CN102039137A - Honeycomb catalyst for catalytically incinerating sulfur recovery tail gases and preparation method - Google Patents
Honeycomb catalyst for catalytically incinerating sulfur recovery tail gases and preparation method Download PDFInfo
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- CN102039137A CN102039137A CN 200910204274 CN200910204274A CN102039137A CN 102039137 A CN102039137 A CN 102039137A CN 200910204274 CN200910204274 CN 200910204274 CN 200910204274 A CN200910204274 A CN 200910204274A CN 102039137 A CN102039137 A CN 102039137A
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Abstract
The invention provides a honeycomb catalyst for catalytically incinerating sulfur recovery tail gases and a preparation method. The catalyst is a honeycomb monomer and comprises the following active ingredients by weight percent: 1.0-15% of oxide of vanadium, 1.0-12.0% of oxide of iron and 73-98% of oxide of titanium. The preparation method is characterized by dipping vanadium and iron on a honeycomb titanium dioxide carrier. The catalyst has the characteristics of high performance, low cost, simple adaptable process, high removal rates of hydrogen sulfide and carbonyl sulfide and the like, and can be used for incinerating compounds in the sulfur recovery tail gases or other waste gases, such as hydrogen sulfide, carbon disulfide, carbonyl sulfide and the like.
Description
Technical field
The present invention relates to cellular sulfur recovery tail gas catalytic incineration catalyst and preparation method thereof, be applicable to the exhaust-gas treatment of sulfur-containing compounds such as all kinds of sulfide hydrogens, carbon disulfide and cos, above-mentioned sulfide can be converted into stink and all lower sulfur dioxide of toxicity, the catalytic burning that is specially adapted to sulfur recovery claus process tail gas, geothermal power plant's waste gas is handled.
Background technology
Hydrogen sulfide and organic sulfur compound (as carbon disulfide, cos) are that a class has the odorant pollutant of toxicity in various degree to human body, mainly from industrial tail gas such as oil refining, natural gas, chemical industry, sewage disposal, geothermal power generations, China has issued its discharging of the strict qualification of odorant pollutant discharge standard (GB 14554-93).With the oil plant is example, and the sulphur in its processing crude oil is most of to be reclaimed by the form of its sulfur recovery unit with elemental sulfur, and sulfur recovery technology mainly comprises claus process and Crouse+tail-gas deep process for purifying two classes.The claus process sulfur recovery rate generally is no more than 96%, and Crouse+tail-gas deep process for purifying sulfur recovery rate is generally 98.5%～99.8%, and the sulphur of Hui Shouing does not enter sulfur recovery tail gas with forms such as hydrogen sulfide, sulfur dioxide, carbon disulfide, cos.No matter adopt which kind of sulfur recovery technology,,, could discharge after must burning for satisfying the odorant pollutant discharge standard because of containing a certain amount of hydrogen sulfide and organic sulfur compound in its tail gas.Owing to be lower than 3% of tail gas total amount the combustible component (as hydrogen sulfide, cos, carbon monoxide, carbon disulfide, hydrogen, elementary sulfur and a small amount of oil gas) in the Claus tail gases, necessary postcombustion, could completing combustion, and be sulfur dioxide with sulfide oxidation.The tail gas burning process has thermal incineration and catalytic burning two classes.The thermal incineration method is carried out excessive oxygen and 650～820 ℃ usually, owing to be difficult to accurately control operating condition such as incineration temperature, often occurred low temperature in the practice and causes burning not exclusively, or the excessive temperature situation that causes incinerator to crumple.Catalytic burning can make hydrogen sulfide, cos sulfides in the tail gas be oxidized to sulfur dioxide with lower temperature (as 300～400 ℃) under catalyst action.The output investment ratio thermal incineration of catalytic burning is slightly high, but the thermal incineration device of comparable equal scale is saved 60% fuel consumption at least, and satisfies environmental protection and energy-conservation needs simultaneously.Along with the maturation of technology and rising steadily of fuel price, the potentiality of catalytic burning technology manifest gradually.In addition, for satisfying strict emission control standards day by day, simple Sulfur Recovery Unit technology will progressively upgrade to Crouse+tail-gas deep process for purifying (as SCOT technology), and advanced purification process tail gas cleans relatively, catalyst is difficult for polluting or poisoning, and is more suitable for catalytic burning.The catalytic burning device can be built with the thermal incineration system is parallel, accident emergency when the vent gas treatment facility when catalytic burning runs well as sulfur recovery unit, thermal incineration break down as catalytic burning system, SCOT exhaust treatment system or whole sulfur recovery system burns means.
Catalyst is the pith of sulphide-rich gas catalytic burning technology, and the key of this class catalyst performance is how to overcome the sulfation of catalyst active center, the stability of the long-time running of maintenance catalyst and active.CN1049299 discloses a kind of sulfur-bearing organic catalyst to burned waste gas and preparation method thereof, and this catalyst is a carrier with the natural mordenite zeolite of sulfuric acid treatment modification, V
2O
5Be main active component, noble metals such as a spot of platinum, palladium are the auxiliary activity component, V
2O
5Content is that 0.4%～0.7% (percentage composition of catalytic component is the quality percentage composition, down together), platinum content is 0.01%～0.02%, and palladium content is 0.02%～0.03%, also can contain one or more of 0.01%～0.07% cobalt, manganese, molybdenum, nickel, potassium, na oxide.At 320～380 ℃ of reaction temperatures, air speed 4800～10000h
-1, during organic sulfur concentration 800～10000mg/L, conversion ratio 〉=99%.This catalyst loading noble metal, cost is higher, sulfur poisoning-resistant is limited in one's ability.CN1163785 discloses the catalytic burning technique of hydrogen sulfide in a kind of gas, is suitable for handling Claus tail gases, and with the activated carbon catalyst, be under 200～400 ℃ in temperature, be sulfur dioxide with the hydrogen sulfide catalytic oxidation.Hydrogen sulfide content is 0.5%～4% (v/v), moisture content 4%～30% (v/v), air speed 3000～10000h
-1, the conversion ratio of hydrogen sulfide is 100%, sulfur dioxide production rate 90%～99%.USP4576184, USP4444908, USP4528277, USP4444741, USP4444742, USP4314983 discloses a class hydrogen sulfide catalyst for catalytic oxidation and a technology, this activity of such catalysts component comprises vanadium and bismuth, also can constitute by vanadium and tin or antimony, carrier is the porous refractory oxide, by aluminium oxide, silica-alumina, silica, titanium dioxide, zirconia, silica-titania, silica-zirconia, one or more formations in silica-zirconia-titanium dioxide, hydrogen sulfide can be oxidized to sulphur or sulfur dioxide, characteristics are when steam exists, and still have high activity and stability.For example active component is 11.6%Bi
2O
3+ 8.6%V
2O
5Catalyst, at 240 ℃ of reaction temperatures, air speed 2000h
-1, the hydrogen sulfide of 0.27% (v/v) is converted into sulfur dioxide fully, and hydrogen and methane are not oxidized.USP4427576, USP4937058 discloses a kind of catalyst and preparation technology thereof who hydrogen sulfide or organic sulfur is oxidized to sulfur dioxide, the carrier of this catalyst is a titanium dioxide, or the mixture of titanium dioxide and zirconia or silica, active component is made of at least a of a kind of alkali earth metal sulfate and following metal: copper, silver, zinc, cadmium, yttrium, lanthanum, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, rhodium, iridium, nickel, palladium, platinum, tin and bismuth, the content of carrier is 60%～99%, the content of alkali earth metal sulfate is 1%～40%, and the specific surface of catalyst is 20～500m
2/ g.380 ℃ of reaction temperatures, air speed 1800h
-1Feeding gas sulfide hydrogen 0.08% (v/v), cos 0.01% (v/v), carbon disulfide 0.05% (v/v), sulfur dioxide 0.04% (v/v), oxygen 2%, steam 30%, nitrogen 67.82%, the catalytic conversion of hydrogen sulfide＞99%, the catalytic conversion 61%～98% of carbon disulfide, the catalytic conversion 52%～94% of cos.It can be the catalyst of sulfur dioxide with selective oxidation of sulfur containing compounds in particular that USP5278123 discloses a kind of, and carrier is a titanium dioxide, and active component is iron and platinum.USP4169136, USP4092404, USP4171347, USP4088743 disclose the catalytic burning technique of hydrogen sulfide in the class gas, this technology can be oxidized to sulfur dioxide with hydrogen sulfide, operating temperature is 150～480 ℃, the activity of such catalysts component is the oxide of vanadium and/or the sulfide of vanadium, and carrier is non-alkaline porous refractory oxide.A kind of well behaved catalyst is 5%～15% V
2O
5/ hydrogenation mordenite or aluminium oxide.Hydrogen in the feeding gas, carbon monoxide, lighter hydrocarbons and ammonia are not oxidized, and patent has been used for geothermal power plant's treatment of waste gas.USP4399112 discloses a kind of sulphur-containing exhaust gas catalytic burning technique, can be used for the processing of Claus tail gases, this technology has two stages to constitute, be hydrogen sulfide at first with carbon disulfide, cos, mercaptan sulfides hydrogenating reduction, and then be sulfur dioxide with the hydrogen sulfide catalytic oxidation, the catalyst of its oxidation panel is ferric sulfate/titanium dioxide.
Above-mentioned existing catalytic incineration catalyst for sulfur-containing compound exhaust air has the component complexity, sulfur tolerance is poor, cost is high and need to adopt one or more deficiencies in the complex techniques process etc., in addition, above-mentioned catalyst is generally sphere, the catalytic burning reactor bed vapour lock of filling this type of catalyst is bigger, and the operation air speed is higher.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of cellular sulfur recovery tail gas catalytic incineration catalyst and preparation method thereof, advantage such as catalyst of the present invention has the performance height, cost is low, catalytic activity is high, the applicable craft flow process is simple, hydrogen sulfide and cos clearance height, sulfur tolerance are good.
Sulfur recovery tail gas catalytic incineration catalyst of the present invention is that monomer is cellular, and active component is made up of the oxide of vanadium, the oxide and the titanyl compound of iron.Catalyst active ingredient by weight is oxide content 1.0%～15%, the oxide content 1.0%～12.0% of iron, the titanium dioxide 73%～98% or 1%～8% of vanadium.The specific area of catalyst is 300～2100m
2/ m
3, the pitch of holes of cellular catalytic incineration catalyst is 1.45～7.0mm, and the wall thickness of cellular catalytic incineration catalyst is 0.25～1.0mm, and the endoporus length of side of cellular catalytic incineration catalyst is for being 1.0～6.0mm.
Can comprise the honeycomb support that inert material is made in the cellular catalytic incineration catalyst, this moment, the content of active component titanium dioxide was 1%～8%, and inert material is as pottery, cordierite etc.; Cellular catalytic incineration catalyst also can not contain the honeycomb support that inert material is made, and directly makes cellular catalytic incineration catalyst by the active component that comprises titanium dioxide, and this moment, the active component content of titanium dioxide was 73%～98%.
Catalyst activity of the present invention can be used for sulfur recovery tail gas or other contains the burning disposal of compound exhaust airs such as hydrogen sulfide, carbon disulfide or cos, and above-claimed cpd is oxidized to sulphur, sulfur dioxide, carbon dioxide and water.The operating temperature of catalyst is 200～400 ℃, and air speed is 1500～30000h
-1, crossing oxygen quotient is 1.0～5.0.320 ℃ of catalyst operating temperatures, air speed 6000h
-1, when crossing oxygen quotient 2.0, concentration of hydrogen sulfide 0.2% (v/v), cos concentration 0.05% (v/v), the clearance 100% of hydrogen sulfide, the clearance of cos is higher than 90%, the sulfur dioxide production rate is higher than 98%.
The optimum shape of catalyst of the present invention is that monomer is cellular, and aperture 1.0～3.0mm adopts molding in integral or the concrete preparation procedure of saturated immersion process for preparing as follows:
(1) on honeycomb inert material (as pottery etc.) carrier, prepares coating of titanium dioxide, adopt infusion process load active component V then
2O
5And Fe
2O
3The honeycomb ceramic carrier coating of titanium dioxide can adopt the sol-gel process preparation, and butyl titanate is dissolved in absolute ethyl alcohol by a certain percentage, is mixed with solution 1; Glacial acetic acid, hydrochloric acid, distilled water and absolute ethyl alcohol are mixed by a certain percentage, be mixed with solution 2; Solution 2 slowly is added drop-wise in the solution 1, and stirring 1h obtains colloidal sol under 30 ℃; Honeycomb ceramic carrier boils 0.5h with 5% nitric acid, then with distilled water flushing and dry; This carrier of handling well is immersed colloidal sol, take out behind 2～5min, 80～150 ℃ of oven dry, 400～550 ℃ of roasting 2～4h prepare single coating; Repeat to immerse colloidal sol, oven dry and roasting, can prepare the multilayer coated of appointed thickness.But coating of titanium dioxide honeycomb ceramic carrier single-steeping and roasting or twice dipping and roasting load active component V
2O
5And Fe
2O
3Single-steeping and method of roasting are: the water soluble compound with vanadium is dissolved in oxalic acid solution earlier, adds the water soluble compound of iron then, is prepared into maceration extract; The coating of titanium dioxide honeycomb ceramic carrier directly with the saturated dipping of above-mentioned maceration extract, is obtained final catalyst after gained sample drying, the roasting; The water soluble compound of vanadium is decomposed into V through roasting
2O
5, the water soluble compound of iron is decomposed into Fe through roasting
2O
3Double-steeping and method of roasting are: the water soluble compound of vanadium is dissolved in oxalic acid solution, is prepared into maceration extract 1; The water soluble compound of iron is dissolved in pure water, is prepared into maceration extract 2; The coating of titanium dioxide honeycomb ceramic carrier is directly used maceration extract 1 saturated dipping, after gained sample drying, the roasting, use maceration extract 2 saturated dippings again, gained sample drying, roasting obtain final catalyst; The water soluble compound of vanadium is decomposed into V through roasting
2O
5, the water soluble compound of iron is decomposed into Fe through roasting
2O
3Baking temperature is 110～150 ℃, and be 2～12h drying time, and sintering temperature is 450～550 ℃, and roasting time is 2～5h.The water soluble compound of vanadium is preferably ammonium metavanadate, and ammonium metavanadate need be by oxalic acid: the ammonium metavanadate mol ratio was dissolved in the oxalic acid solution in 1: 1～3: 1.The water soluble compound of iron is preferably ferric nitrate.
(2) with a certain amount of titania powder, methylcellulose powder and ammonium metavanadate mixed grinding, add iron nitrate solution (ferric nitrate is dissolved in distilled water), stir and be kneaded into the suitable lotion of hardness, this lotion is put into 40～100 ℃ of honeycomb die extrusion modlings and 100～150 ℃ dry 1～8h respectively, 200～350 ℃ and 400～550 ℃ of difference roasting 2～16h obtain final catalyst.
(3) with a certain proportion of titania powder, vanadium pentoxide powder, ferric oxide powder mixed grinding, adding an amount of polyacrylamide and activated carbon powder fully mixes, adding monoethanolamine and water stirs evenly, mediates, make the suitable lotion of hardness, this lotion is put into the honeycomb die extrusion modling, dry 1～8h respectively for 40～100 ℃ and 100～150 ℃, 200～350 ℃ and 400～550 ℃ of difference roasting 2～16h obtain final catalyst.
In general, the oxide weight percentage composition of vanadium and iron respectively is about 5%, about titanium dioxide 90%, get final product for general sulfur compound waste gas, if the sulfide concentration in the waste gas is lower, also can adopt the lower vanadium and the oxide content of iron, otherwise can adopt the higher vanadium and the oxide content of iron.Those skilled in the art can select to determine according to concrete applicable cases.
Catalyst of the present invention is used for the catalytic burning of sulphide-rich gas (as hydrogen sulfide, carbon disulfide, cos etc.), is specially adapted to the catalytic burning of oil plant Sulfur Recovery Unit process tail gas.Its technical process is: sulphide-rich gas is mixed with excess air, after the preheating, with 1500～30000h
-1Air speed by the integral type catalytic reactor, under 200～400 ℃ of reaction temperatures, hydrogen sulfide, carbon disulfide and cos are sulphur, sulfur dioxide, carbon dioxide and water by catalytic oxidation.
Sulfur recovery tail gas catalytic incineration catalyst of the present invention is a main active component with vanadium and ferriferous oxide and titanium dioxide, under the condition that keeps the hydrogen sulfide higher conversion, improved the conversion rate of oxidation of carbon disulfide and cos greatly, can adopt simple one section catalytic burning technique simultaneous oxidation to handle multiple sulfur compound, catalyst applied widely, technique for applying is simple.
Specifically, sulfur recovery catalytic incineration catalyst of the present invention has following advantage: alveolate texture, and the bed vapour lock is less, and the operation air speed is higher; 200～400 ℃ of operating temperatures, empty scooter 30000h
-1Catalyst life is longer, all anti-sulfation of carrier and active component; The catalytic activity height, under optimum conditions, the oxygenation efficiency of hydrogen sulfide is 100%, and the oxygenation efficiency of carbon disulfide and cos is higher than 90%, and the sulfur dioxide production rate is higher than 95%; The catalyst cost is lower, and goes for simple catalytic burning technique flow process, and the application investment is low.
The specific embodiment
Embodiment 1
The butyl titanate of measuring 50mL adds in the 500mL beaker, adds the 50mL absolute ethyl alcohol under electromagnetic agitation, stirs under the room temperature and is mixed with solution A.Preparation glacial acetic acid, hydrochloric acid, distilled water and absolute ethyl alcohol volume ratio are respectively 25%, 5%, 10% and 60% solution B 100mL.Solution A drips solution B under electromagnetic agitation, prepare flaxen colloidal sol after fully stirring evenly.Honeycomb ceramic carrier is boiled 30min in 5% salpeter solution, take out with behind the distilled water flushing 5 times oven dry.Behind the ceramic honey comb immersion colloidal sol 2min that handles well, slowly take out, in 105 ℃ of oven dry, in Muffle furnace, 500 ℃ of following roasting 2h naturally cool to room temperature then, repeat above-mentioned steps 6 times, obtain the carrier of required coating of titanium dioxide thickness.
Take by weighing 100g oxalic acid (C
2H
2O
42H
2O) be dissolved in 80ml distilled water (heating is short molten in water-bath), add 48g ammonium metavanadate (NH then
4VO
3), after fully reacting and leaving standstill 2h, add 168g ferric nitrate (Fe (NO
3)
39H
2O), fully after the dissolving and after leaving standstill 2h, be settled to 250ml, be prepared into maceration extract.The honeycomb ceramic carrier of coating titanium dioxide is dipped in the maceration extract, and places 2h.The gained sample is 150 ℃ of dry 4h, 500 ℃ of roasting 4h in air atmosphere.Make the V that consists of of catalyst activity composition
2O
52.0%, Fe
2O
31.5%, TiO
23.0%, specific area is 1850m
2/ m
3, average pore size is 5.0nm.
Comparative example 1
Press embodiment 1 described method, just do not contain active component Fe in the catalyst
2O
3, V
2O
5Content increases to 3.0%.
Comparative example 2
According to embodiment 1 described method, just do not contain TiO in the catalyst
2, but, preparing silica containing catalyst by same procedure silicon-coating colloidal sol, silica content by weight is 3.0%.
Embodiment 2
With the titania powder of 300g, the methylcellulose powder of 5g and ammonium metavanadate mixed grinding 45min in ball mill of 20g, add the iron nitrate solution (Fe (NO of 68g
3)
39H
2O is dissolved in 70mL distilled water), continue to grind 15min, and add distilled water and make abrasive material evenly be mixed into the suitable lotion of hardness, this lotion is put into the honeycomb die extrusion modling, 60 ℃ of oven dry 5h and 105 ℃ of oven dry 6h, 250 ℃ of roasting 8h and 500 ℃ of roasting 10h.The specific area that makes catalyst is 1150m
2/ m
3, pitch of holes is 3.0mm, wall thickness is 0.5mm.Catalyst consist of V
2O
54.5%, Fe
2O
34.0%, TiO
290.5%.
Embodiment 3
With the titania powder of 450g, the vanadium pentoxide powder of 25g, the ferric oxide powder of 20g, the polyacrylamide of 6g and activated carbon powder mixed grinding 45min in ball mill of 2g, grind on the limit, ethanolamine solutions (monoethanolamine and distilled water volume ratio are 1: 5) is slowly added on the limit, make the suitable lotion of hardness, this lotion is put into the honeycomb die extrusion modling, 60 ℃ of oven dry 7h and 105 ℃ of oven dry 4h, 250 ℃ of roasting 8h and 500 ℃ of roasting 10h.The specific area that makes catalyst is 980m
2/ m
3, pitch of holes is 3.0mm, wall thickness is 0.5mm.Catalyst consist of V
2O
55.0%, Fe
2O
34.0%, TiO
291.0%.
Embodiment 4
On small-sized catalytic burning experimental rig, embodiment 1 catalyst is estimated, feeding gas consists of hydrogen sulfide 0.2% (v/v), cos 0.05% (v/v), steam 3.0% (v/v), oxygen 0.75% (v/v), all the other are high pure nitrogen, 350 ℃ of reaction temperatures, air speed 6000h
-1, the conversion ratio of hydrogen sulfide and cos is respectively 100% and 90%, and the sulfur dioxide production rate is 95%, and the sulphur production rate is 5%.
By the catalyst that above-mentioned identical condition evaluating comparative example 1～2 prepares, the result is as follows.
Comparative example 1: the conversion ratio of hydrogen sulfide and cos is respectively 96% and 75%, and the sulfur dioxide production rate is 88%, and the sulphur production rate is 12%.
Comparative example 2: the conversion ratio of hydrogen sulfide and cos is respectively 99% and 70%, and the sulfur dioxide production rate is 85%, and the sulphur production rate is 15%.
From the foregoing description data and comparative example data as can be seen, catalyst of the present invention has higher hydrogen sulfide and cos conversion rate, and higher sulfur dioxide production rate.
Embodiment 5
On small-sized catalytic burning experimental rig, to embodiment 2 catalyst capable evaluation, feeding gas consists of hydrogen sulfide 0.24% (v/v), cos 0.06% (v/v), steam 3.0% (v/v), oxygen 0.90% (v/v), all the other are high pure nitrogen, 350 ℃ of reaction temperatures, air speed 6000h
-1, the conversion ratio of hydrogen sulfide and cos is respectively 100% and 92%, and the sulfur dioxide production rate is 97%, and the sulphur production rate is 3%.
Embodiment 6
On small-sized catalytic burning experimental rig, to embodiment 3 catalyst capable evaluation, feeding gas consists of hydrogen sulfide 0.21% (v/v), cos 0.07% (v/v), steam 3.0% (v/v), oxygen 0.84% (v/v), all the other are high pure nitrogen, 320 ℃ of reaction temperatures, air speed 6000h
-1, the conversion ratio of hydrogen sulfide and cos is respectively 100% and 90%, and the sulfur dioxide production rate is 90%, and the sulphur production rate is 10%.350 ℃ of reaction temperatures, other condition is the same, and the conversion ratio of hydrogen sulfide and cos is respectively 100% and 93%, and the sulfur dioxide production rate is 98%, and the sulphur production rate is 2%.
From the data of embodiment 5 and embodiment 6 as can be seen, directly make cellular catalytic incineration catalyst by the active component that comprises titanium dioxide and have more outstanding serviceability.
Claims (8)
1. cellular sulfurous gas catalytic incineration catalyst, it is characterized in that: catalytic incineration catalyst for sulfur-containing compound exhaust air is cellular, active component is made up of the oxide of vanadium, the oxide and the titanyl compound of iron, the oxide content 1.0%～12% of the oxide content 1.0%～15% of vanadium, iron, titanium dioxide 73%～98% or 1%～8% in the catalyst by weight.
2. according to the described catalyst of claim 1, it is characterized in that: the specific area of catalyst is 300～2100m
2/ m
3, the pitch of holes of cellular catalytic incineration catalyst is 1.45～7.0mm, and the wall thickness of cellular catalytic incineration catalyst is 0.25～1.0mm, and the endoporus length of side of cellular catalytic incineration catalyst is 1.0～6.0mm.
3. according to the described catalyst of claim 1, it is characterized in that: comprise the honeycomb support that inert material is made in the cellular catalytic incineration catalyst, the content of active component titanium dioxide is 1%～8%.
4. according to the described catalyst of claim 1, it is characterized in that: directly make cellular catalytic incineration catalyst by the active component that comprises titanium dioxide, the active component content of titanium dioxide is 73%～98%.
5. the application of the arbitrary catalyst of claim 1 to 4 in containing hydrogen sulfide, carbon disulfide or the processing of cos burned waste gas, the operating temperature of catalyst is 200～400 ℃, air speed is 1500～30000h
-1, crossing oxygen quotient is 1.0～5.0.
6. the described Preparation of catalysts method of claim 1 is characterized in that: prepare coating of titanium dioxide on honeycomb inert material carrier, adopt infusion process load active component V
2O
5And Fe
2O
3
7. described Preparation of catalysts method of claim 1, it is characterized in that: with titania powder, methylcellulose powder and ammonium metavanadate mixed grinding, add iron nitrate solution, stir and be kneaded into the suitable lotion of hardness, this lotion is put into the honeycomb die extrusion modling, dry 1～8h respectively at 40～100 ℃ and 100～150 ℃,, obtain final catalyst at 200～350 ℃ and 400～550 ℃ of difference roasting 2～16h.
8. described Preparation of catalysts method of claim 1, it is characterized in that: with titania powder, vanadium pentoxide powder, ferric oxide powder mixed grinding, adding an amount of polyacrylamide and activated carbon powder fully mixes, adding monoethanolamine and water stirs evenly, mediates, make the suitable lotion of hardness, this lotion is put into the honeycomb die extrusion modling, dry 1～8h respectively at 40～100 ℃ and 100～150 ℃, at 200～350 ℃ and 400～550 ℃ of difference roasting 2～16h, obtain final catalyst.
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| CN1269568C (en) * | 2004-09-28 | 2006-08-16 | 北京联合大学生物化学工程学院 | Composite nano-photo-catalyst used for purifying air |
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| CN110639494A (en) * | 2019-10-31 | 2020-01-03 | 北京北科环境工程有限公司 | Blast furnace gas carbonyl sulfide hydrolytic agent and preparation method thereof |
| CN113813965A (en) * | 2021-09-28 | 2021-12-21 | 洛阳理工学院 | NH3-SCR denitration catalyst and preparation method and application thereof |
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