JP2004108616A - Hot-water supply system for co2 refrigerating cycle - Google Patents

Hot-water supply system for co2 refrigerating cycle Download PDF

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JP2004108616A
JP2004108616A JP2002268700A JP2002268700A JP2004108616A JP 2004108616 A JP2004108616 A JP 2004108616A JP 2002268700 A JP2002268700 A JP 2002268700A JP 2002268700 A JP2002268700 A JP 2002268700A JP 2004108616 A JP2004108616 A JP 2004108616A
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hot water
temperature
water supply
gas
line
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JP3877207B2 (en
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Tomoiku Yoshikawa
吉川　朝郁
Shuji Fukano
深野　修司
Hirokazu Yoneda
米田　弘和
Katsumi Fujima
藤間　克己
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Mayekawa Manufacturing Co
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Mayekawa Manufacturing Co
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2309/00—Gas cycle refrigeration machines
    • F25B2309/06—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide
    • F25B2309/061—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide with cycle highest pressure above the supercritical pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2339/00—Details of evaporators; Details of condensers
    • F25B2339/04—Details of condensers
    • F25B2339/047—Water-cooled condensers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being carbon dioxide

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  • Heat-Pump Type And Storage Water Heaters (AREA)
  • Compression-Type Refrigeration Machines With Reversible Cycles (AREA)

Abstract

<P>PROBLEM TO BE SOLVED: To provide a hot-water supply for CO<SB>2</SB>refrigerating cycle effectively using an oil cooler provided for preventing over-heating of lubricating oil; providing the oil cooler adjacent to a gas cooler; certainly and efficiently cooling sensible heat of high pressure/temperature CO<SB>2</SB>coolant in a high pressure side by variously combining with a gas cooler; and conducting efficient hot-water supply. <P>SOLUTION: The hot-water supply system for a CO<SB>2</SB>refrigerating cycle is structured by connecting a gas hot-water supply line 12a of the gas cooler 12 and a hot-water supply line 13a of the oil cooler 13 in a CO<SB>2</SB>supercritical refrigerating cycle 10 in series. <P>COPYRIGHT: (C)2004,JPO

Description

【０００１】
【発明の属する技術分野】
本発明は、圧縮機、ガスクーラ、膨張弁、蒸発器よりなるＣＯ２超臨界冷凍サイクルにおいて、ガスクーラによるガス給湯ラインと圧縮機のオイルクーラによるオイル給湯ラインとの組み合わせにより、直列若しくは並列接続または個別に形成された給湯ラインを備える構成とした、効率的構成よりなるＣＯ２冷凍サイクルの給湯システムに関する。
【０００２】
【従来の技術】
上記ＣＯ２超臨界冷凍サイクルに使用されるＣＯ２冷媒は、地球環境汚染防止、とりわけ、オゾン層破壊、地球温暖化防止のため、フロンより遥かにその悪影響が少なく、毒性もなく、自然界に多く存在する自然冷媒の一つとしてその存在が注目されるようになり、また、ＣＯ２を冷媒として使用した蒸気圧縮冷凍サイクルが多用される傾向にある。
しかし、ＣＯ２は温度３１．０６℃の低い温度で臨界点に達するので、これを使用する蒸気圧縮冷凍サイクルは、前記臨界点を越えた超臨界域を含むサイクルを形成することになり、一般の蒸気圧縮式冷凍サイクルに見られた凝縮過程を伴うことなく顕熱変化による冷却を受け、超臨界の高圧高温冷媒より高圧低温冷媒となり、ついで、膨張弁による断熱膨張により気液二相混合状態をなし、蒸発器で蒸発させ冷熱を外部に送出している。例えば、特許文献１に示す提案がある。
【０００３】
図７には、圧縮機１０１、ガスクーラ（ガス冷却器または放熱器という）１０２、膨張機１０３、蒸発器１０４よりなるＣＯ２蒸気圧縮式冷凍サイクルの概略構成を示してある。また、図８には、図７の冷凍サイクルにおけるＣＯ２超臨界冷凍サイクルを示すモリエル線図が示してある。
図８に見るように、ＣＯ２冷媒はスクリュー圧縮機である圧縮機１０１で圧縮され、Ａ→Ｂに示すように臨界点Ｋ（臨界温度３１．１℃、臨界圧力ＰＫ＝７５．２８ｋｇ／ｃｍ２）を越えた圧力Ｐ２まで圧縮される。ついで、図のＢ→Ｃに示すように、この圧縮された高圧高温ＣＯ２の顕熱をガスクーラ１０２で大気に放熱し、さらに放熱された高圧低温ＣＯ２を図のＣ→Ｄに示すように膨張弁１０３で等エンタルピ線に沿って膨張させ圧力を降下させる。この圧力降下により気液二相混合の湿り蒸気となってＣＯ２冷媒を蒸発器１０４で液相を気化し冷熱を外部へ放出する。
【０００４】
上記図８に見るように、臨界点Ｋを通る等温線ＴＫの右側であって飽和蒸気線の臨界圧ＰＫ（７５．２８ｋｇ／ｃｍ２）以上の蒸気圧の右側領域では密度の高いガス状態となり、この領域では一般に液化されることなく、ガスクーラを使用しての顕熱冷却により前記等温線ＴＫの左側の液状可能の状態の高圧低温ＣＯ２を得て、次工程の膨張減圧に移行させているが、そのためには前記ガスクーラ単独での冷却には大きな吸熱容量を必要としている。
【０００５】
一方ＣＯ２超臨界冷凍サイクルの場合は圧縮機に吸入される冷媒は高温状態となり潤滑油の劣化の問題があり、圧縮機各部の破損の原因を形成し、冷凍効率の向上とともにこれらの画期的な解決手段の実現が望まれている。
上記高熱化を防ぐために過熱度を低くし、図８の点Ａの状態で運転すると、圧縮機に液相冷媒が流入し、圧縮機の破損の原因を形成する、そのため一般にわずかに飽和蒸気線Ｓｖより右の状態で運転している。
【０００６】
そのため、スクリュー圧縮機においてはオイルクーラを設け、インジェクション冷却部とジャーナル冷却部とより構成している。前者は、圧縮ガスの冷却とシール効果を得るため、圧縮室入口に潤滑油をインジェクションにより噴射し、冷媒ガスとともに吐出された前記潤滑油は油分離器により分離され、分離した油を冷却水や冷媒で冷却する冷却部を設け、後者は、圧縮室のケーシングを冷却水で冷却する冷却部を指し、オイルクーラはその両者により行なう構成にしてある。
【０００７】
【特許文献１】
特開２００１−４２３５公報
【０００８】
【発明が解決しようとする課題】
本発明は、上記した問題点に鑑みなされたもので、
潤滑油過熱防止のために設けてあるオイルクーラの有効利用を図り、該オイルクーラをガスクーラに併設させ、ガスクーラとの多様的組合せにより、高圧側の高圧高温ＣＯ２冷媒の顕熱冷却をより確実且つ効率的に行う、ＣＯ２冷凍サイクルの給湯システムの提供を目的とするものである。
【０００９】
【課題を解決するための手段】
そこで、本発明の第１の発明であるＣＯ２冷凍サイクルの給湯システムは、
スクリュー圧縮機、ガスクーラ、膨張弁、蒸発器よりなるＣＯ２冷凍サイクルの前記圧縮機により得られた高圧側の高温超臨界ＣＯ２を放熱冷却させるガスクーラを使用したＣＯ２超臨界冷凍サイクルの給湯システムにおいて、
前記給湯システムは、前記ガスクーラの出口より常温水を供給して入口で中温水を得る向流式のガス給湯ラインと、該ガス給湯ラインを出た中温水をスクリュー圧縮機のオイルクーラに導入しその出口で高温水を得るようにしたオイル給湯ラインとより構成し、
前記ガス給湯ラインとオイル給湯ラインとを直列接続したことを特徴とする。
【００１０】
上記第１の発明は、ＣＯ２超臨界冷凍サイクルの高圧側の約９０℃の高温超臨界ＣＯ２を放熱冷却させて高圧低温ＣＯ２を得る冷却手段に、ガスクーラによるガス給湯ラインとオイルクーラによるオイル給湯ラインとを直列状に設け、それぞれが受け持つ冷却温度分担区域を決めガス給湯ラインにより５０〜６０℃の中温水を得て、ついでオイル給湯ラインにより７０〜８０℃の高温水を得る構成とするとともに、オイルクーラの有効利用を図ったものである。
そして、前記ガス給湯ラインは向流式を使用し、ガスクーラの高圧側高温超臨界ＣＯ２の出口側より常温水を導入し、入口側より中温水を得るようにしてある。
【００１１】
また、上記第１の発明のＣＯ２冷凍サイクルの給湯システムにおける、
前記ガス給湯ラインとオイル給湯ラインは、温度変化を縦軸にとりエンタルピ変化を横軸にとるＣＯ２温度エンタルピ曲線に対し下側温度領域に近接して設けられ、ガス給湯ラインの吸熱状況を示す温度エンタルピ直線の中温側端部と、オイルとの熱交換をするオイル給湯ラインの温度エンタルピ直線の中温側端部とを折れ線状に接続し、それぞれの吸熱容量に対応して冷却するＣＯ２エンタルピ変化量を内分比分担をする構成が好ましい。
【００１２】
上記第１の実施例の発明は、前記第１の発明における高圧側ＣＯ２の冷却に際して、直列状に接続したガス給湯ラインとオイル給湯ラインのそれぞれの吸熱容量に対応した最適冷却を可能とする仕様につき特定したものである。
圧縮機により約９０℃の吐出温度まで加熱された高圧側の高圧高温ＣＯ２は、前記冷却手段により約３０℃（夏季の場合）又は約１０℃（冬季の場合）に冷却される。
この場合、前記ガス給湯ラインとオイル給湯ラインのそれぞれの吸熱状況を示す温度エンタルピ直線と、高圧高温ＣＯ２が前記冷却手段により冷却される過程を示すＣＯ２温度エンタルピ曲線とを、縦軸に温度変化をとり横軸にエンタルピ変化を示すＴ−Ｈ座標に示す場合に、図２に示すように、ガス給湯ラインの温度エンタルピ直線２１ａとオイル給湯ラインの温度エンタルピ直線２２ａとは前記ＣＯ２温度エンタルピ曲線２０の下側温度領域で折れ線接続させるとともに、それぞれの吸熱容量△ＨＧＣ、△ＨＯＣにより高圧側の高温超臨界ＣＯ２の冷却されるエンタルピ総量Ｈｃを内分比する最適位置関係にあるよう構成する。
【００１３】
そして、上記ガス給湯ラインとオイル給湯ラインの折れ線接続をして最適位置関係を形成した、ガス給湯ラインの温度エンタルピ直線２１ａとオイル給湯ラインの温度エンタルピ直線２２ａは、前記ＣＯ２温度エンタルピ曲線２０に接触又は交叉することなく、より近接した位置に設定される。
【００１４】
また、上記第１の発明のＣＯ２冷凍サイクルの給湯システムにおける、
前記ガス給湯ラインは、ＣＯ２温度エンタルピ曲線の変極点の下部付近で第１ガスラインと第２ガスラインに分割して折れ線接続させ、第２ガスラインが前記ＣＯ２温度エンタルピ曲線に接触ないし交叉する事無くその下側の近接位置に位置させるとともに、高温側端部をオイル給湯ラインの低温側端部に折れ線接続をさせ、前記ＣＯ２温度エンタルピ曲線の下側温度領域に多折給湯ラインを形成する構成にしても良い。
【００１５】
上記発明は、前記請求項２記載の第１の実施例とは別の構成を持つ第２の実施例を示すもので、
図３に示すように、前記ガス給湯ラインの温度エンタルピ直線をＣＯ２温度エンタルピ曲線２０の変極点Ｆの下側付近で第１ガスライン２１ａＸと第２ガスライン２１ａＹに分割折れ線接続をさせ、第２ガスラインの温度エンタルピ直線２１ａＹは前記ＣＯ２温度エンタルピ曲線２０に対し略切線状に設ける構成としたもので、このような多折給湯ラインの形成により前記位置関係をより最適化したものである。
【００１６】
また、本発明の第２の発明であるＣＯ２冷凍サイクルの給湯システムは、
スクリュー圧縮機、ガスクーラ、膨張弁、蒸発器よりなるＣＯ２冷凍サイクルの前記圧縮機により得られた高圧側高温超臨界ＣＯ２を放熱冷却させるガスクーラを使用したＣＯ２超臨界冷凍サイクルの給湯システムにおいて、
前記給湯システムを形成する給湯ラインは、高圧側高温ＣＯ２の放熱をするガス給湯ラインと圧縮機オイルの熱交換をするオイルクーラのオイル給湯ラインとより構成し、
前記ガス給湯ラインとオイル給湯ラインには、それぞれの所定給湯水による個別給湯若しくは直並列給湯をさせたことを特徴とする。
【００１７】
上記発明は、前記第１の発明とはその構成内容を異にする第２の発明について記載されたもので、第１の発明の給湯システムはガス給湯ラインとオイル給湯ラインとを直列状に構成したものであるが、第２の発明においてはそれぞれの給湯ラインを独立させ個別の自立した給湯ラインを形成させ、それらを適宜組み合わせて並列ないし直並列させる構成にしてある。
なお、前記ガス給湯ラインは適宜分割しても良い。
【００１８】
また、上記第２の発明のＣＯ２冷凍サイクルの給湯システムにおける、
前記ガス給湯ラインを、ＣＯ２温度エンタルピ曲線の変極点の下部付近で低温側の第１ガスラインと高温側の第２ガスラインに分割し、
前記第１ガスラインにより変極点までのＣＯ２温度エンタルピ曲線の熱量の回収により中温給湯水を得るよう水量制御をし、
前記第２ガスラインとオイル給湯ラインは、ＣＯ２冷媒のガスクーラ入口側より下流側に向けそれぞれを併設して並列接続する構成とし、ＣＯ２温度エンタルピ曲線の高温域の熱量を回収させるとともに、ＣＯ２冷媒のガスクーラ入口温度に出来るだけ近接する高温給湯水を得るよう水量制御をして、
前記中温給湯水と高温給湯水とを混合して所定温度の給湯を可能とした構成が好ましい。
【００１９】
上記発明は、前記本発明の第２の発明の給湯システムを示す一実施例で、
図５に示すように、前記ガス給湯ラインの温度エンタルピ直線をＣＯ２温度エンタルピ曲線２０の変極点Ｆの下側付近で第１ガスライン２１ａＸＸと第２ガスライン２１ａＹＹに分割して個別の給湯ラインを形成させ、
前記第１ガスライン２１ａＸＸにより変極点ＦまでのＣＯ２温度エンタルピ曲線の熱量を回収させ、該回収により中温給湯を可能とする水量制御をし、
前記第２ガスライン２１ａＹＹとオイル給湯ライン２２ａは、ＣＯ２冷媒のガスクーラ入口側よりガスクーラに沿って下流側に向けそれぞれを併設させ、ＣＯ２温度エンタルピ曲線２０の高温域の熱量を回収させるとともに、ＣＯ２冷媒のガスクーラ入口温度に出来るだけ近接する高温給湯水を得るよう水量制御をして、前記中温給湯水と高温給湯水とを混合して所定温度の給湯を可能としたものである。
【００２０】
本実施例の場合は、他の実施例のように各給湯ラインがＣＯ２温度エンタルピ曲線２０の下部の温度領域で折れ線接続せずに、その両端の低温部と高温部に給湯ラインを個別に配設する構成にしてあるため、各給湯ラインは前記ＣＯ２温度エンタルピ曲線に出来る限り接近した状況での熱の授受を行うことができ、高い給湯効率を上げることができる。
【００２１】
そして上記第１及び第２の発明における、
前記オイル給湯ラインは、インジェクション給湯ラインとジャーナル給湯ラインに分岐し、分岐した二つのラインを直列接続した構成が好ましい。
【００２２】
【発明の実施の形態】
以下、本発明を図に示した実施例を用いて詳細に説明する。但し、この実施例に記載される構成部品の寸法、材質、形状、その相対配置などは特に特定的記載が無い限り、この発明の範囲をそれのみに限定する趣旨ではなく単なる説明例に過ぎない。
図１は本発明の第１の発明のＣＯ２冷凍サイクルの給湯システムの概略構成を示す図で、図２は図１の直列接続する第１の実施例を示す図で、ガス給湯ラインとオイル給湯ラインの吸熱エンタルピによる分割給湯の状況を示す図である。図３は図１の第２の実施例を示す図である。図４は本発明の第２の発明のＣＯ２冷凍サイクルの給湯システムの概略構成を示す図で、図５は図４の一実施例を示す図で、図６は図４の別の実施例を示す図である。
【００２３】
図１、図４に見るように、本発明のＣＯ２冷凍サイクルの給湯システムは、当該冷凍サイクルのガスクーラと、スクリュー圧縮機の加熱オイルを冷却するオイルクーラとの二つの組合せにより形成された冷却手段を有効に利用した給湯システムに係わるもので、図１に示す第１の発明は前記ガスクーラとオイルクーラとを直列状に接続する構成を備えたシステムである。
【００２４】
図１に示すＣＯ２冷凍サイクルの給湯システムは、ＣＯ２超臨界冷凍サイクル１０のガスクーラ１２のガス給湯ライン１２ａと、オイルクーラ１３のオイル給湯ライン１３ａとの直列状接続により構成する。
【００２５】
図２は、図１の直列接続するガス給湯ライン１２ａとオイル給湯ライン１３ａがそれぞれの吸熱能力に対応して高圧高温ＣＯ２のエンタルピを分割給湯する状況を示す図で、ＣＯ２超臨界冷凍サイクル１０の高圧側の高温ＣＯ２は、圧縮機１１の吐出側温度（約９０℃）よりガスクーラ１２の出口温度（夏季は約３０℃、冬季は約１０℃）まで冷却されるが、その温度変化（縦軸）に対するエンタルピ変化（横軸）の状況をＣＯ２温度エンタルピ曲線２０で示してあり、
また、上記ＣＯ２温度エンタルピ曲線２０の下部温度領域には、前記高圧側のＣＯ２冷媒を冷却するガス給湯ライン１２ａとオイル給湯ライン１３ａの吸熱能力を表すガス温度エンタルピ直線２１ａとオイル温度エンタルピ直線２２ａが示してある。
【００２６】
なお、上記ガス給湯ライン１２ａは常温の給水を受けその出口で中温水まで加熱され、加熱された中温水はオイル給湯ライン１３ａに受け継がれその出口で約８５℃の高温給湯水を得る構成にしてあるので、前記ガス温度エンタルピ直線２１ａの下端Ａは給水温度ｔ（夏季は約２５℃、冬季は約５℃）で始まり、中間の折れ線状継なぎ点Ｃを経由して得られた中温水は、オイル温度エンタルピ直線２２ａに接続されその出口Ｂで温度約８５℃の高温の給湯水を得る位置関係を持つ構成にしてある。
【００２７】
ところで、上記構成の最適位置関係は前記折れ線状継なぎ点Ｃの位置設定に係わり、
その継なぎ点Ｃは図示のように、ＣＯ２の冷却に要する総エンタルピ量Ｈｃに対する、ガス温度エンタルピ直線２１ａの吸熱エンタルピ△ＨＧＣと、オイル温度エンタルピ直線２２ａの吸熱エンタルピ△ＨＯＣとの内分比分割点により構成するのが好適である。
則ち、この場合は、ガス温度エンタルピ直線（Ａ−Ｃ）２１ａとオイル温度エンタルピ直線（Ｃ−Ｂ）２２ａは前記内分比点Ｃで折れ線接続され、前記ＣＯ２温度エンタルピ曲線２０の下側温度領域で前記曲線に接触ないし交叉することのない位置関係を維持する構成とし、ガスクーラ１２とオイルクーラ１３との直列状接続により高圧側ＣＯ２の顕熱冷却を行うとともに、ガスクーラに給水した常温水より約８５℃の高温給湯水を得る構成にしてある。
【００２８】
図３において、ガス給湯ライン１２ａを折れ線状に二分割して、二分割した高温側給湯ラインの出口にオイル給湯ラインを折れ線接続して、図に示すように当該ＣＯ２温度エンタルピ曲線２０の下側温度領域に多折給湯ラインＡ−Ｄ−Ｅ−Ｂを形成させたものである。
前記ガス給湯ライン１２ａの二分割された第１ガス温度エンタルピ直線２１ａＸと第２ガス温度エンタルピ直線２１ａＹとの継なぎ点Ｄは、前記ＣＯ２温度エンタルピ曲線２０の変極点Ｆの近接位置に設け、そして前記第２ガス温度エンタルピ直線２１ａＹには点Ｅを介して折れ線接続するオイル温度エンタルピ直線２２ｂを接続して、多折給湯ラインＡ−Ｄ−Ｅ−ＢをＣＯ２温度エンタルピ曲線２０の下側温度領域で該曲線の湾曲に対応させ、効率的に熱の授受を行う構成にしてある。
【００２９】
図４に示す第２の発明は、ガス給湯ライン１２ａとオイル給湯ライン１３ａを、それぞれ所定給湯水施設を持つ独立した個別給湯ラインより構成し、構成されたそれぞれの独立給湯ラインを並列または直列接続させ、それをさらに組合せたものである。
なお、前記ガス給湯ライン１２ａは更に複数個に分割しても良い。
【００３０】
図４のオイル給湯ライン１３ａにおいて、図に見るように、スクリュー圧縮機１１に設けてある前記オイルクーラ１３はインジェクション冷却部１４とジャーナル冷却部１５とより構成する。
そして、前記インジェクション冷却部１４は、圧縮ガスの冷却とシール効果を得るため、圧縮室入口に潤滑油を図示していないインジェクションにより噴射し、冷媒ガスとともに吐出された前記潤滑油を油分離器１１ａで分離し、分離した油をインジェクション冷却部１４へ導入してインジェクション給湯ライン１４ａを形成するとともに、
前記ジャーナル冷却部１５は、圧縮室のケーシングを冷却水により冷却する冷却部よりなり、ジャーナル給湯ライン１５ａを形成し、上記形成されたインジェクション給湯ライン１４ａとジャーナル給湯ライン１５ａとを直列接続する構成にしてある。
なお、上記オイルクーラ１３の構造は図１のオイルクーラ１３にも適用できる。
【００３１】
図５に見るように、ガス給湯ライン１２ａの温度エンタルピ直線をＣＯ２温度エンタルピ曲線２０の変極点Ｆの下側付近で第１ガスライン２１ａＸＸと第２ガスライン２１ａＹＹに分割して個別の独立給湯ラインを形成させたものである。そして、前記第１ガスライン２１ａＸＸにより変極点ＦまでのＣＯ２温度エンタルピ曲線２０の熱量の回収を行い、該回収により中温給湯を可能とする水量制御をし、
一方前記第２ガスライン２１ａＹＹとオイル給湯ライン２２ａは、ＣＯ２冷媒のガスクーラ入口側よりガスクーラに沿って下流側に向けそれぞれを併設させ、ＣＯ２温度エンタルピ曲線２０の高温域の熱量を回収させるとともに、ＣＯ２冷媒のガスクーラ入口温度に出来るだけ近接する高温給湯水を得るよう水量制御をして、前記中温給湯水と高温給湯水とを混合して所定温度の給湯を可能としたものである。
【００３２】
本実施例の場合は、他の実施例のように各給湯ラインがＣＯ２温度エンタルピ曲線２０の下部の温度領域で折れ線接続せずに、その両端の低温部と高温部に給湯ラインを個別に配設する構成にしてあるため、各給湯ラインは前記ＣＯ２温度エンタルピ曲線に出来る限り接近した状況での熱の授受を可能として高い給湯効率を上げることができる。
【００３３】
図６に示すように、本給湯システムは、スクリュー圧縮機１１と油分離器１１ａとガスクーラ１２とオイルクーラ１３等を含む構成よりなり、前記ガスクーラ１２は４個の直列ガスクーラＧＣ１、ＧＣ２、ＧＣ３、ＧＣ４とよりなる分割構成とし、オイルクーラ１３は二組みの直列インジェクション冷却部が形成するＯＣ１、ＯＣ２より構成する。
なお、太線実線ラインは当該ＣＯ２超臨界冷凍サイクルのＣＯ２冷媒の流れを示し、太線点線ラインは同じく圧縮機１１の潤滑油の流れを示してある。
この場合は、前記ガスクーラ１２は二組ずつ直列状に結合したものを二組用意し、負荷の状況に応じ、その一組を使用して、
ａ、配管２５より給水を導入して、配管２６→ＧＣ４→ＧＣ３→配管２６ａ→タンク１６の経路を経てタンク１６に貯留後ポンプ１８ｂにより配管２９を経由してタンク１７に約５５℃の中温水を供給する。
ｂ、又は、配管２５より給水を導入して、配管２６→ＧＣ４→ＧＣ３→配管２６ａ→タンク１６→ポンプ１８ａ→配管２８→ＧＣ２→ＧＣ１→配管２８ａを経由してタンク１７に約８０℃の高温水を供給する。
ｃ、一方、配管２５よりの給水を、配管３０を経由、オイルクーラ１３へ導入して、配管３１より約８０℃の高温水を得て、タンク１７へ貯留する構成にしてある。図６に示すように図４の発明の場合は冷凍容量の変動に対応して多様性を持たせている。
【００３４】
【発明の効果】
本発明は、上記構成により、下記効果を奏する。
潤滑油過熱防止のために設けてあるオイルクーラの有効利用を図り、該オイルクーラをガスクーラに併設させ、ガスクーラとの多様的組合せにより、高圧側の高圧高温ＣＯ２冷媒の顕熱冷却をより確実且つ効率的に行い、且つ効率的給湯を行うことができる。
【図面の簡単な説明】
【図１】本発明の第１の発明のＣＯ２冷凍サイクルの給湯システムの概略構成を示す図である。
【図２】図１の直列接続する給湯ラインの第１の実施例を示す図で、ガス給湯ラインとオイル給湯ラインの吸熱量による分割給湯の状況を示す図である。
【図３】図１の第２の実施例を示す図である。
【図４】本発明の第２の発明のＣＯ２冷凍サイクルの給湯システムの概略構成を示す図である。
【図５】図４の一実施例を示す図である。
【図６】図４の別の実施例を示す図である。
【図７】従来のＣＯ２超臨界冷凍サイクルの概略構成を示す図である。
【図８】図７のＣＯ２冷媒の状態変化を示すモリエル線図である。
【符号の説明】
１０　　ＣＯ２超臨界冷凍サイクル
１１　　スクリュー圧縮機
１１ａ　油分離器
１２　　ガスクーラ
１２ａ　ガス給湯ライン
１３　　オイルクーラ
１３ａ　オイル給湯ライン
１４　　インジェクション冷却部
１４ａ　インジェクション給湯ライン
１５　　ジャーナル冷却部
１５ａ　ジャーナル給湯ライン
２０　　ＣＯ２温度エンタルピ曲線
２１ａ　ガス温度エンタルピ直線（ガス給湯ラインの温度エンタルピ直線）
２２ａ、２２ｂ　オイル温度エンタルピ直線（オイル給湯ラインの温度エンタルピ直線）
２１ａＸ　ガス第１温度エンタルピ直線（第１ガスライン）
２１ａＹ　ガス第２温度エンタルピ直線（第２ガスライン）
２１ａＸＸ　第１ガスライン
２１ａＹＹ　第２ガスライン
２５、２６、２６ａ、２８、２８ａ、２９、３０、３１　　配管
１６、１７　　タンク
１８ａ、１８ｂ　　ポンプ[0001]
TECHNICAL FIELD OF THE INVENTION
The present invention relates to a CO 2 supercritical refrigeration cycle including a compressor, a gas cooler, an expansion valve, and an evaporator, which is connected in series or in parallel or individually by a combination of a gas hot water line by a gas cooler and an oil hot water line by an oil cooler of a compressor. The present invention relates to a hot water supply system for a CO 2 refrigeration cycle having an efficient configuration having a configuration including a hot water supply line formed in a hot water supply line.
[0002]
[Prior art]
CO 2 refrigerant used in the CO 2 supercritical refrigeration cycle, the prevention of global environmental pollution, inter alia, ozone depletion, prevention of global warming, much its adverse effects less than Freon, no toxicity, many in nature Attention has been paid to one of the existing natural refrigerants, and a vapor compression refrigeration cycle using CO 2 as a refrigerant tends to be frequently used.
However, since CO 2 reaches a critical point at a low temperature of 31.06 ° C., a vapor compression refrigeration cycle using the same will form a cycle including a supercritical region exceeding the critical point, and generally Cooling by sensible heat without the condensation process seen in the vapor compression refrigeration cycle of the above, becomes a high-pressure low-temperature refrigerant from a supercritical high-pressure high-temperature refrigerant, and then a gas-liquid two-phase mixed state by adiabatic expansion by an expansion valve And evaporates with an evaporator to send cold heat to the outside. For example, there is a proposal shown in Patent Document 1.
[0003]
FIG. 7 shows a schematic configuration of a CO 2 vapor compression refrigeration cycle including a compressor 101, a gas cooler (referred to as a gas cooler or a radiator) 102, an expander 103, and an evaporator 104. FIG. 8 is a Mollier diagram showing a CO 2 supercritical refrigeration cycle in the refrigeration cycle of FIG.
As shown in FIG. 8, the CO 2 refrigerant is compressed by a compressor 101 which is a screw compressor, and as shown in A → B, a critical point K (critical temperature 31.1 ° C., critical pressure P K = 75.28 kg / cm 2) is compressed to a pressure P 2 beyond the. Then, as shown in B → C in the figure, the sensible heat of the compressed high-pressure high-temperature CO 2 is radiated to the atmosphere by the gas cooler 102, and the radiated high-pressure low-temperature CO 2 is further cooled as shown in C → D in the figure. The expansion valve 103 expands the pressure along the isenthalpy line to lower the pressure. Due to this pressure drop, the vapor phase becomes the wet vapor of the gas-liquid two-phase mixture, and the CO 2 refrigerant is vaporized in the evaporator 104 to evaporate the liquid phase and release cold heat to the outside.
[0004]
As shown in FIG. 8, the gas having a high density is located on the right side of the isotherm T K passing through the critical point K and on the right side of the vapor pressure not lower than the critical pressure P K (75.28 kg / cm 2 ) of the saturated vapor line. a state, in general without being liquefied in this region to obtain a high-pressure low-temperature CO 2 liquid possible states of the left of the isotherms T K by sensible cooling using gas cooler, the expansion pressure reduction in the next step However, the cooling by the gas cooler alone requires a large heat absorption capacity.
[0005]
On the other hand, in the case of the CO 2 supercritical refrigeration cycle, the refrigerant sucked into the compressor is in a high temperature state, and there is a problem of deterioration of the lubricating oil. It is desired to realize a practical solution.
When the degree of superheat is reduced to prevent the above-mentioned high temperature, and operation is performed in the state of the point A in FIG. 8, the liquid-phase refrigerant flows into the compressor and forms a cause of damage to the compressor. We are driving in the right state than S v.
[0006]
Therefore, an oil cooler is provided in the screw compressor, and is constituted by an injection cooling unit and a journal cooling unit. The former injects lubricating oil into the compression chamber inlet by injection in order to obtain a cooling and sealing effect of the compressed gas, and the lubricating oil discharged together with the refrigerant gas is separated by an oil separator, and the separated oil is cooled with cooling water or the like. A cooling unit for cooling with a refrigerant is provided, and the latter refers to a cooling unit for cooling a casing of a compression chamber with cooling water, and an oil cooler is configured to perform cooling by both.
[0007]
[Patent Document 1]
JP 2001-4235 A
[Problems to be solved by the invention]
The present invention has been made in view of the above problems,
Efficient use of the oil cooler provided to prevent overheating of the lubricating oil. The oil cooler is installed in the gas cooler. By various combinations with the gas cooler, the sensible heat cooling of the high-pressure, high-temperature, high-temperature CO 2 refrigerant on the high-pressure side is ensured. It is an object of the present invention to provide a hot water supply system for a CO 2 refrigeration cycle that is performed efficiently.
[0009]
[Means for Solving the Problems]
Therefore, a hot water supply system for a CO 2 refrigeration cycle according to a first aspect of the present invention includes:
A hot water supply system for a CO 2 supercritical refrigeration cycle using a gas cooler that radiates and cools high-temperature high-temperature supercritical CO 2 obtained by the compressor of the CO 2 refrigeration cycle including a screw compressor, a gas cooler, an expansion valve, and an evaporator. At
The hot water supply system supplies a normal-temperature water from an outlet of the gas cooler and obtains a medium-temperature water at an inlet.A countercurrent gas hot water supply line, and introduces the medium-temperature water exiting the gas hot water line into an oil cooler of a screw compressor. Composed of an oil hot water line that obtains high-temperature water at its outlet,
The gas hot water supply line and the oil hot water supply line are connected in series.
[0010]
The first aspect of the present invention provides a cooling means for radiating and cooling high-temperature supercritical CO 2 at about 90 ° C. on the high pressure side of a CO 2 supercritical refrigeration cycle to obtain high-pressure low-temperature CO 2 , wherein a gas hot water supply line using a gas cooler and an oil cooler are used. An oil hot water supply line is provided in series, a cooling temperature sharing area for each is determined, a gas hot water supply line is used to obtain 50-60 ° C medium-temperature water, and then an oil hot water supply line is used to obtain 70-80 ° C high-temperature water. In addition, the oil cooler is effectively used.
The gas hot water supply line uses a countercurrent type, in which room-temperature water is introduced from the outlet side of the high-temperature supercritical CO 2 on the high-pressure side of the gas cooler, and medium-temperature water is obtained from the inlet side.
[0011]
In the hot water supply system for a CO 2 refrigeration cycle according to the first aspect,
The gas hot water supply line and the oil hot water supply line are provided in the vicinity of a lower temperature region with respect to a CO 2 temperature enthalpy curve in which a vertical axis indicates a temperature change and a horizontal axis indicates an enthalpy change, and indicates a heat absorption state of the gas hot water line. A CO 2 enthalpy change in which the middle temperature end of the enthalpy straight line and the middle temperature end of the temperature enthalpy straight line of the oil hot water supply line for heat exchange with oil are connected in a broken line, and the cooling is performed in accordance with each heat absorption capacity. It is preferable that the amount is internally divided.
[0012]
The invention of the first embodiment enables optimal cooling corresponding to the heat absorption capacity of each of the gas hot water supply line and the oil hot water supply line connected in series when cooling the high-pressure side CO 2 in the first invention. It is specified for the specification.
The high-pressure high-temperature CO 2 on the high-pressure side heated to a discharge temperature of about 90 ° C. by the compressor is cooled to about 30 ° C. (for summer) or about 10 ° C. (for winter) by the cooling means.
In this case, a temperature enthalpy straight line indicating a heat absorption state of each of the gas hot water supply line and the oil hot water supply line, and a CO 2 temperature enthalpy curve indicating a process in which high-pressure high-temperature CO 2 is cooled by the cooling means, in the case shown in T-H coordinates indicating the enthalpy change the horizontal axis changes, as shown in FIG. 2, the CO 2 temperature enthalpy and temperature enthalpy linear 22a of the temperature enthalpy straight 21a and the oil hot-water supply line of the gas water line A line is connected in the lower temperature region of the curve 20, and the heat absorption capacities △ HGC and △ HOC are in an optimal positional relationship for internally dividing the total amount Hc of enthalpy to be cooled of the high-temperature supercritical CO 2 on the high pressure side. I do.
[0013]
The gas enthalpy straight line 21a of the gas hot water supply line and the temperature enthalpy straight line 22a of the oil hot water supply line formed by the broken line connection of the gas hot water supply line and the oil hot water supply line correspond to the CO 2 temperature enthalpy curve 20. It is set at a closer position without contact or crossover.
[0014]
In the hot water supply system for a CO 2 refrigeration cycle according to the first aspect,
The gas hot water supply line is divided into a first gas line and a second gas line near a lower portion of the inflection point of the CO 2 temperature enthalpy curve and connected in a broken line, and the second gas line contacts or crosses the CO 2 temperature enthalpy curve. Without lowering, the high temperature side end is connected to the low temperature side end of the oil hot water supply line by a broken line connection, and the multi-fold hot water supply line is connected to the lower temperature region of the CO 2 temperature enthalpy curve. It may be configured to be formed.
[0015]
The above invention shows a second embodiment having a different configuration from the first embodiment of the second aspect,
As shown in FIG. 3, the temperature enthalpy straight line of the gas hot water supply line is divided and connected to the first gas line 21aX and the second gas line 21aY near the lower side of the inflection point F of the CO 2 temperature enthalpy curve 20, The temperature enthalpy straight line 21aY of the two gas lines is configured to be provided in a substantially cut line shape with respect to the CO 2 temperature enthalpy curve 20, and the positional relationship is further optimized by forming such a multi-fold hot water supply line. .
[0016]
Further, a hot water supply system for a CO 2 refrigeration cycle according to a second invention of the present invention includes:
In a hot water supply system of a CO 2 supercritical refrigeration cycle using a gas cooler that radiates and cools high pressure side high temperature supercritical CO 2 obtained by the compressor of the CO 2 refrigeration cycle including a screw compressor, a gas cooler, an expansion valve, and an evaporator. ,
The hot water supply line forming the hot water supply system includes a gas hot water supply line that radiates high-pressure-side high-temperature CO 2 and an oil cooler oil hot water line that exchanges heat of compressor oil.
The gas hot water supply line and the oil hot water supply line are provided with individual hot water supply or predetermined parallel hot water supply with respective predetermined hot water supply.
[0017]
The above invention has been described with respect to a second invention having a different configuration from the first invention, and the hot water supply system of the first invention has a gas hot water supply line and an oil hot water supply line arranged in series. However, in the second invention, each hot water supply line is made independent to form an independent and independent hot water supply line, and they are appropriately combined and arranged in parallel or in series.
In addition, the gas hot water supply line may be appropriately divided.
[0018]
In the hot water supply system for a CO 2 refrigeration cycle according to the second invention,
The gas hot water supply line is divided into a first gas line on the low temperature side and a second gas line on the high temperature side near a lower part of the inflection point of the CO 2 temperature enthalpy curve,
The first gas line controls the amount of water so as to obtain medium-temperature hot water by collecting the heat of the CO 2 temperature enthalpy curve up to the inflection point,
The second gas line and the oil hot water line are configured so as to be connected in parallel from the gas cooler inlet side of the CO 2 refrigerant to the downstream side so as to collect heat in a high temperature region of the CO 2 temperature enthalpy curve, and (2) Control the water volume so as to obtain high-temperature hot water as close as possible to the gas cooler inlet temperature of the refrigerant,
It is preferable that the medium-temperature hot water and the high-temperature hot water are mixed to supply hot water at a predetermined temperature.
[0019]
The above invention is an embodiment showing the hot water supply system of the second invention of the present invention,
As shown in FIG. 5, the temperature enthalpy straight line of the gas hot water supply line is divided into a first gas line 21aXX and a second gas line 21aYY near a lower side of the inflection point F of the CO 2 temperature enthalpy curve 20, and individual hot water supply lines are provided. To form
The first gas line 21aXX allows the calorific value of the CO 2 temperature enthalpy curve up to the inflection point F to be recovered, and by performing the recovery, the water amount is controlled to enable the medium-temperature hot water supply.
The second gas line 21aYY and the oil hot water supply line 22a are respectively provided in parallel from the gas cooler inlet side of the CO 2 refrigerant toward the downstream side along the gas cooler, and recover the heat amount in the high temperature region of the CO 2 temperature enthalpy curve 20, Water amount is controlled so as to obtain high-temperature hot water as close as possible to the gas cooler inlet temperature of the CO 2 refrigerant, and the medium-temperature hot water and high-temperature hot water are mixed to enable hot water supply at a predetermined temperature.
[0020]
In the case of the present embodiment, each hot water supply line is not connected in a broken line in the temperature region below the CO 2 temperature enthalpy curve 20 as in the other embodiments, and the hot water supply lines are individually connected to the low-temperature portion and the high-temperature portion at both ends. Because of the arrangement, each hot water supply line can transfer heat in a situation as close as possible to the CO 2 temperature enthalpy curve, and high hot water supply efficiency can be increased.
[0021]
In the first and second inventions,
It is preferable that the oil hot water supply line is branched into an injection hot water supply line and a journal hot water supply line, and the two branched lines are connected in series.
[0022]
BEST MODE FOR CARRYING OUT THE INVENTION
Hereinafter, the present invention will be described in detail using embodiments shown in the drawings. However, the dimensions, materials, shapes, relative arrangements, and the like of the components described in this embodiment are not merely intended to limit the scope of the present invention, but are merely illustrative examples unless otherwise specified. .
FIG. 1 is a diagram showing a schematic configuration of a hot water supply system for a CO 2 refrigeration cycle according to a first invention of the present invention, and FIG. 2 is a diagram showing a first embodiment of a series connection of FIG. It is a figure showing the situation of division hot water supply by heat absorption enthalpy of a hot water supply line. FIG. 3 is a diagram showing a second embodiment of FIG. 4 is a diagram showing a schematic configuration of a hot water supply system for a CO 2 refrigeration cycle according to a second invention of the present invention, FIG. 5 is a diagram showing one embodiment of FIG. 4, and FIG. 6 is another embodiment of FIG. FIG.
[0023]
As shown in FIGS. 1 and 4, the hot water supply system for a CO 2 refrigeration cycle of the present invention has a cooling system formed by two combinations of a gas cooler for the refrigeration cycle and an oil cooler for cooling the heating oil of the screw compressor. The first invention shown in FIG. 1 relates to a hot water supply system that effectively uses means, and is a system having a configuration in which the gas cooler and the oil cooler are connected in series.
[0024]
The hot water supply system of the CO 2 refrigeration cycle shown in FIG. 1 is configured by connecting a gas hot water supply line 12 a of a gas cooler 12 and an oil hot water supply line 13 a of an oil cooler 13 in a CO 2 supercritical refrigeration cycle 10 in series.
[0025]
Figure 2 is a diagram illustrating a situation where the gas water line 12a and the oil hot-water supply line 13a to be connected in series in Figure 1 divides hot water enthalpy of the high-pressure high-temperature CO 2 corresponding to each of the heat absorption capacity, CO 2 supercritical refrigeration cycle The high-temperature CO 2 on the high-pressure side 10 is cooled from the discharge-side temperature of the compressor 11 (about 90 ° C.) to the outlet temperature of the gas cooler 12 (about 30 ° C. in summer and about 10 ° C. in winter). The state of the enthalpy change (horizontal axis) with respect to the (vertical axis) is shown by a CO 2 temperature enthalpy curve 20,
In the lower temperature region of the CO 2 temperature enthalpy curve 20, a gas temperature enthalpy straight line 21a and an oil temperature enthalpy straight line 21a representing the heat absorption capacity of the gas hot water supply line 12a and the oil hot water supply line 13a for cooling the high-pressure side CO 2 refrigerant. 22a is shown.
[0026]
The gas hot water supply line 12a receives normal-temperature water supply and is heated to intermediate-temperature water at an outlet thereof. The heated medium-temperature water is passed to an oil hot water supply line 13a to obtain hot water of approximately 85 ° C. at the outlet. Therefore, the lower end A of the gas temperature enthalpy straight line 21a starts at the feed water temperature t (about 25 ° C. in summer and about 5 ° C. in winter), and the medium-temperature water obtained via the intermediate broken line joint C is The outlet B is connected to the oil temperature enthalpy straight line 22a, and has a positional relationship of obtaining hot water at a temperature of about 85 ° C.
[0027]
Incidentally, the optimal positional relationship of the above configuration relates to the position setting of the polygonal joint point C,
The joint point C is, as shown in the figure, the internal ratio of the endothermic enthalpy of the gas temperature enthalpy line 21a ａHGC and the endothermic enthalpy of the oil temperature enthalpy line 22a △ HOC to the total enthalpy amount Hc required for cooling CO 2. It is preferable to configure by dividing points.
That is, in this case, the gas temperature enthalpy straight line (AC) 21a and the oil temperature enthalpy straight line (CB) 22a are connected in a broken line at the internal division point C, and the lower side of the CO 2 temperature enthalpy curve 20 In the temperature region, a configuration is maintained that does not touch or cross the curve, and the gas cooler 12 and the oil cooler 13 are connected in series to perform sensible heat cooling of the high-pressure side CO 2 and to supply the gas cooler with normal temperature. It is configured to obtain hot water of about 85 ° C higher than water.
[0028]
3, a gas water line 12a by bisection into polygonal line, the two divided into the outlet of the high-temperature hot-water supply line oil hot-water supply line and a polygonal line connecting, under the CO 2 temperature enthalpy curve 20 as shown in FIG. A multi-fold hot water supply line ADEB is formed in the side temperature region.
A junction point D between the first gas temperature enthalpy straight line 21aX and the second gas temperature enthalpy straight line 21aY of the gas hot water supply line 12a is provided at a position near an inflection point F of the CO 2 temperature enthalpy curve 20, An oil temperature enthalpy straight line 22b connected in a broken line via a point E is connected to the second gas temperature enthalpy straight line 21aY so that the multi-fold hot water supply line ADEB is below the CO 2 temperature enthalpy curve 20. The configuration is such that heat is transferred efficiently in accordance with the curvature of the curve in the temperature region.
[0029]
In the second invention shown in FIG. 4, the gas hot water supply line 12a and the oil hot water supply line 13a are constituted by independent individual hot water supply lines each having a predetermined hot water supply facility, and the individual independent hot water supply lines are connected in parallel or in series. And combining them further.
The gas hot water supply line 12a may be further divided into a plurality.
[0030]
In the oil hot water supply line 13a of FIG. 4, as shown in the figure, the oil cooler 13 provided in the screw compressor 11 comprises an injection cooling unit 14 and a journal cooling unit 15.
Then, the injection cooling unit 14 injects the lubricating oil into the compression chamber inlet by injection (not shown) to obtain the cooling effect and the sealing effect of the compressed gas, and discharges the lubricating oil discharged together with the refrigerant gas into the oil separator 11a. And the separated oil is introduced into the injection cooling unit 14 to form the injection hot water supply line 14a,
The journal cooling unit 15 includes a cooling unit that cools the casing of the compression chamber with cooling water, forms a journal hot water supply line 15a, and is configured to connect the formed injection hot water supply line 14a and the journal hot water supply line 15a in series. It is.
The structure of the oil cooler 13 can be applied to the oil cooler 13 shown in FIG.
[0031]
As shown in FIG. 5, the temperature enthalpy straight line of the gas hot water supply line 12a is divided into a first gas line 21aXX and a second gas line 21aYY near a lower side of the inflection point F of the CO 2 temperature enthalpy curve 20, and the individual independent hot water supply is performed. Lines are formed. Then, the amount of heat of the CO 2 temperature enthalpy curve 20 up to the inflection point F is collected by the first gas line 21aXX, and the amount of water is controlled to enable medium-temperature hot water supply by the collection.
On the other hand, the second gas line 21aYY and the oil hot water supply line 22a are provided side by side from the gas cooler inlet side of the CO 2 refrigerant to the downstream side along the gas cooler to collect heat in the high temperature region of the CO 2 temperature enthalpy curve 20. In addition, the water amount is controlled so as to obtain high-temperature hot water as close as possible to the gas cooler inlet temperature of the CO 2 refrigerant, and the medium-temperature hot water and high-temperature hot water are mixed to enable hot water supply at a predetermined temperature.
[0032]
In the case of the present embodiment, each hot water supply line is not connected in a broken line in the temperature region below the CO 2 temperature enthalpy curve 20 as in the other embodiments, and the hot water supply lines are individually connected to the low-temperature portion and the high-temperature portion at both ends. Since the hot water supply lines are arranged, the hot water supply lines can exchange heat in a situation as close as possible to the CO 2 temperature enthalpy curve, thereby increasing the hot water supply efficiency.
[0033]
As shown in FIG. 6, the hot water supply system has a configuration including a screw compressor 11, an oil separator 11a, a gas cooler 12, an oil cooler 13, and the like. The gas cooler 12 has four in-line gas coolers GC1, GC2, GC3, The oil cooler 13 is composed of OC1 and OC2 formed by two sets of serial injection cooling units.
Incidentally, the heavy solid line lines indicate the flow of the CO 2 refrigerant in the CO 2 supercritical refrigeration cycle, a thick line dotted line are also shown the flow of the lubricating oil in the compressor 11.
In this case, two sets of the gas coolers 12 connected in series by two sets are prepared, and one set is used according to a load condition.
a, water is introduced from the pipe 25, and is stored in the tank 16 via the path of the pipe 26 → GC4 → GC3 → the pipe 26a → the tank 16; Supply.
b, or water is introduced from the pipe 25, and a high temperature of about 80 ° C. is supplied to the tank 17 via the pipe 26 → GC4 → GC3 → pipe 26a → tank 16 → pump 18a → pipe 28 → GC2 → GC1 → pipe 28a. Supply water.
(c) On the other hand, water supplied from the pipe 25 is introduced into the oil cooler 13 via the pipe 30 to obtain high-temperature water of about 80 ° C. from the pipe 31 and stored in the tank 17. As shown in FIG. 6, in the case of the invention of FIG. 4, diversity is given in accordance with the fluctuation of the refrigeration capacity.
[0034]
【The invention's effect】
The present invention has the following effects by the above configuration.
Efficient use of the oil cooler provided to prevent overheating of the lubricating oil. The oil cooler is installed in the gas cooler. By various combinations with the gas cooler, the sensible heat cooling of the high-pressure, high-temperature, high-temperature CO 2 refrigerant on the high-pressure side is ensured. In addition, it can be performed efficiently and hot water can be efficiently supplied.
[Brief description of the drawings]
FIG. 1 is a diagram showing a schematic configuration of a hot water supply system for a CO 2 refrigeration cycle according to a first invention of the present invention.
FIG. 2 is a view showing a first embodiment of the hot water supply lines connected in series in FIG. 1, and is a view showing a state of split hot water supply by a heat absorption amount of a gas hot water supply line and an oil hot water supply line.
FIG. 3 is a diagram showing a second embodiment of FIG. 1;
FIG. 4 is a diagram showing a schematic configuration of a hot water supply system for a CO 2 refrigeration cycle according to a second invention of the present invention.
FIG. 5 is a diagram showing one embodiment of FIG. 4;
FIG. 6 is a diagram showing another embodiment of FIG. 4;
FIG. 7 is a diagram showing a schematic configuration of a conventional CO 2 supercritical refrigeration cycle.
FIG. 8 is a Mollier diagram showing a state change of the CO 2 refrigerant in FIG. 7;
[Explanation of symbols]
Reference Signs List 10 CO 2 supercritical refrigeration cycle 11 Screw compressor 11a Oil separator 12 Gas cooler 12a Gas hot water supply line 13 Oil cooler 13a Oil hot water supply line 14 Injection cooling unit 14a Injection hot water supply line 15 Journal cooling unit 15a Journal hot water supply line 20 CO 2 temperature enthalpy curve 21a Gas temperature enthalpy straight line (temperature enthalpy straight line of gas hot water supply line)
22a, 22b Oil temperature enthalpy straight line (oil enthalpy straight line for hot water supply line)
21aX gas first temperature enthalpy straight line (first gas line)
21aY gas second temperature enthalpy straight line (second gas line)
21aXX First gas line 21aYY Second gas line 25, 26, 26a, 28, 28a, 29, 30, 31 Piping 16, 17 Tank 18a, 18b Pump

Claims (6)

スクリュー圧縮機、ガスクーラ、膨張弁、蒸発器よりなるＣＯ２冷凍サイクルの前記圧縮機により得られた高圧側の高温超臨界ＣＯ２を放熱冷却させるガスクーラを使用したＣＯ２超臨界冷凍サイクルの給湯システムにおいて、
前記給湯システムは、前記ガスクーラの出口より常温水を供給して入口で中温水を得る向流式のガス給湯ラインと、該ガス給湯ラインを出た中温水をスクリュー圧縮機のオイルクーラに導入しその出口で高温水を得るようにしたオイル給湯ラインとより構成し、
前記ガス給湯ラインとオイル給湯ラインとを直列接続したことを特徴とするＣＯ２冷凍サイクルの給湯システム。A hot water supply system for a CO 2 supercritical refrigeration cycle using a gas cooler that radiates and cools high-temperature high-temperature supercritical CO 2 obtained by the compressor of the CO 2 refrigeration cycle including a screw compressor, a gas cooler, an expansion valve, and an evaporator. At
The hot water supply system supplies a normal-temperature water from an outlet of the gas cooler and obtains a medium-temperature water at an inlet.A countercurrent gas hot water supply line, and introduces the medium-temperature water exiting the gas hot water line into an oil cooler of a screw compressor. Composed of an oil hot water line that obtains high-temperature water at its outlet,
A hot water supply system for a CO 2 refrigeration cycle, wherein the gas hot water supply line and the oil hot water supply line are connected in series. 前記ガス給湯ラインとオイル給湯ラインは、温度変化を縦軸にとりエンタルピ変化を横軸にとるＣＯ２温度エンタルピ曲線の下側温度領域に近接して設けられ、ガス給湯ラインの吸熱状況を示す温度エンタルピ直線の中温側端部と、オイルとの熱交換をするオイル給湯ラインの温度エンタルピ直線の中温側端部とを折れ線状に接続し、それぞれの吸熱容量に対応して冷却するＣＯ２エンタルピ変化量を内分比分担をする構成としたことを特徴とする請求項１記載のＣＯ２冷凍サイクルの給湯システム。The gas hot water supply line and the oil hot water supply line are provided in the vicinity of a lower temperature region of a CO 2 temperature enthalpy curve in which a vertical axis indicates a temperature change and a horizontal axis indicates a change in enthalpy, and a temperature enthalpy indicating a heat absorption state of the gas hot water line. CO 2 enthalpy change amount in which the straight-line middle temperature end and the medium-temperature side enthalpy of the oil hot water line for heat exchange with oil are connected in a polygonal line and cooled in accordance with each heat absorption capacity The hot water supply system for a CO 2 refrigeration cycle according to claim 1, wherein the internal division ratio is divided. 前記ガス給湯ラインを、ＣＯ２温度エンタルピ曲線の変極点の下部付近で低温側より第１ガスラインと第２ガスラインに分割して折れ線接続させ、第２ガスラインが前記ＣＯ２温度エンタルピ曲線に接触ないし交叉する事無くその下側の近接位置に位置させるとともに、その高温側端部をオイル給湯ラインの低温側端部に折れ線接続させ、前記ＣＯ２温度エンタルピ曲線の下側温度領域に多折給湯ラインを形成したことを特徴とする請求項１記載のＣＯ２冷凍サイクルの給湯システム。The gas hot water supply line is divided into a first gas line and a second gas line near the lower part of the inflection point of the CO 2 temperature enthalpy curve from the low temperature side and connected in a broken line, and the second gas line is connected to the CO 2 temperature enthalpy curve. It is located at the lower position without contact or crossover, and its high-temperature end is connected to the low-temperature end of the oil hot water supply line in a broken line, so that it can be folded into the lower temperature region of the CO 2 temperature enthalpy curve. The hot water supply system for a CO 2 refrigeration cycle according to claim 1, wherein a hot water supply line is formed. スクリュー圧縮機、ガスクーラ、膨張弁、蒸発器よりなるＣＯ２冷凍サイクルの前記圧縮機により得られた高圧側の高温超臨界ＣＯ２を放熱冷却させるガスクーラを使用したＣＯ２超臨界冷凍サイクルの給湯システムにおいて、
前記給湯システムを形成する給湯ラインは、高圧側の高温ＣＯ２の放熱をするガス給湯ラインと圧縮機オイルの熱交換をするオイル給湯ラインとより構成し、前記ガス給湯ラインとオイル給湯ラインには、それぞれの所定給湯水による個別給湯若しくは直並列給湯をさせたことを特徴とするＣＯ２冷凍サイクルの給湯システム。A hot water supply system for a CO 2 supercritical refrigeration cycle using a gas cooler that radiates and cools high-temperature high-temperature supercritical CO 2 obtained by the compressor of the CO 2 refrigeration cycle including a screw compressor, a gas cooler, an expansion valve, and an evaporator. At
The hot water supply line forming the hot water supply system includes a gas hot water supply line for radiating high-temperature high-temperature CO 2 on the high-pressure side and an oil hot water supply line for heat exchange of compressor oil. A hot water supply system for a CO 2 refrigeration cycle, wherein individual hot water supply or series-parallel hot water supply by predetermined hot water is performed. 前記ガス給湯ラインを、ＣＯ２温度エンタルピ曲線の変極点の下部付近で低温側の第１ガスラインと高温側の第２ガスラインに分割し、
前記第１ガスラインにより変極点までのＣＯ２温度エンタルピ曲線の熱量の回収により中温給湯水を得るよう水量制御をし、
前記第２ガスラインとオイル給湯ラインは、ＣＯ２冷媒のガスクーラ入口側より下流側に向けそれぞれを併設させ、ＣＯ２温度エンタルピ曲線の高温域の熱量を回収させるとともに、ＣＯ２冷媒のガスクーラ入口温度に出来るだけ近接する高温給湯水を得るよう水量制御をして、
前記中温給湯水と高温給湯水とを混合して所定温度の給湯を可能とした請求項４記載のＣＯ２冷凍サイクルの給湯システム。The gas hot water supply line is divided into a first gas line on the low temperature side and a second gas line on the high temperature side near a lower part of the inflection point of the CO 2 temperature enthalpy curve,
The first gas line controls the amount of water so as to obtain medium-temperature hot water by collecting the heat of the CO 2 temperature enthalpy curve up to the inflection point,
The second gas line and the oil hot water supply line are provided in parallel with each other from the gas cooler inlet side of the CO 2 refrigerant to the downstream side to recover the heat amount in the high temperature region of the CO 2 temperature enthalpy curve, and to reduce the gas cooler inlet temperature of the CO 2 refrigerant. Control the amount of hot water to get hot water as close as possible to
The hot water supply system for a CO 2 refrigeration cycle according to claim 4, wherein the medium-temperature hot water and the high-temperature hot water are mixed to supply hot water at a predetermined temperature. 前記オイル給湯ラインは、インジェクション給湯ラインとジャーナル給湯ラインに分岐し、分岐した二つのラインを直列接続をしたことを特徴とする請求項１若しくは請求項４記載のＣＯ２冷凍サイクルの給湯システム。5. The hot water supply system for a CO 2 refrigeration cycle according to claim 1, wherein the oil hot water supply line is branched into an injection hot water supply line and a journal hot water supply line, and the two branched lines are connected in series.
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JP2013068403A (en) * 2011-09-09 2013-04-18 Mitsubishi Electric Corp Heat pump water heater
WO2014199479A1 (en) 2013-06-13 2014-12-18 三菱電機株式会社 Heat pump device
JP6075451B2 (en) * 2013-06-13 2017-02-08 三菱電機株式会社 Heat pump equipment
EP3071904A4 (en) * 2013-10-31 2017-07-19 Emerson Climate Technologies, Inc. Heat pump system
US10156384B2 (en) 2013-10-31 2018-12-18 Emerson Climate Technologies, Inc. Heat pump system
JP2015038354A (en) * 2014-09-29 2015-02-26 三浦工業株式会社 Heat recovery system
CN109323475A (en) * 2018-09-11 2019-02-12 西安交通大学 A kind of critical-cross carbon dioxide system and its optimization coupling process
CN109323475B (en) * 2018-09-11 2020-05-19 西安交通大学 Transcritical carbon dioxide system and optimized coupling method thereof

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