KR101294948B1 - Power system for improved thermal and condensing efficiency - Google Patents

Abstract

The present invention is connected to the evaporator and the evaporator provided to evaporate the working fluid and the heating fluid containing at least two components and the heating fluid to evaporate, the separator for receiving the evaporated working fluid and separated into thick and lean flow A thickener connected to the thickener outlet of the separator and connected to the energy converting means and the energy converting means which are provided to expand the thickener to generate useful energy, and the energy-hungry thickener and the separator which pass through the energy converting means. The lean flow discharged from the mixer is connected to the mixer and the mixer, and is connected between the condenser and the evaporator provided to condense the working fluid by exchanging the mixed working fluid with a cooling fluid supplied from a low heat source. A power generation system comprising pumping means for pressurizing a working fluid that has passed through a condenser. The present invention relates to a power generation system including a working fluid storage tank disposed at a lower end of the outlet of the condenser so that the working fluid is smoothly discharged from an accumulator. According to the present invention, it is possible to reduce the amount of cooling fluid in the condenser and supply heat, thereby improving thermal efficiency. In addition, the condenser and working fluid storage tank can be configured and arranged in a carina cycle to prevent condensation of working fluid in the condenser, thereby increasing condensation efficiency.

Description

Power system for improved thermal and condensing efficiency

The present invention relates to a power generation system with improved thermal efficiency and condensation efficiency. Specifically, the configuration of the condenser and the arrangement of the working fluid storage tank in the power generation system implemented using a carina cycle using water and ammonia mixed fluid as a working fluid are adjusted. To increase the condensation efficiency and to improve the thermal efficiency through heat exchange with a heating fluid circulating a heat source.

Thermal power plants using coal, oil or gas as fuel typically use water as the working fluid. In the case of LNG combined cycle, the exhaust gas from the gas turbine is very high, 500 ~ 600 ℃, so the water is converted into steam to drive the steam turbine to generate electricity.

The low-temperature thermal power generation technology for generating power using the heat source of lower temperature than the existing steam power generation at 100-500 ℃ is being developed and expanded. In order to generate electricity at low temperatures, a working fluid having a boiling point at low temperatures, ie a refrigerant or a hydrocarbon-based fuel, is used. Depending on the nature of the working fluid or the system configuration, the organic Rankine cycle, the Kalina cycle, and the Uehara cycle are largely classified. The organic Rankine cycle uses one working fluid, while the Karina and Uehara cycles use a mixture of ammonia and water.

Organic Rankine cycle is composed of the basic elements of the evaporator 40, the turbine 50, the condenser 20, the pump 30, as shown in Figure 1 which is a typical Rankine cycle, the turbine 50, the generator 50 Is connected to convert the mechanical energy converted in the turbine 50 into electrical energy. The evaporator 40 is a place where the working fluid is changed into a gas by receiving heat, the turbine 50 serves to change the pressure difference between the evaporator 40 and the condenser 20 to work, the condenser 20 is a turbine ( It changes the low temperature low pressure working fluid from 50) into liquid. The pump 30 serves to supply the low-pressure working fluid in the condenser to the evaporator.

In this Rankine cycle, the low temperature low pressure working fluid 1 passes through the pump 30 to become a low temperature high pressure working fluid 2, and passes through the evaporator 40 to become a high temperature high pressure working fluid 3. After passing through the turbine 50, it becomes a low pressure working fluid 4, and then passes through the condenser 20 to become a low temperature low pressure working fluid 1, and the working fluid circulates this cycle to generate useful energy. do. The organic Rankine cycle differs from the Rankine cycle in working fluids that evaporate at low temperatures using organic materials with lower boiling points than water. Organic Rankine cycle is an organic material in which the working fluid consists of one component.

On the other hand, the carina cycle uses ammonia water mixed with water and ammonia as the working fluid, unlike the organic Rankine cycle using pure materials as the working fluid. Specifically, as shown in FIG. 2, the low-temperature low-pressure working fluid 1 is discharged to the high-pressure working fluid 2 through the pump 30, and is preheated by the preheater or regenerator 45 to produce the medium-temperature working fluid 5. do. Thereafter, the gas is vaporized through the evaporator 40 to become a high-temperature high-pressure working fluid 3, and the working fluid 3 flows into the gas-liquid separator 60. Here, the saturated liquid containing a large amount of water is separated into a lean stream (7) containing little ammonia and a concentrated stream (6), which is a saturated steam which is mainly composed of ammonia. The concentrated stream (6) is supplied to the turbine The turbine 50 converts the chemical energy into mechanical energy and the mechanical energy produces electricity through a generator (not shown), whereupon the enrichment stream 6 is converted to the spent enrichment stream 4 ).

The lean stream 7 in a high temperature state is sent to a preheater or regenerator 45 to recover heat while preheating the working fluid 2 to become a heat exchanged working fluid 8. This heat exchanged working fluid 8 is supplied to a throttle valve The pressure is lowered to the pressure at the rear end of the turbine 50 and becomes the lean stream 9 of low pressure. The low-pressure lean stream 9 and the spent rich stream 4 are mixed in the absorber 80 to become the working fluid 10. The working fluid 10 is supplied to the condenser 11 and becomes the working fluid 1 in a state where the working fluid 10 is condensed by the cooling water of low temperature.

The evaporator 40 is supplied and discharged with a heating fluid having a high temperature heat source, and the cooling water is supplied and discharged to the condenser 20. The carina cycle may adjust the opening degree of the pressure controller 70 while adjusting the level of the gas-liquid separator 60.

References to US Pat. Nos. 5,953,918, 5,572,871, 5,440,882, and 4,982,568 may supplement the contents of the Carina cycle.

Here, as shown in FIG. 2, a typical carina cycle includes one condenser, and there may be a case in which a working drum or a small drum is not installed at the rear end of the condenser. In order to improve the condensation efficiency, the condenser is usually enlarged, and a method of increasing the length or increasing the number of plate heat exchangers installed in the condenser is used. However, in this case, the pressure loss increases due to the increased friction between the plate heat exchanger and the working fluid, causing the pressure to fall below the condensation pressure, thereby causing a factor of reducing the condensation efficiency.

In addition, to reduce the installation space of the system, the elements of the system are designed at the same height. If the condenser and the working fluid storage tank are designed at the same position, or the condenser rear pipe is located higher than the height of the condenser, the condensed operation inside the condenser Fluid stagnation also causes a decrease in condensation efficiency.

This moves less working fluid than the design flow and lowers the system pressure, making it difficult to achieve the design output in the turbine / generator.

In addition, in the carina cycle design, the working fluid 5 entering the evaporator 40 is supplied at a temperature of the saturated liquid obtained at a normal working pressure. This is because the efficiency of the evaporator can be maximized. However, when the working fluid 5 is supplied to the temperature of the saturated liquid, the diluent 7 separated in the gas-liquid separator 60 is supplied to the working fluid 2 supplied from the preheater 45 through the pump 30, The amount Q of heat is consumed while the amount of heat Q is not large, so that the working fluid 10 maintains a relatively high temperature.

Accordingly, the heat must be cooled by the cooling water in the condenser 20. That is, the amount of cooling water supplied to the condenser 20 should increase and the condenser itself should also increase. This has the effect of lowering the power generation efficiency, which is defined as the power generation output Qout for the supply calorific value Qin.

The present invention reduces the amount of cooling fluid used in the condenser by sufficiently cooling the leans obtained through the gas-liquid separator in the Carina cycle, and supplying without affecting the power generation output at the power generation efficiency defined as the power generation output (Qout) for the supply heat quantity (Qin). It aims to reduce heat and ultimately improve thermal efficiency.

In addition, it is an object to increase the condensation efficiency by preventing the remaining of the working fluid in the condenser through the configuration and arrangement of the condenser and the working fluid storage tank in the carina cycle.

In order to achieve the above object, an embodiment of the present invention provides a power generation system as follows.

The power generation system of the present invention is connected to the evaporator and the evaporator provided to evaporate the working fluid and the heating fluid containing at least two components, the working fluid is evaporated, and receives the evaporated working fluid to separate the thick and lean flow A thickener connected to the separator and the rich outlet of the separator, the energy converting means being provided to expand the thickener to generate useful energy, and the energy converting means passing through the energy converting means, The lean discharged from the separator is connected to the mixer and the mixer, and the mixed working fluid is exchanged with a cooling fluid supplied from a low heat source to connect the working fluid between the condenser and the evaporator. Pumping means for pressurizing the working fluid passed through the condenser; In the power generation system having a, it may be configured to include a working fluid storage tank disposed at the lower end of the outlet of the condenser to smoothly discharge the working fluid from the condenser.

The first heat exchanger may be provided at the inlet of the condenser, and the first heat exchanger may be configured to heat exchange with the cooling fluid of the condenser before the working fluid is introduced into the condenser, thereby improving condensation efficiency.

In addition, the condenser may be provided in plurality, and may be configured to be parallel to the horizontal to improve the condensation efficiency by reducing the pressure loss when passing the working fluid.

In addition, the first heat exchanger is installed between the evaporator and the separator, and the lean flow and the heating fluid discharged from the separator are provided to exchange heat.

The heating fluid may further include a heating fluid circulation structure in which the heating fluid circulates so as to circulate the heat exchanger, the evaporator, and the first heat exchanger, wherein the heating fluid receives heat from an external heat source.

One embodiment of the present invention the power generation system through the above configuration, by sufficiently cooling the lean flow obtained through the gas-liquid separator to reduce the amount of cooling fluid in the condenser and is defined as the power generation output (Qout) for the supply heat (Qin) In power generation efficiency, there is an effect of ultimately improving thermal efficiency by reducing the supply heat without affecting the power output.

In addition, it is possible to prevent the operating fluid remaining inside the condenser to prevent operation with a smaller amount of the working fluid than the design flow rate, the power generation system pressure is lowered there is an effect to prevent the output decrease in the turbine / generator.

In addition, by arranging a heat exchanger before the working fluid is introduced into the condenser, the cooling fluid used in the condenser is subjected to a pre-cooling process, and then introduced into the condenser, or a plurality of condensers are arranged in parallel so that the working fluid passes through the condenser. It can be expected to reduce the pressure loss to maintain a certain range of condensing pressure to increase the condensation efficiency.

1 is a block diagram of a conventional Rankine cycle.
2 is a block diagram of a conventional carina cycle.
3 is a configuration diagram of an embodiment of a power generation system according to the present invention.
4 is a configuration diagram showing a condenser arranged in parallel in the embodiment shown in FIG.
FIG. 5 is a diagram illustrating a state in which a heat exchanger is disposed at a condenser inlet in the embodiment shown in FIG. 3.
6 is a configuration diagram of another embodiment of the power generation system according to the present invention.
FIG. 7 is a configuration diagram showing a condenser arranged in parallel in the embodiment shown in FIG. 6.
FIG. 8 is a view illustrating a state in which a heat exchanger is disposed at a condenser inlet in the embodiment illustrated in FIG. 6.

In order to help the understanding of the features of the present invention as described above, it will be described in more detail with respect to the power generation system according to the embodiment of the present invention.

Hereinafter, exemplary embodiments will be described based on embodiments best suited for understanding the technical characteristics of the present invention, and the technical features of the present invention are not limited by the illustrated embodiments, It is to be understood that the present invention may be implemented as illustrated embodiments.

Accordingly, the present invention may be modified in various ways within the technical scope of the present invention through the embodiments described below, and such modified embodiments fall within the technical scope of the present invention.

In order to facilitate the understanding of the embodiments described below, in the reference numerals shown in the accompanying drawings, among the constituent elements that perform the same function in the respective embodiments, the related constituent elements are indicated by the same or an extension line number.

Embodiments related to the present invention are basically defined as the power generation output (Qout) for the supply heat (Qin) to reduce the amount of cooling fluid in the condenser 110 by sufficiently cooling the lean flow obtained through the separator in the Carina cycle In the power generation efficiency, the supply heat is reduced without affecting the power generation output and ultimately the thermal efficiency is improved, and in the carina cycle, the condenser 110 and the working fluid storage tank 115 are configured and arranged to maintain residual fluid in the condenser 110. To increase condensation efficiency.

Hereinafter, a specific embodiment of the present invention will be described with reference to the accompanying drawings.

3 is a configuration diagram of a power generation system according to the present invention, Figure 6 is another configuration diagram of a power generation system according to the present invention.

3 and 6, the present invention is the power generation system is connected to the evaporator 150 and the evaporator 150 provided to evaporate the working fluid by at least a heat-exchanging working fluid and a heating fluid containing at least two components, And an energy conversion means connected to a separator 160 for receiving the evaporated working fluid into a rich stream and a lean stream and a rich stream outlet of the separator 160 to expand the rich stream to generate useful energy. 170 is connected to the energy conversion means 170 and is connected to the mixer and the mixer in which the rich energy consumed through the energy conversion means 170 and the lean stream discharged from the separator 160 are mixed. The condenser 110 is provided between the condenser 110 and the condenser 110 and the evaporator 150 provided to condense the working fluid by exchanging a mixed working fluid with a cooling fluid supplied from a low heat source. In the power generation system having a pumping means 120 for pressurizing the working fluid passed through, the working fluid storage tank 115 is disposed at the lower end of the outlet of the condenser 110 so that the working fluid is discharged smoothly from the condenser 110 It may be configured to include).

The working fluid containing two or more components used in the present invention is a multicomponent working flow comprising a component having a low boiling point and a component having a high boiling point. Such preferred working streams are ammonia water mixtures, two or more hydrocarbons, two or more Freons, hydrocarbons and Freon mixtures. In general, working fluids are mixtures of various components with advantageous thermodynamic properties and solubility.

Here, particularly preferred working flows can be used water and ammonia mixtures. Hereinafter, the ammonia water mixed with water and ammonia will be described as limited to the working fluid used in the present invention.

The working fluid used in the present invention maintains the same concentration starting from the mixing section 190, passing through the condenser 110, the evaporator 150, and entering the separator 160 to separate the thick and the lean. .

The working fluid S1 condensed in the condenser 110 is pumped at a high pressure by the pump 120 to generate a high pressure working fluid S2. The high pressure working fluid S2 exchanges heat with the lean flow S9 in the preheater 130 to become a heated working fluid S3. The elevated working fluid (S3) is introduced into the evaporator 150, the working fluid in the evaporator 150 becomes a working fluid (S4) evaporated by phase change while heat exchange with the heating fluid. At this time, the thermal energy is converted into chemical energy.

The evaporated working fluid (S4) is supplied to the separator (160), and separated from the thickener (S5) in the vapor state and the lean (S9) in the liquid state in the separator (160). Here, the rich stream (S5) means that a low boiling point fluid such as ammonia is relatively high in the working fluid, and the lean stream (S9) means that a low boiling point fluid such as ammonia is relatively low in the working fluid. In the separator 160, the gas has a high concentration of low boiling point fluid such as ammonia, and the liquid has a low concentration of low boiling point fluid such as ammonia.

Here, the gas separated in the separator 160 will correspond to a rich stream because the concentration of ammonia is relatively high, and the liquid will correspond to a lean stream because the concentration of ammonia is relatively low.

The rich stream S5 is supplied to an energy converting means 170 such as a turbine, in which the rich stream S5 is depressurized, whereby chemical energy is converted into mechanical energy. The generator 180 is connected to the energy conversion means 170 such as a turbine to produce electricity with mechanical energy. The rich stream S5 is energy consumed while passing through an energy conversion means 170 such as a turbine, resulting in a spent rich stream S6. The spent rich stream S6 is in a state of the lean flow S11 passing through the throttle valve and the working fluid S8 before being mixed, joined in the mixing unit 190, and separated again.

On the other hand, the lean flow (S9) is separated from the separator 160 and flows to the preheater (130). In the preheater 130, a high pressure working fluid S2, which is pressurized by the pump 120, passes, and the temperature of the lean flow S9 is higher than that of the high pressure working fluid S2. Therefore, heat is transferred from the lean flow (S9) to the high pressure working fluid (S2) so that the high pressure working fluid (S2) becomes a heated working fluid (S3) and the lean flow (S9) has a low temperature. It becomes the flow S11.

However, according to another embodiment as shown in FIG. 6, the lean flow S9 may first perform heat exchange with a heating fluid in which a heat source is connected before passing through the preheater 130.

That is, another embodiment of the present invention is installed between the separator 160 and the preheater 130, the heat exchanger is provided so that the lean flow (S9) and the heating fluid (H2) discharged from the separator 160 to exchange heat It may be configured to further include (450).

Accordingly, a heating fluid circulation structure in which the heating fluid H2 circulates so that the heating fluid H2 receives heat from an external heat source, and circulates the heat exchanger 410, the evaporator 150, and the heat exchanger 450 ( 420 may be further included.

In detail, the lean stream S9 separated from the separator 160 is heated in the heat exchanger 450 installed between the separator 160 and the preheater 130 before passing through the preheater 130. Exchange heat with H2).

At this time, since the temperature of the heating fluid H2 after passing through the evaporator 150 is lower than the lean flow S10, heat energy is transferred from the lean flow S10 to the heating fluid H2. Therefore, the lean flow S10 becomes the lean flow S11 of low temperature while passing through the heat exchanger 450, while the heating fluid H2 passes through the heat exchanger 450, and the heating fluid H3 rises in temperature. )

Thus, the lean flow (S10) having a lower temperature is subjected to heat exchange with a high-pressure working fluid (S2) while passing through the preheater (130) again to become a lean flow (S11) having a low temperature again.

The lean flow (S11) passing through the preheater (130) passes through the pressure regulating means (V), such as a throttle valve, falls to the pressure of the end of the energy conversion means (170) to become a low pressure lean flow (S12). At this time, the pressure control means may be adjusted according to the liquid level of the separator 160, so that the low pressure lean flow (S12) is joined to the spent thickening (S6) in the mixing section 190 to the working fluid (S8) ), The working fluid (S8) is provided to the condenser (110).

In the condenser 110, the working fluid S8 is condensed into the liquid phase by a cooling fluid such as cooling water, and becomes a liquid condensing working fluid S1. In this way, the working fluid converts thermal energy received from the heating fluid into electrical energy during one cycle.

In the apparatus for converting thermal energy into useful energy (for example, electrical energy) as in the present invention, in the case of the lean flow S9 separated from the separator 160, it is not supplied to the energy conversion means 170. In the prior art, the working fluid 2 (see FIG. 2) and the lean flow (7; FIG. 2) pass through the preheater 45 (see FIG. 2) and enter the condenser 20 (see FIG. 2) in the middle. In the case where the temperature of the lean flow is not sufficiently lowered at 130, the condenser 20 takes a large condensation load, which increases the overall size of the apparatus by increasing the condenser 110, and requires a lot of condensate.

The lean (S9) may be considered to lower the load of the condenser 110 by increasing the heat exchange amount of the preheater 130 before joining the spent thickening (S6) in the mixing section 190, As mentioned in the background art, in order to increase the heat exchange efficiency of the evaporator 150, the amount of heat exchange of the preheater 130 is inevitably limited because it must be added as a saturated liquid at the inlet end of the evaporator 150.

In the present invention, the lean flow (S9) is supplied to the heat exchanger 450, the heat exchanger 450 returns a portion of the thermal energy back to the heating fluid (H2).

The role of the heat exchanger 450 is to supply a portion of the energy that the working fluid that is not supplied to the energy conversion means 170 to be discarded through the condenser 110 to the heating fluid H2, which is energy conversion. It is to reduce the amount of energy Qin flowing into the system without affecting the amount of energy Qout converted in the means 170.

Considering that the power generation efficiency = the power generation amount Qout / the input energy amount Qin, it is understood that the efficiency of the cycle is increased because the amount of input energy decreases while the power generation amount is maintained.

In particular, in a power generation system such as the present invention using a working fluid containing two or more components, the exhaust gas or the waste heat source is used as a heat source, and the exhaust gas is not directly supplied to the evaporator 150, but exhaust gas is generated. Heat is extracted from the generator 430 to heat the heating fluid H1 through the heat exchanger 410, and the heating fluid H1 circulates through the evaporator 150, the heat exchanger 450, and the heat exchanger 410. Heat from a waste heat source such as exhaust gas is transferred to the working fluid S3 through the evaporator 150. Thus, heating the heating fluid H2 is to reduce the heat that the heating fluid H1 receives through the heat exchanger 410 and to reduce the amount of incoming energy Qin in the entire cycle including the heating fluid. .

In one embodiment of the invention, the temperature of the heating fluid (H1) flowing into the evaporator 150 is 150 ℃, the temperature of the working fluid (S3) is 116 ℃, the heating fluid (H2) exiting the evaporator 150 ) Is 120 ℃, the working fluid (S4) is 142 ℃. Since the working fluid S4 is separated into the lean stream S9 and the rich stream S5 without changing the temperature in the separator 160, the temperature of the working fluid S9 supplied to the heat exchanger 450 is 142 ° C. The temperature of the heating fluid H2 supplied to the group 450 is 120 ° C., so that heat is transferred from the working fluid S9 to the heating fluid H2 in the heat exchanger 450 as opposed to the evaporator 150.

After passing through the heat exchanger 450, the temperature of the working fluid (S10) fell to 125 ℃, the heating fluid (H3) rose to 124 ℃.

By returning some unused energy back to the heating fluid H2 as in the above embodiment, the heating fluid H2 after the evaporator 150 without the heat exchanger 450 is transferred to the evaporator 150 shear heating fluid H1. It is possible to reduce the amount of heat introduced through the heat exchanger 410 to be heated by approximately 13.3% through the heat exchanger, thereby improving the efficiency of the entire cycle.

In addition, as the lean temperature is lowered, the cooling load in the condenser 110 can be reduced, which not only reduces the power supply to the pump (not shown) of the condenser 110 that drives the generated power, but also the condenser ( 110 It is also possible to reduce the size of itself.

On the other hand, the working fluid mixed at the inlet of the condenser 110 is introduced into the condenser 110 to proceed with condensation. In this process, due to the difference between the height of the outlet of the working fluid of the condenser 110 and the height of the inlet of the working fluid storage tank 115, the working fluid is not completely discharged and remains at the bottom of the condenser.

In order to solve the above problems, the present invention arranges the working fluid storage tank 115 at the lower end of the outlet height line of the condenser 110, so that the working fluid does not remain at the bottom of the condenser 110 and the working fluid does not remain. It was completely discharged to the storage tank (115).

Next, Figure 4 is a block diagram showing a condenser arranged in parallel in the present invention shown in Figure 3, Figure 5 is a block diagram showing a state in which the heat exchanger is arranged in the condenser inlet in the present invention shown in FIG. to be. FIG. 7 is a diagram illustrating a condenser arranged in parallel in the present invention illustrated in FIG. 6, and FIG. 8 is a diagram illustrating a state in which a heat exchanger is arranged at a condenser inlet in the present invention illustrated in FIG. 6.

4 and 7, the present invention power generation system is provided with a second heat exchanger 140 at the inlet of the condenser 110, in the second heat exchanger 140 a working fluid to the condenser 110. It may be configured to heat exchange with the cooling fluid of the condenser 110 before the input to improve the condensation efficiency.

This is because the cooling fluid used for the working fluid that has already moved by mounting the second heat exchanger 140 before the working fluid flowing into the condenser 110 from the mixing unit 190 into the condenser 110. To reuse.

Accordingly, the cooling fluid is once again transferred from the working fluid to the outside of the cooling ellipse, etc., and the working fluid goes through the pre-cooling process before entering the condenser 110, the condenser 110 Less heat of condensation is released and ultimately condensation efficiency is improved.

Here, in another embodiment, the second heat exchanger 140 may be considered to be another condenser 110, and a method of condensing in multiple stages may be considered.

5 and 8, the inventors of the power generation system is provided with a plurality of condenser 110, it is arranged in parallel to the horizontal can be configured to improve the condensation efficiency to reduce the pressure loss when passing the working fluid.

In order to increase the condensation efficiency by using one large condenser 110, increasing the length of the plate or increasing the number of plates is performed between the plate and the rear end of the plate into which the working fluid is discharged. The friction increases the pressure loss, which in turn reduces the condensation pressure, which in turn may lower the condensation efficiency.

Thus, by arranging one or more small condensers 111 and 113 in parallel instead of one large condenser 110 to allow the working fluid to be divided into the condensers 111 and 113, the pressure loss reduction rate can be reduced.

When the pressure loss of the working fluid passing between the long plate heat exchanger plates is 1, the pressure loss when the long plate heat exchanger plate is divided in half and the working fluid is flowed is about 0.3 to 0.4. Pressure loss occurs. In other words, it is possible to prevent the pressure loss by 0.2 ~ 0.4 can be expected to increase the condensation efficiency by that much.

In the carina cycle, the lean flow obtained through the separator is sufficiently cooled to reduce the amount of cooling fluid in the condenser and ultimately reduce the supply heat without affecting the power output at the power generation efficiency defined as the power output (Qout) for the supply heat (Qin). This has the effect of improving the thermal efficiency.

In addition, through the configuration and arrangement of the condenser and the working fluid storage tank in the carina cycle can also be expected to increase the condensation efficiency by preventing the remaining of the working fluid in the condenser.

The foregoing merely illustrates specific embodiments of the power generation system 100.

Therefore, it should be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the present invention as defined by the following claims. do.

110 Condenser 115 Working fluid storage tank
120 pumping means 130 preheater
140 ... Second Heat Exchanger 150 ... Evaporator
160 ... Separator 170 ... Energy Conversion Means
180 ... generator 190 ... mixing unit
410 ... heat exchange section 420 ... heat circulation structure
430 ... heat source 450 ... heat exchanger

Claims (7)

An evaporator 150 provided to evaporate the working fluid by exchanging a working fluid containing a heating fluid and two or more components;
A separator (160) connected to the evaporator (150) and receiving the evaporated working fluid into a thick and a lean stream;
Heat exchanger 450 is installed between the evaporator 150 and the separator 160, the lean flow and the heating fluid discharged from the separator 160 is provided to exchange heat
Energy conversion means (170) connected to the rich outlet of the separator (160) and provided to expand the rich stream to produce useful energy;
A mixer 190 connected to the energy converting means 170 and mixing rich energy consumed through the energy converting means 170 and lean streams discharged from the separator 160;
A condenser 110 connected to the mixer 190 and provided to condense the working fluid by heat-exchanging the mixed working fluid with a cooling fluid supplied from a low heat source; And
Pumping means (120) connected between the condenser (110) and the evaporator (150) to pressurize the working fluid passing through the condenser (110);
Power generation system with improved thermal efficiency and condensation efficiency.
delete An evaporator 150 provided to evaporate the working fluid by exchanging a working fluid containing a heating fluid and two or more components;
A separator (160) connected to the evaporator (150) and receiving the evaporated working fluid into a thick and a lean stream;
Energy conversion means (170) connected to the rich outlet of the separator (160) and provided to expand the rich stream to produce useful energy;
A mixer 190 connected to the energy converting means 170 and mixing rich energy consumed through the energy converting means 170 and lean streams discharged from the separator 160;
A condenser 110 connected to the mixer 190 and provided to condense the working fluid by heat-exchanging the mixed working fluid with a cooling fluid supplied from a low heat source; And
Pumping means (120) connected between the condenser (110) and the evaporator (150) to pressurize the working fluid passing through the condenser (110);
, ≪ / RTI &
A second heat exchanger 140 is provided at the inlet of the condenser 110, and the second heat exchanger 140 exchanges heat with the cooling fluid of the condenser 110 before the working fluid is introduced into the condenser 110. Power generation system with improved thermal efficiency and condensation efficiency, characterized in that to improve the condensation efficiency.
An evaporator 150 provided to evaporate the working fluid by exchanging a working fluid containing a heating fluid and two or more components;
A separator (160) connected to the evaporator (150) and receiving the evaporated working fluid into a thick and a lean stream;
Energy conversion means (170) connected to the rich outlet of the separator (160) and provided to expand the rich stream to produce useful energy;
A mixer 190 connected to the energy converting means 170 and mixing rich energy consumed through the energy converting means 170 and lean streams discharged from the separator 160;
A condenser 110 connected to the mixer 190 and provided to condense the working fluid by heat-exchanging the mixed working fluid with a cooling fluid supplied from a low heat source; And
Pumping means (120) connected between the condenser (110) and the evaporator (150) to pressurize the working fluid passing through the condenser (110);
, ≪ / RTI &
The condenser 110 is provided with a plurality, the horizontal parallel arrangement is to improve the thermal efficiency and condensation efficiency, characterized in that to improve the condensation efficiency by reducing the pressure loss when passing the working fluid.
The method according to claim 3 or 4,
A working fluid storage tank (115) disposed at the lower end of the outlet of the condenser (110) so that the working fluid is smoothly discharged from the condenser (110).
The method according to claim 3 or 4,
A heat exchanger (450) installed between the evaporator (150) and the separator (160), the heat exchanger (450) being provided to heat-exchange the lean and discharge fluid discharged from the separator (160). Power generation system with improved efficiency.
The method of claim 1,
A heat exchange part 410 for supplying heat from an external heat source to a heating fluid; And
The heat exchanger 410 and the evaporator to evaporate the working fluid in the evaporator 150 by the heating fluid supplied from the heat exchanger 410 and to supply heat to the lean flow in the heat exchanger 450. A heating fluid circulation structure 420 integrally circulated between the 150 and the heat exchanger 450;
The power generation system with improved thermal efficiency and condensation efficiency, further comprising a.

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