CN115750009A - Energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization and operation method - Google Patents
Energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization and operation method Download PDFInfo
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Abstract
An energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization and an operation method thereof are liquid air energy storage, LNG cold energy utilization, a gas generator set and CO 2 The green energy-storing peak-regulating technology includes air compressing unit, air liquefying unit, liquid-air storage tank, liquid-air pump, gasifier, LNG storage tank, LNG pump, gas generator set, CO 2 Trapping unit, gas expansion generator set, heat storage device and cold storage deviceThe device creates a synergistic effect for the large-scale storage and peak-time power generation of renewable energy power or valley electricity, and the thermodynamic efficiency of the distributed energy storage system is improved by recycling the multi-stage cold and heat energy; meanwhile, the method is also a synergistic effect of the peak regulation of the LNG pipe network and the peak regulation height of the gas turbine set, and a large amount of LNG cold energy released in the peak LNG supply process is used for meeting the requirements of a liquid air energy storage system and CO 2 The cold demand in the process is collected, the energy utilization rate is improved, and the purposes of energy conservation and emission reduction are achieved.
Description
Technical Field
The invention relates to the technical fields of cryogenic liquefaction energy storage, peak shaving technology of a gas power station, liquefied natural gas cold energy utilization technology and carbon dioxide capture, in particular to an energy storage power peak shaving system for carbon capture and liquefied natural gas cold energy utilization and an operation method.
Background
The energy development requires further improvement of energy efficient utilization development and enhancement of power grid peak regulation capacity, and in order to optimize an energy structure, promote clean and efficient development and utilization of coal, the energy development of renewable energy sources and promotion of traditional power generation mode transformation are required to be vigorously promoted. In a traditional power generation mode transformation scheme, for example, a large number of thermal power generating units are used for participating in deep peak shaving of a power grid, but when a gas generating unit participates in peak shaving, the problems that the peak shaving of electricity compensation only in peak shaving is insufficient and the like are solved. In order to realize the peak clipping and valley filling capabilities of the off-peak power storage and the peak power supply of the gas power station, the state proposes that a large-scale energy storage technology is involved in energy utilization and power grid peak shaving to solve the energy problem, and the peak shaving gas power station with the large-scale energy storage function is developed, so that the energy conversion rate, the energy utilization rate and the power grid flexible peak shaving capability can be further improved.
Liquid Air Energy Storage (LAES) is used as a novel energy storage mode, and has the characteristics of high energy storage density, no limitation of geographical conditions, longer storage period, capability of depending on the existing mature technology, capability of realizing large-scale system design, stronger technical flexibility and the like, so that the peak-shaving gas power station utilizing the Liquid air energy storage has wider large-scale engineering application and novel energy technology development prospect.
The working principle of the peak shaving gas power station utilizing the liquid air for energy storage is as follows: in the low-ebb period of power utilization, the liquid air energy storage is utilized to store renewable energy power or surplus power in the ebb period, and the electric energy is stored by high-grade cold energy of low-temperature liquid air; during the power consumption peak, the liquid air energy storage system and the gas power station are started simultaneously, liquid air is pressurized and gasified and then is sent into the combustion chamber to be mixed and combusted with natural gas, the generated high-temperature gas enters the gas turbine to do work, electric energy is generated and is input into a power grid during the peak, and then the gas after pressure reduction and temperature reduction is discharged out of the system. In order to solve the problems, chinese patent CN114352366A provides a thermal power plant compressed air cryogenic energy storage and oxygen-enriched combustion carbon capture system, the system drives a compressor to compress air by surplus electric energy, stores heat in a compression process through a lava heat storage system and a solid particle heat storage system, cryogenically separates nitrogen and oxygen through compressed air, and stores electric energy in the forms of liquid nitrogen and liquid oxygen; when the power demand, liquid nitrogen liquid oxygen pressurization, entering expander after the granule heat exchanger heating, high-pressure air inflation work of doing drives the engine electricity generation and merges the electric wire netting to mix boiler flue gas circulation with turbine exhaust and get into the boiler, aim at effectively utilize the exhaust internal energy and improve carbon dioxide concentration in the exhaust, effectively reduce carbon capture running cost. However, the system still has the following problems: aiming at the low-temperature cold energy of liquid air (liquid nitrogen and liquid oxygen), the low-temperature cold energy is not recycled, and the high-grade cold energy in the gasification process is not efficiently utilized; in the energy release process, only a part of liquid air is used for expansion to do work, so that the ratio of air liquefaction power consumption (energy storage) to expanded recovery (energy release) is very low, and the energy recovery rate of the liquid air energy storage system is low; in addition, the high-temperature waste heat of the boiler is not efficiently recycled.
Chinese patent CN108443018A proposes a gas turbine power generation peak regulation system based on liquid air energy storage technology, which stores redundant electric energy of a power generation subsystem in liquid nitrogen and oxygen in a low-temperature cold energy mode during the electricity utilization valley, pressurizes and gasifies the liquid nitrogen and expands to generate power during the electricity utilization peak, converts the cold energy of the liquid nitrogen into electric energy, heats and gasifies the liquid oxygen and supplies the gasified liquid oxygen to a combustion chamber to perform oxygen-enriched combustion with fuel, and meanwhile, pushes a gas turbine to generate power; the system adopts a liquid air energy storage technology, can recover the exhaust waste heat of the gas turbine and reduce the air inlet temperature of the gas turbine, provides an oxygen-enriched combustion environment for a gas power station, effectively improves the efficiency of the gas turbine, and can also improve the stability of power generation and transmission and realize the functions of peak clipping and valley filling after grid connection. However, when the natural gas is supplied in liquid form, i.e., as Liquefied Natural Gas (LNG), the patent does not solve the problem of efficient recycling of a large amount of cold energy in the LNG gasification process.
In order to avoid the waste of a large amount of LNG cold energy, chinese patent CN112254561A provides a liquid air energy storage system utilizing LNG cold energy and gas peak shaving power generation waste heat, the liquid air energy storage system utilizes the LNG cold energy and the gas peak shaving power generation waste heat to improve the efficiency and the energy utilization rate of the liquid air energy storage system, is a coupling of a liquid air energy storage subsystem, a gas peak shaving power generation subsystem and a steam circulation power generation subsystem, and aims to integrate the peak shaving capacity of the system and the flexible peak shaving performance under the condition of variable working conditions. However, in the valley electricity period of the system, the cold energy required by the air compression system comes from the regasification process of the LNG, and the gasified natural gas enters the natural gas pipe network later, so that the valley electricity energy storage process of the system is influenced by the peak valley electricity utilization of the natural gas pipe network, and the LNG cold energy recycling efficiency can be reduced if the matching is unbalanced; in addition, the system does not consider the problem of exhaust carbon emission of the gas peak-shaving generating set, but discharges a large amount of carbon dioxide generated after combustion, so that the content of carbon dioxide in the atmosphere can be increased, and the aim of reducing carbon emission of an energy system is not achieved.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide an energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization and an operation method thereof, and the system is a liquid air energy storage system, an LNG cold energy utilization system, a gas generator set and a CO generator set 2 The coupled green energy storage peak regulation technology is captured, a synergistic effect is created for the large-scale storage of valley electricity and the power generation during peak, and the thermodynamic efficiency of the distributed energy storage system is improved by recycling the multistage cold and heat energy; meanwhile, the method is also a synergistic effect of the peak regulation of the LNG pipe network and the peak regulation height of the gas turbine set, and a large amount of LNG cold energy released in the peak LNG supply process is used for meeting the requirements of a liquid air energy storage system and CO 2 The cold demand of entrapment process further utilizes the residual pressure energy of discharging tail gas to increase extra electric power output, utilizes the waste heat after the gas turbine set burning to promote the efficiency of gas expander, further improves energy multistage utilization ratio such as LNG cold energy, heat of combustion, improves clean energy utilization ratio, utilizes simultaneouslyHigh efficiency CO 2 The trapping technology is used for solving the problem of carbon emission of the exhaust gas and achieving the purposes of energy conservation and emission reduction.
In order to achieve the purpose, the invention adopts the technical scheme that:
an energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization comprises an air compression unit 1, pure air enters the air compression unit 1, the heat output of the air compression unit 1 is connected with a heat storage device 11, a power grid supplies power to the air compression unit 1, the air output of the air compression unit 1 is connected with the air input of a liquid air storage tank 3 through an air liquefaction unit 2, air liquefaction is completed, and electric power is converted into liquid air and stored in the liquid air storage tank 3; the liquid air output of the liquid air storage tank 3 is connected with the first flow input of the vaporizer 5 through the output of the liquid air pump 4, the second flow input of the vaporizer 5 is connected with the output of the LNG storage tank 6 through the first flow output of the LNG pump 7, the cold energy output of the vaporizer 5 is connected with the cold energy input of the cold storage device 12, and the cold energy output of the cold storage device 12 is connected with the cold energy input of the air liquefaction unit 2; the two gas outputs of the gasifier 5 are connected with the input of the gas generator set 8, namely, the gasified air and the natural gas enter the gas generator set 8 to be mixed and combusted, and the power generation is completed and the power is input into a power grid; exhaust gas and CO generated by gas generator set 8 2 The first input of the capture unit 9 is connected, CO 2 The second input of the capture unit 9 is connected to the second LNG output of the LNG pump 7, CO 2 The capture unit 9 reacts and condenses by using LNG cold energy to generate H which is removed from the exhaust gas 2 O and CO 2 High pressure natural gas from CO after release of cold energy 2 CO discharged from the trap unit 9 2 The dry decarbonization exhaust gas of the capture unit 9 enters a gas expansion generator set 10 to push the gas expansion generator set 10 to do work and generate power to be input into a power grid, the dry decarbonization exhaust gas after pressure reduction and temperature reduction is finally exhausted from tail gas of the gas expansion generator set 10, and heat required by the gas expansion generator set 10 is provided by a gas generator set 8; the components must operate in a matched and coordinated operation at the electrical, work, cold, heat energy conversion and material levels.
The air liquefaction unit 2 comprises a basic liquefaction circulating system and a liquefaction circulating system with a low-temperature expander.
The heat storage device 11 comprises a liquid heat storage tank and a solid packed bed type, the heat storage device 11 comprises a heat storage process and a heat release process, the heat storage process is operated in an energy storage stage of the system, and the heat release process is used for industrial heat in an energy release stage or other periods of the system.
The cold accumulation device 12 comprises two forms of a liquid refrigerant cold accumulation tank and a solid packed bed; the cold accumulation device 12 includes a cold accumulation process and a cold release process, the cold accumulation process operates in the energy release stage, and the cold release process operates in the energy storage stage.
The CO is 2 The trap unit 9 includes two modes of an absorption method and a low-temperature method.
The operation method of the energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization comprises an energy storage stage and an energy release stage;
in the energy storage stage, a liquid air energy storage system consisting of an air compression unit 1, an air liquefaction unit 2, a liquid air storage tank 3, a heat storage device 11 and a cold accumulation device 12 is operated to store renewable energy/valley time electric power in the form of liquid air, compression heat is stored in the heat storage device 11, and cold energy in the liquefaction process comes from the cold accumulation device 12;
in the energy release stage, a liquid air pressurizing and regasification unit consisting of a liquid air pump 4 and a vaporizer 5, an LNG cold energy utilization unit consisting of an LNG pump 7 and an LNG storage tank 6, a gas generator set 8, CO are operated 2 The capture unit 9 and the gas expansion generator set 10 complete the utilization of the LNG cold energy, the power output and the carbon capture of the discharged tail gas, and simultaneously store the cold energy of the liquid air regasification and the LNG regasification process in the cold storage device 12.
The specific process flow of the energy storage stage is as follows: in the period of renewable energy sources enrichment or electricity consumption valley, firstly, the air compression unit 1 is operated, the electric power during the surplus/valley of the renewable energy sources is used for driving the air compression unit, the electric energy is converted into the shaft work of the compressor and high-temperature and high-pressure air is obtained, then, the heat storage process of the heat storage device 11 is operated, the compressor-stage post-cooling heat exchanger is used for cooling the compressed air, the heat storage medium is used for absorbing the compression heat in the cooling heat exchanger and storing the compression heat in the heat storage device 11, then, the cold release process of the air liquefaction unit 2 and the cold storage device 12 is operated, the cooled high-pressure and normal-temperature air is sequentially subjected to precooling, throttling and gas-liquid separation to complete the liquefaction of the air, and the separated liquid air is stored in the liquid-air storage tank 3, wherein the cold energy required by the liquefaction process is provided by the cold storage device 12. .
The energy release stage operates under the electricity peak time stage, and the specific process flow is as follows:
firstly, simultaneously operating a liquid air pressurization regasification unit and an LNG cold energy utilization unit, pumping liquid air stored in a liquid air storage tank 3 out through a liquid air pump 4 in a pressurization mode to obtain high-pressure liquid air, pumping LNG in an LNG storage tank 6 out through an LNG pump 7 in a pressurization mode, then operating a cold accumulation process of a vaporizer 5 and a cold accumulation device 12, inputting high-pressure low-temperature liquid air and a first stream of high-pressure low-temperature LNG into the vaporizer 5 to complete rewarming gasification, and obtaining high-pressure normal-temperature air and high-pressure normal-temperature natural gas, wherein all cold energy released in the liquid air and the LNG gasification process is stored in the cold accumulation device 12;
secondly, operating the gas generator set 8, mixing high-pressure normal-temperature air of the liquid air pressurization regasification unit and high-pressure normal-temperature natural gas after gasification by the gasifier 5, entering the combustion chamber, entering high-temperature exhaust tail gas after complete combustion of the natural gas into the gas turbine to push the blades to do work, reducing the temperature and the pressure, outputting electric power to a power grid, wherein the exhaust tail gas after pressure and temperature reduction contains air and CO 2 And H 2 O；
Third step, running CO 2 A capture unit 9 for introducing CO into the second high-pressure low-temperature LNG and all the discharged tail gas generated after combustion power generation 2 In the capture unit 9, LNG cold energy is utilized to condense and remove H 2 O and CO 2 ；
Fourthly, operating the gas expansion generating set 10, enabling the dehydrated and decarbonized exhaust gas to enter the gas expansion generating set 10, reducing the temperature and the pressure and outputting electric power, wherein the heat source of the gas expansion generating set 10 comes from the gas generating set 8; and finally, discharging the discharged tail gas after decarburization and expansion depressurization are finished.
The invention has the beneficial effects that:
1. the invention relates to the cooperative operation of peak regulation height of an LNG pipe network and peak regulation height of a gas turbine set, and a large amount of LNG cold energy released in the LNG supply process during peak is used for meeting the requirements of a liquid air energy storage system and CO 2 The cold demand in the process is collected, the comprehensive utilization rate of the LNG cold energy is improved, and a new process method can be provided for the development of a low-temperature energy coupling technology and the efficient recycling of high-grade low-temperature cold energy.
2. Aiming at the problems of residual pressure energy and high-temperature waste heat waste and the like in the operation process of a gas power station, the invention utilizes the extra power output by the gas expander to supply the combustion waste heat to the gas expander so as to improve the power generation efficiency of the gas expander, so the process of the invention can reduce the energy waste and further improve the power generation efficiency and the comprehensive energy utilization rate of the gas power station.
3. The invention combines and utilizes the high-efficiency CO of LNG cold energy 2 The invention relates to a trapping method for realizing low-carbon or near-zero carbon emission of exhaust gas, which can solve the environmental problems of greenhouse gas emission and the like of the traditional gas power station and CO 2 The invention has the advantages of achieving the aim of reducing carbon emission of a gas power station, improving the power generation efficiency and economic benefit of the equipment and the like at the same time.
4. The invention relates to a multistage energy comprehensive utilization integrated technology operation method for reducing carbon emission based on renewable energy power/off-peak power resource large-scale storage, peak shaving of a gas power station and LNG cold energy utilization.
Drawings
Fig. 1 is a schematic structural diagram of embodiment 1 of the present invention.
Fig. 2 is a schematic structural diagram of a 47MW stage in example 2 of the present invention.
Detailed Description
The technical solution of the present invention is described in detail below with reference to the embodiments and the accompanying drawings.
Embodiment 1, referring to fig. 1, an energy storage power peak shaving system for carbon capture and liquefied natural gas cold energy utilization is liquid air energy storage, LNG cold energy utilization, gas generator set and CO 2 The novel green energy storage peak shaving technology for trapping high coupling comprises an air compression unit 1, pure air enters the air compression unit 1, the heat output of the air compression unit 1 is connected with a heat storage device 11, a power grid supplies power to the air compression unit 1, the air output of the air compression unit 1 is connected with the air input of a liquid air storage tank 3 through an air liquefaction unit 2, air liquefaction is completed, and electric power is converted into liquid air and stored in the liquid air storage tank 3; the liquid air output of the liquid air storage tank 3 is connected with the first flow input of the vaporizer 5 through the output of the liquid air pump 4, the second flow input of the vaporizer 5 is connected with the output of the LNG storage tank 6 through the first flow output of the LNG pump 7, the cold energy output of the vaporizer 5 is connected with the cold energy input of the cold storage device 12, and the cold energy output of the cold storage device 12 is connected with the cold energy input of the air liquefaction unit 2; the two gas outputs of the gasifier 5 are connected with the input of the gas generator set 8, namely, the gasified air and the natural gas enter the gas generator set 8 to be mixed and combusted, and the power generation is completed and the power is input into a power grid; exhaust gas and CO discharged from gas generator set 8 2 The first input of the capture unit 9 is connected, CO 2 The second input of the capture unit 9 is connected to the second LNG output of the LNG pump 7, CO 2 The capture unit 9 utilizes LNG cold energy to condense and remove H in the exhaust gas 2 O and CO 2 High pressure natural gas from CO after release of cold energy 2 CO discharged from the trap unit 9 2 The dry decarbonization exhaust gas of the capture unit 9 enters a gas expansion generator set 10 to push the gas expansion generator set 10 to do work and generate power to be input into a power grid, the dry decarbonization exhaust gas after pressure reduction and temperature reduction is finally exhausted from the gas expansion generator set 10, and the heat required by the gas expansion generator set 10 is provided by a gas generator set 8; the components must operate in a matched and coordinated operation at the electrical, work, cold, heat energy conversion and material levels.
An operation method of an energy storage power peak shaving system for carbon capture and liquefied natural gas cold energy utilization comprises an energy storage stage and an energy release stage;
in the energy storage stage, a liquid air energy storage system consisting of an air compression unit 1, an air liquefaction unit 2, a liquid air storage tank 3, a heat storage device 11 and a cold accumulation device 12 is operated to store renewable energy/valley time electric power in the form of liquid air, compression heat is stored in the heat storage device 11, and cold energy in the liquefaction process comes from the cold accumulation device 12; the specific process flow is as follows: in the period of renewable energy sources enrichment or electricity consumption valley, firstly, the air compression unit 1 is operated, the electric power during the surplus/valley of the renewable energy sources is used for driving the air compression unit, the electric energy is converted into the shaft work of the compressor and high-temperature and high-pressure air is obtained, then, the heat storage process of the heat storage device 11 is operated, the compressor-stage post-cooling heat exchanger is used for cooling the compressed air, the heat storage medium is used for absorbing the compression heat in the cooling heat exchanger and storing the compression heat in the heat storage device 11, then, the cold release process of the air liquefaction unit 2 and the cold storage device 12 is operated, the cooled high-pressure and normal-temperature air is sequentially subjected to precooling, throttling and gas-liquid separation to complete the liquefaction of the air, and the separated liquid air is stored in the liquid-air storage tank 3, wherein the cold quantity required by the liquefaction process is provided by the cold storage device 12.
The air liquefaction unit 2 comprises a basic liquefaction circulating system and a liquefaction circulating system with a low-temperature expander; the heat storage device 11 comprises a liquid heat storage tank and a solid packed bed type, the heat storage device 11 comprises a heat storage process and a heat release process, the heat storage process is operated in an energy storage stage of the system, and the heat release process is used for industrial heat in an energy release stage or other periods of the system.
The cold accumulation device 12 comprises two forms of a liquid refrigerant cold accumulation tank and a solid packed bed; the cold accumulation device 12 comprises a cold accumulation process and a cold release process, wherein the cold accumulation process operates in an energy release stage, and the cold release process operates in an energy storage stage; the liquid refrigerant cold accumulation tank type cold accumulation device is designed according to the grading of cold energy temperature areas required by air liquefaction and is divided into a low temperature area and a lower temperature area, wherein the temperature area of a refrigerant selected for cold accumulation in the low temperature area is-180 to-80 ℃, and the temperature area of the refrigerant selected for cold accumulation in the lower temperature area is-80 to 25 ℃; the solid packed bed type cold accumulation device comprises two forms of a solid sensible heat cold accumulation packed bed and a solid-liquid PCM (phase change material) cold accumulation packed bed.
In the electricity consumption peak period, the energy releasing period is operated, and the liquid air pressurizing and regasification unit consisting of the liquid air pump 4 and the vaporizer 5, the LNG cold energy utilization unit consisting of the LNG pump 7 and the LNG storage tank 6, the gas generator set 8, the CO are operated 2 The collecting unit 9 and the gas expansion generator set 10 finish the utilization of LNG cold energy, the output of electric power and the carbon collection of discharged tail gas, and simultaneously store the cold energy of the liquid air regasification and the LNG regasification process in the cold storage device 12; the specific process flow is as follows:
firstly, simultaneously operating a liquid air pressurizing and regasification unit and an LNG cold energy utilization unit, pressurizing and pumping liquid air stored in a liquid air storage tank 3 by a liquid air pump 4 to obtain high-pressure liquid air, pressurizing and pumping LNG in an LNG storage tank 6 by an LNG pump 7, then operating a cold accumulation process of a vaporizer 5 and a cold accumulation device 12, inputting the high-pressure low-temperature liquid air and a first stream of high-pressure low-temperature LNG into the vaporizer 5 by the two streams of pressurized fluids to complete re-temperature gasification, and obtaining high-pressure normal-temperature air and high-pressure normal-temperature natural gas, wherein all cold energy released in the liquid air and the LNG gasification process is stored in the cold accumulation device 12;
secondly, operating the gas generator set 8, mixing the high-pressure normal-temperature air gasified by the gasifier 5 and the high-pressure normal-temperature natural gas into a combustion chamber, and ensuring that the discharged tail gas only contains air and CO in order to efficiently utilize the chemical energy of the natural gas and avoid the generation of flue gas such as CO and the like 2 And H 2 The proportion of the natural gas to oxygen in the air is to ensure that the natural gas is subjected to complete combustion reaction, and high-temperature exhaust tail gas obtained after the natural gas is completely combusted enters a gas turbine to push blades to do work, so that the temperature and the pressure are reduced, and then electric power is output;
third, to reduce greenhouse gas emissions, CO is operated 2 A capturing unit 9 for introducing CO into the second high-pressure low-temperature LNG and all the exhaust tail gas generated after combustion power generation 2 In the capture unit 9, the LNG cold energy is used for removing H 2 O and CO 2 The pressure of the exhaust gas after expansion of the gas turbine is higher than that of CO 2 The three-phase point pressure of the reactor is 0.52MPa, and the aim is to avoid CO from appearing in the operation process 2 The solidification phenomenon affects the normal operation of system equipment, particularly a heat exchanger, so that the exhaust gas enters CO 2 The pressure at the capture unit 9 is higher than 0.52MPa;
fourthly, operating the gas expansion generating set 10, enabling the dehydrated and decarbonized exhaust gas (the main component is air) to enter the gas expansion generating set 10, reducing the temperature and the pressure and outputting electric power, wherein the heat source of the gas expansion generating set 10 is from the gas generating set 8; and finally, discharging the discharged tail gas after decarburization and expansion depressurization are finished.
The CO is 2 The trap unit 9 includes two modes of an absorption method and a low-temperature method: the absorption method can utilize the hydramine aqueous solution to treat CO in the exhaust gas 2 Capture, typically CO absorption based on aqueous alcohol amine solutions 2 The trapping system comprises an amine absorption tower, an amine regeneration tower, a reboiler, a booster pump, a lean-rich solution heat exchanger and the like, and CO is obtained 2 Discharging the rest of the discharged tail gas from the top of the absorption tower; the low-temperature method is to remove H in the exhaust gas in turn by adopting a condensation method 2 O and CO 2 (to avoid the low temperature freezing phenomenon in the condensing heat exchanger, H 2 O condensing heat exchanger and CO 2 The temperature of the tail gas discharged from the condensing heat exchanger is respectively higher than H 2 O and CO 2 The temperature of the triple point of the gas and the pressure of the discharged tail gas are higher than that of CO 2 Triple point pressure) H can be condensed using LNG cold energy 2 O and CO 2 The method does not need an absorption tower and an alcohol amine water solution, and can save the cost of absorption tower equipment and an absorption solvent.
For by-products, e.g. stored heat of excess compression, CO removal as a heat source for other industrial applications 2 Can be used for CO 2 Refrigeration system or CO 2 And in the power generation system, the gasified high-pressure natural gas enters a natural gas pipe network and is supplied to distributed energy users according to the demand of the natural gas consumption.
Example 2 referring to fig. 2, in addition to example 1, a three-stage compressor unit, a basic liquefaction cycle, a cold storage tank type cold storage device, a heat storage tank type heat storage device, and a low temperature C using LNG cold energy are usedO 2 A trapping unit;
the air compression unit 1 adopts a three-stage compressor unit and comprises a three-stage air compression unit 1-1 and three-stage aftercoolers 1-2, the output of each compressor is connected with the first input of each stage aftercooler, air passes through the three-stage air compression unit 1-1 and the three-stage aftercoolers 1-2 in sequence to obtain air with normal temperature and high pressure, and a renewable energy power grid supplies power to the air compression unit 1 during valley time.
The air is output by the air compression unit 1 and input into the air liquefaction unit 2, the air liquefaction unit 2 comprises an air condenser 2-1, a Joule-Thomson valve 2-2 and an air gas-liquid separator 2-3 which are sequentially connected, the air liquefaction is completed, the electric power is converted into liquid air, and the liquid air is stored in the liquid air storage tank 3; the liquid air output of the liquid air storage tank 3 is connected with the first stream input of the vaporizer 5 through the output of the liquid air pump 4, the output of the LNG storage tank 6 and the output of the LNG pump 7 are sequentially connected with the second stream input of the vaporizer 5, the liquid air and the LNG complete rewarming gasification in the vaporizer 5, the first output and the second output of the vaporizer 5 are connected with the first input and the second input of the reheater 13, and the rewarming air and the natural gas are heated again.
The air and natural gas output of the reheater 13 is connected with the input of a gas generator set 8, and the gas generator set 8 comprises a combustion chamber 8-1, a gas turbine 8-2 and a gas generator set cooler 8-3 which are connected in sequence; the natural gas and the air are subjected to complete combustion reaction in the combustion chamber 8-1, the discharged tail gas after combustion is introduced into the gas turbine 8-2 to push turbine blades to do work to generate power and input the power grid, and the discharged tail gas after pressure reduction is cooled in the gas turbine set cooler 8-3; the discharged tail gas is primarily cooled by a gas unit cooler 8-3, and then is secondarily output by the gas unit cooler 8-3 and CO 2 The trapping unit 9 is connected to trap carbon in the exhaust gas; said CO 2 The capture unit 9 adopts low-temperature CO utilizing LNG cold energy 2 The trapping device comprises a first precooler 9-1, a first gas-liquid separator 9-2, a second precooler 9-3, a second gas-liquid separator 9-4, a component separator 9-5, and CO 2 9-6 parts of condenser, liquid CO 2 9-7 parts of a storage tank, 9-8 parts of a liquid refrigerant cold storage tank and 9-9 parts of a heat regenerator; first precooler 9-1 first output andthe first gas-liquid separator 9-2 is connected in input, condenses and separates H 2 O, a gas phase outlet of the first gas-liquid separator 9-2 is connected with an input of a second gas-liquid separator 9-4 through a second precooler 9-3, and liquid CO is separated by condensation 2 And a small amount of H remains 2 O, a gas phase outlet of the second gas-liquid separator 9-4 is connected with an input of the component separator 9-5, and CO of the component separator 9-5 2 The component is treated with CO 2 Condensers 9-6 and liquid CO 2 The storage tanks 9-7 are connected, and residual CO is discharged 2 Separated, condensed and stored in liquid CO 2 In a storage tank 9-7, the output of dry decarbonization exhaust gas (the main component is air) of a component separator 9-5 is connected with a first input of a gas unit cooler 8-3 to obtain heat, then the first output of the gas unit cooler 8-3 is connected with a gas expansion generator set 10, high-temperature dry decarbonization exhaust gas does work in the gas expansion generator set 10 and generates electricity to be input into a power grid, the dry decarbonization exhaust gas after pressure reduction and temperature reduction is output from the gas expansion generator set 10 and connected with a first input of a reheater 13, and finally the dry decarbonization exhaust gas is discharged out of the system through a first output of the reheater 13; CO 2 2 The refrigerant inlet of the condenser 9-6 is connected with the inlet of the liquid refrigerant cold accumulation tank 9-8 through the heat regenerator 9-9, and CO 2 The refrigerant outlet of the condenser 9-6 is sent to another liquid refrigerant cold accumulation tank 9-8.
The heat storage device 11 adopts a heat storage tank type heat storage device and comprises a low-temperature heat conduction oil storage tank 11-5, the output of the low-temperature heat conduction oil storage tank 11-5 is connected with the second input of three-stage after-coolers 1-2 through a low-temperature heat conduction oil pump 11-6, the second output of the three-stage after-coolers 1-2 is connected with the input of a high-temperature heat conduction oil storage tank 11-1, and compression heat is stored in the high-temperature heat conduction oil storage tank 11-1; the output of the high-temperature heat conduction oil storage tank 11-1 is connected with the input of other industrial heat systems 11-3 through a high-temperature heat conduction oil pump 11-2; the output of other industrial heat systems 11-3 is connected with the input of a low-temperature heat conducting oil storage tank 11-5 through a high-temperature heat conducting oil cooler 11-4.
The cold accumulation device 12 comprises a low-temperature liquid methanol storage tank 12-1, the output of the low-temperature liquid methanol storage tank 12-1 is connected with a high-temperature section refrigerant inlet of an air condenser 2-1 of the air liquefaction unit 2 through a low-temperature liquid methanol pump 12-2, and a high-temperature section refrigerant outlet of the air condenser 2-1 is connected with a high-temperature section refrigerant inlet of the gasifier 5 through a high-temperature liquid methanol storage tank 12-3, a high-temperature liquid methanol pump 12-4; the outlet of the high-temperature section refrigerant of the gasifier 5 is connected with the input of a low-temperature liquid methanol storage tank 12-1; the output of the low-temperature liquid propane storage tank 12-5 is connected with a low-temperature section refrigerant inlet of an air condenser 2-1 of the air liquefaction unit 2 through a low-temperature liquid propane pump 12-6, and a low-temperature section refrigerant outlet of the air condenser 2-1 is connected with a low-temperature section refrigerant inlet of the gasifier 5 through a high-temperature liquid propane storage tank 12-7 and a high-temperature liquid propane pump 12-8; the low-temperature section refrigerant outlet of the gasifier 5 is connected with the input of a low-temperature liquid propane storage tank 12-5.
The operation method of the energy storage power peak shaving system for carbon capture and liquefied natural gas cold energy utilization comprises an energy storage stage and an energy release stage, wherein specific key settings and performance parameters of a certain operation condition of the system in the embodiment refer to a table 1;
in the energy storage stage, firstly, purified air enters a three-stage air compression unit, a renewable energy source electric power/valley power is used for driving a three-stage air compression unit 1-1 with an equal pressure ratio to obtain high-temperature and high-pressure air, the equal pressure ratio is 4.93, the highest pressure of a compressor is 12MPa, then the compressed air is cooled through a three-stage after-cooler 1-2 to obtain air with normal temperature and high pressure, wherein low-temperature heat conduction oil and the high-temperature compressed air exchange heat in the three-stage after-cooler 1-2, the low-temperature heat conduction oil absorbs compression heat to obtain heat and then outputs the heat as high-temperature heat conduction oil, and the compression heat is then stored in a heat conduction oil high-temperature storage tank 11-1; then, normal-temperature high-pressure air enters an air liquefaction unit 2, precooling, cooling and throttling depressurization are sequentially carried out through an air condenser 2-1 and a Joule-Thomson valve 2-2 to 0.1MPa, the air is throttled, cooled and depressurized to be in a low-temperature gas-liquid saturated state, air liquefaction is completed, and low-temperature and low-pressure saturated gas-liquid mixed air is obtained, wherein the cold energy in the air precooling process is provided by two parts, one part is provided by low-temperature refrigerants stored in a low-temperature liquid methanol storage tank 12-1 and a low-temperature liquid propane storage tank 12-5, and the other part is provided by low-temperature backflow air separated after throttling liquefaction; then, the gas-liquid mixed air enters an air-liquid separator 2-3 to separate a liquid air product and low-temperature gaseous air; finally, the part of the reverse flow air is finallyThe air is mixed with the purified air and then enters the three-stage air compressor unit 1-1 again, circulation is carried out, and the separated liquid air is stored in the liquid air storage tank 3. In the power consumption peak period, in the energy releasing operation stage, firstly, liquid air stored in the liquid air storage tank 3 is pumped out through the liquid air pump 4 to obtain 7MPa of supercritical liquid air, and LNG stored in the LNG storage tank 6 is pumped out through the LNG pump 7 to obtain 7MPa of supercritical LNG; then, the supercritical liquid air is gasified in the gasifier 5, the supercritical LNG enters from the middle section of the gasifier 5 and is gasified, wherein the liquid air and the cold energy released in the LNG gasification process are taken away by the circulating refrigerant in the cold storage device 12 and are stored in the low-temperature liquid methanol storage tank 12-1 and the low-temperature liquid propane storage tank 12-5; next, the regasified air and a portion of the regasified natural gas are reheated in the reheater 13 and then mixed into the gas-fired power generator set 8; to ensure that the exhaust gas is only air and H 2 O and CO 2 The natural gas and the air are subjected to complete combustion reaction in the combustion chamber 8-1, and it is noted that the current application technology of exhaust gas cooling and high-temperature-resistant ceramic materials limits the inlet temperature of the gas turbine 8-2, and when the temperature of the gas turbine 8-2 exceeds 1650 ℃, the strong heat radiation can cause the refrigeration failure of a gas unit cooler 8-3 behind the gas turbine, so that CO of the exhaust gas can be generated 2 The trapping system cannot function, so the maximum combustion temperature of this embodiment is set to 1500 ℃, and in view of this, the ratio of the oxygen component in the air to the natural gas needs to meet the above requirements; the discharged tail gas is then introduced into a gas turbine 8-2 to push turbine blades to do work to generate power and is input into a peak-time power grid, and the discharged tail gas after pressure reduction immediately flows into a gas unit cooler 8-3 to finish primary cooling; then, the exhaust gas after primary cooling enters low-temperature CO 2 H in the trap unit 9 2 O and CO 2 The removing process comprises the following specific steps: the discharged tail gas passes through a first precooler 9-1 and a first gas-liquid separator 9-2 in sequence, H is condensed and separated 2 O, then the liquid CO passes through a second precooler 9-3 and a second gas-liquid separator 9-4, and a small amount of liquid CO is separated by condensation 2 And a small amount of H remains 2 O, discharge from gas outlet of the second gas-liquid separator 9-4 at this timeThe tail gas is completely removed with H 2 O, but residual CO 2 The components still need to be removed continuously, so that the exhaust tail gas is introduced into a component separator 9-5, and the residual CO in the exhaust tail gas is removed 2 Separation and removal of CO in this example 2 The removal rate reaches 99.99 percent; CO separated in component separator 9-5 2 Gas utilization of LNG cold energy in CO 2 Condensing in a condenser 9-6 to obtain liquid CO 2 Storage in liquid CO 2 In the storage tank 9-7, the LNG is CO 2 After cold energy is provided by condensation, the residual part of the cold energy is recycled and stored in a liquid refrigerant cold storage tank 9-8 through a heat regenerator 9-9, then enters a second precooler 9-3 and a first precooler 9-1 to provide cold energy for precooling the discharged tail gas, and finally natural gas at high pressure and normal temperature is obtained and can be used as a fuel source of distributed energy; removal of H 2 O and CO 2 And the decarbonized exhaust gas (mainly composed of air) is discharged from the component separator 9-5, then flows back to the gas turbine unit cooler 8-3 to obtain heat and raise the temperature, then the high-temperature dry decarbonized exhaust gas enters the gas expansion generator set 10 to expand to generate power for an input peak time power grid, and the dry decarbonized exhaust gas after being reduced in pressure and temperature is returned to the reheater 13 to be further cooled to the ambient temperature, and finally is discharged.
It is noted that CO is present at low temperatures 2 In the trapping unit, in order to avoid low-temperature freezing phenomenon, which affects normal operation of system pipelines and equipment, particularly a condensing heat exchanger, the pressure of the exhaust gas discharged after expansion is higher than that of CO 2 At a triple point pressure of 0.52MPa and in addition, at H 2 O and CO 2 When in condensation removal, the temperature of the tail gas discharged from the first precooler 9-1 and the second precooler 9-3 is respectively higher than H 2 O and CO 2 The triple point temperature of (0 ℃ C. And-56.56 ℃ C., respectively).
In order to further illustrate the technical effect of the embodiment, the process simulation calculation is performed on the embodiment 2, the key system parameters and key systematics of the embodiment refer to table 1, the environmental pressure is 0.1MPa, and the environmental temperature is 25 ℃; the mass flow of air at the inlet of the compressor, the outlet pressure of the compressor unit, the storage pressure of liquid air, the pressure of the liquid air pump and the pressure of the LNG pump are respectively set as200000kg/h, 12MPa, 0.1MPa, 7MPa and 7MPa; low temperature CO 2 The inlet pressure of the capture unit and the pressure before the gas expander are both 0.8MPa; when the power grid is in the peak, the gas generator set 8 and the gas expansion generator set 10 do work and generate power simultaneously, and the total generated power is calculated to be 47.21MW; in addition, CO 2 The capture rate (mole fraction) can reach more than 99.99 percent;
TABLE 1
System for controlling a power supply
Efficiency is the key performance indicator for evaluating the overall energy utilization and energy depreciation characteristics of the system, and thus, for the energy release stage in embodiment 2
Efficiency is calculated, the energy release phase of this embodiment
Efficiency being the total output of the energy-releasing stage
And total input of energy release stage
Ratio of the energy release stages
The result of efficiency was 74.71%; total output of the energy release phase
IncludedThe output work of the gas turbine 8-2, the output work of the gas expansion generating set 10 and the cold stored in the cold storage device 12
Cold stored in low temperature liquid methanol tank 12-1 and low temperature liquid propane tank 12-5
Liquid H generated by the first gas-liquid separator 9-2 2 Physical of O
Liquid CO produced by the second gas-liquid separator 9-4 2 Physics of physics
Storage in liquid CO 2 Liquid CO of storage tank 9-7 2 Physics of physics
And physical discharge of high pressure natural gas
Total input of the energy release phase
Including liquid air physics provided by liquid air storage tank 3
LNG input cold of LNG storage tank 6
The input work of the liquid air pump 4, the input work of the LNG pump 7 and the total input net chemical energy of the natural gas used as fuel, which is the product of the total input mass flow of the natural gas used as fuel and the net Heating Value (LHV) of the natural gas.
The calculation of the power generation efficiency of example 2 is to evaluate the power generation capacity of the system at the system peak, which is the ratio of the total output work (the total work of the gas turbine 8-2 and the gas expansion power generation unit 10) and the total fuel input purification chemical in the energy release stage of the system, and the calculation result of the power generation efficiency is 88.62%.
Calculating the energy recovery Efficiency (RTE) of example 2, namely, evaluating the ratio of the sum of the compressor power consumption and the total fuel input net chemical energy in the energy storage stage of the system to the net output power (the difference between the total work of the gas turbine 8-2 and the gas expansion generator set 10 and the total power consumption of the liquid air pump 4 and the LNG pump 7) in the energy release stage of the system, and calculating the result of the energy recovery Efficiency to be 54.28%; for a large-scale energy storage peak shaving system, the energy recovery efficiency of the system is considered to be economical when the energy recovery efficiency is greater than 50%, and therefore, the technical scheme of the embodiment is feasible.
Those of ordinary skill in the art will understand that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. An energy storage power peak shaving system that carbon entrapment and liquefied natural gas cold energy utilized, includes air compression unit (1), its characterized in that: pure air enters the air compression unit (1), the heat output of the air compression unit (1) is connected with the heat storage device (11), the power grid supplies power to the air compression unit (1), the air output of the air compression unit (1) is connected with the air input of the liquid air storage tank (3) through the air liquefaction unit (2), air liquefaction is completed, and electric power is converted into liquid air and stored in the liquid air storage tank (3); the liquid air output of the liquid air storage tank (3) is connected with the first stream input of the gasifier (5) through the output of the liquid air pump (4), the second stream input of the gasifier (5) is connected with the output of the LNG storage tank (6) through the first stream LNG output of the LNG pump (7), and the cold energy output of the gasifier (5) is connected with the output of the LNG storage tank (6)The cold energy input of the cold accumulation device (12) is connected, and the cold energy output of the cold accumulation device (12) is connected with the cold energy input of the air liquefaction unit (2); two gas outputs of the gasifier (5) are connected with the input of the gas generator set (8), namely, gasified air and natural gas enter the gas generator set (8) to be mixed and combusted, and power generation is completed and the air and the natural gas are input into a power grid; exhaust gas and CO discharged by gas generator set (8) 2 A first input of the capture unit (9) is connected with CO 2 The second input of the capture unit (9) is connected with the second LNG output of the LNG pump (7), and CO 2 The capture unit (9) utilizes LNG cold energy to condense and remove H in the exhaust gas 2 O and CO 2 High pressure natural gas from CO after release of cold energy 2 CO discharged from the trap unit (9) 2 The dry decarbonization exhaust gas of the gathering unit (9) enters a gas expansion generator set (10), the gas expansion generator set (10) is pushed to do work and generate power to be input into a power grid, the dry decarbonization exhaust gas after pressure reduction and temperature reduction is finally discharged from the gas expansion generator set (10), and heat required by the gas expansion generator set (10) is provided by a gas generator set (8); the components must operate in a matched and coordinated operation at the electrical, work, cold, heat energy conversion and material levels.
2. The system of claim 1, wherein: the air liquefaction unit (2) comprises a basic liquefaction circulating system and a liquefaction circulating system with a low-temperature expansion machine.
3. The system of claim 1, wherein: the heat storage device (11) comprises a liquid heat storage tank and a solid packed bed type, the heat storage device (11) comprises a heat storage process and a heat release process, the heat storage process is operated in the energy storage stage of the system, and the heat release process is used for industrial heat in the energy release stage or other periods of the system.
4. The system of claim 1, wherein: the cold accumulation device (12) comprises two forms of a liquid refrigerant cold accumulation tank and a solid packed bed; the cold accumulation device (12) comprises a cold accumulation process and a cold release process, wherein the cold accumulation process is operated in the energy release stage of the system, and the cold release process is operated in the energy storage stage of the system.
5. The system of claim 1, wherein: the CO is 2 The trap unit (9) includes two modes, an absorption method and a low-temperature method.
6. The method of claim 1 for operating a carbon capture and lng cold energy utilization energy storage power peak shaving system comprising an energy storage stage and an energy release stage;
in the energy storage stage, a liquid air energy storage system consisting of an air compression unit (1), an air liquefaction unit (2), a liquid air storage tank (3), a heat storage device (11) and a cold accumulation device (12) is operated to store renewable energy/valley time electric power in the form of liquid air, compression heat is stored in the heat storage device (11), and cold energy in the liquefaction process comes from the cold accumulation device (12);
in the energy release stage, a liquid air pressurization regasification unit consisting of a liquid air pump (4) and a gasifier (5), an LNG cold energy utilization unit consisting of an LNG pump (7) and an LNG storage tank (6), a gas generator set (8), and CO are operated 2 The collecting unit (9) and the gas expansion generator set (10) finish LNG cold energy utilization, power output and carbon collection of discharged tail gas, and simultaneously store cold energy of liquid air regasification and LNG regasification processes in the cold storage device (12).
7. The method according to claim 6, wherein the specific process flow of the energy storage stage is as follows: in the period of renewable energy sources enrichment or electricity consumption valley, firstly, the air compression unit (1) is operated, the electric power during the surplus/valley of the renewable energy sources is used for driving the air compression unit, the electric energy is converted into the shaft work of the compressor and high-temperature and high-pressure air is obtained, then, the heat storage process of the heat storage device (11) is operated, the compressor-stage post-cooling heat exchanger is used for cooling the compressed air, the heat storage medium is used for absorbing the compression heat in the cooling heat exchanger and storing the compression heat in the heat storage device (11), then, the cold release process of the air liquefaction unit (2) and the cold storage device (12) is operated, the cooled high-pressure and normal-temperature air is sequentially subjected to precooling, throttling and gas-liquid separation to complete air liquefaction, and the separated liquid air is stored in the liquid-air storage tank (3), wherein the cold energy required by the liquefaction process is provided by the cold storage device (12).
8. The method according to claim 6, wherein the energy release stage is operated in a peak power utilization stage, and the specific process flow is as follows:
the method comprises the steps that firstly, a liquid air pressurizing and regasification unit and an LNG cold energy utilization unit are operated at the same time, liquid air stored in a liquid air storage tank (3) is pressurized and pumped out through a liquid air pump (4) to obtain high-pressure liquid air, LNG in an LNG storage tank (6) is pressurized and pumped out through an LNG pump (7), then a cold accumulation process of a vaporizer (5) and a cold accumulation device (12) is operated, high-pressure low-temperature liquid air and a first stream of high-pressure low-temperature LNG are input into the vaporizer (5) to complete re-warming gasification, high-pressure normal-temperature air and high-pressure normal-temperature natural gas are obtained, and all cold energy released in the liquid air and the LNG gasification process is stored in the cold accumulation device (12);
and secondly, operating the gas generator set (8), mixing high-pressure normal-temperature air gasified by the gasifier (5) and high-pressure normal-temperature natural gas together to enter a combustion chamber, feeding high-temperature exhaust tail gas after the natural gas is completely combusted into the gas turbine to push the blades to do work, cooling and reducing the pressure, outputting electric power to a power grid, wherein the exhaust tail gas after reducing the pressure and the temperature contains air and CO 2 And H 2 O；
Third step, running CO 2 A capturing unit (9) for introducing CO into the second high-pressure low-temperature LNG and all the discharged tail gas after combustion power generation 2 In the capture unit (9), LNG cold energy is utilized to condense and remove H 2 O and CO 2 ；
Fourthly, operating the gas expansion generating set (10), enabling the dehydrated and decarbonized exhaust gas to enter the gas expansion generating set (10), reducing the temperature and the pressure and outputting electric power, wherein the heat source of the gas expansion generating set (10) comes from the gas generating set (8); and finally, discharging the discharged tail gas after decarburization and expansion depressurization are finished.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117220305A (en) * | 2023-08-31 | 2023-12-12 | 中海石油气电集团有限责任公司 | Efficient energy storage power generation peak shaving system based on LNG cold energy recovery |
| CN118167452A (en) * | 2024-05-09 | 2024-06-11 | 势加透博(成都)科技有限公司 | Waste heat energy storage system and method |
| CN118167452B (en) * | 2024-05-09 | 2024-07-23 | 势加透博(成都)科技有限公司 | Waste heat energy storage system and method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117220305A (en) * | 2023-08-31 | 2023-12-12 | 中海石油气电集团有限责任公司 | Efficient energy storage power generation peak shaving system based on LNG cold energy recovery |
| CN117220305B (en) * | 2023-08-31 | 2024-05-17 | 中海石油气电集团有限责任公司 | Efficient energy storage power generation peak shaving system based on LNG cold energy recovery |
| CN118167452A (en) * | 2024-05-09 | 2024-06-11 | 势加透博(成都)科技有限公司 | Waste heat energy storage system and method |
| CN118167452B (en) * | 2024-05-09 | 2024-07-23 | 势加透博(成都)科技有限公司 | Waste heat energy storage system and method |
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