CN109126392A - It is a kind of that CO in flue gas is carried out using ionic liquid2The device and technique of trapping - Google Patents
It is a kind of that CO in flue gas is carried out using ionic liquid2The device and technique of trapping Download PDFInfo
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- CN109126392A CN109126392A CN201811023173.XA CN201811023173A CN109126392A CN 109126392 A CN109126392 A CN 109126392A CN 201811023173 A CN201811023173 A CN 201811023173A CN 109126392 A CN109126392 A CN 109126392A
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- 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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D49/00—Separating dispersed particles from gases, air or vapours by other methods
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- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
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- 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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/30—Ionic liquids and zwitter-ions
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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
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- 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
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
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Abstract
The invention discloses one kind using ionic liquid as cyclic absorption agent, using low-boiling organic steam as circulation steam stripping agent, using high-gravity rotating bed as hypergravity regeneration and absorption plant, carries out CO in flue gas2Isolated device and technique are trapped, including the poor rich liquid heat exchanger connected according to certain way, rich solution heater, hypergravity regenerating unit, gas-liquid heat-exchange, condenser, gas-liquid separator, counterbalance valve, steam generator, lean solution delivery pump, lean solution cooler, hypergravity absorption plant, rich solution delivery pump, demister.The device of the invention and technique may be implemented to CO in flue gas2Effective trapping separation, have that decarburization efficiency is high, regeneration energy consumption is low, material consumption is low, equipment volume is small, advantages of environment protection, the CO suitable for the industrial smokes such as fire coal, plant gas2Trapping separation.
Description
Technical field
The present invention relates to one kind using ionic liquid as cyclic absorption agent, strips using low-boiling organic steam as circulation
Agent is used as absorption and desorption equipment using high-gravity rotating bed, the trapping separation CO from flue gas2, and obtain high-purity CO2Product gas
Device and technique.The advantages that present invention has decarburization efficiency high, and regeneration energy consumption is low, and equipment volume is small, environmentally friendly, is applicable in
In coal-burning power plant, CO in the industrial process flue gas such as plant gas2Trapping separation.
Background technique
The CO that coal-fired plant flue gas and other industrial circles largely discharge2, it is considered to be influence the one of Global climate change
A key factor controls CO2Gas discharge, mitigation of climate change have become the important composition portion of China's strategy of sustainable development
Point.Meanwhile CO2As important basic chemical, in chemical industry synthesis, food storage, the fields such as refrigeration are widely used, demand
It is huge.Therefore, CO in the industrial process flue gas such as coal-fired and plant gas2Trapping separation not only can be effectively controlled greenhouse gases row
It puts, moreover it is possible to obtain important basic chemical, there is important environmental value and economic value.
Currently, CO2Trapping technique and method mainly include adsorption separation method, membrane separation process, low temperature processing, solvent inhale
Receipts method etc..Wherein, the carbon capture technology based on chemical absorption method, CO2Removal efficiency it is high and be suitble to the CO such as coal-fired plant flue gas2
Divide lower operating condition.For traditional chemical absorption method using absorption tower as mass transfer apparatus, flue gas enters suction from absorb the bottom of the tower
Tower is received, contacts generation chemical reaction inversely with the absorbent solution sprayed by tower top in Ta Nei to reach removing CO2Purpose.It should
The power resources of reverse contact flow are gravitational fields between liquid phase in the process, and because gravity limits, liquid decrease speed is slower, together
When, in order to avoid liquid flooding and serious entrainment, the gas phase rate of climb is also smaller, therefore relative velocity is smaller between two-phase, passes
Matter is limited.In addition, chemical absorbent mostly uses alkaline aqueous solution or organic amine aqueous solution, absorbing liquid big to equipment extent of corrosion,
It is easy to produce volatile organic compounds (VOC) under desorption technique hot conditions, causes absorbent loss and secondary pollution.Base
In problem above, the advantages of the applicant (Beijing University of Chemical Technology) combines ionic liquid in 102580462 B of patent CN and
High-gravity rotating bed advantage, a kind of open new method for having invented collecting carbonic anhydride separation, this method is using anhydrous, no
Volatile ionic liquid is as absorbent, it is possible to prevente effectively from secondary pollution, prevents equipment from corroding, meanwhile, select hypergravity
Revolving bed is that absorption equipment enhances gas-liquid mass transfer efficiency, reduces the adverse effect that ionic liquid viscosity higher band is come.However,
Original patent of invention intermediate ion liquid-absorbant, which is not able to achieve, to be recycled, CO2Fail from absorbent after being captured effectively
Separation, therefore the CO of high-purity cannot be obtained2Product.The present invention is then improved on the basis of original invention,
It proposes the new use ionic liquid of one kind and carries out CO in flue gas2The process system of trapping, may be implemented ionic liquid absorbent
It recycles, and the CO of high-purity can be obtained2Product.
Above-mentioned purpose is realized, by CO2Efficiently separate from absorbent is important step.Traditional CO2Trap separating technology
In, such as hot potassium carbonate and organic amine absorption and separation CO2Technique can pass through reboiler since absorbent is aqueous solution
So that water vapor in absorbent is generated water vapour as stripping gas, stripped vapor in regenerator with rich solution counter current contacting, in heat
With CO is released under the action of steam2, the CO of release2It is separated by condensing with steam, becomes the CO of high-purity2Product gas；It can also
Steam stripped method is directly purged using water vapour and carries out absorbent regeneration, while obtaining high-purity CO2Product gas, such as CN
101549274A discloses one kind and directlys adopt water vapour conduct purging stripping gas progress hot potassium carbonate or organic amine absorbent regeneration,
High-purity CO is obtained simultaneously2The method of product gas is condensed in this method after water vapor desorption, sends absorbing liquid configuration back to
It realizes and recycles in tank.However, these traditional regeneration methods are not particularly suited for carrying out CO using ionic liquid2The work of trapping
Skill.On the one hand, ionic liquid is the water-free absorbent of the zwitterion composition of ionized state, itself has very low steaming
Air pressure, it is almost non-volatile, steam can not be generated by the reboiler technique in traditional hot potassium carbonate or organic amine absorbent method make
For stripping gas.And steam stripping regeneration is carried out using the mode that water vapour directly purges, part water vapour condenses in ionic liquid, meeting
Absorbent is reduced in the trapping effect of absorptive unit, meanwhile, greatly improve the energy consumption of entire technique.On the other hand, with aqueous solution
Absorbent is compared, ionic liquid viscosity usually with higher, its flowing slowly even is difficult to flow in traditional tower equipment
Dynamic, the effect of mass transfer and heat transfer is poor, and regeneration efficiency is low, and energy consumption is high.Therefore, absorbent is improved in highly viscous ionic liquid
Diffusion velocity reduces the energy consumption of regenerative process, is to realize to carry out CO using ionic liquid2Trap process industry it is crucial because
Element.Technical solution of the present invention then solves above-mentioned two critical issue, use first it is high-gravity rotating bed for core again
Generating apparatus enhances CO2Diffusion process in high viscosity ionic liquid；Secondly, the present invention uses low boiling point, small low of thermal capacitance
Boiling point organic steam is passed through organic steam purging ionic liquid absorption liquid in high-gravity rotating bed, strips it as steam stripping agent
In CO2, and the process by condensing and separating re-evaporation, realize recycling for stripping working medium, while significantly reducing CO2It catches
The energy consumption of collection process.
Summary of the invention
The object of the present invention is to provide one kind using super-gravity device as core equipment, using ionic liquid as absorbent, catches
Collection separation CO2Device and technique be suitable for coal-burning power plant, plant gas etc. wherein include complete desorption technique method
CO in industrial process flue gas2Trapping separation.
CO in flue gas is carried out using ionic liquid the invention proposes a kind of2The device of trapping, including (1) rich or poor liquid heat exchange
Device, (2) rich solution heater, (3) hypergravity regenerating unit, (4) gas-liquid heat-exchange, (5) condenser, (6) gas-liquid separator, (7)
Counterbalance valve, (8) steam generator, (9) lean solution delivery pump, (10) lean solution cooler, (11) hypergravity absorption plant, (12) rich solution
Delivery pump, (13) demister.Wherein, the liquid outlet of described (11) the hypergravity absorption plant is connected by (12) rich solution delivery pump
(1) poor rich liquid heat exchanger, one of (1) poor rich liquid heat exchanger outlet is by (2) rich solution heater and (3) hypergravity regenerating unit
Liquid-inlet is connected, and the liquid outlet of (3) hypergravity regenerating unit connects (1) poor rich liquid heat exchanger by (9) lean solution delivery pump,
Using the liquid-inlet of (10) lean solution cooler connection (11) hypergravity absorption plant, the gas of (11) hypergravity absorption plant
Outlet connection (13) demister, (13) demister liquid outlet connect the outlet tube road of (11) hypergravity absorption plant, and (3) are overweight
The gas vent of power regenerating unit connects (4) gas-liquid heat-exchange, and the outlet of (4) gas-liquid heat-exchange connects (6) gas by (5) condenser
Liquid/gas separator, (6) gas-liquid separator gas vent connect (7) counterbalance valve, and (6) gas-liquid separator liquid outlet passes through (4) gas-liquid
Heat exchanger, reconnects (8) steam generator, and (8) steam generator outlet connects (3) hypergravity regenerating unit air inlet.
Preferably, the hypergravity regenerating unit (3) and hypergravity absorption plant (11) are high-gravity rotating bed.
The present invention provides use above-mentioned apparatus to trap CO2Technique, specifically comprise the following steps:
(1) contain CO after cooling dedusting2Industrial smoke enter hypergravity absorption plant, and ionic liquid counter current contacting,
CO therein2By ionic liquid absorption, the flue gas after decarburization removes the liquid being entrained with by demister, is discharged or is sent to downstream
Technique；
(2) CO is absorbed in step (1)2Ionic liquid afterwards is conveyed by rich solution delivery pump, is exchanged heat by rich or poor liquid
Enter hypergravity regenerating unit after the preheating of device and rich solution heater to be desorbed；
(3) CO is absorbed in step (2)2Ionic liquid afterwards in hypergravity regenerating unit with the vapour from steam generator
Mention steam counter-flow contact, CO2It is transferred to gas phase from ionic liquid, leaves hypergravity regenerating unit with stripped vapor；
(4) gas-liquid heat-exchange is first passed through from the mixed gas that hypergravity regenerating unit leaves in step (3) recycle its heat,
It is further condensed using condenser, gas-liquid separation is carried out by gas-liquid separator later, the liquid phase isolated enters gas-liquid and changes
It is sent to steam generator after hot device preheating, is used for generating steam circulation again, CO2From gas-liquid separator separates, pass through
Counterbalance valve is sent to downstream process or collection；
(5) ionic liquid in step (3) after desorption leaves from hypergravity regenerating unit, is carried out by lean solution delivery pump
Conveying is sent to absorption section after recycling heat and lean solution cooler cooling by poor rich liquid heat exchanger so that cyclic absorption makes
With.
Preferably, in step (1), temperature, ionic liquid temperature are 15~60 in flue-gas temperature, hypergravity absorption plant
DEG C, most preferably 25~40 DEG C, the pressure of system is 0.1~0.5MPa when absorption；The hypergravity of hypergravity absorption plant is horizontal
It is 50~1000, gas-liquid volume flow ratio is 50:1~500:1；Absorbing liquid used is the ionic liquid containing basic functional group
Or mixed ionic liquid, including [proline oxycholine salt] ([Choline] [Pro]), [1- (3- Propylamino) -3- butyl miaow
The double trifluoro methylsulphur inferior amine salts of azoles] ([Apbim] [Tf2N]), [1- (1- aminopropyl) -3- butyl imidazole bromide] ([NH2p-mim]
[Br]) etc..
Preferably, step (2) intermediate ion liquid rich solution is heated to 50~150 DEG C.
Preferably, temperature is 50~150 DEG C in hypergravity regenerating unit in step (3), and pressure is 0.01~2MPa；It is overweight
The hypergravity level of power regenerating unit is 100~1000；The volume flow ratio of stripped vapor and ionic liquid rich solution be 30:1~
200:1；Stripped vapor used is the steam, including pentane, hexane, hexamethylene etc. of the lower organic matters of boiling points such as hydro carbons.
Preferably, the temperature of step (4) condensator outlet is 0~20 DEG C；Temperature is 50~100 DEG C in steam generator.
Preferably, the ionic liquid regenerated is cooled to 15~60 DEG C by lean solution cooler in step (5).
Compared with prior art, the present invention has following benefit:
(1) decarburization efficiency is high.The present invention specifically selects high-gravity rotating bed, reinforcing using super-gravity device as core equipment
CO2Mass transport process in highly viscous ionic liquid makes gas-liquid mass transfer breach the limitation of gravity, so that it is de- to reach depth
The purpose removed.
(2) regeneration energy consumption is low.In traditional CO2In regenerative process, a large amount of steam is needed to remove the CO in extracting rich solution2, this portion
Divide steam from absorbent itself, the part water in absorbent is heated to boiling point in reboiler, generates steam, this part
Steam rises along regenerator, in tower top with CO2After leaving regenerator, it is condensed and sends regenerator back to maintain the water in absorbent
It balances, the latent heat of water vapour is wasted in whole process, increases regenerated energy consumption.Regeneration technology according to the present invention is direct
It is passed through overheat organic steam into hypergravity regenerating unit as stripping gas and extracts CO2, then by organic steaming by way of condensation
Vapour and CO2Gas-liquid separation is carried out, condensate liquid can be vaporized again to be recycled as steam stripping agent, solves ionic liquid conduct
CO2Trapping cyclic absorption agent can not lead to the problem of stripped vapor.During this, condensate liquid can be first before vaporizing again
It is preheated with regenerative mixed gas, thus effectively reclaiming steam latent heat.In addition, regeneration technology side according to the present invention
In method, low boiling point has been used, thermal capacitance and the small organic steam of vaporization enthalpy are lowered regeneration energy consumption further, as pentane boils
Point 36.05 DEG C, 68.75 DEG C of n-hexane boiling point, this substance can generate a large amount of steam at lower temperatures, and have than water more
Low specific heat capacity and vaporization enthalpy, if pentane specific heat capacity is 2.25kJ/ (kgK), vaporization enthalpy 25.79kJ/mol, and water
Specific heat capacity is 4.2kJ/ (kgK), therefore vaporization enthalpy 40.63kJ/mol uses this kind of organic steam as needed for stripping gas
Heat much smaller than using water vapour as heat needed for stripping gas.
(3) material consumption is low.In process flow of the present invention, absorbent is used ionic liquid as, not due to absorbent
Volatilization, thermal stability is strong, and anti-degradation, therefore, absorbent is almost without loss.Meanwhile the present invention realizes absorbent ionic liquid
Body is recycled with stripping working medium organic steam, is effectively reduced material consumption, is reduced operating cost.
(4) equipment volume is small.In high-gravity rotating bed, gas-liquid mass transfer mass tranfer coefficient has one compared with conventional filler tower
The advantage of the order of magnitude, hypergravity equipment volume is small, and driving and parking is easy, and can carry out skid design.
(5) environmentally friendly.Ionic liquid fusing point is low, and liquid temperature range is not wide, volatile, not will cause VOC volatilization
Equal secondary pollutions, the use of the absorbent of non-alkaline aqueous solution also can effectively prevent equipment corrosion.
The present invention can be by the CO in flue gas2It is effectively separated trapping, CO2Removal efficiency can reach 90% or more, regeneration
CO2Purity can achieve 98% or more, with traditional hot potassium carbonate and organic amine aqueous solution CO2Capture method is compared, present invention process
Energy consumption can reduce by 20~30%.
Detailed description of the invention
Attached drawing Fig. 1 is that a kind of use ionic liquid of the invention carries out CO in flue gas2The schematic device of trapping.
In Fig. 1: 1- poor rich liquid heat exchanger, 2- rich solution heater, 3- hypergravity regenerating unit, 4- gas-liquid heat-exchange, 5- are cold
Condenser, 6- gas-liquid separator, 7- counterbalance valve, 8- steam generator, 9- lean solution delivery pump, 10- lean solution cooler, 11- hypergravity
Absorption plant, 12- rich solution delivery pump, 13- demister.
Specific embodiment
Referring to shown in attached drawing, embodiment of the present invention is described further with reference to the accompanying drawings and examples.
CO in flue gas is carried out using apparatus of the present invention2The technique of trapping is as follows: containing CO after cooling dedusting2Work
Industry flue gas, CO2Concentration is 15vol%, the CO into hypergravity absorption plant and ionic liquid absorbent counter current contacting, in flue gas2
It is absorbed, obtained purification gas is sent to smoke stack emission or send to downstream process, and the rich solution after absorbing exchanges heat by rich or poor liquid
Enter hypergravity regenerating unit after the preheating of device recycling heat and rich solution heater, carry out counter current contacting regeneration with stripped vapor,
Obtained regenerative mixed gas first passes through the heat of gas-liquid heat-exchange recovered steam, condenses steam using condenser, in gas-liquid
CO is isolated in separator2As product or it is sent to downstream process, condensate liquid sends steam generator back to and can be re-used for generating vapour
Steam is mentioned, the poor ionic liquid for regenerating generation can be re-used for absorbing after poor rich liquid heat exchanger recycling heat.
Embodiment 1
CO in flue gas is carried out using above-mentioned apparatus2Trapping.Wherein, ionic liquid absorbent used is [1- (3- propylamine
Base) the double trifluoro methylsulphur inferior amine salts of -3- butyl imidazole] ([Apbim] [Tf2N]), the temperature in hypergravity absorption plant is controlled 30
~40 DEG C, pressure is 0.1~0.2MPa, and hypergravity level is 150, and gas-liquid volume flow ratio is 150:1~200:1；Ionic liquid
Body rich solution is heated to 110 DEG C in rich solution heater；In hypergravity regenerating unit temperature be 110 DEG C, pressure be 0.1~
0.2MPa, hypergravity level are 200, and stripped vapor and ionic liquid rich solution volume flow ratio are 70:1~100:1, vapour used
Mentioning steam is pentane steam；Condensator outlet temperature is 0~10 DEG C；Temperature is 75 DEG C in steam generator；Lean solution cooler
The ionic liquid regenerated is cooled to 30~40 DEG C.
In hypergravity absorption plant gas vent sampling analysis, CO2Concentration is 1.5%, exports and samples in gas-liquid separator
Analysis, CO2Purity is up to 99%.
Embodiment 2
As described in Example 1, other conditions are constant, and hypergravity absorption plant temperature is adjusted to 50 DEG C.It absorbs and fills in hypergravity
Set gas vent sampling analysis, CO2Concentration is 1.8%, exports sampling analysis, CO in gas-liquid separator2Gas purity is reachable
99%.
Embodiment 3
As described in Example 1, other conditions are constant, and the hypergravity level of hypergravity absorption plant is adjusted to 200.In hypergravity
Absorption plant gas vent sampling analysis, CO2Concentration is 1.2%, exports sampling analysis, CO in gas-liquid separator2Gas purity can
Up to 99%.
Embodiment 4
As described in Example 1, other conditions are constant, and gas-liquid volume flow ratio is adjusted to 200:1 in hypergravity absorption plant
~250:1.In hypergravity absorption plant gas vent sampling analysis, CO2Concentration is 1.6%, exports and samples in gas-liquid separator
Analysis, CO2Gas purity is up to 99%.
Embodiment 5
As described in Example 1, other conditions are constant, and hypergravity regenerating unit temperature is adjusted to 120 DEG C.It absorbs and fills in hypergravity
Set gas vent sampling analysis, CO2Concentration is 1.3%, exports sampling analysis, CO in gas-liquid separator2Gas purity is reachable
99%.
Embodiment 6
As described in Example 1, other conditions are constant, and the hypergravity level of hypergravity regenerating unit is adjusted to 250.In hypergravity
Absorption plant gas vent sampling analysis, CO2Concentration is 1.2%, exports sampling analysis, CO in gas-liquid separator2Gas purity can
Up to 99%.
Embodiment 7
As described in Example 1, other conditions are constant, the body of stripped vapor and ionic liquid rich solution in hypergravity regenerating unit
Product flow-rate ratio is adjusted to 100:1~120:1.In hypergravity absorption plant gas vent sampling analysis, CO2Concentration is 1.1%,
Gas-liquid separator exports sampling analysis, CO2Gas purity is up to 99%.
Embodiment 8
As described in Example 1, other conditions are constant, and steam-generator temperature is adjusted to 90~100 DEG C.It absorbs and fills in hypergravity
Set gas vent sampling analysis, CO2Concentration is 1.2%, exports sampling analysis, CO in gas-liquid separator2Gas purity is reachable
99%.
Embodiment 9
As described in Example 1, other conditions are constant, 10~20 DEG C of condensator outlet temperature tune.It is exported in gas-liquid separator
Sampling analysis, CO2Purity is 98%.
Embodiment 10
As described in Example 1, other conditions are constant, and ionic liquid absorbent used is adjusted to [proline oxycholine salt]
([Choline][Pro]).In hypergravity absorption plant gas vent sampling analysis, CO2Concentration is 1.3%, in gas-liquid separator
Export sampling analysis, CO2Gas purity is up to 99%.
Comparative example 1
As described in Example 1, other conditions are constant, and hypergravity absorption plant temperature is adjusted to 65 DEG C.It is absorbed in hypergravity
Device gas vent sampling analysis, CO2Content 3.0%.
Comparative example 2
As described in Example 1, other conditions are constant, and the hypergravity level of hypergravity absorption plant is adjusted to 20.In hypergravity
Absorption plant gas vent sampling analysis, CO2Content 3.2%.
Comparative example 3
As described in Example 1, other conditions are constant, and the hypergravity level of hypergravity regenerating unit is adjusted to 20.In hypergravity
Absorption plant gas vent sampling analysis, CO2Concentration is 3.5%, exports sampling analysis, CO in gas-liquid separator2Gas purity can
Up to 99%.
Comparative example 4
As described in Example 1, other conditions are constant, and hypergravity regenerating unit temperature is adjusted to 40 DEG C.It absorbs and fills in hypergravity
Set gas vent sampling analysis, CO2Concentration is 3.5%, exports sampling analysis, CO in gas-liquid separator2Gas purity is reachable
99%.
Comparative example 5
As described in Example 1, other conditions are constant, and steam-generator temperature is adjusted to 40 DEG C.In hypergravity absorption plant gas
Body exports sampling analysis, CO2Concentration is 3.0%, exports sampling analysis, CO in gas-liquid separator2Gas purity is up to 99%.
Comparative example 6
As described in Example 1, other conditions are constant, and condensator outlet temperature is adjusted to 40 DEG C.It is taken in gas-liquid separator outlet
Sample analysis, CO2Purity 95%.
Comparative example 7
As described in Example 1, other conditions are constant, and stripped vapor used is changed to alcohol vapour.Reach it is identical removing and
Regeneration effect, steam-generator temperature improve 20~30 DEG C, and energy consumption improves 5%.
Comparative example 8
As described in Example 1, other conditions are constant, and stripped vapor used is changed to vapor.Reach it is identical removing and again
It comes into force fruit, steam-generator temperature improves 40~50 DEG C, and energy consumption improves 10%.
Comparative example 9
CO is removed using traditional MEA aqueous solution2And regenerated technique, MEA mass fraction 30%, regeneration is using again
It boils device and generates stripping steam, reach identical removing and regeneration effect, energy consumption increases by 20~30%.
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
Those familiar with the art in the technical scope disclosed by the present invention, can easily think of the change or the replacement, and should all contain
Lid is within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (10)
1. a kind of carry out CO in flue gas using ionic liquid2The device of trapping, it is characterised in that: including poor rich liquid heat exchanger (1),
Rich solution heater (2), hypergravity regenerating unit (3), gas-liquid heat-exchange (4), condenser (5), gas-liquid separator (6), counterbalance valve
(7), steam generator (8), lean solution delivery pump (9), lean solution cooler (10), hypergravity absorption plant (11), rich solution delivery pump
(12), demister (13), wherein the liquid outlet of the hypergravity absorption plant (11) connects poor by rich solution delivery pump (12)
The liquid of rich solution heater (2) and hypergravity regenerating unit (3) is passed through in rich solution heat exchanger (1), one of poor rich liquid heat exchanger (1) outlet
Body import is connected, and the liquid outlet of hypergravity regenerating unit (3) connects poor rich liquid heat exchanger (1) by lean solution delivery pump (9), then
By the liquid-inlet of lean solution cooler (10) connection hypergravity absorption plant (11), the gas of hypergravity absorption plant (11) goes out
Mouth connection demister (13), demister (13) liquid outlet connect the outlet tube road of hypergravity absorption plant (11), and hypergravity is again
The gas vent of generating apparatus (3) connects gas-liquid heat-exchange (4), and gas-liquid heat-exchange (4) outlet is by condenser (5) connection gas-liquid point
From device (6), gas-liquid separator (6) gas vent connects counterbalance valve (7), and gas-liquid separator (6) liquid outlet passes through gas-liquid heat exchange
Device (4) reconnects steam generator (8), steam generator (8) outlet connection hypergravity regenerating unit (3) air inlet.
2. the apparatus according to claim 1, it is characterised in that hypergravity regenerating unit (3) and hypergravity absorption plant (11)
It is high-gravity rotating bed.
3. a kind of carry out CO in flue gas using ionic liquid2The technique of trapping, which is characterized in that this technique includes the following steps:
(1), contain CO after cooling dedusting2Industrial smoke enter hypergravity absorption plant, and ionic liquid counter current contacting, wherein
CO2By ionic liquid absorption, the flue gas after decarburization removes the liquid being entrained with by demister, is discharged or is sent to downstream work
Skill；
(2), CO is absorbed in step (1)2Ionic liquid afterwards is conveyed by rich solution delivery pump, by poor rich liquid heat exchanger and
Enter hypergravity regenerating unit after the preheating of rich solution heater to be desorbed；
(3), CO is absorbed in step (2)2Ionic liquid afterwards steams in hypergravity regenerating unit with the stripping from steam generator
Vapour counter current contacting, CO2It is transferred to gas phase from ionic liquid, leaves hypergravity regenerating unit with stripped vapor；
(4), gas-liquid heat-exchange is first passed through from the mixed gas that hypergravity regenerating unit leaves in step (3) recycle its heat, then
It is further condensed by condenser, gas-liquid separation is carried out by gas-liquid separator later, the liquid phase isolated enters gas-liquid heat exchange
It is sent to steam generator after device preheating, is used for generating steam circulation again, CO2From gas-liquid separator separates, pass through back
Pressure valve is sent to downstream process or collection；
(5), the ionic liquid in step (3) after desorption leaves from hypergravity regenerating unit, is carried out by lean solution delivery pump defeated
It send, recycles heat and the cooling absorption section that is sent to later of lean solution cooler by poor rich liquid heat exchanger for cyclic absorption use.
4. technique according to claim 3, which is characterized in that in step (1), in flue-gas temperature, hypergravity absorption plant
Temperature, ionic liquid temperature are 15~60 DEG C, and the pressure of system is 0.1~0.5MPa when absorption；Hypergravity absorption plant surpasses
Gravity horizontal is 50~1000, and gas-liquid volume flow ratio is 50:1~500:1；Absorbing liquid used is containing basic functional group
Ionic liquid.
5. technique according to claim 4, which is characterized in that in step (1), in flue-gas temperature, hypergravity absorption plant
Temperature, ionic liquid temperature are 25~40 DEG C；The ionic liquid containing basic functional group is selected from [proline oxycholine
Salt], [1- (3- Propylamino) -3- butyl imidazole double trifluoro methylsulphur inferior amine salts], [1- (1- aminopropyl) -3- butyl imidazole bromide]
Or mixtures thereof.
6. technique according to claim 3, which is characterized in that step (2) intermediate ion liquid rich solution is heated to 50~150
℃。
7. technique according to claim 3, which is characterized in that in step (3) in hypergravity regenerating unit temperature be 50~
150 DEG C, pressure is 0.01~2MPa；The hypergravity level of hypergravity regenerating unit is 100~1000；Stripped vapor and ionic liquid
The volume flow ratio of body rich solution is 30:1~200:1；Stripped vapor used is low-boiling organic steam.
8. technique according to claim 7, which is characterized in that the stripped vapor includes pentane, hexane or hexamethylene etc..
9. technique according to claim 3, which is characterized in that the temperature of step (4) condensator outlet is 0~20 DEG C；It steams
Temperature is 50~100 DEG C in vapour generator.
10. technique according to claim 3, which is characterized in that the ionic liquid that lean solution cooler will regenerate in step (5)
Body is cooled to 15~60 DEG C.
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