CN107442135A - A kind of renovation process of arsenic poisoning SCR denitration - Google Patents
A kind of renovation process of arsenic poisoning SCR denitration Download PDFInfo
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- CN107442135A CN107442135A CN201710741285.8A CN201710741285A CN107442135A CN 107442135 A CN107442135 A CN 107442135A CN 201710741285 A CN201710741285 A CN 201710741285A CN 107442135 A CN107442135 A CN 107442135A
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- catalyst
- scr denitration
- arsenic poisoning
- gas
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- 208000008316 Arsenic Poisoning Diseases 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000008569 process Effects 0.000 title claims abstract description 23
- 238000009418 renovation Methods 0.000 title claims abstract description 22
- 239000003054 catalyst Substances 0.000 claims abstract description 127
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 230000009467 reduction Effects 0.000 claims abstract description 18
- 239000008367 deionised water Substances 0.000 claims abstract description 16
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 16
- 238000002791 soaking Methods 0.000 claims abstract description 11
- 238000005406 washing Methods 0.000 claims abstract description 11
- 239000012670 alkaline solution Substances 0.000 claims abstract description 8
- 238000007664 blowing Methods 0.000 claims abstract description 3
- 239000004071 soot Substances 0.000 claims abstract description 3
- 238000012545 processing Methods 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 25
- 238000004140 cleaning Methods 0.000 claims description 20
- 239000008246 gaseous mixture Substances 0.000 claims description 17
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 10
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 10
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 7
- 239000000243 solution Substances 0.000 claims description 7
- DLCOPLYGCSRNAY-UHFFFAOYSA-N molybdenum titanium vanadium Chemical compound [Ti][Mo][V] DLCOPLYGCSRNAY-UHFFFAOYSA-N 0.000 claims description 6
- WKXHZKXPFJNBIY-UHFFFAOYSA-N titanium tungsten vanadium Chemical compound [Ti][W][V] WKXHZKXPFJNBIY-UHFFFAOYSA-N 0.000 claims description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 5
- 239000001294 propane Substances 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000012159 carrier gas Substances 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Inorganic materials O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 claims description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 4
- 230000001603 reducing effect Effects 0.000 claims description 4
- 230000002000 scavenging effect Effects 0.000 claims description 4
- 238000005245 sintering Methods 0.000 claims description 4
- 239000011800 void material Substances 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 11
- 238000000605 extraction Methods 0.000 abstract description 11
- 230000003197 catalytic effect Effects 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 23
- 239000003546 flue gas Substances 0.000 description 18
- 229910052785 arsenic Inorganic materials 0.000 description 15
- 230000008929 regeneration Effects 0.000 description 14
- 238000011069 regeneration method Methods 0.000 description 14
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 13
- 239000003795 chemical substances by application Substances 0.000 description 10
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 8
- 238000004380 ashing Methods 0.000 description 8
- 238000012512 characterization method Methods 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000003638 chemical reducing agent Substances 0.000 description 8
- 235000013399 edible fruits Nutrition 0.000 description 8
- 238000010926 purge Methods 0.000 description 8
- 238000012360 testing method Methods 0.000 description 8
- 238000010792 warming Methods 0.000 description 8
- 229910001868 water Inorganic materials 0.000 description 8
- 239000003643 water by type Substances 0.000 description 8
- 230000002829 reductive effect Effects 0.000 description 7
- XKRFYHLGVUSROY-UHFFFAOYSA-N argon Substances [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- 229910052786 argon Inorganic materials 0.000 description 6
- COHDHYZHOPQOFD-UHFFFAOYSA-N arsenic pentoxide Chemical compound O=[As](=O)O[As](=O)=O COHDHYZHOPQOFD-UHFFFAOYSA-N 0.000 description 6
- 239000003245 coal Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- GOLCXWYRSKYTSP-UHFFFAOYSA-N Arsenious Acid Chemical compound O1[As]2O[As]1O2 GOLCXWYRSKYTSP-UHFFFAOYSA-N 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 5
- IKIWQIUJLIJZJB-UHFFFAOYSA-N [N].O=[C] Chemical compound [N].O=[C] IKIWQIUJLIJZJB-UHFFFAOYSA-N 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 3
- 208000005374 Poisoning Diseases 0.000 description 3
- SAIFTDNQIARTIU-UHFFFAOYSA-N [N].CCC Chemical compound [N].CCC SAIFTDNQIARTIU-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- UGHRHQDUDTYQNE-UHFFFAOYSA-N ethene helium Chemical compound [He].C=C UGHRHQDUDTYQNE-UHFFFAOYSA-N 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 231100000614 poison Toxicity 0.000 description 3
- 231100000572 poisoning Toxicity 0.000 description 3
- 230000000607 poisoning effect Effects 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 231100000631 Secondary poisoning Toxicity 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- MJLGNAGLHAQFHV-UHFFFAOYSA-N arsenopyrite Chemical compound [S-2].[Fe+3].[As-] MJLGNAGLHAQFHV-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000007096 poisonous effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910017251 AsO4 Inorganic materials 0.000 description 1
- BFVBQNYINQMZDO-UHFFFAOYSA-N [O].[As] Chemical compound [O].[As] BFVBQNYINQMZDO-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000001994 activation Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000002513 implantation Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000011941 photocatalyst Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010301 surface-oxidation reaction Methods 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
- B01J23/90—Regeneration or reactivation
- B01J23/92—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
- B01D53/565—Nitrogen oxides by treating the gases with solids
-
- 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
- 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
- B01D53/88—Handling or mounting catalysts
-
- 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
-
- B01J35/56—
-
- 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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/02—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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
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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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/10—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using elemental hydrogen
-
- 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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/14—Treating with free oxygen-containing gas with control of oxygen content in oxidation gas
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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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
- B01J38/64—Liquid treating or treating in liquid phase, e.g. dissolved or suspended using alkaline material; using salts
-
- 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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
- B01J38/64—Liquid treating or treating in liquid phase, e.g. dissolved or suspended using alkaline material; using salts
- B01J38/66—Liquid treating or treating in liquid phase, e.g. dissolved or suspended using alkaline material; using salts using ammonia or derivatives thereof
-
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
Abstract
The invention belongs to green technology and catalytic denitration field, and in particular to a kind of renovation process of arsenic poisoning SCR denitration.The present invention carries out soot blowing removal of impurities to arsenic poisoning SCR denitration first, then it is cleaned by ultrasonic with deionized water in the case where being passed through ozone-air mixed gas, then soaking and washing is carried out with weakly alkaline solution, two-stage gradient reduction is then carried out using different reducibility gas at different temperature, finally obtains regenerated catalyst through the roasting that is rapidly heated in atmosphere.After being regenerated using the method for the present invention to arsenic poisoning SCR denitration, denitration efficiency returns to fresh catalyst level, and separating by extraction is up to more than 99%, and the anti-arsenic poisoning ability of regenerated catalyst is increased dramatically.In addition, the method technique in the present invention is simple, there is stronger operability, be adapted to large-scale industrial production.
Description
Technical field
The invention belongs to green technology and denitration catalyst field, and in particular to a kind of arsenic poisoning SCR denitration is again
Generation method.
Background technology
SCR (SCR) denitration method has the advantages that denitration efficiency is high, selectivity is good and technical perfection, is mesh
Preceding most widely used gas denitrifying technology.Catalyst is the core of SCR denitration technology, and it is whole that its performance directly affects SCR system
The denitration effect of body.However, in actual use, because working environment is very severe, catalyst because wearing, blocking, in
Poison or sintering etc. reason and inactivate, cause denitration efficiency to significantly reduce, when catalyst can not meet SCR system entirety denitration performance
It is required that when, it need to just change in time.Contain plurality of heavy metal and V in decaying catalyst2O5Deng for having rich in a variety of hypertoxic elements
Evil solid waste, if mishandling, will be unfavorable for the sustainable development of technology, economy and environment.It is catalyzed in order to which specification inactivates
The disposal method of agent, Chinese Ministry of Environmental Protection was in issue in 2010《Thermal power plant's nitrogen oxides technological policy for treatment》(ring sends out [2010] No. 10)
Deng clearly being proposed in file, spent catalyst should preferentially carry out regeneration treatment, encourage the regeneration and safe disposal of spent catalyst
The development and application of technology.It can be seen that regeneration already turns into the inevitable choice of decaying catalyst disposal.
Arsenic is one of important poisonous substance for causing catalyst poisoning to inactivate.Arsenic species in boiler tail flue gas are mainly derived from
Fossil fuel coal.Contain a certain amount of arsenic in the coal in China, and the arsenic species in coal are mainly mispickel, fraction
For organo-arsenic.The content of arsenic species changes with the change of coal, and arsenic contains in the coal of Southwestern China portion, particularly Guizhou exploitation
Amount is very high.During coal burns in stove, mispickel is oxidized to As at high temperature2O3(g), As caused by oxidation2O3
(g) catalyst is diffused into by siphonage.On the one hand, as As in catalyst micropore2O3(g) partial pressure balances more than it
During partial pressure, then it can condense and be adhered in surface site, the situation in blocking catalyst duct, reaction gas is not reached in hole
Active site, trigger catalyst poisoning inactivation；On the other hand, due to photocatalyst surface sites and As2O3(g) have between
Very high adhesion, As2O3(g) easily adsorb in the active sites and non-active site on surface, oxidation reaction life occurs immediately
Into As2O5, As caused by oxidation2O5Constantly accumulated in catalyst surface, form an arsenic coating, blocked NH3Absorption with
Activation process, catalyst poisoning is caused to inactivate.
Regeneration technology about arsenic poisoning catalyst, have scholar at present and probed into, achieve certain achievement.Always
For, existing renovation process is summarized as following classification：First, using strong oxidizer cleaning and regeneration；Second, successively use
Strong weak base salt solution and dilute acid soln cleaning and regeneration；Third, successively use strong base solution and strong acid solution cleaning and regeneration；Its
Four, directly regenerated at high temperature using reductive organic matter；Organic solution cleaning and regeneration is used afterwards fifth, first heat-treating.
Existing arsenic poisoning catalyst recovery process is made a general survey of it can be found that wet reclamation technology has relatively excellent effect of removing arsenic, but
It is the secondary phenomenon poisoned with a large amount of loss by dissolution of active component for being usually associated with catalyst；Thermal reduction regeneration can be good at
Evade disadvantages mentioned above, but existing thermal reduction regeneration technology need to be carried out under thermal extremes, therefore there is also catalyst high temperature
Phenomena such as sintering and avtive spot destroy.
Based on above mentioned problem, the present invention is directed to arsenic poisoning SCR denitration, special around its exclusive physics, chemistry
Property, based on existing correlative study, the renovation process of arsenic poisoning SCR denitration is explored, is sought rationally effective, suitable
The technical scheme of production scale maximization.
The content of the invention
It is an object of the invention to provide a kind of rationally effective arsenic poisoning SCR denitration renovation process, using this
The denitration efficiency of method regeneration gained catalyst returns to fresh catalyst level, and separating by extraction regenerates up to more than 99%
The anti-arsenic poisoning ability of catalyst is increased dramatically.
According to method provided by the invention, this method comprises the following steps：
(1) mechanical soot blowing processing is carried out to arsenic poisoning SCR denitration first, then with deionized water be passed through it is smelly
It is cleaned by ultrasonic in the case of oxygen-air gas mixture；
(2) catalyst after step (1) processing is placed in weakly alkaline solution and carries out soaking and washing, during cleaning
Carry out the stirring of discontinuity；
(3) catalyst after step (2) processing is rinsed with deionized water, be then dried；
(4) catalyst after step (3) processing is placed in reactor, be passed through using inert gas as carrier gas, with hydrogen or
A kind of strong reducing property gas of or above two gaseous mixture composition in carbon monoxide, carries out one-level reduction at low temperature, its
In, void fraction is 1~30%, and reduction temperature is 250~300 DEG C, and the recovery time is 1~6h；Then, it is passed through with inertia
Gas is carrier gas, with a kind of or above-mentioned gas week reduction gas formed in ethene, propane or propylene
Second-stage reduction is carried out at high temperature, wherein, void fraction is 1~30%, and reduction temperature is 350~550 DEG C, the recovery time
For 0.5~1.5h；Finally, regenerated catalyst is obtained after the roasting that is rapidly heated in atmosphere.
Preferably, in described step (1), arsenic poisoning SCR denitration is vanadium tungsten titanium (V2O5-WO3/TiO2) system
Or vanadium molybdenum titanium (V2O5-MoO3/TiO2) system honeycomb type denitrification catalyst.
Preferably, in described step (1), the cleaning temperature of deionized water is 40~60 DEG C, scavenging period is 5~
20min。
Preferably, in described step (1), the concentration of ozone is 10~250mg/L in ozone-air mixed gas.
Preferably, in described step (2), weakly alkaline solution is one or two kinds of weak base in MEA or ammoniacal liquor
The mixed liquor of property solution, and solution concentration is 0.05~1.0mol/L, scavenging period is 10~60min.
Preferably, in described step (3), drying temperature is 80~150 DEG C, and drying time is 4~12h.
Preferably, in described step (4), sintering temperature is 400~550 DEG C, and heating rate is 20~30 DEG C/min, roasting
The burning time is 1~5h.
Beneficial effects of the present invention are：
The present invention is regenerated with wet-cleaning with heat-treating the method being combined to arsenic poisoning catalyst.First, this hair
It is bright to be carried out being cleaned by ultrasonic the flying dust that removed catalyst surface and deposit with deionized water, while be passed through during cleaning smelly
Oxygen, there is many beneficial effects：Ozone has strong oxidizing property, on the one hand can be by the most As of catalyst surface2O3It is oxidized to
As2O5, be advantageous to the removing of arsenic species.Another aspect ozone can not only be by the V of catalyst surface4+V is oxidized in appropriate amount5+, reach
To regulation active component valence state, optimization catalyst surface V4+/V5+The purpose of ratio, and can also be by the carbon distribution of catalyst surface
Oxidation removes, and the specific surface area and pore volume for enabling catalyst are recovered, and are advantageous to the recovery of catalytic activity.In addition, according to it
He is handled the strong oxidizer of type, can bring many negative effects, although being handled for example with hydrogen peroxide or potassium permanganate
Also can be by As2O3It is oxidized to As2O5, but a large amount of dissolvings or the K of active component are may result in during handling+Deng metal from
The introducing of sub- impurity, cause secondary Poisoning Phenomenon.Then, the present invention is cleaned using specific weakly alkaline solution, same tool
There are many beneficial effects：First, the As of indissoluble in the basic conditions2O5Can be with AsO4 3-Form be transferred in solution, thus energy
It is enough to be removed to greatest extent, be advantageous to the recovery of catalyst activity；Second, it can be kept away using MEA or ammoniacal liquor cleaning
Exempt from Na+Or K+Deng the introducing of impurity metal ion, secondary Poisoning Phenomenon will not be produced, while can be made most in catalyst
V2O5And WO3(or MoO3) etc. important component retained, thus the active implantation step of conventional regeneration technology can be omitted；
Third, can be by destruction control of the cleaning fluid to catalyst physical structure in the scope of minimum, to catalytic mechanical performance shadow
Sound is smaller.Then, the present invention is handled arsenic poisoning catalyst using unique two-step heating gradient reducing process, with thoroughly
The arsenic species of remained on surface are removed, (250~300 DEG C) can remove using the progress one-level reduction of strong reducing property gas at low temperature
The arsenic species of catalyst surface residual, (350~550 DEG C) use week reduction gas progress second-stage reduction can be clear at high temperature
Except the arsenic species adsorbed in catalyst micropore, and have the advantages that：First, catalyst table can be removed to greatest extent
The arsenic species of face residual, separating by extraction is up to more than 99%；Second, after weakly alkaline solution is handled, catalyst and the arsenic oxygen of residual
Interaction force between compound weakens, thus reduction temperature is relatively low, and avoiding progress high temperature reduction for a long time may cause
Catalyst carrier and active component architectural characteristic deterioration.Finally, obtained in atmosphere through the roasting that is rapidly heated, catalyst activity
To recover, denitration activity reaches fresh catalyst level, one-step optimization catalyst void structure of going forward side by side, is retaining a large amount of micropores
On the basis of, add part mesopore and macropore.Even if the catalyst after regeneration in actual flue gas running micropore by arsenic
Being blocked Deng poisonous substance, mesopore and macropore still can keep its catalytic activity as the duct that gas circulates, therefore, arsenic poisoning catalysis
After above-mentioned regeneration treatment, its anti-arsenic poisoning performance is significantly enhanced for agent.
Embodiment
The invention provides a kind of renovation process of arsenic poisoning SCR denitration, with reference to embodiment pair
The present invention is described further.
Embodiment 1
Embodiment 1 describes a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium molybdenum titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 80mg/L and mixes
Gas is closed, ultrasonic vibration cleans 20min at 40 DEG C；
(2) MEA that the catalyst after step (1) processing is moved to enough 0.25mol/L prepared in advance is molten
Soaking and washing 40min in liquid, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through the hydrogen that hydrogen volume concentration is 6%
Gas-argon gas gaseous mixture reduces 3h at 280 DEG C, and the ethene-helium mix gas for then switching to volume of ethylene concentration to be 12% exists
1.5h is reduced at 450 DEG C, finally catalyst is moved in Muffle furnace and is warming up to 500 DEG C with 25 DEG C/min speed, and in the temperature
The lower roasting 3h of degree obtains regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 90.67%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 2
Embodiment 2 also illustrates a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium molybdenum titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 80mg/L and mixes
Gas is closed, ultrasonic vibration cleans 20min at 40 DEG C；
(2) MEA that the catalyst after step (1) processing is moved to enough 0.5mol/L prepared in advance is molten
Soaking and washing 30min in liquid, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through carbon monoxide volumetric concentration as 6%
Carbon monoxide-nitrogen mixture 3h is reduced at 280 DEG C, then switch to volume of ethylene concentration be 12% ethene-helium
Gaseous mixture reduces 1h at 500 DEG C, finally moves in Muffle furnace catalyst and is warming up to 500 DEG C with 25 DEG C/min speed, and
3h is calcined at such a temperature obtains regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 91.00%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 3
Embodiment 3 also illustrates a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium molybdenum titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 120mg/L
Gaseous mixture, ultrasonic vibration cleans 16min at 40 DEG C；
(2) MEA that the catalyst after step (1) processing is moved to enough 0.75mol/L prepared in advance is molten
Soaking and washing 20min in liquid, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through the hydrogen that hydrogen volume concentration is 6%
Gas-argon gas gaseous mixture reduces 3h at 280 DEG C, and the ethene-helium mix gas for then switching to volume of ethylene concentration to be 12% exists
0.5h is reduced at 550 DEG C, finally catalyst is moved in Muffle furnace and is warming up to 500 DEG C with 25 DEG C/min speed, and in the temperature
The lower roasting 3h of degree obtains regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 92.00%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 4
Embodiment 4 also illustrates a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium molybdenum titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 120mg/L
Gaseous mixture, ultrasonic vibration cleans 16min at 40 DEG C；
(2) MEA that the catalyst after step (1) processing is moved to enough 1.0mol/L prepared in advance is molten
Soaking and washing 10min in liquid, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through carbon monoxide volumetric concentration as 6%
Carbon monoxide-nitrogen mixture 3h is reduced at 280 DEG C, then switch to propane volumetric concentration be 12% propane-nitrogen
Gaseous mixture reduces 1.5h at 450 DEG C, finally moves in Muffle furnace catalyst and is warming up to 500 DEG C with 25 DEG C/min speed,
And it is calcined 3h at such a temperature and obtains regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 91.33%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 5
Embodiment 5 also illustrates a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium tungsten titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 160mg/L
Gaseous mixture, ultrasonic vibration cleans 12min at 40 DEG C；
(2) catalyst after step (1) processing is moved in enough 0.25mol/L prepared in advance ammonia spirit
Soaking and washing 40min, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through the hydrogen that hydrogen volume concentration is 6%
Gas-argon gas gaseous mixture reductase 12 .5h at 300 DEG C, then switch to propane-nitrogen mixture that propane volumetric concentration is 12%
1.0h is reduced at 500 DEG C, finally catalyst is moved in Muffle furnace and is warming up to 500 DEG C with 25 DEG C/min speed, and at this
Roasting temperature 3h obtains regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 92.00%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 6
Embodiment 6 also illustrates a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium tungsten titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 160mg/L
Gaseous mixture, ultrasonic vibration cleans 12min at 40 DEG C；
(2) catalyst after step (1) processing is moved in enough 0.5mol/L prepared in advance ammonia spirit
Soaking and washing 30min, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through carbon monoxide volumetric concentration as 6%
Carbon monoxide-nitrogen mixture at 300 DEG C reductase 12 .5h, then switch to propane volumetric concentration be 12% propane-nitrogen
Gas gaseous mixture reduces 0.5h at 550 DEG C, finally moves in Muffle furnace catalyst and is warming up to 500 with 25 DEG C/min speed
DEG C, and be calcined 3h at such a temperature and obtain regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 92.33%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 7
Embodiment 7 describes a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium tungsten titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 200mg/L
Gaseous mixture, ultrasonic vibration cleans 8min at 40 DEG C；
(2) catalyst after step (1) processing is moved in enough 0.75mol/L prepared in advance ammonia spirit
Soaking and washing 20min, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through the hydrogen that hydrogen volume concentration is 6%
Gas-argon gas gaseous mixture reductase 12 .5h at 300 DEG C, then switch to propylene-argon gas gaseous mixture that propylene volumetric concentration is 12%
1.0h is reduced at 500 DEG C, finally catalyst is moved in Muffle furnace and is warming up to 500 DEG C with 25 DEG C/min speed, and at this
Roasting temperature 3h obtains regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 91.66%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
Embodiment 8
Embodiment 8 also illustrates a kind of renovation process of arsenic poisoning SCR denitration, and its specific step includes：
(1) the vanadium tungsten titanium system honeycomb fashion SCR denitration of arsenic poisoning is chosen, mechanical ashing is carried out to it first, then
With the compressed air purging 1h of 2Mpa clean drieds, remove catalyst surface and hole inside ash, 5 × 5 holes for extracting high 60mm are urged
Agent block, then it is immersed in enough deionized waters, while is passed through the ozone-air that ozone concentration is 200mg/L
Gaseous mixture, ultrasonic vibration cleans 8min at 40 DEG C；
(2) catalyst after step (1) processing is moved in enough 1.0mol/L prepared in advance ammonia spirit
Soaking and washing 10min, the stirring of discontinuity is carried out during cleaning；
(3) catalyst after step (2) processing is rinsed repeatedly with deionized water, catalyst is then put into baking
Case, 8h is dried at 110 DEG C；
(4) catalyst after step (3) processing is placed in reactor, while is passed through carbon monoxide volumetric concentration as 6%
Carbon monoxide-nitrogen mixture at 300 DEG C reductase 12 .5h, then switch to propylene volumetric concentration be 12% propylene-argon
Gas gaseous mixture reduces 0.5h at 550 DEG C, finally moves in Muffle furnace catalyst and is warming up to 500 with 25 DEG C/min speed
DEG C, and be calcined 3h at such a temperature and obtain regenerated catalyst.
The performance of regenerated catalyst is evaluated using simulated flue gas condition, with NH3For reducing agent, typical flue gas operating mode
Under：NO is 300ppm, SO2For 300ppm, O2For 3vol%, H2O is 5vol%, and ammonia nitrogen ratio is 1: 1, N2For Balance Air, air speed is
4500h-1, the denitration efficiency when reaction temperature is 350 DEG C is 92.33%.Characterization test, knot are carried out to regenerated catalyst simultaneously
Fruit shows its separating by extraction up to more than 99%.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
God any modification, equivalent substitution and improvements done etc., should be included within the scope of the present invention with principle.
Claims (7)
1. a kind of renovation process of arsenic poisoning SCR denitration, it is characterised in that this method comprises the following steps：
(1) mechanical soot blowing processing is carried out to arsenic poisoning SCR denitration first, is then being passed through ozone-sky with deionized water
It is cleaned by ultrasonic in the case of oxygen mixture；
(2) catalyst after step (1) processing is placed in weakly alkaline solution and carries out soaking and washing, carried out during cleaning
The stirring of discontinuity；
(3) catalyst after step (2) processing is rinsed with deionized water, be then dried；
(4) catalyst after step (3) processing is placed in reactor, be passed through using inert gas as carrier gas, with hydrogen or an oxygen
Change a kind of strong reducing property gas of the or above two gaseous mixture composition in carbon, carry out one-level reduction at low temperature, wherein, gas
Body volumetric concentration is 1~30%, and reduction temperature is 250~300 DEG C, and the recovery time is 1~6h；Then, it is passed through with inert gas
For carrier gas, with a kind of or above-mentioned gas week reduction gas formed in ethene, propane or propylene in height
Temperature is lower to carry out second-stage reduction, wherein, void fraction is 1~30%, and reduction temperature is 350~550 DEG C, and the recovery time is
0.5~1.5h；Finally, regenerated catalyst is obtained after the roasting that is rapidly heated in atmosphere.
2. the renovation process of a kind of arsenic poisoning SCR denitration according to claim 1, it is characterised in that described
In step (1), arsenic poisoning SCR denitration is vanadium tungsten titanium (V2O5-WO3/TiO2) system or vanadium molybdenum titanium (V2O5-MoO3/TiO2)
The honeycomb type denitrification catalyst of system.
3. the renovation process of a kind of arsenic poisoning SCR denitration according to claim 1, it is characterised in that described
In step (1), the cleaning temperature of deionized water is 40~60 DEG C, and scavenging period is 5~20min.
4. the renovation process of a kind of arsenic poisoning SCR denitration according to claim 1, it is characterised in that described
In step (1), the concentration of ozone is 10~250mg/L in ozone-air mixed gas.
5. the renovation process of a kind of arsenic poisoning SCR denitration according to claim 1, it is characterised in that described
In step (2), weakly alkaline solution is the mixed liquor of MEA or one or two kinds of weakly alkaline solution in ammoniacal liquor, and solution
Concentration is 0.05~1.0mol/L, and scavenging period is 10~60min.
6. the renovation process of a kind of arsenic poisoning SCR denitration according to claim 1, it is characterised in that described
In step (3), drying temperature is 80~150 DEG C, and drying time is 4~12h.
7. the renovation process of a kind of arsenic poisoning SCR denitration according to claim 1, it is characterised in that described
In step (4), sintering temperature is 400~550 DEG C, and heating rate is 20~30 DEG C/min, and roasting time is 1~5h.
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| CN108126521A (en) * | 2017-12-27 | 2018-06-08 | 吉林省电力科学研究院有限公司 | A kind of regeneration method for coal steam-electric plant smoke denitration vanadium Ti-base catalyst |
| CN109999923A (en) * | 2019-04-28 | 2019-07-12 | 上海理工大学 | A kind of method and device for realizing SCR catalyst in-situ activation using ozone |
| CN110385044A (en) * | 2019-07-24 | 2019-10-29 | 中国科学院过程工程研究所 | A kind of method of useless SCR catalyst dearsenification desiliconization |
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| CN106732655A (en) * | 2016-12-05 | 2017-05-31 | 江苏肯创催化剂再生技术有限公司 | A kind of arsenic poisoning SCR denitration renovation process |
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| CN110385044A (en) * | 2019-07-24 | 2019-10-29 | 中国科学院过程工程研究所 | A kind of method of useless SCR catalyst dearsenification desiliconization |
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