JPH0231207B2 - - Google Patents
Info
- Publication number
- JPH0231207B2 JPH0231207B2 JP57120470A JP12047082A JPH0231207B2 JP H0231207 B2 JPH0231207 B2 JP H0231207B2 JP 57120470 A JP57120470 A JP 57120470A JP 12047082 A JP12047082 A JP 12047082A JP H0231207 B2 JPH0231207 B2 JP H0231207B2
- Authority
- JP
- Japan
- Prior art keywords
- heat medium
- evaporator
- steam
- turbine
- medium
- 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
- 238000010248 power generation Methods 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 7
- 230000005611 electricity Effects 0.000 claims description 5
- 239000010696 ester oil Substances 0.000 claims description 4
- 229920005862 polyol Polymers 0.000 claims description 3
- 150000003077 polyols Chemical class 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims 2
- 235000011187 glycerol Nutrition 0.000 claims 1
- 229920006395 saturated elastomer Polymers 0.000 description 10
- 238000010586 diagram Methods 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 2
- 239000000969 carrier Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012071 phase 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
Description
本発明は発電プラントに係る。特に、蒸発器で
発生させた蒸気によりタービンを駆動して発電を
行う発電プリントに関する。
従来、この種の発電プラントにおいては、蒸発
器に導入するタービン駆動用作動媒体として所謂
湿り型の熱媒体つまりその飽和蒸気を断熱膨脹さ
せた時に湿り域に入る熱媒体を用いるのが一般的
である。このような従来の発電プラントの代表例
を第１図に示す。この従来例の主要構成要素は予
熱器１、蒸発器２、過熱器３、タービン４、発電
機５、凝縮器６、循環ポンプ７である。この例は
凝縮器６からの作動媒体を循環ポンプ７で昇圧
し、予熱器１で予熱し、蒸発器２で飽和蒸気１０
１を発生させ、更に過熱器３で過熱蒸気１０２と
してタービン４へ導入し、タービン４を駆動して
発電した後、再び凝縮器６へ戻す系統になつてい
る。その過程をＴ−Ｓ線図（温度−エントロピー
線図）で第２図に示した。
ところがこのような従来技術にあつては、ター
ビンに作動媒体を過熱蒸気の状態で導くべく、図
の如く蒸発器２の後段にどうしても過熱器３を設
ける必要があつた。その理由は、蒸発器２で発生
した飽和蒸気１０１を直接タービン導入すると蒸
気が断熱膨張した時に湿り蒸気となり、蒸気中に
液滴が混入し、液滴が混入するとタービン性能が
低下すると共に、液滴のアタツクによりタービン
ブレードが損傷する虞が大きいためである。この
ため従来の発電プラントでは、断熱膨脹時にター
ビン内で湿り蒸気とならないように、タービンへ
過熱蒸気１０２を流入させることが不可欠であ
る。従つて、従来の発電プラントでは、蒸発器２
で発生した飽和蒸気１０１を更に加熱して過熱蒸
気１０２にする過熱器３が必要であり、これを廃
することはできなかつたわけである。
よつて従来の発電プラントは、熱交換器が大型
にならざるを得ないという問題点を残している。
本発明の目的は、発電プラントにおいてその蒸
発器で直接過熱蒸気を発生させるようにし、特別
な過熱器は不要としてコンパクトで高性能の発電
プラントを提供することにある。
この目的を達成するため、本発明においてはタ
ービン駆動用の作動媒体として断熱膨脹時に湿り
域に入る熱媒体（これを本明細書中で熱媒体Ａと
称する）と該熱媒体Ａより沸点の高い他の熱媒体
（同じくこれを熱媒体Ｂと称する）とを用い、こ
れを蒸発器に導入してタービン駆動を行う構成と
する。
本発明は以下のような知見に基づいてなされた
ものである。即ちある一定圧力の蒸気を発生させ
る場合、上記したような熱媒体Ａと該熱媒体Ａよ
り沸点の高い熱媒体Ｂとを混合することにより、
熱媒体Ａのみの飽和蒸気温度より高い温度の過熱
蒸気が発生する性質があること、また、熱媒体
Ａ，Ｂの混合比を変えることにより過熱度が変わ
る性質があることが一般に知られている。本発明
者らはこの性質について実験でも確認した。本発
明者らはこの性質に着目し、更に種々検討を重ね
た結果、前記二成分の熱媒体を混合させることに
より生ずる性質を発電プラントに適用し、蒸発器
内の作動媒体としての熱媒体Ａに、これより沸点
の高い熱媒体Ｂを混合させ、過熱蒸気を発生させ
るようにする本発明に至つたものである。また、
熱媒体Ａ，Ｂの混合比を変えて、必要な過熱度を
得られるようにしたものである。
以下本発明の一実施例を第３図により説明す
る。
この発電プラントは、蒸発器２で発生させた蒸
気１０２によりタービン４を駆動して発電を行う
ものであつて、蒸発器２には作動媒体として、断
熱膨脹時に湿り域に入る熱媒体Ａと、この熱媒体
Ａより沸点の高い他の熱媒体Ｂとを導入して構成
したものである。
この結果、混合熱媒体の作用により、蒸発器２
においてすでに過熱器（従来例の第１図参照）で
過熱されたのと同様な過熱蒸気を得ることができ
る。従つて過熱器を用いなくて済み、プラントを
コンパクトにすることができる。また熱媒体Ａ，
Ｂの混合比は任意に変えられることから、発生す
る蒸気の過熱度を自由に変えることもできる。
本実施例の構成と作用効果とを一層詳しく説明
すれば、下記の通りである。本例の発電プラント
の主な構成要素は、予熱器１、蒸発器２、タービ
ン４、発電機５、凝縮器６、循環ポンプ７であ
る。凝縮器６からの作動媒体を循環ポンプ７で昇
圧して予熱器１へ送り、予熱して、蒸発器２で過
熱蒸気１０２を発生させてタービンを回転させ、
発電した後、再び凝縮器６へ戻す。発電プラント
の蒸発器２に、従来より使用してきた作動媒体と
しての熱媒体Ａより沸点の高い熱安定性の良い熱
媒体Ｂを内容させておき、これに熱媒体Ａを混合
させ、Ａ，Ｂの混合液を蒸発器２で加熱して過熱
蒸気１０２を発生させる。これは第２図における
蒸発工程と過熱工程を同時に蒸発器２内で行つて
いることを示している。また、熱媒体Ａ，Ｂの混
合比を変えることにより発生する蒸発の過熱度を
自由に変えられる効果があるので、プラントの性
能を上げるため、タービン排気を飽和蒸気にする
ことができる。
本発明の実施に用い得る断熱膨脹時に湿り域に
入る作動体Ａ、及びこれと混合する熱媒体Ｂの組
合せの一例を次の表に示す。下記例は、低沸点媒
体たる各種フロンを熱媒体Ａとした場合と、従来
より作動媒体として多く用いられている水の熱媒
体Ａとして本発明を実施する場合について例示し
たものである。
The present invention relates to a power plant. In particular, it relates to power generation printing that generates electricity by driving a turbine using steam generated in an evaporator. Conventionally, in this type of power generation plant, it has been common to use a so-called wet heat carrier, that is, a heat carrier that enters the wet region when the saturated steam is adiabatically expanded, as the turbine-driving working medium introduced into the evaporator. be. A typical example of such a conventional power generation plant is shown in FIG. The main components of this conventional example are a preheater 1, an evaporator 2, a superheater 3, a turbine 4, a generator 5, a condenser 6, and a circulation pump 7. In this example, the working medium from the condenser 6 is pressurized by the circulation pump 7, preheated by the preheater 1, and saturated steam is
1 is generated, and then introduced into the turbine 4 as superheated steam 102 in the superheater 3, and after driving the turbine 4 to generate electricity, it is returned to the condenser 6 again. The process is shown in FIG. 2 as a T-S diagram (temperature-entropy diagram). However, in such a conventional technique, it was necessary to provide a superheater 3 downstream of the evaporator 2 as shown in the figure, in order to introduce the working medium in the state of superheated steam to the turbine. The reason for this is that when the saturated steam 101 generated in the evaporator 2 is directly introduced into the turbine, it becomes wet steam when it expands adiabatically, and droplets are mixed into the steam. This is because there is a high possibility that the turbine blades will be damaged by the droplet attack. Therefore, in conventional power plants, it is essential to allow superheated steam 102 to flow into the turbine so that it does not become wet steam within the turbine during adiabatic expansion. Therefore, in a conventional power plant, the evaporator 2
A superheater 3 is required to further heat the saturated steam 101 generated in the above process to convert it into superheated steam 102, and this cannot be abolished. Therefore, conventional power plants still have the problem that the heat exchanger has to be large. An object of the present invention is to provide a compact, high-performance power plant in which superheated steam is directly generated in the evaporator of the power plant, eliminating the need for a special superheater. To achieve this objective, the present invention uses a heat medium (herein referred to as heat medium A) that enters a humid region during adiabatic expansion as a working medium for driving a turbine, and a heat medium with a boiling point higher than that of heat medium A. The configuration is such that another heat medium (also referred to as heat medium B) is introduced into the evaporator to drive the turbine. The present invention was made based on the following findings. That is, when generating steam at a certain constant pressure, by mixing the heat medium A as described above and the heat medium B whose boiling point is higher than that of the heat medium A,
It is generally known that there is a property that superheated steam is generated at a temperature higher than the saturated steam temperature of heat medium A alone, and that the degree of superheating can be changed by changing the mixing ratio of heat medium A and B. . The present inventors also confirmed this property through experiments. The present inventors focused on this property, and as a result of further various studies, applied the properties produced by mixing the above-mentioned two-component heat medium to a power generation plant, and used the heat medium A as the working medium in the evaporator. The present invention has been achieved in which a heat medium B having a higher boiling point is mixed with the heat medium B to generate superheated steam. Also,
By changing the mixing ratio of heat media A and B, the required degree of superheat can be obtained. An embodiment of the present invention will be described below with reference to FIG. This power generation plant generates electricity by driving a turbine 4 using steam 102 generated in an evaporator 2, and the evaporator 2 has a heat medium A, which enters a humid region during adiabatic expansion, as a working medium, and This heat medium A is constructed by introducing another heat medium B having a boiling point higher than that of the heat medium A. As a result, due to the action of the mixed heat medium, the evaporator 2
It is possible to obtain superheated steam similar to that already superheated in the superheater (see FIG. 1 of the conventional example). Therefore, there is no need to use a superheater, and the plant can be made more compact. In addition, heat medium A,
Since the mixing ratio of B can be changed arbitrarily, the degree of superheating of the generated steam can also be changed freely. The structure and effects of this embodiment will be explained in more detail as follows. The main components of the power plant of this example are a preheater 1, an evaporator 2, a turbine 4, a generator 5, a condenser 6, and a circulation pump 7. The working medium from the condenser 6 is pressurized by the circulation pump 7 and sent to the preheater 1 for preheating, and the evaporator 2 generates superheated steam 102 to rotate the turbine.
After generating electricity, it is returned to the condenser 6 again. The evaporator 2 of the power generation plant contains heat medium B, which has a higher boiling point and better thermal stability than heat medium A, which has been used conventionally as a working medium, and heat medium A is mixed with this, and A, B The mixed liquid is heated in the evaporator 2 to generate superheated steam 102. This shows that the evaporation process and superheating process in FIG. 2 are performed simultaneously in the evaporator 2. Furthermore, by changing the mixing ratio of the heat mediums A and B, the degree of superheating of the generated evaporation can be freely changed, so that the turbine exhaust can be made into saturated steam in order to improve the performance of the plant. The following table shows an example of a combination of the working body A that enters the wet region during adiabatic expansion and the heat medium B that is mixed with the working body A that can be used in carrying out the present invention. The following examples illustrate cases in which the heat medium A is various kinds of fluorocarbons, which are low boiling point media, and cases in which the present invention is implemented using water as the heat medium A, which has been conventionally often used as a working medium.
【表】
熱媒体ＡとしてフロンR12、熱媒体Ｂとしてポ
リオールエステル油を組合せた場合のＡ，Ｂの混
合比の決め方の一例を以下に示す。第２図におい
て、凝縮圧力9.8Kg／cm2abs（飽和で40℃）と蒸発
圧力34Kg／cm2abs（飽和で100℃）とのランキンサ
イクルで、プランントの性能を上げるため、ター
ビン排気を9.8Kg／cm2absの飽和蒸気40℃にするに
は、タービン入口の蒸気は飽和蒸気温度100℃よ
り約10℃（Δt）過熱する必要がある。蒸発圧力
を高くすると過熱度Δtが高くなるわけであり、
従つて熱媒体Ｂの割合を大きくすると過熱度Δt
は高くなるのあるが、このような10℃程度の過熱
を蒸発器２において達成するには、熱媒体Ａのフ
ロンR12と熱媒体Ｂのポリオールエステル油の混
合比は、ラウルの法則から体積比約１：１の割合
で混合すれば良いことがわかる。この１：１とい
うのは概算であるが、厳密にはラウルの法則を用
いて両者のモル分率を求め、これを体積比に換算
すればよく、計算で正確に求めることができるも
のである。
以下に、ラウルの法則による計算方法を説明す
る。
熱媒体Ａ，Ｂの純成分の蒸気圧PA、PBは温度
の関数であり、PA＝fA（Ｔ）、PB＝fB（Ｔ）と表せ
る。従つて、蒸発器の圧力Ｐ、温度Ｔが決まれ
ば、ラウルの法則から、熱媒体Ａ，Ｂの液相のモ
ル分率xA，xBは、
xA＝（Ｐ−PB）／（PA−PB）
xB＝（PA−Ｐ）／（PA−PB）
より計算できる。
ここで、熱媒体Ａ，Ｂの気相モル分率yA，yB
は、
yA＝PAxA／（PAxA＋PBxB）
yB＝PBxB／（PAxA＋PBxB）
で表せ、PA≫PBであり、yB０であるので、混
合媒体の蒸気の主成分は熱媒体Ａとなる。従つ
て、第２図のTS線図の蒸気を、近似的に熱媒体
Ａの蒸気表を用いて計算することができる。
なお前記凝縮圧力や蒸発圧力の値は、冷却水温
度やタービン圧力その他諸要素によつて定められ
るものである。
このように本実施例によれば、発電プラントの
蒸発器において、過熱蒸気を発生させる効果があ
るのでコンパクト高性能の発電プラントを提供で
きる。
上述の如く本発明によれば、発電プラントにお
いて、その蒸発器で直接、過熱蒸気を発生させる
ことができるので、特別な過熱器は要さず発電プ
ラントを小型化でき、従つて同型であれば効率の
良い高性能のものとすることができるという効果
がある。
なお、当然のことではあるが、本発明は上述し
た実施例にのみ限定されるものではない。[Table] An example of how to determine the mixing ratio of A and B when Freon R12 is used as heat medium A and polyol ester oil is used as heat medium B is shown below. Figure 2 shows a Rankine cycle with a condensing pressure of 9.8 kg/cm 2 ab s (40°C at saturation) and an evaporation pressure of 34 kg/cm 2 ab s (100°C at saturation). In order to make 9.8Kg/cm 2 ab s of saturated steam at 40°C, the steam at the turbine inlet needs to be superheated by about 10°C (Δt) above the saturated steam temperature of 100°C. Increasing the evaporation pressure increases the superheat degree Δt,
Therefore, if the proportion of heat medium B is increased, the degree of superheating Δt
However, in order to achieve superheating of about 10°C in evaporator 2, the mixing ratio of Freon R12 as heat medium A and polyol ester oil as heat medium B must be determined by volume ratio according to Raoult's law. It can be seen that mixing at a ratio of approximately 1:1 is sufficient. This ratio of 1:1 is an approximation, but strictly speaking, it is sufficient to find the mole fraction of both using Raoult's law and convert it to a volume ratio, which can be determined accurately by calculation. . The calculation method using Raoult's law will be explained below. The vapor pressures P A and P B of the pure components of the heat carriers A and B are functions of temperature, and can be expressed as P A = f A (T) and P B = f B (T). Therefore, once the pressure P and temperature T of the evaporator are determined, from Raoult's law, the mole fractions x A and x B of the liquid phase of heat carriers A and B are x A = (P-P B )/( It can be calculated from P A − P B ) x B = (P A − P)/(P A − P B ). Here, the gas phase molar fractions y A , y B of heat media A and B
can be expressed as y A = P A x A / (P A x A + P B x B ) y B = P B x B / (P A x A + P B x B ), where P A ≫ P B and y Since B 0, the main component of the vapor of the mixed medium is the heat medium A. Therefore, the steam in the TS diagram of FIG. 2 can be approximately calculated using the steam table of heat medium A. Note that the values of the condensing pressure and evaporation pressure are determined by cooling water temperature, turbine pressure, and other various factors. As described above, according to this embodiment, since the evaporator of the power plant has the effect of generating superheated steam, it is possible to provide a compact, high-performance power plant. As described above, according to the present invention, superheated steam can be directly generated in the evaporator of a power generation plant, so a special superheater is not required and the power generation plant can be downsized. This has the effect of making it efficient and high performance. Note that, as a matter of course, the present invention is not limited to the above-described embodiments.
第１図は従来の発電プラントの系統図、第２図
は熱サイクル図を示す。第３図は本発明の発電プ
ラントの一実施例の系統図を示す。
１……予熱器、２……蒸発器、４……タービ
ン、５……発電機、１０１……飽和蒸気、１０２
……過熱蒸気、１０３……飽和蒸気（タービン排
気）、１０４……液体（媒体）。
Figure 1 shows a system diagram of a conventional power generation plant, and Figure 2 shows a thermal cycle diagram. FIG. 3 shows a system diagram of an embodiment of the power generation plant of the present invention. 1... Preheater, 2... Evaporator, 4... Turbine, 5... Generator, 101... Saturated steam, 102
... Superheated steam, 103 ... Saturated steam (turbine exhaust), 104 ... Liquid (medium).
Claims (1)
動して発電を行う発電プラントにおいて、蒸発器
に導入する作動媒体として、断熱膨張時に湿り域
に入る熱媒体Ａと該熱媒体Ａより沸点が高い他の
熱媒体Ｂとをラウルの法則に従い混合した混合作
動媒体であつてタービンで膨張した時に該混合作
動媒体の蒸気が湿り蒸気とならない混合比で混合
したものを使用したことを特徴とする発電プラン
ト。 ２ 熱媒体ＡとしてフロンR12、フロンR21、フ
ロンR22のいずれかを用い熱媒体Ｂとしてポリオ
ールエステル油、エステル油のいずれかを用いて
混合作動媒体とし、あるいは、熱媒体Ａとして水
を用い熱媒体Ｂとしてグリセリン、エチレングリ
コールのいずれかを用いて混合作動媒体とするこ
とを特徴とする特許請求の範囲第１項記載の発電
プラント。[Claims] 1. In a power generation plant that generates electricity by driving a turbine using steam generated in an evaporator, a heat medium A that enters a humid region during adiabatic expansion and the heat medium are used as a working medium introduced into the evaporator. The use of a mixed working medium that is mixed with another heat medium B, which has a higher boiling point than A, according to Raoult's law, at a mixing ratio that does not cause the steam of the mixed working medium to become wet steam when expanded in the turbine. A power generation plant featuring: 2. Use either Freon R12, Freon R21, or Freon R22 as heat medium A, and use either polyol ester oil or ester oil as heat medium B as a mixed working medium, or use water as heat medium A as a heat medium. 2. The power generation plant according to claim 1, wherein B is either glycerin or ethylene glycol as a mixed working medium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12047082A JPS5912107A (en) | 1982-07-13 | 1982-07-13 | Power generating plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12047082A JPS5912107A (en) | 1982-07-13 | 1982-07-13 | Power generating plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5912107A JPS5912107A (en) | 1984-01-21 |
| JPH0231207B2 true JPH0231207B2 (en) | 1990-07-12 |
Family
ID=14786962
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12047082A Granted JPS5912107A (en) | 1982-07-13 | 1982-07-13 | Power generating plant |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5912107A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54105652A (en) * | 1978-02-07 | 1979-08-18 | Daikin Ind Ltd | Rankine cycle working fluid |
| JPS5683504A (en) * | 1979-12-10 | 1981-07-08 | Agency Of Ind Science & Technol | Power plant |
| JPS5696106A (en) * | 1979-12-28 | 1981-08-04 | Sumitomo Heavy Ind Ltd | Heat engine to use mixed liquid as operating medium |
-
1982
- 1982-07-13 JP JP12047082A patent/JPS5912107A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54105652A (en) * | 1978-02-07 | 1979-08-18 | Daikin Ind Ltd | Rankine cycle working fluid |
| JPS5683504A (en) * | 1979-12-10 | 1981-07-08 | Agency Of Ind Science & Technol | Power plant |
| JPS5696106A (en) * | 1979-12-28 | 1981-08-04 | Sumitomo Heavy Ind Ltd | Heat engine to use mixed liquid as operating medium |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5912107A (en) | 1984-01-21 |
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