CN110465176B - Flue gas dust removal desulfurization tower and flue gas desulfurization and wastewater treatment method - Google Patents
Flue gas dust removal desulfurization tower and flue gas desulfurization and wastewater treatment method Download PDFInfo
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- CN110465176B CN110465176B CN201810440431.8A CN201810440431A CN110465176B CN 110465176 B CN110465176 B CN 110465176B CN 201810440431 A CN201810440431 A CN 201810440431A CN 110465176 B CN110465176 B CN 110465176B
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- 239000003546 flue gas Substances 0.000 title claims abstract description 217
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 215
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 130
- 230000023556 desulfurization Effects 0.000 title claims abstract description 130
- 239000000428 dust Substances 0.000 title claims abstract description 113
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 208
- 238000005189 flocculation Methods 0.000 claims abstract description 94
- 230000016615 flocculation Effects 0.000 claims abstract description 94
- 230000003647 oxidation Effects 0.000 claims abstract description 90
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 90
- 238000005507 spraying Methods 0.000 claims abstract description 67
- 238000003756 stirring Methods 0.000 claims abstract description 50
- 238000005192 partition Methods 0.000 claims abstract description 45
- 239000002351 wastewater Substances 0.000 claims abstract description 22
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 12
- 239000002002 slurry Substances 0.000 claims description 90
- 239000007789 gas Substances 0.000 claims description 49
- 238000000034 method Methods 0.000 claims description 43
- 230000001590 oxidative effect Effects 0.000 claims description 43
- 239000012670 alkaline solution Substances 0.000 claims description 34
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 33
- 239000000779 smoke Substances 0.000 claims description 33
- 239000002245 particle Substances 0.000 claims description 31
- 230000001105 regulatory effect Effects 0.000 claims description 23
- 239000007921 spray Substances 0.000 claims description 21
- 239000000243 solution Substances 0.000 claims description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 239000008394 flocculating agent Substances 0.000 claims description 16
- 239000013505 freshwater Substances 0.000 claims description 15
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 14
- 230000009471 action Effects 0.000 claims description 14
- 230000008569 process Effects 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 10
- 229910052751 metal Inorganic materials 0.000 claims description 10
- 239000002184 metal Substances 0.000 claims description 10
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 8
- 238000012546 transfer Methods 0.000 claims description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 6
- 230000005484 gravity Effects 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
- 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 5
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 5
- 150000003839 salts Chemical class 0.000 claims description 5
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 238000004523 catalytic cracking Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000005381 potential energy Methods 0.000 claims description 4
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 3
- 238000007667 floating Methods 0.000 claims description 3
- 239000003365 glass fiber Substances 0.000 claims description 3
- 238000005259 measurement Methods 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 239000010452 phosphate Substances 0.000 claims description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 3
- 235000010265 sodium sulphite Nutrition 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000012209 synthetic fiber Substances 0.000 claims description 3
- 229920002994 synthetic fiber Polymers 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- BYMMIQCVDHHYGG-UHFFFAOYSA-N Cl.OP(O)(O)=O Chemical compound Cl.OP(O)(O)=O BYMMIQCVDHHYGG-UHFFFAOYSA-N 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
- 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
- CYUOWZRAOZFACA-UHFFFAOYSA-N aluminum iron Chemical compound [Al].[Fe] CYUOWZRAOZFACA-UHFFFAOYSA-N 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
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 2
- -1 and meanwhile Substances 0.000 claims description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 2
- 238000004939 coking Methods 0.000 claims description 2
- 239000002131 composite material Substances 0.000 claims description 2
- 238000007334 copolymerization reaction Methods 0.000 claims description 2
- 239000011790 ferrous sulphate Substances 0.000 claims description 2
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 2
- 229910000359 iron(II) 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
- 229920002401 polyacrylamide Polymers 0.000 claims description 2
- 239000013535 sea water Substances 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
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims 2
- 238000011010 flushing procedure Methods 0.000 claims 2
- 229910052742 iron Inorganic materials 0.000 claims 1
- 229920002627 poly(phosphazenes) Polymers 0.000 claims 1
- 238000001914 filtration Methods 0.000 abstract description 7
- 238000010276 construction Methods 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 description 13
- 230000001276 controlling effect Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 230000007547 defect Effects 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-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
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000006243 chemical reaction Methods 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
- 239000000203 mixture Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 210000004911 serous fluid Anatomy 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
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- 238000003466 welding Methods 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 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
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- 239000002440 industrial waste Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 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
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 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
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- 239000011734 sodium Substances 0.000 description 1
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- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Images
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
-
- 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
-
- 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
-
- 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
-
- 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
-
- 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
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- Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
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- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a flue gas dust removal desulfurization tower and a flue gas desulfurization and wastewater treatment method. The flue gas dedusting and desulfurizing tower comprises a flue gas discharge area, a demisting area, a tower tray area, a spraying area and a wastewater treatment area from top to bottom in sequence; the flue gas discharge area is connected with the demisting area through a cone-shaped reducing area, and the tower disc area is connected with the spraying area through an inverted cone-shaped reducing area; the center of the wastewater treatment area is divided into an oxidation flocculation area and a circulating clear liquid area by a vertical partition plate I, and the top of the circulating clear liquid area completely separates the circulating clear liquid area from the oxidation flocculation area and a spraying area by a partition plate II; the oxidation flocculation area is provided with a stirring device; the vertical partition plate I is provided with a filter medium; the invention carries out flue gas dust removal, desulfurization and wastewater treatment in one tower, utilizes the flue gas to stir the wastewater to realize the operation of oxidation flocculation concentration, utilizes the liquid level difference at two sides of the vertical clapboard as a driving force to realize the filtration operation of the desulfurization wastewater, greatly reduces the floor area, and obviously reduces the cost required by the construction and the reconstruction of the device and the operation cost of the device.
Description
Technical Field
The invention belongs to the field of industrial waste gas purification, and relates to a flue gas dust removal desulfurization tower and a flue gas desulfurization and wastewater treatment method.
Background
The boiler flue gas and the flue gas discharged by a factory contain sulfur dioxide and dust, the sulfur dioxide and the dust are main component dust of atmospheric pollutants, the sulfur dioxide is a main reason for forming acid rain, and the dust with small particle size is one of the chief causes of haze formation.
The wet desulphurization has the advantages of high desulphurization rate, reliable device operation, simple operation and the like, so the existing flue gas desulphurization technology of various countries in the world mainly takes wet desulphurization as the main technology. The traditional wet desulphurization technology mainly comprises a limestone-gypsum method, a double alkali desulphurization method, a sodium alkali desulphurization method, an ammonia desulphurization method and the like. The flue gas desulfurization technology mainly adopts countercurrent spray, alkaline slurry is sprayed from the upper part of a desulfurization tower, and is free to settle under the action of gravity to be in countercurrent contact with flue gas to realize desulfurization reaction, but the diameter of sprayed liquid drops is relatively large, the contact area of single liquid drop and the flue gas is small, so that in order to improve the desulfurization efficiency, the number of times of circulating spray of the slurry needs to be increased, the liquid drops are in contact with the flue gas for many times to improve the absorption effect of the liquid drops on sulfur dioxide, the flow of a slurry circulating pump at the bottom of the tower is very large, the power of a motor is also very large, the power consumption of the slurry circulating pump is very large, and the operation cost is high.
The particle size of dust in the flue gas is small, most of the dust is 0.1-200 mu m, and the existing flue gas dust removal technology mainly comprises a cloth bag type dust removal technology, an electrostatic dust removal technology and a wet dust removal technology. Because the flue gas contains moisture, dust absorbs moisture and is bonded on a filter bag of the cloth bag type dust collector to block the pores of the filter bag, so that the filter bag needs to be cleaned or replaced frequently, and the application of the cloth bag type dust collector is greatly limited; the main disadvantages of the electrostatic dust collector are that the manufacturing cost is high, the requirements of installation, maintenance and management are strict, high-voltage power transformation and rectification control equipment is required, the power consumption is high, and the occupied area is large; the wet dust removal technology mainly removes dust carried in flue gas through spray water, and liquid drops with smaller particle sizes are still discharged out of a chimney along with the flue gas after being combined with the dust.
The desulfurization wastewater treatment processes disclosed in CN201110153423.3, CN201310338193.7 and CN201310421183.X are all provided with a flocculation tank and an oxidation tank, the flocculation tank and the oxidation tank are both provided with a stirrer, and slurry is conveyed by a pump. The dust removal and desulfurization wastewater treatment process disclosed by CN201310338193.7 and CN201310421183.X adopts a hydrocyclone to carry out solid-liquid separation. The desulfurization wastewater treatment process has the advantages of longer flow, more equipment and higher energy consumption.
Because the pollution emission index established by the state is more and more strict, enterprises with boilers and factories with flue gas emission need to modify newly-added flue gas dust removal and desulfurization devices or old devices so as to meet the standard emission of flue gas. Because most boilers and flue gas discharging devices are built according to old standards before, and the flue gas needs further deep dedusting and desulfurization when in construction, enough construction land is not reserved for flue gas dedusting and desulfurization modification during construction, and the flue gas dedusting and desulfurization devices or the old devices need to be newly built in the existing limited area. The wet desulphurization technology comprises flue gas desulphurization, desulphurization waste water oxidation treatment or regeneration units, the flow is long, the equipment is more, the occupied area is larger, the construction and upgrading reconstruction of the dust removal desulphurization device are seriously restricted, and partial devices and boilers cannot be upgraded and reconstructed due to the lack of enough space, so that the flue gas emission index cannot meet the current national standard and is forced to be shut down or destroyed and reconstructed. Therefore, the development of flue gas desulfurization technology with short flow, less equipment and less floor space is urgently needed.
With the large-scale popularization and application of the wet desulfurization technology in China, an obvious and difficult-to-overcome defect of the wet desulfurization technology gradually appears, and the defect is that the discharged flue gas can generate 'white smoke' at the opening of a chimney, even forms 'long white smoke' of kilometers, brings strong visual impact to people, and sometimes generates 'dust rain' on the ground. Therefore, how to eliminate the phenomenon of "white smoke" is a problem to be solved urgently.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides the flue gas dust removal desulfurization tower and the flue gas desulfurization and wastewater treatment method.
The flue gas dedusting and desulfurizing tower comprises a flue gas discharge area, a demisting area, a tower tray area, a spraying area and a wastewater treatment area from top to bottom in sequence; the center of the wastewater treatment area is divided into an oxidation flocculation area and a circulating clear liquid area through a vertical partition plate I, wherein the oxidation flocculation area is communicated with the spraying area, and the top of the circulating clear liquid area completely separates the circulating clear liquid area from the oxidation flocculation area and the spraying area through a partition plate II; the partition plate I is provided with at least one opening, preferably 1-20 openings, more preferably 1-4 openings, and the area of the opening is 10% -90% of that of the partition plate I, preferably 50% -70%; a filter medium is fixed on the opening of the clapboard I; the filter medium is a net structure made of natural fibers, synthetic fibers, glass fibers and metal wires, and the mesh size is 0.1-1000 mu m, preferably 5-100 mu m.
The two ends of the baffle plate II are respectively connected with the baffle plate I and the tower wall of the circulating clear liquid area, and the included angle of the joint of the baffle plate I and the baffle plate II is generally 45-165 degrees, preferably 120-150 degrees. The partition plates I and II are sealed with the tower wall, so that gas and liquid short circuits at two sides of the partition plates are avoided.
The flue gas discharge area and the demisting area are preferably connected through conical reducing, and the tower diameter ratio of the demisting area to the flue gas discharge area is 1.2-5; the tower disc area and the spraying area are preferably connected through an inverted cone-shaped reducing area, and a wastewater treatment area is arranged below the spraying area; the tower diameter ratio of the tower tray area to the spraying area is 1.2-3.
The flue gas discharge area is generally a chimney structure in the conventional wet flue gas desulfurization process, the bottom of the chimney is connected with the tower body of the demisting area, preferably, the chimney is connected with the tower body of the demisting area through a cone-shaped reducing pipe, and the top of the chimney is provided with a flue gas outlet; preferably, an outer sleeve is arranged at the top of the chimney, the outer sleeve is of a cylindrical structure with an upper opening and a lower opening, and can be cylindrical or conical, the upper edge of the outer sleeve is higher than the top of the chimney by a certain distance, generally 0.2-10 m, preferably 0.5-5 m, the lower edge of the outer sleeve is lower than the upper edge of the chimney, preferably 0.5-5 m; an annular space is formed between the outer sleeve and the chimney, and the diameter of the bottom opening is preferably 1.01-1.2 times of that of the top opening of the chimney. The smoke enters the outer sleeve from the top of the chimney and is discharged from the top of the outer sleeve, the gas velocity of the smoke is high, negative pressure is generated between the chimney and the outer sleeve when the smoke flows through the outer sleeve, air flows through an annular space between the chimney and the outer sleeve under the action of suction of the negative pressure and enters the upper part of the outer sleeve, the air is mixed with the smoke in the outer sleeve and then is discharged from the top of the outer sleeve, the smoke is fully mixed with the air before leaving the top of the outer sleeve and being discharged, and the generation amount of 'white smoke' is greatly reduced.
The demisting zone is provided with demisting equipment for removing liquid drops carried by the flue gas, and the demisting equipment can be one or more of a cyclone demister, a wet electrostatic demister, a wire mesh demister or a baffling demister.
The tower tray area can be provided with one or more layers of tower trays, and the number of the tower trays is preferably 2-6; the tower tray can be one type of tower tray or various types of combined tower trays, comprises a float valve tower tray, a sieve tray, a guide sieve tray, a tongue fixing tower tray, a tongue floating tower tray or a three-dimensional mass transfer tower tray and the like, is used for gas-liquid full contact reinforced mass transfer to realize deep desulfurization of flue gas, captures micro dust particles between 0.1 mu m and 5 mu m in the flue gas to realize deep dust removal of the flue gas, and captures a large amount of micro fog drops carried by the flue gas to reduce the separation load of a demisting area.
And a liquid distributor is arranged between the tower tray area and the demisting area, and is connected with a circulating clear liquid pipeline I and used for uniformly distributing circulating clear liquid on the tower tray.
One or more layers of spraying pipelines are arranged at the upper part of the spraying area, and when the plurality of layers of spraying pipelines are arranged, the distance between the spraying pipelines is 0.5-5 m, and the preferable distance is 1-2.5 m; the spraying pipeline is connected with a circulating clear liquid pipeline II and is provided with a plurality of atomizing nozzles; the spraying area is used for atomizing the circulating clear liquid, and the atomized small liquid drops are in countercurrent contact with the flue gas to remove dust and sulfur dioxide carried in the flue gas; and the lower part of the spraying area is provided with a flue gas inlet I for connecting a flue gas pipeline I.
One side of the oxidation flocculation area, which is close to the tower wall, is respectively connected with an alkaline solution pipeline I, a flocculating agent pipeline and a liquid level meter I; the alkaline solution pipeline I is provided with a flow regulating valve for adding an alkaline solution into the desulfurization wastewater to regulate the pH value of the desulfurization wastewater; the flocculant pipeline is used for injecting a flocculant into the desulfurization wastewater, so that small-particle dust in the desulfurization wastewater is coagulated into large particles.
The bottom of the oxidation flocculation area is connected with a flue gas pipeline II and an outer discharging slurry pipeline; the part of the flue gas pipeline II extending to the oxidation flocculation area is provided with a plurality of nozzles for heating, concentrating and stirring the serous fluid in the oxidation flocculation area; the external slurry discharge pipeline is used for discharging the slurry after oxidation and flocculation to a subsequent treatment unit, and a flow regulating valve and a pH meter are arranged on the external slurry discharge pipeline; the flow regulating valve regulates the flow of the discharged slurry according to a signal fed back by the liquid level meter I and is used for controlling the liquid level of the liquefaction flocculation area; the pH meter is used for measuring the pH value of the discharged slurry and feeding back a signal to the flow regulating valve on the alkaline solution pipeline I through the controller.
The bottom of the oxidation flocculation area is provided with a stirring device which is connected to the bottom of the dedusting and desulfurization tower through a fixing piece; the upper part of the fixing piece is of a hollow cylindrical structure, and the bottom of the fixing piece is fixed at the bottom of the dedusting and desulfurizing tower; a rotating shaft of the stirring device is vertically inserted into the cylindrical structure of the fixing piece, and can rotate around the central line of the rotating shaft; the rotating shaft is sequentially fixed with a rotating impeller, a guide plate and a stirring paddle from top to bottom; the rotary impeller, the guide plate and the stirring paddle are symmetrically distributed by taking the rotary shaft as the center; the rotary impeller consists of a plurality of blades, the blades are uniformly distributed in the horizontal direction, and the included angle between the plane where the blades are located and the horizontal plane is 15-75 degrees, preferably 30-60 degrees; the guide plate is of an inverted cone structure, the top of the inverted cone structure is of an open structure, a gap is formed between the inverted cone bottom of the guide plate and the rotating shaft, the guide plate is generally positioned above the liquid level of the oxidation flocculation area and used for guiding airflow to the two sides of the rotating impeller, and slurry passing through the rotating impeller enters the oxidation flocculation area through the gap between the guide plate and the rotating shaft; the stirring paddle sets up a plurality of groups along axial level, preferably 2~4 groups. When the desulfurization slurry flows down from the spraying area and passes through the rotary impeller, horizontal force is generated on the blades of the rotary impeller, and the rotary impeller is pushed to rotate around the rotary shaft to drive the stirring paddle to rotate around the rotary shaft, so that the desulfurization slurry is stirred. The stirring paddle is positioned below the liquid level of the oxidation flocculation area.
One side of the circulating clear liquid zone, which is close to the tower wall, is connected with a fresh water pipeline, an alkaline solution pipeline II, an oxidizing gas pipeline and a liquid level meter II; the fresh water pipeline is provided with a flow regulating valve which is used for regulating the flow of fresh water according to a signal fed back by the liquid level meter II and controlling the liquid level of the circulating clear liquid area; the alkaline solution pipeline II is provided with a flow regulating valve for regulating the flow of the alkaline solution filled into the circulating clear liquid area; the oxidizing gas pipeline is connected with the fan, extends to one side of the partition plate I of the circulating clear liquid zone and is connected with the oxidizing gas distribution pipe; the oxidizing gas distribution pipe is provided with a plurality of nozzles, the nozzles are opposite to the filter medium on the partition plate I, the oxidizing gas is sprayed out from the nozzles and penetrates through the filter medium to blow up dust particles on the filter medium in the oxidation flocculation area, the blown-up dust and the oxidizing gas are taken away by the rotary desulfurization slurry, the dust and a flocculating agent are coagulated into large particles to be deposited at the bottom of the oxidation flocculation area under the action of gravity, and sulfite in the slurry is oxidized into sulfate by the oxidizing gas, so that the COD of the desulfurization wastewater reaches the standard.
The tower wall at the top of the circulating clear liquid area is provided with an air vent for ensuring the stable pressure of the circulating clear liquid area and avoiding the damage to the filter medium caused by overlarge pressure fluctuation.
The bottom of the circulating clear liquid zone is connected with a clear liquid leading-out pipeline, the leading-out pipeline is divided into two paths, one path of pipeline is connected with an external clear liquid discharging pipeline, the other path of pipeline is connected with a circulating clear liquid pump, a pH meter is arranged on the pipeline, and the circulating clear liquid pump is connected with a circulating clear liquid pipeline I and a circulating clear liquid pipeline II through a cooler; the pH meter is used for measuring the pH value of the circulating clear liquid and feeding back a measurement signal to the regulating valve of the alkaline solution pipeline II through the controller.
The method for flue gas desulfurization and wastewater treatment comprises the following steps:
(1) the flue gas enters the flue gas dust removal desulfurization tower in two ways, one way enters from the lower part of a spray zone of the flue gas dust removal desulfurization tower through a flue gas pipeline I, the other way enters from the bottom of an oxidation flocculation zone of the flue gas dust removal desulfurization tower through a flue gas pipeline II and passes through slurry in the oxidation flocculation zone, the two ways of flue gas are converged and then are in countercurrent contact with circulating clear liquid in the spray zone to remove most of dust and sulfur dioxide carried in the flue gas, the flue gas passing through the spray zone enters a tower panel zone, deep dust removal and desulfurization are carried out on the tower panel zone and the circulating clear liquid, the purified flue gas enters a flue gas discharge zone after being demisted in a demisting zone, the purified flue gas enters an outer sleeve from the top of a chimney and is fully mixed with air and then is discharged from the top of the flue gas discharge zone;
(2) the desulfurization slurry absorbing dust and sulfur dioxide flows through the rotary impeller from the spraying area to enter the oxidation flocculation area from the liquid descending port at the lower part of the guide plate, when the desulfurization slurry flows down from the spraying area and passes through the rotary impeller, horizontal force is generated on blades of the rotary impeller, the gravitational potential energy of the desulfurization slurry is converted into kinetic energy, the rotary impeller is pushed to rotate around the rotary shaft and drives the stirring paddle fixed on the rotary shaft to rotate to stir the desulfurization slurry, the desulfurization slurry is fully mixed with oxidizing gas, flocculating agent and alkaline solution under the stirring action of the stirring paddle, sulfite in the desulfurization slurry is oxidized into sulfate, small particle dust in the desulfurization slurry is flocculated into large particles, and meanwhile, flue gas with certain temperature from a flue gas pipeline II enables moisture in the desulfurization slurry to be continuously volatilized, and the salt concentration is gradually increased;
(3) the desulfurization slurry flows through a filter medium on a partition plate I to realize solid-liquid separation under the action of liquid level difference on two sides of the partition plate I, dust particles in the desulfurization slurry are filtered and left in an oxidation flocculation area, clear liquid enters a circulating clear liquid area, and the slurry after oxidation flocculation is led out from the bottom of the oxidation flocculation area and enters a subsequent treatment unit through an external discharge pipeline;
(4) oxidizing gas enters from the circulating clear liquid zone, is sprayed out from a nozzle of the oxidizing gas distribution pipe and penetrates through the filter medium, dust particles on the filter medium of the oxidation flocculation zone are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and a flocculating agent are aggregated into large particles under the action of gravity and are deposited at the bottom of the oxidation flocculation zone, sulfite in the slurry is oxidized into sulfate by the oxidizing gas, and COD of the desulfurization wastewater reaches the standard;
(5) the clear liquid entering the circulating clear liquid zone after being filtered by the filter medium is mixed with fresh water and alkaline solution in the circulating clear liquid zone and then is led out from the bottom of the circulating clear liquid zone, a small amount of clear liquid is directly discharged to reduce the salt concentration of the circulating clear liquid, the rest clear liquid enters the cooler after being pressurized by the circulating clear liquid pump, one part of the clear liquid cooled by the cooler enters the spraying area, is atomized by the atomizing nozzle and then is in countercurrent contact with the flue gas to remove dust and sulfur, the other part of the clear liquid flows through the liquid distributor and enters the tower disc area, the deep desulfurization of flue gas is realized with the abundant contact of flue gas intensive mass transfer effect on the tray to catch the small dust particle between 0.1 mu m ~5 mu m in the flue gas, realize the degree of depth dust removal of flue gas, a large amount of small fog drops that the flue gas carried through the spray area also are caught by the clear liquid on the tray, have reduced the separation load that removes the fog district.
In the method, the flue gas is coal-fired boiler flue gas, coal-fired power plant flue gas, catalytic cracking catalyst regeneration flue gas, process heating furnace flue gas, coking flue gas or steel sintering flue gas and the like. The ratio of the amount of the flue gas entering the flue gas pipeline I to the amount of the flue gas entering the flue gas pipeline II is 20-500; the ratio of the circulating clear liquid to the flue gas in the spraying area is 5-50L/Nm3The preferred proportion is 8-25L/Nm3And the ratio of the circulating clear liquid to the flue gas in the tower tray area is 3-15L/Nm3。
In the method, the alkaline solution is selected from one or more of sodium hydroxide solution, calcium hydroxide solution, magnesium hydroxide solution, sodium carbonate solution, sodium sulfite solution, sodium citrate solution, limestone slurry, ammonia water or seawater and the like.
In the method of the invention, the oxidizing gas is one or more of air, oxygen, ozone and the like, and is preferably air.
In the method, the flow of the oxidizing gas is adjusted according to the Chemical Oxygen Demand (COD) of the slurry after flocculation concentration, and the COD control index is not more than 60 mg/L.
In the method, the flocculating agent is aluminum sulfate, alum, sodium aluminate, ferric chloride, ferrous sulfate, ferric sulfate, polyaluminium chloride, polyaluminium sulfate and polyaluminium phosphateOne or more of polyferric chloride, polyferric sulfate, polyferric phosphate, polyferric chloride, polyaluminum phosphate chloride, polyferric silicate sulfate, polyaluminum ferric sulfate chloride, polyferric silicate flocculant, aluminum-iron copolymerization composite flocculant, polysilicic acid flocculant, polyacrylamide flocculant and the like, wherein the addition amount of the flocculant is 0.05-2 kg/m3。
In the method, the pH value of the slurry after oxidation flocculation is controlled to be 7-9, the pH online detector is positioned on a slurry external discharge pipeline, and the pH value of the desulfurized slurry is controlled by adjusting an adjusting valve on an alkaline solution pipeline I.
In the method, the liquid level difference between two sides of the partition plate I is 0.5-6 m, and the liquid level of the oxidation flocculation area is higher than that of the circulating clear liquid area.
In the method, the liquid level height of the oxidation flocculation area is controlled by an adjusting valve on an external slurry discharge pipeline.
In the method, the liquid level height of the circulating clear liquid area is controlled by an adjusting valve on a fresh water pipeline.
In the method, the pH value of the circulating clear liquid area is controlled to be 6-11, the preferable control range of the pH value is 7-8, the pH on-line detector is positioned on an inlet pipeline of a circulating pump at the bottom of the tower, and the pH value of the circulating clear liquid is controlled by adjusting an adjusting valve on an alkaline solution pipeline II.
In the method, the discharged slurry in the step (3) and the discharged clear liquid in the step (5) enter a subsequent treatment unit, can be used for preparing or producing products such as gypsum, sodium sulfite, sodium bisulfite, magnesium sulfite, magnesium sulfate, magnesium oxide, sodium sulfate, ammonium bisulfate and the like, and can also be discharged after being filtered to reach the standard.
Compared with the prior art, the invention has the advantages that:
1. the lower part of the flue gas dedusting and desulfurizing tower is provided with a wastewater treatment area which is divided into an oxidation flocculation area and a circulating clear liquid area by two clapboards, and the oxidation flocculation area realizes the oxidation, flocculation and concentration of the desulfurization wastewater; the vertical clapboard in the center of the wastewater treatment area is provided with a filter medium, and the filtration operation of the desulfurization slurry is realized by using the liquid level difference at the two sides of the vertical clapboard as a driving force. The circulating clear liquid obtained by filtering is used as a circulating medium for dust removal and desulfurization, and because the circulating clear liquid does not contain dust or has low dust content, compared with the prior art that slurry containing dust is used as the circulating medium for dust removal and desulfurization, the method has high dust removal efficiency. The stirring device is arranged in the oxidation flocculation area, the energy of the falling desulfurization slurry is recovered by adopting the rotary impeller, the gravitational potential energy of the desulfurization slurry is converted into kinetic energy, the stirring paddle is driven to stir the desulfurization slurry, the materials in the oxidation flocculation area are fully mixed and contacted, and the oxidation flocculation reaction is favorably carried out. The invention divides the inlet flue gas into two paths, wherein the high-temperature flue gas entering from the bottom of the oxidation flocculation area is fully contacted with the desulfurization slurry under the stirring action of the stirring paddle, so that dust and sulfur-containing oxides in the flue gas are absorbed to a certain extent, and simultaneously, the waste heat of the high-temperature flue gas is fully utilized, so that a large amount of moisture in the dedusting and desulfurization wastewater is vaporized, the preliminary concentration of the desulfurization wastewater is realized in the oxidation flocculation area, and the energy consumption of subsequent units is reduced. Meanwhile, the oxidizing gas is introduced from the circulating clear liquid zone instead of directly entering the oxidation flocculation zone, and the oxidizing gas is used for washing the filter medium, so that washing equipment is omitted. The invention saves conventional stirring equipment and filtering equipment, does not need to consume additional energy in the wastewater treatment process, and greatly reduces the device investment and the operation cost.
2. According to the invention, the inverted cone-shaped reducing is arranged between the tray area and the spraying area, so that the gas velocity of the tray area is favorably reduced, the gas-liquid mass transfer effect is enhanced, the dust removal efficiency and the desulfurization efficiency of flue gas in the tray area are improved, and entrainment is reduced, so that the load of the demisting area is reduced; the smoke discharging area and the demisting area are provided with the cone-shaped reducing areas, so that the flow speed of smoke is improved, the higher the gas speed of the smoke is, the higher the lifting height of the smoke after the smoke leaves the smoke discharging area is, the more the smoke is favorably diffused, and smoke plumes are shorter.
3. The smoke discharging area of the smoke desulfurizing and dedusting tower adopts a structure of a chimney and an outer sleeve, after smoke is accelerated by a demisting area and a cone-shaped reducing area, negative pressure is generated when the smoke flows through the outer sleeve to suck outside air, the smoke and the air are fully mixed in the outer sleeve and then are discharged from the top of the outer sleeve, and the generation amount of white smoke is greatly reduced.
4. The invention completes flue gas dust removal, flue gas desulfurization and wastewater treatment in one tower, realizes triple functions of deep flue gas dust removal, desulfurization and standard-reaching wastewater COD discharge, and has the advantages of cooperative and cooperative function of all functional areas, mutual promotion, short process flow, great reduction of occupied area, and remarkable reduction of the cost required by device construction and transformation.
Drawings
FIG. 1 is a schematic structural diagram of a flue gas dedusting and desulfurizing tower of the present invention.
FIG. 2 is a schematic view of the structure of the separator in the direction of A.
FIG. 3 is a schematic structural view of a stirring device according to the present invention.
FIG. 4 is a B-direction structural schematic view of the stirring device of the present invention.
FIG. 5 is a schematic view of the process of the present invention.
In the figure: 1-a flue gas discharge zone; 2-conical reducing; 3-a demisting area; 4-tower disc area; 5-inverted cone-shaped reducing; 6-spraying area; 6-1-circulating clear liquid line II; 6-2-flue gas pipeline I; 7-a wastewater treatment zone; 8-an oxidative flocculation zone; 8-1-level gauge I; 8-2-alkaline solution line I; 8-3-flocculant line; 8-4-an efflux slurry line; 8-5-flue gas pipeline II; 9-circulating clear liquid area; 9-1-level gauge II; 9-2-fresh water line; 9-3-alkaline solution line II; 9-4-oxidizing gas line; 9-5-clear liquid outlet line; 9-6-an efflux supernatant line; 10-a flue gas inlet; 11-a demister; 12-a liquid distributor; 12-1-recycle serum line I; 13-trays; 14-a spray line; 15-an atomizing nozzle; 16-a vent; 17-a stirring device; 18-oxidizing gas shower; 19-separator II; 20-a separator I; 21-a filter medium; 22-a sealing strip; 23-a fastening screw; 24-a rotating impeller; 25-blades; 26-a baffle; 27-a fluid-lowering port; 28-stirring paddle; 29-a fixing member; 30-a rotation axis; 31-a fan; 32-a cooler; 33-circulating clear liquid pump; 34-a chimney; 35-outer sleeve.
Detailed Description
The present invention will be described in detail below with reference to the drawings and examples.
The flue gas dedusting and desulfurizing tower comprises a flue gas discharge area 1, a demisting area 3, a tower tray area 4, a spraying area 6 and a wastewater treatment area 7 from top to bottom in sequence; the flue gas emission area 1 is connected with the demisting area 3 through the cone-shaped reducing area 2, the tray area 4 is arranged below the demisting area 3, the tray area 4 is connected with the spraying area 6 through the inverted cone-shaped reducing area 5, and the wastewater treatment area 7 is arranged below the spraying area 6; waste water treatment district 7 central authorities divide into oxidation flocculation district 8 and circulation clear solution district 9 through a vertical baffle I20, wherein oxidation flocculation district 8 and spraying district 6 intercommunication, circulation clear solution district 9 top is separated circulation clear solution district 9 and oxidation flocculation district 8 and spraying district 6 completely through baffle II 19.
The partition plate I20 is provided with at least one opening, preferably 1-20 openings, more preferably 1-4 openings, and the area of the opening is 10% -90% of the area of the partition plate I20, preferably 50% -70%; a filter medium 21 is fixed on the opening of the clapboard I20; the filtering medium 21 is a net structure made of natural fibers, synthetic fibers, glass fibers and metal wires, preferably a metal net, and the mesh size is 0.1-1000 mu m, preferably 5-100 mu m; the filter medium 21 is fixed to the opening of the partition 20 by a seal strip 22 and a fastening screw 23.
Two ends of the partition plate II 19 are respectively connected with the partition plate I20 and the tower wall of the circulating clear liquid zone 9, and the included angle of the joint of the partition plate I20 and the partition plate II 19 is generally 45-165 degrees, preferably 120-150 degrees. The partition plates I20 and II 19 are sealed with the tower wall, so that gas and liquid short circuits at two sides of the partition plates are avoided.
The tower diameter ratio of the demisting area 3 to the flue gas discharge area 1 is 1.2-5; the tower tray area 4 and the spray area 6 have the tower diameter ratio of 1.2-3.
The flue gas discharge area 1 is generally a chimney 34 structure in the conventional wet flue gas desulfurization process, the bottom of the chimney 34 is connected with the tower body of the demisting area 3, preferably connected with the tower body of the demisting area 3 through the cone-shaped reducing area 2, and the top of the chimney 34 is provided with a flue gas outlet; preferably, an outer sleeve 35 is arranged at the top of the chimney 34, the outer sleeve 35 is a cylindrical structure with an upper opening and a lower opening, and can be cylindrical or conical, the upper edge of the outer sleeve 35 is higher than the top of the chimney 34 by a certain distance, generally 0.2-10 m, preferably 0.5-5 m, the lower edge of the outer sleeve 35 is lower than the upper edge of the chimney 34, preferably 0.5-5 m lower than the upper edge of the chimney 34; the diameter of the bottom opening of the outer sleeve 35 is larger than that of the top opening of the chimney 34, and preferably 1.01-1.2 times of that of the top opening of the chimney 34; the smoke enters the outer sleeve 35 from the top of the chimney 34 and is discharged from the top of the outer sleeve 35, the smoke is high in speed, negative pressure is generated between the chimney 34 and the outer sleeve 35 when the smoke flows through the outer sleeve 35, air flows through an annular space between the chimney 34 and the outer sleeve 35 under the suction effect of the negative pressure and enters the upper portion of the outer sleeve 35, the air is mixed with the smoke in the outer sleeve 35 and then is discharged from the top of the outer sleeve 35, the smoke is fully mixed with the air before being discharged from the top of the outer sleeve 35, and the generation amount of 'white smoke' is greatly reduced.
Demisting zone 3 set up demisting equipment for detach the liquid drop that the flue gas carried, demisting equipment can be for one or several kinds among whirl defroster, wet-type electrostatic defroster, silk screen defroster or baffling formula defroster etc..
One or more layers of tower trays 13 can be arranged in the tower tray area 4, and the number of the tower tray layers is preferably 2-6; the tower tray can be one type of tower tray or various types of combined tower trays, comprises a float valve tower tray, a sieve tray, a guide sieve tray, a tongue fixing tower tray, a tongue floating tower tray or a three-dimensional mass transfer tower tray and the like, is used for gas-liquid full contact reinforced mass transfer to realize deep desulfurization of flue gas, captures micro dust particles between 0.1 mu m and 5 mu m in the flue gas to realize deep dust removal of the flue gas, and captures a large amount of micro fog drops carried by the flue gas to reduce the separation load of a demisting area 3.
And a liquid distributor 12 is arranged between the tray area 4 and the demisting area 3, and the liquid distributor 12 is connected with a circulating clear liquid pipeline I12-1 and is used for uniformly distributing circulating clear liquid on a tray 13.
One or more layers of spraying pipelines 14 are arranged at the upper part of the spraying area 6, and when the plurality of layers of spraying pipelines 14 are arranged, the distance between the spraying pipelines 14 is 0.5-5 m, and the preferable distance is 1-2.5 m; the spraying pipeline 14 is connected with the circulating clear liquid pipeline II 6-1, and a plurality of atomizing nozzles 15 are arranged on the spraying pipeline 14; the spraying area 6 is used for atomizing the circulating clear liquid, and the atomized small liquid drops are in countercurrent contact with the flue gas to remove dust and sulfur dioxide carried in the flue gas; the lower part of the spraying area 6 is provided with a flue gas inlet 10 which is used for connecting a flue gas pipeline I6-2.
One side of the oxidation flocculation area 8, which is close to the tower wall, is respectively connected with an alkaline solution pipeline I8-2, a flocculant pipeline 8-3 and a liquid level meter I8-1; the alkaline solution pipeline I8-2 is provided with a flow regulating valve for adding an alkaline solution into the desulfurization wastewater to regulate the pH value of the desulfurization wastewater; and the flocculant pipeline 8-3 is used for injecting a flocculant into the desulfurization wastewater so as to coagulate small-particle dust in the desulfurization wastewater into large particles.
The bottom of the oxidation flocculation area 8 is connected with a flue gas pipeline II 8-5 and an outer discharge slurry pipeline 8-4; the part of the flue gas pipeline II 8-5 extending to the oxidation flocculation area 8 is provided with a plurality of nozzles for heating, concentrating and stirring the serous fluid in the oxidation flocculation area 8; the external slurry discharge pipeline 8-4 is used for discharging oxidized and flocculated slurry to a subsequent treatment unit, and a flow regulating valve and a pH meter are arranged on the external slurry discharge pipeline 8-4; the flow regulating valve regulates the flow of the discharged slurry according to a signal fed back by the liquid level meter I8-1 and is used for controlling the liquid level of the liquefaction flocculation area; the pH meter is used for measuring the pH value of the discharged slurry and feeding back a signal to the flow regulating valve on the alkaline solution pipeline I8-2 through the controller.
The bottom of the oxidation flocculation area 8 is provided with a stirring device 17, and the stirring device 17 is connected to the bottom of the dedusting and desulfurization tower through a fixing part 29; the upper part of the fixing part 29 is of a hollow cylindrical structure, and the bottom of the fixing part is fixed at the bottom of the dedusting and desulfurizing tower; a rotating shaft 30 of the stirring device is vertically inserted into the cylindrical structure of the fixing part 29, and the rotating shaft 30 can rotate around the central line of the rotating shaft; the stirring device 17 is sequentially fixed with a rotary impeller 24, a guide plate 26 and a stirring paddle 28 from top to bottom; the rotary impeller 24 is composed of a plurality of blades 25, the blades 25 are uniformly distributed in the horizontal direction, the included angle between the plane where the blades 25 are located and the horizontal plane is 15-75 degrees, and the preferred angle is 30-60 degrees; the guide plate 26 is in an inverted cone structure, the top of the inverted cone structure is in an open structure, a gap is arranged between the inverted cone bottom of the guide plate 26 and the rotating shaft 30, the guide plate 26 is generally positioned above the liquid level of the oxidation flocculation zone 8 and used for guiding airflow to the two sides of the rotating impeller 24, and slurry passing through the rotating impeller 24 enters the oxidation flocculation zone 8 through the gap between the guide plate 26 and the rotating shaft 30; the stirring paddles 28 are horizontally arranged in a plurality of groups along the axial direction, and preferably 2-4 groups. When the desulfurization slurry flows down from the spraying region 6 and passes through the rotary impeller 24, a horizontal force is generated on the blades of the rotary impeller 24, and the rotary impeller 24 is pushed to rotate around the rotating shaft 30 to drive the stirring paddle 28 to rotate around the rotating shaft 30, so that the desulfurization slurry is stirred. The stirring paddle 28 is positioned below the liquid level of the oxidation flocculation zone 8.
One side of the circulating clear liquid zone 9, which is close to the tower wall, is connected with a fresh water pipeline 9-2, an alkaline solution pipeline II9-3, an oxidizing gas pipeline 9-4 and a liquid level meter II 9-1; a flow regulating valve is arranged on the fresh water pipeline 9-2, and the flow of the fresh water is regulated according to a signal fed back by the liquid level meter II9-1, so as to control the liquid level of the circulating clear water area 9; the alkaline solution pipeline II9-3 is provided with a flow regulating valve for regulating the flow of the alkaline solution filled into the circulating clear liquid zone 9; the oxidizing gas pipeline 9-4 is connected with a fan 31, extends to one side of the partition plate I20 of the circulating clear liquid zone 9 and is connected with an oxidizing gas spray pipe 18; the oxidizing gas spraying pipe 18 is provided with a plurality of nozzles, the nozzles are opposite to the filter medium 21 on the partition plate I20, the oxidizing gas is sprayed out from the nozzles and penetrates through the filter medium 21 to blow up dust particles on the filter medium 21 of the oxidation flocculation zone 8, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and a flocculating agent are aggregated into large particles under the action of gravity to be deposited at the bottom of the oxidation flocculation zone 8, and sulfite in the slurry is oxidized into sulfate by the oxidizing gas, so that the COD of the desulfurization wastewater reaches the standard.
And the tower wall at the top of the circulating clear liquid area 9 is provided with an air vent 16 for ensuring the stable pressure of the circulating clear liquid area 9 and avoiding the damage to the filter medium 21 caused by overlarge pressure fluctuation.
The bottom of the circulating clear liquid zone 9 is connected with a clear liquid outlet pipeline 9-5, the outlet pipeline is divided into two paths, one path of pipeline is connected with an externally-discharged clear liquid pipeline 9-6, the other path of pipeline is connected with a circulating clear liquid pump 33, a pH meter is arranged on the pipeline, and the circulating clear liquid pump 33 is connected with a circulating clear liquid pipeline I12-1 and a circulating clear liquid pipeline II 6-1 through a cooler 32; the pH meter is used for measuring the pH value of the circulating clear liquid and feeding back a measurement signal to the regulating valve of the alkaline solution pipeline II9-3 through the controller.
Example 1
The utility model provides a flue gas dust removal desulfurizing tower, is flue gas discharge district 1, defogging district 3, tower tray district 4, spray district 6 and waste water treatment district 7 from top to bottom in proper order, and flue gas discharge district 1 links to each other through the conical reducing 2 with defogging district 3, and 3 below in defogging district are tower tray district 4, and tower tray district 4 links to each other through the reducing 5 of the inverted cone with spray district 6, and 6 below in spray district are waste water treatment district 7.
The flue gas emission area 1 is provided with a chimney 34 structure in a conventional flue gas wet desulphurization process, the bottom of the chimney 34 is connected with a demisting area 3 tower body through a cone-shaped reducing pipe 2, the top of the chimney 34 is provided with an outer sleeve 35, the outer sleeve 35 is of a cylindrical structure with an upper opening and a lower opening, the upper edge of the outer sleeve 35 is 5m higher than the top of the chimney 34, and the lower edge of the outer sleeve 35 is 1m lower than the upper edge of the chimney 34.
A wet-type electrostatic demister 11 is arranged in the demisting area 3, a liquid distributor 12 is arranged below the wet-type electrostatic demister 11, a tower tray area 4 is arranged below the liquid distributor 12, the tower tray area 4 is provided with 4 layers of tower trays, and sieve tray trays are selected; the spraying area 6 is provided with 3 layers of spraying pipelines 14, the distance between the spraying pipelines 14 is 2m, and the atomizing nozzles 15 are uniformly arranged on the spraying pipelines 14.
Waste water treatment district 7 central authorities divide into oxidation flocculation district 8 and circulation clear solution district 9 through a vertical baffle I20, and wherein oxidation flocculation district 8 and spraying district 6 intercommunication, circulation clear solution district 9 top is separated circulation clear solution district 9 and oxidation flocculation district 8 and spraying district 6 completely through baffle II 19, and baffle I20 links to each other through welding mode with baffle II 19, and baffle I20, baffle II 19 link to each other through welding mode between with the tower wall. An opening is formed in the partition plate I20, a metal net 21 with the aperture of 100 mu m is fixed in the opening area on one side of the oxidation flocculation area 8, and the metal net 21 is fixed on the partition plate I20 through a sealing strip 22 and a fastening screw 23; a flue gas pipeline II 8-5 is arranged at the bottom of the oxidation flocculation area 8, and a plurality of nozzles are arranged on the part of the flue gas pipeline II 8-5 extending to the oxidation flocculation area 8; the bottom of the oxidation flocculation area 8 is welded with a fixing part 29, and the fixing part 29 is connected with the stirring device 17; agitating unit 17 from the top down fixes rotatory impeller 24 in proper order, guide plate 26, stirring rake 28, rotatory impeller 24 is fixed in on the rotation axis 30, rotatory impeller 24 comprises a plurality of blades 25, all blades 25 are the same with the contained angle homogeneous phase of vertical direction, the plane at blade 25 place is 45 with the contained angle of horizontal plane, guide plate 26 is the back taper structure, the back taper top is uncovered structure, set up the gap between the back taper bottom of guide plate 26 and the rotation axis 30, guide plate 26 is located above 8 liquid levels in oxidation flocculation district, the stirring rake sets up 3 groups along the axial level, stirring rake 28 is located below 8 liquid levels in oxidation flocculation district.
An oxidizing gas pipeline 9-4 is arranged on one side of the circulating clear liquid zone 9 close to the tower wall, and the oxidizing gas pipeline 9-4 extends to one side of a partition plate I20 of the circulating clear liquid zone 9 and is connected with an oxidizing gas spray pipe 18; the oxidizing gas spray pipe 18 is provided with a plurality of nozzles which are opposite to the filter medium 21 on the partition plate I20; the tower wall at the upper part of the circulating clear liquid zone 9 is provided with an air vent 16.
The flue gas treated by the method is regenerated flue gas of a catalytic cracking catalyst containing dust and sulfur dioxide, but the method is not limited to the flue gas. The method for flue gas dust removal, desulfurization and wastewater treatment specifically comprises the following steps:
(1) the flue gas enters the flue gas dust removal and desulfurization tower in two paths, one path enters from the lower part of a spraying area 6 of the flue gas dust removal and desulfurization tower through a flue gas pipeline I6-2, the other path enters from the bottom of an oxidation flocculation area 8 of the flue gas dust removal and desulfurization tower through a flue gas pipeline II 8-5 and passes through the slurry in the oxidation flocculation area 8, wherein the flow ratio of the flue gas in the flue gas pipeline I6-2 to the flue gas pipeline II 8-5 is 20, the two paths of flue gas are converged and then are in countercurrent contact with circulating clear liquid in the spraying area 6 to remove most of dust and sulfur dioxide carried in the flue gas, the flue gas passing through the spraying area 6 enters the tower disc area 4, deep dedusting and desulfurization are carried out on the tower tray area 4 and the circulating clear liquid, the purified flue gas enters the flue gas discharge area 1 after being demisted in the demisting area 3, enters the outer sleeve 35 from the top of the chimney 34 and is fully mixed with air, and then is discharged from the top of the flue gas discharge area 1;
(2) the desulfurization slurry absorbing dust and sulfur dioxide flows from the spraying area 6 through the rotary impeller 24 and enters the oxidation flocculation area 8 from the liquid descending port 27 at the lower part of the guide plate 26, when the desulfurization slurry flows down from the spraying area 6 and passes through the rotary impeller 24, horizontal force is generated on the blades 25 of the rotary impeller 24, the gravitational potential energy of the desulfurization slurry is converted into kinetic energy, the rotary impeller 24 is pushed to rotate around the rotary shaft 30, the stirring paddle 28 fixed on the rotary shaft 30 is driven to rotate to stir the desulfurization slurry, the desulfurization slurry is fully mixed with air, a polysilicic acid flocculating agent and a sodium hydroxide solution under the stirring action of the stirring paddle 28, sulfite in the desulfurization slurry is oxidized into sulfate, small particle dust in the desulfurization slurry is flocculated into large particles, meanwhile, the flue gas with a certain temperature enables the moisture in the desulfurization slurry to be continuously volatilized, the salt concentration is gradually increased, and the pH value of the desulfurization wastewater in the oxidation flocculation area 8 is controlled to be 7.5 by adjusting the flow rate of the sodium hydroxide solution (32 wt%) 8, performing filtration;
(3) controlling the liquid level height of an oxidation flocculation area 8 by adjusting the flow of discharged slurry 8-6, and controlling the liquid level height of a circulating clear liquid area 9 by adjusting the flow of fresh water 9-2, so that the liquid level difference between the liquid level of the oxidation flocculation area 8 and the liquid level difference between the circulating clear liquid area 9 is kept at 1.0-2.0 m, the desulfurization slurry flows through a metal net 21 on a partition plate I20 under the action of the liquid level difference between two sides of a partition plate I20 to realize solid-liquid separation, dust particles in the desulfurization slurry are filtered and left in the oxidation flocculation area 8, clear liquid enters the circulating clear liquid area 9, and the slurry after oxidation flocculation is led out from the bottom of the oxidation flocculation area 8 and enters a subsequent treatment unit through a discharge pipeline;
(4) oxidizing gas from a fan 31 enters from the circulating clear liquid zone 9, is sprayed out from a nozzle of the oxidizing gas spray pipe 18 and penetrates through the metal mesh 21, dust particles on the metal mesh 21 of the oxidation flocculation zone 8 are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and the flocculating agent are aggregated into large particles to be deposited at the bottom of the oxidation flocculation zone under the action of gravity, sulfite in the slurry is oxidized into sulfate by the oxidizing gas, and the COD of the desulfurization wastewater reaches the standard;
(5) controlling the pH value of the desulfurization wastewater in the circulating clear liquid zone 9 to be 7.0-7.5 by adjusting the flow of a sodium hydroxide solution (32 wt%) entering the circulating clear liquid zone 9, filtering the mixture by a metal mesh 21, mixing the clear liquid entering the circulating clear liquid zone 9 with fresh water and a sodium hydroxide solution in the circulating clear liquid zone 9, leading out the mixture from the bottom of the circulating clear liquid zone 9, directly discharging a small amount of clear liquid to reduce the sodium sulfate content of the circulating clear liquid, pressurizing the rest clear liquid by a circulating clear liquid pump 33, then cooling the rest clear liquid to 40 ℃ by a cooler 32, leading one part of the clear liquid cooled by the cooler 32 into a spray zone 6, atomizing the clear liquid by an atomizing nozzle 15, then carrying out dust removal and desulfurization on the flue gas by countercurrent contact with the flue gas, leading the other part of the clear liquid to flow through a liquid distributor 12, entering a tray tower 4, fully contacting with the flue gas on a tray 13 to strengthen the mass transfer effect to realize the deep desulfurization of the flue gas, and catching the tiny dust particles between 0.1 mu m and 5 mu m in the flue gas, the deep dust removal of the flue gas is realized, a large amount of micro fog drops carried by the flue gas through the spraying area 6 are also captured by clear liquid on the tower tray 13, and the separation load of the demisting area 3 is reduced.
The temperature of the flue gas discharged from the flue gas discharge zone 1 was 49 ℃ and the dust content was 7.2mg/Nm3， SO2The content is 12.6mg/Nm3Is superior to the regulation of GB 31570-2015 emission Standard of pollutants for Petroleum refining industry (the regenerated flue gas particulate matters of the catalytic cracking catalyst are not more than 50mg/Nm3，SO2≯100mg/Nm3(ii) a Particulate matter in key areas is not more than 30mg/Nm3， SO2≯50mg/Nm3）
Example 2
The flue gas temperature of a boiler of a certain enterprise is 135 ℃, wherein SO2The concentration is 850mg/Nm3The dust concentration was 280mg/Nm3By adopting the flue gas dedusting and desulfurizing tower, the diameter of a chimney 27 is 4m, the diameter of an outer sleeve is 5m, the diameters of tower bodies of a demisting area 3 and a tower tray area 4 are 10m, and the diameters of tower bodies of a spraying area 6 and a wastewater treatment area 7 are 8 m. The temperature of the flue gas discharged from the flue gas discharge area 1 was 48 ℃ and the dust content was 6.5mg/Nm3，SO2The content is 10mg/Nm3(ii) a Under the conditions that the ambient temperature is 25 ℃, the ambient wind speed is 4m/s and the ambient humidity is 70 percent, the length of the white smoke at the opening of the chimney is 45 m.
Example 3
In contrast, the flue gas dust removal desulfurization tower was not provided with the outer sleeve 28, and the length of "white smoke" at the chimney port was 80m as in example 1.
Claims (26)
1. The utility model provides a flue gas dust removal desulfurizing tower which characterized in that: the device comprises a flue gas discharge area, a demisting area, a tower tray area, a spraying area and a wastewater treatment area from top to bottom in sequence; the smoke discharge area is of a chimney structure, the bottom of the chimney is connected with the tower body of the demisting area, and the top of the chimney is provided with a smoke outlet; an outer sleeve is arranged at the top of the chimney, the outer sleeve is of a cylindrical structure with an upper opening and a lower opening, the upper edge of the outer sleeve is higher than the top of the chimney by a certain distance, the lower edge of the outer sleeve is lower than the upper edge of the chimney, and an annular space is formed between the outer sleeve and the chimney; the demisting area is provided with demisting equipment; one or more layers of trays are arranged in the tray area; the center of the wastewater treatment area is divided into an oxidation flocculation area and a circulating clear liquid area through a vertical partition plate I, wherein the oxidation flocculation area is communicated with the spraying area, the top of the circulating clear liquid area completely separates the circulating clear liquid area from the oxidation flocculation area and the spraying area through a partition plate II, and a vent is arranged on the tower wall at the top of the circulating clear liquid area; the partition plate I is provided with at least one opening, and the area of the opening is 10% -90% of that of the partition plate I; a filter medium is fixed on the opening of the clapboard I; the bottom of the oxidation flocculation area is provided with a stirring device which is connected to the bottom of the dedusting and desulfurization tower through a fixing piece; the upper part of the fixing piece is of a hollow cylindrical structure, and the bottom of the fixing piece is fixed at the bottom of the dedusting and desulfurizing tower; a rotating shaft of the stirring device is vertically inserted into the cylindrical structure of the fixing piece, and can rotate around the central line of the rotating shaft; the rotating shaft is sequentially fixed with a rotating impeller, a guide plate and a stirring paddle from top to bottom; the rotary impeller, the guide plate and the stirring paddle are symmetrically distributed by taking the rotary shaft as the center; rotatory impeller constitute by a plurality of blades, the blade evenly distributed on the horizontal direction, the contained angle of blade place plane and horizontal plane is 15~75, the guide plate be the back taper structure, the back taper top is open structure, sets up the gap between the back taper bottom of guide plate and the rotation axis, the stirring rake set up a plurality of groups along the axial level.
2. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the upper edge of the outer sleeve is 0.2-10 m higher than the top of the chimney; the lower edge of the outer sleeve is 0.5-5 m lower than the upper edge of the chimney; the diameter of the bottom opening of the outer sleeve is 1.01-1.2 times of the diameter of the top opening of the chimney.
3. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the filter medium is of a net structure, the filter medium is made of one or more of natural fibers, synthetic fibers, glass fibers or metal wires, and the mesh size is 0.1-1000 mu m.
4. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the two ends of the partition plate II are respectively connected with the partition plate I and the tower wall of the circulating clear liquid area, and the included angle of the joint of the partition plate I and the partition plate II is 45-165 degrees.
5. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the flue gas emission area and the demisting area are connected through the conical reducing, and the tower diameter ratio of the demisting area to the flue gas emission area is 1.2-5.
6. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the tower disc area is connected with the spraying area through the inverted cone-shaped reducing area; the tower diameter ratio of the tower tray area to the spraying area is 1.2-3.
7. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the demisting device is one or more of a cyclone demister, a wet electrostatic demister, a wire mesh demister or a baffling demister.
8. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the tray is one or a combination of a float valve tray, a sieve tray, a fixed tongue tray, a floating tongue tray or a three-dimensional mass transfer tray.
9. The flue gas dust removal desulfurization tower of claim 1, characterized in that: and a liquid distributor is arranged between the tower tray area and the demisting area, and is connected with a circulating clear liquid pipeline I and used for uniformly distributing circulating clear liquid on the tower tray.
10. The flue gas dust removal desulfurization tower of claim 1, characterized in that: one or more layers of spraying pipelines are arranged at the upper part of the spraying area; when a plurality of layers of spraying pipelines are arranged, the distance between the spraying pipelines is 0.5-5 m; the spraying pipeline is connected with a circulating clear liquid pipeline II and is provided with a plurality of atomizing nozzles; and the lower part of the spraying area is provided with a flue gas inlet I which is connected with a flue gas pipeline I.
11. The flue gas dust removal desulfurization tower of claim 1, characterized in that: one side of the oxidation flocculation area, which is close to the tower wall, is respectively connected with an alkaline solution pipeline I, a flocculating agent pipeline and a liquid level meter I; and the alkaline solution pipeline I is provided with a flow regulating valve.
12. The flue gas dust removal desulfurization tower of claim 1, characterized in that: one side of the circulating clear liquid zone, which is close to the tower wall, is connected with a fresh water pipeline, an alkaline solution pipeline II, an oxidizing gas pipeline and a liquid level meter II; a flow regulating valve is arranged on the fresh water pipeline; and the alkaline solution pipeline II is provided with a flow regulating valve for regulating the flow of the alkaline solution filled into the circulating clear liquid area.
13. The flue gas dust removal desulfurization tower of claim 12, wherein: the oxidizing gas pipeline is connected with the fan, extends to one side of the partition plate I of the circulating clear liquid zone and is connected with the oxidizing gas distribution pipe; the oxidizing gas distribution pipe is provided with a plurality of nozzles, and the nozzles are opposite to the filter medium on the partition plate I.
14. The flue gas dust removal desulfurization tower of claim 1, characterized in that: the bottom of the circulating clear liquid zone is connected with a clear liquid leading-out pipeline, the leading-out pipeline is divided into two paths, one path of pipeline is connected with an external clear liquid discharging pipeline, the other path of pipeline is connected with a circulating clear liquid pump, a pH meter is arranged on the pipeline, and the circulating clear liquid pump is connected with a circulating clear liquid pipeline I and a circulating clear liquid pipeline II through a cooler; the pH meter is used for measuring the pH value of the circulating clear liquid and feeding back a measurement signal to the regulating valve of the alkaline solution pipeline II through the controller.
15. A method for flue gas desulfurization and wastewater treatment in the flue gas dust removal desulfurization tower of any one of claims 1 to 14, characterized by comprising the following steps: (1) the flue gas enters the flue gas dust removal desulfurization tower in two ways, one way enters from the lower part of a spray zone of the flue gas dust removal desulfurization tower through a flue gas pipeline I, the other way enters from the bottom of an oxidation flocculation zone of the flue gas dust removal desulfurization tower through a flue gas pipeline II and passes through slurry in the oxidation flocculation zone, the two ways of flue gas are converged and then are in countercurrent contact with circulating clear liquid in the spray zone to remove most of dust and sulfur dioxide carried in the flue gas, the flue gas passing through the spray zone enters a tower panel zone, deep dust removal and desulfurization are carried out on the tower panel zone and the circulating clear liquid, the purified flue gas enters a flue gas discharge zone after being demisted in a demisting zone, the purified flue gas enters an outer sleeve from the top of a chimney and is fully mixed with air and then is discharged from the top of the flue gas discharge zone; (2) the desulfurization slurry absorbing dust and sulfur dioxide flows through the rotary impeller from the spraying area to enter the oxidation flocculation area from the liquid descending port at the lower part of the guide plate, when the desulfurization slurry flows down from the spraying area and passes through the rotary impeller, horizontal force is generated on blades of the rotary impeller, the gravitational potential energy of the desulfurization slurry is converted into kinetic energy, the rotary impeller is pushed to rotate around the rotary shaft and drives the stirring paddle fixed on the rotary shaft to rotate to stir the desulfurization slurry, the desulfurization slurry is fully mixed with oxidizing gas, flocculating agent and alkaline solution under the stirring action of the stirring paddle, sulfite in the desulfurization slurry is oxidized into sulfate, small particle dust in the desulfurization slurry is flocculated into large particles, and meanwhile, flue gas with certain temperature from a flue gas pipeline II enables moisture in the desulfurization slurry to be continuously volatilized, and the salt concentration is gradually increased; (3) the desulfurization slurry flows through a filter medium on a partition plate I to realize solid-liquid separation under the action of liquid level difference on two sides of the partition plate I, dust particles in the desulfurization slurry are filtered and left in an oxidation flocculation area, clear liquid enters a circulating clear liquid area, and the slurry after oxidation flocculation is led out from the bottom of the oxidation flocculation area and enters a subsequent treatment unit through an external slurry pipeline; (4) oxidizing gas enters from the circulating clear liquid zone, is sprayed out from a nozzle of the oxidizing gas distribution pipe and penetrates through the filter medium, dust particles on the filter medium of the oxidation flocculation zone are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and a flocculating agent are aggregated into large particles under the action of gravity and are deposited at the bottom of the oxidation flocculation zone, sulfite in the slurry is oxidized into sulfate by the oxidizing gas, and COD of the desulfurization wastewater reaches the standard; (5) the clear liquid which is filtered by the filter medium and enters the circulating clear liquid area is mixed with fresh water and alkaline solution in the circulating clear liquid area and then is led out from the bottom of the circulating clear liquid area, a small amount of clear liquid is directly discharged to reduce the salt concentration of the circulating clear liquid, the rest clear liquid enters the cooler after being pressurized by the circulating clear liquid pump, one part of the clear liquid cooled by the cooler enters the spraying area, is atomized by the atomizing nozzle and then is in countercurrent contact with the flue gas to remove dust and sulfur, the other part of the clear liquid flows through the liquid distributor and enters the tower disc area to be in full contact with the flue gas on the tower disc, and a large amount of micro fog drops carried by the spraying area are captured by the micro dust particles and the flue gas.
16. The method of claim 15, wherein: the flue gas in the step (1) is one or more of flue gas of a coal-fired boiler, flue gas of a coal-fired power plant, regenerated flue gas of a catalytic cracking catalyst, flue gas of a process heating furnace, coking flue gas or steel sintering flue gas.
17. The method of claim 15, wherein: the ratio of the amount of the flue gas entering the flue gas pipeline I to the amount of the flue gas entering the flue gas pipeline II is 20-500; the ratio of the circulating clear liquid to the flue gas in the spraying area is 5-50L/Nm3And the ratio of the circulating clear liquid to the flue gas in the tower tray area is 3-15L/Nm3。
18. The method of claim 15, wherein: the alkaline solution is selected from one or more of sodium hydroxide solution, calcium hydroxide solution, magnesium hydroxide solution, sodium carbonate solution, sodium sulfite solution, sodium citrate solution, limestone slurry, ammonia water or seawater.
19. The method of claim 15, wherein: the oxidizing gas is one or more of air, oxygen or ozone.
20. The method of claim 15, wherein: the flocculating agent is one or more of aluminum sulfate, alum, sodium aluminate, ferric trichloride, ferrous sulfate, ferric sulfate, polyaluminum chloride, polyaluminum sulfate, polyaluminum phosphate, polyaluminum chloride, polyferric sulfate, polyaluminum phosphate, polyphosphazene chloride, polyaluminum phosphate chloride, polysilicate iron, polysilicate ferric sulfate, polyaluminum sulfate silicate, polyaluminum ferric sulfate chloride, polyaluminum ferric silicate flocculating agent, aluminum-iron copolymerization composite flocculating agent, polysilicate flocculating agent or polyacrylamide flocculating agent.
21. The method of claim 15, wherein: the pH value of the slurry after the oxidative flocculation concentration is controlled to be 7-9, the pH on-line detector is positioned on an outer slurry discharge pipeline, and the pH value of the desulfurization slurry is controlled by adjusting an adjusting valve on an alkaline solution pipeline I.
22. The method of claim 15, wherein: the liquid level difference of the two sides of the partition plate I is 0.5-6 m, and the liquid level of the oxidation flocculation area is higher than that of the circulating clear liquid area.
23. The method of claim 15, wherein: the liquid level height of the oxidation flocculation area is controlled by an adjusting valve on an external slurry discharge pipeline.
24. The method of claim 15, wherein: and the flushing water spray pipe of the oxidation flocculation area regularly flushes the filter medium on the partition plate I, and the flushing time interval is 0.5-2 h.
25. The method of claim 15, wherein: the liquid level height of the circulating clear liquid area is controlled by an adjusting valve on a fresh water pipeline.
26. The method of claim 15, wherein: the pH value of the circulating clear liquid area is controlled to be 6-11, the pH on-line detector is positioned on an inlet pipeline of a tower bottom circulating pump, and the pH value of the circulating clear liquid is controlled by adjusting an adjusting valve on an alkaline solution pipeline II.
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