CN101224423A - Active component block distributed catalyst and preparing method thereof - Google Patents
Active component block distributed catalyst and preparing method thereof Download PDFInfo
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- CN101224423A CN101224423A CNA2008100576788A CN200810057678A CN101224423A CN 101224423 A CN101224423 A CN 101224423A CN A2008100576788 A CNA2008100576788 A CN A2008100576788A CN 200810057678 A CN200810057678 A CN 200810057678A CN 101224423 A CN101224423 A CN 101224423A
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Abstract
The invention provides an active component bock-distributed catalyst, wherein the active component is distributed along the axial direction in a plurality of sections, or/and shows multi-layer distribution with a coating layer along the longitudinal direction. The invention applies a block coating method and can load different active components such as noble metal onto different catalyst beds according to the requirements, thus more fully utilizing the various purification functions of various active components to CO, HC and NOx to form synergistic effect, finally improving the activity and selectivity of the catalyst, improving the utilization of active components and reducing production cost in maximum.
Description
Technical field
The present invention relates to a kind of catalyst, specifically, relate to a kind of active component block distributed catalyst and preparation method thereof.
Background technology
The method of catalytic purification is that engine exhaust is controlled one of effective method, and catalyst is the core of catalysis and purification technology.Catalyst can change into the carbon monoxide CO in the middle of the automobile exhausting, hydrocarbon HC, dissolved organic matter SOF, nitrogen oxide NOx and even solid particulate matter the steam H of nuisanceless or low public hazards by catalytic oxidation and catalytic reduction reaction
2O, nitrogen N
2With carbon dioxide CO
2Deng.The method of catalytic purification also is one of most effectual way of various stationary source emission controls, and catalyst is more extensive in industrial application.
Different active constituent in the catalyst, effect in catalytic reaction and bearing of task are also different.Temperature and corresponding required time that different components reach its effective active also are not quite similar.
For example, when catalyst is used in vehicular emission control field, often adopt noble metal as active constituent.And rhodium Rh is higher to the reducing activity of nitrogen oxide NOx in three kinds of noble metals, and Pd is higher to the oxidation activity of HC, and Pd and Rh at high temperature easily form alloy again and lose activity.Triplicity can be got up, unite use, improve the utilization rate of active component.
At present, adopt the mode of series connection catalyst in the associating use, this mode increases blast pipe length, causes the welding trouble, and heat transmits untimely, influences catalytic effect.
Summary of the invention
The purpose of this invention is to provide a kind of active component block distributed catalyst, can make full use of rare noble metal isoreactivity component, and help heat transfer, the diabatic process of beds simultaneously, with the utilization rate that improves active constituent to greatest extent and reduce manufacturing cost.
Another object of the present invention provides a kind of preparation method of active component block distributed catalyst.
In order to realize the object of the invention, a kind of active component block distributed catalyst of the present invention, activity of such catalysts component segmentation in the axial direction distribute, or/and coating is layer distributed in a longitudinal direction.
That is, catalyst of the present invention in the axial direction, coating, active constituent kind and load capacity are that segmentation distributes: coating and/or active constituent on each section of catalyst bed have nothing in common with each other; Different blocks load different activities component and/or coating.
Specifically, active component block distributed catalyst of the present invention includes but not limited to: 1) active constituent difference on each section of catalyst bed, but coating is the block distributed catalyst of individual layer; 2) coating is that multilayer distributes on each section of catalyst bed, but the identical block distributed catalyst of active constituent; 3) active constituent difference on each section of catalyst bed, and the coating of each section is the block distributed catalyst that multilayer distributes.Can give full play to the effect of different activities component like this, with utilization rate and the reduction manufacturing cost that improves active constituent to greatest extent.
Active constituent of the present invention is the distribution more than 2 sections in the axial direction.Preferably 3 sections distributions.
Described coating is the distribution more than 2 layers in a longitudinal direction.Preferably 3 layers of distribution.
Described segmentation distribution form includes but not limited to: be interrupted distribution, continuous distributed and graded profile.
The main component of described coating is an aluminium oxide, includes but not limited to alumina slurry, cerium zirconium compound oxide slurry.
Described active constituent includes but not limited to platinum (Pt) salt, rhodium (Rh) salt, palladium (Pd) salt etc.
Coating is identical on each section of catalyst bed, and active constituent is not simultaneously, and the preparation method of active component block distributed catalyst of the present invention comprises the steps:
1) activated alumina, cerium zirconium sosoloid and nitric acid are mixed, add water then and carry out ground and mixed, controlling total solid content is 30～60%, makes alumina slurry C0;
2) then carrier is immersed slurry C 0 after, take out, blow most residual slurry, dry and roasting, make semi-finished product G0;
3) again semi-finished product G0 is continued roasting 3～12hrs; Make catalyst semi-finished product (being loaded with coating) G1;
4) getting concentration is that 5～20% proportionings are respectively Pt: Rh=5～10: 1, Pt: Pd=5～10: 2, Pt: Rh=5～10: 1, above-mentioned catalyst semi-finished product G1 one end A 1/3rd be impregnated among the active constituent solution P1 1～5 minute, and take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
5) catalyst semi-finished product G1 other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds was immersed among the active constituent solution P2 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
6) catalyst carrier other end B 1/3rd is immersed among the active constituent solution P3,1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out.
Wherein, the weight proportion of activated alumina, cerium zirconium sosoloid and nitric acid is in the step 1): 20～50: 5～10: 0.3～1.Described water is deionized water.
The time of described ground and mixed is 3～12hrs.
Step 2) carrier described in is metal or ceramic honeycomb carrier, and carrier before use must be through processes such as cleaning, oxidation or dryings.
The time that carrier immerses in the slurry C 0 is 5～30s.
Bake out temperature is 80～120 ℃, and the time is 3～8h; Sintering temperature is 450～650 ℃, and the time is 1～4h.
Compressed air with 1～5MPa purges residual slurry.
The temperature of baking and banking up with earth in the step 3) is 300～600 ℃, and the time is 3～12hrs.
The temperature of baking and banking up with earth step 4-6) is 300～500 ℃.
When the active constituent of each section of catalyst bed is identical, and coating is not simultaneously, and the preparation method of active component block distributed catalyst of the present invention comprises the steps:
1) the different alumina slurry C1 of preparation, C2 and C3, controlling total solid content is 25～60%, and activated alumina and cerium zirconium sosoloid weight proportion are among the C1: 20～50: 5～10, and the weight proportion of aluminium oxide and cerium zirconium sosoloid is among the C2: 5～10: 20～40; Only add aluminium oxide among the C3, do not add cerium zirconium sosoloid.
2) catalyst carrier one end A 1/3rd impregnated in 10～15s in the slurry C 1, takes out, and blows off raffinate, oven dry and roasting;
3) catalyst carrier other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds is immersed 10～15s in the slurry C 2, take out, blow off raffinate, oven dry and roasting;
4) catalyst carrier other end B 1/3rd is immersed 10～15s in the slurry C 3, take out, keep direction constant, blow off raffinate, oven dry and roasting make semi-finished product G1;
5) getting concentration is 5～10% precious metal solution (as: Pt/Rh=5: 10～2), take the equivalent impregnation method, supported active component on G1; Naturally cool to room temperature after then it being baked and banked up with earth, take out.
Wherein, step 2-4) bake out temperature is 80～120 ℃, and the time is 3～8hrs; Sintering temperature is 450～650 ℃, and the time is 1～4hrs.
Sintering temperature is 300～500 ℃ in the step 5), and the time is 1～3hrs.
For the preparation method of all different block distributed catalyst of coating on each section bed and active constituent composition, exactly above-mentioned two kinds of methods are carried out combination, specifically comprise the steps:
1) the different alumina slurry C1 of preparation, C2 and C3, controlling total solid content is 25～60%, and the weight proportion of activated alumina and cerium zirconium sosoloid nitric acid is among the C1: 20～50: 5～10, and the weight proportion of aluminium oxide and cerium zirconium sosoloid is among the C2: 5～10: 20～40; Component among the C3 is an aluminium oxide;
2) catalyst carrier one end A 1/3rd impregnated in 10～15s in the slurry C 1, takes out, and blows off raffinate, oven dry and roasting;
3) catalyst carrier other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds is immersed 10～15s in the slurry C 2, take out, blow off raffinate, oven dry and roasting;
4) catalyst carrier other end B 1/3rd is immersed 10～15s in the slurry C 3, take out, keep direction constant, blow off raffinate, oven dry and roasting make semi-finished product G1;
5) getting concentration is that 5～20% proportionings are respectively Pt: three kinds of nitrate solution P1 of Rh=5～10: 1, Pt: Pd=5～10: 2, Pt: Rh=5～10: 1, P2, P3, above-mentioned catalyst semi-finished product G1 one end A 1/3rd be impregnated among the active constituent solution P1 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
6) catalyst semi-finished product G1 other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds was immersed among the active constituent solution P2 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
7) catalyst carrier other end B 1/3rd is immersed among the active constituent solution P3,1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out.
Salting liquid of the present invention includes but not limited to nitrate solution, acetate solution.
Catalyst of the present invention can be used for gasoline engine, diesel engine and various alternative fuel engine, various hybrid power have active constituent with three-way catalyst TWC, oxidation catalyst OC, catalyst for purification of nitrogen oxides DeNOx and load not type various forms of particle trappers; Various types of industrial catalysts, stationary source control catalyst etc.
The outstanding feature of the catalyst of the present invention's preparation is: catalyst activity component segmentation on beds distributes, and brings into play different effects, thereby improves the utilization rate of active constituent greatly.
The present invention adopts the block painting method, Rh can be loaded on the front end bed place of catalyst, and Pd is loaded on bed place, catalyst rear end.Utilize the activity of Rh mainly NOx to be carried out catalytic reduction, and mainly HC is carried out catalytic oxidation, thereby can utilize the effect of various active constituents more fully, form synergy, finally improve activity of such catalysts and selectivity etc. in the bed rear end at the bed front end.
By the block paint-on technique, can be in the coating of beds front end absorption-storage medium and corresponding active constituents such as HC, NOx in the load, and in load on the bed of catalyst rear end the corresponding active constituent that can carry out effective catalytic purification to HC or NOx.(as engine cold starting) can utilize the absorption-storage medium of beds front end that HC and NOx are stored so at low temperatures, and after waiting beds to raise, discharge again, just in time on the beds of rear end, carry out corresponding catalytic reaction, reach the effect of purifying exhaust air.
Catalyst by method for preparing can make full use of rare noble metal isoreactivity component, and helps heat transfer, the diabatic process of beds simultaneously, has much practical value.
The specific embodiment
Following examples are used to illustrate the present invention, but are not used for limiting the scope of the invention.
Embodiment 1
The present embodiment active component block distributed catalyst is made by following step:
(1) takes by weighing activated alumina 40kg, cerium zirconium sosoloid 7kg, nitric acid 1kg and deionized water 52kg, put into ball grinder ball milling 8h, make alumina slurry.
(2) will clean, the metal beehive carrier after the oxidation is dipped in 10s in the above-mentioned slurry, takes out the back and blows most residual slurry with 4MPa compressed air, dries 3h for 120 ℃, 500 ℃ of roasting 2h make semi-finished product G0.
(3) semi-finished product G0 is put into net belt type continuous drying calcining kiln, heating 8hrs, the highest sintering temperature is controlled at 500 ℃, makes catalyst semi-finished product (being loaded with coating) G1.
(4) getting concentration is 10% P1 (Pt: Rh=10: 1) solution, 10% P2 (Pt: Pd=10: 2) solution and 10% P3 (Pt: Rh=5: 1) solution, above-mentioned catalyst semi-finished product one end A about 1/3rd is dipped in 5min in the P1 solution, take out, keep direction constant, vertically blow off raffinate with compressed air from other end B, 500 ℃ of roasting 2h naturally cool to room temperature in the calcining kiln, take out.
(5) catalyst carrier other end B 1/3rd is immersed in the deionized water, 10 minutes, take out, keep direction constant, vertically blow off raffinate with compressed air from other end A.Keep direction constant, carrier 2/3rds was immersed in the P2 solution 5 minutes, take out, keep direction constant, vertically blow off raffinate with compressed air from other end A.500 ℃ of roasting 2h naturally cool to room temperature in the calcining kiln, take out.
(6) B of catalyst end 1/3rd is immersed in the P3 solution 5 minutes, take out, keep direction constant, vertically blow off raffinate from other end A with compressed air, 500 ℃ of roasting 2h naturally cool to room temperature in the calcining kiln, take out.Can make the identical and active component of coating different the block type catalyst.
Embodiment 2
Basic process is with embodiment 1, and different is:
(1) alumina slurry is: activated alumina 50kg, cerium zirconium sosoloid 5kg, nitric acid 0.5kg and deionized water 44.5kg, ball milling 3h.
(2) slurry soaks 30s in ceramic honeycomb carrier, and take out the back and blow most residual slurry with 5MPa compressed air, 100 ℃ of oven dry 5h, 650 ℃ of roasting 1h make semi-finished product G0.
(3) again in net belt type continuous drying calcining kiln, heating 12hrs, the highest sintering temperature is controlled at 300 ℃, makes catalyst semi-finished product (being loaded with coating) G1.
(4) getting concentration is that (Pt: Rh=8: 1) (Pt: Pd=5: 2) (Pt: Rh=10: 1) solution, catalyst semi-finished product one end A 1/3rd is dipped in 3min in the P1 solution, 300 ℃ of roasting 3h for solution and 10% P3 for solution, 10% P2 for 20% P1.
(5) catalyst carrier other end B 1/3rd is immersed in the deionized waters, 15 minutes, take out, then carrier 2/3rds was immersed in the P2 solution 1 minute, take out, again at 300 ℃ of roasting 3h, naturally cool to room temperature afterwards, take out.
(6) B of catalyst end 1/3rd is immersed in the P3 solution 1 minute,, naturally cool to room temperature, take out at 400 ℃ of roasting 3h.Can make the identical and active component of coating different the block type catalyst.
Embodiment 3
Basic process is with embodiment 1, and different is:
(1) alumina slurry is: activated alumina 20kg, cerium zirconium sosoloid 10kg, nitric acid 0.3kg and deionized water 69.7kg, ball milling 12h.
(2) slurry soaks 5s in ceramic honeycomb carrier, and take out the back and blow most residual slurry with 1MPa compressed air, 80 ℃ of oven dry 8h, 450 ℃ of roasting 4h make semi-finished product G0.
(3) again in net belt type continuous drying calcining kiln, heating 3hrs, the highest sintering temperature is controlled at 600 ℃, makes catalyst semi-finished product (being loaded with coating) G1.
(4) getting concentration is that (Pt: Rh=10: 1) (Pt: Pd=8: 2) (Pt: Rh=8: 1) solution is dipped in 3min in the P1 solution, 400 ℃ of roasting 1h with above-mentioned catalyst semi-finished product one end A 1/3rd for solution and 10% P3 for solution, 10% P2 for 5% P1.
(5) catalyst carrier other end B 1/3rd is immersed in the deionized waters, 12 minutes, take out, afterwards carrier 2/3rds was immersed in the P2 solution 3 minutes, at 400 ℃ of roasting 1h.
(6) B of catalyst end 1/3rd is immersed in the P3 solution 3 minutes,, naturally cool to room temperature, take out at 300 ℃ of following roasting 2h.Can make the identical and active component of coating different the block type catalyst.
Embodiment 4
The present embodiment active component block distributed catalyst is made by following step:
(1) takes by weighing activated alumina 40kg, cerium zirconium sosoloid 10kg, nitric acid 1kg and deionized water 49kg, put into ball grinder ball milling 8h, make alumina slurry C1.
(2) take by weighing activated alumina 10kg, cerium zirconium sosoloid 40kg, nitric acid 1kg and deionized water 49kg, put into ball grinder ball milling 8h, make alumina slurry C2.
(3) take by weighing activated alumina 50kg, nitric acid 1kg and deionized water 49kg, put into ball grinder ball milling 8h, make alumina slurry C3.
(4) preliminary treatment is good metal beehive carrier one end A about 1/3rd is dipped in 15s in the C1 slurry, takes out, and keeps direction constant, vertically blows off raffinate from other end B with compressed air, 120 ℃ of oven dry 3h, 500 ℃ of roasting 2h.
(5) catalyst carrier other end B 1/3rd is immersed in the deionized water, 10 minutes, take out, keep direction constant, vertically blow off raffinate with compressed air from other end A.Keep direction constant, carrier 2/3rds is immersed 15s in the C2 slurry, take out, keep direction constant, vertically blow off raffinate with compressed air from other end A.120 ℃ of oven dry 3h, 500 ℃ of roasting 2h.
(6) catalyst carrier other end B 1/3rd is immersed 15s in the slurry C 3, take out, keep direction constant, vertically blow off raffinate with compressed air, 120 ℃ of oven dry 3h, 500 ℃ of roasting 2h from other end A.Make the catalyst semi-finished product.
(7) get 10% precious metal solution (Pt: Rh=5: 10), noble metal is carried on the above-mentioned catalyst coat,, can makes identical and the block type catalyst that coating is different of active component in 500 ℃ of roasting 2h by the equivalent impregnation method.
Embodiment 5
Basic process is with embodiment 4, and different is:
(1) takes by weighing activated alumina 50kg, cerium zirconium sosoloid 5kg, nitric acid 0.5kg and deionized water 44.5kg, put into ball grinder ball milling 12h, make alumina slurry C1.
(2) take by weighing activated alumina 5kg, cerium zirconium sosoloid 30kg, nitric acid 0.5kg and deionized water 49kg, put into ball grinder ball milling 12h, make alumina slurry C2.
(3) take by weighing activated alumina 60kg, nitric acid 0.5kg and deionized water 39.5kg, put into ball grinder ball milling 12h, make alumina slurry C3.
(4) preliminary treatment is good ceramic honeycomb carrier one end A 1/3rd is dipped in 10s in the C1 slurry, and bake out temperature is 100 ℃ and carries out 5h that sintering temperature is 650 ℃ and carries out 4h.
(5) catalyst carrier other end B 1/3rd soaked deionized water 15 minutes, and carrier 2/3rds immerses 10s in the C2 slurry, 100 ℃ of oven dry 5h, 650 ℃ of roasting 4h.
(6) catalyst carrier other end B 1/3rd is immersed 10s in the slurry C 3,80 ℃ of oven dry 8h, 650 ℃ of roasting 1h.
(7) get 8% precious metal solution (Pt: Rh=5: 2), noble metal is carried on the above-mentioned catalyst coat,, can makes identical and the block type catalyst that coating is different of active component in 300 ℃ of roasting 3h by the equivalent impregnation method.
Embodiment 6
Basic process is with embodiment 4, and different is:
(1) takes by weighing activated alumina 20kg, cerium zirconium sosoloid 8kg, nitric acid 0.3kg and deionized water 71.7kg, put into ball grinder ball milling 3h, make alumina slurry C1.
(2) take by weighing activated alumina 8kg, cerium zirconium sosoloid 20kg, nitric acid 0.3kg and deionized water 71.7kg, put into ball grinder ball milling 3h, make alumina slurry C2.
(3) take by weighing activated alumina 25kg, nitric acid 0.3kg and deionized water 74.7kg, put into ball grinder ball milling 3h, make alumina slurry C3.
(4) metal beehive carrier one end A about 1/3rd is dipped in 12s in the C1 slurry, and bake out temperature is 80 ℃, carries out 8h, and sintering temperature is 450 ℃ and carries out 2h.
(5) catalyst carrier other end B 1/3rd was soaked deionized water 12 minutes, carrier 2/3rds immerses 12s in the C2 slurry, takes out 80 ℃ of oven dry 8h, 450 ℃ of roasting 1h.
(6) catalyst carrier other end B 1/3rd is immersed 12s in the slurry C 3,100 ℃ of oven dry 5h, 450 ℃ of roasting 4h.Make the catalyst semi-finished product.
(7) get 5% precious metal solution (Pt: Rh=5: 8), noble metal is carried on the above-mentioned catalyst coat,, can makes identical and the block type catalyst that coating is different of active component in 450 ℃ of roasting 1h by the equivalent impregnation method.
Embodiment 7
The coating on each section bed of present embodiment is made by following steps with all different block distributed catalyst of active constituent composition:
1) preparation process is made the different catalyst semi-finished product of each section coating with the step 1-6 of embodiment 4.
2) preparation process is made the coating block distributed catalyst all different with the active constituent composition on each section bed with the step 4-6 of embodiment 2.
Embodiment 8
The coating on each section bed of present embodiment is made by following steps with all different block distributed catalyst of active constituent composition:
1) preparation process is made the different catalyst semi-finished product of each section coating with the step 1-6 of embodiment 5.
2) preparation process is made the coating block distributed catalyst all different with the active constituent composition on each section bed with the step 4-6 of embodiment 1.
Embodiment 9
The coating on each section bed of present embodiment is made by following steps with all different block distributed catalyst of active constituent composition:
1) preparation process is made the different catalyst semi-finished product of each section coating with the step 1-6 of embodiment 6.
2) preparation process is made the coating block distributed catalyst all different with the active constituent composition on each section bed with the step 4-6 of embodiment 3.
Though above the present invention is described in detail with a general description of the specific embodiments, on basis of the present invention, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements all belong to the scope of protection of present invention without departing from theon the basis of the spirit of the present invention.
Claims (9)
1. an active component block distributed catalyst is characterized in that, activity of such catalysts component multistage in the axial direction distributes, and distributes or/and coating is multilayer in a longitudinal direction.
2. active component block distributed catalyst according to claim 1, it is characterized in that, described active component block distributed catalyst includes but not limited to: 1) active constituent difference on each section of catalyst bed, but coating is the block distributed catalyst of individual layer; 2) coating is that multilayer distributes on each section of catalyst bed, but the identical block distributed catalyst of active constituent; 3) active constituent difference on each section of catalyst bed, and the coating of each section is the block distributed catalyst that multilayer distributes.
3. active component block distributed catalyst according to claim 1 and 2 is characterized in that, described active constituent is three sections distributions in the axial direction, and described coating is three layers of distribution in a longitudinal direction.
4. according to any described active component block distributed catalyst of claim 1-3, it is characterized in that described active constituent includes but not limited to platinum salt, rhodium salt, palladium salt.
5. prepare the method for the described active component block distributed catalyst of claim 4, it is characterized in that, comprise the steps:
1) activated alumina, cerium zirconium sosoloid and nitric acid are mixed, add water then and carry out ground and mixed, controlling total solid content is 30～60%, makes alumina slurry C0;
2) then carrier is immersed slurry C 0 after, take out, blow most residual slurry, dry and roasting, make semi-finished product G0;
3) again semi-finished product G0 is continued roasting 3～12hrs; Make catalyst semi-finished product G1;
4) getting concentration is 5～20%, proportioning is respectively Pt: Rh=5～10: 1, Pt: Pd=5～10: 2, Pt: Rh=5～10: 1 three kinds of nitrate solution P1, P2, P3, above-mentioned catalyst semi-finished product G1 one end A 1/3rd be impregnated among the active constituent solution P1 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
5) catalyst semi-finished product G1 other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds was immersed among the active constituent solution P2 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
6) catalyst carrier other end B 1/3rd is immersed among the active constituent solution P3,1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out.
6. according to the preparation method of the described active component block distributed catalyst of claim 5, it is characterized in that the weight proportion of activated alumina, cerium zirconium sosoloid and nitric acid is in the step 1): 20～50: 5～10: 0.3～1.
7. prepare the method for the described active component block distributed catalyst of claim 4, it is characterized in that, comprise the steps:
1) the different alumina slurry C1 of preparation, C2 and C3, controlling total solid content is 25～60%, aluminium oxide and cerium zirconium sosoloid weight proportion are among the C1: 20～50: 5～10, the weight proportion of aluminium oxide and cerium zirconium sosoloid is among the C2: 5～10: 20～40; Only add aluminium oxide among the C3;
2) catalyst carrier one end A 1/3rd impregnated in 10～15s in the slurry C 1, takes out, and blows off raffinate, oven dry and roasting;
3) catalyst carrier other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds is immersed 10～15s in the slurry C 2, take out, blow off raffinate, oven dry and roasting;
4) catalyst carrier other end B 1/3rd is immersed 10～15s in the slurry C 3, take out, keep direction constant, blow off raffinate, oven dry and roasting make semi-finished product G1;
5) getting concentration is 5～10% precious metal solution, takes the equivalent impregnation method, supported active component on G1; Naturally cool to room temperature after then it being baked and banked up with earth, take out.
8. according to the preparation method of the described active component block distributed catalyst of claim 7, it is characterized in that step 2-4) bake out temperature is 80～120 ℃, the time is 3～8hrs; Sintering temperature is 450～650 ℃, and the time is 1～4hrs; Sintering temperature is 300～500 ℃ in the step 5), and the time is 1～3hrs.
9. prepare the method for the described active component block distributed catalyst of claim 4, it is characterized in that, comprise the steps:
1) the different alumina slurry C1 of preparation, C2 and C3, controlling total solid content is 25～60%, the weight proportion of aluminium oxide and cerium zirconium sosoloid is among the C1: 20～50: 5～10, the weight proportion of aluminium oxide and cerium zirconium sosoloid is among the C2: 5～10: 20～40; Component among the C3 is an aluminium oxide;
2) catalyst carrier one end A 1/3rd impregnated in 10～15s in the slurry C 1, takes out, and blows off raffinate, oven dry and roasting;
3) catalyst carrier other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds is immersed 10～15s in the slurry C 2, take out, blow off raffinate, oven dry and roasting;
4) catalyst carrier other end B 1/3rd is immersed 10～15s in the slurry C 3, take out, keep direction constant, blow off raffinate, oven dry and roasting make semi-finished product G1;
5) getting concentration is that 5～20% proportionings are respectively Pt: three kinds of nitrate solution P1 of Rh=5～10: 1, Pt: Pd=5～10: 2, Pt: Rh=5～10: 1, P2, P3, above-mentioned catalyst semi-finished product G1 one end A 1/3rd be impregnated among the active constituent solution P1 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
6) catalyst semi-finished product G1 other end B 1/3rd is immersed in the deionized water, 10～15 minutes, take out, blow off raffinate; Keep direction constant, carrier 2/3rds was immersed among the active constituent solution P2 1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out;
7) catalyst carrier other end B 1/3rd is immersed among the active constituent solution P3,1～5 minute, take out, blow off raffinate; Roasting naturally cools to room temperature, takes out.
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| CN2008100576788A CN101224423B (en) | 2008-02-04 | 2008-02-04 | Active component block distributed catalyst and preparing method thereof |
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| CN101224423A true CN101224423A (en) | 2008-07-23 |
| CN101224423B CN101224423B (en) | 2010-12-22 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103157520A (en) * | 2013-03-04 | 2013-06-19 | 上海云汇环保科技有限公司 | Radial gradient load three-way catalyst and preparation method |
| CN104399459A (en) * | 2014-10-31 | 2015-03-11 | 金华欧仑催化科技有限公司 | Catalyst for rear-stage three-way catalytic converter |
| CN106076331A (en) * | 2016-06-22 | 2016-11-09 | 无锡威孚环保催化剂有限公司 | A kind of preparation method of three-way catalyst |
| WO2019109999A1 (en) * | 2017-12-08 | 2019-06-13 | 庄信万丰(上海)化工有限公司 | Novel multi-region twc for treatment of exhaust gas from gasoline engine |
-
2008
- 2008-02-04 CN CN2008100576788A patent/CN101224423B/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103157520A (en) * | 2013-03-04 | 2013-06-19 | 上海云汇环保科技有限公司 | Radial gradient load three-way catalyst and preparation method |
| CN104399459A (en) * | 2014-10-31 | 2015-03-11 | 金华欧仑催化科技有限公司 | Catalyst for rear-stage three-way catalytic converter |
| CN106076331A (en) * | 2016-06-22 | 2016-11-09 | 无锡威孚环保催化剂有限公司 | A kind of preparation method of three-way catalyst |
| CN106076331B (en) * | 2016-06-22 | 2018-06-19 | 无锡威孚环保催化剂有限公司 | A kind of preparation method of three-way catalyst |
| WO2019109999A1 (en) * | 2017-12-08 | 2019-06-13 | 庄信万丰(上海)化工有限公司 | Novel multi-region twc for treatment of exhaust gas from gasoline engine |
| US11439987B2 (en) | 2017-12-08 | 2022-09-13 | Johonson Matthey (Shanghai) Chemicals Co., Ltd | Multi-region TWC for treatment of exhaust gas from gasoline engine |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101224423B (en) | 2010-12-22 |
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