CN216825546U - Carbon dioxide capture adsorption system based on solar drive and energy storage - Google Patents
Carbon dioxide capture adsorption system based on solar drive and energy storage Download PDFInfo
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- CN216825546U CN216825546U CN202220398581.9U CN202220398581U CN216825546U CN 216825546 U CN216825546 U CN 216825546U CN 202220398581 U CN202220398581 U CN 202220398581U CN 216825546 U CN216825546 U CN 216825546U
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Abstract
A carbon dioxide capturing and adsorbing system based on solar drive and energy storage comprises a flue gas pipeline, a first water cooler, a first compression and expansion integrated machine, a second water cooler and a second tail gas heat exchanger which are sequentially connected through pipelines, and a third water cooler and the first tail gas heat exchanger are connected through a compressor or the second compression and expansion integrated machine; the outlet flue gas of the first tail gas heat exchanger is respectively introduced into a first adsorber or a second adsorber through a gas-liquid separator, and the first adsorber or the second adsorber is connected with a vacuum pump or a third compression-expansion integrated machine; desorbing the carbon dioxide adsorbed by the first adsorber or the second adsorber in a vacuumizing mode, and introducing the desorbed carbon dioxide into a carbon dioxide gas pipeline through a fifth water cooler; the solar power generation device provides system operation electric energy, and the solar heat collector and the organic Rankine cycle device form a working medium driving cycle subsystem. The utility model discloses can reduce coal fired power plant flue gas entrapment carbon dioxide's energy consumption, improve economic nature.
Description
Technical Field
The utility model belongs to the technical field of coal fired power plant gas cleaning and greenhouse gas reduce discharging, concretely relates to carbon dioxide entrapment adsorption system based on solar drive and energy storage.
Background
In recent years, with the increasing extreme weather around the world, the problem of climate change has become more and more recognized, and one of the main factors causing climate change is greenhouse effect caused by artificial large amount of carbon dioxide emission. Among greenhouse gases causing global warming, carbon dioxide is one of its main components, and contributes to the greenhouse effect more than the sum of other greenhouse gases. Meanwhile, carbon dioxide as waste gas is a valuable carbon and oxygen resource, and the reserve of the carbon dioxide on the earth is several times more than the sum of natural gas, petroleum and coal. However, since measures for recovering carbon dioxide are disadvantageous, the amount of carbon dioxide recovered and reused every year is less than 1% of the emission amount, which causes atmospheric pollution and greenhouse effect, and wastes valuable resources.
Therefore, the research on the development and utilization of carbon dioxide has gradually become a popular topic of scientific and technological development departments of various countries, and has become an important direction for the future socioeconomic development. In China, the absolute amount of carbon dioxide gas discharged from the flue gas of a coal-fired power plant accounts for about half of the total amount of carbon dioxide gas discharged in China, and is the most main emission source of greenhouse gas in China. Therefore, the emission reduction of the carbon oxide gas in the flue gas of the coal-fired power plant is one of the bottlenecks of the future sustainable development of coal-fired power generation in China and is not slow at all.
The flue gas of the coal-fired power plant is characterized in that the partial pressure of carbon dioxide is very low, the using amount of an absorbent in the separation process is very large, and the heat consumption of the regeneration of the absorbent is also very large. The heat source form of the existing flue gas carbon dioxide capture device for the power plant mostly takes steam extraction, flue gas waste heat and the like of the power plant as a regenerative heat source, so that the power generation efficiency of the power plant is reduced. Therefore, reducing the energy consumption of carbon dioxide capture and improving the process economy are the main problems of carbon dioxide capture in coal-fired power plants.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to the problem among the above-mentioned prior art, provide a carbon dioxide entrapment adsorption system based on solar drive and energy storage, realize the entrapment process of carbon dioxide and renewable energy utilization and the high integration of energy storage, have the characteristics that the operating process is simple, elasticity is big, environment friendly and the utilization efficiency of the energy is high, the operation is stable, safety.
In order to achieve the above object, the present invention provides the following technical solutions:
a carbon dioxide capture adsorption system based on solar drive and energy storage comprises a solar power generation device, a solar heat collector and an organic Rankine cycle device, wherein a flue gas pipeline is sequentially connected with a first water cooler, a first compression and expansion integrated machine, a second water cooler and a second tail gas heat exchanger through pipelines, and is connected with a third water cooler and the first tail gas heat exchanger through a compressor or a second compression and expansion integrated machine; the outlet flue gas of the first tail gas heat exchanger is respectively introduced into a first adsorber or a second adsorber through a gas-liquid separator, the first adsorber and the second adsorber are connected through a pipeline to form an adsorption subsystem, and the first adsorber or the second adsorber is further connected with a vacuum pump or a third compression-expansion integrated machine; desorbing the carbon dioxide adsorbed by the first adsorber or the second adsorber in a vacuumizing mode, and introducing the desorbed carbon dioxide into a carbon dioxide gas pipeline through a fifth water cooler; the solar power generation device provides system operation electric energy, and the solar heat collector and the organic Rankine cycle device form a working medium driving cycle subsystem.
Preferably, a lower channel of the first adsorber or the second adsorber is sequentially connected with a compression end of a vacuum pump or a third compression-expansion all-in-one machine, a fifth water cooler and a carbon dioxide gas pipeline, and an upper channel of the first adsorber or the second adsorber is sequentially connected with an expansion end of the first compression-expansion all-in-one machine, a shell side of the first tail gas heat exchanger and a tail gas pipeline; and the fifth water cooler, the shell pass of the second tail gas heat exchanger and each liquid outlet of the gas-liquid separator are connected with a water pipeline through pipelines.
Preferably, the utility model discloses carbon dioxide entrapment adsorption system still includes first conduction oil storage tank and second conduction oil storage tank, solar collector's conduction oil entry and the exit linkage of first conduction oil storage tank, solar collector's conduction oil export in proper order with the entry linkage of second conduction oil storage tank, organic rankine cycle device's conduction oil passageway and first conduction oil storage tank.
Preferably, the temperature of the heat conducting oil of the solar heat collector is 80-160 ℃;
the pressure of the organic working medium provided by the organic Rankine cycle device is 1.5-4.0 MPa.
Preferably, an outlet of an organic working medium channel of the organic Rankine cycle device is respectively connected with inlets of expansion ends of the second compression-expansion all-in-one machine and the third compression-expansion all-in-one machine through pipelines, and an outlet of the expansion end of the organic working medium channel of the organic Rankine cycle device is sequentially connected with inlets of organic working medium channels of the fourth water cooler, the booster pump and the organic Rankine cycle device through pipelines.
Preferably, the carbon dioxide capturing and adsorbing system of the present invention further comprises a plurality of control valves, among the control valves, a first control valve is disposed on a pipeline between the second tail gas heat exchanger and the compressor, a second control valve is disposed on a pipeline between the second tail gas heat exchanger and the second compression and expansion integrated machine, a third control valve is disposed on a pipeline between the compressor and the third water cooler, and a fourth control valve is disposed on a pipeline between the second compression and expansion integrated machine and the third water cooler; a fifth control valve is arranged on a pipeline between the vacuum pump and the fifth water cooler, a sixth control valve is arranged on a pipeline between the third compression-expansion all-in-one machine and the fifth water cooler, a seventh control valve is arranged on a pipeline between the first adsorber or the second adsorber and the vacuum pump, and an eighth control valve is arranged on a pipeline between the first adsorber or the second adsorber and the third compression-expansion all-in-one machine; a ninth control valve and a tenth control valve are respectively arranged on a pipeline of the gas-liquid separator, which is connected with the first adsorber and the second adsorber, and an eleventh control valve and a twelfth control valve are respectively arranged on a pipeline of the first adsorber and the second adsorber, which is connected with the vacuum pump or the third compression-expansion all-in-one machine; a thirteenth control valve and a fourteenth control valve are respectively arranged on a pipeline of the first adsorber and the second adsorber which are connected with the first compression-expansion all-in-one machine; and a fifteenth control valve is arranged on a pipeline between the second heat conduction oil storage tank and the organic Rankine cycle device, and a sixteenth control valve is arranged on a pipeline between the first heat conduction oil storage tank and the solar heat collector.
Preferably, the vacuum pump and the compressor are connected with the solar power generation device through cables.
Preferably, the inlet flue gas temperature of the compression end of the first compression-expansion all-in-one machine is 30-50 ℃, and the outlet flue gas pressure of the first compression-expansion all-in-one machine is 0.15-0.3 MPa; the temperature of the compression end of the second compression-expansion all-in-one machine or the inlet flue gas of the compressor is 5-40 ℃, and the pressure of the outlet flue gas of the second compression-expansion all-in-one machine is 0.5-1.5 MPa; the inlet pressure of the third compression-expansion all-in-one machine is 0.002 MPa-0.005 MPa, and the pressure of the outlet carbon dioxide is normal pressure.
Preferably, the first adsorber or the second adsorber has a pressure of 0.5MPa to 1.5MPa at the time of adsorption operation and a temperature of-30 ℃ to 30 ℃, and has a pressure of 0.005MPa to 0.020MPa at the time of desorption operation and a temperature of-25 ℃ to 35 ℃.
A control method of a carbon dioxide capturing and adsorbing system based on solar drive and energy storage utilizes the on-off of a control valve to execute the following processes:
in the sunshine time, the solar power generation device and the solar heat collector are in the power generation and heating working states; the flue gas sequentially enters a first water cooler, a compression end of a first compression and expansion integrated machine, a second water cooler, a second tail gas heat exchanger tube pass, a compressor, a third water cooler and a first tail gas heat exchanger tube pass, is subjected to gradual pressurization and cooling, then enters a first adsorber or a second adsorber, and carbon dioxide in the flue gas is adsorbed under the conditions of high pressure and low temperature until adsorption saturation; the high-pressure low-temperature tail gas without carbon dioxide enters an expansion end of the first compression-expansion all-in-one machine, is expanded, decompressed and cooled, and then sequentially enters shell passes of the first tail gas heat exchanger and the second tail gas heat exchanger to provide cold energy for the first tail gas heat exchanger and the second tail gas heat exchanger, and the normal-temperature and normal-pressure tail gas after reheating and heating is sent out of a battery limit zone; vacuumizing the first adsorber or the second adsorber by using a vacuum pump, desorbing the adsorbed carbon dioxide from the first adsorber or the second adsorber, and regenerating the first adsorber or the second adsorber; the desorbed carbon dioxide enters a fifth water cooler, and all or part of the cooled carbon dioxide gas at normal temperature and normal pressure is sent out of the battery limits; normal-temperature heat conducting oil from the first heat conducting oil storage tank enters the solar heat collector, and after the normal-temperature heat conducting oil is heated, high-temperature heat conducting oil enters the second heat conducting oil storage tank to be stored, so that the storage capacity meets the heat utilization requirement of the organic Rankine cycle device during night operation;
in the non-sunshine time, the solar power generation device and the solar heat collector stop working; closing the compressor and the vacuum pump, and respectively replacing the daytime working compressor and the vacuum pump with a compression end of a second compression-expansion all-in-one machine and a compression end of a third compression-expansion all-in-one machine; meanwhile, sending the high-temperature heat conduction oil in the second heat conduction oil storage tank to an inlet of a heat conduction oil channel of the organic Rankine cycle device; in the organic Rankine cycle device, the heat of high-temperature heat conduction oil is absorbed by the organic working medium, the heat is returned to the first heat conduction oil storage tank again to be stored after the temperature of the heat conduction oil is reduced, and the storage capacity can meet the total amount of the heat conduction oil flowing out of the organic Rankine cycle device at night; in the organic Rankine cycle device, the organic working medium absorbing heat is evaporated at high temperature to form high-pressure organic working medium gas, the high-pressure organic working medium gas respectively enters the compression end of the second compression and expansion all-in-one machine and the expansion end of the third compression and expansion all-in-one machine, the organic working medium gas after expansion, pressure reduction and temperature reduction enters the fourth water cooler, is condensed into organic working medium liquid by circulating cooling water, is pressurized by a pressure pump and returns to the inlet of the organic working medium channel of the organic Rankine cycle device again.
Compared with the prior art, the utility model discloses following beneficial effect has at least:
the utility model discloses can realize the all-weather uninterrupted continuous stable operation of power plant's flue gas carbon dioxide entrapment, the flue gas of power plant is through pressure boost step by step and cooling back, lets in first adsorber or second adsorber respectively, under the microthermal condition of high pressure, carbon dioxide in the flue gas is adsorbed and gets off, until adsorbing saturation, by the vacuum pump to first adsorber or second adsorber evacuation, will be desorbed from first adsorber or second adsorber by adsorbed carbon dioxide, the normal atmospheric temperature and pressure carbon dioxide gas after the cooling is whole or the part sends out the boundary area. The first adsorber and the second adsorber are connected through a pipeline to form an adsorption subsystem, when the first adsorber is in an adsorption state, the second adsorber is in a regeneration state, when the first adsorber is saturated in adsorption, the first adsorber is switched to the regeneration state, and the second adsorber is correspondingly switched to the adsorption state, so that the operation is repeated in cycles and switched mutually, and the continuous and stable operation of the system is realized. The solar power generation device and the solar heat collector achieve the purpose of storing solar energy in the daytime, and the storage capacity of the solar power generation device can meet the heat utilization requirement of the organic Rankine cycle device in night operation. The utility model has the characteristics of operation process is simple, elasticity is big, environment friendly and energy efficiency is high, can effectively reduce coal fired power plant flue gas entrapment carbon dioxide's energy consumption, improves the economic nature of process, can realize with renewable energy solar energy the effect of the comprehensive replacement power plant steam consumption.
Drawings
FIG. 1 is a schematic structural view of a carbon dioxide capturing and adsorbing system based on solar drive and energy storage;
in the drawings: 1-a solar power generation device; 2-a solar heat collector; 3-fifth water cooler; 4-a first compression-expansion all-in-one machine; 5-a second water cooler; 6-a first tail gas heat exchanger; 7-a second tail gas heat exchanger; 8-a compressor; 9-a third water cooler; 10-a second compression-expansion all-in-one machine; 11-a vacuum pump; 12-a third compression-expansion all-in-one machine; 13-a gas-liquid separator; 14-a first adsorber; 15-a second adsorber; 16-an organic rankine cycle device; 17-a first conduction oil storage tank; 18-a second conduction oil storage tank; 19-a first water cooler; 20-a fourth water cooler; 21-a pressure pump; 30-a first control valve; 31-a second control valve; 32-a third control valve; 33-a fourth control valve; 34-a fifth control valve; 35-a sixth control valve; 36-a seventh control valve; 37-an eighth control valve; 38-a ninth control valve; 39-tenth control valve; 40-an eleventh control valve; 41-twelfth control valve; 42-a thirteenth control valve; 43-a fourteenth control valve; 44-a fifteenth control valve; 45-sixteenth control valve; 50-a flue gas duct; 51-a carbon dioxide gas pipeline; 52-a water pipeline; 53-tail gas pipeline.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples.
Referring to fig. 1, the carbon dioxide capturing and adsorbing system based on solar driving and energy storage of the present invention includes a solar power generation device 1, a solar heat collector 2, an organic rankine cycle device 16, a compression and expansion integrated machine, a compressor 8, a water cooler, a tail gas heat exchanger, an adsorber, a vacuum pump 11, a pressure pump 21, a heat transfer oil storage tank, a gas-liquid separator 13, and a control valve group.
The flue gas pipeline 50 is sequentially connected with a first water cooler 19, a first compression and expansion integrated machine 4, a second water cooler 5 and a second tail gas heat exchanger 7 through pipelines, and is connected with a third water cooler 9 and a first tail gas heat exchanger 6 through a compressor 8 or a second compression and expansion integrated machine 10; the flue gas at the outlet of the first tail gas heat exchanger 6 is respectively introduced into a first adsorber 14 or a second adsorber 15 through a gas-liquid separator 13, the first adsorber 14 and the second adsorber 15 are connected through a pipeline to form an adsorption subsystem, the first adsorber 14 or the second adsorber 15 is further connected with a vacuum pump 11 or a third compression-expansion integrated machine 12, the carbon dioxide adsorbed by the first adsorber 14 or the second adsorber 15 is desorbed through a vacuum pumping mode, and the desorbed carbon dioxide is introduced into a carbon dioxide gas pipeline 51 through a fifth water cooler 3. The solar power generation device 1 provides system operation electric energy, and the vacuum pump 11 and the compressor 8 are connected with the solar power generation device 1 through cables. The solar heat collector 2 and the organic Rankine cycle device 16 form a working medium driving cycle subsystem. In this embodiment, the lower channel of the first adsorber 14 or the second adsorber 15 is sequentially connected to the compression end of the vacuum pump 11 or the third compression-expansion all-in-one machine 12, the fifth water cooler 3, and the carbon dioxide gas pipeline 51, and the upper channel thereof is sequentially connected to the expansion end of the first compression-expansion all-in-one machine 4, the shell side of the first tail gas heat exchanger 6, the second tail gas heat exchanger 7, and the tail gas pipeline 53; and the fifth water cooler 3, the shell pass of the second water cooler 5, the shell pass of the second tail gas heat exchanger 7 and each liquid outlet of the gas-liquid separator 13 are connected with a water pipeline 52 through pipelines. The heat conduction oil storage tank comprises a first heat conduction oil storage tank 17 and a second heat conduction oil storage tank 18, a heat conduction oil inlet of the solar heat collector 2 is connected with an outlet of the first heat conduction oil storage tank 17, and a heat conduction oil outlet of the solar heat collector 2 is sequentially connected with the second heat conduction oil storage tank 18, a heat conduction oil channel of the organic Rankine cycle device 16 and an inlet of the first heat conduction oil storage tank 17. In this embodiment, an outlet of an organic working medium channel of the organic rankine cycle device 16 is connected to inlets of expansion ends of the second compression-expansion all-in-one machine 10 and the third compression-expansion all-in-one machine 12 through pipelines, and an outlet of an expansion end of the organic working medium channel is connected to inlets of an organic working medium channel of the organic rankine cycle device 16, a fourth water cooler 20 and a pressure pump 21 through pipelines in sequence. In this embodiment, the control valve group includes a plurality of control valves, wherein a first control valve 30 is arranged on a pipeline between the second tail gas heat exchanger 7 and the compressor 8, a second control valve 31 is arranged on a pipeline between the second tail gas heat exchanger 7 and the second integrated compression-expansion machine 10, a third control valve 32 is arranged on a pipeline between the compressor 8 and the third water cooler 9, and a fourth control valve 33 is arranged on a pipeline between the second integrated compression-expansion machine 10 and the third water cooler 9; a fifth control valve 34 is arranged on a pipeline between the vacuum pump 11 and the fifth water cooler 3, a sixth control valve 35 is arranged on a pipeline between the third compression-expansion all-in-one machine 12 and the fifth water cooler 3, a seventh control valve 36 is arranged on a pipeline between the first adsorber 14 or the second adsorber 15 and the vacuum pump 11, and an eighth control valve 37 is arranged on a pipeline between the first adsorber 14 or the second adsorber 15 and the third compression-expansion all-in-one machine 12; a ninth control valve 38 and a tenth control valve 39 are respectively arranged on a pipeline of the gas-liquid separator 13 connecting the first adsorber 14 and the second adsorber 15, and an eleventh control valve 40 and a twelfth control valve 41 are respectively arranged on a pipeline of the first adsorber 14 and the second adsorber 15 connecting the vacuum pump 11 or the third compression-expansion all-in-one machine 12; a thirteenth control valve 42 and a fourteenth control valve 43 are respectively arranged on a pipeline of the first adsorber 14 and the second adsorber 15 connected with the first compression-expansion all-in-one machine 4; a fifteenth control valve 44 is arranged on a pipeline between the second heat conduction oil storage tank 18 and the organic Rankine cycle device 16, and a sixteenth control valve 45 is arranged on a pipeline between the first heat conduction oil storage tank 17 and the solar heat collector 2.
In one embodiment, the temperature of the heat transfer oil of the solar heat collector 2 is 80-160 ℃; the pressure of the organic working medium provided by the organic Rankine cycle device 16 is 1.5MPa to 4.0 MPa. The inlet flue gas temperature of the compression end of the first compression-expansion all-in-one machine 4 is 30-50 ℃, and the outlet flue gas pressure of the first compression-expansion all-in-one machine 4 is 0.15-0.3 MPa; the temperature of the compression end of the second compression-expansion all-in-one machine 10 or the inlet flue gas of the compressor 8 is 5-40 ℃, and the outlet flue gas pressure of the second compression-expansion all-in-one machine 10 is 0.5-1.5 MPa; the inlet pressure of the third compression-expansion all-in-one machine 12 is 0.002 MPa-0.005 MPa, and the pressure of the outlet carbon dioxide is normal pressure. The pressure of the first adsorber 14 or the second adsorber 15 during adsorption operation is 0.5MPa to 1.5MPa, the temperature is-30 ℃ to 30 ℃, the pressure during desorption operation is 0.005MPa to 0.020MPa, and the temperature is-25 ℃ to 35 ℃.
The utility model discloses carbon dioxide entrapment adsorption system's control method based on solar drive and energy storage utilizes the break-make of manipulating control flap to carry out following process:
in the sunshine hours (namely, the daytime), the solar power generation device 1 and the solar heat collector 2 are in the power generation and heating working states; the flue gas sequentially enters a first water cooler 19, a compression end of a first compression and expansion integrated machine 4, a second water cooler 5, a tube pass of a second tail gas heat exchanger 7, a compressor 8, a third water cooler 9 and a tube pass of a first tail gas heat exchanger 6, is subjected to gradual pressurization and cooling, then enters a first adsorber 14 or a second adsorber 15, and carbon dioxide in the flue gas is adsorbed under the conditions of high pressure and low temperature until adsorption saturation; the high-pressure low-temperature tail gas without carbon dioxide enters an expansion end of the first compression-expansion all-in-one machine 4, is expanded, decompressed and cooled, then sequentially enters shell passes of a first tail gas heat exchanger 6 and a second tail gas heat exchanger 7 to provide cooling capacity for the tail gas, and the normal-temperature and normal-pressure tail gas after reheating and warming is sent out of a battery limit; the first adsorber 14 or the second adsorber 15 is evacuated by the vacuum pump 11 to desorb the adsorbed carbon dioxide from the first adsorber 14 or the second adsorber 15, thereby regenerating the first adsorber 14 or the second adsorber 15; the desorbed carbon dioxide enters a fifth water cooler 3, and all or part of the cooled carbon dioxide gas at normal temperature and normal pressure is sent out of the battery limits; the normal-temperature heat conducting oil from the first heat conducting oil storage tank 17 enters the solar heat collector 2, and after being heated, the high-temperature heat conducting oil enters the second heat conducting oil storage tank 18 to be stored, so that the reserve volume meets the heat utilization requirement of the organic Rankine cycle device 16 during night operation;
in the non-sunshine period (i.e. at night), the solar power generation device 1 and the solar heat collector 2 stop working; closing the compressor 8 and the vacuum pump 11, and respectively replacing the daytime working compressor 8 and the vacuum pump 11 by a compression end of a second compression-expansion all-in-one machine 10 and a compression end of a third compression-expansion all-in-one machine 12; meanwhile, the high-temperature heat conduction oil in the second heat conduction oil storage tank 18 is sent to the inlet of a heat conduction oil channel of the organic Rankine cycle device 16; in the organic Rankine cycle device 16, the heat of the high-temperature heat conduction oil is absorbed by the organic working medium, the heat is returned to the first heat conduction oil storage tank 17 again to be stored after the temperature of the heat conduction oil is reduced, and the storage capacity can meet the total amount of the heat conduction oil flowing out of the organic Rankine cycle device 16 at night; in the organic Rankine cycle device 16, the organic working medium absorbing heat is evaporated at high temperature to form high-pressure organic working medium gas, the high-pressure organic working medium gas respectively enters inlets of a compression end of the second compression and expansion all-in-one machine 10 and an expansion end of the third compression and expansion all-in-one machine 12, the organic working medium gas after expansion, decompression and temperature reduction enters the fourth water cooler 20, is condensed into organic working medium liquid by circulating cooling water, is pressurized by the pressure pump 21, and returns to an organic working medium channel inlet of the organic Rankine cycle device 16 again.
The solar power generation device 1 of the utility model can generate power in the daytime and meet the power consumption requirement of the compressor 8 and the vacuum pump 11 in the daytime; the solar heat collector 2 can meet the heat demand of the organic Rankine cycle device 16 at night (namely, no sunshine). The utility model discloses the memory space of first conduction oil storage tank 17 in the system can satisfy the needs of the 16 operation at night of organic rankine cycle device, and the memory space of second conduction oil storage tank 18 can satisfy the needs of 2 day operations of solar collector.
In the above control process, when the first adsorber 14 is in the adsorption state, the second adsorber 15 is in the regeneration state; when the first adsorber 14 becomes saturated, it can be switched to the regeneration state by means of the control valve block, and the second adsorber 15 is correspondingly switched to the adsorption state. The operation is switched repeatedly and mutually, and the continuous and stable operation of the system is realized.
Meanwhile, in the above process, the water from the second water cooler 5, the shell pass of the first water cooler 19, the shell pass of the second tail gas heat exchanger 7 and the liquid discharge ports at the bottom of the gas-liquid separator 13 are combined together, and are connected with the water pipeline 52 through pipelines and sent out of the boundary area.
The utility model discloses an all-weather uninterrupted operation and operation process are simple, elasticity is big, environment friendly and the high flue gas carbon dioxide entrapment system of power plant of energy efficiency reach the effect with renewable energy solar energy comprehensively replaces power plant's steam consumption.
The present invention will be described in more detail with reference to specific examples.
Example 1:
the temperature of the flue gas of a certain power plant is 61 ℃, the pressure is 0.105MPa, and the flow is 200000Nm3/hr, wherein the content of carbon dioxide is 11.19%.
During daytime operation, the solar power generation device 1 and the solar heat collector 2 are in normal power generation and heating working states; meanwhile, except for the ninth to fourteenth control valves 38 to 43, the first, third, fifth, seventh and sixteenth control valves 30, 32, 34, 36 and 45 are kept open, and the second, fourth, sixth, eighth and fifteenth control valves 31, 33, 35, 37 and 44 are kept closed.
The flue gas of the power plant with the normal pressure firstly enters a first water cooler 19 to be cooled to 35 ℃, and then sequentially enters a compression end of a first compression and expansion all-in-one machine 4, a second water cooler 5 and a tube pass of a second tail gas heat exchanger 7, the pressure of the flue gas is increased to 0.196MPa, the temperature of the flue gas is reduced to 28.09 ℃, and then sequentially enters a compressor 8, a third water cooler 9 and a tube pass of a first tail gas heat exchanger 6, the pressure of the flue gas is increased to 0.50MPa, and the temperature of the flue gas is reduced to 5.0 ℃. Then, the high-pressure low-temperature flue gas enters the first adsorber 14 or the second adsorber 15, and carbon dioxide in the flue gas is adsorbed until the adsorption is saturated; the high-pressure low-temperature tail gas without carbon dioxide enters an expansion end of the first compression-expansion integrated machine 4, after expansion, pressure reduction and temperature reduction, the low-temperature normal-pressure tail gas sequentially enters shell passes of a first tail gas heat exchanger 6 and a second tail gas heat exchanger 7 to provide cooling capacity for the tail gas, and the normal-temperature normal-pressure tail gas after reheating and temperature rise is sent out of a battery limit; the first adsorber 14 or the second adsorber 15 reaching the saturation state is vacuumized by the vacuum pump 11, so that the adsorbed carbon dioxide is desorbed and regenerated, the suction pressure of the vacuum pump 11 is 0.010MPa, the temperature is-5.54 ℃, the carbon dioxide enters the fifth water cooler 3, and the cooled carbon dioxide gas at normal temperature and normal pressure is sent out of a boundary area; the normal temperature heat conducting oil from the first heat conducting oil storage tank 17 enters the solar heat collector and is heated to 150 ℃, and the high temperature heat conducting oil enters the second heat conducting oil storage tank 18 and is stored, so that the purpose of storing solar energy in the daytime is achieved.
During night operation, the solar power generation device 1 and the solar thermal collector 2 are both stopped, and the second control valve 31, the fourth control valve 33, the sixth control valve 35, the eighth control valve 37, the ninth control valve 38, and the fifteenth control valve 44 are kept open, and the first control valve 30, the third control valve 32, the fifth control valve 34, the seventh control valve 36, and the sixteenth control valve 45 are kept closed, except for the ninth control valve 38 to the fourteenth control valve 43.
For this reason, the compressor 8 and the vacuum pump 11 need to be shut down, and the compression end of the second integrated compression-expansion machine 10 and the compression end of the third integrated compression-expansion machine 12 are respectively used for replacing the compressor 8 and the vacuum pump 11 which work in the daytime; meanwhile, high-temperature heat transfer oil stored in the second heat transfer oil storage tank 18 in the daytime is sent to a heat transfer oil channel inlet of the organic Rankine cycle device 2; in the organic Rankine cycle device 2, the heat of the high-temperature heat conduction oil is absorbed by the organic working medium, and after the temperature of the organic working medium is reduced, the organic working medium returns to the first heat conduction oil storage tank 17 again and is stored; meanwhile, the organic working medium absorbing heat is evaporated at high temperature to form high-pressure organic working medium gas, the pressure of the organic working medium gas is 3.0MPa, the high-pressure organic working medium gas enters the inlets of the expansion ends of the second compression-expansion all-in-one machine 10 and the third compression-expansion all-in-one machine 12 through the outlet of the organic working medium channel of the organic Rankine cycle device 2 and is used for driving the compression ends of the second compression-expansion all-in-one machine and the third compression-expansion all-in-one machine to work, the organic working medium gas after being expanded, decompressed and cooled enters the fourth water cooler 20, is condensed into organic working medium liquid by circulating cooling water, is pressurized by a pressurizing pump and returns to the inlet of the organic working medium channel of the organic Rankine cycle device 2 again, and an organic Rankine cycle process is completed.
When the first adsorber 14 is in the adsorption state, the ninth control valve 38 and the thirteenth control valve 42 are opened, and the tenth control valve 39 and the fourteenth control valve 43 are closed; at this time, the second adsorber 15 is in the regeneration state, the eleventh control valve 40 is closed, and the twelfth control valve 41 is opened. When the first adsorber 14 is saturated, the eleventh control valve 40 is opened, the twelfth control valve 41 is closed, and the regeneration state is switched to; at this time, the second adsorber 15 is switched to the adsorption state, and the tenth control valve 39 and the fourteenth control valve 43 are opened, and the ninth control valve 38 and the thirteenth control valve 42 are closed. The operation is repeated in such a way, and the continuous and stable operation of the flue gas carbon dioxide capture system is realized by switching operation.
Meanwhile, in the above process, the water from the fifth water cooler 3, the shell pass of the first water cooler 5, the shell pass of the second tail gas heat exchanger 7 and the water from each liquid discharge port at the bottom of the gas-liquid separator 13 are combined together and are collectively sent out of the boundary area.
The removal rate of the flue gas carbon dioxide is 91%, the power consumption of the compression end of the compressor 8 or the second compression-expansion all-in-one machine 10 is 6752.6kW, and the power consumption of the compression end of the vacuum pump 11 or the third compression-expansion all-in-one machine 12 is 2048.1 kW. In summary, in example 1, 1Nm is separated and recovered from the flue gas of the power plant3The power or electricity consumption of the carbon dioxide gas is 0.4322 kW.
Example 2:
in this embodiment, the temperature of the inlet flue gas at the compression end of the first compression-expansion integrated machine 4 is 40 ℃, and the pressure of the outlet flue gas is 0.199 MPa; the temperature of the inlet flue gas of the compression end or the compressor of the second compression-expansion integrated machine 10 is 26.07 ℃, and the pressure of the outlet flue gas, namely the adsorption operation pressure, is 0.60 Mpa; the inlet pressure of the expansion and contraction end of the third compression and expansion integrated machine 12, namely the desorption operation pressure, is 0.010 MPa; the adsorption operation temperature was 0 ℃ and the desorption operation temperature was 0.48 ℃. The remaining conditions were the same as in example 1.
In the process, the removal rate of the carbon dioxide in the flue gas is 96%, the power consumption of the compression end of the compressor 8 or the second compression-expansion all-in-one machine 10 is 8075.9kW, and the power consumption of the compression end of the vacuum pump 11 or the third compression-expansion all-in-one machine 12 is 2125.3 kW. In summary, 1Nm is separated and recovered from the flue gas of the power plant3The power or electricity consumption of the carbon dioxide gas is 0.5010 kW.
Example 3:
in this embodiment, the temperature of the inlet flue gas at the compression end of the first compression-expansion integrated machine 4 is 50 ℃, and the pressure of the outlet flue gas is 0.205 MPa; the temperature of the inlet flue gas of the compression end or the compressor of the second compression-expansion integrated machine 10 is 22.64 ℃, and the pressure of the outlet flue gas, namely the adsorption operation pressure, is 0.60 Mpa; the inlet pressure of the expansion and contraction end of the third compression and expansion integrated machine 12, namely the desorption operation pressure, is 0.005 MPa; the adsorption operation temperature was 10 ℃ and the desorption operation temperature was 10.61 ℃. The remaining conditions were the same as in example 1.
In the process, the removal rate of the carbon dioxide in the flue gas is 95%, the power consumption of the compression end of the compressor 8 or the second compression-expansion all-in-one machine 10 is 7708.6kW, and the power consumption of the compression end of the vacuum pump 11 or the third compression-expansion all-in-one machine 12 is 3047.6 kW. In summary, 1Nm is separated and recovered from the flue gas of the power plant3The power or electricity consumption of the carbon dioxide gas is 0.5282 kW.
The utility model discloses utilize clean energy solar energy to realize the task of hot carbon dioxide emission reduction, utilize the entrapment process of carbon dioxide and the highly integrated of renewable energy utilization and storage, have easy operation simultaneously, characteristics such as load adjustment elasticity is big, safe and reliable can improve the economic nature of power plant flue gas carbon dioxide entrapment greatly, can use in the engineering, for coal fired power plant flue gas purification and greenhouse gas emission reduction device technical field, provide a new optimization solution system and technological method.
The above-mentioned embodiments are only preferred embodiments of the present invention, and it should be understood by those skilled in the art that the technical solution of the present invention can be modified and replaced easily without departing from the spirit and principle of the present invention, and the modified and replaced embodiments also fall within the protection scope of the appended claims.
Claims (9)
1. A carbon dioxide capturing and adsorbing system based on solar energy driving and energy storage is characterized by comprising a solar power generation device (1), a solar heat collector (2) and an organic Rankine cycle device (16), wherein a flue gas pipeline (50) is sequentially connected with a first water cooler (19), a first compression and expansion integrated machine (4), a second water cooler (5) and a second tail gas heat exchanger (7) through pipelines, and is connected with a third water cooler (9) and a first tail gas heat exchanger (6) through a compressor (8) or a second compression and expansion integrated machine (10); the flue gas at the outlet of the first tail gas heat exchanger (6) is respectively introduced into a first adsorber (14) or a second adsorber (15) through a gas-liquid separator (13), the first adsorber (14) and the second adsorber (15) are connected through a pipeline to form an adsorption subsystem, and the first adsorber (14) or the second adsorber (15) is further connected with a vacuum pump (11) or a third compression-expansion integrated machine (12); desorbing the carbon dioxide adsorbed by the first adsorber (14) or the second adsorber (15) in a vacuumizing mode, and introducing the desorbed carbon dioxide into a carbon dioxide gas pipeline (51) through a fifth water cooler (3); the solar power generation device (1) provides system operation electric energy, and the solar heat collector (2) and the organic Rankine cycle device (16) form a working medium driving cycle subsystem.
2. The carbon dioxide capturing and adsorbing system based on solar energy driving and energy storage is characterized in that the lower channel of the first adsorber (14) or the second adsorber (15) is sequentially connected with the compression end of a vacuum pump (11) or a third compression-expansion all-in-one machine (12), a fifth water cooler (3) and a carbon dioxide gas pipeline (51), and the upper channel of the first adsorber is sequentially connected with the expansion end of the first compression-expansion all-in-one machine (4), the first tail gas heat exchanger (6), the shell side of the second tail gas heat exchanger (7) and a tail gas pipeline (53); and the fifth water cooler (3), the shell pass of the second water cooler (5), the shell pass of the second tail gas heat exchanger (7) and each liquid outlet of the gas-liquid separator (13) are connected with a water pipeline (52) through pipelines.
3. The carbon dioxide capture and adsorption system based on solar energy driving and energy storage is characterized by further comprising a first conduction oil storage tank (17) and a second conduction oil storage tank (18), wherein a conduction oil inlet of the solar heat collector (2) is connected with an outlet of the first conduction oil storage tank (17), and a conduction oil outlet of the solar heat collector (2) is sequentially connected with the second conduction oil storage tank (18), a conduction oil channel of the organic Rankine cycle device (16) and an inlet of the first conduction oil storage tank (17).
4. The solar-powered and energy-storage-based carbon dioxide capture adsorption system of claim 3,
the temperature of the heat conducting oil of the solar heat collector (2) is 80-160 ℃;
the pressure of the organic working medium provided by the organic Rankine cycle device (16) is 1.5-4.0 MPa.
5. The carbon dioxide capture and adsorption system based on solar energy driving and energy storage is characterized in that an outlet of an organic working medium channel of the organic Rankine cycle device (16) is respectively connected with inlets of expansion ends of the second compression-expansion all-in-one machine (10) and the third compression-expansion all-in-one machine (12) through pipelines, and an outlet of an expansion end of the organic working medium channel of the organic Rankine cycle device (16) is sequentially connected with inlets of organic working medium channels of a fourth water cooler (20), a booster pump (21) and the organic Rankine cycle device (16) through pipelines.
6. The carbon dioxide capturing and adsorbing system based on solar energy driving and energy storage as claimed in claim 5, further comprising a plurality of control valves, wherein a first control valve (30) is arranged on a pipeline between the second tail gas heat exchanger (7) and the compressor (8), a second control valve (31) is arranged on a pipeline between the second tail gas heat exchanger (7) and the second compression-expansion all-in-one machine (10), a third control valve (32) is arranged on a pipeline between the compressor (8) and the third water cooler (9), and a fourth control valve (33) is arranged on a pipeline between the second compression-expansion all-in-one machine (10) and the third water cooler (9);
a fifth control valve (34) is arranged on a pipeline between the vacuum pump (11) and the fifth water cooler (3), a sixth control valve (35) is arranged on a pipeline between the third compression-expansion all-in-one machine (12) and the fifth water cooler (3), a seventh control valve (36) is arranged on a pipeline between the first adsorber (14) or the second adsorber (15) and the vacuum pump (11), and an eighth control valve (37) is arranged on a pipeline between the first adsorber (14) or the second adsorber (15) and the third compression-expansion all-in-one machine (12);
a ninth control valve (38) and a tenth control valve (39) are respectively arranged on a pipeline of the gas-liquid separator (13) connecting the first adsorber (14) and the second adsorber (15), and an eleventh control valve (40) and a twelfth control valve (41) are respectively arranged on a pipeline of the first adsorber (14) and the second adsorber (15) connecting the vacuum pump (11) or the third compression-expansion integrated machine (12);
a thirteenth control valve (42) and a fourteenth control valve (43) are respectively arranged on a pipeline of the first compression-expansion all-in-one machine (4) connected with the first adsorber (14) and the second adsorber (15);
a fifteenth control valve (44) is arranged on a pipeline between the second heat conduction oil storage tank (18) and the organic Rankine cycle device (16), and a sixteenth control valve (45) is arranged on a pipeline between the first heat conduction oil storage tank (17) and the solar heat collector (2).
7. The solar-driven and energy-stored carbon dioxide capture and adsorption system according to claim 1, wherein the vacuum pump (11) and the compressor (8) are connected with the solar power generation device (1) through cables.
8. The carbon dioxide capturing and adsorbing system based on solar drive and energy storage as claimed in claim 1, wherein the inlet flue gas temperature at the compression end of the first compression-expansion all-in-one machine (4) is 30-50 ℃, and the outlet flue gas pressure of the first compression-expansion all-in-one machine (4) is 0.15-0.3 MPa; the temperature of the compression end of the second compression-expansion all-in-one machine (10) or the inlet flue gas of the compressor (8) is 5-40 ℃, and the outlet flue gas pressure of the second compression-expansion all-in-one machine (10) is 0.5-1.5 MPa; the inlet pressure of the third compression-expansion integrated machine (12) is 0.002 MPa-0.005 MPa, and the pressure of the outlet carbon dioxide is normal pressure.
9. The carbon dioxide capture and adsorption system based on solar energy drive and energy storage according to claim 1, characterized in that the first adsorber (14) or the second adsorber (15) has a pressure of 0.5MPa to 1.5MPa and a temperature of-30 ℃ to 30 ℃ during adsorption operation, and a pressure of 0.005MPa to 0.020MPa and a temperature of-25 ℃ to 35 ℃ during desorption operation.
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