CN202387354U - Equipment for capturing carbon dioxide in flue gas of power station and with high efficiency and low energy consumption - Google Patents

Equipment for capturing carbon dioxide in flue gas of power station and with high efficiency and low energy consumption Download PDF

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CN202387354U
CN202387354U CN2011205460588U CN201120546058U CN202387354U CN 202387354 U CN202387354 U CN 202387354U CN 2011205460588 U CN2011205460588 U CN 2011205460588U CN 201120546058 U CN201120546058 U CN 201120546058U CN 202387354 U CN202387354 U CN 202387354U
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pipeline
gas
heat exchanger
input port
absorption
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王志龙
张岩丰
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Wuhan Kaidi Engineering Technology Research Institute Co Ltd
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Wuhan Kaidi Engineering Technology Research Institute Co Ltd
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • 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
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals

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Abstract

The utility model relates to equipment for capturing carbon dioxide in flue gas of a power station, which has high efficiency and low energy consumption. The equipment comprises an absorption tower, a sloping plate clarification tank, a regenerating tower, a gas-liquid separator, a drier, a compressor and a condenser, and is characterized in that the underflow outlet of the sloping plate clarification tank is communicated with the first medium input port of a second heat exchanger through a pipeline, a pregnant solution pump is arranged on the pipeline, and the supernatant liquor overflow port of the sloping plate clarification tank is communicated with the input port of a circulating absorption liquid storage box through a pipeline; the output port of the circulating absorption liquid storage box is communicated with the spraying pipe at the spraying layer in the absorption tower through the pipeline, and an absorption liquid circulating pump is arranged on the pipeline; the second medium output port of the second heat exchanger is communicated with the input port of the circulating absorption liquid storage box through a pipeline, and a filter is arranged on the pipeline. The equipment has the advantages of high capturing efficiency, low energy consumption, and simple process flow.

Description

A kind of high-efficiency low energy consumption captures the equipment of carbon dioxide in the generating plant flue gas
Technical field
The utility model relates to the reduction of discharging and the application technology as the second resource field of carbon dioxide in the flue gas in power station boiler, refers to a kind of equipment that captures carbon dioxide in the generating plant flue gas particularly.
Background technology
Get into 21st century; One of human ultimate challenge that is faced is " greenhouse effects " that greenhouse gases caused of a large amount of dischargings, causes global warming, climate change thus and to the global environment problem of aspects such as ecology, economy, society generation combined influence.Carbon dioxide is the primary product of organic substance and fossil fuel burning, also is considered to one of main component that causes greenhouse effects and global warming simultaneously, accounts for 2/3 of greenhouse gases.At present, the CO2 emissions that the whole world is annual rose to 30,600,000,000 tons in 2010, and China has become CO2 emission first big country, and discharge capacity is also in continuous increase.
In November, 2009, China is to world's solemn commitment: to the GDP CO2 emission of the year two thousand twenty unit than decline 40%～45% in 2005.And generating plant flue gas is CO 2The emission source of concentrating steady in a long-term is CO 2The most important thing that reduces discharging, exploitation generating plant flue gas CO 2Reduce discharging new technology and device, make China's economic development avoid the influence of carbon emission index, its social benefit and economic benefit are huge.
CO 2Capture method has multiple, and what commercial Application was more is chemical absorption method, and its principle is the CO in the flue gas 2React with chemical solvent and be absorbed, absorb CO 2The chemical solvent that reaches balance becomes rich solution, and rich solution gets into the regenerator heating and decomposition and emits CO 2Gas and become lean solution, lean solution go to circulate again and absorb the CO in the flue gas 2, so through absorbent solution circular flow in absorption tower and regenerator, the CO in the flue gas 2Obtain separating purifying and be captured down.Absorb CO with alkanolamine solution at present 2Chemical absorption method use the extensivelyst, mainly contain MEA, MDEA and mix absorbent such as organic amine.Actual engineering is verified; In the alkanolamine solution absorption process of chemical field application recent two decades, though infiltration rate is fast, absorbability is strong, when being used in generating plant flue gas; The ubiquity drawback: (1) hydramine oxidative degradation foaming influences equipment operation steady in a long-term, and solution losses is also bigger; (2) equipment corrosion is serious; (3) concentration of MEA absorbs CO usually below 20% 2Amount limited, the regeneration energy consumption is high; Above reason causes the cost that adopts alkanolamine solution to reclaim carbon dioxide very high.
Summary of the invention
The purpose of the utility model is to provide a kind of high-efficiency low energy consumption to capture the equipment of carbon dioxide in the generating plant flue gas, and this equipment can be realized the purpose that arresting efficiency is high, energy consumption is low.
For realizing above-mentioned purpose, the technical scheme that the utility model is taked is: a kind of high-efficiency low energy consumption captures the equipment of carbon dioxide in the generating plant flue gas, and it comprises absorption tower, swash plate depositing reservoir, regenerator, gas-liquid separator, drier, compressor and condenser; The rich solution of bottom, absorption tower carries out layering from flowing into the swash plate depositing reservoir, and the gas vent of gas-liquid separator is connected with drier, compressor, condenser and liquid carbon dioxide accumulator tank successively;
It is characterized in that:
The outlet of the underflow of swash plate depositing reservoir is through pipeline be connected with first medium (mixing coagulation liquid) input port of second heat exchanger (carrying out the intensification first time); Described pipeline is provided with the rich solution pump, and the supernatant overfall of swash plate depositing reservoir is connected through the input port of pipeline with the circulating absorption solution storage tank; The delivery outlet of circulating absorption solution storage tank is connected through the shower of the spraying layer in pipeline and the absorption tower, and said pipeline is provided with the absorption liquid circulating pump;
First medium of second heat exchanger (mixing coagulation liquid) delivery outlet is through pipeline be connected with first medium (mixing coagulation liquid) input port of first heat exchanger (carry out the second time heat up); First medium of first heat exchanger (mixing coagulation liquid) delivery outlet is connected through the import of pipeline with regenerator top; The gas liberation port at the second heat exchanger top is connected through the pipeline that links to each other between pipeline and first heat exchanger and the cooler; The gas vent on regenerator top is through the second medium (gas of the pipeline and first heat exchanger; Heat first medium) input port is connected; The second medium delivery outlet of first heat exchanger is connected with the input port of cooler through pipeline, and the delivery outlet of cooler links to each other with the import of gas-liquid separator through pipeline;
The liquid outlet of regenerator bottom is connected with the second medium input port of second heat exchanger through pipeline; Said pipeline is provided with lean pump; The second medium delivery outlet of second heat exchanger is connected through the input port of pipeline with the circulating absorption solution storage tank, and said pipeline is provided with filter; The condensation water overfall of gas-liquid separator is connected through the input port of pipeline with the circulating absorption solution storage tank; The solution storage tank that is used to store the composite absorber aqueous solution is connected through the input port of pipeline with the circulating absorption solution storage tank, and said pipeline is provided with solution pump.
Described absorption tower is pneumatic bubble tower; Be disposed with sieve plate, pneumatic bubble level, packing layer and demister from bottom to top in the absorption tower between the exhanst gas outlet at the gas approach of bottom, absorption tower and top, absorption tower; Also be provided with spraying layer in the absorption tower; Spraying layer is provided with 2～4 showers altogether; Every shower is provided with a plurality of nozzles (spray head), and the manhole area of sieve plate and the ratio of plate area are 30～40%, and demister is made up of upper and lower two layers of demist filter screen and the cleaning sprinkler part between upper and lower two layers of demist filter screen.
A kind of high-efficiency low energy consumption captures the method for carbon dioxide in the generating plant flue gas, it is characterized in that it comprises the steps:
1) press organic amine and ion liquid mol ratio and be (1～1.1): 1, organic amine, ionic liquid and water are mixed, obtain the composite absorber aqueous solution, wherein the concentration of the composite absorber aqueous solution is 20～40wt%;
The composite absorber aqueous solution of forming with organic amine and ionic liquid is as CO 2Absorbent evenly is ejected into the composite absorber aqueous solution through in the station boiler tail flue gas after conventional dedusting and the desulfurization processing, makes the flue gas that moves upward contact CO in flue gas with the composite absorber aqueous solution full regression that sprays downwards 2Gas and composite absorber generation gas-liquid two-phase chemical reaction and be absorbed, composite absorber absorbs CO 2Mechanism as follows; (A-organic amine; The B-ionic liquid; Following reaction equation is not represented actual course of reaction, wherein comprises physical absorption and chemical absorbing);
A+CO 2→A·CO 2
B+CO 2→B·CO 2
The control liquid-gas ratio is at 5～25L/m 3Scope, CO in the flue gas 2Can be with the reaction temperature of the composite absorber aqueous solution preferably 40～55 ℃ scope, reaction pressure is 0.01～10atm; Like this, the composite absorber aqueous solution can be under suitable temperature and pressure with flue gas in CO 2Reaction fully completely takes place, and generates and is rich in ACO 2And BCO 2Liquid;
2) absorbed CO 2Be rich in ACO 2And BCO 2Two kinds of materials, through the cohesion of self, form the different liquids layer through static clarification; Be rich in ACO 2And BCO 2Liquid be in lower floor, the composite absorber aqueous solution is in the upper strata, then lower floor's solution separating is come out, and obtains being rich in ACO 2And BCO 2Mixing material;
That separates is rich in ACO 2And BCO 2Mixing material through heat exchange, be rich in ACO 2And BCO 2Mixing material in by the portion C O of composite absorber aqueous solution dissolving or absorption 2Gas just is evaporated, and obtains heat exchange and comes out to be rich in ACO 2And BCO 2Mixing material;
3) heat exchange is come out to be rich in ACO 2And BCO 2Mixing material heat dissection process, the CO of chemical absorbing 2Parsed, regeneration obtains high concentration CO 2The gas and the composite absorber aqueous solution; Its chemical reaction mechanism is:
A·CO 2→A+CO 2↑
A+B·CO 2→A·CO 2+B→A+B+CO 2↑
4) the step 3) gained composite absorber aqueous solution is returned in the step 1), as CO 2Absorbent continues to recycle;
5) to the isolated high concentration CO of step 3) 2Gas carries out cooling processing, the hot water and steam that wherein contains is produced condense;
6) to the high concentration CO of step 5) cooling processing 2Gas carries out gas-liquid separation to be handled, and removes the moisture content that condenses wherein, obtains the CO of purity>=99% 2Gas (high-purity CO 2Gas);
7) with step 6) gained high-purity CO 2Gas is further dry, and (baking temperature is 110 ℃, and the time is 0.1～5min), again through overcompression and condensation process, with its liquefy, processes high-concentration industrial level liquid carbon dioxide finished product.
In above-mentioned steps 1) in, ionic liquid can be any one or any mixing that (contains two kinds) more than two kinds in conventional ion liquid, functionalized ion liquid, the polymeric ionic liquid, and any is any proportioning when (containing two kinds) more than two kinds and mixing.
Conventional ion liquid comprises any one or any mixing that (contains two kinds) more than two kinds in imidazole salt, pyrroles's salt, pyridine salt, ammonium salt class, the Sulfonates ionic liquid, and any is any proportioning when (containing two kinds) more than two kinds and mixing.
Described functionalized ion liquid is for introducing amino ionic liquid.
Described conventional ion liquid is any one or any mixing that (contains two kinds) more than two kinds in the two fluoroform sulfimide salt of 1-butyl-3-methyl imidazolium tetrafluoroborate, 1-butyl-3-methylimidazole hexafluorophosphate, 1-hexyl-3-methylimidazole, the 1-hexyl-3-methylimidazole hexafluorophosphate etc., and any is any proportioning when (containing two kinds) more than two kinds and mixing.
The amino ionic liquid of described introducing is any one or any mixing that (contains two kinds) more than two kinds in 1-(1-aminopropyl)-3-methylimidazole bromine salt, 1-(3 the Propylamino)-3-butyl imidazole tetrafluoroborate etc., and any is any proportioning when (containing two kinds) more than two kinds and mixing.
Described polymeric ionic liquid for gather 1-(4-styryl)-3-methyl imidazolium tetrafluoroborate, gather 1-(4-styryl)-3-methylimidazole hexafluorophosphate, gather 1-(4-styryl)-the adjacent benzene methylsulfonyl of 3-methylimidazole inferior amine salt, gather 1-(4-styryl)-3-methylimidazole fluoroform sulfimide salt and any one or any mixing that (contains two kinds) more than two kinds that gather in 1-(4-styryl)-3-methyl imidazolium tetrafluoroborate etc., any is any proportioning when (containing two kinds) more than two kinds and mixing.
In above-mentioned steps 1) in, organic amine is any one or any mixing that (contains two kinds) more than two kinds in monoethanolamine (MEA), the N methyldiethanol amine alcamines such as (MDEA), any is any proportioning when (containing two kinds) more than two kinds and mixing.
In above-mentioned steps 3) in, the heating dissection process is under 80～110 ℃ of temperature, pressure 0.01～10atm, to resolve, the parsing time is 1～5min, ACO 2Decompose at first rapidly, i.e. ACO 2Decompose generation A, and discharge CO 2, BCO 2Be difficult for discharging CO with this understanding 2Because A will be easy to capture absorption BCO in solution 2In CO 2Generate ACO 2, follow ACO 2Continue to decompose and discharge CO 2
In above-mentioned steps 5) in, carrying out cooling processing is with the isolated high concentration CO of institute 2Gas cooled is handled the optimum temperature range to 20～35 ℃, and be 1～5min cool time.Like this, the wherein water recovery of the overwhelming majority is come out, return the Analytic Tower recycle then.
The utlity model has following outstanding effect:
1, adopt said structure, this equipment can be realized the purpose that arresting efficiency is high, energy consumption is low.
2, the composite absorber aqueous solution that adopts organic amine and ionic liquid to form, the removal efficiency of carbon dioxide is higher by 10% than amine process; Two kinds of materials all absorb or absorbing carbon dioxide, absorption or the carbon dioxide that absorbs in the unit volume, and through the short decomposition of the inner transmission of regenerator, can be fast with the carbon dioxide release of all regenerating; This method has the high characteristics of arresting efficiency.
And this composite absorber aqueous solution product is prone to the phase inter coagulation; Form the different liquids layer with water; Be full of carbon dioxide the product liquid level partly be separated and get into regenerator regeneration, having reduced the aqueous solution, to get into regenerator inner, thereby reduced system energy consumption in a large number;
Behind second heat exchanger (poor rich liquid heat exchanger), just come out by the portion gas of composite absorber dissolving or absorption in the rich solution by the lean solution heating evaporation, reduce the quality that gets into heating rich solution in the regenerator, thereby reduced energy consumption; The low temperature rich solution that comes out from the absorption tower simultaneously improves the temperature of rich solution through the high-temperature barren liquor of regenerator bottom, twice heating of high temperature carbon dioxide gas at top, further reduces system energy consumption; Top high temperature carbon dioxide gas has reduced the cooling water consumption of cooler thereafter through the heat exchange cooling of rich solution, reduces energy consumption once more.
3, simple, investment of its device structure and operating cost are low.The utility model has overcome that the amine process equipment corrosion is serious, the regeneration energy consumption is high, utilize ionic liquid almost not have the advantage of vapour pressure to reduce the shortcomings such as easy loss of simple organic amine as absorbent.
Description of drawings
Fig. 1 is the structural representation of the utility model equipment.
Among the figure: 1-absorption tower, 2-spraying layer, 3-packing layer, the pneumatic bubble level of 4-, 5-sieve plate, 6-gas approach; 7-swash plate depositing reservoir, 8-rich solution pump, 9-absorption liquid circulating pump, 10-circulating absorption solution storage tank, 11-solution pump, 12-solution storage tank; The 13-lean pump, 14-reboiler, 15-liquid carbon dioxide accumulator tank, 16-condenser, 17-compressor; The 18-drier, 19-gas-liquid separator, 20-cooler, 21-first heat exchanger, 22-regenerator; 23-second heat exchanger (poor rich liquid heat exchanger), 24-filter, 25-nozzle, 26-demister, 27-exhanst gas outlet.
The specific embodiment
In order to understand the utility model better, further illustrate the content of the utility model below in conjunction with accompanying drawing and embodiment, but the content of the utility model not only is confined to following embodiment.
Embodiment 1:
As shown in Figure 1; A kind of high-efficiency low energy consumption captures the equipment of carbon dioxide in the generating plant flue gas, and it comprises absorption tower 1, swash plate depositing reservoir 7, second heat exchanger 23, first heat exchanger 21, regenerator 22, gas-liquid separator 19, drier 18, compressor 17 and condenser 16;
Absorption tower 1 is pneumatic bubble tower, and the top on absorption tower 1 is that packing layer, middle part are that pneumatic bubble level, lower floor are sieve plate; Regenerator 22 is a sieve-plate tower;
Be disposed with sieve plate 5, pneumatic bubble level 4, packing layer 3 and demister 26 from bottom to top in the absorption tower 1 between the exhanst gas outlet 27 at the gas approach 6 of 1 bottom, absorption tower and 1 top, absorption tower; Also be provided with spraying layer 2 in the absorption tower 1; Spraying layer 2 is provided with 2～4 showers altogether and (among Fig. 1 is 3; First top that is positioned at sieve plate 5; Second top that is positioned at pneumatic bubble level 4, the 3rd top that is positioned at packing layer 3), every shower is provided with a plurality of nozzles (spray head) 25, and (concrete quantity is confirmed according to flow; Establish 2-20 nozzle on general every shower); The manhole area of sieve plate 5 and the ratio of plate area are 30～40%, and demister 26 is made up of upper and lower two layers of demist filter screen and the cleaning sprinkler part between upper and lower two layers of demist filter screen, to remove the composite absorber drop of carrying secretly in the flue gas fully;
The rich solution outlet of 1 bottom, absorption tower is connected through the input port of pipeline with swash plate depositing reservoir 7; The rich solution of 1 bottom, absorption tower carries out layering from flowing into swash plate depositing reservoir 7; Supernatant in swash plate depositing reservoir 7 (for the composite absorber aqueous solution) is main; Underflow in swash plate depositing reservoir 7 is main with product mixing coagulation liquid; The underflow outlet of swash plate depositing reservoir 7 is connected with first medium (mixing coagulation liquid) input port of second heat exchanger 23 (carrying out heating up the first time) through pipeline, and described pipeline is provided with rich solution pump 8, and the supernatant overfall of swash plate depositing reservoir 7 is connected through the input port of pipeline with circulating absorption solution storage tank 10; The delivery outlet of circulating absorption solution storage tank 10 is connected through the shower of the spraying layer 2 in pipeline and the absorption tower 1, and said pipeline is provided with absorption liquid circulating pump 9;
First medium of second heat exchanger 23 (mixing coagulation liquid) delivery outlet is through pipeline be connected with first medium (mixing coagulation liquid) input port of first heat exchanger 21 (carry out the second time heat up); First medium of first heat exchanger 21 (mixing coagulation liquid) delivery outlet is connected through the import of pipeline with regenerator 22 tops; The gas liberation port at second heat exchanger, 23 tops is connected through the pipeline that links to each other between pipeline and first heat exchanger 21 and the cooler 20; The gas vent on regenerator 22 tops is through the second medium (gas of the pipeline and first heat exchanger 21; Heat first medium) input port is connected; The second medium delivery outlet of first heat exchanger 21 is connected through the input port of pipeline with cooler 20, and the delivery outlet of cooler 20 links to each other with the import of gas-liquid separator 19 through pipeline;
Be arranged on the bottom outside of regenerator with regenerator 22 supporting reboilers 14, the delivery outlet of reboiler 14 is connected with regenerator bottom reservoir through pipeline, and the input port of reboiler 14 is connected through pipeline reservoir bottom regenerator; The liquid outlet of regenerator 22 bottoms is connected with the second medium input port of second heat exchanger 23 through pipeline; Said pipeline is provided with lean pump 13; The second medium delivery outlet of second heat exchanger 23 is connected through the input port of pipeline with circulating absorption solution storage tank 10, and said pipeline is provided with filter 24;
The gas vent of gas-liquid separator 19 is connected with drier 18, compressor 17, condenser 16 and liquid carbon dioxide accumulator tank 15 successively; The condensation water overfall of gas-liquid separator 19 is connected through the input port of pipeline with circulating absorption solution storage tank 10;
The solution storage tank 12 that is used to store the composite absorber aqueous solution is connected through the input port of pipeline with circulating absorption solution storage tank 10, and said pipeline is provided with solution pump 11 (the composite absorber aqueous solution and the water that replenish join solution storage tank 12).
Above each several part equipment is the chemical field common equipment, and its concrete structure repeats no more.
The gas approach top of bottom, above-mentioned absorption tower is provided with the sieve plate that impels flue gas evenly to distribute and contact with gas-liquid, and the ratio of the hole area of sieve plate and plate area is 30～40%.Like this, flue gas is upwards through behind the sieve plate on the one hand, and the air-flow more even distribution has effectively been eliminated flue gas stream dead angle, helps flue gas and fully contacts with absorbent solution; On the other hand under the mutual jet-action of many group showers, can reach more than 300% the spray coverage rate in cross section, absorption tower, the carbon dioxide in the flue gas is fully contacted with absorption liquid, can fully fully react and be absorbed.
Poor rich liquid heat exchanger is set; The rich bottoms liquid outlet of swash plate depositing reservoir links to each other with the upper inlet of regenerator through rich solution pump, second (rich or poor liquid) heat exchanger, first heat exchanger, and the outlet of regenerator lean solution links to each other with circulating absorption solution storage tank top inlet through lean pump, second (rich or poor liquid) heat exchanger.Like this, can make full use of the waste heat of regenerator lean solution and regenerator outlet flue gas, the rich solution preheating that give to get into regenerator, the flue gas cool-down that comes out in the lean solution of being come out in the regenerator bottom simultaneously and top is realized the benign cycle of heat exchange, the saving heat resource.
Operation principle is following:
After conventional dedusting of process of station boiler tail flue gas and desulfurization are handled, in the gas approach 6 entering absorption towers 1 by 1 bottom, absorption tower, up through air-flow distribution, pneumatic bubble level 4, the packing layer 3 of sieve plate 5.Meanwhile, the composite absorber aqueous solution sprays downwards through spraying layer 2, and the control liquid-gas ratio is at 5～25L/m 3Scope, CO in the flue gas 2Can be with the reaction temperature of the composite absorber aqueous solution preferably 40～55 ℃ scope, reaction pressure is 0.01～10atm.At this moment, the CO in the flue gas 2Gas contacts CO at packing layer 3 with pneumatic bubble level 4 place's full regressions with the composite absorber aqueous solution 2By chemical absorbing or be adsorbed onto in the solution.
Be removed most of CO 2Flue gas continue upwards to flow, remove the absorbent droplet through the demister 26 that is arranged in 1 top, absorption tower after, cleaning flue gases directly enters atmosphere.And absorption CO 2The rich solution that the back generates falls into the bottom on absorption tower 1, flows into swash plate depositing reservoir 7 certainly and condenses layering, and supernatant is the solution that contains a small amount of composite absorber, and underflow is main with the composite absorber product slurries of cohesion.Swash plate depositing reservoir underflow through rich solution pump 8 carry that tube side through second heat exchangers (poor rich liquid heat exchanger) 23 once heats up, secondary temperature elevation in first heat exchanger 21, send in the tower from the upper inlet of regenerator 22 then.Rich solution is partly dissolved or CO absorption after heating through second heat exchanger (poor rich liquid heat exchanger) 23 2Gas is released out.
Be absorbed or CO absorption 2Rich solution is sprayed to regenerator 22, and successively through each sieve plate, the Steam Heating that the product of composite absorber is risen is decomposed, CO 2Be released out, decompose infull composite absorber product slurries and fall at the bottom of the tower, be heated to 80～110 ℃, further parse high concentration CO through tower bottom reboiler 14 2Gas makes the composite absorber product resolve fully simultaneously.
The CO that parses 2Gas is flowed out by the upper gas outlet of regenerator 22 in company with a large amount of water vapours; Get into first heat exchanger 21; Rich solution to after second heat exchanger (poor rich liquid heat exchanger), 23 heating heats once more; Gas and entering cooler 20 after the gas that discharges through second heat exchanger (poor rich liquid heat exchanger) 23 heating mixes after the heat exchange are at this CO 2Air-flow is cooled to 25～35 ℃, and most of water vapor is wherein freeze-outed.
Regenerator 22 decomposes the composite absorbent agent solution that produces; Promoting tube side that the back gets into second heat exchangers (poor rich liquid heat exchanger) 23 through lean pump 13 emits after heat is cooled; Get into filter 24; Remove the heavy metal that dissolves in the flue gas or react the impurity that produces; Handle pure composite absorbent agent solution and flow to the circulating absorption solution storage tank 10 certainly from a high position, the composite absorber and the fresh water (FW) that replenish join solution storage tank 12, and solution storage tank 12 adds to and circulating absorption solution storage tank 10 through solution pump 11.Circulating absorption solution is transported to through the absorption liquid circulating pump that spraying layer 2 sprays absorption in the absorption tower.
High concentration CO after subcooler 20 is handled 2Gas gets in the gas-liquid separator 19, through centrifugal action with CO 2The condensation water of carrying secretly in the gas is separated fully, obtains purity and is higher than 99% CO 2Gas.Isolated condensation water from the outlet of the condensation water of gas-liquid separator 19 from flowing into the circulating absorption solution storage tank 10, recycle.Isolated high-purity CO 2Gas is then sent into drier 18, after dried, delivers to compressor 17, after processed compressed, gets into condenser 16 again, is condensed into liquid state, processes high-concentration industrial class liquid CO 2 finished product, sends at last in the liquid carbon dioxide accumulator tank 15 and preserves.
A kind of high-efficiency low energy consumption captures the method for carbon dioxide in the generating plant flue gas, and it comprises the steps:
1) is 1.01: 1 by organic amine and ion liquid mol ratio, organic amine, ionic liquid and water mixed that obtain the composite absorber aqueous solution, wherein the concentration of the composite absorber aqueous solution is 20wt%;
Described ionic liquid is the 1-butyl-3-methyl imidazolium tetrafluoroborate in the conventional ion liquid;
Described organic amine is monoethanolamine (MEA);
The composite absorber aqueous solution of forming with organic amine and ionic liquid is as CO 2Absorbent evenly is ejected into the composite absorber aqueous solution through in the station boiler tail flue gas after conventional dedusting and the desulfurization processing, makes the flue gas that moves upward contact CO in flue gas with the composite absorber aqueous solution full regression that sprays downwards 2Gas and composite absorber generation gas-liquid two-phase chemical reaction and be absorbed;
The control liquid-gas ratio is 20L/m 3(liquid refers to the composite absorber aqueous solution, and gas refers to flue gas), CO in the flue gas 2With the reaction temperature of the composite absorber aqueous solution be 50 ℃ scope, the absorption tower inlet pressure is 1.2atm; Like this, the composite absorber aqueous solution can be under suitable temperature and pressure with flue gas in CO 2Reaction fully completely takes place, and generates and is rich in ACO 2And BCO 2Liquid, A is an organic amine; B is a functionalized ion liquid;
2) absorbed CO 2Be rich in ACO 2And BCO 2Two kinds of materials, through the cohesion of self, form the different liquids layer through static clarification; Be rich in ACO 2And BCO 2Liquid be in lower floor, the composite absorber aqueous solution is in the upper strata, then lower floor's solution separating is come out;
3) will separate and be rich in ACO 2And BCO 2Liquid heat dissection process, row heating dissection process is under 100 ℃ of temperature, regenerator outlet pressure 0.3atm (be 2min heat time heating time), ACO 2Decompose at first rapidly, i.e. ACO 2Decompose generation A, and discharge CO 2, BCO 2Be difficult for discharging CO with this understanding 2Because A will be easy to capture absorption BCO in solution 2In CO 2Generate ACO 2, follow ACO 2Continue to decompose and discharge CO 2Regeneration obtains high concentration CO 2The gas and the composite absorber aqueous solution;
4) the step 3) gained composite absorber aqueous solution is returned in the step 1), as CO 2Absorbent continues to recycle;
5) to the isolated high concentration CO of step 3) 2Gas carries out cooling processing, the hot water and steam that wherein contains is produced condense; Carrying out cooling processing is with the isolated high concentration CO of institute 2Gas cooled is handled to 30 ℃ (are 1.5min cool time); Like this, the wherein water recovery of the overwhelming majority is come out, return the Analytic Tower recycle then;
6) to the high concentration CO of step 5) cooling processing 2Gas carries out gas-liquid separation and handles through gas-liquid separator, and the water vapour that will condense is separated, and obtains purity and is higher than 99% CO 2Gas;
7) with step 6) gained high-purity CO 2Gas is dry (baking temperature is 110 ℃, and the time is 2min) further, passes through compressor compresses and heat exchange condensation process to 20 ℃, 72atm again, with its liquefy CO 2, promptly can be made into high-concentration industrial level liquid carbon dioxide finished product.
Record through experiment:
Absorption tower inlet flue gas CO 2Content 12% (volume), absorption tower outlet flue gas CO 2Content 0.7% (volume), carbon dioxide absorption efficient reaches 94.2%;
Tradition MEA absorbs CO 2The regeneration energy consumption is 2.1 * 10 7KJ/h, it is 1.52 * 10 that this experiment records the regeneration energy consumption 7KJ/h, energy consumption reduces by 27.6%.

Claims (2)

1. a high-efficiency low energy consumption captures the equipment of carbon dioxide in the generating plant flue gas, and it comprises absorption tower (1), swash plate depositing reservoir (7), regenerator (22), gas-liquid separator (19), drier (18), compressor (17) and condenser (16); The rich solution of bottom, absorption tower (1) carries out layering from flowing into swash plate depositing reservoir (7), and the gas vent of gas-liquid separator (19) is connected with drier (18), compressor (17), condenser (16) and liquid carbon dioxide accumulator tank (15) successively;
It is characterized in that:
The underflow outlet of swash plate depositing reservoir (7) is connected with the first medium input port of second heat exchanger (23) through pipeline; Described pipeline is provided with rich solution pump (8), and the supernatant overfall of swash plate depositing reservoir (7) is connected through the input port of pipeline with circulating absorption solution storage tank (10); The delivery outlet of circulating absorption solution storage tank (10) is connected through the shower of the interior spraying layer (2) in pipeline and absorption tower (1), and said pipeline is provided with absorption liquid circulating pump (9);
The first medium delivery outlet of second heat exchanger (23) is connected with the first medium input port of first heat exchanger (21) through pipeline; The first medium delivery outlet of first heat exchanger (21) is connected through the import of pipeline with regenerator (22) top; The gas liberation port at second heat exchanger (23) top is connected through the pipeline that links to each other between pipeline and first heat exchanger (21) and the cooler (20); The gas vent on regenerator (22) top is connected with the second medium input port of first heat exchanger (21) through pipeline; The second medium delivery outlet of first heat exchanger (21) is connected through the input port of pipeline with cooler (20), and the delivery outlet of cooler (20) links to each other with the import of gas-liquid separator (19) through pipeline;
The liquid outlet of regenerator (22) bottom is connected with the second medium input port of second heat exchanger (23) through pipeline; Said pipeline is provided with lean pump (13); The second medium delivery outlet of second heat exchanger (23) is connected through the input port of pipeline with circulating absorption solution storage tank (10), and said pipeline is provided with filter (24); The condensation water overfall of gas-liquid separator (19) is connected through the input port of pipeline with circulating absorption solution storage tank (10); The solution storage tank (12) that is used to store the composite absorber aqueous solution is connected through the input port of pipeline with circulating absorption solution storage tank (10), and said pipeline is provided with solution pump (11).
2. a kind of high-efficiency low energy consumption according to claim 1 captures the equipment of carbon dioxide in the generating plant flue gas; It is characterized in that: described absorption tower (1) is pneumatic bubble tower; Be disposed with sieve plate (5), pneumatic bubble level (4), packing layer (3) and demister (26) from bottom to top in the absorption tower (1) between the exhanst gas outlet (27) at the gas approach (6) of bottom, absorption tower (1) and top, absorption tower (1); Also be provided with spraying layer (2) in the absorption tower (1); Spraying layer (2) is provided with 2～4 showers altogether; Every shower is provided with a plurality of nozzles (25), and the manhole area of sieve plate (5) and the ratio of plate area are 30～40%, and demister (26) is made up of upper and lower two layers of demist filter screen and the cleaning sprinkler part between upper and lower two layers of demist filter screen.
CN2011205460588U 2011-12-23 2011-12-23 Equipment for capturing carbon dioxide in flue gas of power station and with high efficiency and low energy consumption Withdrawn - After Issue CN202387354U (en)

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Cited By (8)

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CN102553396A (en) * 2011-12-23 2012-07-11 武汉凯迪工程技术研究总院有限公司 Method for trapping carbon dioxide in flue gas of power station with high efficiency and low energy consumption and equipment adopting same
CN103591603A (en) * 2012-08-16 2014-02-19 中国石油化工集团公司 Synchronous decarburization method in flue gas afterheat recovery of heating furnace
CN104772007A (en) * 2014-01-14 2015-07-15 现代自动车株式会社 Reboiling device and regeneration tower
CN105457447A (en) * 2015-12-16 2016-04-06 中石化节能环保工程科技有限公司 Carbon dioxide trapping system based on diphase system
CN106881010A (en) * 2017-04-18 2017-06-23 长沙紫宸科技开发有限公司 A kind of double-tower type circularly trapping device for being adapted to continuous collecting carbon dioxide from fuel gas
CN107115776A (en) * 2017-04-18 2017-09-01 长沙紫宸科技开发有限公司 One kind CO suitable for cement kiln flue gas2The change system continuously trapped
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CN115523004A (en) * 2022-10-18 2022-12-27 北京百利时能源技术股份有限公司 Amine process CO 2 Process medium heat energy recovery combined power generation device and method in trapping device

Cited By (12)

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Publication number Priority date Publication date Assignee Title
CN102553396A (en) * 2011-12-23 2012-07-11 武汉凯迪工程技术研究总院有限公司 Method for trapping carbon dioxide in flue gas of power station with high efficiency and low energy consumption and equipment adopting same
WO2013091439A1 (en) * 2011-12-23 2013-06-27 武汉凯迪工程技术研究总院有限公司 Method for capturing carbon dioxide in power station flue gas and device therefor
CN102553396B (en) * 2011-12-23 2014-06-04 武汉凯迪工程技术研究总院有限公司 Method for trapping carbon dioxide in flue gas of power station with high efficiency and low energy consumption and equipment adopting same
CN103591603A (en) * 2012-08-16 2014-02-19 中国石油化工集团公司 Synchronous decarburization method in flue gas afterheat recovery of heating furnace
CN103591603B (en) * 2012-08-16 2016-01-13 中国石油化工集团公司 The method of the synchronous decarburization of a kind of waste heat of flue gas of heating furnace removal process
CN104772007A (en) * 2014-01-14 2015-07-15 现代自动车株式会社 Reboiling device and regeneration tower
CN104772007B (en) * 2014-01-14 2018-10-26 现代自动车株式会社 Reboiling device and regenerator
CN105457447A (en) * 2015-12-16 2016-04-06 中石化节能环保工程科技有限公司 Carbon dioxide trapping system based on diphase system
CN106881010A (en) * 2017-04-18 2017-06-23 长沙紫宸科技开发有限公司 A kind of double-tower type circularly trapping device for being adapted to continuous collecting carbon dioxide from fuel gas
CN107115776A (en) * 2017-04-18 2017-09-01 长沙紫宸科技开发有限公司 One kind CO suitable for cement kiln flue gas2The change system continuously trapped
CN114225669A (en) * 2022-02-25 2022-03-25 中国华能集团清洁能源技术研究院有限公司 Absorption tower
CN115523004A (en) * 2022-10-18 2022-12-27 北京百利时能源技术股份有限公司 Amine process CO 2 Process medium heat energy recovery combined power generation device and method in trapping device

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