CN118129067A - Energy recovery type supercritical compressed carbon dioxide energy storage system and constant-pressure energy release method - Google Patents
Energy recovery type supercritical compressed carbon dioxide energy storage system and constant-pressure energy release method Download PDFInfo
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- CN118129067A CN118129067A CN202410324506.1A CN202410324506A CN118129067A CN 118129067 A CN118129067 A CN 118129067A CN 202410324506 A CN202410324506 A CN 202410324506A CN 118129067 A CN118129067 A CN 118129067A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 412
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 209
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 203
- 238000011084 recovery Methods 0.000 title claims abstract description 80
- 238000004146 energy storage Methods 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000005338 heat storage Methods 0.000 claims abstract description 20
- 230000008569 process Effects 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims description 178
- 238000010438 heat treatment Methods 0.000 claims description 19
- 238000009825 accumulation Methods 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 7
- 230000008859 change Effects 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 3
- 230000000704 physical effect Effects 0.000 description 3
- 238000005381 potential energy Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 125000004122 cyclic group Chemical group 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 206010037660 Pyrexia Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
Abstract
The invention provides an energy recovery type supercritical compressed carbon dioxide energy storage system which comprises a low-pressure gas storage tank, a high-pressure gas storage tank, a compressor, a cooler I, a cooler II, a low-grade heat recovery tank, a heat storage tank, a cold storage tank, a reheater and an expander, wherein the low-pressure gas storage tank is connected with the high-pressure gas storage tank; the air outlet of the low-pressure air storage tank is communicated with the air inlet of the compressor; the compressed air outlet is communicated with the air inlet of the cooler I; the air outlet of the cooler I is communicated with the air inlet of the high-pressure air storage tank; the air outlet of the high-pressure air storage tank is communicated with the air inlet of the reheater; the air outlet of the reheater is communicated with the air inlet of the expander; the air outlet of the expander is communicated with the air inlet of the cooler II; and the air outlet of the cooler II is communicated with the air inlet of the low-pressure air storage tank. By the system, low-grade energy can be recycled in the circulation process, and the circulation efficiency of the compressed carbon dioxide energy storage system is improved.
Description
Technical Field
The invention relates to a carbon dioxide energy storage system, in particular to an energy recovery type supercritical compressed carbon dioxide energy storage system and a constant pressure energy release method.
Background
The compressed carbon dioxide energy storage technology is a novel physical energy storage technology, has the advantages of high energy storage density, long operation life, compact system equipment and the like, and has good development and application prospects. However, in the discharging process of the compressed carbon dioxide energy storage system, the pressure in the high-pressure gas storage tank is gradually reduced along with continuous discharge of high-pressure gas, so that the operation conditions of key parts such as a turbine are continuously changed, even the system is unstable in operation, and the circulation efficiency is difficult to improve. In addition, a large amount of low-grade heat is carried by working media at the positions of an air outlet of the expander, an inlet of the cold accumulation tank and the like, and the working media are cooled by natural cooling water or air cooling directly, so that the working media are difficult to utilize, and the system efficiency is greatly reduced.
Therefore, in order to solve the above-mentioned technical problems, a new technical means is needed.
Disclosure of Invention
In view of the above, the present invention aims to provide an energy recovery type supercritical compressed carbon dioxide energy storage system and a constant pressure energy release method, which can solve the problem that the pressure in a high pressure gas storage tank is reduced along with the discharge of gas in the process of supercritical compressed carbon dioxide energy storage and cyclic discharge, and can realize the recovery and utilization of low-grade energy in the cyclic process.
The invention provides an energy recovery type supercritical compressed carbon dioxide energy storage system which comprises a low-pressure gas storage tank, a high-pressure gas storage tank, a compressor, a cooler I, a cooler II, a low-grade heat recovery tank, a heat storage tank, a cold storage tank, a reheater and an expander, wherein the low-pressure gas storage tank is connected with the high-pressure gas storage tank;
the air outlet of the low-pressure air storage tank is communicated with the air inlet of the compressor, and the low-pressure air storage tank is used for storing low-pressure carbon dioxide;
the air outlet of the compressor is communicated with the air inlet of the cooler I, and the compressor is used for compressing low-pressure carbon dioxide into high-pressure carbon dioxide;
The air outlet of the cooler I is communicated with the air inlet of the high-pressure air storage tank through an air flow channel, the air flow channel between the air outlet of the cooler I and the air inlet of the high-pressure air storage tank passes through the low-grade heat recovery tank, and the cooler I is used for cooling the compressed carbon dioxide and absorbing compression heat generated by the compressor;
The liquid outlet I of the low-grade heat recovery tank is communicated with the liquid inlet of the high-pressure gas storage tank through a liquid flow channel; the liquid inlet I of the low-grade heat recovery tank is communicated with the liquid outlet of the high-pressure gas storage tank through a liquid flow channel; the low-grade heat recovery tank is used for absorbing low-grade heat carried by the carbon dioxide output by the cooler I, providing low-grade heat for the high-pressure gas storage tank through a heat exchange medium, heating the carbon dioxide in the high-pressure gas storage tank to be in a supercritical state, and keeping the pressure of the carbon dioxide in the high-pressure gas storage tank constant in the gas release process;
The air outlet of the high-pressure air storage tank is communicated with the air inlet of the reheater, and the high-pressure air storage tank is used for storing high-pressure carbon dioxide;
The air outlet of the reheater is communicated with the air inlet of the expander, and the reheater is used for heating supercritical carbon dioxide to change the carbon dioxide in the reheater into a high-temperature and high-pressure state;
The air outlet of the expander is communicated with the air inlet of the cooler II, and the expander is used for enabling the carbon dioxide to perform constant-pressure expansion to apply work outwards;
the air outlet of the cooler II is communicated with the air inlet of the low-pressure air storage tank, and the cooler II is used for cooling the expanded carbon dioxide;
The liquid inlet of the cooler II is communicated with the liquid outlet II of the low-grade heat recovery tank through a liquid flow channel, the liquid outlet of the cooler II is communicated with the liquid inlet II of the low-grade heat recovery tank through a liquid flow channel, the liquid inlet of the cooler II is communicated with the liquid outlet of the cooler II through a liquid flow channel, and the cooler II is also used for absorbing low-grade heat carried by carbon dioxide in the cooler II;
The liquid inlet of the heat storage tank is communicated with the liquid outlet of the cooler I through a liquid flow channel, and the liquid outlet of the heat storage tank is communicated with the liquid inlet of the reheater through a liquid flow channel; the heat storage tank stores high-grade heat generated by the compressor through a heat exchange medium and provides the high-grade heat for the reheater through the heat exchange medium;
the liquid inlet of the cold accumulation tank is communicated with the liquid outlet of the reheater through a liquid flow channel, the communicated liquid flow channel passes through the low-grade heat recovery tank, and the liquid outlet of the cold accumulation tank is communicated with the liquid inlet of the cooler I through the liquid flow channel; the cold accumulation tank is used for storing the cooled heat exchange medium in the reheater and providing the cooled heat exchange medium for the cooler I; the low-grade heat recovery tank is also used for absorbing low-grade heat in the cooled heat exchange medium in the reheater.
Further, a liquid outlet of the high-pressure gas storage tank is arranged at one side of a gas inlet of the high-pressure gas storage tank; the liquid inlet of the high-pressure gas storage tank is arranged on one side of the gas outlet of the high-pressure gas storage tank.
Further, a liquid inlet of the high-pressure gas storage tank is communicated with a liquid outlet of the high-pressure gas storage tank by adopting a spiral liquid flow channel; the spiral liquid flow channel is used for enabling the heat exchange medium in the spiral liquid flow channel to realize countercurrent heat exchange with the carbon dioxide in the high-pressure air storage tank.
Further, the air inlet, the air outlet, the liquid inlet and the liquid outlet of the high-pressure air storage tank are all provided with valves.
Further, the device also comprises a temperature sensor and a pressure sensor;
The temperature sensor is arranged in the high-pressure air storage tank and is used for measuring the temperature in the high-pressure air storage tank and the temperature of the heat exchange medium in the spiral liquid flow channel;
The pressure sensor is arranged in the high-pressure air storage tank and is used for measuring the pressure in the high-pressure air storage tank.
Further, the device also comprises a pump body, a control box and a display screen;
the output port of the pump body is communicated with the liquid inlet of the high-pressure gas storage tank and the liquid inlet of the cooler II, and the pump body is used for sucking the heat exchange medium in the low-grade heat recovery tank and inputting the heat exchange medium into a spiral liquid flow channel or a liquid flow channel of the cooler II;
The input end of the control box is connected with the output end of the temperature sensor and the output end of the pressure sensor, and the output end of the control box is connected with a valve of a liquid inlet of the high-pressure gas storage tank, a valve of a liquid outlet of the high-pressure gas storage tank and the output end of the pump body; the control box is used for controlling the pump body to extract the heat exchange medium in the low-grade heat recovery tank according to the temperature and the pressure in the high-pressure air storage tank and the temperature of the heat exchange medium, and controlling the inflow of the heat exchange medium by controlling the opening of a valve of a liquid inlet of the high-pressure air storage tank;
The input end of the display screen is connected with the output end of the temperature sensor and the output end of the pressure sensor and is used for displaying the temperature in the high-pressure air storage tank, the temperature of the heat exchange medium in the spiral liquid flow channel and the pressure in the high-pressure air storage tank.
Further, drain outlets are formed in the bottoms of the high-pressure air storage tank and the low-pressure air storage tank; the drain outlet of the high-pressure air storage tank and the drain outlet of the low-pressure air storage tank are both provided with valves, and the drain outlet of the high-pressure air storage tank and the drain outlet of the low-pressure air storage tank are used for discharging impurity in the tank.
Correspondingly, the invention also provides a constant-pressure energy release method based on the energy recovery type supercritical compressed carbon dioxide energy storage system, which comprises the following steps of:
S1, inputting low-pressure carbon dioxide into a compressor by a low-pressure gas storage tank, and compressing the low-pressure carbon dioxide to a high-temperature high-pressure state;
S2, inputting carbon dioxide in a high-temperature and high-pressure state into a cooler I by a compressor, and inputting the carbon dioxide into a high-pressure air storage tank by the cooler I; the low-grade heat recovery tank is adopted to supply heat to the carbon dioxide in the high-pressure gas storage tank, so that the temperature of the carbon dioxide in the high-pressure gas storage tank is maintained within the range of [ A-B, A-C ];
wherein A represents the quasi-critical point temperature of the carbon dioxide in the high-pressure gas storage tank, [ A-B, A-C ] represents the temperature near the quasi-critical point of the carbon dioxide, A-C represents the upper limit value of the temperature near the quasi-critical point of the carbon dioxide, and A-B represents the lower limit value of the temperature near the quasi-critical point of the carbon dioxide;
S3, opening a valve at an air outlet of the high-pressure air storage tank, inputting carbon dioxide in the high-pressure air storage tank into the reheater, and controlling the flow Q of a heat exchange medium input spiral flow channel of the low-grade heat recovery tank by the control box to enable the real-time pressure of the dioxide in the high-pressure air storage tank to be equal to the preset pressure;
s4, the reheater receives carbon dioxide with constant pressure and heats the carbon dioxide, and the heated carbon dioxide is input into the expander to perform constant pressure energy release.
Further, in step S3, the flow Q is calculated by the following formula:
Wherein M represents the mass of carbon dioxide in the high-pressure air storage tank, h d represents the specific enthalpy of the carbon dioxide in the high-pressure air storage tank under the set pressure, h r represents the specific enthalpy of the carbon dioxide in the high-pressure air storage tank under the real-time pressure, C l represents the specific heat capacity of the heat exchange medium, t 1 and t 2 respectively represent the heating start time and the heating time of the low-grade heat recovery tank to the carbon dioxide with the temperature range of [ A-B, A-C ] to the designated pressure, and dT represents the changing temperature of the heat exchange medium in the spiral liquid flow channel in the high-pressure air storage tank.
Further, h d and h r are calculated by the following formula:
hr＝refpropm('h′,'T′,Tg,r,'P′,Pr,'CO2’)
hd＝refpropm('h′,'P′,Pd,'D′,ρ,'CO2’)
Wherein refpropm denotes a function, P d denotes a preset pressure of carbon dioxide in the high-pressure gas storage tank, P r denotes an actual pressure of carbon dioxide in the high-pressure gas storage tank, T g,r denotes a real-time temperature of carbon dioxide in the high-pressure gas storage tank, ρ denotes a density of carbon dioxide in the high-pressure gas storage tank, 'h', 'T', 'P', and 'D' respectively denote enthalpy, temperature, pressure, and density, and 'CO 2' denotes a working medium of carbon dioxide.
The invention has the beneficial effects that: the invention utilizes the characteristic that the density of the carbon dioxide is changed with the temperature in the vicinity of the quasi-critical point, recovers the low-grade heat of the compressed carbon dioxide energy storage system and is used for heating the high-pressure gas storage tank, and controls the temperature and the pressure of the carbon dioxide in the high-pressure gas storage tank to be in the vicinity of the quasi-critical point; when the pressure in the tank is reduced, the reduction value of the pressure of the air storage tank can be rapidly supplemented only by slightly increasing the heating temperature, so that the constant-voltage discharge process of the energy storage system is realized; meanwhile, low-grade energy in the system can be used for a heating process of the high-pressure air storage tank, so that the energy utilization rate of the system is improved.
Drawings
The invention is further described below with reference to the accompanying drawings and examples:
FIG. 1 is a schematic diagram of a system architecture of the present invention;
FIG. 2 is a schematic view of a portion of the structure of the high-pressure air tank of the present invention;
FIG. 3 is a graph showing supercritical carbon dioxide physical properties;
FIG. 4 is a flow chart of the present invention;
Reference numerals: 1-a low pressure air storage tank; a 2-compressor; 3-cooler I; 4-a low-grade heat recovery tank; 5-a high-pressure air storage tank; a 6-reheater; 7-an expander; 8-a cooler II; 9-a heat storage tank; 10-a cold accumulation tank; 11-a high-pressure gas storage tank body; 12-a high-pressure air storage tank air inlet; 13-a high-pressure air storage tank air outlet; 14-a sewage outlet of the high-pressure air storage tank; 15-a supporting seat; 16-a liquid inlet of the high-pressure gas storage tank; 17-a liquid outlet of the high-pressure gas storage tank; 18-spiral flow channels; 19-a temperature sensor; 20-a pressure sensor; 21-a control box; 22-display screen.
Detailed Description
The invention is further described below with reference to the accompanying drawings of the specification:
The invention provides an energy recovery type supercritical compressed carbon dioxide energy storage system, which is shown in figure 1, and comprises a low-pressure gas storage tank 1, a high-pressure gas storage tank 5, a compressor 2, a cooler I3, a cooler II 8, a low-grade heat recovery tank 4, a heat storage tank 9, a cold storage tank 10, a reheater 6 and an expander 7;
in fig. 1, a thick solid line represents a carbon dioxide passage, a thin solid line represents a liquid flow passage, a broken line represents heat exchange, and a thin broken line represents a flow passage of a heat exchange medium in the low-grade heat recovery tank 4;
the air outlet of the low-pressure air storage tank 1 is communicated with the air inlet of the compressor, and the low-pressure air storage tank 1 is used for storing low-pressure carbon dioxide;
The air outlet of the compressor 2 is communicated with the air inlet of the cooler I3, and the compressor 2 is used for compressing low-pressure carbon dioxide into high-pressure carbon dioxide; the compressor 2 compresses carbon dioxide by adopting surplus electric energy of a power grid or electric energy generated by renewable energy discharge; the electric energy is essentially stored in a pressure potential energy and heat energy mode, and the pressure potential energy and the heat energy respectively enter the high-pressure air storage tank 5 and the heat storage tank 9 for storage along with the output of the compressor;
The air outlet of the cooler I3 is communicated with the air inlet of the high-pressure air storage tank 5 through an air flow channel, the air flow channel between the air outlet of the cooler I3 and the air inlet of the high-pressure air storage tank 5 passes through the low-grade heat recovery tank 4, and the cooler I3 is used for cooling the compressed carbon dioxide and absorbing the compression heat generated by the compressor 2;
The liquid outlet I of the low-grade heat recovery tank 4 is communicated with the liquid inlet of the high-pressure gas storage tank 5 through a liquid flow channel; the liquid inlet I of the low-grade heat recovery tank 4 is communicated with the liquid outlet of the high-pressure gas storage tank 5 through a liquid flow channel; the low-grade heat recovery tank 4 is used for absorbing low-grade heat carried by carbon dioxide output by the cooler I3, providing low-grade heat for the high-pressure gas storage tank 5 through a heat exchange medium, heating the carbon dioxide in the high-pressure gas storage tank 5 to be in a supercritical state, and keeping the pressure of the carbon dioxide in the high-pressure gas storage tank 5 constant in the gas release process; the low-grade heat recovery technology is the prior art and is not described in detail herein;
the air outlet of the high-pressure air storage tank 5 is communicated with the air inlet of the reheater 6, and the high-pressure air storage tank 5 is used for storing high-pressure carbon dioxide;
The air outlet of the reheater 6 is communicated with the air inlet of the expander 7, and the reheater 6 is used for heating supercritical carbon dioxide so that the carbon dioxide in the reheater 6 is in a high-temperature and high-pressure state;
The air outlet of the expander 7 is communicated with the air inlet of the cooler II 8, and the expander 7 is used for enabling the carbon dioxide to perform constant-pressure expansion to work outwards;
The air outlet of the cooler II 8 is communicated with the air inlet of the low-pressure air storage tank 1, and the cooler II 8 is used for cooling the expanded carbon dioxide;
The liquid inlet of the cooler II 8 is communicated with the liquid outlet II of the low-grade heat recovery tank 4 through a liquid flow channel, the liquid outlet of the cooler II 8 is communicated with the liquid inlet II of the low-grade heat recovery tank 4 through a liquid flow channel, the liquid inlet of the cooler II 8 is communicated with the liquid outlet of the cooler II 8 through a liquid flow channel, and the low-grade heat recovery tank 4 is also used for absorbing low-grade heat carried by carbon dioxide in the cooler II 8 and is also used for absorbing the cooler II;
the liquid inlet of the heat storage tank 9 is communicated with the liquid outlet of the cooler I3 through a liquid flow channel, and the liquid outlet of the heat storage tank 9 is communicated with the liquid inlet of the reheater 6 through a liquid flow channel; the heat storage tank 9 stores high-grade heat generated by the compressor 2 through a heat exchange medium and provides the high-grade heat for the reheater 6 through the heat exchange medium;
The liquid inlet of the cold accumulation tank 10 is communicated with the liquid outlet of the reheater 6 through a liquid flow channel, the communicated liquid flow channel passes through the low-grade heat recovery tank 4, and the liquid outlet of the cold accumulation tank 10 is communicated with the liquid inlet of the cooler I3 through the liquid flow channel; the cold accumulation tank 10 is used for storing the cooled heat exchange medium in the reheater 6 and providing the cooled heat exchange medium for the cooler I3; the low-grade heat recovery tank 4 is also used for absorbing low-grade heat in the heat exchange medium cooled in the reheater 6.
The cooler I3 is internally provided with an air flow channel, the air flow channel of the cooler I3 is connected between an air inlet and an air outlet of the cooler I3, the air flow channel is used for circulating carbon dioxide, the cooler I3 is internally provided with a liquid flow channel, the liquid flow channel of the cooler I3 is connected between a liquid inlet and a liquid outlet, and the liquid flow channel is used for circulating a heat exchange medium; the rest of the structures in the cooler I3 adopt the existing structures, and are not described in detail herein; the cooler I3 contains a heat exchange medium, and when carbon dioxide carries compression heat and enters a gas flow channel in the cooler I3, the carbon dioxide exchanges heat with the heat exchange medium contained in the cooler I3, and the heat exchange medium in the cooler I3 exchanges heat with the heat exchange medium in the liquid flow channel, so that the compression heat generated by the compressor flows into the heat storage tank 9 along with the heat exchange medium in the liquid flow channel;
The inside of the reheater 6 is provided with an air flow channel, the air flow channel of the reheater 6 is connected between the air inlet and the air outlet of the reheater 6, the inside of the reheater 6 is also provided with a liquid flow channel, the liquid flow channel of the reheater 6 is connected between the liquid inlet and the liquid outlet of the reheater 6, and the reheater 6 is filled with heat exchange medium; when the heat exchange medium in the heat storage tank 9 flows into the reheater along with the liquid flow channel, the heat exchange medium in the liquid flow channel exchanges heat with the heat exchange medium in the reheater 6, and the heat exchange medium in the reheater 6 exchanges heat with carbon dioxide in the gas flow channel, so that heating of the carbon dioxide is realized, and the heat exchange medium absorbed with heat in the liquid flow channel passes through the low-grade heat recovery tank along with the liquid flow channel and enters the cold storage tank 10;
The cooler II 8 is internally provided with an air flow channel, the air flow channel of the cooler II 8 is connected between an air inlet and an air outlet of the cooler II 8, the cooler II 8 is internally provided with a liquid flow channel, and the liquid flow channel of the cooler II 8 is connected between a liquid inlet and a liquid outlet of the cooler II 8; and the cooler II 8 contains a heat exchange medium; the rest of the structures in the cooler II 8 adopt the existing structures, and are not described in detail herein; after the expanded carbon dioxide enters the airflow channel of the cooler II 8, the expanded carbon dioxide exchanges heat with the heat exchange medium in the cooler II 8, and the heat exchange medium in the cooler II 8 exchanges heat with the heat exchange medium in the flow channel, so that the low-grade heat of the expanded carbon dioxide is absorbed by the low-grade heat recovery tank;
Three low-grade heat sources are arranged in the low-grade heat recovery tank 4, the first is low-grade heat carried in carbon dioxide when the cooler I3 inputs carbon dioxide into the high-pressure gas storage tank 5, and the low-grade heat recovery tank 4 absorbs heat when an airflow channel passes through the low-grade heat recovery tank 4; the second is that when the reheater 6 inputs a heat exchange medium to the cold storage tank 10, the heat exchange medium output by the reheater 6 through a liquid flow channel carries low-grade heat, the liquid flow channel passes through the low-grade heat recovery tank 4, and at the part of the liquid flow channel passing through the low-grade heat recovery tank 4, the heat exchange medium in the liquid flow channel exchanges heat with the heat exchange medium in the low-grade heat recovery tank 4, and at this time, the low-grade heat recovery tank 4 absorbs the low-grade heat in the liquid flow channel; and thirdly, in the cooler II 8, a heat exchange medium in a liquid flow channel in the cooler II 8 exchanges heat with carbon dioxide in a gas flow channel in the cooler II 8, and the heat exchange medium absorbs low-grade heat carried in the carbon dioxide and is recycled to the low-grade heat recycling tank 4 through the liquid flow channel.
By the system, low-grade energy can be recycled in the circulation process, and the circulation efficiency of the compressed carbon dioxide energy storage system is improved.
The air inlet and the air outlet are carbon dioxide circulation ports, the air flow channel is a carbon dioxide circulation channel, and when gaseous carbon dioxide is converted into liquid, the gaseous carbon dioxide still flows in the air flow channel; the liquid inlet and the liquid outlet are the circulation ports of the heat exchange medium, and the liquid flow channel is the circulation channel of the heat exchange medium; the materials used for the airflow channel and the liquid flow channel have the property of good heat conducting performance; the heat exchange medium adopted by the invention is water or oil. The low-pressure air storage tank, the high-pressure air storage tank, the cooler, the reheater, the cold storage tank, the heat storage tank, the compressor and the expander which are adopted in the invention all adopt the existing devices, and the details are not repeated here.
In this embodiment, the liquid outlet of the high-pressure gas storage tank 5 is disposed at one side of the gas inlet of the high-pressure gas storage tank 5; the liquid inlet of the high-pressure gas storage tank 5 is arranged at one side of the gas outlet of the high-pressure gas storage tank 5; as shown in fig. 2, the support body in fig. 2 is for supporting a tank body 11 of a high-pressure gas storage tank;
The liquid inlet of the high-pressure gas storage tank 5 is communicated with the liquid outlet of the high-pressure gas storage tank 5 by adopting a spiral liquid flow channel 18; the upper and lower sides of the spiral flow channel 18 are attached to the inner wall of the high-pressure air storage tank 5, as shown in fig. 2, the spiral flow channel 18 is used for implementing countercurrent heat exchange between the heat exchange medium in the spiral flow channel and the carbon dioxide in the high-pressure air storage tank, the countercurrent heat exchange means that the high-temperature fluid and the low-temperature fluid flow in opposite directions in the heat exchanger, so that the high-temperature fluid can heat the low-temperature fluid, and heat transfer from the high-temperature fluid to the low-temperature fluid is implemented, that is, the heat exchange medium in the spiral flow channel and the carbon dioxide in the high-pressure air storage tank flow in opposite directions. The spiral liquid flow channel is adopted, so that the heat exchange efficiency can be improved and the space can be saved; and the countercurrent heat exchange can strengthen heat transfer, so that the temperature difference is uniformly distributed.
In this embodiment, the air inlet, the air outlet, the liquid inlet and the liquid outlet of the high-pressure air storage tank 5 are all provided with valves; valves can also be arranged at the other air outlets, the air inlets, the liquid outlets and the liquid inlets, and the valves are specifically arranged according to the requirements. In the invention, the valves of the liquid inlet and the liquid outlet of the high-pressure gas storage tank are controlled by the control box 21, and other valves can be controlled manually or automatically by adopting the existing automatic control valve.
In this embodiment, a temperature sensor 19 and a pressure sensor 20 are also included;
The temperature sensor 19 is arranged in the high-pressure air storage tank 5 and is used for measuring the temperature in the high-pressure air storage tank 5 and the temperature of the heat exchange medium in the pipe of the spiral flow channel 18;
The pressure sensor 20 is disposed in the high-pressure air storage tank 5, and is used for measuring the pressure in the high-pressure air storage tank 5.
In this embodiment, the device further comprises a pump body (not shown in the figure), a control box 21 and a display screen 22;
The output port of the pump body is communicated with the liquid inlet of the high-pressure gas storage tank 5 and the liquid inlet of the cooler II 8, and the pump body is used for sucking the heat exchange medium in the low-grade heat recovery tank 4 and inputting the heat exchange medium into the spiral liquid flow channel 18 or the liquid flow channel of the cooler II 8; the pump body is arranged according to the heat exchange medium, when the heat exchange medium is water, an existing water pump is adopted, and when the heat exchange medium is oil, an existing oil pump is adopted;
The input end of the control box 21 is connected with the output end of the temperature sensor 19 and the output end of the pressure sensor 20, and the output end of the control box 21 is connected with a valve of a liquid inlet of the high-pressure gas storage tank 5, a valve of a liquid outlet of the high-pressure gas storage tank 5 and the output end of the pump body; the control box 21 is used for controlling the pump body to pump the heat exchange medium in the low-grade heat recovery tank 4 according to the temperature and the pressure in the high-pressure air storage tank 5 and the temperature of the heat exchange medium, and controlling the inflow of the heat exchange medium by controlling the opening of a valve of a liquid inlet of the high-pressure air storage tank 5;
The input end of the display screen 22 is connected with the output end of the temperature sensor 19 and the output end of the pressure sensor 20, and is used for displaying the temperature in the high-pressure air storage tank 5, the temperature of the heat exchange medium in the pipe of the spiral liquid flow channel 18 and the pressure in the high-pressure air storage tank 5.
According to the invention, the control box calculates the flow of the heat exchange medium according to the pressure in the high-pressure gas storage tank, the critical pressure to be achieved, the temperature in the tank and the temperature in the heat exchange medium, so that the pressure in the high-pressure gas storage tank reaches the critical value; the required heat exchange medium flow is calculated according to the existing pressure, the temperature in the critical pressure tank required to be reached and the temperature in the heat exchange medium, which is not described in detail herein.
In this embodiment, drain outlets are provided at the bottoms of the high-pressure air storage tank 5 and the low-pressure air storage tank 1; the bottom provided with the drain outlet is the relative position, the position of the drain outlet is related to the placement position of the air storage tank, as shown in figure 2, when the high-pressure air storage tank is placed upside down, the drain outlet is positioned at the position shown in the figure, and when the low-pressure air storage tank is placed vertically, the drain outlet is arranged beside the air outlet I of the low-pressure air storage tank;
Valves are arranged at the drain outlet 14 of the high-pressure air storage tank 5 and the drain outlet (not shown in the figure) of the low-pressure air storage tank 1, the drain outlet of the high-pressure air storage tank 5 and the drain outlet of the low-pressure air storage tank 1 are used for discharging impurity in the tank, and the impurity refers to impurities carried by carbon dioxide or greasy dirt in the tank; when the carbon dioxide gas flows to the high-pressure gas storage tank 5, the gas inlet valve and the gas outlet valve of the high-pressure gas storage tank 5 are in a closed state, and at the moment, the low-pressure gas storage tank 1 is free of carbon dioxide gas, and the valve of the sewage outlet can be opened to discharge the impurity in the low-pressure gas storage tank 1; the high-pressure air storage tank 5 is similar, and the pollution discharge period is determined according to the actual use requirement. The impurity in the discharged gas storage tank can keep the cleaning of the gas storage tank, prolong the service life of equipment and improve the gas quality.
The carbon dioxide energy storage system provided by the invention comprises three processes:
the energy storage process comprises the following steps: the low-pressure gas storage tank inputs carbon dioxide into the compressor, and the compressor converts electric energy into pressure potential energy and heat energy which are respectively stored in the high-pressure gas storage tank and the heat storage tank;
energy release process: the high-pressure gas storage tank inputs the stored carbon dioxide into a reheater, and the reheater inputs the carbon dioxide into an expander to do work;
The recovery process comprises the following steps: the expander inputs the carbon dioxide with energy release completed into a cooler II, and the cooler II inputs the cooled carbon dioxide into a low-pressure air storage tank for storage.
Correspondingly, the invention also provides a constant-pressure energy release method based on the energy recovery type supercritical compressed carbon dioxide energy storage system, which comprises the following steps of:
S1, inputting low-pressure carbon dioxide into a compressor by a low-pressure gas storage tank, and compressing the low-pressure carbon dioxide to a high-temperature high-pressure state;
S2, inputting carbon dioxide in a high-temperature and high-pressure state into a cooler I by a compressor, and inputting the carbon dioxide into a high-pressure air storage tank by the cooler I; the low-grade heat recovery tank is adopted to supply heat to the carbon dioxide in the high-pressure gas storage tank, so that the temperature of the carbon dioxide in the high-pressure gas storage tank is maintained within the range of [ A-B, A-C ];
wherein A represents the quasi-critical point temperature of the carbon dioxide in the high-pressure gas storage tank, [ A-B, A-C ] represents the temperature near the quasi-critical point of the carbon dioxide, A-C represents the upper limit value of the temperature near the quasi-critical point of the carbon dioxide, and A-B represents the lower limit value of the temperature near the quasi-critical point of the carbon dioxide;
S3, opening a valve at an air outlet of the high-pressure air storage tank, inputting carbon dioxide in the high-pressure air storage tank into the reheater, and controlling the flow Q of a heat exchange medium input spiral flow channel of the low-grade heat recovery tank by the control box to enable the real-time pressure of the dioxide in the high-pressure air storage tank to be equal to the preset pressure;
S4, the reheater receives carbon dioxide with constant pressure and heats the carbon dioxide, and the heated carbon dioxide is input into the expander to perform constant pressure energy release;
The constant-pressure energy release means that the carbon dioxide does work in the expansion machine at constant pressure, and the constant-pressure work refers to work on the outside under the condition that the system pressure is constant, namely, the high-pressure gas storage tank inputs the carbon dioxide with constant pressure, and the expansion machine receives the carbon dioxide with constant pressure and does work on the outside. Through the steps, the carbon dioxide in the high-pressure air storage tank can be heated by utilizing the temperature sensitivity characteristic of the carbon dioxide near the quasi-critical point, constant-pressure air release is ensured, and constant-pressure energy release is further realized.
In the embodiment, in step S1, the low-pressure gas storage tank inputs low-pressure carbon dioxide into the compressor, and compresses the low-pressure carbon dioxide to a high-temperature and high-pressure state; the compressor compresses carbon dioxide by adopting surplus electric energy of a power grid or electric energy generated by renewable energy discharge;
The high temperature and high pressure state refers to the fact that the temperature and pressure of the carbon dioxide exceed the critical temperature and critical pressure of the carbon dioxide in the supercritical state, and the supercritical is the existing concept and is not described herein;
Low pressure means well below the critical pressure of carbon dioxide (7.38 MPa); for example, 0.1MPa, a specific low pressure standard is determined on demand, but must be met below the critical pressure;
High pressure means exceeding the critical pressure of carbon dioxide; high temperature refers to temperatures in excess of 200 degrees celsius.
In the embodiment, in step S2, the compressor inputs carbon dioxide in a high-temperature and high-pressure state into the cooler i, and then inputs the carbon dioxide into the high-pressure gas storage tank through the cooler i; the low-grade heat recovery tank is adopted to supply heat to the carbon dioxide in the high-pressure gas storage tank, so that the temperature of the carbon dioxide in the high-pressure gas storage tank is maintained within the range of [ A-B, A-C ];
Wherein A represents the quasi-critical point temperature of the carbon dioxide in the high-pressure gas storage tank, [ A-B, A-C ] represents the temperature near the quasi-critical point of the carbon dioxide, A-C represents the upper limit value of the temperature near the quasi-critical point of the carbon dioxide, and A-B represents the lower limit value of the temperature near the quasi-critical point of the carbon dioxide; taking 4 as C and taking 8 as B, taking 8MPa as an example, and taking the quasi-critical point temperature of the carbon dioxide at 8MPa as about 308K, wherein the temperature near the quasi-critical point of the carbon dioxide is [300K,304K ]; the quasi-critical state area refers to an area, near the quasi-critical point, of which the physical properties change with temperature severely; the quasi-critical point is the point where the specific heat capacity will appear as a peak value in the process of heating the supercritical fluid in an isobaric manner, and the point where the peak value appears is the quasi-critical point;
Because the carbon dioxide working medium is in a quasi-critical state area, the physical properties of the carbon dioxide working medium can be changed drastically, and the physical parameters of the carbon dioxide working medium are particularly sensitive to temperature change. As shown in fig. 3, taking a pressure of 8MPa as an example, the pseudo-critical temperature of carbon dioxide is 308K, the density thereof decreases drastically with a slight increase in temperature around 308K, and has a larger expansion coefficient around 308K; this means that only a slight temperature rise is required to achieve a substantial pressure increase at this time; according to the characteristic, the recovered low-grade heat is used for heating the high-pressure air storage tank, so that the temperature in the tank is controlled to be near the quasi-critical temperature, and when the pressure in the tank is reduced, the reduced value of the pressure of the air storage tank can be rapidly supplemented by only slightly increasing the heating temperature, so that the constant-voltage discharge process of the energy storage system is realized.
In the embodiment, in step S3, a valve at an air outlet of a high-pressure air storage tank is opened, carbon dioxide in the high-pressure air storage tank is input into a reheater, and a control box controls a heat exchange medium of a low-grade heat recovery tank to be input into a flow Q of a spiral liquid flow channel, so that the real-time pressure of the dioxide in the high-pressure air storage tank is equal to a preset pressure;
The flow Q is calculated by the following formula:
Wherein M represents the mass of carbon dioxide in the high-pressure air storage tank, h d represents the specific enthalpy of the carbon dioxide in the high-pressure air storage tank under the set pressure, h r represents the specific enthalpy of the carbon dioxide in the high-pressure air storage tank under the real-time pressure, C l represents the specific heat capacity of the heat exchange medium, t 1 and t 2 respectively represent the heating start time and the heating time of the low-grade heat recovery tank to the carbon dioxide with the temperature range of [ A-B, A-C ] to the designated pressure, and dT represents the changing temperature of the heat exchange medium in the spiral liquid flow channel in the high-pressure air storage tank.
In this embodiment, h d and h r are calculated by the following formula:
hr＝refpropm(‘h’，‘T’，Tg,r,'P',Pr,'CO2’)
hd＝refpropm('h','P',Pd,'D',ρ,'CO2’)
Wherein refpropm denotes a function, which is not described in detail herein, for the prior art, P d denotes a preset pressure of carbon dioxide in the high-pressure gas storage tank, P r denotes an actual pressure of carbon dioxide in the high-pressure gas storage tank, T g,r denotes a real-time temperature of carbon dioxide in the high-pressure gas storage tank, ρ denotes a density of carbon dioxide in the high-pressure gas storage tank, h ', ' T ', ' P ', and ' D ' respectively denote enthalpy, temperature, pressure, and density, and ' CO 2 ' denotes a working medium of carbon dioxide.
In the embodiment, in step S4, the reheater receives carbon dioxide with constant pressure and heats the carbon dioxide, and the heated carbon dioxide is input into the expander to perform constant pressure energy release; although the heat storage tank is used for reheating the carbon dioxide with constant pressure in the reheater, the pressure of the output carbon dioxide is changed to a certain extent, and the along-path pressure loss exists in the output process, the change of the pressure value is small and can be ignored;
through the steps, the carbon dioxide can be ensured to stably apply work to the expander, so that constant-pressure energy release is realized.
The invention also includes: the output end of the expander is connected with a generator, and when the carbon dioxide works at constant pressure in the expander, the expander drives the generator to work so as to generate stable electric energy.
The invention also includes: and (3) inputting the carbon dioxide subjected to work application of the expansion machine into a cooler II, cooling the carbon dioxide by adopting a heat exchange medium in a low-grade heat recovery tank, and inputting the cooled carbon dioxide into a low-pressure air storage tank to complete one cycle. By the method, resources can be saved, and the environment is protected.
Finally, it is noted that the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications and equivalents may be made thereto without departing from the spirit and scope of the technical solution of the present invention, which is intended to be covered by the scope of the claims of the present invention.
Claims (10)
1. An energy recovery type supercritical compressed carbon dioxide energy storage system, which is characterized in that: the low-grade heat recovery device comprises a low-pressure air storage tank (1), a high-pressure air storage tank (5), a compressor (2), a cooler I (3), a cooler II (8), a low-grade heat recovery tank (4), a heat storage tank (9), a cold storage tank (10), a reheater (6) and an expander (7);
The air outlet of the low-pressure air storage tank (1) is communicated with the air inlet of the compressor (2), and the low-pressure air storage tank (1) is used for storing low-pressure carbon dioxide;
the air outlet of the compressor (2) is communicated with the air inlet of the cooler I (3), and the compressor (2) is used for compressing low-pressure carbon dioxide into high-pressure carbon dioxide;
The air outlet of the cooler I (3) is communicated with the air inlet of the high-pressure air storage tank (5) through an air flow channel, the air flow channel between the air outlet of the cooler I (3) and the air inlet of the high-pressure air storage tank (5) passes through the low-grade heat recovery tank (4), and the cooler I (3) is used for cooling the compressed carbon dioxide and absorbing the compression heat generated by the compressor (2);
The liquid outlet I of the low-grade heat recovery tank (4) is communicated with the liquid inlet of the high-pressure gas storage tank (5) through a liquid flow channel; the liquid inlet I of the low-grade heat recovery tank (4) is communicated with the liquid outlet of the high-pressure gas storage tank (5) through a liquid flow channel; the low-grade heat recovery tank (4) is used for absorbing low-grade heat carried by carbon dioxide output by the cooler I (3), providing low-grade heat for the high-pressure gas storage tank (5) through a heat exchange medium, heating the carbon dioxide in the high-pressure gas storage tank (5) to be in a supercritical state, and keeping the pressure of the carbon dioxide in the high-pressure gas storage tank (5) constant in the gas release process;
the air outlet of the high-pressure air storage tank (5) is communicated with the air inlet of the reheater (6), and the high-pressure air storage tank (5) is used for storing high-pressure carbon dioxide;
the air outlet of the reheater (6) is communicated with the air inlet of the expander (7), and the reheater (6) is used for heating supercritical carbon dioxide to change the carbon dioxide in the reheater (6) into a high-temperature and high-pressure state;
the air outlet of the expander (7) is communicated with the air inlet of the cooler II (8), and the expander (7) is used for enabling the carbon dioxide to perform work outwards through constant-pressure expansion;
The air outlet of the cooler II (8) is communicated with the air inlet of the low-pressure air storage tank (1), and the cooler II (8) is used for cooling the expanded carbon dioxide;
the liquid inlet of the cooler II (8) is communicated with the liquid outlet II of the low-grade heat recovery tank (4) through a liquid flow channel, the liquid outlet of the cooler II (8) is communicated with the liquid inlet II of the low-grade heat recovery tank (4) through a liquid flow channel, the liquid inlet of the cooler II (8) is communicated with the liquid outlet of the cooler II (8) through a liquid flow channel, and the cooler II is further used for absorbing low-grade heat carried by carbon dioxide in the cooler II (8) and the low-grade heat recovery tank (4);
The liquid inlet of the heat storage tank (9) is communicated with the liquid outlet of the cooler I (3) through a liquid flow channel, and the liquid outlet of the heat storage tank (9) is communicated with the liquid inlet of the reheater (6) through a liquid flow channel; the heat storage tank (9) stores high-grade heat generated by the compressor (2) through a heat exchange medium and provides the high-grade heat for the reheater (6) through the heat exchange medium;
the liquid inlet of the cold accumulation tank (10) is communicated with the liquid outlet of the reheater (6) through a liquid flow channel, the communicated liquid flow channel passes through the low-grade heat recovery tank (4), and the liquid outlet of the cold accumulation tank (10) is communicated with the liquid inlet of the cooler I (3) through the liquid flow channel; the cold accumulation tank (10) is used for storing the cooled heat exchange medium in the reheater (6) and providing the cooled heat exchange medium for the cooler I (3); the low-grade heat recovery tank (4) is also used for absorbing low-grade heat in the heat exchange medium cooled in the reheater (6).
2. The energy recovery type supercritical compressed carbon dioxide energy storage system according to claim 1, wherein: the liquid outlet of the high-pressure gas storage tank (5) is arranged at one side of the gas inlet of the high-pressure gas storage tank (5); the liquid inlet of the high-pressure gas storage tank (5) is arranged on one side of the gas outlet of the high-pressure gas storage tank (5).
3. The energy recovery type supercritical compressed carbon dioxide energy storage system according to claim 2, wherein: the liquid inlet of the high-pressure gas storage tank (5) is communicated with the liquid outlet of the high-pressure gas storage tank (5) by adopting a spiral liquid flow channel; the spiral liquid flow channel is used for enabling the heat exchange medium in the spiral liquid flow channel to realize countercurrent heat exchange with the carbon dioxide in the high-pressure air storage tank (5).
4. The energy recovery type supercritical compressed carbon dioxide energy storage system according to claim 3, wherein: the air inlet, the air outlet, the liquid inlet and the liquid outlet of the high-pressure air storage tank (5) are all provided with valves.
5. The energy recovery type supercritical compressed carbon dioxide energy storage system according to claim 4, wherein: the device also comprises a temperature sensor and a pressure sensor;
the temperature sensor is arranged in the high-pressure air storage tank (5) and is used for measuring the temperature in the high-pressure air storage tank (5) and the temperature of the heat exchange medium in the spiral liquid flow channel;
The pressure sensor is arranged in the high-pressure air storage tank (5) and is used for measuring the pressure in the high-pressure air storage tank (5).
6. The energy recovery type supercritical compressed carbon dioxide energy storage system according to claim 5, wherein: the device also comprises a pump body, a control box and a display screen;
The output port of the pump body is communicated with the liquid inlet of the high-pressure gas storage tank (5) and the liquid inlet of the cooler II (8), and the pump body is used for sucking a heat exchange medium in the low-grade heat recovery tank (4) and inputting the heat exchange medium into a spiral liquid flow channel (18) or a liquid flow channel of the cooler II (8);
The input end of the control box is connected with the output end of the temperature sensor and the output end of the pressure sensor, and the output end of the control box is connected with a valve of a liquid inlet of the high-pressure gas storage tank (5), a valve of a liquid outlet of the high-pressure gas storage tank (5) and the output end of the pump body; the control box is used for controlling the pump body to extract the heat exchange medium in the low-grade heat recovery tank (4) according to the temperature and the pressure in the high-pressure air storage tank (5) and the temperature of the heat exchange medium, and controlling the inflow of the heat exchange medium by controlling the opening of a valve of a liquid inlet of the high-pressure air storage tank (5);
The input end of the display screen is connected with the output end of the temperature sensor and the output end of the pressure sensor and is used for displaying the temperature in the high-pressure air storage tank (5), the temperature of the heat exchange medium in the spiral liquid flow channel and the pressure in the high-pressure air storage tank (5).
7. The energy recovery type supercritical compressed carbon dioxide energy storage system according to claim 1, wherein: the bottoms of the high-pressure air storage tank (5) and the low-pressure air storage tank (1) are provided with drain outlets; the drain outlet of the high-pressure air storage tank (5) and the drain outlet of the low-pressure air storage tank (1) are both provided with valves, and the drain outlet of the high-pressure air storage tank (5) and the drain outlet of the low-pressure air storage tank (1) are used for discharging impurity in the tank.
8. A constant pressure energy release method based on the energy recovery type supercritical compressed carbon dioxide energy storage system according to any one of claims 1 to 7, characterized in that: the method comprises the following steps:
S1, inputting low-pressure carbon dioxide into a compressor by a low-pressure gas storage tank, and compressing the low-pressure carbon dioxide to a high-temperature high-pressure state;
S2, inputting carbon dioxide in a high-temperature and high-pressure state into a cooler I by a compressor, and inputting the carbon dioxide into a high-pressure air storage tank by the cooler I; the low-grade heat recovery tank is adopted to supply heat to the carbon dioxide in the high-pressure gas storage tank, so that the temperature of the carbon dioxide in the high-pressure gas storage tank is maintained within the range of [ A-B, A-C ];
wherein A represents the quasi-critical point temperature of the carbon dioxide in the high-pressure gas storage tank, [ A-B, A-C ] represents the temperature near the quasi-critical point of the carbon dioxide, A-C represents the upper limit value of the temperature near the quasi-critical point of the carbon dioxide, and A-B represents the lower limit value of the temperature near the quasi-critical point of the carbon dioxide;
S3, opening a valve at an air outlet of the high-pressure air storage tank, inputting carbon dioxide in the high-pressure air storage tank into the reheater, and controlling the flow Q of a heat exchange medium input spiral flow channel of the low-grade heat recovery tank by the control box to enable the real-time pressure of the dioxide in the high-pressure air storage tank to be equal to the preset pressure;
s4, the reheater receives carbon dioxide with constant pressure and heats the carbon dioxide, and the heated carbon dioxide is input into the expander to perform constant pressure energy release.
9. The constant pressure energy release method according to claim 8, wherein: in step S3, the flow Q is calculated by the following formula:
Wherein M represents the mass of carbon dioxide in the high-pressure air storage tank, h d represents the specific enthalpy of the carbon dioxide in the high-pressure air storage tank under the set pressure, h r represents the specific enthalpy of the carbon dioxide in the high-pressure air storage tank under the real-time pressure, C l represents the specific heat capacity of the heat exchange medium, t 1 and t 2 respectively represent the heating start time and the heating time of the low-grade heat recovery tank to the carbon dioxide with the temperature range of [ A-B, A-C ] to the designated pressure, and dT represents the changing temperature of the heat exchange medium in the spiral liquid flow channel in the high-pressure air storage tank.
10. The constant pressure energy release method according to claim 9, wherein: h d and h r are calculated by the following formula:
hr＝refpropm('h','T',Tg,r,'P',Pr,'CO2’)
hd＝refpropm('h','P',Pd,'D',ρ,'CO2’)
Wherein refpropm denotes a function, P d denotes a preset pressure of carbon dioxide in the high-pressure gas storage tank, P r denotes an actual pressure of carbon dioxide in the high-pressure gas storage tank, T g,r denotes a real-time temperature of carbon dioxide in the high-pressure gas storage tank, ρ denotes a density of carbon dioxide in the high-pressure gas storage tank, 'h', 'T', 'P', and 'D' respectively denote enthalpy, temperature, pressure, and density, and 'CO 2' denotes a working medium of carbon dioxide.
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