CN113398952A - Flue gas wide-temperature SCR denitration catalyst and production process thereof - Google Patents
Flue gas wide-temperature SCR denitration catalyst and production process thereof Download PDFInfo
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- CN113398952A CN113398952A CN202110684324.1A CN202110684324A CN113398952A CN 113398952 A CN113398952 A CN 113398952A CN 202110684324 A CN202110684324 A CN 202110684324A CN 113398952 A CN113398952 A CN 113398952A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 104
- 239000003546 flue gas Substances 0.000 title claims abstract description 52
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 21
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 20
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 claims abstract description 20
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 claims abstract description 20
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910052751 metal Inorganic materials 0.000 claims abstract description 13
- 239000002184 metal Substances 0.000 claims abstract description 13
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000005751 Copper oxide Substances 0.000 claims abstract description 10
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910000420 cerium oxide Inorganic materials 0.000 claims abstract description 10
- 229910000423 chromium oxide Inorganic materials 0.000 claims abstract description 10
- 229910000428 cobalt oxide Inorganic materials 0.000 claims abstract description 10
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910000431 copper oxide Inorganic materials 0.000 claims abstract description 10
- 229910000476 molybdenum oxide Inorganic materials 0.000 claims abstract description 10
- QGLKJKCYBOYXKC-UHFFFAOYSA-N nonaoxidotritungsten Chemical compound O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 QGLKJKCYBOYXKC-UHFFFAOYSA-N 0.000 claims abstract description 10
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 claims abstract description 10
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 claims abstract description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910001930 tungsten oxide Inorganic materials 0.000 claims abstract description 10
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 8
- 230000008569 process Effects 0.000 claims abstract description 8
- 239000002808 molecular sieve Substances 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims abstract description 6
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000004408 titanium dioxide Substances 0.000 claims abstract description 5
- 239000002243 precursor Substances 0.000 claims description 55
- 238000001035 drying Methods 0.000 claims description 42
- 230000032683 aging Effects 0.000 claims description 18
- 230000000630 rising effect Effects 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 239000008367 deionised water Substances 0.000 claims description 9
- 229910021641 deionized water Inorganic materials 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 9
- 238000002791 soaking Methods 0.000 claims description 9
- PHFQLYPOURZARY-UHFFFAOYSA-N chromium trinitrate Chemical group [Cr+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O PHFQLYPOURZARY-UHFFFAOYSA-N 0.000 claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical group [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 claims description 6
- 230000009467 reduction Effects 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical group [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- HSJPMRKMPBAUAU-UHFFFAOYSA-N cerium(3+);trinitrate Chemical compound [Ce+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O HSJPMRKMPBAUAU-UHFFFAOYSA-N 0.000 claims description 4
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical group [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 claims description 4
- 229910001981 cobalt nitrate Inorganic materials 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 229910021542 Vanadium(IV) oxide Inorganic materials 0.000 claims description 3
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 claims description 3
- 239000011609 ammonium molybdate Substances 0.000 claims description 3
- 229940010552 ammonium molybdate Drugs 0.000 claims description 3
- 235000018660 ammonium molybdate Nutrition 0.000 claims description 3
- XUFUCDNVOXXQQC-UHFFFAOYSA-L azane;hydroxy-(hydroxy(dioxo)molybdenio)oxy-dioxomolybdenum Chemical compound N.N.O[Mo](=O)(=O)O[Mo](O)(=O)=O XUFUCDNVOXXQQC-UHFFFAOYSA-L 0.000 claims description 3
- UNTBPXHCXVWYOI-UHFFFAOYSA-O azanium;oxido(dioxo)vanadium Chemical compound [NH4+].[O-][V](=O)=O UNTBPXHCXVWYOI-UHFFFAOYSA-O 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 3
- AMKLQLYNAGNCJE-UHFFFAOYSA-N cerium(3+);lanthanum(3+);hexanitrate Chemical compound [La+3].[Ce+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O AMKLQLYNAGNCJE-UHFFFAOYSA-N 0.000 claims description 3
- VGBWDOLBWVJTRZ-UHFFFAOYSA-K cerium(3+);triacetate Chemical compound [Ce+3].CC([O-])=O.CC([O-])=O.CC([O-])=O VGBWDOLBWVJTRZ-UHFFFAOYSA-K 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 229940071125 manganese acetate Drugs 0.000 claims description 3
- UOGMEBQRZBEZQT-UHFFFAOYSA-L manganese(2+);diacetate Chemical compound [Mn+2].CC([O-])=O.CC([O-])=O UOGMEBQRZBEZQT-UHFFFAOYSA-L 0.000 claims description 3
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000004806 packaging method and process Methods 0.000 claims description 3
- 239000000843 powder Substances 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 235000012239 silicon dioxide Nutrition 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 230000035882 stress Effects 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 3
- GRUMUEUJTSXQOI-UHFFFAOYSA-N vanadium dioxide Chemical compound O=[V]=O GRUMUEUJTSXQOI-UHFFFAOYSA-N 0.000 claims description 3
- 229910002651 NO3 Inorganic materials 0.000 claims description 2
- 229910000503 Na-aluminosilicate Inorganic materials 0.000 claims description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 2
- QGAVSDVURUSLQK-UHFFFAOYSA-N ammonium heptamolybdate Chemical compound N.N.N.N.N.N.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.[Mo].[Mo].[Mo].[Mo].[Mo].[Mo].[Mo] QGAVSDVURUSLQK-UHFFFAOYSA-N 0.000 claims description 2
- 239000011230 binding agent Substances 0.000 claims description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 2
- 229920002521 macromolecule Polymers 0.000 claims description 2
- WFLYOQCSIHENTM-UHFFFAOYSA-N molybdenum(4+) tetranitrate Chemical compound [N+](=O)([O-])[O-].[Mo+4].[N+](=O)([O-])[O-].[N+](=O)([O-])[O-].[N+](=O)([O-])[O-] WFLYOQCSIHENTM-UHFFFAOYSA-N 0.000 claims description 2
- 239000000429 sodium aluminium silicate Substances 0.000 claims description 2
- 235000012217 sodium aluminium silicate Nutrition 0.000 claims description 2
- 239000000853 adhesive Substances 0.000 claims 1
- 230000001070 adhesive effect Effects 0.000 claims 1
- MVFCKEFYUDZOCX-UHFFFAOYSA-N iron(2+);dinitrate Chemical group [Fe+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MVFCKEFYUDZOCX-UHFFFAOYSA-N 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 6
- 230000003197 catalytic effect Effects 0.000 abstract description 6
- 231100000572 poisoning Toxicity 0.000 abstract description 4
- 230000000607 poisoning effect Effects 0.000 abstract description 4
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000010304 firing Methods 0.000 abstract description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 45
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 9
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 9
- 235000011130 ammonium sulphate Nutrition 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 8
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 6
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical group [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000000428 dust Substances 0.000 description 5
- 238000006722 reduction reaction Methods 0.000 description 4
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 235000019270 ammonium chloride Nutrition 0.000 description 3
- CAMXVZOXBADHNJ-UHFFFAOYSA-N ammonium nitrite Chemical compound [NH4+].[O-]N=O CAMXVZOXBADHNJ-UHFFFAOYSA-N 0.000 description 3
- 150000003863 ammonium salts Chemical class 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 230000002779 inactivation Effects 0.000 description 3
- 238000005245 sintering Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- -1 coal Chemical class 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 125000004433 nitrogen atom Chemical group N* 0.000 description 1
- 150000002831 nitrogen free-radicals Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 125000004430 oxygen atom Chemical group O* 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
- 229910003158 γ-Al2O3 Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8986—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with manganese, technetium or rhenium
-
- 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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
-
- 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
Abstract
The patent discloses a flue gas wide-temperature SCR denitration catalyst and a production process thereof, and the catalyst comprises a carrier, an active component loaded on the carrier and a forming auxiliary agent for bonding, wherein the carrier is any one of titanium dioxide, aluminum oxide and a molecular sieve; the active component is at least one of platinum group metal, manganese oxide, tungsten oxide, chromium oxide, vanadium pentoxide, cerium oxide, molybdenum oxide, iron oxide, copper oxide and cobalt oxide; the forming auxiliary agent comprises an inorganic auxiliary agent and an organic auxiliary agent. The wide-temperature SCR denitration catalyst disclosed by the invention has the characteristics of high catalytic activity and good nitrogen selectivity in a wider temperature range (60-550 ℃), and has good steam and SO resistance2The poisoning ability and the cost performance are high,the raw materials are easy to obtain; the SCR denitration catalyst production process disclosed by the invention is simple in process, low in energy consumption, high in raw material utilization rate, difficult to crack during firing, high in finished product rate, high in finished product strength and high in catalytic activity.
Description
Technical Field
The invention relates to the field of flue gas denitration, in particular to a flue gas wide-temperature SCR denitration catalyst and a production process thereof.
Background
Along with the increasing improvement of the living standard of people, the consumption of fossil energy is increased year by year, and the problem of air pollution caused by the combustion of fossil fuel gradually draws attention of people. Wherein nitrogen oxides (NOx) are one of three main atmospheric pollutants, which are extremely harmful, and central government and local government have issued many relevant policy and regulation to limit the emission of nitrogen oxides, such as coal, electricity, steel, aluminum industry, cementThe nitrogen oxide emission of the important industry with atmospheric pollution needs to reach the standard of ultralow emission, namely the emission concentration of NOx is less than 50 mg/m3。
Currently, there are three main measures for controlling nitrogen oxides: low nitrogen burner technology (LNB), selective non-catalytic reduction denitration technology (SNCR), selective catalytic reduction denitration technology (SCR). Different technologies have different applicable scenarios and conditions: the LNB is mainly used for controlling NOx generated in the combustion process and reducing the initial generation concentration of the NOx, and the LNB technology can only control the initial concentration of the NOx below a certain concentration and cannot meet the national control requirement on the NOx emission concentration in the smoke; while SNCR and SCR are mainly used to reduce NOx in flue gas, SNCR is suitable for flue gas temperature: 800-1200 ℃, is mainly limited by a reaction mechanism, and can not reduce the use temperature; traditional SCR is suitable for flue gas temperature: 300-420 ℃, is mainly limited by SCR denitration catalyst, and can reduce the temperature of the used flue gas to less than 200 ℃ by adopting different SCR denitration catalysts.
Along with the stricter and stricter emission standards, higher and higher requirements are put forward on the environmental protection technology, the traditional mature denitration technology (LNB, SNCR and SCR) has more problems in the use process of some industries, for example, the flue gas temperature of various roasting furnaces in steel sintering machines and smelting industries is lower, the traditional flue gas selective catalytic denitration (SCR) technology can be normally put into operation only by being heated to a higher temperature (more than 300 ℃), a large amount of energy is wasted, the catalytic activity of the denitration catalyst at a low temperature can be improved by the rapid SCR denitration reaction, and meanwhile, in order to avoid other problems of low-temperature inactivation of the catalyst, such as ammonium bisulfate deposition, water resistance, sulfur poisoning resistance and the like, a special SCR denitration catalyst needs to be matched.
Particularly, due to the limitation of production process, a proper NOx control process temperature window does not exist in some industries, for example, the temperature of flue gas at the outlet of a sintering machine in the steel sintering process is less than 180 ℃; in some industries, flue gas contains components which can poison the SCR catalyst, such as alkali metal dust, tar, sticky dust, heavy metals and the like, for example, flue gas discharged by a coking plant and a waste incineration power plant contains sticky dust, and flue gas generated by a biomass incineration power plant contains alkali metals such as sodium oxide with high concentration, and the flue gas can be denitrated after dust removal. The temperature of the flue gas after dust removal is generally less than 200 ℃, and is not in the range of the temperature of the flue gas used by the traditional SCR denitration catalyst. If the flue gas needs to be denitrated, the flue gas needs to be heated up firstly, and then SCR denitration is carried out after the temperature is raised to about 300 ℃, so that a large amount of energy needs to be consumed for heating the flue gas, and the pollution treatment cost is greatly increased. Therefore, the wide-temperature SCR denitration catalyst with low denitration flue gas temperature, high denitration efficiency and high reliability needs to be developed urgently.
Disclosure of Invention
Aiming at the problems in the existing flue gas SCR denitration technology, the invention provides a flue gas wide-temperature SCR denitration catalyst and a production process thereof, and the SCR catalyst produced according to a formula and a matched production process can carry out SCR high-efficiency denitration on flue gas with the temperature within the range of 60-550 ℃. Novel SCR catalyst can spray NH in SCR upstream flue gas3Conversion to NH at the catalyst surface2Radical (1) with NH2High reactivity of the radicals and NOx in the flue gas can realize wide-temperature SCR (selective catalytic reduction) high-efficiency denitration, (2) NH2With acid gases in the flue gas, e.g. SO2、 SO3HCl, and H in flue gas2The O reaction is very weak, so that ammonium salt layers such AS Ammonium Bisulfate (ABS), Ammonium Sulfate (AS), ammonium chloride, ammonium nitrate, ammonium nitrite and the like are difficult to generate on the surface of the SCR catalyst, and the inactivation of the SCR catalyst during ammonia spraying denitration at low temperature can be avoided.
The technical scheme of the invention is as follows: a flue gas wide-temperature SCR denitration catalyst comprises a carrier, an active component loaded on the carrier and a forming auxiliary agent for bonding, wherein the carrier is any one of titanium dioxide, aluminum oxide and a molecular sieve; the active component is at least one of platinum group metal, manganese oxide, tungsten oxide, chromium oxide, vanadium pentoxide, cerium oxide, molybdenum oxide, iron oxide, copper oxide and cobalt oxide; the forming auxiliary agent comprises an inorganic auxiliary agent and an organic auxiliary agent.
Preferably, anatase titanium dioxide is used when the carrier is titanium dioxide, and gamma-Al is used when the carrier is aluminum oxide2O3When the carrier is a molecular sieve, the carrier adopts silicon dioxide and aluminium oxide as main componentsAnd (5) screening by using a secondary screen.
Preferably, in the active component, a precursor of a platinum group metal is chloroplatinic acid, a precursor of manganese oxide is at least one of manganese nitrate and manganese acetate, a precursor of tungsten oxide is at least one of ammonium tungstate and ammonium metatungstate, a precursor of chromium oxide is chromium nitrate, a precursor of vanadium pentoxide is at least one of ammonium metavanadate and vanadium dioxide, a precursor of cerium oxide is at least one of cerium acetate, cerium nitrate, ammonium ceric nitrate and lanthanum cerium nitrate, a precursor of molybdenum oxide is at least one of ammonium molybdate, ammonium heptamolybdate, ammonium dimolybdate, ammonium tetramolybdate and molybdenum nitrate, a precursor of iron oxide is ferric nitrate, a precursor of copper oxide is copper nitrate, and a precursor of cobalt oxide is cobalt nitrate.
Preferably, the inorganic auxiliary in the forming auxiliary is an inorganic mineral raw material mainly containing sodium aluminosilicate as a main component; the organic assistant in the forming assistant is mainly a binder taking organic macromolecules as main components.
A production process of a flue gas wide-temperature SCR denitration catalyst comprises the following steps:
1) preparing active liquid, namely dissolving a precursor of an active component by using deionized water to prepare a precursor solution with a certain concentration;
2) mixing, adding carrier powder and a proper amount of deionized water, starting stirring, dissolving the active component precursor with the formula amount by using the deionized water, adding the active component precursor into the mixed material, and simultaneously adding a forming auxiliary agent to assist in forming and extruding;
3) ageing, namely putting the catalyst mud blank in an ageing chamber with set temperature and relative humidity for ageing for a period of time to eliminate stress among particles in the catalyst mud blank, and simultaneously enabling the moisture in the catalyst mud blank to be more uniform so as to further improve the performance of the catalyst mud blank;
4) filtering and pre-extruding, namely feeding the aged catalyst mud blank into an extruding device for filtering and pre-extruding, removing impurity blocks in the mixed mud to prevent a mould from being blocked during forming and uniformly dispersing substances in the mud, sealing the mud after filtering and aging again;
5) extruding and forming, namely feeding the secondarily aged mud into an extruding device to extrude the mud according to the required size to form a honeycomb-shaped mud blank, packaging the blank by using a paper box with a sponge lining, and placing the blank on a drying trolley;
6) primary drying, namely conveying the catalyst mud blank formed on the drying trolley into a primary drying chamber for drying, and drying the mud blank by controlling the temperature and humidity of the drying chamber;
7) secondary drying, namely taking the catalyst mud blank subjected to primary drying out of the carton, putting the catalyst mud blank on a secondary drying vehicle, conveying the catalyst mud blank into a secondary drying chamber, and blowing and drying the catalyst mud blank by hot air or high-temperature water vapor until the moisture in the mud blank is reduced to below 5%;
8) primary roasting, namely sequentially passing through a temperature rising section I, a constant temperature section II, a secondary temperature rising section I, a secondary constant temperature section II, a tertiary temperature rising section I, a tertiary constant temperature section II and a temperature reduction section;
9) the active component is reloaded, the roasted catalyst is placed in a liquid tank containing an active component precursor solution with special configuration for soaking for 0.5 to 2 hours, and the liquid in the tank is in a flowing state in the soaking process;
10) and (3) secondary roasting, namely fully fusing the newly loaded active component and the newly fired catalyst together through a temperature rising section I, a constant temperature section II, a secondary temperature rising section I, a secondary constant temperature section II and a temperature reduction section in sequence.
Preferably, the temperature in the ageing room in the step 3) is 15-35 ℃, the relative humidity is more than or equal to 60%, the ageing time is 12-48 hours, and the soaking time in the step 9) is 1 hour.
Preferably, the temperature of the primary drying chamber in the step 6): the primary drying takes 7 to 12 days at a temperature of between 25 and 55 ℃; the temperature of the hot air in the step 7) is (60 +/-5) DEG C, and the humidity is 20 +/-5%.
Preferably, the maximum roasting temperature of the primary roasting in the step 8) is 450-650 ℃, the heating rate is less than or equal to 6 ℃/min, and the cooling rate is less than or equal to 6 ℃/min.
Preferably, the maximum roasting temperature of the secondary roasting in the step 10) is 350-550 ℃, the heating rate is less than or equal to 6 ℃/min, and the cooling rate is less than or equal to 6 ℃/min.
Preferably, the catalyst finished product prepared by the production process at least contains one of active components of platinum group metal, manganese oxide, tungsten oxide, chromium oxide, vanadium pentoxide, cerium oxide, molybdenum oxide, iron oxide, copper oxide and cobalt oxide, and the proportion of any active component in the total mass of the catalyst finished product is less than or equal to 10% in terms of metal content.
The SCR catalyst produced by the invention can spray NH into the upstream of the SCR catalyst by the action of high-energy particles3Adsorbed on the surface of SCR catalyst and converted into NH2Radical, NH, at a temperature of between 60 ℃ and 550 ℃2The group has higher reactivity with NOx in the flue gas, thereby realizing wide-temperature high-efficiency SCR denitration. At the same time, NH adsorbed on the surface of the catalyst3Is reacted to generate NH2Radicals, with SO in flue gases2、SO3The reaction of HCl and NOx is very weak, ammonium salt layers such AS Ammonium Bisulfate (ABS), Ammonium Sulfate (AS), ammonium chloride, ammonium nitrate and ammonium nitrite are difficult to generate, and the inactivation of the SCR catalyst during ammonia spraying denitration at low temperature can be avoided. The wide-temperature SCR catalyst can resist SO in flue gas at the same time even at low temperature2And H2And the toxic effect of O on the denitration reaction process of the SCR denitration catalyst enables the SCR catalyst to be capable of stably and efficiently denitrating at low temperature. Can realize the efficient, stable and reliable SCR denitration within the temperature range of 60-550 ℃.
The wide-temperature SCR denitration catalyst provided by the invention has the characteristics of high catalytic activity and good nitrogen selectivity in a wide temperature range (60-550 ℃), and has good steam and SO resistance2The poisoning ability. The SCR denitration catalyst disclosed by the patent has the advantages of high cost performance and easily obtained raw materials, and the production process of the SCR denitration catalyst disclosed by the invention has the advantages of simple process, low energy consumption, high raw material utilization rate, difficulty in cracking during firing, high finished product rate, high finished product strength and high catalytic activity.
Detailed Description
The present invention is further illustrated in detail by the following examples, which are not intended to limit the scope of the invention.
Example 1
A flue gas wide-temperature SCR denitration catalyst comprises a carrier, an active component loaded on the carrier and a forming auxiliary agent for bonding,
the carrier adopts anatase titanium dioxide;
in the active components, a precursor of platinum group metal is chloroplatinic acid, a precursor of manganese oxide is manganese nitrate, a precursor of tungsten oxide is ammonium tungstate, a precursor of chromium oxide is chromium nitrate, a precursor of vanadium pentoxide is ammonium metavanadate, a precursor of cerium oxide is cerium acetate, a precursor of molybdenum oxide is ammonium molybdate, a precursor of iron oxide is ferric nitrate, a precursor of copper oxide is cupric nitrate, and a precursor of cobalt oxide is cobalt nitrate.
The forming auxiliary agent adopts inorganic auxiliary agent and organic auxiliary agent.
Example 2
The carrier adopts gamma-Al2O3；
In the active components, a precursor of platinum group metal is chloroplatinic acid, a precursor of manganese oxide is manganese acetate, a precursor of tungsten oxide is ammonium metatungstate, a precursor of chromium oxide is chromium nitrate, a precursor of vanadium pentoxide is vanadium dioxide, a precursor of cerium oxide is lanthanum cerium nitrate, a precursor of molybdenum oxide is ammonium dimolybdate, a precursor of iron oxide is ferric nitrate, a precursor of copper oxide is copper nitrate, and a precursor of cobalt oxide is cobalt nitrate;
the forming auxiliary agent adopts inorganic auxiliary agent and organic auxiliary agent.
Example 3
The carrier adopts a molecular sieve taking silicon dioxide and aluminum oxide as main components.
The production process of the flue gas wide-temperature SCR denitration catalyst as claimed in claim 1, comprises the following steps:
1) preparing active liquid, namely dissolving a precursor of an active component by using deionized water to prepare a precursor solution with a certain concentration;
2) mixing, adding carrier powder and a proper amount of deionized water, starting stirring for more than 4 hours, dissolving the active component precursor with the formula amount by using the deionized water, adding the active component precursor into the mixed material, and simultaneously adding a forming auxiliary agent to help forming and extruding a catalyst mud blank;
3) ageing, namely putting the catalyst mud blank in an ageing chamber with set temperature and relative humidity for ageing for a period of time to eliminate stress among particles in the catalyst mud blank, and simultaneously enabling the moisture in the catalyst mud blank to be more uniform so as to further improve the performance of the catalyst mud blank;
4) filtering and pre-extruding, namely feeding the aged catalyst mud blank into an extruding device for filtering and pre-extruding, removing impurity blocks in the mixed mud to prevent a mould from being blocked during forming and uniformly dispersing substances in the mud, sealing the mud after filtering and aging again;
5) extruding and forming, namely feeding the secondarily aged mud into an extruding device to extrude the mud according to the required size to form a honeycomb-shaped mud blank, packaging the blank by using a paper box with a sponge lining, and placing the blank on a drying trolley;
6) primary drying, namely conveying the catalyst mud blank formed on the drying trolley into a primary drying chamber for drying, and drying the mud blank by controlling the temperature and humidity of the drying chamber;
7) secondary drying, namely taking the catalyst mud blank subjected to primary drying out of the carton, putting the catalyst mud blank on a secondary drying vehicle, conveying the catalyst mud blank into a secondary drying chamber, and blowing and drying the catalyst mud blank by hot air or high-temperature water vapor until the moisture in the mud blank is reduced to below 5%;
8) primary roasting, namely sequentially passing through a temperature rising section I, a constant temperature section II, a secondary temperature rising section I, a secondary constant temperature section II, a tertiary temperature rising section I, a tertiary constant temperature section II and a temperature reduction section;
9) the active component is reloaded, the roasted catalyst is placed in a liquid tank containing an active component precursor solution with special configuration for soaking for 0.5 to 2 hours, and the liquid in the tank is in a flowing state in the soaking process;
10) and (3) secondary roasting, namely fully fusing the newly loaded active component and the newly fired catalyst together through a temperature rising section I, a constant temperature section II, a secondary temperature rising section I, a secondary constant temperature section II and a temperature reduction section in sequence.
The temperature in the ageing room in the step 3) is 15-35 ℃, the relative humidity is more than or equal to 60%, the ageing time is 24 hours, and the soaking time in the step 9) is 1 hour.
Temperature of the primary drying chamber in step 6): the primary drying takes 7 to 12 days at a temperature of between 25 and 55 ℃; the temperature of the hot air in the step 7) is (60 +/-5) DEG C, and the humidity is 20 +/-5%. The maximum roasting temperature of the primary roasting in the step 8) is 450-650 ℃, the heating rate is less than or equal to 6 ℃/min, and the cooling rate is less than or equal to 6 ℃/min. The maximum roasting temperature of the secondary roasting in the step 10) is 350-550 ℃, the temperature rising rate is less than or equal to 6 ℃/min, and the temperature reducing rate is less than or equal to 6 ℃/min.
The finished catalyst product prepared by the production process at least contains one of active components of platinum group metal, manganese oxide, tungsten oxide, chromium oxide, vanadium pentoxide, cerium oxide, molybdenum oxide, iron oxide, copper oxide and cobalt oxide, and the proportion of any active component in the total mass of the finished catalyst product is less than or equal to 10% by weight of the metal content.
The SCR catalyst can utilize a reducing agent (such as NH) within a wide range of flue gas temperatures, such as 60-550 DEG C3) On the surface of the catalyst, NOx in the flue gas is catalytically reduced, and the reaction product is N2And H2And O, removing NOx in the flue gas.
The catalyst can spray NH into the upstream of the SCR catalyst at the temperature range of 60-550 ℃ under the action of high-energy particles3Adsorbed on the surface of SCR catalyst and converted into NH2A group and make NH2The group and NOx in the flue gas are subjected to rapid and efficient SCR denitration reaction, so that efficient SCR denitration is realized.
NH adsorbed on the surface of the catalyst3Is reacted to generate NH2Radicals, not capable of reacting with SO in flue gas2、SO3HCl and NOx react to generate ammonium salt layers such AS Ammonium Bisulfate (ABS), Ammonium Sulfate (AS), ammonium chloride, ammonium nitrate and ammonium nitrite, and the SCR catalyst can be prevented from being deactivated during ammonia spraying denitration operation at low temperature.
The SCR catalysts with different active components have different suitable denitration temperatures, and the suitable temperature range of the iron-based SCR catalyst is as follows: 120-550 ℃, and the suitable temperature range of the vanadium-titanium based SCR catalyst is as follows: the temperature is between 80 and 450 ℃, and the suitable temperature range of the copper-based SCR catalyst is as follows: the temperature is 60-400 ℃, and the suitable temperature range of the manganese-based SCR catalyst is as follows: 80 to 450 ℃.
The catalyst can cooperate with high-energy particles to complete SCR denitration reaction, and the high-energy particles contain at least one of active nitrogen atoms, nitrogen free radicals, oxygen free radicals, ozone, active oxygen atoms and the like.
The catalyst has strong steam and SO resistance at low temperature2Capability of poisoning in water vapor and SO2When the catalyst coexists, the nitrogen oxides in the flue gas can be reliably, stably and efficiently removed.
Claims (10)
1. The utility model provides a wide temperature SCR denitration catalyst of flue gas which characterized in that: the adhesive comprises a carrier, an active component loaded on the carrier and a forming aid for adhesion, wherein the carrier is any one of titanium dioxide, aluminum oxide and a molecular sieve; the active component is at least one of platinum group metal, manganese oxide, tungsten oxide, chromium oxide, vanadium pentoxide, cerium oxide, molybdenum oxide, iron oxide, copper oxide and cobalt oxide; the forming auxiliary agent comprises an inorganic auxiliary agent and an organic auxiliary agent.
2. The wide-temperature flue gas SCR denitration catalyst of claim 1, wherein anatase titanium dioxide is used when the carrier is titanium dioxide, and gamma-Al is used when the carrier is aluminum oxide2O3When the carrier is a molecular sieve, the molecular sieve taking silicon dioxide and aluminum oxide as main components is adopted.
3. The flue gas wide-temperature SCR denitration catalyst according to claim 1, wherein a precursor of a platinum group metal in the active component is chloroplatinic acid, a precursor of manganese oxide is at least one of manganese nitrate and manganese acetate, a precursor of tungsten oxide is at least one of ammonium tungstate and ammonium metatungstate, a precursor of chromium oxide is chromium nitrate, a precursor of vanadium pentoxide is at least one of ammonium metavanadate and vanadium dioxide, a precursor of cerium oxide is at least one of cerium acetate, cerium nitrate, ammonium ceric nitrate and lanthanum cerium nitrate, a precursor of molybdenum oxide is at least one of ammonium molybdate, ammonium heptamolybdate, ammonium dimolybdate, ammonium tetramolybdate and molybdenum nitrate, a precursor of iron oxide is iron nitrate, a precursor of copper oxide is copper nitrate, and a precursor of cobalt oxide is cobalt nitrate.
4. The flue gas wide-temperature SCR denitration catalyst of claim 1, wherein the inorganic auxiliary in the forming auxiliary is an inorganic mineral raw material mainly containing sodium aluminosilicate as a main component; the organic assistant in the forming assistant is mainly a binder taking organic macromolecules as main components.
5. The production process of the flue gas wide-temperature SCR denitration catalyst according to claim 1, characterized by comprising the following steps:
1) preparing active liquid, namely dissolving a precursor of an active component by using deionized water to prepare a precursor solution with a certain concentration;
2) mixing, adding carrier powder and a proper amount of deionized water, starting stirring, dissolving the active component precursor with the formula amount by using the deionized water, adding the active component precursor into the mixed material, and simultaneously adding a forming auxiliary agent to assist in forming and extruding;
3) ageing, namely putting the catalyst mud blank in an ageing chamber with set temperature and relative humidity for ageing for a period of time to eliminate stress among particles in the catalyst mud blank, and simultaneously enabling the moisture in the catalyst mud blank to be more uniform so as to further improve the performance of the catalyst mud blank;
4) filtering and pre-extruding, namely feeding the aged catalyst mud blank into an extruding device for filtering and pre-extruding, removing impurity blocks in the mixed mud to prevent a mould from being blocked during forming and uniformly dispersing substances in the mud, sealing the mud after filtering and aging again;
5) extruding and forming, namely feeding the secondarily aged mud into an extruding device to extrude the mud according to the required size to form a honeycomb-shaped mud blank, packaging the blank by using a paper box with a sponge lining, and placing the blank on a drying trolley;
6) primary drying, namely conveying the catalyst mud blank formed on the drying trolley into a primary drying chamber for drying, and drying the mud blank by controlling the temperature and humidity of the drying chamber;
7) secondary drying, namely taking the catalyst mud blank subjected to primary drying out of the carton, putting the catalyst mud blank on a secondary drying vehicle, conveying the catalyst mud blank into a secondary drying chamber, and blowing and drying the catalyst mud blank by hot air or high-temperature water vapor until the moisture in the mud blank is reduced to below 5%;
8) primary roasting, namely sequentially passing through a temperature rising section I, a constant temperature section II, a secondary temperature rising section I, a secondary constant temperature section II, a tertiary temperature rising section I, a tertiary constant temperature section II and a temperature reduction section;
9) the active component is reloaded, the roasted catalyst is placed in a liquid tank containing an active component precursor solution with special configuration for soaking for 0.5 to 2 hours, and the liquid in the tank is in a flowing state in the soaking process;
10) and (3) secondary roasting, namely fully fusing the newly loaded active component and the newly fired catalyst together through a temperature rising section I, a constant temperature section II, a secondary temperature rising section I, a secondary constant temperature section II and a temperature reduction section in sequence.
6. The production process of the flue gas wide-temperature SCR denitration catalyst according to claim 5, characterized by comprising the following steps: the temperature in the ageing room in the step 3) is 15-35 ℃, the relative humidity is more than or equal to 60%, the ageing time is 12-48 hours, and the soaking time in the step 9) is 1 hour.
7. The production process of the flue gas wide-temperature SCR denitration catalyst according to claim 5, characterized by comprising the following steps: the temperature of the primary drying chamber in the step 6): the primary drying takes 7 to 12 days at a temperature of between 25 and 55 ℃; the temperature of the hot air in the step 7) is (60 +/-5) DEG C, and the humidity is 20 +/-5%.
8. The production process of the flue gas wide-temperature SCR denitration catalyst according to claim 5, characterized by comprising the following steps: the maximum roasting temperature of the primary roasting in the step 8) is 450-650 ℃, the heating rate is less than or equal to 6 ℃/min, and the cooling rate is less than or equal to 6 ℃/min.
9. The production process of the flue gas wide-temperature SCR denitration catalyst according to claim 5, characterized by comprising the following steps: the maximum roasting temperature of the secondary roasting in the step 10) is 350-550 ℃, the temperature rising rate is less than or equal to 6 ℃/min, and the temperature reducing rate is less than or equal to 6 ℃/min.
10. The production process of the flue gas wide-temperature SCR denitration catalyst according to claim 5, characterized by comprising the following steps: the finished catalyst product prepared by the production process at least contains one of active components of platinum group metal, manganese oxide, tungsten oxide, chromium oxide, vanadium pentoxide, cerium oxide, molybdenum oxide, iron oxide, copper oxide and cobalt oxide, and the proportion of any active component in the total mass of the finished catalyst product is less than or equal to 10% by weight of the metal content.
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Application publication date: 20210917 |