CN107019998A - A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change - Google Patents
A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change Download PDFInfo
- Publication number
- CN107019998A CN107019998A CN201710179868.6A CN201710179868A CN107019998A CN 107019998 A CN107019998 A CN 107019998A CN 201710179868 A CN201710179868 A CN 201710179868A CN 107019998 A CN107019998 A CN 107019998A
- Authority
- CN
- China
- Prior art keywords
- tower
- gas
- low temperature
- phase change
- film
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
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
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- 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
- B01D53/002—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 condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7022—Aliphatic hydrocarbons
- B01D2257/7025—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- 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
- Y02C20/20—Capture or disposal of greenhouse gases of methane
Abstract
The invention discloses the CO that a kind of infiltration of film is combined with low temperature phase change2Capture method, first by CO2/N2/H2O mixed gas input condenser pipe, is placed in 60 DEG C of environment, makes water vapour liquefaction for aqueous water and discharged；CO2And N2Enter gas membrane permeator of hollow fiber in a gaseous form, permeated by film, infiltration gas is placed in 120 DEG C of environment, makes CO2Solid is frozen into, the surface of heat exchanger is frozen in, non-permeate gas is discharged；Again by solid-state CO2Scrape off, and by itself and gaseous state N2It is placed in 80 DEG C of environment, high-purity solid CO2It is stored, by N2Gas is discharged.The present invention is combined by film infiltration and low temperature phase change, realizes H2O and CO2In the separation of different parts, CO is improved2The purity of product is permeated and simple low temperature phase change process cost height with simple film is prevented effectively from, the drawbacks of energy consumption is big.
Description
Technical field
The present invention relates to the gas separating method that a kind of low temperature is combined, more particularly to a kind of cryogenic film infiltration and low temperature phase change
Compound CO2Capture method.
Background technology
Global warming and greenhouse gases CO2Emission reduction is the focus and difficulties of current global concern.Using clean energy resource
Substituting fossil energy is control and reduces CO2The most desirable route of discharge, but the adjustment made in the short term to energy resource structure
It is extremely limited.In this context, scientists from all over the world are in CO2Trapping, recycling and Plugging Technology Applied field have been done and largely ground
Study carefully, to slow down the problems such as using greenhouse effects caused by fossil fuel.Wherein, CO2Trapping process is whole CCUS
It is most basic and most important during (Carbon Capture, Utilization and Storage carbon is captured, using with sealing up for safekeeping)
Link.However, current CO2The main bottleneck of trapping technique application is that cost and energy consumption are still higher.
The existing associated analog research in this area shows that simple film permeates CO2Trapping process has that cost is higher (to be needed many
The processing of section film permeation unit), and CO2Purity is difficult to require while meeting with the rate of recovery.And simple low temperature phase change CO2Trapping process
By CO2Concentration influence in burning waste gas, overall energy consumption can be with CO2The reduction of initial concentration and it is significantly raised.Institute in the present invention
The CO that a kind of new film infiltration being related to is combined with low temperature phase change2Capture method, realizes that UF membrane traps skill with low temperature phase change
Art is efficient and organically couples, and reaches reduction CO2Trap the final purpose of energy consumption.Different from film infiltration and both low temperature phase changes
Simple series connection, this method promotes the differential permeability of membrane material using the surface characteristics and internal structure effect of Low temperature regulation membrane material
Can, and at ambient pressure by low temperature phase change by CO2Trapped from burning waste gas.Film permeates the integrated coupling with low temperature phase change technology
Close, can more efficiently play the advantage of the two, improve CO2Separative efficiency and reduction trapping energy consumption.
Retrieval research both domestic and external, 2012, French famous membrane science man Eric Favre etc. proposed low temperature and oozed with film
The CO being combined thoroughly2Trapping technique, and it is applied to post-combustion capture.The technology utilizes film permeation unit by different emission sources
CO in waste gas2(25%-30%) composition is concentrated, then by cryogenic unit by the CO of high concentration2Gas carries out phase transformation
(liquefaction) is reclaimed.2014, Norway scientist David Berstad etc. proposed that film is combined CO with low temperature phase change2Trapping technique.Should
Technology is permeated the CO in waste gas by one section of film first2Concentration is promoted to 50%-75%, is then compressed using two ends, by height
CO2Concentration gases are compressed to liquefaction pressure.Meanwhile, with propane (Propane) and ethane (Ethane) for refrigerant, by CO2With liquid
The form of body is from N2Trapped in (gas phase).Although relevant film infiltration is combined CO with low temperature phase change2The research of trapping technique has been achieved with
Certain preliminary progress, but simple series connection is difficult to the combination of realizing the two advantage to greatest extent.The present invention is film infiltration
With the organic coupling of low temperature phase change, mixed gas first passes through cryogenic film infiltration, then carries out low temperature phase change.For polymer membrane material
Material, separating property is not generally high, is easily limited by " the Robeson upper limits ", exists between permeability of the membrane and selectivity mutual
The problem of restriction.But membrane material is under cryogenic, high selectivity and the permeability slightly declined can be maintained.So this
On the one hand invention is conducive to improving the performance of membrane material, and on the other hand being permeated by film reduces the gas into low temperature phase change
Amount, is conducive to reducing the energy consumption of low temperature phase change.
The content of the invention
The purpose of the present invention, is in CO2During trapping, in order to avoid simple film permeates and simple low temperature phase change process
Drawback (such as cost is high, and energy consumption is big), by film infiltration and low temperature phase change organic coupling, it is preliminary that mixed gas first passes through cryogenic film infiltration
Purify, then carry out low temperature phase change and further improve product purity, last CO2It is saved in the form of solid-state.
The present invention is achieved by the following technical solutions：
A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change, with following steps：
(1) by CO2/N2/H2O mixed gas input condenser pipe 7, the condenser pipe is placed in the interior tower A6 for precooling tower 1,
Temperature in controlling in tower A6 is -60 DEG C；Water vapour liquefies at a temperature of this, forms aqueous water, aqueous water is in condensation-water drain
Discharge；Because now interior tower A6 temperature is higher than CO2And N2Freezing point, make CO2And N2Enter gaseous jet simulation in a gaseous form
Device 9, permeates by film, and infiltration gas enters the interior tower B15 of main cooling tower 2 from vent outlet 10 is oozed by vavuum pump 11, non-to ooze
Ventilation body is discharged by impermeable gas outlet 12；
The gaseous jet simulation device 9 is polyimide hollow fiber gaseous jet simulation device；
(2) temperature is set to be -120 DEG C the interior tower B15 of main cooling tower 2, because interior tower B15 temperature is less than CO2It is solidifying
Solid point, makes CO2Solid is frozen into, the surface of heat exchanger is frozen in；And now interior tower B15 temperature remains above N2Freezing point,
N2Still enter storage tower 3 in a gaseous form；It is frozen in the solid-state CO on the surface of heat exchanger 142, make solid-state by rotating scraping board 18
CO2Fall 16 to enter in storage tower 3；
(3) it is -80 DEG C, the CO of high-purity that temperature is set in storage tower 32It is stored in the form of solid-state, uncooled N2With
Gaseous form is discharged by gas discharge outlet 19, is completed to CO2Separation；
The precooling tower 1, main cooling tower 2, storage tower 3 is vertically arranged successively by upper, middle and lower.
Step (1) CO2/N2/H2CO in O mixed gas2For 13-15vol%, N2For 77-82vol%, H2O is 5-
8vol%.
Step (1) the infiltration gas is 45vol%CO2And 55vol%N2, non-permeate gas is 8vol%CO2With
92vol%N2。
The mixed gas of the step (1) is CO2/CH4/H2O。
Beneficial effects of the present invention are as follows：
1. application of the hollow-fibre membrane in low temperature environment.Compared with traditional normal temperature or high temperature membrane process of osmosis, low temperature
The surface characteristics and internal structure of enhancement of environment membrane material, are conducive to improving the CO of hollow-fibre membrane2Stalling characteristic.Meanwhile, just
In realizing efficient, integrated combination between film permeation unit and low temperature phase change unit, be conducive to improving CO2Arresting efficiency and drop
The energy consumption of low whole trapping process.
2. provide CO using sterlin refrigerator2The low temperature environment that phase transformation is reclaimed.CO2The low temperature that phase transformation removal process needs
Environment is provided by free-piston type sterlin refrigerator, it is to avoid multi-stage compression, cooling, distillation in Conventional cryogenic distillation technique
High energy consumption process.Meanwhile, reduce traditional CO2The large scale equipment such as compressor, destilling tower, knockout tower makes during trapping
With reducing CO2The input and operating cost of catching apparatus.
3.CO2Low temperature phase change trapping carry out at ambient pressure, relative to traditional CO2Low-temperature liquefaction (under condition of high voltage) is returned
Receipts process, reduces the requirement to pressure condition, reduces the energy consumption of cryogenic unit.Meanwhile, it is enriched in low-temperature heat exchange piece surface
Phase change layer is peeled off in time by mechanical treatment, is conducive to maintaining efficient quality and energy transfer between each phase (gas/solid).
Brief description of the drawings
Fig. 1 is the CO that the film infiltration of the present invention and low temperature phase change are combined2The schematic device of capture method.
Reference is as follows：
1 --- precooling tower 2 --- main cooling tower
3 --- storage tower 4 --- refrigeration machine A
5 --- air inlet 6 --- interior tower A
7 --- condenser pipe 8 --- condensation-water drains
9 --- gaseous jet simulation devices 10 --- ooze vent outlet
11 --- dry vacuum pump 12 --- impermeable gas are exported
13 --- refrigeration machine B 14 --- heat exchangers
15 --- interior tower B 16 --- solid-state CO2
17 --- motor 18 --- rotate scraping board
19 --- gas discharge outlet 20 --- refrigeration machine C
Embodiment
The present invention will be further described with reference to the accompanying drawings and examples.
Fig. 1 is the structural representation for the carbon dioxide capture device that a kind of film infiltration of the invention is combined with low temperature phase change, bag
Include：Tower 1 is precooled, main cooling tower 2, the part of storage tower 3 three is vertically arranged, is stainless steel material successively by upper, middle and lower, its appearance
Face is provided with pearl cotton heat-insulating material.Gaseous jet simulation device 9 is cylindrical shape, is perpendicularly fixed at the Nei Tanei for precooling tower, gas
There are thousands of Polyimide Hollow Fiber silks the inside of membrane separator 9.Precool and interior tower A6 is provided with tower 1, precool tower 1
It is vacuum state between interior tower A6；Interior tower B15 is provided with main cooling tower 2, is also true between main cooling tower 2 and Nei Ta B15
Dummy status；Precool and do not connected between tower 1 and main cooling tower 2 and interior tower A6 and Nei Ta B15；Interior tower A6, interior tower B15 appearance
Face is provided with aluminum foil material.
Interior tower A6, interior tower B15 and storage tower 3 are respectively arranged with refrigeration machine A4, refrigeration machine B13 and refrigeration machine C20, refrigeration machine
B13 heat exchanger 14 is arranged on interior tower B15 middle position；The periphery of heat exchanger 14 is provided with rotation and scrapes sassafras plate 18, main cooling
Tower 2 is additionally provided with motor 17 to control rotation to scrape sassafras plate 18；
Condenser pipe 7 is provided with the interior tower A6 for precooling tower 1, the top for precooling tower 1 is provided with the air inlet of condenser pipe 7
5, the side wall for precooling tower 1 is provided with the condensation-water drain 8, two of condenser pipe 7 and oozes the outlet 12 of vent outlet 10 and impermeable gas,
The lower end of condenser pipe 7 extends to the air inlet of gaseous jet simulation device 9；Through membrane separation, infiltration gas is by precooling the side wall two of tower 1
The interior tower B15 that vent outlet 10 enters main cooling tower 2 by vavuum pump 11 is oozed, the side wall of tower 1 is non-to be oozed impermeable gas by precooling
Vent outlet 12 is discharged；CO into interior tower B15 gas2It is frozen in the surface of heat exchanger 14, the rotation that motor 17 is controlled
Scraping board 18 is by solid-state CO2The storage tower 3 for falling into and being connected with interior tower B15 is scraped, the gas not solidified passes through the side of storage tower 3
The gas discharge outlet 15 of wall is discharged.
Present invention process principle is as follows：
Unstripped gas (CO2/N2/H2O or CO2/CH4/H2O mixed gas) enter the interior tower for precooling tower 1 from air inlet 5
A6 condenser pipe 7, interior tower A6 temperature is -60 DEG C, it is possible to achieve the liquefaction of water vapour, forms the water of liquid, aqueous water is by cold
Discharged in solidifying pipe outlet 8.Because the temperature in interior tower A6 is higher than CO2Freezing point (about -78.5 DEG C) and N2Freezing point (about-
209.86 DEG C), CO2And N2Gas (CH4Gas) in a gaseous form into the air inlet of gaseous jet simulation device 9, permeate, permeate by film
Gas enters the interior tower B15 of main cooling tower 2 from vent outlet 10 is oozed by vavuum pump 11, and impermeable gas exports 12 by impermeable gas
Discharge.Main cooling tower 2 is by the sterlin refrigerator B13 being connected with it, and it is -120 DEG C to control the temperature in interior tower B15, is less than
CO2Freezing point, the CO in interior tower B152Solid is frozen into, the surface of heat exchanger 14 is frozen in, it is achieved thereby that H2O and CO2
In the separation of different parts.It is frozen in the solid-state CO of heat exchanger surface216, the rotation scraping board 18 driven by motor 17 enters
Row is scraped, and it is fallen into storage tower 3.Storage tower 3 controls temperature in storage tower 3 by the sterlin refrigerator C20 being connected with it
Spend for -80 DEG C, the CO of high-purity2It is stored in the form of solid-state.Uncooled N2(or CH4Gas) pass through the row of gas discharge outlet 19
Go out.
Embodiment 1
With CO2/N2/H2Composition after O mixed gas simulated combustion in flue gas, wherein CO2For 13vol%, N2For
82vol%, H2O is 5vol%.The CO being combined using the film infiltration in the present invention with low temperature phase change2Capture method, carries out CO2's
Separation, specific implementation process is as follows：
Mixed gas enters condenser pipe 7 from air inlet 5, and the interior tower A6 for precooling tower 1 is connected with sterlin refrigerator A4, controls
Temperature in system in tower A6 is -60 DEG C.Water vapour liquefies at a temperature of this, forms aqueous water and (prevents and to form ice pipeline is blocked up
Plug), the water of liquid is discharged from condensation-water drain 8.Because now temperature is higher than CO2Freezing point (about -78.5 DEG C) and N2Solidification
Point (about -209.86 DEG C), makes CO2And N2Smoothly enter gaseous jet simulation device 9 in a gaseous form, permeated by film, infiltration gas is (about
45%CO2And 55%N2) from vent outlet 10 is oozed by vavuum pump 11 into the interior tower B15 of main cooling tower 2, impermeable gas is (about
92%N2) discharged by impermeable gas outlet 12.The interior tower B15 of main cooling tower 1 is connected with sterlin refrigerator B13, interior tower
B15 setting temperature is -120 DEG C, because temperature now is less than CO2Freezing point, make CO2Solid is frozen into, is frozen in and changes
The surface of hot device 14, and this temperature remains above N2Freezing point, so N2Storage tower 3 is still entered with gaseous state.It is frozen in heat exchanger 14
The solid-state CO on surface216, the rotation scraping board 18 driven by motor 17 is scraped, and makes solid-state CO216 fall into storage tower 3
It is interior.
Storage tower 3 is connected with sterlin refrigerator C20, and the setting temperature of storage tower 3 is -80 DEG C, the CO of high-purity2With
The form of solid-state is stored, uncooled N2Discharged in a gaseous form by gas discharge outlet 19.
The CO that mixed gas is combined by the film infiltration in the present invention with low temperature phase change2Capture method, realizes low temperature CO2
Separation.Finally, water vapour is discharged from the condensation-water drain 8 for the interior tower A6 for precooling tower in liquid form, CO2With solid-state
Form is stored in storage tower, uncooled gas (N2), discharged from the gas discharge outlet 19 in storage tower.The present invention oozes film
Thoroughly with low temperature phase change organic coupling, it is to avoid simple film infiltration and simple low temperature phase change process cost are high, the drawbacks of energy consumption is big, most
Finished product high purity 98% and the rate of recovery are up to 97%, and overall energy consumption only needs 1.3MJ/KgCO2.
When mixed gas is CO2/CH4/H2During O, the present invention can also be realized.
Claims (4)
1. a kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change, with following steps：
(1) by CO2/N2/H2O mixed gas input condenser pipe (7), the condenser pipe is placed in the interior tower A (6) for precooling tower (1)
Interior, it is -60 DEG C to control the temperature in interior tower A (6)；Water vapour is liquefied at a temperature of this, forms aqueous water, and aqueous water is gone out by condensed water
Discharged in mouthful；Because the temperature of now interior tower A (6) is higher than CO2And N2Freezing point, make CO2And N2Enter gas in a gaseous form
Membrane separator (9), permeates by film, and infiltration gas passes through vavuum pump (11) into main cooling tower (2) from vent outlet (10) is oozed
Interior tower B (15), non-permeate gas by impermeable gas export (12) discharge；
The gaseous jet simulation device (9) is polyimide hollow fiber gaseous jet simulation device；
(2) temperature is set to be -120 DEG C the interior tower B (15) of main cooling tower (2), because the temperature of interior tower B (15) is less than CO2It is solidifying
Solid point, makes CO2Solid is frozen into, the surface of heat exchanger is frozen in；And now the temperature of interior tower B (15) remains above N2Solidification
Point, N2Still enter storage tower (3) in a gaseous form；It is frozen in the solid-state CO on heat exchanger (14) surface2, by rotating scraping board
(18) solid-state CO is made2Fall (16) to enter in storage tower (3)；
(3) it is -80 DEG C, the CO of high-purity that temperature is set in storage tower (3)2It is stored in the form of solid-state, uncooled N2With gas
State form is discharged by gas discharge outlet (19), is completed to CO2Separation；
The precooling tower (1), main cooling tower (2), storage tower (3) is vertically arranged successively by upper, middle and lower.
2. the collecting carbonic anhydride method that a kind of film infiltration according to claim 1 is combined with low temperature phase change, it is characterised in that institute
State step (1) CO2/N2/H2CO in O mixed gas2For 13-15vol%, N2For 77-82vol%, H2O is 5-8vol%.
3. the collecting carbonic anhydride method that a kind of film infiltration according to claim 1 is combined with low temperature phase change, it is characterised in that institute
It is 45vol%CO to state step (1) infiltration gas2And 55vol%N2, non-permeate gas is 8vol%CO2And 92vol%N2。
4. the collecting carbonic anhydride method that a kind of film infiltration according to claim 1 is combined with low temperature phase change, it is characterised in that institute
The mixed gas for stating step (1) is CO2/CH4/H2O。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710179868.6A CN107019998A (en) | 2017-03-23 | 2017-03-23 | A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710179868.6A CN107019998A (en) | 2017-03-23 | 2017-03-23 | A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107019998A true CN107019998A (en) | 2017-08-08 |
Family
ID=59525861
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710179868.6A Pending CN107019998A (en) | 2017-03-23 | 2017-03-23 | A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107019998A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108261890A (en) * | 2018-02-06 | 2018-07-10 | 常州大学 | CO in integrated form trapping flue gas2And N2Capturing device |
| CN110787596A (en) * | 2019-10-04 | 2020-02-14 | 天津大学 | Low-temperature and membrane-coupled flue gas separation method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101285573A (en) * | 2007-01-23 | 2008-10-15 | 气体产品与化学公司 | Purification of carbon dioxide |
| CN101733029A (en) * | 2008-11-14 | 2010-06-16 | 中国科学院大连化学物理研究所 | Method for preparing CO2 separation membrane material and composite membrane |
| CN201799206U (en) * | 2010-08-06 | 2011-04-20 | 镇江汉龙环保科技有限公司 | Carbon dioxide separation and storage device |
| CN102036736A (en) * | 2008-05-20 | 2011-04-27 | 鲁姆斯科技公司 | Carbon dioxide purification |
| CN105126551A (en) * | 2015-09-11 | 2015-12-09 | 东南大学 | Device and method for capturing CO2 in coal-fired flue gas by grades based on membrane method |
| CN105854519A (en) * | 2016-06-10 | 2016-08-17 | 成都中科能源环保有限公司 | Mixed gas separation method and system |
| CN106237648A (en) * | 2016-09-29 | 2016-12-21 | 天津大学 | Low-temperature carbon dioxide segregation apparatus |
-
2017
- 2017-03-23 CN CN201710179868.6A patent/CN107019998A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101285573A (en) * | 2007-01-23 | 2008-10-15 | 气体产品与化学公司 | Purification of carbon dioxide |
| CN102036736A (en) * | 2008-05-20 | 2011-04-27 | 鲁姆斯科技公司 | Carbon dioxide purification |
| CN101733029A (en) * | 2008-11-14 | 2010-06-16 | 中国科学院大连化学物理研究所 | Method for preparing CO2 separation membrane material and composite membrane |
| CN201799206U (en) * | 2010-08-06 | 2011-04-20 | 镇江汉龙环保科技有限公司 | Carbon dioxide separation and storage device |
| CN105126551A (en) * | 2015-09-11 | 2015-12-09 | 东南大学 | Device and method for capturing CO2 in coal-fired flue gas by grades based on membrane method |
| CN105854519A (en) * | 2016-06-10 | 2016-08-17 | 成都中科能源环保有限公司 | Mixed gas separation method and system |
| CN106237648A (en) * | 2016-09-29 | 2016-12-21 | 天津大学 | Low-temperature carbon dioxide segregation apparatus |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108261890A (en) * | 2018-02-06 | 2018-07-10 | 常州大学 | CO in integrated form trapping flue gas2And N2Capturing device |
| CN108261890B (en) * | 2018-02-06 | 2020-09-08 | 常州大学 | Integrated CO capture in flue gas2And N2Collecting device |
| CN110787596A (en) * | 2019-10-04 | 2020-02-14 | 天津大学 | Low-temperature and membrane-coupled flue gas separation method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2018157628A1 (en) | Atmospheric water extraction device for island and water extraction method thereof | |
| CN106237648B (en) | Low-temperature carbon dioxide separator | |
| CN101851946B (en) | Water generating method by utilizing separating membrane to enrich air water vapor and device thereof | |
| CN104406364B (en) | The argon of a kind of double tower coupling reclaims purifier apparatus and argon reclaims purification process | |
| CN103274406B (en) | Novel carbon dioxide trapping device performing liquefaction and sublimation | |
| CN110207457B (en) | Air separation equipment capable of preparing liquid nitrogen and application method thereof | |
| JP2010266154A (en) | Carbon dioxide liquefying apparatus | |
| CN103277980A (en) | Carbon dioxide capture device utilizing both part oxygen-enriched combustion and nitrogen-and-oxygen separation | |
| CN107019998A (en) | A kind of collecting carbonic anhydride method that film infiltration is combined with low temperature phase change | |
| CN109078447A (en) | A kind of device and method of off-gas recovery dry ice | |
| EP3771485B1 (en) | Process for obtaining carbon dioxide from furnace combustion fumes | |
| CN106890546A (en) | Film permeates the carbon dioxide capture device being combined with low temperature phase change | |
| CN206911078U (en) | A kind of film infiltration and the compound carbon dioxide capture device of low temperature phase change | |
| CN108786371B (en) | Oxygen recovery system and method for high-temperature oxygen-enriched flue gas | |
| CN207299718U (en) | The low-temperature liquefaction purifying plant of special gas | |
| CN105783423A (en) | Air separation system | |
| CN207533246U (en) | A kind of carbon trapping system regeneration gas heat reclaim unit | |
| CN204079928U (en) | A kind of low-temperature fractionation and embrane method coupling EOR extraction gas separating system | |
| CN108452644A (en) | A kind of coal-burning power plant's carbon dioxide membrane trapping coupling nitrogen preparation process | |
| CN103589550A (en) | Carbon dioxide balanced system for beer brewing technology | |
| CN105271144A (en) | Device and method for extraction and refinement of N2O from petrochemical industrial tail gas | |
| JP2013525718A (en) | Method and apparatus for compressing and cooling air | |
| CN208990490U (en) | A kind of device of off-gas recovery dry ice | |
| CN103739024A (en) | Device and method for desalting seawater by gasified absorption heat of liquefied natural gas | |
| US2070099A (en) | Method of separating and purifying gases |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170808 |