CN107008121A - A kind of flue gas removal sulfur dioxide method and device - Google Patents
A kind of flue gas removal sulfur dioxide method and device Download PDFInfo
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- CN107008121A CN107008121A CN201710372133.5A CN201710372133A CN107008121A CN 107008121 A CN107008121 A CN 107008121A CN 201710372133 A CN201710372133 A CN 201710372133A CN 107008121 A CN107008121 A CN 107008121A
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- Prior art keywords
- absorption tower
- separator
- absorber portion
- flue gas
- group
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 239000003546 flue gas Substances 0.000 title claims abstract description 50
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000010521 absorption reaction Methods 0.000 claims abstract description 93
- 239000007788 liquid Substances 0.000 claims abstract description 85
- 239000006096 absorbing agent Substances 0.000 claims abstract description 58
- 239000007787 solid Substances 0.000 claims abstract description 36
- 230000008929 regeneration Effects 0.000 claims abstract description 30
- 238000011069 regeneration method Methods 0.000 claims abstract description 30
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 25
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 10
- 239000012134 supernatant fraction Substances 0.000 claims abstract description 10
- 239000007864 aqueous solution Substances 0.000 claims abstract description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 43
- 230000003647 oxidation Effects 0.000 claims description 42
- 238000002156 mixing Methods 0.000 claims description 37
- 230000001172 regenerating effect Effects 0.000 claims description 18
- 239000010440 gypsum Substances 0.000 claims description 14
- 229910052602 gypsum Inorganic materials 0.000 claims description 14
- 239000000243 solution Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 11
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 claims description 2
- 239000011575 calcium Substances 0.000 claims description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 2
- 239000000292 calcium oxide Substances 0.000 claims description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 2
- 230000008859 change Effects 0.000 claims description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims 1
- 241000790917 Dioxys <bee> Species 0.000 claims 1
- 229910052791 calcium Inorganic materials 0.000 claims 1
- 238000005516 engineering process Methods 0.000 description 12
- 238000006477 desulfuration reaction Methods 0.000 description 11
- 230000023556 desulfurization Effects 0.000 description 10
- 230000008569 process Effects 0.000 description 10
- 239000011734 sodium Substances 0.000 description 7
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 229910052708 sodium Inorganic materials 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 239000002585 base Substances 0.000 description 4
- 235000010261 calcium sulphite Nutrition 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000006073 displacement reaction Methods 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000013589 supplement Substances 0.000 description 4
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910052925 anhydrite Inorganic materials 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 241001274216 Naso Species 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000007115 recruitment Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/464—Sulfates of Ca from gases containing sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/12—Methods and means for introducing reactants
- B01D2259/124—Liquid reactants
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Geology (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a kind of flue gas removal sulfur dioxide method and device.Methods described carries out absorption removal sulfur dioxide including the use of absorption tower to flue gas, and the absorption tower is divided into the first absorber portion and the second absorber portion from top to bottom, and the flue gas circulates from bottom to top from absorption tower, and sequentially passes through the second absorber portion and the first absorber portion；First paragraph absorbing liquid is obtained using sodium hydrate aqueous solution as the absorbing liquid of the first absorber portion and after the first absorber portion absorbs to flue gas, first paragraph absorbing liquid enters the second absorber portion and continues that flue gas absorb to obtain second segment absorbing liquid, second segment absorbing liquid draws absorption tower by absorption tower bottom, and isolate supernatant fraction and solid portion by regeneration treatment, supernatant fraction sends the absorbing liquid absorbed in absorption tower as second segment back to by the second absorber portion, and absorb flue gas with entering after the first paragraph absorbing liquid of the second absorber portion is mixed, then drawn by absorption tower bottom and carry out regeneration treatment again to recycle.
Description
Technical field
It is to be related to a kind of flue gas removal sulfur dioxide method and device specifically the present invention relates to flue gas desulfurization field.
Background technology
At present, Chinese large-sized coal fired power plant flue gas desulfurization technique uses Gypsum Wet more than 90%.Lime stone-
Gypsum wet be also world wide technology it is the most ripe, using achievement most wide sulfur removal technology.But due to a variety of causes, the technique
The problems such as there is a large amount of corrosion, wears, serious fouling, blocking, high energy consumption in application in Chinese large-sized coal-burning power plant.Particularly I
State is new《Fossil-fuel power plant atmospheric pollutant emission standard》(GB13223-2011) since performing, it is desirable to which thermal power plant reaches that the world is most tight
Emission limit.The difficulty of governance of flue gas desulfurization, soot emissions is further increased in " ultra-clean discharge " target.These new marks
Accurate, target is to bring unprecedented challenge using Limestone-gypsum Wet Flue Gas Desulfurization Process, is continuously increased thermal power plant's new round transformation
New measure, such as series connection double tower, wet static dedusting etc., power plant is answered in the way of " disregarding cost, regardless of expense "
It is right.
At present, flue gas desulfurization technique both domestic and external is relatively more, and current limestone-gypsum method is prevailing technology, but exists all
Desulfurizing tower in many problems, engineer applied is mostly hollow-spraying-tower, also sub-fraction packed tower, but hollow-spraying-tower efficiency is inclined
It is low；And packed tower there are problems that being easy to occur.Under higher and higher Environmental Protection Situation, Gypsum Wet
The original technology economy advantage of desulfurization has not existed.In the urgent need to research and inquirement has more the new technology of advantage.Dual alkali is current
Small generator set desulfurization is essentially available for, separating effect is not good during due to regeneration of absorption solution, it is easy to form the easy foulings of CaSO3 so that
Easily blocked using high efficiency towers such as packed towers.Sea water desulfuration does not have incrustation situation by control ph substantially, and economical
Upper economical operation is reasonable, but the technology is not applied to still to the large coal-fired power plant of hinterland at present.
Coke oven gas desulfurization has two-stage method related process report, and oven gas main component is H2, CH4, CO, H2S, NH3Deng,
Its entirety is reproducibility atmosphere, and oxygen content 0.3%~0.8%, its desulfurization refers to removing H2S therein.Except to take off on a small quantity
The pollution beyond the region of objective existence removed is substantially target product, belongs to the more clean gas processing method for having obvious economic benefit, substantially
The problems such as without the concern for fouling, its spatial load forecasting and structure design are also relatively loose, using traditional tower or carry out compared with
Simple segmentation can be realized.Operating mode for the high fouling tendency of the high dustiness in coal-burning power plant is not applied to simultaneously.For conventional at present
Means of flue gas desulfurization of power plant technique fouling it is serious the problem of, how overall higher load is maintained while fouling is avoided, effectively
The sulfur dioxide in big flow waste gas is removed, spy proposes the present invention.
The content of the invention
It is an object of the present invention to provide a kind of flue gas removal sulfur dioxide method；This method takes off titanium dioxide using sodium base
Sulphur absorbing liquid carries out flue gas removal sulfur dioxide；
Another object of the present invention is to provide a kind of flue gas removal sulfur dioxide device.
For up to above-mentioned purpose, on the one hand, the invention provides a kind of flue gas removal sulfur dioxide method, wherein, methods described
Absorption removal sulfur dioxide is carried out to flue gas including the use of absorption tower, the absorption tower is divided into the first absorber portion and second from top to bottom
Absorber portion, the flue gas circulates from bottom to top from absorption tower, and sequentially passes through the second absorber portion and the first absorber portion；Use hydrogen
Aqueous solution of sodium oxide as the first absorber portion absorbing liquid and obtain after the first absorber portion absorbs to flue gas first paragraph and inhale
Liquid is received, first paragraph absorbing liquid enters the second absorber portion and continues that flue gas absorb to obtain second segment absorbing liquid, and second segment absorbs
Liquid draws absorption tower by absorption tower bottom, and isolates supernatant fraction and solid portion by regeneration treatment, and supernatant fraction is by the
Send the absorbing liquid absorbed in absorption tower as second segment at two absorber portions back to, and with entering the first paragraph absorbing liquid of the second absorber portion
Flue gas is absorbed after mixing, is then drawn by absorption tower bottom and carries out regeneration treatment again to recycle；The solid portion passes through
Oxidation dehydration prepares gypsum.
According to some specific embodiments of the invention, wherein, the mass concentration of the sodium hydroxide is more than 15%；Preferably
20-30%.
According to some specific embodiments of the invention, wherein, first paragraph absorbs the controllable absorber portion of entrance second of flow quantity
Continue that flue gas absorb to obtain second segment absorbing liquid.
According to some of the invention specific embodiments, wherein, regenerative agent used in the regeneration treatment be calcium ion again
Raw agent；It is preferred that one or more combinations of the regenerative agent in calcium hydroxide, calcium oxide；It is preferred that second segment absorbing liquid by
Absorb tower bottom to draw behind absorption tower, be that regeneration treatment is first carried out in the presence of regenerative agent, then by the suction of regeneration treatment
Receive liquid and pass through the isolated supernatant fraction of separator and solid portion.
According to some specific embodiments of the invention, wherein, the solid portion is to carry out oxygen in high turbulent flow oxidator
Change.
On the other hand, present invention also offers a kind of flue gas removal sulfur dioxide device, wherein, described device includes order and gone here and there
Absorption tower (1), regeneration of absorption solution system 2, oxidation unit 3 and the dehydration device 4 of connection.
According to some specific embodiments of the invention, wherein, the absorption tower 1 is two-part absorption tower, is divided from top to bottom
For interconnected the first absorber portion 13 and the second absorber portion 14, the absorption tower includes being arranged on the cigarette of the second absorber portion bottom
Gas air inlet 11, the exhaust outlet 12 being arranged at the top of absorption tower and the leakage fluid dram 15 for being arranged on absorption tower bottom, and inhaled each
The top for receiving section sets spray equipment 131,141 respectively；It is preferred that also setting up demister 132 at the top of the first absorber portion；It is preferred that
At the top of the first absorber portion bottom or the second absorber portion or the first absorber portion and the second absorber portion intersection set liquid to collect again
Distribution apparatus 133.
According to some specific embodiments of the invention, wherein, the regeneration of absorption solution system 2 includes the mixing arrangement of series connection
21 and separator 22, the mixing arrangement 21 is connected with the leakage fluid dram 15 on absorption tower, the separator 22 and oxidation unit 3
Connection.
According to some specific embodiments of the invention, wherein, the mixing arrangement 21 and separator 22 set for integral type
Meter.
According to some specific embodiments of the invention, wherein, the separator is a separator or at least two
The separator group of separator composition, the separator includes charging aperture 221, regenerated liquid outlet 222 and solid outlet 223, described
Charging aperture is connected with mixing arrangement, and the regenerated liquid outlet is connected with absorption tower, and the solid outlet is connected with oxidation unit.
According to some specific embodiments of the invention, wherein, the separator is the separator that 2-8 platforms separator is constituted
Group.
According to some specific embodiments of the invention, wherein, the separator group is point that 2-8 platform separators are composed in series
From device group, the charging aperture of wherein First is connected with mixing arrangement, and last regenerated liquid outlet is connected with absorption tower, middle
It is attached in the way of the regenerated liquid outlet of previous is connected with the charging aperture of latter, the solid outlet and oxygen of First
Connection is put in makeup, is connected after the convergence of remaining solid outlet with the charging aperture of First.
According to some specific embodiments of the invention, wherein, the separator group is 2 separators.
According to some specific embodiments of the invention, wherein, the separator group is point that 2-8 platform separators are composed in series
From device group, the charging aperture of wherein First is connected with mixing arrangement, regenerated liquid outlet is connected with absorption tower, and remaining is according to previous
Solid outlet be attached with the mode that the charging aperture of latter is connected, last solid outlet and oxidation unit connect
Connect, be connected after remaining regenerated liquid outlet convergence with the charging aperture of First.
According to some specific embodiments of the invention, wherein, the separator group is 2 separators.
According to some specific embodiments of the invention, wherein, the separator group is point that 2-8 platform separators are composed in parallel
From device group, wherein the charging aperture of every is connected with mixing arrangement respectively, the solid outlet of every is connected with oxidation unit respectively, often
The regenerated liquid outlet of platform is connected with absorption tower.
According to some specific embodiments of the invention, wherein, the separator component is two groups be linked in sequence, every group of bag
Include 1-4 separator, wherein the charging aperture of first group of each separator is connected with mixing arrangement, regenerated liquid outlet collect after with the
The charging aperture connection of two groups of each separator, the regenerated liquid outlet of second group of each separator is connected after collecting with absorption tower；The
The solid outlet of one group and second group of each separator is connected after collecting with oxidation unit.
According to some specific embodiments of the invention, wherein, first group includes 1 or 4 separators, and second group includes 4
Individual separator.
According to some specific embodiments of the invention, wherein, the removal sulfur dioxide device also includes pump 5,5 points of the pump
Lian Jie not absorption tower 1 and regenerative system 2.
According to some specific embodiments of the invention, wherein, the pump connects leakage fluid dram 15 and the regeneration on absorption tower 1 respectively
The blender of system 2.
The device of the present invention, makes full use of and has played absorption tower and the flue gas system of Dual alkali removal sulfur dioxide " clean "
Advantage and seawater method removal sulfur dioxide packed tower successful application advantage, improve " mixed regeneration ", " separation ", " oxidation ",
System and device, under the premise of rational investment and operating cost, realize SO2, the ultra-clean emissions object of flue dust.Absorbed in traditional handicraft
Liquid regeneration-oxidation is integral, CaSO3When being oxidized to gypsum, Na2SO3Largely aoxidized, influence gypsum qualitt.
One aspect of the present invention is based on the efficient mixed regeneration technology of absorbing liquid so that absorbing liquid is efficiently fully mixed with displacement slurries
Close after reaction, by CaSO3It is enriched with by efficient cyclone and pressure oxidation is carried out in high turbulent flow reactor, improves gypsum qualitt
While reduce scaling.
Another aspect of the present invention is used uses relatively inexpensive anti-corrosion material and light to greatest extent in partition type packed tower, tower
Matter filler.Absorbing liquid is run in non-fouling region with high concentration, and high pH regions use new absorbing liquid, it is to avoid fouling；Easy fouling area
The low pH operations of underload are adopted in domain, a large amount of to use regenerable absorbent liquid, reduce cost；The final stage of removal sulfur dioxide, by higher
The fresh alkali lye of concentration come realize end absorb, obtain more than 99% clearance.
According to some specific embodiments of the invention, wherein, demister 132 is also set up at the top of the first absorber portion.
According to some specific embodiments of the invention, wherein, set liquid to collect redistribution dress in the first absorber portion bottom
Put 133.
According to some specific embodiments of the invention, wherein, the regeneration of absorption solution system 2 includes the mixing arrangement of series connection
21 and separator 22, the mixing arrangement 21 is connected with the leakage fluid dram 15 on absorption tower, the separator 22 and oxidation unit 3
Connection.
Based on multiphase flow high efficiency static hybrid technology so that absorbing liquid is efficiently sufficiently mixed reaction regeneration with displacement slurries.
Blender uses smooth internal face, and multiple deflectors are set in internal mixer, and chooses flow rates 15-25m/s, comes real
Its existing internal flow Reynolds number is not less than 105The requirement of magnitude, so that efficient mixing is realized, and the violent scour for passing through particle
To offset equipment scaling tendency.
According to some specific embodiments of the invention, wherein, the removal sulfur dioxide device also includes pump 5,5 points of the pump
Lian Jie not absorption tower 1 and regenerative system 2；It is preferred that the pump connects the mixing of the leakage fluid dram 15 and regenerative system 2 on absorption tower 1 respectively
Device.
Oxidation unit 3 of the present invention can be oxidation unit commonly used in the art, and according to some tools of the present invention
Body embodiment, wherein, the oxidation unit 3 is high turbulent flow oxidator, it is characterized in that internal flow Reynolds number is not less than 105,
And by strong agitation or set multiple deflectors to realize.
Calcium sulfite oxidation process is individually carried out in high turbulent flow oxidator, by setting full envelope in removal sulfur dioxide leading portion
The pipe-line system closed, reduces the entrance of air so that sodium base removal sulfur dioxide is easier in the case where suppressing the state of oxidation carry out (non-stone
Cream crystallized region), the reduction of medicament supplementary cost.
With reference to equipment of the present invention, method of the invention can be more specifically：
Sodium base absorbing liquid in absorption tower with former smoke contacts, the SO in absorbing and removing flue gas2, generate with NaSO3Based on
Absorbing liquid.Absorbing liquid is discharged from tower, into blender, the Ca (OH) with addition2Displacement regeneration, slurries will through efficient cyclone
CaSO3Concentrating and separating, the NaSO after displacement3Slurries return to absorption tower and repeat to absorb, CaSO3Slurries enter oxidation unit, fill
Divide and be oxidized to CaSO4, further dewater treatment.
The absorption process first stage carries out high load capacity using higher concentration alkali lye and quickly absorbed, and absorbing liquid enters second segment, newly
Supplement NaOH all enters first paragraph, can run and non-scaling close under saturated concentration；Second stage uses stronger buffer capacity
The absorbing liquid that the absorbing liquid of power comes from one section of packed tower passes through buffering, by maintaining certain HCO in system3-Concentration, easily
Steadily controlled in realizing.First stage high load capacity (load improves 1.5-5 times)；(supplement is oxidized NaOH solution magnitude of recruitment
Na2SO3) by the way that pH controls in first paragraph bottom are determined between 9-10, so as to form flat with second stage regenerated liquid waste
Weighing apparatus；Second stage is controlled within the 200% of seawater removal sulfur dioxide load.
Mixed regeneration device.Based on multiphase flow high efficient separation technology so that during regeneration of absorption solution, carry out in the separator,
With the flowing of liquid phase, CaSO3Gradually form, chemical reaction is basically completed in pipe-line mixer；Separator is subsequently entered, with
The progress of reaction, sediment flco is gradually grown up with current, and the largest particles and Cmax is obtained in separator outlet,
And it is final in slag notch discharge, the process coupling integrated with separation process of particle precipitation is carried out.Overflowing liquid returns to supplement and absorbed
Liquid, underflow liquid (or after secondary concentration) enters oxidator.
Calcium sulfite oxidation process is individually carried out in high turbulent flow oxidator, greatly reduces the oxidation of sodium sulfite, has
Help obtain higher gypsum qualitt, while reducing absorbing liquid loss.By being passed through oxidation in the static mixing oxidation unit
Air, forces CaSO3As CaSO4.The system, which has, simultaneously suppresses oxidation, is consumed beneficial to reduction medicine, oxygen in pannikin kiln gas
Content is general>10%, SO3 2-Be oxidized in technique previous stage it is more, supplement NaOH it is more, but large-sized boiler oxygen content compared with
Low, about in 5-10%, for the angle for suppressing oxidation, often there is reagent consumption asking excessively in traditional sodium method removal sulfur dioxide
Topic.The invention in removal sulfur dioxide leading portion by setting totally enclosed pipe-line system so that sodium base removal sulfur dioxide is easier to
Suppress to carry out (non-gypsum crystallization section), the reduction of medicament supplementary cost under the state of oxidation.
In summary, the invention provides a kind of flue gas removal sulfur dioxide method and device.The solution of the present invention has such as
Lower advantage：
The method amount of scale buildup of the present invention is small, and equipment is easy to maintain.
The present invention to react-isolation integral technology as core regeneration of absorption solution technology so that the removal sulfur dioxide side
Method can use the high efficiency towers such as packed tower, rather than as limestone-gypsum method uses void tower, by greatly increasing contact area,
Make absorption process stable operation at low load, and possess on compared with large-sized unit economic feasibility.
The present invention efficiently mixed based on multiphase flow and isolation technics mixed regeneration device and high turbulent flow oxidator setting,
So that the coupling integrated with separation process of the process of particle precipitation is carried out, and calcium sulfite oxidation process is real by oxidation
It is existing, so that solving traditional sodium method removal sulfur dioxide often has the problem of reagent consumption is excessive.
Brief description of the drawings
Fig. 1~6 are respectively the schematic diagram of the device of the embodiment of the present invention 1~6.
Embodiment
The beneficial effect for describing the implementation process of the present invention in detail below by way of specific embodiment and producing, it is intended to which help is read
Reader more fully understand the present invention essence and feature, not as to this case can practical range restriction.
Embodiment 1
Flue gas removal sulfur dioxide device as shown in Figure 1, wherein, described device includes the two-part absorption tower of sequential series
1st, regeneration of absorption solution system 2, oxidation unit 3, dehydration device 4 and pump 5.The absorption tower includes the first absorber portion 13 and second and inhaled
Section 14 is received, exhaust outlet 12 is set and at absorption tower bottom in the second absorber portion bottom setting smoke air inlet 11, at the top of absorption tower
Portion sets leakage fluid dram 15, and sets at the top of each absorber portion spray equipment 131,141 and demister 132 respectively；
First absorber portion bottom sets liquid re-distributor 133.The regeneration of absorption solution system 2 includes the mixing arrangement of series connection
21 and a separator 22, the mixing arrangement 21 is connected with the leakage fluid dram 15 on absorption tower, the separator 22 and oxidation
Device 3 is connected.The separator includes charging aperture 221, regenerated liquid outlet 222 and solid outlet 223, and the charging aperture is with mixing
Device is connected, and the regenerated liquid outlet is connected with absorption tower, and the solid outlet is connected with oxidation unit.The pump is connected respectively
The leakage fluid dram 15 on absorption tower 1 and the blender of regenerative system 2.
Absorption removal sulfur dioxide is carried out to flue gas using Fig. 1 absorption tower, flue gas is from absorption tower from bottom to top by the
Two absorber portions and the first absorber portion, flue gas flow rate control are≤5m/s；Use quality concentration is 20% sodium hydrate aqueous solution
As the absorbing liquid of the first absorber portion, first paragraph absorbing liquid is obtained after the first absorber portion absorbs to flue gas, first paragraph is inhaled
Receive liquid to continue that flue gas absorb to obtain second segment absorbing liquid into the second absorber portion, second segment absorbing liquid is by absorption tower bottom
Absorption tower is drawn, and supernatant fraction and solid portion are isolated by regeneration treatment, supernatant fraction is sent back to by the second absorber portion
The absorbing liquid absorbed in absorption tower as second segment, and absorb cigarette with entering after the first paragraph absorbing liquid of the second absorber portion is mixed
Gas, is then drawn by absorption tower bottom and carries out regeneration treatment with calcium hydroxide again to recycle；The solid portion is through too high
The oxidation dehydration of turbulent flow oxidator prepares gypsum.Equipment is run 6 months, has no obvious fouling.
Embodiment 2
As shown in Fig. 2 the flue gas removal sulfur dioxide apparatus structure and embodiment 1 of the present embodiment are basically identical, difference is
The regenerative system 2 of the present embodiment is by mixing arrangement 21 and two separators 22 (primary separator 22 ' and second-stage separator 22 ")
It is composed in series, wherein mixing arrangement 21 is connected with the charging aperture of First separator 22 ', First separator 22 ' is again
Raw liquid outlet is connected with the charging aperture of second separator 22 ", the solid outlet and oxidation unit of First separator 22 '
Connection, the regenerated liquid outlet of second separator 22 " is connected with absorption tower, the solid outlet of second separator 22 " and
Pipeline connection between the charging aperture of mixing arrangement and First separator 22 '.Equipment is run 6 months, has no obvious fouling.
Embodiment 3
As shown in figure 3, the flue gas removal sulfur dioxide apparatus structure and embodiment 1 of the present embodiment are basically identical, difference is
The regenerative system 2 of the present embodiment is by mixing arrangement 21 and two separators 22 (primary separator 22 ' and second-stage separator 22 ")
It is composed in series, wherein mixing arrangement 21 is connected with the charging aperture of First separator 22 ', First separator 22 ' is again
Raw liquid outlet is connected with absorption tower, and the charging aperture of the solid outlet of First separator 22 ' and second separator 22 " connects
Connect, the solid outlet of second separator 22 " is connected with oxidation unit, the regenerated liquid outlet of second separator 22 " with
Pipeline connection between the charging aperture of mixing arrangement and First separator 22 '.Equipment is run 6 months, has no obvious fouling.
Embodiment 4
As shown in figure 4, the flue gas removal sulfur dioxide apparatus structure and embodiment 1 of the present embodiment are basically identical, difference is
The regenerative system 2 of the present embodiment is made up of the separator 22 in parallel of mixing arrangement 21 and four, and wherein mixing arrangement 21 is distinguished
It is connected with the charging aperture of four separators, the regenerated liquid outlet of four separators is connected after collecting respectively with absorption tower, four
The solid outlet of platform separator is connected after collecting respectively with oxidation unit.Equipment is run 6 months, has no obvious fouling.
Embodiment 5
As shown in figure 5, the flue gas removal sulfur dioxide apparatus structure and embodiment 1 of the present embodiment are basically identical, difference is
The regenerative system 2 of the present embodiment is by mixing arrangement 21 and two groups of separators 22 (primary separator 22 ' and the second-order separations of series connection
Device 22 ") composition, wherein first group 22 ' is a separator, second group 22 " is 4 separators in parallel.Mixing arrangement
21 are connected with first group of separator charging aperture, and the regenerated liquid of first group of separator exports respectively with second group four points
Charging aperture from device is connected, and the regenerated liquid outlet of second group of four separators is connected after collecting respectively with absorption tower, and four
The solid outlet of platform separator is connected after collecting respectively with oxidation unit.Equipment is run 6 months, has no obvious fouling.
Embodiment 6
As shown in fig. 6, the flue gas removal sulfur dioxide apparatus structure and embodiment 1 of the present embodiment are basically identical, difference is
The regenerative system 2 of the present embodiment is by mixing arrangement 21 and two groups of separators (primary separator group 22 ' and the second-order separations of series connection
Device group 22 ") composition, wherein every group is respectively 4 separators in parallel.The charging aperture of first group 22 ' of four separators
It is connected after collecting respectively with mixing arrangement 21, regenerated liquid outlet collects the rear charging aperture with second group 22 " of four separators
Connect respectively, the regenerated liquid outlet of second group 22 " of four separators is connected after collecting respectively with absorption tower, eight separation dresses
The solid outlet put is connected after collecting respectively with oxidation unit.Equipment is run 6 months, has no obvious fouling.
Claims (10)
1. a kind of flue gas removal sulfur dioxide method, wherein, methods described carries out absorbing de- dioxy including the use of absorption tower to flue gas
Change sulphur, the absorption tower is divided into the first absorber portion and the second absorber portion from top to bottom, the flue gas from absorption tower from bottom to top
Circulation, and sequentially pass through the second absorber portion and the first absorber portion；The absorption of the first absorber portion is used as using sodium hydrate aqueous solution
Liquid simultaneously obtains first paragraph absorbing liquid after the first absorber portion absorbs to flue gas, first paragraph absorbing liquid enter the second absorber portion after
Continuous that flue gas absorb to obtain second segment absorbing liquid, second segment absorbing liquid draws absorption tower by absorption tower bottom, and by again
Supernatant fraction and solid portion are isolated in raw processing, and supernatant fraction is sent back in absorption tower by the second absorber portion to be inhaled as second segment
The absorbing liquid of receipts, and flue gas is absorbed with entering after the first paragraph absorbing liquid of the second absorber portion is mixed, then drawn by absorption tower bottom
Go out and carry out regeneration treatment again to recycle；The solid portion prepares gypsum through peroxidating dehydration.
2. flue gas removal sulfur dioxide method according to claim 1, wherein, the mass concentration of the sodium hydroxide is more than
15%；Preferably 20-30%.
3. flue gas removal sulfur dioxide method according to claim 1, wherein, first paragraph absorbs the controllable entrance of flow quantity the
Two absorber portions continue that flue gas absorb to obtain second segment absorbing liquid.
4. removal sulfur dioxide method according to claim 1, wherein, regenerative agent used in the regeneration treatment be calcium from
Sub- regenerative agent；It is preferred that one or more combinations of the regenerative agent in calcium hydroxide, calcium oxide；It is preferred that second segment absorbs
Liquid is drawn behind absorption tower by absorption tower bottom, is that regeneration treatment is first carried out in the presence of regenerative agent, then by regeneration treatment
Absorbing liquid pass through the isolated supernatant fraction of separator and solid portion.
5. removal sulfur dioxide method according to claim 1, wherein, the solid portion is entered in high turbulent flow oxidator
Row oxidation.
6. a kind of flue gas removal sulfur dioxide device, wherein, described device includes the absorption tower (1) of sequential series, regeneration of absorption solution
System (2), oxidation unit (3) and dehydration device (4).
7. removal sulfur dioxide device according to claim 6, wherein, the absorption tower (1) is two-part absorption tower, from upper
And under be divided into interconnected the first absorber portion (13) and the second absorber portion (14), the absorption tower includes being arranged on the second absorption
The smoke air inlet (11) of section bottom, the exhaust outlet (12) being arranged at the top of absorption tower and the leakage fluid dram for being arranged on absorption tower bottom
(15) spray equipment (131,141), and at the top of each absorber portion is set respectively；It is preferred that being also set up at the top of the first absorber portion
Demister (132)；It is preferred that at the top of the first absorber portion bottom or the second absorber portion or the first absorber portion and the second absorber portion are handed over
Liquid re-distributor (133) is set at boundary.
8. removal sulfur dioxide device according to claim 6, wherein, the regeneration of absorption solution system (2) includes series connection
Mixing arrangement (21) and separator (22), the mixing arrangement (21) are connected with the leakage fluid dram (15) on absorption tower, the separation
Device (22) is connected with oxidation unit (3)；It is preferred that the mixing arrangement (21) and separator (22) design for integral type.
9. removal sulfur dioxide device according to claim 8, wherein, the separator is for a separator or at least
The separator group of two separator compositions, the separator includes charging aperture (221), regenerated liquid outlet (222) and solid outlet
(223), the charging aperture is connected with mixing arrangement, and the regenerated liquid outlet is connected with absorption tower, the solid outlet and oxidation
Device is connected；It is preferred that the separator is the separator group that 2-8 platforms separator is constituted；
It is preferred that the separator group is the separator group that 2-8 platform separators are composed in series, wherein the charging aperture of First is with mixing
Device is connected, and last regenerated liquid outlet is connected with absorption tower, middle to be exported and latter according to the regenerated liquid of previous
Charging aperture connection mode be attached, the solid outlet of First is connected with oxidation unit, remaining solid outlet converge
It is connected afterwards with the charging aperture of First；More preferably described separator group is 2 separators；
Or preferably described separator group is the separator group that is composed in series of 2-8 platform separators, wherein the charging aperture of First with
Mixing arrangement connection, regenerated liquid outlet are connected with absorption tower, and remaining is according to the solid outlet and the charging aperture of latter of previous
The mode of connection is attached, and last solid outlet is connected with oxidation unit, remaining regenerated liquid outlet convergence after with
The charging aperture connection of First；More preferably described separator group is 2 separators；
Or preferably described separator group is the separator group that 2-8 platform separators are composed in parallel, wherein the charging aperture difference of every
It is connected with mixing arrangement, the solid outlet of every is connected with oxidation unit respectively, the regenerated liquid outlet of every is connected with absorption tower；
Or preferably described separator component is two groups be linked in sequence, every group includes 1-4 separator, wherein first group each
The charging aperture of separator is connected with mixing arrangement, and the charging aperture that regenerated liquid outlet collects afterwards with second group of each separator is connected,
The regenerated liquid outlet of second group of each separator is connected after collecting with absorption tower；The solid of first group and second group of each separator
Outlet is connected after collecting with oxidation unit；More preferably first group includes 1 or 4 separators, and second group includes 4 separators.
10. removal sulfur dioxide device according to claim 6, wherein, the removal sulfur dioxide device also includes pump (5),
The pump (5) connects absorption tower (1) and regenerative system (2) respectively；It is preferred that the pump connects the leakage fluid dram of absorption tower (1) respectively
(15) and regenerative system (2) blender.
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Application publication date: 20170804 |