CN115680809A - Shunt recompression pure oxygen combustion circulation system - Google Patents
Shunt recompression pure oxygen combustion circulation system Download PDFInfo
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- CN115680809A CN115680809A CN202211288202.1A CN202211288202A CN115680809A CN 115680809 A CN115680809 A CN 115680809A CN 202211288202 A CN202211288202 A CN 202211288202A CN 115680809 A CN115680809 A CN 115680809A
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- pressure compressor
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- 238000002485 combustion reaction Methods 0.000 title claims abstract description 55
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 title claims description 28
- 239000007789 gas Substances 0.000 claims abstract description 82
- 239000002918 waste heat Substances 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 26
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 78
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 39
- 239000001569 carbon dioxide Substances 0.000 claims description 39
- 239000000446 fuel Substances 0.000 claims description 21
- 229930195733 hydrocarbon Natural products 0.000 claims description 19
- 239000004215 Carbon black (E152) Substances 0.000 claims description 18
- 150000002430 hydrocarbons Chemical class 0.000 claims description 18
- 238000010248 power generation Methods 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000012530 fluid Substances 0.000 claims description 8
- 229940123973 Oxygen scavenger Drugs 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 3
- 230000002000 scavenging effect Effects 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 8
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000005611 electricity Effects 0.000 description 3
- 230000009919 sequestration Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 125000001183 hydrocarbyl group Chemical group 0.000 description 1
- 150000002431 hydrogen Chemical group 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Images
Classifications
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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
- F01K21/00—Steam engine plants not otherwise provided for
- F01K21/04—Steam engine plants not otherwise provided for using mixtures of steam and gas; Plants generating or heating steam by bringing water or steam into direct contact with hot gas
-
- 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
- F01K9/00—Plants characterised by condensers arranged or modified to co-operate with the engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
- F02B29/00—Engines characterised by provision for charging or scavenging not provided for in groups F02B25/00, F02B27/00 or F02B33/00 - F02B39/00; Details thereof
- F02B29/04—Cooling of air intake supply
- F02B29/0406—Layout of the intake air cooling or coolant circuit
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
-
- 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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/12—Improving ICE efficiencies
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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)
- Thermal Sciences (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
A combustion chamber, a gas turbine, a waste heat boiler, a first low-pressure compressor, a first intercooler and a first high-pressure compressor are sequentially connected in series, a low-pressure steam turbine, a condenser, a condensate pump, a deaerator and a water feed pump are sequentially connected in series, a hot end outlet side of the waste heat boiler is connected with a high-temperature inlet side of the low-pressure steam turbine and an inlet side of the first low-pressure compressor, working media flowing out of the hot end outlet side of the waste heat boiler are enabled to be divided, a liquid outlet side of the water feed pump is connected with a cold end inlet side of the waste heat boiler, a high-pressure steam turbine is arranged between the cold end outlet side of the waste heat boiler and the inlet side of the combustion chamber, a low-temperature outlet side of the high-pressure steam turbine is respectively connected with the cold end of the first intercooler and the gas turbine, an outlet side of the first intercooler is connected with the inlet side of the combustion chamber, a hot end inlet side is connected with the outlet side of the first low-pressure compressor, and a hot end outlet side of the first high-pressure compressor is connected with the cold end of the first high-pressure compressor.
Description
The application is a divisional application of Chinese patent application with the application date of 2022, 1 month and 24 days, the application number of 202210079459.X, and the invention name of the invention of a split-flow recompression pure oxygen combustion circulating system.
Technical Field
The application relates to the field of cyclic power generation, in particular to a technical device for controlling greenhouse gas emission, a carbon emission reduction technical device, a carbon capture and carbon sequestration technology and a utilization system.
Background
Although the existing coal-fired power plant and gas-steam combined cycle power plant can ensure stable power supply, the cycle power generation system of the power plant generally adopts air as a combustion improver at present, and in this case, CO is not added in the working medium 2 Since there are other types of gases, such as nitrogen, the decarburization process using the carbon capture and storage utilization measures is complicated, greatly affects the system efficiency, and is expensive.
On the other hand, in the conventional gas-steam combined cycle power generation system, the working medium flowing in the top cycle (gas power generation) and the working medium flowing in the bottom cycle (steam power generation) are generally operated separately, and heat exchange is only performed at the waste heat boiler, so that the heat exchange loss is large and the energy utilization efficiency is low.
Therefore, an advanced thermodynamic cycle form for a future power generation system is urgently needed, which can maximally reduce carbon emission and even realize near zero emission while satisfying high energy utilization efficiency and stable operation, and is used for electric bottom supporting to ensure stable supply of electric power.
Disclosure of Invention
The present application has been made in view of the state of the art described above. An object of this application is to provide a reposition of redundant personnel recompression pure oxygen combustion cycle system, it can separate the target exhaust gas through simple gas-liquid separation structure to with steam cycle and gas circulation organic combination, reduce the heat transfer loss with the principle of energy cascade utilization, improved energy efficiency.
Therefore, the following technical scheme is adopted in the application.
A flow-dividing recompression pure oxygen combustion circulating system is provided, which is a circulating power generation system taking pure oxygen as a combustion improver, a combustion chamber, a gas turbine, a waste heat boiler, a first low-pressure compressor, a first intercooler and a first high-pressure compressor are sequentially connected in series to form a flow path for circulation of a working medium, a low-pressure steam turbine, a condenser, a condensate water pump, a deaerator and a water feed pump are sequentially connected in series to form a flow path for gas-liquid separation,
the hot end outlet side of the waste heat boiler is connected with the high-temperature inlet side of the low-pressure steam turbine and the inlet side of the first low-pressure compressor, so that the working medium flowing out of the hot end outlet side of the waste heat boiler is divided,
the liquid outlet side of the water feeding pump is connected with the cold end inlet side of the waste heat boiler, a high-pressure steam turbine is arranged on a flow path between the cold end outlet side of the waste heat boiler and the inlet side of the combustion chamber, the low-temperature outlet side of the high-pressure steam turbine is respectively connected with the cold end inlet side of the first intercooler and the gas turbine, the cold end outlet side of the first intercooler is connected with the inlet side of the combustion chamber, the hot end inlet side is connected with the outlet side of the first low-pressure compressor, and the hot end outlet side is connected with the inlet side of the first high-pressure compressor.
The target exhaust gas can be separated by a gas-liquid separation structure of a simple structure such as a condenser, and the steam cycle including each steam turbine and the gas cycle including the gas turbine are organically combined to reduce heat exchange loss by the principle of energy cascade utilization, thereby improving energy utilization efficiency. In addition, the position of the first intercooler is arranged, so that the temperature difference of the cold end and the hot end of the first intercooler is reduced, and the heat exchange loss is further reduced.
In at least one embodiment, a medium-pressure steam turbine is provided in the flow path between the high-pressure steam turbine and the gas turbine.
Through setting up middling pressure steam turbine, when still having higher residual pressure from the working medium that high pressure steam turbine flows, can utilize middling pressure steam turbine to carry out the secondary expansion and do work, turn into mechanical energy with heat energy and in order to drive the generator to can improve energy utilization efficiency more high-efficiently.
In at least one embodiment, when the fuel supplied to the combustion chamber is hydrogen, the gas deoxygenated in the deoxygenator is directly discharged to the outside.
The liquid working medium and the target exhaust gas to be collected can be obtained through a simple gas-liquid separation structure, so that the working procedure is simple, and the cost is reduced.
In at least one embodiment, further comprising a carbon dioxide capture system that receives gases from the gas outlet side of the condenser and the gas outlet side of the oxygen scavenger when the fuel supplied to the combustion chamber is a hydrocarbon.
By providing the carbon dioxide capture system, the carbon dioxide discharged from the condenser and the deaerator can be effectively collected for utilization or sequestration.
In at least one embodiment, the carbon dioxide capture system includes a second low-pressure compressor, a middle-pressure compressor, a second high-pressure compressor, and a second intercooler, an inlet side of the second low-pressure compressor is connected to a gas outlet side of the condenser, an outlet side of the second low-pressure compressor is connected to a hot end inlet side of the second intercooler, a hot end outlet side of the second intercooler is connected to an inlet side of the middle-pressure compressor, an outlet side of the middle-pressure compressor is connected to an inlet side of the second high-pressure compressor, and a gas outlet side of the deaerator is connected to an inlet side of the second high-pressure compressor.
As described above, the total capture of carbon dioxide can be achieved only by a plurality of compressors and intercoolers, and zero emission can be achieved with a simple process and low cost.
In at least one embodiment, the exhaust-heat boiler further comprises a flow dividing device, the flow dividing device is arranged at a branch of the exhaust-heat boiler to the first low-pressure compressor and the low-pressure steam turbine, and is used for adjusting the ratio of the working medium flowing to the low-pressure steam turbine and the first low-pressure compressor.
Can adapt to the supply of different hydrocarbon fuels, and ensures the high energy utilization efficiency.
In at least one embodiment, if the proportion of carbon in the hydrocarbon fuel is increased, the proportion of the working medium flowing to the low-pressure steam turbine in the working medium flowing out of the waste heat boiler is decreased by the flow dividing device.
The proportion of the working medium of each branch can be adjusted according to the proportion of hydrocarbon, so that the utilization efficiency of high energy is ensured.
In at least one embodiment, the low pressure steam turbine discharges a portion of the working fluid to the deaerator to heat the liquid working fluid in the deaerator prior to expansion to perform work.
The heat of the working medium in the flow path can be directly utilized to carry out thermal type deoxidization, thereby realizing the energy gradient utilization and reducing the heat exchange loss.
In at least one embodiment, an oxygen scavenger is added to the oxygen scavenger to remove oxygen.
Oxygen removal is carried out by a simple chemical oxygen removal means.
In at least one embodiment, the working fluid flowing through the flow path from the condenser to the waste heat boiler is water, and the working fluid flowing through the flow path other than the flow path from the condenser to the waste heat boiler is steam or a mixture of steam and carbon dioxide.
Compared with power circulation using carbon dioxide and other gases as working media, when water vapor or a mixture of the water vapor and the carbon dioxide is used as the working media, the equipment used by the circulation system has lower processing difficulty and lower cost.
Drawings
FIG. 1 illustrates a schematic diagram of a split-flow recompression pure oxygen combustion cycle system of an embodiment of the present application when the fuel is a hydrocarbon.
FIG. 2 illustrates a schematic diagram of a split-flow recompression pure oxygen combustion cycle system of an embodiment of the present application when the fuel is hydrogen.
Description of the reference numerals
1. Combustion chamber
2. Gas turbine
3. Waste heat boiler
4. First low-pressure compressor
5. First intercooler
6. First high-pressure compressor
7. Low-pressure steam turbine
8. Condenser
9. Condensate pump
10. Deaerator
11. Water supply pump
12. High-pressure steam turbine
13. Medium pressure steam turbine
14. Carbon dioxide capture system
141. Second low-pressure compressor
142. Medium pressure gas compressor
143. Second high-pressure compressor
144. Second intercooler
15. Flow divider
Detailed Description
Exemplary embodiments, features and aspects of the present application will be described in detail below with reference to the accompanying drawings.
In the following detailed description, numerous specific details are set forth in order to provide a better understanding of the present application. It will be understood by those skilled in the art that the present application may be practiced without some of these specific details. In some instances, methods, means, elements well known to those skilled in the art have not been described in detail so as not to obscure the present application.
The technical idea of the present application is briefly described below. The application provides a novel reposition of redundant personnel recompression pure oxygen combustion cycle system. The circulating system takes pure oxygen as a combustion improver and steam as a power circulating working medium, realizes zero emission of carbon dioxide by arranging a carbon dioxide trapping system with simple structure and low cost in the circulating system, and reduces heat exchange loss to the maximum extent by a principle of energy gradient utilization in a shunting recompression mode. The method is suitable for the circulating power generation system taking hydrocarbon or pure hydrogen as fuel, and can effectively improve the utilization rate of energy.
The following description will first describe a split-flow recompression pure oxygen combustion cycle system in accordance with a first embodiment of the present application with reference to the accompanying drawings.
First embodiment
The split-flow recompression pure oxygen combustion cycle system of the present embodiment can be applied to the case where the fuel is hydrocarbon. As shown in fig. 1, a combustion chamber 1, a gas turbine 2, a waste heat boiler 3, a flow dividing device 15, a first low-pressure compressor 4 and a first high-pressure compressor 6 are sequentially connected in series to form a flow path for working medium circulation, the flow path may be a semi-closed loop, and a low-pressure steam turbine 7, a condenser 8, a condensate water pump 9, a deaerator 10 and a water feed pump 11 are sequentially connected in series to form a flow path for gas-liquid separation.
Specifically, the outlet side of the combustion chamber 1 is connected to the high-temperature inlet side of the gas turbine 2, the low-temperature outlet side of the gas turbine 2 is connected to the hot-end inlet side of the exhaust-heat boiler 3, and the hot-end outlet side of the exhaust-heat boiler 3 is branched at the branching device 15 to be respectively connected to the high-temperature inlet side of the low-pressure steam turbine 7 and the inlet side of the first low-pressure compressor 4, thereby completing the gas power generation and the branching from the exhaust-heat boiler 3.
A first intercooler 5 may be provided in the flow path between the first low-pressure compressor 4 and the first high-pressure compressor 6. On a flow path from the flow dividing device 15 to the combustion chamber 1 via the first low-pressure compressor 4, the first intercooler 5 and the first high-pressure compressor 6, an outlet side of the first low-pressure compressor 4 is connected to an inlet side of a hot end of the first intercooler 5, an outlet side of the hot end of the first intercooler 5 is connected to an inlet side of the first high-pressure compressor 6, and an outlet side of the first high-pressure compressor 6 is connected to an inlet side of the combustion chamber. Thereby, compression of the working medium is completed.
On the flow path from a flow dividing device 15 to a waste heat boiler 3 through a low-pressure steam turbine 7, a condenser 8, a condensate water pump 9, a deaerator 10 and a water supply pump 10, the low-pressure steam turbine 7 receives working media from a hot end outlet of the waste heat boiler 3 after being divided, the working media are expanded to do work to complete conversion of heat energy to mechanical energy, part of extracted air is used for deaerating the deaerator 10, the outlet working media are connected with the inlet side of the condenser 8, the gas outlet side of the condenser 8 is connected with a carbon dioxide capture system 14, the liquid outlet side is connected with the inlet side of the condensate water pump 9, the outlet side of the condensate water pump 9 is connected with the outside and the liquid inlet side of the deaerator 10, the gas outlet side of the deaerator 10 is connected with the carbon dioxide capture system 14, the liquid outlet side is connected with the water supply pump 11, and the outlet side of the water supply pump 11 is connected with the cold end inlet side of the waste heat boiler 3. Thus, the gas-liquid separation of the working medium and the capture of the carbon dioxide are completed.
A high-pressure steam turbine 12 is provided in the flow path between the outlet side of the cold end of the waste heat boiler 3 and the inlet side of the combustion chamber 1, and an intermediate-pressure steam turbine 13 is provided between the high-pressure steam turbine 12 and the gas turbine 2. The low-temperature outlet side of the high-pressure steam turbine 12 is connected to the cold-end inlet side of the first intercooler 5 and the high-temperature inlet side of the intermediate-pressure steam turbine 13, respectively, and the low-temperature outlet side of the intermediate-pressure steam turbine 13 is connected to the gas turbine 2. In the first intercooler 5, the outlet side of the cold end is connected to the inlet side of the combustion chamber 1, the inlet side of the hot end is connected to the outlet side of the first low-pressure compressor 4, and the outlet side of the hot end is connected to the inlet side of the first high-pressure compressor 6. Therefore, the steam power generation and the preheating of the working medium after the expansion and the work of each steam turbine are completed.
The flow path and the energy change of the working medium according to the embodiment of the present invention will be further explained below.
First, a hydrocarbon having a pressure of, for example, 4MPa as a fuel and high-pressure pure oxygen as a combustion improver are supplied to the combustion chamber 1, and after combustion, a high-temperature gas containing mainly steam and carbon dioxide doped therein is generated, the temperature of which increases and the pressure of which slightly decreases. Then, the high-temperature gas enters the gas turbine 2 to be expanded and work, and the thermal energy is converted into mechanical energy to cause the gas turbine to drive a generator (not shown) to generate electricity. In one example, the pressure of the high-temperature gas flowing into the gas turbine 2 may be, for example, 3.8MPa, and the pressure of the gas flowing out of the gas turbine 2 may be, for example, 0.1MPa. The gas working medium with reduced temperature and pressure after expansion work enters the hot end inlet side of the waste heat boiler 3, the gas with further reduced temperature is obtained at the hot end outlet side of the waste heat boiler 3, the gas is divided into one flow flowing to the low-pressure steam turbine 7 at the dividing device 15, the other flow flows to the first low-pressure compressor 4, and the pressure of the two flows is 0.1MPa for example. In one example, the inlet pressure of the low-pressure steam turbine 7 may be, for example, 0.1MPa and the outlet pressure may be, for example, 2.5kPa.
As for the gas flowing to the first low-pressure compressor 4, the gas is compressed in the first low-pressure compressor 4 to a pressure increased to, for example, 1.4 MPa. The gas flows out from the outlet side of the first low-pressure compressor 4 and flows into the hot end inlet side of the first intercooler 5, and the working medium flowing into the cold end is preheated in the first intercooler 5 and flows out from the hot end outlet side. The gas flowing out from the hot end outlet side of the first intercooler 5 flows into the first high-pressure compressor 6, is compressed in the first high-pressure compressor 6 to be increased in temperature and suddenly increased in pressure to be almost the same as the pressure of the hydrocarbon and the pure oxygen, flows out from the first high-pressure compressor 6, and returns to the combustion chamber 1. In one example, the inlet pressure of the high pressure compressor 6 may be, for example, 1.4MPa and the outlet pressure may be, for example, 4MPa.
As for the gas flowing to the low pressure steam turbine 7, a part of the gas directly flows to the deaerator 10 without performing expansion work for thermal deaerating of a liquid working medium described later, and the other part of the gas expands in the low pressure steam turbine 7 to perform work due to a vacuum environment connected at an outlet of the low pressure steam turbine 7, and the pressure is reduced to be close to vacuum, so that gas-liquid separation in the condenser 8 described later is performed. The near-vacuum gas flows out of the low-pressure steam turbine 7 and flows into the condenser 8 to be subjected to gas-liquid separation, that is, in the condenser 8, the steam in the near-vacuum gas working medium is cooled into liquid water and discharged to the condensate pump 9 to be pressurized, and on the other hand, the carbon dioxide in the near-vacuum gas working medium is kept in a gaseous state and discharged to the carbon dioxide capture system 14. A part of the water pressurized by the condensate pump 9 is directly discharged to the outside, and the other part of the water flows into the deaerator 10. The liquid water flowing into the deaerator 10 is separated into residual carbon dioxide by the higher temperature gas discharged from the low pressure steam turbine 7, and is discharged to the carbon dioxide capture system 14 through the gas outlet of the deaerator 10. So far, the capture of carbon dioxide in the circulating system is completed, and the zero emission of the carbon dioxide is realized.
The liquid working medium flowing out of the liquid outlet side of the deaerator 10 is pressurized in the feed water pump 11, and the pressurized liquid working medium increases in pressure abruptly and flows into the cold end inlet side of the waste heat boiler 3. The liquid working medium flowing into the exhaust-heat boiler 3 is heated and pressurized into a supercritical gas (i.e., steam) working medium with a pressure of 20MPa or more, and then flows into the high-temperature inlet side of the high-pressure steam turbine 12 from the outlet of the cold end of the exhaust-heat boiler 3. The gas flowing into the high pressure steam turbine 12 expands to work, converts the thermal energy into mechanical energy to allow the steam turbine to drive the generator to generate electricity, and discharges a gas working medium with a pressure reduced to, for example, 4MPa from the low temperature outlet side of the high pressure steam turbine 12. A part of the gas flowing out of the high-pressure steam turbine 12 flows into the cold-side inlet side of the first intercooler 5, and the other part flows into the high-temperature inlet side of the intermediate-pressure steam turbine 13. The gas flowing into the cold end of the first intercooler 5 is preheated and then discharged from the cold end outlet side to the combustion chamber 1. On the other hand, the temperature and pressure of the gas flowing into the intermediate pressure steam turbine 13 are reduced in the intermediate pressure steam turbine 13, and the gas flows out from the low temperature outlet side and flows into the gas turbine 2 for cooling the gas turbine 2, and here, if the pressure of the gas working medium flowing out from the high pressure steam turbine 12 is high and the ratio of the inlet pressure to the outlet pressure of the intermediate pressure steam turbine 13 can be made to be 1.2 or more, the intermediate pressure steam turbine 13 performs expansion work to drive the steam turbine to generate electricity in the same manner as the high pressure steam turbine 12, and if the pressure of the gas working medium flowing out from the high pressure steam turbine 12 is low and the ratio of the inlet pressure to the outlet pressure of the intermediate pressure steam turbine 13 is made to be less than 1.2, the intermediate pressure steam turbine 13 does not perform expansion work and only slightly reduces the temperature pressure of the working medium.
Hereinafter, the above-mentioned carbon dioxide capture system 14 will be described.
The carbon dioxide capture system 14 comprises a second low-pressure compressor 141, an intermediate-pressure compressor 142, a second high-pressure compressor 143 and a second intercooler 144, wherein the inlet side of the second low-pressure compressor 141 is connected with the gas outlet side of the condenser 8, the outlet side of the second low-pressure compressor 141 is connected with the hot end inlet side of the second intercooler 144, the hot end outlet side of the second intercooler 144 is connected with the inlet side of the intermediate-pressure compressor 142, the outlet side of the intermediate-pressure compressor 142 is connected with the inlet side of the second high-pressure compressor 143, and the gas outlet side of the deaerator 10 is connected with the inlet side of the second high-pressure compressor 143.
The gas discharged from the condenser 8, i.e., carbon dioxide, flows into the second low-pressure compressor 141 for compression, flows into the intermediate-pressure compressor 142 via the second intercooler 144 for recompression, and the gas flowing out of the intermediate-pressure compressor 142 flows into the second high-pressure compressor 143 together with the gas discharged from the deaerator 10 for final use or sequestration.
The flow split when different hydrocarbon fuels are supplied will be explained further below.
A proportional splitter valve for adjusting the flow rate of each branch may be provided in the splitter 15, and when the hydrocarbon ratio of the hydrocarbon fuel supplied to the combustion chamber 1 is changed, the ratio of the working medium flowing to the first low-pressure compressor 4 and the working medium flowing to the low-pressure steam turbine 7 may be adjusted by adjusting the proportional splitter valve, so that the efficiency of the circulation system is maximized. Specifically, because the proportion of the carbon dioxide in the combustion product increases with the increase of the carbon-hydrogen ratio in the fuel, the proportion of water decreases, and the specific heat capacity of the carbon dioxide is about one half of that of water under the same temperature and pressure, therefore, the heat release quantity of the hot end of the waste heat boiler is lower when the proportion of the carbon dioxide is higher, and the cold end working medium is pure matter of water, therefore, under the same temperature difference, the heat absorption quantity of the cold end does not change along with the change of the fuel, and is only related to the working medium flow, which leads to that the heat release quantity of the hot end of the waste heat boiler 3 is positively related to the cold end working medium flow, that is, when the proportion of the carbon dioxide is larger, the heat release quantity of the hot end of the waste heat boiler 3 is smaller, and the cold end working medium flow is smaller. Therefore, if the proportion of carbon in the hydrocarbon fuel is increased, the proportion of the working medium flowing to the low-pressure steam turbine 7 in the working medium flowing out of the waste heat boiler 3 is decreased by the flow dividing device 15, and the utilization rate of energy is increased.
According to the circulation system as described above, the following effects can be obtained:
(1) Compared with the traditional gas-steam combined cycle system, the combined cycle system organically combines a gas cycle comprising a gas turbine and a steam cycle comprising each steam turbine, thereby realizing the joint of mass and energy and improving the energy utilization efficiency by the principle of energy cascade utilization.
(2) By providing the first intercooler at the position as described above, the temperature difference between the outlet and the inlet of the intercooler can be reduced as compared with the case where the intercooler is provided between the exhaust-heat boiler and the high-pressure steam turbine in the past, thereby reducing the heat exchange loss.
(3) Through setting up middling pressure steam turbine, when the gaseous working medium that flows from high pressure steam turbine still has great residual pressure, can utilize middling pressure steam turbine to carry out the secondary expansion and do work, turn into mechanical energy with heat energy in order to drive the generator to can improve energy utilization efficiency more high-efficiently.
(4) The proportion of working media in each branch is adjusted by arranging the flow dividing device, so that even if different hydrocarbon fuels are supplied to the combustion chamber 1, the efficient operation under the supply of different hydrocarbon fuels can be met by adjusting the proportion of the working media in each branch.
(5) By using pure oxygen as a combustion improver and using the working medium as steam, the carbon dioxide doped in the steam can be separated by using the simple gas-liquid separation part of the condenser 8 to capture the carbon dioxide, so that carbon neutralization can be performed with low cost.
(6) Through setting up carbon dioxide entrapment system, can collect the carbon dioxide of following condenser and oxygen-eliminating device exhaust effectively, realize the zero release.
Second embodiment
FIG. 2 illustrates a split-flow recompression pure oxygen combustion cycle system in accordance with a second embodiment of the present application. The same or similar components as those of the first embodiment are denoted by the same or similar reference numerals, and detailed description thereof is omitted.
The split-flow recompression pure oxygen combustion cycle system of the embodiment can be applied to the condition that the fuel is hydrogen. As shown in fig. 2, the difference from the first embodiment is that: (1) Since the combustion products of hydrogen and oxygen are water vapor, not doped with carbon dioxide, the circulation system of the present embodiment does not include the carbon dioxide capture system 14; (2) Because the working medium proportion of each branch is not required to be adjusted according to the hydrocarbon proportion of hydrocarbons, the flow dividing device 15 provided with the proportion adjusting valve is not arranged, and only one path of gas working medium flowing into the hot end inlet side of the waste heat boiler is connected with the first low-pressure compressor 4 on the hot end outlet side, and the other path of gas working medium is connected with the low-pressure steam turbine 7.
Of course, the present application is not limited to the above-described embodiments, and those skilled in the art can make various modifications to the above-described embodiments of the present application without departing from the scope of the present application under the teaching of the present application.
(i) It is to be understood that although the flow dividing device 15 for adjusting the flow dividing ratio is provided in the first embodiment, the flow dividing device is not limited to this, and may be simply provided as two independent flow paths leading from the waste heat boiler 3 without providing the flow dividing device 15, as long as the working medium is divided into two from the outlet side of the waste heat boiler 3. In addition, the flow rate of each flow path can be adjusted by a valve provided in the flow path.
(ii) It is to be understood that although the intermediate pressure steam turbine 13 for expanding the working medium flowing out from the high pressure steam turbine 12 by the residual pressure is provided in the above two embodiments, the present invention is not limited thereto, and the intermediate pressure steam turbine 13 may not be provided, and whether the intermediate pressure steam turbine 13 needs to be provided may be determined based on the calculation/measurement result of the pressure, the temperature, and the like of the working medium flowing out from the high pressure steam turbine 12 in the actual power generation.
(iii) It is to be understood that although the oxygen removal is performed by feeding the working gas having a relatively high temperature to the oxygen remover in the above two embodiments, the oxygen removal is not limited thereto, and may be performed by other means, such as chemical oxygen removal.
(iv) It will be appreciated that the split-flow recompression pure oxygen combustion cycle system of the embodiment shown in FIG. 1 can be used not only for hydrocarbon fuel but also for pure hydrogen fuel where the flow path to the carbon dioxide capture system 14 can be closed.
It will be appreciated that the split-flow recompression pure oxygen combustion cycle system, particularly the embodiment shown in FIG. 1, may also be applied in the case of mixed fuels.
Claims (6)
1. A split-flow recompression pure oxygen combustion circulation system is characterized in that the split-flow recompression pure oxygen combustion circulation system is a circulation power generation system taking pure oxygen as a combustion improver, a combustion chamber (1), a gas turbine (2), a waste heat boiler (3), a first low-pressure compressor (4), a first intercooler (5) and a first high-pressure compressor (6) are sequentially connected in series to form a flow path for working medium circulation, a low-pressure steam turbine (7), a condenser (8), a condensate water pump (9), a deaerator (10) and a water feed pump (11) are sequentially connected in series to form a flow path for gas-liquid separation,
the hot end outlet side of the waste heat boiler (3) is connected with the high-temperature inlet side of the low-pressure steam turbine (7) and the inlet side of the first low-pressure compressor (4) to enable the working medium flowing out of the hot end outlet side of the waste heat boiler (3) to be divided,
a liquid outlet side of the water feed pump (11) is connected with a cold end inlet side of the waste heat boiler (3), a high-pressure steam turbine (12) is arranged on a flow path between the cold end outlet side of the waste heat boiler (3) and an inlet side of the combustion chamber (1), a low-temperature outlet side of the high-pressure steam turbine (12) is respectively connected with a cold end inlet side of the first intercooler (5) and the gas turbine (2), a cold end outlet side of the first intercooler (5) is connected with an inlet side of the combustion chamber (1), a hot end inlet side is connected with an outlet side of the first low-pressure compressor (4), and a hot end outlet side is connected with an inlet side of the first high-pressure compressor (6),
the split-flow recompression pure oxygen combustion cycle system further comprises a carbon dioxide capture system (14), the carbon dioxide capture system (14) receiving gases from a gas outlet side of the condenser (8) and a gas outlet side of the oxygen scavenger (10) when the fuel supplied to the combustion chamber (1) is a hydrocarbon,
the carbon dioxide trapping system (14) comprises a second low-pressure compressor (141), an intermediate-pressure compressor (142), a second high-pressure compressor (143) and a second intercooler (144), wherein the inlet side of the second low-pressure compressor (141) is connected with the gas outlet side of the condenser (8), the outlet side of the second low-pressure compressor (141) is connected with the hot end inlet side of the second intercooler (144), the hot end outlet side of the second intercooler (144) is connected with the inlet side of the intermediate-pressure compressor (142), the outlet side of the intermediate-pressure compressor (142) is connected with the inlet side of the second high-pressure compressor (143), and the gas outlet side of the deaerator (10) is connected with the inlet side of the second high-pressure compressor (143).
2. A split-flow recompression pure oxygen combustion cycle system as claimed in claim 1, wherein a medium pressure steam turbine (13) is provided in the flow path between said high pressure steam turbine (12) and said gas turbine (2).
3. The split-flow recompression pure oxygen combustion cycle system as claimed in claim 1 or 2, further comprising a splitting device (15), wherein the splitting device (15) is disposed at a split point of the exhaust heat boiler (3) branching to the first low pressure compressor (4) and the low pressure steam turbine (7) for adjusting a ratio of the working medium flowing to the low pressure steam turbine (7) and the first low pressure compressor (4).
4. The split-flow recompression pure oxygen combustion cycle system as claimed in claim 1 or 2, wherein the low pressure steam turbine (7) discharges a portion of the working fluid to the deaerator (10) to heat the liquid working fluid in the deaerator (10) before expansion work is performed.
5. A split-flow recompression pure oxygen combustion cycle system as claimed in claim 1 or 2, wherein oxygen scavenger is added to the oxygen scavenger (10) for oxygen scavenging.
6. The split-flow recompression pure oxygen combustion cycle system as claimed in claim 1 or 2, wherein the working fluid flowing on the flow path from the condenser (8) to the waste heat boiler (3) is water, and the working fluid flowing on the flow paths other than the flow path from the condenser (8) to the waste heat boiler (3) is steam or a mixture of steam and carbon dioxide.
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| CN202210079459.XA CN114382562B (en) | 2022-01-24 | 2022-01-24 | Shunt recompression pure oxygen combustion circulation system |
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| CN114382562B (en) | 2022-11-08 |
| CN114382562A (en) | 2022-04-22 |
| CN115680809B (en) | 2024-06-25 |
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