KR101289189B1 - Apparatus for converting thermal energy - Google Patents

Abstract

PURPOSE: A thermal energy conversion apparatus capable of controlling the concentration of a working fluid is provided to form high pressure on the front end of a turbine and low pressure on the rear end of the turbine. CONSTITUTION: A thermal energy conversion apparatus comprises a first separator (160), a first heat exchanger (125), a second separator (165), a second heat exchanger (185), and a second pumping unit. The first separator receives an evaporation working fluid (213) from between an evaporator and an energy conversion unit, and separates the evaporation working fluid into a first dense fluid (214) and a second rarefied fluid (215). The first heat exchanger is located on the front end of the evaporator, where the working fluid, which passes through a working fluid before being condensed and a pumping unit, performs heat exchange. The second separator is located in between the heat exchanger and the evaporator; receives the heat exchanging working fluid; and separates the working fluid into a second dense fluid (204) and a second rarefied fluid (206). The second heat exchanger condenses the working fluid in which a second rarefied fluid and a second dense fluid are joined. The second pumping unit pumps the working fluid to have high pressure on the rear end of the second heat exchanger.

Description

Apparatus for Converting Thermal Energy

The present invention relates to a device for converting heat energy from a heat source by using a working fluid expanded and regenerated, and more specifically, a thermodynamic cycle for switching low temperature heat energy using two or more mixed working fluids, To an apparatus for converting thermal energy capable of raising power generation efficiency by having ammonia concentration.

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. To generate power at low temperatures, a working fluid with a boiling point at low temperatures, ie refrigerants or hydrocarbon-based fuels, is used. Depending on the nature of the working fluid or the system configuration, it is classified into an organic rankine cycle system, a kalina cycle, and a uehara cycle system. The organic Rankine cycle uses one working fluid, while the Karina and Uehara cycle systems use a mixture of ammonia and water.

The organic Rankine cycle is constituted by basic elements of an evaporator 40, a turbine 50, a condenser 20 and a pump 30 as shown in FIG. 1 which is a typical Rankine cycle. The turbine 50 is connected to a generator 50, And converts the mechanical energy converted by the turbine 50 into electric 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 is a function to change 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 and becomes the low temperature high pressure working fluid 2, and passes through the evaporator 40 to become the 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, which circulates the cycle to generate useful energy. do.

The difference between the organic Rankine cycle and the Rankine cycle is in working fluids that evaporate at low temperatures using organic materials that have a lower boiling point than water. The organic Rankine cycle utilizes organic materials 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, which uses pure materials as the working fluid. Specifically, as shown in FIG. 2, the low temperature low pressure working fluid 1 is discharged into the high pressure working fluid 2 through the pump 30, and is preheated in the preheater or regenerator 45 so that the medium temperature working fluid 5 is discharged. do. It is then vaporized through the evaporator 40 to become a high-temperature, high-pressure working fluid 3, which is introduced into the gas-liquid separator 60. Here, a saturated solution containing a lot of water is separated into a lean stream (7) having low ammonia and a thick stream (6), which is saturated steam having ammonia as its main component, and the thick stream (6) is supplied to the turbine (50) and consumed. It is converted into the rich (11), the turbine 50 converts chemical energy into mechanical energy and the mechanical energy is produced through a generator (not shown) and the rich (6) is consumed rich (11) )

The lean stream (7) at high temperature is sent to the preheater or regenerator (45) to recover heat while preheating the working fluid (2), and the heat exchanged lean stream (8) becomes a throttle valve. As it passes through the pressure controller 70, the pressure is lowered to the pressure at the rear end of the turbine 50, resulting in a low pressure lean flow 9. The low pressure lean 9 and spent thick 11 are mixed in the absorber 80 to form 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 low temperature cooling water.

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 with 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.

In order to increase the amount of power generated by the turbine 50 in the design of the carina cycle, the pressure difference between the front end and the rear end of the turbine 50 must be large. However, in a working fluid consisting of water and ammonia, the ammonia has a low evaporation temperature, the higher the ammonia concentration, the higher the pressure at the downstream end of the turbine, and the lower the ammonia concentration at the downstream end of the turbine, There is a problem in that the amount of evaporation of the working fluid is small and the power generation amount is small.

It is an object of the present invention to provide an apparatus for switching thermal energy capable of achieving a low pressure at the rear end of a turbine while achieving a high pressure at the front end of the turbine.

It is also an object of the present invention to provide an apparatus for converting thermal energy capable of adjusting the concentration of the working fluid so as to provide a uniform output according to the temperature of an external heat source or cooling fluid.

It is also an object of the present invention to provide a device for converting thermal energy of a structure in which heat energy from a heat source is used to heat a fluid having a low boiling point, without the need for additional cooling water.

The present invention is to achieve the above object, and provides an apparatus for converting the following thermal energy.

The present invention is an apparatus for converting thermal energy using a working fluid in which two evaporators, energy conversion means, a condenser and a first pumping means are connected and two or more different boiling points are mixed, and evaporated between the evaporator and the energy conversion means. A first separator receiving the working fluid and separating the first thick and the first lean streams; A first heat exchanger positioned in front of the evaporator and configured to exchange heat between the working fluid before condensation and the working fluid passing through the first pumping means; A second separator positioned between the heat exchanger and the evaporator to receive a heat exchange working fluid to separate the second rich stream and the second lean stream; The second lean flow merges with the first lean flow or the working fluid or branches to join the second rich stream, and a second heat exchanger condenses the working fluid with the second lean flow and the second rich stream joined. ; And a second pumping means for pumping a working fluid to a high pressure at a rear end of the second heat exchanger, wherein in the second heat exchanger, the working fluid in which the second lean stream and the second rich stream are combined is provided with a first pumping means. Provided is a device for converting thermal energy that exchanges heat with a passing working fluid.

At this time, the first heat exchanger may be disposed between the condenser and the confluence point where the second lean flow, the first lean flow and the consumable working fluid passing through the energy conversion means join.

The first lean flow separated from the first separator may include a third heat exchanger in which the working fluid having passed through the second pumping means exchanges heat, and a part of the working fluid having passed through the first pumping means may be disposed. It may be supplied to the second heat exchanger, and the rest may be supplied to the first heat exchanger.

At this time, the working fluid heated while passing through the first pumping means and the second heat exchanger joins the working fluid before passing through the first heat exchanger, or a part joins the working fluid before passing through the first heat exchanger, 1 Can join working fluid that has passed through the heat exchanger.

The present invention is to solve the above problems, while achieving a high pressure at the front end of the turbine, it is possible to provide a device for converting thermal energy capable of high efficiency by achieving a low pressure at the rear end of the turbine.

In addition, the present invention can provide a device for converting thermal energy capable of adjusting the concentration of the working fluid so as to provide a uniform output depending on the temperature of the external heat source or the cooling fluid.

In the present invention, placing the first heat exchanger between the confluence point and the condenser is advantageous for heat exchange due to the rich flow rate in the first heat exchanger due to the confluence of the rich and lean flows in the turbine.

In addition, the present invention can reduce the amount of cooling water by reducing the amount of cooling water by not using the additional cooling water in the second heat exchange and reduce the size of the cooling tower.

1 is a block diagram of a conventional Rankine cycle.
2 is a configuration diagram of a conventional carina cycle.
3 is a schematic diagram of an apparatus for converting heat energy according to the present invention.
4 is another schematic diagram of an apparatus for converting heat energy according to the present invention.

Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings.

In the embodiment of the present invention, a mixture of water and ammonia is used as the working fluid, but the present invention corresponds to the working fluid of the present invention when two or more kinds of fluids having different boiling points are mixed and used.

In the cycle of converting thermal energy, electric power is produced by a generator connected to an energy conversion means such as a turbine. In the turbine, the amount of energy generated is determined by the difference between the pressure at the input side and the pressure at the output side. The efficiency of the cycle can be improved if the pressure can be increased or the pressure at the output side can be reduced.

In general, the pressure at the input is determined by the pressure pumped by the pump, which is connected to the evaporating temperature, so that the pressure in the cycle using water and ammonia as the heat source for the working fluid is increased. There is a limit. However, when a mixture of water and ammonia is used as the working fluid, the lower the ammonia concentration, the lower the condensation at the same temperature, the lower the pressure at the downstream and the output side of the turbine.

Thus, even if the pressure at the rear end of the turbine is lowered, the pressure at the front end of the turbine does not change, so that the pressure difference between the front end and the rear end of the turbine is increased, so that the amount of energy that the turbine can switch is increased, thus increasing the efficiency.

In the present invention, when using water and ammonia as the working fluid, it is possible to condense at a lower pressure when there is a lot of water, so that some or all of the liquid working fluid containing a lot of water in the primary heated working fluid through the separator Is circulated to the rear end of the turbine, and the remainder is saturated through the evaporator and then fed to the turbine to generate power, thereby lowering the pressure at the rear end of the turbine, thereby improving cycle efficiency.

In addition, the pumping is carried out in two stages, and the first stage is pumped and then heated first to circulate a lean stream containing a lot of water to the rear stage of the turbine, and the remainder is secondary pumped after condensation, and is provided to the turbine via an evaporator. Secondarily separated after the evaporator, the overcondensed ammonia gas component is separated and fed to the turbine, and the liquid component is fed to the heat exchanger for use as a heat source for primary heating.

3 is a block diagram of a cycle for converting the thermal energy of the present invention.

The working fluid, which is a mixture of water and ammonia, is the same concentration after confluence 180 and before condenser 120, first heat exchanger 125, and before entering second separator 165 (201, 202, 203). Has

The working fluid 201 condensed in the condenser 120 is pumped to a high pressure by the pump 130 to produce a high pressure working fluid 202. The high pressure working fluid 202 exchanges heat with the one lean stream 218 in the first heat exchanger 125, some of which phase changes into gas to become the elevated temperature working fluid 203.

The elevated temperature working fluid 203 flows into the second separator 165 where gas / liquid is separated. The gas side becomes a second thick stream 204 having a high concentration of ammonia, that is, a low boiling point fluid, and the liquid side becomes a second lean stream 205 having a high concentration of water, that is, a high boiling point fluid.

The second lean stream 205 branches into a second lean stream 206 joining the second thick stream 204 and a second lean stream 207 joining the first lean stream 218. At this time, the second lean flow 206 is adjusted by the flow rate control valve 174 before the second confluence 176 joins the second rich stream 204. This is to adjust the concentration of the working fluid 212 to the evaporator 140 may be changed in conjunction with the temperature of the hot liquid entering the evaporator 140 or the low temperature liquid entering the condenser 120.

In addition, the second lean flow 207 joining the first lean flow 219 is the first lean flow 219 at the confluence 180 after the pressure is lowered to low pressure at the second throttle valve 175. ) And the spent rich 217. At this time, the second throttle valve 175 is connected to the liquid level controller 195 that senses the liquid level of the second separator 165, and thus the second lean flow 207 of the second confluence 179 joining the first confluence 179. The amount can also be adjusted.

On the other hand, the working fluid 209 joined with the second rich stream 204 in the confluence 176 passes through the evaporator 140 and exchanges heat with the heat source fluid to become the evaporating working fluid 213. Evaporative working fluid 213 flows into the first separator 160 and is separated into a first thick stream 214 and a first lean stream 215 in the first separator 160. The first separator 160 prevents the turbine 150 from being damaged when liquid is introduced into the turbine 150, and the evaporator 140 after the second lean flow 206 is joined at the confluence 176. The working fluid, which has not passed through the but not vaporized, is separated into the first lean flow 215.

The first enriched stream 214 separated from the first separator 160 is fed to an energy conversion means such as turbine 150, whereby the first enriched stream 214 in the turbine 150 has a pressure drop, thereby Chemical energy is converted into mechanical energy. Energy conversion means such as turbine 150 may be connected to a generator, to produce electricity from the converted mechanical energy. In addition, the first rich stream 214 becomes a spent rich stream 217 in which energy is consumed while passing through the turbine 150.

On the other hand, the first lean flow 215 separated from the first separator 160 drops to a low pressure while passing through the first throttle valve 170 to become the first lean flow 218 of low pressure. At this time, the first throttle valve 170 is connected to the liquid level controller 190 for detecting the liquid level of the first separator 160, thereby adjusting the amount of the first lean flow (216).

The low pressure first lean flow 218 passing through the first throttle valve 170 heats the working fluid 202 as it passes through the first heat exchanger 125, after which the first lean at the confluence 180. Joins the stream 209 and the spent rich stream 217 to become the working fluid 220.

In the embodiment of FIG. 3, a second separator 165 and a first heat exchanger 125 are included to separate the second lean stream 205 and the second thick stream 204 with the second separator 165. The concentration of the working fluid supplied to the evaporator 140 can be adjusted through the flow control valve 174 which controls the confluence of the second lean stream 205 and the portion 206 of the second thick stream 204. have.

In addition, by forming a low concentration of the working fluid on the condenser 120 side, the pressure at the rear end of the turbine 150 is lowered, thereby high power can be obtained for the same heat source.

4 is another configuration diagram of a cycle for converting thermal energy of the present invention.

The working fluid, which is a mixture of water and ammonia, from the third confluence unit 180 to the first heat exchanger 125 and the condenser 120 before being introduced into the second separator 165 (201, 202, 203). Have the same concentration.

The working fluid 201 condensed in the condenser 120 is pumped to medium pressure by the pump 130 to produce the medium pressure working fluid 202. The medium pressure working fluid 202 heat exchanges in the first heat exchanger 125, and partly phase changes into a liquid to become the elevated pressure medium working fluid 203.

The medium pressure working fluid 202 is partially branched 222 to cool the working fluid 209 in the second heat exchanger 185. The branched medium pressure working fluid 222 is elevated while passing through the second heat exchanger 185, depending on the temperature, partly joins the elevated medium pressure working fluid 203, and the other part 224 again is the medium pressure working fluid 202. To join).

The elevated pressure medium working fluid 203 flows into the second separator 165, and gas / liquid is separated from the second separator 165. The gas side becomes a second thick stream 204 having a high concentration of ammonia, that is, a low boiling point fluid, and the liquid side becomes a second lean stream 205 having a high concentration of water, that is, a high boiling point fluid.

The second lean 205 branches into the second lean 206 joining the second thick stream 204 and the second lean 207 joining the first lean stream 218. At this time, the second lean flow 206 is adjusted by the flow rate control valve 174 before the second confluence 176 joins the second rich stream 204. This is to adjust the concentration of the working fluid 212 to the evaporator 140 may be changed in conjunction with the temperature of the hot liquid entering the evaporator 140 or the low temperature liquid entering the condenser 120.

In addition, the second lean flow 207 joining the first lean flow 218 is the first lean flow at the first confluence 179 after the pressure is lowered to low pressure at the second throttle valve 175. Join (218). At this time, the second throttle valve 175 is connected to the liquid level controller 195 that senses the liquid level of the second separator 165, and thus the second lean flow 207 of the second confluence 179 joining the first confluence 179. The amount can also be adjusted.

On the other hand, the working fluid 209 joined with the second rich stream 204 at the second confluence 176 passes through the second heat exchanger 185 before being pumped to a high pressure, and is all phase-changed into liquid. This is because pressurization may be difficult when gas and liquid are mixed, but if a pump capable of gas-liquid mixing pumping is used, the second heat exchanger 185 may not be used. The low temperature fluid may be used for the second heat exchanger 185, and the medium pressure working fluid 202 before recycling the low temperature fluid passed through the condenser 120 or passing the first heat exchanger 125 to prevent unnecessary load. It is also possible to heat exchange with.

Thus, the liquid working fluid 210, which is all liquid while passing through the second heat exchanger 185, is pressurized to a desired high pressure by the pump 135, which is an additional pumping means, to become a high pressure working fluid 211. The high pressure working fluid 211 is preheated while exchanging heat with the first lean flow 215 in the third heat exchanger 145 to become the elevated high pressure working fluid 212.

The elevated temperature high pressure working fluid 212 exchanges heat with the heat source fluid while passing through the evaporator 140 to become the evaporating working fluid 213. The evaporating working fluid may evaporate entirely, but some liquids may not evaporate when using a medium temperature heat source, and in particular when using a waste heat source, the amount of heat provided by the heat source may not be constant ( Change in temperature or change in heat source flow rate).

Evaporative working fluid 213 flows into the first separator 160 and is separated into a first thick stream 214 and a first lean stream 215 in the first separator 160. In the case of the first separator 160, it may be unnecessary when all liquids are evaporated in the evaporator 140, but as described above, in the low-temperature power generation, the amount of heat provided by the waste heat source may not be constant, and the amount of heat is insufficient. It is preferable to include the first separator 160 because there is a part of the liquid, and the actuator including the part of the liquid may seriously damage the blade of the turbine 150 when it is introduced into the turbine 150. .

On the other hand, the first rich stream 214 separated from the first separator 160 is supplied to an energy conversion means such as the turbine 150, the first rich stream 214 in the turbine 150 is a pressure drop, This converts chemical energy into mechanical energy. Energy conversion means such as turbine 150 may be connected to a generator, to produce electricity from the converted mechanical energy. In addition, the first rich stream 214 becomes a spent rich stream 217 in which energy is consumed while passing through the turbine 150.

Alternatively, the first lean stream 215 separated from the first separator 160 may heat up the high-pressure working fluid 211 while passing through the third heat exchanger 145 and the first lean stream 216 having a lower temperature. ) The first lean flow 216 drops to a low pressure while passing through the first throttle valve 170 to become the first lean flow 218 of low pressure. At this time, the first throttle valve 170 is connected to the liquid level controller 190 for detecting the liquid level of the first separator 160, thereby adjusting the amount of the first lean flow (216).

The low pressure first lean flow 218 passing through the first throttle valve 170 joins the second lean flow 208 at the first confluence portion 179 to become a lean flow 219. The lean flow 219 joins the spent rich stream 217 in the third confluence portion 180 to become the working fluid 220.

In the present exemplary embodiment, the first confluence unit 179 and the third confluence unit 180 are represented by different points, but the present invention is not limited thereto. 219, the second lean stream 208 and the spent rich stream 217 may meet together.

The working fluid 220 exchanges heat with the medium pressure working fluid 202 in the first heat exchanger 125 to become a working fluid 221 whose temperature has fallen. Placing the first heat exchanger between the confluence point and the condenser is because when the rich and lean flows in the turbine are combined, the temperature may be somewhat lower, but the flow rate is abundant. It is possible for heat exchange to occur sufficiently. As the heat exchange is performed well in the first heat exchanger 125, the amount of the second rich stream 204 of the second separator 165 is increased, so that the second lean stream 205 having low concentration of ammonia is first lean stream. 218 may be joined. Meanwhile, the working fluid 221 passing through the first heat exchanger 125 passes through the condenser 120 to become the working fluid 201 and completes one cycle. After that, the cycle described above is continuously completed.

In the present invention, the working fluid 201 is pressurized to medium pressure and then passed through the first heat exchanger 125 and then passed through the second separator 165 to the second lean stream 205 and the second thick stream 204. Isolate. This is accomplished by separating and separating the medium pressure working fluid 202 with the thermal energy of the working fluid 220 passing through the turbine 150 or the third heat exchanger 145, thereby separating the second rich stream 204 or the second rich stream. Not only can a high concentration of the working fluid 209 be mixed with some of the second lean 206 in 204, but it is also possible to maintain a relatively low concentration of the working fluid 221 in the condenser 120. .

Thus, making a low concentration of the working fluid 221 in the condenser 120 is to lower the pressure in the condenser 120, which is to increase the pressure difference between the front end and the rear end of the turbine 150. The larger the pressure difference between the front end and the rear end of the turbine 150, the more the turbine 150 is to do more work, a greater amount of power generation is possible. This is because when the pressure and temperature of the front end of the turbine 150 are the same, the turbine 150 undergoes an isentropic process, and thus the output is proportionally improved according to the pressure drop width.

For example, a pressure of 3.8 bar is applied at 32 ° C at 50% ammonia concentration. When the concentration of ammonia is about 70%, the temperature must be lowered to 8 ° C to produce 3.8 bar. If the concentration of ammonia is around 70%, if it is condensed at 32 ° C, a pressure of 8.1 bar is applied.

If the temperature of the first rich stream 214 in front of the turbine 150 is 142 ° C. and the pressure is 30 bar, the efficiency of about 10.21% is obtained when the pressure in the rear end of the turbine 150 is 8.1 bar. When the temperature / pressure of the first thick stream 214 at the front end is the same, the efficiency may increase to 15.49% when the rear end pressure of the turbine 150 is 3.8 bar.

In the second heat exchanger, the working fluid 210 can be sufficiently condensed even when the working fluid 223 is used without utilizing low temperature cooling water. Because if the ammonia concentration of the working fluid 210 is 80%, it condenses at 40 ^o C at 12 bar and fully condensed at 50 ^o C at 16 bar. That is, if the temperature of the working fluid 223 is 30 ^° C level can be sufficiently cooled. Therefore, the pump 130 may select the pump boosting standard according to the required temperature. By not using the cooling water has the advantage of reducing the amount of cooling water by reducing the amount of cooling water pump and cooling tower size.

Since the pressure at the rear end of the turbine 150 is dependent on the pressure of the working fluid passing through the condenser 120, when the concentration of the working fluid passing through the condenser 120 and the temperature is 50% is 50%, the pressure of the turbine is 3.8 bar. If the concentration of the working fluid is 70% is passed through the working condenser 120, the temperature is lowered to 8.1bar on the rear end of the turbine 150 (the temperature of the working fluid passing through the condenser is 32). In degrees Celsius).

Therefore, by lowering the concentration of the working fluid passed through the condenser 120, high efficiency can be achieved. For this purpose, the concentration of the low boiling point fluid in the working fluid passed through the condenser 120 is preferably less than 50%.

In addition, in the present invention, the pressure is divided into medium pressure / high pressure, and since the ammonia may be evaporated even at a low temperature at medium pressure, it is possible to evaporate even by heat exchange in the first heat exchanger 125 instead of the evaporator 140, and the second pressure. By passing through separator 165, a high concentration of working fluid can be provided to evaporator 140. In addition, even when the concentration of the working fluid 201 is low, the concentration of the working fluid flowing into the evaporator 140 and the turbine 150 may be high.

The medium concentration of the ammonia working fluid in the second confluence portion 176 is 90% ammonia concentration, wherein the temperature and pressure of the second heat exchanger 185 is 38 ^o C or less, 15 bar or more is preferable for the efficiency of the cycle. That is, the pump 130 should be boosted to 15 bar level and cooled in the second heat exchanger 185 using a low ammonia concentration working fluid 209 below 38 ^° C.

In addition, according to the present invention, the ammonia concentration in the working fluid can be adjusted according to the temperature and fluid amount of the heat source fluid flowing into the evaporator 140, and the temperature of the cooling fluid, thereby causing a cycle problem due to external factors. Alternatively, changes in efficiency can be minimized.

That is, when the temperature of the external heat source is low, the flow rate control valve 174 is closed to increase the concentration of ammonia, and when the temperature of the external heat source is high, the flow rate control valve 174 is opened to open the second lean flow 206. When the second rich stream 204 is mixed and supplied to lower the concentration of ammonia, the output is increased, which is advantageous for stabilizing the power generation output.

Although the above has been described with reference to specific embodiments of the present invention, the present invention is not limited to d, but can be modified in various forms.

For example, two or three fluids other than water and ammonia may be used as the working fluid, and the position of the third heat exchanger 145 may be located at various positions in view of regenerating the energy of the first lean stream 215. Can be deployed.

Similarly, the first heat exchanger 125 may also be configured to exchange heat with a heat source that is discarded through regeneration heat or the evaporator if it is possible to adjust the concentration of the working fluid before the evaporator 140.

120: condenser 125: first heat exchanger
130, 135: Pump 140: Evaporator
145: third heat exchanger 150: turbine
160: first separator 165: second separator
170: first throttle valve 174: flow control valve
175: second throttle valve 176: second confluence
179: first joining unit 180: third joining unit
190: first liquid level controller 195: second liquid level controller

Claims (6)

An apparatus for converting thermal energy using a working fluid mixed with two fluids having two or more boiling points connected to an evaporator, an energy conversion means, a condenser and a first pumping means,
A first separator for receiving an evaporative working fluid between the evaporator and the energy conversion means and separating the evaporated working fluid into a first enriched stream and a first diluent;
A first heat exchanger positioned in front of the evaporator and configured to exchange heat between the working fluid before condensation and the working fluid passing through the first pumping means;
A second separator positioned between the heat exchanger and the evaporator to receive a heat exchange working fluid to separate the second rich stream and the second lean stream; The second lean is branched to join the first lean and the working fluid or to join the second rich stream,
A second heat exchanger for condensing the working fluid in which the second diluent and the second rich stream are combined; And
A second pumping means for pumping a working fluid to a high pressure at a rear end of the second heat exchanger,
And wherein in the second heat exchanger, a working fluid in which the second lean stream and the second rich stream are joined converts thermal energy to exchange heat with the working fluid passed through the first pumping means. The method of claim 1,
And the first heat exchanger is disposed between the condenser and the confluence point at which the second lean flow, the first lean flow and the spent working fluid passing through the energy conversion means join. 3. The method according to claim 1 or 2,
And a third heat exchanger for heat exchange between the first lean flow separated from the first separator and the working fluid passing through the second pumping means. 3. The method according to claim 1 or 2,
A portion of the working fluid passing through the first pumping means is supplied to the second heat exchanger and the remainder is supplied to the first heat exchanger. 5. The method of claim 4,
And the working fluid heated while passing through the first pumping means and the second heat exchanger joins the working fluid before passing through the first heat exchanger. 5. The method of claim 4,
A portion of the working fluid heated up while passing through the first pumping means and the second heat exchanger joins the working fluid before passing through the first heat exchanger, and the remaining part joins the working fluid passed through the first heat exchanger. Device to switch.

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