CN110465176A - Flue-gas dust-removing and desulfurization tower and flue gas desulfurization and wastewater treatment method - Google Patents
Flue-gas dust-removing and desulfurization tower and flue gas desulfurization and wastewater treatment method Download PDFInfo
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- CN110465176A CN110465176A CN201810440431.8A CN201810440431A CN110465176A CN 110465176 A CN110465176 A CN 110465176A CN 201810440431 A CN201810440431 A CN 201810440431A CN 110465176 A CN110465176 A CN 110465176A
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- area
- flue gas
- zone
- gas
- desulfurization
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- Granted
Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 220
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 217
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 130
- 230000023556 desulfurization Effects 0.000 title claims abstract description 124
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 206
- 230000001590 oxidative effect Effects 0.000 claims abstract description 118
- 230000003311 flocculating effect Effects 0.000 claims abstract description 79
- 238000004140 cleaning Methods 0.000 claims abstract description 69
- 238000005192 partition Methods 0.000 claims abstract description 60
- 238000005507 spraying Methods 0.000 claims abstract description 56
- 239000003595 mist Substances 0.000 claims abstract description 46
- 239000002351 wastewater Substances 0.000 claims abstract description 21
- 239000002002 slurry Substances 0.000 claims description 90
- 239000007789 gas Substances 0.000 claims description 57
- 239000000428 dust Substances 0.000 claims description 56
- 238000000034 method Methods 0.000 claims description 50
- 239000007921 spray Substances 0.000 claims description 34
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 33
- 239000012670 alkaline solution Substances 0.000 claims description 32
- 239000002245 particle Substances 0.000 claims description 22
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 230000003009 desulfurizing effect Effects 0.000 claims description 17
- 230000000694 effects Effects 0.000 claims description 15
- 239000013505 freshwater Substances 0.000 claims description 15
- 235000019504 cigarettes Nutrition 0.000 claims description 14
- 230000003647 oxidation Effects 0.000 claims description 14
- 238000007254 oxidation reaction Methods 0.000 claims description 14
- 238000005189 flocculation Methods 0.000 claims description 13
- 230000016615 flocculation Effects 0.000 claims description 13
- 239000000243 solution Substances 0.000 claims description 13
- 238000009826 distribution Methods 0.000 claims description 12
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 10
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 239000005864 Sulphur Substances 0.000 claims description 7
- 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
- 238000012545 processing Methods 0.000 claims description 7
- 239000000779 smoke 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
- 238000002156 mixing Methods 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 5
- 239000000835 fiber Substances 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 5
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 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
- 239000003513 alkali Substances 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 238000004523 catalytic cracking Methods 0.000 claims description 4
- 239000003517 fume Substances 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- 229920000642 polymer Polymers 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000001816 cooling Methods 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
- 239000011574 phosphorus Substances 0.000 claims description 3
- 229910052698 phosphorus Inorganic materials 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
- 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
- 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
- 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
- 239000000701 coagulant Substances 0.000 claims description 2
- 239000003245 coal Substances 0.000 claims description 2
- 238000004939 coking Methods 0.000 claims description 2
- 229920001577 copolymer Polymers 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims description 2
- 239000011790 ferrous sulphate Substances 0.000 claims description 2
- 235000003891 ferrous sulphate Nutrition 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
- 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 2
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 2
- 229910000360 iron(III) sulfate Inorganic materials 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
- 239000000463 material Substances 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
- 229920002401 polyacrylamide Polymers 0.000 claims description 2
- 238000006116 polymerization reaction Methods 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
- SZUMNSLVXYNSKK-UHFFFAOYSA-L [Fe](Cl)Cl.[P] Chemical compound [Fe](Cl)Cl.[P] SZUMNSLVXYNSKK-UHFFFAOYSA-L 0.000 claims 1
- 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
- 239000001257 hydrogen Substances 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 238000005406 washing Methods 0.000 claims 1
- 238000010276 construction Methods 0.000 abstract description 6
- 230000009466 transformation Effects 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 9
- 229910052751 metal Inorganic materials 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 238000000889 atomisation Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 238000003466 welding 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
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 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
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000010355 oscillation Effects 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000012716 precipitator Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 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
- 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
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
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- 238000011161 development Methods 0.000 description 1
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- 238000009792 diffusion process Methods 0.000 description 1
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- 230000009977 dual effect Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- MVZXTUSAYBWAAM-UHFFFAOYSA-N iron;sulfuric acid Chemical compound [Fe].OS(O)(=O)=O MVZXTUSAYBWAAM-UHFFFAOYSA-N 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
- 238000007726 management method Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 229940079827 sodium hydrogen sulfite Drugs 0.000 description 1
- 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
- 238000009987 spinning Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
-
- 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
-
- 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
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
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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
- C02F1/78—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
-
- 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 desulfurization and wastewater treatment methods.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；Flue gas emission area is connected with mist eliminating zone by cone-shaped variable diameter, and tower tray area is connected with spraying zone by reverse taper deformation diameter；Wastewater treatment area center 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；Agitating device is arranged in the oxidizing, flocculating area；Filter medium is arranged in the vertical clapboard I；The present invention carries out flue gas ash removal, desulfurization and wastewater treatment in a tower, waste water is stirred using flue gas and realizes oxidizing, flocculating concentration operation, the filter operation of desulfurization wastewater is realized using the liquid level difference of vertical clapboard two sides as motive force, occupied area is greatly reduced, expense and the operating cost of device needed for significantly 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 desulfurization and wastewater treatment
Method.
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.
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 desulfurization and wastewater treatment side
Method, flue-gas dust-removing and desulfurization tower of the invention integrate flue gas ash removal, desulfurization and wastewater treatment, and the method for the present invention process is short, sets
It is standby less, occupied area it is few, have broad application prospects.
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 filtering is situated between
Matter is natural fiber, synthetic fibers, glass fiber, reticular structure made of wire, and mesh size is 0.1 ~ 1000 μm, preferably
5~100µm。
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
Several nozzles are provided on to the part in oxidizing, flocculating area, carry out heating concentration and stirring for the slurries to oxidizing, flocculating area；
The outlet slurry line is used to that subsequent processing units will to be drained into outside the slurries after oxidizing, flocculating, is arranged in outlet slurry line
Flow control valve and pH meter；The flow control valve is used for according to the flow of the liquidometer I Signal Regulation outlet slurries fed back
The liquid level of control liquefaction flocculation zone；The pH meter is used to measure the pH value of outlet slurries, and signal via controller is fed back to
Flow control valve on alkaline solution line I.
Agitating device is arranged in the oxidizing, flocculating area bottom, and agitating device is connected to dedusting and desulfurizing tower by fixing piece
Bottom；The fixing piece top is hollow cylinder-like structure, and dust-removal and desulfurizing tower bottom is fixed in bottom；The agitating device
Rotary shaft is plugged in vertically in the cylinder-like structure of fixing piece, and rotary shaft can be rotated around its center line；The rotary shaft is by upper
Rotary blade, deflector, agitating paddle are successively fixed under；During rotary blade, deflector and the agitating paddle with rotary shaft be
The heart is symmetric；The rotary blade is made of several blades, and blade is uniformly distributed in the horizontal direction, flat where blade
The angle of face and horizontal plane is 15 ~ 75 °, preferably 30 ~ 60 °；The deflector is inverted cone-shaped structure, is open at the top of back taper
Gap is arranged in structure between the back taper bottom of deflector and rotary shaft, deflector is normally at oxidizing, flocculating area liquid level or more,
For air-flow to be oriented to rotary blade two sides, entered across the slurries of rotary blade by the gap deflector and rotary shaft
Oxidizing, flocculating area；The axial horizontally disposed several groups in the agitating paddle edge, preferably 2 ~ 4 groups.When desulfurization slurry is from spraying zone stream
When lower process rotary blade, horizontal force is generated on the blade of rotary blade, is pushed rotary blade to rotate drive around rotary shaft and is stirred
It mixes paddle to rotate around the axis of rotation, for being stirred desulfurization slurry.Agitating paddle is located at the liquid level in oxidizing, flocculating area or less.
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, the desulfurization slurry band that the dust and oxidizing gas blown afloat is rotated
It walks, under the effect of gravity to oxidizing, flocculating area bottom deposit, oxidizing gas will for dust and flocculant effect coacervating large particle
Sulfite oxidation in slurries is sulfate, 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 desulfurization and wastewater treatment of the invention, 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 passes through descending liquid mouth of the rotary blade from deflector lower part from spraying zone
Water is generated on the blade of rotary blade when desulfurization slurry is flowed down from spraying zone by rotary blade into oxidizing, flocculating area
Flat power, the gravitional force of desulfurization slurry are converted into kinetic energy, and rotary blade is pushed to rotate around rotary shaft, and drive and be fixed on rotary shaft
On agitating paddle rotation desulfurization slurry is stirred, desulfurization slurry and oxidizing gas, wadding under the stirring action of agitating paddle
Solidifying agent and alkaline solution are sufficiently mixed, and the sulphite in desulfurization slurry is oxidized to sulfate, the little particle in desulfurization slurry
Dust flocculates into bulky grain, and the flue gas with certain temperature for being simultaneously from flue gas pipeline II keeps the moisture in desulfurization slurry continuous
Volatilization, salinity gradually increase；
(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, and oxidizing gas is by slurries
In sulfite oxidation be sulfate, keep 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, the flue gas is fire coal boiler fume, coal-fired plant flue gas, catalytic cracking catalyst regeneration
Flue gas, Furnace flue gas, coking flue gas or steel sintering flue gas etc..The flue gas pipeline I and flue gas pipeline II enters
The ratio of the amount of flue gas is 20 ~ 500；Circulating clear liquid and the ratio of flue gas are 5 ~ 50L/Nm in spraying zone3, it is preferably in a proportion of 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, it is molten that the alkaline solution is selected from sodium hydroxide solution, calcium hydroxide solution, magnesium hydroxide
One of liquid, sodium carbonate liquor, sodium sulfite solution, sodium citrate solution, lime stone slurry, ammonium hydroxide or seawater etc. are several
Kind.
In the method for the present invention, the oxidizing gas is one or more of air, oxygen, ozone etc., preferably
Air.
In the method for the present invention, the oxidizing gas flowrate is according to the slurries COD (COD) after flocculation concentration
It is adjusted, COD Con trolling index is ≯ 60mg/L.
In the method for the present invention, the flocculant is aluminum sulfate, alum, sodium aluminate, ferric trichloride, ferrous sulfate, sulfuric acid
Iron, aluminium polychloride, polyaluminium sulfate, polymer phosphate aluminium, poly-ferric chloride, bodied ferric sulfate, polymer phosphate iron, poly- phosphorus chlorination
Iron, poly- phosphorus aluminium chloride, ferric-polysilicate, poly-silicic acid iron sulfate, polysilicate sulfuric acid aluminium, polyaluminum sulfate ferric-aluminum chloride, polymerization Polyferric Sulfate silicon
One or more of flocculant, Al-fe Co Polymer Inorganic Coagulant, polysilicon acid flocculant, polyacrylamide flocculant etc., wadding
The additional amount of solidifying agent is 0.05 ~ 2kg/m3。
In the method for the present invention, the slurry pH value after the oxidizing, flocculating, which is controlled, is located at slurries in 7 ~ 9, pH on-line detector
On 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 is 0.5 ~ 6m, and the liquid level in oxidizing, flocculating area is higher than
The liquid level of circulation cleaning liquid zone.
In the method for the present invention, the oxidizing, flocculating area liquid level is controlled by the regulating valve in outlet slurry line
System.
In the method for the present invention, the circulation cleaning liquid zone liquid level is controlled by the regulating valve on fresh water pipeline.
In the method for the present invention, 6 ~ 11, the control range of preferable ph is 7 ~ 8 for the circulation cleaning liquid zone pH value control,
PH on-line detector is located on tower bottom pump entry pipeline, is followed by adjusting the regulating valve on alkaline solution line II to control
The pH value of ring 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.Agitating device is arranged in oxidizing, flocculating area in the present invention, the desulfurization slurry to be fallen using rotary blade recycling
Energy, convert kinetic energy for the gravitional force of desulfurization slurry, drive agitating paddle to be stirred desulfurization slurry, make oxidizing, flocculating
Material in area is sufficiently mixed contact, is conducive to the progress of oxidizing, flocculating reaction.Inlet flue gas is divided into two-way by the present invention, wherein
It is come into full contact under the stirring action of agitating paddle with desulfurization slurry by the high-temperature flue gas that oxidizing, flocculating area bottom enters, in flue gas
Dust and sulfur-containing oxide obtain certain absorption, while also taking full advantage of high-temperature flue gas waste heat, make in dust-removal and desulfurizing waste water
Moisture largely vaporize, in the preliminary concentrate that oxidizing, flocculating area realizes desulfurization wastewater, reduce the energy consumption of subsequent cell.Together
When, oxidizing gas of the invention not directly enters oxidizing, flocculating area, but introduces from circulation cleaning liquid zone, utilizes oxidizing gas
Filter medium is rinsed, flushing device is eliminated.Present invention eliminates conventional mixing plant and filter plant, at waste water
Reason process greatly reduces plant investment and operating cost without expending the additional energy.
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 mutually promotes, and process flow is short, greatly
Width reduces occupied 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 agitating device structural schematic diagram of the present invention.
Fig. 4 is agitating device B of the present invention to structural schematic diagram.
Fig. 5 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- agitating device；18- oxidizing gas
Spray tube；19- partition II；20- partition I；21- filter medium；22- sealing strip；23- fastening screw；24- rotary blade；25- leaf
Piece；26- deflector；27- descending liquid mouth；28- agitating paddle；29- fixing piece；30- rotary shaft；31- blower；32- cooler；33- is followed
Ring clear liquid pump；34- chimney；35- 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 34 structure of chimney in conventional flue gas wet desulphurization process, the cigarette
34 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 34
Exhanst gas outlet；It is preferred that outer sleeve 35 is arranged at the top of chimney 34, the outer sleeve 35 is the tubular structure of upper and lower opening, can be with
For cylindric or cone cylinder shape, along being higher by 34 top certain distance of chimney, generally 0.2~10m, preferably 0.5 on outer sleeve 35
~5m, the lower edge of outer sleeve 35 is lower than the upper edge of chimney 34, preferably shorter than along 0.5 ~ 5m on chimney 34；35 bottom of outer sleeve
The diameter of portion's opening is greater than 34 top opening diameter of chimney, preferably 1.01~1.2 times of 34 top opening diameter of chimney；It is described
Flue gas at the top of chimney 34 enter outer sleeve 35, be discharged at the top of outer sleeve 35, the gas velocity of flue gas is higher, is flowing through outer sleeve
Negative pressure can be generated when 35 between chimney 34 and outer sleeve 35, air flows through chimney 34 and outer sleeve under the suction of negative pressure
Annular space between 35 enters 35 top of outer sleeve, and air is pushed up from outer sleeve 35 together after mixing in outer sleeve 35 with flue gas
Portion's discharge, flue gas have just mixed well with air before leaving 35 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 is extended on the part in oxidizing, flocculating area 8 and is provided with several nozzles, is added for the slurries to oxidizing, flocculating area 8
Thermal concentration and stirring；The outlet slurry line 8-4 is used to that subsequent processing units will to be drained into outside the slurries after oxidizing, flocculating, outside
It arranges and flow control valve and pH meter is set on slurry line 8-4；The signal that the flow control valve is fed back according to liquidometer I 8-1
The flow for adjusting outlet slurries, for controlling the liquid level of liquefaction flocculation zone；The pH meter is used to measure the pH value of outlet slurries,
And signal via controller is fed back into the flow control valve on alkaline solution line I 8-2.
Agitating device 17 is arranged in 8 bottom of oxidizing, flocculating area, and agitating device 17 is connected to dedusting by fixing piece 29
Desulfurizing tower bottom；29 top of fixing piece is hollow cylinder-like structure, and dust-removal and desulfurizing tower bottom is fixed in bottom；Described stirs
The rotary shaft 30 for mixing device is plugged in vertically in the cylinder-like structure of fixing piece 29, and rotary shaft 30 can be rotated around its center line；Institute
The agitating device 17 stated successively fixes rotary blade 24, deflector 26, agitating paddle 28 from top to bottom；The rotary blade 24 by
Several blades 25 form, and blade 25 is uniformly distributed in the horizontal direction, and the angle of 25 place plane of blade and horizontal plane is 15 ~
75 °, optimized angle is 30 ~ 60 °；The deflector 26 is inverted cone-shaped structure, is uncovered structure, deflector 26 at the top of back taper
Back taper bottom and rotary shaft 30 between gap is set, deflector 26 is normally at 8 liquid level of oxidizing, flocculating area or more, for will
Air-flow is oriented to 24 two sides of rotary blade, across the slurries of rotary blade 24 by gap deflector 26 and rotary shaft 30 into
Enter oxidizing, flocculating area 8；The agitating paddle 28 is along axial horizontally disposed several groups, and preferably 2 ~ 4 groups.When desulfurization slurry is from spray
When area 6 flows down by rotary blade 24, horizontal force is generated on the blade of rotary blade 24, pushes rotary blade 24 around rotary shaft
30 rotations drive agitating paddle 28 to rotate around rotary shaft 30, for being stirred to desulfurization slurry.Agitating paddle 28 is located at oxidation wadding
Below the liquid level of coagulation zone 8.
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 31, and extends to 20 side partition I of circulation cleaning liquid zone 9, with oxidizing gas spray tube
18 are connected；Several nozzles are provided on the oxidizing gas spray tube 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, the sulfite oxidation in slurries is sulfate by oxidizing gas, makes desulfurization
The COD of waste water is 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 33, is provided with pH meter, circulation cleaning liquid pump 33 on the pipeline
Circulating clear liquid pipeline I 12-1 and circulating clear liquid pipeline II 6-1 is connected through cooler 32；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 dust-removing and desulfurization 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 and gives up
Water treatment zone 7, flue gas emission area 1 are connected with mist eliminating zone 3 by cone-shaped variable diameter 2, are tower tray area 4, tower tray area below mist eliminating zone 3
4 are connected with spraying zone 6 by reverse taper deformation diameter 5, are wastewater treatment area 7 below spraying zone 6.
34 structure of chimney in conventional flue gas wet desulphurization process is arranged in flue gas emission area 1, and 34 bottom of chimney passes through cone
Bodily form variable diameter 2 is connected with 3 tower body of mist eliminating zone, and outer sleeve 35 is arranged at the top of chimney 34, and outer sleeve 35 is the cylinder of upper and lower opening
Shape structure, along being higher than 34 top 5m of chimney on outer sleeve 35,35 lower edge of outer sleeve lower than on chimney 34 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 several nozzles；8 bottom welding fixture 29 of oxidizing, flocculating area, fixing piece 29 connect agitating device 17；It stirs
It mixes device 17 and successively fixes rotary blade 24, deflector 26, agitating paddle 28 from top to bottom, rotary blade 24 is fixed on rotary shaft 30
On, rotary blade 24 is made of several blades 25, and the angle of all blades 25 and vertical direction is all the same, flat where blade 25
The angle of face and horizontal plane is 45 °, and deflector 26 is inverted cone-shaped structure, is uncovered structure at the top of back taper, and deflector 26 falls
Gap is set between conical lower portion and rotary shaft 30, and deflector 26 is located at 8 liquid level of oxidizing, flocculating area or more, and agitating paddle is along axial water
Flat 3 groups of setting, agitating paddle 28 is located at the liquid level in oxidizing, flocculating area 8 or less.
Oxidizing gas pipeline 9-4 is arranged close to tower wall side in circulation cleaning liquid zone 9, and oxidizing gas pipeline 9-4 is extended to
20 side partition I of circulation cleaning liquid zone 9, is connected with oxidizing gas spray tube 18；On the oxidizing gas spray tube 18
Several nozzles are provided with, nozzle faces the filter medium 21 on partition I 20；It is provided in the tower wall on 9 top of circulation cleaning liquid zone
Blow vent 16.
A kind of method of flue gas desulfurization and wastewater treatment, the flue gas of the present embodiment processing are containing dust, sulfur dioxide
Catalytic cracking catalyst regenerated flue gas, it is not limited to such flue gas.The flue gas ash removal, desulfurization and wastewater treatment of the present embodiment
Method specifically include 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 35 mixes well with air at the top of chimney 34 and arranged from flue gas
Put 1 top discharge of area；
(2) desulfurization slurry for absorbing dust and sulfur dioxide passes through rotary blade 24 from 26 lower part of deflector from spraying zone 6
Descending liquid mouth 27 enters oxidizing, flocculating area 8, when desulfurization slurry is flowed down from spraying zone 6 by rotary blade 24, in rotary blade 24
Blade 25 on generate horizontal force, the gravitional force of desulfurization slurry is converted into kinetic energy, and rotary blade 24 is pushed to revolve around rotary shaft 30
Turn, and the agitating paddle 28 being fixed in rotary shaft 30 rotation is driven to be stirred desulfurization slurry, makees in the stirring of agitating paddle 28
It is sufficiently mixed with lower desulfurization slurry and air, polysilicon acid flocculant and sodium hydroxide solution, the sulphite quilt in desulfurization slurry
It 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 desulfurization
Moisture in slurries constantly volatilizees, and salinity gradually increases, and controls oxygen by adjusting the flow of sodium hydroxide solution (32wt%)
The pH value for changing 8 desulfurization wastewater of flocculation zone is 7.5 ~ 8；
(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 oxidizing gas of blower 31 from circulation cleaning liquid zone 9, sprayed from the nozzle of oxidizing gas spray tube 18
And metal mesh 21 is passed through, the dust particles on 8 metal mesh 21 of oxidizing, flocculating area are blown afloat, the dust and oxidizing gas quilt blown afloat
The slurries of rotation are taken away, dust and flocculant effect coacervating large particle under the effect of gravity to oxidizing, flocculating area bottom deposit,
Sulfite oxidation in slurries is sulfate by oxidizing gas, 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 32 after the pressurization of circulation cleaning liquid pump 33 and is cooled to 40 DEG C, after cooler 32 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.
The flue-gas temperature discharged from flue gas emission area 1 is 49 DEG C, dust content 7.2mg/Nm3, SO2Content is
12.6mg/Nm3, it is better than the regulation (catalytic cracking catalyst of GB 31570-2015 " petroleum refining industry pollutant emission standard "
Regenerated flue gas particulate matter ≯ 50mg/Nm3, SO2≯100mg/Nm3；Key area particulate matter ≯ 30mg/Nm3, SO2≯50mg/
Nm3)
Embodiment 2
Certain enterprise's boiler smoke temperature is 135 DEG C, wherein SO2Concentration is 850mg/Nm3, dust concentration 280mg/Nm3, use
Flue-gas dust-removing and desulfurization tower of the present invention, 27 diameter of chimney are 4m, outer sieeve diameter 5m, the tower of mist eliminating zone 3 and tower tray area 4
Body diameter is 10m, and the diameter of 7 tower body of spraying zone 6 and wastewater treatment area is 8m.From flue gas emission area 1 discharge flue-gas temperature be
48 DEG C, dust content 6.5mg/Nm3, SO2Content is 10mg/Nm3；It is 25 DEG C, ambient wind velocity 4m/s, environment in environment temperature
In the case that humidity is 70%, " white cigarette " length of throat is 45m.
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 80m.
Claims (26)
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；Agitating device is arranged in the oxidizing, flocculating area bottom, and agitating device passes through fixing piece
It is connected to dust-removal and desulfurizing tower bottom；The fixing piece top is hollow cylinder-like structure, and dust-removal and desulfurizing tower bottom is fixed in bottom；
The rotary shaft of the agitating device is plugged in vertically in the cylinder-like structure of fixing piece, and rotary shaft can be rotated around its center line；
The rotary shaft from top to bottom successively fixes rotary blade, deflector, agitating paddle；It the rotary blade, deflector and stirs
Paddle is mixed to be symmetric centered on rotary shaft；The rotary blade is made of several blades, and blade is equal in the horizontal direction
Even distribution, the angle of plane and horizontal plane where blade is 15 ~ 75 °, and the deflector is inverted cone-shaped structure, back taper top
For uncovered structure, gap is set, and the agitating paddle is along axial horizontally disposed between the back taper bottom of deflector and rotary shaft
Several groups.
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 of natural fiber, synthetic fibers, glass fiber or wire or a variety of, 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 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: 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.
13. 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.
14. 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.
15. a kind of method of flue gas desulfurization and wastewater treatment, it is characterised in that including following content: (1) flue gas divides two-way to enter
Flue-gas dust-removing and desulfurization tower enters through flue gas pipeline I from the spraying zone lower part of flue-gas dust-removing and desulfurization tower all the way, and another way is through fume pipe
Line II enters through the slurries in oxidizing, flocculating area from the oxidizing, flocculating area bottom of flue-gas dust-removing and desulfurization tower, and two-way flue gas converges
The most of dust and sulfur dioxide carried in flue gas is removed with the circulating clear liquid counter current contacting of spraying zone afterwards, across spraying zone
Flue gas 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 demisting
Enter flue gas emission area afterwards, enters after outer sleeve mixes well with air from chimney top from flue gas emission area top discharge；(2)
The desulfurization slurry for absorbing dust and sulfur dioxide enters oxygen from the descending liquid mouth of deflector lower part by rotary blade from spraying zone
Change flocculation zone and generate horizontal force on the blade of rotary blade when desulfurization slurry is flowed down from spraying zone by rotary blade, takes off
The gravitional force of sulphur slurries is converted into kinetic energy, and rotary blade is pushed to rotate around rotary shaft, and drives and be fixed on stirring in rotary shaft
Paddle rotation is mixed to be stirred desulfurization slurry, under the stirring action of agitating paddle desulfurization slurry and oxidizing gas, flocculant and
Alkaline solution is sufficiently mixed, and the sulphite in desulfurization slurry is oxidized to sulfate, the little particle dust wadding in desulfurization slurry
Bulky grain is congealed into, the flue gas with certain temperature for being simultaneously from flue gas pipeline II makes the moisture in desulfurization slurry constantly volatilize,
Salinity gradually increases；(3) desulfurization slurry under the action of partition I two sides liquid level difference, realize by the filter medium flowed through on partition I
It is separated by solid-liquid separation, the dust particles in desulfurization slurry, which are filtered, stays in oxidizing, flocculating area, and clear liquid enters circulation cleaning liquid zone, oxidation
Slurries after flocculation are drawn from oxidizing, flocculating area bottom enters subsequent processing units through outlet pipeline；(4) oxidizing gas is from following
Ring clear liquid area enters, and filter medium is sprayed and passed through from the nozzle of oxidizing gas distributor pipe, by oxidizing, flocculating area filter medium
On dust particles blow afloat, the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, dust and flocculant effect agglomerate
At bulky grain under the effect of gravity to oxidizing, flocculating area bottom deposit, the sulfite oxidation in slurries is sulphur by oxidizing gas
Hydrochlorate keeps the COD of desulfurization wastewater up to standard；(5) into the clear liquid and fresh water and alkali in circulating clear liquid area after filter media
Property solution circulation cleaning liquid zone mixing after from circulation cleaning liquid zone bottom draw, a small amount of direct outlet of clear liquid is to reduce circulating clear liquid
Salinity, remaining clear liquid enter cooler after the pressurization of circulation cleaning liquid pump, enter spray through cooler clear liquid a part after cooling
Area is drenched, is contacted after atomizer is atomized with flue gas adverse current and desulfurization is dusted to flue gas, another part clear liquid flows through liquid point
Cloth device enters tower tray area, comes into full contact on tower tray with flue gas, by flue gas tiny dust particles and flue gas pass through spraying zone
Entrained a large amount of mist droplets capture.
16. according to the method for claim 15, 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.
17. according to the method for claim 15, 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/Nm of ratio of flue gas3。
18. according to the method for claim 15, 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.
19. according to the method for claim 15, it is characterised in that: the oxidizing gas is air, oxygen or ozone
One or more of.
20. according to the method for claim 15, 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.
21. according to the method for claim 15, it is characterised in that: the control of slurry pH value after the flocculation concentration 7 ~
9, pH on-line detectors are located on slurries outlet pipeline, and desulfurization slurry is controlled by adjusting the regulating valve on alkaline solution line I
The pH value of liquid.
22. according to the method for claim 15, it is characterised in that: the liquid level difference of the two sides partition I is 0.5 ~ 6m, oxygen
The liquid level for changing flocculation zone is higher than the liquid level of circulation cleaning liquid zone.
23. according to the method for claim 15, it is characterised in that: the oxidizing, flocculating area liquid level is by outlet slurries
Regulating valve on pipeline is controlled.
24. according to the method for claim 15, it is characterised in that: the flushing water sprayer tube in the oxidizing, flocculating area is regular
Filter medium on partition I is rinsed, 0.5 ~ 2h is divided between washing time.
25. according to the method for claim 15, it is characterised in that: the circulation cleaning liquid zone liquid level is by fresh water pipe
Regulating valve on line is controlled.
26. according to the method for claim 15, it is characterised in that: the circulation cleaning liquid zone pH value is controlled in 6 ~ 11, pH
On-line detector is located on tower bottom pump entry pipeline, by adjusting the regulating valve on alkaline solution line II come control loop
The pH value of clear liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810440431.8A CN110465176B (en) | 2018-05-10 | 2018-05-10 | Flue gas dust removal desulfurization tower and flue gas desulfurization and wastewater treatment method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810440431.8A CN110465176B (en) | 2018-05-10 | 2018-05-10 | Flue gas dust removal desulfurization tower and flue gas desulfurization and wastewater treatment method |
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| Publication Number | Publication Date |
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| CN110465176A true CN110465176A (en) | 2019-11-19 |
| CN110465176B CN110465176B (en) | 2021-10-08 |
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| CN201810440431.8A Active CN110465176B (en) | 2018-05-10 | 2018-05-10 | Flue gas dust removal desulfurization tower and flue gas desulfurization and wastewater treatment method |
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| CN110465176B (en) | 2021-10-08 |
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