CN107899376A - The joint of carbon dioxide in flue gas and nitrogen traps retracting device and method - Google Patents
The joint of carbon dioxide in flue gas and nitrogen traps retracting device and method Download PDFInfo
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- CN107899376A CN107899376A CN201711208089.0A CN201711208089A CN107899376A CN 107899376 A CN107899376 A CN 107899376A CN 201711208089 A CN201711208089 A CN 201711208089A CN 107899376 A CN107899376 A CN 107899376A
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- gas
- flue gas
- carbon dioxide
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 187
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 186
- 239000003546 flue gas Substances 0.000 title claims abstract description 157
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 156
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 93
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 238000000034 method Methods 0.000 title claims abstract description 60
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 38
- 239000007789 gas Substances 0.000 claims abstract description 179
- 238000000926 separation method Methods 0.000 claims abstract description 129
- 239000012466 permeate Substances 0.000 claims abstract description 37
- 230000008676 import Effects 0.000 claims abstract description 35
- 239000000779 smoke Substances 0.000 claims abstract description 32
- 239000000047 product Substances 0.000 claims abstract description 13
- 239000012528 membrane Substances 0.000 claims description 102
- 239000012535 impurity Substances 0.000 claims description 79
- 239000007788 liquid Substances 0.000 claims description 43
- 239000007787 solid Substances 0.000 claims description 37
- 238000007906 compression Methods 0.000 claims description 13
- 230000006835 compression Effects 0.000 claims description 12
- 230000018044 dehydration Effects 0.000 claims description 11
- 238000006297 dehydration reaction Methods 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 10
- 239000000835 fiber Substances 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 4
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 claims description 3
- 229960004424 carbon dioxide Drugs 0.000 description 70
- 230000008569 process Effects 0.000 description 14
- 238000001764 infiltration Methods 0.000 description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 238000001914 filtration Methods 0.000 description 7
- 230000008595 infiltration Effects 0.000 description 7
- 238000004064 recycling Methods 0.000 description 7
- 230000008901 benefit Effects 0.000 description 6
- 239000011368 organic material Substances 0.000 description 6
- 235000019504 cigarettes Nutrition 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 229910002090 carbon oxide Inorganic materials 0.000 description 4
- 239000004568 cement Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 229920000642 polymer Polymers 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- -1 steel plant Chemical compound 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 241000790917 Dioxys <bee> Species 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 239000008258 liquid foam Substances 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-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
- 238000000429 assembly Methods 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 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
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 235000015110 jellies Nutrition 0.000 description 1
- 239000008274 jelly Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000006467 substitution reaction Methods 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
- B01D53/22—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
- B01D53/228—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 characterised by specific membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
- C01B21/0438—Physical processing only by making use of membranes
- C01B21/0444—Physical processing only by making use of membranes characterised by the membrane
-
- 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
-
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention provides a kind of joint of carbon dioxide in flue gas and nitrogen trapping retracting device and method.The device includes smoke processing system, the first CO2Film separation unit, the 2nd CO2Film separation unit and N2Film separation unit；Smoke processing system is provided with processing import and processing exports, and smoke processing system is used to handle flue gas；First CO2Film separation unit is provided with the first air inlet, the first carbon dioxide enriched gas outlet and the outlet of the first high pressure non-permeate gas, and the first air inlet is connected with processing outlet；2nd CO2Film separation unit is provided with the second air inlet, the outlet of carbon dioxide product gas and the outlet of the second high pressure non-permeate gas, and the second air inlet is connected with the first carbon dioxide enriched gas outlet；N2Film separation unit is provided with the outlet of nitrogen-rich gas, and N2The air inlet of film separation unit is connected with the outlet of the first high pressure non-permeate gas.Above device has the high enrichment degree to carbon dioxide, and can recycle nitrogen, avoids the wasting of resources.
Description
Technical field
The present invention relates to gas recovery techniques field, in particular to a kind of carbon dioxide in flue gas and the connection of nitrogen
Close trapping retracting device and method.
Background technology
Global warming is one of main environmental problem in the world at present, is causing the various greenhouse gases of 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.The CO that mankind's activity produces2Discharge most parts and come from coal fired power generation, CO in the combustion tail gas of coal-burning power plant2Discharge
Have the characteristics that concentration is low, stable, collection dosis neutralisata is big, be extensive emission reduction CO2One of optimal field.Meanwhile in tail gas also
Include the nitrogen (N a large amount of concentration 70% or so2), concentration is less than the concentration of nitrogen in air, and 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 can not only be injected
Field, improves the rate of oil and gas recovery, can also be widely used in anthropogenics, manufacture soda etc., realize recycling.
Coal-burning power plant CO2Separation and collection technology has a extensive future, and has significant environmental benefit, economic benefit and social benefit.Cause
This, separation and collection CO2Technology is to be related to the important technology of 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 of the various gases in film and diffusion
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 in film if the gases such as methane, nitrogen, carbon monoxide is enriched with, so that reaching mixed gas separates it
Purpose.Compared with other methods, UF membrane trapping CO2With without chemical reaction, will not produce pollutant, device structure is compact,
Floor space is small, start flexibly, safeguard and run the advantages that facilitating.
However, for coal-burning power plant, since the exhaust gas volumn of its generation is huge, it is desirable to the CO of trapping2Amount is also huge, for list
A power plant, usual amount of collected need 1,000,000 tons/year, cause to utilize membrane separation process processing coal-burning power plant's cigarette in prior art processes
Still there are the problem of enrichment degree is low, complex process during gas.And solid particle polluter and liquid impurity in coal-fired plant flue gas
Content is higher, and easily membrane separation assemblies are polluted or even are damaged, have impact on UF membrane efficiency.Meanwhile to CO2Caught
During collection, a large amount of nitrogen that are enriched with can also be wasted.
The content of the invention
It is a primary object of the present invention to provide a kind of carbon dioxide in flue gas and nitrogen joint trap retracting device and
Method, to solve in the prior art using the CO in membrane separation process trapping recovered flue gas2When existing enrichment degree is low, technique is multiple
Miscellaneous, UF membrane inefficient, and largely it is enriched with the problem of nitrogen is wasted.
To achieve these goals, according to an aspect of the invention, there is provided a kind of carbon dioxide in flue gas and nitrogen
Joint trapping retracting device, it includes：Smoke processing system, smoke processing system is provided with processing import and processing exports,
Smoke processing system is used to handle flue gas, to remove the liquid impurity and solid impurity in flue gas；First CO2UF membrane
Unit, the first CO2Film separation unit is provided with the first air inlet, the first carbon dioxide enriched gas outlet and the first high pressure non-permeate
Gas exports, and the first air inlet is connected with processing outlet；2nd CO2Film separation unit, the 2nd CO2Film separation unit is provided with second
Air inlet, the outlet of carbon dioxide product gas and the outlet of the second high pressure non-permeate gas, the second air inlet and first carbon dioxide enriched
Gas outlet is connected；And N2Film separation unit, N2Film separation unit is provided with the outlet of nitrogen-rich gas, and N2Film separation unit
Air inlet is connected with the outlet of the first high pressure non-permeate gas.
Further, device further includes：3rd CO2Film separation unit, the 3rd CO2Film separation unit is provided with the 3rd air inlet
Mouth, the 3rd carbon dioxide enriched gas outlet and offgas outlet, the 3rd air inlet are connected with the outlet of the second high pressure non-permeate gas；Gas
Mixer, gas mixer is arranged on the pipeline that the first carbon dioxide enriched gas outlet is connected with the second air inlet, and gas
Mixer, which is additionally provided with, returns return air inlet, returns return air inlet and is connected with the 3rd carbon dioxide enriched gas outlet.
Further, the first CO2Film separation unit, the 2nd CO2Film separation unit and the 3rd CO2Film in film separation unit
Component is separately selected from hollow-fibre membrane, rolled film or plate membrane.
Further, device further includes：First compressor, the first compressor are connected with processing import；Second compressor, the
Two compressors are arranged on the pipeline that gas mixer is connected with the second air inlet.
Further, smoke processing system includes filter, and the import of filter is processing import, and the outlet of filter is
Processing outlet.
Further, smoke processing system further includes：Cooler, the import of cooler is processing import, and cooler goes out
Mouth is connected with the import of filter.
Further, smoke processing system further includes demister, and the import of demister is connected with the outlet of cooler, demisting
The outlet of device is connected with the import of filter.
Further, device further includes dehydration device, and gas inlet and dehydration exhanst gas outlet are provided with dehydration device, is taken off
Water exhanst gas outlet is connected with the import of the first compressor.
According to another aspect of the present invention, the joint trapping recycling side of a kind of carbon dioxide in flue gas and nitrogen is additionally provided
Method, it includes：Flue gas is handled, to remove the liquid impurity and solid impurity in flue gas, obtains processing flue gas；Will processing
Flue gas carries out first time CO2Membrane separation, obtains the first carbon dioxide enriched gas and the first high pressure non-permeate gas；By the one or two
Carbonoxide enriched gas carries out second of CO2Membrane separation, obtains carbon dioxide product gas and the second high pressure non-permeate gas；And
N is carried out to the first high pressure non-permeate gas2Membrane separation, obtains nitrogen-rich gas.
Further, after the step of obtaining the second high pressure non-permeate gas, method is further comprising the steps of：To the second high pressure
Impermeable gas carries out third time CO2Membrane separation, obtains the 3rd carbon dioxide enriched gas and tail gas；And by the 3rd titanium dioxide
Carbon enrichment gas is returned and mixed with the first carbon dioxide enriched gas, to carry out second of CO2Membrane separation.
Further, first time CO2Membrane separation, second of CO2Membrane separation and third time CO2Membrane separation
The step of in the membrane module that uses separately be selected from hollow-fibre membrane, rolled film or plate membrane.
Further, before the step of flue gas being handled to remove liquid impurity and solid impurity, method further includes
The step of first compression is carried out to flue gas；It is preferred that in the step of first compression, gas pressure is set to be more than 0.3MPa.
Further, the first carbon dioxide enriched gas and optional 3rd carbon dioxide enriched gas are subjected to second of CO2
Before the step of membrane separation, method is further included the first carbon dioxide enriched gas and optional 3rd carbon dioxide enriched gas
The step of carrying out second-compressed；Preferably, in the step of second-compressed, gas pressure is made to be more than 0.3MPa.
Further, flue gas is handled to include the step of removing liquid impurity and solid impurity：Flue gas is carried out
Filtering, obtains processing flue gas.
Further, before the step of being filtered to flue gas, flue gas is handled to remove liquid impurity and consolidate
The step of body impurity, further includes：Flue gas is cooled down, condenses liquid impurity, obtains cooled flue gas；Cooled flue gas is carried out
Filtering, obtains processing flue gas.
Further, before the step of being filtered to cooled flue gas, flue gas is handled to remove liquid impurity
And the step of solid impurity, further includes：Demisting is carried out to cooled flue gas, obtains demisting flue gas；And demisting flue gas was carried out
Filter, obtains processing flue gas.
Further, before the step of flue gas being carried out first compression, the above method, which further includes, carries out at dehydration flue gas
The step of reason.
Apply the technical scheme of the present invention, there is provided the joint trapping recycling dress of a kind of carbon dioxide in flue gas and nitrogen
Put, it includes smoke processing system, the first CO2Film separation unit, the 2nd CO2Film separation unit and N2Film separation unit；Flue gas
Processing system is provided with processing import and processing exports, and smoke processing system is used to handle flue gas, to remove in flue gas
Liquid impurity and solid impurity；First CO2Film separation unit is provided with the first air inlet, the first carbon dioxide enriched gas outlet
And first high pressure non-permeate gas outlet, the first air inlet with processing export is connected；2nd CO2Film separation unit be provided with second into
Gas port, the outlet of carbon dioxide product gas and the outlet of the second high pressure non-permeate gas, the second air inlet and the first carbon dioxide enriched gas
Outlet is connected；N2Film separation unit is provided with the outlet of nitrogen-rich gas, and N2The air inlet of film separation unit with the first high pressure is non-oozes
Vent outlet is connected.
Using above device, before membrane separation is carried out to coal-fired plant flue gas, first with smoke processing system energy
Liquid impurity (such as moisture and some fluid organic materials) and the solid impurity in flue gas are enough removed, to prevent liquid impurity and solid
The presence of impurity influences the efficiency of UF membrane.After the treatment, flue gas enters the first CO2Film separation unit and the 2nd CO2UF membrane
Unit, using successively membrane separating process is enriched with the carbon dioxide in flue gas twice.Above reason can significantly improve two
The enrichment degree of carbonoxide.Meanwhile utilize N2First high pressure non-permeate gas can also be exported the gas of discharge by film separation unit
UF membrane is further carried out to recycle nitrogen.In addition, the carbon dioxide in recovered flue gas is trapped using the device of the invention,
Technique is simple, without the further enrichment process such as follow-up chemisorbed, be not only suitable in coal-fired plant flue gas carbon dioxide and
The combined separation of nitrogen, is also applied for the combined separation of carbon dioxide and nitrogen in the low-concentration flue gas such as steel plant, cement plant and catches
Collection.
Brief description of the drawings
The accompanying drawings which form a part of this application are used for providing a further understanding of the present invention, and of the invention shows
Meaning property embodiment and its explanation are used to explain the present invention, do not form inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 shows a kind of trapping retracting device schematic diagram of carbon dioxide in flue gas of embodiment according to the present invention.
Wherein, above-mentioned attached drawing is marked including the following drawings：
10th, smoke processing system；11st, cooler；12nd, demister；13rd, filter；14th, heat exchanger；20th, the first CO2Film
Separative element；30th, the 2nd CO2Film separation unit；40th, the 3rd CO2Film separation unit；50th, gas mixer；60th, the first compression
Machine；70th, the second compressor；80、N2Film separation unit.
Embodiment
It should be noted that in the case where there is no conflict, the feature in embodiment and embodiment in the application can phase
Mutually combination.Below with reference to the accompanying drawings and the present invention will be described in detail in conjunction with the embodiments.
The application is described in further detail below in conjunction with specific embodiment, these embodiments are it is not intended that limit this
Apply for scope claimed.
As background section is described, the CO in recovered flue gas is trapped using membrane separation process in the prior art2When
There are the problem of enrichment degree is low, complex process.
In order to solve the problems, such as this, the present invention provides a kind of trapping retracting device of carbon dioxide in flue gas, as inscribed 1 institute
Show, it includes smoke processing system 10, the first CO2Film separation unit 20, the 2nd CO2Film separation unit 30 and N2UF membrane list
Member 80, smoke processing system 10 is provided with processing import and processing exports, and smoke processing system 10 is used to handle flue gas,
To remove the liquid impurity and solid impurity in flue gas；First CO2Film separation unit 20 is provided with the first air inlet, the first dioxy
Change the outlet of carbon enrichment gas and the outlet of the first high pressure non-permeate gas, the first air inlet is connected with processing outlet；2nd CO2UF membrane list
Member 30 is provided with the second air inlet, the outlet of carbon dioxide product gas and the outlet of the second high pressure non-permeate gas, the second air inlet and the
One carbon dioxide enriched gas outlet is connected；N2Film separation unit 80 is provided with the outlet of nitrogen-rich gas, and N2Film separation unit 80
Air inlet is connected with the outlet of the first high pressure non-permeate gas.
Using the above device of the present invention, before membrane separation is carried out to coal-fired plant flue gas, at flue gas
Reason system 10 can remove liquid impurity (such as moisture and some fluid organic materials) and solid impurity in flue gas, to prevent liquid
The presence of impurity and solid impurity influences the efficiency of UF membrane.After the treatment, flue gas enters the first CO220 He of film separation unit
2nd CO2Film separation unit 30, using successively membrane separating process is enriched with the carbon dioxide in flue gas twice.Above reason
The enrichment degree of carbon dioxide can be significantly improved.Meanwhile utilize N2Film separation unit 80 can also be by the first high pressure non-permeate
The gas of gas outlet discharge further carries out UF membrane to recycle nitrogen.In addition, trapped and recycled using the device of the invention
Carbon dioxide in flue gas, technique is simple, without the further enrichment process such as follow-up chemical absorbing or absorption, is not only suitable for
The separation of carbon dioxide in coal-fired plant flue gas, is also applied for point of carbon dioxide in the low-concentration flue gas such as steel plant, cement plant
From trapping.
Above-mentioned first CO2Film separation unit 20, the 2nd CO230 and the 3rd CO of film separation unit2Film in film separation unit 40
Component is to be easy to penetrate CO2And it is not easy to penetrate N2With the gas separation membrane of oxygen；N2Membrane module in film separation unit 80 is
To oxygen permeable to N2Impervious gas separation membrane.In specific operating process, flue gas is (through dedusting, desulphurization denitration
Combustion product gases after processing) enter after smoke processing system 10 removes liquid impurity and solid impurity, enter from the first air inlet
First CO2Film separation unit 20, obtains the on high-tension side impermeable gas of first segment and low-pressure side after first time membrane separation
Permeate gas.The infiltration gas of first segment low-pressure side is rich in CO2, enter the second air inlet after the first carbon dioxide enriched gas outlet discharge
Mouthful, utilize the 2nd CO2Film separation unit 30 carries out second of membrane separation, obtains second segment impermeable gas and infiltration gas.Its
CO in middle second segment infiltration gas2Purity it is higher, can be directly as CO2Product gas, which is sent outside, to be collected.First segment is on high-tension side
Impermeable gas contains N2Concentration is higher, this portion gas is passed through N2Film separation unit 80 can by nitrogen therein and oxygen separation,
Nitrogen is discharged and is collected from impermeable side, as nitrogen-rich gas, sold after can further compressing.N2UF membrane
Predominant gas in the infiltration gas of unit 80 is that oxygen also has some a small amount of CO2, oxygen content be higher than air in oxygen content,
Utilize CO2Film can further UF membrane CO2And oxygen, obtain the CO of high-purity2With oxygen product gas.
Partial CO 2 is carried in above-mentioned second segment impermeable gas, in order to further recycle this partial CO 2,
In a kind of preferred embodiment, as shown in Figure 1, above device further includes the 3rd CO2Film separation unit 40 and gas mixer
50, the 3rd CO2Film separation unit 40 is provided with the 3rd air inlet, the 3rd carbon dioxide enriched gas exports and offgas outlet, and the 3rd
Air inlet is connected with the outlet of the second high pressure non-permeate gas；Gas mixer 50 is arranged on the first carbon dioxide enriched gas outlet and the
On the pipeline of two air inlets connection, and gas mixer 50 is additionally provided with and returns return air inlet, returns return air inlet and the 3rd titanium dioxide
The outlet of carbon enrichment gas is connected.So second segment impermeable gas can be subjected to further membrane separation, by titanium dioxide therein
Carbon further after enrichment, is back in gas mixer 50, and then the gas with the first carbon dioxide enriched gas outlet discharge mixes
Enter the 2nd CO after conjunction together2Film separation unit 30 is handled.The work of such multistage UF membrane and separator pumparound
Skill is combined, and can further improve the enrichment degree of carbon dioxide in flue gas, improves the rate of recovery, increases amount of collected.
In a kind of preferred embodiment, above-mentioned first CO2Film separation unit 20, the 2nd CO2Film separation unit 30 and the 3rd
CO2Membrane module in film separation unit 40 is separately selected from hollow-fibre membrane, rolled film or plate membrane.Here " difference
Independently selected from " refer to the first CO2Film separation unit 20, the 2nd CO230 and the 3rd CO of film separation unit2Film separation unit 40
In membrane module each be selected from one kind in above-mentioned three kinds of membrane modules, three may be the same or different between each other.It is preferred that
Ground, the material of membrane module is high molecular polymer organic material.Compared to inoranic membrane as membrane module, using high molecular polymer
Its processing technology of the membrane module of organic material formation is simple, and manufacture cost is relatively low, for separating and recovering coal-burning power plant's cigarette on a large scale
CO in gas2Project investment cost can greatly be reduced.Meanwhile coal-fired plant flue gas concentration is very low (about 12%), has
The selective higher of machine film, can further improve CO2Separation and recovery rate and amount of collected.Special instruction, the present invention pass through
Organic film, which is efficiently solved, using smoke processing system 10 is easily subject to the pollution of the solid impurities such as particulate matter, to humidity requirement and temperature
The problem of more demanding is spent, can more effectively give play to its own advantages.
In a kind of preferred embodiment, above device further includes the first compressor 60 and the second compressor 70, the first pressure
Contracting machine 60 is connected with processing import；Second compressor 70 is arranged on the pipeline that gas mixer 50 is connected with the second air inlet.
Can be the first CO using the first compressor 602The CO of film separation unit 202Infiltration further provides for pressure-driven；Similarly, utilize
Second compressor 70 can be the 2nd CO2The CO of film separation unit 302Infiltration further provides for pressure-driven.And need what is illustrated
It is to utilize the first compressor 60 and the second compression using the method for vacuumizing or purging decompression, the present invention compared in per-meate side
Machine 70 is capable of providing enough pressure differentials, to drive enough CO2Through film, particularly organic film, so as to further improve
CO2The trapping rate of recovery.
The effect of smoke processing system 10 is the liquid impurity and solid impurity removed in flue gas, avoids it from influencing organic film
Separative efficiency.In a preferred embodiment, as shown in Figure 1, smoke processing system 10 includes filter 13, filter 13
Import for processing import, and the outlet of filter 13 for processing export.It can so be removed by filtration treatment in flue gas
Liquid impurity and solid impurity.
It is highly preferred that as shown in Figure 1, smoke processing system 10 further includes：Cooler 11, the import of cooler 11 is processing
Import, the outlet of cooler 11 are connected with the import of filter 13.Flue gas by the cooling of cooler 11 can by flue gas, into
Entering filter 13 can further be condensed with liquid, then be removed by filter 13, so as to further remove impurity.
It is further preferred that smoke processing system 10 includes being sequentially connected with the cooler 11 of setting, demister 12 and filtering
Device 13, the import of cooler 11 is processing import, and the outlet of filter 13 exports for processing.It is cold that flue gas enters cooler 11
, can be by condensable liquid foam, droplet and the solids removal that may be entrained in flue gas into demister 12 after jelly.Then
The objectionable impurities such as the fine liquid that may be carried secretly in unstripped gas can be further removed into filter 13.In short, utilize the cigarette
Gas processing system 10 can substantially more remove the impurity such as liquid impurity in flue gas, solid particle, so as to further improve
The trapping effect of carbon dioxide.Meanwhile set cooler 11 effectively to control flue-gas temperature, to further improve organic film
Operation stability.
Preferably, above-mentioned filter 13 is condensation type filter.So it can further remove raw material using condensation process
The objectionable impurities such as the fine liquid that may be carried secretly in gas, while can also be by the fume collection after filtering in case subsequent treatment.
In a kind of preferred embodiment, smoke processing system 10 further includes heat exchanger 14, and heat exchanger 14 is provided with to be added
Hot import and outlet to be heated, import to be heated are connected with the outlet of filter 13, and outlet to be heated is processing outlet.So
It can will remove the flue gas after impurity to carry out heat exchange in heat exchanger 14 and be heated, make it away from dew point simultaneously constant system
Operation temperature.
In a kind of preferred embodiment, above device further includes the first compressor 60 and the second compressor 70, the first pressure
Contracting machine 60 is connected with processing import, and the second compressor 70 is arranged on the pipeline that gas mixer 50 is connected with the second air inlet；
First compressor 60 is additionally provided with exhaust branch and air inlet branch road, and heat exchanger 14 is additionally provided with thermal medium inlet and thermal medium goes out
Mouthful, thermal medium inlet is connected with exhaust branch, and thermal medium outlet is connected with air inlet branch road.In this way, through compressed cigarette for the first time
Qi leel is handled into cooler 11 into two-way, enters heat exchanger 14 as heating medium all the way, with completing removal of impurities all the way
Flue gas exchanges heat.After the completion of heat exchange, handled as cooler 11 is returned to after the high pressure flue gas cool-down of heating medium.
This can further utilize the heat of flue gas itself, reduce process energy consumption, make trapping process more environmentally protective.Specifically, it is cold
But the type of cooling of machine 11 is water cooling.
In order to further remove the liquid impurity carried in flue gas, in a kind of preferred embodiment, above device also wraps
Dehydration device is included, gas inlet and dehydration exhanst gas outlet are provided with dehydration device, is dehydrated exhanst gas outlet and the first compressor 60
Import be connected.So can first it be carried out dehydrating before flue gas enters smoke processing system 10.
According to another aspect of the present invention, the joint trapping recycling side of a kind of carbon dioxide in flue gas and nitrogen is additionally provided
Method, it includes：Flue gas is handled, to remove the liquid impurity and solid impurity in flue gas, obtains processing flue gas；Will processing
Flue gas carries out first time CO2Membrane separation, obtains the first carbon dioxide enriched gas and the first high pressure non-permeate gas；By the one or two
Carbonoxide enriched gas carries out second of CO2Membrane separation, obtains carbon dioxide product gas and the second high pressure non-permeate gas；And
N is carried out to the first high pressure non-permeate gas2Membrane separation, obtains nitrogen-rich gas.
Using the above method of the present invention, before membrane separation is carried out to coal-fired plant flue gas, first remove in flue gas
Liquid impurity (such as moisture and some fluid organic materials) and solid impurity, can prevent the presence of liquid impurity and solid impurity
Influence the efficiency of UF membrane.After the treatment, flue gas enters first time CO2Membrane separation and second of CO2Membrane separation,
Utilize successively CO twice2Membrane separation is enriched with the carbon dioxide in flue gas.Above reason can significantly improve dioxy
Change the enrichment degree of carbon.Meanwhile utilize N2First high pressure non-permeate gas can also further be carried out UF membrane by membrane separation
To recycle nitrogen.In addition, using the carbon dioxide in the method trapping recovered flue gas of the present invention, technique is simple, without after
The further enrichment process such as continuous chemical absorbing or absorption, is not only suitable for the separation of carbon dioxide in coal-fired plant flue gas, also fits
Separation and collection for carbon dioxide in the low-concentration flue gas such as steel plant, cement plant.
In a kind of preferred embodiment, after the step of obtaining the second high pressure non-permeate gas, method further includes following step
Suddenly：Third time CO is carried out to the second high pressure non-permeate gas2Membrane separation, obtains the 3rd carbon dioxide enriched gas and tail gas；With
And the 3rd carbon dioxide enriched gas is returned and is mixed with the first carbon dioxide enriched gas, to carry out second of CO2At UF membrane
Reason.Such multistage UF membrane is combined with the technique of circulating reflux, can further improve the enrichment of carbon dioxide in flue gas
Degree, improves the rate of recovery, increases amount of collected.
In a kind of preferred embodiment, first time CO2Membrane separation, second of CO2Membrane separation and third time
CO2The membrane module used in the step of membrane separation is separately selected from hollow-fibre membrane, rolled film or plate membrane, and film
The material of component is high molecular polymer organic material.It is organic using high molecular polymer compared to inoranic membrane as membrane module
Its processing technology of the membrane module of material formation is simple, and manufacture cost is relatively low, for separating and recovering on a large scale in coal-fired plant flue gas
CO2Project investment cost can greatly be reduced.Meanwhile coal-fired plant flue gas concentration is very low (about 12%), organic film
Selective higher, CO can be further improved2Separation and recovery rate and amount of collected.Special instruction, the present invention by using
Smoke processing system 10, which efficiently solves organic film, to be easily subject to the pollution of the solid impurities such as particulate matter, humidity requirement and temperature is wanted
The problem of higher is asked, can more effectively give play to its own advantages.
In a kind of preferred embodiment, the step of flue gas being handled to remove liquid impurity and solid impurity it
Before, method further includes the step of carrying out first compression to flue gas；It is preferred that in the step of first compression, it is more than gas pressure
0.3MPa.First carbon dioxide enriched gas and optional 3rd carbon dioxide enriched gas are subjected to second of CO2Membrane separation
The step of before, method is further included carries out secondary pressure by the first carbon dioxide enriched gas and optional 3rd carbon dioxide enriched gas
The step of contracting；Preferably, in the step of second-compressed, gas pressure is made to be more than 0.3MPa.
Can be first time CO using first compression2The CO of UF membrane2Infiltration further provides for pressure-driven；Similarly, utilize
Second-compressed can be second of CO2The CO of UF membrane2Infiltration further provides for pressure-driven.And it should be noted that compared to
Enough pressure differentials are capable of providing using the mode of compression using the method for vacuumizing or purging decompression, the present invention in per-meate side,
To drive enough CO2Through film, particularly organic film, so as to further improve CO2The trapping rate of recovery.Moreover, utilize pressure
The first high pressure non-permeate gas that the mode of contracting obtains has certain pressure in itself, and the nitrogen obtained after nitrogen recycling also has in itself
Have elevated pressures, then it is further compressed after can be sold as nitrogen product gas, reached recycling to a certain extent
The effect of pressure energy.
In a preferred embodiment, flue gas is handled to be wrapped the step of removing liquid impurity and solid impurity
Include：Flue gas is filtered, obtains the flue gas.Liquid impurity and solid impurity filtering can so be removed.It is highly preferred that
Before the step of being filtered to flue gas, flue gas is handled also to be wrapped the step of removing liquid impurity and solid impurity
Include：Flue gas is cooled down, condenses liquid impurity, obtains cooled flue gas；Cooled flue gas is filtered, obtains processing cigarette
Gas.It can so utilize cooling procedure further out to filter the liquid condensation carried secretly in flue gas to remove.
It is further preferred that before the step of being filtered to cooled flue gas, flue gas is handled miscellaneous to remove liquid
The step of matter and solid impurity, further includes：Cooled flue gas is subjected to demisting, obtains demisting flue gas；And demisting flue gas was carried out
Filter, obtains processing flue gas., can be by condensable liquid foam, droplet and possible quilt in flue gas by demisting after flue gas is first cooled
Entrained solid particle removes.Then fine liquid that may be carried secretly in unstripped gas etc. can further be removed by filtration treatment
Objectionable impurities.In short, liquid impurity, the solid particle in flue gas can be substantially more removed using above-mentioned fume treatment mode
Deng impurity, so as to further improve the trapping effect of carbon dioxide.Meanwhile can also effectively it be controlled by carrying out cooling to flue gas
Flue-gas temperature, to further improve the operation stability of organic film.
In a preferred embodiment, before the step of flue gas being carried out first compression, method is further included to flue gas
The step of being carried out dehydrating.It so can first be carried out dehydrating, be more advantageous to before flue gas enters the fume treatment stage
Moisture impurity is removed, controls smoke moisture, accordingly further improves the UF membrane efficiency of organic film.
Embodiment 1
To certain coal-burning power plant, flue gas is tested, and accounts the device shown in Fig. 1 of the present invention for low dense in flue gas
Spend CO2The trapping recycling effect of technique.The results are shown in Table 1 for mass balance：
The trapping retracting device of 1 carbon dioxide in flue gas of table handles CO in certain coal-burning power plant's flue gas2Mass balance table
As shown in Table 1, when flue-gas flow rate of certain power plant after dust-removal and desulfurizing of processing is 10000Nm3/ h, CO2Content is
When 12.37%, second segment CO2 film separation units infiltration gas (product gas) flow that the membrane separation process in the present embodiment obtains is
699Nm3/ h, CO2Content is 97.11%.The N of acquisition2Membrane separator impermeable gas flow 6702Nm3/ h, N2Content is
98.07%.
It can be seen from the above description that the above embodiments of the present invention realize following technique effect：
Using carbon dioxide in flue gas provided by the invention and nitrogen joint trapping retracting device and method, to flue gas into
Before row membrane separation, liquid impurity and solid impurity in flue gas can be removed first with smoke processing system, to prevent
The presence of liquid impurity and solid impurity influences the efficiency of UF membrane.After the treatment, flue gas enters the first CO2Film separation unit
With the 2nd CO2Film separation unit, using successively membrane separating process is enriched with the carbon dioxide in flue gas twice.Above reason
The enrichment degree of carbon dioxide can be significantly improved.Meanwhile utilize N2Film separation unit can also be by the first high pressure non-permeate gas
The gas of outlet discharge further carries out UF membrane to recycle nitrogen.Moreover, trapped using the device of the invention in recovered flue gas
Carbon dioxide, technique is simple, pollution-free without the further enrichment process such as follow-up chemical absorbing or absorption, is not only suitable for
The separation of carbon dioxide in coal-fired plant flue gas, is also applied for point of carbon dioxide in the low-concentration flue gas such as steel plant, cement plant
From trapping.
The foregoing is only a preferred embodiment of the present invention, is not intended to limit the invention, for the skill of this area
For art personnel, the invention may be variously modified and varied.Within the spirit and principles of the invention, that is made any repaiies
Change, equivalent substitution, improvement etc., should all be included in the protection scope of the present invention.
Claims (17)
1. the joint of a kind of carbon dioxide in flue gas and nitrogen traps retracting device, it is characterised in that including：
Smoke processing system (10), the smoke processing system (10) is provided with processing import and processing exports, at the flue gas
Reason system (10) is used to handle flue gas, to remove the liquid impurity and solid impurity in the flue gas；
First CO2Film separation unit (20), the first CO2Film separation unit (20) is provided with the first air inlet, the first titanium dioxide
Carbon enrichment gas exports and the outlet of the first high pressure non-permeate gas, and first air inlet is connected with the processing outlet；
2nd CO2Film separation unit (30), the 2nd CO2Film separation unit (30) is provided with the second air inlet, carbon dioxide production
Product gas exports and the outlet of the second high pressure non-permeate gas, second air inlet and the described first carbon dioxide enriched gas outlet phase
Even；And
N2Film separation unit (80), the N2Film separation unit (80) is provided with the outlet of nitrogen-rich gas, and the N2UF membrane list
The air inlet of first (80) is connected with the first high pressure non-permeate gas outlet.
2. device according to claim 1, it is characterised in that described device further includes：
3rd CO2Film separation unit (40), the 3rd CO2Film separation unit (40) is provided with the 3rd air inlet, the 3rd titanium dioxide
Carbon enrichment gas exports and offgas outlet, and the 3rd air inlet is connected with the second high pressure non-permeate gas outlet；
Gas mixer (50), the gas mixer (50) are arranged on the described first carbon dioxide enriched gas outlet and described the
On the pipeline of two air inlets connection, and the gas mixer (50) is additionally provided with and returns return air inlet, it is described return return air inlet with
The 3rd carbon dioxide enriched gas outlet is connected.
3. the apparatus of claim 2, it is characterised in that the first CO2Film separation unit (20), the 2nd CO2
Film separation unit (30) and the 3rd CO2Membrane module in film separation unit (40) separately selected from hollow-fibre membrane,
Rolled film or plate membrane.
4. the apparatus of claim 2, it is characterised in that described device further includes：
First compressor (60), first compressor (60) are connected with the processing import；
Second compressor (70), second compressor (70) are arranged on the gas mixer (50) and second air inlet
On the pipeline of connection.
5. device according to any one of claim 1 to 4, it is characterised in that the smoke processing system (10) includes
Filter (13), the import of the filter (13) is the processing import, and the outlet of the filter (13) is the place
Reason outlet.
6. device according to claim 5, it is characterised in that the smoke processing system (10) further includes：Cooler
(11), the import of the cooler (11) is the processing import, the outlet of the cooler (11) and the filter (13)
Import be connected.
7. device according to claim 6, it is characterised in that the smoke processing system (10) further includes：Demister
(12), the import of the demister (12) is connected with the outlet of the cooler (11), the outlet of the demister (12) and institute
The import for stating filter (13) is connected.
8. device according to claim 4, it is characterised in that described device further includes：
Dehydration device, gas inlet and dehydration exhanst gas outlet, the dehydration exhanst gas outlet and institute are provided with the dehydration device
The import for stating the first compressor (60) is connected.
9. the joint of a kind of carbon dioxide in flue gas and nitrogen traps recovery method, it is characterised in that including：
The flue gas is handled, to remove the liquid impurity and solid impurity in the flue gas, obtains processing flue gas；
The processing flue gas is subjected to first time CO2Membrane separation, obtains the first carbon dioxide enriched gas and the first high pressure is non-oozes
It is ventilative；
Described first carbon dioxide enriched gas is subjected to second of CO2Membrane separation, obtains carbon dioxide product gas and second high
Press impermeable gas；And
N is carried out to the first high pressure non-permeate gas2Membrane separation, obtains nitrogen-rich gas.
10. according to the method described in claim 9, it is characterized in that, after the step of obtaining the second high pressure non-permeate gas,
The method is further comprising the steps of：
Third time CO is carried out to the second high pressure non-permeate gas2Membrane separation, obtains the 3rd carbon dioxide enriched gas and tail
Gas；And
Described 3rd carbon dioxide enriched gas is returned and is mixed with the described first carbon dioxide enriched gas, to carry out described second
Secondary CO2Membrane separation.
11. the according to the method described in claim 9, it is characterized in that, first time CO2Membrane separation, described second
CO2Membrane separation and the third time CO2The membrane module used in the step of membrane separation is separately selected from hollow fibre
Tie up film, rolled film or plate membrane.
12. the method according to any one of claim 9 to 11, it is characterised in that handled the flue gas to go
Before the step of liquid impurity and solid impurity, the method further includes the step of carrying out first compression to the flue gas；It is excellent
In the step of selecting the first compression, gas pressure is set to be more than 0.3MPa.
13. according to the method for claim 12, it is characterised in that by the described first carbon dioxide enriched gas and optional institute
State and carry out second of CO described in the 3rd carbon dioxide enriched gas2Before the step of membrane separation, the method is further included institute
The step of stating the first carbon dioxide enriched gas and the optional 3rd carbon dioxide enriched gas progress second-compressed；Preferably,
In the step of second-compressed, gas pressure is set to be more than 0.3MPa.
14. the method according to any one of claim 9 to 13, it is characterised in that handled the flue gas to go
Except the step of liquid impurity and solid impurity, includes：The flue gas is filtered, obtains the processing flue gas.
15. according to the method for claim 14, it is characterised in that, will before the step of being filtered to the flue gas
The flue gas is handled to be further included the step of removing liquid impurity and solid impurity：
The flue gas is cooled down, condenses liquid impurity, obtains cooled flue gas；And
The cooled flue gas is filtered, obtains the processing flue gas.
16. according to the method for claim 15, it is characterised in that filtered to the cooled flue gas the step of it
Before, the flue gas is handled to be further included the step of removing liquid impurity and solid impurity：
Demisting is carried out to the cooled flue gas, obtains demisting flue gas；And
The demisting flue gas is filtered, obtains the processing flue gas.
17. according to the method for claim 12, it is characterised in that by the flue gas carry out the first compression the step of it
Before, the method further includes the step of being carried out dehydrating to the flue gas.
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| CN108905488A (en) * | 2018-07-11 | 2018-11-30 | 华电电力科学研究院有限公司 | A kind of low-carbon clean and effective type distributed energy resource system and its operation method |
| CN110127700A (en) * | 2019-06-14 | 2019-08-16 | 林千果 | The combined recovery device and method of carbon dioxide in flue gas, nitrogen and oxygen |
| CN110272046A (en) * | 2019-07-08 | 2019-09-24 | 中国能源建设集团广东省电力设计研究院有限公司 | A kind of trapping of carbon dioxide separation and cooling drying system |
| CN113028844A (en) * | 2021-04-02 | 2021-06-25 | 攀枝花攀钢集团设计研究院有限公司 | Blast furnace hot blast stove flue gas waste heat recovery device and recovery method |
| CN113893653A (en) * | 2021-12-09 | 2022-01-07 | 胜利油田胜机石油装备有限公司 | Flue gas component adjusting equipment and working method thereof |
| CN113998677A (en) * | 2021-10-19 | 2022-02-01 | 碳和科技(北京)有限公司 | Recovery of CO from chemical process2System and method for producing nitrogen from waste gas |
| CN114210195A (en) * | 2021-11-10 | 2022-03-22 | 北京城市排水集团有限责任公司 | Gas-liquid separation membrane biological deodorization equipment and method |
| CN115999311A (en) * | 2023-01-05 | 2023-04-25 | 中海石油气电集团有限责任公司 | Coupling system and method for skid-mounted natural gas hydrogen production and carbon capture of flue gas |
| CN117732211A (en) * | 2024-01-18 | 2024-03-22 | 中海石油气电集团有限责任公司 | Carbon dioxide membrane separation system in flue gas |
| DE102024103334A1 (en) | 2023-02-08 | 2024-08-08 | Hangzhou Oxygen Plant Group Co., Ltd. | Apparatus and method for recovering carbon dioxide and nitrogen from flue gas |
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| CN108905488A (en) * | 2018-07-11 | 2018-11-30 | 华电电力科学研究院有限公司 | A kind of low-carbon clean and effective type distributed energy resource system and its operation method |
| CN110127700A (en) * | 2019-06-14 | 2019-08-16 | 林千果 | The combined recovery device and method of carbon dioxide in flue gas, nitrogen and oxygen |
| CN110272046A (en) * | 2019-07-08 | 2019-09-24 | 中国能源建设集团广东省电力设计研究院有限公司 | A kind of trapping of carbon dioxide separation and cooling drying system |
| CN113028844A (en) * | 2021-04-02 | 2021-06-25 | 攀枝花攀钢集团设计研究院有限公司 | Blast furnace hot blast stove flue gas waste heat recovery device and recovery method |
| CN113998677B (en) * | 2021-10-19 | 2023-10-24 | 碳和科技(北京)有限公司 | CO recovery from chemical process 2 System and method for preparing nitrogen from waste gas of (a) a reactor |
| CN113998677A (en) * | 2021-10-19 | 2022-02-01 | 碳和科技(北京)有限公司 | Recovery of CO from chemical process2System and method for producing nitrogen from waste gas |
| WO2023066134A1 (en) * | 2021-10-19 | 2023-04-27 | 碳和科技(北京)有限公司 | System and method for preparing nitrogen from waste gas obtained by recovering co2 via chemical method |
| CN114210195A (en) * | 2021-11-10 | 2022-03-22 | 北京城市排水集团有限责任公司 | Gas-liquid separation membrane biological deodorization equipment and method |
| CN114210195B (en) * | 2021-11-10 | 2024-03-12 | 北京城市排水集团有限责任公司 | Gas-liquid separation membrane biological deodorization equipment and method |
| CN113893653A (en) * | 2021-12-09 | 2022-01-07 | 胜利油田胜机石油装备有限公司 | Flue gas component adjusting equipment and working method thereof |
| CN115999311A (en) * | 2023-01-05 | 2023-04-25 | 中海石油气电集团有限责任公司 | Coupling system and method for skid-mounted natural gas hydrogen production and carbon capture of flue gas |
| DE102024103334A1 (en) | 2023-02-08 | 2024-08-08 | Hangzhou Oxygen Plant Group Co., Ltd. | Apparatus and method for recovering carbon dioxide and nitrogen from flue gas |
| CN117732211A (en) * | 2024-01-18 | 2024-03-22 | 中海石油气电集团有限责任公司 | Carbon dioxide membrane separation system in flue gas |
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Application publication date: 20180413 |