CN100534602C - Component in gas-solid fluidized beds - Google Patents
Component in gas-solid fluidized beds Download PDFInfo
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- CN100534602C CN100534602C CNB2006101141534A CN200610114153A CN100534602C CN 100534602 C CN100534602 C CN 100534602C CN B2006101141534 A CNB2006101141534 A CN B2006101141534A CN 200610114153 A CN200610114153 A CN 200610114153A CN 100534602 C CN100534602 C CN 100534602C
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Abstract
The invention relates to an inner component used for a gas-solid fluidized bed, which consists of at least two layers of horizontal grates, wherein, each layer of horizontal grates comprise a plurality of mobile areas, and a series of guide vanes are ranked and arranged in the identical direction inside each mobile area, the guide vanes form an angle with the horizontal direction, and the arrangement directions of the guide vanes in the adjacent mobile areas are opposite, thereby facilitating the gas phase and solid phase to generate the cross flow, and the guide vanes inside the corresponding mobile areas of the two upper and lower adjacent horizontal grates are arranged oppositely to facilitate the gas phase and solid phase to flow along a zigzag shape. By using the inner component, not only the stability of the operation can be improved, and the mass transfer efficiency between the bubble phase inside a bed layer and an emulsion phase can be effectively improved, but also the axial back mixing of the gas phase and particulate phase inside the bed layer can be greatly reduced.
Description
Technical field
The invention belongs to technical field of chemical, particularly a kind of component in gas-solid fluidized beds and the fluid bed that is provided with this type inner member.
Background technology
Fluid bed is used industrial having obtained widely owing to the particle transport mode that has good heat transfer and mass-transfer performance and be similar to fluid.Gas-solid fluidized bed is most widely used a kind of in the fluid bed, but because the existence of bubble causes the gas short circuit easily, makes gas flow substantial deviation piston flow, to the obvious effect of reaction.The existence of bubble simultaneously also causes the serious back-mixing of solid particle, when solid particle need be continuously removed, can cause the phenomenon of particle at the time of staying of reactor skewness, causes the average conversion in solid particle exit to reduce.
For bubble crushing and inhibition bubble coalescence, thereby improve fluidization quality effectively; Reduce the back-mixing of gas and solid particle, improve its time of staying distribution, to bring into play gas-solid fluidized bed advantage better, adding inner member is a kind of measure of adopting usually.
Domestic and international reported fluid bed inner member mainly contains horizontal member, vertical member and three kinds of forms of composite component at present.Horizontal member and vertical member only are suitable for using under lower superficial gas velocity, common horizontal member form has porous plate, singly revolves or revolve more guiding inner member etc., but at some special occasions, also use some other forms of inner members, for example the disc-annular shape baffle plate inner members that use in the FCC stripper more.When surpassing certain gas speed, small quantities of particles " air cushion " can appear containing in the horizontal member below, and " moral " will occur between vertical member.The appearance of " air cushion " and " moral " can reduce the production intensity of reactor, and heat transfer and mass transfer are also had certain adverse effect.
Chinese patent CN 85100040A has proposed a kind of composite inner component, two kinds of patterns of two kinds of turriforms and ridged are arranged, this type inner member it is said it is that the organic of horizontal baffle inner member and vertical inner member fused, and can eliminate the appearance of " air cushion " and " moral ", and can carry out industry easily and amplify.This type inner member can bring inconvenience in manufacturing, installation and maintenance process, thereby limit it in industrial extensive use because structure is too complicated but according to the description of this patent document as can be seen.
A series of novel inner member forms that are suitable for commercial Application have appearred in recent years, by bed being divided into numerous less flowing and mass transfer unit, in reaction, play the effect of bubble crushing and restriction bubble coalescence, and standard flowing of gas-solid two-phase, the time of staying of having improved two-phase distributes.This class inner member as FCC stripper and regenerator etc., has demonstrated good result of use by the application on commercial plant.
USP 5,716, and 585 have proposed a kind of waveform filler inner member, are used for FCC stripper.This type inner member is staggered by corrugated screen and forms, and which floor is divided into is placed in the stripper, and gas-solid two-phase circuitous process of flowing in filler has reached the purpose of strengthening contact and mass transfer.It is exactly that regional area forms the fluidisation dead band easily that the stripping filler of this structure has a shortcoming, and under the bigger situation of catalyst quality flow rate, catalyst is easy to generate smooth, the problem such as " bridge formation " that flows.
USP 6,224, and 833 have proposed a kind of fluid bed inner member of being made up of the many groups of tabular components that intersect each other, it is said to improve gas-solid mass-transfer efficiency in the fluid bed greatly, and when as the catalyst stripping inner member, steam stripping efficiency can improve nearly 20 percentage points.But also there is the local fluidization dead band in this stripping filling-material structure, when being used for the spent agent stripping, easily produces problems such as oil gas coking.
CN1403190A has proposed a kind of material filling type inner member that is used for gas-liquid, the gentle liquid-solid system reinforcement of gas-solid mass transfer, and it is formed by a series of panels intersections that have the ligulate inclined hole, thereby plays the effect of bubble crushing, reaches the purpose that improves mass-transfer efficiency.Structure is too complicated but this type inner member is same, has limited its industrial application.
Summary of the invention
One of purpose of the present invention is that a kind of modified grid inner member is provided on the basis of existing technology, this inner member is used for industrial fluidized bed, and not only bubble crushing and suppress the coalescence of bubble effectively improves mass-transfer efficiency, reduce gas-solid two-phase back-mixing, improve the conversion ratio and the selectivity of reaction; And have processing and advantage easy for installation.
Another object of the present invention provides the fluid bed that is provided with described inner member.
For achieving the above object, the invention provides a kind of gas-solid fluidized bed inner member that is used for, this type inner member comprises at least two layers of horizontal grate, every layer of horizontal grate is made up of a plurality of flow regions, arrange in the same way in each flow region a series of guide vanes are set, the setting of these guide vanes and horizontal direction are an angle, and the guide vane in the adjacent flow zone that direction is set is opposite, and in the neighbouring two-layer horizontal grate in the corresponding flow region guide vane oppositely be provided with each other.
For adapting to the design of all kinds of fluid beds, inner member of the present invention should adapt (being generally circle) with the fluid bed inwall that institute's desire is used, and the flow region of composition horizontal grate also can have different shapes.According to preferred specific embodiments of the present invention, every layer of horizontal grate is made up of a plurality of parallel flow regions; Perhaps, every layer of horizontal grate is made up of a plurality of concentric annularly flows zone.
By inner member of the present invention is set in fluid bed, the guide vane that oppositely is provided with in the adjacent flow zone in device operation will make the gas-solid two-phase produce staggered flowing through every layer of grid the time, and the guide vane that oppositely is provided with in the corresponding flow region between neighbouring two-layer grid can make the gas-solid two-phase form " it " font in vertical direction to flow simultaneously.Such type of flow will reach broken air pocket and suppress the effect of bubble coalescence, thereby strengthened the alternate contact effect of gas-solid two, simultaneously also help reducing the back-mixing of gas-solid phase, thereby improve the mass transfer effect between gas-solid and the operating efficiency of fluidized bed plant greatly.
Inner member of the present invention can be widely used in multiple industrial fluidized bed device, is particularly useful for the continuous type device that solid particle constantly shifts out.As the case may be, the preferred parameter designing of inner member of the present invention can have:
The acute angle angle that direction and horizontal direction are set of described guide vane is 30-75 °, spacing between adjacent guide vane is 20-200mm (guide vane in each flow region is provided with substantially parallel, and this spacing promptly refers to adjacent two interlobate vertical ranges in the same flow region); Height of grid is 20-250mm (also can claim grid thickness); The flow region width is 20-250mm (generally speaking, this flow region width is substantially equal to the width of guide vane).
Spacing between the adjacent two layers horizontal grate is doubly height of grid of 0-10 (referring to intermarginal vertical range on the lower edge of upper strata grid and the lower floor's grid).In addition, the general minimum needs of horizontal grate are provided with two-layer, but in order to satisfy the needs of fluidized bed plant, also can have more than 2 layers.
In use can be according to the different requirements of device on performances such as mass transfer and gas-solid back-mixing, by what change guide vane angle, blade pitgh, flow region width, the grid number of plies and the isoparametric mode of spacing be set, satisfy the needs of different device operation.
The adjacent flow of grid is interregional selects to be provided with the dividing plate that adapts with this flow region, also can dividing plate be set, that is, the vertical height of dividing plate be the guide vane height 0-1 doubly, generally also be vertical setting.Dividing plate is set when between flow region, and dividing plate is can be with guide vane contour or a little less than guide vane, the side of guide vane can be connected with described dividing plate and fix this moment; Dividing plate is not set between flow region, and the guide vane in adjacent flow zone is affixed mutually by the side that intersects, and for example, the blade that the adjacent flow zone is intersected by welding or inserting mode interconnects fixing.
The present invention provides a kind of fluid bed simultaneously, is provided with inner member of the present invention in it.When described inner member is provided with in fluid bed, preferably with the basic horizontal setting in the packing section of fluid bed of each layer grid, the vertical interval between the two-layer up and down adjacent grid be the grid oneself height 0-10 doubly.Concrete form and size according to fluid bed, every layer of grid assembling can be processed into the profile that adapts with the reactor wall face, guide vane in each flow region is pre-fixed by designing requirement, then grid layer is fixed on the reactor wall by designing requirement.
Inner member provided by the invention is mainly used in traditional gas-solid fluidized bed (carry bed with respect to fast bed and strength, operating linear velocity is lower), generally in bubbling and the operation of turbulence fluidization zone.More specifically, industrial applicable occasion comprises the stripper of catalytic cracking unit and regenerator, Fischer-Tropsch synthesis device, produces the synthesis reactor of industrial chemicals such as phthalic anhydride, vinyl acetate, propylene cyanogen, butadiene, maleic anhydride and dichloroethanes and other fluidized bed plants that is used for drying, adsorption process etc.
In sum, compared with prior art, adopt component in gas-solid fluidized beds provided by the present invention and be provided with the fluid bed of inner member of the present invention, can be broken effectively in the work and suppress bubble in the fluid bed, thus strengthen the contact effect between the gas-solid two-phase; Inner member of the present invention is simple in structure, can and install by any known mode and means processing, and the while also makes things convenient for maintenance and safeguards; Can also pass through reasonably adjustment structure parameter, reduce the alternate back-mixing of gas-solid, improve its time of staying distribution; And, adopting inner member of the present invention, bed did not have the fluidisation dead band during gas-solid was flowed, and can also reduce the volume of air cushion in bigger gas speed scope, increased the bed effective rate of utilization, improved the operating flexibility of fluid bed.
In a word, inner member provided by the invention can be widely used in multiple fluid bed commercial plant, is particularly useful for the continuous type device that needs solid particle constantly to shift out, can significantly improve flowing and mass transfer of gas-solid two-phase.
Description of drawings
Figure 1A and Figure 1B are a kind of grid form of inner member of the present invention.
Fig. 2 is the example of the another kind of grid form of inner member of the present invention.
Fig. 3 is the arrangement method schematic diagram of grid inner member of the present invention in fluid bed.
Fig. 4 is that the ciculation fluidized device that is provided with inner member of the present invention carries out the schematic diagram that cold conditions is tested.
Fig. 5 is for adopting the stripper and the conventional disc ring baffle stripper steam stripping efficiency comparison diagram of inner member of the present invention.
The specific embodiment
Further specify fluid bed inner member provided by the present invention and adopt the characteristics of the fluid bed of this inner member below in conjunction with accompanying drawing, but therefore the present invention is not subjected to any restriction.
Embodiment one
See also shown in Figure 1A and Figure 1B, provided the grid form of the inner member of the present invention's one specific embodiment.This type grid inner member global shape is designed to circle for the shape (being generally circular) that adapts to cross section in the fluid bed, the main member of forming every layer of grid comprises dividing plate 1 and guide vane 2, guide vane 2 parallel are set as a plurality of row, every row blade is from the horizontal by certain angle and substantially parallel setting, and the inclination mode between the adjacent two row blades 2 is opposite.Dividing plate 1 is vertical setting, height is basic identical or a little less than height of grid (as shown in phantom in Figure 2) with height of grid, this moment, the side or the bilateral of guide vane were welded on dividing plate 1 according to the angle of setting, and blade 2 and dividing plate 1 are connected and fixed are one, formed flow region between the dividing plate.Also dividing plate can be set, can directly be solidly connected with each other adjacent two row guide vanes 2 respectively this moment to intersect mode, for example by modes such as welding, grafting, every row guide vane self becomes a flow region (that is, the structure among Fig. 2 does not comprise dotted line).
Shown in Figure 1A, each sheet guide vane of square Regional Representative of every band oblique line wherein, thick lines are represented the limit of blade top, hachure is represented the limit of blade below.Figure 1B provided A-A among Figure 1A to cutaway view, reflected guide vane arrangement in vertical direction.Comprehensive Figure 1A and 1B are as can be seen, this grid (fluid bed cross section) is divided into a plurality of parallel flow regions, a series of substantially parallel guide vanes 2 are set in each flow region, the water conservancy diversion direction of the guide vane 2 in the same flow region is basic identical, and the water conservancy diversion direction of the blade 2 of adjacent flow region is opposite.
As shown in Figure 1A and 1B, the flow region width W is 20-250mm, preferred 40-150mm, every layer of height of grid H are 20-250mm, preferred 50-150mm, guide vane space D are 20-200mm, preferred 30-120mm, blade 2 is 30-75 ° with the acute angle angle α (can reflect the water conservancy diversion direction) of horizontal plane, preferred 35-70 °.
After according to the fluid bed section form every layer of grid being processed, be fixed in the fluid bed, see also shown in Figure 3, inner member in fluid bed on the vertical direction with the layout of a determining deviation, each layer grid be the basic horizontal setting in fluid bed, and the guide vane on the same vertical cross-section in the adjacent flow zone that direction is set is opposite, tilt angle alpha can be basic identical, the vertical interval H between the two-layer grid
LBe 0-10 height of grid H doubly, preferred 0.5-5 height of grid H doubly.The several height according to fluidized bed plant of the grid layer of installing reach to be decided the actual needs of mass transfer and back-mixing.
By said structure and set-up mode, on the one hand, in the fluid bed stripping section, on the same horizontal direction,, and make the gas-solid two-phase produce staggered flowing owing to the water conservancy diversion direction of the guide vane 2 in adjacent flow zone in every layer of grid is opposite; On the other hand, on the vertical direction in fluid bed, because the water conservancy diversion direction of the guide vane in the corresponding flow region of neighbouring two-layer grid is opposite, flow and make the gas-solid two-phase form " it " font in vertical direction, thereby play bubble crushing and suppress bubble coalescence, the reduction gas-solid effect of back-mixing mutually, and almost do not have the fluidisation dead band in the bed, thereby significantly improved flowing and mass transfer of gas-solid two-phase.
Embodiment two
See also shown in Figure 2ly, provided the grid form of the inner member of another specific embodiment of the present invention.Be installation requirements (adapting to cross section in the fluid bed), the global shape of the grid of this embodiment is circular substantially.Different with Figure 1A and Figure 1B is, the flow region of the grid of this embodiment is set to a series of concentric annulars, and dividing plate 1 is an annular.A series of guide vanes 2 (with each sheet guide vane of square region representation of every band oblique line in scheming, wherein thick lines are represented the limit of blade top, and hachure is represented the limit of blade below) are set, water conservancy diversion direction basically identical in each annularly flow zone.And the water conservancy diversion direction of the guide vane 2 in the adjacent annularly flow zone is opposite.Equally, dividing plate 1 (or claiming baffle plate) also can be cancelled, and directly adjacent guide vane 2 directly is fixed together.
In the grid inner member of this type structure, the less border circular areas of curvature of centre 3 also can improve the inner member structure of fluidisation behavior for other because the inconvenience of blade processing can be adopted the venetian blind type horizontal member.When this central area was not provided with any member, the grid of this embodiment integral body was annular, thereby is specially adapted to have in the fluid bed of ring section, for example has in the FCC stripper of interior riser, and this annular inner member is sheathed on interior riser outer wall.
The angle α of the flow region width W of the grid inner member in the present embodiment, height of grid H, guide vane space D, blade and horizontal plane, and the vertical interval H between each layer grid when being arranged in the fluid bed
LBut the value reference example one of parameter is set with the structures such as set-up mode of guide vane 2.In the fluidized bed process process, flow and because the water conservancy diversion direction of the guide vane 2 in the corresponding flow region of neighbouring two-layer grid is opposite at every layer of grid staggered by the gas-solid two-phase, flow and make the gas-solid two-phase form " it " font in vertical direction, thereby play bubble crushing and suppress bubble coalescence, the reduction gas-solid effect of back-mixing mutually, and almost do not have the fluidisation dead band in the bed, thereby significantly improved flowing and mass transfer of gas-solid two-phase.
Embodiment three
Present embodiment further specifies the implementation result of inner member of the present invention in conjunction with concrete experiment.
See also shown in Figure 4ly, show the general configuration of the cold conditions experimental provision that present embodiment adopted, the purpose of this experiment is the improved action of checking novel inner member of the present invention to spent catalytic cracking catalyst stripper Srteam Stripping effect.As shown in the figure, described device is a ciculation fluidized device, catalyst is promoted to settler 5 in riser 10, with after the two-stage of cyclone separator 4 is separated, enter stripping section 6, after stripping finishes through one-level inertia separator 11, enter storage bin 7, quantitatively add pre-lifter 9 through screw feeder 8, enter into riser 10 again, carry out the next round circulation.The riser 10 diameter 80mm that experiment is adopted, high 4.5m; Stripping section 6 diameters are 200mm, and height overall is 1.5m; Be provided with the inner member of record among the embodiment one in the stripping section 6, flow region 20～40mm, the acute angle inclination angle scope of blade and horizontal plane is 35～60 °, vertical distance range is 20～40mm between grille blades, the height of grid scope is 30～60mm, grid spacing range 30～50 is mm, and 8 layers of grids are set in this stripping section altogether.In the experiment with carbon dioxide as the fluidizing gas of stripping section 6, the air of carrying secretly with the catalyst granules that flows down from settler 5 is simulated the oil gas or the flue gas of catalyst entrainment the industrial stripper.The initial concentration of nitrogen is 78% in the air of catalyst entrainment, and behind the process stripping, nitrogen gas concn constantly reduces, and the reduction value of the nitrogen gas concn in the gas of carrying secretly in the catalyst with stripping section 6 bottoms is as the evaluation criterion of steam stripping efficiency.The computational methods of steam stripping efficiency are as follows:
Wherein, η-steam stripping efficiency, %
y
0The percentage concentration of nitrogen the gas that-catalyst that comes out from riser is carried secretly, %
The percentage concentration of nitrogen in the fluid bed emulsification interphase gas in the y-stripping section, %
Adopt experimental rig same as described above, but adopt 6 layers of traditional disc-annular shape baffle plate to compare experiment at stripping section 6, experiment process is all identical with the experiment of above-mentioned employing inner member of the present invention with other operating condition, calculates steam stripping efficiency at last.
It is 90kg (m that Fig. 5 has provided in the catalyst quality flow rate
2S)
-1Condition under, adopt the stripper and the steam stripping efficiency comparison diagram of conventional disc ring baffle stripper under different superficial gas velocity conditions of above-mentioned inner member.As seen from the figure, adopt the steam stripping efficiency of the stripper of inner member of the present invention on average to exceed 20.9 percentage points than the steam stripping efficiency that adopts the disc-annular shape baffle arrangement.And utilize inner member structure of the present invention can in the broad opereating specification, realize having shown good operating flexibility by stripping efficiently.
Claims (10)
1, a kind ofly is used for gas-solid fluidized bed inner member, it is characterized in that, comprise at least two layers of horizontal grate, every layer of horizontal grate is made up of a plurality of flow regions, arrange in the same way in each flow region a series of guide vanes are set, the setting of these guide vanes and horizontal direction are an angle, and the direction that is provided with of the guide vane in the adjacent flow zone makes the gas-solid two-phase produce staggered flowing mutually on the contrary, and the interior guide vane of corresponding flow region oppositely is provided with each other in the neighbouring two-layer horizontal grate.
2, inner member according to claim 1 is characterized in that, every layer of horizontal grate is made up of a plurality of parallel flow regions.
3, inner member according to claim 1 is characterized in that, every layer of horizontal grate is made up of a plurality of concentric annularly flows zone.
4, inner member according to claim 1 is characterized in that, the spacing between the adjacent two layers horizontal grate is a 0-10 height of grid doubly.
5, inner member according to claim 4 is characterized in that, the spacing between the adjacent two layers horizontal grate is a 0.5-5 height of grid doubly.
6, inner member according to claim 1, it is characterized in that the acute angle angle that direction and horizontal direction are set of described guide vane is 30-75 °, the spacing between adjacent guide vane is 20-200mm, height of grid is 20-250mm, and the flow region width is 20-250mm.
7, according to each described inner member of claim 1-3, it is characterized in that, the interregional dividing plate that adapts with this flow region that is provided with of described adjacent flow, the vertical height of this dividing plate is 0-1 a times of guide vane height.
8, inner member according to claim 7 is characterized in that, the side of guide vane is connected with described dividing plate.
9, inner member according to claim 7 is characterized in that, the guide vane in adjacent flow zone is affixed mutually by the side that intersects.
10, a kind of gas-solid fluidized bed, it is characterized in that be horizontally disposed with any described inner member of the requirement 1-9 that has the right in its packing section, the outer rim of inner member and fluid bed inwall adapt.
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| CNB2006101141534A CN100534602C (en) | 2006-10-31 | 2006-10-31 | Component in gas-solid fluidized beds |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102049224B (en) * | 2009-10-27 | 2013-01-23 | 中国石油化工股份有限公司 | Flow field turbulator |
| CN101912753B (en) * | 2010-08-13 | 2012-01-11 | 中国石油大学(北京) | Composite inner component for gas-solid fluidized bed |
| CN102721070B (en) * | 2012-05-21 | 2015-07-08 | 华电电力科学研究院 | Heat insulating sludge drying incineration device and heat insulating sludge drying incineration method |
| CN102989267B (en) * | 2012-12-12 | 2017-03-29 | 湖南碧绿环保产业发展有限公司 | A kind of rule stream packed bed and its installation method |
| CN104930887A (en) * | 2014-03-18 | 2015-09-23 | 中国石油大学(北京) | Method for improving operation of vertical-tube-bundle gas-solid fluidized bed external heat remover |
| CN106215635B (en) * | 2016-08-31 | 2019-03-01 | 中节能工业节能有限公司 | Spray tower for vent gas treatment |
| CN108889111A (en) * | 2018-08-08 | 2018-11-27 | 中国恩菲工程技术有限公司 | The mercury removal device of flue gas |
| CN111760545B (en) * | 2020-06-30 | 2022-05-06 | 昆山新普发塑料有限公司 | Spider-web-imitated plastic filler |
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