CN107149916A - A kind of vertical fluidized bed for being used to prepare catalyst and system - Google Patents
A kind of vertical fluidized bed for being used to prepare catalyst and system Download PDFInfo
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- CN107149916A CN107149916A CN201710502828.0A CN201710502828A CN107149916A CN 107149916 A CN107149916 A CN 107149916A CN 201710502828 A CN201710502828 A CN 201710502828A CN 107149916 A CN107149916 A CN 107149916A
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- section
- fluidisation
- inlet duct
- fluidized bed
- drawing mechanism
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
Abstract
The invention provides a kind of vertical fluidized bed for being used to prepare catalyst and system.Vertical fluidized bed includes fluid bed body, feed arrangement, spray equipment, inlet duct and drawing mechanism, and feed arrangement, spray equipment, inlet duct and drawing mechanism are arranged on fluid bed body；Fluid bed body includes fluidisation section and expanding reach, and the diameter of expanding reach is more than the diameter of fluidisation section, and expanding reach is located at the top of fluidisation section；Feed arrangement and spray equipment are arranged in fluidisation section, and feed arrangement is located at the top of spray equipment；Inlet duct is located in the lower section of fluidisation section, and drawing mechanism is located at the lower section of inlet duct, and inlet duct is connected with fluidisation section and drawing mechanism respectively.The present invention use fluid bed as the main equipment of dipping, solve because contacted between maceration extract and carrier it is uneven and caused by the situation that dipping is uneven, catalyst activity component load is uneven.
Description
Technical field
The invention belongs to chemical field, in particular it relates to a kind of vertical fluidized bed for being used to prepare catalyst and system.
Background technology
Catalyst is the foundation stone of chemical industry, without catalyst just without modern chemical industry.According to statistics, it there are about 90%
Catalyst, such as chemical industry, petrochemical industry, biochemistry, environmental protection are used in industrial process above.
In catalyst preparation and production process, there are a variety of production methods, such 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 method more commonly used.In infusion process, by activearm
Point be impregnated on carrier is most important of which step.Traditional catalyst carrier impregnating equipment mainly has impregnating autoclave, and dipping is hung
Basket, impregnates guipure, impregnates roller, impregnates rotary drum, dipping bowling machine etc..
When being impregnated in the prior art using dipping rotary drum, carrier is placed into rotary drum, and dipping solution is imported
Into rotary drum to enable solution impregnated carrier.The lead-in mode of solution is directly to flow liquid into rotary drum.This
In the case of, the imbibition requirement of carrier, i.e. saturation leaching could be met by only importing carrier hole saturation or importing excessive dipping solution
Stain even supersaturation dipping.So can not only cause the waste of substantial amounts of solution, also result in can not meet production active component it is non-
The requirement of homogeneous catalyst.
The content of the invention
In view of the deficiencies of the prior art, present invention aim to address during preparation catalyst,
Occur because contacted between maceration extract and carrier it is uneven and caused by dipping is uneven, catalyst activity component load is uneven
The problems such as.
A kind of vertical fluidized bed for being used to prepare catalyst that the present invention is provided, including fluid bed body, feed arrangement, spray
Shower device, inlet duct and drawing mechanism, the feed arrangement, the spray equipment, the inlet duct and discharging dress
Put and be arranged on the fluid bed body；
The fluid bed body includes fluidisation section and expanding reach, and the diameter of the expanding reach is more than the straight of the fluidisation section
Footpath, the expanding reach is located at the top of the fluidisation section；
The feed arrangement and the spray equipment are arranged in the fluidisation section, and the feed arrangement is located at the spray
The top of device；The inlet duct is located in the lower section of the fluidisation section, and the drawing mechanism is located at the inlet duct
Lower section, the inlet duct is connected with the fluidisation section and the drawing mechanism respectively.
Preferably, the inlet duct includes being evenly distributed with stomata on gas distributor, the gas distributor, described
Drop expects pipe is installed, the drop expects pipe is connected with the fluidisation section and the drawing mechanism respectively in the middle part of gas distributor.
Preferably, a diameter of 3mm~8mm of the stomata.
Preferably, the centre-to-centre spacing of two neighboring stomata is 1~5 times of the gas distributor caliber.
Preferably, the cross-sectional area of the drop expects pipe is the 10%~40% of the cross-sectional area of the fluidisation section.
Preferably, the gas distributor is conical or spherical.
Preferably, the spray equipment includes dipping liquid storage tank, measuring pump, check valve, sprayer and gas bypassing, described
Dipping liquid storage tank, the measuring pump, the check valve, the sprayer are sequentially connected, and the sprayer is arranged on the fluidisation
On the inwall of section, the gas bypassing is arranged on the connecting line between the measuring pump and the check valve.
On this basis, present invention also offers a kind of system for preparing catalyst, it includes described vertical stream
Change bed, drier and heat storage type pyrolysis revolving bed, the drier untwists with vertical fluidized bed, the heat-accumulation type hot respectively
Rotated bed is connected.
Preferably, the drier is Caterpillar-type dryer, vacuum crawler formula drier or drum dryer.
Preferably, warming-up section, constant temperature zone and temperature descending section are divided into the heating of the heat storage type pyrolysis revolving bed.
The present invention use fluid bed as the main equipment of dipping, solve because contacted between maceration extract and carrier it is uneven and
The situation that dipping is uneven, catalyst activity component load is uneven caused so that the dipping of catalyst is more uniform.
Further, the fluid bed that the present invention is provided can realize that quantification of the catalyst in dipping process is operated, continuously
Change operation.
Further, the system that the present invention is provided can realize the serialization of catalyst, mass production operation, prepare
Catalyst performance stabilised, product is homogeneous.
Further, the thermocatalyst in drier directly can be transported in revolving bed by the present invention is calcined, and is saved
Save the consumption of heat.
In addition, the revolving bed that uses of the present invention can be by adjusting revolving bed radiant tube in the quantity combusted of combustion gas (become
Temperature), rotating speed, to realize the sintering temperature of be calcined catalyst and the requirement of roasting time, adaptability is stronger.
Brief description of the drawings
Fig. 1 be the embodiment of the present invention in a kind of vertical fluidized bed structural representation.
Fig. 2 is a kind of structural representation for being used to prepare the system of catalyst in the embodiment of the present invention.
In figure：
100th, fluid bed body, 101, fluidisation section, 102, expanding reach；
200th, feed arrangement, 201, carrier storage tank, 202, feed auger；
301st, liquid storage tank is impregnated, 302, measuring pump, 303, check valve, 304, sprayer, 305, gas access；
400th, inlet duct, 401, air inlet pipe, 402, gas distributor, 4021, drop expects pipe, 403, gas access；
500th, drawing mechanism, 501, discharging spiral, 502, discharging opening；
1st, vertical fluidized bed；
2nd, drier；
3rd, heat storage type pyrolysis revolving bed, A, warming-up section, B, constant temperature zone, C, temperature descending section, a, charging aperture, b, discharging opening.
Embodiment
Below in conjunction with drawings and examples, the embodiment to the present invention is described in more details, so as to energy
Enough more fully understand the solution of the present invention and the advantage of its various aspects.However, specific embodiments described below and reality
Apply the purpose that example is only explanation, rather than limitation of the present invention.
It should be noted that in the present invention, the orientation or position relationship of the instruction such as term " top ", " lower section ", " interior ", only
It is for the ease of the description present invention or simplifies description, rather than to indicate or imply that signified equipment or unit must have specific
Orientation or with specific azimuth configuration or operation, therefore be not considered as limiting the invention.Heretofore described " phase
Even ", unless otherwise clear and definite regulation or restriction, it should broadly understood, can be joined directly together or by intermediary
It is connected；Can be mechanical connection or electrical connection.In addition, all " cross-sectional areas " referred to of the present invention, refer to hang down
Directly in the area in the section of the longitudinal axis.
In order to solve during preparation catalyst, appearance because contacting uneven between maceration extract and carrier
And the problems such as the dipping that causes is uneven, catalyst activity component load is uneven, the present invention devises a kind of vertical fluidized bed
(present invention is also by its letter for (present invention is also referred to as " fluid bed ") and a kind of reaction system of continuous production catalyst
Referred to as " system ").It is described in detail below with reference to Fig. 1 to Fig. 2 fluid beds provided the present invention and the system being made from it.
As shown in figure 1, the vertical fluidized bed that the present invention is provided includes fluid bed body 100, feed arrangement 200, spray dress
Put, inlet duct 400 and drawing mechanism 500.
Feed arrangement 200, spray equipment, inlet duct 400 and drawing mechanism 500 are arranged on fluid bed body 100.
Fluid bed body 100 includes fluidisation section 101 and expanding reach 102, and the diameter of expanding reach 102 is more than fluidisation section 101
Diameter, expanding reach 102 is located at the top of fluidisation section 101.The main function of expanding reach 102 is to reduce the gas velocity of reacting gas, is made
The carrier little particle carried secretly in gas settles down, and returns in fluidisation section 101.
Feed arrangement 200 and spray equipment are arranged in fluidisation section 101, and feed arrangement 200 is located at the top of spray equipment.
Inlet duct 400 is located in the lower section of fluidisation section 101, and drawing mechanism 500 is located at the lower section of inlet duct 400, inlet duct 400
It is connected respectively with fluidisation section 101 and drawing mechanism 500.
In Fig. 1, feed arrangement 200 is made up of feed auger 202 and carrier storage tank 201, passes through the defeated of feed auger 202
Send, carrier be transported in fluid bed, section 101 can be fluidized according to quantitative be conveyed into carrier of rotating speed of feed auger 202,
Realize quantitative conveying.Feed arrangement 200 may also be other structures, as long as carrier can be transported to fluidisation section 101.
As shown in figure 1, spray equipment includes dipping liquid storage tank 301, measuring pump 302, check valve 303, sprayer 304, gas
Body entrance 305 (i.e. gas bypassing).Dipping liquid storage tank 301, measuring pump 302, check valve 303, sprayer 304 are sequentially connected, and are sprayed
Day with fog 304 is arranged on the inwall of fluidisation section 101.Gas access 305 is arranged on the connection between measuring pump 302, check valve 303
On pipeline.Maceration extract in dipping liquid storage tank 301 is driven into fluidisation section 101 by measuring pump 302, is connect with the carrier of fluidisation
Touch, homogeneous impregnation；Sprayer 304 can have one or more, and it can uniformly spray spray liquid；When discovery measuring pump 302 dozens
When not going out maceration extract (being probably that shower nozzle is blocked), measuring pump 302 can be closed, gas is conveyed from gas bypassing, tamper is blown
Fall, proceed dipping.Spray equipment can also be other structures, as long as maceration extract can be squeezed into fluidisation section 101, homogeneous impregnation
Carrier.
In Fig. 1, inlet duct 400 is made up of air inlet pipe 401 and gas distributor 402.Uniformly divide on gas distributor 402
Be furnished with the middle part of stomata (not shown), gas distributor be provided with drop expects pipe 4021, drop expects pipe 4021 respectively with fluidisation section 101 and
Drawing mechanism 500 is connected.Fluidizing gas is entered by gas access 403, is entered by air inlet pipe 401 under gas distributor 402
End, then by the stomata on gas distributor 402, is entered in fluidisation section 101.Inlet duct 400 can also be other knots
Structure, as long as enough gas can be entered so that uniformly contacted between maceration extract and carrier.
In the preferred embodiment of the invention, a diameter of 3mm~8mm of stomata.It is highly preferred that in two neighboring stomata
The heart is away from 1~5 times for the caliber of gas distributor 402.It is further preferred that the centre-to-centre spacing of two neighboring stomata is gas distributor
1.5~3 times of 402 calibers.Stomata is too small or stomata between far apart, deficiency of air, it is difficult to blow carrier, thus can not
So that uniformly being contacted between maceration extract and carrier；Stomata too big or stomata is too intensive, and maceration extract enters gas easily by stomata
In distributor 402.
The shape of gas distributor 402 is without being particularly limited to, in Fig. 1, and gas distributor 402 is cone.In the present invention
In another preferred embodiment, gas distributor 402 is spherical.Conical and spherical surface area is big, thus gas cell distribution is more, has
Fully contacted with maceration extract beneficial to carrier.Moreover, conical and spherical industrially make is also convenient for.
The carrier impregnated is entered in drawing mechanism 500 by dropping expects pipe 4021 from fluidisation section 101, drops the horizontal stroke of expects pipe 4021
Sectional area is the 10%~40% of the cross-sectional area of fluidisation section 101.The cross-sectional area for dropping expects pipe 4021 is excessive, gas distributor
402 effective surface area (area that can set the surface of stomata) very little, the gas for entering fluidisation section 101 from stomata is few,
It is not easy to blow carrier, it is impossible to so that uniformly contacting between maceration extract and carrier.The cross-sectional area for dropping expects pipe 4021 is too small, easily
Result in blockage, and slowing of passing through of carrier, the production capacity of fluid bed diminishes.
Drawing mechanism 500 is located in the bottommost of fluid bed, the embodiment shown in Fig. 1, and drawing mechanism 500 includes discharging spiral shell
Rotation 501 and discharging opening 502.Carrier is entered in discharging spiral 501 by dropping expects pipe 4021, and discharging is sent to by discharging spiral 501
Mouth 502, is then exhausted from outside fluid bed.Drawing mechanism 500 can also be other structures, as long as carrier can be sent out into fluid bed.
Fluidizing gas enters fluidisation section 101 from gas access 403, and the flow velocity of fluidizing gas is more than fluidizing velocity.Charging
Spiral 202 is according to certain inlet amount fixed rotating speed, held stationary charging, by carrier feeding fluidisation section 101.Spray equipment according to
The weight proportion of maceration extract and carrier, in the presence of measuring pump 302, quantitatively conveys maceration extract to fluidisation section 101.Drawing mechanism
500 load is identical with the inlet amount of feed arrangement 200.Fluid bed is in a dynamic equilibrium.
In the fluidisation section 101 of fluid bed, fresh carrier constantly enters the stream of fluidisation section 101 from feed arrangement 200
Change in layer, carrier is mixed into rapidly fluidization in fluosolids with fluidizing gas, and constantly rolls, " boiling is presented
Shape ".Maceration extract is equably sprayed onto in fluosolids by sprayer 304, and maceration extract is by carrier absorption, and carrier is constantly to move
Fluidized state in, maceration extract can be distributed in whole fluidised fluosolids quickly.So as to just solve because of maceration extract
The situation that dipping is uneven and catalyst activity component load is uneven that is uneven and causing is contacted between carrier.In fluidisation
The drawing mechanism 500 of the bottom of bed endlessly exports impregnated good carrier from fluid bed, it is achieved thereby that even
Continuousization, homogenization impregnated catalyst.
The present invention use fluid bed as the main equipment of dipping, solve because contacted between maceration extract and carrier it is uneven and
The situation that dipping is uneven, catalyst activity component load is uneven caused so that the dipping of catalyst is more uniform.
In addition, the fluid bed that the present invention is provided can realize that quantification operation, serialization of the catalyst in dipping process are grasped
Make.
Fig. 2 show a kind of system for preparing catalyst that the present invention is provided, including vertical fluidized bed 1, drier 2
With heat storage type pyrolysis revolving bed 3 (present invention in be also referred to as revolving bed), drier 2 respectively with vertical fluidized bed 1 and rotation
Rotated bed 3 is connected.
The catalyst carrier impregnated discharged from fluid bed 1, is delivered in drier 2, in drier 2, dipping
Excessive moisture is dried, volatilized in liquid, so as to cause active component to be more evenly distributed in the surface of catalyst carrier.
The dried catalyst carrier from drier 2, is delivered directly in revolving bed 3 without cooling, is entered by charging aperture a and rotated
It is calcined in bed.In revolving bed 3, catalyst is drawn off after roasting and cooling from the discharging opening b of revolving bed 3.So as to
Catalyst is completed from dipping, the production processes dried, be calcined whole.
The system that the present invention is provided can realize the serialization of catalyst, mass production operation, the catalyst prepared
Performance is stable, and product is homogeneous.
The of the invention directly thermocatalyst in drier 2 is transported in revolving bed 3 is calcined, and saves disappearing for heat
Consumption.
In order to realize serialization, the mass production operation of catalyst, drier 2 is preferably the equipment of serialization.At this
In invention preferred embodiment, drier 2 is Caterpillar-type dryer, vacuum crawler formula drier or drum dryer.
Revolving bed 3 can be by adjusting quantity combusted (alternating temperature), the rotating speed of combustion gas in radiant tube, to realize be calcined catalysis
The sintering temperature of agent and the requirement of roasting time, adaptability are stronger.In order to be able to more preferable calcined catalyst, multiple catalysts are met
Roasting requirement, in the preferred embodiment of the invention, warming-up section A, constant temperature zone B and temperature descending section C are divided into the heating of revolving bed.
Below with reference to specific embodiment, the present invention will be described.Institute's taking technique condition value is in following embodiments
Exemplary, its desirable number range is as shown in foregoing summary.Detection method used in following embodiments is one's own profession
The conventional detection method of industry.
Embodiment
Platinum/Al is prepared using the system shown in the fluid bed and Fig. 2 shown in Fig. 12O3Reforming catalyst.In the present embodiment, stream
Change bed 1 is vertical cylinder, wherein, 1.5 times of the diameter of a diameter of fluidisation section 101 of expanding reach 102, gas distributor 402
Hole diameter be 3mm, the centre-to-centre spacing of two neighboring stomata is 5 times of the caliber of gas distributor 402, and gas distributor 402 is
Cone, the cross-sectional area of drop expects pipe 4021 is the 10% of the cross-sectional area of fluidisation section 101.Drier 2 is Caterpillar-type dryer.
Fluidizing gas is nitrogen.
With high-purity, diameter 3mm γ-Al2O3Bead is carrier, and the chloroplatinic acid that concentration is 2.45g/L is maceration extract.Every thousand
Gram γ-Al2O3Impregnate 0.6L platinum acid chloride solution.
Fluid bed 1 is fed with 150Kg/h, and measuring pump 302 is sprayed with 90L/h.After dipping is complete, from discharging spiral shell
Fluid bed 1 is drawn off in rotation 501.Delivered to and be dried in drier 2 by feed belt.Under conditions of 120 DEG C, catalyst exists
3h is dried in drier 2.Then, it is sent directly into revolving bed 3 and is calcined.In revolving bed 3, first in warming-up section A with 160
DEG C/h heating rate carries out roasting 3h (i.e. from 120 DEG C of roastings to 600 DEG C), then with 600 DEG C it is calcined 1h in constant temperature zone B, then
Temperature descending section C coolings 1h.Drawn off therewith from revolving bed 3, produce platinum/Al2O3Reforming catalyst.
It was found from above-described embodiment, the system provided using the present invention, it is possible to achieve serialization, the batch metaplasia of catalyst
Catalyst is produced, and obtained catalyst prod performance is stable, and product is homogeneous.
To sum up, the present invention uses fluid bed as the main equipment of dipping, solves because being contacted not between maceration extract and carrier
Dipping that is uniform and causing is uneven, catalyst activity component loads uneven situation so that the dipping of catalyst is more equal
It is even.
Further, the fluid bed that the present invention is provided can realize that quantification of the catalyst in dipping process is operated, continuously
Change operation.
Further, the system that the present invention is provided can realize the serialization of catalyst, mass production operation, prepare
Catalyst performance stabilised, product is homogeneous.
Further, the thermocatalyst in drier directly can be transported in revolving bed by the present invention is calcined, and is saved
Save the consumption of heat.
In addition, the revolving bed that uses of the present invention can be by adjusting revolving bed radiant tube in the quantity combusted of combustion gas (become
Temperature), rotating speed, to realize the sintering temperature of be calcined catalyst and the requirement of roasting time, adaptability is stronger.
Obviously, above-described embodiment is only intended to clearly illustrate example of the present invention, and not to embodiment
Limit.For those of ordinary skill in the field, other multi-forms can also be made on the basis of the above description
Change or variation.There is no necessity and possibility to exhaust all the enbodiments.And thus amplify out it is apparent
Change or change still in protection scope of the present invention among.
Claims (10)
1. a kind of vertical fluidized bed for being used to prepare catalyst, it is characterised in that including fluid bed body, feed arrangement, spray
Device, inlet duct and drawing mechanism, the feed arrangement, the spray equipment, the inlet duct and the drawing mechanism
It is arranged on the fluid bed body；
The fluid bed body includes fluidisation section and expanding reach, and the diameter of the expanding reach is more than the diameter of the fluidisation section, institute
State the top that expanding reach is located at the fluidisation section；
The feed arrangement and the spray equipment are arranged in the fluidisation section, and the feed arrangement is located at the spray equipment
Top；The inlet duct is located in the lower section of the fluidisation section, and the drawing mechanism is located at the lower section of the inlet duct,
The inlet duct is connected with the fluidisation section and the drawing mechanism respectively.
2. vertical fluidized bed according to claim 1, it is characterised in that the inlet duct includes gas distributor, institute
State and stomata is evenly distributed with gas distributor, drop expects pipe, the drop expects pipe difference are installed in the middle part of the gas distributor
It is connected with the fluidisation section and the drawing mechanism.
3. vertical fluidized bed according to claim 2, it is characterised in that a diameter of 3mm~8mm of the stomata.
4. vertical fluidized bed according to claim 3, it is characterised in that the centre-to-centre spacing of the two neighboring stomata is described
1~5 times of gas distributor caliber.
5. vertical fluidized bed according to claim 2, it is characterised in that the cross-sectional area of the drop expects pipe is the fluidisation
The 10%~40% of the cross-sectional area of section.
6. vertical fluidized bed according to claim 2, it is characterised in that the gas distributor is conical or spherical.
7. vertical fluidized bed according to claim 1, it is characterised in that the spray equipment includes dipping liquid storage tank, meter
Measure pump, check valve, sprayer and gas bypassing, the dipping liquid storage tank, the measuring pump, the check valve, the sprayer
It is sequentially connected, the sprayer is arranged on the inwall of the fluidisation section, and the gas bypassing is arranged on the measuring pump and institute
State on the connecting line between check valve.
8. a kind of system for preparing catalyst, it is characterised in that including any described vertical stream in claim 1~7
Change bed, drier and heat storage type pyrolysis revolving bed, the drier untwists with vertical fluidized bed, the heat-accumulation type hot respectively
Rotated bed is connected.
9. system according to claim 8, it is characterised in that the drier is Caterpillar-type dryer, vacuum crawler formula
Drier or drum dryer.
10. system according to claim 8, it is characterised in that liter is divided into the heating of the heat storage type pyrolysis revolving bed
Temperature section, constant temperature zone and temperature descending section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710502828.0A CN107149916A (en) | 2017-06-27 | 2017-06-27 | A kind of vertical fluidized bed for being used to prepare catalyst and system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710502828.0A CN107149916A (en) | 2017-06-27 | 2017-06-27 | A kind of vertical fluidized bed for being used to prepare catalyst and system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110721753A (en) * | 2019-09-23 | 2020-01-24 | 新疆兵团现代绿色氯碱化工工程研究中心(有限公司) | Solid particle impregnation device and method |
| CN111485225A (en) * | 2020-04-13 | 2020-08-04 | 合肥科晶材料技术有限公司 | Ultrasonic atomization fluidized bed device |
| CN113797856A (en) * | 2021-09-23 | 2021-12-17 | 中北大学 | Supergravity rotating fluidized field enhanced liquid-solid adsorption equipment and method |
-
2017
- 2017-06-27 CN CN201710502828.0A patent/CN107149916A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110721753A (en) * | 2019-09-23 | 2020-01-24 | 新疆兵团现代绿色氯碱化工工程研究中心(有限公司) | Solid particle impregnation device and method |
| CN110721753B (en) * | 2019-09-23 | 2024-03-12 | 新疆至臻化工工程研究中心有限公司 | Solid particle impregnating device and method thereof |
| CN111485225A (en) * | 2020-04-13 | 2020-08-04 | 合肥科晶材料技术有限公司 | Ultrasonic atomization fluidized bed device |
| CN111485225B (en) * | 2020-04-13 | 2021-11-26 | 合肥科晶材料技术有限公司 | Ultrasonic atomization fluidized bed device |
| CN113797856A (en) * | 2021-09-23 | 2021-12-17 | 中北大学 | Supergravity rotating fluidized field enhanced liquid-solid adsorption equipment and method |
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