CN212549475U - Efficient-circulation uniform fluidizer and spouted bed - Google Patents
Efficient-circulation uniform fluidizer and spouted bed Download PDFInfo
- Publication number
- CN212549475U CN212549475U CN202021222709.3U CN202021222709U CN212549475U CN 212549475 U CN212549475 U CN 212549475U CN 202021222709 U CN202021222709 U CN 202021222709U CN 212549475 U CN212549475 U CN 212549475U
- Authority
- CN
- China
- Prior art keywords
- spouted bed
- bucket body
- air injection
- fluidizer
- injection bucket
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model discloses a uniform fluidizer and a spouted bed with high-efficiency circulation, wherein the uniform fluidizer is arranged in the spouted bed main body; the fluidizer comprises an air injection bucket body which is axially arranged from the top to the bottom in a tapering and gradually shrinking manner and has an open top, a main nozzle is arranged at the bottom of the air injection bucket body, a plurality of side nozzles are distributed on the side wall of the air injection bucket body, the bottom of the air injection bucket body is also fixed with the bottom end of a rotational flow blade, and the axial central axis of the rotational flow blade is superposed with the axial central axis of the air injection bucket body; the air injection bucket body is arranged at the bottom of the spouted bed main body, the top edge of the air injection bucket body is in contact with the inner wall of the spouted bed main body and is hermetically arranged, and a space between the air injection bucket body and the spouted bed main body is a conical annular air inlet channel; the top ends of the rotational flow blades are flush with the air outlet at the top of the straight pipe section, and the axial central axes of the rotational flow blades are coincident with the axial central axis of the straight pipe section. The utility model discloses even fluidizer makes gas and granule contact rapidly, improves circulation efficiency, improves spouted bed's whole material handling capacity.
Description
Technical Field
The utility model belongs to the chemical industry equipment field relates to spouted bed, concretely relates to even fluidizer and spouted bed of high-efficient circulation.
Background
The column-cone type spouted bed is a highly efficient gas-solid reactor which is developed rapidly at present, and is widely applied to various unit operation processes in the field of chemical production, such as drying, coating, granulation, low-temperature pyrolysis of waste rubber, solution drying and crushing, gasification of low-quality coal, desulfurization of coal-fired flue gas, desulfurization and hydrochloric acid removal of waste incineration flue gas, removal of carbon dioxide and the like.
Spouted beds have been developed for over 50 years and have been available in many forms, with the most widely used, most typical spouted bed being a column-cone type spouted bed, which presents a distinct three-zone flow structure: dilute phase injection zone, dense phase annular space zone and fountain zone. The particles in the spraying area are carried by the high-speed gas and are contacted with the gas in a forward flow mode, and after falling back to the annular space area from the fountain area, the particles slowly move downwards and are contacted with the gas in the annular space area in a reverse flow mode, namely the medium particles of the spraying bed have obvious characteristics of inner and outer layered flow. However, this spouted bed also has some disadvantages for the treatment of fine particles: the annular space area, especially the conical area of the spouted bed, has slow particle movement, the particles are agglomerated and nodular and even have flow dead zones, and the annular space area, the particles and the gas in the spouting area are lack of radial mixing, thereby influencing and reducing the whole material treatment efficiency and the chemical reaction rate of the spouted bed.
Disclosure of Invention
Not enough to prior art exists, the utility model aims to provide a high-efficient endless even fluidization ware and spouted bed solves among the prior art on the basis of guaranteeing that the blind spot does not appear flowing, technical problem that circulation efficiency is not enough.
In order to solve the technical problem, the utility model discloses a following technical scheme realizes:
a spouted bed with high-efficiency circulation comprises a spouted bed main body, wherein the spouted bed main body is divided into a straight pipe section and a conical pipe section which are axially and integrally communicated, the top of the straight pipe section is provided with an air outlet, the bottom of the conical pipe section is provided with an air inlet, and a uniform fluidizer is arranged in the spouted bed main body;
the fluidizer comprises an air injection bucket body which is axially arranged from the top to the bottom in a tapered gradually-shrinking manner and has an open top, a main nozzle is arranged at the bottom of the air injection bucket body, a plurality of side nozzles are distributed on the side wall of the air injection bucket body, the bottom of the air injection bucket body is also fixed with the bottom end of a rotational flow blade, and the axial central axis of the rotational flow blade is superposed with the axial central axis of the air injection bucket body;
the air injection hopper body is arranged at the bottom of the spouted bed main body, the top edge of the air injection hopper body is in contact with the inner wall of the spouted bed main body and is hermetically arranged, and a space between the air injection hopper body and the spouted bed main body is a conical annular air inlet channel;
the top ends of the rotational flow blades are flush with the air outlet at the top of the straight pipe section, and the axial central axes of the rotational flow blades are coincident with the axial central axis of the straight pipe section.
The utility model discloses still protect a high-efficient endless even fluidizer, include that the axial is passed from conicity such as top to bottom and is contracted the setting and open air injection bucket in top, the main nozzle has been seted up to the bottom of air injection bucket, and it has a plurality of side nozzles to distribute on the lateral wall of air injection bucket, and the bottom of air injection bucket still is fixed with the bottom of whirl blade, and the axial central axis of whirl blade coincides with the axial central axis of air injection bucket.
The utility model discloses still have following technical characteristic:
the side nozzles are distributed on the side wall of the air injection bucket body in a sparse-upper-lower-dense mode and are divided into an upper layer, a middle layer and a lower layer, the number of the holes in the same layer in the middle is 2 times of the number of the holes in the same layer in the upper layer, and the number of the holes in the same layer in the lower layer is 2 times of the number of the holes in the same layer in the middle.
The included angle between the side wall of the air injection bucket body and the horizontal plane is 40-60 degrees.
The swirl blades are single-head spiral swirl blades, and the number of rotation turns of the swirl blades is 3-7.
The width of the swirl vane is equal to the inner diameter of the main nozzle.
Compared with the prior art, the utility model, following technological effect has:
(I) the utility model discloses a spouted bed compares in traditional spouted bed, and even fluidization ware inscription is at spouted bed column cone connecting portion, strengthens the radial motion of spouting district and annular space district granule, strengthens granule and jet gas's momentum, heat and mass transfer process. The utility model discloses even fluidizer makes gas and granule contact rapidly, improves circulation efficiency, improves spouted bed's whole material handling capacity.
(II) the utility model discloses a spouted bed compares in traditional spouted bed, introduces the whirl effect and makes the double-phase bigger area of contact that obtains of gas-solid, reduces the production in traditional spouted bed flow blind spot, has reduced the dwell time of material in the bed simultaneously, and the processing to heat-sensitive material has guiding meaning in the industrial and agricultural production.
(III) the utility model discloses an even fluidization ware simple structure is simple in the installation moreover, convenient operation.
Drawings
Fig. 1 is a schematic structural view of the highly efficient circulating spouted bed of the present invention.
Fig. 2 is a schematic structural view of the uniform fluidizer of the present invention.
Fig. 3(a) is a particle volume fraction distribution cloud chart of a conventional spouted bed, in which t is 5s, t is 5.2s, t is 5.4s, and t is 5.6s after stable spout in the bed is respectively selected on an axial section of Y is 0.
Fig. 3(b) is a particle volume fraction distribution cloud chart of example 1, in which t is 5s, t is 5.2s, t is 5.4s, and t is 5.6s after stable spout in the spouted bed with high efficiency is selected on an axial section with Y being 0.
Fig. 4(a) is a cloud graph of the simulated temperature distribution of particles in a conventional spouted bed when the axial section Y is equal to 0, and t is 10s, 10.2s, 10.4s, and 10.6s, which are selected relatively late at the time point in order to ensure the temperature in the bed to reach an equilibrium state.
Fig. 4(b) is a cloud chart of the multi-nozzle spouted bed particle simulated temperature distribution when the axial section Y is equal to 0, t is equal to 10s, t is equal to 10.2s, t is equal to 10.4s, and t is equal to 10.6s, in order to ensure that the temperature in the bed reaches an equilibrium state, and the time point is selected relatively later.
Fig. 4(c) is a simulated temperature distribution cloud chart of the spouted bed particles of the uniform fluidizer when the axial section Y is equal to 0 and the time point t is 10s, 10.2s, 10.4s and 10.6s after the fixed selection in order to ensure the temperature in the bed to reach the equilibrium state.
Fig. 5(a) shows the number of revolutions (rotation) r of the inner swirl blade at the time point where t is 5s, 5.2s, 5.4s, and 5.6s on the axial section Y is 01Case 3Q.
Fig. 5(b) shows the number of revolutions (rotation) r of the inner swirl blade at the time point where t is 5s, 5.2s, 5.4s, and 5.6s on the axial section Y is 02Case 5Q.
Fig. 5(c) shows the number of revolutions (rotation) r of the inner swirl blade at the time point where t is 5s, 5.2s, 5.4s, and 5.6s on the axial section Y is 03Case 7Q.
Fig. 6(a) shows the included angles δ between the air injection bucket and the horizontal plane at the time points t of 5s, 5.2s, 5.4s and 5.6s on the axial section Y of 01The particle volume fraction distribution cloud for the 60 case.
Fig. 6(b) shows the included angles δ between the air injection bucket and the horizontal plane at the time points t of 5s, 5.2s, 5.4s and 5.6s on the axial section Y of 02Particle volume fraction distribution cloud for the 50 case.
Fig. 6(c) shows the included angles δ between the air injection bucket and the horizontal plane at the time points t of 5s, 5.2s, 5.4s and 5.6s on the axial section Y of 03The particle volume fraction distribution cloud for the 40 case.
Fig. 7 shows that on the axial section Y being equal to 0, the air injection bucket body with the selected time points t being equal to 5s, 5.2s, 5.4s and 5.6s respectively has different included angles with the horizontal plane, namely delta1＝60°、δ2＝50°、δ3A cloud of pressure profiles for comparison for the 40 ° case;
FIG. 8 shows the angle delta between the air injection bucket body and the horizontal plane1＝60°、δ2＝50°、δ3The case spouted bed overall bed pressure drop profile was 40 °.
Fig. 9(a) is a cloud chart of solid pressure distribution of the conventional spouted bed at the axial section Y of 0 and at selected time points t of 5s, 5.2s, 5.4s, and 5.6s, respectively.
Fig. 9(b) is a cloud of solid pressure distributions of the spouted bed with high-efficiency circulation, in which t is 5s, 5.2s, 5.4s, and 5.6s, respectively, at the axial section Y is 0.
The meaning of the individual reference symbols in the figures is: 1-a spouted bed main body, 2-a uniform fluidizer and 3-a conical annular air inlet channel; 101-straight pipe section, 102-conical pipe section, 103-air inlet, 104-air outlet; 201-air injection bucket body, 202-main nozzle, 203-side nozzle and 204-swirl vane.
The following examples are provided to explain the present invention in further detail.
Detailed Description
The introduction of the swirl effect into the conventional fluid is a novel secondary flow enhanced heat transfer technology, and simultaneously, the swirl effect is combined with a side nozzle to increase and exchange a more powerful enhanced heat transfer effect with smaller resistance, so that the swirl effect becomes a research hotspot of advanced enhanced heat transfer at present, and the basic mechanism is as follows: when the reactor normally works, part of the fluid is redistributed through the side nozzle and the main nozzle, part of the fluid is sprayed out from the side wall to enable the airflow to have radial velocity, part of the fluid generates strong radial disturbance under the rotational flow effect of the cyclone connected with the main nozzle, the fluid rotates around the blades to enable the fluid to be in contact with particles in a spiral form, radial mixing is enhanced, and the strong fluid disturbance enhances momentum transfer and heat transfer between the fluid and the particles. Flow motion principle is reinforceed based on fluid whirl effect, the utility model discloses will realize the radial motion of fine granule through the gas whirl, destroy the fine granule in spouted bed annular space district, circular cone district and gather to play and reinforce the mixed process of interior granule of spouted bed and fluidic.
It should be noted that, in the present invention, the horizontal plane refers to an axial cross section perpendicular to the axial center axis of the air injection bucket body 201.
It is to be noted that all the components and materials of the present invention are known in the art, and the components and materials are not specifically described.
The following embodiments of the present invention are given, and it should be noted that the present invention is not limited to the following embodiments, and all the equivalent transformations made on the basis of the technical solution of the present application all fall into the protection scope of the present invention.
Example 1:
the embodiment provides a high-efficiency circulating spouted bed, as shown in fig. 1 and 2, which comprises a spouted bed main body 1, wherein the spouted bed main body 1 is divided into a straight pipe section 101 and a conical pipe section 102 which are axially and integrally communicated, the top of the straight pipe section 101 is provided with an air outlet 104, the bottom of the conical pipe section 102 is provided with an air inlet 103, and the spouted bed main body 1 is internally provided with a uniform fluidizer 2;
the fluidizer 2 comprises an air injection bucket body 201 which is axially arranged in a tapering and shrinking manner from top to bottom and has an open top, a main nozzle 202 is arranged at the bottom of the air injection bucket body 201, a plurality of side nozzles 203 are distributed on the side wall of the air injection bucket body 201, the bottom of the air injection bucket body 201 is also fixed with the bottom end of a swirl vane 204, and the axial central axis of the swirl vane 204 is superposed with the axial central axis of the air injection bucket body 201;
the air injection bucket body 201 is installed at the bottom of the spouted bed main body 1, the top edge of the air injection bucket body 201 is in contact with the inner wall of the spouted bed main body 1 and is installed in a sealing manner, and a space between the air injection bucket body 201 and the spouted bed main body 1 is a conical annular air inlet channel 3;
the top ends of the swirl vanes 204 are flush with the air outlet 104 at the top of the straight pipe section 101, and the axial central axes of the swirl vanes 204 are coincident with the axial central axis of the straight pipe section 101.
In the utility model, the spouted bed main body 1 is an inverted-column conical spouted bed.
As a preferable scheme of this embodiment, the distribution of the plurality of side nozzles 203 on the side wall of the air injection bucket body 201 is sparse at the top and dense at the bottom, and is divided into three layers, namely, an upper layer, a middle layer and a lower layer, the number of openings of the middle layer is 2 times that of the upper layer, and the number of openings of the lower layer is 2 times that of the middle layer.
As a preferable scheme of this embodiment, an included angle between the side wall of the air injection bucket body 201 and a horizontal plane is 40 ° to 60 °.
The utility model discloses in, swirl blade 204's the main action is at the air current passageway in the spouted bed main part, introduces the whirl effect in the gaseous phase of mainly in vertical direction motion, makes its part produce the disturbance in footpath.
Specifically, the bottom ends of the swirl vanes 204 are connected with the main nozzles 202 at the bottom of the air injection bucket body 201 in a gapless manner. Therefore, the swirl blades 204 can be ensured to have enough arrangement size and influence space, and the influence of the swirl blades 204 on the internal flow field of the spouted bed main body 1 can be maximized.
As a preferable scheme of the present embodiment, the swirl vane 204 is a single-end spiral swirl vane, and the number of rotations of the swirl vane 204 is 3 to 7.
As a preferable aspect of the present embodiment, the width of the swirl vanes 204 is equal to the inner diameter of the main nozzle 202.
When the high-efficiency circulating spouted bed works, gas entering through the gas inlet 103 is divided into two parts, one part directly enters the straight pipe section 101 through the main nozzle 202 continuously in the axial direction, and a swirl effect is introduced under the action of the swirl vanes 204 to generate radial disturbance; the other part passes through the conical annular air inlet channel 3, enters the air injection bucket body 201 from the side nozzle 203 of the air injection bucket body 201, and then axially enters the straight pipe section 101.
And (3) performance testing:
as an example of a specific highly efficient circulating spouted bed, specific structural dimensions are as follows:
diameter D of air inlet124mm, high H of taper pipe section1115mm, 700mm high of the spouted bed body and diameter D of the straight pipe section2152 mm. The included angle between the conical pipe section and the horizontal plane is 60 degrees.
Aperture D of main nozzlec19mm, bore diameter D of the side nozzles＝4mm。
The side nozzles are distributed on the side wall of the air injection bucket body in a manner of being sparse at the upper part and dense at the lower part, and the number n of the openings on the same layer at the upper part14, the number of openings n in the middle layer2Number n of openings in the lower layer, 83＝12。
The width of the swirl vanes is 19mm and the thickness is 1 mm.
The performance test was performed using the above-described specific high-efficiency circulating spouted bed as an example.
The calculation parameters and boundary conditions of the numerical simulation are shown in tables 1 and 2.
Table 1 spouted bed geometry and numerical simulation parameter set-up
| Model parameters | Parameter value | Model parameters | Parameter value |
| Diameter of cylinder | 152mm | Diameter of inlet | 24mm |
| Height of the whole bed | 700mm | Height of stationary bed | 325mm |
| Angle of the cone | 30° | Particle diameter | 1.41mm |
| Density of particles | 2503kg/m3 | Angle of internal friction of particles | 28.5° |
| Maximum volume fraction of particles | 0.59 | Maximum friction volume fraction of particles | 0.588 |
| Particle recovery coefficient | 0.9 | Operating pressure | 0.1mpa |
| Density of gas | 1.225kg/m3 | Viscosity of gas | 1.7894×10-5Pa·s |
| Step of |
2×10-5s | Calculating |
1×10-4 |
TABLE 2 model boundary condition settings
When the spraying bed works, high-speed gas with certain pressure enters the spraying bed from the gas inlet and is divided into an axial part and a lateral part at the bottom cone, wherein most of gas phase vertically and upwards directly enters the main gas inlet of the uniform cyclone, the gas generates a cyclone effect on an internally connected cyclone impeller and generates disturbance in the radial direction, the air is spirally sent out from the spraying area to enter the fountain area and the annular space area, so that the gas and the solid are efficiently contacted, the two phases are more effectively mixed and continuously rise and enter the fountain area, then under the influence of gravity, the material enters the annular space area along the wall surface of the spraying bed and slowly drops in the annular space area, and finally, under the action of gravity, the particle material returns to the bottom end of the spraying bed; at the moment, the other part of gas enters a gap between the bottom conical surfaces at the inlet, and is blown into the annular space area of the spouted bed obliquely upwards through the open holes on the side wall, more gas phases are introduced into the area with higher solid-phase bulk density, and scene disturbance between gas phases and solid phases is increased, so that the gas-solid phase contact efficiency of the annular space area is greatly enhanced, the boring reciprocating circulation is enhanced, and more efficient physical action or chemical reaction is realized.
Control group 1:
this comparative example is except not installing the utility model discloses an even fluidizer 2, spouted bed lathe bed, other parameters and experimental conditions all are the same as embodiment 1.
Control group 2:
this comparative example is not installed except that the swirl vanes 204 in the uniform fluidizer 2 of the utility model, and the spouted bed body, other parameters and experimental conditions are the same as those of embodiment 1.
Through numerical simulation research, the effect of the uniform fluidizer on the flow in the spouted bed is as follows:
first, the gas volume fraction distribution clouds of example 1 and comparative example were taken on an axial cross section with Y equal to 0, after a stable in-bed spout, t equal to 5s, t equal to 5.2s, t equal to 5.4s, and t equal to 5.6s, respectively.
It can be seen from fig. 3 that with the addition of a uniform cyclone, the central swirl vanes break up the three distinct zones present in conventional spouted beds, the flow pattern is more irregular than in conventional column-cone spouted beds and side-nozzle spouted beds, and the passage created by the breakthrough of the inlet gas into the tightly packed solid phase particles produces a deviation in the z-axis rather than a distribution of the two in the center of the bed as in the former case. But at the same time we can also observe that after the gas-solid two-phase spouted in the bed layer reaches stability, the circulation of the solid phase in the bed can still be observed within a certain time span, compared with the traditional spouted bed and spouted beds only provided with side nozzles, the novel spouted bed emphasizing on the active interference of the internal swirl blades on the gas flow direction can guide the gas flow to enter the annular space region, increase the radial mixing of the two phases and stir partial dead regions, thereby improving the gas-solid contact efficiency of the spouted bed with greater efficiency and improving the inherent defects of the traditional spouted bed.
Secondly, in order to ensure that the temperature in the bed reaches an equilibrium state, when t is 10s, 10.2s, 10.4s and 10.6s, the axial section Y is 0, a cloud chart of the temperature distribution of the particles of the conventional spouted bed, the multi-nozzle spouted bed and the uniform fluidizer spouted bed is selected, and the cloud chart is shown in fig. 4.
The cloud chart of fig. 4 shows that after the internal swirl vanes break the flow direction of the injection region of the spouted bed, the centers of high-energy particles further move in the bed layer along with time, most effective reactions of the spouted bed are concentrated in the surrounding annular space region with larger particle bulk density, and therefore compared with the traditional spouted bed which is concentrated in the bottom of the fountain region and the range of the injection region, the reformed spouted bed can better ensure the full contact between particles at each part and gas, and the treatment efficiency of the whole bed layer on materials is improved.
Thirdly, in the same axial section Y equal to 0, the internal swirl blades with different degrees of rotation, i.e., r, at the time points t equal to 5s, 5.2s, 5.4s, and 5.6s, respectively, are selected1＝3Q、r2＝5Q、r3The case of 7Q was compared as shown in fig. 5.
From the particle volume fraction distribution plot of FIG. 5, the originally axial injected gas tends to move more axially as the swirl vanes within the spouted bed increase in swirl, as shown by the plot when r is1When equal to 3Q, compare with r2＝5Q、r3The two-phase main contact surface of 7Q gas-solid is near the axle center, along with the increase of blade number of turns, the air current removes to the wall under the corresponding effect of whirl, leads to spouted bed one side pressure drop to compare the opposite side and is showing and reduce, and bed one side solid particle volume fraction is showing and is reducing, and the opposite side is closely piling up, leads to whole bed treatment effeciency to reduce. Thus selecting r1The radial disturbance of gas phase to the particle phase can be guaranteed to 3Q, and gas on the wall surface can be concentrated on one side of the spouted bed to cause the reduction of gas-solid contact efficiency.
Fourthly, similarly, at the axial section Y equal to 0, the different angles δ of the air injection bucket body, i.e., the time points t equal to 5s, 5.2s, 5.4s and 5.6s, are selected1＝60°、δ2＝50°、δ3The comparison was made for the 40 case as shown in fig. 6 (particle volume fraction distribution cloud), fig. 7 (pressure distribution cloud), fig. 8 (pressure drop profile).
From the integration of the cloud charts in FIGS. 6 and 7, the spouted bed of the uniform fluidizer is delta2When 50 degrees, the gas phase sprayed into the bed through the side wall open hole compensates for unequal distribution of the internal swirl blades to the gas flow, so that the gas phase is stable and rises in swirl near the axis, the balance is broken again after the inclination angle is reduced, particles on one side of the bed layer are densely accumulated, and the gas flow on one side is concentrated to blow away the particles. Meanwhile, comparing the pressure distribution cloud chart of fig. 7, it can be seen that the pressure of the bottom cone area is increased along with the decrease of the inclination angle of the side wall. Whereas the pressure drop profile 8 shows an overall upward trend, δ1＝60°、δ2Two structures do not differ much when 50 °, but δ3Bed pressure drop at 40 ° compared to δ2Increase by 41.5% for 50 °. Thus comprehensively considering δ2The better solution is 50 degrees.
Fifthly, on the axial section Y being 0, the cases of different structures of spouted beds with time points t being 5s, 5.2s, 5.4s and 5.6s are selected for comparison, as shown in fig. 9(a) and 9(b) of solid pressure distribution cloud charts.
In fig. 9(a) and 9(b), the solid pressure is represented as the difficulty of the solid phase moving along with the gas phase, and from the overall view, the cyclone blades change the movement components of the gas phase in all directions, so that the particle phase in the whole bed layer is more easily driven by the gas flow to be circularly mixed, thereby not only ensuring the reduction of dead zones, but also reducing the retention time of the material in the bed, and having strong significance for some specific industrial scenes such as the drying treatment, breeding and the like of partial heat-sensitive materials (organic materials such as wheat, rice and the like).
To sum up, the utility model discloses an even fluidization ware is on the basis that the side nozzle carries out the first distribution to the import gas, and inside whirl blade has introduced the whirl effect in the bed, has broken the obvious limit between injection zone, annular space district and the fountain district in traditional spouted bed, has more greatly realized the double-phase large tracts of land contact of gas-solid, has promoted the treatment effeciency of bed material, and simple easy hand repacking does not need too big work load simultaneously, can customize the controllable of assurance cost on former spouted bed basis. The utility model discloses an in the research scope, the dominant texture of even fluidization ware is that the lateral wall trompil is delta 50 with radial plane contained angle, and the whirl blade is difficult too big on whole bed rotation number, and other more even are compared in the flow field when r 3Q.
Use the utility model discloses an even fluidizer is applicable to the spouted bed that foundation structure is three-dimensional column cone type, can guarantee effectively that the district of spouting and the solid double-phase intensive mixing of annular space district interior gas, and the radial motion of district and annular space district granule is spouted in the reinforcing, strengthens the transmission that looks meet of annular space district momentum, heat, not only can compensate the inherent defect that traditional spouted bed exists, reduces material bed dwell time simultaneously to improve spouted bed's overall efficiency and productivity effect.
Claims (10)
1. A high-efficiency circulating spouted bed comprises a spouted bed main body (1), wherein the spouted bed main body (1) is divided into a straight pipe section (101) and a conical pipe section (102) which are axially and integrally communicated, the top of the straight pipe section (101) is provided with an air outlet (104), and the bottom of the conical pipe section (102) is provided with an air inlet (103), and is characterized in that a uniform fluidizer (2) is arranged in the spouted bed main body (1);
the fluidization device (2) comprises an air injection bucket body (201) which is axially arranged from the top to the bottom in an equal taper gradually-shrinking mode and is open at the top, a main nozzle (202) is arranged at the bottom of the air injection bucket body (201), a plurality of side nozzles (203) are distributed on the side wall of the air injection bucket body (201), the bottom of the air injection bucket body (201) is further fixed with the bottom end of a swirl vane (204), and the axial central axis of the swirl vane (204) is overlapped with the axial central axis of the air injection bucket body (201);
the jet bucket body (201) is installed at the bottom of the spouted bed main body (1), the top edge of the jet bucket body (201) is in contact with the inner wall of the spouted bed main body (1) for sealing installation, and a space between the jet bucket body (201) and the spouted bed main body (1) is a conical annular air inlet channel (3);
the top ends of the swirl vanes (204) are flush with the air outlet (104) at the top of the straight pipe section (101), and the axial central axis of the swirl vanes (204) is superposed with the axial central axis of the straight pipe section (101).
2. The high-efficiency circulating spouted bed of claim 1, wherein the distribution of the plurality of side nozzles (203) on the side wall of the air-injecting bucket body (201) is sparse from top to bottom, and is divided into an upper layer, a middle layer and a lower layer, the number of openings of the middle layer is 2 times of the number of openings of the upper layer, and the number of openings of the lower layer is 2 times of the number of openings of the middle layer.
3. A high efficiency circulating spouted bed according to claim 1 wherein the side wall of the air-injecting bucket (201) is at an angle of 40 ° to 60 ° to the horizontal.
4. A high efficiency circulating spouted bed according to claim 1 wherein the swirl vanes (204) are single-start helical swirl vanes and the number of revolutions of the swirl vanes (204) is 3 to 7.
5. A high efficiency circulating spouted bed according to claim 1, wherein the width of the swirl vanes (204) is equal to the inner diameter of the main nozzle (202).
6. The utility model provides a high-efficient endless homogeneous fluidization ware, its characterized in that, include that the axial is from top to bottom isotachy progressively contract setting and open-topped jet-propelled bucket body (201), main nozzle (202) have been seted up to the bottom of jet-propelled bucket body (201), it has a plurality of side nozzles (203) to distribute on the lateral wall of jet-propelled bucket body (201), the bottom of jet-propelled bucket body (201) still is fixed with the bottom of whirl blade (204), the axial central axis of whirl blade (204) and the axial central axis coincidence of jet-propelled bucket body (201).
7. The high-efficiency uniform circulating fluidizer of claim 6, wherein said plurality of side nozzles (203) are distributed on the side wall of the air injection bucket body (201) in three layers, namely upper, middle and lower layers, the number of openings of the middle layer is 2 times of the number of openings of the upper layer, and the number of openings of the lower layer is 2 times of the number of openings of the middle layer.
8. The high-efficiency uniform circulating fluidizer of claim 6, wherein said side wall of said air injecting funnel (201) is at an angle of 40 ° to 60 ° with respect to the horizontal plane.
9. A high efficiency circulating homogenous fluidized bed as claimed in claim 6 wherein said swirl vanes (204) are single helical swirl vanes and the number of revolutions of the swirl vanes (204) is 3 to 7.
10. The high-efficiency circulating uniform fluidizer of claim 6, wherein said swirler vanes (204) have a width equal to an inner diameter of the main nozzle (202).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021222709.3U CN212549475U (en) | 2020-06-28 | 2020-06-28 | Efficient-circulation uniform fluidizer and spouted bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021222709.3U CN212549475U (en) | 2020-06-28 | 2020-06-28 | Efficient-circulation uniform fluidizer and spouted bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212549475U true CN212549475U (en) | 2021-02-19 |
Family
ID=74614790
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021222709.3U Active CN212549475U (en) | 2020-06-28 | 2020-06-28 | Efficient-circulation uniform fluidizer and spouted bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212549475U (en) |
-
2020
- 2020-06-28 CN CN202021222709.3U patent/CN212549475U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3202483B1 (en) | Rotational flow and sink flow-coupling integrated system for ultra-clean desulphuration and dedusting and desulphuration and dedusting method therefor | |
| CN207012954U (en) | A kind of gas distributor and organic silicon fluidized bed | |
| US3807705A (en) | Process and apparatus for solids blending | |
| JP2009106862A (en) | Granulator and method of granulation using the same | |
| CN1121575C (en) | Method and arrangement for supplying air to fluidized bed boiler | |
| US20150093295A1 (en) | Gas distributors for circulating fluidized bed reactors | |
| CN212549475U (en) | Efficient-circulation uniform fluidizer and spouted bed | |
| WO2020097657A1 (en) | Fluidized bed facility and method for conveying a solid bulk product | |
| CN108504395B (en) | Coal gasification device | |
| CN109985573B (en) | Hydrogenation reactor for improving liquid phase uniformity | |
| CN111790321A (en) | Efficient-circulation uniform fluidizer and spouted bed | |
| CN202983935U (en) | Reversed spraying nozzle for wet-method smoke washing | |
| CN102538433A (en) | Double-layer air distribution method for fluidized bed dryer and equipment | |
| CN203400626U (en) | Circulating fluidized bed reactor with low-resistance single-tube internal circulation, and function of simultaneous desulfurization and denitrification for smoke | |
| CN112023839A (en) | Gas pre-distributor of fluidized bed reactor | |
| CN103008138A (en) | Reversed-spraying wet-method smoke washing nozzle | |
| CN1207088C (en) | Fluidized bed reactor gases distributing plate | |
| CN114432973A (en) | Tubular gas distributor and gas-solid fluidized reactor | |
| CN215138595U (en) | High-efficient flue gas desulfurization device | |
| CN201023984Y (en) | Solid particle flowing pipe line gas-locked material-discharging non-mechanical device | |
| CN107297187A (en) | A kind of fluidized-bed reactor with helical blade | |
| CN110624482B (en) | Gas distribution plate of step-shaped fluidized bed | |
| CN207294701U (en) | A kind of gasifier nozzle for strengthening mixing | |
| KR101895474B1 (en) | A circulating fluidized bed reactor and reaction method for increasing the residence time of solid particles | |
| CN205803389U (en) | Feeding device in low order fine coal hydrogenation pressurization fast low temperature gas retort |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |