CN117753172A - Multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of secondary reheating unit - Google Patents
Multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of secondary reheating unit Download PDFInfo
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- CN117753172A CN117753172A CN202311570550.2A CN202311570550A CN117753172A CN 117753172 A CN117753172 A CN 117753172A CN 202311570550 A CN202311570550 A CN 202311570550A CN 117753172 A CN117753172 A CN 117753172A
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- 238000003303 reheating Methods 0.000 title claims abstract description 44
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 37
- 238000000605 extraction Methods 0.000 claims abstract description 45
- 239000003463 adsorbent Substances 0.000 claims abstract description 23
- 230000008929 regeneration Effects 0.000 claims abstract description 12
- 238000011069 regeneration method Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 265
- 239000007788 liquid Substances 0.000 claims description 96
- 238000001179 sorption measurement Methods 0.000 claims description 52
- 238000010521 absorption reaction Methods 0.000 claims description 36
- 238000003795 desorption Methods 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 23
- 238000000034 method Methods 0.000 claims description 21
- 239000003638 chemical reducing agent Substances 0.000 claims description 20
- 238000005086 pumping Methods 0.000 claims description 14
- 239000000428 dust Substances 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 7
- 230000003009 desulfurizing effect Effects 0.000 claims description 6
- 230000001172 regenerating effect Effects 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 10
- 239000003546 flue gas Substances 0.000 abstract description 10
- 230000000295 complement effect Effects 0.000 abstract description 2
- 238000002485 combustion reaction Methods 0.000 description 16
- 239000007789 gas Substances 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 9
- 238000004891 communication Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 7
- 230000008901 benefit Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
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- 238000000746 purification Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
The invention provides a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit, and belongs to the technical field of electric power engineering. The invention is directed to CO 2 The continuous steam extraction requirement of the capturing device adopts BEST steamTurbine replaces the existing main turbine, CO 2 The extraction steam source of the capturing device is changed into four-way steam source complementary air intake so as to meet the continuous extraction steam requirement under the variable load operation condition; the invention realizes continuous collection of CO in flue gas under variable working condition operation condition of the secondary reheating unit of the coal-fired power plant 2 Is self-balanced, ensures CO under different operating conditions, especially under low-load operating conditions 2 The continuity and reliability of the heat source required for adsorbent regeneration improves the carbon capture efficiency and stability.
Description
Technical Field
The invention relates to the technical field of electric power engineering, in particular to a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit.
Background
The statements in this section merely provide background information related to the present disclosure and may not necessarily constitute prior art.
CO 2 An important source of emissions is coal-fired power plants, which form an important component of the energy infrastructure, also CO 2 One of the most concentrated sources of emissions. Given the central role played by coal-fired power plants in energy structures, they are under tremendous pressure to save energy and reduce carbon. Power plants are not only meeting energy demands, but are also subject to technical innovation to reduce the carbon footprint and mitigate adverse environmental impact. One of the main ways in which power plants perform the function of reducing carbon is to increase their energy conversion efficiency so that the same amount of energy can be produced with less CO emissions 2 . Furthermore, CO is captured before the flue gas is discharged into the atmosphere 2 The total emission of the flue gas of the power plant can be remarkably reduced.
In CO 2 In the field of trapping, power plants mainly rely on three technologies: these technologies all have unique features, advantages and challenges for pre-combustion trapping, in-combustion trapping and post-combustion trapping.
CO before combustion 2 The trapping is mainly used for an Integrated Gasification Combined Cycle (IGCC) power plant. The process first gasifies coal to produce synthesis gas, which is a mixture of mainly CO and H 2 A mixture of components. The synthesis gas is then reacted with steam in a conversion unit, the reaction resulting in the formation of CO 2 And H 2 . The subsequent steps involve separation of the CO by physical or chemical separation processes 2 The method comprises the steps of carrying out a first treatment on the surface of the After separation, CO 2 Compressed and stored, while the hydrogen-enriched fuel is directed to a gas turbine for power generation, however, this process typically results in a reduction in the power generation efficiency of the power plant of about 7% to 10%.
CO in combustion 2 The trapping is based on the oxyfuel combustion technology. In this method, air is first separated using an air separation device to extract O 2 Such high purity O 2 Subsequent combustion of the fuel to produce a fuel consisting essentially of CO 2 And H 2 The smoke component composed of O is separated from CO by condensation process 2 For controlling the combustion temperature, a part of the flue gas is recycled into the boiler, a significant advantage of this method is due to the use of high purity O 2 While increasing CO in the flue gas 2 Concentration of this kindThe increase helps to reduce CO 2 Capturing the required energy consumption; however, this advantage is to some extent exploited by the air separation unit to produce O 2 The required energy consumption is counteracted. Thus, the power generation efficiency of a power plant employing this method may be reduced by about 10% to 12%.
Post-combustion CO 2 Trapping mainly uses a chemical absorption method. The coal dust and air are burnt in the boiler, and the generated flue gas is led into CO after being treated by denitration, dust removal, desulfurization and the like 2 And a trapping device. CO present in flue gas 2 Reacts with the absorbent to cause it to be absorbed. The absorbed CO is then separated by heating the absorbent 2 Then it is compressed and stored, which has the advantage of not changing the original combustion mode, and in the past decades, it has made rapid progress, now becoming the most widely used CO 2 The effectiveness of capture technology has been demonstrated in numerous power plants, highlighting its potential for widespread commercial use worldwide.
However, the inventors found that the post-combustion trapping method has the following problems: the absorbent regeneration process is critical to the operation of the technology but results in a loss of thermal efficiency, since air is the oxidant in the combustion process, the flue gas contains a significant amount of N 2 ，N 2 The presence of (C) means CO 2 The relatively low concentration results in higher energy consumption in the separation process, which typically results in a reduction in the power generation efficiency of 8% to 13%.
As shown in FIG. 1, the existing typical coal-fired power plant secondary reheating system adopts CO required by the carbon capture technology after combustion 2 The consumption of steam required by the desorption and regeneration of the adsorbent is large, and when the unit is operated under variable working conditions, a single heat source is difficult to ensure that the steam parameters can always meet the CO under the low-load working condition 2 Desorbing and regenerating parameters of the adsorbent; moreover, in a typical coal-fired power plant secondary reheating system, the thermodynamic integrated solution adopting the post-combustion carbon capture technology is to extract steam on a communication pipe of a medium pressure cylinder and a low pressure cylinder for CO 2 The trapping device can effectively meet the requirement of CO when the secondary reheating unit operates at a load 2 Adsorbent desorption and regenerationThe steam consumption required by the heat generating source, but when the secondary reheating unit is in variable load operation, particularly in low load operation, the method can cause excessive superheat degree of steam extracted from the communication pipe, more steam flow is consumed, the residual steam quantity flowing into the low-pressure cylinder is obviously reduced, serious steam turbine thermal efficiency reduction is caused, and even the risk of low-pressure cylinder blade flutter and blast heating can be caused.
Disclosure of Invention
In order to solve the defects in the prior art, the invention provides a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit, which realizes continuous capture of flue gas CO under variable-working-condition operation conditions of the secondary reheating unit of a coal-fired power plant 2 Is self-balanced, ensures CO under different operating conditions, especially under low-load operating conditions 2 The continuity and reliability of the heat source required for adsorbent regeneration improves the carbon capture efficiency and stability.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
in a first aspect, the invention provides a multi-heat source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit.
A multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit, comprising: denitration device, dust remover, desulfurizing device and CO 2 Adsorption tower, CO 2 Rich liquid/lean liquid heat exchanger and CO 2 Adsorption tower analysis tower and CO 2 An absorption liquid regenerator, a condenser, a gas-liquid separator, a pressurized gas storage device, a BEST steam turbine generator, a steam attemperator, a steam pressure reducer and a sub-bin pressure equalizing hole plate type self-balancing steam-water mixer;
the denitration device is communicated with the main turbine ultrahigh pressure cylinder through a pipeline, and the denitration device, the dust remover, the desulfurizing device and the CO are connected with each other through pipelines 2 The adsorption towers are sequentially communicated with each other through pipelines, and CO 2 Rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower is communicated with CO 2 Adsorption tower and CO 2 The rich liquid/lean liquid heat exchanger is communicated;
CO 2 rich liquid/lean liquid heat exchanger and CO 2 The resolving tower of the adsorption tower is communicated,CO 2 absorption liquid regenerator and CO 2 The rich liquid/lean liquid heat exchanger is communicated with CO 2 The absorption liquid regenerator is communicated with a shell-and-tube low-pressure feed water heater, and CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 The absorption liquid regenerator is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer;
the low-pressure feed water heater is communicated with the low-pressure cylinder of the main turbine, the low-pressure feed water heater is respectively communicated with the shell-and-tube low-pressure feed water heater and the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer, the shell-and-tube low-pressure feed water heater is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer, the high-pressure feed water heater is communicated with the ultrahigh-pressure cylinder of the main turbine, and the shell-and-tube low-pressure feed water heater is communicated with the high-pressure feed water heater after passing through the deaerator and the feed water pump;
the main turbine ultrahigh pressure cylinder is communicated with the BEST turbine, the BEST turbine is communicated with the high-pressure feed water heater, the BEST turbine is communicated with the sub-compartment pressure equalizing hole plate type self-balancing steam-water mixer, the main turbine ultrahigh pressure cylinder is communicated with the sub-compartment pressure equalizing hole plate type self-balancing steam-water mixer after passing through the steam attemperator and the steam pressure reducer, the BEST turbine is communicated with the deaerator, the pressurizing gas storage is communicated with the gas-liquid separator, and the gas-liquid separator is respectively communicated with the condenser and the CO 2 And the adsorption tower and the desorption tower are communicated.
As a further limitation of the first aspect of the invention, the boiler, the main turbine ultra-high pressure cylinder, the main turbine medium pressure cylinder, the main turbine low pressure cylinder, the condenser, the condensate pump and the shaft seal heater are communicated through pipelines in sequence, and the main generator is communicated with the main turbine low pressure cylinder;
The low-pressure feed water heater comprises a first low-pressure feed water heater, a second low-pressure feed water heater, a third low-pressure feed water heater, a fourth low-pressure feed water heater and a fifth low-pressure feed water heater which are communicated in sequence;
the first low-pressure feed water heater is respectively communicated with the condenser and the condensate pump, the condenser is communicated with a pipeline between the condensate pump and the shaft seal heater, and the condenser is communicated with a pipeline between the third low-pressure feed water heater and the fourth low-pressure feed water heater;
the main turbine intermediate pressure cylinder is communicated with a fifth low-pressure feed water heater, and the fifth low-pressure feed water heater is communicated with a shell-and-tube low-pressure feed water heater.
As a further limitation of the first aspect of the invention, the shaft seal heater is in communication with the condenser and the main turbine low pressure cylinder is in communication with the first low pressure feedwater heater, the second low pressure feedwater heater, the third low pressure feedwater heater and the fourth low pressure feedwater heater, respectively.
As a further limitation of the first aspect of the present invention, the high-pressure feedwater heater includes a first high-pressure feedwater heater, a second high-pressure feedwater heater, a third high-pressure feedwater heater, a fourth high-pressure feedwater heater, and a fifth high-pressure feedwater heater, which are sequentially connected by a pipe;
The first high-pressure feed water heater is respectively communicated with the feed water pump and the deaerator, and the BEST steam turbine is respectively communicated with the first high-pressure feed water heater, the second high-pressure feed water heater, the third high-pressure feed water heater and the fourth high-pressure feed water heater;
the main turbine ultrahigh pressure cylinder is communicated with a fifth high pressure feed water heater, the fifth high pressure feed water heater is communicated with a boiler, and the BEST turbine is communicated with a BEST turbine generator.
In a second aspect, the invention provides a multi-heat source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit.
A multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit, comprising: denitration device, dust remover, desulfurizing device and CO 2 Adsorption tower, CO 2 Rich liquid/lean liquid heat exchanger and CO 2 Adsorption tower analysis tower and CO 2 An absorption liquid regenerator, a condenser, a gas-liquid separator, a pressurized gas storage device, a BEST steam turbine generator, a steam attemperator, a steam pressure reducer and a pressure equalizing four-way valve type self-balancing steam-water mixer;
the denitration device is communicated with the main turbine ultrahigh pressure cylinder through a pipeline, and the denitration device, the dust remover, the desulfurizing device and the CO are connected with each other through pipelines 2 The adsorption towers are sequentially communicated with each other through pipelines, and CO 2 Rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower is communicated with CO 2 Adsorption tower and CO 2 The rich liquid/lean liquid heat exchanger is communicated;
CO 2 rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The rich liquid/lean liquid heat exchanger is communicated with CO 2 The absorption liquid regenerator is communicated with the mixed low-pressure feed water heater, and CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 The absorption liquid regenerator is communicated with the pressure equalizing four-way valve type self-balancing steam-water mixer;
the low-pressure feed water heater is communicated with the low-pressure cylinder of the main turbine, the low-pressure feed water heater is respectively communicated with the mixed low-pressure feed water heater and the pressure-equalizing four-way valve type self-balancing steam-water mixer, the mixed low-pressure feed water heater is communicated with the pressure-equalizing four-way valve type self-balancing steam-water mixer through the steam attemperator and the steam pressure reducer, the high-pressure feed water heater is communicated with the ultrahigh-pressure cylinder of the main turbine, and the mixed low-pressure feed water heater is communicated with the high-pressure feed water heater after passing through the deaerator and the feed water pump;
the main turbine ultrahigh pressure cylinder is communicated with the BEST turbine, the BEST turbine is communicated with the high-pressure feed water heater, the BEST turbine is communicated with the pressure-equalizing four-way valve type self-balancing steam-water mixer after passing through the steam attemperator and the steam pressure reducer, the main turbine ultrahigh pressure cylinder is communicated with the dividing pressure-equalizing hole plate type self-balancing steam-water mixer after passing through the steam attemperator and the steam pressure reducer, the BEST turbine is communicated with the deaerator, the pressurizing gas storage is communicated with the gas-liquid separator, and the gas-liquid separator is respectively communicated with the condenser and the CO 2 And the adsorption tower and the desorption tower are communicated.
As a further limitation of the second aspect of the present invention, the boiler, the main turbine ultra-high pressure cylinder, the main turbine medium pressure cylinder, the main turbine low pressure cylinder, the condenser, the condensate pump and the shaft seal heater are sequentially communicated through pipelines, and the main generator is communicated with the main turbine low pressure cylinder;
the low-pressure feed water heater comprises a first low-pressure feed water heater, a second low-pressure feed water heater, a third low-pressure feed water heater, a fourth low-pressure feed water heater and a fifth low-pressure feed water heater which are communicated in sequence;
the first low-pressure feed water heater is respectively communicated with the condenser and the condensate pump, the condenser is communicated with a pipeline between the condensate pump and the shaft seal heater, and the condenser is communicated with a pipeline between the third low-pressure feed water heater and the fourth low-pressure feed water heater;
the main turbine intermediate pressure cylinder is communicated with a fifth low-pressure feed water heater, and the fifth low-pressure feed water heater is communicated with a shell-and-tube low-pressure feed water heater.
As a further limitation of the second aspect of the invention, the shaft seal heater is in communication with the condenser and the main turbine low pressure cylinder is in communication with the first low pressure feedwater heater, the second low pressure feedwater heater, the third low pressure feedwater heater and the fourth low pressure feedwater heater, respectively.
As a further limitation of the second aspect of the present invention, the high-pressure feedwater heater includes a first high-pressure feedwater heater, a second high-pressure feedwater heater, a third high-pressure feedwater heater, a fourth high-pressure feedwater heater, and a fifth high-pressure feedwater heater, which are sequentially connected by a pipe;
the first high-pressure feed water heater is respectively communicated with the feed water pump and the deaerator, and the BEST steam turbine is respectively communicated with the first high-pressure feed water heater, the second high-pressure feed water heater, the third high-pressure feed water heater and the fourth high-pressure feed water heater;
the main turbine ultrahigh pressure cylinder is communicated with a fifth high pressure feed water heater, the fifth high pressure feed water heater is communicated with a boiler, and the BEST turbine is communicated with a BEST turbine generator.
In a third aspect, the invention provides a working method of a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit.
The working method of the multi-heat-source self-balancing thermodynamic system for the variable-working-condition carbon capture of the secondary reheating unit comprises the following steps of:
under the full-load operation condition of the secondary reheating unit, the first path of steam source is a main steam source, and under the full-load operation condition, the steam discharged by the variable-speed back-pumping type water feeding pump steam turbine enters a low-pressure water feeding heater and is used for heating condensed water in a water-steam circulation system of the power plant, wherein the first path of steam source is a medium-pressure cylinder and low-pressure cylinder communicating pipe steam-extracting source;
Under the working condition that the secondary reheating unit is operated at full load to 70% of load, extracting part of exhaust steam of the BEST steam turbine to enter a thermodynamic self-balancing steam-water mixer to serve as a second path of steam source, wherein the auxiliary first path of steam source is a medium-pressure cylinder and low-pressure cylinder communicating pipe steam extraction source which are used for heating the CO2 adsorbent for desorption and regeneration;
under the working condition that the secondary reheating unit runs from 70% to 50% under the load, on the basis of the extraction of the first path of steam source and the extraction of the second path of steam source, extracting a third path of steam source, which is a previous stage of extraction steam source of the variable-speed back-extraction water supply pump turbine steam exhaust, into a thermodynamic self-balancing steam-water mixer to serve as an auxiliary steam source for heating the CO2 adsorbent for desorption and regeneration, and under the working condition of full load, the path of extraction steam is used for entering a deaerator for heating water supply;
under the working condition that the secondary reheating unit runs from 50% of load to 30% of load, the ultrahigh pressure cylinder of the main turbine is extracted on the basis of the extraction of the first path of steam source, the extraction of the second path of steam source and the extraction of the third path of steam source, and is used as a fourth path of steam source, and after parameters are adjusted by a desuperheater reducer, the steam enters a thermodynamic self-balancing steam-water mixer to be used as an auxiliary steam source for heating the CO2 adsorbent for desorption and regeneration.
As a further limitation of the second aspect of the invention, the cooled water-steam mixture is returned to the shell-and-tube low-pressure feed water heater, the fourth steam source is the main turbine ultra-high pressure cylinder exhaust steam source, and under the full-load operation condition, the main turbine ultra-high pressure cylinder exhaust steam is divided into three parts which are respectively used for the variable-rotation-speed back-pumping feed water pump turbine steam inlet, the final-stage high-pressure feed water heater steam source and the boiler reheat cold section steam.
Compared with the prior art, the invention has the beneficial effects that:
1. the invention provides a secondary re-useMultiple heat source self-balancing thermodynamic system for variable working condition carbon capture of heat engine set, which can be more reliable, more economical and more efficient for CO required by carbon capture technology after combustion 2 The adsorbent desorption regeneration process provides a heat source, is mainly suitable for the technical field of power plant flue gas purification, and is particularly suitable for a secondary reheating coal-fired power plant unit adopting a variable-rotation-speed back-pumping feed pump turbine.
2. The invention adopts a variable-speed back-pumping type water supply pump turbine, all the extraction steam of an ultrahigh pressure cylinder, a high pressure cylinder and a medium pressure cylinder of a main turbine in a typical secondary reheating system of a coal-fired power plant is transferred to the variable-speed back-pumping type water supply pump turbine, the exhaust steam and the extraction steam of the variable-speed back-pumping type water supply pump turbine and the exhaust steam of the ultrahigh pressure cylinder are fully utilized, four auxiliary heating steam sources are arranged according to the change condition of parameters of a water-steam circulation system when a secondary reheating unit runs under variable working conditions, and the four steam sources are combined with the load running condition of the unit to jointly heat CO 2 The adsorbent is desorbed and regenerated.
3. According to the invention, the thermodynamic self-balancing of the temperature, the pressure and the enthalpy values of different steam sources after mixing is realized through the thermodynamic self-balancing steam-water mixer, so that the stability and the continuity of heating the steam sources are realized, and a complicated steam temperature and pressure regulating system and a complicated water-steam bypass system are not required to be additionally arranged; the temperature and pressure parameters of each throttle plate in the mixer are correspondingly regulated so as to control the fluctuation of mixed gas in the start-stop process of multiple steam sources, avoid the situation that high-temperature high-pressure steam is directly mixed into low-pressure pipeline steam to cause the reverse flow of the high-pressure pipeline steam, effectively reduce the consumption of the high-temperature high-pressure steam through thermodynamic self-balancing, namely reduce the consumption of the high-enthalpy steam, and be beneficial to energy conservation and consumption reduction.
4. The invention collects the waste heat of the gas at the outlet of the analytic tower and the waste heat of the condenser to replace the heat of the extracted steam for heating the water supply, thereby further improving the overall heat economy of the thermodynamic system; multiple heat sources combined steam supply ensures CO in variable load operation process of unit 2 The adsorbent desorption regeneration heat source provides more stable, more reliable and more efficient steam, and the self-balancing steam-water mixer is beneficial to the simplification of a thermodynamic system and reduces The heat loss caused by the complicated system is reduced, the economy of the thermodynamic system of the unit is improved, and the method has good practical application value.
Additional aspects of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention.
FIG. 1 is a schematic diagram of a conventional typical coal-fired power plant secondary reheat system water-steam thermodynamic system as mentioned in the background;
FIG. 2 is a schematic structural diagram of a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit provided by embodiment 1 of the present invention;
FIG. 3 is a schematic structural diagram of a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit provided in embodiment 2 of the present invention;
1, a boiler; 2. an ultrahigh pressure cylinder of the main turbine; 3. a main turbine high pressure cylinder; 4. a main turbine intermediate pressure cylinder; 5. a main turbine low pressure cylinder; 6. a main generator; 7. a condenser; 8. a condensate pump; 9. a shaft seal heater; 10a, a first low pressure feedwater heater; 10b, a second low pressure feedwater heater; 10c, a third low pressure feedwater heater; 10d, a fourth low pressure feedwater heater; 10e, fifth low pressure feedwater heater; 11a, a shell-and-tube low-pressure feedwater heater; 11b, a hybrid low pressure feedwater heater; 12. a deaerator; 13. a water feed pump; 14a, a first high pressure feedwater heater; 14b, a second high pressure feedwater heater; 14c, a third high pressure feedwater heater; 14d, fourth high pressure feedwater heater; 14e, fifth high pressure feedwater heater; 101. a denitrator; 102. a dust remover; 103. a desulfurizer; 104. CO 2 An adsorption tower; 105. CO 2 A rich/lean heat exchanger; 106. CO 2 An adsorption tower desorption tower; 107. CO 2 An absorption liquid regenerator; 108. a condenser; 109. a gas-liquid separator; 110. pressurized gas storageA device; 201. a BEST turbine; 202. BEST turbo generator; 203. a steam attemperator; 204 a steam reducer; 205. a sub-bin pressure equalizing hole plate type self-balancing steam-water mixer; 206. pressure equalizing four-way valve type self-balancing steam-water mixer.
Detailed Description
The invention will be further described with reference to the drawings and examples.
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
Embodiments of the invention and features of the embodiments may be combined with each other without conflict.
Example 1:
as shown in fig. 1, embodiment 1 of the present invention provides a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit, comprising: denitration device 101, dust remover 102, desulfurization device 103, and CO 2 Adsorption tower 104, CO 2 Rich/lean liquid heat exchanger 105, CO 2 Adsorption tower desorption tower 106, CO 2 An absorption liquid regenerator, a condenser 108, a gas-liquid separator 109, a pressurized gas storage 110, a BEST steam turbine 201, a BEST steam turbine generator 202, a steam attemperator 203, a steam pressure reducer 204 and a split pressure equalizing hole plate type self-balancing steam-water mixer 205;
the denitrator 101 is communicated with the main turbine ultrahigh pressure cylinder 2 through a pipeline, and the denitrator 101, the dust remover 102, the desulfurizer 103 and CO 2 The adsorption towers 104 are sequentially communicated with each other through pipelines, and CO 2 Rich/lean heat exchanger 105 and CO 2 The adsorption tower 104 is communicated with CO 2 Adsorption tower 104 and CO 2 The rich/lean heat exchanger 105 communicates;
CO 2 the rich liquid/lean liquid heat exchanger 105 is communicated with the CO2 adsorption tower desorption tower 106, and CO 2 Absorption liquid regenerator 107 and CO 2 The rich liquid/lean liquid heat exchanger 105 is communicated with CO 2 The absorption liquid regenerator is communicated with a shell-and-tube low-pressure feed water heater 11a, and CO 2 Absorption liquid regenerator 107 and CO 2 The adsorption tower and the desorption tower 106 are communicated with each other, CO 2 Absorption liquid regenerator 107 and CO 2 The adsorption tower and the desorption tower 106 are communicated with each other, CO 2 The absorption liquid regenerator is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer 205;
the low-pressure feed water heater is communicated with the low-pressure cylinder 5 of the main turbine, the low-pressure feed water heater is respectively communicated with the shell-and-tube low-pressure feed water heater 11a and the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer 205, the shell-and-tube low-pressure feed water heater 11a is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer 205, the high-pressure feed water heater is communicated with the ultrahigh-pressure cylinder 2 of the main turbine, and the shell-and-tube low-pressure feed water heater 11a is communicated with the high-pressure feed water heater after passing through the deaerator 12 and the feed water pump 13;
The main turbine ultra-high pressure cylinder 2 is communicated with the BEST turbine 201, the BEST turbine 201 is communicated with a high-pressure feed water heater, the BEST turbine 201 is communicated with a sub-bin pressure equalizing hole plate type self-balancing steam-water mixer 205, the main turbine ultra-high pressure cylinder 2 is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer 205 after passing through a steam attemperator 203 and a steam pressure reducer 204, the BEST turbine 201 is communicated with the deaerator 12, the pressurizing gas storage 110 is communicated with a gas-liquid separator 109, and the gas-liquid separator 109 is respectively communicated with a condenser 108 and CO 2 The adsorption column desorption column 106 communicates.
As a further limitation of the first aspect of the present invention, the boiler 1, the main turbine ultra-high pressure cylinder 2, the main turbine high pressure cylinder 3, the main turbine intermediate pressure cylinder 4, the main turbine low pressure cylinder 5, the condenser 7, the condensate pump 8 and the shaft seal heater 9 are sequentially communicated through pipelines, and the main generator 6 is communicated with the main turbine low pressure cylinder 5;
a low-pressure feedwater heater including a first low-pressure feedwater heater 10a, a second low-pressure feedwater heater 10b, a third low-pressure feedwater heater 10c, a fourth low-pressure feedwater heater 10d, and a fifth low-pressure feedwater heater 10e that are sequentially communicated;
the first low-pressure feed water heater 10a is respectively communicated with the condenser 7 and the condensate pump 8, the condenser 108 is communicated with a pipeline between the condensate pump 8 and the shaft seal heater 9, and the condenser 108 is communicated with a pipeline between the third low-pressure feed water heater 10c and the fourth low-pressure feed water heater 10 d;
The main turbine intermediate pressure cylinder 4 communicates with a fifth low pressure feedwater heater 10e, and the fifth low pressure feedwater heater 10e communicates with a shell-and-tube low pressure feedwater heater 11 a.
In the present embodiment, it is preferable that the shaft seal heater 9 is communicated with the condenser 7, and the main turbine low pressure cylinder 5 is respectively communicated with the first low pressure feedwater heater 10a, the second low pressure feedwater heater 10b, the third low pressure feedwater heater 10c and the fourth low pressure feedwater heater 10 d.
In this embodiment, preferably, the high-pressure feedwater heater includes a first high-pressure feedwater heater 14a, a second high-pressure feedwater heater 14b, a third high-pressure feedwater heater 14c, a fourth high-pressure feedwater heater 14d, and a fifth high-pressure feedwater heater 14e that are sequentially connected by pipes;
the first high-pressure feedwater heater 14a communicates with the feedwater pump 13 and the deaerator 12, respectively, and the BEST steam turbine 201 communicates with the first high-pressure feedwater heater 14a, the second high-pressure feedwater heater 14b, the third high-pressure feedwater heater 14c, and the fourth high-pressure feedwater heater 14d, respectively;
the main turbine ultra-high pressure cylinder 2 is communicated with a fifth high pressure feed water heater 14e, the fifth high pressure feed water heater 14e is communicated with the boiler 1, and the BEST turbine 201 is communicated with the BEST turbine generator 202.
As the change of the extraction parameters is larger when the secondary reheating unit runs under variable working conditions, and meanwhile, the CO in the post-combustion carbon capture technology 2 The amount of steam extraction consumed by the regeneration of the adsorbent is large, especially when the unit is operated at low load, CO 2 The extraction steam consumption of the capture system will seriously affect the thermal efficiency of the main turbine. Thus, for CO 2 Continuous steam extraction requirement of capturing device, using BEST steam turbine (variable speed back-pumping water supply pump steam turbine, back pressure Extraction Steam Turbine) to replace existing main steam turbine, CO 2 The extraction steam sources of the capturing device are changed into four-way steam sources which are complementary to air so as to meet the continuous extraction steam requirement under the variable load operation working condition, and the four-way steam sources are respectively:
the first path of steam source is a communication pipe steam extraction source of a main turbine intermediate pressure cylinder 4 and a main turbine intermediate pressure cylinder 5, and the path of steam source is a secondary reheating unit set for load operationThe thermodynamic parameters of the main steam source under the working condition just meet the requirements of CO 2 The temperature and pressure conditions required for desorption and regeneration of the adsorbent;
the second path of steam source is a variable-speed back-pumping type water supply pump steam turbine 201 steam exhaust steam source, under the full-load operation condition, the variable-speed back-pumping type water supply pump steam turbine exhaust steam enters a low-pressure water supply heater 11a for heating condensed water in a power plant water-steam circulation system, under the full-load operation condition to 70% load operation condition of a secondary reheating unit, the extracted part of the BEST steam turbine 201 exhaust steam enters a thermodynamic self-balancing steam-water mixer for assisting the first path of steam source to be a main steam turbine medium pressure cylinder 4 and a main steam turbine medium pressure cylinder 5 communication pipe steam exhaust steam source for heating CO together 2 Desorbing and regenerating the adsorbent;
the third steam source is a previous stage steam extraction source for exhausting steam of the variable-speed back-extraction type water feeding pump steam turbine 201, under the full-load operation condition, the steam extraction is used for entering the deaerator 12 to heat water supply, under the 70% load operation to 50% load operation condition of the secondary reheating unit, on the basis of the steam extraction of the first and second steam sources, the third steam source is extracted to enter the thermodynamic self-balancing steam-water mixer 205 to be used as an auxiliary steam source for heating CO together 2 Desorbing and regenerating the adsorbent;
the fourth path of steam source is the ultra-high pressure cylinder 2 steam exhaust source of the main turbine, under the full-load operation condition, the ultra-high pressure cylinder 2 steam exhaust of the main turbine is divided into three parts, and is respectively used for the steam inlet of the variable-rotation-speed back-pumping type feed pump steam turbine 201, the steam source of the final stage (according to the feed water flow direction) fifth high-pressure feed water heater 14e and the reheat cold section steam of the boiler 1, under the operation condition from 50% load operation to 30% load operation of the secondary reheating unit, the ultra-high pressure cylinder 2 steam exhaust of the main turbine is extracted on the basis of the extraction of the first, second and third paths of steam sources, and enters the thermodynamic self-balancing steam-water mixer 205 after the parameters are adjusted by the attemperator 203 and the pressure reducer 204, and is used as an auxiliary steam source for heating CO together 2 The adsorbent is desorbed and regenerated, and the cooled water-steam mixture is returned to the shell-and-tube low-pressure feed water heater 11a.
In order to ensure that each path of steam source enters the thermodynamic self-balancing steam-water mixer 205 without abnormal working conditions such as flash evaporation and the like during the variable working condition operation, all stages of extraction steam and water in the thermodynamic self-balancing steam-water mixer are mixed, and the temperature and pressure parameters are correspondingly regulated by each throttle orifice in the mixer so as to control the fluctuation of mixed gas in the process of starting and stopping of multiple steam sources.
Meanwhile, in this embodiment, the waste heat of the gas at the outlet of the resolving tower 106 and the waste heat of the condenser 108 are also collected to replace the heat of the extracted steam for heating the water supply, so that the overall thermal economy of the thermodynamic system is further improved, the heated water supply is taken from the outlet position of the condensate pump 8, and the heated water supply is returned and injected to the outlet of the third low-pressure feedwater heater 10 c.
Example 2:
as shown in fig. 2, embodiment 2 of the present invention provides a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit, comprising: denitration device 101, dust remover 102, desulfurization device 103, and CO 2 Adsorption tower 104, CO 2 Rich/lean liquid heat exchanger 105, CO 2 Adsorption tower desorption tower 106, CO 2 An absorption liquid regenerator, a condenser 108, a gas-liquid separator 109, a pressurized gas storage 110, a BEST steam turbine 201, a BEST steam turbine generator 202, a steam attemperator 203, a steam pressure reducer 204 and a pressure equalizing four-way valve type self-balancing steam-water mixer 206;
The denitrator 101 is communicated with the main turbine ultrahigh pressure cylinder 2 through a pipeline, and the denitrator 101, the dust remover 102, the desulfurizer 103 and the CO2 adsorption tower 104 are sequentially communicated through pipelines, and CO 2 Rich/lean heat exchanger 105 and CO 2 The adsorption tower 104 is communicated with CO 2 Adsorption tower 104 and CO 2 The rich/lean heat exchanger 105 communicates;
CO 2 rich/lean heat exchanger 105 and CO 2 The adsorption tower and the desorption tower 106 are communicated with each other, CO 2 Absorption liquid regenerator and CO 2 The rich liquid/lean liquid heat exchanger 105 is communicated with CO 2 The absorption liquid regenerator is communicated with a mixed low-pressure feed water heater 11b, and CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower 106 are communicated with each other, CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower 106 are communicated with each other, CO 2 The absorption liquid regenerator is communicated with a pressure equalizing four-way valve type self-balancing steam-water mixer 206;
the low-pressure feed water heater is communicated with the main turbine low-pressure cylinder 5, the low-pressure feed water heater is respectively communicated with the mixed low-pressure feed water heater 11b and the pressure-equalizing four-way valve type self-balancing steam-water mixer 206, the mixed low-pressure feed water heater 11b is communicated with the pressure-equalizing four-way valve type self-balancing steam-water mixer 206 through the steam attemperator 203 and the steam attemperator 204, the high-pressure feed water heater is communicated with the main turbine ultrahigh-pressure cylinder 2, and the mixed low-pressure feed water heater 11b is communicated with the high-pressure feed water heater after passing through the deaerator 12 and the feed water pump 13;
The main turbine ultra-high pressure cylinder 2 is communicated with the BEST turbine 201, the BEST turbine 201 is communicated with a high-pressure feed water heater, the BEST turbine 201 is communicated with a pressure-equalizing four-way valve type self-balancing steam-water mixer 206 after passing through a steam attemperator 203 and a steam pressure reducer 204, the main turbine ultra-high pressure cylinder 2 is communicated with a separation pressure-equalizing hole plate type self-balancing steam-water mixer 205 after passing through the steam attemperator 203 and the steam pressure reducer 204, the BEST turbine 201 is communicated with a deaerator 12, the pressurizing gas storage 110 is communicated with a gas-liquid separator 109, and the gas-liquid separator 109 is respectively communicated with a condenser 108 and CO 2 The adsorption column desorption column 106 communicates.
In this embodiment, preferably, the boiler 1, the main turbine ultra-high pressure cylinder 2, the main turbine high pressure cylinder 3, the main turbine intermediate pressure cylinder 4, the main turbine low pressure cylinder 5, the condenser 7, the condensate pump 8 and the shaft seal heater 9 are sequentially communicated through pipelines, and the main generator 6 is communicated with the main turbine low pressure cylinder 5;
a low-pressure feedwater heater including a first low-pressure feedwater heater 10a, a second low-pressure feedwater heater 10b, a third low-pressure feedwater heater 10c, a fourth low-pressure feedwater heater 10d, and a fifth low-pressure feedwater heater 10e that are sequentially communicated;
the first low-pressure feed water heater 10a is respectively communicated with the condenser 7 and the condensate pump 8, the condenser 108 is communicated with a pipeline between the condensate pump 8 and the shaft seal heater 9, and the condenser 108 is communicated with a pipeline between the third low-pressure feed water heater 10c and the fourth low-pressure feed water heater 10 d;
The main turbine intermediate pressure cylinder 4 communicates with a fifth low pressure feedwater heater 10e, and the fifth low pressure feedwater heater 10e communicates with a shell-and-tube low pressure feedwater heater 11 a.
In the present embodiment, it is preferable that the shaft seal heater 9 is communicated with the condenser 7, and the main turbine low pressure cylinder 5 is respectively communicated with the first low pressure feedwater heater 10a, the second low pressure feedwater heater 10b, the third low pressure feedwater heater 10c and the fourth low pressure feedwater heater 10 d.
In this embodiment, preferably, the high-pressure feedwater heater includes a first high-pressure feedwater heater 14a, a second high-pressure feedwater heater 14b, a third high-pressure feedwater heater 14c, a fourth high-pressure feedwater heater 14d, and a fifth high-pressure feedwater heater 14e that are sequentially connected by pipes;
the first high-pressure feedwater heater 14a communicates with the feedwater pump 13 and the deaerator 12, respectively, and the BEST steam turbine 201 communicates with the first high-pressure feedwater heater 14a, the second high-pressure feedwater heater 14b, the third high-pressure feedwater heater 14c, and the fourth high-pressure feedwater heater 14d, respectively;
the main turbine ultra-high pressure cylinder 2 is communicated with a fifth high pressure feed water heater 14e, the fifth high pressure feed water heater 14e is communicated with the boiler 1, and the BEST turbine 201 is communicated with the BEST turbine generator 202.
In this embodiment, the four-way steam source enters the pressure equalizing four-way valve type self-balancing steam-water mixer 206 as an auxiliary steam source for heating CO 2 The adsorbent is desorbed and regenerated, and the cooled water-steam mixture is returned to the hybrid low-pressure feedwater heater 11b.
Example 3:
the embodiment 3 of the invention provides a working method of a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit, which is characterized by comprising the following steps of:
under the full-load operation condition of the secondary reheating unit, the first path of steam source is a main steam source, and under the full-load operation condition, steam discharged by a steam turbine of the variable-speed back-pumping type water supply pump 13 enters a low-pressure water supply heater and is used for heating condensed water in a water-steam circulation system of the power plant, wherein the first path of steam source is a medium-pressure cylinder and low-pressure cylinder communicating pipe steam-extracting source;
in IIUnder the working condition that the secondary reheating unit is operated at full load to 70% of load, the exhaust steam of the extraction part BEST steam turbine 201 enters a thermodynamic self-balancing steam-water mixer to serve as a second path of steam source, and the auxiliary first path of steam source is a medium-pressure cylinder and low-pressure cylinder communicating pipe extraction steam source which are used for heating CO together 2 Desorbing and regenerating the adsorbent;
under the working condition that the secondary reheating unit operates from 70% of load to 50% of load, on the basis of the extraction of the first path of steam source and the extraction of the second path of steam source, extracting a third path of steam source to enter a thermodynamic self-balancing steam-water mixer, and taking the third path of steam source as an auxiliary steam source to be used for heating CO together 2 The adsorbent is desorbed and regenerated, the third steam source is a previous stage steam extraction source of steam exhausted by a steam turbine of a variable-speed back-extraction water feed pump 13, and under the full-load operation condition, the third steam source is used for entering a deaerator 12 to heat water supply;
under the working condition that the secondary reheating unit runs from 50% to 30% under the load, the ultrahigh pressure cylinder 2 of the main turbine is extracted to serve as a fourth steam source on the basis of the first steam source extraction, the second steam source extraction and the third steam source extraction, and the parameters are adjusted by a desuperheater pressure reducer and then the steam source enters a thermodynamic self-balancing steam-water mixer to serve as an auxiliary steam source for heating CO together 2 Desorbing and regenerating the adsorbent;
the cooled water-steam mixture returns to the shell-and-tube low-pressure feed water heater 11a, the fourth steam source is the steam exhaust source of the main turbine ultrahigh pressure cylinder 2, and under the full-load operation condition, the steam exhaust of the main turbine ultrahigh pressure cylinder 2 is divided into three parts which are respectively used for the steam inlet of the variable-rotation-speed back-pumping feed water pump 13 turbine, the steam exhaust of the final-stage high-pressure feed water heater and the reheat cold-section steam of the boiler 1.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A multi-heat source self-balancing thermodynamic system for capturing carbon under variable working conditions of a secondary reheating unit is characterized in that,
the denitration device is communicated with the main turbine ultrahigh pressure cylinder through a pipeline, and the denitration device, the dust remover, the desulfurizing device and the CO are connected with each other through pipelines 2 The adsorption towers are sequentially communicated with each other through pipelines, and CO 2 Rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower is communicated with CO 2 Adsorption tower and CO 2 The rich liquid/lean liquid heat exchanger is communicated;
CO 2 rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The rich liquid/lean liquid heat exchanger is communicated with CO 2 The absorption liquid regenerator is communicated with a shell-and-tube low-pressure feed water heater, and CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 The absorption liquid regenerator is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer;
the low-pressure feed water heater is communicated with the low-pressure cylinder of the main turbine, the low-pressure feed water heater is respectively communicated with the shell-and-tube low-pressure feed water heater and the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer, the shell-and-tube low-pressure feed water heater is communicated with the sub-bin pressure equalizing hole plate type self-balancing steam-water mixer, the high-pressure feed water heater is communicated with the ultrahigh-pressure cylinder of the main turbine, and the shell-and-tube low-pressure feed water heater is communicated with the high-pressure feed water heater after passing through the deaerator and the feed water pump;
The main turbine ultrahigh pressure cylinder is communicated with the BEST turbine, the BEST turbine is communicated with the high-pressure feed water heater, the BEST turbine is communicated with the sub-compartment pressure equalizing hole plate type self-balancing steam-water mixer, the main turbine ultrahigh pressure cylinder is communicated with the sub-compartment pressure equalizing hole plate type self-balancing steam-water mixer after passing through the steam attemperator and the steam pressure reducer, the BEST turbine is communicated with the deaerator, the pressurizing gas storage is communicated with the gas-liquid separator, and the gas-liquid separator is respectively communicated with the condenser and the CO 2 And the adsorption tower and the desorption tower are communicated.
2. The multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit of claim 1,
the boiler, the main turbine ultrahigh pressure cylinder, the main turbine high pressure cylinder, the main turbine intermediate pressure cylinder, the main turbine low pressure cylinder, the condenser, the condensate pump and the shaft seal heater are sequentially communicated through pipelines, and the main generator is communicated with the main turbine low pressure cylinder;
the low-pressure feed water heater comprises a first low-pressure feed water heater, a second low-pressure feed water heater, a third low-pressure feed water heater, a fourth low-pressure feed water heater and a fifth low-pressure feed water heater which are communicated in sequence;
the first low-pressure feed water heater is respectively communicated with the condenser and the condensate pump, the condenser is communicated with a pipeline between the condensate pump and the shaft seal heater, and the condenser is communicated with a pipeline between the third low-pressure feed water heater and the fourth low-pressure feed water heater;
The main turbine intermediate pressure cylinder is communicated with a fifth low-pressure feed water heater, and the fifth low-pressure feed water heater is communicated with a shell-and-tube low-pressure feed water heater.
3. The multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit as set forth in claim 2,
the shaft seal heater is communicated with the condenser, and the main turbine low-pressure cylinder is respectively communicated with the first low-pressure feed water heater, the second low-pressure feed water heater, the third low-pressure feed water heater and the fourth low-pressure feed water heater.
4. The multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit as set forth in claim 2,
the high-pressure feed water heater comprises a first high-pressure feed water heater, a second high-pressure feed water heater, a third high-pressure feed water heater, a fourth high-pressure feed water heater and a fifth high-pressure feed water heater which are communicated through pipelines in sequence;
the first high-pressure feed water heater is respectively communicated with the feed water pump and the deaerator, and the BEST steam turbine is respectively communicated with the first high-pressure feed water heater, the second high-pressure feed water heater, the third high-pressure feed water heater and the fourth high-pressure feed water heater;
the main turbine ultrahigh pressure cylinder is communicated with a fifth high pressure feed water heater, the fifth high pressure feed water heater is communicated with a boiler, and the BEST turbine is communicated with a BEST turbine generator.
5. A multi-heat source self-balancing thermodynamic system for capturing carbon under variable working conditions of a secondary reheating unit is characterized in that,
the denitration device is communicated with the main turbine ultrahigh pressure cylinder through a pipeline, and the denitration device, the dust remover, the desulfurizing device and the CO are connected with each other through pipelines 2 The adsorption towers are sequentially communicated with each other through pipelines, and CO 2 Rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower is communicated with CO 2 Adsorption tower and CO 2 The rich liquid/lean liquid heat exchanger is communicated;
CO 2 rich liquid/lean liquid heat exchanger and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The rich liquid/lean liquid heat exchanger is communicated with CO 2 The absorption liquid regenerator is communicated with the mixed low-pressure feed water heater, and CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 Absorption liquid regenerator and CO 2 The adsorption tower and the desorption tower are communicated, CO 2 The absorption liquid regenerator is communicated with the pressure equalizing four-way valve type self-balancing steam-water mixer;
the low-pressure feed water heater is communicated with the low-pressure cylinder of the main turbine, the low-pressure feed water heater is respectively communicated with the mixed low-pressure feed water heater and the pressure-equalizing four-way valve type self-balancing steam-water mixer, the mixed low-pressure feed water heater is communicated with the pressure-equalizing four-way valve type self-balancing steam-water mixer through the steam attemperator and the steam pressure reducer, the high-pressure feed water heater is communicated with the ultrahigh-pressure cylinder of the main turbine, and the mixed low-pressure feed water heater is communicated with the high-pressure feed water heater after passing through the deaerator and the feed water pump;
The main turbine ultrahigh pressure cylinder is communicated with the BEST turbine, the BEST turbine is communicated with the high-pressure feed water heater, the BEST turbine is communicated with the pressure-equalizing four-way valve type self-balancing steam-water mixer after passing through the steam attemperator and the steam pressure reducer, the main turbine ultrahigh pressure cylinder is communicated with the dividing pressure-equalizing hole plate type self-balancing steam-water mixer after passing through the steam attemperator and the steam pressure reducer, the BEST turbine is communicated with the deaerator, the pressurizing gas storage is communicated with the gas-liquid separator, and the gas-liquid is separatedThe condenser is respectively connected with the condenser and the CO 2 And the adsorption tower and the desorption tower are communicated.
6. The multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit as set forth in claim 5,
the boiler, the main turbine ultrahigh pressure cylinder, the main turbine high pressure cylinder, the main turbine intermediate pressure cylinder, the main turbine low pressure cylinder, the condenser, the condensate pump and the shaft seal heater are sequentially communicated through pipelines, and the main generator is communicated with the main turbine low pressure cylinder;
the low-pressure feed water heater comprises a first low-pressure feed water heater, a second low-pressure feed water heater, a third low-pressure feed water heater, a fourth low-pressure feed water heater and a fifth low-pressure feed water heater which are communicated in sequence;
the first low-pressure feed water heater is respectively communicated with the condenser and the condensate pump, the condenser is communicated with a pipeline between the condensate pump and the shaft seal heater, and the condenser is communicated with a pipeline between the third low-pressure feed water heater and the fourth low-pressure feed water heater;
The main turbine intermediate pressure cylinder is communicated with a fifth low-pressure feed water heater, and the fifth low-pressure feed water heater is communicated with a shell-and-tube low-pressure feed water heater.
7. The multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit as set forth in claim 6,
the shaft seal heater is communicated with the condenser, and the main turbine low-pressure cylinder is respectively communicated with the first low-pressure feed water heater, the second low-pressure feed water heater, the third low-pressure feed water heater and the fourth low-pressure feed water heater.
8. The multi-heat source self-balancing thermodynamic system for variable-duty carbon capture of a secondary reheat unit as set forth in claim 6,
the high-pressure feed water heater comprises a first high-pressure feed water heater, a second high-pressure feed water heater, a third high-pressure feed water heater, a fourth high-pressure feed water heater and a fifth high-pressure feed water heater which are communicated through pipelines in sequence;
the first high-pressure feed water heater is respectively communicated with the feed water pump and the deaerator, and the BEST steam turbine is respectively communicated with the first high-pressure feed water heater, the second high-pressure feed water heater, the third high-pressure feed water heater and the fourth high-pressure feed water heater;
the main turbine ultrahigh pressure cylinder is communicated with a fifth high pressure feed water heater, the fifth high pressure feed water heater is communicated with a boiler, and the BEST turbine is communicated with a BEST turbine generator.
9. A working method of a multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit, characterized by using the multi-heat-source self-balancing thermodynamic system for variable-working-condition carbon capture of a secondary reheating unit according to any one of claims 1-8, comprising the following processes:
under the full-load operation condition of the secondary reheating unit, the first path of steam source is a main steam source, and under the full-load operation condition, the steam discharged by the variable-speed back-pumping type water feeding pump steam turbine enters a low-pressure water feeding heater and is used for heating condensed water in a water-steam circulation system of the power plant, wherein the first path of steam source is a medium-pressure cylinder and low-pressure cylinder communicating pipe steam-extracting source;
under the working condition that the secondary reheating unit is operated at full load to 70% of load, extracting part of exhaust steam of the BEST turbine enters a thermodynamic self-balancing steam-water mixer to serve as a second path of steam source, and the auxiliary first path of steam source is a medium-pressure cylinder and low-pressure cylinder communicating pipe steam extraction source which are used for heating CO together 2 Desorbing and regenerating the adsorbent;
under the working condition that the secondary reheating unit operates from 70% of load to 50% of load, on the basis of the extraction of the first path of steam source and the extraction of the second path of steam source, extracting a third path of steam source to enter a thermodynamic self-balancing steam-water mixer, and taking the third path of steam source as an auxiliary steam source to be used for heating CO together 2 The adsorbent is desorbed and regenerated, the third steam source is a previous stage of steam extraction source of the variable-speed back-extraction type water feeding pump turbine exhaust steam, and under the full-load operation condition, the third steam source is used for entering the deaerator to heat water feeding;
under the working condition that the secondary reheating unit runs from 50% of load to 30% of load, the ultrahigh pressure cylinder of the main turbine is extracted on the basis of the extraction of the first path of steam source, the extraction of the second path of steam source and the extraction of the third path of steam source, and is used as a fourth path of steam source, and after parameters are adjusted by a desuperheater reducer, the steam enters a thermodynamic self-balancing steam-water mixer to be used as an auxiliary steam source for heating the CO2 adsorbent for desorption and regeneration.
10. The method for operating a multiple heat source self-balancing thermodynamic system for variable duty carbon capture of a secondary reheat unit as claimed in claim 9,
the cooled water-steam mixture returns to the shell-and-tube low-pressure feed water heater, the fourth steam source is the main turbine ultrahigh pressure cylinder steam exhaust source, and under the full-load operation condition, the main turbine ultrahigh pressure cylinder steam exhaust is divided into three parts which are respectively used for variable-rotation-speed back-pumping feed water pump turbine steam inlet, final-stage high-pressure feed water heater steam source and boiler reheat cold section steam.
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