JPH0421110B2 - - Google Patents
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- Publication number
- JPH0421110B2 JPH0421110B2 JP58109432A JP10943283A JPH0421110B2 JP H0421110 B2 JPH0421110 B2 JP H0421110B2 JP 58109432 A JP58109432 A JP 58109432A JP 10943283 A JP10943283 A JP 10943283A JP H0421110 B2 JPH0421110 B2 JP H0421110B2
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- solution
- absorption
- temperature
- concentration
- pump
- Prior art date
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Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、溶液サイクルが休止中においても、
吸収溶液における結晶析出を防止する手段を講じ
た吸収冷凍機の運転方法に関する。[Detailed Description of the Invention] [Industrial Field of Application] The present invention provides the following advantages:
The present invention relates to a method of operating an absorption refrigerator that takes measures to prevent crystal precipitation in an absorption solution.
従来の吸収冷凍機は、その停止（発生器での加
熱を停止し、溶液サイクルを休止させる）中に結
晶析出を防止する機能を有していない。そのた
め、従来は、機械の停止時に冷媒を吸収溶液側に
移動して吸収溶液を希釈し、その際の濃度は、年
間を通しての最低温度（概略０℃）まで室温が低
下しても結晶析出を生じない濃度〔臭化リチウム
（LiBr）−水系の場合に約56％程度〕とするのが
通常である。そこで、夏季のように最低気温がそ
れほど低下しない場合、又は自動発停を繰返すよ
うな場合には、不必要に吸収溶液を薄めてしま
い、この過度の希釈は、省エネルギー及び起動特
性の点で好ましくなかつた。これらの点を添付図
面を参照して具体的に説明する。
Conventional absorption refrigerators do not have the ability to prevent crystal precipitation during shutdown (stopping heating in the generator and pausing the solution cycle). Therefore, conventionally, when the machine is stopped, the refrigerant is moved to the absorption solution side to dilute the absorption solution, and the concentration at that time is such that crystal precipitation does not occur even if the room temperature drops to the lowest temperature throughout the year (approximately 0°C). Normally, the concentration is set to such a level that it does not occur (approximately 56% in the case of lithium bromide (LiBr)-water systems). Therefore, when the minimum temperature does not drop much, such as in the summer, or when automatic start and stop operations are repeated, the absorption solution will be diluted unnecessarily, and this excessive dilution is undesirable in terms of energy saving and startup characteristics. Nakatsuta. These points will be specifically explained with reference to the accompanying drawings.
第１図は、従来の単効用吸収冷凍機の装置の一
例の系統図である。第１図において、Ｅは蒸発
器、Ａは吸収器、Ｇは発生器、Ｃは凝縮器、EX
は溶液熱交換器、RPは冷媒ポンプ、SPは溶液ポ
ンプ、SVは液戻し弁、HVは蒸気圧力調節弁を
意味する。 FIG. 1 is a system diagram of an example of a conventional single-effect absorption refrigerating machine. In Figure 1, E is an evaporator, A is an absorber, G is a generator, C is a condenser, EX
stands for solution heat exchanger, RP stands for refrigerant pump, SP stands for solution pump, SV stands for liquid return valve, and HV stands for vapor pressure control valve.
これらの機器を接続して、管路１〜５、散布管
６、管路７，８、散布管９、管路１０が設けられ
ている。冷媒ポンプRPの吐出側の管路８と溶液
ポンプSPの吸込側の管路とは、液戻し弁SVを備
えた希釈回路１３により接続されている。 Pipes 1 to 5, a dispersion pipe 6, pipes 7 and 8, a dispersion pipe 9, and a pipe 10 are provided to connect these devices. The discharge-side pipe line 8 of the refrigerant pump RP and the suction-side pipe line of the solution pump SP are connected by a dilution circuit 13 equipped with a liquid return valve SV.
１４は加熱管であり、発生器Ｇ内の溶液を加熱
するために蒸気などの熱媒流体が導かれ、その熱
媒流体の流量は蒸気圧力調節弁HVで制御され加
熱量の調節が行われる。１５は冷水管であり、冷
水出口温度を温度検出器１６にて検出し、その信
号により蒸気圧力調節弁HVを調節するようにな
つている。１７，１８は冷却水管である。 Reference numeral 14 denotes a heating pipe through which a heat medium fluid such as steam is guided in order to heat the solution in the generator G, and the flow rate of the heat medium fluid is controlled by a steam pressure control valve HV to adjust the amount of heating. . Reference numeral 15 denotes a cold water pipe, and the cold water outlet temperature is detected by a temperature detector 16, and the steam pressure regulating valve HV is adjusted based on the signal. 17 and 18 are cooling water pipes.
蒸発器Ｅ内の冷媒液面を検出するために、液面
検出器１２が設けられている。液面検出器１２に
は、異なる液面高さの検出が行うように複数個の
検出端S1，S4が配設されている。一般に溶液サイ
クル中の溶液の温度は、ほぼ蒸発器Ｅ内の冷媒液
量、すなわち液面高さに相当せしめることができ
る。検出端S4は、希釈完了レベルである。 A liquid level detector 12 is provided to detect the refrigerant liquid level within the evaporator E. The liquid level detector 12 is provided with a plurality of detection ends S 1 and S 4 so as to detect different liquid level heights. Generally, the temperature of the solution during the solution cycle can be made to approximately correspond to the amount of refrigerant liquid in the evaporator E, that is, the liquid level height. The detection end S4 is the dilution completion level.
第１図に示した吸収冷凍機に停止信号が入る
と、発生器の加熱を停止すると共に、弁SVを開
として蒸発器内の冷媒液を溶液側に移行する。冷
媒の液レベルS4により、弁SVを閉とすると共に
冷媒ポンプを停止して冷媒移行を完了させる。溶
液側に局所的な高濃度領域が残ることを避けるた
め、すなわち吸収溶液濃度の平均化を図るため
に、溶液ポンプの運転は続行し、所定時間後に溶
液ポンプを停止すると共に冷却水ポンプも停止す
る。なお、冷水ポンプの運転は、吸収冷凍機に対
する信号の種類により、冷却水と共に止める場合
もあれば、続行する場合もある（冷水温が低下
し、一時的に吸収冷凍機を停止する場合は冷水ポ
ンプの運転を続行する）。ただし、完全に運転を
完了する停止であれば、冷水ポンプの運転も停止
する。前記のような運転を行つた場合の各溶液の
温度変化等を第２図に示す。すなわち第２図は、
従来の吸収冷凍機の停止時における吸収溶液の温
度及び濃度の経時変化を、時間（分）（横軸）と、
温度（℃）（縦軸）及び吸収溶液の平均濃度ξｍ
（重量％）（縦軸）との関係で示したグラフであ
る。第２図において、tGは発生器出口の液温、tA
は溶液熱交換器出口（吸収器入口）の液温、tWは
冷却水温を意味する。第２図に示したように、従
来は、希釈完了後の吸収溶液の平均濃度は、該液
温が０℃程度まで低下しても結晶が析出しないよ
うな濃度に希釈している。 When a stop signal is input to the absorption refrigerator shown in FIG. 1, heating of the generator is stopped, and valve SV is opened to transfer the refrigerant liquid in the evaporator to the solution side. Depending on the refrigerant liquid level S4 , the valve SV is closed and the refrigerant pump is stopped to complete the refrigerant transfer. In order to avoid leaving a local high concentration area on the solution side, that is, to average the concentration of the absorbed solution, the solution pump continues to operate, and after a predetermined time, the solution pump is stopped and the cooling water pump is also stopped. do. Depending on the type of signal sent to the absorption chiller, the operation of the chilled water pump may be stopped along with the cooling water or continued (if the chilled water temperature drops and the absorption chiller is temporarily stopped, the operation of the chilled water pump is (continue pump operation). However, if the stoppage completes the operation, the cold water pump will also stop operating. FIG. 2 shows the temperature changes of each solution when the above-mentioned operation was performed. In other words, Figure 2 is
Changes in the temperature and concentration of the absorption solution over time when a conventional absorption refrigerator is stopped are expressed as time (minutes) (horizontal axis),
Temperature (°C) (vertical axis) and average concentration of absorption solution ξm
(wt%) (vertical axis). In Figure 2, t G is the liquid temperature at the generator outlet, t A
is the liquid temperature at the solution heat exchanger outlet (absorber inlet), and t W is the cooling water temperature. As shown in FIG. 2, conventionally, the average concentration of the absorption solution after completion of dilution is such that crystals do not precipitate even if the temperature of the solution drops to about 0°C.
こうすると、再起動時には希釈された溶液を所
定の濃度まで加熱濃縮する必要があり、これに要
する時間と消費エネルギーはかなりのものであ
る。他方、短時間の停止の場合に、過度の希釈が
好ましくないことは明らかである。その際、希釈
を行わない方法も考えられるが、結晶析出の危険
性と再起動に要する時間の不定性のため、やはり
好ましくない。 In this case, when restarting, it is necessary to heat and concentrate the diluted solution to a predetermined concentration, which requires considerable time and energy consumption. On the other hand, it is clear that excessive dilution is undesirable in the case of short stoppages. At that time, a method without dilution can be considered, but it is still not preferable because of the risk of crystal precipitation and the uncertainty of the time required for restarting.
本発明は、従来技術の問題点を解決するために
なされたものであり、その目的は、過度の希釈に
よるエネルギーの浪費を防ぎ、かつ起動特性が良
好な吸収冷凍機を提供することにある。
The present invention has been made to solve the problems of the prior art, and its purpose is to provide an absorption refrigerator that prevents energy wastage due to excessive dilution and has good startup characteristics.
本発明を概説すれば、本発明は吸収冷凍機の運
転方法に関する発明であつて、溶液サイクルと冷
凍サイクルとが形成されている吸収冷凍機を運転
する方法において、溶液サイクルの休止中も含め
て常時、吸収溶液の濃度と温度とを検知し、吸収
溶液の温度と結晶析出の濃度との既知の相関々係
より吸収溶液の結晶析出を監視し、溶液サイクル
の休止中に運転状態の濃度で休止した吸収溶液が
結晶析出の温度の限界値に近付いた場合に、冷媒
ポンプと溶液ポンプとを発停させて、温度の低下
分に見合うだけ必要最小限の吸収溶液の希釈を行
つて、結晶析出の防止を段階的に行うことを特徴
とする。
To summarize the present invention, the present invention relates to a method of operating an absorption chiller, and the present invention relates to a method of operating an absorption chiller in which a solution cycle and a refrigeration cycle are formed. The concentration and temperature of the absorption solution are constantly detected, the crystal precipitation of the absorption solution is monitored based on the known correlation between the temperature of the absorption solution and the concentration of crystal precipitation, and the concentration of the absorption solution is monitored at the operating state concentration during pauses in the solution cycle. When the temperature of the resting absorption solution approaches the limit value for crystal precipitation, the refrigerant pump and the solution pump are started and stopped to dilute the absorption solution to the minimum necessary amount to compensate for the temperature drop, and the crystal precipitation is performed. It is characterized by preventing precipitation in stages.
本発明は、吸収冷凍機の停止時に、吸収溶液に
できるだけ多量の濃度エネルギーを保有させたま
まの状態で休止を行い、エネルギーの無駄な消費
をなくすと共に、起動（再起動）をも速くするこ
とを意図したものである。そして、高濃度で休止
させるため結晶析出の危険性が生じるので、従来
とは異なり、溶液サイクルの休止中であつても、
常時結晶析出の監視を行い、吸収溶液に結晶析出
の危険が生じた場合、所定の濃度までの希釈、す
なわち必要最小限の濃度付近までの希釈を行うも
のである。更に、吸収溶液の冷却も、必要最小限
の冷却に止めてエネルギー消費を少なくする。し
かして、吸収冷凍機で使用する冷媒、例えば臭化
リチウム−水系では、温度と結晶析出の濃度との
間に、直線で表される相関関係があるから、上記
の必要最小限の濃度とは、冷媒ポンプを運転し、
希溶液と濃溶液とを混合して、ほぼ均一化した吸
収溶液の濃度、すなわち既述のξｍが、吸収冷凍
機の周囲温度（又は吸収溶液の温度）における結
晶析出濃度未満でその直下濃度を意味する。また
前記した必要最小限の冷却とは、１つには、二重
効用吸収冷凍機を全負荷状態で冷媒ポンプを停止
すると高温発生器内圧が高く、高温発生器と低温
発生器間の液シールが利かず、ガスバイパスが生
じて異常音が発生すると共に、熱交換器の腐食、
摩耗が発生するので、最低液シールの破れない圧
力（又は温度）まで冷却しておく必要があり、こ
の必要最小限の冷却をいう。また２つとしては、
単効用又は二重効用のいずれであつても、チユー
ブの熱膨張又は溶液ポンプの許容値等から、吸収
器に直接導入してよい溶液の温度には上限があ
り、その温度程度まで冷却しておく必要があるた
め、これを必要最小限の冷却という。 The present invention aims to stop an absorption refrigerator while retaining as much concentration energy as possible in the absorption solution, thereby eliminating wasteful energy consumption and speeding up startup (restart). It is intended. Since there is a risk of crystal precipitation due to suspension at high concentrations, unlike conventional methods, even during suspension of the solution cycle,
Crystal precipitation is constantly monitored, and if there is a risk of crystal precipitation in the absorption solution, it is diluted to a predetermined concentration, that is, to around the minimum necessary concentration. Furthermore, cooling of the absorption solution is kept to the minimum necessary to reduce energy consumption. However, in the case of refrigerants used in absorption refrigerators, such as lithium bromide-water systems, there is a linear correlation between temperature and the concentration of crystallization, so the above-mentioned minimum concentration is , operate the refrigerant pump,
The concentration of the absorbing solution made almost uniform by mixing the dilute solution and the concentrated solution, that is, the above-mentioned ξm, is lower than the crystal precipitation concentration at the ambient temperature of the absorption refrigerator (or the temperature of the absorbing solution) and the concentration immediately below it. means. In addition, the above-mentioned minimum necessary cooling means that, for one thing, when the refrigerant pump is stopped with a double-effect absorption refrigerator at full load, the internal pressure of the high-temperature generator is high, and the liquid seal between the high-temperature generator and the low-temperature generator is gas bypass occurs, causing abnormal noise and corrosion of the heat exchanger.
Since abrasion occurs, it is necessary to cool the liquid to the minimum pressure (or temperature) that does not break the liquid seal, and refers to this minimum necessary cooling. Also, two things are
Regardless of whether it is single effect or dual effect, there is an upper limit to the temperature of the solution that can be directly introduced into the absorber due to the thermal expansion of the tube or the allowable value of the solution pump, and the solution must be cooled to that temperature. This is called the minimum necessary cooling.
本発明における吸収溶液の濃度及び温度の検知
は、溶液熱交換器濃溶液出口部で行うのが好適で
ある。それは、他の場所でもよいが、通常運転時
に当該箇所が最も結晶析出を生じやすい場所であ
り、また停止後の溶液混合をほとんど行わずに止
める場合には、当該箇所が最高濃度を示すからで
ある。 In the present invention, the concentration and temperature of the absorption solution are preferably detected at the concentrated solution outlet of the solution heat exchanger. Although it may be any other location, this is the location where crystal precipitation is most likely to occur during normal operation, and if the solution is stopped with little mixing after stopping, this location will have the highest concentration. be.
しかして温度は、熱電対又は測温抵抗体等の通
常の温度センサーで容易に測定することができ
る。なお、この温度検知は、上記の箇所でもよい
が、自然冷却の際、最も温度低下の大きい箇所、
例えば大気に露出された細い配管中の吸収溶液に
ついて検知を行うのがよい。次に濃度は、濃度の
直接測定又は比重測定（例えば、浮力測定計、γ
線密度計若しくは振動式比重計を用いる測定）等
で測定することができる。その他の方法として、
濃度は、吸収溶液から分離されている冷媒量か
ら、その平均濃度を推定できる。それには、例え
ば蒸発器Ｅ内にフロート作動の可変抵抗子のよう
なレベル検出器Ｒを設け、そのレベルから分離冷
媒量を求める。他方、このレベル検出器を吸収器
Ａ内に設けてもよく、その場合に蒸発器Ｅにおけ
るとは逆に、液面が高い程、吸収溶液の濃度が小
なることを示す。なお、このレベル測定は、公知
の方法におけるように、連続測定でも段階的でも
よい（特開昭55−105157号公報参照）。 Temperature can thus easily be measured with conventional temperature sensors such as thermocouples or resistance temperature detectors. Note that this temperature detection may be performed at the locations mentioned above, but during natural cooling, the locations where the temperature decreases the most,
For example, it is preferable to perform detection on an absorbing solution in a thin pipe exposed to the atmosphere. Concentration can then be determined by direct measurement of concentration or specific gravity measurements (e.g., buoyancy meter, γ
It can be measured using a linear densitometer or a vibrating hydrometer. As another method,
The average concentration can be estimated from the amount of refrigerant separated from the absorption solution. To do this, for example, a level detector R such as a float-operated variable resistor is provided in the evaporator E, and the amount of separated refrigerant is determined from the level. On the other hand, this level detector may also be provided in the absorber A, in which case, contrary to in the evaporator E, a higher liquid level indicates a lower concentration of the absorption solution. Note that this level measurement may be continuous measurement or stepwise measurement as in a known method (see Japanese Patent Laid-Open No. 105157/1983).
本発明において、吸収溶液を希釈する手段は、
吸収溶液から分離されている冷媒液を吸収溶液中
に混入する設備、又は更にその後吸収溶液濃度の
平均化を行う設備であるのが好ましい。 In the present invention, the means for diluting the absorption solution is
Preferably, the equipment is one that mixes the refrigerant liquid that has been separated from the absorption solution into the absorption solution, or that further averages the concentration of the absorption solution afterwards.
本発明の吸収冷凍機における停止時の変化の一
例を、第３図により説明する。すなわち第３図
は、本発明の吸収冷凍機の一例の停止時における
吸収溶液の温度及び濃度の経時変化を、時間
（分）（横軸）と、温度（℃）（縦軸）及び吸収溶
液の平均濃度ξｍ（重量％）（縦軸）との関係で
示したグラフである。第３図における各符号は、
第２図と同義である。 An example of changes when the absorption refrigerator of the present invention is stopped will be explained with reference to FIG. 3. In other words, FIG. 3 shows the changes over time in the temperature and concentration of the absorption solution when an example of the absorption refrigerator of the present invention is stopped, in terms of time (minutes) (horizontal axis), temperature (°C) (vertical axis), and absorption solution. It is a graph shown in relation to the average concentration ξm (weight %) (vertical axis). Each symbol in Figure 3 is
This is the same as in Figure 2.
吸収冷凍機に停止信号が入ると、発生器での加
熱を停止する。溶液サイクルの温度が既述のよう
に許容できる温度まで低下してから（例えばtGを
検知）、冷却水ポンプを停止して溶液の冷却を停
止する(a)。溶液ポンプの運転は続行して、吸収溶
液濃度を均一化する。タイマー又は溶液サイクル
温度の差温（例えば、発生器出口と吸収器出口の
液温差）で、均一化の完了を検知してから、溶液
ポンプの運転を停止する(b)。吸収溶液温度は比較
的高い状態であり、これから自然放熱により徐徐
に冷却が行われる。溶液の濃度が、例えば62重量
％（LiBr−水系）であるとすれば、その結晶析
出温度は27℃程度であるので、余裕をみて吸収溶
液が32℃程度まで低下したら、吸収溶液の希釈を
行う(c)。この希釈により、例えば濃度を61重量％
にすれば、その結晶析出温度は22℃であるから、
当分放置しておいてよい。もし、この(b)〜(c)の間
で吸収冷凍機の再起動があれば、濃度エネルギー
の損失はなかつたことになる。従来では、第２図
に示したように、停止後すぐに希釈されてしまう
から、この点で本発明は従来のものに比して著し
い差を有するものである。 When the absorption refrigerator receives a stop signal, the generator stops heating. After the temperature of the solution cycle has decreased to an acceptable temperature as described above (eg, t G detected), the cooling water pump is stopped to stop cooling the solution (a). Operation of the solution pump continues to equalize the absorption solution concentration. After detecting the completion of homogenization using a timer or a difference in solution cycle temperature (for example, the difference in liquid temperature between the generator outlet and the absorber outlet), the operation of the solution pump is stopped (b). The absorption solution temperature is in a relatively high state, and cooling is gradually performed by natural heat dissipation. If the concentration of the solution is, for example, 62% by weight (LiBr-water system), the crystal precipitation temperature is about 27℃, so if the absorption solution drops to about 32℃, dilute the absorption solution. do (c). This dilution increases the concentration to 61% by weight, for example.
Then, the crystal precipitation temperature is 22℃, so
You can leave it alone for the time being. If the absorption refrigerator was restarted between (b) and (c), there would be no loss of concentration energy. In the conventional method, the liquid is diluted immediately after stopping as shown in FIG. 2, so the present invention is significantly different from the conventional method in this respect.
本発明による吸収溶液の希釈の際(c)に、蒸発器
チユーブ上に冷媒液を散布しながら吸収溶液を散
布すると、たとえ冷却水が通水されていなくても
冷水が凍結することがあるので、冷媒液の散布と
吸収溶液の散布とが同時に起らないようにするの
が好適である。また、冷水ポンプの運転は、既述
の従来技術と同様であるが、続行させておく方が
好適である。例えば、冷水ポンプが停止している
場合には、冷水ポンプを起動し、蒸発器に被冷却
流体を供給しながら、冷媒液の混入、吸収溶液の
平均化を行う。 When diluting the absorption solution according to the present invention (c), if the absorption solution is sprinkled while spraying the refrigerant liquid onto the evaporator tube, the cold water may freeze even if the cooling water is not flowing. It is preferable that the dispersion of the refrigerant liquid and the dispersion of the absorption solution do not occur at the same time. Further, although the operation of the cold water pump is similar to that of the prior art described above, it is preferable to continue operating the cold water pump. For example, when the cold water pump is stopped, the cold water pump is started and the refrigerant liquid is mixed in and the absorption solution is averaged while supplying the fluid to be cooled to the evaporator.
ただし、停止時の運転状態が低負荷の場合に
は、発生器の圧力は比較的低く、吸収溶液をほと
んど冷却せずに溶液ポンプを停止することができ
る。この場合、吸収溶液の均一化はほとんどでき
ていないが、前記したように、最高濃度部、又は
最高濃度が容易に推定できる場所を監視するので
あれば、前述した均一化を行わなくても差支えな
い。 However, if the operating state at the time of shutdown is a low load, the pressure of the generator is relatively low, and the solution pump can be stopped with little cooling of the absorption solution. In this case, the absorption solution is hardly homogenized, but as mentioned above, if you are monitoring the highest concentration area or a place where the highest concentration can be easily estimated, there is no need to perform the above-mentioned homogenization. do not have.
以下、本発明の吸収冷凍機の運転の態様を列挙
して例示するが、本発明はこれら態様に限定され
ない。
Hereinafter, modes of operation of the absorption refrigerator of the present invention will be listed and illustrated, but the present invention is not limited to these modes.
なお第４図は、本発明の一実施の態様である吸
収冷凍機の装置の系統図である。第４図におい
て、第１図と同符号は第１図と同義であり、SV1
は弁、S1〜S4は液面検出端を意味する。 Note that FIG. 4 is a system diagram of an absorption refrigerating machine that is an embodiment of the present invention. In Figure 4, the same symbols as in Figure 1 have the same meanings as in Figure 1, and SV 1
is a valve, and S 1 to S 4 are liquid level detection ends.
１ 第３図における溶液ポンプ停止までの運転の
態様
(1) 溶液サイクル停止時に、吸収溶液中に冷媒
液の混入を行わないで、単に吸収溶液濃度の
平均化を行つた後（又は所定時間の経過後）、
溶液ポンプ停止する。1 Mode of operation until the solution pump stops in Figure 3 (1) When the solution cycle is stopped, the absorption solution concentration is simply averaged (or after a predetermined period of time) without mixing the refrigerant into the absorption solution. after the elapsed time),
Stop the solution pump.
(2) 溶液サイクル停止時に、発生器（二重効用
における高温発生器、単効用における発生
器）の圧力又は温度が所定の値以下になつた
とき、吸収溶液濃度の平均化が終了する前で
あつても冷却水ポンプを停止し、吸収溶液濃
度の平均化が終了後で、発生器の圧力又は温
度も所定の値以下になつたときに溶液ポンプ
を停止する。 (2) When the pressure or temperature of the generator (high-temperature generator for dual effect, generator for single effect) falls below a predetermined value when the solution cycle is stopped, before the averaging of the absorption solution concentration is completed. In any case, the cooling water pump is stopped, and after the absorption solution concentration has been averaged, the solution pump is stopped when the pressure or temperature of the generator also falls below a predetermined value.
２ 本発明による希釈の際の運転の態様
(1) 第４図でSV1がない場合
結晶析出の危険が生じた場合に、まず冷媒
ポンプRPを運転して、蒸発器Ｅ内の冷媒液
の所定量（例えば、第３図で62重量％のS2レ
ベルにある液を、61重量％のS3レベルとなる
まで）を、吸収溶液側に移行させる（このと
き、蒸発器チユーブに冷媒液が散布されても
差支えない）。冷媒ポンプRPを停止し、所定
時間経過後（例えば蒸発器チユーブ表面の冷
媒の落下をタイマー等で検知する）、溶液ポ
ンプSPを起動し、所定時間運転して吸収溶
液濃度の平均化を行う。2 Mode of operation during dilution according to the present invention (1) When SV 1 is not present in Fig. 4 If there is a risk of crystal precipitation, first operate the refrigerant pump RP to drain the refrigerant liquid in the evaporator E. Transfer a predetermined amount (for example, the liquid at the S 2 level of 62% by weight in Figure 3 to the S 3 level of 61% by weight) to the absorption solution side (at this time, the refrigerant liquid is transferred to the evaporator tube). (There is no problem even if it is dispersed). The refrigerant pump RP is stopped, and after a predetermined period of time has elapsed (for example, the fall of refrigerant on the surface of the evaporator tube is detected by a timer, etc.), the solution pump SP is started and operated for a predetermined period of time to average the absorption solution concentration.
(2) 第４図でSV1がある場合
SV1を閉じて、冷媒ポンプRPを運転して
も、蒸発器Ｅチユーブ上に冷媒液が散布しな
いようにする。冷媒ポンプRPと溶液ポンプ
SPの起動は同時でよい。所定量〔例えば、
上記(1)の場合と同様〕の冷媒液移行後の冷媒
ポンプRPの停止は、タイマー又は蒸発器レ
ベル（吸収溶液の平均濃度に相当）で行い、
溶液ポンプSPの停止は、平均化の完了をタ
イマー又は濃度検知して行う。 (2) If SV 1 is present in Figure 4, close SV 1 to prevent refrigerant liquid from spraying onto the evaporator E tube even if the refrigerant pump RP is operated. Refrigerant pump RP and solution pump
SPs can be started at the same time. A predetermined amount [e.g.
The refrigerant pump RP is stopped after the refrigerant liquid transfer (same as in case (1) above) is performed by a timer or at the evaporator level (corresponding to the average concentration of the absorption solution).
The solution pump SP is stopped by detecting the completion of averaging using a timer or by detecting the concentration.
以上詳細に説明したように、本発明の吸収冷凍
機によれば、運転停止時の吸収溶液の濃度が濃く
ても、そのまま停止することができ、更には、停
止時の吸収溶液の温度を高めておくことにより、
長時間の高濃度放置が可能となり、従来の運転停
止時に希釈のため放出される濃度エネルギー及び
温度エネルギーを貯えておくことが可能となつ
た。したがつて、不必要に吸収溶液の濃度を薄く
しないで運転停止をすることが可能となり、従来
の吸収冷凍機と比較して、熱源及びポンプ動力の
省エネルギー化が図れるだけでなく、起動特性も
改善され、更によりきめの細かに制御ができると
いう顕著な効果が奏せられる。
As explained in detail above, according to the absorption refrigerator of the present invention, even if the concentration of the absorption solution at the time of shutdown is high, the operation can be stopped as is, and furthermore, the temperature of the absorption solution at the time of shutdown can be increased. By keeping
It has become possible to leave high concentrations for long periods of time, and it has become possible to store the concentration energy and temperature energy that would otherwise be released for dilution when the operation is stopped. Therefore, it is possible to shut down the operation without unnecessarily diluting the concentration of the absorption solution, and compared to conventional absorption refrigerators, not only can the heat source and pump power be saved, but the startup characteristics are also improved. This has the remarkable effect of providing improved and even more fine-grained control.
第１図は従来の単効用吸収冷凍機の装置の一例
の系統図、第２図は従来の吸収冷凍機の停止時に
おける、時間と吸収溶液の温度及び平均濃度との
関係を示すグラフ、第３図は本発明の吸収冷凍機
の停止時における、時間と吸収溶液の温度及び平
均濃度との関係を示すグラフ、第４図は本発明の
一実施の態様である吸収冷凍機の装置の系統図で
ある。
Ｅ：蒸発器、Ａ：吸収器、Ｇ：発生器、Ｃ：凝
縮器、EX：溶液熱交換器、RP：冷媒ポンプ、
SP：溶液ポンプ、SV：液戻し弁、HV：蒸気圧
力調節弁、６及び９：散布管、１２：液面検出
器、１３：希釈回路、１４：加熱管、１６：温度
検出器。
Figure 1 is a system diagram of an example of a conventional single-effect absorption refrigerating machine, and Figure 2 is a graph showing the relationship between time, temperature, and average concentration of the absorption solution when the conventional absorption refrigerating machine is stopped. Figure 3 is a graph showing the relationship between time and the temperature and average concentration of the absorption solution when the absorption refrigerator of the present invention is stopped, and Figure 4 is a system diagram of an apparatus for an absorption refrigerator that is an embodiment of the present invention. It is a diagram. E: Evaporator, A: Absorber, G: Generator, C: Condenser, EX: Solution heat exchanger, RP: Refrigerant pump,
SP: solution pump, SV: liquid return valve, HV: steam pressure control valve, 6 and 9: spray pipe, 12: liquid level detector, 13: dilution circuit, 14: heating pipe, 16: temperature detector.
Claims (1)
いる吸収冷凍機を運転する方法において、溶液サ
イクルの休止中も含めて常時、吸収溶液の濃度と
温度とを検知し、吸収溶液の温度と結晶析出の濃
度との既知の相関々係より吸収溶液の結晶析出を
監視し、溶液サイクルの休止中に運転状態の濃度
で休止した吸収溶液が、結晶析出の温度の限界値
に近付いた場合に、冷媒ポンプと溶液ポンプとを
発停させて、温度の低下分に見合うだけ必要最小
限の吸収溶液の希釈を行つて、結晶析出の防止を
段階的に行うことを特徴とす吸収冷凍機の運転方
法。1. In a method of operating an absorption refrigerator in which a solution cycle and a refrigeration cycle are formed, the concentration and temperature of the absorption solution are detected at all times, including during suspension of the solution cycle, and the temperature of the absorption solution and the temperature of crystal precipitation are monitored. The crystallization of the absorption solution is monitored based on the known correlation with the concentration, and if the absorption solution resting at the operating state concentration approaches the temperature limit for crystallization during the suspension of the solution cycle, the refrigerant pump is activated. A method for operating an absorption chiller, characterized in that prevention of crystal precipitation is carried out in stages by starting and stopping a solution pump and a solution pump to dilute the absorption solution to the minimum necessary amount commensurate with the decrease in temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10943283A JPS602858A (en) | 1983-06-20 | 1983-06-20 | Absorption refrigerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10943283A JPS602858A (en) | 1983-06-20 | 1983-06-20 | Absorption refrigerator |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP30710691A Division JPH0613941B2 (en) | 1991-10-28 | 1991-10-28 | Absorption refrigerator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS602858A JPS602858A (en) | 1985-01-09 |
| JPH0421110B2 true JPH0421110B2 (en) | 1992-04-08 |
Family
ID=14510094
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10943283A Granted JPS602858A (en) | 1983-06-20 | 1983-06-20 | Absorption refrigerator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS602858A (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62200871A (en) * | 1986-02-28 | 1987-09-04 | Canon Inc | Color image information input device |
| JPH0448455Y2 (en) * | 1986-03-19 | 1992-11-16 | ||
| JPH0240459A (en) * | 1988-08-01 | 1990-02-09 | Hitachi Zosen Corp | Method for preventing crystal precipitation of absorption liquid in absorption refrigerator |
| JP2672619B2 (en) * | 1989-01-13 | 1997-11-05 | 株式会社日立製作所 | Crystallization method of absorption refrigerator |
| JPH0813169B2 (en) * | 1990-12-01 | 1996-02-07 | 三洋電機株式会社 | Charging device and charging method |
| JP3331678B2 (en) * | 1993-07-01 | 2002-10-07 | 東京瓦斯株式会社 | Absorption refrigerator |
| JP2902305B2 (en) * | 1994-07-15 | 1999-06-07 | リンナイ株式会社 | Absorption air conditioner |
| JP3920619B2 (en) * | 2001-10-19 | 2007-05-30 | 株式会社日立製作所 | Absorption chiller / heater and control method thereof |
| JP4155797B2 (en) * | 2002-11-01 | 2008-09-24 | 株式会社荏原製作所 | Operation method of absorption refrigerator |
| CN101852521B (en) * | 2010-06-10 | 2012-09-12 | 大连三洋制冷有限公司 | Load adjusting method |
| CN101852524B (en) * | 2010-06-10 | 2012-07-04 | 大连三洋制冷有限公司 | Refrigerant pollution automatic monitoring and scavenging system |
| JP2018105603A (en) * | 2016-12-28 | 2018-07-05 | 荏原冷熱システム株式会社 | Absorption refrigerator, control program, and absorption refrigerator control method |
| JP6820050B2 (en) * | 2017-03-07 | 2021-01-27 | 荏原冷熱システム株式会社 | Absorption chiller, control program and control method of absorption chiller |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5595071A (en) * | 1979-01-12 | 1980-07-18 | Ebara Mfg | Absorption type refrigerating machine |
| JPS55105157A (en) * | 1979-02-05 | 1980-08-12 | Ebara Mfg | Absorption refrigerating machine |
-
1983
- 1983-06-20 JP JP10943283A patent/JPS602858A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS602858A (en) | 1985-01-09 |
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