CN106621808A - Wet type integrated purification system and method for recovery of residual heat in flue gas - Google Patents
Wet type integrated purification system and method for recovery of residual heat in flue gas Download PDFInfo
- Publication number
- CN106621808A CN106621808A CN201710001638.0A CN201710001638A CN106621808A CN 106621808 A CN106621808 A CN 106621808A CN 201710001638 A CN201710001638 A CN 201710001638A CN 106621808 A CN106621808 A CN 106621808A
- Authority
- CN
- China
- Prior art keywords
- wet type
- flue gas
- slurries
- desulphurization denitration
- denitration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 85
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000011084 recovery Methods 0.000 title claims abstract description 18
- 238000000746 purification Methods 0.000 title claims abstract description 17
- 239000000428 dust Substances 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims abstract description 21
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 8
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 8
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910052753 mercury Inorganic materials 0.000 claims abstract description 8
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 7
- 230000000694 effects Effects 0.000 claims abstract description 6
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000002002 slurry Substances 0.000 claims description 134
- 238000006477 desulfuration reaction Methods 0.000 claims description 92
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 33
- 230000008929 regeneration Effects 0.000 claims description 33
- 238000011069 regeneration method Methods 0.000 claims description 33
- 239000000779 smoke Substances 0.000 claims description 32
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical group [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 22
- 238000010521 absorption reaction Methods 0.000 claims description 18
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 15
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 14
- 238000005119 centrifugation Methods 0.000 claims description 13
- 206010022000 influenza Diseases 0.000 claims description 13
- 239000002918 waste heat Substances 0.000 claims description 13
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 12
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 12
- 239000003517 fume Substances 0.000 claims description 12
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 11
- 235000010265 sodium sulphite Nutrition 0.000 claims description 11
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 10
- 238000012545 processing Methods 0.000 claims description 10
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 claims description 10
- 230000023556 desulfurization Effects 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 9
- 230000001172 regenerating effect Effects 0.000 claims description 9
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 8
- 230000008014 freezing Effects 0.000 claims description 8
- 238000007710 freezing Methods 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 7
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 7
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 7
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 7
- 238000002425 crystallisation Methods 0.000 claims description 7
- 230000008025 crystallization Effects 0.000 claims description 7
- ZGTMUACCHSMWAC-UHFFFAOYSA-L EDTA disodium salt (anhydrous) Chemical compound [Na+].[Na+].OC(=O)CN(CC([O-])=O)CCN(CC(O)=O)CC([O-])=O ZGTMUACCHSMWAC-UHFFFAOYSA-L 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 6
- 239000006227 byproduct Substances 0.000 claims description 6
- 230000001351 cycling effect Effects 0.000 claims description 6
- 239000011790 ferrous sulphate Substances 0.000 claims description 6
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 6
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 6
- 239000000395 magnesium oxide Substances 0.000 claims description 6
- 239000011259 mixed solution Substances 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 230000008439 repair process Effects 0.000 claims description 6
- 230000003252 repetitive effect Effects 0.000 claims description 6
- 239000012047 saturated solution Substances 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 6
- 235000011152 sodium sulphate Nutrition 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 239000005864 Sulphur Substances 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 5
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000292 calcium oxide Substances 0.000 claims description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 5
- UEUXEKPTXMALOB-UHFFFAOYSA-J tetrasodium;2-[2-[bis(carboxylatomethyl)amino]ethyl-(carboxylatomethyl)amino]acetate Chemical compound [Na+].[Na+].[Na+].[Na+].[O-]C(=O)CN(CC([O-])=O)CCN(CC([O-])=O)CC([O-])=O UEUXEKPTXMALOB-UHFFFAOYSA-J 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 4
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims description 3
- 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 claims description 3
- 239000000356 contaminant Substances 0.000 claims description 3
- -1 dirt Chemical compound 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 3
- BHZRJJOHZFYXTO-UHFFFAOYSA-L potassium sulfite Chemical compound [K+].[K+].[O-]S([O-])=O BHZRJJOHZFYXTO-UHFFFAOYSA-L 0.000 claims description 3
- 235000019252 potassium sulphite Nutrition 0.000 claims description 3
- 238000003303 reheating Methods 0.000 claims description 3
- 239000011734 sodium Substances 0.000 claims description 3
- 229910052708 sodium Inorganic materials 0.000 claims description 3
- 239000012265 solid product Substances 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- 239000003610 charcoal Substances 0.000 claims description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims 1
- 239000011440 grout Substances 0.000 claims 1
- 229910052742 iron Inorganic materials 0.000 claims 1
- 229910017604 nitric acid Inorganic materials 0.000 claims 1
- 239000001301 oxygen Substances 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000005054 agglomeration Methods 0.000 abstract 1
- 230000002776 aggregation Effects 0.000 abstract 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 abstract 1
- 238000010531 catalytic reduction reaction Methods 0.000 abstract 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 abstract 1
- 239000003292 glue Substances 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 abstract 1
- 239000002699 waste material Substances 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000000945 filler Substances 0.000 description 13
- 238000012856 packing Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 230000006378 damage Effects 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- WWILHZQYNPQALT-UHFFFAOYSA-N 2-methyl-2-morpholin-4-ylpropanal Chemical compound O=CC(C)(C)N1CCOCC1 WWILHZQYNPQALT-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000010410 dusting Methods 0.000 description 2
- 239000011859 microparticle Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 231100000567 intoxicating Toxicity 0.000 description 1
- 230000002673 intoxicating effect Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- SJZFFCZQDPVHQI-UHFFFAOYSA-N potassium;sulfurous acid Chemical compound [K].OS(O)=O SJZFFCZQDPVHQI-UHFFFAOYSA-N 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
-
- 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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- 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
- B01D53/64—Heavy metals or compounds thereof, e.g. mercury
-
- 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
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/608—Sulfates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/90—Chelants
- B01D2251/902—EDTA
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/70—Non-metallic catalysts, additives or dopants
- B01D2255/702—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Biomedical Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a wet type integrated purification system and method for recovery of residual heat in flue gas. The system comprises a flue gas cooling and heat exchange device (1), a flue gas dedusting device (2), a pressurizing fan (3), a wet type pre-desulfurizing and denitration device, a flue gas reheater (9), and a wet type deep desulfurizing and denitration device. The system has the advantages that the dust, nitrogen oxide, sulfur oxide, particulate dust, mercury and other heavy metals in the flue gas are simultaneously removed at low temperature, and NOx in glue gas is changed into harmless N2 and discharged; the problems of ammonia escape, agglomeration and blockage of ammonium bisulfate, difficulty in disposal of failed SCR (selective catalytic reduction) catalyst as dangerous wastes and the like due to an SCR high-temperature denitration technique are solved; meanwhile, the residual heat in the flue gas is recovered and reutilized, the integrated purification treatment benefit of the flue gas is further improved, and the energy-saving and emission-reduction effects are realized.
Description
Technical field
The invention belongs to a kind of flue gas waste heat recovery wet type in energy-conserving and environment-protective field, particularly Air Pollution Control field
The processing system and its purification method of flue gas integrated purifying.
Background technology
The pollution of acid rain and its harm for causing have become one of main Environmental Problems of countries in the world concern.SO2And NOx
It is that discharge capacity is most, two kinds of pollution sources that harmfulness is maximum.Nitrogen oxides can also be formed photochemical pollution, produce greenhouse effects,
Damage the ozone layer, have intoxicating to act on to human body.
In recent years in the practice to the smoke pollution emission control engineering such as coal-burning boiler, Industrial Stoves, each side is gradually
Recognize to smoke pollution emission control be used alone dedusting, desulphurization and denitration technology, such as by SNCR and SCR carry out denitration,
Electric precipitation (or electric bag dust or bag-type dusting), wet desulphurization (having part dry method and semi-dry desulphurization), wet-esp or pipe
Beam formula demisting dedusting etc. is difficult to meet the environment protection emission requirement for increasingly improving, and dedusting, desulphurization and denitration and removing Hg is used alone
Deng the control technology of the hazardous contaminants such as heavy metal, there is equipment complexity, difficult in maintenance, floor space is big, invest and transport
The difficulties such as row expense height.
Therefore, in consideration of it, being necessary to provide a kind of new gas pollution control technology with flue gas integrated purifying function
To adapt to growing energy-conservation and environment protection emission requirement.
The content of the invention
The present invention in order to overcome prior art in wet desulphurization SCR or SNCR must be coordinated to can be only achieved NOxDischarge will
The deficiency asked, SNCR denitration is inefficient can not to meet emission request, SCR catalyst poisoning and deactivation, the escaping of ammonia and SCR catalysis
Agent regeneration intractability is big, harm is big, and dead catalyst can only treat as the problems such as danger is useless to be processed, and after-cost is high, while
In order to effectively mitigate because SCR catalyst is to the SO in flue gas2Oxidation causes SO in flue gas3Generation greatly improve, so as to produce more
The series of problems such as many ammonium hydrogen sulfate blocking air preheaters, there is provided a kind of Wet smoke integrated purifying processing system and its purification side
Method.
For achieving the above object, the technical scheme taken of the present invention is：
A kind of flue gas waste heat recovery wet method integrated purifying processing system, including flue gas cool-down heat-exchanger rig, flue gas ash removal dress
Put, booster fan, the pre- desulfuring and denitrifying apparatus of wet type, smoke re-heater, wet type deep desulfuration denitrification apparatus, wherein,
The pre- desulfuring and denitrifying apparatus of wet type include alkali liquor absorption slurries preparation unit, slurry storage tank, slurry feeding pump, wet type
Pre- desulphurization denitration tower；
Wet type deep desulfuration denitrification apparatus include that denitration absorbing liquor is prepared and storage element, denitration liquid delivery pump, wet type depth
Degree desulphurization denitration tower, circulating pump, saturation slurries regeneration unit；
The flue gas cool-down heat-exchanger rig, fume dust remover, booster fan, smoke re-heater, the pre- desulphurization denitration of wet type
Tower, wet type deep desulfuration denitrating tower, saturation slurries regeneration unit pass sequentially through flue or pipeline connection；It is prepared by alkali liquor absorption slurries
The pre- desulphurization denitration tower of unit, slurry storage tank, slurry feeding pump, wet type is sequentially connected；Denitration absorbing liquor is prepared and storage element
It is connected with wet type deep desulfuration denitrating tower by circulating pump；Saturation slurries regeneration unit is by denitration liquid delivery pump and wet type depth
Desulphurization denitration tower is connected to form circulation.
Further, the wet type deep desulfuration denitrating tower top arranges dedusting demister, and the dedusting demister is flat board
Formula demister, ridge type demister, bundled tube dedusting demister or electrostatic bundled tube dedusting demister.
Further, the flue gas cool-down heat-exchanger rig is gas-liquid heat-exchange or gas-gas heat exchanger.
Further, the smoke re-heater is gas-gas heat exchanger.
A kind of purification method based on the flue gas waste heat recovery wet method integrated purifying processing system, it is characterised in that bag
Include following steps：
Step 1：Will be containing heavy metal contaminants such as oxysulfide, nitrogen oxides, dirt, mercury using flue gas cool-down heat-exchanger rig
Flue-gas temperature 180 DEG C of ＜ is reduced to for 180 DEG C by ＞；
Step 2：The dust in the flue gas after cooling is removed using fume dust remover；
Step 3：Smoke re-heater will be sent into using booster fan after the flue gas supercharging after dedirt, flue gas Jing exchanges heat again drop
The pre- desulphurization denitration tower of wet type is returned to after temperature, pre- desulphurization denitration is carried out, the desulfuration efficiency of the pre- desulphurization denitration tower of wet type is controlled 40%
Wet type deep desulfuration denitrating tower is entered back into smoke re-heater heat exchange Jing flues Jing after intensification reheating after～98%, is carried out continuously
It is changed into neat stress Jing flues after desulphurization denitration demisting, depth dust removal process and enters smoke stack emission；
Step 4：In wet type deep desulfuration denitrating tower the slurries of slurry pool Jing after desulphurization denitration can gradually saturation, after saturation
Absorption slurries send into desulphurization denitration saturation slurries regeneration unit, the desulphurization denitration slurries of Jing reducing/regeneratings continue to return wet type
Recycle in deep desulfuration denitrating tower；
Step 5：Desulphurization denitration slurries in wet type deep desulfuration denitrating tower are with constantly recycling, the sulfuric acid in slurries
Root can build up, when in desulphurization denitration slurries sulfate concentration reach >=1.0mol/L after, using saturation slurries regeneration unit
The 20%-50% of saturation slurries is carried out into discharge opeing process, the solid product of sulphite or sulfate is isolated, the liquid isolated
State slurries are returned in desulphurization denitration saturated solution regenerative system Jing after regeneration, modulation, enter into wet type deep desulfuration denitrating tower weight
It is multiple to recycle.
Further, the fume dust remover after exchanging heat in the step 2 is electric cleaner, electrostatic fabric filter or bag-type dusting
Device.
Further, the absorption slurries in the pre- desulphurization denitration tower of wet type are alkaline slurry, specially desulfurization alkaline slurry, including
Ammonia spirit, calcium oxide, calcium carbonate, magnesia and sodium carbonate, NaOH.
Further, the desulphurization denitration slurries in depth wet type desulfurizing denitrating tower are ferrous salt, sulphite, the mixing of EDTA
Solution, specific ferrous salt be ferrous sulfate, frerrous chloride, ferrous nitrate, sulphite be sodium sulfite, potassium sulfite,
EDTA is EDTA-2Na and EDTA-4Na.
Further, desulphurization denitration slurries include catalyst in the wet type deep desulfuration denitrating tower, and the catalyst is powder
Last activated carbon, its pH value is not less than 7, and 200 ㎡ of specific surface area/g～1100 ㎡/g, granularity is 80 mesh～400 mesh, and its addition is
0.0%wt～1.0%wt.
Further, deep desulfuration denitration saturation slurries regeneration temperature is in wet type deep desulfuration denitrating tower in the step 5
40 DEG C～80 DEG C, recovery time 15min～90min.
Further, activity is added in the desulphurization denitration slurries regenerative process in the step 5 wet type deep desulfuration denitrating tower
Charcoal makees catalyst, and activated carbon addition is 1.0%wt～5.0%wt, and the pH value of activated carbon is 2～11, and 200 ㎡ of specific surface/g～
500 ㎡/g, wear-resisting intensity is not less than 85%.
Further, start to part as sulfate concentration >=1mol/L in saturation desulphurization denitration slurries in the step 5
Desulphurization denitration slurries carry out separating treatment, separate using centrifugation after evaporative crystallization concentration or using centrifugation point after freezing and crystallizing
From mode.
Further, source, evaporative crystallization concentration are adjusted as pH value using ammoniacal liquor in deep desulfuration denitrating tower in the step 4
The mixture of solid byproducts ammonium sulfate or ammonium sulfite and ammonium sulfate is centrifuged out afterwards.
Further, source, freezing and crystallizing are adjusted as system pH value using soda in deep desulfuration denitrating tower in the step 4
Centrifugation afterwards goes out the mixture of solid byproducts sodium sulphate or sodium sulphate and sodium sulfite.
The invention has the beneficial effects as follows：
Remove simultaneously under the achievable low-temperature condition of the present invention dirt in flue gas, nitrogen oxides, oxysulfide, microparticle dirt and
The purpose of the heavy metals such as mercury, can become harmless N by the NOx in flue gas2Discharge.Avoid because using SCR high temperature denitration technologies
The escaping of ammonia that brings, the blocking of ammonium hydrogen sulfate caking and the SCR catalyst that fails the difficult problem such as are difficult to dispose as danger is useless, while because right
The recycling that waste heat in flue gas has been carried out, further improves the benefit of flue gas integrated purifying process, has reached both energy-conservations
The effect for reducing discharging again.
Description of the drawings
Fig. 1 is the system composition schematic diagram of the present invention.
Specific embodiment
Such as Fig. 1, a kind of flue gas waste heat recovery Wet smoke integrated purifying system of the present invention, including flue gas cool-down heat exchange dress
Put 1, fume dust remover 2, the pre- desulfuring and denitrifying apparatus of booster fan 3, wet type, smoke re-heater 9, wet type deep desulfuration denitration dress
Put, wherein,
The pre- desulfuring and denitrifying apparatus of wet type include alkali liquor absorption slurries preparation unit 4, slurry storage tank 5, slurry feeding pump 6,
The pre- desulphurization denitration tower 7 of wet type；
Wet type deep desulfuration denitrification apparatus include that denitration absorbing liquor is prepared and storage element 12, denitration liquid delivery pump 13, wet
Formula deep desulfuration denitrating tower 8, circulating pump 10, saturation slurries regeneration unit 11；
Flue gas cool-down heat-exchanger rig 1, fume dust remover 2, booster fan 3, the pre- desulphurization denitration of smoke re-heater 9, wet type
Tower 7, wet type deep desulfuration denitrating tower 8, saturation slurries regeneration unit 11 pass sequentially through flue or pipeline connection；Alkali liquor absorption slurries
The pre- desulphurization denitration tower 7 of preparation unit 4, slurry storage tank 5, slurry feeding pump 6, wet type is sequentially connected；Denitration absorbing liquor prepare and
Storage element 12 is connected by circulating pump 10 with wet type deep desulfuration denitrating tower 8；Saturation slurries regeneration unit 11 passes through denitration liquid
Delivery pump 13 is connected to form circulation with wet type deep desulfuration denitrating tower 8.
The pre- desulphurization denitration tower 7 of wet type can be equipped with rotation converge coupled desulfurization tower (SPC-3D), can be spray column, can also
It is bubble tower, wet type desulfurizing denitrating tower is provided with multiple stage circulation slurry pump, can meets according to wet type desulfurizing denitrating tower exiting flue gas
Middle SO2Concentration carries out the requirement of real-time regulation control.Absorption slurries in the pre- desulphurization denitration tower 7 of wet type are alkaline slurry, specifically
For desulfurization alkaline slurry, including ammonia spirit, calcium oxide, calcium carbonate, magnesia and sodium carbonate, NaOH
Wet type deep desulfuration denitrating tower 8 includes the rotation remittance coupling device (patent No. arranged from bottom to top：
CN201735324U), packing layer, equal liquid distributor and dedusting demister.Wherein packing layer is multilayer, is arranged on every layer of packing layer
One efficiently equal liquid distributor.Desulphurization denitration slurries in depth wet type desulfurizing denitrating tower in 8 bottom slurry ponds are ferrous salt, Asia
The mixed solution of sulfate, EDTA and catalyst, specific ferrous salt be ferrous sulfate, frerrous chloride, ferrous nitrate, sulfurous
Hydrochlorate is sodium sulfite, potassium sulfite, and EDTA is EDTA-2Na and EDTA-4Na.Catalyst is Powdered Activated Carbon, and its pH value is not
Less than 7,200 ㎡ of specific surface area/g～1100 ㎡/g, granularity is 80 mesh～400 mesh, and its addition is 0.0%wt～1.0%wt.
Catalyst can be added in above-mentioned desulphurization denitration slurries can also be without.
Saturation slurries regeneration unit 11 includes evaporation concentration device or freezing and crystallizing device and centrifugal separating device, is used for
Isolate the solid-states such as sulphite or sulfate in the desulphurization denitration slurries in the bottom slurry pond of wet type deep desulfuration denitrating tower 8
Product.The liquid slurry isolated returns to repetitive cycling in wet type deep desulfuration denitrating tower 8 and uses by denitration liquid delivery pump 13.
Prepared by denitration absorbing liquor and storage element 12 is used to prepare storage desulphurization denitration slurries, using circulating pump 10 by desulphurization denitration slurries
In being transported to wet type deep desulfuration denitrating tower 8.
It is capable of achieving under low-temperature condition to remove dirt in flue gas, nitrogen oxides, sulphur oxidation simultaneously by the cleaning system of the present invention
The purpose of the heavy metals such as thing, microparticle dirt and mercury, can become harmless N by the NO in flue gas2Discharge.Simultaneously because in flue gas
Waste heat recycled, further improve the benefit of flue gas integrated purifying process, the again reduction of discharging that reached not only energy-conservation
Effect.
From the spherical hollow ball dumped packing of PP materials, specific surface is 50 ㎡/m to the filler of packing layer3～800 ㎡/m3,
Bulk density is bulk density 20kg/m3～200kg/m3, 2～6 layers of filler filling, per layer height about 0.1m～1.5m, per layer is filled out
The efficiently equal liquid distributor of material top arrangement.
Dedusting demister can be plate-type dedusting demister, ridge type dedusting demister, or bundled tube dedusting is removed
Day with fog, or electrostatic bundled tube dedusting demister, the preferred bundled tube dedusting demister (patent No.：CN 104368215B)
Or electrostatic bundled tube dedusting demister (application number CN201620105537.9).
High temperature original flue gas enters flue gas cool-down heat-exchanger rig 1 by flue, and flue gas is removed after heat exchange cooling into flue gas
Dirt device 2, the flue gas after removing dust enters booster fan 3 by flue, and flue gas enters flue gas reheat Jing after the supercharging of booster fan 3
Device 9, subsequently into the pre- desulphurization denitration tower 7 of wet type, flue gas enters smoke re-heater 9 and then enters Jing after the pre- desulphurization denitration of wet type is processed
Enter wet type deep desulfuration denitrating tower 8, the pre- desulphurization denitration tower 7 of wet type and wet type deep desulfuration denitrating tower 8 and smoke re-heater 9 are point
It is body, or merging into a single whole.Smoke re-heater 9 is gas-gas heat exchanger.
Alkali liquor absorption slurries preparation unit 4 is prepared and absorbs slurries, and absorption slurries are alkaline slurry, specially desulfurization alkalescence slurry
Liquid, including ammonia spirit, calcium oxide, calcium carbonate, magnesia and sodium carbonate, NaOH.Absorb slurries and be transported to slurries
Holding vessel 5, is transported to the slurries for preparing in the slurry pool of the pre- desulphurization denitration tower 7 of wet type by slurry feeding pump 6.
A kind of purification method based on the flue gas waste heat recovery wet method integrated purifying processing system, comprises the following steps：
Step 1：Will be containing heavy metal pollutions such as oxysulfide, nitrogen oxides, dirt, mercury using flue gas cool-down heat-exchanger rig 1
The flue-gas temperature of thing is reduced to 180 DEG C of ＜ for 180 DEG C by ＞；
Step 2：The dust in the flue gas after cooling is removed using fume dust remover 2；Fume dust remover 2 is removed for electricity
Dirt device, electrostatic fabric filter or sack cleaner；
Step 3：Smoke re-heater 9 will be sent into after the flue gas supercharging after dedirt using booster fan 3, flue gas Jing exchanges heat again
The pre- desulphurization denitration tower 7 of wet type is returned to after cooling, pre- desulphurization denitration is carried out, the desulfuration efficiency for controlling the pre- desulphurization denitration tower 7 of wet type exists
Wet type deep desulfuration denitrating tower 8 is entered back into the heat exchange Jing flues Jing after intensification reheating of smoke re-heater 9 after 40%～98%, even
It is continuous to carry out being changed into neat stress Jing flues after desulphurization denitration demisting, depth dust removal process entering smoke stack emission.
Absorption slurries in the pre- desulphurization denitration tower 7 of wet type are alkaline slurry, and specially desulfurization alkaline slurry, including ammoniacal liquor is molten
Liquid, calcium oxide, calcium carbonate, magnesia and sodium carbonate, NaOH.
8 desulphurization denitration slurries are ferrous salt, sulphite, EDTA and catalyst in depth wet type desulfurizing denitrating tower
Mixed solution, specific ferrous salt is ferrous sulfate, frerrous chloride, ferrous nitrate, and sulphite is sodium sulfite, sulfurous acid
Potassium, EDTA is EDTA-2Na and EDTA-4Na.Catalyst is Powdered Activated Carbon, and its pH value is not less than 7,200 ㎡ of specific surface area/g
～1100 ㎡/g, granularity is 80 mesh～400 mesh, and its addition is 0.0%wt～1.0%wt.
Step 4：In wet type deep desulfuration denitrating tower 8 slurries of slurry pool Jing after desulphurization denitration can gradually saturation, by saturation
Absorption slurries afterwards are sent into desulphurization denitration saturation slurries regeneration unit 11, and the desulphurization denitration slurries of Jing reducing/regeneratings continue to return
Recycle in wet type deep desulfuration denitrating tower 8.
When source is adjusted as system pH value using ammoniacal liquor in deep desulfuration denitrating tower 8, then concentrated using evaporative crystallization laggard
Row centrifugation goes out the mixture of solid byproducts ammonium sulfate or ammonium sulfite and ammonium sulfate；When adopting in deep desulfuration denitrification apparatus
Adjust source as system pH value with soda, then using centrifugation after freezing and crystallizing go out solid byproducts sodium sulphate or sodium sulphate and
The mixture of sodium sulfite.
Step 5：Desulphurization denitration slurries in wet type deep desulfuration denitrating tower 8 are with constantly recycling, the sulphur in slurries
Acid group can build up, when in desulphurization denitration slurries sulfate concentration reach >=1.0mol/L after, it is single using the regeneration of saturation slurries
The 20%-50% of saturation slurries is carried out discharge opeing process by unit 11, is separated using centrifugation after evaporative crystallization concentration or using cold
Freeze centrifugation mode after crystalline substance.The solid product of sulphite or sulfate is isolated, the liquid slurry isolated returns to de-
In sulphur denitration saturated solution regenerative system Jing after regeneration, modulation, enter into repetitive cycling in wet type deep desulfuration denitrating tower 8 and use.
Deep desulfuration denitration saturation slurries regeneration temperature is 40 DEG C～80 DEG C in wet type deep desulfuration denitrating tower 8, during regeneration
Between 15min～90min.Add activated carbon in desulphurization denitration slurries regenerative process and make catalyst, activated carbon addition is 1.0%wt
～5.0%wt, the pH value of activated carbon is 2～11, and 200 ㎡ of specific surface/g～500 ㎡/g, wear-resisting intensity is not less than 85%.
Embodiment 1
Containing 5300mg/Nm3SO2、NOxAbout 600mg/Nm3、29g/Nm3Dirt and 0.041mg/Nm3Mercury, 380 DEG C of combustion
Coal burning boiler high-temperature flue gas, first Jing flue gas cool-downs heat-exchanger rig 1 carries out heat exchange and cools to 140 DEG C, carries out entering flue gas after recuperation of heat
Dust arrester 2, then smoke re-heater 9 (being herein gas-gas heat exchanger) is sent into Jing after booster fan 3 carries out secondary heat exchange, flue gas
Jing flues enter the pre- desulphurization denitration tower 7 of wet type, flue gas flue gas Jing Jing after the process of pre- desulphurization denitration after further cooling to about 90 DEG C
Flue carries out entering deep desulfuration denitrating tower after flue gas is warmed up to about 90 DEG C into smoke re-heater 9 (being herein gas-gas heat exchanger)
In 8, smoke stack emission is entered for neat stress Jing flues Jing after deep desulfuration denitration, dedusting demisting.
In wet type deep desulfuration denitrating tower filler from PP materials spherical hollow ball dumped packing, specific surface be 300 ㎡/
m3, bulk density is bulk density 50kg/m3, filler loads 6 layers, and per layer height about 0.4m, every layer of filler top arrangement is efficiently
Liquid distributor.
Slurries are the slurries of lime stone or lime in pre- system for desulfuration and denitration, by control ph between 5～6, control
Liquid-gas ratio be 8～18, so as to control pre- desulphurization denitration tower in desulfuration efficiency be 60%～95%, in the present embodiment pH value control exist
5.8, when liquid-gas ratio is 12, desulfuration efficiency is 90%.
Desulphurization denitration slurries in wet type deep desulfuration denitrating tower 8 are ferrous sulfate, sodium sulfite, EDTA-2Na and ratio
The activated carbon mixed solution of 325 mesh of 450 ㎡ of surface/g, the addition of activated carbon is 0.15%wt.Sodium carbonate is adopted for depth
PH value in system for desulfuration and denitration adjusts source.
When in wet type deep desulfuration denitrating tower desulphurization denitration slurries gradually saturation loses desulphurization denitration ability when, start to full
Regeneration process is carried out with desulphurization denitration slurries, 80 DEG C of regeneration temperature, recovery time 15min regenerates slurry pH value 6.7, saturation slurry
Add 400 ㎡ of specific surface/g, the activated carbon 2%wt of 200 mesh in liquid regenerative process.
As sulfate concentration about 1.51mol/L in saturation desulphurization denitration slurries, desulphurization denitration saturated absorption liquid is carried out
Discharge opeing is processed, and the saturation desulphurization denitration slurries of about a quarter is carried out into freezing and crystallizing, centrifugation and goes out sodium sulfite and sulfuric acid
The mixture of sodium is accessory substance, and the liquid slurry isolated is returned in desulphurization denitration saturated solution regenerative system Jing after regeneration, modulation,
Enter into repetitive cycling in wet type deep desulfuration denitrification apparatus to use.
In the above-described example, the discharge index of neat stress is 27mg/Nm3SO2、49mg/Nm3NOx, 4.1mg/Nm3's
Dirt, 0.019mg/Nm3Mercury.
Embodiment 2
Containing 3987mg/Nm3SO2、NOxAbout 1035mg/Nm3、17g/Nm3245 DEG C of dirt coking high-temperature flue gas, first Jing cigarettes
Gas temperature-reducing heat-exchange device 1 (herein using gas-liquid heat exchange device) carries out heat exchange and cools to 120 DEG C, carries out entering flue gas after recuperation of heat
Dust arrester 2, then smoke re-heater 9 (gas-gas heat exchanger) is sent into Jing after booster fan 3 carries out secondary heat exchange, and flue gas is further
Jing flues enter the pre- desulphurization denitration tower 7 of wet type after cooling to about 76 DEG C, and flue gas flue gas Jing flues Jing after the process of pre- desulphurization denitration enter
Entering smoke re-heater 9 (gas-gas heat exchanger) carries out entering after flue gas is warmed up to about 76 DEG C in deep desulfuration denitrating tower 8, and Jing depth takes off
Smoke stack emission is entered after sulphur denitration, dedusting demisting for neat stress Jing flues.
From the regular corrugation plate filler of PP materials, specific surface is 500 ㎡/m to filler in wet type deep desulfuration denitrating tower3,
Bulk density is bulk density 120kg/m3, filler loads 2 layers, and per layer height about 1.2m, every layer of filler top arrangement is efficiently
Liquid distributor.
In pre- desulphurization denitration tower slurries be deposed ammonia solution, by control ph 5.7～7.5, control liquid-gas ratio be 3～
10, so as to control pre- desulphurization denitration tower in desulfuration efficiency be 50%～90%.PH value control is 7.1 in the present embodiment, liquid-gas ratio
For 5 when, desulfuration efficiency is 88%.
Desulphurization denitration slurries in wet type deep desulfuration denitrating tower are ferrous sulfate, sodium sulfite, EDTA-2Na and ratio
The activated carbon mixed solution of 325 mesh of 670 ㎡ of surface/g, the addition of activated carbon is 0.10%wt.Deposed ammonia is adopted for depth
PH value in system for desulfuration and denitration adjusts source.
When in wet type deep desulfuration denitrating tower desulphurization denitration slurries gradually saturation loses desulphurization denitration ability when, start to full
Regeneration process is carried out with desulphurization denitration slurries, 60 DEG C of regeneration temperature, recovery time 35min regenerates slurry pH value 6.37, saturation slurry
Add 220 ㎡ of specific surface/g, the activated carbon 5%wt of 325 mesh in liquid regenerative process.
As sulfate concentration about 2.6mol/L in saturation desulphurization denitration slurries, desulphurization denitration saturated absorption liquid is arranged
About 1/3rd saturation desulphurization denitration slurries are evaporated crystallization, centrifugation and go out the mixture of ammonium sulfate and are by liquid process
Accessory substance, the liquid slurry isolated return in desulphurization denitration saturated solution regenerative system Jing regeneration, modulation after, enter into wet type depth
Repetitive cycling is used in degree desulfuring and denitrifying apparatus.
In the above-described example, the discharge index of neat stress is 82mg/Nm3SO2、100mg/Nm3NOx、10mg/Nm3's
Dirt.
Embodiment 3
Containing 2870mg/Nm3SO2、NOxAbout 374mg/Nm3、19g/Nm3325 DEG C of dirt sintering flue gas, first Jing flue gases drop
Warm heat-exchanger rig gas-liquid heat-exchange 1 carries out heat exchange and cools to 180 DEG C, carries out entering fume dust remover 2, Ran Houjing after recuperation of heat
Smoke re-heater gas-gas heat exchanger 9 is sent into after booster fan 3 carries out Jing cigarettes after secondary heat exchange flue gas further cools to about 95 DEG C
Road enters the pre- desulphurization denitration tower 7 of wet type, and flue gas flue gas Jing flues Jing after the process of pre- desulphurization denitration are changed into smoke re-heater gas gas
Hot device 9 carries out being entered in deep desulfuration denitrating tower 8 after flue gas is warmed up to 95 DEG C, is net Jing after deep desulfuration denitration, dedusting demisting
Flue gas Jing flues enter smoke stack emission.
From the regular corrugation plate filler of PP materials, specific surface is 200 ㎡/m to filler in wet type deep desulfuration denitrating tower3,
Bulk density is bulk density 45kg/m3, filler loads 3 layers, and per layer height about 0.7m, every layer of filler top arrangement is efficiently uniform
Liquid device.
Slurries are magnesium oxide solution in pre- system for desulfuration and denitration, and control ph controls liquid-gas ratio for 3 between 5.4～7.2
～17, it is 40%～98% to control desulfuration efficiency in pre- desulphurization denitration tower；PH value is controlled 5.4 in the present embodiment, and liquid-gas ratio is 3
When, desulfuration efficiency is 98%.
Desulphurization denitration slurries in wet type deep desulfuration denitrating tower are frerrous chloride, sodium sulfite, EDTA-4Na and ratio
The activated carbon mixed solution of 120 mesh of 800 ㎡ of surface/g, the addition of activated carbon is 0.35%wt.NaOH is adopted for deep
PH value in degree system for desulfuration and denitration adjusts source.
When in wet type deep desulfuration denitrating tower desulphurization denitration slurries gradually saturation loses desulphurization denitration ability when, start to full
Enter with desulphurization denitration slurries.Row regeneration is processed, 60 DEG C of regeneration temperature, recovery time 35min, regenerates slurry pH value 6.37, saturation
Add 500 ㎡ of specific surface/g, the activated carbon 2.8%wt of 325 mesh in slurries regenerative process.
As sulfate concentration about 1.0mol/L in saturation desulphurization denitration slurries, desulphurization denitration saturated absorption liquid is arranged
About 1/5th saturation desulphurization denitration slurries are carried out freezing and crystallizing, centrifugation and go out sodium sulfite accessory substance by liquid process, point
The liquid slurry for separating out return in desulphurization denitration saturated solution regenerative system Jing regeneration, modulation after, enter into wet type deep desulfuration take off
Repetitive cycling is used in nitre device.
In the above-described example, the discharge index of neat stress is NOx, 5mg/Nm3 of SO2,49mg/Nm3 of 18mg/Nm3
Dirt.
The foregoing is only presently preferred embodiments of the present invention, not to limit the present invention, all spirit in the present invention and
Within principle, any modification, equivalent substitution and improvements made etc. should be included within the scope of the present invention.
Claims (14)
1. a kind of flue gas waste heat recovery wet method integrated purifying processing system, it is characterised in that including flue gas cool-down heat-exchanger rig
(1), fume dust remover (2), booster fan (3), the pre- desulfuring and denitrifying apparatus of wet type, smoke re-heater (9), wet type deep desulfuration
Denitrification apparatus, wherein,
The pre- desulfuring and denitrifying apparatus of wet type include alkali liquor absorption slurries preparation unit (4), slurry storage tank (5), slurry feeding pump
(6), the pre- desulphurization denitration tower (7) of wet type；
Wet type deep desulfuration denitrification apparatus include that denitration absorbing liquor is prepared and storage element (12), denitration liquid delivery pump (13), wet
Formula deep desulfuration denitrating tower (8), circulating pump (10), saturation slurries regeneration unit (11)；
The flue gas cool-down heat-exchanger rig (1), fume dust remover (2), booster fan (3), smoke re-heater (9), wet type are pre-
Desulphurization denitration tower (7), wet type deep desulfuration denitrating tower (8), saturation slurries regeneration unit (11) pass sequentially through flue or pipeline connects
Connect；The pre- desulphurization denitration tower (7) of alkali liquor absorption slurries preparation unit (4), slurry storage tank (5), slurry feeding pump (6), wet type according to
It is secondary to be connected；Prepared by denitration absorbing liquor and storage element (12) is connected by circulating pump (10) with wet type deep desulfuration denitrating tower (8)；
Saturation slurries regeneration unit (11) is connected to form circulation by denitration liquid delivery pump (13) and wet type deep desulfuration denitrating tower (8).
2. flue gas waste heat recovery wet method integrated purifying processing system as claimed in claim 1, it is characterised in that the wet type depth
Degree desulphurization denitration tower (8) top arrange dedusting demister, the dedusting demister be Flat defroster, ridge type demister,
Bundled tube dedusting demister or electrostatic bundled tube dedusting demister.
3. flue gas waste heat recovery wet method integrated purifying processing system as claimed in claim 1, it is characterised in that the flue gas drop
Warm heat-exchanger rig (1) is gas-liquid heat-exchange or gas-gas heat exchanger.
4. flue gas waste heat recovery wet method integrated purifying processing system as claimed in claim 1, it is characterised in that the flue gas is again
Hot device (9) is gas-gas heat exchanger.
5. a kind of purification method based on the flue gas waste heat recovery wet method integrated purifying processing system, it is characterised in that include
Following steps：
Step 1：Will be containing heavy metal contaminants such as oxysulfide, nitrogen oxides, dirt, mercury using flue gas cool-down heat-exchanger rig (1)
Flue-gas temperature 180 DEG C of ＜ is reduced to for 180 DEG C by ＞；
Step 2：The dust in the flue gas after cooling is removed using fume dust remover (2)；
Step 3：Smoke re-heater (9) will be sent into after the flue gas supercharging after dedirt using booster fan (3), flue gas Jing exchanges heat again
The pre- desulphurization denitration tower (7) of wet type is returned to after cooling, pre- desulphurization denitration is carried out, the desulfurization effect of the pre- desulphurization denitration tower (7) of wet type is controlled
Rate enters back into wet type deep desulfuration denitration after 40%～98% with smoke re-heater (9) heat exchange Jing flues Jing after intensification reheating
Tower (8), is carried out continuously after desulphurization denitration demisting, depth dust removal process and is changed into neat stress Jing flues and enters smoke stack emission；
Step 4：In wet type deep desulfuration denitrating tower (8) slurries of slurry pool Jing after desulphurization denitration can gradually saturation, after saturation
Absorption slurries send into desulphurization denitration saturation slurries regeneration unit (11), the desulphurization denitration slurries of Jing reducing/regeneratings continue to return
Recycle in wet type deep desulfuration denitrating tower (8)；
Step 5：Desulphurization denitration slurries in wet type deep desulfuration denitrating tower (8) are with constantly recycling, the sulfuric acid in slurries
Root can build up, when in desulphurization denitration slurries sulfate concentration reach >=1.0mol/L after, using saturation slurries regeneration unit
(11) 20%-50% of saturation slurries is carried out into discharge opeing process, isolates the solid product of sulphite or sulfate, isolated
Liquid slurry return in desulphurization denitration saturated solution regenerative system Jing regeneration, modulation after, enter into wet type deep desulfuration denitrating tower
(8) repetitive cycling is used in.
6. purification method as claimed in claim 5, it is characterised in that the fume dust remover (2) after exchanging heat in the step 2
For electric cleaner, electrostatic fabric filter or sack cleaner.
7. purification method as claimed in claim 5, it is characterised in that the absorption slurries in the pre- desulphurization denitration tower (7) of wet type are
Alkaline slurry, specially desulfurization alkaline slurry, including ammonia spirit, calcium oxide, calcium carbonate, magnesia and sodium carbonate, hydrogen-oxygen
Change sodium.
8. purification method as claimed in claim 5, it is characterised in that the desulphurization denitration of (8) in depth wet type desulfurizing denitrating tower
Slurries are ferrous salt, sulphite, the mixed solution of EDTA, and specific ferrous salt is ferrous sulfate, frerrous chloride, nitric acid Asia
Iron, sulphite is sodium sulfite, potassium sulfite, and EDTA is EDTA-2Na and EDTA-4Na.
9. purification method as claimed in claim 5, it is characterised in that desulfurization in the wet type deep desulfuration denitrating tower (8) takes off
Nitre slurries include catalyst, and the catalyst is Powdered Activated Carbon, and its pH value is not less than 7,200 ㎡ of specific surface area/g～1100
㎡/g, granularity is 80 mesh～400 mesh, and its addition is 0.0%wt～1.0%wt.
10. purification method as claimed in claim 5, it is characterised in that wet type deep desulfuration denitrating tower (8) in the step 5
Middle deep desulfuration denitration saturation slurries regeneration temperature is 40 DEG C～80 DEG C, recovery time 15min～90min.
11. purification methods as claimed in claim 5, it is characterised in that in the step 5 wet type deep desulfuration denitrating tower (8)
Desulphurization denitration slurries regenerative process in add activated carbon and make catalyst, activated carbon addition is 1.0%wt～5.0%wt, living
Property charcoal pH value be 2～11,200 ㎡ of specific surface/g～500 ㎡/g, wear-resisting intensity is not less than 85%.
12. purification methods as claimed in claim 5, it is characterised in that when sulphur in saturation desulphurization denitration slurries in the step 5
During acid group concentration >=1mol/L, start to carry out partial desulfurization denitration grout separating treatment, separate using after evaporative crystallization concentration
Centrifugation or using centrifugation mode after freezing and crystallizing.
13. purification methods as claimed in claim 5, it is characterised in that adopt in deep desulfuration denitrating tower (8) in the step 4
Adjust source as pH value with ammoniacal liquor, be centrifuged out after evaporative crystallization concentration solid byproducts ammonium sulfate or ammonium sulfite and
The mixture of ammonium sulfate.
14. purification methods as claimed in claim 5, it is characterised in that adopt in deep desulfuration denitrating tower (8) in the step 4
Source is adjusted as system pH value with soda, centrifugation after freezing and crystallizing goes out solid byproducts sodium sulphate or sodium sulphate and sulfurous acid
The mixture of sodium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710001638.0A CN106621808A (en) | 2017-01-03 | 2017-01-03 | Wet type integrated purification system and method for recovery of residual heat in flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710001638.0A CN106621808A (en) | 2017-01-03 | 2017-01-03 | Wet type integrated purification system and method for recovery of residual heat in flue gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106621808A true CN106621808A (en) | 2017-05-10 |
Family
ID=58837942
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710001638.0A Pending CN106621808A (en) | 2017-01-03 | 2017-01-03 | Wet type integrated purification system and method for recovery of residual heat in flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106621808A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107420925A (en) * | 2017-07-07 | 2017-12-01 | 江苏盐环实业有限公司 | A kind of environmentally friendly novel denitration desulphurization plant |
| CN107551813A (en) * | 2017-09-08 | 2018-01-09 | 浙江工业大学 | A kind of ship desulfurization and denitrification integral process and its device |
| CN109173711A (en) * | 2018-10-07 | 2019-01-11 | 张金明 | A kind of desulfurizing and denitrifying process |
| CN109200813A (en) * | 2018-11-21 | 2019-01-15 | 安徽工业大学 | A kind of denitrfying agent and preparation method catalytic-reduction denitrified for sintering flue gas |
| CN110981059A (en) * | 2019-12-09 | 2020-04-10 | 常州中源工程技术有限公司 | System and process for treating waste water containing sodium sulfate salt and sodium sulfite salt dinaphthol |
| CN111644032A (en) * | 2020-03-12 | 2020-09-11 | 上海守望者喷雾智能系统有限公司 | Low-temperature NO oxidation and removal process system |
| CN113398728A (en) * | 2021-05-28 | 2021-09-17 | 江苏奥利思特环保科技有限公司 | Method and system for flue gas desulfurization, denitrification and recycling |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0852159A2 (en) * | 1997-01-06 | 1998-07-08 | Haldor Topsoe A/S | Process for the desulphurization of gaseous substrate |
| CN101306308A (en) * | 2008-01-23 | 2008-11-19 | 华东理工大学 | Method for synchronously treating the combined pollution exhaust gas containing nitric oxide and sulfur dioxide |
| CN101485957A (en) * | 2009-01-08 | 2009-07-22 | 浙江大学 | Device and method of simultaneous desulfuration and denitration for flue gas using ozone oxygenation combined with double-tower washing |
| CN204502749U (en) * | 2014-11-28 | 2015-07-29 | 中冶长天国际工程有限责任公司 | Use the flue gas desulfurization and denitrification device of the two adsorption tower of series connection |
| CN105169942A (en) * | 2015-09-23 | 2015-12-23 | 广州创能环保科技有限公司 | Glass melter flue gas dust removal, desulfurization and denitrification synergetic treatment system, treatment method and application |
| CN204952637U (en) * | 2015-08-19 | 2016-01-13 | 江苏源能环境工程有限公司 | Double tower SOx/NOx control equipment |
| CN206746318U (en) * | 2017-01-03 | 2017-12-15 | 北京清新环境技术股份有限公司 | A kind of flue gas waste heat recovery wet method integrated purifying system |
-
2017
- 2017-01-03 CN CN201710001638.0A patent/CN106621808A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0852159A2 (en) * | 1997-01-06 | 1998-07-08 | Haldor Topsoe A/S | Process for the desulphurization of gaseous substrate |
| CN101306308A (en) * | 2008-01-23 | 2008-11-19 | 华东理工大学 | Method for synchronously treating the combined pollution exhaust gas containing nitric oxide and sulfur dioxide |
| CN101485957A (en) * | 2009-01-08 | 2009-07-22 | 浙江大学 | Device and method of simultaneous desulfuration and denitration for flue gas using ozone oxygenation combined with double-tower washing |
| CN204502749U (en) * | 2014-11-28 | 2015-07-29 | 中冶长天国际工程有限责任公司 | Use the flue gas desulfurization and denitrification device of the two adsorption tower of series connection |
| CN204952637U (en) * | 2015-08-19 | 2016-01-13 | 江苏源能环境工程有限公司 | Double tower SOx/NOx control equipment |
| CN105169942A (en) * | 2015-09-23 | 2015-12-23 | 广州创能环保科技有限公司 | Glass melter flue gas dust removal, desulfurization and denitrification synergetic treatment system, treatment method and application |
| CN206746318U (en) * | 2017-01-03 | 2017-12-15 | 北京清新环境技术股份有限公司 | A kind of flue gas waste heat recovery wet method integrated purifying system |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107420925A (en) * | 2017-07-07 | 2017-12-01 | 江苏盐环实业有限公司 | A kind of environmentally friendly novel denitration desulphurization plant |
| CN107551813A (en) * | 2017-09-08 | 2018-01-09 | 浙江工业大学 | A kind of ship desulfurization and denitrification integral process and its device |
| CN107551813B (en) * | 2017-09-08 | 2020-10-02 | 浙江工业大学 | Ship desulfurization and denitrification integrated process and device |
| CN109173711A (en) * | 2018-10-07 | 2019-01-11 | 张金明 | A kind of desulfurizing and denitrifying process |
| CN109200813A (en) * | 2018-11-21 | 2019-01-15 | 安徽工业大学 | A kind of denitrfying agent and preparation method catalytic-reduction denitrified for sintering flue gas |
| CN110981059A (en) * | 2019-12-09 | 2020-04-10 | 常州中源工程技术有限公司 | System and process for treating waste water containing sodium sulfate salt and sodium sulfite salt dinaphthol |
| CN111644032A (en) * | 2020-03-12 | 2020-09-11 | 上海守望者喷雾智能系统有限公司 | Low-temperature NO oxidation and removal process system |
| CN113398728A (en) * | 2021-05-28 | 2021-09-17 | 江苏奥利思特环保科技有限公司 | Method and system for flue gas desulfurization, denitrification and recycling |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106621808A (en) | Wet type integrated purification system and method for recovery of residual heat in flue gas | |
| CN206746318U (en) | A kind of flue gas waste heat recovery wet method integrated purifying system | |
| CN206652386U (en) | A kind of minimum discharge purifier of burning city domestic garbage flue gas | |
| CA3159632C (en) | Controlling aerosol production during absorption in ammonia-based desulfurization | |
| US9895661B2 (en) | Process and device for desulphurization and denitration of flue gas | |
| JP4995084B2 (en) | Super-cleaning of combustion gases including CO2 removal | |
| US7255842B1 (en) | Multi-component removal in flue gas by aqua ammonia | |
| CN108636098A (en) | A kind of the minimum discharge purifier and its method of burning city domestic garbage flue gas | |
| KR890000512B1 (en) | Process for removal of nitrogen oxides and sulfur oxides from waste gases | |
| CN112808746B (en) | Resource treatment method for incineration slag and fly ash | |
| CN103619445B (en) | There is the carbon dioxide capture system based on freezing ammonia and the using method of recovery ammonia | |
| CN105214478A (en) | The integral process of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery | |
| WO2008052465A1 (en) | A sintered flue gas wet desulfurizing and dedusting process | |
| CN108176224A (en) | A kind of regeneration fume from catalytic cracking ammonia process of desulfurization denitration dust collecting method and device | |
| CN103429317A (en) | Apparatus and system for NOX reduction in wet flue gas | |
| CN102441321A (en) | Abdotbrnt internal and external circulating device and their methods for treatment of high temperature flue gases containing sulfur oxides and boron compounds | |
| KR102374520B1 (en) | Combustion System Including Energy-Saving Flue Gas Treatment Facility | |
| CN100534583C (en) | Sulphur dioxide in flue gas recovering method and device with ammonia as material | |
| CN109133012B (en) | Sulfur recovery process for high-concentration acid gas | |
| CN113251420A (en) | Industrial waste treatment method and device | |
| CN106178877A (en) | A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique | |
| CN109224808A (en) | A kind of carbon baking kiln gas ultra-clean discharge cleaning equipment and purification method | |
| CN218741209U (en) | Useless active carbon pyrolysis regeneration gas cleaning system of danger | |
| CN215863435U (en) | Industrial waste's processing apparatus | |
| CN110307553A (en) | A kind of activated coke activation exhaust treatment system and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170510 |
|
| RJ01 | Rejection of invention patent application after publication |