CN105149013A - Catalyst production technology - Google Patents
Catalyst production technology Download PDFInfo
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- CN105149013A CN105149013A CN201410256141.XA CN201410256141A CN105149013A CN 105149013 A CN105149013 A CN 105149013A CN 201410256141 A CN201410256141 A CN 201410256141A CN 105149013 A CN105149013 A CN 105149013A
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Abstract
The invention discloses a catalyst production technology comprising the following steps: 1, driving a rotary drum body (1) in which is equipped with a carrier to rotate in order to flip the carrier, and spraying a dipping solution to the carrier with a sprayer; 2, discharging evaporated gas in the dipping process to the outside of the rotary drum body (1) through an exhaust port disposed on the rotary drum body (1). The catalyst production technology can save the dipping solution and has stable quality of the catalyst product.
Description
Technical field
The present invention relates to field of catalyst preparation, particularly, relate to a kind of Catalyst Production technique.
Background technology
In catalyst preparing and production process, there is multiple production method, as infusion process, roll coating process, the precipitation method, mixing method, ion-exchange, gas phase synthesis method etc.Wherein infusion process is a kind of comparatively conventional method.
In infusion process, it will activity component impregnation to carrier be wherein most important step.Traditional impregnation of catalyst carriers equipment mainly contains impregnating autoclave, dipping hanging basket, dipping guipure, dipping cylinder, dipping rotary drum, dipping bowling machine etc.Fluidized bed immersion is applicable to the dipping of porous carrier, but there is finished catalyst yield low (80 ~ 90%), easily caking, the problem such as uneven.
Use dipping rotary drum when flooding in prior art, carrier is placed in rotary drum, and dipping solution is imported in rotary drum to make solution can impregnated carrier.The lead-in mode of solution directly makes liquid flow in rotary drum.Be understandable that in this case, only have that to import carrier hole saturated or import the imbibition requirement that excessive dipping solution could meet carrier, i.e. saturated dipping even supersaturation dipping.So not only can cause the waste of a large amount of solution, also cause the requirement that cannot meet production active component heterogeneous catalyst.In addition, in impregnation technology, especially in the impregnation technology preparing heterogeneous catalyst, need constantly to remove the boil-off gas (being generally water) produced because of heating, otherwise can be unfavorable to dipping process.But dipping rotary drum of the prior art is closed device, usually need to adopt the method vacuumized to remove boil-off gas.And vacuumize the dipping solution taking a lot of atomizations away, not only cause the loss of a large amount of dipping solutions, the metering in catalyst preparation process also can be caused inaccurate difficult with control.Further, the closed state flooding rotary drum also can cause difficulty to the importing of liquid.
Therefore, production technology of the prior art haves much room for improvement.
Summary of the invention
The object of this invention is to provide a kind of Catalyst Production technique, in order to reduce the loss of dipping solution, and realize the dipping and the active component distribution in the catalyst that control active component flexibly, thus make the quality of catalyst prod more stable.
To achieve these goals, the invention provides a kind of Catalyst Production technique, comprise the following steps: step 1, drive the inner rotary drum body that carrier is housed to carry out rotating to stir carrier, and by sprayer, dipping solution is sprayed to carrier; Step 2, is disposed to the outside of rotary drum body by the boil-off gas in dipping process by the exhaust outlet offered on rotary drum body.
Preferably, in step 1, rotated by the drive shaft rotary drum body be connected on rotary drum body, wherein, the velocity of rotation of rotary drum body is 0.5 turn/min ~ 100 turn/min, be preferably 5 turns/min ~ 60 turn/min, more preferably 10 turns/min ~ 50 turn/min.
Preferably, rotary drum body is taper or the biconial sharing same cone bottom surface, and driving shaft is connected to position bottom taper or diconical cone, wherein, floss hole in step 2 is opened in the connecting portion of driving shaft and rotary drum body, and the holding temperature of rotary drum body is 40 DEG C to 90 DEG C.
Preferably, the sprayer in step 1 comprises multiple shower nozzle, the described diconical position near at least one vertex of a cone that shower nozzle is arranged on the inside of rotary drum body, wherein, shower nozzle towards regulating, and shower nozzle is adjustable to the distance of diconical inwall.
Preferably, the diameter of the drop that shower nozzle sprays is 1 μm to 1000 μm, is preferably 10 μm to 500 μm, more preferably 20 μm to 200 μm.
Preferably, the fluid pressure of shower nozzle is 0.05MPa-10.0MPa, is preferably 0.1MPa-5.0MPa, more preferably 0.2MPa-2.0MPa, the mist flow of shower nozzle is 0.1L/min-10.0L/min, is preferably 0.2L/min-8.0L/min, more preferably 0.5L/min-5.0L/min.
Preferably, also comprise the step be placed to by carrier in rotary drum body before step 1, wherein, the inlet amount of carrier controls to criticize for 20kg/ criticizes-1000kg/, and preferably 50kg/ criticizes-800kg/ and criticizes, and more preferably 100kg/ criticizes-300kg/ and criticizes.
Preferably, also comprise after step 2 and the carrier through dipping is carried out quick-drying step, wherein, to drop on the dry zone for dried material via the guiding of distributing device through the carrier of dipping.
Preferably, the carrier through flooding forms the bed of material of 0.2cm to 5.0cm on dry zone, is preferably the bed of material of 0.5cm to 3.0cm, the more preferably bed of material of 0.5cm to 2.0cm.
Preferably, the width of described dry zone (101) is 0.5m to 3m, is preferably 0.5m-2.0m; The baking temperature of described dry zone (101) is 50 DEG C to 600 DEG C, is preferably 100 DEG C to 500 DEG C, more preferably 120 DEG C to 400 DEG C.
Preferably, the dip time of carrier in rotary drum body is 1min to 120min, is preferably 5min to 60min, more preferably 10min to 30min.
Pass through technique scheme, in Catalyst Production technique of the present invention, first rotary drum body and spray structure are cooperatively interacted, thus dipping solution can be sprayed onto in the inner space of rotary drum body quickly and evenly with the form of drop, and then dipping solution is made to be impregnated into carrier quickly and evenly.By this, saturated dipping or supersaturation dipping can be carried out, thus greatly reduce the waste of dipping solution, and can pickling efficiency be improved; Secondly floss hole for discharging boil-off gas is set on rotary drum body.By arranging these floss holes, the mode that vacuumizes can be re-used to extract boil-off gas.The loss of dipping solution can be greatly reduced by this, investment and the maintenance cost of vaccum-pumping equipment can also be saved.The dipping and the active component distribution in the catalyst that control active component flexibly can be realized thus, thus make the quality of catalyst prod more stable.
Other features and advantages of the present invention are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the structural representation of the Catalyst Production equipment for implementing Catalyst Production technique of the present invention.
Description of reference numerals
1 rotary drum body 11 first vertex of a cone 12 second vertex of a cone
2 driving shaft 3 pedestal 4 links
5 nozzle 6 motor 7 reductors
8 carrier feed unit 9 fluid delivery unit
101 dry zone 102 distributing devices
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The invention provides a kind of Catalyst Production technique.With reference to figure 1, display be the structural representation of Catalyst Production equipment for implementing Catalyst Production technique of the present invention.As shown in fig. 1, this Catalyst Production equipment comprises dipping drum device and rapid drying device.Wherein, dipping drum device is for realizing by the activity component impregnation of dipping solution to carrier, and the carrier through dipping is carried out rapid draing for realizing by rapid drying device.
In more detail, in order to realize the activity component impregnation of dipping solution on carrier, according to embodiments of the invention, dipping drum device comprise dipping rotary drum for implementing dipping process, for add in rotary drum body 1 carrier carrier feed unit 8 and for carrying the fluid delivery unit 9 of dipping solution in rotary drum body 1.Wherein, flood rotary drum and comprise rotary drum body 1.In dipping process, catalyst carrier is placed in rotary drum body 1.
In Catalyst Production technique of the present invention, first comprise and utilize carrier feed unit 8 carrier to be placed to step in described rotary drum body 1.Specifically, carrier feed unit 8 comprises the hopper for holding carrier and the control valve for controlling charging rate.According to embodiments of the invention, the outlet of control valve is the output of carrier feed unit 8, and this output removably can be connected to the vertex of a cone position of rotary drum body 1.Further, according to embodiments of the invention, the inlet amount of carrier is determined according to the amount of solution, the speed of spraying, the rotating speed of rotary drum body 1 and default dip time.By control valve, the inlet amount of carrier is controlled to criticize for 20kg/ criticizes-1000kg/, be preferably 50kg/ and criticize-800kg/ and criticize, more preferably 100kg/ criticizes-300kg/ and criticizes.Further, the inlet amount of carrier can regulate according to the size of equipment, to reach the object of effectively producing smoothly
Next, according to production technology of the present invention, need to implement to drive the inner rotary drum body 1 that carrier is housed to carry out rotating to stir the step of carrier.For this reason, as shown in fig. 1, flood rotary drum and also comprise motor 6 for driving rotary drum body 1 to rotate and reductor 7.Rely on gear, hinge and/or belt transmission between motor 6 and reductor 7, and the output of reductor 7 is connected with the driving shaft 2 for exporting rotating torque.Dipping rotary drum also comprises the pedestal 3 for supporting rotary drum body 1, and driving shaft 2 can be connected to pedestal 3 rotationally by the structure of such as bearing.When motor 6 and reductor 7 unlatching make driving shaft 2 rotate, rotating torque can be passed to rotary drum body 1 by driving shaft 2, thus the carrier in rotary drum body 1 is stirred, to reach good dipping effect.According to embodiments of the invention, the velocity of rotation of rotary drum body 1 can select 0.5 turn/min ~ 100 turn/min, is preferably 5 turns/min ~ 60 turn/min, more preferably 10 turns/min ~ 50 turn/min.At these speeds, carrier stirs evenly, good fluidity.Many experiments data show, during lower than this rotating speed, carrier to stir effect bad, during higher than this rotating speed, catalyst particle attrition, efflorescence can be caused.
According to embodiments of the invention, rotary drum body 1 can be set to the biconial of the shared same cone bottom surface shown in taper or Fig. 1.The driving shaft 2 rotated for driving rotary drum body 1 can be connected to position bottom taper or diconical cone.Like this, when driving shaft 2 drives rotary drum body 1 to rotate, due to the effect of centrifugal force, the carrier carried in rotary drum body 1 can move towards the cone top part displacement away from driving shaft 1.
Next, according to production technology of the present invention, while stirring carrier, also need the step implementing by sprayer, dipping solution to be sprayed to carrier.For this reason, according to embodiments of the invention, the solution that dipping rotary drum is also provided with for adding dipping solution in rotary drum body 1 imports unit.In Catalyst Production technique, realize activity component impregnation on carrier by adding dipping solution in rotary drum body 1.According to embodiments of the invention, solution importing unit comprises the sprayer on the inwall being connected to rotary drum body 1.Rotated and the cooperatively interacting of spray structure by rotary drum body 1, dipping solution can be sprayed onto in the inner space of rotary drum body 1 quickly and evenly with the form of drop, thus make dipping solution be impregnated into carrier quickly and evenly.By this, saturated dipping or supersaturation dipping can be carried out on the one hand, thus the waste of dipping solution can be greatly reduced; Pickling efficiency can also be improved on the other hand.
In more detail, according to embodiments of the invention, sprayer comprises multiple shower nozzle 5 that can regulate spray angle.These shower nozzles 5 can carry out horizontal and vertical ordered arrangement according to the distribution of carrier in rotary drum body 1, thus ensure that the liquid of ejection can fully receive by loaded body.The spray angle of shower nozzle 5 can be controlled by automaton.According to embodiments of the invention, the selection of shower nozzle can need to carry out according to the preparation of catalyst, such as but not limited to, can selection pressure shower nozzle, two phase flow shower nozzle, ultrasonic nozzle and/or static nozzle.In order to reduce costs, can pressure nozzle that preferably use cost is lower.According to embodiments of the invention, the diameter of the drop that shower nozzle sprays is chosen as 1 μm to 1000 μm, can be preferably 10 μm to 500 μm, can more preferably 20 μm to 200 μm.Such atomized drop, can be of a size of the carrier of 1mm ~ 5mm by multiple-contact, make substrate monolith appearance uniform, and in each carrier, active component present non-uniform Distribution.In addition, according to embodiments of the invention, when measuring the size of drop, drop can be sprayed at and scribble on the glass plate of wax material, then amplify 100 times under the microscope, measure the diameter of drop.
Further, in Catalyst Production technique of the present invention, also comprise the step utilizing fluid delivery unit 9 mentioned above to provide dipping solution to shower nozzle 5.For this reason, the output of fluid delivery unit 9 is connected to the input that solution imports unit.Wherein, fluid delivery unit 9 comprises solution storage tank, constant pressure pump and control valve, and control valve may be used for the fluid pressure and the mist flow that control shower nozzle 5.In Catalyst Production technique of the present invention, preferably the fluid pressure of shower nozzle 5 may be controlled to 0.05MPa-10.0MPa, is preferably 0.1MPa-5.0MPa, more preferably 0.2MPa-2.0MPa.According to the difference of shower nozzle, corresponding atomization condition can be selected, reach good atomizing effect.Droplet size is relevant with the size of pressure, and the requirement of granule carrier to atomizing effect is higher.Mist flow may be controlled to 0.1L/min-10.0L/min, is preferably 0.2L/min-8.0L/min, more preferably 0.5L/min-5.0L/min.According to the number that output and carrier add, the flow of matching liquid.When meeting above-mentioned condition, according to a preferred embodiment of the invention, the diameter of the drop that shower nozzle sprays is chosen as 1 μm to 1000 μm, can be preferably 10 μm to 500 μm, can more preferably 20 μm to 200 μm.Such atomized drop, can be of a size of the carrier of 1mm ~ 5mm by multiple-contact, make substrate monolith appearance uniform, and in each carrier, active component present non-uniform Distribution.In addition, according to embodiments of the invention, when measuring the size of drop, drop can be sprayed at and scribble on the glass plate of wax material, then amplify 100 times under the microscope, measure the diameter of drop.
According to above-mentioned, because the rotating speed of rotary drum body 1, the system pressure of sprayer and flow can be controlled by automatics, therefore, production technology of the present invention can realize the dipping and the active component distribution in the catalyst that control active component flexibly.Thereby eliminate the shortcoming of traditional Catalyst Production technique, solve the change of impregnating equipment and technique and the upgrading of catalyst prod in catalyst preparation process.Especially, in the process for producing of heterogeneous catalyst, the catalyst prod that quality is more stable can be obtained.
Next, according to production technology of the present invention, dipping rotary drum is provided with intensification unit for heating drum body 1, to ensure intensification in dipping process and insulation.In a preferred embodiment of the invention, the holding temperature of rotary drum body 1 is chosen as 40 DEG C to 90 DEG C.Rotary drum body 1 can produce boil-off gas after being warmed unit heating.Therefore, according to production technology of the present invention, also need the step implementing the outside boil-off gas in dipping process being disposed to rotary drum body 1.For this reason, in Catalyst Production technique of the present invention, rotary drum body 1 arranges the floss hole for discharging these boil-off gas.By arranging these floss holes, the mode that vacuumizes can be re-used to extract boil-off gas.By this, the loss of dipping solution can be greatly reduced on the one hand, investment and the maintenance cost of vaccum-pumping equipment can also be saved on the other hand.More specifically, according to embodiments of the invention, the floss hole for discharging boil-off gas can be opened in the connecting portion of driving shaft 2 and rotary drum body 1.As mentioned above, carrier can move towards cone top part displacement away from driving shaft 1 under the influence of centrifugal force, and that is carrier can move towards the direction away from floss hole, and carrier therefore can be avoided to leak from floss hole.
According to embodiments of the invention, the shape of rotary drum body 1 can be the shape such as cydariform or ellipse roughly.Preferably, the shape of rotary drum body 1 can be set to the biconial shown in Fig. 1.This biconial can be the biconial of shared same cone bottom surface, also can be the biconial not sharing same cone bottom surface.The driving shaft 2 rotated for driving rotary drum body 1 can be connected to the side of rotary drum body 1.That is, position, diconical cone bottom is connected to as illustrated in figure 1.Like this, when driving shaft 2 drives rotary drum body 1 to rotate, due to the effect of centrifugal force, the carrier carried in rotary drum body 1 can move towards the cone top part displacement away from driving shaft 1.According to embodiments of the invention, the floss hole for discharging boil-off gas can be opened in the connecting portion of driving shaft 2 and rotary drum body 1.As mentioned above, carrier can move towards cone top part displacement away from driving shaft 1 under the influence of centrifugal force, and that is carrier can move towards the direction away from floss hole, and carrier therefore can be avoided to leak from floss hole.In addition, according to embodiments of the invention, shower nozzle 5 is arranged on the diconical position near at least one vertex of a cone diconical.That is, shower nozzle 5 can be arranged in one of them taper diconical, and the position of the vertex of a cone of this taper close; Also can be separately positioned in two tapers, and respectively near the position of the vertex of a cone of two tapers.And in the present embodiment, the distance of the inwall of shower nozzle 5 to taper is adjustable.That is, shower nozzle 5 can move along the radial direction of taper.Above, by shower nozzle 5 being arranged on the position at the top near taper, can make the position that shower nozzle 5 can be concentrated closer to carrier; By regulating shower nozzle 5 relative to the spacing of conical inboard wall, the adjustment of the jet length of shower nozzle 5 can be realized, thus ensure that the dipping solution of predetermined amount can be ejected on carrier; By controlling the sprinkling direction of shower nozzle 5, shower nozzle 5 can be controlled better and be sprayed onto effective spray area on carrier.
Further, in Catalyst Production technique of the present invention, the link 4 by umbrella frame shape between driving shaft 2 and the outer wall of rotary drum body 1 can be connected to each other.Wherein, as shown in fig. 1, the top of the gathering of link 4 is connected to driving shaft 2, and one end strutted of link 4 is connected to the outside wall surface of rotary drum body 1.Like this, in the outside wall surface of rotary drum body 1, can enclose by the position be connected with link 4 region forming a similar round.According to embodiments of the invention, can be opened in the region of this similar round for the floss hole discharging boil-off gas.Further, link 4 can be formed by many reinforcement welding, and link 4 can be connected on the internal face of rotary drum body 1 by welding or cold rolling mode.Like this, can drain from the spacing (spacing between each bar umbrella frame of also i.e. umbrella frame shape structure) between reinforcing bar from the boil-off gas of floss hole discharge.
By said structure, the sprinkling of dipping solution can be implemented in drum rotating process, and by boil-off gas Natural excrement in dipping process, thus meet the working condition of catalyst particularly heterogeneous catalyst preferably.In addition, in production technology of the present invention, the dip time of carrier in rotary drum body is 1min to 120min, is preferably 5min to 60min, more preferably 10min to 30min.
Next, according to production technology of the present invention, also need the carrier implemented through dipping to carry out quick-drying step.For this reason, according to embodiments of the invention, rapid drying device is provided with dry zone 101 and distributing device 102.Wherein, distributing device 102 can be arranged on the top of dry zone 101, for the carrier through dipping in rotary drum body 1 is guided to dry zone 101.According to embodiments of the invention, distributing device 102 can be arranged to infundibulate, and the outlet of this funnel can be arranged on directly over dry zone 102.In a preferred embodiment, rotary drum body 1 is biconial, and this diconical first vertex of a cone 11 is removably connected with the output of carrier feed unit 8.Further, when first vertex of a cone 11 is connected with the output of carrier feed unit 8, diconical second vertex of a cone 12 is just to the arrival end of distributing device 102.That is, when discharging discharging, first vertex of a cone 11 (being now relatively in top) can be connected with the outlet of the control valve of carrier feed unit 8, below now second vertex of a cone 12 is relatively in and just to the entrance of distributing device 102.Like this, discharging and discharging can complete in an operation, thus increase work efficiency.Be understandable that, because second vertex of a cone 12 is now in the bottommost of rotary drum body 1, and the inferior pyramidal of rotary drum body 1 is infundibulate, and therefore carrier can draw off easily from second vertex of a cone 12.
According to embodiments of the invention, the width of dry zone 101 is 0.5m to 3m, is preferably 0.5m-2.0m.By the control of width, both can uniform distribution be reached, again can the object of uniform drying.The baking temperature of dry zone 101 is 50 DEG C to 600 DEG C, is preferably 100 DEG C to 500 DEG C, more preferably 120 DEG C to 400 DEG C, thus completes the quick-drying object of catalyst.Many experiments data show, if baking temperature is not suitable for, can cause deliquescence, cause moisture to turn back in catalyst, affect the quality of finished product.In addition, according to embodiments of the invention, on dry zone 101, to be formed the bed of material of 0.2cm to 5.0cm through the carrier of dipping by distributing device 102, be preferably the bed of material of 0.5cm to 3.0cm, then be preferably the bed of material of 0.5cm to 2.0cm.The control of thickness of feed layer, can make catalyst fully dry, avoids causing because the bed of material is too thick moisture adsorbing and destroying the performance of catalyst in the catalyst.In addition, if thickness of feed layer is unreasonable, the moisture inner layer on top layer can be caused to absorb and lose product qualified rate
In addition, in the preferred embodiment of production technology of the present invention, lifting blade can be provided with on the internal face of rotary drum body 1.Thus when rotary drum body 1 rotates, carrier can be kicked up certain height under the carrying in lifting portion.By this, carrier can be realized in rotary drum body 1, carry out more effective stirring, thus promote the contact of carrier and dipping solution, to increase the uniformity of catalyst preparing and overall uniformity.According to embodiments of the invention, lifting blade can distribute in length and breadth thus form grille-like on the inwall of rotary drum body 1.Preferably, grid can be triangle, rectangle or trapezoidal.More preferably, grid is rectangle.Further, according to embodiments of the invention, lifting blade is not more than 300mm relative to the height of projection of the internal face of rotary drum body 1, is preferably not more than 150mm, more preferably 10mm to 100mm.Many experiments data show, and when being less than this height of projection, the carrying capacity of lifting blade is not enough, when being greater than this height of projection, can cause catalyst particle attrition, efflorescence.In addition, the inwall of rotary drum body 1 and the material of lifting blade can be preferably stainless steel.
Below the preferred embodiment of the present invention is described in detail by reference to the accompanying drawings; but; the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each the concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode.In order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (11)
1. a Catalyst Production technique, is characterized in that, comprises the following steps:
Step 1, drives the inner rotary drum body (1) that carrier is housed to carry out rotating to stir carrier, and by sprayer, dipping solution is sprayed to carrier;
Step 2, is disposed to the outside of described rotary drum body (1) by the boil-off gas in dipping process by the exhaust outlet offered on described rotary drum body (1).
2. Catalyst Production technique according to claim 1, it is characterized in that, in step 1, described rotary drum body (1) is driven to rotate by the driving shaft (2) be connected on described rotary drum body (1), wherein, the velocity of rotation of described rotary drum body (1) is 0.5 turn/min ~ 100 turn/min, be preferably 5 turns/min ~ 60 turn/min, more preferably 10 turns/min ~ 50 turn/min.
3. Catalyst Production technique according to claim 2, it is characterized in that, described rotary drum body (1) is taper or the biconial sharing same cone bottom surface, and described driving shaft (2) is connected to position bottom described taper or diconical cone
Wherein, the described floss hole in step 2 is opened in the connecting portion of described driving shaft (2) and described rotary drum body (1), and the holding temperature of described rotary drum body (1) is 40 DEG C to 90 DEG C.
4. Catalyst Production technique according to claim 3, it is characterized in that, described sprayer in step 1 comprises multiple shower nozzle (5), described shower nozzle (5) is arranged on the described diconical position near at least one vertex of a cone of the inside of described rotary drum body (1)
Wherein, described shower nozzle (5) towards regulating, and described shower nozzle (5) is adjustable to the distance of described diconical inwall.
5. Catalyst Production technique according to claim 4, is characterized in that, wherein, the diameter of the drop that described shower nozzle (5) sprays is 1 μm to 1000 μm, is preferably 10 μm to 500 μm, more preferably 20 μm to 200 μm.
6. Catalyst Production technique according to claim 5, it is characterized in that, the fluid pressure of described shower nozzle (5) is 0.05MPa-10.0MPa, be preferably 0.1MPa-5.0MPa, more preferably 0.2MPa-2.0MPa, the mist flow of described shower nozzle (5) is 0.1L/min-10.0L/min, is preferably 0.2L/min-8.0L/min, more preferably 0.5L/min-5.0L/min.
7. Catalyst Production technique according to claim 3, is characterized in that, also comprises the step be placed to by carrier in described rotary drum body (1) before step 1,
Wherein, the inlet amount of carrier controls to criticize for 20kg/ criticizes-1000kg/, and preferably 50kg/ criticizes-800kg/ and criticizes, and more preferably 100kg/ criticizes-300kg/ and criticizes.
8. Catalyst Production technique according to claim 3, is characterized in that, also comprises after step 2 and the carrier through dipping is carried out quick-drying step,
Wherein, through the dry zone (101) that drops on for dried material via the guiding of distributing device (102) of carrier of dipping.
9. Catalyst Production technique according to claim 8, it is characterized in that, the described carrier through dipping, at the upper bed of material forming 0.2cm to 5.0cm of described dry zone (101), is preferably the bed of material of 0.5cm to 3.0cm, the more preferably bed of material of 0.5cm to 2.0cm.
10. Catalyst Production technique according to claim 8 or claim 9, it is characterized in that, the width of described dry zone (101) is 0.5m to 3m, is preferably 0.5m-2.0m; The baking temperature of described dry zone (101) is 50 DEG C to 600 DEG C, is preferably 100 DEG C to 500 DEG C, more preferably 120 DEG C to 400 DEG C.
11. Catalyst Production techniques according to any one of claim 1-9, it is characterized in that, the dip time of carrier in described rotary drum body (1) is 1min to 120min, is preferably 5min to 60min, more preferably 10min to 30min.
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| CN201410256141.XA CN105149013B (en) | 2014-06-10 | 2014-06-10 | It is catalyzed agent producing process |
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| CN201410256141.XA CN105149013B (en) | 2014-06-10 | 2014-06-10 | It is catalyzed agent producing process |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6043188A (en) * | 1997-11-14 | 2000-03-28 | Hyundai Motor Company | Process for manufacturing palladium ternary catalyst |
| CN203550524U (en) * | 2013-10-29 | 2014-04-16 | 中国石油化工股份有限公司 | Double-frustum converter |
-
2014
- 2014-06-10 CN CN201410256141.XA patent/CN105149013B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6043188A (en) * | 1997-11-14 | 2000-03-28 | Hyundai Motor Company | Process for manufacturing palladium ternary catalyst |
| CN203550524U (en) * | 2013-10-29 | 2014-04-16 | 中国石油化工股份有限公司 | Double-frustum converter |
Non-Patent Citations (2)
| Title |
|---|
| 张继光主编: "《催化剂制备过程技术》", 31 October 2011, 北京：中国石化出版社 * |
| 朱洪法，刘丽芝编: "《催化剂制备及应用技术》", 30 June 2011, 北京：中国石化出版社 * |
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