阅读说明：本技术 一种利用液化天然气进行带碳捕集发电的集成系统 (Integrated system for carbon-carrying capture power generation by utilizing liquefied natural gas ) 是由 杨敬东 刘清友 杨晓明 汤晓勇 田静 陆永康 廖勇 赵石兵 顾爱英 王亮 周亚洲 于 2021-09-23 设计创作，主要内容包括：本发明公开了一种利用液化天然气进行带碳捕集发电的集成系统,包括LNG气化及冷能利用系统、空分制氧系统、富氧燃烧透平循环发电及尾气碳回收系统。与现有技术相比,本发明的积极效果是：本发明集LNG气化、冷能制氧、富氧发电与碳捕获于一体,优点是在LNG气化,制氧和碳捕获环节的能耗都能大大降低,LNG冷能利用率提高、发电效率提高、将捕集的二氧化碳注入地底咸水封存则可以实现零碳排放发电效果。本发明通过利用LNG冷能进行纯氧制取,纯氧与天然气参与富氧燃烧透平循环发电,发电尾气进行二氧化碳捕集,旨在降低LNG气化,制氧和碳捕获环节的能耗,打造零碳发电技术,符合未来碳中和的社会需求,应用前景广阔。(The invention discloses an integrated system for carrying out carbon capture power generation by utilizing liquefied natural gas, which comprises an LNG gasification and cold energy utilization system, an air separation oxygen generation system, an oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system. Compared with the prior art, the invention has the following positive effects: the invention integrates LNG gasification, cold energy oxygen generation, oxygen-enriched power generation and carbon capture, has the advantages that the energy consumption in the links of LNG gasification, oxygen generation and carbon capture can be greatly reduced, the utilization rate of LNG cold energy is improved, the power generation efficiency is improved, and the zero-carbon-emission power generation effect can be realized by injecting the captured carbon dioxide into the saline water at the bottom of the ground for storage. According to the invention, the LNG cold energy is utilized to prepare the pure oxygen, the pure oxygen and the natural gas participate in the oxygen-enriched combustion turbine cycle power generation, and the power generation tail gas is captured by the carbon dioxide, so that the energy consumption of the links of LNG gasification, oxygen production and carbon capture is reduced, a zero-carbon power generation technology is created, the social requirement of future carbon neutralization is met, and the application prospect is wide.)

1. An integrated system for carbon capture power generation by using liquefied natural gas is characterized in that: including LNG gasification and cold energy utilization system, empty system oxygen system, oxygen boosting combustion turbine circulation electricity generation and tail gas carbon recovery system that divides, wherein:

the LNG gasification and cold energy utilization system comprises an LNG storage tank, an LNG booster pump, a cold box and a heat exchanger which are connected in sequence; and a nitrogen circulation loop consisting of a nitrogen compressor, a first heat exchanger, a first cold box, a liquid nitrogen separator, a second cold box and the nitrogen compressor;

the air separation oxygen generation system comprises an air filtering device, an air compressor, a second heat exchanger, an air dehydration device, a third heat exchanger, a second cold box, an air expander and an air rectifying tower which are sequentially connected, wherein an outlet at the upper part of the air rectifying tower is sequentially connected with the second cold box and the third heat exchanger, the bottom of the air rectifying tower is respectively connected with an inlet of the second cold box and an inlet of the liquid oxygen booster pump, an outlet of the second cold box is connected with an inlet of the air rectifying tower, and an outlet of the liquid oxygen booster pump is connected with an inlet of the second heater;

the system comprises an LNG storage tank, a second LNG booster pump, a first heater, a mixed combustor, a turbine generator, a fourth heat exchanger, a first cooler, a carbon dioxide separator, a carbon dioxide compressor and a second cooler which are sequentially connected, wherein the outlet of the second cooler is divided into two paths, one path is connected to an external transportation and storage channel, and the other path is sequentially connected with the carbon dioxide booster pump, the fourth heat exchanger and the mixed combustor; the outlet of the second heater is connected with the inlet of the mixing burner.

2. The integrated system for carbon capture with lng power generation of claim 1, wherein: and a regulating valve is arranged between the first cold box of the nitrogen circulation loop and the liquid nitrogen separator.

3. The integrated system for carbon capture with lng power generation of claim 1, wherein: the liquid nitrogen separator of the nitrogen circulation loop is provided with two outlets, the two outlets are connected with different inlets of the second cold box, and the pipelines of the two outlets corresponding to the second cold box are connected to the nitrogen compressor after being combined.

4. The integrated system for carbon capture with lng power generation of claim 1, wherein: and a regulating valve is arranged between the outlet of the second cold box and the inlet of the air rectifying tower.

5. The integrated system for carbon capture with lng power generation of claim 1, wherein: the air separation oxygen generation system comprises an ethylene glycol circulation loop consisting of an ethylene glycol booster pump, a first cooling box, a second heat exchanger and an ethylene glycol booster pump.

6. The integrated system for carbon capture with lng power generation of claim 1, wherein: in the LNG gasification and cold energy utilization system, low-pressure LNG forms high-pressure LNG at 100MPa and-162 ℃ through an LNG booster pump and then is sent to a first cold box for cold energy recovery, the high-pressure LNG is discharged from the first cold box to form low-temperature high-pressure natural gas at 10MPa and 0 ℃, and the low-temperature high-pressure natural gas is subjected to cold energy recovery through a heat exchanger and then is exported as normal-temperature high-pressure natural gas.

7. The integrated system for carbon capture with lng power generation of claim 1, wherein: in the LNG gasification and cold energy utilization system, nitrogen gas at 0.5MPa and-40 ℃ is pressurized to 4.5MPa and 288 ℃ by a nitrogen compressor, enters a first heat exchanger for heat exchange and cooling to 4.5MPa and 30 ℃, enters a first cold box for heat exchange with LNG to form liquid nitrogen at 4.5MPa and-150 ℃, is depressurized and cooled to 0.5MPa and-179 ℃, is conveyed to a liquid nitrogen separator for gas-liquid separation, becomes low-temperature gas nitrogen and liquid nitrogen, is respectively conveyed to a second cold box for cold energy recovery, becomes nitrogen gas and normal-temperature gas nitrogen, and is conveyed to the nitrogen compressor to complete nitrogen recycling.

8. The integrated system for carbon capture with lng power generation of claim 1, wherein: in the air separation oxygen generation system, air is conveyed to an air compressor to be pressurized to 5MPa and 700 ℃ after being filtered by an air filtering device in sequence, then is conveyed to an air dehydration device to remove moisture after being subjected to heat exchange and cooled to minus 30 ℃ through a second heat exchanger and then is conveyed to a third heat exchanger to be subjected to heat exchange, the air becomes clean air and is conveyed to a second cold box to be subjected to heat exchange and cooled to minus 170 ℃ again, low-temperature air after heat exchange enters an air expansion machine to generate electricity, and low-pressure air discharged from the air expansion machine enters an air rectification tower to be rectified: air is separated into ascending-183 ℃ low-temperature nitrogen and liquid oxygen with the bottom of-183 ℃ in an air rectifying tower, wherein the low-temperature nitrogen is pumped out from the upper part and is conveyed to a second cold box, cold energy is recovered and is conveyed to a third heat exchanger to exchange heat with the air, and then the nitrogen is directly discharged as normal-temperature nitrogen; liquid oxygen is extracted from the bottom and then divided into two streams of liquid oxygen with the pressure of 0.1MPa, one stream of liquid oxygen enters a second cold box for cold energy recovery and then is conveyed back to an air rectifying tower under reduced pressure, the other stream of liquid oxygen is pressurized to 3MPa by a liquid oxygen booster pump to become high-pressure liquid oxygen, enters a second heater for heat exchange, and the high-pressure liquid oxygen is heated to become high-pressure oxygen and then is conveyed to a mixed combustor.

9. The integrated system for carbon capture with lng power generation of claim 1, wherein: in the air separation oxygen generation system, ethylene glycol with the normal temperature of 20 ℃ is pressurized to 1.6MPa by an ethylene glycol booster pump and then is sent to a first cooling box for heat exchange, and the ethylene glycol with the temperature reduced to-40 ℃ is sent to a second heat exchanger for heat exchange and then returns to the ethylene glycol booster pump to complete ethylene glycol circulation.

10. The integrated system for carbon capture with lng power generation of claim 1, wherein: in the oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system, the reaction pressure of a mixed combustor is 3MPa, LNG is pressurized to 3MPa by a second LNG booster pump and then is preheated by a first heater to generate high-pressure natural gas which is conveyed to the mixed combustor; the high-pressure oxygen after heat exchange by the second heater is sent to a mixed combustor to be mixed with CO₂The natural gas is conveyed to a turbine generator after mixed combustion and expansion, generates power through gas expansion and outputs current, then high-temperature tail gas is conveyed to a fourth heat exchanger for heat exchange, enters a first cooler for reusing waste heat to heat cold water after exiting the fourth heat exchanger, enters a carbon dioxide separator after exiting the first cooler for analyzing water and then enters a carbon dioxide compressor, and carbon dioxide is compressed and then conveyed to a second cooler for useAfter the hot water is preheated, one part of the hot water is used as supercritical carbon dioxide for external transportation and sealing, and the other part of the hot water is conveyed to a No. four heat exchanger through a carbon dioxide booster pump for heating again to become high-temperature high-pressure carbon dioxide and then conveyed to a mixed combustor.

Technical Field

The invention relates to an integrated system for carrying out carbon capture power generation by utilizing liquefied natural gas, in particular to a system for carrying out pure oxygen preparation by utilizing LNG cold energy, carrying out circular power generation by using pure oxygen, natural gas and carbon dioxide in an oxygen-enriched combustion turbine and carrying out carbon dioxide capture on power generation tail gas.

Background

In recent years, attention has been paid to the greenhouse effect, and studies have shown that atmospheric CO₂Is one of the most influential gases on the greenhouse effect. The heating effect produced by the temperature-increasing device is about 63 percent of the total heating effect. As a large carbon emission country, China faces a severe carbon emission reduction pressure.

Liquefied Natural Gas (LNG) is mainly composed of methane, and the atmospheric boiling point of methane is-161 ℃. The manufacturing process is that the natural gas produced by the gas field is purified (dehydrated, dealkylated and deacidified), then the methane is changed into liquid by adopting the processes of throttling, expansion and refrigeration of an external cold source, and the methane is required to be heated externally and gasified again when in use. The liquefied natural gas has the advantages of no impurities and pure components, and the amount of greenhouse gas released in the combustion process is far less than that of other fossil fuels, so that the liquefied natural gas is an ideal clean and efficient power generation fuel. LNG can release about 830kJ/kg of cold energy in the gasification process, and has great utilization value. However, in the global view, the utilization degree of LNG cold energy is only about 20%, the development and utilization rate of cold energy resources is low, and cold energy is usedThe waste is serious. Carbon Capture and Sequestration (CCS) technology is considered one of the major measures for carbon abatement in electric power, with oxycombustion technology being considered the most amenable to industrial, scale-up carbon capture. The main factor limiting the popularization of the oxygen-enriched combustion technology at present is that the energy consumption is large, and the main factors are mainly focused on air separation oxygen generation and CO generation₂And compressing the capturing link.

There are many kinds of oxygen-enriched combustion turbine cycles, taking the best-known Allam-Fetvedt cycle as an example, the Allam-Fetvedt cycle is a Brayton cycle technology, and the worldwide breakthrough technology was selected from Massachusetts science and technology review in 2018. The technology adopts oxygen-enriched combustion and converts supercritical CO₂As a working fluid, it is possible to recover waste heat and eliminate traditional pollutants and CO₂And (5) discharging. As a by-product, pipeline CO will be produced which can be used for sequestration₂. According to the measurement and calculation of a foreign well-known mechanism, the power supply efficiency of the Allam-Fetvedt cycle at the working pressure of 30MPa and the turbine inlet temperature of 1100 ℃ is 2.3 percent higher than that of the natural gas combined cycle of the existing F-grade gas turbine, natural gas or coal can be combusted to prepare synthetic gas, complete carbon capture is realized, and NO pollutants such as NOx are discharged.

The LNG gasification, cold energy oxygen generation, oxygen-enriched power generation, carbon capture and other technologies are combined in the cross-field mode, and the LNG gasification, oxygen generation and carbon capture links have the advantages that the energy consumption can be greatly reduced, the LNG cold energy utilization rate is improved, the power generation efficiency is improved, and the zero-carbon-emission power generation effect can be realized by injecting the captured carbon dioxide into the underground saline water for sealing; meanwhile, the system adopts a multistage heat exchange thought, on one hand, the heat exchange temperature difference is reduced, and the heat exchanger is improvedEfficiency, on the other hand, reduces the compression power consumption of the compressor. Compared with the traditional gas power plant technology, the invention can realize zero-carbon-emission power generation, has high efficiency, cleanness, environmental protection, safety, reliability and good economic benefit, and can be conveniently transferred to other areas for continuous service when the demand changes.

Disclosure of Invention

In order to develop a technology for reducing the decarbonization cost of liquefied natural gas power generation, the invention provides an integrated system for generating power by capturing carbon by utilizing liquefied natural gas, pure oxygen is prepared by utilizing LNG cold energy, the pure oxygen and the natural gas participate in oxygen-enriched combustion turbine cycle power generation, and the power generation tail gas is captured by carbon dioxide.

The technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides an utilize liquefied natural gas to carry out integrated system who takes carbon entrapment electricity generation, includes that LNG gasification and cold energy utilize system, empty system oxygen system, oxygen boosting combustion turbine cycle electricity generation and tail gas carbon recovery system that divides, wherein:

the LNG gasification and cold energy utilization system comprises an LNG storage tank, an LNG booster pump, a cold box and a heat exchanger which are connected in sequence; and a nitrogen circulation loop consisting of a nitrogen compressor, a first heat exchanger, a first cold box, a liquid nitrogen separator, a second cold box and the nitrogen compressor;

the air separation oxygen generation system comprises an air filtering device, an air compressor, a second heat exchanger, an air dehydration device, a third heat exchanger, a second cold box, an air expander and an air rectifying tower which are sequentially connected, wherein an outlet at the upper part of the air rectifying tower is sequentially connected with the second cold box and the third heat exchanger, the bottom of the air rectifying tower is respectively connected with an inlet of the second cold box and an inlet of the liquid oxygen booster pump, an outlet of the second cold box is connected with an inlet of the air rectifying tower, and an outlet of the liquid oxygen booster pump is connected with an inlet of the second heater;

the system comprises an LNG storage tank, a second LNG booster pump, a first heater, a mixed combustor, a turbine generator, a fourth heat exchanger, a first cooler, a carbon dioxide separator, a carbon dioxide compressor and a second cooler which are sequentially connected, wherein the outlet of the second cooler is divided into two paths, one path is connected to an external transportation and storage channel, and the other path is sequentially connected with the carbon dioxide booster pump, the fourth heat exchanger and the mixed combustor; the outlet of the second heater is connected with the inlet of the mixing burner.

Compared with the prior art, the invention has the following positive effects:

the invention integrates LNG gasification, cold energy oxygen generation, oxygen-enriched power generation and carbon capture, has the advantages that the energy consumption in the links of LNG gasification, oxygen generation and carbon capture can be greatly reduced, the utilization rate of LNG cold energy is improved, the power generation efficiency is improved, and the captured carbon dioxide is injected into the saline water at the bottom of the ground for sealing and storageThe zero carbon emission power generation effect can be achieved. The LNG gasification considers the utilization of cold energy, two-stage cooling is adopted, the temperature of oxygen is reduced by reducing the temperature of ethylene glycol, and the explosion danger caused by the direct contact of the oxygen and the LNG is avoided. The invention also considers the pressure bearing capacity of the pressure vessel, and utilizes a plurality of compression devices to adjust the inlet pressure, thereby avoiding the operation of the device in high load and high pressure dangerous states. Meanwhile, the system adopts a multistage heat exchange thought, on one hand, the heat exchange temperature difference is reduced, and the heat exchanger is improvedEfficiency, on the other hand, reduces the compression power consumption of the compressor. The invention also considers methane in supercritical CO₂Laminar flame propagation velocity ratio in atmosphere at subcritical CO₂100 times higher in/air mixture and no rich fuel extinction limit exists; supercritical CO of methane₂The direct combustion temperature rise in the atmosphere has good combustion heat exchange efficiency, and supports the following turbine power generation to obtain excellent power generation efficiency; natural gas in supercritical CO₂The tail gas is combusted in a pure oxygen mixture, so that the tail gas has no NOx emission problem; the inlet and outlet of the turbine are in supercritical and subcritical states respectively, the output power of the turbine is high, the turbine is favorable for removing moisture in combustion tail gas through a cooler and a separator, in order to keep the total flow of the circulating working medium unchanged, the increment of carbon dioxide generated by combustion is continuously discharged out of the system and is captured, and the carbon capture of 100% power generation tail gas can be realized.

Drawings

The invention will now be described, by way of example, with reference to the accompanying drawings, in which:

FIG. 1 is a schematic diagram of an integrated system for carbon capture power generation using liquefied natural gas;

the reference numbers in the figures include: LNG storage tank 1, LNG booster pump 2, cold box 3, heat exchanger 4, nitrogen compressor 5, air filtration unit 6, air compressor 7, heat exchanger 8, air dehydration device 9, heat exchanger 10, cold box 11, air expander 12, air rectifying tower 13, first governing valve 14, second governing valve 15, liquid nitrogen separator 16, liquid oxygen booster pump 17, ethylene glycol booster pump 18, LNG booster pump 19, heater 20, heater 21, mixed combustor 22, turbo generator 23, heat exchanger 24, cooler 25, carbon dioxide separator 26, carbon dioxide compressor 27, cooler 28, carbon dioxide booster pump 29.

Detailed Description

As shown in fig. 1, an integrated system for power generation with carbon capture by using liquefied natural gas includes an LNG gasification and cold energy utilization system, an air separation oxygen generation system, an oxygen-enriched combustion turbine cycle power generation and a tail gas carbon recovery system; wherein:

LNG gasification and cold energy utilization system

The LNG gasification and cold energy utilization system comprises an LNG storage tank 1, a first LNG booster pump 2, a first cold box 3, a first heat exchanger 4, a nitrogen compressor 5, a second regulating valve 15 and a liquid nitrogen separator 16;

the connection mode of equipment in the LNG gasification and cold energy utilization system is as follows: an LNG storage tank 1 is arranged at the inlet of the first LNG booster pump 2, and then the first LNG booster pump is sequentially connected with a first cold box 3 and a first heat exchanger 4; the outlet of the nitrogen compressor 5 is connected with the heat exchanger 4, then connected with the first cold box 3, the outlet of the first cold box 3 is connected with the second regulating valve 15, then connected with the liquid nitrogen separator 16, the liquid nitrogen separator is provided with two outlets, the two outlets are connected with different inlets of the second cold box 11, and the pipelines of the two outlets corresponding to the second cold box 11 are combined and then connected to the nitrogen compressor 5 to form a closed loop.

In the LNG gasification and cold energy utilization system:

the low-pressure LNG with the pressure of 0.4-1.0 MPa is formed into 100MPa from an LNG storage tank 1 through a pipeline by a first LNG booster pump 2, the high-pressure LNG with the temperature of-162 ℃ is sent to a first cold box 3 for cold energy recovery, the high-pressure LNG is discharged from the first cold box 3 to form low-temperature high-pressure natural gas with the pressure of 10MPa and the temperature of 0 ℃, and the low-temperature high-pressure natural gas is subjected to secondary cold energy recovery through heat exchange with nitrogen by a first heat exchanger 4 to become normal-temperature high-pressure natural gas for external transportation;

0.5MPa and-40 ℃ nitrogen is pressurized to 4.5MPa through a nitrogen compressor 5, the pressure is 4.5MPa after the nitrogen enters a first heat exchanger 4 at 288 ℃ and is subjected to first heat exchange with low-temperature high-pressure natural gas, the pressure is 4.5MPa after the nitrogen enters a first cold box 3 at 30 ℃ and is subjected to heat exchange with LNG to form 4.5MPa, the pressure of 150 ℃ liquid nitrogen is reduced through a second regulating valve 15, the pressure and the temperature are reduced to 0.5MPa, the nitrogen and the liquid nitrogen are conveyed to a liquid nitrogen separator 16 at 179 ℃ and are separated into low-temperature gas nitrogen and liquid nitrogen, the low-temperature gas nitrogen and the liquid nitrogen are respectively conveyed to a second cold box 11 for cold energy recovery, the low-temperature gas nitrogen and the liquid nitrogen become nitrogen and normal-temperature gas nitrogen respectively and are conveyed to the nitrogen compressor 5 to complete nitrogen recycling.

Two, air separation oxygen production system

The air separation oxygen generation system comprises a second cooling box 11, an air filtering device 6, an air compressor 7, a second heat exchanger 8, a third heat exchanger 10, an air dehydration device 9, an air expander 12, an air rectifying tower 13, a liquid oxygen booster pump 17, a first regulating valve 14 and an ethylene glycol booster pump 18;

the equipment connection mode in the air separation oxygen generation system is as follows: an inlet of the ethylene glycol booster pump 18 is connected with the second heat exchanger 8, an inlet of the second heat exchanger 8 is connected with the first cold box outlet 3, and an inlet of the first cold box 3 is connected with an outlet of the ethylene glycol pump 18 to form a closed loop; an outlet of the air filtering device 6 is connected with an inlet of an air compressor 7, an outlet of the air compressor 7 is connected with an outlet of a second heat exchanger 8, the second heat exchanger 8 is connected with an inlet of an air dehydrating device 9, an outlet of the air dehydrating device 9 is connected with an inlet of a second cold box 11 after being connected with a third heat exchanger 10, an outlet of the second cold box 11 is connected with an inlet of an air expander 12, an outlet of the air expander 12 is connected with an air rectifying tower 13, an upper outlet of the air rectifying tower 13 is connected with an inlet of the second cold box 11, an outlet of the second cold box 11 is connected with a third heat exchanger 10, the bottom of the air rectifying tower 13 is respectively connected with an inlet of the second cold box 11 and a liquid oxygen booster pump 17, an outlet of the second cold box 11 is connected with a first regulating valve 14 and then connected with the rectifying tower 13, and an outlet of the liquid oxygen booster pump 17 is connected with a second heater 21.

In an air separation oxygen generation system:

the ethylene glycol with the normal temperature of 20 ℃ is pressurized to 1.6MPa by the ethylene glycol booster pump 18 and then is sent to the first cooling box 3 to exchange heat, the temperature of the ethylene glycol after exchange is minus 40 ℃, the ethylene glycol with the reduced temperature is sent to the second heat exchanger 8 to exchange heat with air and then returns to the ethylene glycol booster pump 18 to complete ethylene glycol circulation; air is sequentially filtered by an air filtering device 6 to remove impurities, then conveyed to an air compressor 7 to be pressurized to 5MPa, the temperature is 700 ℃, then is subjected to heat exchange with ethylene glycol through a second heat exchanger 8 to be cooled to-30 ℃, then is conveyed to an air dehydrating device 9 to remove moisture, is conveyed to a third heat exchanger 10 to be subjected to heat exchange with low-temperature nitrogen, is conveyed to a second cold box 11 to be subjected to heat exchange again to reduce the temperature to-170 ℃, the low-temperature air after heat exchange enters an air expander 12 to generate electricity, the electricity is output, and the low-pressure air (liquid air) output from the air expander 12 enters an air rectifying tower 13 to be rectified;

the air is separated into ascending-183 ℃ low-temperature nitrogen and-183 ℃ liquid oxygen at the bottom in the air rectifying tower 13; low-temperature nitrogen is pumped out from the upper part and conveyed to a second cold box 11, cold energy is recovered and conveyed to a third heat exchanger 10 to be directly discharged as normal-temperature nitrogen after being subjected to heat exchange with air, liquid oxygen is pumped out from the bottom and then divided into two strands of liquid oxygen with the pressure of 0.1MPa, one strand of liquid oxygen enters the second cold box 11 to be subjected to cold energy recovery and then is conveyed back to an air rectifying tower 13 after being subjected to pressure reduction through a first regulating valve 14, the other strand of liquid oxygen is pressurized to 3MPa through a liquid oxygen booster pump 17 to become high-pressure liquid oxygen, and then the high-pressure liquid oxygen enters a second heater 21 to be subjected to heat exchange with hot water, the hot water is cooled to form cold water after heat exchange and then is discharged, and the high-pressure liquid oxygen is heated to become high-pressure oxygen and then is conveyed to a mixed combustor 22.

Third, oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system

Oxygen boosting combustion turbine cycle power generation and tail gas carbon recovery system includes: a second LNG booster pump 19, a first heater 20, a second heater 21, a mixed combustor 22, a turbine generator 23, a carbon dioxide compressor 27, a carbon dioxide separator 26, a first cooler 25, a fourth heat exchanger 24, a carbon dioxide booster pump 29 and a second cooler 28;

the connection mode of the oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system is as follows: an inlet of a second LNG booster pump 19 is connected with the LNG storage tank 1, an outlet of the second LNG booster pump 19 is connected with a first heater 20, the first heater 20 is connected with a mixing combustor 22, an outlet of the mixing combustor 22 is connected with a turbine generator 23, an outlet of the turbine generator 23 is connected with a fourth heat exchanger 24, the fourth heat exchanger 24 is connected with an inlet of a first cooler 25, an outlet of the first cooler 25 is connected with a carbon dioxide separator 26, an outlet of the carbon dioxide separator 26 is connected with a carbon dioxide compressor 27, the carbon dioxide compressor 27 is connected with an inlet of a second cooler 28, an outlet of the second cooler 28 is connected with a carbon dioxide booster pump 29 or an external device, and an outlet of the carbon dioxide booster pump 29 is connected with the fourth heat exchanger 24 and then connected with the mixing combustor 22 to form a closed loop; the outlet of the second heater 21 is connected with the inlet of the mixing burner 22.

In the oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system:

the reaction pressure of the hybrid combustor 22 was 3 MPa. LNG is output from an LNG storage tank 1, is pressurized to 3MPa by a second LNG booster pump 19, is preheated by a first heater 20 to generate high-pressure natural gas, and is conveyed to a mixed combustor 22; the high-pressure oxygen after heat exchange by the second heater 21 is sent to a mixed burner 22 and CO₂Mixing natural gas according to a proportion, wherein carbon dioxide accounts for 94%, natural gas accounts for 1.25%, oxygen accounts for 4.75%, and when reaction occurs, the components can form dynamic change due to the reaction process; the high-temperature tail gas enters a first cooler 25 after exiting the fourth heat exchanger 24 to be heated by waste heat again, enters a carbon dioxide separator 26 after exiting the first cooler 25 to be analyzed and then enters a carbon dioxide compressor 27, the carbon dioxide is compressed and then is conveyed to a second cooler 28 to be preheated by hot water to be supercritical carbon dioxide, one part of the high-temperature and high-pressure carbon dioxide is conveyed to the fourth heat exchanger 24 through a carbon dioxide booster pump 29 to be heated again to be high-temperature and high-pressure carbon dioxide and then is conveyed to a mixed combustor 22, and the other part of the supercritical carbon dioxide is output and sealed.