CN101306317A - Tower top discharge type flue gas desulfurization method - Google Patents
Tower top discharge type flue gas desulfurization method Download PDFInfo
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- CN101306317A CN101306317A CNA2008100335974A CN200810033597A CN101306317A CN 101306317 A CN101306317 A CN 101306317A CN A2008100335974 A CNA2008100335974 A CN A2008100335974A CN 200810033597 A CN200810033597 A CN 200810033597A CN 101306317 A CN101306317 A CN 101306317A
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- Prior art keywords
- flue gas
- tower
- absorption liquid
- discharge type
- top discharge
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 239000003546 flue gas Substances 0.000 title claims abstract description 110
- 230000003009 desulfurizing Effects 0.000 title claims description 92
- 238000006477 desulfuration reaction Methods 0.000 title claims description 50
- 239000007788 liquid Substances 0.000 claims abstract description 87
- 239000007921 spray Substances 0.000 claims abstract description 75
- 238000010521 absorption reaction Methods 0.000 claims abstract description 72
- 230000005587 bubbling Effects 0.000 claims abstract description 47
- 238000005406 washing Methods 0.000 claims abstract description 43
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims abstract description 15
- 239000000203 mixture Substances 0.000 claims abstract description 14
- 230000003647 oxidation Effects 0.000 claims abstract description 11
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 11
- 239000000779 smoke Substances 0.000 claims abstract description 9
- 238000002425 crystallisation Methods 0.000 claims abstract description 5
- 230000005712 crystallization Effects 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims abstract description 5
- 239000012265 solid product Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 239000007787 solid Substances 0.000 claims description 24
- 238000004140 cleaning Methods 0.000 claims description 20
- 239000000463 material Substances 0.000 claims description 19
- 238000000746 purification Methods 0.000 claims description 12
- 229910052602 gypsum Inorganic materials 0.000 claims description 11
- 239000010440 gypsum Substances 0.000 claims description 11
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 10
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 9
- LSNNMFCWUKXFEE-UHFFFAOYSA-L Sulphite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 claims description 8
- 239000000047 product Substances 0.000 claims description 8
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 6
- 239000011575 calcium Substances 0.000 claims description 6
- 229910052791 calcium Inorganic materials 0.000 claims description 6
- 230000002035 prolonged Effects 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 125000005843 halogen group Chemical group 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 3
- 239000008258 liquid foam Substances 0.000 claims description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate dianion Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxyl anion Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 239000000284 extract Substances 0.000 claims 2
- 241000282326 Felis catus Species 0.000 claims 1
- JJEJDZONIFQNHG-UHFFFAOYSA-O [NH4+].[C+4] Chemical compound [NH4+].[C+4] JJEJDZONIFQNHG-UHFFFAOYSA-O 0.000 claims 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-O azanium;sulfuric acid Chemical compound [NH4+].OS(O)(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-O 0.000 claims 1
- 239000002245 particle Substances 0.000 claims 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N tin hydride Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 claims 1
- 238000010276 construction Methods 0.000 abstract description 9
- 239000003344 environmental pollutant Substances 0.000 abstract description 7
- 231100000719 pollutant Toxicity 0.000 abstract description 5
- 239000006260 foam Substances 0.000 abstract description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract 2
- 238000005536 corrosion prevention Methods 0.000 abstract 1
- 238000004904 shortening Methods 0.000 abstract 1
- 239000000945 filler Substances 0.000 description 21
- 239000000243 solution Substances 0.000 description 15
- 239000002253 acid Substances 0.000 description 11
- 230000000694 effects Effects 0.000 description 11
- 230000000875 corresponding Effects 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 230000004087 circulation Effects 0.000 description 8
- 238000005260 corrosion Methods 0.000 description 8
- 238000007599 discharging Methods 0.000 description 8
- 241000196324 Embryophyta Species 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N HCl Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 229910002089 NOx Inorganic materials 0.000 description 6
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Ammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 5
- 235000019738 Limestone Nutrition 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000006028 limestone Substances 0.000 description 5
- -1 salt compound Chemical class 0.000 description 5
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 5
- 229960005069 Calcium Drugs 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L Calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium monoxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 230000002708 enhancing Effects 0.000 description 4
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 4
- CSNNHWWHGAXBCP-UHFFFAOYSA-L mgso4 Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 229960003563 Calcium Carbonate Drugs 0.000 description 3
- GBAOBIBJACZTNA-UHFFFAOYSA-L Calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 3
- 230000002378 acidificating Effects 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 description 3
- 235000010261 calcium sulphite Nutrition 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- ZLNQQNXFFQJAID-UHFFFAOYSA-L Magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 2
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 2
- 230000001070 adhesive Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- 235000012255 calcium oxide Nutrition 0.000 description 2
- 235000011132 calcium sulphate Nutrition 0.000 description 2
- 239000004567 concrete Substances 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000006194 liquid suspension Substances 0.000 description 2
- 239000001095 magnesium carbonate Substances 0.000 description 2
- 239000011776 magnesium carbonate Substances 0.000 description 2
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 2
- 239000000395 magnesium oxide Substances 0.000 description 2
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 2
- 235000019341 magnesium sulphate Nutrition 0.000 description 2
- 239000004570 mortar (masonry) Substances 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 229910052813 nitrogen oxide Inorganic materials 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 230000001737 promoting Effects 0.000 description 2
- 230000001105 regulatory Effects 0.000 description 2
- 230000003014 reinforcing Effects 0.000 description 2
- 235000009566 rice Nutrition 0.000 description 2
- 230000035939 shock Effects 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N Ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- PRKQVKDSMLBJBJ-UHFFFAOYSA-N Ammonium carbonate Chemical compound N.N.OC(O)=O PRKQVKDSMLBJBJ-UHFFFAOYSA-N 0.000 description 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- 229920000114 Corrugated plastic Polymers 0.000 description 1
- 206010022000 Influenza Diseases 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 241000216843 Ursus arctos horribilis Species 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000001099 ammonium carbonate Substances 0.000 description 1
- 235000012501 ammonium carbonate Nutrition 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L cacl2 Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003365 glass fiber Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 load Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- QDHHCQZDFGDHMP-UHFFFAOYSA-N monochloramine Chemical compound ClN QDHHCQZDFGDHMP-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 230000001590 oxidative Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002335 preservative Effects 0.000 description 1
- 239000003755 preservative agent Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000001187 sodium carbonate Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The invention relates to a tower top emission type flue gas desulphurization method, which comprises a flue gas desulphurization tower and is characterized in that an upright smoke emission tube is arranged above a purified flue gas outlet of the desulphurization tower. Original flue gas flows upward to pass through a spray section after entering the desulphurization tower, and is in counter-flow contact with a washing absorption liquid which is sprayed downward from a sprayer, thereby removing sulfur dioxide and other pollutants, the mixture continually goes upward to enter a packing section for removing the foam, the obtained purified flue gas enters an upright smoke tube above a flue gas outlet arranged at the top of the desulphurization tower to be directly discharged to the atmosphere, the absorption liquid falls from the spray section and enters a bubbling section at the bottom of the desulphurization tower for oxidation and crystallization, and a sulfate solid product is obtained by separation. The desulphurization method of the invention enables the desulfurized purified flue gas not to be discharged form the original chimney, thereby avoiding the corrosion prevention and the enhanced construction of the original chimney, saving the investment and shortening the construction period.
Description
Technical field
The present invention relates to a kind of tower top discharge type gas cleaning discharging integrated desulfurization method, relate in particular to the technology that from flue gas, reclaims oxysulfide, belong to electric power, metallurgy, environmental protection, chemical technology field, especially be fit to the flue gas desulfurization technique field.
Background technology
Huge chimney is the indispensable device of vast boiler, thermal power plant always.And the construction technology of chimney is very complicated, influences industrial maintenance, reinforcing, enhancing construction and is generally repelled.For example, be that a large amount of boiler flues are discharged in the thermal power plant of fuel with coal or oil, directly arrange through chimney to atmosphere.The blowdown stack height of boiler of power plant generally all adopts reinforcing bar to mix earth material as the intensity shell between 120～250m.Owing to contain acidic gaseous materials such as SOx, NOx, HCl and HF, SO especially wherein in the flue gas
3Gas makes flue gas show acid dew piont corrosion.The acid dew point of flue gas is with SO in the flue gas
3Increase and increase with moisture content, generally between 100～150 ℃.In order to ensure not occurring acid dew piont corrosion in the fume emission process, from the steam generator system outlet, the flue-gas temperature of promptly common boiler induced-draft fan outlet is higher 15～25 ℃ than dew point.But for the purpose of safety and over-designed, inner wall of stack all needs liner insulation, especially anti-corrosion material, and with acid resistant adhesive mortar, inferior nexine lining is with acidproof brick at the innermost layer lining that contacts with flue gas.
Along with environmental requirement is more and more stricter, power plant or boiler all need to install flue gas desulfur device, and the flue gas desulfurization technique of main flow all is the method that the aqueous slurry washing absorbs, or be called wet method, desulfurizing agent is an alkaline matter, such as natural lime stone, i.e. calcium carbonate, magnesia/magnesium carbonate, NaOH/sodium carbonate, perhaps synthetic ammonia etc., desulfurization product is respectively gypsum (a calcium sulphate dihydrate crystal), epsom salt crystal, sodium sulphate or ammonium sulfate.A common ground of these methods all is that the desulfidation tail gas exhaust temperature is lower than the acid dew piont corrosion temperature, and near the water saturated water dew point temperature of flue gas, between 40～60 ℃, although at desulphurization plant, is commonly referred in the desulfurizing tower SO
3Removal efficiency also very high, but because SO
3Meet water and can form acid mist, impossible 100% removes, and the tail gas after the desulfurization contains sulfuric acid mist, still shows obvious corrosion.
Eliminate the way that the desulfidation tail gas acid mist can not adopt heating, because the boiling point of sulfuric acid is greater than 320 ℃, energy that can not consume significant is heated to boiling point above sulfuric acid with tail gas.
Existing method is that the original chimney of boiler is further implemented anti-corrosion treatment, such as at original acid resistant adhesive mortar layer inside lining anti-corrosive material again, strengthens its anti-corrosion capability.For newly-built unit, the anticorrosion construction period that makes of enhancing property prolongs greatly, and the anticorrosion chimney construction cost that makes of enhancing property increases, and the difficulty that follow-up maintenance and anti-corrosion material upgrade is also very big.For old unit, if original chimney is carried out new preservative treatment, difficulty of construction is big, long construction period, and more crucial is that this production to unit or boiler can affect greatly, and lacks using value in practice.
Summary of the invention
The invention discloses a kind of tower top discharge type gas cleaning sulfur method, also disclose the novel tower top discharge type gas cleaning discharging integrated desulfurization tower that uses this method, especially disclose a kind of desulfurizing tower that from flue gas, reclaims oxysulfide.This method makes flue gas again in the desulfurizing tower behind the cleaning and desulfurization, and the upright smoke evacuation tube discharging that directly is provided with from desulfurizing tower top exhanst gas outlet top enters atmosphere, no longer needs through huge smoke stack emission originally.Like this, chimney originally no longer needs to carry out anticorrosion enhancing to be handled, even original chimney discarded fully, has overcome the above-mentioned defective that prior art exists, and has saved investment, has also obviously shortened the construction period.
Major technique innovation of the present invention also is, makes flue gas in desulfurizing tower inside, and with respect to the washing absorption liquid adverse current that flows downward upwards, it is last directly from the up discharging of upright chimney of desulfurizing tower to purify flue gas, no longer needs through original smoke stack emission.Therefore, the upright chimney that the present invention mentions, perhaps in line chimney, perhaps in line flue, all be meant the purification exhanst gas outlet and the direct member of direct connection fume desulfurizing tower to airborne release tail gas, the desulfurizing tower that this member is installed is emission purification gas directly, the original chimney that uses of discarded fully boiler or power plant.
Technological innovation of the present invention also is, its spray section by being provided with in the desulfurizing tower, washing absorption liquid high degree of dispersion is that fine drop fully contacts with flue gas, the transmission of quality and heat takes place simultaneously, improved the effect of desulfidation and purification of flue gas, sulfur in smoke becomes the sulfurous acid acid salt aqueous solution.
Technological innovation of the present invention also is, its packing section by being provided with in the desulfurizing tower is efficiently removed the fog-like liquid of carrying secretly and dripped, or is called the liquid foam from the flue gas that spray section is come, and makes that purifying flue gas can directly discharge through going into upright chimney.
Technological innovation of the present invention is that also its realizes the efficient oxidation of sulphite by bubbling segment of setting in the desulfurizing tower, realizes the efficient crystallization of sulfate simultaneously.Bubbling segment of the present invention is arranged on the bottom or the bottom of flue gas purifying equipment, arrange and flow scheme design by accessory, this bubbling segment can make the washing absorption liquid carry out the circulation between inside and outside of circulation up and down, the tower body of tower body inside, former dose of washing absorption, dissolving tank, oxidation processes, absorption liquid circulating slot four big functions are accepted in performance simultaneously, greatly improve washing and absorbed former dose service efficiency, improved the flue gas washing absorption efficiency.By adding different desulfurizing agents to bubbling segment, bubbling segment can cooperate miscellaneous part, absorb oxious components such as dust, NOx, HCl and HF by physics, chemistry, biological method, can also reclaim oxysulfide in a large number, produce sulfate byproduct with bigger use value.
With reference to accompanying drawing 1, accompanying drawing 2, tower top discharge type flue gas desulfurization purification method disclosed by the invention mainly comprises following processing step:
The first, flue gas enters
Contain SO
2(content is generally at 500-15000mg/Nm
3), SO
3(content is generally at 10-300mg/Nm
3), (content is generally at 100-1000mg/Nm for NOx
3), (content is generally at 10-100mg/Nm for HCl/HF
3), (content is generally at 50-500mg/Nm for dirt
3) wait pollutant, and temperature is 100-160 ℃ flue gas, enters desulfurizing tower from gas approach, preferably adopts air blast that untreated flue gas is sent into desulfurizing tower.
The second, spray washing absorbs
After flue gas entered desulfurizing tower, the spray section of upwards flowing through and being provided with in the desulfurizing tower sprayed the washing absorption liquid droplet counter current contacting of getting off with spray thrower from spray section, and the chemical reaction in gas-liquid mass transferring and the liquid phase takes place, and absorbed and deviate from above pollutant.In spray section, the SO in the flue gas
2Become sulphite when the carbonate, oxide or the hydroxide that adopt calcium are desulfurization material, SO
2Then become calcium sulfite, corresponding circulating absorption solution is a kind of sulfate, sulphite, halid pulpous state aqueous mixtures that contains calcium, and contains solid masses 3-30% in the described pulpous state aqueous mixtures, is preferably 10-20%.When adopting ammonia (can be liquid ammonia, gaseous ammonia, ammonia water mixture or ammonium carbonate) to make SO as desulfurization material
2Then become ammonium sulfite, corresponding circulating absorption solution is a kind of sulfate, sulphite, halid pulpous state aqueous mixtures that contains ammonium, and contains solid masses 3-30% in the described pulpous state aqueous mixtures, is preferably 10-20%.In desulfurization, other acid contaminants in the flue gas also are absorbed purification, SO
3Become sulfate, HCl becomes chloride, and NOx becomes nitric acid or nitrite.The eliminating efficiency of these acid contaminants can reach more than the 95-99%, and the eliminating efficiency of the flyash in the flue gas (dirt) also can be greater than 60%-90%.Especially, the water-cooled that flue gas is absorbed in the liquid swashs and humidification, and temperature is reduced between 40-60 ℃.
The 3rd, the flue gas foam removal
After flue gas is finished desulfurizing and purifying, continue upwards to flow, enter packing section, purpose is to remove the drop that brings from spray section, or claims the liquid foam, and foam removal efficient is greater than 95%.Packing section has two-layer filler, and all there is one group of water jet every layer of filler top, and in order to the attached solid of flushing foam removal filler Shang , such as gypsum, ammonium sulfate or magnesium sulfate etc. prevent to continue to accumulate the gas passage that stops up in the filler.Under the running status, the water jet operation of lower floor's filler during parking, must move water jet a period of time of upper strata filler continuously, and the water jet of preferred upper and lower layer filler moves simultaneously.
The 4th, smoke directly ventilating
Be called the purification flue gas through the flue gas after the packing section, directly enter atmosphere by purifying exhanst gas outlet from upright chimney, no longer enter atmosphere by former chimney, temperature under the purification flue gas carries in the upright chimney is also between 40-60 ℃, and the height of upright chimney is between 20-80 rice, preferably between 30-60 rice.
The 5th, the circulation of washing absorption liquid
The washing absorption liquid is for containing alkaline desulfurizing agent, sulfate and crystalline solid thereof, and the pulpous state aqueous solution of the salt compound of other pollutants, the especially saturated or oversaturated pulpous state aqueous solution by sulfate.The washing absorption liquid is under the effect of circulating pump, realizing that at the bubbling segment of desulfurizing tower bottom with between the spray section on desulfurizing tower top the washing absorption liquid is inside and outside desulfurizing tower, two circulations up and down, to wash absorption liquid and mention spray section from bubbling segment, simultaneously, from spray section, the washing absorption liquid can drop to bubbling segment again naturally.
The 6th, spray thrower multilayer spray in parallel
Big for unit or boiler capacity, perhaps SO in the flue gas
2The situation that concentration is high, if perhaps adopting the extremely low calcium raw material of solubility (can be calcium carbonate, it is lime stone, or calcium oxide, i.e. quick lime, or calcium hydroxide, be calcium hydroxide), the circular flow of washing absorption liquid will be very huge, and existing pump technology is difficult to satisfy the requirement of big flow, and the most a lot of platform circulating pumps are in parallel to be used.Especially, all corresponding cleaning solution import of each circulating pump and one group of cleaning solution spray thrower make the washing absorption liquid through at least one group of spray thrower atomizing.Every group of spray thrower all is made up of the absorption liquid person in charge, arm and nozzle, guarantees to wash absorption liquid and evenly distributes and tiny atomizing along the desulfurizing tower cross section.The quantity of atomizer needs 7 at least, is basic every 0.5-2.0 m with the desulfurizing tower cross-sectional area especially
2Arrange 1 nozzle, and the hydrojet flow of described nozzle is 10～100m
3/ h is preferably 20～50m
3/ h.The flow of every circulating pump is 500-5000m
3/ h.
The 7th, oxidizing and crystallizing
Washing absorption liquid from spray section is got off directly enters the bubbling segment that is positioned at the desulfurizing tower bottom.At bubbling segment, the oxidation air of being sent here by air compressor blasts oxidation air by the air bubbler to the washing absorption liquid, the side that is arranged on bubbling segment is advanced an agitator prolonged agitation, promote chemistry, the Physical Absorption effect of material in the flue gas, absorption liquid is through after the air oxidation, sulphite becomes sulfate, and vitriol is separated out in crystallization under the supersaturation situation.Bubbling segment has also served as the effect of absorption liquid circulating slot, and the absorption liquid that constantly will contain desulfurizing agent through the outer circulating pump of desulfurizing tower is transported to spray section, constantly absorbs the pollutant in the flue gas, especially SO
2, return the bubbling segment of desulfurizing tower bottom.Bubbling segment has also served as the function of desulfurizing agent dissolving tank.Generally speaking, fresh desulfurizing agent is such as the limestone powder slurries of granularity more than the 250-325 order, and magnesia/magnesium carbonate slurries, or liquefied ammonia/vaporous ammonia/ammoniacal liquor directly are added to bubbling segment, mix, dissolve, dilute with absorption liquid.
The 8th, desulfurization product is separated
Must constantly discharge absorption liquid from bubbling segment by discharge pump, the material that it is comprised enters the curing separable programming, for example entering follow-up sulfate solid separates and process equipment, from the remaining liquid of separation equipment, or be called mother liquor, be back to bubbling segment again, make method of the present invention not produce, or seldom produce waste water.
As seen from the above technical solution, the employed desulfurizing tower of tower top discharge type gas cleaning sulfur method of the present invention, four parts have mainly been comprised: be respectively bubbling segment, spray section, packing section and upright chimney from bottom to up, make the polluter of in the cleaning and desulfurization Tata, deviating from the flue gas, especially SO
2Afterwards, cleaning of off-gas is without original boiler chimney discharging, thereby it is anticorrosion to have avoided prior art to strengthen boiler chimney, has saved investment, has shortened the duration.
Particularly, tower top discharge type gas cleaning sulfur method disclosed by the invention preferably uses following tower top discharge type gas cleaning discharging integrated desulfurization tower, and this tower is a cylindrical shape or square, and its novelty design also comprises:
Tower body;
Gas approach on the tower body, position between tower body middle and lower part or middle and lower part to middle and upper part, preferred middle part;
Exhanst gas outlet on the tower body, the position is in tower body top or top, preferred top;
Be arranged on the packing section in the tower body between gas approach and the exhanst gas outlet;
Be arranged on the spray section in the tower body between gas approach and the packing section;
Be arranged on the bubbling segment that is positioned at tower body of gas approach bottom;
Packing section is arranged in parallel with the corrugated plastic plate and forms, and sheet spacing 20～50mm, selected plastics are the composite of polypropylene or it and glass fibre, and the thickness of plastic plate is between 1.0mm～5.0mm, preferably between 2.0mm～3.5mm;
Especially, be arranged on the upright chimney that purifies on the exhanst gas outlet, the cross section of upright chimney be circular, ellipse, square, perhaps rectangle;
In addition, be provided with two sections fillers in the packing section, and all be furnished with water jet on every section filler;
Be provided with gas distributor in the spray section, washing absorption liquid spray thrower and liquid wall stream baffle ring;
Be provided with air sparger and side in the bubbling segment and advanced an agitator, the effect that side is advanced an agitator is, prolonged agitation when equipment moves promotes the mixing and the mass transfer of gas-liquid-solid three-phase slurries and prevents that solid is in bottom deposit, when equipment stopped, prolonged agitation prevented that solid is in bottom deposit;
The cross-sectional area of in line chimney is 0.05～0.35 times of spray section cross-sectional area, is 0.10～0.25 times preferably, preferably 0.125～0.15 times;
The height of in line chimney is between 20～100m, preferably between 30～70m;
Spray section of the present invention can comprise as lower member: the first, and flue gas distributor; The second, washing absorption liquid spray thrower; The 3rd, liquid wall stream baffle plate.
Flue gas distributor design of the present invention has following main points:
The purpose of flue gas distributor is to guarantee that flue gas enters back in the tower and evenly distributes along the cross section of tower, makes the washing absorption liquid even contact of flue gas under can be with spray, guarantees the efficient of washing and absorbing.
Preferred flue gas distributor is the sieve plate shape, and its percent opening is 10～50%, is preferably 20-30%, and bore dia is 10～100mm; Said sieve plate can be a flat board with holes, also can be corrugated plating with holes or flap;
Said percent opening is the perforate gross area and the ratio of the cross-sectional area of tower body;
Perhaps, said flue gas distributor is a screen, and its percent opening is 10～50%, is preferably 20-30%, and the width in grizzly bar slit is 10～100mm, and length is 0.5～15.0m; Said screen can be dull and stereotyped, also can be the camber plate, or swash plate.
Spray thrower design main points of the present invention are as follows:
Spray thrower has two purposes and effect: the one, and the washing absorption liquid is evenly distributed, the 2nd, make washing absorption liquid high degree of dispersion, become tiny drop.
Spray thrower comprises distributor pipe and nozzle, and distributor pipe is connected with nozzle, and nozzle is a spiral nozzle;
Preferred distributor pipe is divided into to be responsible for and arm, and arm is connected with the person in charge, and the person in charge's internal diameter is 0.15～1.5m, and the internal diameter of arm is 0.05～0.5mm; The flowing velocity of absorption liquid in pipe is 1.0～5.0m/s, more preferably 1.5～2.5m/s.
The quantity of nozzle is on the cross section of desulfurizing tower, arranges 1 nozzle for every 0.5-2.0 square metre, and the hydrojet flow of each nozzle is 10～100m
3/ h is optimized for 20～80m
3/ h; The spout internal diameter of nozzle is 10～120mm, is preferably 20～60mm.
Wall stream baffle design main points of the present invention are as follows:
The application purpose of wall stream baffle plate is to weaken or eliminate the liquid flow of desulfurizing tower inwall, and the washing absorption liquid of spray is evenly flowed on the cross section of tower, improves the utilization ratio of washing absorption liquid.Because the angle of the nozzle of spray thrower configuration is bigger, because want high degree of dispersion, the liquid that must have a large amount of sprinklings can be spread across on the inner wall of tower, and the washing absorption liquid that flows downward along inwall and the mass transfer effect of flue gas are relatively poor, thereby has reduced the utilization ratio of washing absorption liquid.
The inner wall of tower that can eliminate the washing absorption liquid that is provided with of wall stream baffle plate flows, and wall flow liquid body is turned in the tower, improves the utilization ratio of washing absorption liquid, can reduce the internal circulating load of washing absorption liquid in some sense.
Wall stream baffle plate directly is connected the inwall of tower, and the angle of the vertical direction that forms with inwall is at 30～90 degree, general below spray thrower 0.5～1.5 meter position, the width of wall stream baffle plate is 0.1～0.5m, wall stream baffle plate can be an integral body, also can disconnect.
Description of drawings
Fig. 1 is the structural representation of tower top discharge type flue gas desulfurization tower.
Fig. 2 is the process flow diagram of tower top discharge type flue gas desulfurization method.
The specific embodiment
Embodiment 1
A kind of tower top discharge type flue gas desulfurization method is used for the desulfurizing and purifying of following condition flue gas:
It is that a kind of flue gas contains SO
23000mg/Nm
3, SO
330mg/Nm
3, NOx 500mg/Nm
3, HCl and HF content 30mg/Nm
3, dust content 100mg/Nm
3Pollutant, and temperature is 135 ℃ the former flue gas of boiler, flue gas flow is 450,000 Nm
3/ h.
Referring to Fig. 1, the gas cleaning discharging integrated desulfurization tower that the present invention adopts is columnar tower, comprising:
Tower body (1), tower body (1) diameter is 8.0m;
Be arranged on the bubbling segment that is positioned at tower body (2) of tower body (1) bottom, be provided with one group of air bubbler in the bubbling segment (2) and three sides are advanced an agitator;
Be arranged on the gas approach (3) of tower body (1) middle part or middle and lower part, its flow area is a rectangle, high 2.5m, wide 6.0m;
Be arranged on the spray section that is positioned at tower body (4) of tower body (1) middle and upper part, spray section is provided with the sieve-board type gas distributor in (4), 2 groups of absorption liquid spray throwers and liquid wall stream baffle plate, and spray thrower is made of the person in charge, arm and nozzle, nozzle is a spiral nozzle, and every group of nozzle quantity is 50;
The packing section that is positioned at tower body (5) on tower body (1) top is set, two sections fillers are set in the packing section (5), all be furnished with water jet on every section filler;
Be arranged on the purification exhanst gas outlet (6) at tower body (1) top;
Be arranged on the upright chimney (7) that purifies on the exhanst gas outlet (6), the cross-sectional area of upright chimney (7) is circular, and to its exhaust outlet, cross-sectional area constantly reduces from its air inlet, is reduced to 0.125 times with the ratio of the cross-sectional area of spray section (4) from 0.25;
The height of in line chimney is 55 meters.
Referring to Fig. 2, the concrete technological design of tower top discharge type flue gas desulfurization method of the present invention is as follows:
Air blast (30) blasts the incorporate purified treatment tower of emission abatement (10) to flue gas from gas approach (3).Desulfurization material is liquid synthetic ammonia, the washing absorption liquid of circulation is ammonium sulfate, ammonium sulfite, the ammonium chloride pulpous state aqueous mixtures of sulfur acid crystalline ammonium solid, and this circulating absorption solution also contains the flyash that washs from flue gas, and it contains solid masses is 15%.The washing absorption liquid under the effect of circulating pump (40), between the bubbling segment (2) of purified treatment tower (10), spray section (4), realize tower body (1) up and down, inside and outside two circulations of tower body (1).
Adopt two circulating pumps, the flow of every circulating pump is 1500m
3/ h.
After flue gas enters the tower body (1) of purified treatment tower (10), the spray section (4) that is provided with in the tower of upwards flowing through.In spray section, two groups of cleaning solution spray throwers continue spray (all corresponding circulating pump separately of each group cleaning solution spray thrower, corresponding cleaning solution import separately), the SO in the flue gas
2Become ammonium sulfite.Flue gas is washed the absorption liquid cold shock, and temperature is reduced to 52 ℃.
In the spray section, the spray flux of each nozzle is 30m
3/ h.
After the flue gas upruss process spray section (4), continue upwards to enter packing section (5).Packing section (5) has two-layer filler, and all there is one group of water jet every layer of filler top.Under the continuous running status of flue gas purifying equipment, the water jet continuous service of lower floor's filler; During parking, the water jet of upper strata filler operation 3 minutes.The method of operation of water jet and the time liquid level with the bubbling segment (2) of tower bottom is that benchmark is regulated.When liquid level is lower than the setting liquid level, open water jet, both washed the demist packing layer, replenish fresh water (FW) to absorption tower (10) again.
Be called the purification flue gas through the flue gas after the packing section (5), directly enter atmosphere, 51 ℃ of delivery temperatures from upright chimney (7) by purifying exhanst gas outlet (6).
From the washing absorption liquid that spray section (4) is got off, directly enter the bubbling segment (2) that is positioned at purified treatment tower (10) bottom.In bubbling segment (2), air compressor machine (20) divides bubbler to blast oxidation air to absorption liquid by air, the ammonium sulfite that spray section is obtained becomes ammonium sulfate, and under the supersaturation situation, separate out ammonia sulfate crystal, the side that is arranged on bubbling segment (2) is advanced an agitator prolonged agitation, promote chemistry, the Physical Absorption effect of material in the flue gas, comprise promoting solution-air and solid-liquid to mix and mass transfer, also promote solid-liquid suspension.The ammonium sulfate solids product is sent into solid-liquid separating equipment (60) by discharge pump (50), specifically comprise Separation of Solid and Liquid, drying and packaging facilities, obtain the ammonium sulfate solids product, the water quality that contains of product is 0.5%, isolates remaining liquid behind the solid simultaneously, for containing the supersaturated solution of ammonium sulfate, be called mother liquor, be back to the bubbling segment (2) of desulfurizing tower (10) bottom,, and be recrystallised to solid ammonium sulfate further by the ammonium sulfate supersaturation that newly absorbs and oxidation obtains.
Desulfurization material, liquefied ammonia, the desulfurization material import from the tower body (1) of the bubbling segment (2) that is positioned at desulfurizing tower (10) bottom directly enters purified treatment tower (10), to guarantee and to absorb acidic gas in flue gas continuously, comprise oxysulfide, hydrogen halides, nitrogen oxide etc., especially SO
2, obtain corresponding ammonium salt at last.
Embodiment 2
The flue gas condition of this embodiment is as follows:
It is that a kind of flue gas contains SO
22000mg/Nm
3, SO
320mg/Nm
3, NOx 500mg/Nm
3, HCl and HF content 30mg/Nm
3, dust content 200mg/Nm
3Pollutant, and temperature is 145 ℃ the former flue gas of boiler, flue gas flow is 300,000 Nm
3/ h.
Referring to Fig. 1, its gas cleaning of adopting discharging integrated desulfurization tower is columnar tower, comprising:
Tower body (1), tower body (1) diameter is 6.6m;
Be arranged on the bubbling segment that is positioned at tower body (2) of tower body (1) bottom, be provided with one group of air bubbler in the bubbling segment (2) and two sides are advanced an agitator;
Be arranged on the gas approach (3) of tower body (1) middle part or middle and lower part, its flow area is a rectangle, high 2.0m, wide 5.0m;
Be arranged on the spray section that is positioned at tower body (4) of tower body (1) middle and upper part, spray section is provided with the sieve-board type gas distributor in (4), 2 groups of absorption liquid spray throwers and liquid wall stream baffle plate, and spray thrower is made of the person in charge, arm and nozzle, nozzle is a spiral nozzle, and every group of nozzle quantity is 40;
The packing section that is positioned at tower body (5) on tower body (1) top is set, two sections fillers are set in the packing section (5), all be furnished with water jet on every section filler;
Be arranged on the purification exhanst gas outlet (6) at tower body (1) top;
Be arranged on the upright chimney (7) that purifies on the exhanst gas outlet (6), the cross-sectional area of upright chimney (7) is circular, and to its exhaust outlet, cross-sectional area constantly reduces from its air inlet, is reduced to 0.125 times with the ratio of the cross-sectional area of spray section (4) from 0.25;
The height of in line chimney is 58 meters.
Referring to Fig. 2, the concrete technological design of tower top discharge type flue gas desulfurization method of the present invention is as follows:
Air blast (30) blasts the incorporate purified treatment tower of emission abatement (10) to flue gas from gas approach (3).Desulfurization material is a calcium carbonate, it is lime stone, the washing absorption liquid of circulation is calcium sulfate, the calcium sulfite of sulfur acid calcium crystallization (being gypsum) solid, the pulpous state aqueous mixtures of calcium chloride, and this circulating absorption solution also contains the flyash that washs from flue gas, and it contains solid masses is 18.0%.The washing absorption liquid under the effect of circulating pump (40), between the bubbling segment (2) of purified treatment tower (10), spray section (4), realize tower body (1) up and down, inside and outside two circulations of tower body (1).
Adopt two circulating pumps, the flow of circulating pump is 2000m
3/ h.
After flue gas enters the tower body (1) of purified treatment tower (10), the spray section (4) that is provided with in the tower of upwards flowing through.In spray section, two groups of cleaning solution spray throwers continue spray (all corresponding circulating pump separately of each group cleaning solution spray thrower, corresponding cleaning solution import separately), the SO in the flue gas
2Become ammonium sulfite.Flue gas is washed the absorption liquid cold shock, and temperature is reduced to 49 ℃.
In the spray section, the spray flux of each nozzle is 50m
3/ h.
After the flue gas upruss process spray section (4), continue upwards to enter packing section (5).Packing section (5) has two-layer filler, and all there is one group of water jet every layer of filler top.Under the continuous running status of flue gas purifying equipment, the water jet continuous service of lower floor's filler; During parking, the water jet of upper strata filler operation 2 minutes.The method of operation of water jet and the time liquid level with the bubbling segment (2) of tower bottom is that benchmark is regulated.When liquid level is lower than the setting liquid level, open water jet, both washed the demist packing layer, replenish fresh water (FW) to absorption tower (10) again.
Be called the purification flue gas through the flue gas after the packing section (5), directly enter atmosphere, 48 ℃ of delivery temperatures from upright chimney (7) by purifying exhanst gas outlet (6).
From the washing absorption liquid that spray section (4) is got off, directly enter the bubbling segment (2) that is positioned at purified treatment tower (10) bottom.In bubbling segment (2), air compressor machine (20) divides bubbler to blast oxidation air to absorption liquid by air, the calcium sulfite that spray section is obtained becomes calcium sulfate, and under the supersaturation situation, separate out gypsum crystal, the side that is arranged on bubbling segment (2) is advanced an agitator prolonged agitation, promote chemistry, the Physical Absorption effect of material in the flue gas, comprise promoting solution-air and solid-liquid to mix and mass transfer, also promote solid-liquid suspension.The gypsum solid product is sent into solid-liquid separating equipment (60) by discharge pump (50), obtain the gypsum solid product, the water quality that contains of product is 8.5%, isolate remaining liquid behind the solid simultaneously, for containing the supersaturated solution of gypsum, be called mother liquor, be back to the bubbling segment (2) of desulfurizing tower (10) bottom, the further gypsum supersaturation that is obtained by absorption and oxidation newly, and be recrystallised to the solid gypsum.
Desulfurization material, lime stone, the desulfurization material import from the tower body (1) of the bubbling segment (2) that is positioned at desulfurizing tower (10) bottom directly enters purified treatment tower (10), to guarantee and to absorb acidic gas in flue gas continuously, comprise oxysulfide, hydrogen halides, nitrogen oxide etc., especially SO
2, obtain corresponding calcium salt at last.
Claims (12)
1, a kind of tower top discharge type flue gas desulfurization method is characterized in that, former flue gas enters to be finished upright smoke evacuation that the purification flue gas that forms behind the desulfurizing and purifying connects from described desulfurization cat head and tin directly enter atmosphere in the desulfurization tower body.
2, tower top discharge type flue gas desulfurization method according to claim 1, it is characterized in that, described former flue gas by the air blast supercharging after, enter in the desulfurization tower body from the gas approach of described desulfurizing tower, and described gas approach be shaped as rectangle, other perhaps approximate rectangular shapes.
3, tower top discharge type flue gas desulfurization method according to claim 2 is characterized in that, described former flue gas enters in the described desulfurization tower body and flows to last, after process spray section desulfurizing and purifying and packing section are removed the liquid foam successively, enters upright smoke evacuation tube again.
4, tower top discharge type flue gas desulfurization method according to claim 3, it is characterized in that, be provided with at least one group of absorption liquid spray thrower in the described spray section, and each group of described cleaning solution spray thrower is all used a washing absorption liquid circulating pump separately, uses the import of a washing absorption liquid separately.
5, tower top discharge type flue gas desulfurization method according to claim 4 is characterized in that, described spray thrower comprises at least 7 nozzles, and being preferably with the spray section cross section serves as that 0.5-2.0 nozzle/m arranged on the basis
2, the hydrojet flow of described nozzle is 10～100m
3/ h is preferably 20～80m
3/ h.
6, tower top discharge type flue gas desulfurization method according to claim 3 is characterized in that, is provided with flue gas distributor in the described spray section, and described flue gas distributor is sieve plate or screen, and its percent opening is 10～50%, is preferably 20-30%.
7; according to each described tower top discharge type flue gas desulfurization method in the claim 3 to 6; it is characterized in that; the liquid that gets off from described spray section directly falls into the bubbling segment of described desulfurization tower body bottom; and at described bubbling segment; air compressor blasts oxidation air by the air bubbler that is arranged in the described bubbling segment to the washing absorption liquid; make sulphite be oxidized to sulfate; and separate out sulfate solid particle or crystal; the side that is arranged on described bubbling segment is advanced an agitator prolonged agitation; promote the mixing and the mass transfer of gas-liquid-solid three-phase slurries and prevent that solid is in bottom deposit.
8, tower top discharge type flue gas desulfurization method according to claim 7, it is characterized in that, use the absorption liquid circulating pump, extract absorption liquid from the washing absorption liquid outlet that described bubbling segment tower body is provided with, be transported to the washing absorption liquid import that is arranged on described spray section, and described circulating pump feed flow is at 500-5000m
3Between/the h.
9, according to claim 7 or 8 described tower top discharge type flue gas desulfurization methods, it is characterized in that, use discharge pump, the discharge gate that is provided with from described bubbling segment tower body extracts absorption liquid, be transported to the external solid-liquid separation equipment of desulfurizing tower, obtain the sulfate solid product, the remaining liq of separation is got back to bubbling segment from the phegma import that described bubbling segment tower body is provided with.
10, according to each described tower top discharge type flue gas desulfurization method of claim 1 to 9, it is characterized in that, the desulfurization material that uses is carbonate, oxide or the hydroxide of calcium, circulating absorption solution is a kind of sulfate, sulphite, halid pulpous state aqueous mixtures that contains calcium, and contain solid masses 3-30% in the described pulpous state aqueous mixtures, be preferably 10-20%, desulfurization product is two water crystallization gypsum, and described gypsum contain water quality between 2.0-20.0%.
11, according to each described tower top discharge type flue gas desulfurization method of claim 1 to 9, it is characterized in that, the desulfurization material that uses is liquid ammonia, gaseous ammonia, ammonia water mixture or carbon ammonium, circulating absorption solution is a kind of sulfate, sulphite, halid pulpous state aqueous mixtures that contains ammonium, and contain solid masses 3-30% in the described pulpous state aqueous mixtures, be preferably 10-20%, desulfurization product is the crystalline sulfuric acid ammonium, and described ammonium sulfate contain water quality between 0.5-5.0%.
12, according to each described tower top discharge type flue gas desulfurization method of claim 1 to 11, it is characterized in that, purify the temperature of flue gas in described upright chimney between 40-60 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100335974A CN101306317A (en) | 2008-02-14 | 2008-02-14 | Tower top discharge type flue gas desulfurization method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100335974A CN101306317A (en) | 2008-02-14 | 2008-02-14 | Tower top discharge type flue gas desulfurization method |
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ID=40123128
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|---|---|---|---|
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101799245A (en) * | 2010-04-02 | 2010-08-11 | 华电重工装备有限公司 | Method and device for realizing waste-steam cooling, desulphurization and smoke removal of power stations through one tower |
| CN102836626A (en) * | 2011-06-26 | 2012-12-26 | 吴火成 | Multifunctional chimney tower |
| CN104607327A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司大连石油化工研究院 | Liquid-phase nozzle and smoke desulfurizing absorption tower with nozzle |
| CN104645817A (en) * | 2015-02-13 | 2015-05-27 | 上海电气电站环保工程有限公司 | Single-tower multi-pH-value graded spraying control desulfurization system and process |
| CN106823753A (en) * | 2017-03-30 | 2017-06-13 | 贵州诺威施生物工程有限公司 | Desulfurizing tower and desulfurization recovery system |
| CN110156134A (en) * | 2018-03-27 | 2019-08-23 | 新疆环境工程技术有限责任公司 | A kind of catalytic ozonation tower sewage treatment equipment |
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| CN112191046A (en) * | 2020-09-27 | 2021-01-08 | 成都国化环保科技有限公司 | Acidolysis tail gas desulfurization system and method |
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| CN101799245A (en) * | 2010-04-02 | 2010-08-11 | 华电重工装备有限公司 | Method and device for realizing waste-steam cooling, desulphurization and smoke removal of power stations through one tower |
| CN102836626A (en) * | 2011-06-26 | 2012-12-26 | 吴火成 | Multifunctional chimney tower |
| CN104607327A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司大连石油化工研究院 | Liquid-phase nozzle and smoke desulfurizing absorption tower with nozzle |
| CN104645817A (en) * | 2015-02-13 | 2015-05-27 | 上海电气电站环保工程有限公司 | Single-tower multi-pH-value graded spraying control desulfurization system and process |
| CN104645817B (en) * | 2015-02-13 | 2017-12-19 | 上海电气电站环保工程有限公司 | The more pH classified sprayings control desulphurization systems of single column and technique |
| CN106823753A (en) * | 2017-03-30 | 2017-06-13 | 贵州诺威施生物工程有限公司 | Desulfurizing tower and desulfurization recovery system |
| CN110156134A (en) * | 2018-03-27 | 2019-08-23 | 新疆环境工程技术有限责任公司 | A kind of catalytic ozonation tower sewage treatment equipment |
| CN110252106A (en) * | 2019-05-17 | 2019-09-20 | 中国石油化工股份有限公司 | It is a kind of for diluting in comprehensive tower the spraying method and spray system of acid lime set |
| CN112191046A (en) * | 2020-09-27 | 2021-01-08 | 成都国化环保科技有限公司 | Acidolysis tail gas desulfurization system and method |
| CN112191046B (en) * | 2020-09-27 | 2022-04-22 | 成都国化环保科技有限公司 | Acidolysis tail gas desulfurization system and method |
| CN112473288A (en) * | 2020-11-25 | 2021-03-12 | 赛得利(九江)纤维有限公司 | Acid bath washing dust removal device and method |
| CN114602306A (en) * | 2022-03-22 | 2022-06-10 | 常熟宏智仓储有限公司 | Sulfur-containing waste gas treatment system |
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Open date: 20081119 |