CN211462639U - Large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling - Google Patents
Large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling Download PDFInfo
- Publication number
- CN211462639U CN211462639U CN201921161923.XU CN201921161923U CN211462639U CN 211462639 U CN211462639 U CN 211462639U CN 201921161923 U CN201921161923 U CN 201921161923U CN 211462639 U CN211462639 U CN 211462639U
- Authority
- CN
- China
- Prior art keywords
- pressure swing
- swing adsorption
- adsorption
- radial
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04636—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model provides a large-scale step air separation plant based on pressure swing adsorption and cryrogenic separation coupling. The outlet of the air pressurizing fan is connected with the inlet of a radial pretreatment adsorption tower group for removing carbon dioxide and drying, the inlet of the purge gas is connected with the outlet of the radial pretreatment adsorption tower group, and the inlet and the outlet of the tower group are provided with program control valves for switching the pretreatment adsorption towers; the inlet of the radial pressure swing adsorption tower set and the outlet of the radial pretreatment adsorption tower set pass through program control valves, program control valves are arranged at the inlet and the outlet of the tower set, and a decompression pump is connected to the inlet of the radial pretreatment adsorption tower set; the outlet of the radial pressure swing adsorption tower group is communicated with a compressor through a program control valve, and then is sequentially connected with a heat exchanger and a low-temperature rectification device; the decompression pump is connected with an inlet of the purge gas through a heat exchanger, and a liquid oxygen pump and a liquid nitrogen pump are installed at an inlet and an outlet of the cryogenic rectification device; the pressure swing adsorption tower group realizes adsorption separation of part of the adsorption towers and desorption regeneration recycling of part of the adsorption towers through the program control valve.
Description
1. Field of the invention
The invention provides a large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling, and belongs to the technical field of air separation.
2. Background of the invention
Modern coal chemical industry, metallurgical industry, petroleum refining, sulfuric acid industry and other production needs to consume a large amount of oxygen, and the demand for nitrogen is small. Among the existing oxygen production methods, the air separation method is the most economical industrial oxygen production method. At present, in the field of air separation, a low-temperature rectification method (cryogenic separation) is a traditional oxygen production method, and a pressure swing adsorption method and a membrane separation method are emerging oxygen production methods. The low-temperature rectification method has mature technology, is suitable for large-scale production of high-pressure oxygen and high-pressure nitrogen, can obtain high-purity oxygen and high-purity nitrogen, and has high recovery rate, but the yield ratio of the oxygen to the nitrogen is too small, and is only 21: 78 (volume ratio), it is difficult to meet the industrial process requirements of high oxygen consumption and low nitrogen consumption. The pressure swing adsorption method has mature technology, is suitable for producing oxygen on a medium and small scale, can obtain low-pressure oxygen with medium purity, and discharges nitrogen at low pressure, but because inert gases such as argon, helium, neon and the like cannot be separated, the oxygen purity is further improved, and the recovery rate needs to be improved. The membrane separation technology is being developed, is suitable for small and ultra-small scale production of oxygen, can obtain low-concentration oxygen, has higher investment and has no separation membrane for large-scale industrial application.
In order to reduce investment, a new type of oxygen generator coupling pressure swing adsorption and cryogenic rectification was used in the 90 s of the 20 th century, which was a united states company University Envirogenics Inc (UEI) engaged in cryogenic engineering equipment development. The method utilizes the advantages of simple device, compact structure, fast oxygen output time and high oxygen purity of the product of the low-temperature rectification method of the pressure swing adsorption method, overcomes the defect that the low-temperature rectification method needs to consume a large amount of expensive nonferrous metals, invests in 2/3 of a conventional unit, and has equivalent energy consumption to the conventional unit. Because the pressure swing adsorption device is arranged between the air compressor and the main heat exchanger of the cryogenic rectification, and nitrogen discharged at low pressure by the pressure swing adsorption device is compressed by the air compressor, the load and energy consumption of the air compressor cannot be reduced after the pressure swing adsorption and the cryogenic rectification are coupled, so that the energy consumption of oxygen generation is equivalent to that of a conventional unit. Therefore, the development of large-scale pressure swing adsorption-cryogenic separation combined air separation process and equipment is urgently needed to meet the requirement of modern industry on low-pressure high-purity oxygen.
3. Summary of the invention
In order to overcome the defects of the existing air pressure swing adsorption separation technology, the invention aims to develop a large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling.
The device adopted by the invention utilizes the radial pressure swing adsorption tower to improve the scale of the pressure swing adsorption separation of the air, reduce the energy consumption of the separation and reduce the oxygen output time, thereby realizing the scale matching of the pressure swing adsorption separation and the cryogenic separation; the load of a compressor, a rectifying tower and a main heat exchanger is greatly reduced through the oxygen-enriched air low-temperature rectifying device, the investment and the use amount of expensive nonferrous metal materials are reduced, and the energy consumption for separating high-pressure high-purity oxygen, nitrogen and inert gas is further reduced; the waste heat of the oxygen-enriched air compression is recovered by utilizing the low-pressure nitrogen discharged by the pressure swing adsorption, the cold energy consumption of the cryogenic separation is reduced, the problems of a blowing gas source and a heat source for heating regeneration of a drying and decarbonizing adsorption tower are solved, and the by-product nitrogen is reasonably utilized, so that the large-scale, high-purity and low-energy-consumption step separation and utilization of air are realized.
The invention relates to a large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling, which is characterized in that: the outlet of the air pressurizing fan is connected with the inlet of a radial pretreatment adsorption tower group for removing carbon dioxide and drying, the inlet of the purge gas is connected with the outlet of the radial pretreatment adsorption tower group, and the inlet and the outlet of the tower group are provided with program control valves for switching the pretreatment adsorption towers; the inlet of the radial pressure swing adsorption tower set and the outlet of the radial pretreatment adsorption tower set pass through program control valves, program control valves are arranged at the inlet and the outlet of the tower set, and a decompression pump is connected to the inlet of the radial pretreatment adsorption tower set; the outlet of the radial pressure swing adsorption tower group is communicated with a compressor through a program control valve, and then is sequentially connected with a heat exchanger and a low-temperature rectification device; the decompression pump is connected with an inlet of the purge gas through a heat exchanger, and a liquid oxygen pump and a liquid nitrogen pump are installed at an inlet and an outlet of the cryogenic rectification device; the pressure swing adsorption tower group realizes adsorption separation of part of the adsorption towers and desorption regeneration recycling of part of the adsorption towers through the program control valve.
In the invention, the adsorbent of the radial pretreatment adsorption tower group is one of zeolite molecular sieve, activated alumina, activated carbon and silica gel.
In the invention, the adsorbent used by the radial pressure swing adsorption tower group is one of a 5A molecular sieve, a lithium X type molecular sieve, a lithium A type molecular sieve, a 13X type molecular sieve and an alkaline earth metal modified molecular sieve thereof.
In the invention, the pressure swing adsorption separation device is vacuum pressure swing adsorption or low pressure swing adsorption.
In the invention, the radial pressure swing adsorption tower is sequentially arranged according to concentric circles from outside to inside by a tower wall, an isolation cylinder and a central pipe, and the top of the isolation cylinder and the top of the central pipe form an adsorption section with a closed upper part through an adsorbent pressing plate; the tower wall and the isolation cylinder form an air chamber with the upper part sealed, the isolation cylinder and the isolation cylinder form an auxiliary adsorption chamber, the isolation cylinder and the central pipe form an adsorption chamber, and the bottom in the central pipe is provided with a dead zone prevention guide cone; the side surface of the bottom of the tower wall is connected with a tangential air inlet, and an adsorbed tail gas outlet is connected with a central pipe and arranged at the top of the tower; the tower wall, the central pipe and the isolation cylinder are hermetically connected with the bottom plate; the bottom of the auxiliary adsorption chamber and the bottom of the adsorption chamber are respectively provided with an auxiliary adsorbent discharge opening and an adsorbent discharge opening.
In the invention, the concentration of the oxygen-enriched air obtained by the pressure swing adsorption separation tower set is 30-85%.
4. Description of the drawings
FIG. 1 is a schematic view of the apparatus of the present invention.
Description of the reference numerals
1. The system comprises a fan, 2, a dehydration and carbon dioxide removal pre-adsorption tower set, 3, a radial pressure swing adsorption tower set, 4, a decompression pump, 5, a compressor, 6, a program control valve, 7, a heat exchanger, 8, a low-temperature rectification device, 9, a liquid nitrogen pump and 10, a liquid oxygen pump.
The device features of the invention are described in detail below with reference to fig. 1 and the examples.
5. Detailed description of the preferred embodiments
The following examples are all in accordance with the large-scale cascaded air separation unit based on pressure swing adsorption coupled with cryogenic separation shown in fig. 1. The process illustrated in fig. 1 specifically includes:
after the filtered air is pressurized by a fan 1 and is pretreated by a dehydration and carbon dioxide removal adsorption tower set 2, the dried and carbon dioxide removal pressurized air is firstly adsorbed and separated by a radial pressure swing adsorption tower 3, 30-85% of oxygen-enriched air flows out of the radial pressure swing adsorption tower set 3, and low-pressure nitrogen is used as an intermediate product; the radial pressure swing adsorption tower set 3 is switched by the program control valve 6, the radial pressure swing adsorption tower which reaches saturated adsorption is regenerated by the pressure reduction pump 4 through pressure reduction desorption, and the radial pressure swing adsorption tower to be adsorbed adsorbs and separates air, so that the radial pressure swing adsorption tower set 3 can be recycled; 30 to 85 percent of oxygen-enriched air is pressurized to 0.5 to 0.7MPa by an oxygen-enriched compressor 5, low-pressure nitrogen enters a cryogenic rectification device 8 after heat exchange is carried out on the low-pressure nitrogen by a heat exchanger 7, liquid oxygen and liquid nitrogen are obtained by separation, and high-pressure and high-purity oxygen and nitrogen are obtained after pressurization, cold recovery and vaporization are carried out by a liquid oxygen pump 10 and a liquid nitrogen pump 9; the heated low-pressure nitrogen is used as a regeneration purge gas for the radial pretreatment adsorption tower set 2, so that the adsorption and desorption circulation of carbon dioxide and water is realized.
The adsorbent of the radial pretreatment adsorption tower group is one of zeolite molecular sieve, activated alumina, activated carbon and silica gel.
The adsorbent used by the radial pressure swing adsorption tower group is one of a 5A molecular sieve, a lithium X-type molecular sieve, a lithium A-type molecular sieve, a 13X-type molecular sieve and an alkaline earth metal modified molecular sieve thereof.
The pressure swing adsorption separation device is vacuum pressure swing adsorption or low pressure swing adsorption.
The radial pressure swing adsorption tower is characterized in that a tower wall, an isolation cylinder and a central pipe are sequentially arranged according to concentric circles from outside to inside, and the top of the isolation cylinder and the top of the central pipe form an adsorption section through an adsorbent pressing plate, and the upper part of the adsorption section is closed; the tower wall and the isolation cylinder form an air chamber with the upper part sealed, the isolation cylinder and the isolation cylinder form an auxiliary adsorption chamber, the isolation cylinder and the central pipe form an adsorption chamber, and the bottom in the central pipe is provided with a dead zone prevention guide cone; the side surface of the bottom of the tower wall is connected with a tangential air inlet, and an adsorbed tail gas outlet is connected with a central pipe and arranged at the top of the tower; the tower wall, the central pipe and the isolation cylinder are hermetically connected with the bottom plate; the bottom of the auxiliary adsorption chamber and the bottom of the adsorption chamber are respectively provided with an auxiliary adsorbent discharge opening and an adsorbent discharge opening.
The concentration of the oxygen-enriched air obtained by the pressure swing adsorption separation is 30-85%.
Example 1
The pretreatment adsorbent of this example is a molecular sieve, the pressure swing adsorption adsorbent is a lithium a type molecular sieve, and the pressure swing adsorption separation is vacuum pressure swing adsorption:
the process is as follows:
after the filtered air is pressurized by a fan 1 and is pretreated by a dehydration and carbon dioxide removal adsorption tower set 2, the dried and carbon dioxide removal pressurized air is firstly adsorbed and separated by a radial zeolite molecular sieve vacuum pressure swing adsorption tower 3, nitrogen is adsorbed by a lithium A type molecular sieve, and 70 percent of oxygen-enriched air flows out of the radial zeolite molecular sieve vacuum pressure swing adsorption tower 3; the radial vacuum pressure swing adsorption tower set 3 is switched through the program control valve 6, the radial vacuum pressure swing adsorption tower which achieves nitrogen saturation adsorption is regenerated through negative pressure desorption by the pressure reduction pump 4, low-pressure nitrogen is used as an intermediate product, the radial vacuum pressure swing adsorption tower to be adsorbed adsorbs the nitrogen, 70% of oxygen-enriched air flows out, and the radial vacuum pressure swing adsorption tower set 3 is recycled; 70 percent of the oxygen-enriched air is pressurized to 0.5-0.7MPa by an oxygen-enriched compressor 5, low-pressure nitrogen enters a cryogenic rectification device 8 after heat exchange is carried out on the low-pressure nitrogen by a heat exchanger 7, more than 99 percent of liquid oxygen, liquid nitrogen and inert gas are obtained by separation, and high-pressure and high-purity oxygen and nitrogen are obtained after pressurization, cold recovery and vaporization are carried out by a liquid oxygen pump 10 and a liquid nitrogen pump 9; the heated low-pressure nitrogen is used as the regeneration purge gas of the radial pretreatment adsorption tower group 2, so that the adsorption and desorption circulation of carbon dioxide and water is realized.
The results show that both the oxygen purity and recovery in the process of example 1 are greater than 99%; the purity of the high-pressure nitrogen is more than 99 percent, and the recovery rate is less than 10 percent; compared with the low-temperature rectification method, the energy consumption of oxygen separation is reduced by 25%, and the investment is reduced by more than 35%.
Example 2
The pretreatment adsorbent of this embodiment is a molecular sieve, the pressure swing adsorption adsorbent is a 5A type molecular sieve, and the pressure swing adsorption separation is low pressure swing adsorption:
the process is as follows:
after the filtered air is pressurized by a fan 1 and is pretreated by a dehydration and carbon dioxide removal adsorption tower set 2, the dried and carbon dioxide removal pressurized air is firstly adsorbed and separated by a radial zeolite molecular sieve low-pressure swing adsorption tower 3, nitrogen is adsorbed by a 5A type molecular sieve, and 70 percent of oxygen-enriched air flows out of the radial zeolite molecular sieve low-pressure swing adsorption tower 3; the radial low-pressure swing adsorption tower set 3 is switched through the program control valve 6, the radial low-pressure swing adsorption tower which achieves nitrogen saturation adsorption is regenerated through pressure reduction desorption by the pressure reduction pump 4, low-pressure nitrogen is used as an intermediate product, the radial low-pressure swing adsorption tower to be adsorbed adsorbs nitrogen, and 30% of oxygen-enriched air flows out, so that the radial low-pressure swing adsorption tower set 3 is recycled; 30% of the oxygen-enriched air is pressurized to 0.5-0.7MPa by an oxygen-enriched compressor 5, low-pressure nitrogen enters a cryogenic rectification device 8 after heat exchange is carried out on the air by a heat exchanger 7, more than 99% of liquid oxygen, liquid nitrogen and inert gas are obtained by separation, and high-pressure and high-purity oxygen and nitrogen are obtained after pressurization, cold recovery and vaporization are carried out by a liquid oxygen pump 10 and a liquid nitrogen pump 9; the heated low-pressure nitrogen is used as the regeneration purge gas of the radial pretreatment adsorption tower group 2, so that the adsorption and desorption circulation of carbon dioxide and water is realized.
The results show that both the oxygen purity and recovery in the process of example 2 are greater than 99%; the purity of the high-pressure nitrogen is more than 99 percent, and the recovery rate is less than 60 percent; compared with the low-temperature rectification method, the energy consumption of oxygen separation is reduced by 10%, and the investment is reduced by more than 15%.
The large-scale cascade air separation device based on the coupling of the pressure swing adsorption and the cryogenic separation utilizes the radial pressure swing adsorption tower to improve the air pressure swing adsorption separation scale by times, and can reach 30000m3More than h, the purpose of scale matching of pressure swing adsorption separation and cryogenic separation is achieved; the load of a compressor, a rectifying tower and a main heat exchanger is effectively reduced through the deep cooling separation of the oxygen-enriched air, the investment is reduced by more than 15 percent, the dosage of expensive nonferrous metal materials is reduced by 30 percent, and the high-pressure high-purity oxygen is further reducedEnergy consumption for separating nitrogen and inert gas; the low-pressure nitrogen discharged by pressure swing adsorption is utilized to recover the waste heat compressed by the oxygen-enriched air, the cold energy consumption of cryogenic separation is reduced, the problems of a blowing gas source and a heat source for heating regeneration of a drying and decarbonizing adsorption tower are solved, and the by-product nitrogen is reasonably utilized, so that the large-scale low-pressure high-purity low-energy-consumption cascade separation and utilization of air are realized.
Claims (6)
1. The large-scale cascade air separation device based on the coupling of pressure swing adsorption and cryogenic separation is characterized in that an outlet of an air pressurizing fan is connected with an inlet of a radial pretreatment adsorption tower group for removing carbon dioxide and drying, an inlet of purge gas is connected with an outlet of the radial pretreatment adsorption tower group, and program control valves for switching the pretreatment adsorption towers are arranged at an inlet and an outlet of the tower group; the inlet of the radial pressure swing adsorption tower set and the outlet of the radial pretreatment adsorption tower set pass through program control valves, program control valves are arranged at the inlet and the outlet of the tower set, and a decompression pump is connected to the inlet of the radial pretreatment adsorption tower set; the outlet of the radial pressure swing adsorption tower group is communicated with a compressor through a program control valve, and then is sequentially connected with a heat exchanger and a low-temperature rectification device; the decompression pump is connected with an inlet of the purge gas through a heat exchanger, and a liquid oxygen pump and a liquid nitrogen pump are installed at an inlet and an outlet of the cryogenic rectification device; the pressure swing adsorption tower group realizes adsorption separation of part of the adsorption towers and desorption regeneration recycling of part of the adsorption towers through the program control valve.
2. The large-scale cascaded air separation plant coupled with cryogenic separation based on pressure swing adsorption of claim 1, wherein the adsorbent of the radial pretreatment adsorption tower set is one of zeolite molecular sieve, activated alumina, activated carbon and silica gel.
3. The large-scale cascaded air separation plant based on pressure swing adsorption and cryogenic separation coupling of claim 1, wherein the adsorbent used in the radial pressure swing adsorption column set is one of a 5A molecular sieve, a lithium X molecular sieve, a lithium A molecular sieve, a 13X molecular sieve and an alkaline earth metal modified molecular sieve thereof.
4. The large-scale cascaded air separation plant coupled with cryogenic separation based on pressure swing adsorption of claim 1, wherein the pressure swing adsorption separation column bank is operated as vacuum pressure swing adsorption or low pressure swing adsorption.
5. The large-scale stepped air separation unit based on pressure swing adsorption and cryogenic separation coupling of claim 1, wherein the radial pressure swing adsorption tower is formed by arranging a tower wall, an isolation cylinder and a central pipe in a concentric circle from outside to inside, and the top of the isolation cylinder and the top of the central pipe form an upper part of an adsorption section through an adsorbent pressing plate to be closed; the tower wall and the isolation cylinder form an air chamber with the upper part sealed, the isolation cylinder and the isolation cylinder form an auxiliary adsorption chamber, the isolation cylinder and the central pipe form an adsorption chamber, and the bottom in the central pipe is provided with a dead zone prevention guide cone; the side surface of the bottom of the tower wall is connected with a tangential air inlet, and an adsorbed tail gas outlet is connected with a central pipe and arranged at the top of the tower; the tower wall, the central pipe and the isolation cylinder are hermetically connected with the bottom plate; the bottom of the auxiliary adsorption chamber and the bottom of the adsorption chamber are respectively provided with an auxiliary adsorbent discharge opening and an adsorbent discharge opening.
6. The large-scale cascaded air separation plant coupled with cryogenic separation based on pressure swing adsorption of claim 1, wherein the oxygen-enriched air concentration obtained by the pressure swing adsorption separation column set is 30-85%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921161923.XU CN211462639U (en) | 2019-07-23 | 2019-07-23 | Large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921161923.XU CN211462639U (en) | 2019-07-23 | 2019-07-23 | Large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211462639U true CN211462639U (en) | 2020-09-11 |
Family
ID=72366588
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921161923.XU Active CN211462639U (en) | 2019-07-23 | 2019-07-23 | Large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211462639U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110394026A (en) * | 2019-07-23 | 2019-11-01 | 中国石油大学(华东) | Extensive pressure-variable adsorption step air-separating plant |
| CN110394028A (en) * | 2019-07-23 | 2019-11-01 | 中国石油大学(华东) | The extensive step air separation unit coupled based on pressure-variable adsorption with cryogenic separation |
-
2019
- 2019-07-23 CN CN201921161923.XU patent/CN211462639U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110394026A (en) * | 2019-07-23 | 2019-11-01 | 中国石油大学(华东) | Extensive pressure-variable adsorption step air-separating plant |
| CN110394028A (en) * | 2019-07-23 | 2019-11-01 | 中国石油大学(华东) | The extensive step air separation unit coupled based on pressure-variable adsorption with cryogenic separation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210340328U (en) | Integrated continuous oxygen and nitrogen making device | |
| CN110394027A (en) | The step space division technique that extensive pressure-variable adsorption is coupled with cryogenic separation | |
| CN211462639U (en) | Large-scale cascade air separation device based on pressure swing adsorption and cryogenic separation coupling | |
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN110395694A (en) | Extensive energy-saving step air-separating technology | |
| CN109437234B (en) | Compound semiconductor epitaxy tail gas recycling device and method | |
| CN101441023A (en) | Energy-saving type air separation process | |
| CN211585920U (en) | Large-scale pressure swing adsorption step air separation device | |
| CN110394026A (en) | Extensive pressure-variable adsorption step air-separating plant | |
| CN201410351Y (en) | Argon purification unit | |
| CN108786371B (en) | Oxygen recovery system and method for high-temperature oxygen-enriched flue gas | |
| CN115970438A (en) | Method and device for producing hydrogen for fuel cell vehicle from ethylbenzene dehydrogenation tail gas | |
| US20230381712A1 (en) | System and method for synchronously recovering nitrogen and carbon dioxide from boiler flue gas | |
| CN115976575B (en) | Small hydrogen production system with drying and purifying functions | |
| CN218321249U (en) | Blast furnace gas carbon capture system | |
| CN217148577U (en) | System for extracting high-purity helium from low-helium BOG | |
| CN110394028A (en) | The extensive step air separation unit coupled based on pressure-variable adsorption with cryogenic separation | |
| CN215208468U (en) | Hydrogen purification system in chlor-alkali tail gas | |
| CN114917723A (en) | CO recovery from flue gas 2 Full temperature range pressure swing adsorption process | |
| CN210030042U (en) | Decarbonization gas hydrogen stripping system | |
| CN113772673A (en) | Process system and method for recovering and purifying carbon dioxide from lime kiln tail gas | |
| CN105038881B (en) | Method for continuously separating biogas by pressure swing adsorption | |
| CN106390679A (en) | Method using pressure swing adsorption to purify hydrogen produced from anaerobic fermentation of kitchen garbage | |
| CN218811566U (en) | Helium refining device capable of removing neon | |
| CN106731497B (en) | Decarbonizing and extracting N from nitric acid industrial tail gas 2 O purification device and process method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |