JPH022401Y2 - - Google Patents
Info
- Publication number
- JPH022401Y2 JPH022401Y2 JP1984137825U JP13782584U JPH022401Y2 JP H022401 Y2 JPH022401 Y2 JP H022401Y2 JP 1984137825 U JP1984137825 U JP 1984137825U JP 13782584 U JP13782584 U JP 13782584U JP H022401 Y2 JPH022401 Y2 JP H022401Y2
- Authority
- JP
- Japan
- Prior art keywords
- compressor
- gas
- evaporator
- heat exchanger
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000012530 fluid Substances 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 239000011550 stock solution Substances 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- 229920006395 saturated elastomer Polymers 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- CYTYCFOTNPOANT-UHFFFAOYSA-N Perchloroethylene Chemical group ClC(Cl)=C(Cl)Cl CYTYCFOTNPOANT-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000015203 fruit juice Nutrition 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 229950011008 tetrachloroethylene Drugs 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000010888 waste organic solvent Substances 0.000 description 1
Description
【考案の詳細な説明】
産業上の利用分野
本考案は、例えば排液、排有機溶剤海水、果汁
等を濃縮、蒸留するのに利用される装置に関す
る。[Detailed Description of the Invention] Industrial Application Field The present invention relates to an apparatus used for concentrating and distilling waste liquid, waste organic solvent seawater, fruit juice, etc., for example.
従来の技術
蒸気再圧縮式蒸発装置は、原液を加熱すること
により発生した蒸気を圧縮して高温高圧にし、こ
の高温高圧の蒸気を原液の加熱源として利用する
所にあり、潜熱を回収できてエネルギー効率が良
く、成績係数は10〜20にもなり、ランニングコス
トが安い等の利点がある。Conventional technology A vapor recompression type evaporator compresses the vapor generated by heating the raw liquid to high temperature and high pressure, and uses this high temperature and high pressure steam as a heating source for the raw liquid, and can recover latent heat. It has advantages such as high energy efficiency, coefficient of performance of 10 to 20, and low running costs.
このような従来の蒸気再圧縮式蒸発装置の系統
図を第４図に示してある。 A system diagram of such a conventional vapor recompression type evaporator is shown in FIG.
濃縮原液は、２つの予熱器１，２で並行に予熱
されて蒸発缶３に入る。蒸発缶３には熱交換器４
が備えられており、予熱されて供給された原液は
熱交換器４にて加熱されて蒸気となる。蒸発缶３
で発生した蒸気は、デミスタ５で液滴を分離後、
遠心式、ルーツ式等のコンプレツサ６に吸入さ
れ、圧縮されて高温高圧の蒸気となる。この高温
高圧蒸気は原液より飽和蒸気温度が高いので、熱
交換器４にて蒸発缶３へ導入された原液を加熱で
き、その結果高温高圧の蒸気は凝縮して蒸留液と
なる。蒸留液はポンプ７で予熱器１へ供給され、
ここで濃縮原液を予備加熱後蒸留液として、一般
には図示しないタンクに溜められる。一方、蒸発
缶３において濃縮された原液はポンプ８で予熱器
２に送られ、濃縮原液を予備加熱後濃縮液とし
て、一般には図示しないタンクに溜められる。な
お、コンプレツサ６は電動機、内燃機関、スチー
ムタービン等の駆動源９で駆動されている。 The concentrated stock solution is preheated in parallel by two preheaters 1 and 2 and then enters the evaporator 3. A heat exchanger 4 is installed in the evaporator 3.
The preheated stock solution is heated in a heat exchanger 4 and turned into steam. Evaporator 3
After the vapor generated is separated into droplets by demister 5,
It is sucked into a compressor 6 such as a centrifugal type or Roots type, and is compressed into high-temperature, high-pressure steam. Since this high-temperature, high-pressure steam has a saturated steam temperature higher than that of the stock solution, the stock solution introduced into the evaporator 3 can be heated by the heat exchanger 4, and as a result, the high-temperature, high-pressure steam condenses to become a distilled liquid. The distillate is supplied to the preheater 1 by a pump 7,
Here, the concentrated stock solution is preheated and then stored as a distillate in a tank (not shown). On the other hand, the concentrated stock solution in the evaporator 3 is sent to the preheater 2 by a pump 8, and after preheating, the concentrated stock solution is stored in a tank (not shown) as a concentrated solution. Note that the compressor 6 is driven by a drive source 9 such as an electric motor, an internal combustion engine, or a steam turbine.
ところで、蒸発缶３で発生した蒸気は飽和蒸気
であり、コンプレツサ６に吸入される時には放熱
ロス、動圧による減圧により若干の湿り状態とな
つてしまい、コンプレツサ６が腐食してしまうの
で、スーパーヒートする為に調整弁１０を設けて
コンプレツサ６からの高温の吐出ガスをコンプレ
ツサ６の吸入側へバイパスして加熱している。 By the way, the steam generated in the evaporator 3 is saturated steam, and when it is sucked into the compressor 6, it becomes slightly moist due to heat radiation loss and decompression due to dynamic pressure, and the compressor 6 corrodes. In order to do this, a regulating valve 10 is provided to bypass and heat the high temperature discharged gas from the compressor 6 to the suction side of the compressor 6.
また、コンプレツサ６の吐出ガスは過熱蒸気と
なつてしまうので、そのまま熱交換器４へ供給す
ると、温度差が付き過ぎ、スケールがこびり付く
ので、減温の為にポンプ７の出口側から熱交換器
４の入口側へ蒸留液を導く配管１１を設けて、高
温高圧の吐出ガス中に蒸留液を噴射するようにし
ている。 In addition, the discharge gas from the compressor 6 becomes superheated steam, so if it is supplied directly to the heat exchanger 4, there will be too much temperature difference and scale will stick to it. A pipe 11 is provided to guide the distillate to the inlet side of the exchanger 4, so that the distillate is injected into the high-temperature, high-pressure discharge gas.
この運転状態を第５図のモリエル線図で説明す
ると、蒸発缶３での発生蒸気ａは調整弁１０を介
して供給されるコンプレツサ６の吐出ガスで加熱
されてｂとなり、コンプレツサ６に吸入され加圧
されてc′となる（断熱圧縮であればｃ点となる
が、実際にはロスがありc′となる）。次に、コン
プレツサ６の吐出ガスは蒸留液の噴射を受けて減
温されてｄ点となつて、熱交換器４に送られる。 To explain this operating state using the Mollier diagram shown in FIG. It is pressurized and becomes point c' (if it were adiabatic compression, it would be point c, but in reality there is a loss and it becomes point c'). Next, the discharged gas from the compressor 6 is injected with distillate and its temperature is reduced to a point d, where it is sent to the heat exchanger 4.
考案が解決しようとする問題点
従来の様に、吐出ガスを吸入側へバイパスする
ためには、コンプレツサ６の容量を大きくする必
要があり動力も増え、発生蒸気量の変化に対して
調整弁１０の開度を変化させる自動制御が必要と
なり、装置が複雑で高価となり、信頼性の低下を
招くという欠点があつた。また、吐出ガスをバイ
パスする代りに、加熱器を設けてスチームで吸入
ガスを加熱する従来の別な方法もあるが、この方
法は、スチームを消費し、ランニングコストの増
大をもたらし、スチームの流量を調整する必要が
あり、高価で信頼性の低下を招くという欠点があ
つた。そこで、本考案は、このような従来の問題
点を解消しようとしてなされたものである。Problems that the invention aims to solve: In order to bypass the discharged gas to the suction side as in the past, it is necessary to increase the capacity of the compressor 6, which also increases the power, and the adjustment valve 10 has to be adjusted in response to changes in the amount of steam generated. This requires automatic control to change the degree of opening of the valve, making the device complicated and expensive, and resulting in a decrease in reliability. In addition, there is another conventional method in which a heater is installed to heat the suction gas with steam instead of bypassing the discharge gas, but this method consumes steam, increases running costs, and increases the flow rate of the steam. The disadvantage is that it requires adjustment, which is expensive and reduces reliability. Therefore, the present invention has been made in an attempt to solve these conventional problems.
問題点を解決するための手段
本考案は、蒸気再圧縮式蒸発装置の蒸発缶（蒸
発機）とコンプレツサ（圧縮機）とを結ぶ流体経
路に、コンプレツサに吸入される飽和蒸気（吸入
流体）とコンプレツサから吐出される高温高圧蒸
気（吐出流体）とを熱交換させる熱交換器を設け
ることにより、従来の問題点を解決している。Means for Solving the Problems The present invention provides a method for connecting saturated vapor (suction fluid) to be sucked into the compressor into a fluid path connecting the evaporator and compressor of a vapor recompression type evaporator. The conventional problems are solved by providing a heat exchanger that exchanges heat with high-temperature, high-pressure steam (discharge fluid) discharged from the compressor.
実施例
以下本考案に係る蒸気再圧縮式蒸発装置の一実
施例について図面を参照して詳細に説明する。Embodiment Hereinafter, an embodiment of the vapor recompression type evaporator according to the present invention will be described in detail with reference to the drawings.
第１図は本考案装置の一実施例を示す系統図で
あり、第４図に示した従来の装置の調整弁１０が
削除され、その代りにガス−ガス熱交換器１２が
設けられており、その他の構成は従来の装置と同
様である。従つて、第１図において第４図と同一
部分には同一符号を附してあるのでその部分の説
明は省略する。 FIG. 1 is a system diagram showing one embodiment of the device of the present invention, in which the regulating valve 10 of the conventional device shown in FIG. 4 is deleted and a gas-gas heat exchanger 12 is provided in its place. , the other configurations are the same as the conventional device. Therefore, in FIG. 1, the same parts as those in FIG. 4 are given the same reference numerals, and the explanation of those parts will be omitted.
第１図において、ガス−ガス熱交換器１２は蒸
発缶３とコンプレツサ６を結ぶ経路に設けられて
いる。すなわち蒸発缶３には熱交換器４が備えら
れており、この熱交換器４によつて蒸発缶３へ導
入される予熱された濃縮原液が加熱されて蒸発
し、この蒸気はデミスタ５へ供給されて液滴が分
離される。そしてデミスタ５を経て液滴の分離さ
れた飽和蒸気がガス−ガス熱交換器１２へ供給さ
れ、このガス−ガス熱交換器１２を経てコンプレ
ツサ６へ吸入されて圧縮される。そして、コンプ
レツサ６から吐出される高温高圧蒸気はガス−ガ
ス熱交換器１２へ供給され、これを経て熱交換器
４へ導入される。 In FIG. 1, a gas-gas heat exchanger 12 is provided in a path connecting the evaporator 3 and the compressor 6. That is, the evaporator 3 is equipped with a heat exchanger 4, and the preheated concentrated stock solution introduced into the evaporator 3 is heated and evaporated by the heat exchanger 4, and this vapor is supplied to the demister 5. to separate the droplets. The saturated vapor from which the droplets have been separated is supplied to the gas-gas heat exchanger 12 via the demister 5, and is sucked into the compressor 6 via the gas-gas heat exchanger 12 and compressed. The high-temperature, high-pressure steam discharged from the compressor 6 is supplied to the gas-gas heat exchanger 12, and then introduced into the heat exchanger 4.
上記のガス−ガス熱交換器１２の具体例とし
て、第２図、第３図に示したものが使用できる。
すなわち、第２図に示したものは一般的なガス−
ガス熱交換器１２であり、外板２０で囲まれた内
部に伝熱管２１と端板２２とにより、２種類のガ
スが混合することなく熱交換を行なう２つの経路
が形成され、夫々に入口２３ａ，２３ｂ、出口２
４ａ，２４ｂが設けられている。従つて、デミス
タ５を経た蒸気は、入口２３ａから導入されて出
口２４ａへ排出され、その蒸気はコンプレツサ６
に吸入される。一方、コンプレツサ６から吐出さ
れた高温高圧蒸気は入口２３ｂから導入されて出
口２４ｂへ排出され、その高温高圧蒸気は熱交換
器４へ供給される。よつて、伝熱管２１を介して
飽和蒸気と高温高圧蒸気との熱交換が行なわれ
る。この伝熱管２１としては、平滑管、コルゲー
ト管、スパイラル管等種々のものが使用でき、ま
たププレート状のもの、蓄熱タイプのもの等もあ
る。 As a specific example of the above gas-gas heat exchanger 12, those shown in FIGS. 2 and 3 can be used.
In other words, what is shown in Figure 2 is a general gas
The gas heat exchanger 12 is surrounded by an outer plate 20 and has two paths formed by heat transfer tubes 21 and end plates 22 for heat exchange without mixing two types of gas, each with an inlet. 23a, 23b, exit 2
4a and 24b are provided. Therefore, the steam that has passed through the demister 5 is introduced from the inlet 23a and discharged to the outlet 24a, and the steam is passed through the compressor 6.
is inhaled. On the other hand, high-temperature, high-pressure steam discharged from the compressor 6 is introduced from the inlet 23b and discharged to the outlet 24b, and the high-temperature, high-pressure steam is supplied to the heat exchanger 4. Therefore, heat exchange between the saturated steam and the high-temperature, high-pressure steam is performed via the heat exchanger tube 21. Various types of heat exchanger tubes 21 can be used, such as smooth tubes, corrugated tubes, and spiral tubes, as well as plate-shaped tubes, heat storage type tubes, and the like.
また、第３図に示したものはヒートパイプを用
いたガス−ガス熱交換器１２であり、２系統のダ
クト２５ａ，２５ｂにヒートパイプ２６を介在さ
せたものである。従つて、一方のダクト２５ａの
入口２３ａから出口２４ａへ飽和蒸気が流れ、他
方のダクト２５ａの入口２３ｂから出口２４ｂへ
高温高圧蒸気が流れ、両蒸気はヒートパイプ２６
を介して熱交換が行なわれる。 Moreover, what is shown in FIG. 3 is a gas-gas heat exchanger 12 using heat pipes, in which a heat pipe 26 is interposed between two systems of ducts 25a and 25b. Therefore, saturated steam flows from the inlet 23a of one duct 25a to the outlet 24a, high-temperature, high-pressure steam flows from the inlet 23b of the other duct 25a to the outlet 24b, and both steams flow through the heat pipe 26.
Heat exchange takes place via.
作 用
上記のように構成された本考案の蒸気再圧縮式
蒸発装置において、デミスタ５を出た蒸気は、ガ
ス−ガス熱交換器１２にてコンプレツサ６の吐出
ガスからの伝熱を受けて過熱状態となつてコンプ
レツサ６に吸入される。そして、コンプレツサ６
で加圧されて過熱蒸気となり、この過熱蒸気はガ
ス−ガス熱交換器１２にてコンプレツサ６に吸入
されるべきデミスタ５を出た蒸気からの伝熱を受
けて、減温される。この減温された蒸気にはまだ
過熱温度が付き過ぎている場合の為に、ポンプ７
から送り出される蒸留液の一部を配管１１を介し
て噴射してさらに減温したうえで熱交換器４に送
られる。Function In the vapor recompression type evaporator of the present invention configured as described above, the vapor exiting the demister 5 is superheated by receiving heat transferred from the discharge gas of the compressor 6 in the gas-gas heat exchanger 12. state and is sucked into the compressor 6. And Compressa 6
The superheated steam is pressurized to become superheated steam, and this superheated steam receives heat transferred from the steam exiting the demister 5 to be sucked into the compressor 6 in the gas-gas heat exchanger 12, and its temperature is reduced. In case this cooled steam is still too hot, pump 7
A part of the distilled liquid sent from the tank is injected through the pipe 11 to further reduce the temperature, and then sent to the heat exchanger 4.
この運転状態を第５図のモリエル線図で示す
と、蒸発缶３で発生した蒸気ａはガス−ガス熱交
換器１２でコンプレツサ６からの吐出ガスによつ
て加熱されてｂとなり、更にコンプレツサ６で圧
縮されてc′となる。そして、コンプレツサ６の吐
出ガスはガス−ガス熱交換器１２で減温されて
d′となり、蒸留液の噴射でさらに冷却されてｄと
なる。 If this operating state is shown in the Mollier diagram of FIG. is compressed to become c′. The discharge gas from the compressor 6 is then cooled down in the gas-gas heat exchanger 12.
It becomes d' and is further cooled by injection of distillate to become d.
なお、コンプレツサ６の圧縮において過熱温度
の付きにくい有機物のテトラクロロエチレン、
R114等は、ガス−ガス熱交換器１２後の蒸留液
の噴射の必要がない場合が多いので、この場合に
は配管１１を省略するか或いは配管１１に弁を設
けてこの弁により蒸留液の通過を遮断すればよ
い。 Note that tetrachloroethylene, an organic material that is difficult to overheat during compression in the compressor 6,
For R114 etc., there is often no need to inject the distillate after the gas-gas heat exchanger 12, so in this case, the piping 11 can be omitted or a valve can be provided in the piping 11 and the distillate can be injected using this valve. Just block the passage.
考案の効果
以上詳述したように、本考案によれば、コンプ
レツサの吸入における加熱と吐出における冷却を
ガス−ガス熱交換器で互いに熱交換するようにし
たので、システムが簡単となり、余分なコンプレ
ツサ容量とコンプレツサ動力や余分なスチームの
消費を避けられるので、経済的になり、かつ信頼
性が向上する蒸気再圧縮式蒸発装置が提供され
る。Effects of the invention As detailed above, according to the invention, heating at the suction and cooling at the discharge of the compressor are exchanged with each other using a gas-gas heat exchanger, which simplifies the system and eliminates the need for an extra compressor. A vapor recompression evaporator is provided that is more economical and more reliable because capacity and compressor power and excess steam consumption are avoided.
そして、本考案によれば、コンプレツサから吐
出される吐出ガスの減温は、蒸発缶に供給される
原液ではなくて、コンプレツサへ入る流入流体を
予熱することで行われるので、原液の供給が連続
していないシステムであつても、吐出ガスの減温
を連続して行うことができる。 According to the present invention, the temperature of the discharged gas discharged from the compressor is lowered by preheating the inflow fluid entering the compressor rather than the undiluted solution supplied to the evaporator, so that the undiluted solution is continuously supplied. Even in systems that do not, the temperature of the discharged gas can be reduced continuously.
また、ガス−ガス熱交換器にヒートパイプを用
いれば、熱交換器通過の圧損が減り、熱交換性能
も良くコンパクトになる。 Furthermore, if a heat pipe is used in the gas-gas heat exchanger, the pressure loss passing through the heat exchanger will be reduced, and the heat exchange performance will be improved and the system will be more compact.
第１図は本考案に係る蒸気再圧縮式蒸発装置の
一実施例を示す系統図、第２図及び第３図は本考
案で使用されるガス−ガス熱交換器の具体例を説
明するために示した断面図、第４図は従来の蒸気
再圧縮式蒸発装置を示す系統図、第５図は本考案
装置の運転状態を説明するためのモリエル線図で
ある。
３……蒸発缶、４……熱交換器、６……コンプ
レツサ、１２……ガス−ガス熱交換器。
Figure 1 is a system diagram showing an embodiment of the vapor recompression type evaporator according to the present invention, and Figures 2 and 3 are for explaining a specific example of the gas-gas heat exchanger used in the present invention. 4 is a system diagram showing a conventional vapor recompression type evaporator, and FIG. 5 is a Mollier diagram for explaining the operating state of the device of the present invention. 3... Evaporator, 4... Heat exchanger, 6... Compressor, 12... Gas-gas heat exchanger.
Claims (1)
で発生した蒸気を圧縮機で圧縮して高温高圧蒸気
とし、この圧縮機からの高温高圧蒸気を前記蒸発
機の加熱源とする蒸気再圧縮式蒸発装置におい
て、前記圧縮機に吸入される吸入流体と前記圧縮
機から吐出される吐出流体とを熱交換させる熱交
換器を前記蒸発機と圧縮機とを結ぶ流体経路に介
在させた蒸気再圧縮式蒸発装置。 Vapor recompression, in which the raw solution is heated and evaporated in an evaporator, the vapor generated by the evaporator is compressed into high-temperature, high-pressure steam, and the high-temperature, high-pressure steam from the compressor is used as the heating source for the evaporator. In the type evaporator, a heat exchanger for exchanging heat between suction fluid drawn into the compressor and discharge fluid discharged from the compressor is interposed in a fluid path connecting the evaporator and the compressor. Compression evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1984137825U JPH022401Y2 (en) | 1984-09-13 | 1984-09-13 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1984137825U JPH022401Y2 (en) | 1984-09-13 | 1984-09-13 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6155901U JPS6155901U (en) | 1986-04-15 |
| JPH022401Y2 true JPH022401Y2 (en) | 1990-01-22 |
Family
ID=30696230
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1984137825U Expired JPH022401Y2 (en) | 1984-09-13 | 1984-09-13 |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH022401Y2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5481808B2 (en) * | 2008-07-31 | 2014-04-23 | 千代田化工建設株式会社 | Method for operating separation process module, method for operating integrated separation process module, method for operating large scale integrated separation process module |
| JP5756900B2 (en) * | 2012-02-01 | 2015-07-29 | 国立大学法人 東京大学 | Distillation equipment |
-
1984
- 1984-09-13 JP JP1984137825U patent/JPH022401Y2/ja not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6155901U (en) | 1986-04-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4932204A (en) | Efficiency combined cycle power plant | |
| CN1061643A (en) | The circulation of combined steamed gas turbine circuit reheated steam | |
| US4542628A (en) | Coupled dual loop absorption heat pump | |
| US4333515A (en) | Process and system for boosting the temperature of sensible waste heat sources | |
| US5369950A (en) | Method for operating a gas and steam turbine system, and gas and stream turbine system operating by the method | |
| US5727397A (en) | Triple effect absorption refrigeration system | |
| US4291545A (en) | Absorption heat pump | |
| JPH0621732B2 (en) | Heating device | |
| US4474025A (en) | Heat pump | |
| JP2782555B2 (en) | Absorption heat pump | |
| JPH022401Y2 (en) | ||
| RU2153080C2 (en) | Combined-cycle power generation process and combined-cycle plant | |
| CN207957817U (en) | A kind of combination system of MGGH systems and low-temperature multi-effect evaporator | |
| JPH0933004A (en) | Waste heat recovery boiler | |
| CN108507219A (en) | A kind of compound two-stage type lithium bromide absorption type heat pump and working method | |
| JPS60168582A (en) | Steam compression type water distillation apparatus | |
| JPS63210579A (en) | Cold and hot water production facility | |
| JPS6117320Y2 (en) | ||
| JPS6311571Y2 (en) | ||
| JPS621796U (en) | ||
| JPS6016802Y2 (en) | Two-stage pressure type exhaust gas economizer | |
| JPS6136662A (en) | Absorption type heat pump device | |
| JPS6051622B2 (en) | Effective energy utilization method in heat supply equipment consisting of a combination of heat pump cycle and cogeneration steam cycle | |
| JPH027412Y2 (en) | ||
| JPS62793A (en) | Combination heater |