CN112023839A - Gas pre-distributor of fluidized bed reactor - Google Patents
Gas pre-distributor of fluidized bed reactor Download PDFInfo
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- CN112023839A CN112023839A CN202010795947.1A CN202010795947A CN112023839A CN 112023839 A CN112023839 A CN 112023839A CN 202010795947 A CN202010795947 A CN 202010795947A CN 112023839 A CN112023839 A CN 112023839A
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- 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
- 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
- B01J8/34—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 stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
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Abstract
The invention discloses a gas pre-distributor of a fluidized bed reactor, belonging to the field of fluidized bed design. The pre-distributor can improve the uniformity of gas distribution and liquid phase distribution and the stability of the operation of the fluidized bed reactor.
Description
Technical Field
The invention relates to a gas predistributor for a fluidized bed reactor.
Background
The fluidized bed reactor has the characteristics of high mass and heat transfer efficiency, relatively uniform temperature distribution, wider operation range and the like. With the development of fluidized bed reactors in various industrial fields and the enlargement of the scale of equipment, the problem of uniform distribution of gas and liquid in fluidized bed reactors becomes one of the key problems in the large-scale industrial design thereof.
In an industrial fluidized bed reactor, a pre-distributor is arranged above a gas inlet at the bottom of the reactor so as to improve the gas flow distribution at the bottom of the reactor and avoid the phenomenon that gas directly impacts a gas distribution plate to cause uneven gas-liquid distribution below the distribution plate. The uniformity of the dispersion of the gas flow below the distributor plate directly affects the quality of fluidization and the proper operation in the fluidized bed reactor. In the actual production process, a higher liquid content area is often formed below the distribution plate, and then serious particle deposition and particle agglomeration phenomena occur, so that the distributor is blocked by polymers, and the stable operation of the device is directly threatened.
The gas pre-distributor used in the fluidized bed in the prior art has a simpler structure and mainly comprises a gas guide pipe and a fluid director. Wherein, the fluid director can be a general hat type, a conical ring, an annular baffle or a conical cap. The predistributor as used in CN102350275B is in the form of a conical cap and a flow-guiding tube. The gas predistributor adopted by CN102847491A is a combination of a cylindrical structure and a conical structure. CN205517661U is a special circular flow guider. However, the operation result of the industrial device shows that the prior pre-distributor can not realize the uniform distribution of gas phase and liquid phase under the condition of high liquid content, so that the distribution plate has the phenomenon of caking and blocking. Therefore, it is necessary to develop a new pre-distributor with wider operation range and capable of ensuring uniform distribution of gas and liquid even under the condition of high liquid content, so as to improve the stability of the operation of the fluidized bed reactor.
Disclosure of Invention
The invention aims to provide a gas pre-distributor of a fluidized bed reactor, which can diffuse inlet gas or gas-liquid mixture and uniformly distribute the gas or gas-liquid mixture reaching a distribution plate, ensure that liquid phase distribution below the distribution plate of the fluidized bed reactor is relatively uniform, further ensure the fluidization quality of the fluidized bed reactor, reduce wall sticking and blockage of the gas pre-distributor and ensure long-term stable operation of the device.
A gas pre-distributor of a fluidized bed reactor comprises a horizontal annular baffle and a multilayer cone-shaped platform flow guide structure which are sequentially, independently and coaxially arranged along the central axis of a gas inlet pipeline of the fluidized bed reactor, wherein the horizontal annular baffle and the multilayer cone-shaped platform flow guide structure are both positioned in the area between a gas inlet and a gas distribution plate of the fluidized bed reactor, and the horizontal annular baffle is close to the gas inlet; one end of the multilayer cone-shaped platform flow guide structure is close to the horizontal annular baffle and is at the same height, and the other end of the multilayer cone-shaped platform flow guide structure is far away from the horizontal annular baffle.
When gas or gas-liquid mixture enters the inside of the pre-distributor through the gas inlet pipeline, gas is firstly dredged through the multilayer cone-shaped platform flow guide structure, but because the multilayer cone-shaped platform flow guide structure is not close to the gas inlet pipeline, the gas or gas-liquid mixture can pass through the outer side of the multilayer cone-shaped platform flow guide structure, and a horizontal annular baffle is added to ensure that the gas or gas-liquid mixture outside the multilayer cone-shaped platform flow guide structure is uniformly distributed. Meanwhile, the inlet gas is prevented from directly impacting the distribution plate, so that the liquid phase below the distribution plate is not uniformly distributed, and the multilayer conical table diversion structure is set to be a conical cap structure.
The horizontal annular baffle and the multilayer conical table diversion structure are both positioned in the area between the gas inlet of the fluidized bed reactor and the gas distribution plate;
the horizontal annular baffle is close to the gas inlet, and the middle part of the horizontal annular baffle is provided with a diameter Di0Of circular hole of outer diameter DO0；
The bottom end of the multilayer conical table flow guide structure and the horizontal annular baffle are at the same horizontal height;
the multilayer tapered platform flow guide structure is internally provided with at least two layers of structures, the tapered surfaces of the inner structure and the outer structure are parallel, a gap exists between every two tapered surfaces, the bottom end and the top end of the multilayer tapered platform flow guide structure are provided with round holes, and the diameter of the round hole at the bottom end is DbiThe diameter of the top round hole is Dui，i＝1,2,……,n，n≥2。
The multilayer conical table guideThe diameter of the bottom circular hole of the flow structure is Di0>Db1>Db2>……>DbnThe diameter of the top circular hole is in relation to Du1>Du2>……>Dun。
In order to ensure that gas or gas-liquid mixture from a bottom inlet can diffuse around the reactor through a gap between the horizontal annular baffle and the multilayer conical table diversion structure and ensure that the gas or gas-liquid mixture reaching the distribution plate is uniformly distributed, the diameter of a round hole at the bottom end of the first layer conical table diversion structure of the multilayer conical table diversion structure is as follows: di0≥Db1Diameter D of the top circular holeu1The value range is as follows: di0≤Du1≤DO0。
The included angle between the conical surface of the multilayer conical table diversion structure and the central axis of the gas inlet pipeline is 15-75 degrees, preferably 15-60 degrees, and the gas or gas-liquid mixture can be ensured to diffuse around the reactor under the diversion effect.
The vertical distance between the outer side of the horizontal annular baffle and the bottom of the fluidized bed reactor is h, and the area S is recorded1＝hπDO0；S1The vertical cylinder side area between the outer side of the horizontal annular baffle and the bottom of the fluidized bed reactor is shown, and the annular area between the horizontal annular baffle and the bottom of the first layer of conical table diversion structure is S2＝π(Di0 2-Db1 2) The area of a circular hole at the bottom end of the flow guide structure of the first layer of the conical table is S3＝πDb1 2/4，S1、S2、S3The relationship between is S3≤S2≤S1The low liquid phase content area below the distribution plate can be reduced, and the uniform distribution of the liquid phase is realized.
When the number of the layers n of the conical table diversion structure is 2, the area of a bottom circular ring between the first layer and the second layer is S4＝π(Db1 2-Db2 2) The area of the circular hole at the bottom end of the flow guide structure of the second layer of the conical table is S5＝πDb2 2/4, the flow guiding structure of the first layer of conical table and the flow guiding structure of the second layer of conical tableArea S of the bottom ring of the chamber4The area S of a circular hole at the bottom of the conical platform flow guide structure of the second layer is larger than or equal to5Wherein 1.5. ltoreq.S is preferred4/S5Less than or equal to 10, and the gas passing through the flow guide structure of the second layer of conical table and the gas quantity passing between the flow guide structures of the two layers of conical tables are uniformly distributed.
The number n of the layers of the conical table diversion structure is more than or equal to 3, and the area S of a bottom circular ring between the 1 st layer of conical table diversion structure and the 2 nd layer of conical table diversion structure4The bottom circular ring area S between the flow guide structure of the conical table at the No. 2 layer and the flow guide structure of the conical table at the No. 3 layer5Not less than … … and not less than n-th layer of conical platform diversion structure bottom circular hole area Sn+3。
For different size reactors, different size gas predistrikers are used. The specific dimensions can be optimized by computational fluid dynamics software Fluent simulation.
Compared with the existing predistributor, the gas predistributor provided by the invention changes the gas flow field by arranging the horizontal annular baffle and the multilayer cone-shaped platform flow guide structure, can improve the phenomenon of uneven distribution of gas phase, particularly liquid phase, below the distribution plate, reduces the impact of fluid on the local part of the distribution plate, and improves the operation stability of the fluidized bed reactor.
Drawings
FIG. 1 is a schematic view of a gas pre-distributor of a fluidized bed reactor with a two-layer conical-shaped flow guiding structure provided by the invention; wherein, 1 is a gas distribution plate, 2 is a second layer of conical table diversion structure, 3 is a first layer of conical table diversion structure, 4 is a horizontal annular baffle, and 5 is a gas inlet pipeline;
FIG. 2 is a schematic diagram showing structural parameters of a gas pre-distributor of a fluidized bed reactor having a two-layer conical flow guiding structure according to the present invention;
FIG. 3 is a cloud of liquid phase distributions below a distributor plate of a fluidized bed reactor using the predistributor of FIG. 1; wherein the upper figure is a side-section liquid phase distribution cloud picture, and the lower figure is a liquid phase distribution cloud picture below the distribution plate.
FIG. 4 is a cloud of liquid phase distributions below a distributor plate of a fluidized bed reactor using a single cone-cap predistributor; wherein the upper figure is a side-section liquid phase distribution cloud picture, and the lower figure is a liquid phase distribution cloud picture below the distribution plate.
FIG. 5 is a graph of the volume fraction of liquid phase below the distributor plate of a fluidized bed reactor using the predistributor shown in FIG. 1.
Detailed Description
Example 1
As shown in fig. 1, the gas predistributor of the fluidized bed reactor of the present invention comprises a horizontal ring-shaped baffle 4 and a multilayer cone-shaped platform flow guiding structure (an outer layer 3 and an inner layer 2) which are independently arranged in sequence along the central axis of a gas inlet pipeline of the fluidized bed reactor, wherein the horizontal ring-shaped baffle 4 and the multilayer cone-shaped platform flow guiding structure are both located in a region between a gas inlet 5 and a gas distribution plate 1 of the fluidized bed reactor, and the horizontal ring-shaped baffle 4 is close to the gas inlet 5; one end of the multilayer cone-shaped platform flow guide structure is close to the horizontal annular baffle 4 and is at the same height, and the other end of the multilayer cone-shaped platform flow guide structure is far away from the horizontal annular baffle 4. The conical table flow guide structures, the conical table flow guide structures and the annular plate, and the annular plate and the bottom end enclosure of the fluidized bed reactor are connected through rib plates.
For a reactor with the inner diameter of 3000m, the structure of the gas pre-distributor is selected after optimization: the structural parameters of the horizontal ring-shaped baffle 4 are respectively Di0＝700mm,DO0:Di0Is 2-2.5. Selecting two layers of cone-shaped platform flow guide structures, wherein the height of the outer layer 2 is 280mm, and the included angle between the two layers of cone-shaped platform flow guide structures 2 and 3 and the central axis of the gas inlet pipeline 4 is 15-60 degrees. The top circular hole diameter D of the two layers of conical table diversion structures 2 and 3 far away from the horizontal annular baffle 4u1And Du2Maximum gap area S of two-layer conical table flow guide structures 2 and 33The area S of the bottom circular hole close to the horizontal annular baffle 4 with the inner layer5The ratio of the two layers of conical table diversion structures 2 and 3 is 1.5-10, and the diameter D of the bottom circular hole of the horizontal annular baffle plate 4 is close to the two layers of conical table diversion structures 2 and 3b2:Db1The ratio of the two layers of conical table diversion structures 2 and 3 is 1.5-2, and the two layers of conical table diversion structures are close to and far away from the bottom and top round holes D of the horizontal annular baffle plate 4ui:DbiThe ratio of the diameters is 2-5.
Example 2
In a gas-solid fluidized bed reactor with the diameter of 3039mm, air is used as a gas-phase fluidized phase, the apparent operating gas velocity of the fluidized bed is 0.6489m/s, the inlet gas velocity is 17.7m/s, and the simulation is carried out by using Fluent fluid mechanics simulation calculation software. The gas predistributor is adopted in the form of a gas predistributor as shown in figure 1: wherein, the inner diameter and the outer diameter of the horizontal annular baffle 4 are 700mm and 1500mm respectively, and the distance from the gas inlet is 140 mm; two layers of cone-shaped platform flow guide structures are selected, the inner diameter and the outer diameter of one end port, close to the gas inlet pipeline 1, of each of the two layers of cone-shaped platform flow guide structures 2 and 3 are respectively 200mm and 395mm, the gap between the two layers of cone-shaped platform flow guide structures 2 and 3 is 50mm, and the inner diameter and the outer diameter of one end port, far away from the gas inlet pipeline 1, of the two layers of cone-shaped platform flow guide structures 2 and 3 are respectively 800mm and 995 mm. The included angle between the two layers of cone-shaped platform flow guide structures 2 and 3 and the central axis of the gas inlet pipeline 5 is 45 degrees, and the height of the cone-shaped platform flow guide structure is 282.84 mm.
Comparative example 1
In a gas-solid fluidized bed reactor with the diameter of 3039mm, air is used as a gas-phase fluidized phase, the apparent operating gas velocity of the fluidized bed is 0.6489m/s, the inlet gas velocity is 17.7m/s, and the simulation is carried out by using Fluent fluid mechanics simulation calculation software. A gas pre-distributor with a single-layer conical cap is used as a comparative example, wherein the inner diameter and the outer diameter of the horizontal annular baffle 4 are respectively 500mm and 1500mm, and the distance from a gas inlet is 140 mm; the diameters of the conical cap structure close to and far away from the gas inlet pipeline are 395mm and 700mm respectively; the included angle between the conical cap and the central axis is 24 degrees, and the height of the conical table flow guide structure is 369.72 mm.
FIG. 3 is a cloud of liquid phase distributions for a fluidized bed reactor of example 2 operating under conditions to produce DGDA6098 brand high density polyethylene plastic, with liquid phase volume fractions between 0.007 and 0.01. As can be seen from FIG. 3, the horizontal annular baffle 4 at the bottom of the fluidized bed reactor presses the inlet airflow to the wall surface of the seal head, the two layers of conical table diversion structures 2 and 3 with the inclination angle of 45 degrees press the inlet airflow to the horizontal annular baffle 4, and the outer layer 2 and the inner layer 3 of the two layers of conical table diversion structures avoid the direct impact of the inlet airflow on the gas distribution plate 1. The gas velocity distribution in the whole gas pre-distributor is relatively uniform, so that the liquid phase distribution under the drive of the gas phase is relatively uniform and reasonable. Meanwhile, FIG. 4 is a liquid phase distribution cloud chart of a comparative example fluidized bed reactor under the operation condition of producing DGDA6098 brand high density polyethylene plastic by adopting a combination form of a horizontal flow deflector, a flow guide pipe and a conical cap designed in CN102350275B, and the volume fraction of a liquid phase is between 0.007 and 0.01. As can be seen from fig. 4, the use of a single conical cap design results in poor uniformity of liquid phase distribution, localized low velocity zones and regions of high liquid content. The liquid phase obtained in the mode that the horizontal annular baffle plate is combined with the multi-layer conical table flow guide structure is more uniform and reasonable in distribution, and a local low-speed area and an area with high liquid content cannot appear.
FIG. 5 is a liquid volume fraction distribution below the distributor plate for a fluidized bed reactor employing the gas predistributor of example 2. Under the effect of two-layer conical table water conservancy diversion structure 2 and 3 and horizontal cyclic annular baffle 4, gas-liquid distribution is comparatively reasonable, and two-layer conical table water conservancy diversion structure 2 and 3 will have obvious the reposition of redundant personnel effect that blocks to central region air current, have avoided inlet gas directly to dash distribution plate 1, and the liquid phase volume fraction below the distribution plate that obtains all is between 0.0097-0.0099, and the distribution is comparatively even.
The above-described embodiments are merely preferred embodiments of the present invention, which should not be construed as limiting the invention. Various changes and modifications may be made by one of ordinary skill in the pertinent art without departing from the spirit and scope of the present invention. Therefore, the technical scheme obtained by adopting the mode of equivalent replacement or equivalent transformation is within the protection scope of the invention.
Claims (10)
1. The utility model provides a fluidized bed reactor's gaseous predistributor, includes horizontal annular baffle and multilayer tapered platform water conservancy diversion structure independent and coaxial setting in proper order along fluidized bed reactor's gas inlet pipeline's axis, its characterized in that:
the horizontal annular baffle and the multilayer conical table diversion structure are both positioned in the area between the gas inlet of the fluidized bed reactor and the gas distribution plate;
the horizontal annular baffle is close to the gas inlet, and a circular hole is formed in the middle of the horizontal annular baffle;
the number of layers of the multilayer conical table flow guide structure is at least two, and the bottom end of each layer of conical table flow guide structure is at the same horizontal height with the flat annular baffle;
round holes are formed in the bottom end and the top end of each layer of conical platform flow guide structure.
2. The gas predistributor of a fluidized bed reactor according to claim 1, characterized in that the top ends of the conical-shaped flow-guiding structures are all located above and at the same height as the horizontal annular baffle.
3. The gas predistributor of the fluidized bed reactor according to claim 1 or 2, wherein the diameter of the bottom circular hole of each layer of the conical table diversion structure is set as DbiThe diameter of the top round hole is DuiThe sequence number i is 1,2, … …, n is more than or equal to 2, and the outer diameter of the horizontal annular baffle is DO0The diameter of the round hole arranged on the upper part is Di0Then D isi0>Db1>Db2>……>Dbn，Du1>Du2>……>Dun。
4. The gas predistributor of the fluidized bed reactor according to claim 3, wherein the diameter D of the circular hole at the top end of the first layer of conical table diversion structureu1The value range is as follows: di0≤Du1≤DO0。
5. The gas predistributor of a fluidized-bed reactor according to any one of claims 1 to 4, characterized in that the conical surfaces of the conical-shaped flow-guiding structures of the respective layers are parallel and a gap is present between each two.
6. The gas predistributor of a fluidized bed reactor according to any one of claims 1 to 5, wherein the angle between the conical surface of the multi-layer conical-shaped flow guiding structure and the central axis of the gas inlet pipe is 15 ° to 75 °.
7. Gas predistributor of a fluidized bed reactor according to any one of claims 1 to 6, characterized in that:
the vertical distance between the outer side of the horizontal annular baffle and the bottom of the fluidized bed reactor is h, and the area S is recorded1＝hπDO0；
The circular ring area between the horizontal annular baffle and the bottom of the first layer of conical table diversion structure is S2＝π(Di0 2-Db1 2)/4；
The area of the circular hole at the bottom end of the flow guide structure of the first layer of conical table is S3＝πDb1 2/4；
Said S1、S2、S3The relationship between is S3≤S2≤S1。
8. The gas pre-distributor of a fluidized bed reactor as set forth in any of claims 1 to 7, wherein the number of layers n of the conical table flow guiding structure is 2, and the bottom annular area S between the first layer of the conical table flow guiding structure and the second layer of the conical table flow guiding structure4The area S of a circular hole at the bottom of the conical platform flow guide structure of the second layer is larger than or equal to5。
9. The gas predistributor of a fluidized-bed reactor according to claim 8, characterized in that 1.5. ltoreq.S4/S5≤10。
10. The gas pre-distributor of the fluidized bed reactor as set forth in any one of claims 1 to 7, wherein the number of layers n of the conical table diversion structure is not less than 3, and the bottom annular area S between the 1 st layer conical table diversion structure and the 2 nd layer conical table diversion structure4The bottom circular ring area S between the flow guide structure of the conical table at the No. 2 layer and the flow guide structure of the conical table at the No. 3 layer5Not less than … … and not less than n-th layer of conical platform diversion structure bottom circular hole area Sn+3。
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| CN202010795947.1A CN112023839A (en) | 2020-08-10 | 2020-08-10 | Gas pre-distributor of fluidized bed reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115212812A (en) * | 2021-04-15 | 2022-10-21 | 中国石油天然气股份有限公司 | Gas pre-distributor of fluidized bed reactor |
| CN116078275A (en) * | 2023-01-03 | 2023-05-09 | 东方电气集团东方锅炉股份有限公司 | High-efficiency gas distributor and vertical large-scale reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115212812A (en) * | 2021-04-15 | 2022-10-21 | 中国石油天然气股份有限公司 | Gas pre-distributor of fluidized bed reactor |
| CN116078275A (en) * | 2023-01-03 | 2023-05-09 | 东方电气集团东方锅炉股份有限公司 | High-efficiency gas distributor and vertical large-scale reactor |
| CN116078275B (en) * | 2023-01-03 | 2024-06-07 | 东方电气集团东方锅炉股份有限公司 | High-efficiency gas distributor and vertical large-scale reactor |
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Application publication date: 20201204 |
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