CN215724557U - Air separation energy storage coupling oxygen-enriched combustion system - Google Patents

Air separation energy storage coupling oxygen-enriched combustion system Download PDF

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CN215724557U
CN215724557U CN202121927621.6U CN202121927621U CN215724557U CN 215724557 U CN215724557 U CN 215724557U CN 202121927621 U CN202121927621 U CN 202121927621U CN 215724557 U CN215724557 U CN 215724557U
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air
outlet
communicated
liquid
inlet
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陈晓乐
檀经考
周屈兰
李娜
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Xian Jiaotong University
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Xian Jiaotong University
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
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    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • 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
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Abstract

The utility model discloses an air separation energy storage coupling oxygen-enriched combustion system, which consists of a compression system, a heat storage subsystem, a packed bed type cold accumulator, an air liquefaction subsystem, an air separation subsystem, an expansion power generation system and a power plant boiler, and can convert valley residual electric energy, help a thermal power generating unit to participate in deep peak shaving and ensure long-time stable operation of the thermal power generating unit; the system operation method comprises the following steps: the air is pressurized and heated in the compression system, and enters the packed bed type regenerator for further cooling after being cooled by a stage-end heat exchanger of the heat storage subsystem; after the high-pressure low-temperature air is expanded by a cryogenic expander, partial high-pressure low-temperature air is liquefied, and liquid air is stored in a liquid-air storage tank through a gas-liquid separator; when air separation and expansion power generation are carried out, liquid air respectively enters an air molecular system after being shunted, and air separation is carried out, so that oxygen-enriched air is generated and is supplied to a boiler for quick combustion; and the other part of liquid air is pressurized by the liquid pump and then enters an expansion power generation system for expansion power generation, and electric energy is output outwards.

Description

Air separation energy storage coupling oxygen-enriched combustion system
Technical Field
The utility model relates to the technical field of liquefied air energy storage, air separation and power plant peak regulation, in particular to a system for generating oxygen-enriched combustion by coupling the liquefied air energy storage and the air separation.
Background
With the increasingly prominent problems of energy sources and environment, the research and application of the energy storage technology are paid great attention, and the large-scale application of the energy storage technology will bring about great revolution to the production and utilization of the energy sources. The liquefied air energy storage technology takes air as a carrier with energy input and output flowing in two directions, and redundant electric energy can be stored in low-temperature liquid air and released when the air is required to be used.
Meanwhile, with the inclination of energy policies in China and the unstable new energy electric quantity grid connection, a large number of thermal power generating units participate in the deep peak shaving of the power grid. Along with participating in deep peak shaving, the thermal power generating unit deviates from the design value for a long time and operates, so that the safety and the economy of the unit are reduced, and the problems of unstable boiler low-load combustion and hydrodynamic circulation safety, full-load investment of a denitration device, low-load cooling of a steam turbine, flexibility of a control system during long-term low load and quick variable load, the problem of equipment operation period and service life attenuation, thermal-electric decoupling of a heat supply unit and the like exist to different degrees.
Disclosure of Invention
In order to solve the problem of performance reduction of the thermal power generating unit participating in deep peak shaving, the utility model provides a system for coupling liquefied air energy storage, air separation and oxygen-enriched combustion, the system utilizes valley surplus electric quantity as system energy input, a part of electric energy drives a compression system to compress and pressurize air, high-pressure air is liquefied and stored in a low-temperature-resistant liquid-air storage tank after deep cooling and expansion work, and enters an expansion machine for work and power generation after being pressurized and reheated by a liquid pump; the other part of electric energy drives an air separation system, liquefied air is separated into oxygen enrichment and nitrogen with higher purity in a rectifying tower, and the generated oxygen enrichment is introduced into a boiler for combustion, so that the boiler can quickly climb peaks. Therefore, the utility model aims to store the valley excess electric quantity, ensure the long-time stable operation of the thermal power generating unit, effectively reduce the reduction of the economic performance and the safety performance of the unit and improve the energy utilization rate.
In order to achieve the purpose, the technical scheme of the utility model is as follows:
an air separation energy storage coupling oxygen-enriched combustion system comprises a compression system 1, a stage end cooler 2, a heat storage tank 3, a packed bed type cold storage device 4, a cryogenic expander 5, a gas-liquid separator 6, a liquid-air storage tank 7, a flow divider 8, a liquid pump 9, a reheater 10, an expansion power generation system 11, a hydraulic machine 12, a rectifying tower 13, a throttle valve 14 and a power plant boiler 15;
a final stage outlet of the compression system 1 is communicated with a hot end inlet of a final stage cooler 2, a hot end outlet of the final stage cooler 2 is communicated with a hot end inlet of a packed bed type cold accumulator 4, a hot end outlet of the packed bed type cold accumulator 4 is communicated with an inlet of a cryogenic expander 5, an outlet of the cryogenic expander 5 is communicated with an inlet of a gas-liquid separator 6, a liquid phase outlet of the gas-liquid separator 6 is communicated with an inlet of a liquid-air storage tank 7, an outlet of the liquid-air storage tank 7 is communicated with an inlet of a flow divider 8, a first outlet of the flow divider 8 is communicated with an inlet of a liquid pump 9, an outlet of the liquid pump 9 is communicated with a first cold end inlet of the packed bed type cold accumulator 4, a first cold end outlet of the packed bed type cold accumulator 4 is communicated with a cold end inlet of a reheater 10, a cold end outlet of the reheater 10 is communicated with a primary expander of an expansion power generation system 11, and a final stage expander of the expansion power generation system 11 is communicated with the atmosphere; an outlet of an interstage cooler of a multi-stage compressor of the compression system 1 is communicated with an inlet of a heat storage tank 3, and an outlet of the heat storage tank 3 is communicated with an interstage inlet of a multi-stage expander of the expansion power generation system 11; the outlet of the cold end of the stage end cooler 2 is communicated with the inlet of the heat storage tank 3, and the outlet of the heat storage tank 3 is communicated with the inlet of the hot end of the reheater 10; a gas-phase outlet of the gas-liquid separator 6 is communicated with a second cold end inlet of the packed bed type regenerator 4, and a second cold end outlet of the packed bed type regenerator 4 is communicated with a primary compressor inlet of the compression system 1; a second outlet of the separator 8 is communicated with an inlet of a hydraulic machine 12, an outlet of the hydraulic machine 12 is communicated with a lower tower inlet of a rectifying tower 13, a lower tower outlet of the rectifying tower 13 is communicated with an inlet of a throttle valve 14, an outlet of the throttle valve 14 is communicated with an upper tower inlet of the rectifying tower 13, and an upper tower outlet of the rectifying tower 13 is communicated with an inlet of a power plant boiler 15;
the interstage heat exchange in the compression system 1, the end-stage cooler 2, the heat storage tank 3, the reheater 10 and the interstage reheater in the expansion power generation system 11 form a heat storage subsystem; the cryogenic expansion machine 5, the gas-liquid separator 6, the liquid-air storage tank 7, the flow divider 8 and the liquid pump 9 form a liquefied air subsystem; the hydraulic press 12, the rectifying tower 13 and the throttle valve 14 form an air separation subsystem.
The system couples liquid air energy storage, air separation and oxygen-enriched combustion, the liquid air energy storage and the air separation share one set of air liquefaction system which consists of a cryogenic expansion machine (5), a gas-liquid separator (6), a liquid-air storage tank (7), a flow divider (8) and a liquid pump (9), air is liquefied and then stored in the liquid-air storage tank (7), and the liquid air is respectively sent to an expansion power generation system (11) for expansion power generation and a rectifying tower (13) for air separation through the flow divider (8); the oxygen-enriched air separated from the rectifying tower 13 is sent to a power plant boiler 15 to complete oxygen-enriched combustion.
The compression system 1 consists of 2-4 stages of compressors, an interstage heat exchanger is arranged between each stage of compressor, and compression is carried out by adopting a constant pressure ratio, so that the structure is simple, and the pressure ratio is high; the outlet air of each stage of compressor of the compression system 1 exchanges heat with the heat storage medium in the interstage heat exchanger, the heat storage medium before exchanging heat is in a normal temperature and normal pressure state, and the high-temperature heat storage medium after exchanging heat is sent to the heat storage tank 3 for storage;
the packed bed type cold accumulator 4 takes spherical particle stones as packing materials, and the outside adopts a vacuum packing heat preservation mode; when the packed bed type cold accumulator 4 is in a working state of storing cold energy, liquid air conveyed by a liquid pump 9 is arranged at an inlet of a first cold end, gaseous low-temperature air conveyed by a gas-liquid separator 6 is arranged at an inlet of a second cold end, and the low-temperature air exchanges heat with a packing material and is vaporized in the packed bed type cold accumulator 4; when the packed bed type cold accumulator 4 is in a working state of releasing cold energy, high-temperature air from the end-stage cooler 2 is arranged at the inlet of the hot end, and the temperature of the high-temperature air is reduced after the high-temperature air exchanges heat with a packing material in the packed bed type cold accumulator 4;
the expansion power generation system 11 consists of 3-4 stages of expansion machines, each expansion machine is coaxially connected with a power generator, and an interstage reheater is arranged between each stage of expansion machine and expansion is carried out by adopting an isobaric ratio; the inlet air of the interstage expander of the expansion power generation system 11 exchanges heat with the high-temperature heat storage medium sent by the heat storage tank 3 in the interstage reheater, and enters the expander to do expansion work after the temperature of the air is increased;
the power plant boiler 15, when the power plant needs promote load fast, with the leading-in combustion chamber to power plant boiler 15 of the oxygen-enriched air that divides the generation, promote the combustion rate of boiler, reach the purpose that promotes load fast.
The stage end cooler 2 exchanges heat with high-temperature air at the outlet of the final stage of the compression system 1 by using a heat storage medium, the temperature of the air is reduced, the heat storage medium is heated to be in a high-temperature state, and the heat storage medium is sent to the heat storage tank 3 from the outlet of the cold end of the stage end cooler 2 for storage;
the heat storage tank 3 is used for storing heat storage media for heat exchange and receiving the heat storage media from the interstage heat exchanger and the end-stage cooler 2 of the compression system 1; then the low-temperature air is sent to an interstage heat exchanger of an expansion power generation system 11 and a reheater 10 through an outlet to heat the low-temperature air;
the reheater 10 is used for heating low-temperature air entering the expansion power generation system 11, and the temperature of the heat storage medium is reduced and the temperature of the air is increased through the heat exchange between the air and the surface of the heat storage medium;
the heat storage medium in the heat storage subsystem is liquid heat conduction oil, the liquid heat conduction oil is in a closed loop state in the heat storage subsystem, and the liquid heat conduction oil is pushed by a circulating pump to work in each heat exchanger; the specific amount of heat transfer oil and the flow rate between the individual heat exchangers need to be determined according to the capacity of the system.
The cryogenic expander 5 is used for expanding high-pressure cryogenic air, the pressure and the temperature of the expanded air are reduced, part of the air is liquefied in the cryogenic expander 5, and the outlet of the cryogenic expander 5 is air mixed with gas and liquid;
the gas-liquid separator 6 is used for separating gas-liquid two-phase mixed air obtained by expansion of the cryogenic expander 5, the gas-liquid two-phase mixed air in the gas-liquid separator 6 is divided into a gas phase and a liquid phase, the liquid phase air is sent to the liquid air storage tank 7 from the liquid phase outlet of the gas-liquid separator 6 for storage, and the gas phase air is sent to the packed bed type cold accumulator 4 from the gas phase outlet of the gas-liquid separator 6 for releasing cold energy;
the liquid-air storage tank 7 is used for storing air generated by liquefaction, is made of low-temperature-resistant materials, adopts a double-layer fixed vacuum powder heat preservation mode outside, and controls the liquid-air gasification rate in the storage tank within 0.3%;
the flow divider 8 is used for regulating and controlling the amount of liquefied air input into the expansion power generation system 11 and the air molecule system;
the cryogenic liquid pump 9 is used for increasing the air pressure entering the expansion power generation system 11.
The hydraulic machine 12 is used for increasing the pressure of liquid air entering the rectifying tower 13;
the rectifying tower 13 is used for separating air and consists of a tower kettle, a tower plate, a cylinder shell and a condensation evaporator, liquid air enters the rectifying tower 13 from the tower kettle, part of the liquid air is vaporized and ascended to perform heat-mass exchange with reflux liquid, the rest of the liquid air is mixed with the refluxed oxygen-enriched liquid air, enters the evaporation side of the condensation evaporator after throttling through a throttling valve 14, the nitrogen on the condensation side is cooled, and the nitrogen is evaporated to be oxygen-enriched air and is led out; after the liquid nitrogen is cooled into a liquid state, one part of the liquid nitrogen is taken as a product and led out from the lower part of a top cover of the condensation evaporator, and the other part of the liquid nitrogen is taken as a reflux liquid to carry out heat-mass exchange with rising gas;
the throttle valve 14 is used for reducing the temperature of the oxygen-enriched liquid air and improving the cooling energy of the oxygen-enriched liquid air.
The purified air is compressed in a compressor of the compression system 1 and exchanges heat in an interstage heat exchanger, and the air is high-temperature and high-pressure air at the outlet of a final stage compressor of the compression system 1; the compressed high-temperature and high-pressure air enters the final stage cooler 2 to exchange heat with the heat storage medium for cooling, and the high-pressure air is changed into normal-temperature air after heat exchange; the heat-exchanged high-temperature heat storage medium enters a heat storage tank 3 for storage;
the cooled high-pressure gas enters a packed bed type cold accumulator 4 to absorb cold energy, and the temperature is reduced to a deep cooling state; the high-pressure low-temperature air enters a cryogenic expansion machine 5 to be expanded and liquefied, the pressure is reduced to normal pressure, the temperature is further reduced to be close to the air liquefaction temperature, partial air is liquefied, and the outlet of the cryogenic expansion machine 5 is gas-liquid two-phase mixed air; gas-liquid two-phase mixed air enters a gas-liquid separator 6 to carry out two-phase separation, gas-phase air is led back to a packed bed type cold accumulator 4 from a gas-phase outlet of the separator 6 to release cold energy, then the gas-phase air returns to a compression system 1 to be recompressed, and liquid-phase air is led to a liquid-air storage tank 7 from a liquid-phase outlet of the separator 6 to be stored;
when liquid air is needed for air separation and energy release, the liquid air is introduced to a flow divider 8 from a liquid air storage tank 7, the flow divider 8 divides the liquid air into two flows, one flow enters a hydraulic machine 12, and the liquid air is pressurized and then sent to a rectifying tower 13; liquid air is separated in the rectifying tower 13, a nitrogen product can be led out under the top cover of a condensation evaporator of the rectifying tower, and an oxygen-enriched air product is led out on the evaporation side; oxygen-enriched air separated out by the rectifying tower 13 is sent into a power plant boiler 15 for oxygen-enriched combustion, so that the combustion efficiency is improved;
the other liquid air which is branched from the flow divider 8 enters a liquid pump 9 to be pressurized; high-pressure liquid air from the liquid pump 9 enters the packed bed type cold accumulator 4 to release cold energy, and the temperature is raised to the normal temperature state and is vaporized into gaseous air; the air from the outlet of the second cold end of the packed bed type regenerator 4 enters a reheater 10 to exchange heat with the high-temperature heat storage medium sent by the heat storage tank 3, and the temperature is further increased to a high-temperature state; the heated high-pressure gas enters an expansion power generation system 11 to do work, and a coaxial generator is pushed to rotate to generate power; the air exchanges heat with the high-temperature heat storage medium sent from the heat storage tank 3 at the interstage reheater of each stage to heat, then enters the next stage of expander to do work through high-temperature gas, and after expansion of the multistage expander, the air pressure at the outlet of the final stage of expander can be consumed up and recovered to the normal pressure state.
The compression system 1, the expansion power generation system 11 and the rectifying tower 13 can be operated simultaneously or independently. The air separation and the liquid air energy storage are coupled by controlling the flow of liquid air conveyed outwards by the liquid air storage tank 7 and the flow dividing rate of the flow divider 8; the coupling of air separation and oxygen-enriched combustion can be achieved by adjusting the amount of oxygen-enriched air generated by the rectifying tower 13 entering the power plant boiler 15 for oxygen-enriched combustion.
Compared with the prior art, the utility model has the following advantages:
(1) the system utilizes the liquefied air generated by the energy storage of the liquefied air into the air separation system, thereby not only achieving the purpose of generating rich oxygen by energy storage and air separation, but also saving the investment and energy consumption in the aspects of compression, liquefaction and the like in the air molecular system.
(2) The system disclosed by the utility model can achieve the purposes of storing off-peak electric energy of a power grid and ensuring stable operation of a thermal power unit of a power plant, and can also utilize oxygen-enriched combustion to quickly promote the load of the thermal power unit and expand to apply work in an energy release stage to generate grid-connected power, so that the thermal power unit is further promoted to participate in deep peak regulation.
(3) The heat storage subsystem in the system can recover compression heat, and the packed bed type cold accumulator can recover cold energy of liquid air, so that the utilization efficiency of energy can be effectively improved.
(4) Adopt liquid air energy storage mode, can greatly reduce the volume of air storage tank, can drop storage pressure to the ordinary pressure simultaneously, require very big reduction to the storage tank material.
(5) The air molecular system produces low temperature nitrogen gas, which can be used to utilize its cold energy or further liquefied for sale as a product.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Detailed Description
Referring to fig. 1, an air separation energy storage coupled oxygen-enriched combustion system according to an embodiment of the present invention includes a compression system 1, a stage end cooler 2, a heat storage tank 3, a packed bed type cold storage 4, a cryogenic expander 5, a gas-liquid separator 6, a liquid-air storage tank 7, a flow divider 8, a liquid pump 9, a reheater 10, an expansion power generation system 11, a hydraulic machine 12, a rectifying tower 13, a throttle valve 14, and a power plant boiler 15;
a final stage outlet of the compression system 1 is communicated with a hot end inlet of a final stage cooler 2, a hot end outlet of the final stage cooler 2 is communicated with a hot end inlet of a packed bed type cold accumulator 4, a hot end outlet of the packed bed type cold accumulator 4 is communicated with an inlet of a cryogenic expander 5, an outlet of the cryogenic expander 5 is communicated with an inlet of a gas-liquid separator 6, a liquid phase outlet of the gas-liquid separator 6 is communicated with an inlet of a liquid-air storage tank 7, an outlet of the liquid-air storage tank 7 is communicated with an inlet of a flow divider 8, a first outlet of the flow divider 8 is communicated with an inlet of a liquid pump 9, an outlet of the liquid pump 9 is communicated with a first cold end inlet of the packed bed type cold accumulator 4, a first cold end outlet of the packed bed type cold accumulator 4 is communicated with a cold end inlet of a reheater 10, a cold end outlet of the reheater 10 is communicated with a primary expander of an expansion power generation system 11, and a final stage expander of the expansion power generation system 11 is communicated with the atmosphere; an outlet of an interstage cooler of a multi-stage compressor of the compression system 1 is communicated with an inlet of a heat storage tank 3, and an outlet of the heat storage tank 3 is communicated with an interstage inlet of a multi-stage expander of the expansion power generation system 11; the outlet of the cold end of the stage end cooler 2 is communicated with the inlet of the heat storage tank 3, and the outlet of the heat storage tank 3 is communicated with the inlet of the hot end of the reheater 10; a gas-phase outlet of the gas-liquid separator 6 is communicated with a second cold end inlet of the packed bed type regenerator 4, and a second cold end outlet of the packed bed type regenerator 4 is communicated with a primary compressor inlet of the compression system 1; the second outlet of the separator 8 is communicated with the inlet of a hydraulic machine 12, the outlet of the hydraulic machine 12 is communicated with the lower tower inlet of a rectifying tower 13, the lower tower outlet of the rectifying tower 13 is communicated with the inlet of a throttle valve 14, the outlet of the throttle valve 14 is communicated with the upper tower inlet of the rectifying tower 13, and the upper tower outlet of the rectifying tower 13 is communicated with the inlet of a power plant boiler 15. The interstage heat exchange in the compression system 1, the end-stage cooler 2, the heat storage tank 3, the reheater 10 and the interstage reheater in the expansion power generation system 11 form a heat storage subsystem; the cryogenic expansion machine 5, the gas-liquid separator 6, the liquid-air storage tank 7, the flow divider 8 and the liquid pump 9 form a liquefied air subsystem; the hydraulic press 12, the rectifying tower 13 and the throttle valve 14 form an air separation subsystem.
The system of the utility model couples links such as liquid air energy storage, air separation, oxygen-enriched combustion and the like, and each link can be operated independently or simultaneously by controlling circulating parameters. The working method of the air separation energy storage coupling oxygen-enriched combustion system comprises the following steps:
air at normal temperature and normal pressure enters a compression system 1 after being filtered and purified to remove water, CO2 and solid impurities in the air; an interstage heat exchanger is arranged between each stage of compressor, heat exchange is carried out between the heat storage medium and high-temperature air at the outlet of each stage of compressor, the air enters the next stage of compressor for compression after the temperature of the air is reduced, and the high-temperature heat storage medium after heat exchange enters a heat storage tank 3 for storage; after the air is compressed by the compression system 1, the pressure is increased to 8MPa from 0.1MPa, and the temperature is increased to 350 ℃ from 20 ℃;
the compressed high-temperature air enters the final stage cooler 2, and exchanges heat with a heat storage medium in the final stage cooler 2 and is cooled, and the temperature of the air is reduced from 350 ℃ to 46 ℃ after heat exchange; the heat-exchanged high-temperature heat storage medium enters a heat storage tank 3 for storage; the cooled air enters a packed bed type cold accumulator 4 for further cooling, and the temperature is reduced from 46 ℃ to-175 ℃; then, the air enters a cryogenic expansion machine 5 to do expansion work, the pressure is reduced from 8MPa to 0.1MPa, the temperature is reduced from-175 ℃ to-196 ℃, partial air is liquefied, and the low-temperature gas-liquid mixed air is arranged at the outlet of the cryogenic expansion machine 5; gas-liquid mixed air enters a gas-liquid separator 6 for two-phase separation, gas-phase air is led out from a gas-phase outlet of the separator 6 and returns to a packed bed type cold accumulator 4 to release cold energy, then the gas-phase air enters a compression system 1 for recompression, and liquid-phase air is led out from a gas-phase outlet of the separator 6 to a liquid-air storage tank 7 for storage;
when the air separation and expansion power generation operation is carried out, liquid air enters the flow divider 8 from the liquid air storage tank 7, the flow divider 8 divides the liquid air into two flows, one flow enters the hydraulic machine 12, the liquid air pressure is increased to 0.7MPa, and then the two flows are sent to the rectifying tower 13; liquid air is separated in the rectifying tower 13, a nitrogen product can be led out under the top cover of a condensation evaporator of the rectifying tower, and an oxygen-enriched air product is led out on the evaporation side; oxygen-enriched air separated out by the rectifying tower 13 is sent into a power plant boiler 15 for oxygen-enriched combustion, so that the combustion efficiency is improved;
the other fluid which is split from the splitter 8 enters a liquid pump 9 to be pressurized, and the pressure is increased to 7 MPa; then the cooled air enters a packed bed type cold accumulator 4 to release cold energy, the temperature is increased and vaporized, and the air temperature is increased from-196 ℃ to 17 ℃; air from the packed bed type cold accumulator 4 enters a reheater 10 to exchange heat with a high-temperature heat storage medium sent by the heat storage tank 3, and the temperature is raised from 17 ℃ to 330 ℃; the heated air enters a turbine expander in the expansion power generation system 11 to do work through expansion, and a coaxial generator is pushed to rotate to generate power; the air expands and does work in each stage of expander, after the temperature and the pressure are reduced, the air enters an interstage reheater to exchange heat with the high-temperature heat storage medium from the heat storage tank 3 and heat up, and after the temperature is increased, the air enters the next stage of expander to expand and do work; after the expansion of the three-stage expander, the air pressure at the outlet of the final-stage expander is exhausted and returns to normal pressure.
The above description is only of the preferred embodiments of the present invention, and it should be noted that: it will be apparent to those skilled in the art that various modifications and adaptations can be made without departing from the principles of the utility model and these are intended to be within the scope of the utility model.

Claims (6)

1. The utility model provides a system of empty energy storage coupling oxygen boosting burning that divides which characterized in that: the system comprises a compression system (1), a stage end cooler (2), a heat storage tank (3), a packed bed type cold storage device (4), a cryogenic expansion machine (5), a gas-liquid separator (6), a liquid-air storage tank (7), a flow divider (8), a liquid pump (9), a reheater (10), an expansion power generation system (11), a hydraulic machine (12), a rectifying tower (13), a throttling valve (14) and a power plant boiler (15);
the final-stage outlet of the compression system (1) is communicated with the hot end inlet of the final-stage cooler (2), the hot end outlet of the final-stage cooler (2) is communicated with the hot end inlet of the packed bed type cold accumulator (4), the hot end outlet of the packed bed type cold accumulator (4) is communicated with the inlet of the cryogenic expander (5), the outlet of the cryogenic expander (5) is communicated with the inlet of the gas-liquid separator (6), the liquid phase outlet of the gas-liquid separator (6) is communicated with the inlet of the liquid-air storage tank (7), the outlet of the liquid-air storage tank (7) is communicated with the inlet of the flow divider (8), the first outlet of the flow divider (8) is communicated with the inlet of the liquid pump (9), the outlet of the liquid pump (9) is communicated with the first cold end inlet of the packed bed type cold accumulator (4), the first cold end outlet of the packed bed type cold accumulator (4) is communicated with the cold end inlet of the reheater (10), the cold end outlet of the reheater (10) is communicated with the primary expander of the expansion power generation system (11), the outlet of the last-stage expander of the expansion power generation system (11) is communicated with the atmosphere; the outlet of an interstage cooler of a multi-stage compressor of the compression system (1) is communicated with the inlet of a heat storage tank (3), and the outlet of the heat storage tank (3) is communicated with the interstage inlet of a multi-stage expander of the expansion power generation system (11); the outlet of the cold end of the stage end cooler (2) is communicated with the inlet of the heat storage tank (3), and the outlet of the heat storage tank (3) is communicated with the inlet of the hot end of the reheater (10); a gas phase outlet of the gas-liquid separator (6) is communicated with a second cold end inlet of the packed bed type regenerator (4), and a second cold end outlet of the packed bed type regenerator (4) is communicated with a primary compressor inlet of the compression system (1); a second outlet of the separator (8) is communicated with an inlet of a hydraulic machine (12), an outlet of the hydraulic machine (12) is communicated with a lower tower inlet of a rectifying tower (13), a lower tower outlet of the rectifying tower (13) is communicated with an inlet of a throttle valve (14), an outlet of the throttle valve (14) is communicated with an upper tower inlet of the rectifying tower (13), and an upper tower outlet of the rectifying tower (13) is communicated with an inlet of a power plant boiler (15);
the interstage heat exchange in the compression system (1), the end-stage cooler (2), the heat storage tank (3), the reheater (10) and the interstage reheater in the expansion power generation system (11) form a heat storage subsystem; the cryogenic expansion machine (5), the gas-liquid separator (6), the liquid-air storage tank (7), the flow divider (8) and the liquid pump (9) form a liquefied air subsystem; the hydraulic machine (12), the rectifying tower (13) and the throttle valve (14) form an air separation subsystem.
2. An air separation energy storage coupled oxycombustion system according to claim 1, characterized in that: the compression system (1) consists of 2-4 stages of compressors, and an interstage heat exchanger is arranged between each stage of compressors and compression is carried out by adopting a constant pressure ratio;
3. an air separation energy storage coupled oxycombustion system according to claim 1, characterized in that: the packed bed type cold accumulator (4) utilizes spherical particle stones as packing materials, and adopts a vacuum packing heat preservation mode outside;
4. an air separation energy storage coupled oxycombustion system according to claim 1, characterized in that: the expansion power generation system (11) consists of 3-4 stages of expansion machines, each expansion machine is coaxially connected with a power generator, and an interstage reheater is arranged between each stage of expansion machine and expansion is carried out by adopting an isobaric ratio.
5. An air separation energy storage coupled oxycombustion system according to claim 1, characterized in that: the heat storage medium in the heat storage subsystem is liquid heat conduction oil, the liquid heat conduction oil is in a closed loop state in the heat storage subsystem, and the liquid heat conduction oil is pushed by a circulating pump to work in each heat exchanger; the specific amount of heat transfer oil and the flow rate between the individual heat exchangers need to be determined according to the capacity of the system.
6. An air separation energy storage coupled oxycombustion system according to claim 1, characterized in that: the rectifying tower (13) is used for separating air and consists of a tower kettle, tower plates, a cylinder shell and a condensation evaporator.
CN202121927621.6U 2021-08-17 2021-08-17 Air separation energy storage coupling oxygen-enriched combustion system Active CN215724557U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113739516A (en) * 2021-08-17 2021-12-03 西安交通大学 Air separation energy storage coupling oxygen-enriched combustion system and method
CN117308663A (en) * 2023-10-18 2023-12-29 浙江大学 Compressed air energy storage system and operation method thereof

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113739516A (en) * 2021-08-17 2021-12-03 西安交通大学 Air separation energy storage coupling oxygen-enriched combustion system and method
CN117308663A (en) * 2023-10-18 2023-12-29 浙江大学 Compressed air energy storage system and operation method thereof

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