JPH08261591A - Vapor boiling absorption hot or chilled water generator and controlling method therefor - Google Patents

Vapor boiling absorption hot or chilled water generator and controlling method therefor

Info

Publication number
JPH08261591A
JPH08261591A JP7065373A JP6537395A JPH08261591A JP H08261591 A JPH08261591 A JP H08261591A JP 7065373 A JP7065373 A JP 7065373A JP 6537395 A JP6537395 A JP 6537395A JP H08261591 A JPH08261591 A JP H08261591A
Authority
JP
Japan
Prior art keywords
solution
heat exchanger
high temperature
temperature regenerator
pressure
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.)
Granted
Application number
JP7065373A
Other languages
Japanese (ja)
Other versions
JP3240343B2 (en
Inventor
Masahiko Oshima
正彦 大島
Masaharu Nomaki
正治 野牧
Masahiko Atsumi
雅彦 渥美
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Yazaki Corp
Original Assignee
Yazaki Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Yazaki Corp filed Critical Yazaki Corp
Priority to JP06537395A priority Critical patent/JP3240343B2/en
Publication of JPH08261591A publication Critical patent/JPH08261591A/en
Application granted granted Critical
Publication of JP3240343B2 publication Critical patent/JP3240343B2/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

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Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00Adapting or protecting infrastructure or their operation
    • Y02A30/27Relating to heating, ventilation or air conditioning [HVAC] technologies
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02BCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62Absorption based systems

Landscapes

  • Sorption Type Refrigeration Machines (AREA)

Abstract

PURPOSE: To effectively use the vapor of low pressure by providing control means for switching a solution bypass valve provided in a bypass circuit for bypassing intermediate concentration solution separated by a separator via a low-temperature regenerator to introduce it into an absorber according to the pressure of vapor supplied to a high-temperature regenerator. CONSTITUTION: When there is pressure in which dual effect operation is impossible due to a pressure drop but single effect cooling operation is possible, control means opens a solution bypass valve 11, closes a solution bypass valve 13 and introduces concentrated solution to the cooling water surface of an absorber 44. If a refrigerant vapor bypass valve is attached, the bypass valve is opened, and hence the refrigerant vapor is introduced to a condenser 26 without being disturbed by a throttle due to the dual effect cooling operation. Accordingly, even if the pressure of a high- temperature regenerator 10 is lower tan the dual effect cooling operation, it flows to the condenser 26. The solution forms the single effect cooling operation by switching the bypass valve, but since it is not passed through the throttle at the time of double effect cooling operation and it is not necessary to supply to a low-temperature regenerator 22, the solution can be circulated by the pressure of a high-temperature regenerator 1. Therefore, the single effect cooling can be performed.

Description

【発明の詳細な説明】Detailed Description of the Invention

【0001】[0001]

【産業上の利用分野】本発明は、蒸気焚き吸収冷温水機
とその制御方法に係り、特に低圧力蒸気の有効利用に配
慮した蒸気焚き吸収冷温水機とその制御方法に関する。
BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a steam-fired absorption chiller-heater and its control method, and more particularly to a steam-fired absorption chiller-heater and its control method in consideration of effective use of low-pressure steam.

【0002】[0002]

【従来の技術】従来、水蒸気を高温再生器の加熱源とす
る蒸気焚き吸収冷温水機において、加熱源である蒸気の
圧力が低下して二重効用運転が不可能な圧力になった場
合、吸収冷温水機へ蒸気を供給する蒸気回路に設けた蒸
気遮断弁を閉じ、高温再生器への蒸気の供給を停止する
とともに吸収冷温水機の運転を停止させ、サイクルの異
常(吸収溶液循環の不具合による晶析、吸収溶液の冷媒
への混入)を防止していた。図9に、蒸気回路に蒸気遮
断弁を設けた蒸気焚き吸収冷温水機の系統構成の例を示
す。
2. Description of the Related Art Conventionally, in a steam-fired absorption chiller-heater using steam as a heating source for a high-temperature regenerator, when the pressure of steam as a heating source is lowered to a pressure that prevents double-effect operation, The steam cutoff valve provided in the steam circuit that supplies steam to the absorption chiller-heater is closed, the supply of steam to the high-temperature regenerator is stopped, and the operation of the absorption chiller-heater is stopped. This prevented crystallization due to defects and mixing of the absorbing solution with the refrigerant. FIG. 9 shows an example of the system configuration of a steam-fired absorption chiller-heater having a steam cutoff valve in the steam circuit.

【0003】[0003]

【発明が解決しようとする課題】しかし、上記従来技術
においては、蒸気の圧力が、二重効用冷房運転は不可能
であるが単効用(一重効用)冷房運転なら可能な圧力の
場合も、吸収冷温水機の運転を停止させることになり、
蒸気の利用の効率を低下させていた。また、蒸気遮断弁
がリークした場合の、蒸気の熱による吸収溶液の晶析
(吸収冷温水機は停止しているため、溶液循環ポンプは
停止しており、蒸気が高温再生器に漏れ込むと、高温再
生器内の吸収溶液の濃縮が進行する。)や、蒸気遮断弁
及びその制御機器設置のためのシステム全体としてのイ
ニシャルコストの増加が避けられなかった。
However, in the above-mentioned prior art, even when the pressure of the steam is such that the double-effect cooling operation is impossible but the single-effect (single-effect) cooling operation allows the pressure to be absorbed, I will stop the operation of the water heater
It reduced the efficiency of steam utilization. Also, when the vapor cutoff valve leaks, the crystallization of the absorption solution due to the heat of the vapor (Because the absorption chiller / heater is stopped, the solution circulation pump is stopped, and the steam leaks into the high temperature regenerator. , And the concentration of the absorption solution in the high temperature regenerator progresses.), And an increase in the initial cost of the system as a whole for installing the vapor cutoff valve and its control equipment was unavoidable.

【0004】本発明の目的は、蒸気焚き二重効用吸収冷
温水機において、二重効用冷房運転が不可能な低い圧力
の蒸気を有効に利用するとともに、イニシャルコストを
増加させることなく、蒸気もれによる吸収溶液の濃縮を
防止するにある。
An object of the present invention is to effectively use low-pressure steam that cannot perform double-effect cooling operation in a steam-fired double-effect absorption chiller-heater, and to increase steam without increasing the initial cost. This is to prevent the absorption solution from concentrating.

【0005】[0005]

【課題を解決するための手段】上記目的は、高温再生器
と、分離器と、低温再生器と、凝縮器と、蒸発器と、吸
収器と、前記分離器に中間濃溶液管を介して加熱流体入
り側を接続させた高温溶液熱交換器と、この高温溶液熱
交換器の加熱流体出側と前記低温再生器を接続する中間
濃溶液管と、前記低温再生器に濃溶液管を介して加熱流
体入り側を接続させた低温溶液熱交換器と、この低温溶
液熱交換器の加熱流体出側と前記吸収器を接続した濃溶
液管と、前記吸収器の希溶液を前記低温溶液熱交換器及
び高温溶液熱交換器の被加熱流体側を経て前記高温再生
器に送りこむ溶液循環ポンプと、を含んでなる蒸気焚き
吸収冷温水機において、前記分離器で分離された中間濃
溶液を低温再生器をバイパスして吸収器に導く第1のバ
イパス回路を設けるとともに、この第1のバイパス回路
に設けられた溶液バイパス弁Aを高温再生器に供給され
る蒸気の圧力の高低に応じて開閉する制御手段を設ける
ことによって達成される。
The above object is to provide a high temperature regenerator, a separator, a low temperature regenerator, a condenser, an evaporator, an absorber, and the separator via an intermediate concentrated solution pipe. A high temperature solution heat exchanger connected to the heating fluid inlet side, an intermediate concentrated solution pipe connecting the heating fluid outlet side of the high temperature solution heat exchanger and the low temperature regenerator, and a concentrated solution pipe to the low temperature regenerator. A low temperature solution heat exchanger connected to the heating fluid inlet side, a concentrated solution pipe connecting the heating fluid outlet side of the low temperature solution heat exchanger and the absorber, and a dilute solution of the absorber to the low temperature solution heat exchanger. In a steam-fired absorption chiller-heater comprising a exchanger and a solution circulation pump that feeds into the high temperature regenerator via the heated fluid side of the high temperature solution heat exchanger, the intermediate concentrated solution separated by the separator is cooled to a low temperature. Providing a first bypass circuit that bypasses the regenerator and leads to the absorber Together, it is achieved by providing a control means for opening and closing in response to the high and low pressure steam supplied to the solution bypass valve A provided in the first bypass circuit in the high temperature regenerator.

【0006】この第1のバイパス回路は、例えば、高温
溶液熱交換器の加熱流体入り側と低温溶液熱交換器の加
熱流体入り側もしくは出側を溶液バイパス弁Aを介して
接続するものとしてもよいし、高温溶液熱交換器の加熱
流体出側と低温溶液熱交換器の加熱流体入り側もしくは
出側を溶液バイパス弁Aを介して接続するものでもよ
い。
In this first bypass circuit, for example, the heating fluid inlet side of the high temperature solution heat exchanger and the heating fluid inlet side or outlet side of the low temperature solution heat exchanger may be connected via a solution bypass valve A. Alternatively, the heating fluid outlet side of the high temperature solution heat exchanger and the heating fluid inlet side or outlet side of the low temperature solution heat exchanger may be connected via the solution bypass valve A.

【0007】さらに、前記第1のバイパス回路に加え、
低温溶液熱交換器の加熱流体出側と前記吸収器を接続す
る濃溶液管と蒸発器底部もしくは吸収器の底部を溶液バ
イパス弁Bを介して接続する第2のバイパス回路を設
け、前記制御手段を高温再生器に供給される蒸気の圧力
の高低に応じて前記溶液バイパス弁A,Bを開閉するも
のとしてもよい。また、第2のバイパス回路を、低温溶
液熱交換器の加熱流体出側と溶液循環ポンプの吸入側を
溶液バイパス弁Bを介して連通するものとしてもよい。
Further, in addition to the first bypass circuit,
The concentrated solution pipe connecting the heating fluid outlet of the low temperature solution heat exchanger and the absorber and the second bypass circuit connecting the bottom of the evaporator or the bottom of the absorber via the solution bypass valve B are provided, and the control means is provided. The solution bypass valves A and B may be opened / closed according to the pressure level of the steam supplied to the high temperature regenerator. Further, the second bypass circuit may connect the heating fluid outlet side of the low temperature solution heat exchanger and the suction side of the solution circulation pump via the solution bypass valve B.

【0008】さらに、前記第1,第2のバイパス回路に
加え、前記分離器の気相部と前記凝縮器を冷媒蒸気バイ
パス弁を介して連通する冷媒蒸気バイパス回路を設け、
前記制御回路を高温再生器に供給される蒸気の圧力の高
低に応じて前記溶液バイパス弁A,B及び冷媒蒸気バイ
パス弁を開閉するものとしてもよい。冷媒蒸気バイパス
回路を設ける代りに、低温再生器に内装された冷媒蒸気
コイルに、該冷媒蒸気コイル内を流れる冷媒の温度に応
じて流路断面積が変更される冷媒制御弁を設けてもよ
い。
Further, in addition to the first and second bypass circuits, a refrigerant vapor bypass circuit is provided which connects the vapor phase portion of the separator and the condenser via a refrigerant vapor bypass valve,
The control circuit may be configured to open and close the solution bypass valves A and B and the refrigerant vapor bypass valve according to the pressure level of the vapor supplied to the high temperature regenerator. Instead of providing the refrigerant vapor bypass circuit, the refrigerant vapor coil incorporated in the low-temperature regenerator may be provided with a refrigerant control valve whose flow passage cross-sectional area is changed according to the temperature of the refrigerant flowing in the refrigerant vapor coil. .

【0009】また、前記制御手段を、高温再生器内の吸
収溶液の温度の高低に応じて溶液バイパス弁A,B及び
冷媒蒸気バイパス弁の開閉を制御するものとしてもよ
い。
Further, the control means may control the opening / closing of the solution bypass valves A and B and the refrigerant vapor bypass valve according to the temperature of the absorbing solution in the high temperature regenerator.

【0010】[0010]

【作用】高温再生器に供給される蒸気の圧力が二重効用
冷房運転可能な圧力を維持している場合、制御手段は、
溶液バイパス弁A,Bをともに閉とし、通常の二重効用
運転のサイクルが維持される。冷媒蒸気バイパス弁が設
けられている場合は、冷媒蒸気バイパス弁も閉に維持さ
れる。
When the pressure of the steam supplied to the high temperature regenerator maintains a pressure capable of double-effect cooling operation, the control means:
The solution bypass valves A and B are both closed, and the normal double-effect operation cycle is maintained. When the refrigerant vapor bypass valve is provided, the refrigerant vapor bypass valve is also kept closed.

【0011】蒸気圧力が低下して二重効用運転は不可能
であるが一重効用(単効用)冷房運転可能な圧力を維持
している場合、制御手段は、溶液バイパス弁Aを開、溶
液バイパス弁Bを閉とし、中間濃溶液を、低温再生器を
バイパスして吸収器の冷却水伝熱面上に導く。冷媒蒸気
バイパス弁が設けられている場合は、冷媒蒸気バイパス
弁も開かれる。冷媒蒸気バイパス弁が開かれることで、
分離器で分離された冷媒蒸気は、二重効用冷房運転のた
めに冷媒蒸気コイルに設けられた絞り部に妨げられるこ
となく凝縮器に導かれるので、高温再生器の圧力が二重
効用冷房運転の場合に比して低くても、容易に凝縮器に
流入できる。前記溶液バイパス弁の開閉により、吸収溶
液は単効用冷房運転のサイクルを形成するが、二重効用
冷房運転時の高温再生器と低温再生器間の圧力差を調整
する絞り部を通らず、また、高い位置にある低温再生器
へ吸収溶液を流入させる必要もないため、低圧蒸気によ
る加熱で高温再生器に形成される圧力で十分吸収溶液を
分離器から吸収器に循環させることができる。吸収溶液
が十分に循環するため、溶液循環不足による晶析、溶液
の分離器内での滞留による冷媒への混入等の不具合がな
くなり、溶液サイクルが正常に作動し、単効用運転での
冷房が可能となる。
When the vapor pressure is lowered and the double-effect operation is impossible, but when the pressure for single-effect (single-effect) cooling operation is maintained, the control means opens the solution bypass valve A, and the solution bypass valve A is opened. The valve B is closed and the intermediate concentrated solution is introduced to the cooling water heat transfer surface of the absorber, bypassing the low temperature regenerator. When the refrigerant vapor bypass valve is provided, the refrigerant vapor bypass valve is also opened. By opening the refrigerant vapor bypass valve,
The refrigerant vapor separated by the separator is guided to the condenser without being obstructed by the throttle part provided in the refrigerant vapor coil for the double-effect cooling operation, so the pressure of the high-temperature regenerator is double-effect cooling operation. Even if it is lower than in the case of 1, it can easily flow into the condenser. By opening and closing the solution bypass valve, the absorbing solution forms a cycle of single-effect cooling operation, but does not pass through the throttle portion that adjusts the pressure difference between the high-temperature regenerator and the low-temperature regenerator during double-effect cooling operation, and Since it is not necessary to flow the absorption solution into the low temperature regenerator located at a high position, the absorption solution can be sufficiently circulated from the separator to the absorber at the pressure formed in the high temperature regenerator by heating with the low pressure steam. Since the absorbing solution circulates sufficiently, problems such as crystallization due to insufficient solution circulation, mixing of the solution with the refrigerant due to retention in the separator, etc. are eliminated, the solution cycle operates normally, and cooling in single-effect operation is possible. It will be possible.

【0012】なお、冷媒蒸気バイパス回路の代りに、冷
媒蒸気コイルに冷媒制御弁が設けられている場合は、冷
媒蒸気コイルに流れる冷媒蒸気温度が予め設定された二
重効用冷房運転可能な温度のとき、冷媒制御弁の流路断
面積は絞り部に相当する大きさとなり、前記予め設定さ
れた温度より低い場合は、冷媒制御弁の流路断面積は十
分に大きいものに変更される。これにより、高温再生器
の圧力が低い場合でも、冷媒蒸気は容易に凝縮器に導か
れ、単効用冷房運転が可能となる。
When a refrigerant control valve is provided in the refrigerant vapor coil instead of the refrigerant vapor bypass circuit, the temperature of the refrigerant vapor flowing through the refrigerant vapor coil is set to a preset temperature for double-effect cooling operation. At this time, the flow passage cross-sectional area of the refrigerant control valve becomes a size corresponding to the throttle portion, and when the temperature is lower than the preset temperature, the flow passage cross-sectional area of the refrigerant control valve is changed to a sufficiently large one. Thereby, even when the pressure of the high temperature regenerator is low, the refrigerant vapor is easily guided to the condenser, and the single-effect cooling operation becomes possible.

【0013】蒸気圧力がさらに低下して単効用運転も不
可能な圧力となった場合、制御手段は、既に開いている
溶液バイパス弁Aに加えて溶液バイパス弁Bを開として
稀釈運転モードを形成し、分離器から流出した吸収溶液
を、低温再生器及び吸収器冷却水伝熱面をバイパスして
溶液循環ポンプ吸入側に導く。吸収溶液は、分離器内に
形成される吸収溶液液面と第2のバイパス回路の高さの
差を駆動力として分離器から単効用冷房運転サイクルの
ルートを流れ、そのルート内の吸収溶液の濃度の高い部
分を稀釈する。
When the vapor pressure further decreases and the single-effect operation becomes impossible, the control means opens the solution bypass valve B in addition to the solution bypass valve A that is already open to form the dilution operation mode. Then, the absorption solution flowing out from the separator is guided to the suction side of the solution circulation pump, bypassing the low temperature regenerator and the heat transfer surface of the cooling water of the absorber. The absorption solution flows from the separator through the route of the single-effect cooling operation cycle by using the difference between the level of the absorption solution formed in the separator and the height of the second bypass circuit as a driving force, and the absorption solution in the route is absorbed. Dilute high density areas.

【0014】高温再生器に供給される蒸気の圧力は、そ
の蒸気で加熱された高温再生器内の吸収溶液の温度と一
定の対応関係にあるから、溶液バイパス弁A,B及び冷
媒蒸気バイパス弁の開閉を、高温再生器内の吸収溶液の
温度の高低に基づいて行っても、蒸気の圧力の高低に基
づいてそれらの弁の開閉制御を行う場合と同様の動作を
行わせることができる。
Since the pressure of the steam supplied to the high temperature regenerator has a fixed correspondence with the temperature of the absorbing solution in the high temperature regenerator heated by the steam, the solution bypass valves A and B and the refrigerant vapor bypass valve Even if the opening and closing are performed based on whether the temperature of the absorbing solution in the high temperature regenerator is high or low, it is possible to perform the same operation as when opening and closing the valves based on the high and low of the pressure of the steam.

【0015】[0015]

【実施例】本発明の第1の実施例である蒸気焚き吸収冷
温水機を図1を参照して説明する。この吸収冷温水機
は、作動流体として、吸収剤であるリチウムブロマイド
(LiBr)に冷媒である水を吸収させた吸収溶液を用い
ている。吸収溶液のLiBr濃度は、作動流体が装置内を
循環するにつれて変動するが、この変動はほぼ3段階に
分けることができ、濃度レベルの低い方から、希溶液、
中間濃溶液、濃溶液と呼ぶ。
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A steam-fired absorption chiller-heater according to a first embodiment of the present invention will be described with reference to FIG. This absorption chiller-heater uses, as a working fluid, an absorbing solution in which lithium bromide (LiBr) which is an absorbent absorbs water which is a refrigerant. The LiBr concentration of the absorbing solution fluctuates as the working fluid circulates in the apparatus, but this fluctuation can be divided into almost three stages.
It is called an intermediate concentrated solution or a concentrated solution.

【0016】図示の蒸気焚き吸収冷温水機は、内包する
吸収溶液(希溶液)を蒸気で加熱する手段を備えた高温
再生器10と、高温再生器10の上方に配置され該高温
再生器10に上昇管14で接続された分離器16と、該
分離器16の気相部分に一端を接続された冷媒蒸気コイ
ル23を内装した低温再生器22と、該低温再生器22
に二次冷媒蒸気通路で連通され前記冷媒蒸気コイル23
の他端が接続されるとともに冷却水コイル(図示せず)
を内装した凝縮器26と、該凝縮器26に液冷媒管で接
続され蒸発コイル(図示せず)を内装した蒸発器34
と、前記蒸発器34に蒸発冷媒蒸気通路で連通され外周
面を冷却水伝熱面とする冷却水コイル(図示せず)を内
装した吸収器44と、吸収器44の底部に希溶液吸入管
52で吸入側を接続された溶液循環ポンプ54と、溶液
循環ポンプ54の吐出側に被加熱流体入り側を接続させ
た低温溶液熱交換器42と、低温溶液熱交換器42の被
加熱流体出側に希溶液送液管53Aを介して被加熱流体
入り側を接続させた高温溶液熱交換器36と、高温溶液
熱交換器36の被加熱流体出側と前記高温再生器10の
希溶液入り側を接続する希溶液送液管53Bと、前記分
離器16の液相部と高温溶液熱交換器36の加熱流体入
り側を接続する中間濃溶液管20と、高温溶液熱交換器
36の加熱流体出側と低温再生器22を接続する絞り部
を備えた中間濃溶液管38と、低温再生器22の液相部
と低温溶液熱交換器42の加熱流体入り側を接続する濃
溶液管40と、低温溶液熱交換器42の加熱流体出側と
吸収器44の上部を接続する濃溶液管41と、高温溶液
熱交換器36の加熱流体出側と低温溶液熱交換器42の
加熱流体出側を溶液バイパス弁A11を介して接続する
第1のバイパス回路12と、濃溶液管41と蒸発器34
底部を溶液バイパス弁B13を介して連通する第2のバ
イパス回路15と、高温再生器10に供給される蒸気の
圧力を検出して出力する圧力検知器17と、圧力検知器
17の出力を入力として溶液バイパス弁A,Bを開閉制
御するコントローラ18と、を含んで構成されている。
The illustrated steam-fired absorption chiller-heater has a high temperature regenerator 10 equipped with means for heating an absorption solution (dilute solution) contained therein, and a high temperature regenerator 10 arranged above the high temperature regenerator 10. A low temperature regenerator 22 in which a separator 16 connected to the above by a riser 14 and a refrigerant vapor coil 23, one end of which is connected to the gas phase portion of the separator 16, are installed;
Is communicated with a secondary refrigerant vapor passage by the refrigerant vapor coil 23.
The other end is connected and a cooling water coil (not shown)
And a condenser 26 in which an evaporation coil (not shown) connected to the condenser 26 by a liquid refrigerant pipe is installed.
An absorber 44 in which a cooling water coil (not shown) having an outer peripheral surface serving as a cooling water heat transfer surface is connected to the evaporator 34 by an evaporating refrigerant vapor passage, and a dilute solution suction pipe at the bottom of the absorber 44. A solution circulation pump 54 connected to the suction side by 52, a low temperature solution heat exchanger 42 in which the heated fluid inlet side is connected to the discharge side of the solution circulation pump 54, and a heated fluid outlet of the low temperature solution heat exchanger 42. Side, the high temperature solution heat exchanger 36 connected to the heated fluid entering side via the dilute solution feed pipe 53A, the heated fluid outlet side of the high temperature solution heat exchanger 36 and the dilute solution entering the high temperature regenerator 10. A dilute solution feed pipe 53B connecting the two sides, an intermediate concentrated solution pipe 20 connecting the liquid phase part of the separator 16 and the heating fluid inlet side of the high temperature solution heat exchanger 36, and heating of the high temperature solution heat exchanger 36. An intermediate concentrated solution with a throttle that connects the fluid outlet and the low temperature regenerator 22. A pipe 38, a concentrated solution pipe 40 connecting the liquid phase portion of the low temperature regenerator 22 and the heating fluid inlet side of the low temperature solution heat exchanger 42, a heating fluid outlet side of the low temperature solution heat exchanger 42 and an upper portion of the absorber 44. And a first bypass circuit 12 connecting the heating fluid outlet side of the high temperature solution heat exchanger 36 and the heating fluid outlet side of the low temperature solution heat exchanger 42 via the solution bypass valve A11. Concentrated solution pipe 41 and evaporator 34
The second bypass circuit 15 that communicates the bottom portion via the solution bypass valve B13, the pressure detector 17 that detects and outputs the pressure of the steam supplied to the high temperature regenerator 10, and the output of the pressure detector 17 are input. And a controller 18 for controlling the opening and closing of the solution bypass valves A and B.

【0017】中間濃溶液管38に設けられた絞り部は、
二重効用運転時の高温再生器と低温再生器の圧力差を調
整するためのものである。第1のバイパス回路12の上
流端は、この絞り部の上流側の中間濃溶液管38に接続
されている。
The squeezing portion provided in the intermediate concentrated solution pipe 38 is
This is to adjust the pressure difference between the high temperature regenerator and the low temperature regenerator during double-effect operation. The upstream end of the first bypass circuit 12 is connected to the intermediate concentrated solution pipe 38 on the upstream side of the throttle portion.

【0018】本実施例の吸収冷温水機では、蒸気圧力P
が8〜3kg/cm2であれば二重効用冷房運転が可能であ
り、蒸気圧力Pが3>P≧1kg/cm2であれば単効用冷
房運転が可能であるが、蒸気圧力が1>P≧0kg/cm2
であれば、単効用冷房運転も不可能である。したがっ
て、コントローラ18は、圧力検知器17から出力され
る蒸気圧力が8〜3kg/cm2のとき、溶液バイパス弁
A,Bをともに閉とし、蒸気圧力Pが3>P≧1kg/c
m2のとき溶液バイパス弁Aを開,溶液バイパス弁Bを閉
とし、蒸気圧力が1>P≧0kg/cm2のとき溶液バイパ
ス弁A,Bをともに開とするようになっている。
In the absorption chiller-heater of this embodiment, the steam pressure P
There are possible double effect cooling operation if 8~3kg / cm 2, although the steam pressure P is possible 3> P ≧ 1 kg / cm single-effect cooling operation if 2, steam pressure of 1> P ≧ 0 kg / cm 2
In that case, single-effect cooling operation is also impossible. Therefore, when the vapor pressure output from the pressure detector 17 is 8 to 3 kg / cm 2 , the controller 18 closes both the solution bypass valves A and B, and the vapor pressure P is 3> P ≧ 1 kg / c.
The solution bypass valve A is opened when m 2 and the solution bypass valve B is closed, and both solution bypass valves A and B are opened when the vapor pressure is 1> P ≧ 0 kg / cm 2 .

【0019】上記の構成の吸収冷温水機においては、溶
液バイパス弁A11を備えた第1のバイパス回路、溶液
バイパス弁B13を備えた第2のバイパス回路、及びこ
れらを制御するコントローラ18が設けられていること
が、図9に示された従来技術と異なっている。
The absorption chiller-heater having the above structure is provided with a first bypass circuit having a solution bypass valve A11, a second bypass circuit having a solution bypass valve B13, and a controller 18 for controlling these. This is different from the prior art shown in FIG.

【0020】上記構成の吸収冷温水機の通常の二重効用
運転時の動作を以下に説明する。この場合、供給される
蒸気の圧力は、8〜3kg/cm2であり、溶液バイパス弁
A,Bともに閉となっている。高温再生器10内の希溶
液は供給される蒸気で加熱されて気液2相状態で上昇管
14内を上昇し、分離器16に流入する。分離器16に
流入した気液2相状態の希溶液は冷媒蒸気と中間濃溶液
に分離され、冷媒蒸気は低温再生器22に内装された冷
媒蒸気コイル23を経て凝縮器26に流入し、中間濃溶
液は中間濃溶液管20を経て高温溶液熱交換器36の加
熱流体側に流入する。高温溶液熱交換器36に流入した
中間濃溶液は、被加熱流体側を流れる希溶液を加熱しつ
つ高温溶液熱交換器36を通過し、中間濃溶液管38を
経て低温再生器22に流入する。冷媒蒸気コイル23内
を流れる冷媒蒸気は、周囲の中間濃溶液を加熱して冷媒
を蒸発させて二次冷媒蒸気を生成し、自身は冷却されて
凝縮し気液2相となって凝縮器26に流入する。低温再
生器22で生成された二次冷媒蒸気も、二次冷媒蒸気通
路を経て凝縮器26に流入し、冷媒蒸気コイル23を経
て流入した冷媒とともに、冷却水コイル内を流れる冷却
水に冷却されて凝縮し、液冷媒となる。
The operation during the normal double-effect operation of the absorption chiller-heater configured as described above will be described below. In this case, the pressure of the supplied steam is 8 to 3 kg / cm 2 , and both solution bypass valves A and B are closed. The dilute solution in the high temperature regenerator 10 is heated by the supplied steam, rises in the rising pipe 14 in a gas-liquid two-phase state, and flows into the separator 16. The dilute gas-liquid two-phase solution that has flowed into the separator 16 is separated into a refrigerant vapor and an intermediate concentrated solution, and the refrigerant vapor flows into the condenser 26 via the refrigerant vapor coil 23 installed in the low temperature regenerator 22, and then the intermediate vapor The concentrated solution flows into the heating fluid side of the high temperature solution heat exchanger 36 through the intermediate concentrated solution pipe 20. The intermediate concentrated solution flowing into the high temperature solution heat exchanger 36 passes through the high temperature solution heat exchanger 36 while heating the dilute solution flowing on the heated fluid side, and then flows into the low temperature regenerator 22 via the intermediate concentrated solution pipe 38. . The refrigerant vapor flowing in the refrigerant vapor coil 23 heats the surrounding intermediate concentrated solution to evaporate the refrigerant to generate a secondary refrigerant vapor, which itself is cooled and condensed to become a gas-liquid two-phase condenser 26. Flow into. The secondary refrigerant vapor generated in the low-temperature regenerator 22 also flows into the condenser 26 via the secondary refrigerant vapor passage, and is cooled to the cooling water flowing in the cooling water coil together with the refrigerant flowing in via the refrigerant vapor coil 23. Are condensed and become a liquid refrigerant.

【0021】凝縮器26で生成された液冷媒は、液冷媒
管30を経て蒸発器34に流入し、蒸発器34に内装さ
れた蒸発コイル上に散布され、蒸発コイル内を流れる熱
媒体(冷温水)の熱を奪って蒸発し、再び冷媒蒸気とな
り、蒸発冷媒蒸気通路を経て吸収器44に流入する。熱
を奪われて冷却された熱媒体は、冷房負荷に導かれ、冷
房を行ったのち再び蒸発コイルに還流する。低温再生器
22で二次冷媒蒸気として冷媒を蒸発させた中間濃溶液
は、濃溶液となり、濃溶液管40を経て低温溶液熱交換
器42の加熱流体入り側に流入する。低温溶液熱交換器
42に流入した濃溶液は、被加熱流体側を流れる希溶液
を加熱しつつ低温溶液熱交換器42を通過し、濃溶液管
41を経て吸収器44に流入する。吸収器44に流入し
た濃溶液は、冷却水コイル伝熱面上に散布され、蒸発器
から流入する冷媒蒸気を吸収して希溶液となる。濃溶液
が冷媒蒸気を吸収するときに発生する吸収熱は、冷却水
コイル内を流れる冷却水に移され、クーリングタワー
(図示せず)に運ばれて大気に放出される。
The liquid refrigerant generated in the condenser 26 flows into the evaporator 34 through the liquid refrigerant pipe 30, is sprayed on the evaporation coil installed in the evaporator 34, and flows in the evaporation coil as a heat medium (cooling temperature). The heat of (water) is taken to evaporate and become refrigerant vapor again, and then flows into the absorber 44 via the evaporated refrigerant vapor passage. The heat medium that has been deprived of heat and cooled is guided to the cooling load, is cooled, and then returns to the evaporation coil again. The intermediate concentrated solution obtained by evaporating the refrigerant as the secondary refrigerant vapor in the low temperature regenerator 22 becomes a concentrated solution, and flows into the heating fluid inlet side of the low temperature solution heat exchanger 42 via the concentrated solution pipe 40. The concentrated solution flowing into the low temperature solution heat exchanger 42 passes through the low temperature solution heat exchanger 42 while heating the dilute solution flowing on the heated fluid side, and then flows into the absorber 44 via the concentrated solution pipe 41. The concentrated solution that has flowed into the absorber 44 is dispersed on the heat transfer surface of the cooling water coil, and absorbs the refrigerant vapor that flows from the evaporator to become a dilute solution. Absorption heat generated when the concentrated solution absorbs the refrigerant vapor is transferred to the cooling water flowing in the cooling water coil, carried to the cooling tower (not shown), and released to the atmosphere.

【0022】吸収器44で生成された希溶液は、希溶液
吸入管52を経て溶液循環ポンプ54に吸入、加圧さ
れ、低温溶液熱交換器42の被加熱流体側及び高温溶液
熱交換器36の被加熱流体側を経て高温再生器10に流
入する。高温再生器10に流入した希溶液は、再び上述
のサイクルを繰り返す。
The dilute solution produced in the absorber 44 is sucked and pressurized by the solution circulation pump 54 through the dilute solution suction pipe 52, and the heated fluid side of the low temperature solution heat exchanger 42 and the high temperature solution heat exchanger 36. Flowing into the high temperature regenerator 10 via the fluid to be heated. The dilute solution flowing into the high temperature regenerator 10 repeats the above cycle again.

【0023】次に、高温再生器に供給される蒸気の圧力
Pが、3kg/cm2以下に低下した場合について説明す
る。表1に、蒸気圧力とそれに対応する溶液バイパス弁
A,Bの開閉状態を示す。高温再生器温度の欄には、蒸
気圧力の欄に記載された圧力の蒸気が高温再生器に供給
された場合の、高温再生器の温度が示されている。
Next, the case where the pressure P of the steam supplied to the high temperature regenerator drops to 3 kg / cm 2 or less will be described. Table 1 shows the vapor pressure and the open / closed states of the solution bypass valves A and B corresponding thereto. The column of high temperature regenerator temperature shows the temperature of the high temperature regenerator when the steam having the pressure described in the column of steam pressure is supplied to the high temperature regenerator.

【0024】[0024]

【表1】 [Table 1]

【0025】まず、高温再生器に供給される蒸気の圧力
Pが、3>P≧1kg/cm2に低下した場合について説明
する。この場合、表1に示されるように、溶液バイパス
弁Aが開かれ、溶液バイパス弁Bが閉のままである。高
温再生器内の温度は、130〜90℃となり、高温再生
器内の圧力も低下する。分離器16で分離され、高温溶
液熱交換器36の加熱流体側を通過した中間濃溶液は、
開かれた溶液バイパス弁A11を通り、低温再生器及び
低温溶液熱交換器42をバイパスして濃溶液管38に導
かれ、吸収器44の冷却水コイル上に散布される。一
方、分離器16で分離された冷媒蒸気は冷媒蒸気コイル
23を経て凝縮器26に流入し、冷却水コイルを流れる
冷却水に冷却されて液冷媒となる。先に述べたように、
吸収溶液は低温再生器22には流入しないので、冷媒蒸
気コイル23を流れる冷媒蒸気はにじ冷媒蒸気を発生さ
せることなくそのまま凝縮器26に流入、液化される。
First, the case where the pressure P of the steam supplied to the high temperature regenerator is lowered to 3> P ≧ 1 kg / cm 2 will be described. In this case, as shown in Table 1, the solution bypass valve A remains open and the solution bypass valve B remains closed. The temperature in the high temperature regenerator becomes 130 to 90 ° C., and the pressure in the high temperature regenerator also decreases. The intermediate concentrated solution separated by the separator 16 and passed through the heated fluid side of the high temperature solution heat exchanger 36 is
It passes through the opened solution bypass valve A11, bypasses the low temperature regenerator and the low temperature solution heat exchanger 42, is guided to the concentrated solution pipe 38, and is sprayed on the cooling water coil of the absorber 44. On the other hand, the refrigerant vapor separated by the separator 16 flows into the condenser 26 through the refrigerant vapor coil 23 and is cooled by the cooling water flowing through the cooling water coil to become a liquid refrigerant. As mentioned earlier,
Since the absorbing solution does not flow into the low temperature regenerator 22, the refrigerant vapor flowing through the refrigerant vapor coil 23 directly flows into the condenser 26 and is liquefied without generating bleeding refrigerant vapor.

【0026】凝縮器26で生成された液冷媒は蒸発器3
4に供給され、蒸発コイル上で蒸発して蒸発コイル内を
流れる熱媒体(冷温水)を冷却し、冷媒蒸気となって吸
収器44に流入する。吸収器44に流入した冷媒蒸気
は、散布される吸収溶液(中間濃溶液)に吸収され、希
溶液となって溶液循環ポンプ54に吸引される。溶液循
環ポンプ54は吸引した希溶液を加圧して、低温溶液熱
交換器42の被加熱流体側、高温溶液熱交換器36の被
加熱流体側を経て高温再生器10に送りこむ。低温溶液
熱交換器42の加熱流体側には加熱流体が流れていない
が、高温溶液熱交換器36の加熱流体側には中間濃溶液
が流れており、希溶液は高温溶液熱交換器36で加熱さ
れたのち、高温再生器10に流入し、上記の循環サイク
ル、すなわち、単効用冷房サイクルを繰り返す。
The liquid refrigerant produced in the condenser 26 is the evaporator 3
4, the heat medium (cooled / hot water) that evaporates on the evaporation coil and flows in the evaporation coil is cooled and flows into the absorber 44 as a refrigerant vapor. The refrigerant vapor that has flowed into the absorber 44 is absorbed by the absorbing solution (intermediate concentrated solution) to be dispersed, becomes a diluted solution, and is sucked by the solution circulation pump 54. The solution circulation pump 54 pressurizes the sucked dilute solution and sends it to the high temperature regenerator 10 via the heated fluid side of the low temperature solution heat exchanger 42 and the heated fluid side of the high temperature solution heat exchanger 36. No heating fluid is flowing on the heating fluid side of the low temperature solution heat exchanger 42, but an intermediate concentrated solution is flowing on the heating fluid side of the high temperature solution heat exchanger 36, and the dilute solution is on the high temperature solution heat exchanger 36. After being heated, it flows into the high temperature regenerator 10 and repeats the above circulation cycle, that is, the single effect cooling cycle.

【0027】高温再生器内の圧力は、供給される蒸気圧
の低下(すなわち蒸気温度低下)に伴って低下している
が、上述の単効用冷房サイクルでは、吸収溶液が高い位
置にある低温再生器をバイパスし、さらに絞り部のある
中間濃溶液管38を通らないので、高温再生器内の圧力
が低くても分離器16から吸収器44への吸収溶液の循
環量が十分に得られ、単効用冷房サイクルとしての機能
が発揮される。
Although the pressure inside the high temperature regenerator decreases with a decrease in the supplied vapor pressure (that is, a decrease in the vapor temperature), in the above-described single-effect cooling cycle, the low temperature regeneration in which the absorbing solution is at a high position. Since it bypasses the reactor and does not pass through the intermediate concentrated solution pipe 38 having a narrowed portion, even if the pressure in the high temperature regenerator is low, a sufficient circulation amount of the absorbing solution from the separator 16 to the absorber 44 can be obtained. Functions as a single-effect cooling cycle.

【0028】このように、供給される蒸気圧力が低下し
ても、単効用冷房サイクルとして機能させるので、溶液
循環不足による晶析、溶液の分離器内での滞留による冷
媒への混入等の不具合の発生がなくなる。
As described above, even if the supplied steam pressure is reduced, the cooling cycle is made to function as a single-effect cooling cycle, so that there is a problem such as crystallization due to insufficient circulation of the solution and mixing of the solution with the refrigerant due to retention of the solution in the separator. Is eliminated.

【0029】次に、高温再生器に供給される蒸気の圧力
Pがさらに低下し、1>P≧0kg/cm2になった場合に
ついて説明する。この場合、高温再生器内の温度は、9
0℃未満となり、高温再生器内の圧力も、吸収溶液を吸
収器に送りこむのに十分でなくなる。この段階では、コ
ントローラは、表1に示されるように、溶液バイパス弁
A,Bをともに開き、冷房運転をやめて稀釈運転を開始
する。稀釈運転では、溶液循環ポンプ54、冷却水ポン
プ、冷温水ポンプの運転はそのまま継続される。溶液循
環ポンプ54で高温再生器に供給された吸収溶液(希溶
液)は、高温再生器10,分離器16,高温溶液熱交換
器の加熱流体側,第1のバイパス回路,濃溶液管41,
第2のバイパス回路,蒸発器34底部を順次経て吸収器
44底部に達し、吸収器44底部から再び溶液循環ポン
プ54に吸引され、このルートを循環してルート内の吸
収溶液を稀釈する。この稀釈により、吸収溶液の晶析が
回避される。
Next, the case where the pressure P of the steam supplied to the high temperature regenerator is further reduced and 1> P ≧ 0 kg / cm 2 is described. In this case, the temperature inside the high temperature regenerator is 9
Below 0 ° C., the pressure in the hot regenerator is also insufficient to pump the absorbent solution into the absorber. At this stage, as shown in Table 1, the controller opens both the solution bypass valves A and B to stop the cooling operation and start the dilution operation. In the dilution operation, the operation of the solution circulation pump 54, the cooling water pump, and the cold / hot water pump is continued as it is. The absorbing solution (dilute solution) supplied to the high temperature regenerator by the solution circulation pump 54 is the high temperature regenerator 10, the separator 16, the heating fluid side of the high temperature solution heat exchanger, the first bypass circuit, the concentrated solution pipe 41,
The second bypass circuit and the bottom of the evaporator 34 are sequentially passed to reach the bottom of the absorber 44, and the solution circulation pump 54 is again sucked from the bottom of the absorber 44 to circulate through this route to dilute the absorption solution in the route. This dilution avoids crystallization of the absorbing solution.

【0030】このルートでは、吸収溶液は濃溶液管41
の蒸発器34底部と同レベルの高さの点から第2のバイ
パス回路を経て蒸発器34底部に流れるようになってお
り、吸収溶液を低温再生器や吸収器の上部にまで押し上
げる必要がなく、高温再生器の圧力が低くても吸収溶液
の循環が容易であり、溶液循環不足による晶析が防止さ
れる。
In this route, the absorbing solution is concentrated solution tube 41.
From the point of the same level as the bottom of the evaporator 34, it flows through the second bypass circuit to the bottom of the evaporator 34, so that it is not necessary to push the absorbing solution to the low temperature regenerator or the upper part of the absorber. Even if the pressure of the high temperature regenerator is low, the absorption solution can be easily circulated, and crystallization due to insufficient solution circulation can be prevented.

【0031】このように、高温再生器に供給される加熱
用蒸気の圧力が、二重効用冷房運転に不十分な圧力に低
下した場合でも、蒸気を遮断して吸収冷温水機を停止さ
せる必要もなく、低圧蒸気を有効に利用できる。蒸気遮
断のための遮断弁も不要になり、イニシャルコストを低
減できる。
As described above, even when the pressure of the heating steam supplied to the high temperature regenerator falls to a pressure insufficient for the double-effect cooling operation, it is necessary to shut off the steam and stop the absorption chiller-heater. Nonetheless, low-pressure steam can be effectively used. A shutoff valve for shutting off steam is not required, and the initial cost can be reduced.

【0032】図2に本発明の第2の実施例を示す。第2
の実施例が第1の実施例と異なるのは、第1のバイパス
回路が、第1の実施例においては、高温溶液熱交換器3
6の加熱流体出側と低温溶液熱交換器42の加熱流体出
側を結んでいるのに対し、第2の実施例においては、高
温溶液熱交換器36の加熱流体出側と低温溶液熱交換器
42の加熱流体入り側を結んでいることである。他の構
成は第1の実施例と同じであるので、同一の符号を付
し、説明を省略する。
FIG. 2 shows a second embodiment of the present invention. Second
Is different from the first embodiment in that the first bypass circuit is the high temperature solution heat exchanger 3 in the first embodiment.
While the heating fluid outlet side of 6 and the heating fluid outlet side of the low temperature solution heat exchanger 42 are connected, in the second embodiment, the heating fluid outlet side of the high temperature solution heat exchanger 36 and the low temperature solution heat exchange are connected. That is, the heating fluid inlet side of the container 42 is connected. Since the other configurations are the same as those of the first embodiment, the same reference numerals are given and the description thereof will be omitted.

【0033】第2の実施例では、分離器16を出た吸収
溶液が、高温溶液熱交換器36と低温溶液熱交換器42
の双方で熱交換を行うので、分離器16を出た吸収溶液
の熱を希溶液に十分に回収でき、効率をあげる利点があ
る。
In the second embodiment, the absorption solution exiting the separator 16 has a high temperature solution heat exchanger 36 and a low temperature solution heat exchanger 42.
Since the heat exchange is performed by both of them, there is an advantage that the heat of the absorbing solution that has left the separator 16 can be sufficiently recovered in the dilute solution and the efficiency is improved.

【0034】図3に本発明の第3の実施例を示す。図3
は、実際の機器、配管の配置に即して描いた吸収冷温水
機の縦断面図である。第3の実施例が第1の実施例と異
なるのは、第1のバイパス回路の設置位置と、高温再生
器10を通過して凝縮されたドレン水の熱を希溶液に回
収する排熱熱交換器66が設けられていることである。
なお、図3には、分離器16の底部と吸収器44の底部
とを冷暖房切換弁56を介して連通する連絡回路が示さ
れているが、図1,2,9では記載が省略されている。
FIG. 3 shows a third embodiment of the present invention. FIG.
FIG. 3 is a vertical cross-sectional view of an absorption chiller-heater drawn according to the actual arrangement of equipment and piping. The third embodiment is different from the first embodiment in that the installed position of the first bypass circuit and the exhaust heat for recovering the heat of drain water condensed through the high temperature regenerator 10 into a dilute solution. That is, the exchanger 66 is provided.
3 shows a communication circuit that connects the bottom of the separator 16 and the bottom of the absorber 44 via the cooling / heating switching valve 56, but the description thereof is omitted in FIGS. There is.

【0035】第1の実施例においては、第1のバイパス
回路は、高温溶液熱交換器36の加熱流体出側と低温溶
液熱交換器42の加熱流体出側を結んでいるのに対し、
第3の実施例においては、中間濃溶液管20と低温溶液
熱交換器42の加熱流体入り側を結んでいる。また、低
温溶液熱交換器42の被加熱流体側を出た希溶液は高温
熱交換器36に流入する前に排熱熱交換器66に流入
し、高温再生器10を通過して凝縮されたドレン水の熱
を回収したのち、高温再生器10に流入するごとく構成
されている。他の構成は第1の実施例と同じであるの
で、同一の符号を付し、説明を省略する。なお、本実施
例では、中央下部に高温再生器10及び排熱熱交換器6
6が配置され、中央上部に分離器16が配置されてい
る。分離器16の上部外側に環状に低温再生器22が配
置され、さらにその外側に凝縮器26が環状に配置され
ている。吸収器44は分離器16の下部外周に環状に配
置され、さらにその外側に蒸発器34が環状に配置され
ている。
In the first embodiment, the first bypass circuit connects the heating fluid outlet side of the high temperature solution heat exchanger 36 and the heating fluid outlet side of the low temperature solution heat exchanger 42, while
In the third embodiment, the intermediate concentrated solution pipe 20 and the low temperature solution heat exchanger 42 are connected to the heating fluid inlet side. Further, the dilute solution exiting from the heated fluid side of the low temperature solution heat exchanger 42 flows into the exhaust heat heat exchanger 66 before flowing into the high temperature heat exchanger 36, passes through the high temperature regenerator 10 and is condensed. After collecting the heat of the drain water, the drain water flows into the high temperature regenerator 10. Since the other configurations are the same as those of the first embodiment, the same reference numerals are given and the description thereof will be omitted. In this embodiment, the high temperature regenerator 10 and the exhaust heat exchanger 6 are provided in the lower center part.
6 is arranged, and the separator 16 is arranged at the upper center. A low-temperature regenerator 22 is annularly arranged outside the upper part of the separator 16, and a condenser 26 is annularly arranged outside thereof. The absorber 44 is annularly arranged around the lower part of the separator 16, and the evaporator 34 is annularly arranged outside the absorber.

【0036】第3の実施例では、第1のバイパス回路は
図から明らかなように、ごく接近した部分を接続するよ
うに配置されており、機器配置が容易であるという利点
がある。
In the third embodiment, as is clear from the figure, the first bypass circuit is arranged so as to connect the parts that are very close to each other, and there is an advantage that the device arrangement is easy.

【0037】なお、上記各実施例で、第1のバイパス回
路を、中間濃溶液管20と低温溶液熱交換器42の加熱
流体出側を結ぶように配置してもよいが、この場合は、
溶液バイパス弁Aを開いた単効用冷房運転の際、分離器
を出た吸収溶液の熱を希溶液で回収することができなく
なり、ある程度効率が低下することになる。
In each of the above embodiments, the first bypass circuit may be arranged so as to connect the intermediate concentrated solution pipe 20 and the heating fluid outlet side of the low temperature solution heat exchanger 42, but in this case,
During the single-effect cooling operation in which the solution bypass valve A is opened, the heat of the absorbing solution that has left the separator cannot be recovered by the dilute solution, and the efficiency decreases to some extent.

【0038】図4に本発明の第4の実施例を示す。第4
の実施例が前記第3の実施例と異なるのは、第1,第2
のバイパス回路の設置位置と、分離器16の気相部と凝
縮器26を冷媒蒸気バイパス弁43を介して接続する冷
媒蒸気バイパス回路45が設けられていること、及び高
温再生器10内の温度を検知する温度検出器19が設け
られコントローラ18は温度検出器から出力される温度
信号の高低に応じて溶液バイパス弁11,13及び冷媒
蒸気バイパス弁43の開閉を行うように構成されている
点である。本実施例においては、第1のバイパス回路
は、高温溶液熱交換器36の加熱流体出側と低温溶液熱
交換器42の加熱流体入り側を結んでおり、第2のバイ
パス回路は、濃溶液管41と吸収器44の底部とを結ん
でいる。また、冷媒蒸気バイパス回路45は、低温再生
器22に内装された冷媒蒸気コイル23の絞り部に比
べ、十分に大きい流路断面積を持つものとしてある。
FIG. 4 shows a fourth embodiment of the present invention. Fourth
This embodiment is different from the third embodiment in that
Is installed, a refrigerant vapor bypass circuit 45 that connects the vapor phase part of the separator 16 and the condenser 26 via the refrigerant vapor bypass valve 43, and the temperature inside the high temperature regenerator 10. A temperature detector 19 for detecting the temperature is provided, and the controller 18 is configured to open and close the solution bypass valves 11 and 13 and the refrigerant vapor bypass valve 43 according to the level of the temperature signal output from the temperature detector. Is. In the present embodiment, the first bypass circuit connects the heating fluid outlet side of the high temperature solution heat exchanger 36 and the heating fluid inlet side of the low temperature solution heat exchanger 42, and the second bypass circuit is the concentrated solution. It connects the tube 41 and the bottom of the absorber 44. Further, the refrigerant vapor bypass circuit 45 has a flow passage cross-sectional area that is sufficiently larger than that of the throttle portion of the refrigerant vapor coil 23 incorporated in the low temperature regenerator 22.

【0039】本実施例においては、高温再生器内の吸収
溶液温度が通常の二重効用冷房運転可能な温度状態で
は、溶液バイパス弁11,13及び冷媒蒸気バイパス弁
は閉じてあるが、蒸気圧力の低下により、温度検出器1
9が出力する高温再生器10内の吸収溶液温度が二重効
用冷房運転が不可能な温度(表1に記載された130〜
90℃)にまで低下した場合、コントローラ18は、溶
液バイパス弁11及び冷媒蒸気バイパス弁を開き、溶液
バイパス弁13を閉じたままとして単効用冷房サイクル
を構成する。
In this embodiment, the solution bypass valves 11 and 13 and the refrigerant vapor bypass valve are closed, but the vapor pressure is high when the temperature of the absorbing solution in the high temperature regenerator is such that normal double effect cooling operation is possible. Temperature sensor 1
The temperature of the absorbing solution in the high-temperature regenerator 10 output by 9 is a temperature at which the double-effect cooling operation is impossible (130 to 130 in Table 1).
When the temperature falls to 90 ° C.), the controller 18 opens the solution bypass valve 11 and the refrigerant vapor bypass valve, and leaves the solution bypass valve 13 closed to form a single-effect cooling cycle.

【0040】この状態で、吸収溶液は高温再生器10内
で加熱され、分離器16で冷媒蒸気を分離して濃縮さ
れ、高温溶液熱交換器36の加熱流体側,第1のバイパ
ス回路,低温溶液熱交換器42の加熱流体側,濃溶液管
41を経て吸収器44に達し、濃溶液分配器46から吸
収器に内装された冷却水コイル48上に散布される。
In this state, the absorbing solution is heated in the high temperature regenerator 10, the refrigerant vapor is separated and concentrated in the separator 16, the heating fluid side of the high temperature solution heat exchanger 36, the first bypass circuit, the low temperature side. It reaches the absorber 44 via the heated fluid side of the solution heat exchanger 42 and the concentrated solution pipe 41, and is sprayed from the concentrated solution distributor 46 onto the cooling water coil 48 installed in the absorber.

【0041】一方、分離器16で分離された冷媒蒸気
は、冷媒蒸気バイパス回路45が冷媒蒸気コイル23に
比べて大きい流路断面積を持っているので、高温再生器
内の圧力が低くても容易に凝縮器26に流入し、凝縮さ
れて液冷媒となる。この液冷媒は蒸発コイル35上に散
布され、蒸発コイル内を循環する冷温水から熱を奪って
蒸発し冷媒蒸気となる。この冷媒蒸気は吸収器44に導
かれ、前記冷却水コイル48上に散布された吸収溶液に
吸収され、希溶液となる。この希溶液は、溶液循環ポン
プ54に吸引、加圧され、低温溶液熱交換器42、排熱
熱交換器66、高温溶液熱交換器36を経て高温再生器
10に送りこまれ、上述のサイクルを繰り返す。
On the other hand, since the refrigerant vapor bypass circuit 45 has a larger flow passage cross-sectional area than the refrigerant vapor coil 23, the refrigerant vapor separated by the separator 16 is low in pressure inside the high temperature regenerator. It easily flows into the condenser 26 and is condensed into a liquid refrigerant. The liquid refrigerant is sprayed on the evaporation coil 35, and heat is taken from the cold / hot water circulating in the evaporation coil to evaporate to become a refrigerant vapor. This refrigerant vapor is guided to the absorber 44, absorbed by the absorbing solution sprinkled on the cooling water coil 48, and becomes a dilute solution. This dilute solution is sucked and pressurized by the solution circulation pump 54, is sent to the high temperature regenerator 10 via the low temperature solution heat exchanger 42, the exhaust heat heat exchanger 66, and the high temperature solution heat exchanger 36, and undergoes the above-mentioned cycle. repeat.

【0042】この場合も、高温再生器10内の温度が低
く吸収溶液を高い位置にある低温再生器に押し上げるほ
どの圧力にならなくても、吸収溶液は低温再生器22を
バイパスして流れるので溶液の循環に支障はなく、単効
用冷房運転を実現できる。さらに、分離器16の気相部
と凝縮器26とを冷媒蒸気バイパス弁43を介して接続
する、十分な流路断面積を備えた冷媒蒸気バイパス回路
45が設けられているから、高温再生器10の圧力(す
なわち分離器16の圧力)が、二重効用運転には不足す
る圧力であっても、冷媒蒸気バイパス弁43を開くこと
により、分離器16で分離された冷媒蒸気は容易に凝縮
器に流入し、液冷媒の生成に不具合は生じない。
In this case as well, the absorbing solution flows by-passing the low temperature regenerator 22 even if the temperature inside the high temperature regenerator 10 is low and the pressure is not enough to push the absorbing solution to the high temperature low temperature regenerator. There is no hindrance to the solution circulation, and single-effect cooling operation can be realized. Further, since the refrigerant vapor bypass circuit 45 having a sufficient flow passage cross-sectional area that connects the vapor phase portion of the separator 16 and the condenser 26 via the refrigerant vapor bypass valve 43 is provided, the high temperature regenerator is provided. Even if the pressure of 10 (that is, the pressure of the separator 16) is insufficient for double-effect operation, the refrigerant vapor bypass valve 43 is opened to easily condense the refrigerant vapor separated in the separator 16. It flows into the vessel and there is no problem in the generation of liquid refrigerant.

【0043】高温再生器10に供給される蒸気の圧力が
さらに低下して高温再生器内の溶液温度が下がり、単効
用冷房運転サイクルの形成も困難な温度(90℃未満)
になったら、コントローラ18はさらに、溶液バイパス
弁13を開く。単効用冷房運転サイクルが不能になった
吸収溶液は、高温再生器10を満たし、さらにその上部
の分離器16内に溜る。分離器16内に溜った吸収溶液
は、その液面と溶液バイパス弁13の高低差hにより、
高温溶液熱交換器36の加熱流体側,第1のバイパス回
路,低温溶液熱交換器42の加熱流体側,濃溶液管4
1、第2のバイパス回路を経て吸収器44下部に流れ、
溶液循環サイクルを形成する。この溶液循環サイクルの
形成で、高温再生器内での高濃度吸収溶液の滞留が防止
され、低圧蒸気での吸収溶液の濃縮による晶析が回避さ
れる。
The pressure of the steam supplied to the high temperature regenerator 10 further decreases, the temperature of the solution in the high temperature regenerator decreases, and it is difficult to form a single-effect cooling operation cycle (less than 90 ° C.).
Then, the controller 18 further opens the solution bypass valve 13. The absorption solution, which has disabled the single-effect cooling operation cycle, fills the high temperature regenerator 10 and collects in the separator 16 above it. The absorbing solution accumulated in the separator 16 has a height difference h between the liquid surface and the solution bypass valve 13,
Heating fluid side of high temperature solution heat exchanger 36, first bypass circuit, heating fluid side of low temperature solution heat exchanger 42, concentrated solution tube 4
Flows to the lower part of the absorber 44 through the first and second bypass circuits,
Form a solution circulation cycle. The formation of this solution circulation cycle prevents the high-concentration absorption solution from staying in the high-temperature regenerator and avoids crystallization due to the concentration of the absorption solution in the low-pressure steam.

【0044】また、この溶液循環サイクルの形成で、吸
収溶液が加熱保温されるため、蒸気圧力が冷房運転可能
な圧力に復帰したときの冷房立ちあげ時間が短縮され
る。蒸気圧力が上昇し、温度検出器19により高温再生
器内の吸収溶液温度が130〜90℃にまで上昇したこ
とが検出されると、コントローラ18は、まず、溶液バ
イパス弁13を閉じる。高温再生器内の圧力は温度の上
昇とともに増加し、低温溶液熱交換器42を出た吸収溶
液は、濃溶液管41を経て吸収器44の上部にまで送り
こまれ、濃溶液分配器46から散布されて単効用冷房運
転が開始される。
Further, since the absorption solution is heated and kept warm by the formation of this solution circulation cycle, the cooling start-up time when the vapor pressure returns to a pressure capable of cooling operation can be shortened. When the vapor pressure rises and the temperature detector 19 detects that the temperature of the absorbing solution in the high temperature regenerator has risen to 130 to 90 ° C., the controller 18 first closes the solution bypass valve 13. The pressure in the high-temperature regenerator increases with the rise in temperature, and the absorbing solution exiting the low-temperature solution heat exchanger 42 is sent to the upper part of the absorber 44 via the concentrated solution pipe 41 and sprayed from the concentrated solution distributor 46. Then, the single-effect cooling operation is started.

【0045】さらに、蒸気圧力が上昇し、温度検出器1
9により高温再生器内の吸収溶液温度が130℃以上に
まで上昇したことが検出されると、コントローラ18
は、溶液バイパス弁11、冷媒蒸気バイパス弁43を閉
じる。高温再生器内の圧力は温度の上昇とともにさらに
増加し、高温溶液熱交換器36を出た吸収溶液は、中間
濃溶液管38を経て高い位置にある低温再生器22に送
りこまれ、分離器16で分離された冷媒蒸気も冷媒蒸気
コイル23を通過しながら二次冷媒蒸気を発生させ、二
重効用冷房運転が開始される。
Further, the steam pressure rises, and the temperature detector 1
When it is detected by 9 that the temperature of the absorbing solution in the high temperature regenerator has risen to 130 ° C. or higher, the controller 18
Closes the solution bypass valve 11 and the refrigerant vapor bypass valve 43. The pressure in the high temperature regenerator further increases as the temperature rises, and the absorbing solution leaving the high temperature solution heat exchanger 36 is sent to the low temperature regenerator 22 at a high position via the intermediate concentrated solution pipe 38, and the separator 16 The refrigerant vapor separated in (2) also generates the secondary refrigerant vapor while passing through the refrigerant vapor coil 23, and the double-effect cooling operation is started.

【0046】図8に、上述の手順をフローチャートとし
て示した。
FIG. 8 shows the above procedure as a flowchart.

【0047】図5に本発明の第5の実施例を示す。本実
施例と前記第4の実施例との相違点は、冷媒蒸気バイパ
ス回路の代りに、冷媒蒸気コイル23の絞り部に流路断
面積を2段階に変えることのできる冷媒制御弁21を用
いたことである。冷媒制御弁21は、内部を流れる冷媒
蒸気の温度が予め設定された温度よりも高い場合は流路
断面積を小さくし、低下した場合は流路断面積を大きく
するようにしたもので、本実施例ではバイメタルを使用
した弁としたが、形状記憶合金を用いたものや、ワック
ス弁を利用してもよい。他の構成は前記第4の実施例と
同じであり、説明は省略する。
FIG. 5 shows a fifth embodiment of the present invention. The difference between this embodiment and the fourth embodiment is that instead of the refrigerant vapor bypass circuit, a refrigerant control valve 21 capable of changing the flow passage cross-sectional area in two stages is used in the throttle portion of the refrigerant vapor coil 23. That is what happened. The refrigerant control valve 21 reduces the flow passage cross-sectional area when the temperature of the refrigerant vapor flowing inside is higher than a preset temperature, and increases the flow passage cross-sectional area when the temperature decreases. Although a valve made of bimetal is used in the embodiment, a valve made of shape memory alloy or a wax valve may be used. The other structure is the same as that of the fourth embodiment, and the description thereof is omitted.

【0048】本実施例によれば、前記第4の実施例と同
様の効果が得られるとともに、第4の実施例にくらべ、
冷媒蒸気バイパス回路やそれを制御する手段を設ける必
要がなく、構成が簡易であるという利点がある。
According to this embodiment, the same effect as that of the fourth embodiment can be obtained, and in comparison with the fourth embodiment,
There is no need to provide a refrigerant vapor bypass circuit or means for controlling the refrigerant vapor bypass circuit, and there is an advantage that the configuration is simple.

【0049】なお、図4、図5において、符号100〜
111で示されている構成要素は、不凝縮ガス抽気装置
であり、本発明と直接の関係がないので説明を省略し
た。
In FIGS. 4 and 5, reference numerals 100-
The component denoted by reference numeral 111 is a non-condensable gas extraction device and is not directly related to the present invention, and therefore its description is omitted.

【0050】図6に本発明の第6の実施例を示す。本実
施例と前記第5の実施例との相違点は、第1、第2のバ
イパス回路の位置が異なることであり、他の構成は同じ
である。本実施例においては、第1のバイパス回路は、
高温溶液熱交換器36の加熱流体入り側と低温溶液熱交
換器42の加熱流体入り側を結んでおり、第2のバイパ
ス回路は、濃溶液管41の蒸発器34底部とほぼ同じ高
さの位置と蒸発器34の底部とを結んでいる。図6は、
機器、配管の配置は前記図3に示したものとほぼ同じで
あり、図5に示したものに比べ、本実施例は各バイパス
回路の配置がスペース的に容易であるという利点があ
る。本実施例においても、前記第5の実施例と同様の効
果が得られる。
FIG. 6 shows a sixth embodiment of the present invention. The difference between this embodiment and the fifth embodiment is that the positions of the first and second bypass circuits are different, and other configurations are the same. In this embodiment, the first bypass circuit is
The heating fluid inlet side of the high temperature solution heat exchanger 36 and the heating fluid inlet side of the low temperature solution heat exchanger 42 are connected to each other, and the second bypass circuit has substantially the same height as the bottom of the evaporator 34 of the concentrated solution pipe 41. It connects the position to the bottom of the evaporator 34. FIG.
The arrangement of equipment and piping is almost the same as that shown in FIG. 3, and in comparison with the arrangement shown in FIG. 5, this embodiment has an advantage that the arrangement of each bypass circuit is easy in terms of space. Also in this embodiment, the same effect as that of the fifth embodiment can be obtained.

【0051】図7に本発明の第7の実施例を示す。本実
施例と前記第6の実施例との相違点は、前記第6の実施
例は冷媒制御弁21が凝縮器26の外に設けられている
のに対し、本実施例では冷媒制御弁21が凝縮器26の
中に配置されていることであり、他の構成は同じであ
る。本実施例によれば、第6の実施例の効果に加え、配
管量、つまり部品数が少なく、工作が容易であるという
利点がある。
FIG. 7 shows a seventh embodiment of the present invention. The difference between the present embodiment and the sixth embodiment is that the refrigerant control valve 21 is provided outside the condenser 26 in the sixth embodiment, whereas the refrigerant control valve 21 is provided in the present embodiment. Are arranged in the condenser 26, and other configurations are the same. According to the present embodiment, in addition to the effect of the sixth embodiment, there is an advantage that the amount of piping, that is, the number of parts is small, and the work is easy.

【0052】上記各実施例では、第2のバイパス回路
は、濃溶液管41と蒸発器底部もしくは吸収器底部を接
続するようになっているが、第2のバイパス回路を設け
る目的は吸収溶液を吸収器の冷却水コイル上に散布する
ことなく溶液循環ポンプに吸引させることであり、濃溶
液管41と希溶液吸引管52を弁を介して連通するよう
にしてもよい。また、上記第1〜3の実施例では、溶液
バイパス弁11,13や冷媒蒸気バイパス弁43は、コ
ントローラ18に入力される蒸気の圧力信号に基づいて
開閉され、第4〜7の実施例では、コントローラ18に
入力される高温再生器内の吸収溶液の温度を示す信号に
基づいて開閉されるが、高温再生器に供給される蒸気の
圧力と高温再生器内の吸収溶液の温度とは一定の対応関
係にあるから、この組合せは、逆であっても差し支えな
い。
In each of the above-mentioned embodiments, the second bypass circuit connects the concentrated solution pipe 41 to the bottom of the evaporator or the bottom of the absorber. However, the purpose of providing the second bypass circuit is to supply the absorption solution. The solution circulation pump is sucked without spraying it on the cooling water coil of the absorber, and the concentrated solution pipe 41 and the dilute solution suction pipe 52 may be connected via a valve. Further, in the first to third embodiments, the solution bypass valves 11 and 13 and the refrigerant vapor bypass valve 43 are opened / closed based on the pressure signal of the vapor input to the controller 18, and in the fourth to seventh embodiments. The temperature of the absorbing solution in the high temperature regenerator and the temperature of the absorbing solution in the high temperature regenerator are constant. Therefore, the combination may be reversed.

【0053】蒸気供給側の弁の漏れにより高温再生器に
蒸気が流入する恐れがある場合、当該弁の遮断後、長時
間(例えば10時間)経過後の高温再生器内の吸収溶液
温度を検出し、設定温度(例えば70〜80℃)を超え
ている時に、稀釈運転モードで間歇運転するようにして
おけばよい。
When steam may flow into the high temperature regenerator due to leakage of the valve on the steam supply side, the temperature of the absorbing solution in the high temperature regenerator after a long time (for example, 10 hours) has elapsed after the valve is shut off is detected. However, when the temperature exceeds the set temperature (for example, 70 to 80 ° C.), the intermittent operation may be performed in the dilution operation mode.

【0054】[0054]

【発明の効果】請求項1,2に記載の本発明によれば、
高温再生器の加熱源として供給される蒸気の圧力が、二
重効用冷房運転を行うことができないほどに低下して
も、その低い圧力の蒸気で単効用冷房運転を行うことが
でき、蒸気を有効に利用することができる。
According to the present invention described in claims 1 and 2,
Even if the pressure of the steam supplied as the heating source of the high temperature regenerator drops to such an extent that the double-effect cooling operation cannot be performed, the low-efficiency steam can perform the single-effect cooling operation, and It can be used effectively.

【0055】請求項3,4に記載の本発明によれば、高
温再生器の加熱源として供給される蒸気の圧力が、二重
効用冷房運転を行うことができないほどに低下しても、
その低い圧力の蒸気で単効用冷房運転を行うことがで
き、さらに、単効用冷房運転を行うことができないほど
に低下しても稀釈運転モードで運転することができるか
ら、蒸気を有効に利用することができるとともに、イニ
シャルコストを増大させることなく吸収溶液の晶析を避
けることができる。
According to the third and fourth aspects of the present invention, even if the pressure of the steam supplied as the heating source of the high temperature regenerator is lowered to the extent that the double effect cooling operation cannot be performed,
The single-effect cooling operation can be performed with the low-pressure steam, and further, the dilution operation mode can be used even if the single-effect cooling operation cannot be performed. In addition, the crystallization of the absorbing solution can be avoided without increasing the initial cost.

【0056】請求項5,6に記載の本発明によれば、請
求項3,4に記載の発明による効果に加え、単効用運転
の際、分離器から凝縮器に冷媒蒸気を導く管路の流路断
面積が大きくすることができ、分離器の圧力が低くても
十分な量の冷媒蒸気を凝縮器に送って液冷媒とし、冷却
能力を確保することが容易になる。
According to the present invention as set forth in claims 5 and 6, in addition to the effects of the invention as set forth in claims 3 and 4, in the single-effect operation, a pipe line for guiding the refrigerant vapor from the separator to the condenser is provided. The cross-sectional area of the flow path can be increased, and even if the pressure of the separator is low, it is easy to ensure sufficient cooling capacity by sending a sufficient amount of refrigerant vapor to the condenser to be a liquid refrigerant.

【0057】請求項7,8に記載の本発明によれば、高
温再生器内の吸収溶液温度に基づいて、溶液バイパス弁
や冷媒蒸気バイパス弁の開閉が制御されるので、制御の
精度をあげることができる。
According to the present invention as set forth in claims 7 and 8, since the opening and closing of the solution bypass valve and the refrigerant vapor bypass valve are controlled based on the temperature of the absorbing solution in the high temperature regenerator, the accuracy of the control is improved. be able to.

【図面の簡単な説明】[Brief description of drawings]

【図1】本発明の第1の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 1 is a system diagram showing a steam-fired absorption chiller-heater according to a first embodiment of the present invention.

【図2】本発明の第2の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 2 is a system diagram showing a steam-fired absorption chiller / heater according to a second embodiment of the present invention.

【図3】本発明の第3の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 3 is a system diagram showing a steam-fired absorption chiller-heater according to a third embodiment of the present invention.

【図4】本発明の第4の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 4 is a system diagram showing a steam-fired absorption chiller-heater according to a fourth embodiment of the present invention.

【図5】本発明の第5の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 5 is a system diagram showing a steam-fired absorption chiller-heater according to a fifth embodiment of the present invention.

【図6】本発明の第6の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 6 is a system diagram showing a steam-fired absorption chiller-heater according to a sixth embodiment of the present invention.

【図7】本発明の第7の実施例である蒸気焚き吸収冷温
水機を示す系統図である。
FIG. 7 is a system diagram showing a steam-fired absorption chiller-heater according to a seventh embodiment of the present invention.

【図8】本発明の実施例を示す手順図である。FIG. 8 is a procedure diagram showing an embodiment of the present invention.

【図9】従来技術の例を示す系統図である。FIG. 9 is a system diagram showing an example of a conventional technique.

【符号の説明】[Explanation of symbols]

10 高温再生器 11 溶液バイ
パス弁A 12 希溶液バイパス管 13 溶液バイ
パス弁B 14 上昇管 15 濃溶液バ
イパス管 16 分離器 17 圧力検出
器 18 コントローラ 19 温度検出
器 20 中間濃溶液管 21 冷媒制御
弁 22 低温再生器 23 冷媒蒸気
コイル 26 凝縮器 30 液冷媒管 34 蒸発器 35 蒸発コイ
ル 36 高温溶液熱交換器 38 中間濃溶
液管 40,41 濃溶液管 42 低温溶液
熱交換器 43 冷媒蒸気バイパス弁 44 吸収器 45 冷媒蒸気バイパス回路 46 濃溶液分
配器 48 冷却水コイル(冷却水伝熱面) 52 希溶液吸
入管 53A,B,C 希溶液送液管 54 溶液循環
ポンプ 56 暖冷房切換弁 66 排熱熱交
換器
10 High Temperature Regenerator 11 Solution Bypass Valve A 12 Dilute Solution Bypass Pipe 13 Solution Bypass Valve B 14 Rise Pipe 15 Concentrated Solution Bypass Pipe 16 Separator 17 Pressure Detector 18 Controller 19 Temperature Detector 20 Intermediate Concentrated Solution Pipe 21 Refrigerant Control Valve 22 Low temperature regenerator 23 Refrigerant vapor coil 26 Condenser 30 Liquid refrigerant pipe 34 Evaporator 35 Evaporation coil 36 High temperature solution heat exchanger 38 Intermediate concentrated solution pipe 40,41 Concentrated solution pipe 42 Low temperature solution heat exchanger 43 Refrigerant vapor bypass valve 44 Absorption 45 Coolant vapor bypass circuit 46 Concentrated solution distributor 48 Cooling water coil (cooling water heat transfer surface) 52 Dilute solution suction pipe 53A, B, C Dilute solution feed pipe 54 Solution circulation pump 56 Heating / cooling switching valve 66 Exhaust heat Exchanger

Claims (9)

【特許請求の範囲】[Claims] 【請求項1】 高温再生器と、分離器と、低温再生器
と、凝縮器と、蒸発器と、吸収器と、前記分離器に中間
濃溶液管を介して加熱流体入り側を接続させた高温溶液
熱交換器と、この高温溶液熱交換器の加熱流体出側と前
記低温再生器を接続する中間濃溶液管と、前記低温再生
器に濃溶液管を介して加熱流体入り側を接続させた低温
溶液熱交換器と、この低温溶液熱交換器の加熱流体出側
と前記吸収器を接続した濃溶液管と、前記吸収器の希溶
液を前記低温溶液熱交換器及び高温溶液熱交換器の被加
熱流体側を経て前記高温再生器に送りこむ溶液循環ポン
プと、を含んでなる蒸気焚き吸収冷温水機において、前
記分離器で分離された中間濃溶液を低温再生器をバイパ
スして吸収器に導く第1のバイパス回路と、この第1の
バイパス回路に設けた溶液バイパス弁Aを高温再生器に
供給される蒸気の圧力の高低に応じて開閉する制御手段
とを設けたことを特徴とする蒸気焚き吸収冷温水機。
1. A high temperature regenerator, a separator, a low temperature regenerator, a condenser, an evaporator, an absorber, and said separator connected to a heating fluid inlet side via an intermediate concentrated solution pipe. A high temperature solution heat exchanger, an intermediate concentrated solution pipe connecting the heating fluid outlet side of the high temperature solution heat exchanger to the low temperature regenerator, and a heating fluid inlet side to the low temperature regenerator via a concentrated solution pipe. Low temperature solution heat exchanger, a concentrated solution pipe connecting the heating fluid outlet side of the low temperature solution heat exchanger and the absorber, and a dilute solution of the absorber to the low temperature solution heat exchanger and the high temperature solution heat exchanger. A solution circulating pump for sending the solution to the high temperature regenerator via the heated fluid side of the steam-fired absorption chiller-heater, the intermediate concentrated solution separated by the separator bypassing the low-temperature regenerator. And a first bypass circuit that leads to the A steam-fired absorption chiller-heater having a control means for opening and closing the solution bypass valve A according to the pressure of steam supplied to the high temperature regenerator.
【請求項2】 前記第1のバイパス回路が、高温溶液熱
交換器の加熱流体入り側と低温溶液熱交換器の加熱流体
入り側を接続するもの、高温溶液熱交換器の加熱流体入
り側と低温溶液熱交換器の加熱流体出側を接続するも
の、高温溶液熱交換器の加熱流体出側と低温溶液熱交換
器の加熱流体入り側を接続するもの、,高温溶液熱交換
器の加熱流体出側と低温溶液熱交換器の加熱流体出側を
接続するもののうちのいずれかであることを特徴とする
請求項1に記載の蒸気焚き吸収冷温水機。
2. The first bypass circuit connects the heating fluid inlet side of the high temperature solution heat exchanger and the heating fluid inlet side of the low temperature solution heat exchanger, and the heating fluid inlet side of the high temperature solution heat exchanger. Connecting the heating fluid outlet of the low temperature solution heat exchanger, connecting the heating fluid outlet of the high temperature solution heat exchanger to the heating fluid inlet of the low temperature solution heat exchanger, heating fluid of the high temperature solution heat exchanger The steam-fired absorption chiller-heater according to claim 1, characterized in that it is one of one that connects the outlet side and the heating fluid outlet side of the low temperature solution heat exchanger.
【請求項3】 前記第1のバイパス回路に加え、低温溶
液熱交換器の加熱流体出側と前記吸収器を接続する濃溶
液管と蒸発器底部もしくは吸収器の底部を溶液バイパス
弁Bを介して接続する第2のバイパス回路を設け、前記
制御手段を高温再生器に供給される蒸気の圧力の高低に
応じて前記溶液バイパス弁A,Bを開閉するものとした
ことを特徴とする請求項1または2に記載の蒸気焚き吸
収冷温水機。
3. In addition to the first bypass circuit, a concentrated solution pipe connecting the heating fluid outlet side of the low temperature solution heat exchanger and the absorber and the bottom of the evaporator or the bottom of the absorber are connected via a solution bypass valve B. 7. A second bypass circuit connected by connecting the solution bypass valves is provided, and the control means opens and closes the solution bypass valves A and B according to the level of the pressure of the steam supplied to the high temperature regenerator. 1. A steam-fired absorption cold / hot water machine according to 1 or 2.
【請求項4】 前記第1のバイパス回路に加え、低温溶
液熱交換器の加熱流体出側と溶液循環ポンプの吸入側を
溶液バイパス弁Bを介して連通する第2のバイパス回路
を設け、前記制御手段を高温再生器に供給される蒸気の
圧力の高低に応じて前記溶液バイパス弁A,Bを開閉す
るものとしたことを特徴とする請求項1または2に記載
の蒸気焚き吸収冷温水機。
4. In addition to the first bypass circuit, a second bypass circuit that connects the heating fluid outlet side of the low temperature solution heat exchanger and the suction side of the solution circulation pump via a solution bypass valve B is provided. The steam-fired absorption chiller-heater according to claim 1 or 2, wherein the control means opens and closes the solution bypass valves A and B in accordance with the pressure of steam supplied to the high temperature regenerator. .
【請求項5】 前記第1,第2のバイパス回路に加え、
前記分離器の気相部と前記凝縮器を冷媒蒸気バイパス弁
を介して連通する冷媒蒸気バイパス回路を設け、前記制
御手段を高温再生器に供給される蒸気の圧力の高低に応
じて前記溶液バイパス弁A,B及び冷媒蒸気バイパス弁
を開閉するものとしたことを特徴とする請求項3または
4に記載の蒸気焚き吸収冷温水機。
5. In addition to the first and second bypass circuits,
A refrigerant vapor bypass circuit that connects the vapor phase portion of the separator and the condenser via a refrigerant vapor bypass valve is provided, and the solution bypass is provided according to the level of the pressure of the vapor supplied to the high temperature regenerator. The steam-fired absorption chiller-heater according to claim 3 or 4, wherein the valves A and B and the refrigerant vapor bypass valve are opened and closed.
【請求項6】 低温再生器に内装された冷媒蒸気コイル
に、該冷媒蒸気コイル内を流れる冷媒の温度に応じて流
路断面積が変更される冷媒制御弁が設けられていること
を特徴とする請求項3または4に記載の蒸気焚き吸収冷
温水機。
6. A refrigerant vapor coil installed in a low-temperature regenerator is provided with a refrigerant control valve whose flow passage cross-sectional area is changed according to the temperature of the refrigerant flowing in the refrigerant vapor coil. The steam-fired absorption chiller-heater according to claim 3 or 4.
【請求項7】 制御手段が、高温再生器に供給される蒸
気の圧力の高低に代えて、高温再生器内の吸収溶液の温
度の高低に応じて溶液バイパス弁A,B及び冷媒蒸気バ
イパス弁の開閉を制御するものであることを特徴とする
請求項1乃至4のいずれかに記載の蒸気焚き吸収冷温水
機。
7. The solution bypass valves A and B and the refrigerant vapor bypass valve according to the temperature of the absorbing solution in the high temperature regenerator, instead of the pressure of the steam supplied to the high temperature regenerator. 5. The steam-fired absorption chiller / heater according to claim 1, wherein the steam-fired absorption chiller-heater is for controlling opening / closing of.
【請求項8】 制御手段が、高温再生器に供給される蒸
気の圧力の高低に代えて、高温再生器内の吸収溶液の温
度の高低に応じて溶液バイパス弁A,B及び冷媒蒸気バ
イパス弁の開閉を制御するものであることを特徴とする
請求項5または6に記載の蒸気焚き吸収冷温水機。
8. The control means, instead of the pressure of the steam supplied to the high temperature regenerator, instead of the pressure of the vapor supplied to the high temperature regenerator, the solution bypass valves A and B and the refrigerant vapor bypass valve depending on the temperature of the absorbing solution in the high temperature regenerator. The steam-fired absorption chiller-heater according to claim 5 or 6, which controls the opening and closing of.
【請求項9】 高温再生器と、分離器と、低温再生器
と、凝縮器と、蒸発器と、吸収器と、前記分離器に中間
濃溶液管を介して加熱流体入り側を接続させた高温溶液
熱交換器と、この高温溶液熱交換器の加熱流体出側と前
記低温再生器を接続する中間濃溶液管と、前記低温再生
器に濃溶液管を介して加熱流体入り側を接続させた低温
溶液熱交換器と、この低温溶液熱交換器の加熱流体出側
と前記吸収器を接続する濃溶液管と、前記吸収器の希溶
液を前記低温溶液熱交換器及び高温溶液熱交換器の被加
熱流体側を経て前記高温再生器に送りこむ溶液循環ポン
プと、を含んでなる蒸気焚き吸収冷温水機を制御する制
御方法において、高温再生器に供給される蒸気の圧力を
検出する手順と、検出した圧力が予め設定された第1の
圧力値未満で第2の圧力値以上のとき、前記分離器で分
離された中間濃溶液を、低温再生器をバイパスして吸収
器に内装された冷却水伝熱面に導く手順と、検出した圧
力が予め設定された前記第2の圧力値未満のとき、前記
分離器で分離された中間濃溶液を、低温再生器及び前記
冷却水伝熱面をバイパスして溶液循環ポンプに導く手順
と、を有してなることを特徴とする蒸気焚き吸収冷温水
機の制御方法。
9. A high temperature regenerator, a separator, a low temperature regenerator, a condenser, an evaporator, an absorber, and the separator are connected to a heating fluid inlet side via an intermediate concentrated solution pipe. A high temperature solution heat exchanger, an intermediate concentrated solution pipe connecting the heating fluid outlet side of the high temperature solution heat exchanger to the low temperature regenerator, and a heating fluid inlet side to the low temperature regenerator via a concentrated solution pipe. Low temperature solution heat exchanger, a concentrated solution pipe connecting the heating fluid outlet side of the low temperature solution heat exchanger and the absorber, and a dilute solution of the absorber to the low temperature solution heat exchanger and the high temperature solution heat exchanger. In the control method for controlling the steam-fired absorption chiller-heater, which comprises a solution circulation pump that is sent to the high-temperature regenerator through the heated fluid side of, a procedure for detecting the pressure of steam supplied to the high-temperature regenerator, , The detected pressure is less than the preset first pressure value and the second pressure When the force value or more, the intermediate concentrated solution separated by the separator is guided to the cooling water heat transfer surface installed in the absorber by-passing the low temperature regenerator, and the detected pressure is set in advance. When the pressure is less than the second pressure value, the intermediate concentrated solution separated by the separator is guided to the solution circulation pump by bypassing the low temperature regenerator and the cooling water heat transfer surface. A method for controlling a steam-fired absorption chiller-heater featuring.
JP06537395A 1995-03-24 1995-03-24 Steam-fired absorption chiller / heater and its control method Expired - Fee Related JP3240343B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP06537395A JP3240343B2 (en) 1995-03-24 1995-03-24 Steam-fired absorption chiller / heater and its control method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP06537395A JP3240343B2 (en) 1995-03-24 1995-03-24 Steam-fired absorption chiller / heater and its control method

Publications (2)

Publication Number Publication Date
JPH08261591A true JPH08261591A (en) 1996-10-11
JP3240343B2 JP3240343B2 (en) 2001-12-17

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110486096A (en) * 2019-08-08 2019-11-22 大唐郓城发电有限公司 A kind of high flexibility double reheat power generation sets peak regulation therrmodynamic system and method
CN112880067A (en) * 2021-01-22 2021-06-01 上海交通大学 Adsorption type refrigeration and dehumidification combined system and method thereof

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110486096A (en) * 2019-08-08 2019-11-22 大唐郓城发电有限公司 A kind of high flexibility double reheat power generation sets peak regulation therrmodynamic system and method
CN112880067A (en) * 2021-01-22 2021-06-01 上海交通大学 Adsorption type refrigeration and dehumidification combined system and method thereof
CN112880067B (en) * 2021-01-22 2022-04-26 上海交通大学 Adsorption type refrigeration and dehumidification combined system and method thereof

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