JPH0545019A - Absorption freezer - Google Patents
Absorption freezerInfo
- Publication number
- JPH0545019A JPH0545019A JP3230796A JP23079691A JPH0545019A JP H0545019 A JPH0545019 A JP H0545019A JP 3230796 A JP3230796 A JP 3230796A JP 23079691 A JP23079691 A JP 23079691A JP H0545019 A JPH0545019 A JP H0545019A
- Authority
- JP
- Japan
- Prior art keywords
- absorption
- solution
- steam turbine
- condenser
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、吸収冷凍機に係り、特
に復水式蒸気タービンコージェネレーションシステムに
おける電力と冷熱の効率化とコトスダウンを実現できる
吸収冷凍機に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an absorption refrigerating machine, and more particularly to an absorption refrigerating machine capable of improving efficiency of electric power and cold heat and reducing cost in a condensing steam turbine cogeneration system.
【０００２】[0002]
【従来の技術】従来、ボイラ、蒸気タービン、吸収冷凍
機からなるコージェネレーションシステムでは８ｋｇ／
ｃｍ2 Ｇの蒸気を蒸気タービンより抽気し、蒸気を再生
器の熱源として用いる二重効用吸収冷凍機により、冷水
を得ていた。上記の方式では冷水容量を多くするために
は、蒸気タービンの抽気量を増加させなければならず、
発電電力が減少する。一方、蒸気を抽気せずに、復水器
の圧力は０．６ｋｇ／ｃｍ2 ａｂｓ程度にして復水器よ
り８０℃の温水を取り出すことは可能である。８０℃の
温水を再生器の熱源とする吸収冷凍機は、太陽熱利用や
ディーゼルエンジンやガスエンジンのシリンダジャケッ
ト冷却水の排熱利用として実用化しているが、いずれも
小規模なものにとどまっている。その理由は、吸収冷凍
機の再生器における温水加熱部の伝熱面積が、蒸気加熱
方式の吸収冷凍機に比べて大きなスペースを要し、ひい
ては重量の増加を招き、大型化が困難であったためであ
る。2. Description of the Related Art Conventionally, a cogeneration system consisting of a boiler, a steam turbine and an absorption refrigerator has a capacity of 8 kg /
Cold water was obtained by a double-effect absorption refrigerating machine using the steam of cm 2 G extracted from a steam turbine and using the steam as a heat source of a regenerator. In the above method, in order to increase the chilled water capacity, it is necessary to increase the extraction amount of the steam turbine,
Generated power is reduced. On the other hand, without extracting steam, it is possible to take hot water at 80 ° C. from the condenser with the pressure of the condenser set to about 0.6 kg / cm 2 abs. Absorption refrigerators that use hot water of 80 ° C as the heat source for the regenerator have been put to practical use as solar heat utilization and exhaust heat utilization of cylinder jacket cooling water for diesel engines and gas engines, but they are all small scale. .. The reason is that the heat transfer area of the hot water heating unit in the regenerator of the absorption chiller requires a larger space than that of the steam chiller type absorption chiller, which in turn increases the weight and makes it difficult to increase the size. Is.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、上記のよう
な従来技術の問題点を解消し、復水式蒸気タービンの復
水器を熱源として、吸収冷凍機再生器の寸法、重量が減
少し、大型化が可能な吸収冷凍機を提供することを課題
とする。SUMMARY OF THE INVENTION The present invention solves the problems of the prior art as described above, and reduces the size and weight of the absorption chiller regenerator by using the condenser of the condensing steam turbine as a heat source. However, it is an object to provide an absorption refrigerator that can be upsized.
【０００４】[0004]
【課題を解決するための手段】上記課題を解決するため
に、本発明では、復水式蒸気タービンの排熱を用いる吸
収冷凍機において、吸収冷凍機の希溶液を復水式蒸気タ
ービンの復水器に設けた熱交換器に導入し、熱交換器か
ら出る加熱された希溶液を吸収冷凍機の再生器に導くよ
うに構成したことを特徴とする吸収冷凍機としたもので
ある。上記吸収冷凍機において、使用する希溶液は低濃
度ＬｉＢｒ水溶液を用いるのがよい。In order to solve the above problems, in the present invention, in an absorption refrigerator using the exhaust heat of a condensing steam turbine, the dilute solution of the absorption refrigerator is condensed in the condensing steam turbine. This is an absorption refrigerating machine characterized by being introduced into a heat exchanger provided in a water vessel and guiding a heated dilute solution discharged from the heat exchanger to a regenerator of the absorption refrigerating machine. In the absorption refrigerator, the dilute solution used is preferably a low-concentration LiBr aqueous solution.
【０００５】[0005]
【作用】本発明は、再生器におけるＬｉＢｒ水溶液等の
希溶液の温水加熱のかわりに、ＬｉＢｒ溶液を蒸気ター
ビン復水器へ直接導き加熱するものであり、温水を介在
させることなく、ＬｉＢｒ水溶液を加熱することができ
るので、吸収冷凍機再生器の寸法、重量が減少し、吸収
冷凍機の大型化が可能となる。According to the present invention, instead of heating a dilute solution such as a LiBr aqueous solution in a regenerator with hot water, the LiBr solution is directly introduced into a steam turbine condenser and heated, and the LiBr aqueous solution is heated without interposing hot water. Since it can be heated, the size and weight of the absorption chiller regenerator are reduced and the absorption chiller can be upsized.
【０００６】[0006]
【実施例】以下、本発明を実施例により具体的に説明す
るが、本発明はこの実施例に限定されるものではない。 実施例１ 図１に本発明の吸収冷凍機のフロー工程図を示す。復水
蒸気タービンは、ボイラ１から発生する高圧蒸気を蒸気
タービン２へ導き、蒸気エネルギーを動力エネルギへ変
換し、発電機３により電気エネルギーが得られる。復水
タービンでは、蒸気タービンの出口蒸気を復水器４へ導
き、冷却水により凝縮させ、蒸気を復水の状態に変え
る。復水された水は、復水ポンプ６により、復水タンク
７へ送られ、ボイラ給水ポンプ８により昇圧され、再び
ボイラ１へ戻る。このサイクルはランキンサイクルと呼
ばれているものである。通常、復水器４への冷却水には
水が使用されるが、本発明は水のかわりに吸収冷凍機の
低濃度ＬｉＢｒ溶液２２を使用する。EXAMPLES The present invention will be specifically described below with reference to examples, but the present invention is not limited to these examples. Example 1 FIG. 1 shows a flow process diagram of an absorption refrigerator according to the present invention. The condensing steam turbine guides high-pressure steam generated from the boiler 1 to the steam turbine 2, converts steam energy into motive energy, and the generator 3 obtains electric energy. In the condensing turbine, the outlet steam of the steam turbine is guided to the condenser 4 and condensed by the cooling water to change the steam into the condensing state. Condensed water is sent to the condensate tank 7 by the condensate pump 6, is pressurized by the boiler feed water pump 8, and returns to the boiler 1 again. This cycle is called Rankin cycle. Normally, water is used as the cooling water to the condenser 4, but the present invention uses the low-concentration LiBr solution 22 of the absorption refrigerator in place of water.
【０００７】吸収式冷凍機の吸収器２１には、低濃度Ｌ
ｉＢｒ溶液２２があり、溶液ポンプ２４により加圧し、
復水器４の中に設置した熱交換器５へ送られる。復水器
４の圧力は０．６ｋｇ／ｃｍ2 ａｂｓ程度に保つと、出
口蒸気の凝縮温度は８５℃程度となる。一方、吸収式冷
凍機の冷水３４の温度は７℃程度であるので、低濃度Ｌ
ｉＢｒ溶液２２の温度は１０℃程度になる。熱交換器５
の伝熱面積及び溶液ポンプ２４の吐出量を適正に定める
と、熱交換器５出口の低濃度ＬｉＢｒ溶液２２の温度は
約８０℃となる。復水器４により、加温された低濃度Ｌ
ｉＢｒ溶液２２は再生器２５の中に設置されたＬｉＢｒ
溶液散水ノズル２６により、充填剤２７の上に、均一に
散布される。充填剤２７の中を滴下することにより低濃
度ＬｉＢｒ溶液２２の中の水分は蒸発し、凝縮器３５に
おいて冷却水２３と熱交換することにより、再び水にか
わる。The absorber 21 of the absorption refrigerator has a low concentration L.
There is an iBr solution 22, which is pressurized by a solution pump 24,
It is sent to the heat exchanger 5 installed in the condenser 4. If the pressure of the condenser 4 is maintained at about 0.6 kg / cm 2 abs, the condensation temperature of the outlet steam becomes about 85 ° C. On the other hand, since the temperature of the cold water 34 of the absorption refrigerator is about 7 ° C., the low concentration L
The temperature of the iBr solution 22 becomes about 10 ° C. Heat exchanger 5
When the heat transfer area and the discharge amount of the solution pump 24 are properly determined, the temperature of the low-concentration LiBr solution 22 at the outlet of the heat exchanger 5 becomes about 80 ° C. Low concentration L heated by the condenser 4
The iBr solution 22 is LiBr installed in the regenerator 25.
The solution spray nozzle 26 sprays the filler 27 evenly. Moisture in the low-concentration LiBr solution 22 is evaporated by dropping the filler 27, and heat is exchanged with the cooling water 23 in the condenser 35, so that the water is replaced with water again.
【０００８】凝縮器２９の水（冷媒）は、蒸発器３１へ
導かれ、冷水３４と熱交換することにより、再び蒸気と
なる。再生器２５より送られた高濃度ＬｉＢｒ溶液２８
は冷却水２３と熱交換することにより蒸発器３１より発
生した蒸気を吸収し、再び低濃度ＬｉＢｒ溶液となる。
吸収冷凍機の成績係数向上のために、溶液熱交換器３０
により熱回収を行う。上述の構成は、吸収冷凍機サイク
ルを記述したものであり、ＬｉＢｒ溶液の加熱に復水タ
ービンの復水器４及び熱交換器５を用い、再生器におけ
るＬｉＢｒ溶液の濃縮に滴下方式を用いることを特徴と
している。The water (refrigerant) in the condenser 29 is introduced into the evaporator 31 and exchanges heat with the cold water 34 to become steam again. High concentration LiBr solution 28 sent from regenerator 25
Heat-exchanges with the cooling water 23 to absorb the vapor generated from the evaporator 31 and become a low-concentration LiBr solution again.
In order to improve the coefficient of performance of the absorption refrigerator, the solution heat exchanger 30
To recover heat. The above-mentioned configuration describes the absorption refrigeration cycle, and the condenser 4 and the heat exchanger 5 of the condensing turbine are used for heating the LiBr solution, and the dropping method is used for concentrating the LiBr solution in the regenerator. Is characterized by.
【０００９】上記図１の本発明の復水上記タービン方式
と従来方式である背圧蒸気タービンとの電力、冷熱の出
力と効率について試算例を表１に示す。同一のボイラ入
熱量に対して発生する電力は復水タービン方式が背圧タ
ービン方式を上回り、逆に冷熱は蒸気二重効用吸収冷凍
機を用いる背圧タービン方式が、単効用吸収冷凍機を用
いる本発明の構成方式を上回る。試算例のエネルギー効
率は、背圧タービン方式において９４．３％、復水ター
ビン方式においても５５．２％であり、復水タービン方
式は著しく劣るように見える。しかし、エクセルギー効
率で比較すると、背圧タービン方式が１３．７％である
のに対して、復水タービン方式は２０．９％となり、エ
クセルギーの面からみると、復水タービン方式による電
力、冷熱の優位性は明らかである。Table 1 shows an example of trial calculation of electric power, cold heat output and efficiency of the above-mentioned turbine system of the present invention shown in FIG. 1 and a conventional back pressure steam turbine. Condensate turbine method exceeds the back pressure turbine method for electric power generated for the same boiler heat input, and conversely, for cold heat, the steam double effect absorption refrigerator uses a double effect absorption refrigerator.The back pressure turbine method uses a single effect absorption refrigerator. It exceeds the configuration method of the present invention. The energy efficiency of the trial calculation example is 94.3% in the back pressure turbine system and 55.2% in the condensing turbine system, and the condensing turbine system seems to be remarkably inferior. However, in comparison with exergy efficiency, the back pressure turbine method is 13.7%, whereas the condensing turbine method is 20.9%. , The superiority of cold heat is clear.
【００１０】[0010]
【表１】 エネルギー効率＝（電力＋冷熱）／ボイラ入熱量 エクセルギー効率＝電力／ボイラ入熱量＋（冷熱／ボイ
ラ入熱量） ×〔１−（２７３＋Ｔ2 ）／（２７３＋Ｔ1 ）〕 ここで、 Ｔ1 ： 気 温 夏３２℃とする Ｔ2 ： 冷熱温度 ７℃とする[Table 1] Energy efficiency = (electric power + cold heat) / boiler heat input Exergy efficiency = power / boiler heat input + (cold heat / boiler heat input) x [1- (273 + T 2 ) / (273 + T 1 )] where T 1 : and cold temperature 7 ° C.: T 2 to the temperature summer 32 ° C.
【００１１】[0011]
【発明の効果】本発明によれば、吸収冷凍機の再生器の
熱交換部分の小型化が可能となり、エクセルギー効率が
優れていても、経済性に難点がある復水蒸気タービン発
電と単効用吸収冷凍機の組合わせからなるコージェネレ
ーションシステムの普及に寄与することができる。According to the present invention, the heat exchange portion of the regenerator of the absorption refrigerator can be downsized, and even if the exergy efficiency is excellent, there is a disadvantage in economic efficiency in the recuperative steam turbine power generation and single-effect. It is possible to contribute to the spread of a cogeneration system including a combination of absorption refrigerators.
【図１】本発明の吸収冷凍機のフロー工程図である。FIG. 1 is a flow process diagram of an absorption refrigerator according to the present invention.
１：ボイラ、２：蒸気タービン、３：発電機、４：復水
器、５：熱交換器、６：復水ポンプ、７：復水タンク、
８：ボイラ給水ポンプ、２１：吸収器、２２：低濃度Ｌ
ｉＢｒ溶液、２３：冷却水、２４：溶液ポンプ、２５：
再生器、２６：ＬｉＢｒ溶液散水ノズル、２７：充填
剤、２８：高濃度ＬｉＢｒ溶液、２９：凝縮器、３０：
溶液熱交換機、３１：蒸発器、３２：冷媒液体（水）、
３３：冷媒ポンプ、３４：冷水、３５：凝縮器1: Boiler, 2: Steam turbine, 3: Generator, 4: Condenser, 5: Heat exchanger, 6: Condensate pump, 7: Condensate tank,
8: Boiler feed pump, 21: Absorber, 22: Low concentration L
iBr solution, 23: cooling water, 24: solution pump, 25:
Regenerator, 26: LiBr solution water spray nozzle, 27: Filler, 28: High concentration LiBr solution, 29: Condenser, 30:
Solution heat exchanger, 31: evaporator, 32: refrigerant liquid (water),
33: Refrigerant pump, 34: Cold water, 35: Condenser
Claims (2)
冷凍機において、吸収冷凍機の希溶液を復水式蒸気ター
ビンの復水器に設けた熱交換器に導入し、熱交換器から
出る加熱された希溶液を吸収冷凍機の再生器に導くよう
に構成したことを特徴とする吸収冷凍機。1. In an absorption refrigerator using exhaust heat of a condensing steam turbine, a dilute solution of the absorption refrigerator is introduced into a heat exchanger provided in a condenser of the condensing steam turbine, and the diluted solution is introduced from the heat exchanger. An absorption refrigerator, which is configured so that the heated diluted solution that emerges is guided to a regenerator of the absorption refrigerator.
液を用いる請求項１記載の吸収冷凍機。2. The absorption refrigerator according to claim 1, wherein a low-concentration LiBr aqueous solution is used as the dilute solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3230796A JPH0545019A (en) | 1991-08-19 | 1991-08-19 | Absorption freezer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3230796A JPH0545019A (en) | 1991-08-19 | 1991-08-19 | Absorption freezer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0545019A true JPH0545019A (en) | 1993-02-23 |
Family
ID=16913411
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3230796A Pending JPH0545019A (en) | 1991-08-19 | 1991-08-19 | Absorption freezer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0545019A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995034789A1 (en) * | 1994-06-10 | 1995-12-21 | Tokyo Gas Co., Ltd. | Absorption water chiller/heater and method of controlling same |
| US5607795A (en) * | 1995-01-26 | 1997-03-04 | Nec Corporation | Battery terminals of miniature electronic apparatus and structure for retaining the same |
| US5863674A (en) * | 1996-05-14 | 1999-01-26 | Nec Corporation | Battery terminals for a miniature electronic apparatus and structure for holding the same |
| JP2010276304A (en) * | 2009-05-29 | 2010-12-09 | Ebara Corp | Steam generation system |
-
1991
- 1991-08-19 JP JP3230796A patent/JPH0545019A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995034789A1 (en) * | 1994-06-10 | 1995-12-21 | Tokyo Gas Co., Ltd. | Absorption water chiller/heater and method of controlling same |
| US5607795A (en) * | 1995-01-26 | 1997-03-04 | Nec Corporation | Battery terminals of miniature electronic apparatus and structure for retaining the same |
| US5863674A (en) * | 1996-05-14 | 1999-01-26 | Nec Corporation | Battery terminals for a miniature electronic apparatus and structure for holding the same |
| JP2010276304A (en) * | 2009-05-29 | 2010-12-09 | Ebara Corp | Steam generation system |
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