CN115615066A - Novel carbon emission reduction refrigeration cycle method - Google Patents
Novel carbon emission reduction refrigeration cycle method Download PDFInfo
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- 238000005057 refrigeration Methods 0.000 title claims abstract description 52
- 230000009467 reduction Effects 0.000 title claims abstract description 50
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 160
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 158
- 239000012071 phase Substances 0.000 claims abstract description 81
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 79
- 239000007788 liquid Substances 0.000 claims abstract description 77
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 76
- 239000012530 fluid Substances 0.000 claims abstract description 70
- 239000007791 liquid phase Substances 0.000 claims abstract description 41
- 239000003507 refrigerant Substances 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims description 198
- 239000012535 impurity Substances 0.000 claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 229910052757 nitrogen Inorganic materials 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
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- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 230000001133 acceleration Effects 0.000 claims description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 239000007792 gaseous phase Substances 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 230000009919 sequestration Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 description 8
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- 230000008569 process Effects 0.000 description 4
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- 230000007423 decrease Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B41/00—Fluid-circulation arrangements
- F25B41/40—Fluid line arrangements
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Abstract
The invention provides a novel carbon emission reduction refrigeration cycle method, which comprises the following steps of S1, connecting a first feeding hole of a cyclone separation device to a gas bottle group to receive gas in the gas bottle group, wherein the gas contains carbon dioxide; s2, condensing the gas by using the cyclone separation device to obtain a first two-phase fluid; s3, separating the first two-phase fluid by using a separation cavity of a cyclone separation device to obtain a liquid-phase refrigerant, wherein a liquid discharge port of the separation cavity of the cyclone separation device is connected to an inlet end of a heat load, and the liquid-phase refrigerant is subjected to heat exchange with the heat load to form a second two-phase fluid; s4, performing circulation treatment on the second two-phase fluid to obtain a circulation liquid, introducing the circulation liquid into the cyclone separation device by adopting a first guide pipe, and repeating the steps S2-S3. The novel carbon emission reduction refrigeration cycle method realizes the wide industrial application value of the natural refrigerant and the carbon emission reduction in the high energy consumption industry.
Description
Technical Field
The invention relates to the technical field of carbon emission reduction, in particular to a novel carbon emission reduction refrigeration cycle method.
Background
The carbon emission reduction technology which is most widely applied at present is carbon capture, utilization and storage (CCS), wherein the capture after combustion is most widely applied, and the capture after combustion mainly comprises an absorption separation method, an adsorption separation method, a membrane separation method and the like.
The cyclone separator is a separation device which is developed rapidly in recent years and is based on a cyclone separation technology, and realizes phase-to-phase separation by utilizing density difference between two phases or multiple phases under the action of centrifugal force. The cyclone separator is commonly used for liquid-liquid separation, solid-liquid separation, gas-solid separation, solid-solid separation, gas-liquid separation and gas-solid-liquid separation, but the gas-gas separation is rarely disclosed.
Disclosure of Invention
In view of the above, the invention provides a novel carbon emission reduction refrigeration cycle method.
In order to solve the technical problems, the invention adopts the following technical scheme:
the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention comprises the following steps:
s1, connecting a first feeding hole of a cyclone separation device to a gas bottle group to receive gas in the gas bottle group, wherein the gas contains carbon dioxide;
s2, condensing the gas by using the cyclone separation device to obtain a first two-phase fluid;
s3, separating the first two-phase fluid by using a separation cavity of a cyclone separation device to obtain a liquid-phase refrigerant, wherein a liquid discharge port of the separation cavity of the cyclone separation device is connected to an inlet end of a heat load, and the liquid-phase refrigerant is subjected to heat exchange with the heat load to form a second two-phase fluid;
s4, performing circulation treatment on the second two-phase fluid to obtain a circulation liquid, introducing the circulation liquid into the cyclone separation device by adopting a first guide pipe, and repeating the steps S2-S3.
Preferably, the step S1 includes:
s11, pressurizing the gas by using a first supercharger, and enabling the pressurized gas to sequentially pass through an ejector, a pipeline static mixer and a buffer;
s12, introducing the gas in the buffer into the cyclone separation device by adopting a second guide pipe;
arranging a pressure regulating valve and a pressure transmitter on the second flow guide pipe to regulate the pressure of the gas to 1.2-2.0 bar;
arranging a temperature transmitter on the second flow guide pipe to adjust the temperature of the gas to 25-40 ℃;
a flow transmitter is arranged on the second flow guide pipe to adjust the flow of the gas to 180 to 200m 3 /h。
Preferably, the step S2 includes:
s21, applying an initial velocity to the introduced gas by using a cylinder part of the cyclone separation device;
s22, accelerating the gas by adopting the cone part of the cyclone separation device.
Preferably, the step S22 includes:
s221, guiding the gas in the barrel part to a tapered section by adopting the flow guide cone of the cone part;
s222, accelerating the gas once by adopting the reducing section, and injecting the accelerated gas to an expanding section;
and S223, performing secondary acceleration on the gas after the primary acceleration by using the expansion section to obtain the liquid refrigerant.
Preferably, the gas further comprises an impurity gas, the impurity gas being one or more of nitrogen, hydrogen, oxygen or carbon monoxide.
Preferably, the cyclone separation device is further used for maintaining the gas phase state of the impurity gas.
Preferably, the step S2 further includes:
s23, connecting a liquid discharge cavity of a cyclone separation device of the cyclone separation device to a discharge hole of the cyclone separation device to receive the first two-phase fluid and the impurity gas;
s24, separating the first two-phase fluid and the impurity gas by adopting a liquid discharge cavity of the cyclone separation device;
s25, connecting one end of a diffuser to an upper exhaust port of a liquid discharge cavity of the cyclone separation device to receive the impurity gas, and pressurizing the impurity gas by using the diffuser;
and S26, communicating the other end of the diffuser with the outside to discharge the pressurized impurity gas.
Preferably, the step S3 includes:
and S31, connecting an air outlet of a separation cavity of the cyclone separation device to a second feed inlet of the cyclone separation device through a third guide pipe.
Preferably, the step S3 further includes:
s32, connecting a liquid outlet of a separation cavity of the cyclone separation device to a liquid storage tank by adopting a fourth guide pipe, and storing the liquid-phase refrigerant by adopting the liquid storage tank;
and S33, connecting the liquid pump to the liquid storage tank to receive the liquid-phase refrigerant, and pumping the liquid-phase refrigerant into the heat load by using the liquid pump.
Preferably, the step S4 includes:
s41, a fifth guide pipe is adopted to be connected with a condensation evaporator, the fifth guide pipe is also used for being connected to the outlet end of the heat load so as to receive the second two-phase fluid, and the condensation evaporator is used for condensing the second two-phase fluid;
s42, connecting a first end of a second booster to the outlet end of the condensing evaporator to receive the circulating liquid, and boosting the circulating liquid by using the second booster;
and S43, connecting the second end of the second supercharger to a third feeding port of the cyclone separation device by using the first guide pipe so as to guide the supercharged circulating liquid into the cyclone separation device.
The technical scheme of the invention at least has one of the following beneficial effects:
(1) According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the cyclone separation device is applied to the carbon capture technology, the carbon dioxide captured by carbon is treated by the cyclone separation device to obtain the liquid refrigerant, and the two-phase fluid applied to the refrigeration system is recycled through cycle treatment, so that carbon emission reduction in the high-energy-consumption industry is realized, and resource utilization is realized in a real sense.
(2) According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the cyclone separation device is utilized to carry out supersonic treatment on the carbon dioxide gas, so that the carbon dioxide gas is condensed into a liquid phase, and thus a first two-phase fluid is formed, and further, the liquid-phase carbon dioxide in the first two-phase fluid is used as a refrigerant, so that the wide industrial application value of a natural refrigerant is realized.
(3) According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the mixed gas mixed with carbon dioxide and collected by using a carbon capture technology is subjected to supersonic speed treatment by using the cyclone separation device, so that the carbon dioxide is firstly condensed and crystallized into liquid-phase carbon dioxide from the mixed gas, the separation of the carbon dioxide and the impurity gas in the mixed gas is realized, and the carbon emission reduction in the high-energy-consumption industry is further realized.
(4) According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the impurity gas is introduced into the cyclone separation device along with the carbon dioxide to play a role in pressurization, so that the condensation of the carbon dioxide in the cyclone separation device can be further promoted, and the yield of a liquid-phase refrigerant is improved.
(5) According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, parameters of gas/mixed gas before entering the cyclone separation device are adjusted by utilizing the pressure regulating valve, the pressure transmitter, the temperature transmitter and the flow transmitter on the second flow guide pipe, so that the yield of the liquid-phase refrigerant is improved.
(6) According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the separation cavity of the cyclone separation device is used for separating the gas-phase carbon dioxide in the first two-phase fluid, the third guide pipe is arranged at the air outlet of the separation cavity, and the other end of the third guide pipe is connected to the second feeding hole of the cyclone separation device, so that the gas-phase carbon dioxide escaping from the first two-phase fluid is guided into the second feeding hole of the cyclone separation device through the third guide pipe, and the yield of the liquid-phase refrigerant can be further improved.
Drawings
FIG. 1 is a schematic diagram of a simulation apparatus for a novel carbon emission reduction refrigeration cycle process;
FIG. 2 is a graph of the effect of different temperatures on carbon dioxide separation performance and refrigeration performance;
FIG. 3 is a graph of the effect of different pressures on carbon dioxide separation performance and refrigeration performance;
FIG. 4 is a graph of the effect of different components on carbon dioxide separation performance;
FIG. 5 is a graph of the effect of different components on the refrigeration performance of carbon dioxide;
FIG. 6 is a graph of the effect of the third draft tube on carbon dioxide separation performance.
Reference numerals
The other cylinder groups 110; CO2 2 A gas cylinder group 120; a first supercharger 130; an ejector 140; a pipeline static mixer 150; a buffer 160;
a second draft tube 200;
a cyclonic separating apparatus 300; a barrel portion 311; the tapered portion 321; the guide cone 321a; a tapered section 321b; an expansion section 321c; a drain chamber 320; a separation chamber 330; a diffuser 340; a third draft tube 350;
a liquid storage tank 410; a liquid pump 420; a thermal load 430; a condensing evaporator 440; a second supercharger 450; a fourth draft tube 460; a fifth draft tube 470;
the first draft tube 500.
Detailed Description
The following detailed description of the preferred embodiments of the present invention is provided to enable those skilled in the art to more readily understand the advantages and features of the present invention and to thereby define the scope of the invention more clearly.
The novel carbon emission reduction refrigeration cycle method according to the embodiment of the invention is specifically described below with reference to the attached drawing 1.
The novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention comprises the following steps:
s1, connecting a first feeding hole of a cyclone separation device 300 to a gas bottle group to receive gas in the gas bottle group, wherein the gas contains carbon dioxide; s2, condensing the gas by using a cyclone separation device 300 to obtain a first two-phase fluid; s3, separating the first two-phase fluid by using the separation cavity 330 of the cyclone separation device 300 to obtain a liquid-phase refrigerant, connecting a liquid outlet of the separation cavity 330 of the cyclone separation device 300 to an inlet end of a heat load 430, and performing heat exchange with the liquid-phase refrigerant through the heat load 430 to form a second two-phase fluid; s4, performing circulation treatment on the second two-phase fluid to obtain a circulation liquid, introducing the circulation liquid into the cyclone separation device 300 by using the first guide pipe 500, and repeating the steps S2 to S3. That is, according to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the carbon dioxide gas is subjected to supersonic treatment by using the cyclone separation device 300, so that the carbon dioxide gas is condensed into liquid-phase carbon dioxide, and thus a first two-phase fluid is formed.
According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the cyclone separation device 300 can be applied to a carbon capture technology, the carbon dioxide captured by carbon is treated by the cyclone separation device 300 to obtain a liquid refrigerant, and the liquid refrigerant applied to a refrigeration system is recycled through cycle treatment, so that carbon emission reduction in the high-energy-consumption industry is realized, and resource utilization is realized in a true sense.
Further, step S1 includes: s11, pressurizing the gas by using a first supercharger 130, and enabling the pressurized gas to sequentially pass through an ejector 140, a pipeline static mixer 150 and a buffer 160; s12, introducing the gas in the buffer 160 into the cyclone separation device 300 by adopting a second guide pipe 200; a pressure regulating valve and a pressure transmitter are arranged on the second flow guide pipe 200 to regulate the pressure of the gas to 1.2 to 2.0 bar; arranging a temperature transmitter on the second flow guide pipe 200 to adjust the temperature of the gas to 25-40 ℃; a flow transmitter is arranged on the second flow guide pipe 200 to adjust the flow of the gas to 180 to 200m 3 H is used as the reference value. That is, the yield of the liquid-phase refrigerant can be improved by adjusting the parameters of the gas before the gas enters the cyclone 300.
Further, step S2 includes: s21, applying initial velocity to the introduced gas by using the cylinder part 311 of the cyclone separation device 300; s22, the gas is accelerated using the cone portion 321 of the cyclonic separating apparatus 300. That is, the cylinder portion 311 of the cyclone 300 applies an initial rotational speed to the gas to make the gas enter the cone portion 321 at a constant speed, and then the gas is accelerated by the cone portion 321.
Further, step S22 includes: s221, guiding the gas in the barrel portion 311 to the tapered section 321b by using the guiding cone 321a of the cone portion 321; s222, accelerating the gas once by using the tapered section 321b, and injecting the accelerated gas to the expansion section 321c; and S223, performing secondary acceleration on the gas subjected to the primary acceleration by using the expansion section 321c to obtain a first two-phase fluid. Specifically, when the gas flows through the tapered section 321b, the gas flow velocity is correspondingly increased due to the continuous reduction of the cross-sectional area of the tapered section 321b, when the gas reaches the narrowest position of the tapered section 321b, the mach number of the subsonic gas becomes 1, and then the gas enters the expanding section 321c from the narrowest position of the tapered section 321b, because the flow velocity is continuously increased, the sonic gas becomes supersonic gas, and the temperature and the pressure of the gas are continuously reduced, so that the carbon dioxide gas is condensed and nucleated to form carbon dioxide liquid.
Further, the gas also contains impurity gas, and the impurity gas is one or more of nitrogen, hydrogen, oxygen or carbon monoxide. That is, the impurity gas can be separated from the carbon dioxide by the cyclone 300. For example: in the carbon capture treatment process of the flue gas and tail gas, the tail gas usually contains nitrogen, hydrogen, oxygen, carbon monoxide and carbon dioxide, the cyclone separation device 300 can firstly separate the carbon dioxide from other gases, so that the high-efficiency separation of the carbon dioxide in the flue gas and tail gas is realized without the action of any chemical absorbent, adsorbent, high molecular membrane material and the like, and the separated liquid carbon dioxide is applied to a refrigeration system.
Further, the cyclone 300 is also used to maintain the gaseous phase of the impurity gas. The impurity gases are introduced into the cyclonic separation apparatus 300 with the carbon dioxide to provide a pressure boost effect that further promotes condensation of the carbon dioxide within the cyclonic separation apparatus 300.
Further, step S2 further includes: s23, connecting the liquid discharge cavity 320 of the cyclone separation device 300 to the discharge hole of the cyclone separation device 300 to receive the first two-phase fluid and the impurity gas; s24, separating the first two-phase fluid from the impurity gas by using a liquid discharge cavity 320 of the cyclone separation device 300; s25, connecting one end of a diffuser 340 to an upper exhaust port of a liquid discharge cavity 320 of the cyclone separation device 300 to receive the impurity gas, and pressurizing the impurity gas by using the diffuser 340; and S26, communicating the other end of the diffuser 340 with the outside to discharge the pressurized impurity gas. That is, the first two-phase fluid is separated from the impurity gas by the liquid discharge chamber 320 of the cyclonic separating apparatus 300.
Further, step S3 includes: s31, connecting the air outlet of the separation cavity 330 of the cyclone separation device 300 to the second feeding hole of the cyclone separation device 300 through the third guide pipe 350. Specifically, the first two-phase fluid has a significant pressure gradient in the cyclonic separating apparatus 300, a large centrifugal force is generated when the first two-phase fluid passes through the conical portion 321 of the cyclonic separating apparatus 300, the flow field in the tapered section 321b generates a low-pressure region in the axial direction of the nozzle under the action of the centrifugal force, when the first two-phase fluid passes through the narrowest position and reaches a supersonic speed, the first two-phase fluid further expands in the expanded section 321c, so that a low pressure is generated in the expanded section 321c, and finally, when the first two-phase fluid and the impurity gas are discharged from the discharge port of the cyclonic separating apparatus 300, a large pressure difference exists, so that the gas-phase carbon dioxide in the separated first two-phase fluid escapes.
According to the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, the separation cavity 330 of the cyclone separation device 300 is used for separating the gas-phase carbon dioxide in the first two-phase fluid, and the gas-phase carbon dioxide is introduced into the cyclone separation device 300 through the third guide pipe 350, so that the return of the escaped gas-phase carbon dioxide can be effectively weakened or avoided, the first two-phase fluid is expanded more fully in the tapered section 321b and the expanded section 321c, the fluid fluctuation resistance and the low-temperature performance of the nozzle can be improved, and the yield of the liquid-phase refrigerant can be further improved.
Further, step S3 further includes: s32, connecting a liquid outlet of the separation cavity 330 of the cyclone separation device 300 to the liquid storage tank 410 by adopting a fourth guide pipe 460, and storing a liquid-phase refrigerant by adopting the liquid storage tank 410; s33, the liquid pump 420 is connected to the receiver tank 410 to receive the liquid-phase refrigerant, and the liquid pump 420 is used to pump the liquid-phase refrigerant into the heat load 430. That is, the liquid-phase carbon dioxide in the first two-phase fluid is used as the refrigerant in the refrigeration system, so that the wide industrial application value of the natural refrigerant is realized.
Further, step S4 includes: s41, connecting the condensing evaporator 440 to the outlet end of the heat load 430 using a fifth flow guide tube 470 to receive the second two-phase fluid, wherein the condensing evaporator 440 is used for condensing the second two-phase fluid; s42, connecting a first end of a second booster 450 to an outlet end of the condensing evaporator 440 to receive the circulating liquid, and boosting the circulating liquid with the second booster 450; s43, the second end of the second booster 450 is connected to the third inlet of the cyclone 300 by using the first flow guide 500 to guide the pressurized circulating liquid into the cyclone 300. That is, the liquid-phase carbon dioxide in the first two-phase fluid is used as the refrigerant, the liquid-phase carbon dioxide is heat-exchanged to form the second two-phase fluid, and the second two-phase fluid is introduced into the cyclone 300 for recycling through a circulation process, thereby realizing the wide industrial application value of the "natural refrigerant".
Example 1
S1, in terms of mole fraction ratio, enabling mixed gas containing 20% of carbon dioxide, 70% of nitrogen and 10% of oxygen to sequentially pass through a first supercharger 130, an ejector 140, a pipeline static mixer 150 and a buffer 160, then introducing the mixed gas into a cyclone separation device 300 by using a second guide pipe 200, respectively adjusting a pressure regulating valve and a pressure transmitter to enable the pressure of the mixed gas to be 1.6bar, enabling the pressure at an outlet of a diffuser 340 of the cyclone separation device 300 to be 1bar, adjusting a temperature transmitter to enable the temperature of the mixed gas to be 30 ℃, and adjusting a flow transmitter to enable the flow of the mixed gas to be 200m 3 /h；
S2, condensing the gas by using a cyclone separation device 300 to obtain a first two-phase fluid;
s3, separating the first two-phase fluid by using the separation cavity 330 of the cyclone separation device 300 to obtain a liquid-phase refrigerant and gas-phase carbon dioxide, connecting the gas-phase carbon dioxide to a second feed inlet of the cyclone separation device 300 through an exhaust port of the separation cavity 330 of the cyclone separation device 300 and a third guide pipe 350 in sequence, and connecting a liquid discharge port of the separation cavity 330 of the cyclone separation device 300 to an inlet end of a heat load 430 to exchange heat with the liquid-phase refrigerant through the heat load 430 to form a second two-phase fluid;
s4, performing circulation treatment on the second two-phase fluid to obtain a circulation liquid, introducing the circulation liquid into the cyclone separation device 300 by using the first flow guide pipe 500, and repeating the steps S2-S3.
Example 2
The difference from example 1 is that the temperature of the mixed gas was 25 ℃.
Example 3
The difference from example 1 is that the temperature of the mixed gas was 35 ℃.
Example 4
The difference from example 1 is that the temperature of the mixed gas was 40 ℃.
Example 5
The difference from example 1 is that the pressure of the mixed gas was 1.2bar.
Example 6
The difference from example 1 is that the pressure of the mixed gas was 1.4bar.
Example 7
The difference from example 1 is that the pressure of the mixed gas was 1.8bar.
Example 8
The difference from example 1 is that the pressure of the mixed gas was 2.0bar.
Example 9
The difference from example 1 is that the pressure of the mixed gas was 2.0bar and the temperature was 40 ℃.
Example 10
The difference from example 1 is that the pressure of the mixed gas is 1.2bar and the temperature is 25 ℃.
Example 11
The difference from example 10 is that the composition of the mixed gas is, in terms of mole fraction ratio: 30% carbon dioxide, 60% nitrogen and 10% oxygen.
Example 12
The difference from example 10 is that the composition of the mixed gas is, in terms of mole fraction ratio: 40% carbon dioxide, 55% nitrogen and 5% oxygen.
Comparative example 1
The difference from example 1 is that the separation chamber 330 of the cyclonic separating apparatus 300 is not provided with an exhaust and third flow conduit 350 and the first two-phase fluid introduced at step S3 directly into the inlet end of the heat load 430.
A simulation apparatus shown in FIG. 1 was used to simulate the novel carbon emission reduction refrigeration cycle method according to examples 1 to 11 and comparative example 1.
Specifically, as shown in fig. 1, the simulation steps of the novel carbon emission reduction refrigeration cycle method are as follows:
SS1 in CO 2 Carbon dioxide gas is stored in the cylinder group 120, other gases (which may be one or more of nitrogen, hydrogen, oxygen, or carbon monoxide) are stored in the other cylinder groups 110, and two first superchargers 130 are respectively connected to the CO 2 The gas cylinder group 120 and the other gas cylinder groups 110 pressurize the carbon dioxide gas and the gas respectively, the pressurized carbon dioxide gas and the other gas are sequentially introduced into the ejector 140, the pipeline static mixer 150 and the buffer, the carbon dioxide gas and the other gas are uniformly mixed, the pressure parameter of the mixed gas is adjusted, the parameter of the mixed gas is further adjusted by arranging a pressure regulating valve, a pressure transmitter, a temperature transmitter and a flow transmitter on the second flow guide pipe 200, and the mixed gas is introduced into the cyclone separation device 300 through the second flow guide pipe 200 after being adjusted.
SS2, the barrel part 311 of the cyclone separation device 300 receives the adjusted mixed gas, and applies an initial velocity to the mixed gas, so that the mixed gas enters the cone part 321 at the constant initial velocity, the mixed gas is guided to the tapered section 321b by the guide cone 321a section of the cone part 321, the flow velocity of the mixed gas is correspondingly increased along with the continuous reduction of the sectional area of the tapered section 321b, when the mixed gas reaches the narrowest position of the tapered section 321b, the Mach number of the subsonic gas is changed into 1, then the mixed gas enters the expanding section 321c from the narrowest position of the tapered section 321b, the flow velocity is continuously increased, so that the sonic gas is changed into supersonic gas, and along with the continuous reduction of the temperature and pressure of the mixed gas, the carbon dioxide in the mixed gas is firstly condensed and nucleated to form liquid-phase carbon dioxide, thereby obtaining a first two-phase fluid and impurity gas at the discharge port of the cyclone separation device 300.
SS3, the first two-phase fluid enters the separation chamber 330 through the lower liquid outlet of the liquid discharge chamber 320, the impurity gas is separated from the first two-phase fluid through the upper gas outlet of the liquid discharge chamber 320, and the impurity gas is discharged to the atmospheric environment through the diffuser 340;
the first two-phase fluid flows into the separation cavity 330, the gas-phase carbon dioxide and the liquid-phase carbon dioxide in the first two-phase fluid are separated by the separation cavity 330, the exhaust port of the separation cavity 330 is connected to the second feed port of the cyclone separation device 300 through the third guide pipe 350, the carbon dioxide escaping from the separation cavity 330 is introduced into the cyclone separation device 300 through the third guide pipe 350, the liquid-phase carbon dioxide is discharged through the liquid discharge port of the separation cavity 330 to obtain a liquid-phase refrigerant, the liquid-phase refrigerant is introduced into the liquid storage tank 410 through the fourth guide pipe 460, the liquid outlet of the liquid storage tank 410 is connected with the liquid pump 420, and the liquid-phase refrigerant is pumped into the heat load 430 through the liquid pump 420;
the heat load 430 exchanges heat with the liquid phase refrigerant to form a second two-phase fluid.
SS4, the condensing evaporator 440 is connected to the outlet end of the heat load 430 by a fifth flow guide tube 470 to receive the second two-phase fluid, the condensing evaporator 440 condenses the second two-phase fluid, the second booster 450 boosts the pressure of the gas-phase carbon dioxide in the second two-phase fluid, and the circulating liquid is guided to the third feed port of the cyclone 300 by the first flow guide tube 500.
In addition, a first decompression sampling valve is arranged at a lower liquid outlet of the liquid discharge cavity 320 to measure the yield and the temperature of the first two-phase fluid, a second decompression sampling valve is arranged at a liquid discharge outlet of the separation cavity 330 to measure the yield of the liquid refrigerant, the emission reduction rate is calculated, and the test and calculation results are shown in table 1.
TABLE 1 emission reduction rates under the Process parameters of examples 1 to 11 and comparative example 1
As can be seen from Table 1, the preferred mixed gas pressure is 1.6bra and the preferred mixed gas temperature is 25 ℃; the liquid-phase carbon dioxide and the gas-phase carbon dioxide in the first two-phase fluid are separated by using the separation chamber 330 of the cyclone separation device 300, and the gas outlet of the separation chamber 330 is provided with the third flow guide pipe 350, and the other end of the third flow guide pipe 350 is connected to the second feed inlet of the cyclone separation device 300, so that the gas-phase carbon dioxide is introduced into the cyclone separation device 300 through the third flow guide pipe 350, and the yield of the liquid-phase refrigerant can be further improved.
Influence of different temperatures on carbon dioxide separation performance and refrigeration performance
As described in example 1~4 above, a mixed gas containing 20% carbon dioxide, 70% nitrogen and 10% oxygen was passed through the first supercharger 130, the ejector 140, the pipe static mixer 150 and the buffer 160 in this order, and then introduced into the cyclone 300 using the second guide pipe 200, and the pressure of the mixed gas was adjusted to 1.6bar by the pressure adjusting valve and the pressure transmitter, respectively, and the pressure at the outlet of the diffuser 340 of the cyclone 300 was adjusted to 1bar by the temperature transmitter, respectively, to 30 ℃ (example 1), 25 ℃ (example 2), 35 ℃ (example 3), and 40 ℃ (example 4), and the flow rate of the mixed gas was adjusted to 200m by the flow rate transmitter (example 4) 3 And a third draft tube 350 is provided at an exhaust port of the separation chamber 330, and the other end of the third draft tube 350 is connected to the second feed port of the cyclone 300, and the influence of different temperatures on the separation performance of carbon dioxide and the refrigeration performance is measured, wherein the refrigeration performance is evaluated by the relative carnot efficiency, which is calculated with reference to equation 1):
wherein, T2 is-11 ℃ (refer to the temperature of a supermarket refrigeration room under the conventional condition); eta: relative carnot efficiency.
As shown in FIG. 2, it can be seen from FIG. 2 that CO increases with the temperature of the mixed gas 2 The emission reduction rate tends to decrease, but the trend changes gently, the overall change is not large, and is maintained at more than 76%, because the temperature of the fluid in the system also tends to increase along with the increase of the temperature of the mixed gas, so that the condensation amount of the liquid-phase carbon dioxide is reduced, and the separation efficiency of the system is reduced. Furthermore, it can be seen that when the refrigeration temperature is maintained at-11 ℃, the relative carnot efficiency of the system gradually decreases with the increase of the temperature of the mixed gas, because the increase of the temperature of the mixed gas causes the viscosity of the gas to increase, thereby affecting the flow resistance of the fluid in the system. That is to say, for the novel carbon emission reduction refrigeration cycle method provided by the embodiment of the invention, in practical application, the lower the temperature of the mixed gas is, the lower the CO emission reduction refrigeration cycle method is 2 The better the separation effect, the better the refrigeration effect.
Influence of different pressures on carbon dioxide separation performance and refrigeration performance
As described in example 1 and example 5~8, the mixed gas containing 20% of carbon dioxide, 70% of nitrogen, and 10% of oxygen was passed through the first booster 130, the ejector 140, the pipe static mixer 150, and the buffer 160 in this order, and then introduced into the cyclone 300 using the second flow guide pipe 200, the pressure of the mixed gas was adjusted to 1.2bar (example 5), 1.4bar (example 6), 1.6bar (example 1), 1.8bar (example 7), and 2.0bar (example 8) by adjusting the pressure control valve and the pressure transmitter, respectively, the pressure at the outlet of the diffuser 340 of the cyclone 300 was 1bar, the temperature of the mixed gas was adjusted to 30 ℃, and the flow rate of the mixed gas was adjusted to 200m by adjusting the flow rate transmitter 3 And a third flow guide pipe 350 is arranged at the exhaust port of the separation cavity 330, the other end of the third flow guide pipe 350 is connected to the second feed port of the cyclone separation device 300, and the influence of different pressures on the separation performance and the refrigeration performance of the carbon dioxide is measured.
As shown in FIG. 3, it can be seen from FIG. 3 that when the pressure of the mixed gas is 1.2 to 1.6bar, the CO2 reduction rate gradually increases and is 1 as the pressure increases.The maximum value was reached at 6 hours, i.e., as a result in example 1, the CO2 reduction rate reached 79%, at which the separation efficiency was the highest. That is, when the gas pressure is 1.2 to 1.6bar, the improvement of the inlet pressure contributes to the improvement of the separation performance of the system. When the pressure ratio is greater than 1.6, CO 2 The emission reduction rate is gradually reduced, and when the gas pressure is between 1.2 and 1.6bar, the fluid can form a low-temperature environment meeting the separation of condensate in the cyclone separation device, thereby being beneficial to the condensation of condensable components. And as can be seen from fig. 3, the relative carnot efficiency of the system increases with increasing mixed gas pressure while maintaining the refrigeration temperature at-11 ℃, but the overall efficiency is > 70%.
Influence of different components on carbon dioxide separation performance and refrigeration performance
As described in examples 10 to 12, a mixed gas A (example 10) containing 20% of carbon dioxide, 70% of nitrogen and 10% of oxygen, a mixed gas B (example 11) containing 30% of carbon dioxide, 60% of nitrogen and 10% of oxygen, and a mixed gas C (example 12) containing 40% of carbon dioxide, 55% of nitrogen and 5% of oxygen were passed through the first supercharger 130, the ejector 140, the pipe static mixer 150 and the buffer 160 in this order, and the mixed gas was introduced into the cyclone 300 using the second draft tube 200, and the pressure of the mixed gas was adjusted to 1.2bar by the pressure adjusting valve and the pressure transmitter, the pressure at the outlet of the diffuser 340 of the cyclone 300 was 1bar by the temperature transmitter to 25 ℃, and the flow rate of the mixed gas was adjusted to 200m by the flow rate transmitter 3 H, and a third guide pipe 350 is provided at the exhaust port of the separation chamber 330, and the other end of the third guide pipe 350 is connected to the second feed port of the cyclone 300, and the influence of the mixed gas of different components on the carbon dioxide separation performance and the refrigeration performance is measured.
The results are shown in FIG. 4~5, where component A in FIG. 4 represents CO of mixed gas A (example 10) 2 Component B in FIG. 4 represents CO of mixed gas B (example 11) 2 Component C in FIG. 4 represents CO of the mixed gas C (example 12) 2 The emission reduction rate of (2); component A in FIG. 5 represents a mixed gas A (practice)Example 10), component B in fig. 5 represents the corresponding relative carnot efficiency of mixed gas B (example 11), and component C in fig. 5 represents the corresponding relative carnot efficiency of mixed gas C (example 12). As can be seen from FIGS. 4 and 5, the CO content of the mixed gas is varied 2 Increase in the ratio of CO 2 The emission reduction rate and the refrigeration performance of the system are increased.
Influence of the third draft tube on carbon dioxide separation Performance
Based on the experiment of the above embodiment 1 and embodiment 5~8, the mixed gas containing 20% of carbon dioxide, 70% of nitrogen and 10% of oxygen sequentially passes through the first booster 130, the ejector 140, the pipeline static mixer 150 and the buffer 160, and then is introduced into the cyclone separation apparatus 300 by using the second draft tube 200, the pressure of the mixed gas is respectively 1.2bar, 1.4bar, 1.6bar, 1.8bar and 2.0bar by respectively adjusting the pressure regulating valve and the pressure transmitter, the pressure at the outlet of the diffuser 340 of the cyclone separation apparatus 300 is 1bar, the temperature of the mixed gas is 30 ℃ by adjusting the temperature transmitter, and the flow rate transmitter is adjusted to make the flow rate of the mixed gas 200m 3 H, the separation chamber 330 of the cyclonic separating apparatus 300 was not provided with an exhaust port and the third flow conduit 350, and the first two-phase fluid introduced into the inlet end of the thermal load 430 in step S3 was conducted directly to compare the influence of the third flow conduit 350 on the separation performance of carbon dioxide.
As a result, as shown in fig. 6, it can be seen from fig. 6 that the separation performance of carbon dioxide can be significantly improved by providing the third draft tube.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. A novel carbon emission reduction refrigeration cycle method is characterized by comprising the following steps:
s1, connecting a first feeding hole of a cyclone separation device (300) to a gas bottle group to receive gas in the gas bottle group, wherein the gas contains carbon dioxide;
s2, condensing the gas by using the cyclone separation device (300) to obtain a first two-phase fluid;
s3, separating the first two-phase fluid by using a separation cavity (330) of a cyclone separation device (300) to obtain a liquid-phase refrigerant, wherein a liquid discharge port of the separation cavity (330) is connected to an inlet end of a heat load (430), and the heat load (430) and the liquid-phase refrigerant are subjected to heat exchange to form a second two-phase fluid;
s4, performing circulation treatment on the second two-phase fluid to obtain a circulation liquid, introducing the circulation liquid into the cyclone separation device (300) by adopting a first guide pipe (500), and repeating the steps S2-S3.
2. The novel carbon emission reduction refrigeration cycle method as set forth in claim 1, wherein said step S1 includes:
s11, pressurizing the gas by using a first booster (130), and enabling the pressurized gas to sequentially pass through an ejector (140), a pipeline static mixer (150) and a buffer (160);
s12, introducing the gas in the buffer (160) into the cyclone separation device (300) by adopting a second guide pipe (200);
a pressure regulating valve and a pressure transmitter are arranged on the second flow guide pipe (200) to regulate the pressure of the gas to 1.2 to 2.0 bar;
arranging a temperature transmitter on the second flow guide pipe (200) to adjust the temperature of the gas to 25-40 ℃;
a flow transmitter is arranged on the second flow guide pipe (200) to adjust the flow of the gas to 180 to 200m 3 /h。
3. The novel carbon emission reduction refrigeration cycle method as set forth in claim 1, wherein said step S2 includes:
s21, applying an initial velocity to the introduced gas by using a cylinder part (311) of the cyclone separation device (300);
s22, accelerating the gas by using the cone part (321) of the cyclone separation device (300).
4. The novel carbon emission reduction refrigeration cycle method as set forth in claim 3, wherein the step S22 includes:
s221, guiding the gas in the barrel part to a tapered section (321 b) by using a flow guide cone (321 a) of the cone part (321);
s222, accelerating the gas once by adopting the reducing section (321 b), and injecting the accelerated gas to an expanding section (321 c);
s223, performing secondary acceleration on the gas after the primary acceleration by adopting the expansion section (321 c) to obtain the first two-phase fluid.
5. The novel carbon emission reduction refrigeration cycle method as claimed in claim 1, wherein the gas further contains an impurity gas, the impurity gas being one or more of nitrogen, hydrogen, oxygen or carbon monoxide.
6. The novel carbon sequestration reduction refrigeration cycle method according to claim 5, characterized in that, the cyclone separation device (300) is also used to maintain the gaseous phase of the impurity gas.
7. The novel carbon emission reduction refrigeration cycle method as set forth in claim 6, wherein said step S2 further includes:
s23, connecting a liquid discharge cavity (320) of the cyclone separation device (300) to a discharge hole of the cyclone separation device (300) to receive the first two-phase fluid and the impurity gas;
s24, separating the first two-phase fluid and the impurity gas by using a liquid discharge cavity (320) of the cyclone separation device (300);
s25, connecting one end of a diffuser (340) to an upper exhaust port of a liquid discharge cavity (320) of the cyclone separation device (300) to receive the impurity gas, and pressurizing the impurity gas by using the diffuser (340);
and S26, communicating the other end of the diffuser (340) with the outside to discharge the pressurized impurity gas.
8. The novel carbon emission reduction refrigeration cycle method as claimed in claim 1, wherein the step S3 includes:
s31, connecting an air outlet of the separation cavity (330) of the cyclone separation device (300) to a second feed inlet of the cyclone separation device (300) through a third guide pipe (350).
9. The novel carbon emission reduction refrigeration cycle method as set forth in claim 1, wherein said step S3 further includes:
s32, connecting a liquid outlet of the separation cavity (330) of the cyclone separation device (300) to a liquid storage tank (410) by using a fourth guide pipe (460), and storing the liquid-phase refrigerant by using the liquid storage tank (410);
s33, connecting a liquid pump (420) to the liquid storage tank (410) to receive the liquid-phase refrigerant, and pumping the liquid-phase refrigerant into the heat load (430) with the liquid pump (420).
10. The novel carbon emission reduction refrigeration cycle method as set forth in claim 1, wherein said step S4 includes:
s41, connecting a condensation evaporator (440) by using a fifth flow guide pipe (470), wherein the fifth flow guide pipe (470) is also used for connecting to the outlet end of the heat load (430) to receive the second two-phase fluid, and the condensation evaporator (440) is used for condensing the second two-phase fluid;
s42, connecting a first end of a second booster (450) to an outlet end of the condensing evaporator (440) to receive the circulating liquid, and boosting the circulating liquid by using the second booster (450);
s43, connecting the second end of the second booster (450) to the third feed port of the cyclone separation device (300) by using the first guide pipe (500) to guide the pressurized circulating liquid into the cyclone separation device (300).
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