JPH0627485B2 - Evaporator for heat recovery equipment - Google Patents
Evaporator for heat recovery equipmentInfo
- Publication number
- JPH0627485B2 JPH0627485B2 JP59200878A JP20087884A JPH0627485B2 JP H0627485 B2 JPH0627485 B2 JP H0627485B2 JP 59200878 A JP59200878 A JP 59200878A JP 20087884 A JP20087884 A JP 20087884A JP H0627485 B2 JPH0627485 B2 JP H0627485B2
- Authority
- JP
- Japan
- Prior art keywords
- evaporator
- working medium
- liquid
- azeotropic mixture
- 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 - Lifetime
Links
- 238000011084 recovery Methods 0.000 title claims description 8
- 239000007788 liquid Substances 0.000 claims description 48
- 239000000203 mixture Substances 0.000 claims description 48
- 238000001704 evaporation Methods 0.000 claims description 35
- 230000008020 evaporation Effects 0.000 claims description 35
- 239000012530 fluid Substances 0.000 claims description 27
- 238000010992 reflux Methods 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 11
- 239000012071 phase Substances 0.000 claims description 8
- 238000010586 diagram Methods 0.000 description 6
- 239000012808 vapor phase Substances 0.000 description 6
- 238000009835 boiling Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000012047 saturated solution Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/06—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Description
【発明の詳細な説明】 産業上の利用分野 この発明は非共沸混合物を作動媒体とする熱回収装置用
の蒸発装置に関する。Description: TECHNICAL FIELD The present invention relates to an evaporator for a heat recovery device using a non-azeotropic mixture as a working medium.
従来の技術 特開昭５７−２８８１９号公報には、熱交換を行う各外
部流体（熱源流体および冷却水）の温度の推移に従って
漸次蒸発し、凝縮するような流体混合物を作動媒体とし
て使用するランキンサイクルにより、熱から機械的エネ
ルギーを生成する方法が記載されている。2. Description of the Related Art Japanese Unexamined Patent Publication (Kokai) No. 57-28819 discloses a Rankine that uses as a working medium a fluid mixture that gradually evaporates and condenses in accordance with the temperature change of each external fluid (heat source fluid and cooling water) for heat exchange. A method of producing mechanical energy from heat by cycling is described.
第３図に示すように、液相の作動媒体は蒸発器(21)で熱
源流体から熱を取り込むことによってその一部が蒸発す
る。液体部分と蒸気部分は分離タンク(20)で分離され
る。蒸気部分はタービン(22)で膨張して仕事をし、ター
ビン(22)と直結している発電機(25)が駆動される。一
方、液相は分離タンク(20)から熱交換器(28)へ送られ、
蒸発器(21)へ送られる凝縮液と熱交換した後、膨張弁(2
9)を通過して膨張し、凝縮器(23)の上流側で、タービン
(22)から出てくる膨張蒸気相と混合する。このようにし
て得られる液−蒸気混合物は凝縮器(23)で冷却用外部流
体に熱を与えて凝縮し、貯蔵槽(26)に集められ、ポンプ
(24)によって蒸発器(21)に再循環せしめられる。As shown in FIG. 3, a part of the liquid-phase working medium is evaporated by taking in heat from the heat source fluid in the evaporator (21). The liquid portion and the vapor portion are separated in the separation tank (20). The steam part expands and does work in the turbine (22), and the generator (25) directly connected to the turbine (22) is driven. On the other hand, the liquid phase is sent from the separation tank (20) to the heat exchanger (28),
After exchanging heat with the condensate sent to the evaporator (21), the expansion valve (2
9) through which it expands and the turbine upstream of the condenser (23)
Mix with the expanded vapor phase emerging from (22). The liquid-vapor mixture thus obtained is condensed in the condenser (23) by applying heat to the external cooling fluid, collected in the storage tank (26), and pumped.
It is recirculated to the evaporator (21) by (24).
このような熱サイクルでは、得られる効率が最大である
ためには、蒸発器に関していえば、作動媒体の蒸発温度
範囲（蒸発開始温度と蒸発終了温度との差）が熱源流体
の温度範囲（蒸発器入口での熱源流体の温度と蒸発器出
口での熱源流体の温度との差）にできる限り近接してい
なければならないことが知られている。そして、第３図
の従来装置では、このような条件に合致するように混合
物の種類や組成を選定する。すなわち、熱がサイクルに
供給されるべき温度範囲が決定すれば、蒸発温度範囲が
温度範囲に近く得られるように、混合物の組成を選定す
る。二成分混合物の場合、蒸発温度範囲は普通第４図の
グラフに示す如く推移する。ある一定の圧力において(T
I)および(TII)なる蒸発温度を有する成分（Ｉ）及び（I
I）の形成する混合物の揮発性の高いほうの成分（Ｉ）
の与えられたモル分率(xI)において、混合物の蒸発は、
液体の起泡温度(TLB)において始まり、蒸気の露点温度
(TVR)において完了する。従って、蒸発温度範囲はこれ
らの温度の差(TVR-TLB)に等しく、適切な組成を選定す
ることによって調節することができる。In such a heat cycle, in order to obtain the maximum efficiency, the evaporation temperature range of the working medium (difference between the evaporation start temperature and the evaporation end temperature) is the temperature range of the heat source fluid (evaporation). It is known that it must be as close as possible to the difference between the temperature of the heat source fluid at the inlet and the temperature of the heat source fluid at the evaporator outlet. Then, in the conventional apparatus of FIG. 3, the kind and composition of the mixture are selected so as to meet such conditions. That is, the composition of the mixture is selected such that the evaporation temperature range is obtained close to the temperature range once the temperature range in which heat should be supplied to the cycle is determined. In the case of a binary mixture, the evaporation temperature range usually changes as shown in the graph of FIG. At a certain pressure (T
Components (I) and (I) having evaporation temperatures of (I) and (TII)
The more volatile component (I) of the mixture formed by I)
At a given mole fraction (xI) of
Dew point temperature of the vapor, starting at the foaming temperature ( TLB ) of the liquid
Completed at (T VR ). Therefore, the evaporation temperature range is equal to the difference between these temperatures (T VR -T LB ) and can be adjusted by choosing an appropriate composition.
発明が解決しようとする課題 しかしながら、初期設定において適切な組成の混合物を
選択したとしても、外部流体即ち熱源流体及び冷却水の
温度が変動すると上記従来装置ではこれに即座に対応す
ることができない。精々、たとえば季節の変わり目に、
装置の稼働を停止して、貯蔵槽(26)内の混合物を異なる
組成のものと全部入れ替えるという操作ができる程度で
ある。However, even if a mixture having an appropriate composition is selected in the initial setting, if the temperature of the external fluid, that is, the heat source fluid and the cooling water fluctuates, the conventional device cannot immediately cope with this. At best, for example at the turn of the season,
It is only possible to stop the operation of the apparatus and replace all the mixture in the storage tank (26) with one having a different composition.
そこで、この発明の目的は、熱源流体の温度が変動して
も、非共沸混合物の蒸発温度範囲が熱源流体の温度範囲
にできる限り近接した状態を確実に維持して、熱交換効
率を高めることにある。Therefore, an object of the present invention is to reliably maintain a state in which the evaporation temperature range of the non-azeotropic mixture is as close as possible to the temperature range of the heat source fluid even if the temperature of the heat source fluid fluctuates, thereby enhancing heat exchange efficiency. Especially.
課題を解決するための手段 この発明の蒸発装置は、蒸発器、蒸気機関、凝縮器及び
ポンプから構成される系内で作動媒体を循環させ蒸気機
関で負荷を駆動するようにした、非共沸混合物を作動媒
体とする熱回収装置用の蒸発装置であって、非共沸混合
物入口をポンプの吐出側に接続し、蒸発すべき非共沸混
合物と熱源たる流体とが完全対向流にて流通する蒸発器
と、蒸発器の非共沸混合物出口に接続するとともに気相
出口を蒸気機関に接続した気液分離器と、気液分離器の
液相出口から蒸発器の非共沸混合物入口に通ずる還流管
と、還流管の途中に設けた可変絞りとからなり、前記可
変絞りで還流液量を調節することによって、蒸発器内に
おける非共沸混合物の濃度を調整し、作動媒体の蒸発温
度範囲を熱源流体の温度範囲にできる限り近接させるよ
うにしたことを特徴とする。Means for Solving the Problems The evaporation device of the present invention is a non-azeotropic apparatus in which a working medium is circulated in a system composed of an evaporator, a steam engine, a condenser and a pump to drive a load by the steam engine. An evaporator for a heat recovery device using a mixture as a working medium, in which the inlet of the non-azeotropic mixture is connected to the discharge side of the pump, and the non-azeotropic mixture to be vaporized and the fluid serving as the heat source flow in a completely opposed flow. A vapor-liquid separator that is connected to the non-azeotropic mixture outlet of the evaporator and the vapor-phase outlet of which is connected to the steam engine, and from the liquid-phase outlet of the vapor-liquid separator to the non-azeotropic mixture inlet of the evaporator. It consists of a circulating reflux pipe and a variable throttle provided in the middle of the reflux pipe. By adjusting the amount of reflux liquid with the variable throttle, the concentration of the non-azeotropic mixture in the evaporator is adjusted, and the evaporation temperature of the working medium is adjusted. Range as close as possible to the temperature range of the heat source fluid The feature is that it is made to do.
作用 非共沸混合物の蒸発温度範囲は蒸発開始温度と蒸発終了
温度の差であって、非共沸混合物を構成する成分の種類
と、非共沸混合物の濃度によって最大値が決定される。
すなわち、どのような種類の成分を混合するかによって
気液平衡線図の気相線と液相線の開きが決まり、同じ種
類の成分からなる混合物であっても、濃度によって蒸発
温度範囲が変わる。ある与えられた濃度のもとでは、蒸
発開始温度及び終了温度がそれぞれ液の沸点温度及び蒸
気の露点温度と一致するとき蒸発温度範囲は最大とな
る。Action The evaporation temperature range of the non-azeotropic mixture is the difference between the evaporation start temperature and the evaporation end temperature, and the maximum value is determined by the types of components that make up the non-azeotropic mixture and the concentration of the non-azeotropic mixture.
That is, the difference between the vapor phase and liquid phase lines of the vapor-liquid equilibrium diagram is determined by what kind of components are mixed, and even if the mixture is composed of the same type of components, the evaporation temperature range changes depending on the concentration. . At a given concentration, the evaporation temperature range is maximized when the evaporation start temperature and the end temperature coincide with the liquid boiling temperature and the vapor dew point temperature, respectively.
上記最大値を限度として、蒸発温度範囲を左右するのは
蒸発開始温度である。可変絞りによる還流液量の調節
は、蒸発器入口における非共沸混合物の濃度を変化させ
るものであり、これにより蒸発開始温度を変化させ、結
果として蒸発温度範囲を調節する。It is the evaporation start temperature that affects the evaporation temperature range within the maximum value. The adjustment of the reflux liquid amount by the variable throttle changes the concentration of the non-azeotropic mixture at the evaporator inlet, which changes the evaporation start temperature and consequently the evaporation temperature range.
第４図に従って説明すると、還流液量を少なくすれば等
濃度線が右側へ、つまり、濃度が高くなる方へ移動して
蒸発開始温度が低くなり、その結果、蒸発温度範囲が大
きくなる。逆に、還流液量を多くすれば等濃度線が左側
へ、つまり、濃度が低くなる方へ移動して蒸発開始温度
が高くなり、その結果、蒸発温度範囲が小さくなる。Explaining with reference to FIG. 4, if the amount of the reflux liquid is reduced, the isoconcentration line moves to the right, that is, toward the higher concentration, and the evaporation start temperature decreases, and as a result, the evaporation temperature range increases. On the contrary, if the amount of reflux liquid is increased, the isoconcentration line moves to the left, that is, to the direction where the concentration decreases, and the evaporation start temperature increases, and as a result, the evaporation temperature range decreases.
実施例 第１図にこの発明の実施例を示す。同図には、第３図の
従来装置と同様にタービンで発電機を駆動する場合が例
示されているが、タービンに代えて、スクリューエキス
パンダーのようなこの分野で知られているその他の蒸気
機関を採用することもできる。なお、この場合の熱回収
装置の作動媒体は非共沸混合物である。ここに非共沸混
合物とは、いわゆる共沸混合物以外の、２成分系もしく
は多成分系の混合物をいうものとする。Embodiment FIG. 1 shows an embodiment of the present invention. The same drawing illustrates the case where the generator is driven by the turbine as in the conventional device of FIG. 3, but instead of the turbine, other steam engines such as a screw expander known in this field are used. Can also be adopted. The working medium of the heat recovery device in this case is a non-azeotropic mixture. Here, the non-azeotropic mixture means a binary or multi-component mixture other than the so-called azeotropic mixture.
第２図は、一定圧力のもとにおける成分Ａおよび成分Ｂ
の単独の飽和温度をそれぞれＴAおよびＴBとするとき、
ＡとＢとからなる非共沸混合物の濃度と温度との関係を
示す。なお、第２図において、濃度は、ＡとＢの重量を
それぞれＧAおよびＧBとするとき、この非共沸混合物の
単位重量当たりに含まれるＢの重量ξをいうものとす
る。すなわち、ξ＝ＧB／（ＧA＋ＧB）。もちろん第４
図のようにモル分率で濃度を表すこともできる。FIG. 2 shows component A and component B under constant pressure.
When the independent saturation temperatures of T A and T B are
The relation between the concentration of the non-azeotropic mixture of A and B and the temperature is shown. In FIG. 2, the concentration means the weight ξ of B contained per unit weight of the non-azeotropic mixture, where the weights of A and B are G A and G B , respectively. That, ξ = G B / (G A + G B). Of course the fourth
As shown in the figure, the concentration can be expressed by the mole fraction.
もし温度Ｔのもとで液相と気相とが平衡状態にあるとき
は液相線および気相線上の温度Ｔに相当する点の位置か
ら、液相の濃度はξであり、気相の濃度はξｇであ
る。さらに、液相と気相の合成の濃度をξとすれば、こ
の混合物の状態は点Ｍで表され、そのときの溶液の重量
と蒸気の重量との割合は、点Ｍから液相線および気相線
に至る水平距離ａおよびｂに逆比例する。If the liquid phase and the gas phase are in equilibrium under the temperature T, the concentration of the liquid phase is ξ from the position of the liquid phase line and the point corresponding to the temperature T on the gas phase line. The concentration is ξg. Furthermore, if the concentration of the synthesis of the liquid phase and the gas phase is ξ, the state of this mixture is represented by the point M, and the ratio of the weight of the solution to the weight of the vapor at that time is calculated from the point M to the liquidus line and It is inversely proportional to the horizontal distances a and b to the vapor line.
つぎに、点Ｍが液相線と気相線とで囲まれる領域内に存
在するときは、混合物は気液両相に分かれるが、点Ｍが
それらの両線と一致するときまたはその領域外に出ると
きは、気、液のどちらか１つの相のみとなる。例えば、
点Ｍ1は不飽和な液体を示すし、また点Ｍ2は過熱蒸気を
表す。しかし、温度が変わると混合物の状態も変化す
る。例えば、点Ｍ1で示される不飽和の液体の温度をＴ2
まで上げると飽和溶液となり、それ以上に温度を上げる
と蒸発を始める。要するに、濃度ξの溶液を定圧のも
とで加熱していくと、点ｃで沸騰（蒸発）が始まり、そ
のとき平衡にある気相（蒸気）の組成と状態は点ｃ′で
示される。さらに加熱して温度Ｔ1になると、点ｈで示
される状態の気相と点ｊで示される状態の溶液がji:ih
の割合で共存する。加熱をさらに続けて温度Ｔ2になる
と点ｄの状態の気相のみになり、それから後も加熱を行
えば単に蒸気を過熱することになる。Next, when the point M exists in the area surrounded by the liquidus line and the vapor phase line, the mixture is divided into both gas-liquid phases, but when the point M coincides with those lines or outside the area. When exiting, there is only one phase, either gas or liquid. For example,
Point M 1 represents unsaturated liquid and point M 2 represents superheated vapor. However, as the temperature changes, so does the state of the mixture. For example, let T 2 be the temperature of the unsaturated liquid indicated by point M 1.
When it is raised to a saturated solution, it becomes a saturated solution. In short, when a solution of concentration ξ is heated under constant pressure, boiling (evaporation) starts at point c, and the composition and state of the gas phase (vapor) in equilibrium at that time are shown by point c ′. When further heated to the temperature T 1 , the gas phase in the state indicated by the point h and the solution in the state indicated by the point j are ji: ih
Coexist at a rate of. When the heating is further continued to reach the temperature T 2 , only the vapor phase in the state of the point d becomes, and if the heating is continued after that, the steam is simply overheated.
ここで、第１図を参照すると、蒸発器(11)は作動媒体の
通路(12)と、工場温排水のような熱源たる流体の通路(1
3)とを有し、作動媒体と熱源流体とは完全対向流の関係
にある。蒸発器(11)の作動媒体入口(14)へはポンプ(24)
により凝縮器(23)からの作動媒体液が供給される。蒸発
器(11)の作動媒体出口(15)には気液分離器(16)を設けて
ある。気液分離器(16)の気相出口はタービン(22)に接続
している。気液分離器(16)の液相出口は、可変絞り(17)
を取り付けた還流管(18)を通じて蒸発器(11)の作動媒体
入口(14)と連絡している。Referring to FIG. 1, the evaporator (11) includes a working medium passage (12) and a fluid passage (1) which is a heat source such as factory hot waste water.
3) and the working medium and the heat source fluid are in a completely countercurrent relationship. Pump (24) to working medium inlet (14) of evaporator (11)
As a result, the working medium liquid from the condenser (23) is supplied. A gas-liquid separator (16) is provided at the working medium outlet (15) of the evaporator (11). The gas phase outlet of the gas-liquid separator (16) is connected to the turbine (22). The liquid phase outlet of the gas-liquid separator (16) has a variable throttle (17).
It communicates with the working medium inlet (14) of the evaporator (11) through a reflux pipe (18) attached to the evaporator.
しかして蒸発器(11)内で発生した作動媒体蒸気は、気液
分離器(16)を経てタービン(22)へ進む。気液分離器(16)
で作動媒体蒸気から分離した作動媒体液は還流管(18)を
通って、凝縮器(23)からの作動媒体液と共に、蒸発器(1
1)へ還流する。Then, the working medium vapor generated in the evaporator (11) proceeds to the turbine (22) via the gas-liquid separator (16). Gas-Liquid Separator (16)
The working-medium liquid separated from the working-medium vapor in (1) passes through the reflux pipe (18), and together with the working-medium liquid from the condenser (23), the evaporator (1
Return to 1).
作動媒体の濃度をξとすると、作動媒体液が蒸発器(1
1)に入ると、まず温度Ｔにて点ｃ′で示される状態の初
蒸気が発生する。作動媒体液が蒸発器(11)内で加熱され
て温度Ｔ2に至るまでに点ｃ′から点ｄまでの気相線上
の各点で示される状態の作動媒体の蒸気が発生する。結
局、蒸発器(11)の作動媒体出口(15)から気液分離器(16)
へ向かうのは、点ｃ′で示される初蒸気から点ｄで示さ
れる最終蒸気までの種々状態（温度、濃度）の蒸気と、
点ｄ′で示される溶液とである。しかしてこれらは気液
分離器(16)で分離されて、作動媒体蒸気はタービン(22)
へ、作動媒体液は還流管(18)へ進む。If the concentration of the working medium is ξ, the working medium liquid is
When entering 1), first, at the temperature T, the initial steam in the state indicated by the point c'is generated. The working medium liquid is heated in the evaporator (11), and vapor of the working medium in the state indicated by each point on the vapor phase line from the point c ′ to the point d is generated before reaching the temperature T 2 . After all, from the working medium outlet (15) of the evaporator (11) to the gas-liquid separator (16)
There are various states (temperature, concentration) of steam from the initial steam shown by the point c ′ to the final steam shown by the point d,
And the solution indicated by the point d ′. Then, these are separated by the gas-liquid separator (16), and the working medium vapor is turbine (22).
To the reflux pipe (18).
還流管(18)は蒸発器(11)の作動媒体入口(14)へ通じてお
り、タービン(22)から排出され、凝縮器(23)にて凝縮し
た作動媒体液と共に蒸発器(11)へ、気液分離器(16)から
の作動媒体液を還流せしめる。しかしながら、上に述べ
たとおり、気液分離器(16)からタービン(22)へ進む作動
媒体蒸気は初蒸気ほか最適濃度ξより高濃度の蒸気を
含むため全体的に濃度が最適濃度ξよりも高くなって
いる。したがって、当然ながら、凝縮器(23)から蒸発器
(11)へと循環する作動媒体の濃度も最適濃度よりも高
い。一方、気液分離器(16)へ入る作動媒体液の濃度は最
適濃度ξよりも低い。そこで、可変絞り(17)により、
気液分離器(16)から還流管(18)を通って還流する作動媒
体液の量を調節し、凝縮器(23)からの分と合流してちょ
うど最適濃度となって蒸発器(11)へ入るようにする。The reflux pipe (18) communicates with the working medium inlet (14) of the evaporator (11) and is discharged from the turbine (22) to the evaporator (11) together with the working medium liquid condensed in the condenser (23). The working medium liquid from the gas-liquid separator (16) is refluxed. However, as described above, the working medium vapor that advances from the gas-liquid separator (16) to the turbine (22) contains initial vapor and other vapors having a higher concentration than the optimal concentration ξ, so that the overall concentration is higher than the optimal concentration ξ. It's getting higher. Therefore, of course, from the condenser (23) to the evaporator
The concentration of working medium circulating to (11) is also higher than the optimum concentration. On the other hand, the concentration of the working medium liquid entering the gas-liquid separator (16) is lower than the optimum concentration ξ. Then, by the variable diaphragm (17),
The amount of working medium liquid that flows back from the gas-liquid separator (16) through the reflux pipe (18) is adjusted, and it joins with the amount from the condenser (23) to reach the optimum concentration, and the evaporator (11) To enter.
また、熱源流体の温度が変動してその温度範囲が変化し
た場合、作動媒体の蒸発温度範囲が熱源流体の温度範囲
にできる限り近接するように、可変絞り(17)の開度を調
節して還流液量を調節することによって作動媒体の濃度
を調節する。たとえば、第４図の気液平衡線図で表され
る作動媒体の場合、熱源流体の温度範囲に近接した蒸発
温度範囲がΔＴであるとき、初期設定において濃度xIを
選定しておくことにより、通常は濃度をxI′に保ち、熱
源流体の温度範囲が変動したときは、それに対応して濃
度を変化させることにより、作動媒体の蒸発温度範囲が
熱源流体の温度範囲にできる限り近接した状態を維持す
ることができる。When the temperature of the heat source fluid fluctuates and its temperature range changes, the opening of the variable throttle (17) is adjusted so that the evaporation temperature range of the working medium is as close as possible to the temperature range of the heat source fluid. The concentration of the working medium is adjusted by adjusting the amount of reflux liquid. For example, in the case of the working medium represented by the vapor-liquid equilibrium diagram of FIG. 4, when the evaporation temperature range close to the temperature range of the heat source fluid is ΔT, by selecting the concentration xI in the initial setting, Normally, keep the concentration at xI ', and when the temperature range of the heat source fluid fluctuates, change the concentration accordingly to keep the evaporation temperature range of the working medium as close as possible to the temperature range of the heat source fluid. Can be maintained.
かかる濃度調整は、通常のプロセス制御技術を応用して
可変絞り(17)を制御することにより容易に達成すること
ができる。たとえば、可変絞りの開度調整は、熱源流体
の温度範囲と作動媒体の蒸発温度範囲を一致させるとい
う手法で行なうことができる。計測項目は熱源流体の蒸
発器出・入口の温度、作動媒体の蒸発器出・入口温度、
作動媒体の蒸発器入口圧力、可変絞り通過液混合後の作
動媒体の蒸発器入口における比重である。蒸発器入口に
おける作動媒体の比重は質量流量計によって連続的に計
測可能である。これらのデータを電気信号（たとえば、
４〜20mAのアナログ信号）として演算機能を持つコント
ローラ（プログラマブルコントローラその他のコンピュ
ータ等）に取り込み、蒸発器入口における作動媒体の比
重と温度から濃度を算出し、濃度と圧力から沸点を計算
する。作動媒体の蒸発器出口温度と沸点の温度差が熱源
流体の蒸発器出・入口温度差と等しくなるように可変絞
りの開度を調節する。なお、蒸発温度範囲と可変絞りの
開度との関係は、（１／蒸発温度範囲）∝可変絞り開度
で表される。Such density adjustment can be easily achieved by applying a normal process control technique to control the variable aperture (17). For example, the adjustment of the opening degree of the variable throttle can be performed by a method of matching the temperature range of the heat source fluid with the evaporation temperature range of the working medium. Measured items are the temperature of the evaporator outlet and inlet of the heat source fluid, the evaporator outlet and inlet temperature of the working medium,
It is the evaporator inlet pressure of the working medium, and the specific gravity at the evaporator inlet of the working medium after mixing the liquid passing through the variable throttle. The specific gravity of the working medium at the evaporator inlet can be continuously measured by a mass flow meter. These data are converted into electrical signals (for example,
The analog signal of 4 to 20 mA) is taken into a controller (programmable controller or other computer) having a calculation function, the concentration is calculated from the specific gravity and temperature of the working medium at the evaporator inlet, and the boiling point is calculated from the concentration and pressure. The opening of the variable throttle is adjusted so that the temperature difference between the evaporator outlet temperature and the boiling point of the working medium becomes equal to the evaporator outlet and inlet temperature difference of the heat source fluid. The relationship between the evaporation temperature range and the opening of the variable throttle is represented by (1 / evaporation temperature range) ∝variable throttle opening.
発明の効果 この発明は、気液分離器からの還流液の量を調節するこ
とにより蒸発器内の非共沸混合物の濃度を調整するよう
にしたから、熱源流体の温度が変化しても、装置の稼働
を停止することなく、非共沸混合物の蒸発温度範囲が熱
源流体の温度範囲にできる限り近接した状態を確実に維
持することができる。Effect of the Invention Since the present invention adjusts the concentration of the non-azeotropic mixture in the evaporator by adjusting the amount of reflux liquid from the gas-liquid separator, even if the temperature of the heat source fluid changes, It is possible to reliably maintain the state in which the evaporation temperature range of the non-azeotropic mixture is as close as possible to the temperature range of the heat source fluid without stopping the operation of the apparatus.
また、この発明の蒸発装置を発電用の熱回収装置におい
て使用する場合、気液分離器からの液を蒸発器の入口に
還流させることにより、ポンプはタービンから排出され
た蒸気の凝縮液だけを蒸発器に戻してやればよいので、
ポンプ動力が少なくて済む。これに対し、第３図の従来
装置のように分離タンクの液を凝縮器の上流側に導く
と、系内を循環する作動媒体の全部をポンプで送らなけ
ればならないため、ポンプの所要動力が多くなる。発電
出力のうち実際に利用できるのはポンプ動力分を差し引
いた残りであることを考慮すると、ポンプ動力の低減に
よる効果は大きい。When the evaporation device of the present invention is used in a heat recovery device for power generation, by circulating the liquid from the gas-liquid separator to the inlet of the evaporator, the pump only collects the condensed liquid of the steam discharged from the turbine. You can just put it back in the evaporator,
It requires less pump power. On the other hand, when the liquid in the separation tank is guided to the upstream side of the condenser as in the conventional device shown in FIG. 3, all of the working medium circulating in the system must be sent by the pump, so that the required power of the pump is reduced. Will increase. Considering that the power output that can actually be used is the remainder after subtracting the pump power, the effect of reducing the pump power is great.
第１図はこの発明の実施例を示すブロック図、第２図は
非共沸混合物の気液平衡線図、第３図は従来の技術を説
明するための熱回収装置のブロック図、第４図はこの発
明の作用を説明するための気液平衡線図である。 １１……蒸発器 １４……作動媒体入口 １５……作動媒体出口 １６……気液分離器 １７……可変絞り １８……還流管FIG. 1 is a block diagram showing an embodiment of the present invention, FIG. 2 is a vapor-liquid equilibrium diagram of a non-azeotropic mixture, FIG. 3 is a block diagram of a heat recovery device for explaining a conventional technique, and FIG. The figure is a vapor-liquid equilibrium diagram for explaining the operation of the present invention. 11 ... Evaporator 14 ... Working medium inlet 15 ... Working medium outlet 16 ... Gas-liquid separator 17 ... Variable throttle 18 ... Reflux pipe
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭58−96110（ＪＰ，Ａ) 特開 昭58−27806（ＪＰ，Ａ) 特開 昭57−28819（ＪＰ，Ａ) ─────────────────────────────────────────────────── ─── Continuation of the front page (56) Reference JP-A-58-96110 (JP, A) JP-A-58-27806 (JP, A) JP-A-57-28819 (JP, A)
Claims (1)
構成される系内で作動媒体を循環させ蒸気機関で負荷を
駆動するようにした、非共沸混合物を作動媒体とする熱
回収装置用の蒸発装置であって、非共沸混合物入口をポ
ンプの吐出口側に接続し、蒸発すべき非共沸混合物と熱
源たる流体とが完全対向流にて流通する蒸発器と、蒸発
器の非共沸混合物出口に接続するとともに気相出口を蒸
気機関に接続した気液分離器と、気液分離器の液相出口
から蒸発器の非共沸混合物入口に通ずる還流管と、還流
管の途中に設けた可変絞りとからなり、前記可変絞りで
還流液量を調節することによって、蒸発器内における非
共沸混合物の濃度を調整し、非共沸混合物の蒸発温度範
囲を熱源流体の温度範囲にできる限り近接させるように
したことを特徴とする非共沸混合物を作動媒体とする熱
回収装置用の蒸発装置。1. A heat recovery device using a non-azeotropic mixture as a working medium, wherein a working medium is circulated in a system composed of an evaporator, a steam engine, a condenser and a pump, and a load is driven by the steam engine. A non-azeotropic mixture inlet, which is connected to the discharge side of the pump, and in which the non-azeotropic mixture to be vaporized and the fluid serving as the heat source flow in a complete counterflow; A gas-liquid separator connected to the non-azeotropic mixture outlet and a gas-phase outlet connected to a steam engine, a reflux pipe leading from the liquid-phase outlet of the gas-liquid separator to the non-azeotropic mixture inlet of the evaporator, and a reflux pipe It consists of a variable throttle provided on the way, and by adjusting the amount of reflux liquid by the variable throttle, the concentration of the non-azeotropic mixture in the evaporator is adjusted, and the evaporation temperature range of the non-azeotropic mixture is set to the temperature of the heat source fluid. It is characterized by making it as close as possible to the range That non-azeotropic mixture evaporator for heat recovery apparatus according to the working medium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59200878A JPH0627485B2 (en) | 1984-09-26 | 1984-09-26 | Evaporator for heat recovery equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59200878A JPH0627485B2 (en) | 1984-09-26 | 1984-09-26 | Evaporator for heat recovery equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6179810A JPS6179810A (en) | 1986-04-23 |
| JPH0627485B2 true JPH0627485B2 (en) | 1994-04-13 |
Family
ID=16431739
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59200878A Expired - Lifetime JPH0627485B2 (en) | 1984-09-26 | 1984-09-26 | Evaporator for heat recovery equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0627485B2 (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5827806A (en) * | 1981-08-10 | 1983-02-18 | Hitachi Ltd | two-fluid power generator |
| JPS5938407B2 (en) * | 1981-12-04 | 1984-09-17 | 千代田化工建設株式会社 | Operation method for power recovery from LNG |
-
1984
- 1984-09-26 JP JP59200878A patent/JPH0627485B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6179810A (en) | 1986-04-23 |
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| Date | Code | Title | Description |
|---|---|---|---|
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| EXPY | Cancellation because of completion of term |