CN102784544B - IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system - Google Patents
IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system Download PDFInfo
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- CN102784544B CN102784544B CN201210275490.7A CN201210275490A CN102784544B CN 102784544 B CN102784544 B CN 102784544B CN 201210275490 A CN201210275490 A CN 201210275490A CN 102784544 B CN102784544 B CN 102784544B
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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
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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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The invention relates to an IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system, which comprises a sulfur-resistant conversion device, an MDEA (Methyl Di Ethanol Amine) desulfurization and decarbonization device and a sulfur and carbon separating device, wherein the sulfur-resistant conversion device is used for converting CO in a synthesis gas into a mixed gas consisting mainly of CO2-H2 in a converting furnace, and the MDEA desulfurization and decarbonization device comprises an absorption tower and a desorption tower; the absorption tower is used for receiving the mixed gas in the sulfur-resistant conversion device and for absorbing CO2 and H2S gases, and the desorption tower is used for receiving CO2 and H2S containing rich solution in the absorption tower and for desorbing CO2 and H2S; the sulfur and carbon separating device comprises a desulfurization purifier for receiving the CO2 and H2S gases in the desorption tower; and H2S gas is absorbed by an H2S absorber, and finally the CO2 gas is obtained. According to the IGCC based pre-combustion CO2 capture system, CO2 and H2S are simultaneously removed by a lean solution-half-lean solution MDEA method, so that the absorption rate of CO2 is improved, and the exhaust to air is reduced; and the heat generated by the conversion process of gas is fully utilized to heat MDEA rich solution for regeneration, and the consumption of medium-pressure steam is reduced.
Description
Technical field
The invention belongs to Clean Coal Power Generating Technologies field, relate to CO before a kind of burning based on IGCC
2trapping system.
Background technology
The Global Environmental Problems that the climate change of take is core is day by day serious, has become one of principal element threatening human kind sustainable development, and cutting down greenhouse gas emission becomes with mitigation of climate change the focus that current international community is paid close attention to.In numerous reduction of greenhouse gas discharge schemes, carbon trapping and Plugging Technology Applied are emerging, to have extensive Emission Reduction Potential technology, are expected to realize the CO that fossil energy is used
2low-carbon emission.
Current CO
2trapping technique route mainly contains three kinds: trapping technique before trapping technique, oxygen-enriched combustion technology and burning after burning.After burning, trapping is mainly used in CO in traditional coal-burning power plant flue gas
2separation, adopt MEA(monoethanolamine) solution is low CO
2cO in concentration flue gas
2absorb and bring up to finite concentration, gas treatment amount is large, need to consume a large amount of steam and electric energy.
Oxygen-enriched combusting CO
2the O that trapping technique technology obtains by air separation
2the oxidant when mist forming with a part of boiler smoke circulating air replaces air as combustion of fossil fuel, keeps temperature in smelting furnace lower than bearing a little, improves CO in combustion product gases
2concentration.In oxygen-enriched burning device, due to CO
2therefore concentration is higher, catch separated cost lower, but the oxygen enrichment cost of supplying with is very high.
IGCC(integrated gasification combined cycle plants) being the clean and effective generation technology of integrated coal gasification and Gas Turbine Combined-cycle, is also economy to carry out easily CO
2trapping and the coal fired power generation technology of sealing up for safekeeping.On the one hand, the generating efficiency of IGCC power plant is higher, and IGCC is than the CO discharging with capacity conventional power plant production per unit electric power
2amount can reduce 10-15%, and along with the lifting of the efficiency of Gas Turbine Combined-cycle, the CO of unit
2discharge capacity can also further reduce; On the other hand, in IGCC device, the CO of synthesis gas can be generated to H by transformationreation
2and CO
2thereby, by CO
2concentration bring up to 35-45%, and there is higher pressure, be convenient to CO
2separated recycle, reduce energy consumption.Therefore, before the burning based on IGCC, trap CO
2technology path aspect energy consumption, compare burning before CO
2trapping technique and oxygen-enriched combusting CO
2trapping technique has certain advantage, adds that IGCC device itself has the H that very large improved efficiency space and trapping produce
2also can be by adopting advanced reforming unit further to raise the efficiency, its advantage aspect minimizing loss in efficiency will be more outstanding.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, the object of the present invention is to provide CO before a kind of burning based on IGCC
2trapping system, this installs CO
2capture rate is high, and energy consumption is low, can realize the low-carbon emission of clean coal power generation device.
To achieve these goals, the technical solution used in the present invention is:
CO before a kind of burning based on IGCC
2trapping system, comprises
Sulphur-resistant conversion device, comprises change furnace 4, and the coal gas synthesis gas that change furnace 4 connects steam and goes out IGCC device gasification furnace, is converted into the CO in coal gas synthesis gas with CO
2-H
2it is main mist;
MDEA desulfurization and decarburization device, comprises absorption tower 14 and desorber 18, and absorption tower 14 picks out the mist of sulphur-resistant conversion device, by CO wherein
2and H
2s GAS ABSORPTION, desorber 18 picks out the CO that contains on absorption tower 14
2and H
2s rich solution, by CO
2and H
2s desorbs;
Sulphur carbon separator, comprises desulfurizing purifier 24,25, and desulfurizing purifier 24,25 picks out the CO of desorber 18
2and H
2s gas, then through H
2s one-level absorber 26 and H
2s secondary absorber 27 is by H
2s GAS ABSORPTION, finally obtains CO
2gas.
Described change furnace 4 is divided into four sections, one section two sections are integrated, three sections four sections are integrated, wherein second stage exit connects three sections of entrances by First Heat Exchanger 3 and the second spray humidifier 6 successively, the coal gas synthesis gas that goes out IGCC device gasification furnace after in First Heat Exchanger 3, heat exchange heats up and steam be linked into one section of entrance, between one section outlet and two sections of entrances, connect between 5, three sections of outlets of the first spray humidifier and four sections of entrances and connect the 3rd spray humidifier 7.
Described absorption tower 14 is MDEA lean solution semi lean solution absorption tower, described with CO
2-H
2be that main mist goes out rear access the second water knockout drum 10 of change furnace 4, the outlet of the second water knockout drum 10 connects stripping tower 11, and the gas outlet of stripping tower 11 connects the bottom on absorption tower 14, from bottom to top first and semi lean solution counter current contacting, on filling surface, there is mass-and heat-transfer reaction, most CO
2and H
2s is absorbed at this, and gas continues upwards to enter lean solution absorber portion, under lean solution effect, and residue CO
2and H
2s is absorbed.
The gas that goes out absorption tower 14 is sent into gas turbine generating set or Metal Palladium film hydrogen purification device after the 4th heat exchanger 15 and the first knockout 16.
Described MDEA desulfurization and decarburization device also comprises regenerator 21, and poor rich liquid heat exchanger 17 is set between the liquid outlet on absorption tower 14 and the liquid outlet of regenerator 21 will go out the CO that contains on absorption tower 14
2and H
2s rich solution with from the lean solution at 21 ends of regenerator, carry out exchange heat, rich solution afterwards just enters into desorber 18.
A liquid outlet of described desorber 18 connects absorption tower 14 centre entrances, and another liquid outlet is connected to the top entrance of regenerator 21, and regenerator 21 bottoms connect reboiler 22, and the liquid outlet of regenerator 21 is connected to the top entrance on absorption tower 14 after poor rich liquid heat exchanger 17.
Described H
2the liquid outlet of S secondary absorber 27 connects the bottom inlet of regeneration tank 28, and regeneration tank 28 bottoms are connected to air supply plant, and the top liquid outlet of regeneration tank 28 connects sulphur foam tank 29, and sulphur foam tank 29 is connected to sulphur filter 30.
Fully recovering after the unreacted process condensate depickling of conversion process gas in device of the present invention, save boiler water consumption, the pre-hot synthesis gas of converting means second stage exit gas, converts the regeneration of four sections of exit gas heating MDEA rich solutions, steam saving consumption, reduces plant energy consumption.Converting means of the present invention adopts stove external spraying humidifying cooling method, reduces steam consumption, reduces energy consumption.The present invention adopts lean solution/semi lean solution MDEA to remove CO simultaneously
2and H
2the method of S, raising CO
2capture rate, reduces regeneration energy consumption, and plant energy consumption is lower than 2.0GJ/tCO
2.
Compared with prior art, the present invention, by the technique that sulphur-resistant conversion, MDEA desulfurization and decarburization, wet oxidation-desulfurizing method are combined, is first converted into CO by the CO in coal gas synthesis gas
2and H
2, first by CO
2and H
2s removes simultaneously, finally removes H
2the method of S, the CO of raising device
2capture rate, has reduced the discharge of greenhouse gases, to protect mankind environment; Pass through device integrated simultaneously, make full use of the energy of device inside, reduce the consumption of extraneous steam and feedwater, reduce plant energy consumption.
Accompanying drawing explanation
Accompanying drawing is trapping system schematic flow sheet of the present invention.
The specific embodiment
Below in conjunction with drawings and Examples, the present invention is described in further details.
As shown in drawings, the inventive system comprises: filter 1, the first water knockout drum 2, First Heat Exchanger 3, change furnace 4, the first humidifiers 5, the second humidifier 6, the 3rd humidifier 7, feed water preheater 9, the second water knockout drums 10, stripping tower 11, gives water pot 12, the three heat exchangers 13, absorption tower 14, the second heat exchanger 15, the first knockouts 16, poor rich liquid heat exchanger 17, desorber 18, the first solution storage trough 19, the second solution storage troughs 20, regenerator 21, reboiler 22, the second knockout 23, desulfurizing purifier 24,25, H
2s one-level absorber 26, H
2s secondary absorber 27, regeneration tank 28, sulphur foam tank 29, sulphur filter 30, holds liquid bath 31.
Filter 1 connects the coal gas synthesis gas that IGCC device gasification furnace produces, the first water knockout drum 2 connects steam, filter 1, between the first water knockout drum 2 and each humidifier, First Heat Exchanger 3 is set, filter 1 and the first water knockout drum 2 all access change furnace 4, change furnace 4 is divided into four sections, one section two sections are integrated, three sections four sections are integrated, wherein second stage exit connects three sections of entrances by First Heat Exchanger 3 and the second spray humidifier 6 successively, the coal gas synthesis gas that goes out IGCC device gasification furnace after in First Heat Exchanger 3, heat exchange heats up and steam be linked into one section of entrance, between one section outlet and two sections of entrances, connect the first spray humidifier 5, between three sections of outlets and four sections of entrances, connect the 3rd spray humidifier 7.
Four sections of outlets of change furnace 4 connect the second water knockout drum 10, and the outlet that feed water preheater 9 and the 3rd heat exchanger 13, the second water knockout drums 10 are set between the two connects stripping tower 11,11 times termination feedwater tanks 12 of stripping tower, and the gas outlet of stripping tower 11 connects the bottom on absorption tower 14.
The gas that goes out absorption tower 14 is sent into gas turbine generating set or Metal Palladium film hydrogen purification device after the 4th heat exchanger 15 and the first knockout 16.Poor rich liquid heat exchanger 17 is set between the liquid outlet of the liquid outlet on absorption tower 14 and regenerator 21, and the rich solution on absorption tower 14 enters into desorber 18, and the top entrance of desorber 18 is connected with the first solution storage trough 19 and the second solution storage trough 20.A liquid outlet of desorber 18 connects absorption tower 14 centre entrances, and another liquid outlet is connected to the top entrance of regenerator 21, and regenerator 21 bottoms connect reboiler 22, and the liquid outlet of regenerator 21 is connected to the top entrance on absorption tower 14 after poor rich liquid heat exchanger 17.The top exit of desorber 18 connects desulfurizing purifier 24,25 by the second knockout 23, and the outlet of desulfurizing purifier 24,25 meets H
2s one-level absorber 26 and H
2s secondary absorber 27, H
2s one-level absorber 26 and H
2the outlet of S secondary absorber 27 connects regeneration tank 28, and regeneration tank 28 connects sulphur foam tank 29, and sulphur foam tank 29 outlet at bottoms connect sulphur filter 30, and sulphur filter 30 connects and holds liquid bath 31.
The course of work of the present invention is as follows:
First the coal gas synthesis gas that IGCC device gasification furnace produces enters filter 1 after dedusting and washing, remove a small amount of flue dust in synthesis gas, entering afterwards First Heat Exchanger 3 heats up with the second stage exit gas converting heat of change furnace 4, the pyroreaction gas being come by second stage exit is heated to 200 ℃, then with through the middle pressure saturated vapor of the first water knockout drum 2, be mixed into a section of change furnace 4, one section outlet gas enters the first spray humidifier 5, enters two sections of change furnace 4 after humidification.Second stage exit reaction gas enters the second spray humidifier 6 at First Heat Exchanger 3 after recuperation of heat, heat exchange cooling enters three sections of change furnace 4 by spray humidification, go out three sections of reaction gases and enter again and enter four sections of change furnace 4 after the 3rd humidifier 7 humidifications, go out 265 ℃ of four sections of reaction gas temperature, CO concentration is less than 1%.
Four sections of reaction gases that go out change furnace 4 enter the second water knockout drum 10 after feed water preheater 9 and the 3rd heat exchanger 13 coolings, the water that the acid water of separating produces after stripping tower 11 enters to water pot 12, with the hydration of outer tinkering a pan stove and after feed water preheater 9 heats up, deliver to the first humidifier 5, the second humidifiers 6, the 3rd humidifier 7.The gas temperature that goes out the second water knockout drum 10 is down to 40 ℃ of left and right, enters the bottom on absorption tower 14, and first and semi lean solution counter current contacting, mass-and heat-transfer reaction occurs on the surface of filler, most CO from bottom to top
2and H
2s is absorbed at this, goes out about 55 ℃ of the gas on absorption tower, and gas continues upwards to enter lean solution absorber portion, under lean solution effect, and residue CO
2and H
2the S overwhelming majority is absorbed, and the gas that goes out absorption tower is delivered to gas turbine generating set or Metal Palladium film hydrogen purification device after the second heat exchanger 15, the first knockouts 16, through Metal Palladium film hydrogen purification device, can obtain purity higher than 99.9% hydrogen.
From 14 bottoms, absorption tower rich solution out with from the lean solution at 21 ends of regenerator, in poor rich liquid heat exchanger 17, carry out, exchange heat, entering normal pressure desorber 18 by most CO
2and H
2s desorbs, and become semi lean solution, at the bottom of tower, be out divided into two parts: most semi lean solution is directly delivered to 14 middle parts, absorption tower, remainder boosts and after the interior heat exchange of the 3rd heat exchanger 13, delivers to regenerator 21 tops with four sections of outlet conversion gas of change furnace 4, solution flows from top to bottom, contact with the water vapour from reboiler 22, make remaining CO in solution
2and H
2s all desorbs, and reaches the object of thorough regeneration.The lean solution that goes out regenerator 21 bottoms is delivered to the top on absorption tower 14 through poor rich liquid heat exchanger 17, the gas that goes out normal pressure desorber 18 tops is sent into desulfurizing purifier 24,25 and carried out H after the second knockout 23
2the absorption and regeneration of S.H in mist therein
2s is adsorbed, first desulfurizing purifier top CO out
2h in gas
2s concentration, lower than 200ppm, is sent CO
2compress and liquefy workshop section, CO
2capture rate higher than 90%.The H being adsorbed
2s is in another desulfurizing purifier after desorb, and the absorption blender of sending into wet desulphurization equipment contacts with first grade desulfurizing lean solution.And the gas not adsorbing in desulfurizing purifier 24,25 enters follow-up CO
2compress and liquefy device.Absorb blender by H
2s one-level absorber 26 and H
2s secondary absorber 27 forms, and gas is introduced into H
2s one-level absorber 26, to about 3000ppm, then enters H by 2.5% hydrogen sulfide stripping
2s secondary absorber 27 bottoms, with the doctor solution counter current contacting of tower top spray, the H in gas
2s is desulfurized liquid absorbing and removing to the qualified emptying of 13ppm.Sulfur removing pregnant solution enters the empty regeneration tank 28 of self-priming, air with doctor solution from bottom to top with doctor solution counter current contacting again, make sulfide, sulfohydrate in solution be oxidized to elemental sulfur, and taken to regeneration tank 28 top liquid levels formation sulphur foams by up air, solution after oxidized regeneration enters sulphur foam tank 29 from regeneration tank, after reaching certain liquid level, deliver in filter 30 and to filter, obtain the sulphur cake that contains certain moisture, filtrate is back to holds liquid bath 31.
The principle of conversion fraction is under the effect of catalyst, and under certain temperature (higher than the initial activity temperature of catalyst) condition, CO and water vapour react, and CO is converted into hydrogen and carbon dioxide.
The principle of MDEA desulfurization and decarburization part be weakly alkaline methyl diethanolamine when low temperature (20 ℃～40 ℃) can be simultaneously with conversion gas in faintly acid gas H
2s and CO
2water generation reaction dissolubility amine salt (being absorption process), resolves into again H at the lower amine salt of high temperature (105 ℃ of >)
2s and CO
2and methyl diethanolamine (being desorption and regeneration process), MDEA is regenerated, recycle.
MDEA solution absorbs H
2s and CO
2the key reaction occurring:
H
2S R
2NCH
3→R
2NH
+CH
3+HS
- （1）
CO
2+H
2O+R
2NCH
3→R
2NH
+CH
3+HCO
3 - （2）
MDEA and H
2the reaction of S is the instantaneous chemical reaction that controlled by air film, and MDEA and CO
2without directly reaction, can only react with its aqueous solution solution this reaction and CO
2solubility in water has much relations, and the huge difference in this reaction mechanism has caused the difference of the speed of reaction, has formed the preferential selective H of absorption of MDEA
2the basis of S.
Reaction (2) because MDEA lacks free hydrogen ion, can not and CO
2directly reaction.Must be first through CO2 hydrolysis generation H+.Then MDEA again with solution in H+ be combined into R2NH+CH3, because hydrolysis rate is slow, need the fully reaction of enough time of staying and contact area, whole absorption process has been subject to the restriction of reaction rate.Can in MDEA solution, add after activator (as R2NH), reaction is just undertaken by following formula:
R
2NH+CO
2==R
2NCOOH (3)
R
2NCOOH+R
2NCH
3+H
2O==R
2NH+R
2CH
3NH
++HCO
3 - (4)
(3)+(4) overall reaction:
R
2NCH
3+CO
2+H
2O==R
2CH
3NH
++HCO
3 - (5)
From formula (3)～(5), activator absorption CO
2, to liquid phase, transmit CO
2, greatly accelerated reaction speed, and MDEA is reproduced.
Wet method direct oxidation desulfurization principle is the H in gas
2s is dissolved in after doctor solution, first with doctor solution in alkali reaction
H
2s (gas phase)=H
2s (liquid phase) (6)
H
2S+Na
2CO
3=NaHS+NaHCO
3 （7）
RSH+Na
2CO
3=RSNa+NaHCO
3 （8）
Under catalyst action, the NaHS of generation again with solution in oxygen there is oxidation and analyse reaction of Salmon-Saxl, generate elemental sulfur and sodium carbonate.In desulfurizing tower, owing to bringing oxygen content deficiency into, the elemental sulfur generating in solution is few, so absorbed after enough hydrogen sulfide when solution, solution has just lost the ability that continues absorbing hydrogen sulphide.For recovering the ability of solution absorbing hydrogen sulphide, just must regenerate to solution, mainly there is oxidation and analyse reaction of Salmon-Saxl in regenerative process:
NaHS+NaHCO
3+1/2O
3＝Na
2CO
3+H
2O+S （9）
2RSNa+2NaHCO
3+1/2O
3＝2Na
2CO
3+H
2O+S （10）
Side reaction: NaHS+2O
3=Na
2s
2o
3+ H
2o (11)
Under the relative strenuous exercise of air and liquid phase, the elemental sulfur phase inter coagulation of separating out, and with ascending air emersion liquid level, leave circulation desulfurization liquid, thus make doctor solution there is again the ability of absorbing hydrogen sulphide.
CO in the coal gas synthesis gas of the present invention's trapping based on IGCC device
2principle be first the CO in synthesis gas to be converted into CO by sulphur-resistant conversion process
2and H
2, the H containing in conversion gas
2s must remove to reduce the corrosion to subsequent technique equipment, in order to improve CO
2capture rate, adopts to the method for adding activator in MDEA solution H
2s and CO
2remove, recycling wet method direct oxidation method removes H simultaneously
2s, reaches trapping CO
2object, CO
2capture rate is higher than 90%.In the present embodiment, make full use of conversion process liberated heat, be used for heating initial synthesis gas, preheating feedwater, heating MDEA rich solution etc., and the acid water that conversion process produces continues on for transformationreation after reclaiming, these measures reduced device to steam, feedwater consumption, plant energy consumption is lower than 2.0GJ/tCO
2.
Finally explanation is, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although the present invention is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can modify or be equal to replacement technical scheme of the present invention, and not departing from aim and the scope of the technical program, it all should be encompassed in the middle of claim scope of the present invention.
Claims (3)
1. CO before the burning based on IGCC
2trapping system, comprises
Sulphur-resistant conversion device, comprises change furnace (4), and the coal gas synthesis gas that change furnace (4) connects steam and goes out IGCC device gasification furnace, is converted into the CO in coal gas synthesis gas with CO
2-h
2it is main mist;
It is characterized in that, also comprise:
MDEA desulfurization and decarburization device, comprises absorption tower (14) and desorber (18), and absorption tower (14) pick out the mist of sulphur-resistant conversion device, by CO wherein
2and H
2s GAS ABSORPTION, desorber (18) picks out the CO that contains on absorption tower (14)
2and H
2s rich solution, by CO
2and H
2s desorbs;
Sulphur carbon separator, comprises desulfurizing purifier (24,25), and desulfurizing purifier (24,25) picks out the CO of desorber (18)
2and H
2s gas, then through H
2s one-level absorber (26) and H
2s secondary absorber (27) is by H
2s GAS ABSORPTION, finally obtains CO
2gas;
Wherein, described change furnace (4) is divided into four sections, one section two sections are integrated, three sections four sections are integrated, wherein second stage exit connects three sections of entrances by First Heat Exchanger (3) and the second spray humidifier (6) successively, the coal gas synthesis gas that goes out IGCC device gasification furnace after in First Heat Exchanger (3), heat exchange heats up and steam be linked into one section of entrance, between one section outlet and two sections of entrances, connect the first spray humidifier (5), between three sections of outlets and four sections of entrances, connect the 3rd spray humidifier (7);
Described absorption tower (14) is MDEA lean solution semi lean solution absorption tower, described with CO
2-h
2be to access the second water knockout drum (10) after main mist goes out change furnace (4), the liquid outlet of the second water knockout drum (10) connects stripping tower (11), the gas outlet of stripping tower (11) connects the bottom of absorption tower (14), from bottom to top first with semi lean solution counter current contacting, on filling surface, there is mass-and heat-transfer reaction, most CO
2and H
2s is absorbed at this, and gas continues upwards to enter lean solution absorber portion, under lean solution effect, and residue CO
2and H
2s is absorbed;
Described MDEA desulfurization and decarburization device also comprises regenerator (21), and the CO that contains that poor rich liquid heat exchanger (17) will go out absorption tower (14) is set between the liquid outlet of absorption tower (14) and the liquid outlet of regenerator (21)
2and H
2s rich solution with from the lean solution at regenerator (21) end, carry out exchange heat, rich solution afterwards just enters into desorber (18);
A liquid outlet of described desorber (18) connects absorption tower (14) centre entrance, another liquid outlet is connected to the top entrance of regenerator (21), regenerator (21) bottom connects reboiler (22), and the liquid outlet of regenerator (21) is connected to the top entrance on absorption tower (14) after poor rich liquid heat exchanger (17).
2. CO according to claim 1
2trapping system, is characterized in that, the gas that goes out absorption tower (14) is sent into gas turbine generating set or Metal Palladium film hydrogen purification device after the 4th heat exchanger (15) and the first knockout (16).
3. CO according to claim 1
2trapping system, is characterized in that, described H
2the liquid outlet of S secondary absorber (27) connects the bottom inlet of regeneration tank (28), and regeneration tank (28) bottom is connected to air supply plant, and the top liquid outlet of regeneration tank (28) connects sulphur foam tank (29), and sulphur foam tank (29) is connected to sulphur filter (30).
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|---|---|---|---|
| CN201210275490.7A CN102784544B (en) | 2012-08-03 | 2012-08-03 | IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system |
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|---|---|---|---|
| CN201210275490.7A CN102784544B (en) | 2012-08-03 | 2012-08-03 | IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system |
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| CN108264940A (en) * | 2017-12-11 | 2018-07-10 | 中国华能集团清洁能源技术研究院有限公司 | CO before a kind of burning based on IGCC2The desulphurization system and technique of trapping |
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| CN106381174A (en) * | 2016-09-06 | 2017-02-08 | 中国华能集团清洁能源技术研究院有限公司 | Poly-generation system based on pre-combustion CO2 collecting |
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| CN106401749B (en) * | 2016-10-11 | 2018-11-02 | 中国华能集团清洁能源技术研究院有限公司 | A kind of near-zero release coal generating system and method based on IGCC |
| CN109812335B (en) * | 2019-01-15 | 2021-11-16 | 中国石油大学(华东) | Zero-carbon-emission integrated coal gasification-steam combined cycle power generation process |
| CN113717758B (en) * | 2021-08-27 | 2024-02-09 | 山东津挚环保科技有限公司 | Desulfurization and decarbonization system for synthesis gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101856579A (en) * | 2010-06-02 | 2010-10-13 | 清华大学 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
| WO2011039059A1 (en) * | 2009-09-30 | 2011-04-07 | Uhde Gmbh | Method for operating an igcc power plant process having integrated co2 separation |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202808740U (en) * | 2012-08-03 | 2013-03-20 | 中国华能集团清洁能源技术研究院有限公司 | Efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion |
-
2012
- 2012-08-03 CN CN201210275490.7A patent/CN102784544B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011039059A1 (en) * | 2009-09-30 | 2011-04-07 | Uhde Gmbh | Method for operating an igcc power plant process having integrated co2 separation |
| CN101856579A (en) * | 2010-06-02 | 2010-10-13 | 清华大学 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108264940A (en) * | 2017-12-11 | 2018-07-10 | 中国华能集团清洁能源技术研究院有限公司 | CO before a kind of burning based on IGCC2The desulphurization system and technique of trapping |
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