CN112915755A - System and method for jointly recovering sulfur dioxide in flue gas and removing nitrogen oxide - Google Patents
System and method for jointly recovering sulfur dioxide in flue gas and removing nitrogen oxide Download PDFInfo
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- CN112915755A CN112915755A CN202110186881.0A CN202110186881A CN112915755A CN 112915755 A CN112915755 A CN 112915755A CN 202110186881 A CN202110186881 A CN 202110186881A CN 112915755 A CN112915755 A CN 112915755A
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- absorption
- flue gas
- sulfur dioxide
- sulfite
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 133
- 238000000034 method Methods 0.000 title claims abstract description 105
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 100
- 239000003546 flue gas Substances 0.000 title claims abstract description 55
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000010521 absorption reaction Methods 0.000 claims abstract description 117
- 230000008569 process Effects 0.000 claims abstract description 55
- 239000007788 liquid Substances 0.000 claims abstract description 51
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 claims abstract description 44
- 229910002651 NO3 Inorganic materials 0.000 claims abstract description 40
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims abstract description 39
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims abstract description 34
- 230000009467 reduction Effects 0.000 claims abstract description 28
- 238000001704 evaporation Methods 0.000 claims abstract description 23
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 23
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 21
- 230000003647 oxidation Effects 0.000 claims abstract description 21
- 230000008020 evaporation Effects 0.000 claims abstract description 20
- 230000002829 reductive effect Effects 0.000 claims abstract description 20
- 239000006227 byproduct Substances 0.000 claims abstract description 17
- 235000010265 sodium sulphite Nutrition 0.000 claims abstract description 16
- 239000003513 alkali Substances 0.000 claims abstract description 15
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 15
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims abstract description 13
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 238000011069 regeneration method Methods 0.000 claims abstract description 12
- 230000008929 regeneration Effects 0.000 claims abstract description 11
- 238000004064 recycling Methods 0.000 claims abstract description 10
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 claims abstract description 7
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000000243 solution Substances 0.000 claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 22
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 238000006477 desulfuration reaction Methods 0.000 claims description 15
- 230000023556 desulfurization Effects 0.000 claims description 15
- 229910052757 nitrogen Inorganic materials 0.000 claims description 13
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 10
- 229910044991 metal oxide Inorganic materials 0.000 claims description 9
- 150000004706 metal oxides Chemical class 0.000 claims description 9
- 150000003863 ammonium salts Chemical class 0.000 claims description 8
- UBEWDCMIDFGDOO-UHFFFAOYSA-N cobalt(II,III) oxide Inorganic materials [O-2].[O-2].[O-2].[O-2].[Co+2].[Co+3].[Co+3] UBEWDCMIDFGDOO-UHFFFAOYSA-N 0.000 claims description 8
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 7
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- 239000013589 supplement Substances 0.000 claims description 6
- 239000011248 coating agent Substances 0.000 claims description 5
- 238000000576 coating method Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 238000003487 electrochemical reaction Methods 0.000 claims description 5
- 230000001590 oxidative effect Effects 0.000 claims description 5
- UPDATVKGFTVGQJ-UHFFFAOYSA-N sodium;azane Chemical compound N.[Na+] UPDATVKGFTVGQJ-UHFFFAOYSA-N 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 4
- 238000003980 solgel method Methods 0.000 claims description 4
- 239000000758 substrate Substances 0.000 claims description 4
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims description 3
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 239000010409 thin film Substances 0.000 claims description 2
- 238000002425 crystallisation Methods 0.000 abstract description 23
- 230000008025 crystallization Effects 0.000 abstract description 23
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 11
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 11
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 11
- 239000002250 absorbent Substances 0.000 abstract description 6
- 230000002745 absorbent Effects 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000011946 reduction process Methods 0.000 abstract description 2
- 238000006722 reduction reaction Methods 0.000 description 25
- 239000010936 titanium Substances 0.000 description 20
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 15
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 15
- 235000011130 ammonium sulphate Nutrition 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 229910001868 water Inorganic materials 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 239000007789 gas Substances 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 239000003337 fertilizer Substances 0.000 description 5
- -1 sulfate radical Chemical class 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 229910052719 titanium Inorganic materials 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 239000004155 Chlorine dioxide Substances 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 1
- YHFXJKYHUWPWSJ-UHFFFAOYSA-L [Na+].[Na+].OS([O-])=O.OS([O-])=O Chemical compound [Na+].[Na+].OS([O-])=O.OS([O-])=O YHFXJKYHUWPWSJ-UHFFFAOYSA-L 0.000 description 1
- VEUACKUBDLVUAC-UHFFFAOYSA-N [Na].[Ca] Chemical compound [Na].[Ca] VEUACKUBDLVUAC-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 150000001447 alkali salts Chemical class 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- ODPSGJKCFPBBDN-UHFFFAOYSA-M azanium sodium hydrogen sulfite Chemical compound [NH4+].[Na+].OS([O-])=O.OS([O-])=O ODPSGJKCFPBBDN-UHFFFAOYSA-M 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 235000019398 chlorine dioxide Nutrition 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000002848 electrochemical method Methods 0.000 description 1
- 239000007772 electrode material Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- YPJKMVATUPSWOH-UHFFFAOYSA-N nitrooxidanyl Chemical compound [O][N+]([O-])=O YPJKMVATUPSWOH-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009331 reductive pathway Effects 0.000 description 1
- 239000012492 regenerant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000012085 test solution Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- 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
- B01D53/76—Gas phase processes, e.g. by using aerosols
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- 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
- B01D53/965—Regeneration, reactivation or recycling of reactants including an electrochemical process step
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- 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
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- 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
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Abstract
本发明公开了一种联合回收烟气中二氧化硫并脱除氮氧化物的系统及方法。通过臭氧氧化烟气中的氮氧化物为二氧化氮；烟气经亚硫酸钠和亚硫酸铵吸收，二氧化硫转化为亚硫酸氢盐，氮氧化物转化为硝酸盐和亚硝酸盐；经蒸发和再生过程将二氧化硫富集回收；利用电化学还原过程将硝酸盐和亚硝酸盐还原为氨氮，氨氮返回吸收塔作为吸收液循环使用。与传统的钠碱湿式吸收方法相比，本发明利用湿式吸收与电化学还原联合技术，在回收二氧化硫的同时，去除烟气中的氮氧化物并将二氧化硫作为吸收剂循环利用；同时，利用铵盐湿法吸收，有效解决氧化副产物硫酸钠低温易结晶导致的堵塞管道问题。
The invention discloses a system and method for combined recovery of sulfur dioxide in flue gas and removal of nitrogen oxides. The nitrogen oxides in the flue gas are oxidized to nitrogen dioxide by ozone; the flue gas is absorbed by sodium sulfite and ammonium sulfite, sulfur dioxide is converted into bisulfite, and nitrogen oxides are converted into nitrate and nitrite; after evaporation and regeneration process The sulfur dioxide is enriched and recovered; the nitrate and nitrite are reduced to ammonia nitrogen by the electrochemical reduction process, and the ammonia nitrogen is returned to the absorption tower for recycling as the absorption liquid. Compared with the traditional sodium-alkali wet absorption method, the present invention utilizes the combined wet absorption and electrochemical reduction technology to remove nitrogen oxides in the flue gas and recycle the sulfur dioxide as an absorbent while recovering sulfur dioxide; Salt-wet absorption can effectively solve the problem of blocked pipelines caused by the easy crystallization of sodium sulfate, a by-product of oxidation at low temperature.
Description
Technical Field
The invention belongs to the field of chemical industry and environmental protection, and relates to a system and a method for jointly recovering sulfur dioxide in flue gas and removing nitrogen oxide; in particular to a system and a method for recovering sulfur dioxide in flue gas and removing nitrogen oxide by combining sodium-ammonium double-alkali wet absorption and electrochemical reduction.
Background
Sulfur dioxide (SO) in the atmosphere2) And Nitrogen Oxides (NO)X) Is an important source of photochemical smog, acid rain and other environmental problems, can cause great harm to the environment and human health, and is an air pollutant of major concern. Therefore, the industrial flue gas can be discharged after being subjected to desulfurization and denitrification to reach the standard.
Flue gas desulfurization is mainly based on a high-concentration acid making technology and a low-concentration recovery method. NOXIs mainly composed of NO2And NO, where NO is more difficult to handle. In recent years, they have attracted more and more attention, and the emission standards set by countries and industries have become stricter. NO in general industrial fumesXIn a lower concentration and with SO2Coexisting and the temperature of the flue gas is low, so that the flue gas is difficult to remove by adopting the traditional reduction and denitrification technology. In view of the above requirements for flue gas desulfurization and denitration and the requirement for multi-pollutant cooperative control, the flue gas purification efficiency needs to be improved by combining new environmental protection requirements. In industry, SO in flue gas is removed conventionally2The technologies of the method are mainly divided into a dry method, a wet method, a semi-dry method and the like, wherein the limestone-gypsum method, the circulating fluidized bed method and the like are widely applied and mature dry process methods, but the problems of non-ideal desulfurization efficiency, a plurality of byproducts and the like still exist. The wet desulphurization efficiency is higher, but the disadvantages of large occupied area and difficult secondary wastewater treatment exist. Removal of NOXThe main method adopts a selective catalytic reduction denitration process, has high denitration efficiency, but has the problems of high operating cost, harsh conditions, high maintenance cost and the like.
Through searching the prior artPatent CN103203176A uses a calcium-based absorbent to oxidize NO and SO by a complex oxidizing agent2The absorption and removal are carried out, but the problems of large consumption of the oxidant and more desulphurization byproducts still exist; patent CN1660474A uses limestone to react with desulfurization solution by sodium-calcium double alkali method to regenerate the desulfurizer, but the treatment of the desulfurization byproduct calcium sulfate is still a problem; patent CN103990362A uses chlorine dioxide gas to oxidize NO, and combines wet method or semi-dry method to synergistically remove NOXAnd SO2But the preparation cost of the oxidant is high, and secondary pollution is easy to cause; in patent CN101347706A, soda ash, caustic soda or waste alkali is used as an absorbent, and carbide slag is used as a regenerant to desulfurize flue gas, so as to treat waste with waste, save energy and reduce emission, but sulfur dioxide in flue gas cannot be reused.
Generally speaking, wet absorption is still a desulfurization and denitrification method with high efficiency and wide application. The traditional sodium sulfite-sodium bisulfite absorption system has low cost and high efficiency, but oxidation side reaction products are easy to reduce the absorption capacity of absorption liquid, and the pipeline is easy to be blocked under the low temperature condition because the solubility of sulfate is low. In addition, the process is directed to NOXHas a limited removal effect.
Disclosure of Invention
The invention aims to provide a system and a method for recovering sulfur dioxide in flue gas and removing nitrogen oxide by combining sodium-ammonium double-alkali wet absorption and electrochemical reduction aiming at the defects of the existing flue gas combined desulfurization and denitrification process technology and combining the advantages of adjustable electrode performance and controllable reactant of the electrochemical reduction method, and simultaneously effectively solve the problem of pipeline blockage caused by low-temperature easy crystallization of oxidation by-product sulfate in the actual process.
The working process of the invention is as follows: nitrogen oxide in the ozone oxidized flue gas after dust removal is nitrogen dioxide, sodium sulfite and ammonium sulfite are used as absorbents to absorb sulfur dioxide and nitrogen oxide in the ozone oxidized flue gas, the sulfur dioxide is converted into sodium bisulfite, and the nitrogen oxide is converted into nitrate and nitrite; then the concentrated sulfur dioxide is released by evaporation and regeneration for enrichment and recovery; nitrate and nitrite are reduced into ammonium salt by virtue of electrochemical reduction reaction, the ammonium salt is recycled to the absorption tank to supplement the ammonium salt in the absorption liquid, and when the ammonium salt reaches a certain concentration, the ammonium salt is concentrated and discharged to be used as a nitrogen fertilizer.
In the system of the invention, nitrate/nitrite is electrochemically reduced into ammonium by an electrochemical method, the process is easy to implement compared with the process of reducing into nitrogen, no chloride ion and the like are added, and the reduction of the generated ammonium is not reduced after the ammonium is returned to an absorption cell2The low-temperature solubility of the oxidation product sulfate radical is far lower than that of sodium sulfate, so that the outstanding problem that the low-temperature pipeline is easy to block in the actual process can be effectively solved. In the system, the ammonium radical has the effect that (1) the solubility of the oxidation product is far greater than that of sodium salt under the low-temperature condition, so that the problem of pipeline blockage is effectively solved; (2) ammonium radical being derived from NOXThe absorption product of (2) does not need to be additionally added; (3) nitrate radical/nitrite radical is reduced into ammonium radical through electrochemical process, the process is easier to realize, and NO can be realized after the absorption tank is reusedXThe cyclic utilization of the NO is realized on the basis of solving the practical process problemXInnocent treatment and utilization; (4) ammonium does not affect SO2And NOXThe absorption effect of (1). In addition, excessive control on the concentration of sulfite and the pH value in the absorption liquid is not needed, because the concentration of sulfite influences the absorption capacity, the higher the concentration is, the larger the absorption capacity is; the method for controlling the pH to be alkaline is to add an alkaline solution, such as sodium hydroxide, and the process itself is a process for increasing the concentration of sulfite.
The purpose of the invention can be realized by the following scheme:
in a first aspect, the invention relates to a method for combined recovery of sulfur dioxide and removal of nitrogen oxides from flue gas, which combines a sodium-ammonium double-alkali wet absorption method and an electrochemical reduction method. The invention combines a sodium-ammonium double-alkali wet absorption desulfurization process method and an electrochemical reduction denitration method to realize the purposes of absorption, regeneration and recovery of sulfur dioxide and absorption, cyclic utilization and removal of nitrogen oxides.
As an embodiment of the present invention, the method comprises the steps of:
s1, removeThe dust-removed flue gas is oxidized by ozone to oxidize nitric oxide NO in the flue gas into nitrogen dioxide NO2；
S2, absorbing sulfur dioxide SO in the flue gas of the step S1 by using sulfite absorption liquid2And nitrogen oxide NOXFormation of bisulfite HSO3 -Nitrate NO3 -And nitrite NO2 -A solution;
s3, evaporating and regenerating the sulfite absorption liquid after the sulfite absorption liquid is saturated, releasing and regenerating sulfur dioxide, and enriching and recovering; carrying out electrochemical reduction denitration on the evaporated and regenerated solution, wherein nitrate and nitrite are reduced into ammonia nitrogen;
s4, recycling the ammonia nitrogen-containing solution subjected to the reduction denitration treatment in the step S3 to the step S2 to be used as a supplementary absorption liquid for recycling; or when the concentration of the ammonium salt in the ammonia-containing nitrogen solution after the reduction denitration treatment in the step S3 exceeds 75%, discharging the ammonia-containing nitrogen solution out of the system. In the system of the present invention, the concentration of ammonium in the absorption liquid gradually increases as the reaction proceeds, but when the ammonium concentration is too high, ammonia slip is easily caused, and the absorption efficiency is lowered due to the decrease in pH.
As an embodiment of the present invention, in step S1, the ozone oxidation process is performed by an ozone generator discharging and oxidizing air or pure oxygen into ozone.
As an embodiment of the present invention, in step S2, the initial sulfite absorbing solution of the reaction is a sodium sulfite solution with a concentration of 10% to 20%; in the reaction process, the sulfite absorption liquid is a mixed liquid of sodium sulfite and ammonium sulfite; the mass ratio of the sodium sulfite to the ammonium sulfite in the mixed solution is 25-100%, and the mass ratio of the ammonium sulfite is 0-75%.
As an embodiment of the present invention, in step S2, the absorption process is carried out under ambient atmospheric pressure (101kPa) and at medium-low temperature (20 ℃ C. to 60 ℃ C.). Preferably, the absorption process is carried out at ambient atmospheric pressure and 40 ℃.
As an embodiment of the present invention, in step S2, during the absorption process, part of the nitrite is oxidized into nitrate and part is oxidized into nitrateO in sulfite absorption liquid by flue gas2Oxidation to the oxidation by-product sulfate.
As an embodiment of the present invention, in step S2, the absorption process is added with supplementary alkali solution, wherein the alkali solution is sodium hydroxide or sodium sulfite. When the treatment is carried out in step S3, sodium bisulfite is evaporated under reduced pressure to release SO2Sodium sulfite is generated, and the part of the sodium sulfite is returned to an absorption tank (a desulfurization absorption tower) to be used as an absorbent; in addition, because the absorption liquid is partially oxidized due to the existence of oxygen in the flue gas, a supplementary alkali liquor is additionally added in the process, and the added alkali liquor is sodium hydroxide or sodium sulfite.
As an embodiment of the present invention, in step S3, the evaporation regeneration process is to regenerate sulfur dioxide by heating decomposition or reduced pressure evaporation process. The temperature for heating and decomposing is 95-100 ℃; the discharged solution after evaporation and regeneration is concentrated and used as fertilizer or building material.
As one embodiment of the present invention, in step S3, the recovered sulfur dioxide is enriched to produce high concentration sulfur dioxide or acid.
In step S3, the electrochemical reduction denitration process is performed in an electrolytic cell, wherein the anode is Ir-Ru/Ti-based inert electrode, the cathode is Ti-based metal oxide electrode, and the cathode and anode are separated by proton exchange membrane.
As an embodiment of the invention, the Ti-based metal oxide electrode is selected from Co3O4/Ti or Fe2O3a/Ti electrode.
As one embodiment of the present invention, the Ti-based metal oxide electrode is obtained by coating a metal oxide-supported thin film on a Ti substrate by a sol-gel method. The metal oxide is Co3O4Or Fe2O3。
In step S3, ammonia nitrogen in the solution in the evaporation and regeneration device is discharged after reaching a predetermined concentration. In the evaporation and regeneration device, oxidation byproducts sodium sulfate and ammonium sulfate generated in the absorption process and the electrochemical reduction process are discharged out of the system and are concentrated to be used as fertilizers, so that economic benefits are generated.
In a second aspect, the invention also relates to a system for jointly recovering sulfur dioxide in flue gas and removing nitrogen oxide, which comprises an ozone generator, a desulfurization absorption tower, an evaporation regenerator, an electrochemical reaction tank and an absorption liquid supplement tank which are sequentially connected; and the supplementary absorption liquid in the absorption liquid supplementary pool reflows to the desulfurization absorption tower through a pipeline.
Compared with the prior art, the invention has the following beneficial effects:
1) the invention forms a sodium sulfite-ammonium sulfite wet absorption system, reduces the crystallization temperature of the absorption system on the premise of ensuring the total absorption efficiency, and effectively solves the problem of pipeline blockage caused by low-temperature oxidation byproducts in the absorption process of the traditional process;
2) the invention utilizes the advantages of the electrochemical denitration method to recover SO in the traditional process2While absorbing NOXAnd the desulfurization and denitrification can be realized at the same time by recycling.
Drawings
Other features, objects and advantages of the invention will become more apparent upon reading of the detailed description of non-limiting embodiments with reference to the following drawings:
FIG. 1 is a schematic overall flow chart of the method for jointly recovering sulfur dioxide and removing nitrogen oxides from flue gas according to the present invention;
wherein: 1. an ozone generator; 2. an absorption tower; 3. an evaporation regenerator; 4. an electrochemical reaction cell; 5. and an absorption liquid replenishing pool 6 and a condenser.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments. The following examples, which are set forth to provide a detailed description of the invention and a detailed description of the operation, will help those skilled in the art to further understand the present invention. It should be noted that the scope of the present invention is not limited to the following embodiments, and that several modifications and improvements made on the premise of the idea of the present invention belong to the scope of the present invention.
Example 1
The embodiment relates to combined recovery of SO in flue gas2And removing NOXThe system comprises an ozone generator 1, an absorption tower 2, an evaporation regenerator 3, an electrochemical reaction tank 4 and an absorption liquid replenishing tank 5 which are connected in sequence as shown in figure 1;
the ozone generator 1 is provided with a flue gas inlet, and the flue gas after dust removal is conveyed to the ozone generator 1 for ozone oxidation treatment;
the absorption tower 2 is provided with a tail gas discharge port and a supplementary absorption liquid inlet, and supplementary absorption liquid in the absorption liquid supplementary tank 5 flows back to the absorption tower 2 through the supplementary absorption liquid inlet; the absorption liquid supplement tank 5 is also provided with an alkali liquid supplement device;
SO is arranged on the evaporation regenerator 32An outlet and an oxidation by-product outlet, evaporating the regenerated SO in the regenerator 32Via SO2Outlet into SO2Release line, said SO2A condenser 6 is arranged on the releasing pipeline and is used for recovering and enriching the SO with high concentration2A gas; and discharging the oxidation byproducts of the sodium sulfate and the ammonium sulfate out of the system through an oxidation byproduct outlet, and concentrating the oxidation byproducts to be used as fertilizer.
The combined recovery of SO in flue gas of the present embodiment2And removing NOXThe method comprises the following steps: the flue gas after dust removal is subjected to an ozone oxidation process to oxidize nitric oxide in the flue gas into nitrogen dioxide; absorbing sulfur dioxide and nitrogen oxides in the flue gas by using sulfite absorption liquid to generate bisulfite, nitrate and nitrite; after absorption saturation, the absorption liquid is subjected to evaporation regeneration, sulfur dioxide is released and regenerated, and enrichment recovery is carried out to prepare high-concentration sulfur dioxide or acid; carrying out electrochemical reduction on the evaporated and regenerated solution, and reducing nitrate and nitrite into ammonia nitrogen; the ammonia nitrogen is circulated to the absorption tank to supplement absorption liquid for recycling, and is discharged out of the system after reaching a certain concentration, so that the ammonia nitrogen is used as fertilizer to produce economic benefit.
The method comprises the following specific steps:
firstly, the flue gas after dust removal is subjected to an ozone oxidation process, and NO in the flue gas is oxidized into NO2This step will further haveBenefit from NOXThe absorbed liquid is absorbed into the liquid phase, and the ozone oxidation process is realized by oxidizing air or pure oxygen into ozone through the discharge of an ozone generator;
NO+O3→NO2+O2
secondly, absorbing SO in the flue gas by sulfite absorption liquid2And NOX，SO2With absorption liquid SO3 2-Reaction to HSO3 -，NOXInto the liquid phase to form NO3 -And NO2 -，NO2 -As the main component; meanwhile, in this process, part of NO2 -Is oxidized to NO3 -Part of SO3 2-Absorption liquid is absorbed by O in flue gas2Oxidation to by-product SO4 2-(ii) a The initial absorption liquid is absorption liquid Na2SO3With NO3 -And NO2 -Reducing absorption liquid SO3 2-Is Na2SO3And (NH)4)2SO3The absorption process is carried out under the conditions of ambient atmospheric pressure and normal temperature;
SO2+SO3 2-+H2O→2HSO3 -
2NO2+SO3 2-+H2O→SO4 2-+2NO2 -+2H+
2NO2+HSO3 -+H2O→SO4 2-+2NO2 -+3H+
NO2+NO+H2O→2NO2 -+2H+
3NO2+H2O→2NO3 -+NO+2H+
2NO2+H2O→NO2 -+NO3 -+2H+
2SO3 2-+O2→2SO4 2-
thirdly, the absorption liquid which is absorbed to saturation is evaporated and regenerated in an evaporation crystallization tower, and SO2Released again and then is enriched and recovered for preparing high-concentration SO2Gas or for acid production; the evaporation and regeneration process realizes SO through heating and reduced pressure evaporation processes2Regeneration;
2HSO3 -→SO3 2-+SO2+H2O
fourthly, evaporating the regenerated solution for electrochemical reduction of NO3 -And NO2 -Is reduced to NH4 +(ii) a The electrochemical reduction denitration process is carried out in an electrolytic cell, wherein the anode of the electrolytic cell is an inert Ir-Ru/Ti-based electrode, and the cathode of the electrolytic cell is Co3O4/Ti、Fe2O3The negative electrode and the positive electrode are separated by a proton exchange membrane; the cathode Co3O4/Ti、Fe2O3the/Ti electrode is prepared by coating a Ti substrate with supported Co by a sol-gel method3O4And Fe2O3A film;
and fifthly, circulating the generated ammonia nitrogen in the electrochemical reaction tank to an absorption tank for supplementing as absorption liquid for recycling, thereby realizing the recycling of N, discharging oxidation byproducts sodium sulfate and ammonium sulfate generated in the absorption process and the electrochemical process out of a system after the ammonia nitrogen reaches a certain concentration, and using the ammonia nitrogen as a fertilizer after concentration to generate economic benefit.
Example 2
The purpose of this example is to consider the crystallization of oxidation by-products sodium sulfate and ammonium sulfate in the sulphurous acid system, and to compare the crystallization temperatures of the sodium sulfate and ammonium sulfate systems.
To 20g of deionized water was added 8g of sodium sulfate (28% by mass, near saturation), to which was added varying amounts of ammonium sulfate, and the crystallization temperature of the mixed sulfate solution was determined.
The crystallization test solution is placed in a water bath, a magnetic stirrer is used for accelerating the temperature transfer and crystallization of the solution, and a temperature sensor and a temperature transmitter are used for monitoring and recording the temperature of the solution to be analyzed. Meanwhile, deionized water was used as a blank comparison. Controlling the temperature of the water bath by a circulating condenser, gradually reducing the temperature of the water bath, and recording the crystallization condition of the mixed liquid. When the temperature of the mixed solution is not reduced and rises suddenly, the temperature of the system is increased due to the heat generated by the crystallization of the solution, and the moment is the crystallization moment. The temperature difference curve can be obtained through the temperature difference between the mixed liquid and the deionized water at each moment, so that the crystallization temperature is obtained.
The crystallization temperature when the mixed system contains more ammonium sulfate with different amounts is as follows:
from the above results, it can be seen that the addition of ammonium sulfate is advantageous for reducing the crystallization temperature of sodium sulfate, and more than 50% of ammonium sulfate can be dissolved under the same conditions, which also proves that the addition of ammonium sulfate can reduce the crystallization temperature and alleviate the problem of pipeline blockage caused by the oxidation by-product sulfate.
Example 3
In this example, the relationship between the quality and content of ammonium sulfate in a mixed system of sodium sulfate and ammonium sulfate and the crystallization temperature was examined.
The crystallization temperature of the mixed sulfate solution was measured by adding a mixed solution of 28%, 25%, 20%, 15%, 10% sodium sulfate and ammonium sulfate (28% being nearly saturated) to 20g of deionized water to change the ammonium sulfate content. The procedure was as in example 2, and the crystallization temperatures were as follows:
from the above results, it can be seen that the crystallization temperature gradually decreases as the ammonium sulfate content increases, regardless of the total mass fraction of the mixed solute. The significant reduction in crystallization temperature again demonstrates that ammonium salts in the system can reduce the crystallization temperature of the absorption liquid and reduce pipe plugging caused by crystallization.
Example 4
The purpose of this example is to investigate the sodium sulfite and ammonium sulfite solutions versus SO2And NOXThe absorption efficiency of (2).
SO pair of sodium sulfite and ammonium sulfite absorption liquid2And NOXThe absorption effect of the method is realized by liquid absorption, the mixed gas of NO, NO2 and SO2 is subjected to full absorption reaction by a bubbling absorption reactor through sodium sulfite and ammonium sulfite absorption liquid under the ambient atmospheric pressure, the absorption temperature is controlled to 40 ℃ in the absorption process, the reaction conditions are ensured to be consistent, and the reaction is fully carried out. Analyzing the gas concentration at the inlet and the outlet of the absorption cell in real time and calculating SO2And NOXGas absorption rate.
NO in mixed gas used in the invention mode2、NO、SO2And O2The concentration ranges of (A) are 300, 50-100, 3000-10000ppm and 0-10% respectively; the total gas flow is 1L/min; the absorbent concentration was 5%.
After complete absorption, detecting and calculating SO of sodium sulfite and ammonium sulfite2The absorption efficiencies of (A) and (B) were 98.18% and 98.47%, respectively, indicating that they have a good adsorption effect: (>98%); for NO2The absorption efficiencies of (1) and (3) are respectively 98.38% and 93.44%, which shows that the removal efficiency is higher and meets the requirement of NO2The removal requirement of (2); the absorption efficiency of NO is 68.89 percent and 69.18 percent respectively, and the removal efficiency is relative to NO2Low, difficult to meet industry emission standards, and therefore ozone is required to oxidize NO to NO prior to absorption2Can greatly increase NOXThe absorption efficiency of (2).
Example 5
The purpose of this example is to investigate the SO in the Combined recovery flue gas2And removing NOXThe sulfite absorption solution used in the method of (1) to NOXThe absorption effect of (1).
Continuously introducing 350ppm NO into 5% sulfite absorption solution2And 50ppm NO, and after absorption for 270 minutes, the concentration of the absorbed product is 0.385g/L NO3 -And 1.627g/L of NO2 -. The results show that the absorption products of nitrogen oxides are mainly NO2 -(majority) and NO3 -，NO3 -Is significantly lower than NO2 -. While in the whole absorption system, NO2 -Not in a stable state, part of it may be oxidized to NO3 -. In addition, in the process from NO3 -During the initial electrochemical reduction, the reduction product comprises NH4 +、N2Etc. of NH4 +Is the most easily reduced product. When a reductive pathway is of interest, NO3 -Is first electrochemically reduced to NO2 -And part of the possible NO, N2O、N2And finally is NH4 +The specific intermediate product depends on electrochemical reduction control, including electrode material, applied voltage, environment, etc. From NO2 -Electrochemical reduction to NH4 +Specific from NO3 -Electrochemical reduction to NH4 +More easily, where the charge of nitrogen is equal to +3, and NO3 -The charge of the medium nitrogen is equal to + 5. Taking into account NO3 -And NO2 -From competing reactions of NO2 -Due to its higher concentration and more favorable electrochemical potential, faster reaction rates are obtained. At the same time, NO3 -It is also considered to be reduced at a sufficient voltage for the reduction reaction. Thus, NO3 -Is the focus of the process.
Example 6
The purpose of this example is to investigate the SO in the Combined recovery flue gas2And removing NOXThe titanium-based metal oxide electrode adopted in the method has an electrochemical denitration effect.
The nitrate wastewater is treated by a commonly used titanium-based metal oxide electrode in an electrochemical reduction denitration process in an electrolytic bath. The object to be processed is CNNaNO 100mg/L3Solution containing 0.1mol/L of Na2SO3The volume of the wastewater is 100 mL.
Mixing Co by sol-gel method3O4、Fe2O3The coating is loaded on a Ti substrate and used as a cathode electrode, and the coating has good effect on the electrochemical reduction of nitrate; the anode of the electrolytic cell adopts an inert Ir-Ru/Ti-based electrode, and the cathode and the anode are separated by a proton exchange membrane; the voltage was set at 5V and the cathode and anode had a submerged area of 15cm2(5 cm. times.3 cm); the current is 0.06A-0.2A in the reaction process.
After 3h, sampling and analyzing, and determining the removal rate of nitrate nitrogen and the generation rate of ammonia nitrogen, wherein the results are as follows.
| Metal oxide electrode | Co3O4/Ti | Fe2O3/Ti |
| NO3 --N removal (%) | 93.7 | 63.8 |
| NH4 +-N production ratio (%) | 85.6 | 49.6 |
As can be seen from the above results, Co3O4the/Ti cathode showed a nitrate removal efficiency of 93.67% which is better than that of Fe2O3Ti, while showing a specific Fe2O3Better ammonia production efficiency (85.56%) by Ti (49.59%). Both cathodes showed a total nitrogen removal efficiency of about 10%, which is present in the form of other gaseous or liquid nitrogen. Overall, both cathodes showed good NO3 -Reducing power, NO3 -Is mainly reduced to NH4 +Nitrogen, and a small part of NO3 -And other forms of nitrogen. It offers the possibility of nitrogen conversion and recycling in the absorption system to achieve the purpose of denitrification. Co3O4Ti has satisfactory reduced NO3 -Efficiency and NH of4 +Efficiency of generation, while SO3 2-The presence of (a) has no inhibitory effect on the electrochemical reduction reaction, again demonstrating the feasibility of this approach.
Example 7
The purpose of this example is to recover SO in flue gas in combination with research2And removing NOXThe influence of continuous operation of the process on the denitration efficiency in the method is avoided.
In order to consider the requirement of continuous operation of the actual process, NO is intermittently added in the electrochemical denitration process3 -N source, added every 2 hours at a concentration corresponding to the initial concentration of nitrate nitrogen, the concentration of each form of nitrogen and the variation of pH value throughout the reaction were examined. Every 2 hours, NO3 -The N concentration is obviously reduced, and the interval removal efficiency is maintained to be more than 60% in the whole process; NH (NH)4 +The N concentration is obviously increased and the interval generation efficiency is maintained to be more than 55.2 percent in the whole process. When the interval time is extended to 3 hours, NO3 -The N removal efficiency is improved to over 86.2 percent; NH (NH)4 +the-N generation efficiency rises to above 72%, and this efficiency will continue to rise over time. The whole denitration and ammonia nitrogen conversion efficiency in the whole process is maintained at a higher level.
The pH value result in the process shows thatThe pH value is rapidly increased from an initial value of 9.26 to 12.45 after the reaction is started, and then is maintained at a higher value of about 12.7-13.1 due to the formation of ammonia (NH)4)2SO3Is a weak alkali salt, has buffering effect on the process, and the pH value of the system is generally stable.
The foregoing description of specific embodiments of the present invention has been presented. It is to be understood that the present invention is not limited to the specific embodiments described above, and that various changes and modifications may be made by one skilled in the art within the scope of the appended claims without departing from the spirit of the invention.
Claims (10)
1. A method for recovering sulfur dioxide in flue gas and removing nitrogen oxide is characterized in that a sodium-ammonium double-alkali wet absorption method and an electrochemical reduction method are used in a combined mode.
2. The method for the combined recovery of sulfur dioxide and removal of nitrogen oxides in flue gases according to claim 1, characterized in that it comprises the following steps:
s1, oxidizing the dedusted flue gas with ozone to oxidize nitric oxide in the flue gas into nitrogen dioxide;
s2, absorbing sulfur dioxide and nitrogen oxides in the flue gas in the step S1 by using a sulfite absorption liquid to generate a solution of bisulfite, nitrate and nitrite;
s3, after being absorbed and saturated, the sulfite absorption liquid is regenerated through reduced pressure evaporation, wherein the sodium bisulfite releases sulfur dioxide, and the sulfur dioxide is enriched and recovered; the solution after evaporation and regeneration enters an electrochemical reduction denitration process, wherein nitrate and nitrite are reduced into ammonia nitrogen;
s4, recycling the ammonia nitrogen-containing solution subjected to the reduction denitration treatment in the step S3 to the step S2 to be used as a supplementary absorption liquid for recycling; or when the concentration of the ammonium salt in the ammonia-containing nitrogen solution after the reduction denitration treatment in the step S3 exceeds 75%, discharging the ammonia-containing nitrogen solution out of the system.
3. The method for jointly recovering sulfur dioxide and removing nitrogen oxides in flue gas according to claim 2, wherein in step S2, the initial sulfite absorption solution of the reaction is sodium sulfite solution with a concentration of 10% -20%; in the reaction process, the sulfite absorption liquid is a mixed liquid of sodium sulfite and ammonium sulfite; the mass ratio of the sodium sulfite to the ammonium sulfite in the mixed solution is 25-100%, and the mass ratio of the ammonium sulfite is 0-75%.
4. The method for jointly recovering sulfur dioxide and removing nitrogen oxides in flue gas according to claim 2, wherein in the step S2, the absorption process is performed under the conditions of ambient atmospheric pressure and medium-low temperature.
5. The method for jointly recovering sulfur dioxide and removing nitrogen oxides in flue gas according to claim 2, wherein in the step S2, in the absorption process, part of sulfite in the sulfite absorption solution is oxidized into sulfate which is an oxidation byproduct; part of the nitrite is further oxidized to nitrate.
6. The method for jointly recovering sulfur dioxide and removing nitrogen oxides in flue gas according to claim 2, wherein in the step S2, a supplementary alkali solution is added in the absorption process, and the alkali solution is sodium hydroxide or sodium sulfite.
7. The method for jointly recovering sulfur dioxide and removing nitrogen oxides in flue gas according to claim 2, wherein in step S3, the evaporation regeneration process is implemented by heating decomposition or reduced pressure evaporation process.
8. The method for combined recovery of sulfur dioxide and removal of nitrogen oxides in flue gas according to claim 2, wherein in step S3, the electrochemical reduction denitration process is performed in an electrolytic cell, wherein the anode is Ir-Ru/Ti-based inert electrode, the cathode is Ti-based metal oxide electrode, and the cathode and the anode are separated by a proton exchange membrane.
9. The integrated sulfur dioxide and nitrogen oxide removal process of claim 8, wherein the Ti-based metal oxide electrode is selected from Co3O4/Ti or Fe2O3a/Ti electrode; obtained by coating a metal oxide-supporting thin film on a Ti substrate by a sol-gel method.
10. A system for jointly recovering sulfur dioxide in flue gas and removing nitrogen oxide is characterized by comprising an ozone generator, a desulfurization absorption tower, an evaporation regenerator, an electrochemical reaction tank and an absorption liquid supplement tank which are sequentially connected; and the supplementary absorption liquid in the absorption liquid supplementary pool reflows to the desulfurization absorption tower through a pipeline.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115093005A (en) * | 2022-06-27 | 2022-09-23 | 中节能工程技术研究院有限公司 | Waste alkali liquor oxidation desulfurization method |
| CN115477370A (en) * | 2022-09-02 | 2022-12-16 | 中国科学院生态环境研究中心 | A method for preparing an electrode that efficiently reduces nitrate and significantly reduces the release of nitrous oxide |
| CN116143081A (en) * | 2023-03-08 | 2023-05-23 | 昆明理工大学 | A method for removing nitrogen oxides in concentrated sulfuric acid |
Citations (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5834722A (en) * | 1994-12-12 | 1998-11-10 | Ebara Corporation | Method and apparatus for treating waste gases by exposure to electron beams |
| CN101053748A (en) * | 2007-04-30 | 2007-10-17 | 武汉凯迪电力环保有限公司 | Simultaneously removing various pollutant wet ammonia flue gas cleaning technology and system thereof |
| CN101524620A (en) * | 2009-04-13 | 2009-09-09 | 山西晋丰环保工程设计有限公司 | Segment-based ammonia flue gas desulfurization process and device thereof |
| CN102247750A (en) * | 2011-07-11 | 2011-11-23 | 华东理工大学 | Device and method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process |
| CN102716648A (en) * | 2012-05-16 | 2012-10-10 | 北京航空航天大学 | Method for automatically controlling desulphurization and denitration by flue gas based on pH value and ORP value and apparatus thereof |
| CN103230734A (en) * | 2013-04-19 | 2013-08-07 | 上海交通大学 | Method for combined removal of sulfur dioxide and nitrogen oxide in flue gas |
| CN104258711A (en) * | 2014-09-30 | 2015-01-07 | 上海援梦电力能源科技咨询中心 | Comprehensive treatment method for carrying out desulfurization, denitration, mercury removal and recycling on flue gas of boiler |
| CN105080317A (en) * | 2014-05-05 | 2015-11-25 | 淮南市明月环保科技有限责任公司 | Method for simultaneously reclaiming sulfur and nitrate |
| CN105344215A (en) * | 2015-11-09 | 2016-02-24 | 武汉悟拓科技有限公司 | Flue gas pollutant cooperation removal technology based on electrolysis |
| CN105413422A (en) * | 2015-11-09 | 2016-03-23 | 武汉钢铁(集团)公司 | Ammonia desulphurization and denitrification process for flue gas by synchronization of complexing absorption and electrolytic regeneration |
| CN105727732A (en) * | 2016-04-21 | 2016-07-06 | 成都华西堂环保科技有限公司 | Flue gas synchronous desulfurization, denitration and dust removal technology combined with cold plasma conversion and sodium alkali method |
| CN205461708U (en) * | 2016-01-08 | 2016-08-17 | 华北电力大学 | A process device for tower boiler recirculation flue gas atomization desulfurization wastewater |
| CN205570054U (en) * | 2016-04-18 | 2016-09-14 | 青岛海德威科技有限公司 | Waste gas denitrification facility |
| US20170197180A1 (en) * | 2014-06-05 | 2017-07-13 | Meihua ZOU | Process and device for desulphurization and denitration of flue gas |
| CN107737520A (en) * | 2017-10-17 | 2018-02-27 | 上海交通大学 | The method that coordinated desulfurization denitration is carried out to Flue Gas of Nonferrous Smelting using sodium alkali is circulated |
| CN109012086A (en) * | 2018-07-19 | 2018-12-18 | 昆明理工大学 | The device and method of sulfur dioxide and nitrogen oxides in a kind of purifying smoke |
| CN112320818A (en) * | 2020-10-20 | 2021-02-05 | 昆明理工大学 | Method for oxidizing sulfite in flue gas desulfurization slurry |
| CN112323097A (en) * | 2020-10-16 | 2021-02-05 | 昆明理工大学 | A method and system for removing sulfur dioxide in flue gas by zinc-ammonia complex coupled persulfate advanced oxidation technology |
-
2021
- 2021-02-08 CN CN202110186881.0A patent/CN112915755B/en active Active
Patent Citations (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5834722A (en) * | 1994-12-12 | 1998-11-10 | Ebara Corporation | Method and apparatus for treating waste gases by exposure to electron beams |
| CN101053748A (en) * | 2007-04-30 | 2007-10-17 | 武汉凯迪电力环保有限公司 | Simultaneously removing various pollutant wet ammonia flue gas cleaning technology and system thereof |
| CN101524620A (en) * | 2009-04-13 | 2009-09-09 | 山西晋丰环保工程设计有限公司 | Segment-based ammonia flue gas desulfurization process and device thereof |
| CN102247750A (en) * | 2011-07-11 | 2011-11-23 | 华东理工大学 | Device and method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process |
| CN102716648A (en) * | 2012-05-16 | 2012-10-10 | 北京航空航天大学 | Method for automatically controlling desulphurization and denitration by flue gas based on pH value and ORP value and apparatus thereof |
| CN103230734A (en) * | 2013-04-19 | 2013-08-07 | 上海交通大学 | Method for combined removal of sulfur dioxide and nitrogen oxide in flue gas |
| CN105080317A (en) * | 2014-05-05 | 2015-11-25 | 淮南市明月环保科技有限责任公司 | Method for simultaneously reclaiming sulfur and nitrate |
| US20170197180A1 (en) * | 2014-06-05 | 2017-07-13 | Meihua ZOU | Process and device for desulphurization and denitration of flue gas |
| CN104258711A (en) * | 2014-09-30 | 2015-01-07 | 上海援梦电力能源科技咨询中心 | Comprehensive treatment method for carrying out desulfurization, denitration, mercury removal and recycling on flue gas of boiler |
| CN105344215A (en) * | 2015-11-09 | 2016-02-24 | 武汉悟拓科技有限公司 | Flue gas pollutant cooperation removal technology based on electrolysis |
| CN105413422A (en) * | 2015-11-09 | 2016-03-23 | 武汉钢铁(集团)公司 | Ammonia desulphurization and denitrification process for flue gas by synchronization of complexing absorption and electrolytic regeneration |
| CN205461708U (en) * | 2016-01-08 | 2016-08-17 | 华北电力大学 | A process device for tower boiler recirculation flue gas atomization desulfurization wastewater |
| CN205570054U (en) * | 2016-04-18 | 2016-09-14 | 青岛海德威科技有限公司 | Waste gas denitrification facility |
| CN105727732A (en) * | 2016-04-21 | 2016-07-06 | 成都华西堂环保科技有限公司 | Flue gas synchronous desulfurization, denitration and dust removal technology combined with cold plasma conversion and sodium alkali method |
| CN107737520A (en) * | 2017-10-17 | 2018-02-27 | 上海交通大学 | The method that coordinated desulfurization denitration is carried out to Flue Gas of Nonferrous Smelting using sodium alkali is circulated |
| CN109012086A (en) * | 2018-07-19 | 2018-12-18 | 昆明理工大学 | The device and method of sulfur dioxide and nitrogen oxides in a kind of purifying smoke |
| CN112323097A (en) * | 2020-10-16 | 2021-02-05 | 昆明理工大学 | A method and system for removing sulfur dioxide in flue gas by zinc-ammonia complex coupled persulfate advanced oxidation technology |
| CN112320818A (en) * | 2020-10-20 | 2021-02-05 | 昆明理工大学 | Method for oxidizing sulfite in flue gas desulfurization slurry |
Non-Patent Citations (5)
| Title |
|---|
| CARLOTA RIDRUEJO: "Electrochemical Fenton-based treatment of tetracaine in synthetic and urban wastewater using active and non-active anodes", 《WATER RESEARCH》 * |
| LIMEI CAO: "Electro-thermal treatment of high concentration ammonia in water by gaseous oxidation in liquid phase (GOLP)", 《CHEMOSPHERE》 * |
| 万金泉: "《造纸工业环境工程导论》", 31 August 2005, 北京：中国轻工业出版社 * |
| 易清风: "电化学法去除SO_2/NO_x的研究进展", 《环境污染治理技术与设备》 * |
| 陈杰: "强化SCR脱硝催化剂转化零价汞的初步研究", 《环境科学与技术》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115093005A (en) * | 2022-06-27 | 2022-09-23 | 中节能工程技术研究院有限公司 | Waste alkali liquor oxidation desulfurization method |
| CN115093005B (en) * | 2022-06-27 | 2023-11-10 | 中节能工程技术研究院有限公司 | Waste alkali liquid oxidation desulfurization method |
| CN115477370A (en) * | 2022-09-02 | 2022-12-16 | 中国科学院生态环境研究中心 | A method for preparing an electrode that efficiently reduces nitrate and significantly reduces the release of nitrous oxide |
| CN116143081A (en) * | 2023-03-08 | 2023-05-23 | 昆明理工大学 | A method for removing nitrogen oxides in concentrated sulfuric acid |
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