CN208742512U - A kind of combined gas distributor and fluidized-bed reactor - Google Patents
A kind of combined gas distributor and fluidized-bed reactor Download PDFInfo
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- CN208742512U CN208742512U CN201820817068.2U CN201820817068U CN208742512U CN 208742512 U CN208742512 U CN 208742512U CN 201820817068 U CN201820817068 U CN 201820817068U CN 208742512 U CN208742512 U CN 208742512U
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Abstract
The utility model belongs to chemical technology field, specifically discloses a kind of combined gas distributor and fluidized-bed reactor.The combined gas distributor includes a gas distributor and secondary air distributor；Gas distributor includes being substantially disposed in conplane gas distribution general pipeline, gas distribution arms and nozzle, and gas distribution general pipeline is connected with gas distribution arms, and nozzle is uniformly arranged in gas distribution general pipeline and gas distribution arms；The secondary air distributor includes the lower layer's porous plate and upper layer porous plate set gradually from lower to upper, and every laminate has interlaced hole；The secondary air distributor is set to above a gas distributor.The utility model makes gas be evenly distributed, it is thus also avoided that the blocking of nozzle, catalyst use efficiency significantly improve by gas distributor of setting and secondary air distributor.The fluidized-bed reactor includes the combined gas distributor, be can be widely applied in chemical field gas solid catalytic reaction.
Description
Technical field
The utility model relates to chemical technology fields, and in particular, to a kind of combined gas distributor and fluidized bed are anti-
Answer device.
Background technique
In Chemical Manufacture, the reactor for gas solid catalytic reaction usually has fixed bed reactors and fluidized-bed reaction
Device.The reaction of cyclic regeneration is needed to be typically chosen stream the reaction or catalyst of stronger reaction heat (highly endothermic or strongly exothermic)
Fluidized bed reactor.
Currently, the bottom gas distributor form of common fluidized-bed reactor has bubble-cap type and two kinds of nozzle-type.
The advantages of bubble-cap type gas distributor be gas be evenly distributed, catalyst use efficiency height etc..The disadvantage is that operation
Stability is poor, difficult in maintenance；Simultaneously because bubble-cap distribution grid is plate, plate pressure resistance performance is poor, is easily deformed, and is not suitable for
Major diameter fluidized-bed reactor, bubble-cap type gas distributor are only applicable to fluidized-bed reactor of the diameter less than 3 meters.
Existing its bottom gas distributor of major diameter fluidized-bed reactor (diameter is greater than 3 meters of fluidized-bed reactor) is equal
Using nozzle-type gas distributor.The advantages of nozzle-type gas distributor is that structure is simple, stable, is particularly suitable for big straight
The fluidized-bed reactor of diameter.
But existing nozzle-type gas distributor has the disadvantage in that
(1) gas is unevenly distributed
For existing nozzle-type gas distributor since nozzle is tubular structure, arrangement effect is unable to reach equilateral triangle row
The effect of column or concentric arrays, be easy to cause gas to be unevenly distributed.
(2) nozzle is easy blocking
Downward due to nozzle, after reactor stops fluidizing, emulsion zone catalyst will for existing nozzle-type gas distributor
Moment largely falls after rise, refunds blast tube, gas distribution arms and gas distribution general pipeline, or even refund gas inlet tube, and formed
Serious blocking.
(3) reactor fluidisation is difficult
Existing nozzle-type gas distributor is since nozzle is easy blocking, and when reactor fluidisation, gas is easy bias current, makes
It is fluidized at reactor difficult.In reactor fluid mapper process, it is easy to happen the phenomenon that catalyst is largely taken out of, causes production thing
Therefore.
(4) catalyst use efficiency is low
Downward due to nozzle, and jet expansion is generally within same level for existing nozzle-type gas distributor, and flows
Fluidized bed reactor bottom bulkhead is generally ellipsoidal head, and therefore, most of catalyst can not in the ellipse head below nozzle
Fluidisation, prolonged stay forms dead zone, and causes to agglomerate, and catalyst use efficiency is low.
For the defect of nozzle-type gas distributor, domestic some research and development institutions and manufacturer are proposed nozzle-type gas
Distributor is divided into multiple distributed areas, while designing multiple gas inlet tubes, the corresponding distributed areas of each gas inlet tube,
And valve is installed on each gas inlet tube, according to the stopping state of each distributed areas, its air inflow is adjusted, is blown with reaching
The purpose of logical nozzle.The nozzle-type gas distributor of multiple distributed areas, may be several in the case where blocking is less tight
Hour nozzle can be blown it is logical, but for block it is more tight in the case of, may all cannot normally fluidize within several days, needed when serious
Catalyst is drawn off so as to nozzle clearing.
Therefore, be badly in need of develop one kind can effectively solve existing gas distributor gas be unevenly distributed, nozzle be easy blocking,
The device for the problems such as reactor fluidisation is difficult, catalyst use efficiency is low.
Utility model content
The purpose of this utility model is to overcome the above-mentioned deficiencies of the prior art, provide a kind of combined gas distribution
Device, the combined gas distributor is with gas is evenly distributed, nozzle does not block, reliable, catalyst use efficiency easy to operate
The advantages that high.
The another object of the utility model is to provide a kind of fluidized-bed reaction including said combination formula gas distributor
Device.
To achieve the goals above, the utility model is achieved by following scheme:
A kind of combined gas distributor, including a gas distributor and secondary air distributor；Gas
Distributor includes being substantially disposed in conplane gas distribution general pipeline, gas distribution arms and nozzle, gas to be distributed general pipeline and connect
Gas distribution arms are connected to, nozzle is uniformly arranged in gas distribution general pipeline and gas distribution arms；The secondary air distribution
Device includes the lower layer's porous plate and upper layer porous plate set gradually from lower to upper, and every laminate has interlaced hole；Described two
Secondary gas distributor is set to above a gas distributor.
Preferably, a gas distributor is connected to gas inlet tube.
It is highly preferred that a gas distributor is connected to gas inlet tube by pipeline.
Preferably, the gas distribution general pipeline is connected to gas inlet tube；The gas distribution arms are circular ring type or comb
The arrangement of comb formula, center line are located in same level.
Preferably, the nozzle opening is downward, including nozzle orifice plate and blast tube, at an angle towards reactor bottom
End socket.
It is highly preferred that the certain angle is 0 °~45 °.
Preferably, the distribution hole on the upper layer porous plate and lower layer's porous plate is equilateral triangle arrangement, upper layer porous plate
With lower layer's porous plate vertical interlaced, i.e. upper layer porous plate and lower layer's porous plate is staggered 90 ° of perpendicular staggeredly modes.
Preferably, the distribution hole on the upper layer porous plate and lower layer's porous plate be concentric arrays, upper layer porous plate with
Lower layer's porous plate is staggered certain angle.
Preferably, rforated plate bracing frame is provided between lower layer's porous plate and upper layer porous plate.
A kind of fluidized-bed reactor including said combination formula gas distributor is also claimed in the utility model.
The carrying out practically process of the fluidized-bed reactor is as follows:
Before fluidized-bed reactor operation, first catalyst is packed into reactor enclosure body.Unreacting gas is by gas feed
Pipe enters fluidized-bed reactor, and successively after the gas of gas distributor distribution general pipeline, gas distribution arms, gas is equal
It is sprayed down from each nozzle evenly, and blows catalyst granules loss and form fluidisation；At this time gas entrained catalyst particles according to
Secondary lower layer's porous plate and upper layer porous plate by secondary air distributor, equably by the catalyst fluidization in reactor.
After fluidized-bed reactor normally fluidizes, due on the lower layer's porous plate and upper layer porous plate of secondary air distributor
Distribution hole controls certain gas flow rate, so that the catalyst granules by upper layer porous plate can not return to lower space,
Therefore, catalyst granules can be constantly blown to above the porous plate of upper layer in the space below secondary air distributor, in this way,
When fluidized-bed reactor operates normally, the space below secondary air distributor forms dilute-phase zone, and catalyst granules all shifts
Space to above the porous plate of upper layer, catalyst are utilized effectively.
After reactor stops fluidizing, catalyst granules will largely be fallen after rise to secondary air distributor, then successively be passed through
The upper layer porous plate of secondary air distributor and the distribution hole of lower layer's porous plate are crossed, is slowly fallen after rise to bottom, at this point, secondary air
Distributor, which plays the role of barrier a large amount of catalyst granules moments, to be fallen after rise to bottom, so that the sky below secondary air distributor
Between catalyst granules be in rarefaction, thus solve the problems, such as gas distributor be easy blocking.
By using the combined gas distributor of the utility model, the diameter of fluidized-bed reactor can be made up to 12 meters
When remain to trouble-free operation.
Fluidized-bed reactor described in the utility model can be applied in chemical field gas solid catalytic reaction, especially in trimerization
Cyanamide or methanation produce, in the production processes such as methanol-to-olefins.
Compared with prior art, the utility model has the following beneficial effects:
(1) gas is evenly distributed
The utility model is due in such a way that a gas distributor is combined with secondary air distributor, that is, first passing through one
Secondary gas distributor is tentatively distributed, and carries out quadratic distribution using secondary air distributor.Due under secondary air distributor
Distribution hole on layer porous plate and upper layer porous plate is equilateral triangle arrangement or concentric arrays, and gas distributes very evenly.
(2) nozzle is not easy to plug
The utility model is due in such a way that a gas distributor is combined with secondary air distributor, when fluidized bed is anti-
After answering device to stop fluidisation, catalyst granules will largely be fallen after rise to secondary air distributor, and secondary air distributor plays
Obstructing a large amount of catalyst granules moments falls the blocking that a gas distributor nozzle is avoided to the effect of bottom after rise.
(3) reactor is easy fluidisation
Gas distributor nozzle is not easy to plug the utility model due to No. one time, and the gas distribution of secondary air distributor is very
Uniformly, therefore, fluidized-bed reactor is easy fluidisation, and usual 1~2 hour normal with regard to energy fluidizing.
(4) catalyst use efficiency is high
The utility model is due in such a way that a gas distributor is combined with secondary air distributor, fluidized-bed reaction
After device normally fluidizes, the space below secondary air distributor forms dilute-phase zone, and it is porous that catalyst granules is transferred to upper layer
Space above plate, whole catalyst are all utilized effectively, and catalyst use efficiency is high.
Detailed description of the invention
Fig. 1 is the use state diagram of combined gas distributor described in the utility model in a fluidized bed reactor.
Fig. 2 is that the first structure of a gas distributor in combined gas distributor described in the utility model is overlooked
Figure.
Fig. 3 is that second of structure of a gas distributor in combined gas distributor described in the utility model is overlooked
Figure.
Fig. 4 is the first structure top view of secondary air distributor described in the utility model porous plate at the middle and upper levels.
Fig. 5 is the first structure top view of lower layer's porous plate in secondary air distributor described in the utility model.
Fig. 6 is second of structure top view of secondary air distributor described in the utility model porous plate at the middle and upper levels.
Fig. 7 is second of structure top view of lower layer's porous plate in secondary air distributor described in the utility model.
Fig. 8 is the structural schematic diagram of nozzle in a gas distributor described in the utility model.
Appended drawing reference: 10- gas inlet tube；11- gas is distributed general pipeline；12- gas distribution arms；13- nozzle；131- spray
Nozzle aperture plate；132- blast tube；The upper layer 20- porous plate；21- lower layer porous plate；22- rforated plate bracing frame；Gas distribution of 30-
Device support frame；40- reactor bottom end socket；50- reactor shell.
Specific embodiment
With reference to the accompanying drawings of the specification and specific embodiment is made the utility model and is further elaborated, the reality
It applies example to be served only for explaining the utility model, is not intended to limit the scope of the utility model.Examination as used in the following examples
Proved recipe method is conventional method unless otherwise specified；Used material, reagent etc., unless otherwise specified, being can be from business way
The reagent and material that diameter obtains.
A kind of combined gas distributor of embodiment 1 and melamine fluidized-bed reactor
A kind of combined gas distributor, as shown in Figure 1, including a gas distributor and secondary air distributor；Institute
Stating a gas distributor includes being substantially disposed in conplane gas distribution general pipeline 11, gas distribution arms 12 and nozzle
13, gas distribution general pipeline 11 are connected with gas distribution arms 12, and nozzle 13 is uniformly arranged on gas distribution general pipeline 11 and gas point
On cloth branch pipe 12；The secondary air distributor includes the lower layer's porous plate 21 and upper layer porous plate set gradually from lower to upper
20, every laminate has interlaced hole；The secondary air distributor is set to above a gas distributor.
Gas distributor is connected to gas inlet tube 10 by pipeline.
The gas distribution general pipeline 11 is connected to gas inlet tube 10；The gas distribution arms 12 are circular ring type (such as Fig. 2
It is shown) or the arrangement (as shown in Figure 3) of comb formula, center line is located in same level.
Open Side Down for the nozzle 13, including nozzle orifice plate 131 and blast tube 132, the court at an angle of blast tube 132
It is as shown in Figure 8 to reactor bottom end socket 40().
The certain angle is 0 °~45 °.
21 distribution hole is that equilateral triangle arrangement (is shown in Fig. 4 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
5), upper layer porous plate 20 and 21 vertical interlaced of lower layer's porous plate, i.e. upper layer porous plate 20 and lower layer's porous plate 21 are staggered 90 ° in vertical
Straight staggeredly mode.
Or 21 distribution hole is that concentric arrays (are shown in Fig. 6 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
7), upper layer porous plate and lower layer's porous plate are staggered certain angle.
Rforated plate bracing frame 22 is provided between lower layer's porous plate 21 and upper layer porous plate 20.
Meanwhile the present embodiment additionally provides a kind of melamine fluidized-bed reactor, is furnished with the combined gas
Distributor.
In melamine fluidized-bed reactor, the reaction that urea generates melamine, reaction equation are carried out are as follows:
6CO(NH2)2(urea)=C3N6H6(melamine)+6NH3 + 3CO2(strong endothermic reaction)
Before fluidized-bed reactor operation, first melamine catalyst is packed into reactor shell 50.After heated
Carrier gas (the NH that temperature is 390 DEG C3 + CO2) reactor entered by gas inlet tube 10, successively by gas distributor
After gas is distributed general pipeline 11, gas distribution arms 12, gas is equably sprayed from each nozzle 13 down, and blows catalyst particles
Grain loss forms fluidisation；At this time gas entrained catalyst particles successively pass through secondary air distributor lower layer's porous plate 21 and on
Layer porous plate 20, equably by the catalyst fluidization in reactor.
After fluidized-bed reactor normally fluidizes, due to the lower layer's porous plate 21 and upper layer porous plate 20 of secondary air distributor
On distribution hole control certain gas flow rate so that the catalyst granules by upper layer porous plate 20 can not return to lower part
Space, therefore, catalyst granules can be constantly blown on upper layer porous plate 20 in the space below secondary air distributor
Side, in this way, the space below secondary air distributor forms dilute-phase zone, catalyst particles when fluidized-bed reactor operates normally
Grain is transferred to the space of 20 top of upper layer porous plate, and catalyst is utilized effectively.
After reactor stops fluidizing, catalyst granules will largely be fallen after rise to secondary air distributor, then successively be passed through
The distribution hole of secondary air distributor upper layer porous plate 20 and lower layer's porous plate 21 is crossed, is slowly fallen after rise to bottom, at this point, secondary gas
Body distributor, which plays the role of barrier a large amount of catalyst granules moments, to be fallen after rise to bottom, so that below secondary air distributor
Space catalyst granules is in rarefaction, to solve the problems, such as that gas distributor is easy blocking.
By using the combined gas distributor of the present embodiment, the diameter of melamine fluidized-bed reactor can be made
Trouble-free operation is remained to when up to 8 meters.
Combined gas distributor and melamine fluidized-bed reactor operation result are as shown in table 1.
The overall target of a kind of combined gas distributor of table 1 and melamine fluidized-bed reactor application front and back compares
(in terms of producing 50000 tons of melamines per year by gas phase quenching process)
| Serial number | Project name | Specification | Before the present embodiment | After the present embodiment |
| 1 | Isoplanar temperature difference in reactor | 3~5 DEG C | 0~1 DEG C | |
| 2 | Spray nozzle clogging situation | It is easy blocking | It does not block | |
| 3 | Reactor normally fluidizes the time | 12~24 hours | 1~2 hour | |
| 4 | Gas distributor clears up frequency | Annual cleaning 5 times or more | It does not need to clear up | |
| 5 | Melamine catalyst consumption per ton | Melamine special-purpose catalyst | 5kg | 1kg |
| 6 | Reactor production capacity | 50000 tons of melamine/years | 60000 tons of melamine/years |
As shown in Table 1, the combined gas distributor of the present embodiment and melamine fluidized-bed reactor fundamentally solve
Large-scale melamine fluidized-bed reactor gas of having determined is unevenly distributed and the problem of spray nozzle clogging, substantially increases reactor
The stability of operation reduces the consumption of catalyst, improves the production capacity of reactor.
A kind of combined gas distributor of embodiment 2 and methanation fluidized-bed reactor
A kind of combined gas distributor, as shown in Figure 1, including a gas distributor and secondary air distributor；Institute
Stating a gas distributor includes being substantially disposed in conplane gas distribution general pipeline 11, gas distribution arms 12 and nozzle
13, gas distribution general pipeline 11 are connected with gas distribution arms 12, and nozzle 13 is uniformly arranged on gas distribution general pipeline 11 and gas point
On cloth branch pipe 12；The secondary air distributor includes the lower layer's porous plate 21 and upper layer porous plate set gradually from lower to upper
20, every laminate has interlaced hole；The secondary air distributor is set to above a gas distributor.
Gas distributor is connected to gas inlet tube 10 by pipeline.
The gas distribution general pipeline 11 is connected to gas inlet tube 10；The gas distribution arms 12 are circular ring type (such as Fig. 2
It is shown) or the arrangement (as shown in Figure 3) of comb formula, center line is located in same level.
Open Side Down for the nozzle 13, including nozzle orifice plate 131 and blast tube 132, the court at an angle of blast tube 132
It is as shown in Figure 8 to reactor bottom end socket 40().
The certain angle is 0 °~45 °.
21 distribution hole is that equilateral triangle arrangement (is shown in Fig. 4 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
5), upper layer porous plate 20 and 21 vertical interlaced of lower layer's porous plate, i.e. upper layer porous plate 20 and lower layer's porous plate 21 are staggered 90 ° in vertical
Straight staggeredly mode.
Or 21 distribution hole is that concentric arrays (are shown in Fig. 6 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
7), upper layer porous plate and lower layer's porous plate are staggered certain angle.
Rforated plate bracing frame 22 is provided between lower layer's porous plate 21 and upper layer porous plate 20.
Meanwhile the present embodiment additionally provides a kind of methanation fluidized-bed reactor, equipped with the combined gas point
Cloth device.
In methanation fluidized-bed reactor, carries out carbon monoxide and carbon dioxide is anti-with hydrogen synthesizing methane respectively
It answers, reaction equation are as follows:
CO + 3H2 = CH4 + H2O (strong exothermal reaction)
CO2 + 4H2 = CH4 + 2H2O (strong exothermal reaction)
Before fluidized-bed reactor operation, first methanation catalyst is packed into reactor shell 50.Temperature after heated
Unstripped gas (the CO+ CO that degree is 300 DEG C2 + H2) by gas inlet tube 10 enter reactor, successively pass through a gas distributor
Gas distribution general pipeline 11, after gas distribution arms 12, gas is equably sprayed from each nozzle 13 down, and blows catalyst
Particle loss forms fluidisation；At this time gas entrained catalyst particles successively pass through secondary air distributor lower layer's porous plate 21 and
Upper layer porous plate 20, equably by the catalyst fluidization in reactor.
After fluidized-bed reactor normally fluidizes, due to the lower layer's porous plate 21 and upper layer porous plate 20 of secondary air distributor
On distribution hole control certain gas flow rate so that the catalyst granules by upper layer porous plate 20 can not return to lower part
Space, therefore, catalyst granules can be constantly blown on upper layer porous plate 20 in the space below secondary air distributor
Side, in this way, the space below secondary air distributor forms dilute-phase zone, catalyst particles when fluidized-bed reactor operates normally
Grain is transferred to the space of 20 top of upper layer porous plate, and catalyst is utilized effectively.
After reactor stops fluidizing, catalyst granules will largely be fallen after rise to secondary air distributor, then successively be passed through
The distribution hole of secondary air distributor upper layer porous plate 20 and lower layer's porous plate 21 is crossed, is slowly fallen after rise to bottom, at this point, secondary gas
Body distributor, which plays the role of barrier a large amount of catalyst granules moments, to be fallen after rise to bottom, so that below secondary air distributor
Space catalyst granules is in rarefaction, to solve the problems, such as that gas distributor is easy blocking.
By using the combined gas distributor of the present embodiment, the diameter of methanation fluidized-bed reactor can be made to reach
Trouble-free operation is remained at 8 meters.
Combined gas distributor and methanation fluidized-bed reactor operation result are as shown in table 2.
A kind of combined gas distributor of table 2 and methanation fluidized-bed reactor application front and back overall target compare (with
Produce 1300000000 Nm per year3Natural gas meter)
| Serial number | Project name | Specification | Before the present embodiment | After the present embodiment |
| 1 | Isoplanar temperature difference in reactor | 10~15 DEG C | 0~5 DEG C | |
| 2 | Spray nozzle clogging situation | It is easy blocking | It does not block | |
| 3 | Reactor normally fluidizes the time | 12~24 hours | 1~2 hour | |
| 4 | Gas distributor clears up frequency | Annual cleaning 3 times or more | It does not need to clear up | |
| 5 | Every 10,000 Nm3The catalyst consumption of natural gas | Methanation special-purpose catalyst | 0.5kg | 0.1kg |
| 6 | Reactor production capacity | 1300000000 Nm3Natural gas/year | 1500000000 Nm3Natural gas/year |
As shown in Table 2, the combined gas distributor of the present embodiment and methanation fluidized-bed reactor fundamentally solve
Large-scale methanation fluidized-bed reactor gas is unevenly distributed and the problem of spray nozzle clogging, substantially increases reactor operation
Stability, reduce the consumption of catalyst, improve the production capacity of reactor.
A kind of combined gas distributor of embodiment 3 and methanol-to-olefins fluidized-bed reactor
A kind of combined gas distributor, as shown in Figure 1, including a gas distributor and secondary air distributor；Institute
Stating a gas distributor includes being substantially disposed in conplane gas distribution general pipeline 11, gas distribution arms 12 and nozzle
13, gas distribution general pipeline 11 are connected with gas distribution arms 12, and nozzle 13 is uniformly arranged on gas distribution general pipeline 11 and gas point
On cloth branch pipe 12；The secondary air distributor includes the lower layer's porous plate 21 and upper layer porous plate set gradually from lower to upper
20, every laminate has interlaced hole；The secondary air distributor is set to above a gas distributor.
Gas distributor is connected to gas inlet tube 10 by pipeline.
The gas distribution general pipeline 11 is connected to gas inlet tube 10；The gas distribution arms 12 are circular ring type (such as Fig. 2
It is shown) or the arrangement (as shown in Figure 3) of comb formula, center line is located in same level.
Open Side Down for the nozzle 13, including nozzle orifice plate 131 and blast tube 132, the court at an angle of blast tube 132
It is as shown in Figure 8 to reactor bottom end socket 40().
The certain angle is 0 °~45 °.
21 distribution hole is that equilateral triangle arrangement (is shown in Fig. 4 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
5), upper layer porous plate 20 and 21 vertical interlaced of lower layer's porous plate, i.e. upper layer porous plate 20 and lower layer's porous plate 21 are staggered 90 ° in vertical
Straight staggeredly mode.
Or 21 distribution hole is that concentric arrays (are shown in Fig. 6 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
7), upper layer porous plate and lower layer's porous plate are staggered certain angle.
Rforated plate bracing frame 22 is provided between lower layer's porous plate 21 and upper layer porous plate 20.
Meanwhile the present embodiment additionally provides a kind of methanol-to-olefins fluidized-bed reactor, is furnished with the combined type gas
Body distributor.
In methanol-to-olefins fluidized-bed reactor, the reaction that methanol is converted into ethylene or propylene, reactional equation are carried out
Formula are as follows:
2CH3OH(methanol)=C2H4(ethylene)+2H2O (strong exothermal reaction)
3CH3OH(methanol)=C3H6(propylene)+3H2O (strong exothermal reaction)
Before fluidized-bed reactor operation, first methanol-to-olefin catalyst is packed into reactor shell 50.Through gasifying
Unstripped gas (the CH that temperature is 250 DEG C after preheating3OH reactor) is entered by gas inlet tube 10, successively by a gas distribution
After the gas of device is distributed general pipeline 11, gas distribution arms 12, gas is equably sprayed from each nozzle 13 down, and blows catalysis
Agent particle loss forms fluidisation；Gas entrained catalyst particles successively pass through lower layer's porous plate 21 of secondary air distributor at this time
And upper layer porous plate 20, equably by the catalyst fluidization in reactor.
After fluidized-bed reactor normally fluidizes, due to the lower layer's porous plate 21 and upper layer porous plate 20 of secondary air distributor
On distribution hole control certain gas flow rate so that the catalyst granules by upper layer porous plate 20 can not return to lower part
Space, therefore, catalyst granules can be constantly blown on upper layer porous plate 20 in the space below secondary air distributor
Side, in this way, the space below secondary air distributor forms dilute-phase zone, catalyst particles when fluidized-bed reactor operates normally
Grain is transferred to the space of 20 top of upper layer porous plate, and catalyst is utilized effectively.
After reactor stops fluidizing, catalyst granules will largely be fallen after rise to secondary air distributor, then successively be passed through
The distribution hole of secondary air distributor upper layer porous plate 20 and lower layer's porous plate 21 is crossed, is slowly fallen after rise to bottom, at this point, secondary gas
Body distributor, which plays the role of barrier a large amount of catalyst granules moments, to be fallen after rise to bottom, so that below secondary air distributor
Space catalyst granules is in rarefaction, to solve the problems, such as that gas distributor is easy blocking.
By using the combined gas distributor of the present embodiment, the straight of methanol-to-olefins fluidized-bed reactor can be made
Trouble-free operation is remained to when diameter is up to 12 meters.
Combined gas distributor and methanol-to-olefins fluidized-bed reactor operation result are as shown in table 3.
A kind of combined gas distributor of table 3 and the overall target ratio of methanol-to-olefins fluidized-bed reactor application front and back
Compared with (to produce per year in terms of 600,000 tons of alkene)
| Serial number | Project name | Specification | Before the present embodiment | After the present embodiment |
| 1 | Isoplanar temperature difference in reactor | 10~15 DEG C | 0~5 DEG C | |
| 2 | Spray nozzle clogging situation | It is easy blocking | It does not block | |
| 3 | Gas distributor clears up frequency | Annual cleaning 3 times or more | It does not need to clear up | |
| 4 | The catalyst consumption of alkene per ton | Methanol-to-olefins special-purpose catalyst | 2kg | 0.5kg |
| 5 | Catalyst carbon deposition situation | Catalyst carbon deposition is serious | Catalyst carbon deposition is not serious | |
| 6 | Reactor production capacity | 600000 tons of alkene/years | 700000 tons of alkene/years |
As shown in Table 3, the combined gas distributor of the present embodiment and methanol-to-olefins fluidized-bed reactor be fundamentally
It solves the problems, such as that large-scale methanol-to-olefins fluidized-bed reactor gas is unevenly distributed and spray nozzle clogging, substantially increases anti-
The stability for answering device to run, reduces the consumption of catalyst, alleviates the carbon distribution of catalyst, improve the production energy of reactor
Power.
A kind of combined gas distributor of embodiment 4 and methanol-to-olefins fluid bed regenerator
A kind of combined gas distributor, as shown in Figure 1, including a gas distributor and secondary air distributor；Institute
Stating a gas distributor includes being substantially disposed in conplane gas distribution general pipeline 11, gas distribution arms 12 and nozzle
13, gas distribution general pipeline 11 are connected with gas distribution arms 12, and nozzle 13 is uniformly arranged on gas distribution general pipeline 11 and gas point
On cloth branch pipe 12；The secondary air distributor includes the lower layer's porous plate 21 and upper layer porous plate set gradually from lower to upper
20, every laminate has interlaced hole；The secondary air distributor is set to above a gas distributor.
Gas distributor is connected to gas inlet tube 10 by pipeline.
The gas distribution general pipeline 11 is connected to gas inlet tube 10；The gas distribution arms 12 are circular ring type (such as Fig. 2
It is shown) or the arrangement (as shown in Figure 3) of comb formula, center line is located in same level.
Open Side Down for the nozzle 13, including nozzle orifice plate 131 and blast tube 132, the court at an angle of blast tube 132
It is as shown in Figure 8 to reactor bottom end socket 40().
The certain angle is 0 °~45 °.
21 distribution hole is that equilateral triangle arrangement (is shown in Fig. 4 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
5), upper layer porous plate 20 and 21 vertical interlaced of lower layer's porous plate, i.e. upper layer porous plate 20 and lower layer's porous plate 21 are staggered 90 ° in vertical
Straight staggeredly mode.
Or 21 distribution hole is that concentric arrays (are shown in Fig. 6 and figure respectively on the upper layer porous plate 20 and lower layer's porous plate
7), upper layer porous plate and lower layer's porous plate are staggered certain angle.
Rforated plate bracing frame 22 is provided between lower layer's porous plate 21 and upper layer porous plate 20.
Meanwhile the present embodiment additionally provides a kind of methanol-to-olefins fluid bed regenerator, is furnished with the combined type gas
Body distributor.
In methanol-to-olefins fluid bed regenerator, progress catalyst carbon deposition is reacted with oxygen combustion, reactional equation
Formula are as follows:
C + O2= CO2(strong exothermal reaction)
Before fluid bed regenerator operation, methanol-to-olefins catalyst to be regenerated is first packed into regenerator shell 50
It is interior.Air after air blower pressurizes enters regenerator by gas inlet tube 10, successively passes through the gas of a gas distributor
After being distributed general pipeline 11, gas distribution arms 12, gas is equably sprayed from each nozzle 13 down, and blows catalyst granules ease
It dissipates and forms fluidisation；At this time gas entrained catalyst particles successively pass through secondary air distributor lower layer's porous plate 21 and upper layer it is more
Orifice plate 20, equably by the catalyst fluidization in regenerator.
After fluid bed regenerator normally fluidizes, due to the lower layer's porous plate 21 and upper layer porous plate 20 of secondary air distributor
On distribution hole control certain gas flow rate so that the catalyst granules by upper layer porous plate 20 can not return to lower part
Space, therefore, catalyst granules can be constantly blown on upper layer porous plate 20 in the space below secondary air distributor
Side, in this way, the space below secondary air distributor forms dilute-phase zone, catalyst particles when fluid bed regenerator operates normally
Grain is transferred to the space of 20 top of upper layer porous plate, and catalyst is utilized effectively.
After regenerator stops fluidizing, catalyst granules will largely be fallen after rise to secondary air distributor, then successively be passed through
The distribution hole of secondary air distributor upper layer porous plate 20 and lower layer's porous plate 21 is crossed, is slowly fallen after rise to bottom, at this point, secondary gas
Body distributor, which plays the role of barrier a large amount of catalyst granules moments, to be fallen after rise to bottom, so that below secondary air distributor
Space catalyst granules is in rarefaction, to solve the problems, such as that gas distributor is easy blocking.
By using the combined gas distributor of the present embodiment, the straight of methanol-to-olefins fluid bed regenerator can be made
Trouble-free operation is remained to when diameter is up to 8 meters.
Combined gas distributor and methanol-to-olefins fluid bed regenerator operation result are as shown in table 4.
A kind of combined gas distributor of table 4 and the overall target ratio of methanol-to-olefins fluid bed regenerator application front and back
Compared with (to produce per year in terms of 600,000 tons of alkene)
| Serial number | Project name | Specification | Before the utility model | After the utility model |
| 1 | Isoplanar temperature difference in regenerator | 10~15 DEG C | 0~5 DEG C | |
| 2 | Spray nozzle clogging situation | It is easy blocking | It does not block | |
| 3 | Regenerator normally fluidizes the time | 12~24 hours | 1~2 hour | |
| 4 | Gas distributor clears up frequency | Annual cleaning 3 times or more | It does not need to clear up | |
| 5 | The catalyst consumption of alkene per ton | Methanol-to-olefins special-purpose catalyst | 2kg | 0.5kg |
| 6 | Catalyst regeneration efficiency | 90% | 95% | |
| 7 | Regenerator processing capacity | 600000 tons of alkene/years | 700000 tons of alkene/years |
As shown in Table 4, the present embodiment combined gas distributor and methanol-to-olefins fluid bed regenerator fundamentally solve
Large-scale methanol-to-olefins fluid bed regenerator gas of having determined is unevenly distributed and the problem of spray nozzle clogging, substantially increases regeneration
The stability of device operation, reduces the consumption of catalyst, improves the regeneration efficiency of catalyst, increase the processing energy of regenerator
Power.
Finally, it should be noted that above embodiments are only to illustrate the technical solution of the utility model rather than to this realities
It is gone back on the basis of above description and thinking for those of ordinary skill in the art with the limitation of novel protected range
It can make other variations or changes in different ways, there is no necessity and possibility to exhaust all the enbodiments.It is all
It is practical new to should be included in this for made any modifications, equivalent replacements, and improvements etc. within the spirit and principles of the utility model
Within type scope of protection of the claims.
Claims (8)
1. a kind of combined gas distributor, which is characterized in that including a gas distributor and secondary air distributor；It is described
Gas distributor includes being substantially disposed in conplane gas distribution general pipeline (11), gas distribution arms (12) and nozzle
(13), gas distribution general pipeline (11) is connected with gas distribution arms (12), and nozzle (13) is uniformly arranged on gas distribution general pipeline
(11) and in gas distribution arms (12)；The secondary air distributor includes the lower layer's porous plate set gradually from lower to upper
(21) and upper layer porous plate (20), every laminate have interlaced hole；The secondary air distributor is set to gas point
Above cloth device.
2. combined gas distributor according to claim 1, which is characterized in that a gas distributor and gas into
Mouth pipe (10) connection.
3. combined gas distributor according to claim 1, which is characterized in that gas distribution general pipeline (11) and gas
Inlet tube (10) connection；The gas distribution arms (12) are that circular ring type or comb formula arrange, and center line is located at same level
On face.
4. combined gas distributor according to claim 1, which is characterized in that Open Side Down for the nozzle (13), including
Nozzle orifice plate (131) and blast tube (132), at an angle towards reactor bottom end socket (40).
5. combined gas distributor according to claim 1, which is characterized in that the upper layer porous plate (20) and lower layer are more
Distribution hole on orifice plate (21) is equilateral triangle arrangement, upper layer porous plate (20) and lower layer's porous plate (21) vertical interlaced.
6. combined gas distributor according to claim 1, which is characterized in that the upper layer porous plate (20) and lower layer are more
Distribution hole on orifice plate (21) is concentric arrays, and upper layer porous plate (20) and lower layer's porous plate (21) are staggered certain angle.
7. combined gas distributor according to claim 1, which is characterized in that lower layer's porous plate (21) and upper layer are more
Rforated plate bracing frame (22) are provided between orifice plate (20).
8. a kind of fluidized-bed reactor, which is characterized in that including the described in any item combined gas distributions of claim 1~7
Device.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108435105A (en) * | 2018-05-29 | 2018-08-24 | 尹明大 | A kind of combined gas distributor and fluidized-bed reactor |
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2018
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108435105A (en) * | 2018-05-29 | 2018-08-24 | 尹明大 | A kind of combined gas distributor and fluidized-bed reactor |
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