10-2011-0014376 (FIG. 2)

　省エネルギーを図るためには、１つの排熱源からできるだけ多くの冷熱を発生させ再利用することが有効な手段となる。そのための手段として、例えば、９０℃程度の温水を単効用サイクルの駆動熱源として利用し、その後、温度が下がった温水を再度２段吸収サイクルの駆動熱源として利用することが考えられる。しかし、この場合、それぞれサイクル構成の異なる吸収式冷凍機が２台必要となり、冷水及び冷却水の配管系統が２つとなるため、配管構成が複雑になってしまい、設置面積が大きくなるとともにコスト増加になってしまう。さらに、吸収式冷凍機を２台とした場合においては、溶液ポンプや冷媒ポンプの数もほぼ倍増してしまうので、消費電力量が多くなってしまう。 In order to save energy, it is an effective means to generate as much cold as possible from one exhaust heat source and reuse it. As a means for that, for example, it is conceivable to use hot water of about 90 ° C. as the driving heat source for the single effect cycle, and then use the hot water whose temperature has decreased again as the driving heat source for the two-stage absorption cycle. However, in this case, two absorption refrigerators having different cycle configurations are required, and two piping systems for chilled water and cooling water are required, which complicates the piping configuration and increases the installation area and costs. Become. Furthermore, when two absorption refrigerators are used, the number of solution pumps and refrigerant pumps is almost doubled, resulting in an increase in power consumption.

　特許文献２の技術では、１台の吸収式冷凍機で上記課題に対応したサイクルとなっている。しかしながら、特許文献２の技術では、単効用サイクル側の吸収器から出た溶液の全量が流下液膜式の熱交換器からなる高圧再生器に流入し、高圧再生器を出た溶液の全量が流下液膜式の熱交換器からなる低圧再生器に流入するシリーズフローになっている。したがって、低圧再生器には、高圧再生器で濃縮された後の溶液が流入する。このため、低圧再生器で濃縮された溶液が最も濃度が濃くなる。溶液は同じ圧力であれば濃度の濃い方の溶液温度が高くなることから、低圧再生器では、高圧再生器で濃縮された溶液より濃度が濃くなることにより、駆動熱源との温度差が小さくなり、必要な伝熱面積が大きくなる。 In the technology of Patent Document 2, a single absorption refrigerator serves as a cycle corresponding to the above problem. However, in the technique of Patent Document 2, the total amount of the solution discharged from the absorber on the single effect cycle side flows into the high-pressure regenerator composed of a falling film heat exchanger, and the total amount of the solution discharged from the high-pressure regenerator is It is a series flow that flows into a low-pressure regenerator consisting of a falling film type heat exchanger. Therefore, the solution after being concentrated in the high pressure regenerator flows into the low pressure regenerator. For this reason, the solution concentrated in the low pressure regenerator has the highest concentration. If the solution has the same pressure, the solution temperature of the higher concentration will be higher, so the concentration difference in the low-pressure regenerator is higher than that of the solution concentrated in the high-pressure regenerator, and the temperature difference from the drive heat source is reduced. The required heat transfer area is increased.

　また、シリーズフローの場合、高圧再生器と低圧再生器で熱交換器サイズが異なった場合に、それぞれに適した溶液流量に調整できない。特に、高圧再生器及び低圧再生器において流下液膜式の熱交換器を用いる場合、溶液の散布密度に適した熱交換器サイズにしようとすると、熱交換器サイズが固定されてしまい、機器の配置の自由度が小さくなってしまう。 Also, in the case of the series flow, when the heat exchanger size is different between the high pressure regenerator and the low pressure regenerator, the solution flow rate suitable for each cannot be adjusted. In particular, when using a falling film type heat exchanger in a high-pressure regenerator and a low-pressure regenerator, the heat exchanger size is fixed when trying to make the heat exchanger size suitable for the spraying density of the solution, The degree of freedom of arrangement becomes small.

　さらに、単効用サイクル側では、溶液の全量を吸収器、高圧再生器、低圧再生器の順で循環させるために、それぞれの出口部に溶液ポンプを設置していることから、溶液ポンプの消費電力量が多くなることが考えられる。吸収式冷凍機では、熱駆動のメリットを出すためには、ポンプ駆動に必要な消費電力量の低減が有効な手段の一つとなる。 Furthermore, on the single-effect cycle side, a solution pump is installed at each outlet in order to circulate the entire amount of the solution in the order of the absorber, high-pressure regenerator, and low-pressure regenerator. The amount can be increased. In the absorption refrigerator, in order to obtain the merit of heat driving, reduction of the power consumption required for driving the pump is one of effective means.

　本発明の目的は、単効用サイクルに２段吸収サイクルを組合せた吸収式冷凍機において、９０℃程度の１つの排熱源から低温度に達するまで熱を回収して冷熱を供給するとともに、低圧再生器を小形化し、各熱交換器の配置に自由度を与え、溶液ポンプの数を適正化することにある。 The object of the present invention is to recover heat from a single exhaust heat source at about 90 ° C. until it reaches a low temperature and supply cold heat in an absorption refrigerator that combines a single-effect cycle with a two-stage absorption cycle, and at low pressure regeneration The purpose of this is to reduce the size of the chamber, give freedom to the arrangement of each heat exchanger, and optimize the number of solution pumps.

　本発明の吸収式冷凍機は、蒸発器と、吸収器と、低圧再生器と、高圧再生器と、補助吸収器と、補助再生器と、凝縮器と、溶液ポンプと、を備え、蒸発器と吸収器とは、気相部が連通し、低圧再生器と補助吸収器とは、気相部が連通し、高圧再生器と補助再生器と凝縮器とは、気相部が連通し、吸収器から高圧再生器に向かう溶液配管は、分岐部を有し、この分岐部には、低圧再生器に向かう溶液配管が連結され、溶液ポンプは、吸収器から分岐部に向かう溶液配管に設けられ、高圧再生器から吸収器に向かう溶液配管は、低圧再生器からの溶液配管と連結された合流部を有する。 An absorption refrigerator according to the present invention includes an evaporator, an absorber, a low-pressure regenerator, a high-pressure regenerator, an auxiliary absorber, an auxiliary regenerator, a condenser, and a solution pump. And the absorber are in communication with the gas phase, the low pressure regenerator and auxiliary absorber are in communication with the gas phase, and the high pressure regenerator, auxiliary regenerator and condenser are in communication with the gas phase, The solution pipe from the absorber to the high pressure regenerator has a branch part, and the solution pipe to the low pressure regenerator is connected to the branch part, and the solution pump is provided in the solution pipe from the absorber to the branch part. The solution piping from the high-pressure regenerator to the absorber has a junction connected to the solution piping from the low-pressure regenerator.

　本発明によれば、単効用サイクルに２段吸収サイクルを組合せた吸収式冷凍機において、９０℃程度の１つの駆動熱源をより低温まで回収して冷熱を供給することができ、かつ、低圧再生器を小形化することができる。 According to the present invention, in an absorption refrigerator that combines a single-effect cycle with a two-stage absorption cycle, one drive heat source of about 90 ° C. can be recovered to a lower temperature and cold can be supplied, and low pressure regeneration can be performed. The vessel can be miniaturized.

　また、本発明によれば、機器の配置に自由度を持たせるとともに、溶液ポンプを削減し、消費電力を低減することができる。 Further, according to the present invention, it is possible to give flexibility to the arrangement of devices, reduce the solution pump, and reduce power consumption.

実施例の吸収式冷凍機を示す模式構成図である。It is a schematic block diagram which shows the absorption refrigerator of an Example. 実施例の吸収式冷凍機の吸収サイクルを示すデューリング線図である。It is a Duhring diagram which shows the absorption cycle of the absorption refrigerator of an Example.

　本発明は、３つの再生器へ熱源媒体を供給し、独立した２つの溶液サイクルからなる吸収式冷凍機に関する。 The present invention relates to an absorption refrigerator that supplies a heat source medium to three regenerators and includes two independent solution cycles.

　以下、本発明の具体的実施例について、図面を用いて説明する。なお、各図において、同一符号を付した部分は同一或いは相当する部分を示している。 Hereinafter, specific examples of the present invention will be described with reference to the drawings. Note that, in each drawing, the portions denoted by the same reference numerals indicate the same or corresponding portions.

　図１は、実施例の吸収式冷凍機を示すサイクル系統図である。 FIG. 1 is a cycle system diagram showing an absorption refrigerator according to an embodiment.

　図２は、溶液の等濃度線からなるデューリング線図中に、本発明のサイクルの状態を示したグラフである。横軸に溶液温度を、縦軸に圧力をとっている。 FIG. 2 is a graph showing the state of the cycle of the present invention in a Duhring diagram composed of isoconcentration lines of the solution. The horizontal axis represents solution temperature and the vertical axis represents pressure.

　図１のＥ、Ａ、ＬＧ、ＨＧ、ＡＡ、ＡＧ、Ｃと、図２のＥ、Ａ、ＬＧ、ＨＧ、ＡＡ、ＡＧ、Ｃとは同じ部分を示す。 1 E, A, LG, HG, AA, AG, C in FIG. 1 and E, A, LG, HG, AA, AG, C in FIG.

　先ず、本発明に係る吸収式冷凍機のサイクルフローについて説明する。 First, the cycle flow of the absorption refrigerator according to the present invention will be described.

　吸収式冷凍機は、単効用サイクル側と補助サイクル側とからなり、それぞれのサイクルで溶液が独立して循環する。単効用サイクル側は、蒸発器１、吸収器９、低圧再生器２２、高圧再生器３３、凝縮器４０、低温溶液熱交換器５５及び高温溶液熱交換器５６の熱交換器要素、冷媒ポンプ６、溶液ポンプ１４、３０などを備えている。補助サイクル側は、補助吸収器１６、補助再生器４４及び中温溶液熱交換器５７の熱交換器要素、溶液ポンプ２９、５４などを備えている。 The absorption refrigerator has a single effect cycle side and an auxiliary cycle side, and the solution circulates independently in each cycle. The single-effect cycle side includes the evaporator 1, the absorber 9, the low pressure regenerator 22, the high pressure regenerator 33, the condenser 40, the heat exchanger elements of the low temperature solution heat exchanger 55 and the high temperature solution heat exchanger 56, and the refrigerant pump 6. And

solution pumps

14 and 30 are provided. The auxiliary cycle side includes the auxiliary absorber 16, the auxiliary regenerator 44, the heat exchanger elements of the intermediate temperature solution heat exchanger 57, the

solution pumps

29 and 54, and the like.

　次に、単効用サイクル側の動作について説明する。 Next, the operation on the single effect cycle side will be described.

　蒸発器１では、冷媒ポンプ６で蒸発器１下部に溜められた冷媒を、冷媒配管７を通って散布装置２に導き、熱交換器３の伝熱管外に散布する。散布された冷媒は、熱交換器３の伝熱管内を流れる冷水に加熱され、一部冷媒蒸気となり、エリミネータ８を介して吸収器９に導かれる。このときに、冷媒が蒸発する際の蒸発潜熱を利用し、熱交換器３の伝熱管内を流れる冷水を冷却する。熱交換器３には、冷水配管４、５が接続され、負荷側に冷熱を供給するための冷水が通水される。 In the evaporator 1, the refrigerant stored in the lower part of the evaporator 1 by the refrigerant pump 6 is guided to the spraying device 2 through the refrigerant pipe 7 and sprayed outside the heat transfer tube of the heat exchanger 3. The sprayed refrigerant is heated by the cold water flowing in the heat transfer tube of the heat exchanger 3, becomes a part of the refrigerant vapor, and is led to the absorber 9 through the eliminator 8. At this time, the cold water flowing in the heat transfer tubes of the heat exchanger 3 is cooled by using the latent heat of vaporization when the refrigerant evaporates. Cold water pipes 4 and 5 are connected to the heat exchanger 3, and cold water for supplying cold heat to the load side is passed through.

　吸収器９では、低圧再生器２２と高圧再生器３３で濃縮された溶液が散布装置１０から熱交換器１１の伝熱管外に散布する。散布された溶液は、蒸発器１からの冷媒蒸気を吸収し、濃度が薄くなった後、溶液配管１５の途中に設置した溶液ポンプ１４で低温溶液熱交換器５５を通過後に分岐点Ａ（分岐部）で分岐し、一方が溶液配管３１の流量調整弁３２（流量調整手段）を介して低圧再生器２２に導かれる。分岐点Ａで分岐したもう一方の溶液は、高温溶液熱交換器５６を通って高圧再生器３３に導かれる。吸収器９の熱交換器１１の伝熱管内には、溶液が冷媒蒸気を吸収する際に発生する吸収熱を取り除くために冷却水が通水される。熱交換器１１には、冷却水配管１２、１３が接続されている。 In the absorber 9, the solution concentrated in the low pressure regenerator 22 and the high pressure regenerator 33 is sprayed from the spray device 10 to the outside of the heat transfer tube of the heat exchanger 11. The sprayed solution absorbs the refrigerant vapor from the evaporator 1 and decreases in concentration, and then passes through the low-temperature solution heat exchanger 55 by the solution pump 14 installed in the middle of the solution pipe 15 and then the branch point A (branch). And one of them is led to the low pressure regenerator 22 via the flow rate adjusting valve 32 (flow rate adjusting means) of the solution pipe 31. The other solution branched at the branch point A is led to the high pressure regenerator 33 through the high temperature solution heat exchanger 56. Cooling water is passed through the heat transfer tube of the heat exchanger 11 of the absorber 9 in order to remove the absorption heat generated when the solution absorbs the refrigerant vapor.

Cooling water pipes

12 and 13 are connected to the heat exchanger 11.

　低圧再生器２２では、吸収器９で濃度の薄くなった溶液が散布装置２３から熱交換器２４の伝熱管外に散布する。散布された溶液は、熱交換器２４の伝熱管内を流れる熱源媒体で加熱され、濃縮された溶液と冷媒蒸気に分離される。濃縮された溶液は、溶液配管２７を通って合流点Ｂ（合流部）で高圧再生器３３からの溶液と合流する。冷媒蒸気は、エリミネータ２１を介して補助サイクル側の補助吸収器１６に導かれる。低圧再生器２２の熱交換器２４には、熱源媒体配管２５、２６が接続されている。 In the low-pressure regenerator 22, the solution whose concentration is reduced by the absorber 9 is sprayed from the spraying device 23 to the outside of the heat transfer tube of the heat exchanger 24. The dispersed solution is heated by a heat source medium flowing in the heat transfer tube of the heat exchanger 24 and separated into a concentrated solution and refrigerant vapor. The concentrated solution passes through the solution pipe 27 and joins with the solution from the high pressure regenerator 33 at the junction B (merging portion). The refrigerant vapor is guided to the auxiliary absorber 16 on the auxiliary cycle side via the eliminator 21. Heat source

medium pipes

25 and 26 are connected to the heat exchanger 24 of the low pressure regenerator 22.

　高圧再生器３３では、吸収器９で濃度の薄くなり、低温溶液熱交換器５５と高温溶液熱交換器５６で昇温された溶液が散布装置３４から熱交換器３５の伝熱管外に散布される。散布された溶液は、熱交換器３５の伝熱管内を流れる熱源媒体で加熱され、濃縮された溶液と冷媒蒸気に分離される。濃縮された溶液は、溶液配管４９の途中に設置した高温溶液熱交換器５６を通って合流点Ｂに導かれる。合流点Ｂで合流した低圧再生器２２と高圧再生器３３からの濃縮された溶液は、溶液ポンプ３０で昇圧され、低温溶液熱交換器５５を通って吸収器９に導かれる。高圧再生器３３で濃縮された溶液から分離された冷媒蒸気は、バッフル３９を介して凝縮器４０に導かれる。高圧再生器３３の熱交換器３５には、熱源媒体配管３６、３７が接続されている。 In the high pressure regenerator 33, the solution whose concentration is reduced by the absorber 9 and heated by the low temperature solution heat exchanger 55 and the high temperature solution heat exchanger 56 is sprayed from the spraying device 34 to the outside of the heat transfer tube of the heat exchanger 35. The The dispersed solution is heated by a heat source medium flowing in the heat transfer tube of the heat exchanger 35 and separated into a concentrated solution and refrigerant vapor. The concentrated solution is guided to the junction B through a high temperature solution heat exchanger 56 installed in the middle of the solution pipe 49. The concentrated solution from the low pressure regenerator 22 and the high pressure regenerator 33 that have joined at the junction B is boosted by the solution pump 30 and led to the absorber 9 through the low temperature solution heat exchanger 55. The refrigerant vapor separated from the solution concentrated by the high pressure regenerator 33 is guided to the condenser 40 through the baffle 39. Heat source

medium pipes

36 and 37 are connected to the heat exchanger 35 of the high pressure regenerator 33.

　凝縮器４０では、高圧再生器３３と補助再生器４４とで濃縮された溶液から分離された冷媒蒸気を、熱交換器４１の伝熱管内を流れる冷却水で冷却し、凝縮液化する。凝縮液化した冷媒は、冷媒配管５０を通って蒸発器１に導かれる。熱交換器４１には、冷却水配管４２、４３が接続される。 In the condenser 40, the refrigerant vapor separated from the solution concentrated in the high pressure regenerator 33 and the auxiliary regenerator 44 is cooled with cooling water flowing in the heat transfer tube of the heat exchanger 41 to be condensed and liquefied. The condensed and liquefied refrigerant is guided to the evaporator 1 through the refrigerant pipe 50. Cooling

water pipes

42 and 43 are connected to the heat exchanger 41.

　次に、補助サイクル側の動作について説明する。 Next, the operation on the auxiliary cycle side will be described.

　補助吸収器１６では、補助再生器４４で濃縮された溶液が散布装置１７から熱交換器１８の伝熱管外に散布される。散布された溶液は、単効用側サイクルの低圧再生器２２からの冷媒蒸気を吸収し濃度が薄くなった後、溶液配管２８の途中に設置された溶液ポンプ２９で中温溶液熱交換器５７を通過後に補助再生器４４に導かれる。補助吸収器１６の熱交換器１８の伝熱管内には、溶液が冷媒蒸気を吸収する際に発生する吸収熱を取り除くために冷却水が通水される。熱交換器１８には、冷却水配管１９、２０が接続されている。 In the auxiliary absorber 16, the solution concentrated in the auxiliary regenerator 44 is sprayed from the spraying device 17 to the outside of the heat transfer tube of the heat exchanger 18. The sprayed solution absorbs the refrigerant vapor from the low-pressure regenerator 22 in the single effect side cycle and decreases in concentration, and then passes through the intermediate temperature solution heat exchanger 57 by the solution pump 29 installed in the middle of the solution pipe 28. Later, it is guided to the auxiliary regenerator 44. Cooling water is passed through the heat transfer tube of the heat exchanger 18 of the auxiliary absorber 16 in order to remove absorption heat generated when the solution absorbs the refrigerant vapor. Cooling water pipes 19 and 20 are connected to the heat exchanger 18.

　補助再生器４４では、補助吸収器１６で濃度の薄くなった溶液が散布装置４５から熱交換器４６の伝熱管外に散布される。散布された溶液は、熱交換器４６の伝熱管内を流れる熱源媒体で加熱され、濃縮された溶液と冷媒蒸気に分離される。濃縮された溶液は、溶液配管５１の途中に設置した溶液ポンプ５４で、中温溶液熱交換器５７を通って補助吸収器１６に導かれる。濃縮された溶液から分離された冷媒蒸気は、バッフル５２を介して凝縮器４０に導かれる。補助再生器４４の熱交換器４６には、熱源媒体配管４７、４８が接続されている。 In the auxiliary regenerator 44, the solution whose concentration has been reduced by the auxiliary absorber 16 is sprayed from the spraying device 45 to the outside of the heat transfer tube of the heat exchanger 46. The dispersed solution is heated by a heat source medium flowing in the heat transfer tube of the heat exchanger 46, and is separated into a concentrated solution and refrigerant vapor. The concentrated solution is guided to the auxiliary absorber 16 through the intermediate temperature solution heat exchanger 57 by the solution pump 54 installed in the middle of the solution pipe 51. The refrigerant vapor separated from the concentrated solution is guided to the condenser 40 through the baffle 52. Heat source

medium pipes

47 and 48 are connected to the heat exchanger 46 of the auxiliary regenerator 44.

　熱源媒体は、例えば、高圧再生器３３の熱交換器３５、低圧再生器２２の熱交換器２４、補助再生器４４の熱交換器４６の順で通水される。このとき、図２に示すように、熱源媒体を、高圧再生器３３出口の溶液温度より高い温度（９０℃程度）から、補助再生器４４出口の溶液温度に近い温度（６０℃程度）まで利用することができる。 The heat source medium is passed through the heat exchanger 35 of the high pressure regenerator 33, the heat exchanger 24 of the low pressure regenerator 22, and the heat exchanger 46 of the auxiliary regenerator 44 in this order, for example. At this time, as shown in FIG. 2, the heat source medium is utilized from a temperature higher than the solution temperature at the outlet of the high pressure regenerator 33 (about 90 ° C.) to a temperature close to the solution temperature at the outlet of the auxiliary regenerator 44 (about 60 ° C.). can do.

　なお、本実施例においては、図１に示すように、蒸発器１では冷媒が、吸収器９、低圧再生器２２、高圧再生器３３及び補助吸収器１６、補助再生器４４では溶液が、各熱交換器上部の散布装置から散布される流下液膜式の熱交換器としている。 In the present embodiment, as shown in FIG. 1, the evaporator 1 is a refrigerant, the absorber 9, the low pressure regenerator 22, the high pressure regenerator 33 and the auxiliary absorber 16, and the auxiliary regenerator 44 is a solution. It is a falling liquid film type heat exchanger sprayed from the spraying device at the top of the heat exchanger.

　以上のように、本発明の構成は、単効用サイクル側の低圧再生器２２と補助サイクル側の補助吸収器１６との気相部を連通し、単効用サイクル側の高圧再生器３３と凝縮器４０と補助サイクル側の補助再生器４４との気相部を連通することによって、単効用サイクルと２段吸収サイクルを組合せて運転することができる。なお、本実施例においては、溶液（吸収剤）として臭化リチウム水溶液を使用し、冷媒として水を使用している。 As described above, the configuration of the present invention communicates the gas phase portion between the low-pressure regenerator 22 on the single effect cycle side and the auxiliary absorber 16 on the auxiliary cycle side, and the high-pressure regenerator 33 and condenser on the single-effect cycle side. By connecting the gas phase part of 40 and the auxiliary regenerator 44 on the auxiliary cycle side, the single effect cycle and the two-stage absorption cycle can be combined and operated. In this embodiment, an aqueous lithium bromide solution is used as the solution (absorbent), and water is used as the refrigerant.

　次に、本発明に係る構成と効果について図１及び図２で説明する。 Next, the configuration and effects according to the present invention will be described with reference to FIGS.

　吸収器９から出た溶液は、低温溶液熱交換器５５を通過後に分岐点Ａで分岐させる。これにより、図２にも示すように、低圧再生器２２には、吸収器９からの濃度の薄い溶液を流入させることができる。つまり、低圧再生器２２に流入させる溶液の温度を、高圧再生器３３出口より濃度が薄い分、低くすることができる。したがって、低圧再生器２２を駆動するための駆動熱源温度との温度差を大きく取ることができ、温度差が大きくなった分、伝熱面積を削減できる。 The solution coming out of the absorber 9 is branched at the branch point A after passing through the low temperature solution heat exchanger 55. As a result, as shown in FIG. 2, a low-concentration solution from the absorber 9 can flow into the low-pressure regenerator 22. That is, the temperature of the solution flowing into the low pressure regenerator 22 can be lowered by the amount that is lower than the outlet of the high pressure regenerator 33. Therefore, a large temperature difference from the drive heat source temperature for driving the low-pressure regenerator 22 can be taken, and the heat transfer area can be reduced by the amount of the increased temperature difference.

　また、吸収器９からの溶液を、分岐点Ａで分岐させることで、高温溶液熱交換器５６での循環量を、吸収器９からの循環量より減らすことができる。これにより、循環量に併せて高温用液熱交換器５６のサイズを小形化できるとともに、溶液の顕熱損失を低減でき、吸収式冷凍機の効率向上を図ることができる。さらに、低圧再生器２２と高圧再生器３３は、低圧再生器２２と接続する溶液配管３１の途中に設けた流量調整弁３２によって、溶液の分配量を調整できるようにした。これにより、低圧再生器２２と高圧再生器３３への溶液の散布量を任意に調整できるので、機器の配置を決定する際に、熱交換器２４、３５のサイズを散布量が調整できる範囲で自由に設定できる。 Further, by branching the solution from the absorber 9 at the branch point A, the circulation amount in the high temperature solution heat exchanger 56 can be reduced from the circulation amount from the absorber 9. Thus, the size of the high-temperature liquid heat exchanger 56 can be reduced in accordance with the circulation amount, and the sensible heat loss of the solution can be reduced, so that the efficiency of the absorption refrigerator can be improved. Furthermore, the low pressure regenerator 22 and the high pressure regenerator 33 can adjust the distribution amount of the solution by a flow rate adjusting valve 32 provided in the middle of the solution pipe 31 connected to the low pressure regenerator 22. As a result, the amount of solution applied to the low-pressure regenerator 22 and the high-pressure regenerator 33 can be arbitrarily adjusted. Therefore, when determining the arrangement of the devices, the size of the

heat exchangers

24 and 35 can be adjusted within the range in which the amount of spray can be adjusted. Can be set freely.

　また、低圧再生器２２と高圧再生器３３とで濃縮された溶液を合流点Ｂで合流し、合流点Ｂと低温溶液熱交換器５５との間に溶液ポンプ３０を配置する構成とした。これにより、高圧再生器３３からの溶液は、溶液ポンプ３０と高圧再生器３３内に溜められる溶液との液ヘッドと、低圧再生器２２との器内圧力差を利用して溶液ポンプ３０に押し込むとともに、低圧再生器２２からの溶液は、溶液ポンプ３０と低圧再生器２２内に溜められる溶液との液ヘッドを利用して溶液ポンプ３０に押し込むことができる。これにより、溶液ポンプ３０で高圧再生器３３と低圧再生器２２からの溶液を吸収器９に導くことができる。つまり、低圧再生器２２と高圧再生器３３の溶液を溶液ポンプ３０の１台で対応できるので、コスト低減とともに消費電力量を削減できる。 Further, the solution concentrated in the low pressure regenerator 22 and the high pressure regenerator 33 is merged at the merge point B, and the solution pump 30 is disposed between the merge point B and the low temperature solution heat exchanger 55. As a result, the solution from the high pressure regenerator 33 is pushed into the solution pump 30 by utilizing the pressure difference between the liquid head of the solution pump 30 and the solution stored in the high pressure regenerator 33 and the low pressure regenerator 22. At the same time, the solution from the low pressure regenerator 22 can be pushed into the solution pump 30 by using a liquid head of the solution pump 30 and the solution stored in the low pressure regenerator 22. Thus, the solution pump 30 can guide the solution from the high pressure regenerator 33 and the low pressure regenerator 22 to the absorber 9. That is, since the solution of the low pressure regenerator 22 and the high pressure regenerator 33 can be handled by one solution pump 30, it is possible to reduce the cost and the power consumption.

　上述の実施例においては、流下液膜式の熱交換器を内蔵した構成について説明したが、本発明の実施形態はこれに限定されるものではなく、１つの排熱源から低温度に達するまで熱を回収する観点から、満液式の熱交換器を内蔵した構成等においても本発明の効果を得ることができる。また、上述の実施例においては、分岐され低圧再生器に向かう溶液流路に流量調整弁を設けた流量調整手段について説明したが、本発明の実施形態はこれに限定されるものではなく、高圧再生器に向かう溶液流路に流量調整弁を設けた構成としてもよいし、弁を設けずに、分岐部の下流側の２つの溶液流路にあらかじめ設定した適切な流路抵抗を設けた構成としてもよい。 In the above-described examples, the configuration including the falling film type heat exchanger is described. However, the embodiment of the present invention is not limited to this, and heat is generated from one exhaust heat source until the temperature reaches a low temperature. From the viewpoint of collecting the effect, the effect of the present invention can be obtained even in a configuration in which a full-liquid heat exchanger is incorporated. Further, in the above-described embodiment, the flow rate adjusting means provided with the flow rate adjusting valve in the solution flow path branched and directed to the low pressure regenerator has been described. However, the embodiment of the present invention is not limited to this, and the high pressure It is good also as a structure which provided the flow volume adjustment valve in the solution flow path which goes to a regenerator, and the structure which provided the appropriate flow path resistance previously set to two solution flow paths downstream of a branch part without providing a valve It is good.

　１：蒸発器、２、１０、１７、２３、３４、４５：散布装置、３、１１、１８、２４、３５、４１、４６：熱交換器、４、５：冷水配管、６：冷媒ポンプ、７、５０：冷媒配管、８、２１：エリミネータ、９：吸収器、１２，１３、１９、２０、４２、４３：冷却水配管、１４、２９、３０、５４：溶液ポンプ、１５、２７、２８、３１、４９、５１：溶液配管、１６：補助吸収器、２２：低圧再生器、２５、２６、３６、３７、４７，４８：熱源媒体配管、３２：流量調整弁、３３：高圧再生器、３９、５２：バッフル、４０：凝縮器、４４：補助再生器、５５：低温溶液熱交換器、５６：高温溶液熱交換器、５７：中温溶液熱交換器。 1:

Evaporator

2, 10, 17, 23, 34, 45: Spreading

device

3, 11, 18, 24, 35, 41, 46: Heat exchanger 4, 5: Cold water piping, 6: Refrigerant pump, 7, 50: Refrigerant piping, 8, 21: Eliminator, 9: Absorber, 12, 13, 19, 20, 42, 43: Cooling water piping, 14, 29, 30, 54: Solution pump, 15, 27, 28 31, 49, 51: solution piping, 16: auxiliary absorber, 22: low pressure regenerator, 25, 26, 36, 37, 47, 48: heat source medium piping, 32: flow control valve, 33: high pressure regenerator, 39, 52: Baffle, 40: Condenser, 44: Auxiliary regenerator, 55: Cold solution heat exchanger, 56: Hot solution heat exchanger, 57: Medium solution heat exchanger.

Claims

　蒸発器と、吸収器と、低圧再生器と、高圧再生器と、補助吸収器と、補助再生器と、凝縮器と、溶液ポンプと、を備え、
　前記蒸発器と前記吸収器とは、気相部が連通し、
　前記低圧再生器と前記補助吸収器とは、気相部が連通し、
　前記高圧再生器と前記補助再生器と前記凝縮器とは、気相部が連通し、
　前記吸収器から前記高圧再生器に向かう溶液配管は、分岐部を有し、この分岐部には、前記低圧再生器に向かう溶液配管が連結され、
　前記溶液ポンプは、前記吸収器から前記分岐部に向かう前記溶液配管に設けられ、
　前記高圧再生器から前記吸収器に向かう溶液配管は、前記低圧再生器からの溶液配管と連結された合流部を有する、吸収式冷凍機。 An evaporator, an absorber, a low pressure regenerator, a high pressure regenerator, an auxiliary absorber, an auxiliary regenerator, a condenser, and a solution pump;
The vaporizer and the absorber communicate with each other in a gas phase part,
The low-pressure regenerator and the auxiliary absorber communicate with the gas phase part,
The high-pressure regenerator, the auxiliary regenerator, and the condenser are in communication with a gas phase part,
The solution pipe from the absorber to the high pressure regenerator has a branch part, and the solution pipe to the low pressure regenerator is connected to the branch part,
The solution pump is provided in the solution pipe from the absorber toward the branch portion,
The absorption refrigerating machine, wherein the solution pipe from the high-pressure regenerator to the absorber has a junction connected to the solution pipe from the low-pressure regenerator.
　前記分岐部から前記低圧再生器に向かう前記溶液配管には、流量調整手段が設けられている、請求項１記載の吸収式冷凍機。 The absorption refrigerating machine according to claim 1, wherein a flow rate adjusting means is provided in the solution pipe from the branch part to the low pressure regenerator.
　前記蒸発器、前記吸収器、前記低圧再生器、前記高圧再生器、前記補助吸収器及び前記補助再生器は、流下液膜式の熱交換器を有する、請求項１又は２に記載の吸収式冷凍機。 The absorption type according to claim 1 or 2, wherein the evaporator, the absorber, the low-pressure regenerator, the high-pressure regenerator, the auxiliary absorber, and the auxiliary regenerator include a falling liquid film type heat exchanger. refrigerator.
　前記合流部から前記吸収器に向かう前記溶液配管には、溶液ポンプが設けられている、請求項１～３のいずれか一項に記載の吸収式冷凍機。 The absorption refrigerator according to any one of claims 1 to 3, wherein a solution pump is provided in the solution pipe from the junction to the absorber.
　前記吸収器から前記分岐部に向かう前記溶液配管と、前記合流部から前記吸収器に向かう前記溶液配管と、が熱交換をする低温溶液熱交換器が設けられている、請求項１～４のいずれか一項に記載の吸収式冷凍機。 The low-temperature solution heat exchanger for exchanging heat between the solution pipe from the absorber toward the branch part and the solution pipe from the junction to the absorber is provided. The absorption refrigerator as described in any one of Claims.
　前記高圧再生器から前記合流部に向かう前記溶液配管と、前記分岐部から前記高圧再生器に向かう前記溶液配管と、が熱交換をする高温溶液熱交換器が設けられている、請求項１～５のいずれか一項に記載の吸収式冷凍機。 A high-temperature solution heat exchanger is provided in which the solution pipe from the high-pressure regenerator to the junction and the solution pipe from the branch to the high-pressure regenerator exchange heat. The absorption refrigerator according to any one of 5.
　前記補助吸収器から前記補助再生器に向かう溶液配管と、前記補助再生器から前記補助吸収器に向かう溶液配管と、が熱交換をする中温溶液熱交換器が設けられている、請求項１～６のいずれか一項に記載の吸収式冷凍機。 An intermediate temperature solution heat exchanger is provided in which a solution pipe from the auxiliary absorber to the auxiliary regenerator and a solution pipe from the auxiliary regenerator to the auxiliary absorber exchange heat. The absorption refrigerator as described in any one of Claims 6.