CN111822048A - Preparation method of catalyst for synchronously purifying NO and volatile organic pollutants in flue gas - Google Patents
Preparation method of catalyst for synchronously purifying NO and volatile organic pollutants in flue gas Download PDFInfo
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- CN111822048A CN111822048A CN202010659018.8A CN202010659018A CN111822048A CN 111822048 A CN111822048 A CN 111822048A CN 202010659018 A CN202010659018 A CN 202010659018A CN 111822048 A CN111822048 A CN 111822048A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 32
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 239000003546 flue gas Substances 0.000 title claims abstract description 24
- 239000002957 persistent organic pollutant Substances 0.000 title claims abstract description 20
- 238000002360 preparation method Methods 0.000 title claims abstract description 8
- 238000001027 hydrothermal synthesis Methods 0.000 claims abstract description 20
- 239000000243 solution Substances 0.000 claims abstract description 16
- 239000011964 heteropoly acid Substances 0.000 claims abstract description 15
- 239000000047 product Substances 0.000 claims abstract description 15
- 239000007787 solid Substances 0.000 claims abstract description 15
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 13
- 239000011259 mixed solution Substances 0.000 claims abstract description 13
- 238000003756 stirring Methods 0.000 claims abstract description 13
- 238000001035 drying Methods 0.000 claims abstract description 11
- 238000000034 method Methods 0.000 claims abstract description 8
- 238000001914 filtration Methods 0.000 claims abstract description 7
- 238000012216 screening Methods 0.000 claims abstract description 7
- 238000005406 washing Methods 0.000 claims abstract description 7
- 150000000703 Cerium Chemical class 0.000 claims abstract description 5
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 5
- 239000000203 mixture Substances 0.000 claims abstract description 3
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 9
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 8
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims 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 6
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 5
- CGFYHILWFSGVJS-UHFFFAOYSA-N silicic acid;trioxotungsten Chemical compound O[Si](O)(O)O.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 CGFYHILWFSGVJS-UHFFFAOYSA-N 0.000 claims description 5
- LZZYPRNAOMGNLH-UHFFFAOYSA-M Cetrimonium bromide Chemical compound [Br-].CCCCCCCCCCCCCCCC[N+](C)(C)C LZZYPRNAOMGNLH-UHFFFAOYSA-M 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
- OZECDDHOAMNMQI-UHFFFAOYSA-H cerium(3+);trisulfate Chemical compound [Ce+3].[Ce+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O OZECDDHOAMNMQI-UHFFFAOYSA-H 0.000 claims description 3
- IYDGMDWEHDFVQI-UHFFFAOYSA-N phosphoric acid;trioxotungsten Chemical compound O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.OP(O)(O)=O IYDGMDWEHDFVQI-UHFFFAOYSA-N 0.000 claims description 3
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 claims description 2
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 2
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 2
- HKVFISRIUUGTIB-UHFFFAOYSA-O azanium;cerium;nitrate Chemical compound [NH4+].[Ce].[O-][N+]([O-])=O HKVFISRIUUGTIB-UHFFFAOYSA-O 0.000 claims description 2
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 claims description 2
- VYLVYHXQOHJDJL-UHFFFAOYSA-K cerium trichloride Chemical compound Cl[Ce](Cl)Cl VYLVYHXQOHJDJL-UHFFFAOYSA-K 0.000 claims description 2
- GHLITDDQOMIBFS-UHFFFAOYSA-H cerium(3+);tricarbonate Chemical compound [Ce+3].[Ce+3].[O-]C([O-])=O.[O-]C([O-])=O.[O-]C([O-])=O GHLITDDQOMIBFS-UHFFFAOYSA-H 0.000 claims description 2
- 239000012153 distilled water Substances 0.000 claims description 2
- 239000008103 glucose Substances 0.000 claims description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 2
- DHRLEVQXOMLTIM-UHFFFAOYSA-N phosphoric acid;trioxomolybdenum Chemical compound O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.OP(O)(O)=O DHRLEVQXOMLTIM-UHFFFAOYSA-N 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 238000004056 waste incineration Methods 0.000 abstract description 13
- 238000000746 purification Methods 0.000 abstract description 7
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 11
- 239000002912 waste gas Substances 0.000 description 4
- 239000000356 contaminant Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
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- 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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/14—Phosphorus; Compounds thereof
- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8678—Removing components of undefined structure
- B01D53/8687—Organic components
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- 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
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/24—Chromium, molybdenum or tungsten
- B01J23/30—Tungsten
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- 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
- B01J37/10—Heat treatment in the presence of water, e.g. steam
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
- B01D2258/0291—Flue gases from waste incineration plants
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Abstract
The invention discloses a preparation method of a catalyst for synchronously purifying NO and volatile organic pollutants in flue gas, and relates to the technical field of waste incineration flue gas treatment, wherein 5-10 mmol of cerium salt and 0.1-0.5 mmol of heteropoly acid are dissolved in 50-100 mL of solution, and the mixture is stirred for 1 hour; adding 0.5-2 g of structure directing agent into the mixed solution, and stirring for 0.5 hour; transferring the solution into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 80-180 ℃, and the hydrothermal time is 6-48 hours; washing and filtering a hydrothermal reaction product, putting the product into a 105 ℃ drying oven, and drying for 12 hours; roasting the dried solid in a muffle furnace; and screening the roasted product. The method is suitable for synchronously removing NO and volatile organic pollutants at low temperature, realizes high-efficiency purification of the flue gas of the waste incineration plant, has low investment and operation cost, and is easy for industrial application.
Description
Technical Field
The invention relates to the technical field of waste incineration flue gas treatment, in particular to a preparation method of a catalyst for synchronously purifying NO and volatile organic pollutants in flue gas.
Background
The NOx and chlorine-containing volatile organic pollutants (CVOCs) in the flue gas of a waste incineration plant seriously pollute the environment. The traditional NH3-SCR technology is mainly applied to the flue gas purification of coal-fired power plants and is suitable for large-scale incinerators with the temperature of 300 ℃ and 450 DEG CThe flue gas temperature is generally less than 300 ℃, and the traditional catalyst is difficult to play a role in the flue gas environment of a complex incinerator. Thus developing NO suitable for use under low temperature conditionsXThe novel catalyst which is removed synchronously with CVOCs is the key for realizing the high-efficiency purification of the flue gas of the waste incineration plant.
With NOXChlorobenzene (volatile organic pollutant) associated with dioxin is used as a target product, heteropoly acid is introduced, acid sites and oxidation active sites on the surface of the cerium dioxide catalyst are constructed, and NO is removed at low temperatureXAnd volatile organic contaminants. The catalytic activity of the catalyst is optimized by optimizing the microstructure of the catalyst. Provides a theoretical basis for the flue gas purification technology of the waste incineration plant.
Disclosure of Invention
The invention aims to provide a preparation method of a reasonably designed catalyst for synchronously purifying NO and volatile organic pollutants in flue gas, aiming at the defects and defects of the prior art, the preparation method is suitable for synchronously removing NO and volatile organic pollutants at low temperature, realizes high-efficiency purification of flue gas of a waste incineration plant, and is low in investment and operation cost and easy for industrial application.
In order to achieve the purpose, the invention adopts the following technical scheme: the operation steps are as follows:
1. dissolving 5-10 mmol of cerium salt and 0.1-0.5 mmol of heteropoly acid in 50-100 mL of solution, and stirring for 1 hour to obtain a mixed solution;
2. adding 0.5-2 g of structure directing agent into the mixed solution, and stirring for 0.5 hour;
3. transferring the solution obtained in the step (2) into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 80-180 ℃, and the hydrothermal time is 6-48 hours, so as to obtain a hydrothermal reaction product;
4. washing and filtering the hydrothermal reaction product, putting the product into a 105 ℃ oven, and drying for 12 hours;
5. roasting the dried solid in a muffle furnace, namely heating the dried solid to 350 ℃ from room temperature at a speed of 1-2 ℃/min, keeping the temperature for 1-3 hours, then continuously heating to 550 ℃ at a speed of 1-2 ℃/min, and keeping the temperature for 1-4 hours;
6. and screening the roasted product by 40-60 meshes to obtain the catalyst.
Further, the solution in step 1 is one of methanol, ethanol, ethylene glycol and distilled water.
Further, the cerium salt in step 1 is one of cerium acetate, cerium sulfate, cerium chloride, cerium nitrate, cerium carbonate and ammonium cerium nitrate.
Further, the heteropoly acid in the step 1 is one of silicotungstic acid, phosphomolybdic acid and phosphotungstic acid.
Further, the structure directing agent in step 2 is one of P123, PVP, F127, CTAB, and a mixture of glucose and acrylic acid.
Further, the reaction conditions of the catalyst are that the concentration of NO is 300ppm, the concentration of NH3 is 300ppm, the concentration of chlorobenzene is 300ppm, and the concentration ratio of NO to NH3 is 1.0; and the catalytic reduction reaction temperature of the catalyst is 150-350 ℃.
After adopting the structure, the invention has the beneficial effects that: the invention provides a preparation method of a catalyst for synchronously purifying NO and volatile organic pollutants in flue gas, which is suitable for synchronously removing NO and volatile organic pollutants at low temperature, realizes high-efficiency purification of flue gas of a waste incineration plant, has low investment and operation cost and is easy for industrial application.
Description of the drawings:
fig. 1 is a graph of removal efficiency of the first embodiment.
Fig. 2 is a graph of removal efficiency for example two.
Fig. 3 is a graph of removal efficiency for the third example.
FIG. 4 is a graph showing the removal efficiency in the fourth embodiment.
The specific implementation mode is as follows:
the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The first embodiment is as follows:
the operation steps of this embodiment are as follows:
1. dissolving 5mmol of cerous nitrate and 0.1mmol of silicotungstic acid in 50mL of methanol solution, and stirring for 1 hour to obtain a mixed solution;
2. adding 0.5g of P123 into the mixed solution, and stirring for 0.5 hour;
3. transferring the solution obtained in the step (2) into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 140 ℃, and the hydrothermal time is 10 hours, so as to obtain a hydrothermal reaction product;
4. washing and filtering the hydrothermal reaction product, putting the product into a 105 ℃ oven, and drying for 12 hours;
5. roasting the dried solid in a muffle furnace, namely heating the dried solid to 350 ℃ from room temperature at a speed of 2 ℃/min, keeping the temperature for 2 hours, then continuously heating the dried solid to 550 ℃ at a speed of 2 ℃/min, and keeping the temperature for 4 hours;
6. screening the roasted product to 40-60 meshes to obtain heteropoly acid modified CeO2A catalyst.
Modifying the obtained heteropoly acid into CeO2Catalyst for low temperature NH3-chlorobenzene is purified synchronously in an SCR reaction, the waste gas atmosphere of a waste incineration plant of the reaction being: the concentration of NO is 300ppm, the concentration of NH3 is 300ppm, the concentration of chlorobenzene is 300ppm, the concentration ratio of NO to NH3 is 1.0, and the heteropoly acid modified CeO2The catalytic reduction reaction temperature of the catalyst is 150-350 ℃; referring to fig. 1, the removal rate of NO can reach 75%, and the removal rate of volatile organic pollutants can reach 100%.
After adopting above-mentioned structure, this embodiment's beneficial effect is as follows:
1. the method is simple, has low cost and accords with actual production;
2. acid sites and oxidation active sites on the surface of the cerium dioxide catalyst are constructed to realize low-temperature NO removalXAnd volatile organic contaminants;
3. the method can be directly used for purifying the flue gas of a waste incineration plant, so that pollutants reach the purification standard and secondary pollution of the pollutants is prevented.
Example two:
the operation steps of this embodiment are as follows:
1. dissolving 5mmol of cerium sulfate and 0.1mmol of phosphotungstic acid in 50mL of ethanol solution, and stirring for 1 hour to obtain a mixed solution;
2. adding 0.5g of CTAB into the mixed solution, and stirring for 0.5 hour;
3. transferring the solution obtained in the step 2 into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 180 ℃, and the hydrothermal time is 12 hours, so as to obtain a hydrothermal reaction product;
4. washing the hydrothermal reaction product, filtering, putting the product in a drying oven at 105 ℃, and drying for 12 hours;
5. roasting the dried solid in a muffle furnace, namely heating the dried solid to 350 ℃ from room temperature at 1 ℃/min, keeping the temperature for 1 hour, then continuously heating to 550 ℃ at 1 ℃/min, and keeping the temperature for 4 hours;
6. screening the roasted product to 40-60 meshes to obtain heteropoly acid modified CeO2A catalyst.
Modifying the obtained heteropoly acid into CeO2Catalyst for low temperature NH3-chlorobenzene is purified synchronously in an SCR reaction, the waste gas atmosphere of a waste incineration plant of the reaction being: NO concentration 300ppm, NH3Concentration 300ppm, chlorobenzene concentration 300ppm, NO and NH3The concentration ratio was 1.0. And the reaction temperature of catalytic reduction is 150-350 ℃; referring to fig. 2, the removal rate of NO can reach 80%, and the removal rate of volatile organic pollutants can reach 100%.
Example three:
the operation steps of this embodiment are as follows:
1. dissolving 6mmol of cerous nitrate and 0.1mmol of silicotungstic acid in 55mL of aqueous solution, and stirring for 1 hour to obtain a mixed solution;
2. adding 0.5g of PVP into the mixed solution, and stirring for 0.5 hour;
3. transferring the solution obtained in the step (2) into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 160 ℃, and the hydrothermal time is 10 hours, so as to obtain a hydrothermal reaction product;
4. washing the hydrothermal reaction product, filtering, putting the product in a drying oven at 105 ℃, and drying for 12 hours;
5. roasting the dried solid in a muffle furnace, namely heating the dried solid to 350 ℃ from room temperature at a speed of 2 ℃/min, keeping the temperature for 2 hours, then continuously heating the dried solid to 550 ℃ at a speed of 2 ℃/min, and keeping the temperature for 4 hours;
6. screening the roasted product to 40-60 meshes to obtain heteropoly acid modified CeO2A catalyst.
Modifying the obtained heteropoly acid into CeO2Catalyst for low temperature NH3-chlorobenzene is purified synchronously in an SCR reaction, the waste gas atmosphere of a waste incineration plant of the reaction being: NO concentration 300ppm, NH3Concentration 300ppm, chlorobenzene concentration 300ppm, NO and NH3The concentration ratio was 1.0. And the reaction temperature of catalytic reduction is 150-350 ℃; referring to fig. 3, the removal rate of NO can reach 85%, and the removal rate of volatile organic pollutants can reach 100%.
Example four:
the operation steps of this embodiment are as follows:
1. dissolving 5mmol of cerium acetate and 0.1mmol of silicotungstic acid in 60mL of glycol solution, and stirring for 1 hour to obtain a mixed solution;
2. adding 0.5g of F127 into the mixed solution, and stirring for 0.5 hour;
3. transferring the solution obtained in the step (2) into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 120 ℃, and the hydrothermal time is 12 hours, so as to obtain a hydrothermal reaction product;
4. washing the hydrothermal reaction product, filtering, putting the product in a drying oven at 105 ℃, and drying for 12 hours;
5. roasting the dried solid in a muffle furnace, namely heating the dried solid to 350 ℃ from room temperature at 1 ℃/min, keeping the temperature for 1 hour, then continuously heating to 550 ℃ at 1 ℃/min, and keeping the temperature for 4 hours;
6. screening the roasted product to 40-60 meshes to obtain heteropoly acid modified CeO2A catalyst.
Modifying the obtained heteropoly acid into CeO2Catalyst for low temperature NH3-chlorobenzene is purified synchronously in an SCR reaction, the waste gas atmosphere of a waste incineration plant of the reaction being: NO concentration 300ppm, NH3The concentration was 300ppm and the chlorobenzene concentration was 300 ppm. NO and NH3The concentration ratio was 1.0. And reaction of catalytic reductionThe temperature is 150-350 ℃; referring to FIG. 4, the removal rate of NO was 85% and the removal rate of volatile organic contaminants (CB: chlorobenzene) was 100%.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that various changes in the embodiments and/or modifications of the invention can be made, and equivalents and modifications of some features of the invention can be made without departing from the spirit and scope of the invention.
Claims (6)
1. The preparation method of the catalyst for synchronously purifying NO and volatile organic pollutants in the flue gas is characterized by comprising the following steps of: the operation steps are as follows:
(1) dissolving 5-10 mmol of cerium salt and 0.1-0.5 mmol of heteropoly acid in 50-100 mL of solution, and stirring for 1 hour to obtain a mixed solution;
(2) adding 0.5-2 g of structure directing agent into the mixed solution, and stirring for 0.5 hour;
(3) transferring the solution obtained in the step (2) into a hydrothermal reaction kettle, wherein the hydrothermal temperature is 80-180 ℃, and the hydrothermal time is 6-48 hours, so as to obtain a hydrothermal reaction product;
(4) washing and filtering the hydrothermal reaction product, putting the product into a 105 ℃ oven, and drying for 12 hours;
(5) roasting the dried solid in a muffle furnace, namely heating the dried solid to 350 ℃ from room temperature at a speed of 1-2 ℃/min, keeping the temperature for 1-3 hours, then continuously heating to 550 ℃ at a speed of 1-2 ℃/min, and keeping the temperature for 1-4 hours;
(6) and screening the roasted product by 40-60 meshes.
2. The method for preparing the catalyst for synchronously purifying NO and volatile organic pollutants in the flue gas according to claim 1, is characterized in that: the solution in the step (1) is one of methanol, ethanol, glycol and distilled water.
3. The method for preparing the catalyst for synchronously purifying NO and volatile organic pollutants in the flue gas according to claim 1, is characterized in that: the cerium salt in the step (1) is one of cerium acetate, cerium sulfate, cerium chloride, cerium nitrate, cerium carbonate and ammonium cerium nitrate.
4. The method for preparing the catalyst for synchronously purifying NO and volatile organic pollutants in the flue gas according to claim 1, is characterized in that: the heteropoly acid in the step (1) is one of silicotungstic acid, phosphomolybdic acid and phosphotungstic acid.
5. The method for preparing the catalyst for synchronously purifying NO and volatile organic pollutants in the flue gas according to claim 1, is characterized in that: the structure directing agent in the step (2) is one of P123, PVP, F127, CTAB and a mixture of glucose and acrylic acid.
6. The method for preparing the catalyst for synchronously purifying NO and volatile organic pollutants in the flue gas according to claim 1, is characterized in that: the reaction conditions of the catalyst are that the concentration of NO is 300ppm, the concentration of NH3 is 300ppm, the concentration of chlorobenzene is 300ppm, and the concentration ratio of NO to NH3 is 1.0; and the catalytic reduction reaction temperature of the catalyst is 150-350 ℃.
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| CN116747865A (en) * | 2023-05-15 | 2023-09-15 | 天津大学 | Catalyst for CVOCs catalytic oxidation and preparation method thereof |
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