CN110394026A - Extensive pressure-variable adsorption step air-separating plant - Google Patents
Extensive pressure-variable adsorption step air-separating plant Download PDFInfo
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- CN110394026A CN110394026A CN201910666399.XA CN201910666399A CN110394026A CN 110394026 A CN110394026 A CN 110394026A CN 201910666399 A CN201910666399 A CN 201910666399A CN 110394026 A CN110394026 A CN 110394026A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 76
- 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 82
- 239000002808 molecular sieve Substances 0.000 claims abstract description 79
- 239000006096 absorbing agent Substances 0.000 claims abstract description 64
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 40
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000010457 zeolite Substances 0.000 claims abstract description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 29
- 238000000926 separation method Methods 0.000 claims abstract description 23
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000012163 sequencing technique Methods 0.000 claims abstract description 15
- 238000003795 desorption Methods 0.000 claims abstract description 8
- 230000018044 dehydration Effects 0.000 claims abstract description 7
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 7
- 239000002156 adsorbate Substances 0.000 claims abstract description 6
- 230000008929 regeneration Effects 0.000 claims abstract description 6
- 238000011069 regeneration method Methods 0.000 claims abstract description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 47
- 239000001301 oxygen Substances 0.000 claims description 47
- 229910052760 oxygen Inorganic materials 0.000 claims description 47
- 239000007789 gas Substances 0.000 claims description 17
- 238000010521 absorption reaction Methods 0.000 claims description 9
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 8
- 229910052744 lithium Inorganic materials 0.000 claims description 8
- 239000003463 adsorbent Substances 0.000 claims description 7
- 230000009466 transformation Effects 0.000 claims description 5
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 3
- 239000004575 stone Substances 0.000 claims description 2
- 229960004424 carbon dioxide Drugs 0.000 claims 1
- 229910002090 carbon oxide Inorganic materials 0.000 claims 1
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 9
- 239000001569 carbon dioxide Substances 0.000 abstract description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 40
- 229910052757 nitrogen Inorganic materials 0.000 description 19
- 238000000034 method Methods 0.000 description 14
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 10
- 230000006837 decompression Effects 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 8
- 238000011084 recovery Methods 0.000 description 7
- 229910052786 argon Inorganic materials 0.000 description 6
- 239000001307 helium Substances 0.000 description 6
- 229910052734 helium Inorganic materials 0.000 description 6
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 229910052754 neon Inorganic materials 0.000 description 3
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000001816 cooling Methods 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
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
- B01D53/0476—Vacuum pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
- C01B13/0259—Physical processing only by adsorption on solids
- C01B13/0262—Physical processing only by adsorption on solids characterised by the adsorbent
- C01B13/027—Zeolites
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
- C01B13/0259—Physical processing only by adsorption on solids
- C01B13/0262—Physical processing only by adsorption on solids characterised by the adsorbent
- C01B13/0274—Other molecular sieve materials
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/116—Molecular sieves other than zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/12—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40043—Purging
- B01D2259/4005—Nature of purge gas
- B01D2259/40052—Recycled product or process gas
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- 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]
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- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
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- Separation Of Gases By Adsorption (AREA)
Abstract
The present invention provides a kind of extensive pressure-variable adsorption step air-separating plant.Air pressurized fan outlet is connected by dehydration carbon dioxide removal adsorption tower with the entrance of radial zeolite molecular sieve pressure-swing absorber group, and tower group entrance is respectively arranged with sequencing valve, and is connected to drawdown pump in the entrance of radial zeolite molecular sieve pressure-swing absorber group；The outlet of radial zeolite molecular sieve pressure-swing absorber group is connected by sequencing valve with the entrance of carbon molecular sieve pressure-swing absorber group, and the outlet of tower group is connected to drawdown pump；Pressure-swing absorber group realizes that part adsorption tower adsorbing separation, partial adsorbates tower desorption and regeneration are recycled by sequencing valve.
Description
1. technical field
The present invention provides extensive pressure-variable adsorption step air-separating plant, belongs to technical field of air separation.
2. background technique
The productions such as Modern Coal-based Chemical, metallurgical industry, petroleum refining and sulfuric acid industry need to consume a large amount of oxygen, and to nitrogen
The demand of gas is smaller.In existing oxygen production method, air separating method is most economical industrial oxygenerating method.Currently, in sky
In gas separation field, cryogenic rectification method (cryogenic separation) is traditional method for producing oxygen through, and pressure swing adsorption method and membrane separation process are emerging
Method for producing oxygen through.Cryogenic rectification method technology maturation, be suitable for be mass produced high pressure oxygen and high pressure nitrogen, can obtain it is high-purity
The oxygen and nitrogen of degree, and the rate of recovery is very high, but oxygen and nitrogen output be than too small, only 21:78 (volume ratio), it is difficult to meet
The industrial process of high oxygen consumption low consumption nitrogen needs.Pressure-variable adsorption law technology is more mature, is suitable for middle and small scale production oxygen, can obtain
To the low oxygen of medium purity, the discharge of nitrogen low pressure, but influenced since the inert gases such as argon gas, helium and neon fail separation
Oxygen purity further increase and the rate of recovery is to be improved.Membrane separation process technology is being developed, and small and extra small scale is suitable for
Production oxygen, the oxygen that low concentration can be obtained, high investment and the seperation film that there is no heavy industrialization to apply.
But acetylene is produced for coal oxygen-enriched combusting, semicoke oxygen thermal method, metal oxygen thermal reduction is smelted, Heavy Oil Thermal gasifies
The production processes such as coupling and sulfuric acid industry need to consume a large amount of low oxygen, and smaller to the demand of nitrogen, using deep cooling
Separation investment is excessive with energy consumption and loss oxygen pressure potential energy, urgent need develop extensive pressure changeable adsorption air-separating technology and dress
It is standby, meet the needs of modern industry is to low pressure high-purity oxygen.
3. summary of the invention
In order to overcome deficiency existing for existing air PSA Technology, the purpose of the present invention is develop a kind of big rule
Mould pressure-variable adsorption step air-separating plant, the device can increase substantially the scale and oxygen of the separation of air pressure-variable adsorption
Purity reduces energy consumption that high pure oxygen is produced and the on a large scale dosage of the investment of oxygen processed and metal material.
Device of the present invention increases substantially the rule of air pressure-variable adsorption separation using radial pressure-swing absorber
Mould reduces high-purity oxygen separating energy consumption, is inhaled by zeolite molecular sieve pressure-swing absorber group selection absorption nitrogen, carbon molecular sieve transformation
The combination measure of attached tower group selection adsorption of oxygen considerably reduces the inert gases such as argon gas, helium and neon in oxygen and contains
Amount, to improve the purity and the rate of recovery of oxygen, while also can be obtained the nitrogen of high-purity, to realize the big rule of air
Mould, low pressure, high-purity, low energy consumption step pressure-variable adsorption separation.
Extensive pressure-variable adsorption step air-separating plant of the invention is characterized in: air pressurized fan outlet passes through dehydration
Carbon dioxide removal adsorption tower is connected with the entrance of radial zeolite molecular sieve pressure-swing absorber group, and tower group entrance is respectively arranged with program-controlled
Valve, and drawdown pump is connected in the entrance of radial zeolite molecular sieve pressure-swing absorber group；Radial zeolite molecular sieve pressure-swing absorber group
Outlet be connected with the entrance of carbon molecular sieve pressure-swing absorber group by sequencing valve, the outlet of tower group is connected to drawdown pump；Transformation is inhaled
Attached tower group realizes that part adsorption tower adsorbing separation, partial adsorbates tower desorption and regeneration are recycled by sequencing valve.
In the present invention, the zeolite molecular sieve loaded in radial zeolite molecular sieve pressure-swing absorber group is 5A molecular sieve, lithium X
One of type molecular sieve, lithium A type molecular sieve, 13X type molecular sieve and its alkali-earth metal modified molecular sieve.
In the present invention, pressure-variable adsorption separator is Vacuum Pressure Swing Adsorption or low pressure pressure swing adsorption operations.
In the present invention, carbon molecular sieve pressure-swing absorber is radial pressure-swing absorber or axial pressure-swing absorber.
In the present invention, radial pressure-swing absorber successively presses concentric circles cloth by tower wall, isolating cylinder and central tube ecto-entad
It sets, the top of isolating cylinder and central tube forms adsorption section closed upper part by adsorbent pressure plate；Tower wall and isolating cylinder are formed
The gas chamber that portion is shut, isolating cylinder and isolating cylinder form auxiliary adsorption chamber, isolating cylinder and central, tubular into adsorption chamber, bottom in central tube
Portion is arranged anti-dead zone and is oriented to cone cylinder；Tower wall bottom sides connect tangential admission mouth, and connection central tube setting in absorption tail gas outlet exists
Top of tower；Tower wall, central tube and isolating cylinder and bottom plate are tightly connected；Auxiliary adsorption chamber and adsorption chamber bottom are installed auxiliary respectively and are inhaled
Attached dose of discharge port and adsorbent discharge port.
In the present invention, the isolated oxygen-enriched air concentration of air radial direction zeolite molecular sieve pressure-swing absorber group is
50%-85%.
4. Detailed description of the invention
Fig. 1 is the device of the invention schematic diagram.
Description of symbols
1. blower, the 2. dehydration pre- adsorption towers of carbon dioxide removal, 3. radial zeolite molecular sieve pressure-swing absorbers, 4. drawdown pumps,
5. carbon molecular sieve pressure-swing absorber, 6. sequencing valves.
The device of the invention feature is described in detail below with reference to Fig. 1 and embodiment.
5. specific embodiment
Following embodiment is according to extensive pressure-variable adsorption step air-separating plant shown in FIG. 1.The tool of process described in Fig. 1
Body includes:
Filtered air is after the pressurization of blower 1, after being pre-processed by dehydration and carbon dioxide removal adsorption tower 2, it is dry and
The forced air of carbon dioxide removal first passes through radial 3 adsorbing separation of zeolite molecular sieve pressure-swing absorber, and nitrogen is by zeolite molecular sieve
Absorption, oxygen-enriched air flow out zeolite molecular sieve pressure-swing absorber 3；Switch zeolite molecular sieve pressure-swing absorber 3 by sequencing valve 6
Group, high pure nitrogen is depressurized pump 4 and desorbs from the decompression of zeolite molecular sieve pressure-swing absorber 3 to be sent outside or outlet as product, boiling
Stone molecular sieve pressure-swing absorber 3 is recycled.The oxygen-enriched air of outflow zeolite molecular sieve pressure-swing absorber 3 enters carbon molecular sieve change
Adsorption tower 5 is pressed, oxygen is adsorbed by carbon molecular sieve, and remaining nitrogen, argon gas and helium etc. flow out outside carbon molecular sieve pressure-swing absorber 5
Row；Switch carbon molecular sieve pressure-swing absorber 5 by sequencing valve 6, high-purity oxygen is depressurized pump 4 from carbon molecular sieve pressure-swing absorber
Decompression is desorbed in 5 sends outside as product, and carbon molecular sieve pressure-swing absorber 5 is recycled.Pressure-swing absorber group passes through program-controlled
Valve realizes that part adsorption tower adsorbing separation, partial adsorbates tower desorption and regeneration are recycled.
The zeolite molecular sieve loaded in the radial zeolite molecular sieve pressure-swing absorber group is 5A molecular sieve, lithium X-type point
One of sub- sieve, lithium A type molecular sieve, 13X type molecular sieve and its alkali-earth metal modified molecular sieve.
The pressure-variable adsorption separator is Vacuum Pressure Swing Adsorption or low pressure pressure swing adsorption operations.
The carbon molecular sieve pressure-swing absorber is radial pressure-swing absorber or axial pressure-swing absorber.
The radial pressure-swing absorber successively presses arranged in concentric circles by tower wall, isolating cylinder and central tube ecto-entad, every
Adsorption section closed upper part is formed by adsorbent pressure plate from the top of cylinder and central tube；Tower wall forms top with isolating cylinder and shuts
Gas chamber, isolating cylinder and isolating cylinder form auxiliary adsorption chamber, isolating cylinder and central, tubular into adsorption chamber, bottom setting in central tube
Anti- dead zone is oriented to cone cylinder；Tower wall bottom sides connect tangential admission mouth, and connection central tube in absorption tail gas outlet is arranged in top of tower；
Tower wall, central tube and isolating cylinder and bottom plate are tightly connected；Auxiliary adsorption chamber and adsorption chamber bottom are installed additional adsorbents respectively and are unloaded
Material mouth and adsorbent discharge port.
The isolated oxygen-enriched air concentration of the air radial direction zeolite molecular sieve pressure-swing absorber group is 50%-
85%.
Embodiment 1
The zeolite molecular sieve of the present embodiment processing is lithium A type molecular sieve, and pressure-variable adsorption separator is Vacuum Pressure Swing Adsorption,
Carbon molecular sieve pressure-swing absorber is radial pressure-swing absorber:
Process is as follows:
Filtered air is after the pressurization of blower 1, after being pre-processed by dehydration and carbon dioxide removal adsorption tower 2, it is dry and
The forced air of carbon dioxide removal first passes through radial 3 adsorbing separation of zeolite molecular sieve Vacuum Pressure Swing Adsorption tower, and nitrogen is by lithium A type point
Son sieve absorption, 70% oxygen-enriched air flow out zeolite molecular sieve Vacuum Pressure Swing Adsorption tower 3；Switch zeolite molecules by sequencing valve 6
Vacuum Pressure Swing Adsorption tower 3 is sieved, high pure nitrogen is depressurized pump 4 and desorbs from the decompression of zeolite molecular sieve pressure-swing absorber 3 as production
Product are sent outside, and zeolite molecular sieve Vacuum Pressure Swing Adsorption tower 3 is recycled；Flow out the 70% of zeolite molecular sieve Vacuum Pressure Swing Adsorption tower 3
Oxygen-enriched air enters radial carbon molecular sieve Vacuum Pressure Swing Adsorption tower 5, and oxygen is adsorbed by carbon molecular sieve, remaining nitrogen, argon gas and helium
5 outlet of the outflows radial direction carbon molecular sieve Vacuum Pressure Swing Adsorption such as gas tower；Switch carbon radial direction molecular sieve Vacuum Pressure Swing by sequencing valve 6 to inhale
Attached tower 5, high-purity oxygen are depressurized pump 4 and desorb outside as product from the decompression of radial carbon molecular sieve Vacuum Pressure Swing Adsorption tower 5
Decompression desorption is sent to send outside as product, radial carbon molecular sieve Vacuum Pressure Swing Adsorption tower 5 is recycled.Pressure-swing absorber group passes through journey
It controls valve and realizes that part adsorption tower adsorbing separation, partial adsorbates tower desorption and regeneration are recycled.
The results show that oxygen purity reaches 99.95% in the technique of embodiment 1, the rate of recovery is greater than 95%；Nitrogen gas purity is
95%, the rate of recovery 85%；Relative low temperature rectification method oxygen separation energy consumption reduces by 35%.
Embodiment 2
The zeolite molecular sieve of the present embodiment processing is 5A type molecular sieve, and pressure-variable adsorption separator is low pressure pressure-variable adsorption,
Carbon molecular sieve pressure-swing absorber is axial pressure-swing absorber:
Process is as follows:
Filtered air is after the pressurization of blower 1, after being pre-processed by dehydration and carbon dioxide removal adsorption tower 2, it is dry and
The forced air of carbon dioxide removal first passes through radial 3 adsorbing separation of zeolite molecular sieve low pressure pressure-swing absorber, and nitrogen is by 5A type point
Son sieve absorption, 65% oxygen-enriched air flow out zeolite molecular sieve low pressure pressure-swing absorber 3；Switch zeolite molecules by sequencing valve 6
Low pressure pressure-swing absorber 3 is sieved, high pure nitrogen is depressurized pump 4 and desorbs from the decompression of zeolite molecular sieve pressure-swing absorber 3 as production
Product are sent outside, and zeolite molecular sieve low pressure pressure-swing absorber 3 is recycled；Flow out the 65% of zeolite molecular sieve low pressure pressure-swing absorber 3
Oxygen-enriched air enters radial carbon molecular sieve low pressure pressure-swing absorber 5, and oxygen is adsorbed by carbon molecular sieve, remaining nitrogen, argon gas and helium
5 outlet of the outflows axial direction carbon molecular sieve low pressure such as gas pressure-swing absorber；Switch carbon axial element by sequencing valve 6 and sieves the suction of low pressure transformation
Attached tower 5, high-purity oxygen are depressurized pump 4 and desorb outside as product from the decompression of radial carbon molecular sieve Vacuum Pressure Swing Adsorption tower 5
Decompression desorption is sent to send outside as product, axial carbon molecular sieve low pressure pressure-swing absorber 5 is recycled.Pressure-swing absorber group passes through journey
It controls valve and realizes that part adsorption tower adsorbing separation, partial adsorbates tower desorption and regeneration are recycled.
The results show that oxygen purity reaches 99% in the technique of embodiment 1, the rate of recovery is greater than 95%；Nitrogen gas purity is
93%, the rate of recovery 80%；Relative low temperature rectification method oxygen separation energy consumption reduces by 25%.
Extensive pressure-variable adsorption step air-separating plant provided by the present invention, makes transformation using radial pressure-swing absorber
The processing capacity of absorption space division significantly improves, and can achieve 30000m3/ h or more reaches the working ability of cryogenic rectification space division；
By zeolite molecular sieve pressure-swing absorber elder generation selective absorption nitrogen, carbon molecular sieve pressure-swing absorber reselection adsorption of oxygen
The oxygen purity of air separation by PSA is greatly improved in combination measure, and it is lazy to reduce argon gas, helium and neon in oxygen etc.
Property gas content, reached the separating effect of cryogenic rectification space division, but high-purity oxygen separating energy consumption cryogenic rectification space division reduces by 25%
More than, thus realize air extensive, low pressure, high-purity, low energy consumption the separation of pressure-variable adsorption step.
Claims (6)
1. extensive pressure-variable adsorption step air-separating plant, which is characterized in that air pressurized fan outlet passes through dehydration de- two
Carbonoxide adsorption tower is connected with the entrance of radial zeolite molecular sieve pressure-swing absorber group, and tower group entrance is respectively arranged with sequencing valve, and
Drawdown pump is connected in the entrance of radial zeolite molecular sieve pressure-swing absorber group；The outlet of radial zeolite molecular sieve pressure-swing absorber group
It is connected by sequencing valve carbon molecular sieve with the entrance of pressure-swing absorber group, the outlet of tower group is connected to drawdown pump；Pressure-swing absorber group
Realize that part adsorption tower adsorbing separation, partial adsorbates tower desorption and regeneration are recycled by sequencing valve.
2. extensive pressure-variable adsorption step air-separating plant according to claim 1, which is characterized in that radial zeolite point
The zeolite molecular sieve loaded in son sieve pressure-swing absorber group is 5A molecular sieve, lithium X-type molecular sieve, lithium A type molecular sieve, 13X type point
One of son sieve and its alkali-earth metal modified molecular sieve.
3. extensive pressure-variable adsorption step air-separating plant according to claim 1, which is characterized in that pressure-variable adsorption point
It is Vacuum Pressure Swing Adsorption or low pressure pressure swing adsorption operations from device.
4. extensive pressure-variable adsorption step air-separating plant according to claim 1, which is characterized in that carbon molecular sieve becomes
Pressing adsorption tower is radial pressure-swing absorber or axial pressure-swing absorber.
5. extensive pressure-variable adsorption step air-separating plant according to claim 1, which is characterized in that radial transformation is inhaled
Attached tower successively presses arranged in concentric circles by tower wall, isolating cylinder and central tube ecto-entad, passes through suction at the top of isolating cylinder and central tube
Attached dose of pressure plate forms adsorption section closed upper part；Tower wall and isolating cylinder form the gas chamber that top is shut, isolating cylinder with tubular is isolated
At auxiliary adsorption chamber, isolating cylinder and central, tubular are at adsorption chamber, and bottom is arranged anti-dead zone and is oriented to cone cylinder in central tube；Tower wall bottom
Side connects tangential admission mouth, and connection central tube in absorption tail gas outlet is arranged in top of tower；Tower wall, central tube and isolating cylinder and bottom
Plate is tightly connected；Additional adsorbents discharge port and adsorbent discharge port are installed in auxiliary adsorption chamber and adsorption chamber bottom respectively.
6. extensive pressure-variable adsorption step air-separating plant according to claim 1, which is characterized in that air radially boils
The isolated oxygen-enriched air concentration of stone molecular sieve pressure-swing absorber group is 50%-85%.
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