KR101864983B1 - Supercritical CO2 power generating system - Google Patents

Supercritical CO2 power generating system Download PDF

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Publication number
KR101864983B1
KR101864983B1 KR1020170010866A KR20170010866A KR101864983B1 KR 101864983 B1 KR101864983 B1 KR 101864983B1 KR 1020170010866 A KR1020170010866 A KR 1020170010866A KR 20170010866 A KR20170010866 A KR 20170010866A KR 101864983 B1 KR101864983 B1 KR 101864983B1
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South Korea
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working fluid
recuperator
supplied
pump
heat exchanger
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KR1020170010866A
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Korean (ko)
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차송훈
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두산중공업 주식회사
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    • 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
    • F01K25/08—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 special vapours
    • F01K25/10—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 special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • F01K25/103—Carbon dioxide
    • 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
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
    • 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
    • F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
    • F01K7/32—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines using steam of critical or overcritical pressure

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

The present invention relates to a supercritical carbon dioxide generating system to improve heat exchange efficiency and cycle efficiency. According to the present invention, when forming a cycle, the cycle is formed in the shape of a recompression closed Brayton cycle (RCBC), and as a flow rate of a working fluid heated in a high temperature recuperator is distributed, heat exchange efficiency of the recuperator is improved, and further, additional heat absorption is possible. Therefore, efficiency of the whole cycle can be improved.

Description

[0001] Supercritical CO2 power generating system [0002]

The present invention relates to a supercritical carbon dioxide power generation system, and more particularly, to a supercritical carbon dioxide power generation system capable of improving heat exchange efficiency and cycle efficiency.

Internationally, there is a growing need for efficient power generation. As the movement to reduce the generation of pollutants is becoming more and more active, various efforts are being made to increase the production of electricity while reducing the generation of pollutants. Research and development of a supercritical carbon dioxide power generation system using supercritical carbon dioxide as a working fluid has been promoted as disclosed in Registration No. 8869531. [

Since supercritical carbon dioxide has a gas-like viscosity at a density similar to that of a liquid state, it can minimize the power consumption required for compression and circulation of the fluid as well as miniaturization of the apparatus. At the same time, the critical point is 31.4 degrees Celsius, 72.8 atmospheres, and the critical point is much lower than the water at 373.95 degrees Celsius and 217.7 atmospheres, which is easy to handle. The supercritical carbon dioxide power generation system has a net generation efficiency of about 45% when operated at a temperature of 550 ° C. and has an advantage of improving the generation efficiency of the steam cycle by 20% or more and reducing the turbo device.

The conventional supercritical carbon dioxide power generation system as described above has one external heat exchanger that receives heat from an external heat source and heats the working fluid. However, when the number of external heat exchangers is one, the working fluid flow rate of the high temperature recuperator and the working fluid flow rate of the external heat exchanger can not be efficiently distributed, which is inefficient in terms of heat exchange.

US Patent No. 8869531 (Registered on Apr. 10, 2014)

It is an object of the present invention to provide a supercritical carbon dioxide power generation system capable of improving heat exchange efficiency and cycle efficiency.

A supercritical carbon dioxide power generation system of the present invention is an RCBC (Recompression Closed Bray Cycle) for recompressing a working fluid among supercritical carbon dioxide power generation systems in which supercritical carbon dioxide is used as a working fluid to produce electric energy, A plurality of recuperators for firstly heating the working fluid that has passed through the pump and a plurality of heat exchangers for reheating the working fluid heated by the recuperator using the waste heat as a heat source, A turbine for driving the pump and the generator, the turbine being connected to the tiller, the pump, and the generator for producing the electric energy in a single shaft, and a heat exchanger for supplying heat to the working fluid through the pump after being supplied to the recuperator And a condenser for cooling the working fluid cooled by the circulation pump On side liqueur and a portion of the working fluid supplied to the buffer radar it characterized in that the heating branches of any one of the heat exchanger.

And the working fluid heated by branching to any one of the heat exchangers is supplied to a front end of the high temperature side recuperator and mixed with the working fluid passed through the pump.

And the working fluid is branched from a downstream end of the low temperature side pump of the pump and is supplied to any one of the heat exchangers.

The working fluid branched from the low temperature side pump and supplied to the low temperature side recuperator of the recuperator is mixed with the working fluid passed through the pump at the front end of the point where the working fluid heated in the heat exchanger is mixed, .

And the working fluid heated by branching to any one of the heat exchangers is supplied to the rear end of the high temperature side recuperator and mixed with the working fluid passed through the high temperature side recuperator.

And the working fluid is branched at a front end of the recuperator and supplied to one of the heat exchangers.

And the working fluid passing through the high temperature side recuperator is supplied to another one of the heat exchangers and reheated and then supplied to the turbine.

The heat exchanger may include any one of a high temperature heat exchanger that performs heat exchange with the high temperature waste heat gas, a medium temperature heat exchanger that performs heat exchange with the middle or low temperature waste gas, or a low temperature heat exchanger.

And the working fluid passing through the high temperature side recuperator is supplied to the high temperature heat exchanger.

And the working fluid branched to any one of the heat exchangers is branched into the mesothermal heat exchanger or the low temperature heat exchanger.

The present invention also relates to a recompression closed cycle cycle (RCBC) system for recompressing the working fluid in a supercritical carbon dioxide power generation system in which supercritical carbon dioxide is used as a working fluid to produce electric energy, Two recuperators for sequentially heating the working fluid that has passed through the pump, a plurality of heat exchangers for reheating the working fluid heated by the recuperator using waste heat as a heat source, A second turbine for driving the pump, a second turbine for driving the pump, a heat exchanger for exchanging heat with the working fluid that has been supplied to the recuperator through the turbine and then through the pump, And a condenser for cooling the working fluid, wherein the high- A portion of the working fluid supplied to is characterized in that the heating branches of any one of the heat exchanger.

And the working fluid heated by branching to any one of the heat exchangers is supplied to a front end of the high temperature side recuperator and mixed with the working fluid passed through the pump.

And the working fluid is branched from a downstream end of the low temperature side pump of the pump and is supplied to any one of the heat exchangers.

The working fluid branched from the low temperature side pump and supplied to the low temperature side recuperator of the recuperator is mixed with the working fluid passed through the pump at the front end of the point where the working fluid heated in the heat exchanger is mixed, .

And the working fluid heated by branching to any one of the heat exchangers is supplied to the rear end of the high temperature side recuperator and mixed with the working fluid passed through the high temperature side recuperator.

And the working fluid is branched at a front end of the recuperator and supplied to one of the heat exchangers.

And the working fluid passing through the high temperature side recuperator is supplied to another one of the heat exchangers and reheated and then supplied to the turbine.

The heat exchanger may include any one of a high temperature heat exchanger that performs heat exchange with the high temperature waste heat gas, a medium temperature heat exchanger that performs heat exchange with the middle or low temperature waste gas, or a low temperature heat exchanger.

And the working fluid passing through the high temperature side recuperator is supplied to the high temperature heat exchanger.

And the working fluid branched to any one of the heat exchangers is branched into the mesothermal heat exchanger or the low temperature heat exchanger.

The supercritical carbon dioxide power generation system according to an embodiment of the present invention is configured in the form of RCBC in the cycle configuration and the flow rate of the working fluid heated in the high temperature recuperator is divided to improve the heat exchange efficiency of the recuperator, . Thus, the efficiency of the entire cycle is improved.

1 is a schematic diagram showing an RCBC of a supercritical carbon dioxide power generation system according to an embodiment of the present invention,
FIG. 2 and FIG. 3 are schematic diagrams showing a modification of the supercritical carbon dioxide power generation system of FIG. 1,
FIG. 4 is a schematic diagram showing an RCBC of a supercritical carbon dioxide power generation system according to another embodiment of the present invention;
FIGS. 5 and 6 are schematic views showing a modification of the supercritical carbon dioxide power generation system of FIG.
7 shows a TQ diagram of a conventional LCBC-based liquefier with a single recuperator,
8 is a TQ diagram of a recuperator according to the RCBC of the present invention,
9 shows a TQ diagram of an external heat exchanger according to a conventional RCBC with a single recuperator,
10 is a TQ diagram of the external heat exchanger according to the RCBC of the present invention.

Hereinafter, a supercritical carbon dioxide power generation system according to an embodiment of the present invention will be described in detail with reference to the drawings.

Generally, a supercritical carbon dioxide power generation system forms a closed cycle that does not discharge the carbon dioxide used for power generation to the outside, and uses supercritical carbon dioxide as a working fluid to construct a single phase power generation system.

Since the supercritical carbon dioxide power generation system uses carbon dioxide as the working fluid, it can be used not only in a single power generation system but also in a hybrid power generation system with a thermal power generation system, since exhaust gas discharged from a thermal power plant can be used. The working fluid of the supercritical carbon dioxide power generation system may separate carbon dioxide from the exhaust gas and supply the carbon dioxide separately.

The working fluid in the cycle is supercritical carbon dioxide, which passes through a heat source such as a compressor and a heater, and becomes a high-temperature high-pressure working fluid, and supercritical carbon dioxide fluid drives the turbine. The turbine is connected to a generator, which is driven by the turbine to produce power. Alternatively, a turbine and a compressor may be coaxially connected, and a compressor may be provided with a gear box or the like to connect the generator. The working fluid used for the production of electric power is cooled through a heat exchanger such as a heat exchanger and a precooler, and the cooled working fluid is supplied to the compressor again to circulate in the cycle. A plurality of turbines or heat exchangers may be provided.

The supercritical carbon dioxide power generation system according to various embodiments of the present invention includes not only a system in which all of the working fluid flowing in a cycle is in a supercritical state but also a system in which most of the working fluid is supercritical and the rest is subcritical It is used as a meaning.

Also, in various embodiments of the present invention, carbon dioxide is used as the working fluid, wherein carbon dioxide refers to pure carbon dioxide in the chemical sense, carbon dioxide in a state where the impurities are somewhat contained in general terms, and carbon dioxide in which at least one fluid is mixed Is used to mean a fluid in a state where the fluid is in a state of being fluidized.

In the present invention, cycles are formed based on a recompression closed-brayton cycle (RCBC). The power generation cycle of the present invention is to propose a supercritical carbon dioxide power generation system composed of a pair of recuperators, a plurality of external heat exchangers, one or more turbines connected in a single shaft or a separate shaft, and a plurality of pumps and a single condenser do.

1 is a schematic diagram showing an RCBC of a supercritical carbon dioxide power generation system according to an embodiment of the present invention.

1, the supercritical carbon dioxide power generation system according to an embodiment of the present invention is based on RCBC having two compressors or compressors 100 for compressing a working fluid, and two external heat exchangers 300, A turbine 400 for driving the pump or compressor 100, a generator 430 driven by the turbine 400, and a condenser 500 for cooling the working fluid. (Hereinafter, a pump will be described as an example for convenience).

Each configuration of the present invention is connected by a transfer pipe through which a working fluid flows (a line corresponding to the numbers 1 to 26 in FIG. 1 represents a transfer pipe), and the working fluid flows through the transfer pipe . However, in the case where a plurality of components are integrated, it is to be understood that the working fluid flows along the conveying pipe, as a matter of course, since there will be a part or region which actually functions as a conveying pipe in the integrated structure. In the case of a separate functioning channel, a further description will be given. The flow of the working fluid will be described by describing the number of the conveying pipe.

In addition, since the temperature or pressure of the working fluid described in the present invention is described by taking one of the cases as an example, it should not be understood as an absolute value.

The details of the cycle are as follows.

The pump 100 includes a first pump 110 and a second pump 130. The first pump 110 and the second pump 130 may be arranged in parallel and one turbine 400 drives the generator 430 and both the first pump 110 and the second pump 130 . However, it is also possible to drive the first pump 110 and the second pump 130 with separate motors.

The recuperator 200 is composed of a first recuperator 230 and a second recuperator 210. The recirculator 230 and the second recuperator 210 are arranged in series so that the working fluid, which has passed through the first recuperator 230, And then flows into the purifier 210 sequentially.

The heat exchanger 300 may include a plurality of heat exchangers 310 and a second heat exchanger 330 as needed. The first and second heat exchangers 310 and 330 use a gas having waste heat (hereinafter referred to as a waste heat gas) such as exhaust gas discharged from a boiler of a power plant as a heat source, and a waste heat gas and a working fluid circulating in the cycle, And serves to heat the working fluid with the heat supplied from the waste heat gas.

When a plurality of heat exchangers 300 are provided, they can be classified into low temperature, medium temperature, and high temperature depending on the temperature of the waste heat gas. That is, as the heat exchanger is closer to the inlet end where the waste heat gas is introduced, heat exchange can be performed at a higher temperature, and heat exchange at a lower temperature becomes closer to the outlet end where the waste heat gas is discharged.

In the present embodiment, the first heat exchanger 310 is a heat exchanger using relatively high temperature or medium temperature waste heat gas as compared with the second heat exchanger 330, and the second heat exchanger 330 is a relatively high temperature or low temperature It may be a heat exchanger using waste heat gas. That is, the first heat exchanger 310 and the second heat exchanger 330 are sequentially arranged from the inlet end to the exhaust end where the waste heat gas flows, will be described as an example.

The turbine 400 is driven by a working fluid and serves to generate electric power by driving a generator 430 connected to the turbine 400. Since the working fluid is expanded while passing through the turbine 400, the turbine 400 also functions as an expander. The generator 430 and the plurality of pumps 100 are connected to the turbine 400 in a single shaft and the generator 430 and the pump 100 are driven by the turbine 400.

The condenser 500 serves as a cooler that passes through the recuperator 200 using air or cooling water as a refrigerant, and secondarily cools the primary cooling fluid. The working fluid cooled through the condenser 500 is supplied to the first pump 110 and some working fluid is branched to be supplied to the second pump 130 before being introduced into the condenser 500. [

The flow of the working fluid according to the cycle configuration is as follows.

 The compressed low-temperature high-pressure working fluid passing through the first pump 110 is sent to the first recuperator 230 (1), heat-exchanged in the first recuperator 230, (2). The low-temperature, high-pressure working fluid that has passed through the second pump 130 is mixed with the working fluid that has passed through the first recuperator 230, and the second recuperator 210 and the second heat exchanger 330, respectively (3A, 3B).

A part of the working fluid that has passed through the first pump 110 and the second pump 130 is branched without going to the first recuperator 210 and sent to the second heat exchanger 330 to make heat exchange with the waste heat gas It is heated first. The working fluid sent to the first recuperator 230 is heat-exchanged with the working fluid supplied to the first recuperator 230 through the (3A) turbine 400, and is heated primarily. The working fluid heated in the first recuperator 230 and the working fluid heated in the second heat exchanger 330 are mixed and supplied to the first heat exchanger 310 (4).

The working fluid flowing through the turbine 400 flows directly into the first recuperator 230 so that the working fluid having a relatively higher temperature than the second recuperator 210 flows into the first recuperator 230. However, if the flow rate of the working fluid to be heat-exchanged in the first recuperator 230 is large, it may be difficult to sufficiently raise the temperature of the working fluid within the same time. At this time, when a part of the working fluid supplied to the first recuperator 230 is branched and mixed with the working fluid heated by the first recuperator 230 in advance by the second heat exchanger 330, the turbine 400 Can quickly increase the temperature of the working fluid to be supplied. Also, since the flow rate of the working fluid supplied to the first recuperator 230 is reduced, the heat exchange efficiency of the working fluid in the first recuperator 230 is increased.

The working fluid heated and mixed in the first recuperator 230 and the second heat exchanger 330 is reheated in the first heat exchanger 310 in a high temperature environment and then supplied to the turbine 400.

The high temperature working fluid expands while passing through the turbine 400 and becomes a medium pressure working fluid. In the first recuperator 230, heat exchange is performed with the working fluid passing through the second pump 130, and the primary working fluid is cooled.

The firstly cooled working fluid is sent to the second recuperator 210 to be heat-exchanged with the working fluid that has passed through the first pump 110 and cooled again. The cooled working fluid partially branches and is supplied to the second pump 130, and the rest is supplied to the condenser 500 to be cooled.

The first recuperator 230 exchanges heat with a working fluid having a temperature relatively higher than that of the second recuperator 210 and passes through the pump 100, 500) through the second pump (130). The second recuperator 210 exchanges heat with a working fluid having a relatively lower temperature than the first recuperator 230 and a working fluid having passed through the pump 100, May be supplied through the first pump (110).

As described above, by distributing the flow rate of the working fluid heated in the hot recuperator, it is possible to improve the heat exchange efficiency of the recuperator and to enable additional heat absorption. Thus, the efficiency of the entire cycle is improved.

Hereinafter, a modified example of the above-described embodiment will be described (detailed description about the same configuration as the above-described embodiment will be omitted).

FIG. 2 and FIG. 3 are schematic diagrams showing a modification of the supercritical carbon dioxide power generation system of FIG.

As shown in FIG. 2, in constructing the cycle of the supercritical carbon dioxide power generation system, a first heat exchanger 310a using the waste heat gas having the same structure as the cycle of FIG. 1 but using a high temperature waste heat gas, The second heat exchanger 330a can be constructed.

At this time, the low-temperature high-pressure working fluid passing through the first pump 110a is branched at the rear end of the first pump 110a and supplied to the second recuperator 210a and the second heat exchanger 330a (1, 2B). The working fluid supplied to the second recuperator 210a is firstly heated by the second recuperator 210a and then supplied to the rear end of the second pump 130a (2A). The working fluid supplied to the second heat exchanger 330a flows through the second pump 130a and the working fluid passing through the first recuperator 230a after being heat-exchanged with the waste heat gas of relatively low temperature (2B) Is passed after the point where the working fluid that has passed through it is mixed.

The working fluid having passed through the second pump 130a is first mixed with the working fluid heated in the first recuperator 230a and then mixed with the working fluid heated in the second heat exchanger 330a, And supplied to the recuperator 230a (3). Exchanged with the working fluid that has passed through the turbine 400a in the first recuperator 230a and then sent to the first heat exchanger 310a (4).

The working fluid heated to a high temperature in the first heat exchanger 310a is supplied to the turbine 400a to drive the turbine 400a and the working fluid that has passed through the turbine 400a flows through the first recuperator 230a ) And the second recuperator (210a). The working fluid that has passed through the second recuperator 210a branches from the front end of the condenser 500a and is supplied to the second pump 130a and the condenser 500a respectively (9B, 9).

In the embodiment of FIG. 1, the working fluid supplied to the first recuperator 230 is partially branched and heated and then mixed at the front end of the first heat exchanger 310 to be finally heated. In the embodiment of FIG. 2, There is a difference in that the working fluid fed to the recuperator 230a is branched in advance and heated by the second heat exchanger 330a to be supplied to the first recirculator 230a. Although there is a difference in the construction of the cycle, the effect of improving the heat exchange efficiency in the first recuperator 230a is the same.

3, the heat exchanger 300b is disposed in the high temperature, middle temperature, and low temperature regions, and the third heat exchanger 350b has the same function as the second heat exchanger 330b in FIG. 2 The working fluid heated in the third heat exchanger 350b may be mixed and then branched to the first recuperator 210b and the third heat exchanger 330b. The embodiment of FIG. 3 also has the effect of improving the heat exchange efficiency in the first recuperator 230b by previously diverting and heating the working fluid supplied to the first recuperator 230b.

In the embodiments of FIGS. 1 to 3, the cycle configuration in which the turbine for driving the pump is driven also has been described, but a cycle including the turbine for driving the generator and the turbine for driving the pump may be separately provided The detailed description of the same constitution as the embodiment will be omitted).

FIG. 4 is a schematic view showing an RCBC of a supercritical carbon dioxide power generation system according to another embodiment of the present invention, and FIGS. 5 and 6 are schematic diagrams showing a modification of the supercritical carbon dioxide power generation system of FIG.

4, the first turbine 400c is connected to the generator 430c, and the second turbine 410c is coaxially connected to the first pump 110c and the second pump 130c. The embodiment of FIG. 4 is different from the embodiment of FIG. 1 in that a cycle is constituted and a part of the working fluid supplied to the first turbine 400c is branched and supplied to the second turbine 400c .

Also, as shown in FIG. 5, the cycle may be configured in the same manner as the embodiment of FIG. 2, and a first turbine 400d and a second turbine 410d may be provided. In this case, as in the embodiment of FIG. 4, a part of the working fluid supplied to the first turbine 400d is branched and supplied to the second turbine 410d.

Alternatively, as shown in FIG. 6, a cycle may be constructed in the same manner as the embodiment of FIG. 3, and a first turbine 400e and a second turbine 410e may be provided. In this case, as in the embodiment of FIG. 4, a part of the working fluid supplied to the first turbine 400e is branched (5B) to the second turbine 410e.

The cycle shown in Figs. 4 to 6 also distributes the flow rate of the working fluid heated in the hot recuperator, as in the above-described embodiments, thereby improving the heat exchange efficiency of the recuperator and enabling further heat absorption. Thus, the efficiency of the entire cycle is improved.

Also, the shaft power required by the first pump and the second pump can be efficiently managed by adjusting the rotational speed (rpm) of the second turbine. Generally, in case of a turbine connected to a generator, it is not possible to adjust the rotational speed of the pump through the corresponding turbine because the rotational speed can not be controlled. However, there is an advantage that the rotational speed can be adjusted when a separate second turbine is driven. This makes it possible to control the power of the pump according to the variation of the heat source and the ambient temperature condition, and the efficiency is improved even in the partial load aspect.

In the supercritical carbon dioxide power generation system according to the above-described embodiments, the temperature distribution of each heat exchanger will be described as follows.

FIG. 7 is a TQ diagram of a conventional recirculator with a single recuperator; and FIG. 8 is a TQ diagram of a recuperator according to the RCBC of the present invention. FIG. 9 is a T-Q diagram of an external heat exchanger according to a conventional RCBC with a single recuperator, and FIG. 10 is a T-Q diagram of an external heat exchanger according to the RCBC of the present invention.

In FIGS. 7 and 8, the range from the zero point to about 7000 kW is the low temperature recuperator area, and the higher temperature corresponds to the high temperature recuperator area. The low temperature recuperator means a recuperator, such as the second recuperator of the above-described embodiments, which is supplied with the working fluid supplied through the turbine after passing through another recuperator. Therefore, the high temperature recuperator becomes the first recuperator.

7, in the case of a conventional RCBC having a single external heat exchanger, the hot side outlet temperature at which the high temperature working fluid is discharged from the hot recuperator and the cold side outlet temperature at which the low temperature working fluid is discharged are several tens It shows the temperature difference of the figure.

However, as shown in FIG. 8, the temperature of the cold side outlet of the hot recuperator is increased by about 10% or more by controlling the flow rate of the working fluid flowing into the hot recuperator. This means that the thermal regeneration efficiency is improved.

9 and 10, the red solid line represents the TQ heat transfer of the waste heat gas at the rear end of the boiler, and the blue solid line represents the TQ heat transfer of the working fluid supplied to the external heat exchanger. As shown in FIG. 9, in the case of the conventional RCBC having a single external heat exchanger, since the working fluid passing through the high temperature recuperator is supplied to the external heat exchanger, there is a limit to absorb heat from the external heat exchanger.

However, when a new heat exchanger is added as shown in Fig. 10 (broken line portion), since a relatively low working fluid before being passed through the high temperature recuperator is supplied to the new heat exchanger, The absorption amount is increased. Therefore, when the new heat exchanger is added, the heat transfer area of the heat exchanger can be reduced, thereby reducing the cycle construction cost. Therefore, there is an advantage that the cycle can be selectively applied to the effect of increasing the efficiency of the cycle or reducing the economic cost.

One embodiment of the present invention described above and shown in the drawings should not be construed as limiting the technical spirit of the present invention. The scope of the present invention is limited only by the matters described in the claims, and those skilled in the art can improve and modify the technical spirit of the present invention in various forms. Accordingly, it is intended that the present invention cover the modifications and variations of this invention provided they come within the scope of the appended claims and their equivalents.

100 to 100e: Pump 200 to 200e: Recuperator
300 to 300e: heat exchanger 400 to 400e, 410c to 410e: turbine
500 ~ 500e: capacitor

Claims (20)

A Recombinant Closed Brayton Cycle (RCBC) for recompressing the working fluid among supercritical carbon dioxide power generation systems using supercritical carbon dioxide as a working fluid to produce electric energy,
Two pumps for compressing and circulating the working fluid,
A plurality of recupillators for primarily heating the working fluid that has passed through the pump,
A plurality of heat exchangers which use waste heat as a heat source and reheat the working fluid heated by the recuperator,
A turbine connected to the pump and the generator for generating the electric energy in a single shaft to drive the pump and the generator,
And a condenser for cooling the working fluid cooled by heat exchange with the working fluid supplied through the turbine and supplied to the recuperator,
A part of the working fluid supplied to the high-temperature-side recirculator of the recuperator is branched to one of the heat exchangers and heated, or a part of the working fluid is supplied to the heat exchanger at a rear end of the low- And the heating is performed in one branch,
A working fluid which is branched from the working fluid supplied to the high temperature side recuperator and sent to one of the heat exchangers is sent to the rear end of the high temperature side recuperator and is branched at the rear end of the low temperature side pump, And the working fluid sent to any one of the first and second heat exchangers is sent to a front end of the high temperature side recuperator. delete delete The method according to claim 1,
The working fluid supplied to the low temperature side recuperator of the recuperator through the low temperature side pump of the pump is mixed with the working fluid passing through the high temperature side pump of the pump and then branched at the downstream end of the low temperature side pump, And the mixed gas is supplied to the high-temperature side recirculator of the recuperator. delete delete 5. The method of claim 4,
And the working fluid passing through the high temperature side recuperator is supplied to the other of the heat exchangers and reheated and then supplied to the turbine. 8. The method of claim 7,
Wherein the heat exchanger includes any one of a high temperature heat exchanger that performs heat exchange with the high temperature waste heat gas and a medium temperature heat exchanger or a low temperature heat exchanger that performs heat exchange with the middle or low temperature waste gas. 9. The method of claim 8,
And the working fluid having passed through the high temperature side recuperator is supplied to the high temperature heat exchanger. 10. The method of claim 9,
And the working fluid branched to any one of the heat exchangers is branched into the intermediate-temperature heat exchanger or the low-temperature heat exchanger. A Recombinant Closed Brayton Cycle (RCBC) for recompressing the working fluid among supercritical carbon dioxide power generation systems using supercritical carbon dioxide as a working fluid to produce electric energy,
Two pumps for compressing and circulating the working fluid,
Two recuplators for firstly heating the working fluid that has passed through the pump,
A plurality of heat exchangers which use waste heat as a heat source and reheat the working fluid heated by the recuperator,
A first turbine connected to a generator for generating the electric energy to drive the generator,
A second turbine for driving the pump,
And a condenser for sequentially cooling the first and second cooled working fluids through the first and second turbines,
A part of the working fluid supplied to the high-temperature-side recirculator of the recuperator is branched to one of the heat exchangers and heated, or a part of the working fluid is supplied to the heat exchanger at a rear end of the low- And the heating is performed in one branch,
A working fluid which is branched from the working fluid supplied to the high temperature side recuperator and sent to one of the heat exchangers is sent to the rear end of the high temperature side recuperator and is branched at the rear end of the low temperature side pump, And the working fluid sent to any one of the first and second heat exchangers is sent to a front end of the high temperature side recuperator. delete delete 12. The method of claim 11,
The working fluid supplied to the low temperature side recuperator of the recuperator through the low temperature side pump of the pump is mixed with the working fluid passing through the high temperature side pump of the pump and then branched at the downstream end of the low temperature side pump, And the mixed gas is supplied to the high-temperature side recirculator of the recuperator. delete delete 15. The method of claim 14,
Wherein the working fluid passing through the high temperature side recuperator is supplied to another one of the heat exchangers and reheated, and then supplied to one of the first turbine and the second turbine. 18. The method of claim 17,
Wherein the heat exchanger includes any one of a high temperature heat exchanger that performs heat exchange with the high temperature waste heat gas and a medium temperature heat exchanger or a low temperature heat exchanger that performs heat exchange with the middle or low temperature waste gas. 19. The method of claim 18,
And the working fluid having passed through the high temperature side recuperator is supplied to the high temperature heat exchanger. 20. The method of claim 19,
And the working fluid branched to any one of the heat exchangers is branched into the intermediate-temperature heat exchanger or the low-temperature heat exchanger.
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109026236A (en) * 2018-08-07 2018-12-18 西安热工研究院有限公司 A kind of efficient supercritical carbon dioxide hot dry rock electricity generation system
KR20210046045A (en) 2018-09-05 2021-04-27 상하이 파워 이큅먼트 리서치 인스티튜트 컴퍼니 리미티드 Compact gas-gas heat exchange tube and its manufacturing and use method
CN114198173A (en) * 2021-11-04 2022-03-18 合肥通用机械研究院有限公司 Full-backheating Brayton cycle and absorption refrigeration integrated electricity-cold combined supply system

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8869531B2 (en) 2009-09-17 2014-10-28 Echogen Power Systems, Llc Heat engines with cascade cycles
KR20160037570A (en) * 2014-09-29 2016-04-06 한국전력공사 Power Generating System Using Supercritical Carbon Dioxide
US9359919B1 (en) * 2015-03-23 2016-06-07 James E. Berry Recuperated Rankine boost cycle

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8869531B2 (en) 2009-09-17 2014-10-28 Echogen Power Systems, Llc Heat engines with cascade cycles
KR20160037570A (en) * 2014-09-29 2016-04-06 한국전력공사 Power Generating System Using Supercritical Carbon Dioxide
US9359919B1 (en) * 2015-03-23 2016-06-07 James E. Berry Recuperated Rankine boost cycle

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109026236A (en) * 2018-08-07 2018-12-18 西安热工研究院有限公司 A kind of efficient supercritical carbon dioxide hot dry rock electricity generation system
KR20210046045A (en) 2018-09-05 2021-04-27 상하이 파워 이큅먼트 리서치 인스티튜트 컴퍼니 리미티드 Compact gas-gas heat exchange tube and its manufacturing and use method
CN114198173A (en) * 2021-11-04 2022-03-18 合肥通用机械研究院有限公司 Full-backheating Brayton cycle and absorption refrigeration integrated electricity-cold combined supply system
CN114198173B (en) * 2021-11-04 2023-10-13 合肥通用机械研究院有限公司 Electric cooling combined supply system integrating full-regenerative brayton cycle and absorption refrigeration

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