JP2020076516A - Heat pump cycle and heat pump type steam generation device - Google Patents
Heat pump cycle and heat pump type steam generation device Download PDFInfo
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本発明は、ヒートポンプサイクルおよびヒートポンプ式蒸気生成装置に関するものである。 The present invention relates to a heat pump cycle and a heat pump type steam generator.
ヒートポンプ装置には、圧縮を二段階にし、一部冷媒を中間経路で高段圧縮入口側に導入することで圧縮機単段当たりの圧縮比を低減するようにしたものがある。この種のヒートポンプ装置では、低段側サイクルの冷媒流量を必要最小限とすることで低段側の圧縮動力を最小化することができ、単段サイクルに比べて効率を向上することが可能となる（例えば特許文献１参照）。 There is a heat pump device in which compression is performed in two stages and a partial refrigerant is introduced to a high stage compression inlet side in an intermediate path to reduce the compression ratio per single stage of the compressor. In this type of heat pump device, it is possible to minimize the compression power on the low-stage side by minimizing the refrigerant flow rate in the low-stage cycle, and it is possible to improve the efficiency compared to the single-stage cycle. (For example, see Patent Document 1).
ところで、ヒートポンプ装置において凝縮器によって被加熱媒体の加熱をする際に、その出力制御を行うためには凝縮器を流通する冷媒の流量を取得する必要がある。例えば特許文献２では、単段圧縮のヒートポンプサイクルにおいて圧縮機吸入圧力、圧縮機吸入温度、圧縮機回転数および圧縮機定数から冷媒の流量を演算する技術について開示されている。一方、中間経路からの冷媒を高段圧縮機入口に合流させる二段圧縮サイクルでは、高段圧縮機に吸入される冷媒の状態を測定することが難しく、従来の流量測定手段を用いることができない。二段圧縮サイクルにおいて高段側を流通する冷媒の流量を求めるためには、高段サイクルの流路に別途流量計を設ける必要があるが、流量計は高価であることから、二段圧縮サイクルにおいても廉価かつ簡易な手段で冷媒流量を求めることが望まれている。 By the way, when the medium to be heated is heated by the condenser in the heat pump device, it is necessary to obtain the flow rate of the refrigerant flowing through the condenser in order to control the output thereof. For example, Patent Document 2 discloses a technique for calculating the flow rate of a refrigerant from a compressor suction pressure, a compressor suction temperature, a compressor rotation speed, and a compressor constant in a single-stage compression heat pump cycle. On the other hand, in the two-stage compression cycle in which the refrigerant from the intermediate path joins the high-stage compressor inlet, it is difficult to measure the state of the refrigerant drawn into the high-stage compressor, and the conventional flow rate measuring means cannot be used. .. In order to obtain the flow rate of the refrigerant flowing through the high-stage side in the two-stage compression cycle, it is necessary to install a separate flow meter in the flow path of the high-stage cycle, but since the flow meter is expensive, the two-stage compression cycle It is also desired to obtain the refrigerant flow rate by a low cost and simple means.
本発明は、上記の課題に鑑みてなされたものであって、二段圧縮サイクルにおいても流量計を用いずに凝縮器を流通する冷媒流量を求めることができるヒートポンプサイクルおよびヒートポンプ式蒸気生成装置を提供することを目的とする。 The present invention has been made in view of the above problems, and a heat pump cycle and a heat pump type steam generator that can determine the flow rate of a refrigerant flowing through a condenser without using a flow meter even in a two-stage compression cycle. The purpose is to provide.
上記目的を達成するため、本発明に係るヒートポンプサイクルは、低段圧縮機構と高段圧縮機構とを持つ二段圧縮機構と、凝縮器と、高圧の冷媒を膨張し中間圧の冷媒および低圧の冷媒を生成する膨張機構と、低圧の冷媒を導入する蒸発器とを環状に接続し、前記中間圧の冷媒を前記高段圧縮機構に供給する中間経路を備えたヒートポンプサイクルにおいて、前記凝縮器と前記膨張機構との間に設けられ、前記凝縮器を通過した冷媒を減圧する減圧部と、前記高段圧縮機構から前記減圧部までの冷媒圧力を測定する減圧部入口圧力測定手段と、前記凝縮器から前記減圧部までの冷媒温度を測定する減圧部入口温度測定手段と、前記減圧部で生じた圧力損失を測定する圧力損失測定手段と、前記減圧部入口圧力測定手段で測定された圧力と前記減圧部入口温度測定手段で測定された温度とに基づき、前記前記減圧部に流入する冷媒密度を算出する密度算出部と、前記密度算出部で算出された密度と前記圧力損失測定手段で測定された圧力損失とに基づき、前記凝縮器を流通する冷媒の流量を算出する流量算出部と、を備えることを特徴とする。 To achieve the above object, the heat pump cycle according to the present invention includes a two-stage compression mechanism having a low-stage compression mechanism and a high-stage compression mechanism, a condenser, and a medium-pressure refrigerant and a low-pressure medium for expanding a high-pressure refrigerant. An expansion mechanism that generates a refrigerant and an evaporator that introduces a low-pressure refrigerant are connected in an annular shape, and in the heat pump cycle including an intermediate path that supplies the intermediate-pressure refrigerant to the high-stage compression mechanism, the condenser and A decompression unit provided between the expansion mechanism and decompressing the refrigerant that has passed through the condenser, a decompression unit inlet pressure measuring unit that measures the refrigerant pressure from the high-stage compression mechanism to the decompression unit, and the condensation Pressure reducing section inlet temperature measuring means for measuring the refrigerant temperature from the pressure reducing unit to the pressure reducing section, pressure loss measuring means for measuring the pressure loss generated in the pressure reducing section, and pressure measured by the pressure reducing section inlet pressure measuring means. Based on the temperature measured by the pressure reducing section inlet temperature measuring means, a density calculating section for calculating the density of the refrigerant flowing into the pressure reducing section, the density calculated by the density calculating section and the pressure loss measuring means. And a flow rate calculation unit that calculates the flow rate of the refrigerant flowing through the condenser based on the determined pressure loss.
また、本発明に係るヒートポンプ式蒸気生成装置は、前記蒸発器に熱源水を供給する熱源水供給部と、前記凝縮器に前記被加熱媒体として水を供給し、生成された蒸気を外部に送出する蒸気生成部と、をさらに備えることを特徴とする。 In addition, the heat pump type steam generator according to the present invention supplies water as the heated medium to the heat source water supply unit that supplies heat source water to the evaporator and the condenser, and sends the generated steam to the outside. And a steam generating unit for controlling the temperature.
本発明によれば、高価かつ複雑な構造の流量計を用いずに凝縮器を流通する冷媒流量を求めることが可能となるため、装置のコスト低減および構造の簡素化による装置全体の信頼性を向上させることが可能となる。 According to the present invention, it is possible to determine the flow rate of the refrigerant flowing through the condenser without using an expensive and complicated flow meter, so that the reliability of the entire device can be reduced by reducing the cost of the device and simplifying the structure. It is possible to improve.
また本発明によれば、減圧部によって生じた圧力損失が、ヒートポンプサイクルにおける膨張機構による減圧膨張の一部を担うような構成となっているため、圧力損失による熱効率の低下を防止することが可能となる。 Further, according to the present invention, since the pressure loss caused by the pressure reducing portion plays a part of the pressure reducing expansion by the expansion mechanism in the heat pump cycle, it is possible to prevent the decrease in thermal efficiency due to the pressure loss. Becomes
（第１実施形態）
以下、図面を参照しながら本発明にかかるヒートポンプ式蒸気生成装置の好適な実施の形態について詳細に説明する。
(First embodiment)
Hereinafter, preferred embodiments of a heat pump steam generator according to the present invention will be described in detail with reference to the drawings.
図１は、本発明の実施の形態であるヒートポンプ式蒸気生成装置１の構成を示す回路構成図である。ここで例示するヒートポンプサイクル１００は、二段圧縮二段膨張サイクルにより、工場排水や使用済冷却水等の排温水から排熱を回収して被加熱媒体である被加熱水を加熱し、温水や蒸気を生成するもので、配管によって順次接続された一体型二段圧縮機１０、凝縮器２１、高段膨張弁（高段膨張機構）５１、気液分離器３１、低段膨張弁（低段膨張機構）５２、蒸発器４１を備えている。 FIG. 1 is a circuit configuration diagram showing a configuration of a heat pump steam generator 1 according to an embodiment of the present invention. The heat pump cycle 100 illustrated here recovers exhaust heat from waste hot water such as factory drainage and used cooling water by a two-stage compression two-stage expansion cycle to heat heated water as a medium to be heated, An integrated two-stage compressor 10, a condenser 21, a high-stage expansion valve (high-stage expansion mechanism) 51, a gas-liquid separator 31, a low-stage expansion valve (low stage) An expansion mechanism) 52 and an evaporator 41 are provided.
一体型二段圧縮機１０は、低段圧縮部（低段圧縮機構）１１および高段圧縮部（高段圧縮機構）１２が一体となった二段圧縮機（多段圧縮機）であり、低段圧縮部１１の吐出口と高段圧縮部１２の吸入口との間の中間ポート１２ａは一体型二段圧縮機１０の筺体内部に設けられている。一体型二段圧縮機１０は例えば１軸型スクロール圧縮機である。低段圧縮部（低段圧縮機構）１１では蒸発器４１から供給された冷媒を中間圧まで圧縮し、高段圧縮部１２の中間吸入ポート１２ａに供給する。高段圧縮部１２は中間吸入ポート１２ａから導入された中間圧冷媒を高圧まで圧縮し、凝縮器２１に供給する。凝縮器２１は、高段圧縮部１２から供給された冷媒と、蒸気生成部２００を流通する被加熱水との熱交換により、水を蒸発させ蒸気を生成するとともに冷媒を凝縮させる。低段圧縮部１１および高段圧縮部１２としては、別個に構成された圧縮機を採用してもよい。 The integrated two-stage compressor 10 is a two-stage compressor (multistage compressor) in which a low-stage compression unit (low-stage compression mechanism) 11 and a high-stage compression unit (high-stage compression mechanism) 12 are integrated, An intermediate port 12 a between the discharge port of the stage compression unit 11 and the suction port of the high stage compression unit 12 is provided inside the housing of the integrated two-stage compressor 10. The integrated two-stage compressor 10 is, for example, a single-axis scroll compressor. The low-stage compression section (low-stage compression mechanism) 11 compresses the refrigerant supplied from the evaporator 41 to an intermediate pressure and supplies the refrigerant to the intermediate suction port 12 a of the high-stage compression section 12. The high-stage compression unit 12 compresses the intermediate-pressure refrigerant introduced from the intermediate suction port 12 a to a high pressure and supplies it to the condenser 21. The condenser 21 heat-exchanges the refrigerant supplied from the high-stage compression section 12 and the heated water flowing through the steam generation section 200 to evaporate water to generate steam and condense the refrigerant. As the low-stage compression section 11 and the high-stage compression section 12, separately configured compressors may be adopted.
減圧部６１は、上流側および下流側の管路よりも内径が小さい細管路により構成され、凝縮器２１を通過して凝縮した液相の冷媒に対して圧力損失を付与する。減圧部６１の上流側配管と下流側配管には、減圧部で冷媒に生じた圧力損失を測定可能とする差圧計（圧力損失測定手段）６２が接続される。高段膨張弁５１は、減圧部６１を通過した液相の冷媒をさらに減圧して気液二相流とし、気液分離器３１に供給する。 The decompression unit 61 is configured by a thin pipe having an inner diameter smaller than that of the upstream and downstream pipes, and imparts a pressure loss to the liquid-phase refrigerant condensed through the condenser 21. A differential pressure gauge (pressure loss measuring means) 62 capable of measuring the pressure loss generated in the refrigerant in the pressure reducing section is connected to the upstream side pipe and the downstream side pipe of the pressure reducing section 61. The high-stage expansion valve 51 further depressurizes the liquid-phase refrigerant that has passed through the depressurization unit 61 to form a gas-liquid two-phase flow, and supplies the gas-liquid separator 31.
気液分離器３１は、高段膨張弁５１から供給された冷媒を導入する上部導入口３１ａ、内部で気液分離された冷媒の内、主に気相の冷媒を外部に吐出する上部吐出口３１ｂおよび主に液相の冷媒を外部に吐出する下部吐出口３１ｃを備えている。 The gas-liquid separator 31 includes an upper inlet 31a for introducing the refrigerant supplied from the high-stage expansion valve 51, and an upper outlet for mainly discharging a gas-phase refrigerant out of the refrigerant that has been gas-liquid separated inside. 31b and a lower discharge port 31c for discharging mainly the liquid-phase refrigerant to the outside.
低段膨張弁５２は、下部吐出口３１ｃを通じて気液分離器３１から吐出された冷媒を減圧して蒸発器４１に供給する。高段膨張弁５１及び低段膨張弁５２としては、与えられた指令に応じて開度を変更することのできる電磁弁を適用している。 The low-stage expansion valve 52 reduces the pressure of the refrigerant discharged from the gas-liquid separator 31 through the lower discharge port 31c and supplies it to the evaporator 41. As the high-stage expansion valve 51 and the low-stage expansion valve 52, electromagnetic valves whose opening can be changed according to a given command are applied.
蒸発器４１は、低段膨張弁５２を通過した冷媒と熱源水供給部３００から供給される熱源水との間で熱交換を行うことにより冷媒を蒸発させ、低段圧縮部１１に供給する。 The evaporator 41 evaporates the refrigerant by exchanging heat between the refrigerant that has passed through the low stage expansion valve 52 and the heat source water supplied from the heat source water supply unit 300, and supplies the refrigerant to the low stage compression unit 11.
また、ヒートポンプサイクル１００には、気液分離器３１の上部吐出口３１ｂと高段圧縮部１２の中間吸入ポート１２ａとの間を連通するように中間経路７１が設けてある。中間経路７１は、気液分離器３１の上部に貯留された冷媒を低段圧縮部１１から吐出された冷媒と共に高段圧縮部１２の中間吸入ポート１２ａに供給する。 Further, the heat pump cycle 100 is provided with an intermediate path 71 so as to connect the upper discharge port 31 b of the gas-liquid separator 31 and the intermediate suction port 12 a of the high-stage compression section 12. The intermediate path 71 supplies the refrigerant stored in the upper part of the gas-liquid separator 31 to the intermediate suction port 12 a of the high-stage compression section 12 together with the refrigerant discharged from the low-stage compression section 11.
密度測定手段８０は、凝縮器２１と減圧部６１の間に設けられた減圧部入口圧力センサ（減圧部入口圧力測定手段）８１および減圧部入口温度センサ（減圧部入口温度測定手段）８２からなる。減圧部入口圧力センサ８１は減圧部６１に流入する冷媒の圧力（減圧部入口冷媒圧力）ＰＨを、減圧部入口温度センサ８２は減圧部６１に流入する冷媒の温度（減圧部入口冷媒温度）Ｔａをそれぞれ測定する。また、凝縮器入口温度センサ（凝縮器入口温度測定手段）８３は高段圧縮部１２と凝縮器２１の間に設けられ、凝縮器２１に流入する冷媒の温度（凝縮器入口冷媒温度）Ｔｂを測定する。制御部４００は、ヒートポンプサイクル１００内を流通する冷媒の状態、例えば差圧計６２、減圧部入口圧力センサ８１、減圧部入口温度センサ８２、凝縮器入口温度センサ８３、その他図示しない各種センサの測定値に基づき、一体型二段圧縮機１０の運転停止制御および回転数制御、高段膨張弁５１および低段膨張弁５２の開度制御などを行う。 The density measuring means 80 includes a pressure reducing portion inlet pressure sensor (pressure reducing portion inlet pressure measuring means) 81 and a pressure reducing portion inlet temperature sensor (pressure reducing portion inlet temperature measuring means) 82 provided between the condenser 21 and the pressure reducing portion 61. .. The pressure reducing portion inlet pressure sensor 81 indicates the pressure of the refrigerant flowing into the pressure reducing portion 61 (pressure reducing portion inlet refrigerant pressure) PH, and the pressure reducing portion inlet temperature sensor 82 indicates the temperature of the refrigerant flowing into the pressure reducing portion 61 (pressure reducing portion inlet refrigerant temperature) Ta. Are measured respectively. Further, a condenser inlet temperature sensor (condenser inlet temperature measuring means) 83 is provided between the high-stage compression section 12 and the condenser 21, and measures the temperature of the refrigerant flowing into the condenser 21 (condenser inlet refrigerant temperature) Tb. taking measurement. The control unit 400 controls the state of the refrigerant flowing in the heat pump cycle 100, for example, the measured values of the differential pressure gauge 62, the pressure reducing unit inlet pressure sensor 81, the pressure reducing unit inlet temperature sensor 82, the condenser inlet temperature sensor 83, and other various sensors not shown. Based on the above, operation stop control and rotation speed control of the integrated two-stage compressor 10 and opening degree control of the high-stage expansion valve 51 and the low-stage expansion valve 52 are performed.
続いて図２に基づいてヒートポンプサイクル１００の熱サイクルを示すＰ−Ｈ線図について説明する。蒸発器４１ではＬｇ点からＬａ点へ移り、飽和蒸気線を超えて過熱蒸気となる。低段圧縮部１１では圧縮により低圧ＰＬのＬａ点から中間圧ＰＭのＬｂ０点を経由して圧力を維持したままＬｂ点へ移る。比エンタルピｈがＬｂ０点からＬｂ点まで下がるのは、中間経路７１からの中圧気相冷媒が合流するためである。高段圧縮部１２では圧縮により中間圧ＰＭのＬｂ点から比エンタルピｈをｈｂまで増大させつつ高圧ＰＨのＬｃ点へ移る。 Subsequently, a PH diagram showing a heat cycle of the heat pump cycle 100 will be described based on FIG. 2. In the evaporator 41, it moves from the Lg point to the La point, and exceeds the saturated vapor line to become superheated vapor. In the low-stage compression section 11, the compression moves from the La point of the low pressure PL to the Lb point while maintaining the pressure via the Lb 0 point of the intermediate pressure PM. The reason that the specific enthalpy h drops from the Lb 0 point to the Lb point is that the medium-pressure gas-phase refrigerant from the intermediate path 71 merges. In the high-stage compression section 12, the compression moves from the Lb point of the intermediate pressure PM to the Lc point of the high pressure PH while increasing the specific enthalpy h to hb.
凝縮器２１では凝縮により高圧ＰＨを維持したままＬｃ点からＬｄ点に移り、飽和蒸気線を超え、さらに飽和液線を越えて過冷却状態となる。ここで、凝縮器２１内では冷媒と被加熱媒体とが共に気液二相状態で熱交換が行われる。飽和液線を越えてのさらなる熱交換は熱交換効率の低下要因となるため、Ｌｄ点は可能な限り飽和液線に近い比エンタルピとなるよう設計されることが望ましい。減圧部６１では、与えられた圧力損失により飽和液線を越えない範囲で比エンタルピｈａを維持したままＬｄ点から圧力ＰＨ‘のＬｄ１点まで減圧される。前述の通りＬｄ点が飽和液線に近い位置となるため、減圧部６１を通過した冷媒が飽和液線を越えないためには、減圧部６１によって与えられる圧力損失は所望の精度を満たす範囲で可能な限り小さくすることが望ましい。本実施形態では、例えば高圧ＰＨが２ＭＰａ、中間圧ＰＭが１ＭＰａである場合、減圧部６１で生じる圧力損失は１０ｋＰａ以上であればよく、５０ｋＰａ以上であることがより望ましい。この場合、Ｌｄ点と飽和液線との圧力差は余裕をもって１００ｋＰａ以上となるように運用されることが望ましい。高段膨張弁５１では比エンタルピｈａを維持したまま減圧により圧力ＰＨ‘のＬｄ１点から中間圧ＰＭのＬｅ点に移り、再び飽和液線を超えて気液二相となる。気液分離器３１では中間圧ＰＭの冷媒が気相と液相に分離されて、気相は飽和蒸気線上のＬｂ１点へと移り、低段圧縮部１１で圧縮されたＬｂ０点の冷媒と合流し、Ｌｂ点に移る。液相は飽和液線上のＬｆ点へと移る。低段膨張弁５２では減圧により中間圧ＰＭのＬｆ点から低圧ＰＬのＬｇ点に移る。 In the condenser 21, due to condensation, the high-pressure PH is maintained and the point moves from the Lc point to the Ld point, exceeds the saturated vapor line, and further exceeds the saturated liquid line, resulting in a supercooled state. Here, in the condenser 21, the refrigerant and the medium to be heated both exchange heat in a gas-liquid two-phase state. Since further heat exchange beyond the saturated liquid line causes a decrease in heat exchange efficiency, it is desirable that the Ld point be designed to have a specific enthalpy as close as possible to the saturated liquid line. In the decompression unit 61, the pressure is reduced from the Ld point to the Ld 1 point of the pressure PH ′ while maintaining the specific enthalpy ha within a range not exceeding the saturated liquid line due to the given pressure loss. As described above, since the Ld point is close to the saturated liquid line, in order that the refrigerant passing through the pressure reducing unit 61 does not cross the saturated liquid line, the pressure loss provided by the pressure reducing unit 61 is within a range that satisfies the desired accuracy. It is desirable to make it as small as possible. In the present embodiment, for example, when the high pressure PH is 2 MPa and the intermediate pressure PM is 1 MPa, the pressure loss generated in the pressure reducing section 61 may be 10 kPa or more, and more preferably 50 kPa or more. In this case, it is desirable that the pressure difference between the Ld point and the saturated liquid line be 100 kPa or more with a margin. In the high-stage expansion valve 51, while maintaining the specific enthalpy ha, the pressure shifts from the Ld 1 point of the pressure PH ′ to the Le point of the intermediate pressure PM, and again exceeds the saturated liquid line to become a gas-liquid two-phase. In the gas-liquid separator 31, the intermediate-pressure PM refrigerant is separated into a gas phase and a liquid phase, the gas phase moves to the point Lb 1 on the saturated vapor line, and the refrigerant at the point Lb 0 compressed in the low-stage compressor 11 is compressed. Merge with and move to Lb point. The liquid phase moves to point Lf on the saturated liquid line. The low-stage expansion valve 52 moves from the Lf point of the intermediate pressure PM to the Lg point of the low pressure PL by depressurization.
続いて凝縮器２１を流通する冷媒の流量算出方法について説明する。減圧部６１で生じる圧力損失ΔＰｆは一般的に
ΔＰｆ＝ｆρ｛Ｖ／（πＤ２／４）｝２ （１）
で表すことができる。ρは減圧部６１に導入される冷媒の密度、Ｖは減圧部６１を流通する冷媒の体積流量、Ｄは減圧部６１の配管直径、ｆは冷媒特性や減圧部６１の配管状態（配管形状、管壁の粗度など）などに基づいて求められる減圧パラメータ式である。なお、｛Ｖ／（πＤ２／４）｝は減圧部６１を流通する冷媒の流速を示す。減圧パラメータ式ｆは実験によって各種条件における値をあらかじめ取得することにより、得ることができる。式（１）において、πは定数であり、配管直径Ｄは装置によりあらかじめ定まる値であるため、減圧パラメータ式ｆ内に含めることができる。これにより、圧力損失ΔＰｆ、密度ρ、冷媒の体積流量Ｖの関係は
ΔＰｆ＝ｆρＶ２ （２）
として表すことができる。これにより、減圧部６１に導入される冷媒の密度（温度および圧力）ρおよび減圧部６１で生じた圧力損失ΔＰｆに基づき、式（２）を用いて減圧部６１を流通する冷媒の体積流量Ｖ、つまり凝縮器２１を流通する冷媒の質量流量を求めることができる。
Next, a method of calculating the flow rate of the refrigerant flowing through the condenser 21 will be described. The pressure loss [Delta] P f caused by the pressure reducing portion 61 is generally ΔP f = fρ {V / ( πD 2/4)} 2 (1)
Can be expressed as ρ is the density of the refrigerant introduced into the pressure reducing section 61, V is the volumetric flow rate of the refrigerant flowing through the pressure reducing section 61, D is the pipe diameter of the pressure reducing section 61, f is the refrigerant characteristics and the piping state of the pressure reducing section 61 (pipe shape, This is a decompression parameter formula calculated based on, for example, the roughness of the pipe wall. Incidentally, {V / (πD 2/ 4)} indicates the flow rate of refrigerant through the evacuating portion 61. The decompression parameter formula f can be obtained by previously acquiring values under various conditions through experiments. In Expression (1), π is a constant, and the pipe diameter D is a value that is predetermined by the device, and thus can be included in the decompression parameter expression f. Accordingly, the relationship among the pressure loss ΔP f , the density ρ, and the volumetric flow rate V of the refrigerant is ΔP f = fρV 2 (2)
Can be expressed as Accordingly, based on the density (temperature and pressure) ρ of the refrigerant introduced into the pressure reducing section 61 and the pressure loss ΔP f generated in the pressure reducing section 61, the volumetric flow rate of the refrigerant flowing through the pressure reducing section 61 is calculated using equation (2). V, that is, the mass flow rate of the refrigerant flowing through the condenser 21 can be obtained.
図３に示すように、制御部４００は、記憶部４１０と、演算部４２０と、回転数制御部４３０と開度制御部４４０とを有する。制御部４００は必ずしも装置の内部に設けられている必要はなく、例えば通信回線を介して接続されていてもよい。記憶部４１０、演算部４２０、回転数制御部４３０および開度制御部４４０は必ずしも一体的に設けられている必要はなく、例えば記憶部４１０はクラウド式であってもよい。 As shown in FIG. 3, the control unit 400 includes a storage unit 410, a calculation unit 420, a rotation speed control unit 430, and an opening degree control unit 440. The control unit 400 does not necessarily have to be provided inside the device, and may be connected via a communication line, for example. The storage unit 410, the calculation unit 420, the rotation speed control unit 430, and the opening degree control unit 440 do not necessarily have to be integrally provided. For example, the storage unit 410 may be a cloud type.
記憶部４１０はプログラムやデータを記憶する部分であり、例えばハードディスクであって減圧パラメータ式ｆ、減圧部入口冷媒温度Ｔａ、凝縮器入口冷媒温度Ｔｂ、減圧部入口冷媒圧力ＰＨ、圧力損失ΔＰｆを示すデータを記憶している。これらの値は、直接的な数値として記憶されていてもよいし、１以上のパラメータから何らかの変換によって求められる間接的な記憶であってもよく、実質的に減圧パラメータ式ｆ、減圧部入口冷媒温度Ｔａ、凝縮器入口冷媒温度Ｔｂ、減圧部入口冷媒圧力ＰＨ、圧力損失ΔＰｆを示すデータであればよい。 The storage unit 410 is a unit that stores programs and data, and is, for example, a hard disk, and stores the decompression parameter formula f, the decompression unit inlet refrigerant temperature Ta, the condenser inlet refrigerant temperature Tb, the decompression unit inlet refrigerant pressure PH, and the pressure loss ΔP f . It stores the data shown. These values may be stored as direct numerical values, or may be indirect storage obtained by some conversion from one or more parameters. The data may be data indicating the temperature Ta, the condenser inlet refrigerant temperature Tb, the pressure reducing section inlet refrigerant pressure PH, and the pressure loss ΔP f .
演算部４２０は、密度算出部４２１と、流量算出部４２２と、加熱出力算出部４２３とを有する。これらの各算出部は演算部４２０の中で明確に区別される必要はなく、例えば一部が重複していてもよいし、いずれかの算出部が他の算出部に含まれていてもよい。演算部４２０は、例えば、ＣＰＵ（Ｃｅｎｔｒａｌ Ｐｒｏｃｅｓｓｉｎｇ Ｕｎｉｔ）等の処理装置にプログラムを実行させること、すなわち、ソフトウェアにより実現してもよいし、ＩＣ（Ｉｎｔｅｇｒａｔｅｄ Ｃｉｒｃｕｉｔ）等のハードウェアにより実現してもよいし、ソフトウェア及びハードウェアを併用して実現してもよい。 The calculation unit 420 has a density calculation unit 421, a flow rate calculation unit 422, and a heating output calculation unit 423. It is not necessary for each of these calculation units to be clearly distinguished in the calculation unit 420. For example, some calculation units may overlap, and one calculation unit may be included in another calculation unit. .. The arithmetic unit 420 may be implemented by causing a processing device such as a CPU (Central Processing Unit) to execute a program, that is, by software, or by hardware such as an IC (Integrated Circuit). However, it may be realized by using software and hardware together.
密度算出部４２１は、減圧部入口冷媒温度Ｔａおよび減圧部入口冷媒圧力ＰＨに基づいて、減圧部６１に導入される冷媒の密度ρを算出する。 The density calculating unit 421 calculates the density ρ of the refrigerant introduced into the pressure reducing unit 61 based on the pressure reducing unit inlet refrigerant temperature Ta and the pressure reducing unit inlet refrigerant pressure PH.
流量算出部４２２は、密度算出部４２１で算出された冷媒の密度ρおよび圧力損失ΔＰｆに基づき、減圧部６１を流通する冷媒の体積流量Ｖを算出する。 The flow rate calculation unit 422 calculates the volume flow rate V of the refrigerant flowing through the pressure reducing unit 61 based on the density ρ of the refrigerant and the pressure loss ΔP f calculated by the density calculation unit 421.
加熱出力算出部４２３は、凝縮器２１内を流通する冷媒が被加熱媒体を加熱する熱出力Ｑを算出する。加熱出力算出部４２３は、まず、減圧部入口冷媒圧力ＰＨおよび減圧部入口冷媒温度Ｔａに基づいて凝縮器２０の吐出口におけるエンタルピｈａを、減圧部入口冷媒圧力ＰＨおよび凝縮器入口冷媒温度Ｔｂに基づいて凝縮器２０の吸入口におけるエンタルピｈｂをそれぞれ算出する。また、質量流量ｖをｖ＝ρＶの式に基づいて計算する。そして加熱出力Ｑを、Ｑ＝ｖ・（ｈｂ−ｈａ）として求める。 The heating output calculation unit 423 calculates the thermal output Q by which the refrigerant flowing in the condenser 21 heats the medium to be heated. The heating output calculation unit 423 first sets the enthalpy ha at the discharge port of the condenser 20 to the pressure reducing unit inlet refrigerant pressure PH and the condenser inlet refrigerant temperature Tb based on the pressure reducing unit inlet refrigerant pressure PH and the pressure reducing unit inlet refrigerant temperature Ta. Based on this, the enthalpy hb at the suction port of the condenser 20 is calculated. Further, the mass flow rate v is calculated based on the equation of v = ρV. Then, the heating output Q is obtained as Q = v · (hb−ha).
回転数制御部４３０は、凝縮器２１による加熱出力Ｑが目標値となるように低段圧縮部１１および高段圧縮部１２の回転数制御を行い、冷媒の体積流量Ｖが調整される。低段圧縮部１１と高段圧縮部１２とが独立した複数台の圧縮機である場合、回転数制御部４３０は、低段圧縮部１１の回転数を一定とし、高段圧縮部１２のみの回転数制御を行ってもよい。また、蒸発器４１に供給される熱源水の流量や、凝縮器２１に供給される被加熱媒体の流量をさらに制御してもよい。 The rotation speed control unit 430 controls the rotation speeds of the low-stage compression unit 11 and the high-stage compression unit 12 so that the heating output Q of the condenser 21 becomes a target value, and the volumetric flow rate V of the refrigerant is adjusted. When the low-stage compression unit 11 and the high-stage compression unit 12 are a plurality of independent compressors, the rotation speed control unit 430 keeps the rotation speed of the low-stage compression unit 11 constant and only the high-stage compression unit 12 operates. Rotational speed control may be performed. Further, the flow rate of the heat source water supplied to the evaporator 41 and the flow rate of the heated medium supplied to the condenser 21 may be further controlled.
開度制御部４４０は、減圧部入口冷媒圧力ＰＨおよび圧力損失ΔＰｆに基づき、高段膨張弁５１を通過後の冷媒圧力が目標値となるように高段膨張弁５１の開度制御を行う。開度制御部４４０は、低段膨張弁５２の開度制御をさらに行ってもよい。この場合、例えば冷暖膨張弁５２の開度は図示しない中間圧力センサに基づき蒸発器４１を流通する冷媒の流量が一定になるように制御を行う。なお、蒸発器４１および低段圧縮部１１を流通する冷媒の流量は、蒸発器４１と低段圧縮部１１との間に温度センサおよび圧力センサを設けることで、低段圧縮部１１の特性値から従来の流量測定手法により求めることができる。 The opening control unit 440 controls the opening of the high-stage expansion valve 51 based on the pressure reducing unit inlet refrigerant pressure PH and the pressure loss ΔP f so that the refrigerant pressure after passing through the high-stage expansion valve 51 reaches a target value. .. The opening control section 440 may further control the opening of the low-stage expansion valve 52. In this case, for example, the opening degree of the cooling / warming expansion valve 52 is controlled based on an intermediate pressure sensor (not shown) so that the flow rate of the refrigerant flowing through the evaporator 41 becomes constant. It should be noted that the flow rate of the refrigerant flowing through the evaporator 41 and the low-stage compression section 11 is set to a characteristic value of the low-stage compression section 11 by providing a temperature sensor and a pressure sensor between the evaporator 41 and the low-stage compression section 11. Can be obtained from the conventional flow rate measurement method.
図４は、ヒートポンプ式蒸気生成装置１の制御手順を示すフローチャートであり、本実施の形態にかかる流量演算方法が含まれる。この手順は微小時間ごとに繰り返し実行される。 FIG. 4 is a flowchart showing the control procedure of the heat pump steam generator 1, which includes the flow rate calculation method according to the present embodiment. This procedure is repeatedly executed every minute time.
ステップＳ１は密度算出ステップであり、密度算出部４２１により減圧部６１に導入される冷媒の密度ρが算出される。ステップＳ２は流量算出ステップであり、流量算出部４２２により減圧部６１を流通する冷媒の体積流量Ｖが算出される。ステップＳ３は加熱出力算出ステップであり、加熱出力算出部４２３により加熱出力Ｑが算出される。ステップＳ４は制御ステップであり、回転数制御部４３０により低段圧縮部１１および高段圧縮部１２の回転数が、開度制御部４４０により高段膨張弁５１の開度がそれぞれ制御される。 Step S1 is a density calculation step, and the density calculation unit 421 calculates the density ρ of the refrigerant introduced into the pressure reducing unit 61. Step S2 is a flow rate calculating step, and the flow rate calculating unit 422 calculates the volume flow rate V of the refrigerant flowing through the pressure reducing unit 61. Step S3 is a heating output calculation step in which the heating output calculator 423 calculates the heating output Q. Step S4 is a control step, in which the rotation speed control unit 430 controls the rotation speeds of the low-stage compression unit 11 and the high-stage compression unit 12, and the opening control unit 440 controls the opening degree of the high-stage expansion valve 51.
このように、ヒートポンプ式蒸気生成装置１においては、一体型二段圧縮機１０の筐体内部に温度センサを設けることが困難であるが、減圧部６１による圧力損失ΔＰｆ、減圧部６１に導入される冷媒の密度ρに基づいて凝縮器２１を流通する冷媒の質量流量ｖが算出される。これにより熱出力Ｑが求まり、適正な出力制御を行うことができる。 As described above, in the heat pump steam generator 1, it is difficult to provide the temperature sensor inside the housing of the integrated two-stage compressor 10, but the pressure loss ΔP f due to the pressure reducing unit 61 is introduced into the pressure reducing unit 61. The mass flow rate v of the refrigerant flowing through the condenser 21 is calculated based on the density ρ of the refrigerant. As a result, the heat output Q is obtained, and proper output control can be performed.
さらに、高価な流量計（例えば冷媒流量計や蒸気流量計など）が不要となりシステムを簡易かつ廉価に構成することができる。 Furthermore, an expensive flow meter (for example, a refrigerant flow meter or a steam flow meter) is not required, and the system can be configured simply and inexpensively.
（第２実施形態）
本発明にかかるヒートポンプ式蒸気生成装置の変形例について図面を用いて詳細に説明する。なお、先の実施形態と同様の部分については説明を省略する。
(Second embodiment)
A modified example of the heat pump steam generator according to the present invention will be described in detail with reference to the drawings. The description of the same parts as those in the previous embodiment will be omitted.
図５は、本発明の実施の形態の変形例であるヒートポンプ式蒸気生成装置１の構成を示す回路構成図である。 FIG. 5: is a circuit block diagram which shows the structure of the heat pump steam generator 1 which is a modification of embodiment of this invention.
減圧部６１を通過した冷媒は、高圧冷媒分岐手段である分岐配管７２により第１高圧冷媒経路７３と第２高圧冷媒経路７４に分岐され、第１高圧冷媒経路７３を流通する冷媒は、高段膨張弁５１で減圧され中間経路７１に導入された後、内部熱交換器（加熱手段）７５で第２高圧冷媒経路７４を流通する液相冷媒から熱を回収し、中間吸入ポート１２ａに導入される。また、第２高圧冷媒経路７４を流通する冷媒は、内部熱交換器７５で中間経路７１を流通する冷媒に熱を与えた後、低段膨張弁５２で減圧され蒸発器４１に導入される。 The refrigerant that has passed through the decompression section 61 is branched into a first high-pressure refrigerant path 73 and a second high-pressure refrigerant path 74 by a branch pipe 72 that is a high-pressure refrigerant branching means, and the refrigerant flowing through the first high-pressure refrigerant path 73 has a high stage. After being decompressed by the expansion valve 51 and introduced into the intermediate passage 71, heat is recovered from the liquid-phase refrigerant flowing through the second high-pressure refrigerant passage 74 by the internal heat exchanger (heating means) 75 and introduced into the intermediate suction port 12a. It Further, the refrigerant flowing through the second high-pressure refrigerant path 74 gives heat to the refrigerant flowing through the intermediate path 71 by the internal heat exchanger 75, and then is decompressed by the low-stage expansion valve 52 and introduced into the evaporator 41.
続いて、図６に基づいて変形例にかかるヒートポンプサイクル１００の熱サイクルを示すＰ−Ｈ線図について説明する。なお、先の実施形態と同様の部分については説明を省略する。 Next, a PH diagram showing a heat cycle of the heat pump cycle 100 according to the modification will be described based on FIG. The description of the same parts as those in the previous embodiment will be omitted.
減圧部６１でＬｄ１点まで減圧された冷媒のうち、第１高圧冷媒経路７３を流通する冷媒は高段膨張弁５１で比エンタルピｈａを維持したまま圧力ＰＨ‘のＬｄ１点から中間圧ＰＭのＬｅ点に移り、飽和液線を超えて気液二相となる。さらに内部熱交換器７５で第２高圧冷媒経路７４を流通する液相冷媒から熱を回収して蒸発し、低段圧縮部１１で圧縮されたＬｂ０点の冷媒と合流し、Ｌｂ点に移る。 Among the refrigerants depressurized to Ld 1 point by the depressurizing unit 61, the refrigerant flowing through the first high-pressure refrigerant path 73 is the intermediate pressure PM from the Ld 1 point of the pressure PH ′ while maintaining the specific enthalpy ha in the high-stage expansion valve 51. To the point Le and cross the saturated liquid line to become a gas-liquid two phase. Further, the internal heat exchanger 75 recovers heat from the liquid-phase refrigerant flowing through the second high-pressure refrigerant path 74 and evaporates it, merges with the refrigerant at the Lb 0 point compressed in the low-stage compression section 11, and moves to the Lb point. ..
減圧部６１で圧力ＰＨ‘のＬｄ１点まで減圧された冷媒のうち、第２高圧冷媒経路７４を流通する冷媒は、内部熱交換器７５で中間経路７１を流通する冷媒に熱を与え、圧力ＰＨ‘を保ったままＬｄ点からＬｈ点まで移る。さらに低段膨張弁５２で圧力ＰＨ‘のＬｈ点から低圧ＰＬのＬｇ点まで移る。 Of the refrigerant depressurized by the depressurizing unit 61 to the Ld 1 point of the pressure PH ′, the refrigerant flowing through the second high-pressure refrigerant path 74 gives heat to the refrigerant flowing through the intermediate path 71 by the internal heat exchanger 75, and Move from Ld point to Lh point while keeping PH '. Further, the low-stage expansion valve 52 moves from the Lh point of the pressure PH ′ to the Lg point of the low pressure PL.
上述した各実施の形態における制御部４００は、低段圧縮部１１の吸入側圧力および温度、高段圧縮部１２の吐出側圧力および温度、蒸気生成部２００を流通する熱源水の温度および流量、熱源水供給部３００を流通する熱源水の温度および流量などに基づきヒートポンプサイクル１００内の高段膨張弁５１および低段膨張弁５２の開度、低段圧縮部１１および高段圧縮部１２を制御してもよい。また、制御部４００は蒸気生成部２００を流通する被加熱水の流量および温度、熱源水供給部３００を流通する熱源水の流量および温度を制御してもよい。 The control unit 400 in each of the above-described embodiments controls the suction-side pressure and temperature of the low-stage compression unit 11, the discharge-side pressure and temperature of the high-stage compression unit 12, the temperature and flow rate of the heat source water flowing through the steam generation unit 200, The opening degree of the high-stage expansion valve 51 and the low-stage expansion valve 52 in the heat pump cycle 100, the low-stage compression unit 11 and the high-stage compression unit 12 are controlled based on the temperature and flow rate of the heat source water flowing through the heat source water supply unit 300. You may. The control unit 400 may control the flow rate and temperature of the heated water flowing through the steam generating unit 200 and the flow rate and temperature of the heat source water flowing through the heat source water supply unit 300.
本実施の形態の密度測定手段８０として、凝縮器２１と減圧部６１との間に設けられた減圧部入口圧力センサ８１および減圧部入口温度センサ８２を例示したが、凝縮器２１と減圧部６１との間を流通する冷媒の圧力および温度が分かればそれには限定されない。例えば、高段圧縮部１２と凝縮器２１との間の冷媒圧力を減圧部６１の入口側冷媒圧力として用いてもよく、凝縮器２１本体の内、冷媒出口に近い部分の温度を測定して減圧部６１の入口側冷媒温度として用いてもよい。また、密度測定手段８０として、単独の密度計を用いてもよい。 As the density measuring means 80 of the present embodiment, the pressure reducing portion inlet pressure sensor 81 and the pressure reducing portion inlet temperature sensor 82 provided between the condenser 21 and the pressure reducing portion 61 are exemplified, but the condenser 21 and the pressure reducing portion 61 are illustrated. If the pressure and temperature of the refrigerant flowing between and are known, it is not limited thereto. For example, the refrigerant pressure between the high-stage compression section 12 and the condenser 21 may be used as the inlet-side refrigerant pressure of the decompression section 61, and the temperature of the portion of the condenser 21 main body near the refrigerant outlet may be measured. It may be used as the temperature of the refrigerant on the inlet side of the pressure reducing portion 61. Further, as the density measuring means 80, a single density meter may be used.
本実施の形態の減圧部６１として細管路を例示しているが、冷媒に圧力損失を付与することができれば、オリフィスや絞り弁を用いてもよい。また、立ち上げ配管による圧力損失付与や、立ち上げ配管と細管路の組合せを用いてもよい。また、減圧部６１前後の冷媒が常に液相である必要はなく、通常運転時など圧力損失を測定するタイミングで減圧部６１前後の冷媒がともに液相になっていればよい。 Although a thin pipe is illustrated as the decompression unit 61 of the present embodiment, an orifice or a throttle valve may be used as long as it can give a pressure loss to the refrigerant. Further, a pressure loss may be imparted by the start-up pipe, or a combination of the start-up pipe and the narrow pipe may be used. Further, the refrigerant before and after the pressure reducing portion 61 does not always have to be in the liquid phase, and it is sufficient that the refrigerant before and after the pressure reducing portion 61 is both in the liquid phase at the timing of measuring the pressure loss during normal operation.
本実施の形態の圧力損失測定手段として差圧計６２を用いているが、差圧計６２に代わり、減圧部６１の上流側と下流側にそれぞれ設けられた単独の圧力計測手段によって求められた値から差を求めてもよい。この場合、減圧部上流側の圧力計測手段は高段圧縮部１２から減圧部６１の間の冷媒圧力を、減圧部下流側の圧力計測手段は第１の実施形態においては減圧部６２から高段膨張弁５１の間、第２の実施形態においては減圧部６２から分岐配管７２の間の冷媒圧力を測定するものであればよい。なお、密度計測手段８０で圧力を測定していれば、その値を減圧部６１の上流側圧力として兼用してもよい。 Although the differential pressure gauge 62 is used as the pressure loss measuring means of the present embodiment, instead of the differential pressure gauge 62, from the values obtained by the independent pressure measuring means provided on the upstream side and the downstream side of the pressure reducing portion 61, respectively. You may ask for the difference. In this case, the pressure measuring unit on the upstream side of the pressure reducing unit measures the refrigerant pressure between the high-stage compression unit 12 and the pressure reducing unit 61, and the pressure measuring unit on the downstream side of the pressure reducing unit increases the pressure from the pressure reducing unit 62 to the high stage in the first embodiment. It suffices to measure the refrigerant pressure between the expansion valves 51, and in the second embodiment between the pressure reducing portion 62 and the branch pipe 72. If the pressure is measured by the density measuring unit 80, the value may be used as the upstream pressure of the pressure reducing unit 61.
本実施の形態の変形例における加熱手段として、内部熱交換器７５を例示しているが、加熱手段はそれに限定されない。例えば、熱源温水など外部熱源との熱交換により高段膨張弁５１を通過した冷媒を蒸発させてもよく、ヒータにより高段膨張弁５１を通過した冷媒を蒸発させてもよい。また、第１の実施の形態における中間経路７１に、上述の各種加熱手段を設けてもよい。 Although the internal heat exchanger 75 is illustrated as the heating means in the modification of the present embodiment, the heating means is not limited thereto. For example, the refrigerant that has passed through the high-stage expansion valve 51 may be evaporated by heat exchange with an external heat source such as heat source hot water, or the refrigerant that has passed through the high-stage expansion valve 51 may be evaporated by a heater. Further, the above-mentioned various heating means may be provided in the intermediate path 71 in the first embodiment.
本発明における減圧部入口圧力測定手段８１、減圧部入口温度測定手段８２、凝縮器入口温度測定手段８３について、圧力一定制御や温度一定制御を行っている場合、その固定値を記憶部４１０に記憶させておき、必要に応じて読み出しを行ってもよい。この場合、記憶部４１０が各種測定手段に該当する。 When the constant pressure control or the constant temperature control is performed on the pressure reducing portion inlet pressure measuring means 81, the pressure reducing portion inlet temperature measuring means 82, and the condenser inlet temperature measuring means 83 in the present invention, the fixed values are stored in the storage portion 410. Then, the data may be read out if necessary. In this case, the storage unit 410 corresponds to various measuring means.
本発明は、上記した実施形態に限定されるものではなく、本発明の主旨を逸脱しない範囲で自由に変更できることは勿論である。 The present invention is not limited to the above-described embodiments, and it goes without saying that the present invention can be freely modified without departing from the spirit of the present invention.
１ ヒートポンプ式蒸気生成装置
１００ ヒートポンプサイクル
２００ 蒸気生成部
３００ 熱源水供給部
４００ 制御部
１０ 一体型二段圧縮機
１１ 低段圧縮部（低段圧縮機構）
１２ 高段圧縮部（高段圧縮機構）
１２ａ 中間吸入ポート
２１ 凝縮器
３１ 気液分離器
３１ａ 上部導入口
３１ｂ 上部吐出口
３１ｃ 下部吐出口
４１ 蒸発器
５１ 高段膨張弁（高段膨張機構）
５２ 低段膨張弁（低段膨張機構）
６１ 減圧部
６２ 差圧計（圧力損失測定手段）
７１ 中間経路
７２ 分岐配管（高圧冷媒分岐手段）
７３ 第１高圧冷媒経路
７４ 第２高圧冷媒経路
７５ 内部熱交換器（加熱手段）
８０ 密度測定手段
８１ 減圧部入口圧力センサ（減圧部入口圧力測定手段）
８２ 減圧部入口温度センサ（減圧部入口温度測定手段）
８３ 凝縮器入口温度センサ（凝縮器入口温度測定手段）
４１０ 記憶部
４２０ 演算部
４２１ 密度算出部
４２２ 流量算出部
４２３ 加熱出力算出部
４３０ 回転数制御部
４４０ 開度制御部
1 Heat Pump Type Steam Generator 100 Heat Pump Cycle 200 Steam Generator 300 Heat Source Water Supply Unit 400 Control Unit 10 Integrated Two-Stage Compressor 11 Low-Stage Compressor (Low-Stage Compression Mechanism)
12 High-stage compression section (high-stage compression mechanism)
12a Intermediate suction port 21 Condenser 31 Gas-liquid separator 31a Upper inlet 31b Upper outlet 31c Lower outlet 41 Evaporator 51 High-stage expansion valve (high-stage expansion mechanism)
52 Low-stage expansion valve (low-stage expansion mechanism)
61 pressure reducing unit 62 differential pressure gauge (pressure loss measuring means)
71 Intermediate path 72 Branch pipe (high pressure refrigerant branching means)
73 first high-pressure refrigerant path 74 second high-pressure refrigerant path 75 internal heat exchanger (heating means)
80 Density measuring means 81 Pressure reducing section inlet pressure sensor (pressure reducing section inlet pressure measuring means)
82 Pressure reducing section inlet temperature sensor (pressure reducing section inlet temperature measuring means)
83 Condenser inlet temperature sensor (condenser inlet temperature measuring means)
410 storage unit 420 calculation unit 421 density calculation unit 422 flow rate calculation unit 423 heating output calculation unit 430 rotation speed control unit 440 opening control unit
Claims (9)
前記凝縮器と前記膨張機構との間に設けられ、前記凝縮器を通過した冷媒を減圧する減圧部と、
前記高段圧縮機構から前記減圧部までの冷媒圧力を測定する減圧部入口圧力測定手段と、
前記凝縮器から前記減圧部までの冷媒温度を測定する減圧部入口温度測定手段と、
前記減圧部で生じた圧力損失を測定する圧力損失測定手段と、
前記減圧部入口圧力測定手段で測定された圧力と前記減圧部入口温度測定手段で測定された温度とに基づき、前記前記減圧部に流入する冷媒密度を算出する密度算出部と、
前記密度算出部で算出された密度と前記圧力損失測定手段で測定された圧力損失とに基づき、前記凝縮器を流通する冷媒の流量を算出する流量算出部と、
を備えることを特徴とするヒートポンプサイクル。 A two-stage compression mechanism having a low-stage compression mechanism and a high-stage compression mechanism, a condenser, an expansion mechanism that expands a high-pressure refrigerant to generate an intermediate-pressure refrigerant and a low-pressure refrigerant, and introduces the low-pressure refrigerant. An evaporator and an annular connection, in a heat pump cycle having an intermediate path for supplying the intermediate pressure refrigerant to the high-stage compression mechanism,
A decompression unit provided between the condenser and the expansion mechanism, for decompressing the refrigerant passing through the condenser,
Decompression section inlet pressure measuring means for measuring the refrigerant pressure from the high-stage compression mechanism to the decompression section,
Decompression section inlet temperature measuring means for measuring the refrigerant temperature from the condenser to the decompression section,
Pressure loss measuring means for measuring the pressure loss generated in the pressure reducing section,
Based on the pressure measured by the pressure reducing portion inlet pressure measuring means and the temperature measured by the pressure reducing portion inlet temperature measuring means, a density calculating portion for calculating the density of the refrigerant flowing into the pressure reducing portion,
Based on the density calculated by the density calculating section and the pressure loss measured by the pressure loss measuring means, a flow rate calculating section for calculating the flow rate of the refrigerant flowing through the condenser,
A heat pump cycle comprising:
前記凝縮器を通過した高圧の冷媒を膨張し前記中間圧の冷媒を生成する高段膨張機構と、
前記中間経路が接続され、前記中間圧の冷媒を気相及び液相に分離する気液分離器と、
前記気液分離器で分離した中間圧の液相冷媒を低圧まで減圧して前記蒸発器に供給する低段膨張機構と、
を備えることを特徴とする請求項１に記載のヒートポンプサイクル。 The expansion mechanism is
A high-stage expansion mechanism that expands the high-pressure refrigerant that has passed through the condenser to generate the intermediate-pressure refrigerant,
A gas-liquid separator connected to the intermediate path, for separating the intermediate-pressure refrigerant into a gas phase and a liquid phase;
A low-stage expansion mechanism for reducing the intermediate-pressure liquid-phase refrigerant separated by the gas-liquid separator to a low pressure and supplying the same to the evaporator,
The heat pump cycle according to claim 1, further comprising:
前記凝縮器を通過した高圧の冷媒を第１高圧冷媒経路と第２高圧冷媒経路とに分岐させる高圧冷媒分岐手段と、
冷媒入口に前記第１高圧冷媒経路、冷媒出口に前記中間経路が接続され、前記第１高圧冷媒経路を流通する高圧の冷媒を膨張し前記中間圧の冷媒を生成する高段膨張機構と、
前記第２高圧冷媒経路を流通する高圧の冷媒を膨張し前記低圧の冷媒を生成する低段膨張機構と、
前記中間経路を流通する冷媒を前記第２高圧冷媒経路を流通する冷媒で加熱する加熱手段と、
を備えることを特徴とする請求項１に記載のヒートポンプサイクル。 The expansion mechanism is
High-pressure refrigerant branching means for branching the high-pressure refrigerant passing through the condenser into a first high-pressure refrigerant path and a second high-pressure refrigerant path,
A first high-pressure refrigerant path to the refrigerant inlet, the intermediate path is connected to the refrigerant outlet, a high-stage expansion mechanism for expanding the high-pressure refrigerant flowing through the first high-pressure refrigerant path to generate the intermediate-pressure refrigerant,
A low-stage expansion mechanism that expands the high-pressure refrigerant flowing through the second high-pressure refrigerant path to generate the low-pressure refrigerant,
Heating means for heating the refrigerant flowing through the intermediate path with the refrigerant flowing through the second high-pressure refrigerant path;
The heat pump cycle according to claim 1, further comprising:
少なくとも前記減圧部入口圧力測定手段で測定された冷媒圧力、前記減圧部入口温度測定手段で測定された冷媒温度、前記凝縮器入口温度測定手段で測定された冷媒温度および前記流量算出部で算出された冷媒流量に基づき、前記凝縮器の加熱出力を算出する加熱出力算出部と、
を備えることを特徴とする請求項１〜３のいずれか１項に記載のヒートポンプサイクル。 Condenser inlet temperature measuring means for measuring the refrigerant temperature from the high-stage compression mechanism to the condenser,
At least the refrigerant pressure measured by the pressure reducing section inlet pressure measuring means, the refrigerant temperature measured by the pressure reducing section inlet temperature measuring means, the refrigerant temperature measured by the condenser inlet temperature measuring means and the flow rate calculating section are calculated. A heating output calculation unit that calculates the heating output of the condenser based on the refrigerant flow rate,
The heat pump cycle according to any one of claims 1 to 3, further comprising:
前記蒸発器に熱源水を供給する熱源水供給部と、
前記凝縮器に前記被加熱媒体として水を供給し、生成された蒸気を外部に送出する蒸気生成部と、
を備えることを特徴とするヒートポンプ式蒸気生成装置。 A heat pump cycle according to claim 1;
A heat source water supply unit for supplying heat source water to the evaporator;
Supplying water as the medium to be heated to the condenser, and a steam generation unit for sending the generated steam to the outside,
A heat pump-type steam generator comprising:
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| JP2018044725A (en) * | 2016-09-15 | 2018-03-22 | 富士電機株式会社 | Refrigerant circuit device |
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