CN220214437U - Low-energy-consumption PSA air separation nitrogen making device - Google Patents
Low-energy-consumption PSA air separation nitrogen making device Download PDFInfo
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- CN220214437U CN220214437U CN202321633139.0U CN202321633139U CN220214437U CN 220214437 U CN220214437 U CN 220214437U CN 202321633139 U CN202321633139 U CN 202321633139U CN 220214437 U CN220214437 U CN 220214437U
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 172
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 81
- 238000000926 separation method Methods 0.000 title claims abstract description 49
- 238000005265 energy consumption Methods 0.000 title claims abstract description 24
- 238000001179 sorption measurement Methods 0.000 claims abstract description 116
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims description 15
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 10
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 10
- 238000000034 method Methods 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 230000008569 process Effects 0.000 description 6
- 239000003463 adsorbent Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000004891 communication Methods 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- NIPNSKYNPDTRPC-UHFFFAOYSA-N N-[2-oxo-2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 NIPNSKYNPDTRPC-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Separation By Low-Temperature Treatments (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The utility model provides a low-energy-consumption PSA air separation nitrogen making device, which relates to the technical field of air separation and comprises an air inlet device, an adsorption device and a supercharging device which are sequentially communicated, and is characterized in that the air inlet device comprises a first supercharger and a dryer which are arranged in series, the adsorption device comprises a first adsorption tower and a second adsorption tower which are arranged in parallel, the bottoms of the first adsorption tower and the second adsorption tower are communicated with an air discharging device, the supercharging device comprises a nitrogen buffer tank, a second supercharger and a high-pressure nitrogen tank, the first supercharger is used for compressing air to a first pressure, and the second supercharger is used for compressing nitrogen from the nitrogen buffer tank to a second pressure. The device can realize energy conservation and consumption reduction under the condition of not reducing the nitrogen pressure of the finally obtained product, and compared with the existing PSA air separation nitrogen production device, the device can reduce the energy consumption by about 10-11%, and has obvious energy conservation effect.
Description
Technical Field
The utility model relates to the technical field of air separation, in particular to a low-energy-consumption PSA air separation nitrogen making device.
Background
At present, two main processes for preparing nitrogen by air separation are available, namely a low-temperature process called cryogenic air separation and a pressure swing adsorption process called PSA process. The medium and small flow nitrogen commonly used in industrial production is generally realized by using air as raw material gas through a PSA pressure swing adsorption technology.
The pressure swing adsorption air separation nitrogen production process generally comprises the steps of compressing air to 0.7-1.0 MPa, drying and purifying, and then introducing into PSA equipment for nitrogen-oxygen separation. The adsorption capacity of the adsorbent increases with the rise of the gas pressure, so that the pressure for pressure swing adsorption air separation nitrogen production is generally 0.8-1.0 MPa, and even 1.5-2.5 MPa is selected in some occasions with high pressure requirements. The adsorbent for preparing nitrogen by pressure swing adsorption air separation is a carbon molecular sieve, the adsorption of the carbon molecular sieve to oxygen is a speed type adsorption, oxygen molecules are smaller, and compared with nitrogen, the oxygen molecules can enter micropores of the carbon molecular sieve more quickly, and the adsorption quantity of the nitrogen can be increased along with the extension of the adsorption time, so that the adsorption time is generally controlled to be 40-60 s. Air/nitrogen (Air/N) is commonly used in the industry 2 ) The ratio of (2) to the Air/N under the same condition 2 The lower the more energy-efficient. Taking nitrogen with purity of 99.5% as an example, air/N under 0.7MPa 2 Generally 2.6, i.e. every 2.6 Air, can produce 1 Air/N with purity of 99.5 percent, and Air/N is increased along with the increase of the nitrogen concentration 2 And also increases.
In the prior art, pressure swing adsorption as disclosed in CN211141530U, CN110237651AThe air separation nitrogen production device is characterized in that air is directly pressurized to the pressure of the finished nitrogen for adsorption, and the gas consumption ratio is 2.6, and the pressure of the product nitrogen is more than or equal to 0.6MPa, so that 1Nm is produced per time 3 Nitrogen gas is required to be 2.6Nm 3 The air pressure is raised to about 0.7MPa (the pressure drop of the raw material air after passing through the adsorbent is generated, so that the raw material air pressure is required to be higher than the nitrogen pressure of the product), and the final pressure is only 1Nm 3 Nitrogen yield, remaining 1.6Nm 3 The air is naturally discharged (simply referred to as "discharged air"). The part of the discharged air is compressed to 0.7MPa from normal pressure and then is directly discharged to the air, so that a great amount of energy waste is caused.
Accordingly, there is a need to provide an improved solution to the above-mentioned deficiencies of the prior art.
Disclosure of Invention
The utility model aims to provide a low-energy-consumption PSA air separation nitrogen making device so as to reduce the energy consumption of air discharge of the air separation nitrogen making device and solve the problem of low energy efficiency of the existing air separation nitrogen making device.
In order to achieve the above object, the present utility model provides the following technical solutions:
the utility model provides a PSA air separation nitrogen generation device of low energy consumption, includes air inlet unit, adsorption equipment and supercharging device that communicates in proper order, air inlet unit includes first booster compressor, the desicator of establishing ties setting, adsorption equipment includes parallelly connected first adsorption tower, the second adsorption tower that sets up, the bottom intercommunication emptying device of first adsorption tower, second adsorption tower, supercharging device includes nitrogen buffer tank, second booster compressor, high-pressure nitrogen tank, first booster compressor is used for compressing air to first pressure, the second booster compressor is used for compressing the nitrogen gas from nitrogen buffer tank to second pressure.
Preferably, the dryer is a gas-liquid separation tank.
Preferably, the emptying device comprises an emptying pipeline and a vacuumizing pipeline which are arranged in parallel, and a vacuum pump is arranged on the vacuumizing pipeline.
Preferably, the outlet of the gas-liquid separation tank is respectively communicated with the bottoms of the first adsorption tower and the second adsorption tower, a first tower bottom valve is arranged on a pipeline which is communicated with the gas-liquid separation tank and the first adsorption tower, a second tower bottom valve is arranged on a pipeline which is communicated with the gas-liquid separation tank and the second adsorption tower, a first tower top valve is arranged on a tower top outlet pipeline of the first adsorption tower, and a second tower top valve is arranged on a tower top outlet pipeline of the second adsorption tower.
Preferably, the top outlets of the first adsorption tower and the second adsorption tower are communicated through an upper pressure equalizing pipeline, and a first pressure equalizing valve is arranged on the upper pressure equalizing pipeline.
Preferably, the blow-down line of the first adsorption tower is provided with a first blow-down valve, the blow-down line of the second adsorption tower is provided with a second blow-down valve, and the blow-down lines of the first adsorption tower and the second adsorption tower are converged and then communicated with a blow-down device.
Preferably, the bottom outlets of the first adsorption tower and the second adsorption tower are communicated through a lower pressure equalizing pipeline, and a second pressure equalizing valve is arranged on the lower pressure equalizing pipeline.
Preferably, a third vent valve is arranged on the vent pipeline, and a stop valve is arranged at the inlet of the vacuum pump.
The beneficial effects are that:
the utility model provides a low-energy-consumption PSA air separation nitrogen production device, which adopts a mode of low-pressure adsorption and nitrogen pressurization, raw material air is pressurized to a lower first pressure by a first booster for adsorption, and then the produced nitrogen is pressurized to a higher second pressure by a second booster, so that energy conservation and consumption reduction are realized under the condition that the finally obtained product nitrogen pressure is not reduced, the energy consumption can be reduced by 9.9 percent or more compared with the existing PSA air separation nitrogen production device, and obvious economic benefit and environmental benefit are realized.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model. Wherein:
FIG. 1 is a process flow diagram of examples 1-2.
FIG. 2 is a process flow diagram of comparative examples 1-2.
Reference numerals: 100. a first supercharger; 200. a dryer; 301. a first adsorption tower; 302. a second adsorption tower; 303. a nitrogen buffer tank; 401. a second supercharger; 402. a high pressure nitrogen tank; 301a, a first bottom valve; 301b, a first overhead valve; 302a, a second bottom valve; 302b, a second overhead valve; 304a, a first pressure equalizing valve; 304b, a second pressure equalizing valve; 305a, a first vent valve; 305b, a second vent valve; 305c, a third vent valve; 306a, a shut-off valve; 306b, vacuum pump.
Detailed Description
The following description of the technical solutions in the embodiments of the present utility model will be clear and complete, and it is obvious that the described embodiments are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which are derived by a person skilled in the art based on the embodiments of the utility model, fall within the scope of protection of the utility model.
The present utility model will be described in detail with reference to examples. It should be noted that, without conflict, the embodiments of the present utility model and features of the embodiments may be combined with each other.
In the description of the present utility model, a number means one or more, a number means two or more, and greater than, less than, exceeding, etc. are understood to not include the present number, and above, below, within, etc. are understood to include the present number. The description of the first and second is for the purpose of distinguishing between technical features only and should not be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated or implicitly indicating the precedence of the technical features indicated.
Furthermore, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first" and "second" may explicitly or implicitly include one or more features.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the term "connected" should be construed broadly, and for example, it may be a fixed connection or an active connection, or it may be a detachable connection or a non-detachable connection, or it may be an integral connection; may be mechanically connected, may be electrically connected, or may be in communication with each other; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements, indirect communication or interaction relationship between the two elements.
The PSA air separation nitrogen making device with low energy consumption of the present utility model is described in detail below by way of specific examples.
Example 1
As shown in fig. 1, the embodiment provides a PSA air separation nitrogen production device with low energy consumption, which comprises an air inlet device, an adsorption device and a supercharging device which are sequentially communicated, wherein the air inlet device comprises a first supercharger 100 and a dryer 200 which are arranged in series, and the air inlet device is used for pressurizing raw material air to adsorption pressure and drying; the adsorption device comprises a first adsorption tower 301 and a second adsorption tower 302 which are arranged in parallel and are used for separating nitrogen from oxygen in the compressed air, the first adsorption tower 301 and the second adsorption tower 302 work in turn, and the bottoms of the first adsorption tower 301 and the second adsorption tower 302 are communicated with a venting device and are used for exhausting residual gas in the towers; the supercharging device comprises a nitrogen buffer tank 303, a second supercharger 401 and a high-pressure nitrogen tank 402, and nitrogen discharged from the first adsorption tower 301 and the second adsorption tower 302 enters the nitrogen buffer tank 303 for temporary storage.
Specifically, the first booster 100 is a low-pressure fan for compressing air to a first pressure, the second booster 401 is a booster for compressing nitrogen from the nitrogen buffer tank 303 to a second pressure, wherein the first pressure is 0.2 to 0.5MPa, and the second pressure is equal to or greater than 0.6MPa, and under such conditions, the blowdown pressures of the first adsorption tower 301 and the second adsorption tower 302 do not exceed the first pressure, that is, 0.2 to 0.5MPa, and are lower than the second pressure of the product nitrogen, thereby achieving energy saving.
Specifically, the outlets of the gas-liquid separation tanks are respectively communicated with the bottoms of the first adsorption tower 301 and the second adsorption tower 302, a first bottom valve 301a is arranged on a pipeline communicated with the dryer 200 and the first adsorption tower 301, a second bottom valve 302a is arranged on a pipeline communicated with the gas-liquid separation tank and the second adsorption tower 302, a first top valve 301b is arranged on a tower top outlet pipeline of the first adsorption tower 301, a second top valve 302b is arranged on a tower top outlet pipeline of the second adsorption tower 302, compressed air is fed through the bottoms of the first adsorption tower 301 and the second adsorption tower 302, and separated nitrogen is discharged through the tops of the first adsorption tower 301 and the second adsorption tower 302.
The top outlets of the first adsorption tower 301 and the second adsorption tower 302 are communicated through an upper pressure equalizing pipeline, and a first pressure equalizing valve 304a is arranged on the upper pressure equalizing pipeline; the bottom outlets of the first adsorption tower 301 and the second adsorption tower 302 are communicated through a lower pressure equalizing pipeline, and a second pressure equalizing valve 304b is arranged on the lower pressure equalizing pipeline.
A first vent valve 305a is arranged on the vent line of the first adsorption tower 301, a second vent valve 305b is arranged on the vent line of the second adsorption tower 302, and the vent lines of the first adsorption tower 301 and the second adsorption tower 302 are converged and then communicated with a vent device; the emptying device comprises an emptying pipeline and a vacuumizing pipeline which are arranged in parallel, a vacuum pump 306b is arranged on the vacuumizing pipeline, a third emptying valve 305c is arranged on the emptying pipeline, and a stop valve 306a is arranged at the inlet of the vacuum pump 306 b.
In the preferred embodiment of the utility model, the dryer 200 is a gas-liquid separation tank, replaces the existing cold dryer in the PSA air separation nitrogen making device for drying, and is equivalent to saving the energy consumption of the cold dryer.
The PSA air separation nitrogen making device with low energy consumption provided in this embodiment has the following working procedures:
step one, raw material air treatment: air is compressed to a first pressure by the first booster 100, and then the compressed air is sent to the dryer 200 for gas-liquid separation to remove liquid water;
step two, adsorbing by a tower: opening a first tower bottom valve 301a and a first tower top valve 301b, sending the compressed air subjected to gas-liquid separation into a first adsorption tower 301 for adsorption to obtain product nitrogen, discharging the product nitrogen from the tower top of the first adsorption tower 301, and entering a nitrogen buffer tank 303;
step three, equalizing pressure in a tower: after the first adsorption tower 301 stops adsorbing, the first tower bottom valve 301a and the first tower top valve 301b are closed, the first pressure equalizing valve 304a is opened, the tower top of the first adsorption tower 301 and the tower top of the second adsorption tower 302 are communicated through an upper pressure equalizing pipeline to perform upper pressure equalizing, after the upper pressure equalizing is finished, the second pressure equalizing valve 304b is opened, the tower bottom of the first adsorption tower 301 and the tower bottom of the second adsorption tower 302 are communicated through a lower pressure equalizing pipeline to perform upper and lower pressure equalizing simultaneously;
step four, two-tower adsorption: after the pressure equalization is finished, the first pressure equalizing valve 304a and the second pressure equalizing valve 304b are closed, the second tower bottom valve 302a and the second tower top valve 302b are opened, compressed air subjected to gas-liquid separation is sent into the second adsorption tower 302 and adsorbed for a certain time to obtain product nitrogen, the product nitrogen is discharged from the tower top of the second adsorption tower 302 and enters the nitrogen buffer tank 303, meanwhile, the first emptying valve 305a and the third emptying valve 305c are opened, the first adsorption tower 301 is emptied, the third emptying valve 305c is closed after the emptying, the stop valve 306a and the vacuum pump 306b are opened, the first adsorption tower 301 is vacuumized, the adsorbent in the first adsorption tower 301 is regenerated, and the stop valve 306a and the vacuum pump 306b are closed after the vacuumization is finished, so that the first adsorption tower 301 is reserved;
step five, equalizing pressure of the two towers: after the second adsorption tower 302 stops adsorbing, the second bottom valve 302a and the second top valve 302b are closed, the first equalizing valve 304a is opened, the top of the second adsorption tower 302 is communicated with the top of the first adsorption tower 301, the upper equalizing valve 304b is opened after the upper equalizing is completed, the bottom of the second adsorption tower 302 is communicated with the bottom of the first adsorption tower 301, the upper equalizing and the lower equalizing are performed simultaneously, the second step is executed after the upper equalizing and the lower equalizing are completed, the second emptying valve 305b and the third emptying valve 305c are opened simultaneously, the second adsorption tower 302 is emptied, the third emptying valve 305c is closed after the emptying, the stop valve 306a and the vacuum pump 306b are opened, and the second adsorption tower 302 is vacuumized.
In the second and fourth steps, the nitrogen gas entering the nitrogen buffer tank 303 is pressurized to a second pressure by the second booster 401, and is sent to the high-pressure nitrogen tank 402 for storage.
The PSA air separation nitrogen making device with low energy consumption has the design production capacity of 1000Nm 3 And/h, for preparing nitrogen with purity of 99.5%, and actually producing 994Nm of nitrogen 3 And/h, nitrogen purity 99.5%, under this condition, first increaseThe total power consumption of the press 100, the vacuum pump 306b and the second booster 401 was 245kW, and the average power consumption was 0.246 kW.h/Nm 3 。
Example 2
The present embodiment adjusts the design throughput to 1500Nm based on embodiment 1 3 And/h for preparing nitrogen gas with purity of 99.5%, and actually producing nitrogen gas 1486Nm 3 In this condition, the total power consumption of the first booster 100, the vacuum pump 306b, and the second booster 401 was 362kW, and the average power consumption was 0.244 kW.h/Nm 3 。
Comparative example 1
This comparative example provides a PSA air separation nitrogen production apparatus, as shown in fig. 2, which is different from that of example 1 in that the air intake apparatus directly pressurizes raw material air to 0.7MPa or more using an air compressor 501, and uses a chiller dryer 502 for drying, and the air discharge apparatus has only an air discharge line, no vacuum pump 306b, no second booster 401, no nitrogen buffer tank 303, and only a high-pressure nitrogen tank 402.
The PSA air separation nitrogen production device has the design production capacity of 1000Nm 3 And/h, for preparing nitrogen gas with purity of 99.5%, and actually producing nitrogen gas 1017Nm 3 Under the working condition, the total power consumption of the air compressor 501 and the cold dryer 502 is 278kW, and the average energy consumption is 0.273 kW.h/Nm 3 。
Comparative example 2
The present comparative example was adjusted to a design throughput of 1500Nm based on comparative example 1 3 And/h for preparing nitrogen gas with purity of 99.5%, actual production of nitrogen gas 1502Nm 3 Per hour, the purity of the nitrogen is 99.5%, and under the working condition, the total power consumption of the air compressor 501 and the cold dryer 502 is 413.4kW, and the average power consumption is 0.275 kW.h/Nm 3 。
It can be seen from comparative examples 1 to 2 and comparative examples 1 to 2 that the total power consumption of the apparatus of example 1 was reduced by 33kW relative to comparative example 1 at the same production capacity and nitrogen purity, and the average power consumption was reduced by 9.9%; the total power consumption of the device of the embodiment 2 is reduced by 51.4kW compared with that of the device of the comparative example 2, the average power consumption is reduced by 11.27%, and the energy-saving effect is obvious.
The above description is only of the preferred embodiments 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 (8)
1. The utility model provides a PSA air separation nitrogen generation device of low energy consumption, includes air inlet unit, adsorption equipment and supercharging device that communicates in proper order, its characterized in that, air inlet unit includes first booster compressor, the desicator of establishing ties, adsorption equipment includes parallelly connected first adsorption tower, the second adsorption tower that sets up, the bottom intercommunication air release device of first adsorption tower, second adsorption tower, supercharging device includes nitrogen buffer tank, second booster compressor, high pressure nitrogen tank, first booster compressor is used for compressing air to first pressure, the second booster compressor is used for compressing the nitrogen gas from nitrogen buffer tank to second pressure.
2. The low energy PSA air separation nitrogen plant of claim 1, wherein the dryer is a gas-liquid separation tank.
3. The low-energy-consumption PSA air separation nitrogen production device according to claim 1, wherein the emptying device comprises an emptying pipeline and a vacuumizing pipeline which are arranged in parallel, and a vacuum pump is arranged on the vacuumizing pipeline.
4. The low-energy-consumption PSA air separation nitrogen production device according to claim 2, wherein the outlets of the gas-liquid separation tanks are respectively communicated with the bottoms of the first adsorption tower and the second adsorption tower, a first tower bottom valve is arranged on a pipeline communicating the gas-liquid separation tanks and the first adsorption tower, a second tower bottom valve is arranged on a pipeline communicating the gas-liquid separation tanks and the second adsorption tower, a first tower top valve is arranged on a tower top outlet pipeline of the first adsorption tower, and a second tower top valve is arranged on a tower top outlet pipeline of the second adsorption tower.
5. The low-energy-consumption PSA air separation nitrogen production device according to claim 4, wherein the top outlets of the first adsorption tower and the second adsorption tower are communicated through an upper pressure equalizing pipeline, and the upper pressure equalizing pipeline is provided with a first pressure equalizing valve.
6. The low-energy-consumption PSA air separation nitrogen making device according to claim 4, wherein the blow-down line of the first adsorption tower is provided with a first blow-down valve, the blow-down line of the second adsorption tower is provided with a second blow-down valve, and the blow-down lines of the first adsorption tower and the second adsorption tower are communicated with the blow-down device after being converged.
7. The low-energy-consumption PSA air separation nitrogen production device according to claim 5, wherein the bottom outlets of the first adsorption tower and the second adsorption tower are communicated through a lower pressure equalizing pipeline, and a second pressure equalizing valve is arranged on the lower pressure equalizing pipeline.
8. A low energy PSA air separation nitrogen plant according to claim 3, wherein the vent line is provided with a third vent valve and the inlet of the vacuum pump is provided with a shut-off valve.
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| CN202321633139.0U CN220214437U (en) | 2023-06-26 | 2023-06-26 | Low-energy-consumption PSA air separation nitrogen making device |
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| CN202321633139.0U CN220214437U (en) | 2023-06-26 | 2023-06-26 | Low-energy-consumption PSA air separation nitrogen making device |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
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| TR01 | Transfer of patent right |
Effective date of registration: 20240124 Address after: No. 2A, No. 13 Jingsheng South Fourth Street, Jinqiao Science and Technology Industrial Base, Zhongguancun Science and Technology Park, Tongzhou District, Beijing, 100000 Patentee after: BEIJING FEDA GERON AIR SEPARATING TECHNIQUE Ltd. Country or region after: China Address before: Room 201, 2nd Floor, Building 19, No.13 Jingsheng South Fourth Street, Economic and Technological Development Zone (Tongzhou), Tongzhou District, Beijing, 101102 Patentee before: Carbon and Technology (Beijing) Co.,Ltd. Country or region before: China |
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| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Li Yuxue Inventor after: Wang Dezhan Inventor after: Gao Yunfeng Inventor after: Qi Li Inventor before: Li Yuxue Inventor before: Wang Dezhan Inventor before: Gao Yunfeng Inventor before: Qi Li |