CN110465175A - Flue-gas dust-removing and desulfurization tower and flue gas ash removal, desulfurization and wastewater treatment method - Google Patents
Flue-gas dust-removing and desulfurization tower and flue gas ash removal, desulfurization and wastewater treatment method Download PDFInfo
- Publication number
- CN110465175A CN110465175A CN201810440425.2A CN201810440425A CN110465175A CN 110465175 A CN110465175 A CN 110465175A CN 201810440425 A CN201810440425 A CN 201810440425A CN 110465175 A CN110465175 A CN 110465175A
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- Prior art keywords
- flue gas
- area
- zone
- oxidizing
- gas
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 264
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 259
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 109
- 230000023556 desulfurization Effects 0.000 title claims abstract description 103
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 194
- 230000001590 oxidative effect Effects 0.000 claims abstract description 116
- 230000003311 flocculating effect Effects 0.000 claims abstract description 79
- 238000004140 cleaning Methods 0.000 claims abstract description 71
- 238000005192 partition Methods 0.000 claims abstract description 63
- 238000005507 spraying Methods 0.000 claims abstract description 48
- 239000003595 mist Substances 0.000 claims abstract description 45
- 238000009826 distribution Methods 0.000 claims abstract description 16
- 239000002002 slurry Substances 0.000 claims description 72
- 239000007789 gas Substances 0.000 claims description 60
- 239000000428 dust Substances 0.000 claims description 59
- 238000000034 method Methods 0.000 claims description 49
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 38
- 239000012670 alkaline solution Substances 0.000 claims description 32
- 239000007921 spray Substances 0.000 claims description 32
- 239000002245 particle Substances 0.000 claims description 26
- 239000002351 wastewater Substances 0.000 claims description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 235000019504 cigarettes Nutrition 0.000 claims description 17
- 230000000694 effects Effects 0.000 claims description 15
- 239000013505 freshwater Substances 0.000 claims description 15
- 239000000243 solution Substances 0.000 claims description 14
- 230000003009 desulfurizing effect Effects 0.000 claims description 13
- 230000003647 oxidation Effects 0.000 claims description 12
- 238000007254 oxidation reaction Methods 0.000 claims description 12
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 11
- 238000005189 flocculation Methods 0.000 claims description 11
- 230000016615 flocculation Effects 0.000 claims description 11
- 230000001105 regulatory effect Effects 0.000 claims description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 8
- 239000005864 Sulphur Substances 0.000 claims description 8
- 238000012545 processing Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 6
- 230000002411 adverse Effects 0.000 claims description 6
- 239000004411 aluminium Substances 0.000 claims description 6
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 6
- 238000004523 catalytic cracking Methods 0.000 claims description 6
- 239000003517 fume Substances 0.000 claims description 6
- 239000000779 smoke Substances 0.000 claims description 6
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 6
- 239000000835 fiber Substances 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 239000003245 coal Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 229920000642 polymer Polymers 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 3
- 239000003365 glass fiber Substances 0.000 claims description 3
- -1 hydrogen Calcium oxide Chemical class 0.000 claims description 3
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 229910021420 polycrystalline silicon Inorganic materials 0.000 claims description 3
- 229920005591 polysilicon Polymers 0.000 claims description 3
- 235000010265 sodium sulphite Nutrition 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 claims description 3
- 239000012209 synthetic fiber Substances 0.000 claims description 3
- 229920002994 synthetic fiber Polymers 0.000 claims description 3
- 238000010257 thawing Methods 0.000 claims description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 2
- 235000019738 Limestone Nutrition 0.000 claims description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 2
- 229910019142 PO4 Inorganic materials 0.000 claims description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 2
- PZIBOVBPVADPBS-UHFFFAOYSA-J S(=O)(=O)([O-])[O-].[Si+4].S(=O)(=O)([O-])[O-] Chemical compound S(=O)(=O)([O-])[O-].[Si+4].S(=O)(=O)([O-])[O-] PZIBOVBPVADPBS-UHFFFAOYSA-J 0.000 claims description 2
- 229910000831 Steel Inorganic materials 0.000 claims description 2
- SZUMNSLVXYNSKK-UHFFFAOYSA-L [Fe](Cl)Cl.[P] Chemical compound [Fe](Cl)Cl.[P] SZUMNSLVXYNSKK-UHFFFAOYSA-L 0.000 claims description 2
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 2
- ZEMWIYASLJTEHQ-UHFFFAOYSA-J aluminum;sodium;disulfate;dodecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.[Na+].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZEMWIYASLJTEHQ-UHFFFAOYSA-J 0.000 claims description 2
- 239000000908 ammonium hydroxide Substances 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 239000000701 coagulant Substances 0.000 claims description 2
- 238000004939 coking Methods 0.000 claims description 2
- 229920001577 copolymer Polymers 0.000 claims description 2
- 238000011010 flushing procedure Methods 0.000 claims description 2
- 239000002737 fuel gas Substances 0.000 claims description 2
- 229910000358 iron sulfate Inorganic materials 0.000 claims description 2
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 claims description 2
- 239000006028 limestone Substances 0.000 claims description 2
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 2
- 239000000347 magnesium hydroxide Substances 0.000 claims description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 2
- 239000010452 phosphate Substances 0.000 claims description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 2
- 239000011574 phosphorus Substances 0.000 claims description 2
- 229910052698 phosphorus Inorganic materials 0.000 claims description 2
- 229920002401 polyacrylamide Polymers 0.000 claims description 2
- 239000011148 porous material Substances 0.000 claims description 2
- 239000013535 sea water Substances 0.000 claims description 2
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 claims description 2
- 238000005245 sintering Methods 0.000 claims description 2
- 229910001388 sodium aluminate Inorganic materials 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 239000001509 sodium citrate Substances 0.000 claims description 2
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 claims description 2
- 239000010959 steel Substances 0.000 claims description 2
- 239000000292 calcium oxide Substances 0.000 claims 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims 1
- 238000002485 combustion reaction Methods 0.000 claims 1
- 239000011790 ferrous sulphate Substances 0.000 claims 1
- 235000003891 ferrous sulphate Nutrition 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims 1
- 238000006116 polymerization reaction Methods 0.000 claims 1
- 238000005406 washing Methods 0.000 claims 1
- 238000010276 construction Methods 0.000 abstract description 7
- 230000002829 reductive effect Effects 0.000 abstract description 5
- 230000009466 transformation Effects 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 9
- 229910052751 metal Inorganic materials 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- 230000002441 reversible effect Effects 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 4
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- 239000003344 environmental pollutant Substances 0.000 description 3
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- 231100000719 pollutant Toxicity 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 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 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 108010081750 Reticulin Proteins 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
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- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- GRNVJAJGRSXFFZ-UHFFFAOYSA-N sulfurous acid;hydrate Chemical compound O.OS(O)=O GRNVJAJGRSXFFZ-UHFFFAOYSA-N 0.000 description 2
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- WWILHZQYNPQALT-UHFFFAOYSA-N 2-methyl-2-morpholin-4-ylpropanal Chemical compound O=CC(C)(C)N1CCOCC1 WWILHZQYNPQALT-UHFFFAOYSA-N 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
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- 239000012530 fluid Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- 235000012245 magnesium oxide Nutrition 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- JESHZQPNPCJVNG-UHFFFAOYSA-L magnesium;sulfite Chemical compound [Mg+2].[O-]S([O-])=O JESHZQPNPCJVNG-UHFFFAOYSA-L 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
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- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- 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
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- C—CHEMISTRY; METALLURGY
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Abstract
The invention discloses a kind of flue-gas dust-removing and desulfurization tower and flue gas ash removals, desulfurization and wastewater treatment method.A kind of flue-gas dust-removing and desulfurization tower is from top to bottom followed successively by flue gas emission area, mist eliminating zone, tower tray area, spraying zone and wastewater treatment area；The wastewater treatment area is oxidizing, flocculating area and circulation cleaning liquid zone by one piece of vertical clapboard I points, passes through partition II at the top of circulation cleaning liquid zone circulation cleaning liquid zone and oxidizing, flocculating area and spraying zone is completely separated；Filter medium is arranged in the vertical clapboard I；The flue gas pipeline II is extended to inside oxidizing, flocculating area, the successively horizontal distribution several groups flue gas branch pipe from bottom to top of the flue gas pipeline II inside oxidizing, flocculating area.The present invention carries out flue gas ash removal, desulfurization and wastewater treatment in a tower, and occupied area is greatly reduced, expense and device operating cost needed for reducing plant construction, transformation.
Description
Technical field
The invention belongs to industrial waste gas purifying field, it is related to a kind of flue-gas dust-removing and desulfurization tower and flue gas ash removal, desulfurization and useless
Method for treating water.
Background technique
Contain sulfur dioxide and dust in the flue gas of boiler smoke and plant emissions, sulfur dioxide and dust are atmosphere dirts
The main composition dust of object is contaminated, sulfur dioxide is the main reason for forming acid rain, and the lesser dust of partial size is the haze to be formed crime
One of stalwart chief culprit.
Environmental pollution is got worse, and haze event takes place frequently, and country is also higher and higher to the attention degree of environmental protection, is gone out in recent years
A series of platform laws and regulations, national standard, the management method of environmental protections.GB 13223-2011 " thermal power plant's atmosphere pollution
Object discharge standard " regulation: fire coal boiler fume dust ≯ 30mg/Nm3, the SO of new construction of coal-fired boiler flue gas2≯100mg/Nm3；Weight
The regional fire coal boiler fume dust ≯ 20mg/Nm of point3, SO2≯50mg/Nm3." implement in full coal-burning power plant's minimum discharge and section
Energy retrofit work scheme " (ring sends out [2015] No. 164) middle regulation coal-fired plant flue gas minimum discharge index are as follows: exhaust gas dust ≯
10mg/Nm3, SO2≯35mg/Nm3.GB 31570-2015 " petroleum refining industry pollutant emission standard " regulation: catalytic cracking
Catalyst regeneration flue gas particles ≯ 50mg/Nm3, SO2≯100mg/Nm3；Key area particulate matter ≯ 30mg/Nm3, SO2≯
50mg/Nm3。
Wet desulphurization is high with desulfurization degree, device is reliable for operation, simple operation and other advantages, thus the existing cigarette in countries in the world
Desulfurization technology is mainly based on wet desulphurization.Traditional Wet Flue Gas Desulfurization Technique mainly has limestone-gypsum method, Dual alkali de-
Sulphur, sodium alkali desulfurization, ammonia process of desulfurization method etc..Above-mentioned flue gas desulfurization technique mainly uses countercurrent spray, and alkaline slurry is from desulfurizing tower
Top is sprayed, and free settling is contacted with flue gas adverse current under the effect of gravity realizes desulphurization reaction, but the liquid due to spraying out
Drop diameter is relatively large, and the contact area very little of single drop and flue gas needs to improve serum recycle to improve desulfuration efficiency
The number of spray, makes drop repeatedly and smoke contacts are to improve drop to the assimilation effect of sulfur dioxide, thus tower bottom slurries follow
The flow of ring pump is very big, and power of motor is also very big, and the power consumption of slurry circulating pump is very big, and operating cost is higher.
The partial size of dust is smaller in flue gas, and most of between 0.1 ~ 200 μm, flue gas ash removal technology is mainly cloth bag at present
Formula dedusting technology, electrostatic precipitator technology, wet dust collection technology.Due to containing moisture in flue gas, dust is in fiber bag precipitator
Moisture absorption is cohered on filter bag, blocks the hole of filter bag, thus needs that frequently filter bag is cleared up or replaced, and fiber bag precipitator is answered
With being extremely limited；The major defect of electrostatic precipitator is that cost is higher, and installation, maintenance, management require strictly, to need height
Buckling electricity and commutation control equipment, power consumption is higher, and occupied area is larger；Wet dust collection technology mainly passes through shower water and removes cigarette
The dust carried in gas, the lesser drop of partial size in conjunction with dust after still can with flue gas be discharged chimney.
At desulfurization wastewater disclosed in CN201110153423.3, CN201310338193.7, CN201310421183.X
Science and engineering skill is provided with flocculation basin and oxidation tank, and flocculation basin and oxidation tank are both needed to setting blender, and slurries need to pass through machine
Pump conveying.Dust-removal and desulfurizing waste water treatment process disclosed in CN201310338193.7, CN201310421183.X uses spinning liquid
Separator is separated by solid-liquid separation.Above-mentioned FGD Wastewater Treatment Process is longer, and equipment is more, and energy consumption is also larger.
Since the disposal of pollutants index that country formulates is increasingly stringenter, possesses the enterprise of boiler and possess the work of flue gas emission
Factory need to be transformed to meet flue gas qualified discharge to newly-increased flue-gas dust-removing and desulfurization device or to old device.Due to most of boiler
It is built with smoke discharging device according to pervious old plant, is not considered that flue gas needs further depth dedusting de- in construction
Sulphur, thus enough construction lands are not reserved to flue-gas dust-removing and desulfurization transformation in construction, it is both needed in existing limited region
Interior newly-built flue-gas dust-removing and desulfurization device is transformed old device.Above-mentioned Wet Flue Gas Desulfurization Technique is useless comprising flue gas desulfurization, desulfurization
Water oxidation processes or regeneration unit, process is longer, and equipment is more, and occupied area is larger, seriously restricts dust-removing desulfurating apparatus
Construction and upgrading, partial devices and boiler in default of enough spaces can not upgrading, lead to flue gas emission index
Existing national standards are unable to satisfy to be forced to stop work or demolish to rebuild.Thus, it would be highly desirable to development process is short, equipment is few, occupied area is few
Flue gas desulfurization technique.
Large-scale promotion application with wet type desulfurizing technology in China, one of wet type desulfurizing technology obvious and be difficult to gram
The shortcomings that taking gradually reveals, which is exactly to discharge flue gas to generate " white cigarette " phenomenon in throat, or even will form number
" the white cigarette long queue " of kilometer, strong visual impact is brought to people, ground there is also " dust-shower " phenomenon sometimes.So how
It is a problem urgently to be resolved at present that " white cigarette " phenomenon, which can be eliminated,.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of flue-gas dust-removing and desulfurization tower and flue gas ash removal, desulfurization and waste water
Processing method, flue-gas dust-removing and desulfurization tower of the invention integrate flue gas ash removal, desulfurization and wastewater treatment, the method for the present invention process
It is short, equipment is few, occupied area is few, and " white cigarette " phenomenon after flue gas emission can be greatly decreased, before wide application
Scape.
Flue-gas dust-removing and desulfurization tower of the invention is from top to bottom followed successively by flue gas emission area, mist eliminating zone, tower tray area, spraying zone
With wastewater treatment area；The wastewater treatment area center is oxidizing, flocculating area and circulating clear liquid by one piece of vertical partition I points
Area, wherein oxidizing, flocculating area is connected to spraying zone, passes through partition II at the top of circulation cleaning liquid zone for circulation cleaning liquid zone and oxidizing, flocculating
Area and spraying zone are completely separated；At least one opening, preferably 1 ~ 20, more preferably 1 ~ 4, opening is arranged in the partition I
Area is the 10% ~ 90% of partition I area, preferably 50% ~ 70%；Filter medium is fixed in the opening of partition I.
The filter medium is natural fiber, synthetic fibers, glass fiber, reticular structure made of wire, and mesh is big
Small is 0.1 ~ 1000 μm, preferably 5 ~ 100 μm.
The both ends partition II are connect with partition I and circulation cleaning liquid zone tower wall respectively, partition I and the junction partition II
Angle is generally 45 ~ 165 °, preferably 120 ~ 150 °.It is sealed between the partition I and partition II and tower wall, avoids demarcation plate
The air-liquid short circuit of two sides.
The flue gas emission area preferably passes through cone-shaped variable diameter with mist eliminating zone and is connected, the mist eliminating zone and flue gas emission
The tower diameter ratio in area is 1.2 ~ 5；Tower tray area preferably passes through reverse taper deformation diameter with spraying zone and is connected, and is wastewater treatment below spraying zone
Area；The tower diameter ratio in the tower tray area and spraying zone is 1.2 ~ 3.
The flue gas emission area is generally the chimney structure in conventional flue gas wet desulphurization process, the chimney bottom
Portion is connected with mist eliminating zone tower body, is preferably connected by cone-shaped variable diameter with mist eliminating zone tower body, and exhanst gas outlet is arranged in chimney top；It is excellent
It is selected in chimney top setting outer sleeve, the outer sleeve, which is the tubular structure of upper and lower opening, to be cylindric or cone cylinder shape,
Along chimney top certain distance, generally 0.2~10m, preferably 0.5~5m is higher by outer sleeve, the lower edge of outer sleeve is lower than
The upper edge of chimney, preferably shorter than along 0.5 ~ 5m on chimney；It is annular space between the outer sleeve and chimney, preferably bottom is opened
Mouth diameter is 1.01~1.2 times of chimney top opening diameter.The flue gas enters outer sleeve from chimney top, from outer sleeve
Top discharge, the gas velocity of flue gas is higher, can generate negative pressure between chimney and outer sleeve when flowing through outer sleeve, air is in negative pressure
Suction under flow through between chimney and outer sleeve annular space enter outer sleeve top, air is in outer sleeve and flue gas
Together from outer sleeve top discharge after mixing, flue gas has just mixed well with air before leaving outer sleeve top discharge, greatly
Width reduces " white cigarette " production quantity.
Defogging equipment is arranged in the mist eliminating zone, and for removing the drop of flue gas carrying, the defogging equipment can be
One or more of vortex-flow and defrosting device, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister etc..
One or more layers settable tower tray of the tower tray area, preferably the tower tray number of plies are 2 ~ 6 layers；The tower tray can be one
The tower tray or multiple types of seed type combine tower tray, including float valve tray, screen hole type tower tray, guiding screen hole type tower tray, Gu Sheta
Disk, directional float tray or combined trapezoid spray tray etc. come into full contact with the deep desulfuration strengthened mass transfer and realize flue gas for gas-liquid, by flue gas
In 0.1 μm ~ 5 μm between tiny dust particles capture the depth dedusting for realizing flue gas, and flue gas carried a large amount of
Mist droplet captures the segregational load for reducing mist eliminating zone.
Liquid distribution trough is set between the tower tray area and mist eliminating zone, and liquid distribution trough connects circulating clear liquid pipeline I, uses
It is evenly dispersed on tower tray in by circulating clear liquid.
The spraying zone top is arranged one or more layers spray pipe, when Multi-layer sprinkling pipeline is set, spray pipe it
Between distance be 0.5 ~ 5m, preferred distance be 1 ~ 2.5m；The spray pipe connects circulating clear liquid pipeline II, on spray pipe
It is provided with multiple atomizers；For circulating clear liquid to be atomized, the droplet after atomization connects the spraying zone with flue gas adverse current
Touching removes the dust and sulfur dioxide carried in flue gas；Smoke inlet I is arranged in the spraying zone lower part, for connecting flue gas
Pipeline I.
The oxidizing, flocculating area is separately connected alkaline solution line I, flocculant line and liquidometer close to tower wall side
I；Flow control valve is set on the alkaline solution line I, adjusts its pH value for filling alkaline solution into desulfurization wastewater；
The flocculant line makes the little particle dust cohesion in desulfurization wastewater at big for filling flocculant into desulfurization wastewater
Grain.
The oxidizing, flocculating area bottom connection flue gas pipeline II and outlet slurry line；The flue gas pipeline II extends
To inside oxidizing, flocculating area and being parallel to partition I, the successively horizontal distribution from bottom to top of the flue gas pipeline II inside oxidizing, flocculating area
Several groups flue gas branch pipe, preferably 2 ~ 4 groups, flue gas branch pipe is connected to flue gas pipeline II；Every group of flue gas branch pipe is by 2 ~ 8 cigarettes
Gas branch pipe composition, flue gas branch pipe be it is arc-shaped, every group of flue gas branch pipe is uniformly distributed in the horizontal direction and rotation direction is identical；Flue gas from
The direction that flue gas branch pipe sprays is the tangential direction of circular arc, and flue gas high speed ejection pushes slurries rotation, for oxidizing, flocculating area
Slurries be stirred, be uniformly mixed material in oxidizing, flocculating area, and dust particles on filter medium are rinsed；Institute
The outlet slurry line stated is used to drain into subsequent processing units outside the slurries after oxidizing, flocculating, and stream is arranged in outlet slurry line
Adjustable valve and pH meter；The flow control valve is according to the flows of the liquidometer I Signal Regulation outlet slurries fed back, for controlling
The liquid level of system liquefaction flocculation zone；The pH meter is used to measure the pH value of outlet slurries, and signal via controller is fed back to alkali
Flow control valve on property solution pipeline I.
The circulation cleaning liquid zone is connected with fresh water pipeline, alkaline solution line II, oxidisability gas close to tower wall side
Fluid line and liquidometer II；Flow control valve is set on the fresh water pipeline, the Signal Regulation fed back according to liquidometer II
The flow of fresh water, the liquid level for control loop clear liquid area；It is provided with flow control valve on the alkaline solution line II,
For adjusting the flow of the alkaline solution filled to circulation cleaning liquid zone；The oxidizing gas pipeline is connected with blower, and prolongs
The side partition I for reaching circulation cleaning liquid zone, is connected with oxidizing gas distributor pipe；It is arranged on the oxidizing gas distributor pipe
There are several nozzles, nozzle faces the filter medium on partition I, and oxidizing gas sprays from nozzle and pass through filter medium, will
Dust particles on oxidizing, flocculating area filter medium are blown afloat, and the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, powder
Dirt and flocculant effect coacervating large particle are under the effect of gravity to oxidizing, flocculating area bottom deposit, into the oxygen in oxidizing, flocculating area
Sulfite oxidation in slurries is sulfate by the property changed gas, keeps the COD of desulfurization wastewater up to standard.
Blow vent is set on the circulation cleaning liquid zone top drum wall, for guaranteeing that circulation cleaning liquid zone pressure is steady, is avoided
Pressure oscillation is excessive to damage filter medium.
The circulation cleaning liquid zone bottom connection clear liquid draws pipeline, draws pipeline and is divided into two-way, pipeline connection is outer all the way
Liquid pipe line is cleared, another way pipeline connects circulation cleaning liquid pump, is provided with pH meter on the pipeline, circulation cleaning liquid pump is connected through cooler
Circulating clear liquid pipeline I and circulating clear liquid pipeline II；The pH meter is used to measure the pH value of circulating clear liquid, and measuring signal is passed through
Controller feeds back to the regulating valve of alkaline solution line II.
The method of flue gas ash removal of the invention, desulfurization and wastewater treatment, including following content:
(1) flue gas divides two-way to enter flue-gas dust-removing and desulfurization tower, all the way through flue gas pipeline I under the spraying zone of flue-gas dust-removing and desulfurization tower
Portion enters, and another way enters through oxidizing, flocculating area from the oxidizing, flocculating area bottom of flue-gas dust-removing and desulfurization tower through flue gas pipeline II
Interior slurries, two-way flue gas converge afterwards with most of dust for carrying in the circulating clear liquid counter current contacting of spraying zone removing flue gas and
Sulfur dioxide enters tower tray area across the flue gas of spraying zone, depth dust-removal and desulfurizing is carried out in tower tray area and circulating clear liquid, after purification
Flue gas after mist eliminating zone demisting enter flue gas emission area, enter after outer sleeve mixes well with air from chimney top from cigarette
Gas discharge region top discharge；
(2) desulfurization slurry for absorbing dust and sulfur dioxide enters oxidizing, flocculating area, in the flue gas entered through flue gas pipeline II
Stirring action under be sufficiently mixed with oxidizing gas, flocculant and alkaline solution, the sulphite in desulfurization slurry is oxidized
For sulfate, the little particle dust in desulfurization slurry flocculates into bulky grain, while there is the flue gas of certain temperature to make desulfurization slurry
In moisture constantly volatilize, salinity gradually increases；
(3) for desulfurization slurry under the action of partition I two sides liquid level difference, the filter medium flowed through on partition I realizes separation of solid and liquid, takes off
Dust particles in sulphur slurries, which are filtered, stays in oxidizing, flocculating area, and clear liquid enters circulation cleaning liquid zone, the slurry after oxidizing, flocculating
Liquid is drawn from oxidizing, flocculating area bottom enters subsequent processing units through outlet pipeline；
(4) oxidizing gas enters from circulation cleaning liquid zone, and filter medium is sprayed and passed through from the nozzle of oxidizing gas distributor pipe,
Dust particles on oxidizing, flocculating area filter medium are blown afloat, the slurries that the dust and oxidizing gas blown afloat is rotated are taken away,
Dust and flocculant effect coacervating large particle are under the effect of gravity to oxidizing, flocculating area bottom deposit, into oxidizing, flocculating area
Sulfite oxidation in slurries is sulfate by oxidizing gas, keeps the COD of desulfurization wastewater up to standard；
(5) clear liquid after filter media into circulating clear liquid area is mixed with fresh water and alkaline solution in circulation cleaning liquid zone
It is drawn afterwards from circulation cleaning liquid zone bottom, a small amount of direct outlet of clear liquid is to reduce the salinity of circulating clear liquid, remaining clear liquid is through recycling
Enter cooler after clear liquid pump pressurization, enters spraying zone through cooler clear liquid a part after cooling, after atomizer is atomized
It is contacted with flue gas adverse current and desulfurization is dusted to flue gas, another part clear liquid flows through liquid distribution trough and enters tower tray area, in tower tray
It is upper to come into full contact with the deep desulfuration for strengthening mass transfer effect realization flue gas with flue gas, and will be micro- between 0.1 μm in flue gas ~ 5 μm
Small dust particle capture is got off, and realizes the depth dedusting of flue gas, flue gas by a large amount of mist droplets entrained by spraying zone also by
Clear liquid on tower tray captures, and reduces the segregational load of mist eliminating zone.
In the method for the present invention, flue gas described in step (1) is that fire coal boiler fume, coal-fired plant flue gas, catalytic cracking are urged
Agent regenerated flue gas, Furnace flue gas, coking flue gas or steel sintering flue gas etc..The flue gas pipeline I and fume pipe
The ratio that line II enters the amount of flue gas is 20 ~ 500；Circulating clear liquid and the ratio of flue gas are 5 ~ 50L/Nm in spraying zone3, preferably compare
Example is 8 ~ 25L/Nm3, 3 ~ 15L/Nm of ratio of circulating clear liquid and flue gas in tower tray area3。
In the method for the present invention, alkaline solution described in step (2) and (5) be selected from sodium hydroxide solution, calcium hydroxide solution,
In magnesium hydroxide solution, sodium carbonate liquor, sodium sulfite solution, sodium citrate solution, lime stone slurry, ammonium hydroxide or seawater etc.
It is one or more of.
In the method for the present invention, oxidizing gas described in step (2) and (4) be one of air, oxygen, ozone etc. or
Several, preferably oxidizing gas is air.
In the method for the present invention, oxidizing gas flowrate described in step (2) and (4) is according to the slurries chemistry after flocculation concentration
Oxygen demand (COD) is adjusted, and COD Con trolling index is ≯ 60mg/L.
In the method for the present invention, flocculant described in step (2) and (4) is aluminum sulfate, alum, sodium aluminate, ferric trichloride, sulphur
Sour ferrous iron, ferric sulfate, aluminium polychloride, polyaluminium sulfate, polymer phosphate aluminium, poly-ferric chloride, bodied ferric sulfate, polymer phosphate
Iron, poly- phosphorus iron chloride, poly- phosphorus aluminium chloride, ferric-polysilicate, poly-silicic acid iron sulfate, polysilicate sulfuric acid aluminium, polyaluminum sulfate ferric-aluminum chloride,
It polymerize one of Polyferric Sulfate silicon flocculant, Al-fe Co Polymer Inorganic Coagulant, polysilicon acid flocculant, polyacrylamide flocculant etc.
Or it is several, the additional amount of flocculant is 0.05 ~ 2kg/m3。
In the method for the present invention, the slurry pH value after oxidizing, flocculating described in step (3) is controlled in 7 ~ 9, pH on-line detector
On slurries outlet pipeline, the pH value of desulfurization slurry is controlled by adjusting the regulating valve on alkaline solution line I.
In the method for the present invention, the liquid level difference of the two sides partition I described in step (3) is 0.5 ~ 6m, and oxidizing, flocculating area
Liquid level is higher than the liquid level of circulation cleaning liquid zone.
In the method for the present invention, oxidizing, flocculating area liquid level described in step (3) is by the regulating valve in outlet slurry line
It is controlled.
In the method for the present invention, circulation cleaning liquid zone liquid level described in step (3) by the regulating valve on fresh water pipeline into
Row control.
In the method for the present invention, the control of circulation cleaning liquid zone pH value described in step (3) ~ (5) is 6 ~ 11, the control of preferable ph
Range is that 7 ~ 8, pH on-line detector is located on tower bottom pump entry pipeline, by adjusting the adjusting on alkaline solution line II
Valve carrys out the pH value of control loop clear liquid.
In the method for the present invention, outlet clear liquid described in outlet slurries described in step (3) and step (5) enters subsequent processing
Unit, can be used for preparing or producing gypsum, sodium sulfite, sodium hydrogensulfite, magnesium sulfite, magnesium sulfate, magnesia, sodium sulphate,
The products such as ammonium sulfate, ammonium hydrogen sulfate may also pass through qualified discharge after filter.
Compared with the prior art, the advantages of the present invention are as follows:
1, wastewater treatment area is arranged in flue-gas dust-removing and desulfurization tower lower part in the present invention, and wastewater treatment is divided into oxygen by two pieces of partitions
Change flocculation zone and circulation cleaning liquid zone, realizes the oxidation, flocculation and concentration of desulfurization wastewater in oxidizing, flocculating area；In wastewater treatment area
Filter medium is set on the vertical clapboard of centre, realizes desulfurization slurry as motive force using the liquid level difference of vertical clapboard two sides
Filter operation.Circulatory mediator of the circulating clear liquid being obtained by filtration as dust-removal and desulfurizing, due in circulating clear liquid do not contain dust or
Dust content is very low, uses the slurries containing dust as the circulatory mediator of dust-removal and desulfurizing compared to existing dust-removal and desulfurizing technology, should
Method high dust collection efficiency.Inlet flue gas is divided into two-way by the present invention, wherein by oxidizing, flocculating area bottom enter high-temperature flue gas from
Arc-shaped flue gas branch pipe sprays along a tangential direction, pushes the rotation of dust-removal and desulfurizing waste liquid, keeps the material in oxidizing, flocculating area sufficiently mixed
Splice grafting touching is conducive to the progress of oxidizing, flocculating reaction, and the dust and sulfur-containing oxide in flue gas also obtain certain absorption, simultaneously
Also high-temperature flue gas waste heat is taken full advantage of, vaporizes the moisture in dust-removal and desulfurizing waste water largely, is realized in oxidizing, flocculating area de-
The preliminary concentrate of sulphur waste water, reduces the energy consumption of subsequent cell.Meanwhile oxidizing gas of the invention not directly enters oxidation wadding
Coagulation zone, but introduced from circulation cleaning liquid zone, filter medium is rinsed using oxidizing gas, eliminates flushing device.This
Invention eliminates conventional mixing plant and filter plant, and wastewater treatment process can be greatly reduced without expending the additional energy
Plant investment and operating cost.
2, reverse taper deformation diameter is arranged in the present invention between tower tray area and spraying zone, advantageously reduces tower tray area gas velocity, by force
Change gas-liquid mass transfer effect, improves flue gas in the efficiency of dust collection and desulfuration efficiency in tower tray area, entrainment is reduced, to reduce mist eliminating zone
Load；Cone-shaped variable diameter is arranged in flue gas emission area and mist eliminating zone, is conducive to the flow velocity for improving flue gas, and the gas velocity of flue gas is bigger,
It is higher that flue gas leaves the rising height behind flue gas emission area, is more conducive to the diffusion of flue gas, thus plume is shorter.
3, fuel gas desulfurization gas wash tower flue gas emission area of the invention is using the structure of " chimney+outer sleeve ", and flue gas is by removing
It generates negative pressure after the acceleration of fog-zone and cone-shaped variable diameter, when flue gas flows through outer sleeve to suck outside air, flue gas and air exist
From outer sleeve top discharge after being sufficiently mixed in outer sleeve, " white cigarette " production quantity is significantly reduced.
4, the present invention completes flue gas ash removal, flue gas desulfurization and wastewater treatment in a tower, realizes flue gas depth and removes
Dirt, desulfurization and waste water COD qualified discharge triple functions, each functional area coordinated, process flow is short, and land occupation is greatly reduced
Area, expense needed for significantly reducing plant construction, transformation.
Detailed description of the invention
Fig. 1 is flue-gas dust-removing and desulfurization tower structure schematic diagram of the present invention.
Fig. 2 is partition A of the present invention to structural schematic diagram.
Fig. 3 is wastewater treatment area B of the present invention to structural schematic diagram.
Fig. 4 is present invention process flow diagram.
In figure: 1- flue gas emission area；2- cone-shaped variable diameter；3- mist eliminating zone；4- tower tray area；5- reverse taper deformation diameter；6- spray
Drench area；6-1- circulating clear liquid pipeline II；6-2- flue gas pipeline I；7- wastewater treatment area；8- oxidizing, flocculating area；8-1- liquidometer I；
8-2-alkaline solution line I；8-3-flocculant line；8-4-outlet slurry line；8-5-flue gas pipeline II；9- circulation cleaning
Liquid zone；9-1-liquidometer II；The fresh water pipeline of 9-2-；9-3- alkaline solution line II；9-4-oxidizing gas pipeline；9-5
Clear liquid draws pipeline；9-6-outlet clear liquid pipeline；10- smoke inlet；11- demister；12- liquid distribution trough；12-1- circulation
Clear liquid pipeline I；13- tower tray；14- spray pipe；15- atomizer；16- blow vent；17- flue gas branch pipe；18- oxidizing gas
Distributor pipe；19- partition II；20- partition I；21- filter medium；22- sealing strip；23- fastening screw；24- blower；25- is cooling
Device；26- circulation cleaning liquid pump, 27- chimney, 28- outer sleeve.
Specific embodiment
Below in conjunction with drawings and examples, the present invention will be described in detail.
Flue-gas dust-removing and desulfurization tower of the invention is from top to bottom followed successively by flue gas emission area 1, mist eliminating zone 3, tower tray area 4, spray
Area 6 and wastewater treatment area 7；The flue gas emission area 1 is connected with mist eliminating zone 3 by cone-shaped variable diameter 2, is below mist eliminating zone 3
Tower tray area 4, tower tray area 4 are connected with spraying zone 6 by reverse taper deformation diameter 5, are wastewater treatment area 7 below spraying zone 6；Described
The center of wastewater treatment area 7 is divided by one piece of vertical partition I 20 for oxidizing, flocculating area 8 and circulation cleaning liquid zone 9, wherein oxidation wadding
Coagulation zone 8 is connected to spraying zone 6, by circulation cleaning liquid zone 9 and oxidizing, flocculating area 8 and is sprayed at the top of circulation cleaning liquid zone 9 by partition II 19
It is completely separated to drench area 6.
The partition I 20 is arranged at least one opening, preferably 1 ~ 20, more preferably 1 ~ 4, opening area be every
The 10% ~ 90% of 20 area of plate I, preferably 50% ~ 70%；Filter medium 21 is fixed in the opening of partition I 20；The filtering is situated between
Matter 21 is natural fiber, synthetic fibers, glass fiber, reticular structure, preferably metal mesh made of wire, and mesh size is
0.1 ~ 1000 μm, preferably 5 ~ 100 μm；Filter medium 21 is fixed in the opening of partition 20 by sealing strip 22, fastening screw 23.
19 both ends partition II are connect with partition I 20 and 9 tower wall of circulation cleaning liquid zone respectively, partition I 20 and partition
The angle of 19 junction II is generally 45 ~ 165 °, preferably 120 ~ 150 °.The partition I 20 and partition II 19 and tower wall
Between seal, avoid demarcation plate two sides air-liquid short circuit.
The tower diameter ratio of the mist eliminating zone 3 and flue gas emission area 1 is 1.2 ~ 5；The tower in the tower tray area 4 and spraying zone 6
Diameter ratio is 1.2 ~ 3.
The flue gas emission area 1 is generally 27 structure of chimney in conventional flue gas wet desulphurization process, the cigarette
27 bottom of chimney is connected with 3 tower body of mist eliminating zone, is preferably connected by cone-shaped variable diameter 2 with 3 tower body of mist eliminating zone, is arranged at the top of chimney 27
Exhanst gas outlet；It is preferred that outer sleeve 28 is arranged at the top of chimney 27, the outer sleeve 28 is the tubular structure of upper and lower opening, can be with
For cylindric or cone cylinder shape, along being higher by 27 top certain distance of chimney, generally 0.2~10m, preferably 0.5 on outer sleeve 28
~5m, the lower edge of outer sleeve 28 is lower than the upper edge of chimney 27, preferably shorter than along 0.5 ~ 5m on chimney 27；28 bottom of outer sleeve
The diameter of portion's opening is greater than 27 top opening diameter of chimney, preferably 1.01~1.2 times of 27 top opening diameter of chimney；It is described
Flue gas at the top of chimney 27 enter outer sleeve 28, be discharged at the top of outer sleeve 28, the gas velocity of flue gas is higher, is flowing through outer sleeve
Negative pressure can be generated when 28 between chimney 27 and outer sleeve 28, air flows through chimney 27 and outer sleeve under the suction of negative pressure
Annular space between 28 enters 28 top of outer sleeve, and air is pushed up from outer sleeve 28 together after mixing in outer sleeve 28 with flue gas
Portion's discharge, flue gas have just mixed well with air before leaving 28 top discharge of outer sleeve, significantly reduce " white cigarette " generation
Amount.
Defogging equipment is arranged in the mist eliminating zone 3, and for removing the drop of flue gas carrying, the defogging equipment can be
One or more of vortex-flow and defrosting device, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister etc..
One or more layers settable tower tray 13 of the tower tray area 4, preferably the tower tray number of plies are 2 ~ 6 layers；The tower tray can
Tower tray is combined for a type of tower tray or multiple types, including float valve tray, screen hole type tower tray, guiding screen hole type tower tray, solid
Tongue tower tray, directional float tray or combined trapezoid spray tray etc. come into full contact with the deep desulfuration strengthened mass transfer and realize flue gas for gas-liquid, will
The tiny dust particles between 0.1 μm ~ 5 μm in flue gas capture the depth dedusting for realizing flue gas, and flue gas is carried
A large amount of mist droplets capture the segregational load for reducing mist eliminating zone 3.
Liquid distribution trough 12 is set between the tower tray area 4 and mist eliminating zone 3, and liquid distribution trough 12 connects circulation cleaning liquid pipe
Line I 12-1, for circulating clear liquid to be evenly dispersed to tower tray 13.
One or more layers spray pipe 14 is arranged in 6 top of spraying zone, when Multi-layer sprinkling pipeline 14 is set, spray tube
The distance between line 14 is 0.5 ~ 5m, and preferred distance is 1 ~ 2.5m；The spray pipe 14 connects circulating clear liquid pipeline II 6-
1, multiple atomizers 15 are provided on spray pipe 14；The spraying zone 6 is small after atomization for circulating clear liquid to be atomized
Drop is contacted with flue gas adverse current, removes the dust and sulfur dioxide carried in flue gas；6 lower part of the spraying zone setting flue gas enters
Mouth 10, for connecting flue gas pipeline I 6-2.
The oxidizing, flocculating area 8 is separately connected alkaline solution line I 8-2, flocculant line 8-3 close to tower wall side
With liquidometer I 8-1；Flow control valve is set on the alkaline solution line I 8-2, for filling alkali into desulfurization wastewater
Property solution adjusts its pH value；The flocculant line 8-3 makes in desulfurization wastewater for filling flocculant into desulfurization wastewater
Little particle dust cohesion is at bulky grain.
8 bottom of oxidizing, flocculating area connects flue gas pipeline II 8-5 and outlet slurry line 8-4；The fume pipe
Line II 8-5 extends to 8 inside of oxidizing, flocculating area and is parallel to partition I20, the flue gas pipeline II 8-5 inside oxidizing, flocculating area 8
Successively horizontal distribution several groups flue gas branch pipe 17, preferably 2 ~ 4 groups, flue gas branch pipe 17 and flue gas pipeline II 8-5 connect from bottom to top
It is logical；Every group of flue gas branch pipe 17 is made of 2 ~ 8 flue gas branch pipes 17, and flue gas branch pipe 17 is arc-shaped, every group of flue gas branch pipe
17 are uniformly distributed and rotation direction is identical in the horizontal direction；Flue gas from the direction that flue gas branch pipe 17 sprays be circular arc tangential direction,
Flue gas high speed ejection pushes slurries rotation, is stirred for the slurries to oxidizing, flocculating area 8, makes the material in oxidizing, flocculating area
It is uniformly mixed, and dust particles on filter medium 21 is rinsed；The outlet slurry line 8-4 is used for oxidizing, flocculating
Subsequent processing units are drained into outside slurries afterwards, and flow control valve and pH meter are set on outlet slurry line 8-4；The flow tune
Valve is saved according to the flow of the liquidometer I 8-1 Signal Regulation outlet slurries fed back, for controlling the liquid level of liquefaction flocculation zone；It is described
PH meter be used to measure the pH value of outlet slurries, and signal via controller is fed back into the flow on alkaline solution line I 8-2
Regulating valve.
The circulation cleaning liquid zone 9 is connected with fresh water pipeline 9-2, alkaline solution line II9-3, oxygen close to tower wall side
The property changed gas line 9-4 and liquidometer II9-1；Flow control valve is set on the fresh water pipeline 9-2, according to liquidometer II
The flow of the Signal Regulation fresh water of 9-1 feedback, the liquid level for control loop clear liquid area 9；The alkaline solution line II
Flow control valve is provided on 9-3, for adjusting the flow of the alkaline solution filled to circulation cleaning liquid zone 9；The oxidisability
Gas line 9-4 is connected with blower 24, and extends to 20 side partition I of circulation cleaning liquid zone 9, with oxidizing gas distributor pipe
18 are connected；Several nozzles are provided on the oxidizing gas distributor pipe 18, nozzle faces Jie of the filtering on partition I 20
Matter 21, oxidizing gas spray from nozzle and pass through filter medium 21, by the dust particles on 8 filter medium 21 of oxidizing, flocculating area
It blows afloat, the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, and dust and flocculant effect coacervating large particle are in weight
To 8 bottom deposit of oxidizing, flocculating area under power effect, into oxidizing, flocculating area 8 oxidizing gas by the sulphite oxygen in slurries
Sulfate is turned to, keeps the COD of desulfurization wastewater up to standard.
Blow vent 16 is set in the 9 top tower wall of circulation cleaning liquid zone, for guaranteeing that 9 pressure of circulation cleaning liquid zone is steady,
It avoids pressure oscillation excessive and filter medium 21 is damaged.
9 bottom of the circulation cleaning liquid zone connection clear liquid draws pipeline 9-5, draws pipeline and is divided into two-way, pipeline connects all the way
Outlet clear liquid pipeline 9-6 is met, another way pipeline connects circulation cleaning liquid pump 26, is provided with pH meter, circulation cleaning liquid pump 26 on the pipeline
Circulating clear liquid pipeline I 12-1 and circulating clear liquid pipeline II 6-1 is connected through cooler 25；The pH meter is for measuring circulation cleaning
The pH value of liquid, and measuring signal via controller is fed back to the regulating valve of alkaline solution line II 9-3.
Embodiment 1
A kind of flue gas ash removal dedusting and desulfurizing tower is from top to bottom followed successively by flue gas emission area 1, mist eliminating zone 3, tower tray area 4, spraying zone 6
With wastewater treatment area 7, it is tower tray area 4, tower below mist eliminating zone 3 that flue gas emission area 1, which is connected with mist eliminating zone 3 by cone-shaped variable diameter 2,
Panel 4 is connected with spraying zone 6 by reverse taper deformation diameter 5, is wastewater treatment area 7 below spraying zone 6.
27 structure of chimney in conventional flue gas wet desulphurization process is arranged in flue gas emission area 1, and 27 bottom of chimney passes through cone
Bodily form variable diameter 2 is connected with 3 tower body of mist eliminating zone, and outer sleeve 28 is arranged at the top of chimney 27, and outer sleeve 28 is the cylinder of upper and lower opening
Shape structure, along being higher than 27 top 5m of chimney on outer sleeve 28,28 lower edge of outer sleeve lower than on chimney 27 along 1m.
Wet-type electrostatic defroster 11 is set in mist eliminating zone 3, liquid distribution trough 12 is set to 11 lower section of wet-type electrostatic defroster,
Tower tray area 4 is set to 12 lower section of liquid distribution trough, and 4 floor tower tray are arranged altogether, select sieve pore tower tray for tower tray area 4；Spraying zone 6 is arranged altogether
3 layers of spray pipe 14, the distance between spray pipe 14 are 2m, and atomizer 15 is uniformly arranged on spray pipe 14.
The center of wastewater treatment area 7 is divided by one piece of vertical partition I 20 for oxidizing, flocculating area 8 and circulation cleaning liquid zone 9,
Middle oxidizing, flocculating area 8 is connected to spraying zone 6, and circulation cleaning liquid zone 9 and oxidation are wadded a quilt with cotton by partition II 19 at the top of circulation cleaning liquid zone 9
Coagulation zone 8 and spraying zone 6 are completely separated, and partition I 20 is connected with partition II 19 by welding manner, partition I 20, partition II 19
It is connected between tower wall by welding manner.An opening is provided on partition I20, positioned at opening for 8 side of oxidizing, flocculating area
Mouth region domain is fixed with the metal mesh 21 that aperture is 100 μm, and metal mesh 21 is fixed on separation by sealing strip 22 and fastening screw 23
On plate I 20；8 bottom of oxidizing, flocculating area is provided with flue gas pipeline II 8-5, and flue gas pipeline II 8-5 extends to oxidizing, flocculating area 8
Part on be provided with 5 groups of flue gas branch pipes 17, every group of flue gas branch pipe 17 is uniformly distributed in the horizontal direction and rotation direction is identical, every group
Flue gas branch pipe 17 is made of 4 flue gas branch pipes 17, flue gas branch pipe 17 be it is arc-shaped,；Circulation cleaning liquid zone 9 is arranged close to tower wall side
Oxidizing gas pipeline 9-4, oxidizing gas pipeline 9-4 extend to 20 side partition I of circulation cleaning liquid zone 9, with oxidisability gas
Body distributor pipe 18 is connected；Several nozzles are provided on the oxidizing gas distributor pipe 18, nozzle faces on partition I 20
Filter medium 21；Blow vent 16 is provided in the tower wall on 9 top of circulation cleaning liquid zone.
A kind of method of flue gas ash removal, desulfurization and wastewater treatment, the flue gas of the present embodiment processing are to contain dust, titanium dioxide
The catalytic cracking catalyst regenerated flue gas of sulphur, it is not limited to such flue gas.The flue gas ash removal, desulfurization and waste water of the present embodiment
The method of processing specifically includes the following contents:
(1) flue gas divides two-way to enter flue-gas dust-removing and desulfurization tower, all the way through flue gas pipeline I 6-2 from the spray of flue-gas dust-removing and desulfurization tower
6 lower part of area enters, and another way is entered through through flue gas pipeline II 8-5 from 8 bottom of oxidizing, flocculating area of flue-gas dust-removing and desulfurization tower
Slurries in oxidizing, flocculating area 8, wherein flue gas flow ratio is 20 in flue gas pipeline I 6-2 and flue gas pipeline II 8-5, two-way cigarette
Gas, which converges, removes the most of dust and sulfur dioxide carried in flue gas with the circulating clear liquid counter current contacting of spraying zone 6 afterwards, passes through
The flue gas of spraying zone 6 enters tower tray area 4, carries out depth dust-removal and desulfurizing in tower tray area 4 and circulating clear liquid, purified flue gas passes through
Enter flue gas emission area 1 after 3 demisting of mist eliminating zone, enters after outer sleeve 28 mixes well with air at the top of chimney 27 and arranged from flue gas
Put 1 top discharge of area；
(2) desulfurization slurry for absorbing dust and sulfur dioxide enters oxidizing, flocculating area 8, by adjusting sodium hydroxide solution
The flow of (32w%) is 7.5 ~ 8 come the pH value for controlling 8 desulfurization wastewater of oxidizing, flocculating area, and desulfurization slurry is through flue gas pipeline II 8-5
It is sufficiently mixed under the stirring action of the flue gas of entrance with air, polysilicon acid flocculant and sodium hydroxide solution, in desulfurization slurry
Sulphite is oxidized to sulfate, and the little particle dust in desulfurization slurry flocculates into bulky grain, while having certain temperature
Flue gas makes the moisture in desulfurization slurry constantly volatilize, and salinity gradually increases；
(3) by adjusting the liquid level in the flow control oxidizing, flocculating area 8 of outlet slurries 8-6, by adjusting fresh water 9-2's
The liquid level of flow control circulation cleaning liquid zone 9 is maintained at the liquid level in oxidizing, flocculating area 8 and the liquid level difference of circulation cleaning liquid zone 9
1.0 ~ 2.0m, for desulfurization slurry under the action of partition I20 two sides liquid level difference, the metal mesh 21 flowed through on partition I 20 realizes solid-liquid
It separates, the dust particles in desulfurization slurry, which are filtered, stays in oxidizing, flocculating area 8, and clear liquid enters circulation cleaning liquid zone 9, oxidation wadding
Slurries after solidifying are drawn from 8 bottom of oxidizing, flocculating area enters subsequent processing units through outlet pipeline；
(4) enter from the air of blower 24 from circulation cleaning liquid zone 9, spray and pass through from the nozzle of oxidizing gas distributor pipe 18
Metal mesh 21 blows afloat the dust particles on 8 metal mesh 21 of oxidizing, flocculating area, what the dust and oxidizing gas blown afloat was rotated
Slurries are taken away, and dust and flocculant effect coacervating large particle are under the effect of gravity to oxidizing, flocculating area bottom deposit, into oxygen
Sulfite oxidation in slurries is sulfate by the oxidizing gas of change flocculation zone 8, keeps the COD of desulfurization wastewater up to standard；
(5) by adjusting sodium hydroxide solution (32wt%) flow for entering circulation cleaning liquid zone 9 come 9 desulfurization of control loop clear liquid area
The pH value of waste water is 7.0 ~ 7.5, and clear liquid and the fresh water and sodium hydroxide that circulating clear liquid area 9 is entered after the filtering of metal mesh 21 are molten
Liquid is drawn after the mixing of circulation cleaning liquid zone 9 from 9 bottom of circulation cleaning liquid zone, and a small amount of direct outlet of clear liquid is to reduce the sulphur of circulating clear liquid
Sour sodium content, remaining clear liquid enters cooler 25 after the pressurization of circulation cleaning liquid pump 26 and is cooled to 40 DEG C, after cooler 25 is cooling
Clear liquid a part enter spraying zone 6, contacted with flue gas adverse current desulfurization be dusted to flue gas after the atomization of atomizer 15, separately
A part of clear liquid flows through liquid distribution trough 12 and enters tower tray area 4, comes into full contact on tower tray 13 with flue gas and strengthens mass transfer effect reality
The deep desulfuration of existing flue gas, and the tiny dust particles between 0.1 μm in flue gas ~ 5 μm are captured, realize the depth of flue gas
Dedusting is spent, flue gas is also captured by the clear liquid on tower tray 13 by a large amount of mist droplets entrained by spraying zone 6, reduces and remove
The segregational load of fog-zone 3.,
Embodiment 2
Certain petroleum chemical enterprise's catalytic cracking flue gas temperature is 120 DEG C, wherein SO2Concentration is 1250mg/Nm3, dust concentration be
320mg/Nm3, using flue-gas dust-removing and desulfurization tower of the present invention, 27 diameter of chimney is 5m, outer sieeve diameter 6m, mist eliminating zone
3 and the tower body diameter in tower tray area 4 be 12m, the diameter of 7 tower body of spraying zone 6 and wastewater treatment area is 8m.From 1 row of flue gas emission area
The flue-gas temperature put is 52 DEG C, dust content 7.5mg/Nm3, SO2Content is 12mg/Nm3, it is better than GB 31570-2015 " stone
Oil refining emission of industrial pollutants standard " regulation (catalytic cracking catalyst regenerated flue gas particulate matter ≯ 50mg/Nm3, SO2≯
100mg/Nm3；Key area particulate matter ≯ 30mg/Nm3, SO2≯50mg/Nm3)；It is 20 DEG C, ambient wind velocity 4m/ in environment temperature
S, in the case that ambient humidity is 70%, " white cigarette " length of throat is 65m.
Embodiment 3
As a comparison, the not set outer sleeve 28 of flue-gas dust-removing and desulfurization tower, remaining is the same as embodiment 1, " white cigarette " length of throat
For 90m.
Claims (27)
1. a kind of flue-gas dust-removing and desulfurization tower, it is characterised in that: be from top to bottom followed successively by flue gas emission area, mist eliminating zone, tower tray area, spray
Drench area and wastewater treatment area；The flue gas emission area is chimney structure, and chimney bottom is connected with mist eliminating zone tower body, chimney top
Exhanst gas outlet is set；Outer sleeve is set in chimney top, the outer sleeve is the tubular structure of upper and lower opening, edge on outer sleeve
It is higher by chimney top certain distance, the lower edge of outer sleeve is lower than the upper edge of chimney, is annular between the outer sleeve and chimney
Space；Defogging equipment is arranged in the mist eliminating zone；One or more layers tower tray is arranged in the tower tray area；The wastewater treatment area
Center is oxidizing, flocculating area and circulation cleaning liquid zone by one piece of vertical partition I points, and wherein oxidizing, flocculating area is connected to spraying zone,
It is by partition II that circulation cleaning liquid zone and oxidizing, flocculating area and spraying zone is completely separated at the top of circulation cleaning liquid zone, circulation cleaning liquid zone top
Blow vent is set in portion's tower wall；At least one opening is arranged in the partition I, and opening area is the 10% ~ 90% of partition I area；
Filter medium is fixed in the opening of partition I；The oxidizing, flocculating area bottom connection flue gas pipeline II and outlet slurry line；Institute
The flue gas pipeline II stated is extended to inside oxidizing, flocculating area and is parallel to partition I, the flue gas pipeline II inside oxidizing, flocculating area by
Under to upper successively horizontal distribution several groups flue gas branch pipe.
2. fuel gas desulfurization gas wash tower described in accordance with the claim 1, it is characterised in that: edge is higher by chimney top 0.2 on outer sleeve
~10m；The lower edge of outer sleeve lower than on chimney along 0.5 ~ 5m；The outer sleeve bottom opening diameter is chimney top opening
1.01~1.2 times of diameter.
3. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the filter medium is reticular structure,
Filter medium material is one or more of natural fiber, synthetic fibers, glass fiber or wire, mesh size is 0.1 ~
1000µm。
4. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the both ends partition II respectively with partition
The angle of I and the connection of circulation cleaning liquid zone tower wall, partition I and the junction partition II is generally 45 ~ 165 °.
5. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the flue gas emission area and mist eliminating zone is logical
It crosses cone-shaped variable diameter to be connected, the tower diameter ratio in the mist eliminating zone and flue gas emission area is 1.2 ~ 5.
6. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: tower tray area and spraying zone pass through the back taper bodily form
Variable diameter is connected；The tower diameter ratio in the tower tray area and spraying zone is 1.2 ~ 3.
7. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the defogging equipment is vortex-flow and defrosting
One or more of device, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister.
8. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the tower tray is float valve tray, sieve pore
One of type tower tray, guiding screen hole type tower tray, solid tongue tower tray, directional float tray or combined trapezoid spray tray or multiple combinations.
9. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: set between the tower tray area and mist eliminating zone
Liquid distribution trough is set, liquid distribution trough connects circulating clear liquid pipeline I, for circulating clear liquid to be evenly dispersed to tower tray.
10. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the spraying zone top is arranged one layer
Or Multi-layer sprinkling pipeline；When Multi-layer sprinkling pipeline is arranged, the distance between spray pipe is 0.5 ~ 5m；The spray pipe connects
Circulating clear liquid pipeline II is met, is provided with multiple atomizers on spray pipe；Smoke inlet I is arranged in the spraying zone lower part,
Connect flue gas pipeline I.
11. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the oxidizing, flocculating area is close to tower wall
Side is separately connected alkaline solution line I, flocculant line and liquidometer I；Flow tune is set on the alkaline solution line I
Save valve.
12. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: every group of flue gas branch pipe is by 2 ~ 8
Flue gas branch pipe composition, flue gas branch pipe be it is arc-shaped, every group of flue gas branch pipe is uniformly distributed in the horizontal direction and rotation direction is identical.
13. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the circulation cleaning liquid zone is close to tower wall
Side is connected with fresh water pipeline, alkaline solution line II, oxidizing gas pipeline and liquidometer II；The fresh water pipeline
Upper setting flow control valve；It is provided with flow control valve on the alkaline solution line II, for adjusting to circulation cleaning liquid zone
The flow of the alkaline solution of filling.
14. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the oxidizing gas pipeline and wind
Machine is connected, and extends to the side partition I of circulation cleaning liquid zone, is connected with oxidizing gas distributor pipe；The oxidizing gas
Several nozzles are provided on distributor pipe, nozzle faces the filter medium on partition I.
15. flue-gas dust-removing and desulfurization tower described in accordance with the claim 1, it is characterised in that: the circulation cleaning liquid zone bottom connection
Clear liquid draws pipeline, draws pipeline and is divided into two-way, and pipeline connects outlet clear liquid pipeline all the way, and another way pipeline connects circulating clear liquid
It pumps, pH meter is provided on the pipeline, circulation cleaning liquid pump connects circulating clear liquid pipeline I and circulating clear liquid pipeline II through cooler；Institute
The pH meter stated is used to measure the pH value of circulating clear liquid, and measuring signal via controller is fed back to the adjusting of alkaline solution line II
Valve.
16. a kind of method of flue gas ash removal, desulfurization and wastewater treatment, it is characterised in that including following content: (1) flue gas divides two-way
Into flue-gas dust-removing and desulfurization tower, enter all the way through flue gas pipeline I from the spraying zone lower part of flue-gas dust-removing and desulfurization tower, another way is through cigarette
Gas pipeline II enters through the slurries in oxidizing, flocculating area, two-way flue gas from the oxidizing, flocculating area bottom of flue-gas dust-removing and desulfurization tower
Converge and remove the most of dust and sulfur dioxide carried in flue gas with the circulating clear liquid counter current contacting of spraying zone afterwards, passes through spray
The flue gas in area enters tower tray area, carries out depth dust-removal and desulfurizing in tower tray area and circulating clear liquid, purified flue gas passes through mist eliminating zone
Enter flue gas emission area after demisting, enters after outer sleeve mixes well with air from chimney top and arranged at the top of flue gas emission area
It puts；(2) desulfurization slurry for absorbing dust and sulfur dioxide enters oxidizing, flocculating area, in the flue gas entered through flue gas pipeline II
It is sufficiently mixed under stirring action with oxidizing gas, flocculant and alkaline solution, the sulphite in desulfurization slurry is oxidized to
Sulfate, the little particle dust in desulfurization slurry flocculates into bulky grain, while there is the flue gas of certain temperature to make in desulfurization slurry
Moisture constantly volatilize, salinity gradually increases；(3) desulfurization slurry flows through partition I under the action of partition I two sides liquid level difference
On filter medium realize and be separated by solid-liquid separation that the dust particles in desulfurization slurry, which are filtered, stays in oxidizing, flocculating area, clear liquid into
Enter circulation cleaning liquid zone, the slurries after oxidizing, flocculating are drawn from oxidizing, flocculating area bottom enters subsequent processing units through outlet pipeline；
(4) oxidizing gas enters from circulation cleaning liquid zone, filter medium is sprayed and passed through from the nozzle of oxidizing gas distributor pipe, by oxygen
The dust particles changed on flocculation zone filter medium are blown afloat, and the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, dust
With flocculant effect coacervating large particle under the effect of gravity to oxidizing, flocculating area bottom deposit, oxidizing gas will be in slurries
Sulfite oxidation is sulfate, keeps the COD of desulfurization wastewater up to standard；(5) into circulating clear liquid area after filter media
Clear liquid is drawn after circulation cleaning liquid zone mixes from circulation cleaning liquid zone bottom with fresh water and alkaline solution, a small amount of direct outlet of clear liquid
To reduce the salinity of circulating clear liquid, remaining clear liquid enters cooler after the pressurization of circulation cleaning liquid pump, after cooling through cooler
Clear liquid a part enters spraying zone, contacts after atomizer is atomized with flue gas adverse current and is dusted desulfurization, another portion to flue gas
It distinguishes liquid stream and enters tower tray area through liquid distribution trough, come into full contact on tower tray with flue gas, by the tiny dust particles in flue gas
It is captured with flue gas by a large amount of mist droplets entrained by spraying zone.
17. according to the method for claim 16, it is characterised in that: flue gas described in step (1) is fire coal boiler fume, combustion
One in coal-fired plant's flue gas, catalytic cracking catalyst regenerated flue gas, Furnace flue gas, coking flue gas or steel sintering flue gas
Kind is a variety of.
18. according to the method for claim 16, it is characterised in that: the flue gas pipeline I and flue gas pipeline II enters cigarette
The ratio of the amount of gas is 20 ~ 500；Circulating clear liquid and the ratio of flue gas are 5 ~ 50L/Nm3, circulating clear liquid in tower tray area in spraying zone
With 3 ~ 15L/Nm3 of ratio of flue gas.
19. according to the method for claim 16, it is characterised in that: the alkaline solution is selected from sodium hydroxide solution, hydrogen
Calcium oxide solution, magnesium hydroxide solution, sodium carbonate liquor, sodium sulfite solution, sodium citrate solution, lime stone slurry, ammonium hydroxide
Or one or more of seawater.
20. according to the method for claim 16, it is characterised in that: the oxidizing gas is air, oxygen or ozone
One or more of.
21. according to the method for claim 16, it is characterised in that: the flocculant be aluminum sulfate, alum, sodium aluminate,
Ferric trichloride, ferrous sulfate, ferric sulfate, aluminium polychloride, polyaluminium sulfate, polymer phosphate aluminium, poly-ferric chloride, polyaluminum sulfate
Iron, polymer phosphate iron, poly- phosphorus iron chloride, poly- phosphorus aluminium chloride, ferric-polysilicate, poly-silicic acid iron sulfate, polysilicate sulfuric acid aluminium, polymerised sulphur
Sour ferric-aluminum chloride, polymerization Polyferric Sulfate silicon flocculant, Al-fe Co Polymer Inorganic Coagulant, polysilicon acid flocculant or polyacrylamide flocculation
One or more of agent.
22. according to the method for claim 16, it is characterised in that: the slurry pH value after flocculation concentration described in step (3)
Control is located on slurries outlet pipeline in 7 ~ 9, pH on-line detector, is controlled by adjusting the regulating valve on alkaline solution line I
The pH value of desulfurization slurry processed.
23. according to the method for claim 16, it is characterised in that: the liquid level difference of the two sides partition I described in step (3) is
0.5 ~ 6m, the liquid level in oxidizing, flocculating area are higher than the liquid level of circulation cleaning liquid zone.
24. according to the method for claim 16, it is characterised in that: oxidizing, flocculating area liquid level described in step (3) by
Regulating valve in outlet slurry line is controlled.
25. according to the method for claim 16, it is characterised in that: the flushing water in oxidizing, flocculating area described in step (3) sprays
Shower pipe is periodically rinsed the filter medium on partition I, and 0.5 ~ 2h is divided between washing time.
26. according to the method for claim 16, it is characterised in that: circulation cleaning liquid zone liquid level described in step (3) by
Regulating valve on fresh water pipeline is controlled.
27. according to the method for claim 16, it is characterised in that: circulation cleaning liquid zone pH value control described in step (3) ~ (5)
System is located on tower bottom pump entry pipeline in 6 ~ 11, pH on-line detector, by adjusting the adjusting on alkaline solution line II
Valve carrys out the pH value of control loop clear liquid.
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| CN201810440425.2A CN110465175B (en) | 2018-05-10 | 2018-05-10 | Flue gas dust removal desulfurization tower and flue gas dust removal, desulfurization and wastewater treatment method |
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