CN116447886A - Method for utilizing combustible CO in sintering flue gas through catalytic combustion - Google Patents
Method for utilizing combustible CO in sintering flue gas through catalytic combustion Download PDFInfo
- Publication number
- CN116447886A CN116447886A CN202310449918.3A CN202310449918A CN116447886A CN 116447886 A CN116447886 A CN 116447886A CN 202310449918 A CN202310449918 A CN 202310449918A CN 116447886 A CN116447886 A CN 116447886A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- reaction
- sintering flue
- combustible
- precipitate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 75
- 239000003546 flue gas Substances 0.000 title claims abstract description 75
- 238000005245 sintering Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000007084 catalytic combustion reaction Methods 0.000 title claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 73
- 239000003054 catalyst Substances 0.000 claims abstract description 57
- 238000002485 combustion reaction Methods 0.000 claims abstract description 46
- 230000003197 catalytic effect Effects 0.000 claims abstract description 30
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 25
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 12
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 11
- 230000023556 desulfurization Effects 0.000 claims abstract description 11
- 229910052751 metal Inorganic materials 0.000 claims abstract description 11
- 239000002184 metal Substances 0.000 claims abstract description 11
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 11
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 11
- 229910052684 Cerium Inorganic materials 0.000 claims abstract description 7
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims abstract description 7
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000013329 compounding Methods 0.000 claims abstract description 7
- 229910052748 manganese Inorganic materials 0.000 claims abstract description 7
- 239000011572 manganese Substances 0.000 claims abstract description 7
- 238000001556 precipitation Methods 0.000 claims abstract description 7
- 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 40
- 238000010438 heat treatment Methods 0.000 claims description 33
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 32
- 239000002244 precipitate Substances 0.000 claims description 30
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 29
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 24
- 239000000047 product Substances 0.000 claims description 22
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 claims description 20
- 239000012286 potassium permanganate Substances 0.000 claims description 20
- 238000005303 weighing Methods 0.000 claims description 19
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 18
- 238000004321 preservation Methods 0.000 claims description 18
- FVAUCKIRQBBSSJ-UHFFFAOYSA-M sodium iodide Chemical compound [Na+].[I-] FVAUCKIRQBBSSJ-UHFFFAOYSA-M 0.000 claims description 18
- 238000003756 stirring Methods 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000001816 cooling Methods 0.000 claims description 16
- 239000008367 deionised water Substances 0.000 claims description 16
- 229910021641 deionized water Inorganic materials 0.000 claims description 16
- 238000005406 washing Methods 0.000 claims description 16
- 238000001354 calcination Methods 0.000 claims description 14
- 238000001291 vacuum drying Methods 0.000 claims description 14
- 239000000377 silicon dioxide Substances 0.000 claims description 13
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 238000002360 preparation method Methods 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 11
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 claims description 9
- 239000006185 dispersion Substances 0.000 claims description 8
- -1 polytetrafluoroethylene Polymers 0.000 claims description 8
- BOTDANWDWHJENH-UHFFFAOYSA-N Tetraethyl orthosilicate Chemical compound CCO[Si](OCC)(OCC)OCC BOTDANWDWHJENH-UHFFFAOYSA-N 0.000 claims description 7
- 238000001132 ultrasonic dispersion Methods 0.000 claims description 7
- GPNNOCMCNFXRAO-UHFFFAOYSA-N 2-aminoterephthalic acid Chemical compound NC1=CC(C(O)=O)=CC=C1C(O)=O GPNNOCMCNFXRAO-UHFFFAOYSA-N 0.000 claims description 6
- OBOSXEWFRARQPU-UHFFFAOYSA-N 2-n,2-n-dimethylpyridine-2,5-diamine Chemical compound CN(C)C1=CC=C(N)C=N1 OBOSXEWFRARQPU-UHFFFAOYSA-N 0.000 claims description 6
- HPTYUNKZVDYXLP-UHFFFAOYSA-N aluminum;trihydroxy(trihydroxysilyloxy)silane;hydrate Chemical group O.[Al].[Al].O[Si](O)(O)O[Si](O)(O)O HPTYUNKZVDYXLP-UHFFFAOYSA-N 0.000 claims description 6
- 229910052621 halloysite Inorganic materials 0.000 claims description 6
- 239000002071 nanotube Substances 0.000 claims description 6
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 6
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 6
- 239000001267 polyvinylpyrrolidone Substances 0.000 claims description 6
- 235000013855 polyvinylpyrrolidone Nutrition 0.000 claims description 6
- 229920000036 polyvinylpyrrolidone Polymers 0.000 claims description 6
- 235000009518 sodium iodide Nutrition 0.000 claims description 6
- DUNKXUFBGCUVQW-UHFFFAOYSA-J zirconium tetrachloride Chemical compound Cl[Zr](Cl)(Cl)Cl DUNKXUFBGCUVQW-UHFFFAOYSA-J 0.000 claims description 6
- 239000002904 solvent Substances 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 238000001035 drying Methods 0.000 claims description 2
- 235000019441 ethanol Nutrition 0.000 claims description 2
- 230000001681 protective effect Effects 0.000 claims description 2
- 239000002131 composite material Substances 0.000 abstract description 7
- WYCDUUBJSAUXFS-UHFFFAOYSA-N [Mn].[Ce] Chemical compound [Mn].[Ce] WYCDUUBJSAUXFS-UHFFFAOYSA-N 0.000 abstract description 4
- 229910000510 noble metal Inorganic materials 0.000 abstract description 3
- 230000001699 photocatalysis Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 235000012239 silicon dioxide Nutrition 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000006479 redox reaction Methods 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 229910052727 yttrium Inorganic materials 0.000 description 3
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000010453 quartz Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 229910001928 zirconium oxide Inorganic materials 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 239000013207 UiO-66 Substances 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009529 body temperature measurement Methods 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 229910000420 cerium oxide Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000011247 coating layer Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 description 1
- SIWVEOZUMHYXCS-UHFFFAOYSA-N oxo(oxoyttriooxy)yttrium Chemical compound O=[Y]O[Y]=O SIWVEOZUMHYXCS-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000003930 superacid Substances 0.000 description 1
- RVRKDGLTBFWQHH-UHFFFAOYSA-N yttrium zirconium Chemical compound [Y][Zr][Y] RVRKDGLTBFWQHH-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- 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
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/656—Manganese, technetium or rhenium
- B01J23/6562—Manganese
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/03—Precipitation; Co-precipitation
- B01J37/031—Precipitation
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/03—Precipitation; Co-precipitation
- B01J37/031—Precipitation
- B01J37/035—Precipitation on carriers
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/08—Heat treatment
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/113—Silicon oxides; Hydrates thereof
- C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27M—INDEXING SCHEME RELATING TO ASPECTS OF THE CHARGES OR FURNACES, KILNS, OVENS OR RETORTS
- F27M2003/00—Type of treatment of the charge
- F27M2003/04—Sintering
-
- 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)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Inorganic Chemistry (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a method for utilizing combustible CO in sintering flue gas by catalytic combustion, which belongs to the technical field of sintering flue gas treatment, wherein the sintering flue gas is sequentially subjected to desulfurization, wet electric precipitation and denitration treatment and then enters a reaction tower, a CO catalytic combustor is arranged in the reaction tower, the CO catalytic combustor is internally provided with a combustion catalyst, and a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that flue gas combusted by the CO combustion catalyst exchanges heat with flue gas before denitration treatment after passing through the heat exchanger; the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium with palladium metal; the invention uses the photocatalytic activity of the manganese-cerium composite metal oxide, uses the manganese-cerium composite metal oxide for the CO combustion catalyst and replaces part of noble metal palladium, and the composite catalyst has low cost and good low-temperature catalytic performance.
Description
Technical Field
The invention relates to the technical field of sintering flue gas treatment, in particular to a method for utilizing CO catalytic combustion of combustible substances in sintering flue gas.
Background
For the treatment of steel flue gas pollutants, the sintering flue gas nitrogen oxide control technology is focused on. In the existing sintering flue gas desulfurization and denitration technology, the current stable sintering flue gas desulfurization and denitration technology is a wet desulfurization and medium-high temperature SCR denitration technology, and the SCR flue gas denitration technology is characterized in that under the action of proper temperature and catalyst, a reducing agent (liquid ammonia, ammonia water or urea) and NO in flue gas x Reduction reaction occurs to make NO x Conversion to N 2 And H 2 O, thereby realizing NO x The aim of removal is that the SCR denitration technology is divided into a medium-high temperature SCR denitration technology and a low-temperature SCR denitration technology according to different reaction temperature ranges of the SCR catalyst, wherein the suitable flue gas reaction temperature of the medium-high temperature SCR denitration catalyst is 280-410 ℃, so that the medium-high temperature SCR denitration technology can reach the denitration reaction temperature only by carrying out heat exchange/heat compensation heating on low-temperature flue gas after desulfurization, and most of heat compensation energy mediums in the prior art adopt blast furnace gas for heat exchange/heat compensation heating.
The fuel heat-supplementing cost of changing/heat-supplementing and heating by adopting blast furnace gas is high, and carbon emission can be increased. It is notable that the sintering flue gas of steel mill has low temp. and high oxygen content, and at the same time is influenced by raw material, fuel and carbon adding quantity, and the sintering flue gas contains a large quantity of combustible component CO whose concentration is typically 6000-12000 mg/Nm3, and CO is rich in chemical energy and oxidated into CO 2 A large amount of heat can be released to heat the flue gas. Calculated, 0.48% of the CO is fully oxidized to CO 2 The temperature of the flue gas can be raised by 30-45 ℃. If usedCO in the sintering flue gas is subjected to catalytic oxidation to replace fuel heat compensation, so that the pollution reduction purpose can be achieved, and the carbon reduction effect can be achieved.
At present, CO catalytic oxidation is usually carried out under the action of a catalyst, but the combustion catalysis used in the prior art is mainly noble metals, such as palladium, ruthenium and the like, and can effectively reduce the combustion oxidation temperature of CO, but the treatment cost is higher, so that the development of the combustion catalyst with low cost and high catalytic effect has important practical application significance.
Disclosure of Invention
Aiming at the problems, the invention provides a method for utilizing CO as a combustible substance in sintering flue gas through catalytic combustion.
The aim of the invention is realized by adopting the following technical scheme:
the method comprises the steps of sequentially carrying out desulfurization, wet electric precipitation and denitration treatment on the sintering flue gas, then introducing the sintering flue gas into a reaction tower, wherein a CO catalytic combustor is arranged in the reaction tower, a combustion catalyst is arranged in the CO catalytic combustor, and a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that the flue gas combusted by the CO catalytic combustor exchanges heat with the flue gas before denitration treatment after passing through the heat exchanger;
the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium and palladium metal.
Preferably, the preparation method of the combustion catalyst comprises the following steps:
respectively weighing cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate, respectively preparing into solutions, firstly mixing the cerium nitrate solution and the potassium hydroxide solution, stirring and heating to 30-40 ℃, then adding the potassium permanganate solution and the palladium nitrate solution, continuously preserving heat and stirring for 30-60min, collecting precipitate after the reaction is finished, washing with deionized water for several times, vacuum drying, heating the dried precipitate to 400-500 ℃ at a speed of 5-10 ℃/min, preserving heat and calcining for 1-2h, and cooling after calcining to obtain the combustion catalyst.
Preferably, the combustion catalyst is supported on a porous carrier, and the preparation method of the combustion catalyst comprises the following steps:
and (3) weighing the porous carrier, dispersing the porous carrier in deionized water, stirring and dispersing the porous carrier in protective atmosphere to obtain dispersion liquid, respectively weighing cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate, respectively preparing the dispersion liquid into solutions, firstly mixing and adding the cerium nitrate solution and the potassium hydroxide solution into the dispersion liquid, stirring and heating to 30-40 ℃, then adding the potassium permanganate solution and the palladium nitrate solution, continuing to perform heat preservation and stirring reaction for 30-60min, collecting precipitate after the reaction is finished, washing the precipitate with deionized water for several times, drying the precipitate in vacuum, heating the dried precipitate to 400-500 ℃ at a speed of 5-10 ℃/min, performing heat preservation and calcination for 1-2h, and cooling the calcined precipitate to obtain the combustion catalyst.
Preferably, the concentration of the cerium nitrate solution is 0.3-0.5mol/L, the concentration of the sodium hydroxide solution is 4-8mol/L, the concentration of the potassium permanganate solution is 0.1-0.4mol/L, the concentration of the palladium nitrate solution is 0.2-0.3mol/L, and the molar ratio of the cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate is (3-5): (10-12): (0.4-0.5): 1.
preferably, the porous support is halloysite nanotubes or porous silica.
Preferably, the porous carrier is modified porous silica, and the preparation method comprises the following steps:
(1) Respectively weighing zirconium chloride and 2-amino terephthalic acid, dissolving in a dimethylformamide solvent, fully mixing, adding acetic acid, carrying out ultrasonic dispersion, transferring into a high-pressure reaction kettle with a polytetrafluoroethylene lining, heating to 120-140 ℃, carrying out heat preservation and reaction for 40-48 hours under autogenous pressure, cooling to room temperature after the reaction is finished, separating precipitate, washing with anhydrous methanol for a plurality of times, and carrying out vacuum drying to obtain a product A;
(2) Weighing the product A, dispersing in deionized water, sequentially adding polyvinylpyrrolidone, yttrium chloride and sodium iodide, ultrasonically dispersing, transferring into a high-pressure reaction kettle with a polytetrafluoroethylene lining, heating to 160-180 ℃, carrying out heat preservation reaction for 1-2h, self-cooling to room temperature after the reaction is finished, separating precipitate, washing with anhydrous methanol for several times, and carrying out vacuum drying to obtain a product B;
(3) Weighing tetraethoxysilane, dissolving the tetraethoxysilane in absolute ethyl alcohol to prepare a solution with the mass concentration of 1-2%, adding 1% deionized water according to the volume fraction, adjusting the pH to be acidic, adding the product B according to the feed liquid ratio of 1-3g/100mL, heating to 30-40 ℃ after ultrasonic dispersion, carrying out heat preservation and stirring reaction for 4-8h, separating precipitate after the reaction is finished, washing with absolute methanol or ethanol, and carrying out vacuum drying to obtain a product C;
(4) Heating the product C to 400-500 ℃ at a speed of 5-10 ℃/min, preserving heat, calcining for 1-2h, and cooling to obtain the modified porous silica.
Preferably, the mass ratio of the zirconium chloride to the 2-amino terephthalic acid to the acetic acid in the step (1) is 1: (0.75-0.8): (12-14).
Preferably, the mass ratio of the product A in the step (2) to the polyvinylpyrrolidone, yttrium chloride and sodium iodide is 10: (12-15): (0.15-0.2): (5.5-5.8).
Preferably, the heat exchanger is a GGH heat exchanger.
Preferably, the reaction tower is an SCR method denitration reaction tower.
The beneficial effects of the invention are as follows:
(1) According to the invention, the combustion catalyst is arranged in the original denitration reactor, so that after the flue gas at the outlet of the denitration reactor exchanges heat with the flue gas before the denitration reactor, the temperature of the flue gas before the denitration reactor can be raised by about 15 ℃, and the consumption of blast furnace gas is reduced by about 50%; the flue gas heat-supplementing mode before the denitration reactor is changed from hot blast stove heating to burner direct combustion heating, and the burner direct combustion heating can burn and consume 5-8% of the sintered flue gas combustible CO, thereby saving the consumption of blast furnace gas.
(2) The invention utilizes the photocatalytic activity of the manganese-cerium composite metal oxide, uses the manganese-cerium composite metal oxide for the combustion catalyst of CO, improves the combustion catalytic performance through the photocatalytic activity, reduces the combustion temperature, can be used for replacing part of noble metal palladium, and has low cost and good low-temperature catalytic performance after being compounded with palladium metal, wherein cerium oxide can be used as a cocatalyst to effectively and rapidly perform the following stepsThe invention also utilizes the reducing Ce (OH) in the water phase through the self-oxidation reduction reaction 3 And oxidative MnO 4 - /Pd 2+ The oxidation-reduction reaction between the two components is carried out to prepare the uniformly dispersed composite catalyst, so that the catalytic performance is improved; furthermore, the composite catalyst prepared by the self-oxidation reduction reaction is uniformly coated on the surface of the porous carrier in situ to form an assembled structure by the porous carrier, so that the combustion catalytic performance and the catalytic stability of the catalyst can be further improved; furthermore, the invention also takes modified silicon dioxide as a carrier material to realize efficient catalysis of CO, specifically, the invention takes yttrium doped UiO-66 metal organic frame material as a template, generates a silicon dioxide coating layer on the surface in situ, and carries out heat treatment on the yttrium-containing metal organic frame coated with mesoporous silicon dioxide to obtain the yttrium oxide stabilized zirconium oxide modified silicon dioxide with a multi-level pore structure, and the yttrium-zirconium solid super acid loaded by the yttrium stabilized zirconium oxide modified silicon dioxide is used as a porous carrier with high specific surface area, can efficiently catalyze oxidation of CO, and greatly improves combustion catalytic performance.
Detailed Description
The invention will be further described with reference to the following examples.
Example 1
The method comprises the steps of sequentially carrying out desulfurization, wet electric precipitation and denitration treatment on the sintering flue gas, then introducing the sintering flue gas into a reaction tower, wherein a CO catalytic combustor is arranged in the reaction tower, a combustion catalyst is arranged in the CO catalytic combustor, and a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that the flue gas combusted by the CO catalytic combustor exchanges heat with the flue gas before denitration treatment after passing through the heat exchanger;
the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium with palladium metal;
the heat exchanger is a GGH heat exchanger;
the reaction tower is an SCR denitration reaction tower;
the preparation method of the combustion catalyst comprises the following steps:
respectively weighing cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate, respectively preparing into solutions, wherein the concentration of the cerium nitrate solution is 0.4mol/L, the concentration of the sodium hydroxide solution is 6mol/L, the concentration of the potassium permanganate solution is 0.2mol/L, the concentration of the palladium nitrate solution is 50mg/mL, firstly mixing the cerium nitrate solution and the potassium hydroxide solution, stirring and heating to 30 ℃, and then adding the potassium permanganate solution and the palladium nitrate solution, wherein the mixing volume ratio of the cerium nitrate solution, the potassium hydroxide solution, the potassium permanganate solution and the palladium nitrate solution is 10:2:2: and 5, continuing to perform heat preservation and stirring reaction for 30min, collecting precipitate after the reaction is finished, washing the precipitate with deionized water for several times, performing vacuum drying, heating the dried precipitate to 450 ℃ at a speed of 5-10 ℃/min, performing heat preservation and calcination for 2h, and cooling after calcination to obtain the combustion catalyst.
Example 2
The method comprises the steps of sequentially carrying out desulfurization, wet electric precipitation and denitration treatment on the sintering flue gas, then introducing the sintering flue gas into a reaction tower, wherein a CO catalytic combustor is arranged in the reaction tower, a combustion catalyst is arranged in the CO catalytic combustor, and a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that the flue gas combusted by the CO catalytic combustor exchanges heat with the flue gas before denitration treatment after passing through the heat exchanger;
the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium with palladium metal;
the heat exchanger is a GGH heat exchanger;
the reaction tower is an SCR denitration reaction tower;
the preparation method of the combustion catalyst comprises the following steps:
weighing halloysite nanotubes, and dispersing the halloysite nanotubes in deionized water according to a feed-liquid ratio of 10g/100mL to obtain a dispersion liquid; respectively weighing cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate, preparing into solutions respectively, wherein the concentration of the cerium nitrate solution is 0.4mol/L, the concentration of the sodium hydroxide solution is 6mol/L, the concentration of the potassium permanganate solution is 0.2mol/L, the concentration of the palladium nitrate solution is 50mg/mL, firstly mixing the cerium nitrate solution and the potassium hydroxide solution into the dispersion, stirring and heating to 30 ℃, then adding the potassium permanganate solution and the palladium nitrate solution, and the mixing volume ratio of the cerium nitrate solution, the potassium hydroxide solution, the potassium permanganate solution and the palladium nitrate solution is 10:10:2:2: and 5, continuing to perform heat preservation and stirring reaction for 30min, collecting precipitate after the reaction is finished, washing the precipitate with deionized water for several times, performing vacuum drying, heating the dried precipitate to 450 ℃ at a speed of 5-10 ℃/min, performing heat preservation and calcination for 2h, and cooling after calcination to obtain the combustion catalyst.
Example 3
The method comprises the steps of sequentially carrying out desulfurization, wet electric precipitation and denitration treatment on the sintering flue gas, then introducing the sintering flue gas into a reaction tower, wherein a CO catalytic combustor is arranged in the reaction tower, a combustion catalyst is arranged in the CO catalytic combustor, and a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that the flue gas combusted by the CO catalytic combustor exchanges heat with the flue gas before denitration treatment after passing through the heat exchanger;
the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium with palladium metal;
the heat exchanger is a GGH heat exchanger;
the reaction tower is an SCR denitration reaction tower;
the preparation method of the combustion catalyst is the same as that of example 2, except that the halloysite nanotubes are replaced by equivalent modified porous silica, and the preparation method of the modified porous silica comprises the following steps:
(1) Respectively weighing zirconium chloride and 2-amino terephthalic acid, dissolving in a dimethylformamide solvent, fully mixing, adding acetic acid, carrying out ultrasonic dispersion, transferring into a high-pressure reaction kettle with a polytetrafluoroethylene lining, heating to 120-140 ℃, carrying out heat preservation and reaction for 40-48 hours under autogenous pressure, cooling to room temperature after the reaction is finished, separating precipitate, washing with anhydrous methanol for a plurality of times, and carrying out vacuum drying to obtain a product A; wherein the mass ratio of the zirconium chloride to the 2-amino terephthalic acid to the acetic acid is 1:0.77:12;
(2) Weighing the product A, dispersing in deionized water, sequentially adding polyvinylpyrrolidone, yttrium chloride and sodium iodide, ultrasonically dispersing, transferring into a high-pressure reaction kettle with a polytetrafluoroethylene lining, heating to 160-180 ℃, carrying out heat preservation reaction for 1-2h, self-cooling to room temperature after the reaction is finished, separating precipitate, washing with anhydrous methanol for several times, and carrying out vacuum drying to obtain a product B; wherein the mass ratio of the product A to the polyvinylpyrrolidone, yttrium chloride and sodium iodide is 10:14:0.156:5.6;
(3) Weighing tetraethoxysilane, dissolving the tetraethoxysilane in absolute ethyl alcohol to prepare a solution with the mass concentration of 1.2%, adding 1% deionized water according to the volume fraction, adjusting the pH value to 4-5, adding the product B according to the feed liquid ratio of 1.5g/100mL, heating to 30-40 ℃ after ultrasonic dispersion, preserving heat and stirring for 5 hours, separating precipitate after the reaction is completed, washing with absolute ethyl alcohol, and vacuum drying to obtain a product C;
(4) And heating the product C to 450 ℃ at a speed of 5-10 ℃/min, preserving heat, calcining for 1.5h, and cooling to obtain the modified porous silica.
Example 4
The method comprises the steps of sequentially carrying out desulfurization, wet electric precipitation and denitration treatment on the sintering flue gas, then introducing the sintering flue gas into a reaction tower, wherein a CO catalytic combustor is arranged in the reaction tower, a combustion catalyst is arranged in the CO catalytic combustor, and a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that the flue gas combusted by the CO catalytic combustor exchanges heat with the flue gas before denitration treatment after passing through the heat exchanger;
the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium with palladium metal;
the heat exchanger is a GGH heat exchanger;
the reaction tower is an SCR denitration reaction tower;
the preparation method of the combustion catalyst is the same as in example 2, except that the halloysite nanotubes are replaced with an equal amount of porous silica, and the preparation method of the porous silica comprises the following steps:
weighing tetraethoxysilane, dissolving in absolute ethyl alcohol to prepare a solution with the mass concentration of 1.2%, adding 1% deionized water according to the volume fraction, adjusting the pH value to 4-5, heating to 30-40 ℃ after ultrasonic dispersion, carrying out heat preservation and stirring reaction for 5h, separating precipitate after the reaction is finished, washing with absolute ethyl alcohol, heating to 450 ℃ at the speed of 5-10 ℃/min after vacuum drying, carrying out heat preservation and calcination for 1.5h, and cooling to obtain the product.
Example 5
A combustion catalyst for CO, the catalyst being palladium metal.
Experimental example
The catalytic performance of the combustion catalysts described in examples 1 to 5 under natural light conditions was measured in a simulated fixed bed reactor, the inside diameter of the quartz tube reactor was 4cm, the outside diameter was 4.3cm, the catalyst was placed in the quartz tube reactor, the catalyst was provided with thermocouple temperature measurement, the catalyst loading was 5g (excluding the mass of porous carrier), and the mixture consisted of CO (V% =2.5%), O 2 (V％＝3％)、N 2 (V% = 94.5%) composition, CO conversion at different temperatures was measured as follows:
finally, it should be noted that the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the scope of the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions can be made to the technical solution of the present invention without departing from the spirit and scope of the technical solution of the present invention.
Claims (10)
1. A method for utilizing combustible CO in sintering flue gas through catalytic combustion is characterized in that the sintering flue gas is sequentially subjected to desulfurization, wet electric precipitation and denitration treatment and then enters a reaction tower, a CO catalytic combustor is arranged in the reaction tower, a combustion catalyst is arranged in the CO catalytic combustor, a heat exchanger is arranged between a flue gas leading-out end of the reaction tower and a flue gas leading-in end before denitration treatment, so that the flue gas combusted by the CO combustion catalyst exchanges heat with the flue gas before denitration treatment after passing through the heat exchanger;
the combustion catalyst is a catalyst obtained by compounding metal oxides of manganese and cerium and palladium metal.
2. The method for catalytic combustion utilization of combustible CO in sintering flue gas according to claim 1, wherein the preparation method of the combustion catalyst comprises the following steps:
respectively weighing cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate, respectively preparing into solutions, firstly mixing the cerium nitrate solution and the potassium hydroxide solution, stirring and heating to 30-40 ℃, then adding the potassium permanganate solution and the palladium nitrate solution, continuously preserving heat and stirring for 30-60min, collecting precipitate after the reaction is finished, washing with deionized water for several times, vacuum drying, heating the dried precipitate to 400-500 ℃ at a speed of 5-10 ℃/min, preserving heat and calcining for 1-2h, and cooling after calcining to obtain the combustion catalyst.
3. The method for catalytic combustion utilization of combustible CO in sintering flue gas according to claim 1, wherein the combustion catalyst is supported on a porous carrier, and the preparation method of the combustion catalyst comprises the following steps:
and (3) weighing the porous carrier, dispersing the porous carrier in deionized water, stirring and dispersing the porous carrier in protective atmosphere to obtain dispersion liquid, respectively weighing cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate, respectively preparing the dispersion liquid into solutions, firstly mixing and adding the cerium nitrate solution and the potassium hydroxide solution into the dispersion liquid, stirring and heating to 30-40 ℃, then adding the potassium permanganate solution and the palladium nitrate solution, continuing to perform heat preservation and stirring reaction for 30-60min, collecting precipitate after the reaction is finished, washing the precipitate with deionized water for several times, drying the precipitate in vacuum, heating the dried precipitate to 400-500 ℃ at a speed of 5-10 ℃/min, performing heat preservation and calcination for 1-2h, and cooling the calcined precipitate to obtain the combustion catalyst.
4. A method for the catalytic combustion utilization of combustible CO in sintering flue gas according to claim 2 or 3, wherein the concentration of the cerium nitrate solution is 0.3-0.5mol/L, the concentration of the sodium hydroxide solution is 4-8mol/L, the concentration of the potassium permanganate solution is 0.1-0.4mol/L, the concentration of the palladium nitrate solution is 0.2-0.3mol/L, and the molar ratio of cerium nitrate, potassium hydroxide, potassium permanganate and palladium nitrate is (3-5): (10-12): (0.4-0.5): 1.
5. a method for the catalytic combustion utilization of combustible CO in sintering flue gas according to claim 3, wherein the porous support is halloysite nanotubes or porous silica.
6. The method for catalytic combustion and utilization of combustible CO in sintering flue gas according to claim 5, wherein the porous carrier is modified porous silica, and the preparation method comprises the following steps:
(1) Respectively weighing zirconium chloride and 2-amino terephthalic acid, dissolving in a dimethylformamide solvent, fully mixing, adding acetic acid, carrying out ultrasonic dispersion, transferring into a high-pressure reaction kettle with a polytetrafluoroethylene lining, heating to 120-140 ℃, carrying out heat preservation and reaction for 40-48 hours under autogenous pressure, cooling to room temperature after the reaction is finished, separating precipitate, washing with anhydrous methanol for a plurality of times, and carrying out vacuum drying to obtain a product A;
(2) Weighing the product A, dispersing in deionized water, sequentially adding polyvinylpyrrolidone, yttrium chloride and sodium iodide, ultrasonically dispersing, transferring into a high-pressure reaction kettle with a polytetrafluoroethylene lining, heating to 160-180 ℃, carrying out heat preservation reaction for 1-2h, self-cooling to room temperature after the reaction is finished, separating precipitate, washing with anhydrous methanol for several times, and carrying out vacuum drying to obtain a product B;
(3) Weighing tetraethoxysilane, dissolving the tetraethoxysilane in absolute ethyl alcohol to prepare a solution with the mass concentration of 1-2%, adding 1% deionized water according to the volume fraction, adjusting the pH to be acidic, adding the product B according to the feed liquid ratio of 1-3g/100mL, heating to 30-40 ℃ after ultrasonic dispersion, carrying out heat preservation and stirring reaction for 4-8h, separating precipitate after the reaction is finished, washing with absolute methanol or ethanol, and carrying out vacuum drying to obtain a product C;
(4) Heating the product C to 400-500 ℃ at a speed of 5-10 ℃/min, preserving heat, calcining for 1-2h, and cooling to obtain the modified porous silica.
7. The method for the catalytic combustion utilization of combustible CO in sintering flue gas according to claim 6, wherein the mass ratio of the zirconium chloride to the 2-amino terephthalic acid to the acetic acid in the step (1) is 1: (0.75-0.8): (12-14).
8. The method for catalytic combustion and utilization of combustible CO in sintering flue gas according to claim 6, wherein the mass ratio of the product a to the polyvinylpyrrolidone, yttrium chloride and sodium iodide in step (2) is 10: (12-15): (0.15-0.2): (5.5-5.8).
9. The method for catalytic combustion utilization of combustible CO in sintering flue gas according to claim 1, wherein the heat exchanger is a GGH heat exchanger.
10. The method for catalytic combustion utilization of combustible CO in sintering flue gas according to claim 1, wherein the reaction tower is an SCR method denitration reaction tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310449918.3A CN116447886A (en) | 2023-04-24 | 2023-04-24 | Method for utilizing combustible CO in sintering flue gas through catalytic combustion |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310449918.3A CN116447886A (en) | 2023-04-24 | 2023-04-24 | Method for utilizing combustible CO in sintering flue gas through catalytic combustion |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116447886A true CN116447886A (en) | 2023-07-18 |
Family
ID=87128532
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310449918.3A Pending CN116447886A (en) | 2023-04-24 | 2023-04-24 | Method for utilizing combustible CO in sintering flue gas through catalytic combustion |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116447886A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103301836A (en) * | 2013-07-01 | 2013-09-18 | 厦门大学 | Cerium-based catalyst for producing chloromethane by catalyzing oxidization reaction of methane chloride and preparation method thereof |
| CN109482052A (en) * | 2018-12-06 | 2019-03-19 | 中国科学院过程工程研究所 | CO and NO in a kind of purifying sintering flue gasxDevice and method |
| CN110227446A (en) * | 2019-05-13 | 2019-09-13 | 吉林晟航科技发展有限公司 | A kind of cerium Mn catalyst and preparation method thereof |
| CN112902680A (en) * | 2021-01-29 | 2021-06-04 | 中冶华天南京工程技术有限公司 | Sintering flue gas SCR denitration energy-saving emission-reducing method and system |
| CN113198319A (en) * | 2021-05-06 | 2021-08-03 | 阳春新钢铁有限责任公司 | Method for utilizing CO in flue gas denitration of sintering flue gas |
| CN113198459A (en) * | 2021-03-29 | 2021-08-03 | 上海中船临港船舶装备有限公司 | Catalyst for low-temperature catalytic combustion and preparation method and application thereof |
| CN115957620A (en) * | 2022-12-28 | 2023-04-14 | 阳春新钢铁有限责任公司 | Reaction equipment for reducing CO emission in flue gas and energy-saving emission-reducing method |
-
2023
- 2023-04-24 CN CN202310449918.3A patent/CN116447886A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103301836A (en) * | 2013-07-01 | 2013-09-18 | 厦门大学 | Cerium-based catalyst for producing chloromethane by catalyzing oxidization reaction of methane chloride and preparation method thereof |
| CN109482052A (en) * | 2018-12-06 | 2019-03-19 | 中国科学院过程工程研究所 | CO and NO in a kind of purifying sintering flue gasxDevice and method |
| CN110227446A (en) * | 2019-05-13 | 2019-09-13 | 吉林晟航科技发展有限公司 | A kind of cerium Mn catalyst and preparation method thereof |
| CN112902680A (en) * | 2021-01-29 | 2021-06-04 | 中冶华天南京工程技术有限公司 | Sintering flue gas SCR denitration energy-saving emission-reducing method and system |
| CN113198459A (en) * | 2021-03-29 | 2021-08-03 | 上海中船临港船舶装备有限公司 | Catalyst for low-temperature catalytic combustion and preparation method and application thereof |
| CN113198319A (en) * | 2021-05-06 | 2021-08-03 | 阳春新钢铁有限责任公司 | Method for utilizing CO in flue gas denitration of sintering flue gas |
| CN115957620A (en) * | 2022-12-28 | 2023-04-14 | 阳春新钢铁有限责任公司 | Reaction equipment for reducing CO emission in flue gas and energy-saving emission-reducing method |
Non-Patent Citations (1)
| Title |
|---|
| 《大气污染控制工程》: "《大气污染控制工程》", 武汉理工大学出版社, pages: 260 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103263928B (en) | Low and medium temperature decomposition of N2O composite oxide catalyst and preparation method thereof | |
| CN105642299A (en) | Nickel-doped lanthanum ferrite/clay nano-structure composite and preparation method and application thereof | |
| CN102500358A (en) | Denitration catalyst with excellent alkali metal and alkaline-earth metal poisoning resistance | |
| CN110075831B (en) | Iridium supported catalyst for catalytic combustion of low-concentration methane and preparation method thereof | |
| CN113198459A (en) | Catalyst for low-temperature catalytic combustion and preparation method and application thereof | |
| CN113070062B (en) | Cerium-based nano-sphere catalyst for catalyzing formic acid to produce hydrogen and preparation method thereof | |
| CN109821531B (en) | Cerium oxide carrier-based flat plate type high-temperature sulfur-resistant SCR denitration catalyst and preparation method thereof | |
| CN110327929A (en) | A kind of cobalt aluminum hydrotalcite Derived Mixed Oxides and the preparation method and application thereof | |
| WO2023231175A1 (en) | Device system and method having sintering flue gas co catalytic heat exchange and medium-and-low-temperature scr denitration connected in series | |
| CN102443454B (en) | Oxygen carrier of chemical-looping combustion and preparation method and application thereof | |
| CN113578333B (en) | Low-temperature denitration catalyst and preparation method and application thereof | |
| CN112774680A (en) | Preparation method of zinc ferrite-graphene composite aerogel | |
| CN111437814A (en) | Tin-doped platinum-titanium catalyst and preparation method and application thereof | |
| CN113262780A (en) | High-activity and high-stability manganese-based carbon smoke catalyst and preparation method and application thereof | |
| CN116447886A (en) | Method for utilizing combustible CO in sintering flue gas through catalytic combustion | |
| CN117181232A (en) | CuZnCeO x Preparation of nano rod catalyst and CO under photo-thermal synergistic catalysis 2 Application in reduction | |
| CN115634684B (en) | High specific surface area biomass charcoal low-temperature SCR catalyst, preparation method and application | |
| CN111282578A (en) | Metal-doped manganese-based low-temperature denitration catalyst and preparation method thereof | |
| CN116510746A (en) | Ruthenium catalyst for catalytic combustion of propane and preparation method thereof | |
| CN110898843A (en) | Mixed rare earth catalytic natural gas combustion catalyst and preparation method thereof | |
| CN115318286A (en) | Platinum catalyst for propane catalytic combustion and preparation method and application thereof | |
| CN110721697A (en) | Sr2FeTaO6Photocatalytic material and preparation method and application thereof | |
| CN114950466B (en) | Non-noble metal catalyst and preparation method and application thereof | |
| CN115591569B (en) | Cobalt-nitrogen-carbon non-noble metal catalyst for removing formaldehyde at room temperature and preparation method thereof | |
| CN116020487B (en) | Noble metal doped perovskite type oxide catalyst and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |