CN110127700A - The combined recovery device and method of carbon dioxide in flue gas, nitrogen and oxygen - Google Patents
The combined recovery device and method of carbon dioxide in flue gas, nitrogen and oxygen Download PDFInfo
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- CN110127700A CN110127700A CN201910518162.7A CN201910518162A CN110127700A CN 110127700 A CN110127700 A CN 110127700A CN 201910518162 A CN201910518162 A CN 201910518162A CN 110127700 A CN110127700 A CN 110127700A
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- carbon dioxide
- dioxide enriched
- nitrogen
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 316
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 242
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 220
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 157
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 110
- 239000003546 flue gas Substances 0.000 title claims abstract description 77
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 63
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 45
- 239000001301 oxygen Substances 0.000 title claims abstract description 45
- 238000011084 recovery Methods 0.000 title claims abstract description 16
- 239000007789 gas Substances 0.000 claims abstract description 284
- 238000000926 separation method Methods 0.000 claims abstract description 100
- 239000012466 permeate Substances 0.000 claims abstract description 62
- 230000008676 import Effects 0.000 claims abstract description 45
- 238000001179 sorption measurement Methods 0.000 claims abstract description 35
- 238000007906 compression Methods 0.000 claims description 55
- 230000006835 compression Effects 0.000 claims description 55
- 239000012528 membrane Substances 0.000 claims description 46
- 239000003517 fume Substances 0.000 claims description 41
- 239000012535 impurity Substances 0.000 claims description 26
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 15
- 229910052799 carbon Inorganic materials 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 15
- 239000007787 solid Substances 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 12
- 239000003463 adsorbent Substances 0.000 claims description 11
- 230000008859 change Effects 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 239000000047 product Substances 0.000 claims description 10
- 241000790917 Dioxys <bee> Species 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 8
- 238000006297 dehydration reaction Methods 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 8
- 238000001764 infiltration Methods 0.000 claims description 7
- 230000008595 infiltration Effects 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000000741 silica gel Substances 0.000 claims description 3
- 229910002027 silica gel Inorganic materials 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 229960004424 carbon dioxide Drugs 0.000 description 114
- 230000000694 effects Effects 0.000 description 8
- 229910002090 carbon oxide Inorganic materials 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 238000007872 degassing Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000009466 transformation Effects 0.000 description 4
- 235000019504 cigarettes Nutrition 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000013618 particulate matter Substances 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000008258 liquid foam Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- MVWDJLOUEUAWIE-UHFFFAOYSA-N O=C=O.O=C=O Chemical compound O=C=O.O=C=O MVWDJLOUEUAWIE-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- -1 steel plant Chemical compound 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- 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
- B01D53/22—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 diffusion
- B01D53/225—Multiple stage diffusion
-
- 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
- B01D53/22—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 diffusion
- B01D53/225—Multiple stage diffusion
- B01D53/226—Multiple stage diffusion in serial connexion
-
- 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
- B01D53/22—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 diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/001—Physical processing by making use of membranes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/0014—Physical processing by adsorption in solids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
- C01B2210/0062—Water
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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]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Chemical & Material Sciences (AREA)
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention provides the combined recovery device and methods of a kind of carbon dioxide in flue gas, nitrogen and oxygen.The device includes the first CO2Film separation unit, N2Pressure-variable adsorption separative unit and the 2nd CO2Film separation unit, the first CO2Film separation unit is provided with gas inlet, the first carbon dioxide enriched gas outlet and the outlet of the first high pressure non-permeate gas；N2Pressure-variable adsorption separative unit is provided with the first high pressure non-permeate gas import, the outlet of nitrogen-rich gas and the outlet of nitrogen removing gas, the first high pressure non-permeate gas import and is connected with the outlet of the first high pressure non-permeate gas；2nd CO2Film separation unit is provided with nitrogen removing gas import, the second carbon dioxide enriched gas outlet and the outlet of oxygen concentration gas, the nitrogen removing gas import and is connected with the outlet of nitrogen removing gas.Flue gas is handled using the device, the enrichment degree of carbon dioxide is higher, and nitrogen and oxygen in energy while separating flue, while realizing the resource utilization of carbon dioxide in flue gas, nitrogen and oxygen.
Description
Technical field
The present invention relates to fume treatment technical fields, in particular to a kind of carbon dioxide in flue gas, nitrogen and oxygen
Combined recovery device and method.
Background technique
Global warming is one of current environmental problem main in the world, in the various greenhouse gases for leading to climate change
In, carbon dioxide (CO2) heating up on the earth influences maximum, control CO2Discharge has become the important technology route of reply climate warming
One of.CO in combustion product gases2Discharge has the characteristics that concentration is low, stable, collection dosis neutralisata is big, is extensive emission reduction CO2Best neck
One of domain.It meanwhile also including nitrogen (N of a large amount of concentration 70% or so in flue gas2) and oxygen (O of the concentration 8%2), concentration
Lower than the concentration of nitrogen in air and oxygen, therefore, it is difficult to utilize.
The CO of high-purity2It is a kind of important industrial gasses, the CO of separation and collection2Oil and natural gas not only can be injected
The rate of oil and gas recovery is improved in field, also can be widely applied to anthropogenics, manufacture soda etc., realizes resource utilization.
CO in flue gas2Separation and collection technical application has a extensive future, and has significant environmental benefit, economic benefit and social benefit.Cause
This, separation and collection CO2Technology is the important technology for being related to coal-burning power plant's reduction of greenhouse gas discharge.
CO at present2Trapping recovery method in, membrane separation process is one of more effective method.The main original of membrane separation process
When reason is that two or more admixture of gas passes through polymeric membrane, due to solubility and diffusion of the various gases in film
The difference of coefficient causes gas with various relative permeation rates in film variant.The wherein relatively fast gas of infiltration rate, such as two
Carbonoxide, vapor, hydrogen, helium, hydrogen sulfide etc. can be preferentially enriched with by permeable membrane；And infiltration rate is relatively slow
Gas, the delay side if the gases such as methane, nitrogen, carbon monoxide in film is enriched with, so that reaching mixed gas separates it
Purpose.It is compared with other methods, UF membrane traps CO2With without chemical reaction, will not generate pollutant, device structure is compact,
Occupied area is small, start flexibly, safeguard and run the advantages that facilitating.
However, due in flue gas nitrogen and oxygen content it is higher, and the opposite infiltration speed of oxygen and nitrogen in film
Rate difference is smaller, still there is remaining CO when resulting in membrane separation process processing flue gas2More problems, this also results in CO2Enrichment
Degree is low, and nitrogen and oxygen difficulty separate, the problem more than the wasting of resources.
Summary of the invention
The main purpose of the present invention is to provide the combined recovery device of a kind of carbon dioxide in flue gas, nitrogen and oxygen and
Method, when solving in the prior art using membrane separation process processing flue gas, CO2Enrichment degree is low, nitrogen and the separation of oxygen difficulty
Problem.
To achieve the goals above, according to an aspect of the invention, there is provided a kind of carbon dioxide in flue gas, nitrogen and
The combined recovery device of oxygen comprising: the first CO2Film separation unit is provided with gas inlet, the first carbon dioxide enriched gas
Outlet and the outlet of the first high pressure non-permeate gas；N2Pressure-variable adsorption separative unit is provided with the first high pressure non-permeate gas import, nitrogen
Enriched gas outlet and the outlet of nitrogen removing gas, the first high pressure non-permeate gas import are connected with the outlet of the first high pressure non-permeate gas；With
And the 2nd CO2Film separation unit is provided with nitrogen removing gas import, the second carbon dioxide enriched gas outlet and oxygen concentration gas and goes out
Mouthful, nitrogen removes gas import and is connected with the outlet of nitrogen removing gas.
Further, device further includes the 3rd CO2Film separation unit, the 3rd CO2Film separation unit is provided with the first titanium dioxide
The import of carbon enrichment gas and CO2Product gas outlet, the first carbon dioxide enriched gas import and the first carbon dioxide enriched gas export phase
Even.
Further, the 3rd CO2Film separation unit is additionally provided with the outlet of the second high pressure non-permeate gas, the first high pressure non-permeate
Gas import and the first high pressure non-permeate gas are exported to be connected by impermeable gas transfer pipeline, the second high pressure non-permeate gas export with it is non-
Letter shoot road is permeated to be connected.
Further, the first carbon dioxide enriched gas import and the first carbon dioxide enriched gas outlet pass through carbon dioxide richness
Gas collection transfer pipeline is connected, and the second carbon dioxide enriched gas outlet is connected with carbon dioxide enriched letter shoot road.
Further, device further includes the first compression unit, and the air inlet where gas inlet is arranged in the first compression unit
On pipeline, for being compressed to flue gas.
Further, device further includes the first fume treatment unit, and the setting of the first fume treatment unit is single in the first compression
On the pipeline that member is connected with gas inlet, for removing solid impurity and liquid impurity in compressed flue gas.
Further, the first fume treatment unit includes the first cooler, the first demister and the first mistake being arranged in series
Filter.
Further, device further includes the second compression unit, and the setting of the second compression unit is conveyed in carbon dioxide enriched gas
On pipeline, and the second carbon dioxide enriched gas outlet is connected to the carbon dioxide enriched letter shoot road of the second compression unit upstream
On, the second compression unit is used for the dioxy to the first carbon dioxide enriched gas outlet and the second carbon dioxide enriched gas outlet discharge
Change carbon enrichment gas to be compressed.
Further, device further includes the second fume treatment unit, and the setting of the second fume treatment unit is single in the second compression
Carbon dioxide enriched letter shoot road between member and the first carbon dioxide enriched gas import, the second fume treatment unit are used for
Remove the moisture in compressed carbon dioxide enriched gas.
Further, the second fume treatment unit includes the second cooler, the second demister and the second mistake being arranged in series
Filter, alternatively, the second fume treatment unit is dehydration device.
Further, the second carbon dioxide enriched gas outlet passes through carbon dioxide enriched gas branch pipe and carbon dioxide enriched gas
Transfer pipeline is connected；Device further includes third compression unit, and third compression unit is arranged on carbon dioxide enriched gas branch pipe.
Further, device further includes third fume treatment unit, and the setting of third fume treatment unit removes gas in nitrogen
The water in nitrogen removing gas on the pipeline that import is connected with the outlet of nitrogen removing gas, for removing nitrogen removing gas outlet discharge
Point.
Further, third fume treatment unit includes the third cooler, third demister and third mistake being arranged in series
Filter, alternatively, third fume treatment unit is dehydration device.
According to another aspect of the present invention, the combined recovery of a kind of carbon dioxide in flue gas, nitrogen and oxygen is additionally provided
Method comprising following steps: flue gas is subjected to first time CO2Membrane separation obtains the carbon dioxide enriched gas of first part
With the first high pressure non-permeate gas；The separation of nitrogen pressure-variable adsorption is carried out to the first high pressure non-permeate gas, obtains nitrogen-rich gas and nitrogen
Qi exhaustion degasification；And nitrogen removing gas is subjected to second of CO2Membrane separation obtains oxygen concentration gas and second part dioxy
Change carbon enrichment gas.
Further, the process conditions in the separation process of nitrogen pressure-variable adsorption are as follows: treatment temperature is -10~120 DEG C, place
Reason pressure is 0.10~1.50MPa of absolute pressure, adsorbent be one of molecular sieve, silica gel, active carbon and its modified adsorbent or
It is a variety of.
Further, the carbon dioxide enriched gas of first part and the carbon dioxide enriched gas of second part are mixed to form dioxy
Change carbon enrichment gas, method further includes carrying out third time CO to carbon dioxide enriched gas2Membrane separation, to obtain CO2Product gas
Step.
Further, third time CO2The second high pressure non-permeate gas is also obtained during membrane separation, method further includes
Second high pressure non-permeate gas is subjected to the step of nitrogen pressure-variable adsorption separates together with the first high pressure non-permeate gas.
Further, first time CO is being carried out2Before the process of membrane separation, method further includes carrying out first to flue gas
In the step of the step of second compression, preferably the first second compression, gas pressure is made to be greater than absolute pressure 0.11MPa.
Further, after the step of the first second compression, method further includes being handled compressed flue gas to remove
The step of solid impurity and liquid impurity therein；Preferably, the step of handling compressed flue gas includes: successively right
Compressed flue gas carries out cooling, demisting and filtering.
Further, third time CO is being carried out2Before the process of membrane separation, method further includes to carbon dioxide enriched
Gas carries out the step of the second second compression；It is preferred that making gas pressure be greater than absolute pressure 0.11MPa in the step of the second second compression.
Further, the carbon dioxide enriched gas of first part and the carbon dioxide enriched gas of second part are being mixed to form two
Before the step of carbonoxide enriched gas, method further includes the steps that compressing the carbon dioxide enriched gas of second part；It is preferred that
In the step of compressing to the carbon dioxide enriched gas of second part, gas pressure is made to be greater than absolute pressure 0.11MPa.
Further, after the step of the second second compression, method further includes in the compressed carbon dioxide enriched gas of removal
The step of moisture；Preferably, the step of removing moisture in compressed carbon dioxide enriched gas includes, successively to compressed two
Carbonoxide enriched gas carries out cooling, demisting and filtering, alternatively, being carried out dehydrating to compressed carbon dioxide enriched gas.
Further, before the step of nitrogen pressure-variable adsorption separates, method further includes in the first high pressure non-permeate gas of removal
The step of moisture；Preferably, the step of removing moisture in the first high pressure non-permeate gas includes: successively to the first high pressure non-permeate gas
Cooling, demisting and filtering are carried out, alternatively, being carried out dehydrating to the first high pressure non-permeate gas.
The present invention provides the combined recovery devices of a kind of carbon dioxide in flue gas, nitrogen and oxygen comprising the first CO2
Film separation unit, N2Pressure-variable adsorption separative unit and the 2nd CO2Film separation unit, the first CO2Film separation unit be provided with flue gas into
Mouth, the first carbon dioxide enriched gas outlet and the outlet of the first high pressure non-permeate gas；N2Pressure-variable adsorption separative unit is provided with first
The import of high pressure non-permeate gas, the outlet of nitrogen-rich gas and the outlet of nitrogen removing gas, the first high pressure non-permeate gas import and first high
Impermeable gas outlet is pressed to be connected；2nd CO2Film separation unit is provided with nitrogen removing gas import, the second carbon dioxide enriched gas goes out
Mouth and the outlet of oxygen concentration gas, the nitrogen removing gas import are connected with the outlet of nitrogen removing gas.
Flue gas is handled using above-mentioned apparatus, the enrichment degree of carbon dioxide is higher, and nitrogen that can simultaneously in separating flue
Gas and oxygen, while realizing the resource utilization of carbon dioxide in flue gas, nitrogen and oxygen.
Detailed description of the invention
The accompanying drawings constituting a part of this application is used to provide further understanding of the present invention, and of the invention shows
Examples and descriptions thereof are used to explain the present invention for meaning property, does not constitute improper limitations of the present invention.In the accompanying drawings:
Fig. 1 shows the combined recovery of carbon dioxide in flue gas according to an embodiment of the present, nitrogen and oxygen
Schematic device.
Wherein, the above drawings include the following reference numerals:
10, the first CO2Film separation unit；20,N2Pressure-variable adsorption separative unit；30, the 2nd CO2Film separation unit；40,
Three CO2Film separation unit；50, the first compression unit；60, the first fume treatment unit；70, the second compression unit；80, the second cigarette
Gas disposal unit；90, third compression unit；100, third fume treatment unit.
Specific embodiment
It should be noted that in the absence of conflict, the features in the embodiments and the embodiments of the present application can phase
Mutually combination.The present invention will be described in detail below with reference to the accompanying drawings and embodiments.
The application is described in further detail below in conjunction with specific embodiment, these embodiments should not be understood as limitation originally
Apply for range claimed.
As described in background technology part, when handling flue gas using membrane separation process in the prior art, there are CO2Enrichment
The problem of degree is low, nitrogen and oxygen difficulty separate.
To solve the above-mentioned problems, the present invention provides the combined recoveries of a kind of carbon dioxide in flue gas, nitrogen and oxygen
Device, as shown in Figure 1 comprising the first CO2Film separation unit 10, N2Pressure-variable adsorption separative unit 20 and the 2nd CO2UF membrane list
Member 30, the first CO2Film separation unit 10 is provided with gas inlet, the first carbon dioxide enriched gas outlet and the first high pressure non-permeate
Gas outlet；N2It is de- that pressure-variable adsorption separative unit 20 is provided with the first high pressure non-permeate gas import, the outlet of nitrogen-rich gas and nitrogen
Degasification outlet, the first high pressure non-permeate gas import are connected with the outlet of the first high pressure non-permeate gas；2nd CO2Film separation unit 30 is set
It is equipped with nitrogen removing gas import, the second carbon dioxide enriched gas outlet and the outlet of oxygen concentration gas, nitrogen and removes gas import and nitrogen
Qi exhaustion degasification outlet is connected.
Different from traditional membrane separation process, present invention employs the device processing that UF membrane and pressure-variable adsorption separation combine
Flue gas.Specifically:
Utilize the first CO2Film separation unit 10 can carry out CO to flue gas first2Membrane separation is needed because of carbon capture
Exhaust gas volumn is huge, utilizes the first CO2Film separation unit 10 advantageously reduces land occupation, and simplifies treatment process.In the first CO2Film point
Under processing from unit 10, most of carbon dioxide in flue gas forms the first carbon dioxide enriched gas from first by seperation film
Carbon dioxide enriched gas outlet discharge, oxygen, nitrogen and a small amount of carbon dioxide then form the discharge of the first high pressure non-permeate gas.
Secondly, utilizing N2Pressure-variable adsorption separative unit 20 can carry out transformation suction to the nitrogen in the first high pressure non-permeate gas
Fufen from.N2Pressure-variable adsorption separative unit 20 is poor for the adsorption rate of nitrogen and oxygen, carbon dioxide based on adsorbent
Different separation carries out nitrogen adsorption.And it experienced the first CO2The processing of film separation unit 10, most of carbon dioxide quilt in flue gas
It separates, the gas concentration lwevel in the first high pressure non-permeate gas significantly reduces, this is advantageous for reducing high concentration titanium dioxide
Influence of the carbon to nitrogen pressure-variable adsorption.It being compared with other methods, pressure-variable adsorption has without chemical reaction, will not generate pollutant,
It is easy to operate, safeguard and run the advantages that facilitating.
Through N2After the processing of pressure-variable adsorption separative unit 20, the nitrogen in the first high pressure non-permeate gas is by separation removal, oxygen
The nitrogen removing gas formed with a small amount of carbon dioxide enters the 2nd CO2Film separation unit 30 carries out further CO2UF membrane,
So as to obtain the higher oxygen concentration gas of purity and；The carbon dioxide enriched gas of another part.
Flue gas is handled using the above-mentioned device of the present invention, while realizing the resource of carbon dioxide in flue gas, nitrogen and oxygen
Change recycling.
In a preferred embodiment, N2Pressure-variable adsorption separative unit 20 includes N2Psa unit and N2Desorption
Unit, N2Psa unit is used for N2Carry out pressure-variable adsorption, N2Desorption unit is used for the adsorbent after absorption carbon dioxide
It is desorbed.Specific desorption mode can be the modes such as to vacuumize.
In a kind of preferred embodiment, as shown in Figure 1, device further includes the 3rd CO2Film separation unit 40, the 3rd CO2Film
Separative unit 40 is provided with the first carbon dioxide enriched gas import and CO2Product gas outlet, the first carbon dioxide enriched gas import
It is connected with the first carbon dioxide enriched gas outlet.Utilize the 3rd CO2Film separation unit 40 can be further to the first carbon dioxide
Carbon dioxide in enriched gas is enriched with, and carbon dioxide product gas is formed.
In a kind of preferred embodiment, the first CO2Film separation unit 10, the 2nd CO2Film separation unit 30 and the 3rd CO2
Membrane module in film separation unit 40 is separately selected from hollow-fibre membrane, rolled film or plate membrane.Here " independently
Ground is selected from " refer to the first CO2Film separation unit 10, the 2nd CO2Film separation unit 30 and the 3rd CO2In film separation unit 40
Membrane module each is selected from one of above-mentioned three kinds of membrane modules, and three may be the same or different between each other.Preferably,
The material of membrane module is high molecular polymer organic material.Compared to inoranic membrane as membrane module, had using high molecular polymer
Its processing technology of the membrane module of machine material formation is simple, and manufacturing cost is lower, for the CO in large-scale separation flue gas2It being capable of pole
The earth reduces project investment cost.Meanwhile in certain flue gases such as coal-fired plant flue gas carbon dioxide concentration it is lower (about
12%), the selectivity of organic film is higher, can further increase CO2Separation and recovery rate and amount of collected.
In a preferred embodiment, the 3rd CO2Film separation unit 40 is additionally provided with the second high pressure non-permeate gas and goes out
Mouthful, the first high pressure non-permeate gas import is exported with the first high pressure non-permeate gas to be connected by impermeable gas transfer pipeline, and second is high
The outlet of pressure impermeable gas is connected with impermeable gas transfer pipeline.It in this way can be by the 3rd CO2What film separation unit 40 was separated
High pressure non-permeate gas and the first CO2The high pressure non-permeate gas that film separation unit 10 is separated carries out N together2Pressure-variable adsorption separation,
To the nitrogen and oxygen in further recovered flue gas.
In order to further recycle carbon dioxide, in a preferred embodiment, the first carbon dioxide enriched gas import
It is connected with the first carbon dioxide enriched gas outlet by carbon dioxide enriched letter shoot road, the second carbon dioxide enriched gas outlet
It is connected with carbon dioxide enriched letter shoot road.It in this way can be by the 2nd CO2The carbon dioxide that film separation unit 30 is separated
Enriched gas and the first CO2The carbon dioxide enriched gas that film separation unit 10 is separated carries out further UF membrane together, rich
Collect carbon dioxide, obtains carbon dioxide product gas.
In a preferred embodiment, device further includes the first compression unit 50, and the setting of the first compression unit 50 exists
On air inlet pipeline where gas inlet, for being compressed to flue gas.It can be the first CO using the first compression unit 502Film
The CO of separative unit 102Infiltration further provides for pressure-driven.And it should be noted that is vacuumized compared to being utilized in per-meate side
Or the method for purging decompression, the present invention is capable of providing enough pressure differences using the first compression unit 50, enough to drive
CO2Through film, especially organic film, to further increase CO2The trapping rate of recovery.Similarly, it is preferable that above-mentioned apparatus is also wrapped
The second compression unit 70 is included, the second compression unit 70 is arranged on carbon dioxide enriched letter shoot road, and the second carbon dioxide
Enriched gas outlet is connected to the carbon dioxide enriched letter shoot road of 70 upstream of the second compression unit, and the second compression unit 70 is used
It is pressed in the carbon dioxide enriched gas of the first carbon dioxide enriched gas outlet and the second carbon dioxide enriched gas outlet discharge
Contracting.
In flue gas other than carbon dioxide, oxygen and nitrogen, also carries some solid impurities (particulate matter) and liquid is miscellaneous
Matter (moisture), in order to reduce these solid impurities and liquid impurity to the first CO2Especially there is seperation film in film separation unit 10
The influence of machine seperation film, in a preferred embodiment, above-mentioned apparatus further include the first fume treatment unit 60, the first cigarette
Gas disposal unit 60 is arranged on the pipeline that the first compression unit 50 is connected with gas inlet, for removing in compressed flue gas
Solid impurity and liquid impurity.Seperation film, especially organic separation membrane are easy by the pollution of the solid impurities such as particulate matter, to wet
Degree requires and the higher problem of temperature requirement, can reduce these influences to the greatest extent using the first fume treatment unit 60, thus into
The treatment effect of one step improvement flue gas.
In one embodiment, the solid impurity and liquid impurity in filter removal flue gas be can use.More preferably
Ground, the first fume treatment unit 60 include the first cooler, the first demister and the first filter being arranged in series.Utilize first
Cooler can further condense the liquid in flue gas, then through the first demister removal wherein condensable liquid foam,
Droplet and the solids that may be entrained finally recycle first filter that can further remove possible entrainment in flue gas
The objectionable impurities such as fine liquid.Meanwhile the first cooler is set and also helps control flue-gas temperature, to further increase first
CO2The operation stability of film separation unit 10.
In a kind of preferred embodiment, the first fume treatment unit 60 further includes heat exchanger, and heat exchanger is provided with to be added
Hot import and outlet to be heated, import to be heated are connected with the outlet of first filter, and outlet to be heated and gas inlet phase
Even.The flue gas after impurity can will be removed in this way to carry out heat exchange in heat exchanger and be heated, and make it away from dew point and constant
The operation temperature of system.
In a kind of preferred embodiment, device further includes the second fume treatment unit 80, the second fume treatment unit 80
It is arranged on the carbon dioxide enriched letter shoot road between the second compression unit 70 and the first carbon dioxide enriched gas import, the
Two fume treatment units 80 are used to remove the moisture in compressed carbon dioxide enriched gas.Be conducive to further increase in this way
Three CO2The operation stability of film separation unit 40.Preferably, which is characterized in that the second fume treatment unit 80 includes that series connection is set
The second cooler, the second demister and the second filter set, alternatively, the second fume treatment unit 80 is dehydration device.Second
Cooler, the second demister and the second filter have similar with the first cooler above, the first demister and first filter
Effect.Also it can use dehydration device and remove moisture in carbon dioxide enriched gas.
Similarly, preferably the second fume treatment unit 80 further includes heat exchanger, and heat exchanger is provided with import to be heated and to be added
Heat outlet, import to be heated are connected with the outlet of the second filter, and outlet to be heated and the 3rd CO2The of film separation unit 40
One carbon dioxide enriched gas import is connected.
Through the 3rd CO2The pressure for the carbon dioxide enriched gas that film separation unit 40 is separated is often slightly lower, a kind of excellent
In the embodiment of choosing, the second carbon dioxide enriched gas outlet is defeated by carbon dioxide enriched gas branch pipe and carbon dioxide enriched gas
Pipeline is sent to be connected；Device further includes third compression unit 90, and third compression unit is arranged on carbon dioxide enriched gas branch pipe.
In a preferred embodiment, device further includes third fume treatment unit 100, third fume treatment unit
100 are arranged on the pipeline that nitrogen removing gas import is connected with the outlet of nitrogen removing gas, for removing nitrogen removing gas outlet row
The moisture in nitrogen removing gas out.Be conducive to improve the 2nd CO in this way2The operation stability of film separation unit 30.Preferably,
Third fume treatment unit 100 includes third cooler, third demister and the third filter being arranged in series, alternatively, third
Fume treatment unit 100 is dehydration device.Third cooler, third demister and third filter and above the first cooler,
First demister and first filter have similar effect.
It is preferred that third fume treatment unit 100 further includes heat exchanger, heat exchanger be provided with import to be heated and it is to be heated go out
Mouthful, import to be heated is connected with the outlet of third filter, and outlet to be heated and the 2nd CO2The nitrogen of film separation unit 30 is de-
Degasification import is connected.
Above-mentioned apparatus is not only suitable for the processing of coal-fired plant flue gas, is also applied for the low-concentration flue gas such as steel plant, cement plant
The separation and collection of middle carbon dioxide, oxygen and nitrogen.
According to another aspect of the present invention, the combined recovery of a kind of carbon dioxide in flue gas, nitrogen and oxygen is additionally provided
Method comprising following steps: flue gas is subjected to first time CO2Membrane separation obtains the carbon dioxide enriched gas of first part
With the first high pressure non-permeate gas；The separation of nitrogen pressure-variable adsorption is carried out to the first high pressure non-permeate gas, obtains nitrogen-rich gas and nitrogen
Qi exhaustion degasification；And nitrogen removing gas is subjected to second of CO2Membrane separation obtains oxygen concentration gas and second part dioxy
Change carbon enrichment gas.Using method provided by the invention, by CO2UF membrane and nitrogen pressure-variable adsorption combine, while realizing flue gas
The resource utilization of middle carbon dioxide, nitrogen and oxygen.
In order to further increase the effect of nitrogen pressure-variable adsorption separation, in a preferred embodiment, nitrogen transformation
Process conditions in adsorption separation process are as follows: treatment temperature is -10~120 DEG C, and processing pressure is 0.10~1.50MPa of absolute pressure
(A), adsorbent is the one or more of active carbon, silica gel, molecular sieve and its modified adsorbent.Preferably, nitrogen pressure-variable adsorption
The step of separation includes: to carry out the suction of nitrogen transformation to the first high pressure non-permeate gas under above-mentioned process conditions using above-mentioned adsorbent
It is attached, it obtains nitrogen removing gas and is adsorbed with the adsorbent of nitrogen；In the state of vacuumizing, the above-mentioned suction for being adsorbed with nitrogen is desorbed
Attached dose, obtain nitrogen-rich gas.
In order to further increase the concentration effect of carbon dioxide, in a preferred embodiment, by first part two
Carbonoxide enriched gas and the carbon dioxide enriched gas of second part are mixed to form carbon dioxide enriched gas, and the above method further includes to two
Carbonoxide enriched gas carries out third time CO2Membrane separation, to obtain CO2The step of product gas.
In order to further increase the concentration effect of nitrogen and oxygen, in a preferred embodiment, third time CO2
The second high pressure non-permeate gas is also obtained during membrane separation, method further includes that the second high pressure non-permeate gas and first is high
Pressure impermeable gas carries out the step of nitrogen pressure-variable adsorption separation together.
In a preferred embodiment, first time CO is being carried out to flue gas2Before the process of membrane separation, method
Further include the steps that carrying out the first second compression to flue gas, the step of preferably the first second compression in, so that gas pressure is greater than 0.10MPa
(A).It in this way can be first time CO2The CO of membrane separation2Infiltration further provides for pressure-driven.Similarly, it is preferable that into
Row third time CO2Before the process of membrane separation, method further includes that the step of the second second compression is carried out to carbon dioxide enriched gas
Suddenly；It is preferred that making gas pressure be greater than 0.11MPa (A) in the step of the second second compression.It is highly preferred that by first part's dioxy
Before the step of change carbon enrichment gas and the carbon dioxide enriched gas of second part are mixed to form carbon dioxide enriched gas, method further includes
The step of carbon dioxide enriched gas of second part is compressed；It is preferred that the carbon dioxide enriched gas of second part is compressed
In step, gas pressure is made to be greater than 0.11MPa (A).
In flue gas other than carbon dioxide, oxygen and nitrogen, also carries some solid impurities (particulate matter) and liquid is miscellaneous
Matter (moisture), in order to reduce these solid impurities and liquid impurity to first time CO2The influence of membrane separation, a kind of preferred
Embodiment in, the step of the first second compression after, method further includes being handled compressed flue gas to remove wherein
Solid impurity and liquid impurity the step of；Preferably, the step of handling compressed flue gas includes: successively to compression
Flue gas afterwards carries out cooling, demisting and filtering.Flue gas first be cooled after, by demisting can by liquid foam condensable in flue gas,
Droplet and the solids that may be entrained removal.Then can further be removed by filtration treatment may entrainment in unstripped gas
The objectionable impurities such as fine liquid.In short, can substantially more remove liquid impurity, the solid in flue gas using aforesaid way
The impurity such as particle, to further increase the trapping effect of carbon dioxide.Meanwhile it can also be effective by carrying out cooling to flue gas
Flue-gas temperature is controlled, to further increase the operation stability of seperation film especially organic separation membrane.
In a preferred embodiment, after the step of the second second compression, method further includes removal compressed two
In carbonoxide enriched gas the step of moisture；Preferably, include the step of moisture in the compressed carbon dioxide enriched gas of removal, according to
It is secondary that cooling, demisting and filtering are carried out to compressed carbon dioxide enriched gas, alternatively, to compressed carbon dioxide enriched gas into
Row dehydration.
In a preferred embodiment, before the step of nitrogen pressure-variable adsorption separates, method further includes removal first
In high pressure non-permeate gas the step of moisture；Preferably, the step of removing moisture in the first high pressure non-permeate gas includes: successively to the
One high pressure non-permeate gas carries out cooling, demisting and filtering, alternatively, being carried out dehydrating to the first high pressure non-permeate gas.
Beneficial effects of the present invention are further illustrated by the following examples:
Embodiment 1
To certain steel plant, flue gas is tested, and accounts device shown in Fig. 1 of the present invention for low concentration CO in flue gas2
The trapping of technique and oxygen and nitrogen recycling treatment effect.
Wherein, hollow-fibre membrane made of organic film material is all made of in carbon dioxide film separation unit；Nitrogen transformation is inhaled
Fufen from the step of in, process conditions are as follows: treatment temperature is 30 degrees Celsius, and processing pressure is 0.47MPa (A), and adsorbent is
Carbon molecular sieve.
The results are shown in Table 1 for mass balance:
Table 1
It can be seen from the above description that the above embodiments of the present invention realized the following chievements: can by table 1
Know, when the throughput of the blast furnace flue gas of processing is 10000Nm3/ h, CO2Content 27.35%, O2Content 6.23%, N2Content
When 65.99%, in the treatment process in the present embodiment, second segment CO2Film separation unit permeates gas (product gas) flow
628Nm3/ h, CO2Content is promoted to 90.11% from 27.35%.N2Pressure-swing absorption apparatus come out adsorbed gas flow be
6393.40Nm3/ h, N2Content is promoted to 97.10% from 65.99%.Third section film separation unit permeating airflow amount is 921Nm3/
H, CO2Content is promoted to 98.50% by 40.18%.O2Content is promoted to 36.43% from 6.23%.Cigarette is handled using above-mentioned apparatus
The enrichment degree of gas, carbon dioxide is higher, and nitrogen and oxygen that can simultaneously in separating flue, while realizing dioxy in flue gas
Change the resource utilization of carbon, nitrogen and oxygen.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, made any to repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (23)
1. the combined recovery device of a kind of carbon dioxide in flue gas, nitrogen and oxygen characterized by comprising
First CO2Film separation unit (10) is provided with gas inlet, the first carbon dioxide enriched gas outlet and the non-infiltration of the first high pressure
Vent outlet；
N2Pressure-variable adsorption separative unit (20) is provided with the first high pressure non-permeate gas import, the outlet of nitrogen-rich gas and nitrogen removing
Gas outlet, the first high pressure non-permeate gas import are connected with the first high pressure non-permeate gas outlet；And
2nd CO2It is rich to be provided with nitrogen removing gas import, the second carbon dioxide enriched gas outlet and oxygen for film separation unit (30)
Gas collection outlet, the nitrogen removing gas import are connected with the outlet of nitrogen removing gas.
2. the apparatus according to claim 1, which is characterized in that described device further includes the 3rd CO2Film separation unit (40),
3rd CO2Film separation unit (40) is provided with the first carbon dioxide enriched gas import and CO2Product gas outlet, described first
Carbon dioxide enriched gas import is connected with the described first carbon dioxide enriched gas outlet.
3. the apparatus of claim 2, which is characterized in that the 3rd CO2Film separation unit (40) is additionally provided with second
The outlet of high pressure non-permeate gas, the first high pressure non-permeate gas import pass through impermeable with the first high pressure non-permeate gas outlet
Letter shoot road is connected, and the second high pressure non-permeate gas outlet is connected with the impermeable gas transfer pipeline.
4. the apparatus of claim 2, which is characterized in that the first carbon dioxide enriched gas import and described first
The outlet of carbon dioxide enriched gas is connected by carbon dioxide enriched letter shoot road, the second carbon dioxide enriched gas outlet with
The carbon dioxide enriched letter shoot road is connected.
5. device according to any one of claim 1 to 4, which is characterized in that described device further includes the first compression list
First (50), first compression unit (50) is arranged on the air inlet pipeline where the gas inlet, for carrying out to flue gas
Compression.
6. device according to claim 5, which is characterized in that described device further includes the first fume treatment unit (60),
First fume treatment unit (60) is arranged on the pipeline that first compression unit (50) is connected with the gas inlet,
For removing solid impurity and liquid impurity in the compressed flue gas.
7. device according to claim 6, which is characterized in that first fume treatment unit (60) includes being arranged in series
The first cooler, the first demister and first filter.
8. device according to claim 4, which is characterized in that described device further includes the second compression unit (70), described
Second compression unit (70) is arranged on the carbon dioxide enriched letter shoot road, and the second carbon dioxide enriched gas goes out
Mouth is connected to the carbon dioxide enriched letter shoot road of the second compression unit (70) upstream, and second compression is single
First (70) are used for the dioxy to the described first carbon dioxide enriched gas outlet and the described second carbon dioxide enriched gas outlet discharge
Change carbon enrichment gas to be compressed.
9. device according to claim 8, which is characterized in that described device further includes the second fume treatment unit (80),
Second fume treatment unit (80) setting second compression unit (70) and the first carbon dioxide enriched gas into
The carbon dioxide enriched letter shoot road between mouthful, second fume treatment unit (80) are compressed for removing
Moisture in the carbon dioxide enriched gas.
10. device according to claim 9, which is characterized in that second fume treatment unit (80) includes that series connection is set
The second cooler, the second demister and the second filter set, alternatively, second fume treatment unit (80) is dehydration dress
It sets.
11. the device according to any one of claim 8 to 10, which is characterized in that the second carbon dioxide enriched gas
Outlet is connected by carbon dioxide enriched gas branch pipe with the carbon dioxide enriched letter shoot road；Described device further includes third
Compression unit (90), the third compression unit are arranged on the carbon dioxide enriched gas branch pipe.
12. device according to any one of claim 1 to 4, which is characterized in that described device further includes at third flue gas
It manages unit (100), third fume treatment unit (100) setting removes gas in nitrogen removing gas import and the nitrogen
The moisture in nitrogen removing gas on the connected pipeline in outlet, for removing the nitrogen removing gas outlet discharge.
13. device according to claim 12, which is characterized in that the third fume treatment unit (100) includes series connection
Third cooler, third demister and the third filter of setting, alternatively, the third fume treatment unit (100) is dehydration
Device.
14. the combined reclamation method of a kind of carbon dioxide in flue gas, nitrogen and oxygen, which is characterized in that the method includes with
Lower step:
The flue gas is subjected to first time CO2Membrane separation obtains the carbon dioxide enriched gas of first part and the non-infiltration of the first high pressure
It is ventilative；
The separation of nitrogen pressure-variable adsorption is carried out to the first high pressure non-permeate gas, obtains nitrogen-rich gas and nitrogen removing gas；With
And
Nitrogen removing gas is subjected to second of CO2Membrane separation, obtains oxygen concentration gas and second part carbon dioxide is rich
Gas collection.
15. according to the method for claim 14, which is characterized in that the technique item in the nitrogen pressure-variable adsorption separation process
Part is as follows: treatment temperature be -10~120 DEG C, processing pressure be 0.10~1.50MPa of absolute pressure, adsorbent be molecular sieve, silica gel,
One of active carbon and its modified adsorbent are a variety of.
16. method according to claim 14 or 15, which is characterized in that by the carbon dioxide enriched gas of the first part and
The carbon dioxide enriched gas of second part is mixed to form carbon dioxide enriched gas, and the method also includes to the carbon dioxide
Enriched gas carries out third time CO2Membrane separation, to obtain CO2The step of product gas.
17. according to the method for claim 16, which is characterized in that the third time CO2It is also obtained during membrane separation
Second high pressure non-permeate gas, the method also includes by the second high pressure non-permeate gas and the first high pressure non-permeate gas
The step of carrying out nitrogen pressure-variable adsorption separation together.
18. method described in any one of 4 to 17 according to claim 1, which is characterized in that carrying out the first time CO2Film point
Before the process of processing, the method also includes carrying out the first second compression to the flue gas, the preferably described first time
In the step of compression, gas pressure is made to be greater than absolute pressure 0.11MPa.
19. according to the method for claim 18, which is characterized in that after the step of first second compression, the method
Further include the steps that handling the compressed flue gas to remove solid impurity and liquid impurity therein；Preferably,
The step of handling the compressed flue gas includes: successively to carry out cooling, demisting and mistake to the compressed flue gas
Filter.
20. according to the method for claim 16, which is characterized in that carrying out the third time CO2The process of membrane separation
Before, the method also includes carrying out the second second compression to the carbon dioxide enriched gas；It is preferred that described second is pressed
In the step of contracting, gas pressure is made to be greater than 0.11MPa (A).
21. according to the method for claim 20, which is characterized in that by the carbon dioxide enriched gas of the first part and institute
Before stating the step of carbon dioxide enriched gas of second part is mixed to form the carbon dioxide enriched gas, the method also includes right
The step of carbon dioxide enriched gas of second part is compressed；It is preferred that being carried out to the carbon dioxide enriched gas of the second part
In the step of compression, gas pressure is made to be greater than 0.11MPa (A).
22. according to the method for claim 20, which is characterized in that after the step of second second compression, the method
Further include the steps that moisture in the compressed carbon dioxide enriched gas of removal；Preferably, the compressed dioxy is removed
The step of changing moisture in carbon enrichment gas includes successively carrying out cooling, demisting and mistake to the compressed carbon dioxide enriched gas
Filter, alternatively, being carried out dehydrating to the compressed carbon dioxide enriched gas.
23. method according to claim 14 or 15, which is characterized in that the nitrogen pressure-variable adsorption separate the step of it
Before, the method also includes removing moisture in the first high pressure non-permeate gas；Preferably, first high pressure is removed
Include: the step of moisture in impermeable gas cooling, demisting and filtering successively are carried out to the first high pressure non-permeate gas, alternatively,
The first high pressure non-permeate gas is carried out dehydrating.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111089373A (en) * | 2019-12-18 | 2020-05-01 | 盐城工业职业技术学院 | Novel ventilation system |
| CN112657313A (en) * | 2020-12-16 | 2021-04-16 | 淮北市森化碳吸附剂有限责任公司 | Pressure swing adsorption treatment process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107899376A (en) * | 2017-11-27 | 2018-04-13 | 北京集封环能科技有限责任公司 | The joint of carbon dioxide in flue gas and nitrogen traps retracting device and method |
| CN210150733U (en) * | 2019-06-14 | 2020-03-17 | 林千果 | Combined recovery device for carbon dioxide, nitrogen and oxygen in flue gas |
-
2019
- 2019-06-14 CN CN201910518162.7A patent/CN110127700A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107899376A (en) * | 2017-11-27 | 2018-04-13 | 北京集封环能科技有限责任公司 | The joint of carbon dioxide in flue gas and nitrogen traps retracting device and method |
| CN210150733U (en) * | 2019-06-14 | 2020-03-17 | 林千果 | Combined recovery device for carbon dioxide, nitrogen and oxygen in flue gas |
Non-Patent Citations (1)
| Title |
|---|
| 罗兰多·M.A.罗克-马勒布等, 国防工业出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111089373A (en) * | 2019-12-18 | 2020-05-01 | 盐城工业职业技术学院 | Novel ventilation system |
| CN112657313A (en) * | 2020-12-16 | 2021-04-16 | 淮北市森化碳吸附剂有限责任公司 | Pressure swing adsorption treatment process |
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Application publication date: 20190816 |
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