CN109499307A - The desulfurization denitration method of pelletizing flue gas - Google Patents
The desulfurization denitration method of pelletizing flue gas Download PDFInfo
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- CN109499307A CN109499307A CN201811490500.2A CN201811490500A CN109499307A CN 109499307 A CN109499307 A CN 109499307A CN 201811490500 A CN201811490500 A CN 201811490500A CN 109499307 A CN109499307 A CN 109499307A
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- flue gas
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- molecular sieve
- temperature
- nitrogen oxides
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 239000003546 flue gas Substances 0.000 title claims abstract description 121
- 238000000034 method Methods 0.000 title claims abstract description 39
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 18
- 230000023556 desulfurization Effects 0.000 title claims abstract description 17
- 238000005453 pelletization Methods 0.000 title claims description 15
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 171
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 45
- 230000008929 regeneration Effects 0.000 claims abstract description 26
- 238000011069 regeneration method Methods 0.000 claims abstract description 26
- 238000005245 sintering Methods 0.000 claims abstract description 25
- 239000008188 pellet Substances 0.000 claims abstract description 21
- 150000003839 salts Chemical class 0.000 claims abstract description 15
- 238000010521 absorption reaction Methods 0.000 claims abstract description 6
- 238000001179 sorption measurement Methods 0.000 claims description 77
- 239000002808 molecular sieve Substances 0.000 claims description 39
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 39
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 38
- 239000007789 gas Substances 0.000 claims description 37
- 239000000463 material Substances 0.000 claims description 34
- 239000007921 spray Substances 0.000 claims description 32
- 239000003463 adsorbent Substances 0.000 claims description 27
- 238000001816 cooling Methods 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 239000003054 catalyst Substances 0.000 claims description 22
- 229910021536 Zeolite Inorganic materials 0.000 claims description 21
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 21
- 239000010457 zeolite Substances 0.000 claims description 21
- 229910021529 ammonia Inorganic materials 0.000 claims description 19
- 230000001590 oxidative effect Effects 0.000 claims description 15
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 14
- 238000000605 extraction Methods 0.000 claims description 13
- 239000000779 smoke Substances 0.000 claims description 12
- 238000005507 spraying Methods 0.000 claims description 11
- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 6
- 229910052717 sulfur Inorganic materials 0.000 claims description 5
- 239000011593 sulfur Substances 0.000 claims description 5
- 229910052720 vanadium Inorganic materials 0.000 claims description 5
- 241000269350 Anura Species 0.000 claims description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 3
- 239000000908 ammonium hydroxide Substances 0.000 claims description 3
- -1 forms logistics F Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 230000000737 periodic effect Effects 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 241001417490 Sillaginidae Species 0.000 claims description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 2
- 239000003818 cinder Substances 0.000 claims description 2
- 230000003009 desulfurizing effect Effects 0.000 claims description 2
- 238000011010 flushing procedure Methods 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 150000003464 sulfur compounds Chemical class 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 claims description 2
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 claims 1
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 229910000831 Steel Inorganic materials 0.000 abstract description 3
- 239000010959 steel Substances 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 33
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 21
- 239000013081 microcrystal Substances 0.000 description 18
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- 239000003517 fume Substances 0.000 description 12
- 239000002918 waste heat Substances 0.000 description 11
- 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 description 10
- 238000003795 desorption Methods 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 10
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 10
- 239000000571 coke Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 230000009471 action Effects 0.000 description 6
- 235000019504 cigarettes Nutrition 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000003245 coal Substances 0.000 description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- 241000209094 Oryza Species 0.000 description 4
- 235000007164 Oryza sativa Nutrition 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 235000009566 rice Nutrition 0.000 description 4
- 239000000377 silicon dioxide Substances 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 229910052746 lanthanum Inorganic materials 0.000 description 2
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 description 2
- 239000000395 magnesium oxide Substances 0.000 description 2
- 238000009992 mercerising Methods 0.000 description 2
- 239000011859 microparticle Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229910052761 rare earth metal Inorganic materials 0.000 description 2
- 150000002910 rare earth metals Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910052684 Cerium Inorganic materials 0.000 description 1
- 241000605716 Desulfovibrio Species 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000007853 buffer solution Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- ZMIGMASIKSOYAM-UHFFFAOYSA-N cerium Chemical compound [Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce] ZMIGMASIKSOYAM-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold 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
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052680 mordenite Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006552 photochemical reaction Methods 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 150000003681 vanadium Chemical class 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 229910052727 yttrium Inorganic materials 0.000 description 1
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 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
- B01D53/74—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
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- 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
- B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
-
- 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
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to a kind of method of pellet sintering flue gas desulfurization and denitrification, mainly solves the problem of that existing pellet sintering flue gas desulfurization and denitrification operating cost is high and generate secondary pollution.The present invention is by using the nitrogen oxides and sulfide in the method removing pellet sintering flue gas of absorption, nitrogen oxides in effluent and sulfide after regeneration carry out the technical solution of salt manufacturing processing, preferably solves the above problem, this method can be used in the industrial production of steel plant's flue gas desulfurization and denitrification.
Description
Technical field
The invention belongs to desulphurization denitration technical fields, and in particular to a kind of pellet sintering flue gas desulfurization and denitration method.
Background technique
SO2And NOXIt is the important atmosphere pollution in China, excessive discharge will cause haze, acid rain and photochemical fog
Deng serious harm ecological environment and human health.The burning of fossil fuel is SO2And NOXMain source.Coal be China most
Important natural energy source, as the second largest coal field in China, carbonization of coal is one of industrial coal field primary pollution source, ball
Group's sintering flue gas is the important pollution sources of atmosphere.
Current pellet sintering flue gas desulfurization field is using more for ammonia process, lime/lime stone method, Dual alkali, magnesia
Method etc. is the Wet Flue Gas Desulfurization Technique and semi-dry desulphurization technology of representative.Wet desulphurization absorption rate is high, but such as lime/stone
Lime stone-gypsum, Dual alkali contain small hydrophilic ionic in magnesium oxide method slurries, are taken out of by flue gas, and be emitted into
In atmosphere, while these particle surfaces are easily absorbing sulfur dioxide, sulfur trioxide, hydrogen chloride, hydrogen fluoride, nitrogen oxides, have
Evil organic matter and bacterium etc., cause the significant increasing of atmosphere suspended particles (usually said PM100, PM10, PM2.5 etc.) content
Add, and cause haze and atmospheric photochemical reaction phenomenon, causes serious environmental pollution.Sodium sulfite (potassium) method sulfur removal technology,
Wei Erman-Luo Defa Desulfovibrio technique, organic acid-acylate buffer-solution method sulfur removal technology, regeneration steam energy consumption it is big and
Regeneration rate is low, therefore it is big to industrialize difficulty.The production process that ammonia corrosion is big in the ammonia process of desulfurization, causes equipment burn into and ammonia is
High energy consumption, high pollution process.Semi-dry desulphurization equipment corrosion compared with wet desulphurization is small, is vented without obvious temperature drop, conducive to chimney
Diffusion, but desulfuration efficiency is relatively low, reaction speed is slow.
The mainstream technology in pellet sintering denitrating flue gas field is NH3-SCR denitration, and SCR technology uses catalyst, and catalysis is made
With reducing reaction activity.It, need to be de- using low temperature since flue gas self-temperature is very low (200 DEG C ~ 300 DEG C) in steel plant
Denox catalyst carries out denitration reaction in this temperature range, and need to spray into ammonia into flue gas and make reducing agent.
Individual desulphurization and denitration technique not only takes up a large area, but also invests, operating cost height.Simultaneous SO_2 and NO removal skill
Art, which has, reduces device configuration, saves space, material source is wide, and price is low, renewable the advantages that recycling.Wherein, with work
Property charcoal (coke) technology be representative dry desulfurization denitrification integral technology be the technology most to the heat energy utilization in flue gas.
Chinese patent 201410119747.9 recycles stack gases waste heat using stack gases waste-heat recovery device, reduces
The temperature of stack gases, the activated adoption ability having using coke and low-temperature denitration catalytic capability realize the de- of stack gases
Sulphur, denitration integration.The concrete operation step of the invention is that 1) stack gases first pass through waste gas residual heat recovery unit, and flue is useless
The waste heat of gas is recovered, and temperature is reduced to 100 DEG C ~ 150 DEG C, is subsequently entered in low-temperature SCR desulphurization denitration unit, in flue gas
SO2 is mixed by the flue gas of desulfurization with ammonia by coke adsorbing and removing, take coke as the catalyst of SCR method, denitration reduction occurs
Reaction, completes the removing of NOX；2) coke in low-temperature SCR desulphurization denitration unit is supplied from by elevator and grader leveling blade
The coke feed unit of conveyer composition, the coke after denitration reduction reaction is expelled in coke main tank, periodically by outlet vehicle
It sends outside；3) flue gas of low-temperature SCR desulphurization denitration unit discharge is sent after gas cleaning unit dust separation to chimney, realizes flue
The qualified discharge of exhaust gas.The waste heat recycled in the waste gas residual heat recovery unit is sent in ammonia steaming device, is generated to coke-oven plant
Remained ammonia carries out ammonia still process processing, provides necessary ammonia for the denitration reduction reaction in low-temperature SCR desulphurization denitration unit.
Chinese patent 201810438291.0 discloses a kind of low-sulfur flue gas desulfurization and denitrification device.The device includes adsorption tower
And vibrating screen, adsorption tower are successively arranged the firstth area, the secondth area and third area along flue gas circulating direction, the firstth area is equipped with flue gas air inlet
Mouthful and positioned at smoke air inlet ammonia-spraying grid, third area is equipped with the gas outlet of flue gas, the active carbon flowed is equipped in the secondth area
Layer, active carbon layer are flowed into from the top entry of adsorption tower, outlet at bottom outflow；The connection of the outlet at bottom of vibrating screen and adsorption tower,
And it is connected by the top entry of conveying mechanism and adsorption tower.
Chinese patent CN201611269710.X discloses a kind of sintering flue gas ammonia charcoal combined desulfurization and denitration method, sintering
Flue gas is after the desulfurization of absorbing liquid containing ammonia again through activated carbon adsorption；Carbonaceous raw material, the gold that the active carbon is 2:1 ~ 5:1 by mass ratio
Belong to oxide source to roast to obtain in 850 ~ 1100 DEG C of countrysidies；The carbonaceous raw material is semicoke, or is the mixed of coal and biomass
Close material.In the present invention, the active carbon as made from by ammonia and the method for the invention is combined, can effective desulphurization denitration, also
Help reduce secondary pollution, reduction technique.
Document above is active carbon (coke) simultaneous SO_2 and NO removal, but can not all be detached from ammonia as this step of reducing agent denitration
Suddenly.Since pelletizing flue flow field is uneven, temperature field is uneven, catalyst failure degree is uneven, the volume fraction of escape ammonia is difficult low
In design discipline.Escape ammonia is exceeded to will cause secondary pollution, and corrosion pipeline material, and there is danger in the use process of ammonia
Property, it is very important to the body harm of people.
In view of the above problems, not using ammonia, simultaneously the invention proposes the technology of molecular sieve adsorption simultaneous SO_2 and NO removal
The SO2 and NOx in pelletizing sintering flue gas are adsorbed, and is worth with certain recycling.
Summary of the invention
The technical problem to be solved by the present invention is to during existing steel plant's pellet sintering smoke gas treatment, operating cost
The technical issues of height, generation secondary pollution, provide a kind of method of pellet sintering flue gas low-temperature desulphurization denitration, the processing method
Short with process, low equipment investment, regeneration is simple, and low energy consumption, advantage without secondary pollution.
In order to solve the above technical problems, a kind of method that the present invention uses pellet sintering flue gas low-temperature desulphurization denitration, including
Following steps:
A) the pellet sintering flue gas of pelletizing flue is drawn sulfur compound and nitrogen oxides, is denoted as material flow A, the material flow A
Temperature is 100 ~ 300 DEG C；
B) material flow A enters spray column, and spraying cooling forms flow B to 30 ~ 80 DEG C；
C) flow B enters the adsorption tower comprising crystallite adsorbent, after adsorbing sulfide and nitrogen oxides, forms flow C；
D) flow C enters smoke stack emission；
E) adsorption tower after adsorbing sulfide and nitrogen oxides saturation in step d), with 100 ~ 10000m3The material flow A or heat of/h
Air regenesis, regenerated flue gas form logistics D, wherein the temperature of the logistics D is 120 ~ 300 DEG C；
F) logistics D enters the oxidizing tower comprising oxidation catalyst, after catalysis oxidation, forms logistics E；
G) logistics E enters regeneration tail gas desulfurizing tower, after water or lye spray, forms logistics F, spray liquid enters wastewater treatment
Perhaps salt extraction system perhaps smelts iron flushing cinder system perhaps system for preparing sulfuric acid or sulfur system to system；
Logistics F enters step the spray column in b).In the above-mentioned technical solutions, preferred technical solution is, the material flow A
Temperature is 140 ~ 280 DEG C；Amount of nitrogen oxides is 100 ~ 1000mg/m3, sulfide content is 30 ~ 3000 mg/m3。
In the above-mentioned technical solutions, preferred technical solution is that the denitrating catalyst includes being selected from SSZ-13 molecule
Sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO type molecular sieve, MCM-22, MCM-
49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/Magadiite,
ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/at least one of Y zeolite or ZSM-5/Y zeolite/modenite.
In the above-mentioned technical solutions, preferred technical solution is that also containing in the denitrating catalyst includes element week
At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in phase table.
In above-mentioned technical proposal, preferred technical solution is, before the step b), flue gas carries out UTILIZATION OF VESIDUAL HEAT IN, adopts
With steam pelletizing, the vapor (steam) temperature of production is 140 ~ 180 DEG C；The flue gas that waste heat pelletizing comes out enters back into heat exchanger, and described changes
Hot device is shell and tube or finned heat exchanger.
In above-mentioned technical proposal, preferred technical solution is that the temperature of the flow C is 30 ~ 100 DEG C；Nitrogen oxides
Content is 1 ~ 200mg/m3, sulfide content is 0.1 ~ 100 mg/m3。
In above-mentioned technical proposal, preferred technical solution is that the quantity of adsorption tower is at least more than two, adsorbent bed operation temperature
Degree is 30 ~ 100 DEG C, and operating pressure is 0.1 ~ 20KPa.
In above-mentioned technical proposal, preferred technical solution is that the temperature of the material flow A is 100 ~ 180 DEG C；Nitrogen oxides
Content is 100-1000mg/m3, sulfide content is 40 ~ 3000 mg/m3。
In the above-mentioned technical solutions, preferred technical solution is that the quantity of adsorption tower is at least more than two, adsorbent bed operation
Temperature is 30 ~ 80 DEG C, and operating pressure gauge pressure is 0.5 ~ 5Kpa.
In the above-mentioned technical solutions, preferred technical solution is that it includes X-type molecular sieve, Y that the crystallite adsorbent, which is selected from,
Type molecular sieve, A type molecular sieve, SSZ-13 molecular sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, β type point
Sub- sieve, SAPO type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y,
MCM-22/ modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/Y zeolite or ZSM-
At least one of 5/Y zeolite/modenite.
In the above-mentioned technical solutions, preferred technical solution is that also containing in the crystallite adsorbent includes element week
At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in phase table.
In the above-mentioned technical solutions, preferred technical solution is that containing in the oxidation catalyst includes period of element
At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in table.
In the above-mentioned technical solutions, preferred technical solution is that the lye is sodium hydroxide solution, ammonium hydroxide, residue
At least one of ammonium hydroxide, sodium carbonate liquor, calcium hydroxide solution.
In the above-mentioned technical solutions, the silica alumina ratio of preferred technical solution, the molecular sieve is greater than 2.
In the above-mentioned technical solutions, preferred technical solution, the IIth element A is selected from magnesium and calcium in the periodic table of elements
At least one of；Ith B race element is selected from least one of copper, silver；IIIth B race element in lanthanum, cerium, yttrium at least
It is a kind of.
In the above-mentioned technical solutions, preferred technical solution, ZSM type adsorbent of molecular sieve in the adsorbent of molecular sieve
Selected from including at least one of ZSM-5, ZSM-23, ZSM-11, ZSM-48, wherein the silica alumina ratio of the molecular sieve is greater than
20。
In the above-mentioned technical solutions, preferred technical solution, adsorbent bed operation temperature be 30 ~ 50 DEG C, operating pressure be 1 ~
3Kpa, gauge pressure.
In the above-mentioned technical solutions, preferred technical solution is passed through air, ozone, double water oxygen water in regeneration gas oxidizing tower
At least one of.
In the above-mentioned technical solutions, preferred technical solution, after the adsorbent of molecular sieve adsorption saturation, heat first
Water rinses, then with 100-300 DEG C of nitrogen regeneration.
By adopting the above technical scheme, using crystallite adsorbent desulphurization denitration, crystallite adsorbent to gas cleaning handle just like
Lower advantage: the sulfur dioxide and nitrogen oxides in flue gas can be effectively adsorbed, discharge standard is made up to；High temperature resistant, structure are steady
It is fixed, iterative regenerable；It is high to adsorb precision, other than adsorb sulfur dioxide, can also dedusting simultaneously remove the harmful substances such as dioxin,
Make up to discharge standard；Crystallite adsorbent long service life, does not generate dangerous waste.By setting up adsorption tower in exhanst gas outlet, benefit
Sulfur dioxide, the nitrogen oxides in flue gas are adsorbed with System of Silica/Aluminum Microparticle hydrochlorate crystallite adsorbent, System of Silica/Aluminum Microparticle in adsorption tower
After hydrochlorate crystallite adsorbent adsorption saturation, crystallite adsorbent is regenerated by high-temperature flue gas, the nitrogen oxides and sulphur of desorption
Compound enters oxidizing tower, is oxidized to sulfur trioxide and nitrogen dioxide, and regenerated flue gas is absorbed with water spray, after effluent part neutralizes,
It is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas spray column circulation.Entire treatment process process is short, equipment investment
It saves, regenerative operation is simple and reliable, and low energy consumption, flue gas emission nitrogen oxides≤50mg/m3, sulfur dioxide≤30mg/m3, dust content
Less than 5 mg/m3, achieve preferable technical effect.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
The flue gas of 106 140 DEG C of ten thousand steres, amount of nitrogen oxides 500mg/m3, sulfide content is 2000 mg/m3, flue gas
Into spray column, spraying cooling is to 50 DEG C, into adsorption tower；Using 6 200m3Adsorption tower, 5 open it is 1 standby, in each adsorption tower
Load 150m3Micro crystal material amounts to 900m3Micro crystal material modenite；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；Cigarette
After gas removes sulfide and nitrogen oxides, into smoke stack emission.Nitrogen oxides in effluent content is 50mg/m3, sulfide content is
20 mg/m3。
Dechlorination, desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, automatically switch circular regeneration after adsorption saturation；
Automatically switch within every 7 days a tower regeneration, the adsorption tower 3000m of saturation3The hot fume of/h is regenerated, the nitrogen oxides of desorption
Enter oxidizing tower with sulfide, is oxidized to sulfur trioxide and nitrogen dioxide；After mixed gas cooling, absorbed with water spray, part
After waste water neutralizes, it is discharged into biochemical system, tail gas enters flue gas spray column.
[embodiment 2]
The flue gas of 116 120 DEG C of ten thousand steres, amount of nitrogen oxides 450mg/m3, sulfide content is 1500 mg/m3, flue gas
Into denitrating tower, at 240 DEG C, under ZSM-5 molecular sieve catalyst action, nitrogen oxides is reduced into nitrogen, the flue gas after reaction
Into waste heat pelletizing, steam is generated, flue-gas temperature is reduced to 180 DEG C or so；Then flue gas enters from heat exchanger, and enters chimney
Cold flue gas heat exchange, temperature is reduced to 110 DEG C or so；For 110 DEG C of flue gas by spraying cooling to 50 DEG C, shower water passes through circulation
It uses, after effluent part neutralizes, removes biochemical system；After flue gas after cooling passes through defogging equipment, into adsorption tower；Using 3
200m3Adsorption tower, two open one standby, and 120m is loaded in each adsorption tower3Micro crystal material amounts to 360 m3The boiling of micro crystal material mercerising
Stone；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；After flue gas removes sulfide and nitrogen oxides, into from heat exchanger, and
After hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 50mg/m3, sulfide content
For 20 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, automatically switch circular regeneration after adsorption saturation；Often
Automatically switch within 7 days a tower regeneration, the adsorption tower 3000m of saturation3The hot fume of/h is regenerated, the nitrogen oxides of desorption and
Sulfide enters oxidizing tower, is oxidized to sulfur trioxide and nitrogen dioxide；It after mixed gas cooling, is absorbed with water spray, part is useless
After water neutralizes, it is discharged into biochemical system or going produces salt extraction workshop, tail gas enters flue gas spray column.
[embodiment 2]
The flue gas of 115 160 DEG C of ten thousand steres, amount of nitrogen oxides 400mg/m3, sulfide content is 100 mg/m3, flue gas
Into denitrating tower, at 240 DEG C, under ZSM-5 molecular sieve catalyst action, nitrogen oxides is reduced into nitrogen, the flue gas after reaction
Into waste heat pelletizing, 150 DEG C of steam are generated, flue-gas temperature is reduced to 140 DEG C or so；Then flue gas enters spraying cooling to 40
DEG C, shower water after effluent part neutralizes, removes biochemical system by being recycled；After flue gas after cooling passes through defogging equipment, into
Enter adsorption tower；Using 3 200m3Adsorption tower, two open one standby, and 120m is loaded in each adsorption tower3Micro crystal material amounts to 360
m3Micro crystal material ZSM-5 molecular sieve；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；Flue gas removes sulfide and nitrogen oxides
Afterwards, into from after heat exchanger and hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is
50mg/m3, sulfide content is 20 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, after adsorption saturation certainly
Dynamic switching circular regeneration；Automatically switch within every 7 days a tower regeneration, the adsorption tower 3000m of saturation3The hot fume of/h carries out again
Raw, the nitrogen oxides and sulfide of desorption enter oxidizing tower, are oxidized to sulfur trioxide and nitrogen dioxide；After mixed gas cooling,
It is absorbed with water spray, after effluent part neutralizes, is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas spray column.
[embodiment 3]
The flue gas of 114 130 DEG C of ten thousand steres, amount of nitrogen oxides 450mg/m3, sulfide content is 200 mg/m3, flue gas
Into denitrating tower, at 200 DEG C, under the ZSM-5 molecular sieve catalyst action of copper load, nitrogen oxides is reduced into nitrogen, reaction
Flue gas afterwards enters waste heat pelletizing, generates 160 DEG C of steam, and flue gas is entered back into from heat exchanger, and enters the cold flue gas heat exchange of chimney,
Temperature is reduced to 110 DEG C or so；110 DEG C of flue gas is reduced to 110 DEG C or so by flue-gas temperature；110 DEG C of flue gas passes through spray
Leaching cools to 50 DEG C, and shower water after effluent part neutralizes, removes biochemical system by being recycled；Flue gas after cooling is by removing
After mist equipment, into adsorption tower；Using 3 200m3Adsorption tower, two open one standby, and 120m is loaded in each adsorption tower3Crystallite material
Material amounts to 360 m3Micro crystal material ZSM-5 molecular sieve；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；Flue gas removes devulcanization
After object and nitrogen oxides, into from after heat exchanger and hot fume heat exchange, reach 110 DEG C or more, into smoke stack emission, nitrogen in flue gas
Oxide content is 40mg/m3, sulfide content is 10 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower,
After adsorption saturation, automatically switch circular regeneration with high-temperature flue gas；Automatically switch within every 7 days a tower regeneration, the adsorption tower of saturation is used
3000m3240 DEG C of flue gases of/h are regenerated, and the nitrogen oxides and sulfide of desorption enter the oxidizing tower containing vanadium series catalyst,
It is oxidized to sulfur trioxide and nitrogen dioxide；It after mixed gas cooling, is absorbed with water spray, after effluent part neutralizes, is discharged into biochemistry
System goes to salt extraction workshop, and tail gas enters flue gas spray column.
[embodiment 4]
The flue gas of 120 180 DEG C of ten thousand steres, amount of nitrogen oxides 1000mg/m3, sulfide content is 500 mg/m3, flue gas
By spraying cooling to 40 DEG C, shower water is by being recycled, after effluent part neutralizes, the salt extraction system of going production；After cooling
Flue gas by after defogging equipment, into adsorption tower；Using 4 200m3Adsorption tower, three open one standby, and each adsorption tower is built-in
Fill out 120m3Micro crystal material amounts to 480 m3Micro crystal material SSZ-13 molecular sieve；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；
After flue gas removes sulfide and nitrogen oxides, into from after heat exchanger and hot fume heat exchange, reaches 100 DEG C or more, arranged into chimney
It puts, nitrogen oxides in effluent content is 50mg/m3, sulfide content is 20 mg/m3.Desulphurization and denitration, dedusting are loaded in adsorption tower
Crystallite adsorbent automatically switches circular regeneration after adsorption saturation；Automatically switch within every 7 days a tower regeneration, the adsorption tower of saturation is used
2000m3The hot fume of/h is regenerated, and the nitrogen oxides and sulfide of desorption enter the oxidizing tower containing Cu-series catalyst, oxygen
It is melted into sulfur trioxide and nitrogen dioxide；It after mixed gas cooling, is absorbed with water spray, after effluent part neutralizes, being discharged into production is mentioned
Salt workshop, tail gas enter flue gas spray column.
[embodiment 5]
The flue gas of 120 180 DEG C of ten thousand stere rice, amount of nitrogen oxides 1000mg/m3, sulfide content is 500 mg/m3, cigarette
Gas enters denitrating tower, and at 180 DEG C, under the ZSM-5 molecular sieve catalyst action of copper zinc load, nitrogen oxides is reduced into nitrogen,
Flue gas after reaction enters waste heat pelletizing, generates 150 DEG C of steam, and flue gas cool-down is to 170 DEG C, and then flue gas enters from heat exchanger,
It exchanges heat with the cold flue gas for entering chimney, temperature is reduced to 130 DEG C or so；Flue gas enters spray column, by spraying cooling to 40 DEG C,
Shower water is by being recycled, after effluent part neutralizes, the salt extraction system of going production；Flue gas after cooling passes through defogging equipment
Afterwards, into adsorption tower；Using 4 200m3Adsorption tower, three open one standby, and 120m is loaded in each adsorption tower3Micro crystal material, altogether
Count 480 m3Micro crystal material copper ZSM-5 molecular sieve；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；Flue gas remove sulfide and
After nitrogen oxides, into from after heat exchanger and hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxidation in flue gas
Object content is 40mg/m3, sulfide content is 10 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent, absorption are loaded in adsorption tower
Automatically switch circular regeneration after saturation；Automatically switch within every 7 days a tower regeneration, the adsorption tower 3000m of saturation3180 DEG C of/h
Flue gas is regenerated, and the nitrogen oxides and sulfide of desorption enter the oxidizing tower containing Cu-series catalyst, is oxidized to sulfur trioxide
And nitrogen dioxide；Mixed gas cooling after, absorbed with water spray, effluent part neutralize after, being discharged into production salt extraction workshop, tail gas into
Enter flue gas spray column.
[embodiment 6]
The flue gas of 160 DEG C of 1200000 sides rice, amount of nitrogen oxides 400mg/m3, sulfide content is 100 mg/m3, flue gas into
Enter denitrating tower, at 250 DEG C or so, under the effect of rare earth mordenite catalyst, nitrogen oxides is reduced into nitrogen, the cigarette after reaction
Gas enters waste heat pelletizing, generates 170 DEG C of steam, and flue gas cool-down is to 175 DEG C, and then flue gas enters from heat exchanger, and enters chimney
Cold flue gas heat exchange, temperature is reduced to 130 DEG C or so；Into spraying cooling to 50 DEG C, for shower water by being recycled, part is useless
After water neutralizes, biochemical system is removed；After flue gas after cooling passes through defogging equipment, into adsorption tower；Using 3 200m3Absorption
Tower, two open standby, a filling 120m in each adsorption tower3Micro crystal material amounts to 360 m3Micro crystal material, micro crystal material include lanthanum and
The ZSM-5 molecular sieve of zinc modification；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；Flue gas removes sulfide and nitrogen oxides
Afterwards, into smoke stack emission, nitrogen oxides in effluent content is 30mg/m3, sulfide content 5mg/m3.The interior filling desulfurization of adsorption tower,
Denitration, dedusting crystallite adsorbent, automatically switch circular regeneration after adsorption saturation；Automatically switch within every 7 days a tower regeneration, saturation
Adsorption tower 4000m3180 DEG C of the flue gas of/h is regenerated, and the nitrogen oxides and sulfide of desorption enter oxidizing tower, 250
DEG C it is oxidized to sulfur trioxide and nitrogen dioxide；It after mixed gas cooling, is absorbed with water spray, after effluent part neutralizes, is discharged into life
Change system goes to salt extraction workshop, and tail gas enters flue gas spray column.
[embodiment 7]
The flue gas of 108 140 DEG C of ten thousand stere rice, amount of nitrogen oxides 400mg/m3, sulfide content is 100 mg/m3, cigarette
Gas enters denitrating tower, and at 240 DEG C, under rare-earth Y molecular sieve catalyst action, nitrogen oxides is reduced into nitrogen, the cigarette after reaction
Gas enters afterheat steam pelletizing, generates 145 DEG C of steam, and flue gas cool-down is to 160 DEG C, and by spraying cooling to 40 DEG C, shower water is logical
It crosses recycling and removes biochemical system after effluent part neutralizes；After flue gas after cooling passes through defogging equipment, into adsorption tower；It adopts
With 3 200m3Adsorption tower, two open one standby, and 120m is loaded in each adsorption tower3Micro crystal material amounts to 360 m3Micro crystal material
ZSM-5 molecular sieve；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；After flue gas removes sulfide and nitrogen oxides, into certainly
After heat exchanger and hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 50mg/m3, sulphur
Compound content is 20 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, automatically switch to follow after adsorption saturation
Ring regeneration；Automatically switch within every 7 days a tower regeneration, the adsorption tower 3000m of saturation3The hot fume of/h is regenerated, desorption
Nitrogen oxides and sulfide enter oxidizing tower, are oxidized to sulfur trioxide and nitrogen dioxide；After mixed gas cooling, inhaled with water spray
It receives, after effluent part neutralizes, is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas spray column.
[embodiment 8]
The flue gas of 118 110 DEG C of ten thousand stere rice, amount of nitrogen oxides 400mg/m3, sulfide content is 100 mg/m3, cigarette
Gas enters denitrating tower, and at 210 DEG C, under the ZSM-5 molecular sieve catalyst action of copper and tungsten load, nitrogen oxides is reduced into nitrogen
Gas, the flue gas after reaction enter waste heat pelletizing, generate 160 DEG C of steam, and flue gas cool-down is to 185 DEG C, and then flue gas enters from heat exchange
Device, and enter the cold flue gas heat exchange of chimney, temperature is reduced to 130 DEG C or so；By spraying cooling to 50 DEG C, shower water is by following
Ring uses, and after effluent part neutralizes, goes to the salt extraction workshop of coking；After flue gas after cooling passes through defogging equipment, into adsorption tower；
Using 4 200m3Adsorption tower, three open one standby, and 150m is loaded in each adsorption tower3Micro crystal material amounts to 600 m3Contain mercerising
The micro crystal material of zeolite and ZSM-5 molecular sieve；Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high；Flue gas removes sulfide and nitrogen
After oxide, into from after heat exchanger and hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent
Content is 50mg/m3, sulfide content is 20 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, absorption is full
With rear automatic switchover circular regeneration；Automatically switch within every 7 days a tower regeneration, the adsorption tower 4000m of saturation3240 DEG C of/h
Flue gas is regenerated, and the nitrogen oxides and sulfide of desorption enter oxidizing tower, is oxidized to sulfur trioxide and nitrogen dioxide；Gaseous mixture
It after body cooling, is absorbed with water spray, after effluent part neutralizes, is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas
Spray column.
Claims (10)
1. a kind of method of pellet sintering flue gas low-temperature desulphurization denitration, comprising the following steps:
A) the pellet sintering flue gas of pelletizing flue is drawn sulfur compound and nitrogen oxides, is denoted as material flow A, the material flow A
Temperature is 100 ~ 300 DEG C；
B) material flow A enters spray column, and spraying cooling forms flow B to 30 ~ 80 DEG C；
C) flow B enters the adsorption tower comprising crystallite adsorbent, after adsorbing sulfide and nitrogen oxides, forms flow C；
D) flow C enters smoke stack emission；
E) adsorption tower after adsorbing sulfide and nitrogen oxides saturation in step d), with 100 ~ 10000m3The material flow A or heat of/h
Air regenesis, regenerated flue gas form logistics D, wherein the temperature of the logistics D is 120 ~ 300 DEG C；
F) logistics D enters the oxidizing tower comprising oxidation catalyst, after catalysis oxidation, forms logistics E；
G) logistics E enters regeneration tail gas desulfurizing tower, after water or lye spray, forms logistics F, spray liquid enters at waste water
Perhaps salt extraction system perhaps smelts iron flushing cinder system perhaps system for preparing sulfuric acid or sulfur system to reason system；
H) logistics F enters step the spray column in b).
2. the method for pellet sintering flue gas desulfurization and denitrification according to claim 1, it is characterised in that the temperature of the material flow A
Degree is 140 ~ 280 DEG C；Amount of nitrogen oxides is 100 ~ 1000mg/m3, sulfide content is 30 ~ 3000 mg/m3。
3. the method for pellet sintering flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that the crystallite
Adsorbent include selected from SSZ-13 molecular sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve,
SAPO type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/
Modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/Y zeolite or ZSM-5/Y zeolite/
At least one of modenite.
4. according to the method for the pellet sintering flue gas low-temperature desulphurization denitration that claim 3 is stated, it is characterised in that the crystallite is inhaled
Also containing including the Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race member in the periodic table of elements in attached dose
At least one of element element.
5. the method for pellet sintering flue gas desulfurization and denitrification according to claim 1, it is characterised in that the temperature of the flow C
Degree is 30 ~ 150 DEG C, and amount of nitrogen oxides is 1 ~ 200mg/m3, sulfide content is 0.1 ~ 100 mg/m3；The logistics E's
Temperature is 100 ~ 350 DEG C.
6. the method for pellet sintering flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that the absorption
For the quantity of tower at least more than two, adsorbent bed operation temperature is 20 ~ 100 DEG C, and operating pressure is 0.1 ~ 20KPa.
7. the method for pellet sintering flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that institute in step f)
The oxidation catalyst stated be selected from including X-type molecular sieve, Y type molecular sieve, A type molecular sieve, SSZ-13 molecular sieve, TS-1, Ti-MWW,
Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-
5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/silk
Geolyte, ZSM-5/ β zeolite/at least one of Y zeolite or ZSM-5/Y zeolite/modenite.
8. the method for pellet sintering flue gas low-temperature desulphurization denitration according to claim 7, it is characterised in that the oxidation
Also containing including the Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race in the periodic table of elements in catalyst
At least one of element element.
9. the method for pellet sintering flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that the logistics D
Into before oxidizing tower, oxidizing tower is entered back into after catalysis reduction into the denitrating tower comprising denitrating catalyst.
10. the method for the pellet sintering flue gas low-temperature desulphurization denitration stated according to claim 1, it is characterised in that described in step g)
Lye be at least one of sodium hydroxide solution, ammonium hydroxide, remained ammonia, sodium carbonate liquor, calcium hydroxide solution.
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| CN113509827B (en) * | 2021-04-19 | 2022-05-03 | 中冶长天国际工程有限责任公司 | Temperature control method in sintering flue gas multi-pollutant treatment process |
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