CN220931509U - High-efficiency energy-saving gas separation device - Google Patents
High-efficiency energy-saving gas separation device Download PDFInfo
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- CN220931509U CN220931509U CN202321565543.9U CN202321565543U CN220931509U CN 220931509 U CN220931509 U CN 220931509U CN 202321565543 U CN202321565543 U CN 202321565543U CN 220931509 U CN220931509 U CN 220931509U
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- 238000000926 separation method Methods 0.000 title claims abstract description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 79
- 239000007789 gas Substances 0.000 claims abstract description 61
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 39
- 239000002808 molecular sieve Substances 0.000 claims abstract description 35
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 238000001816 cooling Methods 0.000 claims abstract description 31
- 239000006096 absorbing agent Substances 0.000 claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 106
- 229910052786 argon Inorganic materials 0.000 claims description 53
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 27
- 238000005194 fractionation Methods 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 11
- 230000000149 penetrating effect Effects 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000004821 distillation Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 11
- 239000000498 cooling water Substances 0.000 abstract description 4
- 230000005611 electricity Effects 0.000 abstract description 3
- 230000008569 process Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 238000003860 storage Methods 0.000 description 9
- 239000006200 vaporizer Substances 0.000 description 9
- 238000009835 boiling Methods 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000030279 gene silencing Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The embodiment of the utility model provides a high-efficiency energy-saving gas separation device, and relates to the technical field of gas separation. The high-efficiency energy-saving gas separation device comprises a lower fractionating tower and an upper fractionating tower, wherein an air filter is arranged at one end of the lower fractionating tower, and a first molecular sieve absorber and a second molecular sieve absorber are arranged at the output end direction of the air filter; on the basis of recovering the cold quantity of the polluted nitrogen by the subcooler and the plate heat exchanger, part of polluted nitrogen enters the water cooling tower and is in countercurrent contact with cooling water pumped by the air cooling tower, so that the temperature of the cooling water is further reduced by 3-5 ℃, and the precooling effect of the air cooling tower on the air entering the tower is improved; the system utilizes the cold energy, simultaneously the liquid expander is arranged to throttle and expand the liquid air after being pressurized by the air booster, and meanwhile, the organic Rankine cycle piece is arranged to convert the internal energy released in the high-pressure air expansion process into electric energy for the system electric equipment to use, so that the system electricity consumption is reduced.
Description
Technical Field
The utility model relates to the technical field of gas separation, in particular to a high-efficiency energy-saving gas separation device.
Background
Air separation, namely air separation; the method is a process of separating components (oxygen, nitrogen, argon, helium and other rare gases) from air by using a low-temperature refrigeration principle, wherein the air is generally compressed and cooled to a very low temperature, or the air is liquefied by an expansion method, and then the air is subjected to low-temperature rectification separation in a rectifying tower; for example, when liquid air boils, the more volatile nitrogen (boiling point-196 ℃ C.) is vaporized first, then argon (boiling point-185.9 ℃ C.) and finally oxygen (boiling point-183 ℃ C.).
Cryogenic separation, also known as low-temperature rectification, is a gas liquefaction technology, and usually adopts methods such as throttling expansion or adiabatic expansion to compress and cool gas, and then rectifies the gas by utilizing differences of boiling points of different gases so as to separate the different gases; the method is characterized in that the purity of the product gas is high, but certain disadvantages still exist, such as high energy consumption for working compression and cooling; along with the proposal of the double-carbon target, the chemical device also becomes a main battlefield for energy conservation and consumption reduction, so that the efficient and energy-saving gas separation device is designed for reducing the energy consumption of the gas separation device, saving the production cost of a factory and improving the efficiency of the factory.
Disclosure of utility model
The utility model aims to provide a high-efficiency energy-saving gas separation device, which can avoid rectification by utilizing the difference of boiling points of different gases after gas compression and cooling, so that the different gases are separated; the method is characterized in that the purity of the product gas is high, but the working compression and cooling energy consumption are large.
The utility model provides a high-efficiency energy-saving gas separation device which comprises a fractionation lower tower and a fractionation upper tower which is arranged at the top of the fractionation lower tower and used for rectifying for many times.
In a specific embodiment, the air filter is a self-cleaning air filter, the output end of the air filter is connected with a raw material air compressor, and the output end of the raw material air compressor is communicated with an air cooling tower through a pipe fitting.
In a specific embodiment, the air delivery ends of the first molecular sieve absorber and the second molecular sieve absorber are connected with an air booster through a pipeline, and one end of the air booster penetrates through the heat exchange part of the plate heat exchanger and is connected with a gas expander.
In a specific embodiment, one end of the gas expander, which is used for conveying gas, is connected with an expander pressurizing end, and one end of the expander pressurizing end is communicated with a liquid expander.
In a specific embodiment, the top delivery end of the upper fractionating tower is connected with a product liquid oxygen pump through a pipe fitting penetrating through the subcooler, and the dirty nitrogen end of the upper fractionating tower is connected with a steam heater and a water cooling tower through pipe fitting penetrating through the subcooler and the plate heat exchanger.
In a specific embodiment, the refined argon column is provided with a crude argon column in the direction of its inlet for the pre-crude distillation of the argon fraction.
In a specific embodiment, a surface of one end of the crude argon column is provided with a crude argon condenser, and the output end of the crude argon column is connected with a circulating phase liquid oxygen pump for liquid oxygen circulation.
In a specific embodiment, a first refined argon condenser and a second refined argon condenser are symmetrically arranged at the top and the bottom of one end of the refined argon tower.
In a specific embodiment, a main condensing evaporator is arranged opposite to the lower fractionating tower and the upper fractionating tower, and the main condensing evaporator is a multi-layer plate fin.
In a specific embodiment, an organic Rankine cycle element for organic heat exchange is mounted at the output end pipe fitting of the air booster and the gas expander.
The beneficial effects of the application are as follows:
1. on the basis of recovering the cold quantity of the polluted nitrogen by the subcooler and the plate heat exchanger, part of polluted nitrogen enters the water cooling tower and is in countercurrent contact with cooling water pumped by the air cooling tower, so that the temperature of the cooling water is further reduced by 3-5 ℃, and the precooling effect of the air cooling tower on the air entering the tower is improved.
2. The system utilizes the cold energy, simultaneously the liquid expander is arranged to throttle and expand the liquid air after being pressurized by the air booster, and meanwhile, the organic Rankine cycle piece is arranged to convert the internal energy released in the high-pressure air expansion process into electric energy for the system electric equipment to use, so that the system electricity consumption is reduced.
3. The organic Rankine cycle part is arranged at the recovery position of the interstage cooling heat energy of a plurality of stages of the air booster, and low-boiling-point organic matters are selected as working media, so that the heat energy is used for generating electricity and supplying power to electric equipment of the system, and the power consumption of the system is reduced.
Finally, the energy consumption of the air separation device system can be effectively reduced and the consumption of steam consumption and electric quantity can be reduced through the coupling of energy-saving measures and the existing device.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some examples of the present utility model and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a perspective flow chart of an overall structure according to an embodiment of the present utility model.
Icon:
1. an air filter; 2. a raw material air compressor; 3. an air cooling tower; 31. a first water pump; 4. a molecular sieve adsorber I; 5. a molecular sieve absorber II; 6. an air booster; 7. a plate heat exchanger; 8. a gas expander; 9. a booster end of the expander; 10. a liquid expander; 11. fractionating the mixture into a lower tower; 12. fractionating and loading on a tower; 13. a subcooler; 14. a product liquid oxygen pump; 15. a steam heater; 16. a water cooling tower; 161. a second water pump; 17. a crude argon column; 171. a crude argon condenser; 172. a circulating phase liquid oxygen pump; 18. a refined argon tower; 181. a refined argon condenser I; 182. a refined argon condenser II; 19. a main condensing evaporator; 20. emptying the muffler; 21. an organic rankine cycle member.
Detailed Description
Because air separation adopts methods such as throttling expansion or adiabatic expansion, gas is compressed and cooled, and then different gases are separated by rectifying the difference of boiling points of the different gases; the method is characterized in that the purity of the product gas is high, but certain disadvantages still exist, such as high energy consumption for working compression and cooling; along with the proposal of the double-carbon target, the chemical device also becomes a main battlefield for energy saving and consumption reduction, so the inventor provides a high-efficiency energy-saving gas separation device through researches, which can avoid rectifying by utilizing the difference of boiling points of different gases after gas compression and cooling, so that the different gases are separated; the method is characterized in that the purity of the product gas is high, but the working compression and cooling energy consumption are large, so that the defects are overcome.
Some embodiments of the present utility model are described in detail below with reference to the accompanying drawings. The following embodiments and features of the embodiments may be combined with each other without conflict.
Referring to fig. 1, an embodiment of the present utility model provides a high-efficiency and energy-saving gas separation device, which includes a lower fractionating tower 11 for air rectification, and an upper fractionating tower 12 disposed at the top of the lower fractionating tower 11 for multiple times rectification, wherein one end of the lower fractionating tower 11 is provided with an air filter 1 for cleaning and purifying gas, the output end direction of the air filter 1 is provided with a first molecular sieve absorber 4 and a second molecular sieve absorber 5 for cooling the gas powder sieve, the first molecular sieve absorber 4 and the second molecular sieve absorber 5 are used in a switching manner, the switching period is four hundred eighty minutes, the timing is automatically switched, the output end direction of the first molecular sieve absorber 4 and the second molecular sieve absorber 5 is provided with a plate heat exchanger 7 for circularly exchanging heat with multiple groups of gas, the input end directions of the lower fractionating tower 11 and the upper fractionating tower 12 are provided with a subcooler 13 for circularly cooling gas and liquid, and the right end directions of the upper fractionating tower 12 and the subcooler 13 are provided with an argon refining tower 18 for rectifying argon fraction.
Specifically, the air filter 1 is a self-cleaning air filter, the output end of the air filter 1 is connected with a raw material air compressor 2 for compressing air through a pipe fitting, the air compressor is mostly a reciprocating piston type, a rotary blade or a rotary screw rod, the air compressor is selected according to actual requirements, the output end of the raw material air compressor 2 is communicated with an air cooling tower 3 through the pipe fitting, the high-temperature compressed air entering through the raw material air compressor 2 is cooled, and the delivery end of the air cooling tower 3 is connected with a water pump 31 through the pipe fitting;
Specifically, one end of the molecular sieve absorber I4 and one end of the molecular sieve absorber II 5 are provided with an emptying muffler 20 for silencing noise, the air delivery ends of the molecular sieve absorber I4 and the molecular sieve absorber II 5 are connected with an air booster 6 through pipelines, the air delivery ends are used for increasing and guiding purified air, and one end of the air booster 6 penetrates through a heat exchange part of the plate heat exchanger 7 and is connected with a gas expander 8;
Specifically, one end of the gas expander 8 for gas delivery is connected with an expander pressurizing end 9, one end of the expander pressurizing end 9 is communicated with a liquid expander 10, the liquid expander 10 and the gas output end of the gas expander 8 are both communicated with the delivery end of the fractionation lower tower 11 through a pipe fitting, and one end of the liquid expander 10 is connected with a motor;
Specifically, the top delivery end of the fractionation upper tower 12 is connected with a product liquid oxygen pump 14 for liquid oxygen delivery through a pipe fitting penetrating through a subcooler 13, and the dirty nitrogen end of the fractionation upper tower 12 is connected with a steam heater 15 and a water cooling tower 16 through pipe fitting penetrating through the subcooler 13 and a plate heat exchanger 7;
The steam heater 15 is used for purifying and utilizing gas and is used as molecular sieve regeneration gas, one end of the steam heater 15 is communicated with the surfaces of the first molecular sieve absorber 4 and the second molecular sieve absorber 5, one end of the water cooling tower 16 is connected with a second water pump 161 used for conveying materials, and one end of the second water pump 161, far away from the water cooling tower 16, is communicated with the surface of the air cooling tower 3;
Specifically, a crude argon column 17 is arranged in the direction of the input end of the refined argon column 18 and is used for pre-crude distillation of the argon fraction;
Specifically, a crude argon condenser 171 is installed on the surface of one end of the crude argon tower 17, and the output end of the crude argon tower 17 is connected with a circulating phase liquid oxygen pump 172 for liquid oxygen circulation;
specifically, a first refined argon condenser 181 and a second refined argon condenser 182 are symmetrically arranged at the top and the bottom of one end of the refined argon tower 18 and are used for the rectification and condensation of liquid argon;
Specifically, a main condensing evaporator 19 is installed at the opposite position of the lower fractionating tower 11 and the upper fractionating tower 12, the main condensing evaporator 19 is a multi-layer plate fin, the nitrogen rising from the lower fractionating tower 11 is condensed in the main condensing evaporator, and the liquid nitrogen flowing back from the upper fractionating tower 12 is evaporated in the main condensing evaporator;
Specifically, the output end pipe fittings of the air booster 6 and the gas expander 8 are provided with an organic Rankine cycle piece 21 for organic heat exchange; the organic Rankine cycle takes low-boiling point organic matters as working media, and the organic working media absorb heat from waste heat flow in the heat exchange piece to generate steam with certain pressure and temperature.
In summary, the working principle of the efficient and energy-saving gas separation device in the embodiment of the utility model is as follows: raw materials are sucked in through an air self-suction inlet of the air filter 1, and dust and other mechanical impurities are removed through the air filter 1; the filtered air enters an air cooling tower 3 for cooling after being processed by a raw material air compressor 2; the air passes through the air cooling tower 3 from bottom to top, and is cleaned while being cooled; the air cooled by the raw material air compressor 2 enters a first molecular sieve absorber 4 and a second molecular sieve absorber 5 which are used in a switching way, and carbon dioxide, hydrocarbon and moisture in the air are absorbed; the first molecular sieve absorber 4 and the second molecular sieve absorber 5 are used in a switching way, and when the first molecular sieve absorber 4 works, the second molecular sieve absorber 5 is used for regeneration; the purified air is divided into three parts: part of air is pumped out by an air booster 6 as product instrument air, the rest of air is boosted by the air booster 6, and then one air enters an expander boosting end 9 in a gas expander 8 for boosting through heat exchange of a plate heat exchanger 7, is cooled to normal temperature by a cooling part, enters an air filter 1 for heat exchange with liquid oxygen, is expanded or throttled by a liquid expander 10 and then is sent into a fractionation lower tower 11; the other air is pumped out from the middle part of the plate heat exchanger 7 and enters the gas expander 8, and after expansion, the air directly enters the fractionation lower tower 11; the air is subjected to preliminary rectification by a lower fractionating tower 11 to obtain liquid air, liquid nitrogen and polluted liquid nitrogen, the liquid air, the liquid nitrogen and the polluted liquid nitrogen are subjected to supercooling by a cooler 13 and then throttled to enter an upper fractionating tower 12, liquid oxygen is obtained at the bottom of a main cooler after the air is subjected to further rectification by the upper fractionating tower 12, part of the liquid oxygen is extracted and compressed by a product liquid oxygen pump 14 and then enters a plate heat exchanger 7 to be reheated and then is discharged from a cold box, and the liquid oxygen enters an external oxygen pipe network; a part of liquid oxygen is supercooled by a supercooler 13 and then enters a storage tank as a product for storage; liquid nitrogen is pumped out from the top of the lower fractionating tower 11, supercooled by the plate heat exchanger 7 and directly sent into a storage tank; leading out pressure nitrogen from the top of the fractionation lower tower 11, entering the plate heat exchanger 7, and taking out a cold box after reheating as a pressure nitrogen product; the dirty nitrogen gas led out from the top of the fractionation upper tower 12 is separated into two parts after being reheated by the cooler 13 and the plate heat exchanger 7 and discharged out of the cold box: part of the waste nitrogen enters a steam heater 15 of a molecular sieve system to be used as molecular sieve regeneration gas, and the rest of the waste nitrogen is dehydrated into a water cooling tower 16; a certain amount of argon fraction is extracted from the middle part of the fractionation upper tower 12 and is sent to a crude argon tower 17, crude argon is obtained at the top part in the crude argon tower 17 after rectification, the crude argon is led into a refined argon tower 18 for rectification, refined argon is obtained at the bottom part of the refined argon tower 18, and the refined argon is sent to a liquid argon storage tank for finishing processing.
After the processing is finished, liquid oxygen extracted by the lower fractionating tower 11 and the upper fractionating tower 12 of the air separation device is conveyed into a liquid oxygen storage tank, and gaseous oxygen formed by evaporation in the liquid oxygen tank is discharged; part of liquid oxygen discharged from the bottom of the storage tank is filled into the tank wagon through the wagon filling pump, and the other part of liquid oxygen is boosted through the product liquid oxygen pump 14 and then enters the external water bath type vaporizer, so that the liquid oxygen is quickly vaporized into gaseous oxygen by water of the vaporizer, the water in the vaporizer is heated by steam, and the vaporized oxygen goes to a user pipe network; liquid nitrogen extracted by the lower fractionating tower 11 and the upper fractionating tower 12 of the air separation device is conveyed into a liquid nitrogen storage tank, gaseous nitrogen formed by evaporation in the liquid nitrogen tank is vented, and part of liquid nitrogen discharged from the bottom of the storage tank is boosted by a liquid nitrogen charging pump and then is charged into a tank car; part of the nitrogen is boosted by a centrifugal high-pressure product liquid oxygen pump 14 or a piston high-pressure product liquid oxygen pump 14 and then enters a water bath type vaporizer, the nitrogen is quickly vaporized into gaseous nitrogen by water of the vaporizer, the water in the vaporizer is heated by steam, most of the vaporized nitrogen directly enters a user high-pressure nitrogen pipe network, and a small part of the vaporized nitrogen enters a user low-pressure nitrogen pipe network after being decompressed; the other part of liquid nitrogen is boosted by a low-pressure liquid nitrogen pump and then enters a water bath type vaporizer, the liquid nitrogen is rapidly vaporized into gaseous nitrogen by water of the vaporizer, the water in the vaporizer is heated by steam, and the vaporized nitrogen is sent to a low-pressure nitrogen pipe network of a user; liquid argon extracted from the lower fractionating tower 11 and the upper fractionating tower 12 by air separation equipment is delivered to a liquid argon storage tank if the purity is qualified, and gaseous argon formed by evaporation in the liquid argon tank is emptied or returned to the lower fractionating tower 11 and the upper fractionating tower 12; liquid argon discharged from the bottom of the tank is pumped into the tank truck by a truck pump.
The above is only a preferred embodiment of the present utility model, and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (6)
1. The utility model provides a high-efficient energy-saving gas separation device, includes fractionating tower (11) to and set up in fractionating tower (11) top multitime rectification's fractionating tower (12), its characterized in that, the one end of fractionating tower (11) is provided with air cleaner (1), the output direction of air cleaner (1) is provided with molecular sieve adsorber one (4) and molecular sieve adsorber two (5), and molecular sieve adsorber one (4) and molecular sieve adsorber two (5) are for switching the use, molecular sieve adsorber one (4) and molecular sieve adsorber two (5)'s output direction is provided with plate heat exchanger (7), fractionating tower (11) and fractionating tower (12)'s defeated guide end direction is provided with subcooler (13), and fractionating tower (12) and subcooler (13)'s right-hand member direction is provided with smart argon tower (18);
The air delivery ends of the first molecular sieve absorber (4) and the second molecular sieve absorber (5) are connected with an air booster (6) through pipelines, and one end of the air booster (6) penetrates through the heat exchange part of the plate heat exchanger (7) and is connected with a gas expander (8);
One end of the gas expander (8) for conveying gas is connected with an expander pressurizing end (9), and one end of the expander pressurizing end (9) is communicated with a liquid expander (10);
The top delivery end of the fractionation upper tower (12) is connected with a product liquid oxygen pump (14) through a pipe fitting penetrating through the subcooler (13), and the dirty nitrogen end of the fractionation upper tower (12) is connected with a steam heater (15) and a water cooling tower (16) through a pipe fitting penetrating through the subcooler (13) and the plate heat exchanger (7);
an organic Rankine cycle (21) for organic heat exchange is arranged at the output end pipe fitting of the air booster (6) and the gas expander (8).
2. The efficient and energy-saving gas separation device according to claim 1, wherein the air filter (1) is a self-cleaning air filter, the output end of the air filter (1) is connected with a raw material air compressor (2), and the output end of the raw material air compressor (2) is communicated with an air cooling tower (3) through a pipe fitting.
3. The energy-efficient gas separation device according to claim 1, characterized in that the refined argon column (18) is provided with a crude argon column (17) in the direction of its input for the pre-crude distillation of the argon fraction.
4. A high efficiency energy saving gas separation apparatus according to claim 3, wherein a crude argon condenser (171) is installed on the surface of one end of the crude argon column (17), and a circulating phase liquid oxygen pump (172) for liquid oxygen circulation is connected to the output end of the crude argon column (17).
5. The efficient and energy-saving gas separation device according to claim 1, wherein a first refined argon condenser (181) and a second refined argon condenser (182) are symmetrically arranged at the top and the bottom of one end of the refined argon tower (18).
6. The efficient and energy-saving gas separation device according to claim 1, wherein a main condensing evaporator (19) is installed at the opposite position of the lower fractionating tower (11) and the upper fractionating tower (12), and the main condensing evaporator (19) is a multi-layer plate fin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321565543.9U CN220931509U (en) | 2023-06-19 | 2023-06-19 | High-efficiency energy-saving gas separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321565543.9U CN220931509U (en) | 2023-06-19 | 2023-06-19 | High-efficiency energy-saving gas separation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220931509U true CN220931509U (en) | 2024-05-10 |
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ID=90967756
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321565543.9U Active CN220931509U (en) | 2023-06-19 | 2023-06-19 | High-efficiency energy-saving gas separation device |
Country Status (1)
| Country | Link |
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| CN (1) | CN220931509U (en) |
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2023
- 2023-06-19 CN CN202321565543.9U patent/CN220931509U/en active Active
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