CN114225936A - Waste incineration flue gas denitration catalyst and preparation method thereof - Google Patents
Waste incineration flue gas denitration catalyst and preparation method thereof Download PDFInfo
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- 239000003054 catalyst Substances 0.000 title claims abstract description 53
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 239000003546 flue gas Substances 0.000 title claims abstract description 30
- 238000004056 waste incineration Methods 0.000 title claims abstract description 24
- 238000002360 preparation method Methods 0.000 title claims abstract description 23
- 238000001354 calcination Methods 0.000 claims abstract description 26
- 229910003145 α-Fe2O3 Inorganic materials 0.000 claims abstract description 24
- 229910006297 γ-Fe2O3 Inorganic materials 0.000 claims abstract description 23
- 238000000498 ball milling Methods 0.000 claims abstract description 19
- 229910000859 α-Fe Inorganic materials 0.000 claims abstract description 15
- 238000007873 sieving Methods 0.000 claims abstract description 11
- 238000000605 extraction Methods 0.000 claims abstract description 6
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 239000006148 magnetic separator Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 2
- 238000007885 magnetic separation Methods 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000463 material Substances 0.000 description 27
- 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 13
- 239000004480 active ingredient Substances 0.000 description 7
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- 239000008367 deionised water Substances 0.000 description 6
- 229910021641 deionized water Inorganic materials 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- 238000005303 weighing Methods 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 239000013078 crystal Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000000443 aerosol Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 229910001566 austenite Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000005389 magnetism Effects 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000011272 standard treatment Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000002087 whitening effect Effects 0.000 description 1
Classifications
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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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/745—Iron
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0027—Powdering
- B01J37/0036—Grinding
-
- 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
-
- 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
- B01J37/16—Reducing
- B01J37/18—Reducing with gases containing free hydrogen
-
- 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
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
-
- 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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses a waste incineration flue gas denitration catalyst and a preparation method thereof, wherein the catalyst comprises alpha-Fe2O3And gamma-Fe2O3Wherein, α -Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.3-1: 9-9.7. The preparation method comprises the following steps: extraction of alpha-Fe from red mud2O3(ii) a Extracting alpha-Fe2O3Ball milling, sieving, calcining in reducing atmosphereAnd the calcination temperature is 500-600 ℃ for the set time, thus obtaining the catalyst.
Description
Technical Field
The invention belongs to the technical field of denitration catalysts, and particularly relates to a waste incineration flue gas denitration catalyst and a preparation method thereof.
Background
The statements herein merely provide background information related to the present disclosure and may not necessarily constitute prior art.
The waste incineration flue gas mainly comprises HCl and SOx、NOxHeavy metal, dioxin, particulate matter and the like, the existing waste incineration flue gas treatment process generally comprises the following steps: selective non-catalytic reduction denitration, high-temperature dust removal, selective catalytic reduction denitration, low-temperature deacidification and whitening and the like. Dioxin generally exists in a granular form, an aerosol form or a gaseous form, and can be partially removed in a dedusting process (such as a high-efficiency bag type dust collector), but in a selective catalytic reduction denitration process, if the process temperature is higher, such as higher than 300 ℃ (the forming temperature of the dioxin is about 300-.
The red mud is industrial solid waste generated by the alumina industry, the cumulative stacking quantity of the red mud all over the world currently exceeds 40 hundred million tons, the comprehensive utilization rate of the red mud in the world does not exceed 10 percent, and the resource waste also poses potential serious threats to the ecological environment.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a waste incineration flue gas denitration catalyst and a preparation method thereof.
In order to achieve the purpose, the invention is realized by the following technical scheme:
in a first aspect, the invention provides a waste incineration flue gas denitration catalyst, which comprises alpha-Fe2O3And gamma-Fe2O3Wherein, α -Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.3-1: 9-9.7.
In a second aspect, the invention provides a preparation method of a waste incineration flue gas denitration catalyst, which comprises the following steps:
extraction of alpha-Fe from red mud2O3；
Extracting alpha-Fe2O3After ball milling and sieving, calcining in a reducing atmosphere at the calcining temperature of 500-600 ℃ for a set time to obtain the catalyst.
The beneficial effects achieved by one or more of the embodiments of the invention described above are as follows:
fe in red mud2O3Mostly in alpha-Fe2O3Crystal form exists, alpha-Fe2O3Under reducing atmosphere, has oriented gamma-Fe at the temperature of above 400 DEG C2O3The characteristics of crystal form conversion are proved by the inventor through experiments, and alpha-Fe is controlled2O3The alpha-Fe with a certain proportion can be prepared and obtained at the calcining temperature and the calcining time in the reducing atmosphere2O3And gamma-Fe2O3The mixed catalyst can realize catalytic denitration on waste incineration flue gas at low temperature, so that secondary synthesis of dioxin is avoided; meanwhile, the inventor also finds that the catalyst has a good removing effect on dioxin in the flue gas during low-temperature catalytic denitration, can remove gaseous dioxin in the flue gas, and is more favorable for realizing standard treatment and emission of waste incineration flue gas.
The catalyst raw material in the invention is the red mud, thereby realizing the resource utilization of the red mud.
Because the waste incineration flue gas has certain reducibility, the alpha-Fe can be ensured2O3/γ-Fe2O3The composite catalyst has longer service life.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
In a first aspect, the invention provides a waste incineration flue gas denitration catalyst prepared by the preparation method, which comprises alpha-Fe2O3And gamma-Fe2O3Wherein, α -Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.3-1: 9-9.7.
In some embodiments, the denitration catalyst comprises alpha-Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.3-0.7: 9.3-9.7.
Further, in the denitration catalyst, alpha-Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.5: 9.5.
Within the mass ratio range, when the temperature of the incineration waste flue gas to be treated is within the temperature range of less than 300 ℃, the catalyst is used for catalytic denitration, so that better denitration efficiency and dioxin removal efficiency can be obtained, and meanwhile, because the denitration temperature is lower, the dioxin can be prevented from being synthesized again, so that the dioxin is discharged after reaching the standard; on the other hand, the general denitration temperature is higher, and the temperature of flue gas after high temperature dust removal is lower, needs to carry out catalytic denitration after the secondary heating, if catalytic denitration temperature is lower, then can save the secondary heating, or reduce because of the energy consumption that the heating needs, and then accord with the environmental protection requirement more.
In a second aspect, the invention provides a preparation method of a waste incineration flue gas denitration catalyst, which comprises the following steps:
extraction of alpha-Fe from red mud2O3；
Extracting alpha-Fe2O3Ball-milling, sieving, calcining in reducing atmosphereAnd (3) calcining at the calcining temperature of 500-600 ℃ for a set time to obtain the catalyst.
In some embodiments, alpha-Fe is extracted from red mud2O3The method of (1) is a strong magnetic separation method.
Further, extracting alpha-Fe from red mud2O3The method comprises the following steps: adding water into the red mud, and uniformly mixing;
and (3) magnetically separating iron oxide from the red mud by using a strong magnetic separator, and cleaning the iron oxide.
Due to Fe in red mud2O3Mostly in alpha-Fe2O3In the form of alpha-Fe2O3Has weak magnetism, and can be separated by a strong magnetic separator.
Furthermore, the mass ratio of the red mud to the water is 2-4:6-8, preferably 3: 7. The solid-liquid ratio is more favorable for improving the extraction efficiency of the ferric oxide.
Further, the iron oxide is washed to a pH of 7.0 to 7.5. So as to remove impurities attached to the surface of the iron oxide.
In some embodiments, α -Fe2O3After ball milling, the mixture is sieved by a 200-mesh sieve.
The alpha-Fe can be improved during calcination by ball milling and sieving2O3To thereby increase the degree of uniformity of heating of the alpha-Fe2O3To gamma-Fe2O3So that alpha-Fe is calcined at a specific temperature for a specific time2O3And gamma-Fe2O3The mass ratio of the catalyst is controllable, so that low-temperature catalytic denitration and dioxin removal are realized.
Further, the ball milling is wet ball milling.
Furthermore, the drying temperature after the wet ball milling is 100-160 ℃; preferably, the drying temperature is 105-.
In some embodiments, the calcination time is 2-4 h.
Furthermore, the calcination temperature is 550-.
In some embodiments, the calcination atmosphere is a mixture of hydrogen and nitrogen, wherein the volume percentage of hydrogen is 2% to 5%, preferably 2% to 4%, and more preferably 3%.
The inventor finds that the volume fraction of the hydrogen influences the alpha-Fe in the catalyst through experiments2O3And gamma-Fe2O3Is a relatively important factor.
The present invention will be further described with reference to the following specific examples.
Example 1
5％α-Fe2O3/95％γ-Fe2O3Preparation of the denitration catalyst active ingredient combination:
1) weighing 10g of the extracted ferric oxide, and washing with deionized water until the pH value is 7.0;
2) performing wet ball milling on the material obtained in the step 1), and sieving the material by a 200-mesh sieve;
3) placing the material obtained in the step 2) in an oven to be dried at 110 ℃ until the quality does not change any more;
4) and 3) placing the material obtained in the step 3) in a tubular furnace, and calcining for 3 hours at 580 ℃ to obtain the denitration catalyst active component combination. The atmosphere conditions were: h in the mixed gas23 vol%, N2The volume of the mixed gas outlet is 97 vol%, the pressure of the secondary reducing valve of the mixed gas outlet is set to be 2bar, and the gas flow rate is 20 mL/min.
Example 2
10％α-Fe2O3/90％γ-Fe2O3Preparation of the denitration catalyst active ingredient combination:
1) weighing 10g of the extracted ferric oxide, and washing with deionized water until the pH value is 7.0;
2) performing wet ball milling on the material obtained in the step 1), and sieving the material by a 200-mesh sieve;
3) placing the material obtained in the step 2) in an oven to be dried at 110 ℃ until the quality does not change any more;
4) and 3) placing the material obtained in the step 3) in a tubular furnace, and calcining the material at 580 ℃ for 2.8 hours to obtain the denitration catalyst active component combination. The atmosphere conditions were: h in the mixed gas22 vol%, N298 vol%, mixed gas outlet two-stage pressure reducing valve pressure deviceSet at 2bar, gas flow rate 20 mL/min.
Example 3
3％α-Fe2O3/97％γ-Fe2O3Preparation of the denitration catalyst active ingredient combination:
1) weighing 10g of the extracted ferric oxide, and washing with deionized water until the pH value is 7.0;
2) performing wet ball milling on the material obtained in the step 1), and sieving the material by a 200-mesh sieve;
3) placing the material obtained in the step 2) in an oven to be dried at 110 ℃ until the quality does not change any more;
4) and 3) placing the material obtained in the step 3) in a tubular furnace, and calcining the material at 580 ℃ for 3.5 hours to obtain the denitration catalyst active component combination. The atmosphere conditions were: h in the mixed gas24 vol%, N2Accounting for 96 vol%, the pressure of the mixed gas outlet secondary pressure reducing valve is set to be 2bar, and the gas flow rate is 20 mL/min.
Comparative example 1
20％α-Fe2O3/80％γ-Fe2O3Preparation of the denitration catalyst active ingredient combination:
1) weighing 10g of the extracted ferric oxide, and washing with deionized water until the pH value is 7.0;
2) performing wet ball milling on the material obtained in the step 1), and sieving the material by a 200-mesh sieve;
3) placing the material obtained in the step 2) in an oven to be dried at 110 ℃ until the quality does not change any more;
4) and 3) placing the material obtained in the step 3) in a tubular furnace, and calcining the material at 580 ℃ for 2.5 hours to obtain the denitration catalyst active component combination. The calcination conditions were: h in the mixed gas21 vol%, N2Accounting for 99 vol%, the pressure of the mixed gas outlet secondary pressure reducing valve is set to be 2bar, and the gas flow rate is 20 mL/min.
Comparative example 2
40％α-Fe2O3/60％γ-Fe2O3Preparation of the denitration catalyst active ingredient combination:
1) weighing 10g of the extracted ferric oxide, and washing with deionized water until the pH value is 7.0;
2) performing wet ball milling on the material obtained in the step 1), and sieving the material by a 200-mesh sieve;
3) placing the material obtained in the step 2) in an oven to be dried at 110 ℃ until the quality does not change any more;
4) and 3) placing the material obtained in the step 3) in a tubular furnace, and calcining for 2 hours at 580 ℃ to obtain the denitration catalyst active component combination. The calcination conditions were: h in the mixed gas20.1 vol%, N299.9 vol%, the mixed gas outlet secondary pressure reducing valve pressure was set to 2bar, and the gas flow rate was 20 mL/min.
Comparative example 3
99％α-Fe2O3/1％γ-Fe2O3Preparation of the denitration catalyst active ingredient combination:
1) weighing 10g of red mud to extract ferric oxide, and washing with deionized water until the pH value is 7.0;
2) performing wet ball milling on the material obtained in the step 1), and sieving the material by a 200-mesh sieve;
3) and (3) drying the material obtained in the step 2) in an oven at 110 ℃ until the mass of the material is not changed any more, and preparing the denitration catalyst active component combination comparison sample.
And (3) performance testing:
the denitration and dioxin removal performance tests of the denitration catalysts obtained in examples 1 to 3 and comparative examples 1 to 3 were carried out, 4.0g of the prepared catalyst active ingredient combination was placed in a continuous flow fixed bed reactor (made of a quartz tube with a diameter of 9 mm), and the test conditions were simulated for the main components of waste incineration flue gas, wherein NO and SO2、O2The volume percentage of CO is respectively 0.2 percent, 0.01 percent, 4.0 percent and 0.01 percent, and N2As a balance gas, dioxin 3ngTEQ/m3The flow rate of the flue gas is 2000mL/min, and the space velocity is 30000h-1。
The test temperature range was 200 ℃ and 425 ℃.
TABLE 1 denitration efficiency of denitration catalysts obtained in examples 1 to 3 and comparative examples 1 to 3
Table 2 dioxin removal efficiency of denitration catalysts obtained in examples 1 to 3 and comparative examples 1 to 3
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The utility model provides a msw incineration flue gas denitration catalyst which characterized in that: it is alpha-Fe2O3And gamma-Fe2O3The mixed catalyst of (1).
2. The waste incineration flue gas denitration catalyst according to claim 1, characterized in that: among the denitration catalysts, alpha-Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.3-1: 9-9.7;
preferably, alpha-Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.3-0.7: 9.3-9.7;
further, in the denitration catalyst, alpha-Fe2O3With gamma-Fe2O3The mass ratio of (A) to (B) is 0.5: 9.5.
3. A preparation method of a waste incineration flue gas denitration catalyst is characterized by comprising the following steps: the method comprises the following steps:
extraction of alpha-Fe from red mud2O3；
Extracting alpha-Fe2O3After ball milling and sieving, calcining in a reducing atmosphere at the calcining temperature of 500-600 ℃ for a set time to obtain the catalyst.
4. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 3, characterized in thatIn the following steps: extraction of alpha-Fe from red mud2O3The method of (1) is a strong magnetic separation method;
further, extracting alpha-Fe from red mud2O3The method comprises the following steps: adding water into the red mud, and uniformly mixing;
magnetically separating iron oxide from the red mud by using a strong magnetic separator, and cleaning the iron oxide;
furthermore, the mass ratio of the red mud to the water is 2-4:6-8, preferably 3: 7;
further, the iron oxide is washed to a pH of 7.0 to 7.5.
5. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 4, characterized by comprising the steps of: alpha-Fe is mixed2O3After ball milling, the mixture is sieved by a 200-mesh sieve.
6. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 4, characterized by comprising the steps of: the ball milling is wet ball milling;
furthermore, the drying temperature after the wet ball milling is 100-160 ℃; preferably, the drying temperature is 105-.
7. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 4, characterized by comprising the steps of: the calcination time is 2-4 h.
8. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 4, characterized by comprising the steps of: the calcination temperature is 550-600 ℃, and the calcination time is 2.5-3.5 h.
9. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 4, characterized by comprising the steps of: the calcining atmosphere is a mixed gas of hydrogen and nitrogen, wherein the volume percentage of the hydrogen is 2-5%.
10. The preparation method of the denitration catalyst for waste incineration flue gas according to claim 9, characterized by comprising the steps of: preferably 2% to 4%, and more preferably 3%.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000297911A (en) * | 1999-04-14 | 2000-10-24 | Toda Kogyo Corp | Method for incinerating refuse |
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