KR101691908B1 - Generation system using supercritical carbon dioxide and method of driving the same by temperature differential of heat source - Google Patents

Generation system using supercritical carbon dioxide and method of driving the same by temperature differential of heat source Download PDF

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KR101691908B1
KR101691908B1 KR1020150183915A KR20150183915A KR101691908B1 KR 101691908 B1 KR101691908 B1 KR 101691908B1 KR 1020150183915 A KR1020150183915 A KR 1020150183915A KR 20150183915 A KR20150183915 A KR 20150183915A KR 101691908 B1 KR101691908 B1 KR 101691908B1
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South Korea
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carbon dioxide
compressor
heat source
turbine
discharged
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KR1020150183915A
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Korean (ko)
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이정익
김민석
백승준
조성국
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한국과학기술원
사우디 아라비안 오일 컴퍼니
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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
    • 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
    • F01K7/16—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 being only of turbine type
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
    • F02C1/02—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid the working fluid being an unheated pressurised gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C9/00—Controlling gas-turbine plants; Controlling fuel supply in air- breathing jet-propulsion plants
    • F02C9/16—Control of working fluid flow

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

Abstract

The present invention relates to a heat source (1) for heating carbon dioxide; A first compressor (5) and a second compressor (7) for pressurizing and discharging carbon dioxide; A turbine (2) into which carbon dioxide heated by the heat source (1) flows; A recuperator (3) for performing heat exchange between carbon dioxide discharged from the turbine (2) and carbon dioxide discharged from the first compressor (5) or a second compressor; A cooler (4) for cooling the carbon dioxide discharged from the turbine (2) and flowing through the heat recovery unit (3); A valve (6) for controlling the inflow of carbon dioxide discharged from the cooler (4) into the first compressor (5) or the second compressor (7); And a generator (8) connected to the turbine (2), wherein the valve controls the amount of the carbon dioxide heated by the heat source and the temperature of the carbon dioxide discharged from the first compressor or the second compressor (The pressure of the carbon dioxide discharged from the compressor) / (the pressure of the carbon dioxide flowing into the compressor), which is higher than that of the second compressor 7, and the first compressor 5 controls the inflow of carbon dioxide Pressure) of the supercritical carbon dioxide power generation system. The supercritical carbon dioxide power generation system according to the present invention has an effect of improving the thermal efficiency of the power generation system by using different compressors according to the temperature difference between the heat source and the carbon dioxide flowing into the heat source.

Description

TECHNICAL FIELD The present invention relates to a supercritical carbon dioxide power generation system and a supercritical carbon dioxide power generation system using the same,

The present invention relates to a supercritical carbon dioxide power generation system for power generation and a method of operating a supercritical carbon dioxide power generation system according to a temperature difference in a heat source. More particularly, the present invention relates to a supercritical carbon dioxide power generation system using supercritical carbon dioxide, The present invention relates to a supercritical carbon dioxide power generation system including an individual compressor used in accordance with a difference in temperature of incoming carbon dioxide and a method of operating the same.

In the existing combined cycle power generation system, the temperature of the gas turbine outlet is maintained as high as 500 to 600 ° C., and steam rankin cycle is introduced to make useful work using such high temperature waste heat. Steam Rankine cycle, despite its excellent thermal efficiency, is the problem of large volumes of heat exchangers, including steam turbines and corrosion of turbine blades when the steam expands in the turbine.

Therefore, studies on supercritical carbon dioxide Brayton cycle using carbon dioxide as a working fluid instead of the Rankine cycle using steam are actively under way. The supercritical Brayton cycle is a thermodynamic cycle in which the operating fluid remains above the critical point in all parts of the cycle and the compressor operating conditions, which are the lowest operating temperature and pressure conditions of the cycle, lie directly above the critical point.

Among the various fluids, carbon dioxide is selected as the working fluid of the supercritical Brayton cycle because the critical temperature of carbon dioxide is near room temperature and it is easy to cool and the critical pressure is lower than other working fluids. Because.

As a related art, Korean Patent Laid-Open No. 10-2015-0036899 discloses a power storage and production apparatus using supercritical carbon dioxide. The power storage and production apparatus includes a low pressure tank for storing low pressure supercritical carbon dioxide, a compressor for adiabatically compressing low pressure supercritical carbon dioxide stored in the low pressure tank and discharging the supercritical carbon dioxide to high pressure supercritical carbon dioxide, A high pressure tank for storing critical carbon dioxide, an electric motor driven by supplying surplus electric power and transmitting rotational force to the compressor, a boiler for heating and discharging supercritical carbon dioxide of high pressure stored in the high pressure tank in case of power shortage, The supercritical carbon dioxide heated by the high pressure supercritical carbon dioxide flows into the supercritical carbon dioxide, and the supercritical carbon dioxide flows into the supercritical carbon dioxide, and the rotary power is generated. .

As a related art, Korean Patent Laid-Open Publication No. 10-2014-0116504 discloses a dual cycle system for generating axial power by using supercritical fluid and fossil fuel. The first cycle is an open air breathing Brayton cycle. The second cycle is a closed supercritical fluid Brayton cycle. After air is compressed in the first cycle, compressed air flows through the first cross-cycle heat exchanger, supercritical fluid from the second cycle is compressed, then expanded in the turbine, and then flows through the first cross-cycle heat exchanger. In the first cross-cycle heat exchanger, the compressed air is heated and the expanded supercritical fluid is cooled.

Such a power generation system using carbon dioxide as a working fluid can reduce the compression work at the temperature and pressure near the critical point of carbon dioxide (30.98 ° C, 7.37 MPa), and when the temperature of the heat source is 450 to 750 ° C, The thermal efficiency of the Rankine cycle is equivalent to that of the Rankine cycle. Furthermore, since the overall size of the system is kept small, there is an advantage in that the size of the compressor, turbine, and heat exchanger, which are the main components, can be reduced. In addition, research is underway on nuclear power generation, power generation systems linked to various heat sources such as solar heat, waste heat recovery, geothermal, and fuel cells.

When a turbine inlet temperature of 500 to 600 ° C is achieved in a heat source such as nuclear and solar, a supercritical carbon dioxide Bleiton cycle of high thermal efficiency can be operated. However, if the temperature of the heat source changes, the compression efficiency of the compressor designed according to the heat source conditions may be reduced.

The inventors of the present invention have been studying a supercritical carbon dioxide power generation system with improved thermal efficiency. The inventors of the present invention have found that when a supercritical carbon dioxide power generation system with improved thermal efficiency is used, an individual compressor used in accordance with a temperature difference between carbon dioxide heated in a heat source and carbon dioxide flowing into a heat source, And a valve for introducing carbon dioxide into each of the individual compressors in accordance with a difference in temperature of the carbon dioxide, and a method for operating the supercritical carbon dioxide power generation system.

In a supercritical carbon dioxide power generation system, the thermal efficiency differs depending on the temperature difference between the carbon dioxide flowing into the heat source and the carbon dioxide discharged from the heat source. In a heat source having a high temperature difference (about 200 ° C. to 250 ° C.) Into the compressor has the maximum thermal efficiency. However, in the case of a heat source having a low temperature difference (about 100 DEG C to 150 DEG C), the introduction of carbon dioxide having a condition near the critical point into the compressor has no maximum thermal efficiency.

If the conditions of the heat source are changed so that the temperature difference in the heat source is lowered from 100 ° C to 150 ° C at 200 ° C to 250 ° C, the efficiency of the compressor designed according to the temperature difference between 200 ° C and 250 ° C may be lowered, The circuit was configured so that the compressors were operated individually.

An object of the present invention is to provide a supercritical carbon dioxide power generation system having a maximized thermal efficiency by separately operating a compressor having a high compression ratio suitable for a high temperature difference and a compressor having a low compression ratio suitable for a low temperature difference, have.

In order to achieve the above object,

A heat source (1) for heating carbon dioxide;

A first compressor (5) and a second compressor (7) for pressurizing and discharging carbon dioxide;

A turbine (2) into which carbon dioxide heated by the heat source (1) flows;

A recuperator (3) for performing heat exchange between carbon dioxide discharged from the turbine (2) and carbon dioxide discharged from the first compressor (5) or a second compressor;

A cooler (4) for cooling the carbon dioxide discharged from the turbine (2) and flowing through the heat recovery unit (3);

A valve (6) for controlling the inflow of carbon dioxide discharged from the cooler (4) into the first compressor (5) or the second compressor (7);

And a generator (8) connected to the turbine (2)

Wherein the valve controls the inflow of carbon dioxide into the first compressor or the second compressor in accordance with the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator,

Wherein the first compressor (5) has a higher compression ratio (pressure of the carbon dioxide discharged from the compressor) / (pressure of the carbon dioxide introduced into the compressor) than that of the second compressor (7) .

In addition,

The pressurized carbon dioxide is discharged from the first compressor 5 or the second compressor 7 and the pressurized carbon dioxide flows into the heat source 1 through the recuperator 3 and is heated (step 1);

The carbon dioxide heated in the heat source 1 of the step 1 is transferred to the turbine 2 and expanded (step 2);

(Step 3) in which the carbon dioxide having passed through the turbine 2 in the step 2 flows into the recuperator 3 again and the heat exchange with the pressurized carbon dioxide introduced in the step 1 is performed (step 3);

The carbon dioxide which has passed through the turbine 2 and the heat exchanger 3 in the step 3 is transferred to the cooler 4 to be cooled and the cooled carbon dioxide is transferred to the valve 6 (step 4); And

The carbon dioxide transferred to the valve 6 in the step 4 is controlled in accordance with the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator, (Step 5) of introducing the supercritical carbon dioxide power generation system into the compressor.

The supercritical carbon dioxide power generation system according to the present invention includes a valve for introducing carbon dioxide into each compressor according to a temperature difference between carbon dioxide heated in the compressor and the heat source and carbon dioxide introduced into the heat source, Thereby maximizing the thermal efficiency of the heat exchanger.

According to another aspect of the present invention, there is provided a method of operating a supercritical carbon dioxide power generation system, comprising the steps of: pressurizing carbon dioxide with a compressor having a compression ratio capable of exhibiting an optimal thermal efficiency according to a temperature difference between carbon dioxide heated in a heat source and carbon dioxide flowing into a heat source; Thereby maximizing the thermal efficiency of the carbon dioxide power generation system.

FIG. 1 is a graph showing the thermal efficiency versus compression ratio for the supercritical carbon dioxide power generation system according to the present invention. In FIG. 1, the left inflection point is a temperature difference between carbon dioxide heated in the heat source and carbon dioxide flowing into the heat source, The optimum inflection point of the supercritical carbon dioxide power generation system is expressed by the following equation: The optimal inflation point of the supercritical carbon dioxide power generation system in which the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide introduced into the heat source is about 200 ° C. to 250 ° C. .
2 is a schematic view schematically showing an example of a supercritical carbon dioxide power generation system according to the present invention;
3 is a schematic view showing a power generation cycle in a supercritical carbon dioxide power generation system according to the present invention when the temperature difference between carbon dioxide flowing into a heat source and carbon dioxide discharged from a heat source is 175 ° C to 275 ° C;
4 is a schematic diagram showing a power generation cycle in a supercritical carbon dioxide power generation system according to the present invention when the temperature difference between carbon dioxide flowing into a heat source and carbon dioxide discharged from a heat source is 75 ° C to 175 ° C.

The present invention

A heat source (1) for heating carbon dioxide;

A first compressor (5) and a second compressor (7) for pressurizing and discharging carbon dioxide;

A turbine (2) into which carbon dioxide heated by the heat source (1) flows;

A recuperator (3) for performing heat exchange between carbon dioxide discharged from the turbine (2) and carbon dioxide discharged from the first compressor (5) or a second compressor;

A cooler (4) for cooling the carbon dioxide discharged from the turbine (2) and flowing through the heat recovery unit (3);

A valve (6) for controlling the inflow of carbon dioxide discharged from the cooler (4) into the first compressor (5) or the second compressor (7);

And a generator (8) connected to the turbine (2)

Wherein the valve controls the inflow of carbon dioxide into the first compressor or the second compressor in accordance with the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator,

Wherein the first compressor (5) has a higher compression ratio (pressure of the carbon dioxide discharged from the compressor) / (pressure of the carbon dioxide introduced into the compressor) than that of the second compressor (7) .

FIG. 2 schematically shows an example of a supercritical carbon dioxide power generation system according to the present invention,

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

A supercritical carbon dioxide power generation system (101) according to the present invention comprises a first compressor (5) and a second compressor (7) for pressurizing carbon dioxide; A heat source (1) for applying heat to the carbon dioxide; A turbine (2) operated by inflow of pressurized and heated carbon dioxide and expansion; A recuperator (401) for performing heat exchange between the carbon dioxide discharged from the first compressor and the second compressor and the discharged carbon dioxide after operating the turbine; A cooler (4) for cooling the carbon dioxide which has passed through the turbine, And a generator (8) for generating electric power through the operation of the turbine.

Generally, supercritical carbon dioxide power generation systems exhibit different thermal efficiencies depending on the temperature difference in a heat source. For example, in a heat source having a high temperature difference (about 200 ° C to 250 ° C), carbon dioxide, It is not possible to introduce carbon dioxide having a condition near the critical point into the compressor in a heat source having a low temperature difference (about 100 DEG C to 150 DEG C), but does not have the maximum thermal efficiency. As a result, the maximum thermal efficiency can not be obtained.

Accordingly, the present invention includes a valve for introducing carbon dioxide into each compressor according to the difference in temperature between the compressor having different compression ratios, the carbon dioxide heated in the heat source and the carbon dioxide flowing into the heat source, Thereby maximizing heat efficiency.

In addition, the compression ratio of the first compressor 5 may be 2.7 to 3.4, preferably 2.9 to 3.4, and more preferably 3.1 to 3.3.

Furthermore, the compression ratio of the second compressor 7 may be 1.6 to 2.2, preferably 1.7 to 2.1, and more preferably 1.8 to 2.0.

The compression ratio may be the pressure of the carbon dioxide discharged from the compressor with respect to the pressure of the carbon dioxide flowing into the compressor, the pressure of the carbon dioxide discharged from the compressor / the pressure of the carbon dioxide flowing into the compressor, Lt; / RTI >

Specifically, the pressure of the first compressor or the second compressor may be 16 MPa to 29 MPa, may be 18 MPa to 27 MPa, and may be 20 MPa to 25 MPa, but the compression ratio of the first and second compressors may be But is not limited thereto.

When the temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide discharged from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 is 75 ° C or higher and lower than 175 ° C, The valve 6 is controlled to block the introduction of carbon dioxide into the first compressor and to introduce carbon dioxide into the second compressor. At this time, the pressure of the carbon dioxide introduced into the second compressor may be 11 MPa to 17 MPa, 12 MPa to 16 MPa, and 13 MPa to 15 MPa.

Further, when the temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide discharged from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 is 175 ° C or higher and lower than 275 ° C, The valve 6 is controlled to block the inflow of carbon dioxide into the second compressor and to introduce carbon dioxide into the first compressor. In this case, the pressure of the carbon dioxide introduced into the first compressor may be 4.5 MPa to 10.5 MPa, 5.5 MPa to 9.5 MPa, and 6.5 MPa to 8.5 MPa.

The supercritical carbon dioxide power generation system 101 according to the present invention includes a first compressor 5 and a second compressor 7, a heat source 1, a turbine 2, a heat exchanger 3, a cooler 4, 6, and each component is connected to each of the flow paths to constitute a closed circuit, and the closed circuit is a system in which carbon dioxide, which is a working fluid, circulates and is generated.

The supercritical carbon dioxide power generation system 101 according to the present invention may be constituted by connecting the respective constituent elements with respective flow paths as follows.

Specifically, a seventh flow path 17 for transferring the carbon dioxide pressurized and discharged from the first compressor 5;

An eighth passage (18) for conveying the carbon dioxide discharged from the second compressor (7);

A ninth passage (19) for transferring the carbon dioxide which has passed through the seventh passage (17) or the eighth passage (18) to the heat storage (3);

A tenth flow path (20) for transferring the carbon dioxide discharged from the heat recovery furnace (3) through the ninth flow path (19) to the heat source (1);

A first flow path (11) for transferring the carbon dioxide discharged from the heat source (1) to the turbine (2);

A second flow path (12) for transferring the carbon dioxide discharged from the turbine (2) to the heat recovery unit (3);

A third flow path 13 for transferring the carbon dioxide discharged from the heat recovery furnace 3 through the second flow path 12 to the cooler 4;

A fourth flow path 14 for transferring the carbon dioxide discharged from the cooler 4 to the valve 6,

A fifth flow path (15) for transferring the carbon dioxide discharged from the valve (6) to the first compressor (5); And

And a sixth flow path 16 for transferring the carbon dioxide discharged from the valve 6 to the second compressor 7.

As described above, the supercritical carbon dioxide power generation system 101 according to the present invention includes the first compressor 5 and the second compressor 7, the heat source 1, the turbine 2, the heat exchanger 3, the cooler 4, , A valve (6) and a flow path (11, 12, 13, 14, 15, 16, 17, 18, 19, 20) connecting the respective components, Carbon dioxide can circulate and develop.

In addition, the carbon dioxide generating system 101 according to the present invention includes a two-path power generation circuit according to the temperature difference between the carbon dioxide flowing into the heat source 1 and the carbon dioxide heated from the heat source.

Specifically, the first power generation circuit includes a first compressor 5, a seventh channel 17, a ninth channel 19, a heat exchanger 3, a tenth channel 20, a heat source 1, (3), the third flow path (13), the cooler (4), the fourth flow path (14) and the fifth flow path (15) And a circuit connected to the first compressor.

The second power generation circuit includes a second compressor 7, an eighth passage 18, a ninth passage 19, a heat exchanger 3, a tenth passage 20, a heat source 1, 11, the turbine 2, the second passage 12, the recuperator 3, the third passage 13, the cooler 4, the fourth passage 14 and the sixth passage 16, 2 < / RTI > compressor.

Further, the first power generation circuit is operated when the temperature difference between the carbon dioxide flowing into the heat source 1 and the carbon dioxide heated from the heat source is 175 ° C or higher and lower than 275 ° C.

The second power generation circuit is operated when the temperature difference between the carbon dioxide flowing into the heat source 1 and the carbon dioxide heated from the heat source is 75 ° C or more and less than 175 ° C.

Furthermore, it is preferable that the turbine 2 and the generator 8 are connected and operated in one axis. The generator is powered by the rotational force of the turbine.

In addition,

The pressurized carbon dioxide is discharged from the first compressor 5 or the second compressor 7 and the pressurized carbon dioxide flows into the heat source 1 through the recuperator 3 and is heated (step 1);

The carbon dioxide heated in the heat source 1 of the step 1 is transferred to the turbine 2 and expanded (step 2);

(Step 3) in which the carbon dioxide having passed through the turbine 2 in the step 2 flows into the recuperator 3 again and the heat exchange with the pressurized carbon dioxide introduced in the step 1 is performed (step 3);

The carbon dioxide which has passed through the turbine 2 and the heat exchanger 3 in the step 3 is transferred to the cooler 4 to be cooled and the cooled carbon dioxide is transferred to the valve 6 (step 4); And

The carbon dioxide transferred to the valve 6 in the step 4 is controlled in accordance with the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator, (Step 5) of introducing the supercritical carbon dioxide power generation system into the compressor.

FIG. 2 schematically shows an example of a supercritical carbon dioxide power generation system according to the present invention,

Hereinafter, a method of operating the supercritical carbon dioxide power generation system according to the present invention will be described in detail with reference to FIG.

In operation 1 of the supercritical carbon dioxide power generation system according to the present invention, pressurized carbon dioxide is discharged from the first compressor (5) or the second compressor (7), and the pressurized carbon dioxide is discharged from the recuperator (3) And flows into the heat source 1 to be heated.

In step 1, the first compressor (5) or the second compressor (7) pressurizes carbon dioxide which is a working fluid, discharges the carbon dioxide, and the discharged carbon dioxide is transferred to the heat exchanger (3) And is heated.

Specifically, the compression ratio of the first compressor 5 in the step 1 may be 2.7 to 3.4, may be 2.8 to 3.3, and may be 2.9 to 3.2.

The compression ratio of the second compressor 7 in the step 1 may be 1.6 to 2.2, may be 1.9 to 2.1, and may be 1.8 to 2.0.

At this time, the compression ratio may be (first or second compressor pressurizing pressure) / (first or second compressor inlet pressure), and the first compressor and the second compressor pressurizing pressure may be the same.

The pressurizing pressure of the first compressor or the second compressor in the step 1 may be 16 MPa to 29 MPa, preferably 18 MPa to 27 MPa, and more preferably 20 MPa to 25 MPa, 1 and the pressure capable of maintaining the compression ratio of the second compressor.

Generally, supercritical carbon dioxide power generation systems are cooled to a pressure of about 7.37 MPa and a temperature of about 31 ° C, which is a critical condition of carbon dioxide, prior to entering the compressor, thereby reducing the consumption of the compressor.

However, when the temperature difference in the heat source is lowered from 75 캜 to below 175 캜, generally cooling to a known critical pressure does not exhibit the maximum thermal efficiency.

Accordingly, in the present invention, it is possible to operate the compressors having different compression ratios, respectively, so as to exhibit the maximum thermal efficiency even when the temperature difference in the heat source changes.

Next, in the method of operating the supercritical carbon dioxide power generation system according to the present invention, the step 2 is a step in which the carbon dioxide heated in the heat source 1 of the step 1 is transferred to the turbine 2 and expanded.

In the step 2, the carbon dioxide heated in the heat source 1 of the step 1 flows into the turbine 2 and expands to operate the turbine 2.

Specifically, the expansion ratio of carbon dioxide flowing into the first turbine may be 1.3 to 4.7: 1, 1.4 to 4.6: 1, and 1.5 to 4.5: 1, but is not limited thereto.

The expansion ratio is the first compressor inlet pressure of the carbon dioxide compared to the carbon dioxide pressure of the first compressor 5 or the second compressor inlet pressure of the carbon dioxide relative to the carbon dioxide pressure of the second compressor 7.

Next, in the method of operating the supercritical carbon dioxide power generation system according to the present invention, step 3 is a step in which the carbon dioxide having passed through the turbine 2 flows into the recuperator 3 again in step 2, And the heat exchange with the carbon dioxide is performed.

In the step 3, carbon dioxide having passed through the turbine 2 flows into the heat recovery unit 3 in the step 2, and heat exchange with carbon dioxide pressurized in the first compressor or the second compressor in the step 1 is performed, to be.

The pressurized carbon dioxide in the first compressor or the second compressor is heat-exchanged with the carbon dioxide introduced into the heat recovery unit 3 through the turbine 2 of the step 3 in the heat recovery unit 3 and is heated.

In the supercritical carbon dioxide power generation system, the temperature of the turbine is lowered due to the higher turbine expansion ratio in the case of steam power generation. In the case of the supercritical carbon dioxide power generation system, the expansion ratio is lower, It is still highly inflated, and if it is enough to utilize it, the efficiency of the power generation system can be increased. Therefore, in the case of the supercritical CO2 generation system, the heat recovery has a great influence on the efficiency of the power generation system.

In the supercritical carbon dioxide power generation system according to the present invention, the heat recovery unit 3 passes the high-temperature heat of the low-pressure portion passing through the turbine 2 to the first compressor 5 through the cooler 4, Or to the low-temperature side of the high-pressure portion which is pressurized and introduced through the second compressor (7). This will ultimately minimize the amount of heat that is wasted externally in the supercritical carbon dioxide power generation system, thereby helping to increase the final thermal efficiency of the power generation system.

Next, in the method of operating the supercritical carbon dioxide power generation system according to the present invention, in step 4, the carbon dioxide having passed through the turbine 2 and the heat recovery unit 3 in the step 3 is transferred to the cooler 4 to be cooled, And transferring the cooled carbon dioxide to the valve (6).

In step 4, the carbon dioxide introduced into the cooler 4 is cooled and flows into the valve 6.

At this time, the cooler 4 is cooled by the carbon dioxide transferred from the heat exchanger 3 through the turbine 2 and transferred in an expanded state, so that the temperature of the carbon dioxide can be controlled to a predetermined temperature and discharged do.

Next, in the method of operating the supercritical carbon dioxide power generation system according to the present invention, the carbon dioxide transferred to the valve 6 in the step 4 in the step 4 is discharged from the carbon dioxide heated in the heat source and discharged from the first compressor or the second compressor And is controlled in accordance with the temperature difference of the carbon dioxide passing through the recuperator to be introduced into the first compressor or the second compressor.

In the step 5, the valve 6 is controlled according to the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator, so that the carbon dioxide flowing into the valve 6 To the first compressor or the second compressor.

Specifically, in step 5, the difference in temperature between the carbon dioxide heated in the heat source 1 and the carbon dioxide discharged from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 is 75 ° C or higher and lower than 175 ° C The valve 6 blocks the inflow of carbon dioxide into the first compressor and transfers the carbon dioxide introduced into the valve 6 to the second compressor.

When the temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide exhausted from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 is less than 175 ° C. and less than 275 ° C. , The valve 6 blocks the inflow of carbon dioxide into the second compressor and transfers the carbon dioxide introduced into the valve 6 of the step 5 to the first compressor.

That is, when the temperature difference between the carbon dioxide flowing into the heat source 1 and the carbon dioxide heated from the heat source is high (175 ° C or more and less than 275 ° C), circulation of 2.7 to 3.4 carbon dioxide exhibits a high thermal efficiency,

When the temperature difference is low (75 DEG C or more and less than 175 DEG C), circulating carbon dioxide at a compression ratio of 1.6 to 2.2 shows a high thermal efficiency, and a different compressor is used depending on each condition.

As described above, the operation method of the supercritical carbon dioxide power generation system according to the present invention uses a compressor designed to have an optimum compressor efficiency according to the temperature difference between the carbon dioxide flowing into the heat source 1 and the carbon dioxide heated from the heat source, It can exhibit higher thermal efficiency than conventional supercritical carbon dioxide power generation systems.

Hereinafter, the present invention will be described in detail with reference to the following examples and experimental examples.

However, the following examples and experimental examples are for illustrative purposes only and are not intended to limit the scope of the present invention.

< Example  1> Supercritical  Operation of carbon dioxide power generation system

&Lt; First power generation circuit &

Carbon dioxide of 8.4 MPa pressure is pressurized and discharged at a pressure of 27.6 MPa in the first compressor 5 and flows into the heat recovery unit 3 through the seventh flow path 17 and the ninth flow path 19. [ The introduced carbon dioxide is heated to a temperature of 291.3 캜, passed through the tenth flow path 20, flows into the heat source 1, and is heated again to a temperature of 520 캜. The heated carbon dioxide expands in the turbine 1 via the first flow path 11 and the expansion ratio expands at an expansion ratio of 3.28: 1, which is the pump pressure: pump inlet pressure (27.6 MPa: 8.4 MPa). The expanded carbon dioxide flows into the heat exchanger 3 through the first flow path 11 and is cooled to 103.1 ° C from the carbon dioxide introduced and pressurized by the first compressor. The cooled carbon dioxide flows into the cooler 4 via the third flow path 13 and is cooled to a temperature of 36.8 캜. The cooled carbon dioxide flows into the first compressor (5) through the fourth flow path (14) and the fifth flow path (15).

&Lt; Second power generation circuit &

Carbon dioxide at a pressure of 14.9 MPa is pressurized and discharged at a pressure of 27.6 MPa in the second compressor 7 and flows into the heat exchanger 3 through the eighth and eighth flow paths 18 and 19. The introduced carbon dioxide is heated to a temperature of 412 캜, passes through a tenth flow path 20, flows into a heat source 1, and is heated again to a temperature of 520 캜. The heated carbon dioxide expands in the turbine 1 via the first flow path 11 and the expansion ratio expands at an expansion ratio of 1.85: 1, which is the pump pressure: pump inlet pressure (27.6 MPa: 14.9 MPa). The expanded carbon dioxide flows into the heat exchanger (3) through the first flow path (11), and is cooled to a temperature of 60.8 DEG C from the carbon dioxide introduced and pressurized by the first compressor. The cooled carbon dioxide flows into the cooler 4 via the third flow path 13 and is cooled to a temperature of 36.8 캜. The cooled carbon dioxide flows into the second compressor 7 through the fourth flow path 14, the sixth flow path 16, and the like.

The supercritical carbon dioxide power generation system is operated by simultaneously operating the first power generation circuit and the second power generation circuit.

< Experimental Example  1> Supercritical  Thermal efficiency analysis of carbon dioxide power generation system

In order to confirm the thermal efficiency of the supercritical carbon dioxide power generation system according to the present invention, only the first power generation circuit is driven in the supercritical carbon dioxide power generation system of the first embodiment, and the temperature of the turbine inlet is set to about 520 DEG C, The pressure of the compressor was about 27.6 MPa, the temperature of the carbon dioxide flowing into the compressor was about 36.8 DEG C, and the compressibility of the compressor was set to 3.28. Then, a simulation of the supercritical carbon dioxide power generation system was performed to measure the thermal efficiency.

The temperature and pressure of the carbon dioxide discharged from each component are shown in Fig. 3, and specific values are as follows.

The pressure and temperature of the carbon dioxide discharged from the first compressor 5 are 27.6 MPa and 90.9 ° C and the pressure and temperature of the carbon dioxide discharged from the recuperator 3 are 27.6 MPa and 291.3 ° C. The pressure and temperature of carbon dioxide are 27.6 MPa and 520 ° C. The pressure and temperature of carbon dioxide discharged from the turbine 2 are 8.4 MPa and 382.2 ° C. The pressure and temperature of carbon dioxide discharged from the cooler 4 are 8.4 MPa and 36.8 / RTI &gt;

At this time, when only the first power generation circuit of the supercritical carbon dioxide power generation system is driven, the mass flow rate of carbon dioxide into the turbine is 20.7 kg / s. In addition, when the carbon dioxide is circulated once, the work done by the turbine is 3.03 MW, the work done by the compressor is 0.78 MW, and the work produced by the generator is 2.25 MW. Therefore, the thermal efficiency of the first power generation circuit is 37.5%.

In the supercritical carbon dioxide power generation system according to the first embodiment, only the second power generation circuit is driven, the temperature of the turbine inlet is set to about 520 DEG C, the pressure of the carbon dioxide discharged from the compressor is set to about 27.6 MPa, Was set at about 36.8 캜, and the compressibility in the compressor was set at 1.85, and then a simulation of the supercritical carbon dioxide power generation system was performed to measure the thermal efficiency.

The temperature and pressure conditions of the carbon dioxide discharged from each component are shown in FIG. 4, and specific values are as follows.

The pressure and temperature of the carbon dioxide discharged from the second compressor 7 are 27.6 MPa and 51.9 ° C. and the pressure and temperature of the carbon dioxide discharged from the recuperator 3 are 27.6 MPa and 412.3 ° C., The pressures and temperatures of carbon dioxide are 27.6 MPa and 520 ° C. The pressures and temperatures of carbon dioxide discharged from the turbine 2 are 14.9 MPa and 445.4 ° C. The pressure and temperature of carbon dioxide discharged from the cooler 4 are 14.9 MPa and 36.8 / RTI &gt;

At this time, when only the second power generation circuit of the supercritical carbon dioxide power generation system is driven, the mass flow rate of the carbon dioxide into the turbine is 44.4 kg / s. In addition, when the carbon dioxide is circulated once, the turbine performs 3.58 MW, the compressor works 0.80 MW, and the generator produces 2.78 MW. Therefore, the thermal efficiency of the second power generation circuit is 46.3%.

Thus, the supercritical carbon dioxide power generation system according to the present invention, through the design of the compressor capable of exhibiting the maximum thermal efficiency when the temperature difference in the heat source is different, exhibits the optimum thermal efficiency under each condition even if the temperature difference is increased or decreased .

101: Supercritical CO2 generation system
1: Heat source 2: Turbine
3: Recuperator 4: Cooler
5: first compressor 6: valve
7: Second compressor 8: Generator
11: first flow path 12: second flow path
13: Third Euro 14: 4th Euro
15: Fifth Euro 16: Sixth Euro
17: Seventh Euro 18: Eighth Euro
19: 9th euro 20: 10th euro

Claims (11)

A heat source (1) for heating carbon dioxide;
A first compressor (5) and a second compressor (7) for pressurizing and discharging carbon dioxide;
A turbine (2) into which carbon dioxide heated by the heat source (1) flows;
A recuperator (3) for performing heat exchange between carbon dioxide discharged from the turbine (2) and carbon dioxide discharged from the first compressor (5) or a second compressor;
A cooler (4) for cooling the carbon dioxide discharged from the turbine (2) and flowing through the heat recovery unit (3);
A valve (6) for controlling the inflow of carbon dioxide discharged from the cooler (4) into the first compressor (5) or the second compressor (7);
And a generator (8) connected to the turbine (2)
Wherein the valve controls the inflow of carbon dioxide into the first compressor or the second compressor in accordance with the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator,
Wherein the first compressor (5) has a higher compression ratio (pressure of the carbon dioxide discharged from the compressor) / (pressure of the carbon dioxide introduced into the compressor) than that of the second compressor (7) .
The method according to claim 1,
And the compression ratio of the first compressor (5) is 2.7 to 3.4.
The method according to claim 1,
And the compression ratio of the second compressor (7) is 1.6 to 2.2.
The method according to claim 1,
The temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide exhausted from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 is 75 ° C or more and less than 175 ° C,
And the valve (6) introduces carbon dioxide into the second compressor.
The method according to claim 1,
The temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide discharged from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 is 175 ° C or higher and less than 275 ° C,
Characterized in that the valve (6) introduces carbon dioxide into the first compressor.
The pressurized carbon dioxide is discharged from the first compressor 5 or the second compressor 7 and the pressurized carbon dioxide flows into the heat source 1 through the recuperator 3 and is heated (step 1);
The carbon dioxide heated in the heat source 1 of the step 1 is transferred to the turbine 2 and expanded (step 2);
(Step 3) in which the carbon dioxide having passed through the turbine 2 in the step 2 flows into the recuperator 3 again and the heat exchange with the pressurized carbon dioxide introduced in the step 1 is performed (step 3);
The carbon dioxide which has passed through the turbine 2 and the heat exchanger 3 in the step 3 is transferred to the cooler 4 to be cooled and the cooled carbon dioxide is transferred to the valve 6 (step 4); And
The carbon dioxide transferred to the valve 6 in the step 4 is controlled in accordance with the temperature difference between the carbon dioxide heated in the heat source and the carbon dioxide discharged from the first compressor or the second compressor and passing through the recuperator, And a step (5) of flowing into the compressor.
The method according to claim 6,
The temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide discharged from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 in the step 5 is 75 ° C or more and less than 175 ° C,
Wherein the carbon dioxide in step 5 is introduced into the second compressor.
The method according to claim 6,
The temperature difference between the carbon dioxide heated in the heat source 1 and the carbon dioxide exhausted from the first compressor 5 or the second compressor 7 and passing through the recuperator 3 in the step 5 is 175 ° C or more and less than 275 ° C,
Wherein the carbon dioxide in step 5 is introduced into the first compressor.
The method according to claim 6,
Wherein the expansion ratio of the turbine (2) in step 2 is 1.5 to 4.5: 1.
8. The method of claim 7,
And the carbon dioxide flowing into the second compressor (7) is pressurized at a compression ratio of 1.6 to 2.2.
9. The method of claim 8,
Wherein the carbon dioxide flowing into the first compressor (5) is pressurized at a compression ratio of 2.7 to 3.4.
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