CN106943965A - A kind of gas-solid fluidized bed reactor gas-solid separating method - Google Patents
A kind of gas-solid fluidized bed reactor gas-solid separating method Download PDFInfo
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- CN106943965A CN106943965A CN201710185208.9A CN201710185208A CN106943965A CN 106943965 A CN106943965 A CN 106943965A CN 201710185208 A CN201710185208 A CN 201710185208A CN 106943965 A CN106943965 A CN 106943965A
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
- B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
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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
- B01J8/38—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 with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—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 with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—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 with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
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Abstract
The present invention relates to gas solid separation technical field, specifically related to a kind of gas-solid fluidized bed reactor gas-solid separating method, this method includes reacting gas and collects the gentle solid separation process of process, reacting gas collects process and is provided with reaction gas accumulation regions (20), and gas solid separation process is provided with gas-solid preseparator (2), two-stage series connection cyclone separator；Gas-solid fluidized bed reactor logistics (11) realizes that reacting gas is collected into reaction gas accumulation regions (20)；Logistics (11C) after gas-solid pre-separation is first after gas-solid preseparator (2) carries out pre-separation, it is delivered directly to the first order cyclone inlet (32) of two-stage series connection cyclone separator, or first order cyclone inlet (32) is entered back into after being introduced into the further reduction catalyst content of settlement space (13), carry out gas solid separation.The separation method not only improves the Quick stop of gas-solid fluidized bed reaction, also reduces the catalyst carrying amount of fluidized-bed reactor gas, reduces catalyst emission consumption.
Description
Technical field
The present invention relates to gas solid separation technical field, and in particular to a kind of gas-solid fluidized bed reactor gas-solid separating method,
It is especially adapted for use in that the catalyst such as methanol hydrocarbon products price is high, needs that control catalyst breakage is few, catalyst emission is few
The catalyst separation of course of reaction.
Background technology
In gas-solid fluidized bed course of reaction, either limitation of the environmental protection to dust emission still reduces catalyst consumption expense
The need for, gas-solid separator is required for.Especially to high processes of catalyst price such as picture methanol-to-olefins, catalyst stack less
Economy is more protruded.
In prior art, gas-solid fluidized bed reactor completes gas solid separation using the cyclone separator of two-stage series connection, due to
Cyclone inlet gas is more containing catalyst, two stage cyclone separator can not meet increasingly improve to catalyst emission
Limitation is required, while because the loss of catalyst increases running cost.
In addition, gas-solid separation equipment is with a height of target of separative efficiency in prior art, efficiency is also pressed in gas-solid separator design
Highest condition is carried out, and does not account for the catalyst breakage problem caused in separation process.
Generally gas-solid fluidized bed reaction regeneration process catalyst discharge consumption be attributed to gas-solid separation equipment efficiency it is low,
By using more " efficiently separating equipment ", or it is further added by separation equipment solution.When requiring reduction dust discharge amount, prior art
In by increase catalyst reclaimer method improve gas-solid separating effect.
The smaller solid gas solid separation of size is more difficult to.The size of gas-solid separating effect and solid particle, especially small
The quantity of grain is relevant.Catalyst emission consumption more important reason is probably to cause catalyst breakage during plant running in fact
It is on the high side；And gas-solid separation equipment is to cause these catalyst breakages, produce short grained major reason in itself, catalyst is added
Recovery difficult.Existing gas-solid separation equipment, such as cyclone separator, vortex flow quick grades, gas flow rate in 16m/s~23m/s, and
It is rotational flow.The effect of centrifugal force makes catalyst occur to touch mutually and with equipment solid material during gas solid separation
Hit, necessarily cause catalyst abrasion to crush.And it is difficult to reclaim small less than less than 15 microns that cyclone separator, vortex flow quick, which grade,
Particle.So that catalyst attrition is reduced, Luoyang engineering company has been separately provided generally outside DMTO reactors in FCC regenerators
" third level cyclone separator " used, further reclaims the small catalyst particle of 10 microns；In addition also in product gas washing ring
Section is provided with washings cleaner, it is therefore an objective to further reclaim the catalyst of molecule, improves catalyst recovery yield, reduction
Catalyst attrition.Although improving catalyst recovering effect, investment and energy consumption are added.
Nature is controlled catalyst breakage to gas-solid fluidized bed reactor and just reduces gas solid separation difficulty, can substantially be dropped
Low catalyst run loss rate, and gas-solid separation equipment problem just become it is simple.Control and reduction catalyst breakage is in engineering
The problem of being contemplated that solution, also has obvious benefit to methanol-to-olefins technology.
The content of the invention
Goal of the invention：
The purpose of the present invention is to provide a kind of low solid breakage for gas-solid fluidized bed reactor (including catalyst regenerator)
The gas-solid separating method of rate, reaches the purpose of reduction catalyst consumption and discharge dustiness.
The gas-solid fluidized bed reactor gas-solid separating method of the present invention is as follows：
This method includes reacting gas and collects the gentle solid separation process of process, and it is poly- provided with reaction gas that reacting gas collects process
Ji Qu, gas solid separation process is provided with gas-solid preseparator, two-stage series connection cyclone separator；The reaction gas accumulation regions are arranged on
The top of gas-solid fluidized bed reactor, gas-solid fluidized bed reactor logistics (i.e. gas-solid fluidized bed reaction gas and the catalyst carried)
Realize that reacting gas is collected into reaction gas accumulation regions；In reaction gas accumulation regions, outlet sets gas-solid handling and conveying pipe, gas-solid thing
Stream delivery pipe is connected with the inlet tube of gas-solid preseparator, and gas-solid fluidized bed reactor logistics first carries out pre- in gas-solid preseparator
Separation, the logistics after gas-solid pre-separation enters back into top two-stage series connection cyclone separator and further carries out gas solid separation；Gas-solid is pre-
The first order cyclone separator of two-stage series connection cyclone separator is delivered directly to after logistics outflow gas-solid preseparator after separation
Entrance, or be introduced into settlement space and further reduce the first order that two-stage series connection cyclone separator is entered back into after catalyst content
Cyclone inlet, carries out gas solid separation.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, the outlet of gas-solid preseparator and two-stage string
Join the first order cyclone inlet air shooter and connecting tube airtight connection of cyclone separator, after gas-solid pre-separation
Logistics is directly entered first order cyclone separator.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, the outer gas stream of gas-solid preseparator lead to
Cross fairlead and enter air shooter, or enter first order cyclone inlet or second level cyclone inlet, with
Logistics mixing after gas-solid pre-separation.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, gas-solid preseparator by outer cover, inlet tube,
Flow distribution pipe, gas solid separation element, gas outlet tube composition, vertically-mounted inlet tube circumference set two or more cross section
For the flow distribution pipe of rectangle, flow distribution pipe upside is flow distribution pipe upper plate, and downside is flow distribution pipe lower plate, logistics point
Pipe arrangement lower plate and flow distribution pipe upper plate are flat board or arc plate；The horizontal both sides of flow distribution pipe are respectively flow distribution pipe foreboard
With flow distribution pipe back plate, flow distribution pipe foreboard and flow distribution pipe back plate are flat board or arc plate；Flow distribution pipe is exported
Gas solid separation element is connected respectively, and gas solid separation element periphery is vertically arranged outer cover, and outer cover upper end sets gas outlet tube；Outer cover
It is catalyst flow export between lower end and inlet tube.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, inlet tube are the cone of half tilt angles theta；Enter
The gas-solid handling and conveying pipe of mouth bottom of the tube and gas-solid fluidized bed reactor is connected, and end socket is provided with the top of inlet tube.Preferably, entrance
Half tilt angles theta of pipe is less than 15 °.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, gas solid separation element uses cyclonic separation
Device or cyclone separator；During using cyclone separator, cyclone separator is designed as circumferentially revolving in inlet tube outer inlet pipe axial line
Rotation structure, is R1 close to the inner side radius of curvature of inlet tube, and lateral curvature radius is R2, and gas solid separation component outlet cross section is
Circular or rectangle.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, sets gas between outer cover and inlet tube
Body fairlead, gas solid separation component outlet forms gas solid separation area outside gas fairlead between gas fairlead and outer cover,
Gas draw-out area is formed between gas fairlead and inlet tube, gas fairlead upper end is connected with gas outlet tube, gas vent
Pipe diameter≤gas draws pipe diameter.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, flow distribution tube inlet gas flow rate is small
In 12m/s；Flow distribution pipe outlet gas velocity is less than 12m/s.Preferably, flow distribution tube inlet gas flow rate is less than 9m/
s；Flow distribution pipe outlet gas velocity is less than 10m/s.In the present invention, preseparator outer cover diameter presses the gas that cross section taken in correspondence is accumulated
Rate of flow of fluid is determined less than 5m/s.
Above-mentioned gas-solid fluidized bed reactor gas-solid separating method, further, the flow distribution pipe lower plate and logistics
Distribution pipe upper plate is flat board, and the inclination angle of flow distribution pipe lower plate and the inclination angle of flow distribution pipe upper plate are less than 45 °；Or logistics point
Pipe arrangement lower plate and flow distribution pipe upper plate are arc plate, the central angle of flow distribution pipe lower plate and the center of circle of flow distribution pipe upper plate
Angle is less than 90 °；Or flow distribution pipe foreboard and flow distribution pipe back plate are flat board, the inclination angle of flow distribution pipe foreboard and logistics
The inclination angle of distribution pipe back plate is less than 30 °；Or flow distribution pipe foreboard and flow distribution pipe back plate are arc plate, flow distribution pipe
The central angle of foreboard and the central angle of flow distribution pipe back plate are less than 90 °.
During specific implementation, equipment components material surface sets wearing layer.
In the present invention, the gas-solid fluidized bed reactor refers to that gas superficial flow velocity is arrived less than turbulent fluidized bed in reactor
The flow velocity or solid of recirculating fluidized bed transition point, catalyst internal circulating load are less than the fluidized-bed reaction of reaction regeneration process internal circulating load
Process.Gas-solid fluidized bed reactor described in the inventive method is academicly being subdivided into bubbling fluidized bed, turbulent fluidized bed and circulation
Fluidized-bed reaction process.
The effect of invention
The present invention for gas-solid fluidized bed reactor provide a kind of low catalyst breakage rate, low catalyst discharge capacity gas-solid
Separation method, the separation method not only improves the Quick stop of gas-solid fluidized bed reaction, also reduces fluidized-bed reactor gas
Catalyst carrying amount, reduces catalyst emission consumption.
Brief description of the drawings：
Fig. 1 is the apparatus structure schematic diagram of embodiment of the present invention one；
Fig. 2 is gas-solid preseparation arrangement schematic diagram in Fig. 1；
Fig. 3 is flow distribution tubular construction schematic diagram in Fig. 2；
Fig. 4 is flow distribution pipe cross-sectional view for A direction views in Fig. 3；
Fig. 5 is connecting tube cross-sectional structure schematic diagram in Fig. 1；
Fig. 6 is embodiment of the present invention two devices structural representation；
Fig. 7 is gas-solid preseparation arrangement schematic diagram in Fig. 6；
Fig. 8 is B-B direction view in Fig. 7；
Fig. 9 is the another form of structural representation of gas-solid preseparator in Fig. 6；
Figure 10 is C-C direction views in Fig. 9；
Figure 11 is the apparatus structure schematic diagram of embodiment of the present invention three；
Figure 12 is gas-solid preseparation arrangement schematic diagram in Figure 11；
Figure 13 is flow distribution pipe partial structurtes enlarged drawing in Figure 12.
Explanation is numbered in figure：
0 gas-solid fluidized bed reactor；20 reaction gas accumulation regions；1 housing, 11 gas-solid fluidized bed reactor logistics, 11C gas-solids
Logistics after pre-separation, the outer gas stream of 11B gas-solids preseparator, 11D catalyst, 12 reactors discharge gas, 13 sedimentations are empty
Between, 14 catalyst outlets, the outlet of 15 reactor product gas, 2 gas-solid preseparators, 21 inlet tubes, 21A gas-solid handling and conveying pipes,
22 gas-solid preseparator cyclone inlets, 22A flow distributions pipe (i.e. first order cyclone inlet connecting tube), 22A-
1 flow distribution pipe lower plate, 22A-3 flow distribution pipe upper plates, 22A-2 flow distribution pipe foreboards, 22A-4 flow distribution pipe back plates,
23 gas solid separation elements, 23B cyclone separator gas outlet tubes, 23C separating catalyst down-comers, 24 air-flow draw-out areas, 25 gas
On body outlet, 26 air shooters, 27 outer covers, 28 gas fairleads, the flow distribution pipe lower plate angles of α 1, the flow distribution pipes of α 2
Plate angle degree, the flow distribution pipe lower plate central angles of α 3, the flow distribution pipe upper plate central angles of α 4, Θ inlet tube semi-cone angles, the logistics of β 1 point
Pipe arrangement foreboard angle, the flow distribution pipe back plate angles of β 2, the flow distribution pipe foreboard central angles of β 3, the flow distribution pipe back plate centers of circle of β 4
Radius of curvature on the inside of angle, R1, R2 lateral curvature radiuses, R3 flow distribution pipe lower plate radius of curvature, R4 flow distribution pipes upper plate is bent
Rate radius, D1 inlet tube stream inlet diameters, D2 inlet tube top end diameters, D3 gases draw pipe diameter, and D4 gas outlet tubes are straight
Footpath, D5 outer cover diameters, 3 first order cyclone separators, 31 first order cyclone separator solids or catalyst outlet pipe, 32 first order
Cyclone inlet, 32A connecting tubes, 32A-1 connecting tube lower plates, 32A-3 connecting tube upper plates, 32A-2 connecting tube back plates, 32A-
4 connecting tube foreboards, 33 first order cyclone separator gas vents, 34 fairleads；4 second level cyclone separators, the rotation of 41 second level
Wind separator solid or catalyst outlet pipe, 42 second level cyclone inlets, 43 second level cyclone separator gas vents；
The set connecting tube of 44 first order cyclone separator gas vents and second level cyclone inlet.
Embodiment
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description, it is intended to helps reader to understand
The features of the present invention and essence, but the drawings and specific embodiments content be not intended to limit the present invention can practical range.
Embodiment one：
As Figure 1-4, gas-solid fluidized bed reactor gas-solid separating method of the invention, including reacting gas collect process
Gentle solid separation process, provided with housing 1, wherein reacting gas collects process and is provided with reaction gas accumulation regions 20, gas solid separation process
It is provided with gas-solid preseparator 2, two-stage series connection cyclone separator；Reaction gas accumulation regions 20 are arranged on gas-solid fluidized bed reactor 0
Top, gas-solid fluidized bed reactor logistics 11 be gas-solid fluidized bed reaction gas and carry catalyst enter reaction gas accumulation regions
20 realize that reacting gas is collected；
As shown in Fig. 2 gas-solid preseparator 2 is by outer cover 27, inlet tube 21, flow distribution pipe 22A, gas solid separation element
23rd, gas outlet tube 25 is constituted, and the vertically-mounted circumference of inlet tube 21 sets the flow distribution that two or more cross section is rectangle
Pipe 22A；The outlet of flow distribution pipe connects gas solid separation element 23 respectively, and the periphery of gas solid separation element 23 is vertically arranged outer cover 27,
The upper end of outer cover 27 sets gas outlet tube 25；It is catalyst flow export between the lower end of outer cover 27 and inlet tube 21；Present embodiment
In, inlet tube 21 is straight tube, and inlet tube stream inlet diameter D1 is equal to inlet tube top end diameter D2；
As shown in Figure 3-4, on the upside of flow distribution pipe 22A it is flow distribution pipe upper plate 22A-3, downside is under flow distribution pipe
Plate 22A-1, the horizontal both sides of flow distribution pipe are respectively flow distribution pipe foreboard 22A-2 and flow distribution pipe back plate 22A-4.Specifically
During implementation, flow distribution pipe lower plate 22A-1 and flow distribution pipe upper plate 22A-3 can be flat board, flow distribution pipe lower plate 22A-1
Inclination angle and flow distribution pipe upper plate 22A-3 inclination angle be less than 45 °；Or flow distribution pipe lower plate 22A-1 and flow distribution pipe
Upper plate 22A-3 is arc plate, the central angle and flow distribution pipe upper plate 22A-3 circular arcs of flow distribution pipe lower plate 22A-1 arc plates
The central angle of plate is less than 90 °；Or flow distribution pipe foreboard 22A-2 and flow distribution pipe back plate 22A-4 is flat board, flow distribution
Pipe foreboard 22A-2 inclination angle and flow distribution pipe back plate 22A-4 inclination angle are less than 30 °；Or flow distribution pipe foreboard 22A-2 and
Flow distribution pipe back plate 22A-4 is arc plate, flow distribution pipe foreboard 22A-2 central angle and flow distribution pipe back plate 22A-4
Central angle be less than 90 °；In present embodiment, flow distribution pipe lower plate 22A-1, flow distribution pipe upper plate 22A-3, flow distribution
Pipe foreboard 22A-2 and flow distribution pipe back plate 22A-4 are flat board, and flow distribution pipe lower plate 22A-1 inclination angle is α 1, logistics point
Pipe arrangement upper plate 22A-3 inclination angle is that α 2, α 1 and α 2 are less than behind 45 °, flow distribution pipe foreboard 22A-2 inclination angle and flow distribution pipe
Plate 22A-4 inclination angle is less than 30 °；
During specific implementation, two-stage series connection cyclone separator is provided with first order cyclone separator 3 and second level cyclone separator
4, first order cyclone separator 3 is provided with first order cyclone inlet 32, first order cyclone separator gas vent 33 and the
Primary cyclone solid or catalyst outlet pipe 31, second level cyclone separator 4 are provided with second level cyclone inlet
42nd, second level cyclone separator gas vent 43 and second level cyclone separator solid or catalyst outlet pipe 41；
During implementation, gas solid separation element 23 can use cyclone separator or cyclone separator, during using cyclone separator,
Cyclone separator is designed as rotating in a circumferential direction structure in inlet tube outer inlet pipe axial line；The exit cross-section of gas solid separation element 23 is
Circular or rectangle；Present embodiment gas solid separation element 23 uses cyclone separator, provided with cyclone separator gas outlet tube 23B
With separating catalyst down-comer 23C；
In the present invention, in reaction gas accumulation regions 20, outlet sets gas-solid handling and conveying pipe 21A, gas-solid handling and conveying pipe 21A
It is connected with the inlet tube 21 of gas-solid preseparator 2, gas-solid fluidized bed reactor logistics 11 is first divided in advance in gas-solid preseparator 2
From the logistics 11C after gas-solid pre-separation enters back into top two-stage series connection cyclone separator and further carries out gas solid separation；Gas-solid is pre-
The first order whirlwind point of two-stage series connection cyclone separator is delivered directly to after logistics 11C outflow gas-solids preseparator 2 after separation
From device entrance 32, or be introduced into settlement space 13 further reduction catalyst content after enter back into two-stage series connection cyclone separator
First order cyclone inlet 32, carry out gas solid separation；In present embodiment, gas-solid preseparator 2 revolves with two-stage series connection
First order cyclone inlet 32 air shooter 26 and the connecting tube 32A airtight connections of wind separator, gas-solid pre-separation
Logistics 11C afterwards is directly entered first order cyclone separator 3；First order cyclone separator gas vent 33 passes through first order whirlwind
Separator gas are exported and the set connecting tube 44 of second level cyclone inlet connects with second level cyclone inlet 42
It is logical；Reactor is discharged gas 12 and discharged from reactor product gas outlet 15, and the catalyst 11D of separation is then drawn by catalyst outlet 14
Go out device；
During specific implementation, as shown in figure 5, being connecting tube upper plate 32A-3 on the upside of connecting tube 32A, downside is connecting tube lower plate
32A-1, the left and right sides is respectively connecting tube foreboard 32A-4 and connecting tube back plate 32A-2；Under connecting tube upper plate 32A-3, connecting tube
Plate 32A-1, connecting tube foreboard 32A-4 and connecting tube back plate 32A-2 can be designed to flat board or arc plate according to requirement of engineering；
On the specific of flow distribution pipe 22A, two-stage series connection cyclone separator, gas solid separation element 23 and connecting tube 32A
Structure, implementation below is similar, is no longer described in detail one by one；
During implementation, the outer gas stream 11B of gas-solid preseparator can enter air shooter 26, Huo Zhejin by fairlead 34
Enter first order cyclone inlet 32 or second level cyclone inlet 42, mixed with the logistics 11C after gas-solid pre-separation
Afterwards, another and entrance two-stage series connection cyclone separator；During specific implementation, fairlead 34 may be provided in on air shooter 26,
On the pipeline or connecting tube that may be alternatively provided at first order cyclone inlet 32 or second level cyclone inlet 42；This implementation
In mode, the outer gas stream 11B of gas-solid preseparator is to be directly entered first order cyclone inlet 32 by fairlead 34,
Mixed with the logistics 11C after gas-solid pre-separation.
Illustrate the implementation process of present embodiment so that methanol produces hydrocarbon reaction as an example：
The gas and carrying catalyst of gas-solid fluidized bed reactor 0 are that gas-solid fluidized bed reactor logistics 11 enters reaction gas
Accumulation regions 20 carry out reacting gas collection；The gas of collection is introduced into gas-solid preseparator 2 through gas-solid handling and conveying pipe 21A and carried out
Pre-separation, enters gas solid separation element 23 from the flow distribution pipe 22A of circle distribution, passes through rotation in gas solid separation element 23
The centrifugal force of generation, separates gas and solid, solid under gravity along separating catalyst down-comer 23C falls downwards,
Logistics 11C after gas-solid pre-separation flows out from gas outlet tube 25, along air shooter 26, first order cyclone inlet 32
It is directly entered in first order cyclone separator 3, now, the outer gas stream 11B of gas-solid preseparator is directly entered by fairlead 34
Enter first order cyclone inlet 32, mixed with the logistics 11C after gas-solid pre-separation, carry out first order cyclonic separation；Solid
With catalyst from first order cyclone separator solid or the falls downward of catalyst outlet pipe 31, gas then enters second level whirlwind point
From second level cyclonic separation is carried out in device 4, reactor is discharged gas 12 and discharged from reactor product gas outlet 15, the catalysis of separation
Agent 11D is then by the ejector of catalyst outlet 14.
Embodiment two：
As shown in fig. 6, the present invention gas-solid fluidized bed reactor gas-solid separating method, including reacting gas collect process and
Gas solid separation process, reacting gas collects process and is provided with reaction gas accumulation regions, and gas solid separation process is provided with gas-solid preseparator
2nd, two-stage series connection cyclone separator；The inlet tube 21 of gas-solid preseparator 2 is assembled by gas-solid handling and conveying pipe 21A and reaction gas
Area outlet connection；
Fig. 7-8 shows a kind of structure type of gas-solid preseparator 2 for present embodiment, by outer cover 27, inlet tube 21,
Flow distribution pipe 22A, gas solid separation element 23, gas outlet tube 25 are constituted；In present embodiment, inlet tube 21 is cone, is entered
Mouth pipe stream inlet diameter D1 is less than inlet tube top end diameter D2, and half tilt angles theta of inlet tube 21 is less than 15 °；Pushed up in inlet tube 21
Portion sets end socket；The vertically-mounted circumference of inlet tube 21 sets the flow distribution pipe 22A that two or more cross section is rectangle, this implementation
It is flow distribution pipe lower plate 22A-1 that mode, which is set on the downside of three flow distribution pipe 22A, flow distribution pipe 22A, and upside is logistics
Distribution pipe upper plate 22A-3, the horizontal both sides of flow distribution pipe are respectively flow distribution pipe foreboard 22A-2 and flow distribution pipe back plate
22A-4；In present embodiment, as Figure 7-8, flow distribution pipe lower plate 22A-1, flow distribution pipe upper plate 22A-3, logistics point
Pipe arrangement foreboard 22A-2 and flow distribution pipe back plate 22A-4 are flat board, and flow distribution pipe lower plate 22A-1 inclination angle is α 1, logistics
Distribution pipe upper plate 22A-3 inclination angle is the (not shown)s of α 2, and α 1 and α 2 are less than 45 °, flow distribution pipe foreboard 22A-2 inclination angle
For β 1, flow distribution pipe back plate 22A-4 inclination angle is less than 30 ° for β 2, β 1 and β 2；Flow distribution pipe outlet connection gas-solid point respectively
From element 23, the periphery of gas solid separation element 23 is vertically arranged outer cover 27, and the upper end of outer cover 27 sets gas outlet tube 25；This embodiment party
In formula, gas solid separation element 23 uses cyclone separator, and cyclone separator is designed as circumferential in inlet tube outer inlet pipe axial line
Rotational structure；As shown in figure 8, the inner side radius of curvature close to inlet tube 21 is R1, lateral curvature radius is R2, gas solid separation member
The exit cross-section of part 23 is circular or rectangle；
Fig. 9-10 is another form structure schematic diagram of present embodiment gas-solid preseparator 2；In present embodiment, thing
Flow point pipe arrangement lower plate 22A-1 and flow distribution pipe upper plate 22A-3 is flat board, and flow distribution pipe lower plate 22A-1 inclination angle is α 1, thing
Flow point pipe arrangement upper plate 22A-3 inclination angle is that α 2, α 1 and α 2 are less than 45 °, flow distribution pipe foreboard 22A-2 and flow distribution pipe back plate
22A-4 is arc plate, as shown in Figure 10, and flow distribution pipe foreboard 22A-2 central angle is β 3, flow distribution pipe back plate 22A-4
Central angle for β 4, β 3 and β 4 be less than 90 °；Other structures form is with the gas-solid preseparator shown in Fig. 7；
In present embodiment, gas fairlead 28 is set between outer cover 27 and inlet tube 21, and gas solid separation element 23 goes out
Mouth forms gas solid separation area, in the He of gas fairlead 28 outside gas fairlead 28 between gas fairlead 28 and outer cover 27
Gas draw-out area 24 is formed between inlet tube 21, the upper end of gas fairlead 28 is connected with gas outlet tube 25, gas outlet pipe diameter
D4≤gas draws pipe diameter D3；It is catalyst flow export between the lower end of outer cover 27 and inlet tube 21；
In present embodiment, two-stage series connection cyclone separator is provided with first order cyclone separator 3 and second level cyclonic separation
Device 4, first order cyclone separator 3 and second level cyclone separator 4 connect one to one, i.e., first order cyclone separator gas goes out
The directly correspondence connection of mouth 33 and second level cyclone inlet 42；First order cyclone inlet 32 and gas outlet tube 25
It is directly connected to；Two-stage series connection cyclone separator is delivered directly to after logistics 11C outflow gas-solids preseparator 2 after gas-solid pre-separation
First order cyclone inlet 32, the outer gas stream 11B of gas-solid preseparator is directly entered the first order by fairlead 34
Cyclone inlet 32, is mixed with the logistics 11C after gas-solid pre-separation.
Present embodiment other parts structure is with embodiment one.
The implementation process of present embodiment is as follows：
After gas-solid fluidized bed reactor logistics 11 carries out reacting gas collection in reaction gas accumulation regions, the gas of collection is through gas
Gu handling and conveying pipe 21A is introduced into gas-solid preseparator 2 and carries out pre-separation, enter gas from the flow distribution pipe 22A of circle distribution
Gu resolution element 23, by rotating the centrifugal force produced in gas solid separation element 23, separates gas and solid, solid is in weight
The lower falls downward of power effect, the logistics 11C after gas-solid pre-separation flows out after being drawn from gas draw-out area 24 from gas outlet tube 25,
It is directly entered in first order cyclone separator 3, now, the outer gas stream 11B of gas-solid preseparator is directly entered by fairlead 34
Enter first order cyclone inlet 32, mixed with the logistics 11C after gas-solid pre-separation, carry out first order cyclonic separation；Solid
With catalyst falls downward, gas, which then enters, carries out second level cyclonic separation in second level cyclone separator 4, reactor discharge gas
The discharger of body 12.
Embodiment three：
As shown in figure 11, gas-solid fluidized bed reactor gas-solid separating method of the invention, including reacting gas collect process
Gentle solid separation process, reacting gas collects process and is provided with reaction gas accumulation regions, and gas solid separation process is provided with gas-solid pre-separation
Device 2, two-stage series connection cyclone separator；The inlet tube 21 of gas-solid preseparator 2 is gathered by gas-solid handling and conveying pipe 21A and reaction gas
Ji Qu outlets connection；
The concrete structure of gas-solid preseparator 2 of present embodiment as illustrated by figs. 12-13, by outer cover 27, inlet tube 21, logistics
Distribution pipe 22A, gas solid separation element 23, gas outlet tube 25 are constituted；In present embodiment, inlet tube 21 is cone, inlet tube
Stream inlet diameter D1 is less than inlet tube top end diameter D2, and half tilt angles theta of inlet tube 21 is less than 15 °；Set at the top of inlet tube 21
End socket；The vertically-mounted circumference of inlet tube 21 sets the flow distribution pipe 22A that two or more cross section is rectangle, flow distribution pipe
It is flow distribution pipe lower plate 22A-1 on the downside of 22A, upside is flow distribution pipe upper plate 22A-3, the horizontal both sides difference of flow distribution pipe
For flow distribution pipe foreboard 22A-2 and flow distribution pipe back plate 22A-4；
In present embodiment, in present embodiment, flow distribution pipe lower plate 22A-1, flow distribution pipe upper plate 22A-3 are circle
Arc plate, flow distribution pipe foreboard and flow distribution pipe back plate are flat board, and flow distribution pipe lower plate 22A-1 central angle is α 3, thing
Flow point pipe arrangement upper plate 22A-3 central angle is that α 4, α 3 and α 4 are less than 90 °, and flow distribution pipe lower plate radius of curvature is R3, logistics point
Pipe arrangement upper plate radius of curvature is R4；The inclination angle and flow distribution pipe back plate inclination angle of flow distribution pipe foreboard are less than 30 °；Flow distribution
Pipe outlet connects gas solid separation element 23 respectively, and the periphery of gas solid separation element 23 is vertically arranged outer cover 27, and the upper end of outer cover 27 is set
Gas outlet tube 25；During specific implementation, gas solid separation element 23 uses cyclone separator, and cyclone separator is designed as in inlet tube
Outer inlet pipe axial line rotates in a circumferential direction structure；
In present embodiment, gas fairlead 28 is set between outer cover 27 and inlet tube 21, and gas solid separation element 23 goes out
Mouth forms gas solid separation area, in the He of gas fairlead 28 outside gas fairlead 28 between gas fairlead 28 and outer cover 27
Gas draw-out area 24 is formed between inlet tube 21, the upper end of gas fairlead 28 is connected with gas outlet tube 25, gas outlet pipe diameter
D4≤gas draws pipe diameter D3；It is catalyst flow export between the lower end of outer cover 27 and inlet tube 21；
In present embodiment, settlement space 13, two are provided between gas-solid preseparator 2 and two-stage series connection cyclone separator
Level cyclones in series is provided with first order cyclone separator 3 and second level cyclone separator 4, first order cyclone separator gas
The directly correspondence connection of outlet 33 and second level cyclone inlet 42；First order cyclone inlet 32, gas outlet tube
25 connect with settlement space；Logistics 11C after gas-solid pre-separation is advanced after flowing out gas-solid preseparator 2 through gas outlet tube 25
Enter settlement space 13, further enter back into first order cyclone inlet 32, gas-solid preseparator after reduction catalyst content
Outer gas stream 11B is in settlement space 13 after preliminary sedimentation, into first order cyclone inlet 32, with gas-solid pre-separation
Logistics 11C mixing afterwards.
Present embodiment other parts structure is with embodiment one.
The implementation process of present embodiment is as follows：
After gas-solid fluidized bed reactor logistics 11 carries out reacting gas collection in reaction gas accumulation regions, the gas of collection is through gas
Gu handling and conveying pipe 21A is introduced into gas-solid preseparator 2 and carries out pre-separation, enter gas from the flow distribution pipe 22A of circle distribution
Gu resolution element 23, by rotating the centrifugal force produced in gas solid separation element 23, separates gas and solid, solid is in weight
The lower falls downward of power effect, the logistics 11C after gas-solid pre-separation flows out after being drawn from gas draw-out area 24 from gas outlet tube 25,
It is introduced into settlement space 13 and isolates partial catalyst, enters back into first order cyclone inlet 32, now, gas-solid pre-separation
The outer gas stream 11B of device also enters first order cyclone inlet 32 by settlement space 13, with the logistics after gas-solid pre-separation
11C is mixed, and carries out first order cyclonic separation；Solid and catalyst falls downward, gas then enter in second level cyclone separator 4
Carry out second level cyclonic separation, the reactor discharge discharger of gas 12.
Embodiment：
Below by taking methanol to olefins reaction as an example, methanol feeds 1,800,000 tons/year, and product is ethene and propylene：
Diameter of the housing 12000mm, if 1 gas-solid preseparator and 18 groups of two-stage series connection cyclone separators, the wherein first order
Cyclone inlet gas flow rate 15m/s, second level cyclone inlet gas flow rate 20m/s；Gas outlet tube passes through
Air shooter and connecting tube are directly directly connected to first order cyclone inlet；Gas is set to draw on air shooter
Outlet pipe, is used as gas stream flow pass outside gas-solid preseparator.
Gas-solid preseparator parameter：
The inlet diameter D1=3200mm of inlet tube 21, Θ=10 °；If cyclone and each 6 of logistics distributor, flow distribution
Device entrance section is accumulated outside 2.0 ㎡, the ㎡ of logistics distributor discharge area 1.6, the ㎡ of cyclone outlet area 1.5, gas-solid preseparator
Cover D5=6500mm, gas fairlead D3=4500mm, gas vent D4=3200mm；Air shooter diameter 3200mm, thing
Fluidic distributor and cyclone cross section are rectangle, and depth-width ratio=2.2, logistics distributor upper and lower plates use arc plate, α 3=20 °, α
4=15 °.
Claims (10)
1. a kind of gas-solid fluidized bed reactor gas-solid separating method, it is characterised in that this method include reacting gas collect process and
Gas solid separation process, reacting gas collects process and is provided with reaction gas accumulation regions (20), and gas solid separation process is provided with gas-solid and divided in advance
From device (2), two-stage series connection cyclone separator；The reaction gas accumulation regions (20) are arranged on the upper of gas-solid fluidized bed reactor (0)
Side, gas-solid fluidized bed reactor logistics (11) realizes that reacting gas is collected into reaction gas accumulation regions (20)；In reaction gas aggregation
Area (20) outlet sets gas-solid handling and conveying pipe (21A), the entrance of gas-solid handling and conveying pipe (21A) and gas-solid preseparator (2)
(21) connection is managed, gas-solid fluidized bed reactor logistics (11) first carries out pre-separation in gas-solid preseparator (2), after gas-solid pre-separation
Logistics (11C) enter back into top two-stage series connection cyclone separator further carry out gas solid separation；Logistics after gas-solid pre-separation
The first order cyclone inlet of two-stage series connection cyclone separator is delivered directly to after (11C) outflow gas-solid preseparator (2)
(32), or it is introduced into settlement space (13) and further enters back into the of two-stage series connection cyclone separator after reduction catalyst content
Primary cyclone entrance (32), carries out gas solid separation.
2. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 1, it is characterised in that gas-solid preseparator (2)
Outlet and first order cyclone inlet (32) air shooter (26) and the connecting tube of two-stage series connection cyclone separator
(32A) airtight connection, the logistics (11C) after gas-solid pre-separation is directly entered first order cyclone separator (3).
3. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 2, it is characterised in that gas-solid preseparator outer gas
Body logistics (11B) enters air shooter (26) by fairlead (34), or enters first order cyclone inlet (32)
Or second level cyclone inlet (42), mixed with the logistics (11C) after gas-solid pre-separation.
4. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 1, it is characterised in that gas-solid preseparator (2)
It is made up of, erects outer cover (27), inlet tube (21), flow distribution pipe (22A), gas solid separation element (23), gas outlet tube (25)
Inlet tube (21) circumference directly installed sets the flow distribution pipe (22A) that two or more cross section is rectangle, flow distribution pipe
It is flow distribution pipe upper plate (22A-3) on the upside of (22A), downside is flow distribution pipe lower plate (22A-1), flow distribution pipe lower plate
(22A-1) and flow distribution pipe upper plate (22A-3) are flat board or arc plate；The horizontal both sides of flow distribution pipe are respectively flow distribution
Pipe foreboard (22A-2) and flow distribution pipe back plate (22A-4), flow distribution pipe foreboard (22A-2) and flow distribution pipe back plate
(22A-4) is flat board or arc plate；The outlet of flow distribution pipe connects gas solid separation element (23), gas solid separation element (23) respectively
Periphery is vertically arranged outer cover (27), and outer cover (27) upper end sets gas outlet tube (25)；Outer cover (27) lower end and inlet tube (21)
Between be catalyst flow export.
5. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 4, it is characterised in that inlet tube (21) is partly to incline
Angle Θ cone；Inlet tube (21) bottom is connected with the gas-solid handling and conveying pipe (21A) of gas-solid fluidized bed reactor (0), entrance
Manage and end socket is provided with the top of (21).
6. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 5, it is characterised in that the half of inlet tube (21)
Tilt angles theta is less than 15 °.
7. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 4, it is characterised in that gas solid separation element (23)
Using cyclone separator or cyclone separator；During using cyclone separator, cyclone separator is designed as in inlet tube outer entrance
Pipe axis rotates in a circumferential direction structure；It is R1 close to the inner side radius of curvature of inlet tube (21), lateral curvature radius is R2；Gas solid separation
Element (23) exit cross-section is circular or rectangle.
8. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 4, it is characterised in that in outer cover (27) and entrance
Setting gas fairlead (28) between (21) is managed, gas solid separation element (23) outlet is outside in gas fairlead (28), in gas
Gas solid separation area is formed between fairlead (28) and outer cover (27), gas is formed between gas fairlead (28) and inlet tube (21) and is drawn
Go out area (24), gas fairlead (28) upper end is connected with gas outlet tube (25), and gas outlet pipe diameter≤gas fairlead is straight
Footpath.
9. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 4, it is characterised in that flow distribution tube inlet gas
Rate of flow of fluid is less than 12m/s；Flow distribution pipe outlet gas velocity is less than 12m/s.
10. gas-solid fluidized bed reactor gas-solid separating method as claimed in claim 4, it is characterised in that the flow distribution pipe
Lower plate (22A-1) and flow distribution pipe upper plate (22A-3) are flat board, the inclination angle (α 1) of flow distribution pipe lower plate (22A-1) and thing
The inclination angle (α 2) of flow point pipe arrangement upper plate (22A-3) is less than 45 °；Or on flow distribution pipe lower plate (22A-1) and flow distribution pipe
Plate (22A-3) is arc plate, the central angle (α 3) of flow distribution pipe lower plate (22A-1) and flow distribution pipe upper plate (22A-3)
Central angle (α 4) is less than 90 °；Or flow distribution pipe foreboard (22A-2) and flow distribution pipe back plate (22A-4) are flat board, logistics
The inclination angle (β 1) of distribution pipe foreboard (22A-2) and the inclination angle (β 2) of flow distribution pipe back plate (22A-4) are less than 30 °；Or logistics
Distribution pipe foreboard (22A-2) and flow distribution pipe back plate (22A-4) are arc plate, the center of circle of flow distribution pipe foreboard (22A-2)
The central angle (β 4) of angle (β 3) and flow distribution pipe back plate (22A-4) is less than 90 °.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020143140A1 (en) * | 2019-01-10 | 2020-07-16 | 清华大学 | Separation system for slurry bed reactor |
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