CN202808740U - Efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion - Google Patents
Efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion Download PDFInfo
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- CN202808740U CN202808740U CN 201220383998 CN201220383998U CN202808740U CN 202808740 U CN202808740 U CN 202808740U CN 201220383998 CN201220383998 CN 201220383998 CN 201220383998 U CN201220383998 U CN 201220383998U CN 202808740 U CN202808740 U CN 202808740U
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- 238000002485 combustion reaction Methods 0.000 title abstract description 6
- 238000002309 gasification Methods 0.000 title abstract description 4
- 238000010521 absorption reaction Methods 0.000 claims abstract description 47
- 239000003034 coal gas Substances 0.000 claims abstract description 13
- 239000006096 absorbing agent Substances 0.000 claims abstract description 12
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 10
- 230000009466 transformation Effects 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 8
- GJEAMHAFPYZYDE-UHFFFAOYSA-N [C].[S] Chemical compound [C].[S] GJEAMHAFPYZYDE-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 79
- 239000007788 liquid Substances 0.000 claims description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims description 20
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 20
- 238000003795 desorption Methods 0.000 claims description 16
- 239000007921 spray Substances 0.000 claims description 13
- 230000003009 desulfurizing effect Effects 0.000 claims description 12
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 239000001257 hydrogen Substances 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 229910052763 palladium Inorganic materials 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 4
- 238000005262 decarbonization Methods 0.000 claims description 3
- 238000006276 transfer reaction Methods 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 29
- 238000000034 method Methods 0.000 abstract description 25
- 230000008929 regeneration Effects 0.000 abstract description 16
- 238000011069 regeneration method Methods 0.000 abstract description 16
- 230000008569 process Effects 0.000 abstract description 10
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 abstract description 7
- 238000005261 decarburization Methods 0.000 abstract description 4
- 230000008859 change Effects 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract description 2
- 238000003786 synthesis reaction Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 53
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 17
- 239000005864 Sulphur Substances 0.000 description 12
- 238000005265 energy consumption Methods 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- 241000238634 Libellulidae Species 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 239000006260 foam Substances 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 6
- 101100204059 Caenorhabditis elegans trap-2 gene Proteins 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 239000012190 activator Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- -1 amine salt Chemical class 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
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- 230000018109 developmental process Effects 0.000 description 1
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- 239000000945 filler Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
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- 238000004519 manufacturing process Methods 0.000 description 1
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Abstract
An efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion comprises a sulfur-resisting transformation system, an MDEA (methyldiethanolamine) desulfuration and decarburization system, and a sulfur-carbon separation system, wherein CO in synthesis gas of coal gas is converted into mixed gas with CO2-H2 as the main gas in a change furnace; the MDEA desulfuration and decarburization system comprises an absorption tower and a desorber, the desorber receives the mixed gas of the sulfur-resisting transformation system and absorbs CO2 and H2S in the mixed gas, and the desorber receives rich liquor containing CO2 and H2S of the absorption tower and desorbs CO2 and H2S; and the sulfur-carbon separation system comprises a desulfuration purifier which receives CO2 and H2S of the desorber, H2S is absorbed through an H2S absorber, and finally CO2 is obtained. According to the device, CO2 and H2S can be removed simultaneously through barren liquor and semi barren liquor MDEA, the absorption efficiency of CO2 is improved, and emission of CO2 is lowered, the heat generated in coal gas conversion process is fully used to heat MDEA rich liquor for regeneration, and consumption of medium-pressure steam is lowered.
Description
Technical field
The utility model belongs to the Clean Coal Power Generating Technologies field, relates to a kind of based on CO before the burning of IGCC
2Efficient capturing device.
Background technology
Global Environmental Problems take climate change as core is day by day serious, has become one of principal element that threatens human kind sustainable development, and cutting down greenhouse gas emission becomes the focus that current international community is paid close attention to mitigation of climate change.In numerous reduction of greenhouse gas discharge schemes, carbon capture and Plugging Technology Applied are emerging, as to have extensive Emission Reduction Potential technology, are expected to the CO that realizes that fossil energy is used
2Low-carbon emission.
Present CO
2The trapping technique route mainly contains three kinds: trapping technique before trapping technique, oxygen-enriched combustion technology and the burning after the burning.Capture after the burning and be mainly used in CO in traditional coal-burning power plant stack gas
2Separation, adopt the MEA(Monoethanolamine MEA BASF) solution will hang down CO
2CO in the concentration flue gas
2Absorption is also brought up to finite concentration, and the gas processing amount is large, needs to consume a large amount of steam and electric energy.
Oxygen-enriched combusting CO
2The O that the trapping technique technology obtains with air separation
2Oxygenant when the mixed gas that consists of with a part of boiler smoke circulation gas replaces air as combustion of fossil fuel keeps temperature in the smelting furnace to be lower than and can bear a little, improves CO in the combustion product gases
2Concentration.In the oxygen-enriched combustion system, because CO
2Concentration is higher, and the cost of therefore catching separation is lower, but the oxygen enrichment cost of supplying with is very high.
The IGCC(integrated gasification combined cycle plants) being the clean and effective generation technology of integrated gasification and Gas Turbine Combined-cycle, also is economy to carry out easily CO
2Capture 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 that discharges with capacity conventional power plant production per unit electric power
2Amount can reduce 10-15%, and along with the lifting of the efficient of Gas Turbine Combined-cycle, the CO of unit
2Quantity discharged can also further reduce; On the other hand, in the IGCC system, the CO of synthetic gas can be generated H by transformationreation
2And CO
2Thereby, with CO
2Concentration bring up to 35-45%, and have higher pressure, be convenient to CO
2Separation and Recovery and utilization, reduce energy consumption.Therefore, capture CO before the burning based on IGCC
2CO before technological line is compared aspect energy consumption and burnt
2Trapping technique and oxygen-enriched combusting CO
2Trapping technique has certain advantage, adds that the IGCC system itself has the H that very large improved efficiency space and capture produce
2Also can further raise the efficiency by adopting advanced conversion system, its advantage aspect the minimizing loss in efficiency will be more outstanding.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, it is a kind of based on CO before the burning of IGCC that the purpose of this utility model is to provide
2Efficient capturing device, the CO of this system
2Capture rate is high, and energy consumption is low, can realize the low-carbon emission of clean coal power generation system.
To achieve these goals, the technical solution adopted in the utility model is:
A kind of based on CO before the burning of IGCC
2Efficient capturing device comprises
The sulfur-resisting transformation system comprises shift converter 4, and the coal gas synthetic gas that shift converter 4 connects steam and goes out IGCC system vapourizing furnace is converted into the CO in the coal gas synthetic gas with CO
2-H
2It is main mixed gas;
The MDEA decarbonization desulfurization system comprises absorption tower 14 and desorption tower 18, and absorption tower 14 picks out the mixed gas of sulfur-resisting transformation system, with CO wherein
2And H
2S gas absorption, desorption tower 18 pick out the CO that contains on absorption tower 14
2And H
2The S rich solution is with CO
2And H
2S desorbs;
Sulphur carbon separation system comprises desulfurizing purifier 24,25, and desulfurizing purifier 24,25 picks out the CO of desorption tower 18
2And H
2S gas is again through H
2S one-level resorber 26 and H
2S secondary absorber 27 is with H
2The S gas absorption finally obtains CO
2Gas.
Described shift converter 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 entrances by First Heat Exchanger 3 and the second spray humidifier 6 successively, the coal gas synthetic gas that goes out IGCC system vapourizing furnace after heat exchange heats up in First Heat Exchanger 3 and vapor mixing be linked into one section entrance, connect between 5, three sections outlets of the first spray humidifier and four sections entrances between one section outlet and the two sections entrances and connect the 3rd spray humidifier 7.
Described absorption tower 14 is MDEA lean solution semi lean solution absorption tower, and is described with CO
2-H
2Be that main mixed gas goes out shift converter 4 rear access the second water traps 10, the outlet of the second water trap 10 connects gas stripping column 11, and the air outlet of gas stripping column 11 connects the bottom on absorption tower 14, from bottom to top elder generation and semi lean solution counter current contact, mass-and heat-transfer reaction, most CO occur at filling surface
2And H
2S is absorbed at this, and gas continues upwards to enter the lean solution absorber portion, under the 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 system or palladium metal film hydrogen purification system behind the 4th interchanger 15 and the first skimmer 16.
Described MDEA decarbonization desulfurization system also comprises regenerator column 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 the liquid outlet on absorption tower 14 and regenerator column 21
2And H
2The S rich solution with carry out thermal exchange from the lean solution at 21 ends of regenerator column, rich solution afterwards just enters into desorption tower 18.
A liquid outlet of described desorption tower 18 connects absorption tower 14 centre entrances, and another liquid outlet is connected to the top entrance of regenerator column 21, and regenerator column 21 bottoms connect reboiler 22, and the liquid outlet of regenerator column 21 is connected to the top entrance on absorption tower 14 behind 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 chute 29, and sulphur foam chute 29 is connected to sulphur filter 30.
Fully recovering behind the unreacted process condensate depickling of the conversion process gas in the system described in the utility model, save the feedwater consumption, the pre-hot synthesis gas of transformation system second stage exit gas, the regeneration of four sections exit gas heating of conversion MDEA rich solution, the steam saving consumption reduces system energy consumption.The utility model transformation system adopts stove external spraying humidifying cooling method, reduces steam consumption, reduces energy consumption.The utility model adopts lean solution/semi lean solution MDEA to remove simultaneously CO
2And H
2The method of S, raising CO
2Capture rate reduces the regeneration energy consumption, and system energy consumption is lower than 2.0GJ/t CO
2
Compared with prior art, the technique of the utility model by sulfur-resisting transformation, MDEA desulfurization and decarburization, wet oxidation-desulfurizing method are combined is converted into CO with the CO in the coal gas synthetic gas first
2And H
2, first with CO
2And H
2S removes simultaneously, removes at last H
2The method of S, the CO of raising system
2Capture rate has reduced the discharging of greenhouse gases, the to protect mankind environment; By the system integration, take full advantage of the energy of internal system simultaneously, reduce the consumption of extraneous steam and feedwater, reduce system energy consumption.
Description of drawings
Accompanying drawing is the utility model capturing device schematic flow sheet.
Embodiment
Below in conjunction with drawings and Examples the utility model is described in further details.
As shown in drawings, system of the present utility model comprises: strainer 1, the first water trap 2, First Heat Exchanger 3, shift converter 4, the first humidifiers 5, the second humidifier 6, the 3rd humidifier 7, feed water preheater 9, the second water traps 10, gas stripping column 11 is given water pot 12, the three interchanger 13, absorption tower 14, the second interchanger 15, the first skimmers 16, poor rich liquid heat exchanger 17, desorption tower 18, the first solution storage trough 19, the second solution storage troughs 20, regenerator column 21, reboiler 22, the second skimmer 23, desulfurizing purifier 24,25, H
2S one-level resorber 26, H
2S secondary absorber 27, regeneration tank 28, sulphur foam chute 29, sulphur filter 30 holds liquid bath 31.
Strainer 1 connects the coal gas synthetic gas that IGCC system vapourizing furnace produces, the first water trap 2 connects steam, strainer 1, between the first water trap 2 and each humidifier First Heat Exchanger 3 is set, strainer 1 and the first water trap 2 all access shift converter 4, shift converter 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 entrances by First Heat Exchanger 3 and the second spray humidifier 6 successively, the coal gas synthetic gas that goes out IGCC system vapourizing furnace after heat exchange heats up in First Heat Exchanger 3 and vapor mixing be linked into one section entrance, connect between 5, three sections outlets of the first spray humidifier and four sections entrances between one section outlet and the two sections entrances and connect the 3rd spray humidifier 7.
Four sections outlets of shift converter 4 connect the second water trap 10, and the outlet that feed water preheater 9 and the 3rd interchanger 13, the second water traps 10 are set between the two connects gas stripping column 11,11 times termination feedwater of gas stripping column tank 12, and the air outlet of gas stripping column 11 connects the bottom on absorption tower 14.
The gas that goes out absorption tower 14 is sent into gas turbine generating system or palladium metal film hydrogen purification system behind the 4th interchanger 15 and the first skimmer 16.Poor rich liquid heat exchanger 17 is set between the liquid outlet of the liquid outlet on absorption tower 14 and regenerator column 21, and the rich solution on absorption tower 14 enters into desorption tower 18, and the top entrance of desorption tower 18 is connected with the first solution storage trough 19 and the second solution storage trough 20.A liquid outlet of desorption tower 18 connects absorption tower 14 centre entrances, and another liquid outlet is connected to the top entrance of regenerator column 21, and regenerator column 21 bottoms connect reboiler 22, and the liquid outlet of regenerator column 21 is connected to the top entrance on absorption tower 14 behind poor rich liquid heat exchanger 17.The top exit of desorption tower 18 connects desulfurizing purifier 24,25 by the second skimmer 23, and desulfurizing purifier 24,25 outlet meet H
2S one-level resorber 26 and H
2S secondary absorber 27, H
2S one-level resorber 26 and H
2The outlet of S secondary absorber 27 connects regeneration tank 28, and regeneration tank 28 connects sulphur foam chute 29, and sulphur foam chute 29 outlet at bottoms connect sulphur filter 30, and sulphur filter 30 connects and holds liquid bath 31.
The utility model working process is as follows:
The coal gas synthetic gas that IGCC system vapourizing furnace produces at first enters strainer 1 through dedusting with after washing, remove a small amount of flue dust in the synthetic gas, the second stage exit gas converting heat that enters afterwards First Heat Exchanger 3 and shift converter 4 heats up, the pyroreaction gas that is come by second stage exit is heated to 200 ℃, then be mixed into a section of shift converter 4 through the middle pressure saturation steam of the first water trap 2, one section outlet gas enters the first spray humidifier 5, enters two sections of shift converter 4 behind the humidification.The second stage exit reaction gas enters the second spray humidifier 6 at First Heat Exchanger 3 after recovery of heat, the heat exchange cooling enters three sections of shift converter 4 by spray humidification, go out three sections reaction gases and enter again four sections that enter shift converter 4 behind the 3rd humidifier 7 humidifications, go out 265 ℃ of four sections reaction gas temperature, CO concentration less than 1%.
Four sections reaction gases that go out shift converter 4 enter the second water trap 10 after feed water preheater 9 and 13 coolings of the 3rd interchanger, the water that the sour water of separating produces behind gas stripping column 11 enters to water pot 12, deliver to the first humidifier 5, the second humidifiers 6, the 3rd humidifier 7 with the hydration of outer tinkering a pan stove and after feed water preheater 9 heats up.The gas temperature that goes out the second water trap 10 is down to about 40 ℃, enters the bottom on absorption tower 14, and elder generation and semi lean solution counter current contact on the surface of filler mass-and heat-transfer reaction, most CO occur 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 the lean solution absorber portion, under the lean solution effect, and residue CO
2And H
2The S overwhelming majority is absorbed, and the gas that goes out the absorption tower is delivered to gas turbine generating system or palladium metal film hydrogen purification system behind the second interchanger 15, the first skimmers 16, can obtain purity through palladium metal film hydrogen purification system and be higher than 99.9% hydrogen.
From 14 bottoms, absorption tower rich solution out with in poor rich liquid heat exchanger 17, carry out thermal exchange from the lean solution at 21 ends of regenerator column after, enter normal pressure desorption tower 18 with most CO
2And H
2S desorbs, and become semi lean solution, out be divided into two portions at the bottom of tower: most semi lean solution is directly delivered to 14 middle parts, absorption tower, remainder boosts and delivers to regenerator column 21 tops with four sections outlet conversion gas of shift converter 4 after the 13 interior heat exchange of the 3rd interchanger, solution flows from top to bottom, contact with the water vapor from reboiler 22, make remaining CO in the solution
2And H
2S all desorbs, and reaches the purpose of thorough regeneration.The lean solution that goes out regenerator column 21 bottoms is delivered to the top on absorption tower 14 through poor rich liquid heat exchanger 17, and the gas that goes out normal pressure desorption tower 18 tops is sent into desulfurizing purifier 24,25 after through the second skimmer 23 and carried out H
2The absorption and regeneration of S.The H in the mixed gas therein
2S is adsorbed, first desulfurizing purifier top CO out
2H in the gas
2S concentration is lower than 200ppm, send CO
2Compress and liquefy workshop section, CO
2Capture rate be higher than 90%.The H that is adsorbed
2After the desorb, the absorption mixing tank of sending into wet desulphurization equipment contacts with the first grade desulfurizing lean solution S in another desulfurizing purifier.And the gas that does not adsorb in the desulfurizing purifier 24,25 enters follow-up CO
2Compress and liquefy system.Absorb mixing tank by H
2S one-level resorber 26 and H
2S secondary absorber 27 forms, and gas is introduced into H
2S one-level resorber 26, the hydrogen sulfide stripping with 2.5% enter H to the 3000ppm again
2S secondary absorber 27 bottoms are with the doctor solution counter current contact of cat head spray, the H in the gas
2S is desulfurized the 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 contact again, make sulfide, sulfohydrate in the solution be oxidized to elemental sulfur, and taken to regeneration tank 28 top liquid levels by up air and form the sulphur foams, solution after the oxidized regeneration enters sulphur foam chute 29 from regeneration tank, deliver to after reaching certain liquid level in the strainer 30 and filter, obtain containing the sulphur cake of certain moisture, filtrate is back to holds liquid bath 31.
The principle of conversion fraction is under the effect of catalyzer, and under certain temperature (the initial activity temperature that is higher than catalyzer) condition, CO and water vapor react, and CO is converted into hydrogen and carbonic acid gas.
The principle of MDEA desulfurization and decarburization part be weakly alkaline methyldiethanolamine when low temperature (20 ℃～40 ℃) can be simultaneously with conversion gas in slightly acidic 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 ℃)
2S and CO
2And methyldiethanolamine (being the desorption and regeneration process), MDEA is regenerated, recycle.
MDEA solution absorption H
2S and CO
2The principal reaction that occurs:
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 is subjected to gas-film controlling, and MDEA and CO
2Without directly reaction, this reaction and CO can only be reacted with its aqueous solution solution
2Solubleness in water has much relations, and the huge difference on this reaction mechanism has caused the difference of the speed of reaction, has consisted of the preferential selectivity of MDEA and has absorbed H
2The basis of S.
The reaction (2) since MDEA lack free hydrogen ion, can not and CO
2Direct 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 residence time and contact area, whole absorption process has been subject to the restriction of speed of reaction.After can adding activator (such as R2NH) in MDEA solution, 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) total reaction:
R
2NCH
3+CO
2+H
2O==R
2CH
3NH
++HCO
3 - (5)
By formula (3)～(5) as can be known, activator absorption CO
2, transmit CO to liquid phase
2, greatly accelerated speed of response, and MDEA is reproduced.
Wet method direct oxidation desulfurization principle is the H in the gas
2After S is dissolved in doctor solution, at 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 Sodium sulfhydrate of generation again with solution in oxygen generation oxidation analyse reaction of Salmon-Saxl, generate elemental sulfur and yellow soda ash.Owing to bring the oxygen level deficiency into, the elemental sulfur that generates in the solution is few in thionizer, thus when solution absorption behind the hydrogen sulfide of capacity, solution has just lost the ability of continuation absorbing hydrogen sulphide.For recovering the ability of solution absorption hydrogen sulfide, just must regenerate to solution, oxidation mainly occurs and analyses 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 mutual coagulation of separating out, and with upstream emersion liquid level, leave circulation desulfurization liquid, thus make doctor solution have again the ability of absorbing hydrogen sulphide.
The utility model captures based on CO in the coal gas synthetic gas of IGCC system
2Principle be first the CO in the synthetic gas to be converted into CO by the sulfur-resisting transformation process
2And H
2, the H that contains in the conversion gas
2S must remove to reduce the corrosion to subsequent technique equipment, in order to improve CO
2Capture rate adopts in MDEA solution and adds the method for activator with H
2S and CO
2Remove simultaneously, recycling wet method direct oxidation method removes H
2S reaches capture CO
2Purpose, CO
2Capture rate is higher than 90%.In the present embodiment, take full advantage of the conversion process liberated heat, be used for heating initial synthetic gas, preheating feedwater, heating MDEA rich solution etc., and the sour water that conversion process produces continues on for transformationreation after reclaiming, these measures reduced system to steam, feedwater consumption, system energy consumption is lower than 2.0GJ/tCO
2.
Explanation is at last, above embodiment is only unrestricted in order to the technical solution of the utility model to be described, although with reference to preferred embodiment the utility model is had been described in detail, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement the technical solution of the utility model, and not breaking away from aim and the scope of the technical program, it all should be encompassed in the middle of the claim scope of the present utility model.
Claims (4)
1. one kind based on CO before the burning of IGCC
2Efficient capturing device comprises
The sulfur-resisting transformation system comprises shift converter (4), and the coal gas synthetic gas that shift converter (4) connects steam and goes out IGCC system vapourizing furnace is converted into the CO in the coal gas synthetic gas with CO
2-H
2It is main mixed gas;
It is characterized in that, also comprise:
The MDEA decarbonization desulfurization system comprises absorption tower (14) and desorption tower (18), and absorption tower (14) pick out the mixed gas of sulfur-resisting transformation system, with CO wherein
2And H
2S gas absorption, desorption tower (18) pick out the CO that contains on absorption tower (14)
2And H
2The S rich solution is with CO
2And H
2S desorbs;
Sulphur carbon separation system comprises desulfurizing purifier (24,25), and desulfurizing purifier (24,25) picks out the CO of desorption tower (18)
2And H
2S gas is again through H
2S one-level resorber (26) and H
2S secondary absorber (27) is with H
2The S gas absorption finally obtains CO
2Gas.
2. capturing device according to claim 1, it is characterized in that, described shift converter (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 entrances by First Heat Exchanger (3) and the second spray humidifier (6) successively, the coal gas synthetic gas that goes out IGCC system vapourizing furnace after heat exchange heats up in First Heat Exchanger (3) and vapor mixing be linked into one section entrance, connect the first spray humidifier (5) between one section outlet and two sections entrances, connect the 3rd spray humidifier (7) between three sections outlets and four sections entrances.
3. capturing device according to claim 1 is characterized in that, described absorption tower (14) are MDEA lean solution semi lean solution absorption tower, and are described with CO
2-H
2Be to access the second water trap (10) after main mixed gas goes out shift converter (4), the liquid outlet of the second water trap (10) connects gas stripping column (11), the air outlet of gas stripping column (11) connects the bottom of absorption tower (14), from bottom to top first with the semi lean solution counter current contact, mass-and heat-transfer reaction, most CO occur at filling surface
2And H
2S is absorbed at this, and gas continues upwards to enter the lean solution absorber portion, under the lean solution effect, and residue CO
2And H
2S is absorbed.
4. according to claim 1 or 3 described capturing devices, it is characterized in that the gas that absorption tower (14) is sent into gas turbine generating system or palladium metal film hydrogen purification system behind the 4th interchanger (15) and the first skimmer (16).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220383998 CN202808740U (en) | 2012-08-03 | 2012-08-03 | Efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220383998 CN202808740U (en) | 2012-08-03 | 2012-08-03 | Efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion |
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| Publication Number | Publication Date |
|---|---|
| CN202808740U true CN202808740U (en) | 2013-03-20 |
Family
ID=47867656
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220383998 Expired - Lifetime CN202808740U (en) | 2012-08-03 | 2012-08-03 | Efficient CO2 collecting device based on IGCC (integrated gasification combined cycle) before combustion |
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| Country | Link |
|---|---|
| CN (1) | CN202808740U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102784544A (en) * | 2012-08-03 | 2012-11-21 | 中国华能集团清洁能源技术研究院有限公司 | IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system |
| CN107115787A (en) * | 2017-05-12 | 2017-09-01 | 华能（天津）煤气化发电有限公司 | A kind of device systems and method for efficiently alleviating MDEA solution deterioration rates based on integral gasification combined circulation technology |
| CN113758147A (en) * | 2021-09-29 | 2021-12-07 | 北京百利时能源技术股份有限公司 | Carbon capture hydrogen plant before burning |
-
2012
- 2012-08-03 CN CN 201220383998 patent/CN202808740U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102784544A (en) * | 2012-08-03 | 2012-11-21 | 中国华能集团清洁能源技术研究院有限公司 | IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system |
| CN107115787A (en) * | 2017-05-12 | 2017-09-01 | 华能（天津）煤气化发电有限公司 | A kind of device systems and method for efficiently alleviating MDEA solution deterioration rates based on integral gasification combined circulation technology |
| CN113758147A (en) * | 2021-09-29 | 2021-12-07 | 北京百利时能源技术股份有限公司 | Carbon capture hydrogen plant before burning |
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Effective date of registration: 20160517 Address after: 100031 Beijing, Xicheng District, the door of the revitalization of the main street, No. 6 Patentee after: Huaneng Power International,Inc. Patentee after: HUANENG CLEAN ENERGY Research Institute Address before: 100098 Beijing city Haidian District No. 48 Zhichun Road Yingdu building A block 26 layer Patentee before: HUANENG CLEAN ENERGY Research Institute |
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