CN208200852U - A kind of gas distributor of fludized bed and fluidized-bed reactor - Google Patents

Abstract

The utility model discloses a kind of gas distributor of fludized bed and fluidized-bed reactors, are related to the fields such as carbonaceous material burning, gasification technology and solid particle drying, can increase the fluid effect of bed, reduce gas in the flow dead zone of top bed.The gas distributor of fludized bed, first shell including cylindrical in shape and upper end opening, lower end closure, first shell is interior to be equipped with gas distribution grid, and gas chamber is surrounded between gas distribution grid and first shell, gas chamber includes the first gas chamber and multiple second gas chambers, mutually isolated between two adjacent gas chambers；Gas distribution grid includes first gas distribution grid and multiple second gas distribution grids, first gas distribution grid is connected with the lower end for the second gas distribution grid for being located at bottom, first gas distribution grid is corresponding with the first gas chamber, and each second gas distribution grid is corresponding at least one second gas chamber.The utility model can be used for the production of coal gas and the drying of solid particle.

Description

A fluidized bed gas distributor and a fluidized bed reactor

technical field

The utility model relates to the technical field of coal gasification and solid drying, in particular to a fluidized bed gas distributor and a fluidized bed reactor.

Background technique

Coal catalytic gasification technology is an important way of clean and efficient utilization of coal, and it is one of the most efficient gasification technologies for coal-to-natural gas. Coal catalytic gasification is usually carried out in a fluidized bed reactor (such as a common fluidized bed gasifier), in which the raw coal is kept under the action of a bottom-up gasification agent. Continuous boiling and suspension state movement, rapid mixing and heat exchange, the coal gas generated by the reaction of raw coal and gasification agent is discharged from the exhaust pipeline at the top of the fluidized bed reactor, and the slag generated by the reaction is discharged from the fluidized bed reactor. It is discharged from the slag discharge line at the bottom of the bed reactor.

In a fluidized bed reactor, the gas distributor is one of the most important components, which plays an important role in uniform gas distribution and supporting solid phase particles, and whether its structural design is reasonable or not greatly affects the fluidized bed reactor The quality of fluidization in the fluidized bed reactor affects the generation of gas in the fluidized bed reactor. Therefore, the design of the gas distributor is very important.

The gas distributor used in the existing fluidized bed reactor includes a shell, a gas distribution plate is arranged inside the shell, a gas chamber is formed between the gas distribution plate and the shell, and the gas distribution plate is a porous plate The structure, the plate is covered with small holes, the gas can enter the reaction chamber through the gas distribution plate to contact the bed, and the gas distributor is arranged at the bottom of the fluidized bed reactor. For normal and low pressure coal gasification processes such as ash fusion and U-Gas, the solid phase bed is relatively low. Using the existing fluidized bed gas distributor can make the gas pass through the bottom of the bed with a relatively high gas density. Speed, so as to achieve good fluidization of particles in the dense phase area of the bed, full contact between gas and solid, and timely heat transfer;

However, for the medium and high pressure coal gasification process, especially the coal catalytic gasification process, the solid phase bed in the fluidized bed reactor is relatively high, and its operating pressure is high, and the gas compression is serious, while the existing gas distributor is Located at the bottom of the fluidized bed reactor, after the gas enters the reaction chamber through the gas distributor, it is only in contact with the bed in a small area of the bottom, and the gas has less contact with the bed in the upper area, which leads to gas and The contact of the entire bed is not uniform, so that the fluidization of the bed is not uniform, and the dead area of the gas flowing in the upper bed is relatively large, which is not conducive to the reaction between the gas and the bed; and the fluidization of the bed is not good. Good, the gas flows in the upper part of the bed with a large dead zone area, which will easily lead to uneven distribution of heat released by the combustion of oxygen in the gas, resulting in local high temperature, which will lead to sintering, slagging and convection of particles in the bed area around the gas distributor. The stability of the fluidized bed reactor has adverse effects, and eventually the fluidized bed reactor cannot run stably and has to be shut down.

Utility model content

The embodiment of the utility model provides a fluidized bed gas distributor and a fluidized bed reactor, which can improve the fluidization effect of the bed and reduce the flow dead zone of the gas in the upper bed.

In order to achieve the above purpose, in the first aspect, the embodiment of the present utility model provides a fluidized bed gas distributor, which includes a cylindrical first shell with an open upper end and a sealed lower end, and the first shell is provided with A gas distribution plate, an air chamber is enclosed between the gas distribution plate and the first housing, and the air chamber includes a first air chamber and a plurality of second air chambers, and the first air chamber and the plurality of second air chambers In the second gas chamber, two adjacent gas chambers are isolated from each other; the gas distribution plate includes a first gas distribution plate and a plurality of cylindrical and vertically arranged second gas distribution plates, a plurality of The second gas distribution plate is distributed along the vertical direction and connected in sequence, the first gas distribution plate is connected to the lower end of the second gas distribution plate located at the bottom, and the first gas distribution plate is connected to the lower end of the second gas distribution plate. Corresponding to the first gas chamber, each of the second gas distribution plates corresponds to at least one of the second gas chambers.

In the fluidized bed gas distributor provided by the embodiment of the utility model, since the gas chamber includes a first gas chamber and a plurality of second gas chambers, and two adjacent gas chambers are separated from each other, the plurality of second gas distribution plates along the Distributed in the vertical direction and connected in sequence, the first gas distribution plate is connected to the lower end of the second gas distribution plate located at the bottom, the first gas distribution plate corresponds to the first gas chamber, and each second gas distribution plate is connected to at least One second gas chamber corresponds, that is, the first gas chamber and multiple second gas chambers are also vertically arranged, so that when the fluidized bed reactor is working, the gas can flow from the first gas chamber to the multiple second gas chambers. The second gas chamber enters the reaction chamber through the gas distribution plate and is in contact with the bed layer. Since the first gas chamber and multiple second gas chambers are also arranged in the vertical direction, the first gas chamber enters the reaction chamber. The gas can be in contact with the bed at the bottom, and the gas entering the reaction chamber from multiple second gas chambers can be in contact with the bed of different heights, so the contact area between the gas and the bed in the reaction chamber can be Greatly increased, improving the uniformity of gas distribution in different height beds, which can increase the fluidization effect of the bed, greatly reduce the flow dead zone of the gas in the upper bed, and then facilitate the flow between the gas and the bed At the same time, the enhancement of the fluidization effect of the bed and the reduction of the flow dead zone of the gas in the upper bed can make the heat released by the combustion of oxygen in the gas evenly distributed, and avoid the local high temperature in the surrounding area of the gas distributor. The particles in the bed layer in the area are sintered and slagged, thus ensuring the stability of the fluidized bed reactor.

In the second aspect, the embodiment of the present utility model provides a fluidized bed reactor, which includes a cylindrical second casing with a sealed upper end and an open lower end, and the fluidized bed gas distributor described in the first aspect. The lower end of the second housing is sealingly connected to the upper end of the first housing of the fluidized bed gas distributor, so that a gap is formed between the second housing and the gas distribution plate of the fluidized bed gas distributor. reaction chamber.

Since the fluidized bed gas distributor included in the fluidized bed reactor provided by the embodiment of the utility model is the same as the fluidized bed gas distributor described in the first aspect, the same technical problem is also solved, achieving Same technical effect.

Description of drawings

In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the accompanying drawings that need to be used in the description of the embodiments or the prior art. Obviously, the accompanying drawings in the following description These are only some embodiments of the utility model, and those skilled in the art can also obtain other drawings based on these drawings without creative work.

Fig. 1 is the structural representation of the fluidized bed reactor of the utility model embodiment;

Fig. 2 is a schematic structural view of a fluidized bed gas distributor according to an embodiment of the present invention (the first gas distribution plate is a conical cylinder structure, and the second gas distribution plate is a cylindrical cylinder structure);

Fig. 3 is a schematic diagram of the arrangement of through holes on the second gas distribution plate in the fluidized bed gas distributor according to the embodiment of the present invention;

Fig. 4 is a schematic diagram of the arrangement of the swirl tubes of the fluidized bed gas distributor according to the embodiment of the present invention in the first plane;

Fig. 5 is a schematic diagram of the arrangement of the swirl tubes of the fluidized bed gas distributor in the embodiment of the present invention in a vertical plane;

Fig. 6 is a schematic structural view of a fluidized bed gas distributor according to an embodiment of the present invention (the first gas distribution plate is a conical cylinder structure, and the second gas distribution plate is a conical cylinder structure);

Fig. 7 is a schematic structural view of a fluidized bed gas distributor according to an embodiment of the present invention (the first gas distribution plate is a flat plate structure, and the second gas distribution plate is a cylindrical structure);

Fig. 8 is a schematic structural diagram of a fluidized bed gas distributor according to an embodiment of the present invention (the first gas distribution plate is a flat plate structure, and the second gas distribution plate is a conical cylinder structure).

Detailed ways

The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of them. example. Based on the embodiments of the present utility model, all other embodiments obtained by persons of ordinary skill in the art without making creative efforts belong to the scope of protection of the present utility model.

In describing the present invention, it should be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal" , "top", "bottom", "inner", "outer" and other indicated orientations or positional relationships are based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the utility model and simplifying the description, rather than indicating Or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as limiting the present invention.

In the description of the present utility model, it should be noted that, unless otherwise clearly stipulated and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense, for example, it can be a fixed connection or a flexible connection. Detachable connection, or integral connection; For those of ordinary skill in the art, the specific meanings of the above terms in the present utility model can be understood in specific situations.

The terms "first" and "second" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance or implicitly specifying the quantity of indicated technical features. Thus, a feature defined as "first" and "second" may explicitly or implicitly include one or more of these features. In the description of the present utility model, unless otherwise specified, "plurality" means two or more.

Example 1

As shown in Figure 2, the utility model embodiment provides a fluidized bed gas distributor, which includes a cylindrical first shell 1 with an open upper end and a sealed lower end, and a gas distribution plate is arranged inside the first shell 1 2. An air chamber 3 is formed between the gas distribution plate 2 and the first housing 1. The air chamber 3 includes a first air chamber 31 and a plurality of second air chambers 32. The first air chamber 31 and the plurality of second air chambers In the chamber 32, two adjacent gas chambers are isolated from each other; the gas distribution plate 2 includes a first gas distribution plate 21 and a plurality of cylindrical and vertically arranged second gas distribution plates 22, and a plurality of second gas distribution plates 22 The distribution plates 22 are distributed along the vertical direction and connected successively. The first gas distribution plate 21 is connected to the lower end of the second gas distribution plate 22 located at the bottom. The first gas distribution plate 21 corresponds to the first gas chamber 31. Each second gas distribution plate 22 corresponds to at least one second gas chamber 32 .

Wherein, the gas distribution plate 2 can be fixedly connected with the first housing 1 so that the gas chamber 3 is enclosed between the two. For example, as shown in FIG. The shells 1 are fixedly connected (such as welding); as shown in Figure 1, in the first air chamber 31 and the plurality of second air chambers 32, two adjacent air chambers can be separated by a heat shield 4 The heat insulation board 4 may be a board made of a heat insulation material, or a board made of a metal plate covered with a heat insulation material layer, which is not specifically limited here. When the heat shield 4 is made of a metal plate covered with a layer of heat insulating material, the metal plate should be provided with expansion joints to offset the thermal stress caused by the different materials between the metal material and the heat insulating material; each The second gas distribution plate 22 may correspond to one second gas chamber 32 (such as shown in FIG. 2 ), or may correspond to multiple second gas chambers 32 , which is not specifically limited here.

The fluidized bed gas distributor provided by the embodiment of the utility model, as shown in FIG. isolation, a plurality of second gas distribution plates 22 are distributed along the vertical direction and connected in sequence, the first gas distribution plate 21 is connected to the lower end of the second gas distribution plate 22 located at the bottom, and the first gas distribution plate 21 is connected to the first gas distribution plate 22. The air chamber 31 corresponds, and each second gas distribution plate 22 corresponds to at least one second air chamber 32, that is, the first air chamber 31 and a plurality of second air chambers 32 are also arranged in the vertical direction, so that in the flow When the fluidized bed reactor works, the gas can enter the reaction chamber 300 from the first gas chamber 31 and a plurality of second gas chambers 32 through the gas distribution plate 2 to be in contact with the bed. A plurality of second gas chambers 32 is also vertically arranged, so that the gas entering the reaction chamber 300 by the first gas chamber 31 can be in contact with the bed at the bottom, and enters into the reaction chamber 300 by a plurality of second gas chambers 32. The gas in the reaction chamber 300 can be in contact with the beds of different heights, so the contact area between the gas and the bed in the reaction chamber 300 can be greatly increased, improving the uniformity of gas distribution in the beds of different heights, Thereby, the fluidization effect of the bed can be increased, and the flow dead zone of the gas in the upper bed can be greatly reduced, thereby facilitating the reaction between the gas and the bed; at the same time, the fluidization effect of the bed is enhanced, and the gas flow in the upper bed The reduction of the flow dead zone of the bed can make the heat released by the oxygen combustion in the gas evenly distributed, and avoid the local high temperature in the surrounding area of the gas distributor, which will cause the sintering and slagging of the bed particles in this area, thus ensuring convection. Stability of bed reactor work.

In the reaction chamber 300, the pressure of the bed at different heights is different, and the pressure of the bed decreases gradually as the height increases. If the diameters of the through holes 221 on the second gas distribution plate 22 are all equal, Then, the gas that passes through the through hole 221 that is positioned at the lower part of the second gas distribution plate 22 is subjected to greater resistance, so that the gas that enters is less; The resistance to the gas is small, so more gas enters, which makes it easy for the gas to pass unevenly in the height direction of the second gas distribution plate 22, so that the gas entering the reaction chamber 300 is distributed in the height direction. uneven. In order to make the gas evenly enter the reaction chamber 300 through the second gas distribution plate 22 and contact the bed, as shown in FIG. decrease. The through hole 221 located at the lower part of the second gas distribution plate 22 has a larger diameter, a smaller pressure drop through the hole, and a lower flow rate when the gas passes through, which can offset the higher pressure of the lower bed and make the gas pass through the second gas distribution plate evenly 22, so that the gas can be distributed more evenly in the beds of different heights, thereby improving the fluidization effect in the reaction chamber 300 .

Since a plurality of second gas distribution plates 22 are distributed in the vertical direction, in order to make the gas pass through all the second gas distribution plates 22 evenly, in two adjacent second gas distribution plates 22, the second gas distribution plate below is The minimum value of the diameter of the through hole 221 on the distribution plate 22 is greater than the maximum value of the diameter of the through hole 221 on the second gas distribution plate 22 above, that is, the plurality of through holes 221 on all the second gas distribution plate 22 The diameter is decreasing from bottom to top, so that the speed of gas passing through the through holes 221 at different heights is different, so that the pressure of the upper bed layer at different heights can be adapted to ensure that the through holes 221 at different heights pass through the same amount of gas, so that the gas The distribution in the beds of different heights is more uniform, and finally the fluidization effect in the reaction chamber 300 is further improved.

On the second gas distribution plate 22, there are many ways to open the through holes 221. The through holes 221 can be opened perpendicular to the cylinder wall of the second gas distribution plate 22, and can also form a certain angle with the cylinder wall of the second gas distribution plate 22. Alternatively, the above two methods can also be combined to ensure that the gas can enter the reaction chamber 300 in different directions and fully contact with the bed.

The diameter of the plurality of through holes 221 is preferably within the range of 1 to 10 mm. By controlling the diameter of the through holes 221 and other parameters such as gas, the speed of the gas passing through the through holes 221 is within the range of 15 to 40 m/s , preferably within 20-30m/s, so as to ensure that the gas enters the reaction chamber 300 through the second gas distribution plate 22 and can be dispersed more uniformly, so that the flow field in the reaction chamber 300 can be optimized and the bed can be improved. The fluidization effect of the layer.

In the fluidized bed gas distributor provided by the embodiment of the present utility model, as shown in FIG. (2) The width of the gas distribution plate 22 in the radial direction) is a very important parameter. m should not be too large, nor too small, if m is too large, the size of the second gas distribution plate 22 in the radial direction is reduced, thereby reducing the cloth distribution area in the second gas distribution plate 22; if m is too small After the gas enters the second gas chamber 32, it directly enters the reaction chamber 300 through the second gas distribution plate 22 before being buffered, which is very unfavorable for sufficient contact between the gas and the bed. Through simulation and experiments, when the size of the m is 3 to 10 times the diameter n of the through hole 221, the cloth distribution area in the second gas distribution plate 22 will not be too small, nor will it affect the sufficient contact between the gas and the bed.

After further simulation and experiments, when the size of m is 4 to 6 times the diameter n of the through hole 221, the size of the cloth distribution area in the second gas distribution plate 22 and the contact state between the gas and the bed can be optimized.

Wherein, when the gap value between the second gas distribution plate 22 and the first shell 1 is not constant, for example, the first shell 1 has a cylindrical structure and the second gas distribution plate 22 has a conical structure, the When the value of m is the average value of the gap between the second gas distribution plate 22 and the first casing 1 in the vertical direction, such as the gap between the second gas distribution plate 22 and the first casing 1 in the vertical direction The maximum value is m ₁ , the minimum value is m ₂ , then m=(m ₁ +m ₂ )/2; when the diameters of the multiple through holes 221 on the second gas distribution plate 22 are different, for example, as shown in FIG. 3 A situation in which the diameters of the plurality of through holes 221 gradually decrease from bottom to top is shown, and at this time n should take the maximum value of the diameters of the plurality of through holes 221 .

In the fluidized bed gas distributor provided by the embodiment of the utility model, as shown in Figure 2, the sum h of the heights of multiple second gas distribution plates 22 is also a very important parameter, and h should not be too large or too large. Small. If h is too large, the gas inlet area of the fluidized bed gas distributor is too large, and the gas enters the reaction chamber 300 from the second gas distribution plate 22 at the top, and it is exhausted from the upper exhaust line before it can fully contact with the bed material. If h is too small, the gas inlet area of the fluidized bed gas distributor is too small, resulting in too small contact area between the gas and the bed material in the reaction chamber 300, which is not conducive to improving the reaction chamber 300. Fluidization effect of bed material. Through experiments and simulations, when h and the diameter d of the lower end of the second gas distribution plate 22 located at the bottom satisfy h=(0.5～3)d, the gas inlet area of the fluidized bed gas distributor is the best, neither causing The waste of gas can also ensure the fluidization effect of the bed material in the reaction chamber 300 .

In order to make the gas passing through the second gas distribution plate 22 more fully contact with the bed in the reaction chamber 300, as shown in FIG. A plurality of swirl tubes 5 are arranged through the cylinder wall of the second gas distribution plate 22 , and an end of each swirl tube 5 away from the second gas distribution plate 22 is located in the second gas chamber 32 . By arranging a plurality of swirl tubes 5 on the cylinder wall of the second gas distribution plate 22, the gas enters the reaction chamber 300 through the swirl tubes 5 to form a tangential air flow, which can flow the reaction chamber 300 from The large bubbles rising from the lower part are cut into multiple small bubbles, so that the gas in the multiple small bubbles can fully contact the bed particles, thereby optimizing the flow field in the bed area in the reaction chamber 300 and improving the bed quality. fluidization effect.

The arrangement of the swirl tube 5 on the cylinder wall of the second gas distribution plate 22 is not unique, for example, one end of the swirl tube 5 may protrude into the reaction chamber 300 . In addition, as shown in FIG. 2 , the inlet of the swirl tube 5 may also be flush with the inner wall of the second gas distribution plate 22 . Compared with one end of the swirl tube 5, which can extend into the reaction chamber 300, when the inlet of the swirl tube 5 is flush with the inner wall of the second gas distribution plate 22, it is possible to avoid the flow in the reaction chamber 300. The bed particles in the melted state are in contact with the swirl tube 5, thereby preventing the swirl tube 5 protruding into the reaction chamber 300 from being worn by the bed particles.

Wherein, the range of the inner diameter of the swirl tube 5 can be between 1 and 10 mm. By controlling the size of the inner diameter of the swirl tube 5 and other parameters such as gas, the velocity of the gas when passing through the swirl tube 5 is 20 to 50 m/s preferably within 25-40m/s, so that the airflow ejected from the swirl tube 5 has a good shearing effect on the large bubbles, thereby ensuring that the gasification agent enters the reaction chamber 300 through the second air chamber 32 It can be more uniformly dispersed, so that the gas can be more fully contacted with the bed particles, and finally achieve the purpose of optimizing the flow field distribution in the reaction chamber 300 .

The swirl tubes 5 passing through the cylinder wall of the second gas distribution plate 22 can be realized in the following way: the swirl tubes 5 can be penetrated in the through hole 221 , and then the swirl tube 5 is welded to the inner wall of the through hole 221 .

In order to improve the shearing effect of the incident gas flow of the swirl tube 5 on the large bubbles in the reaction chamber 300, as shown in FIG. Due to the high pressure of the bed material on the gas distribution plate 2 located below, the gas-solid contact is relatively poor during the process of gas fluidizing the bed material located below, and there are many large bubbles in this area. By setting the swirl tube 5 on the wall of the second gas distribution plate 22 at the bottom, the large air bubbles existing in this area can be better cut, so that the gas-solid contact is more sufficient, thereby improving the flow rate of the bed material in this area. The fluidization effect, and then improve the fluidization effect of the bed material in the reaction chamber 300.

Wherein, as shown in Figure 2, the height _h1 of the second gas distribution plate 22 located at the bottom is an important parameter, since the cylinder wall of the second gas distribution plate 22 located at the bottom is provided with a swirl tube 5, Then the swirl tube 5 will affect the gas entering the reaction chamber 300 to a certain extent. If h ₁ is too large, it will affect the full contact between the gas and the bed, which is not conducive to the sufficient fluidization of the bed in the reaction chamber 300. ; If h ₁ is too small, then it will affect the number of swirl tubes 5 opened, reducing the shear effect of swirl tubes 5 on air bubbles, which is also not conducive to the full fluidization of the bed in this area. Therefore, the value of _h1 needs to be reasonably controlled. Through simulation and experiments, when the distance between h ₁ and the diameter d of the lower end of the second gas distribution plate 22 located at the bottom satisfies h ₁ =(0.25-0.5)d, the gas in the reaction chamber 300 and the bed layer can be achieved. Fully contact with the optimal point of the shearing effect of the swirl tube 5 on the bubbles, thereby facilitating the sufficient fluidization of the bed in the reaction chamber 300 .

In order to improve the shear effect of the incident air flow of the swirl tube 5 on the large bubbles in the reaction chamber 300, it is necessary to reasonably control the angle between the swirl tube 5 and the wall of the second gas distribution plate 22, and the swirl tube 5 The included angle with the cylinder wall of the second gas distribution plate 22 is mainly measured by the size of α and β, wherein, as shown in Figure 4 and Figure 5, α is the included angle between the swirl tube 5 and the first plane 6 , β is the angle between the incident direction of the swirl tube 5 and the first straight line 7 in the first plane 6; wherein, the first plane 6 is perpendicular to the central axis of the second gas distribution plate 22, and passed The plane of the incident point q; the first straight line 7 is the cylinder center point O of the second gas distribution plate 22 and the incident point q of the swirl tube 5 (that is, the central axis of the swirl tube 5 and the second gas distribution plate 22 cylinder intersection points of inner walls).

As shown in Figure 4, β should neither be too large nor too small. If β is too large, the incident flow of the swirl tube 5 is more distributed near the inner wall of the cylinder of the second gas distribution plate 22, resulting in too little gas in the area of the second gas distribution plate 22 near the center of the cylinder, which is not conducive to The shearing of the air bubbles in the area near the center of the cylinder; if β is too small, the incident flow of the swirl tube 5 is more distributed in the central area of the cylinder of the second gas distribution plate 22, causing the second gas distribution plate 22 to be close to the cylinder Too little gas in the area of the inner wall is also unfavorable for shearing the air bubbles in the area near the inner wall of the cylinder. Through simulation and experiments, when β is within 20°-60°, the swirl tube 5 has the best shearing effect on the air bubbles.

Similarly, as shown in Figure 5, α should not be too large. If α is too large, the incident flow of the swirl tube 5 will be more distributed near the inner wall of the second gas distribution plate 22, resulting in the second gas distribution plate 22 If there is too little gas in the area near the center of the cylinder, it is not conducive to the shearing of the bubbles in the area near the center of the cylinder. After simulation and experiments, when α is within 0°～20°, the swirl tube 5 has the best shear effect on the air bubbles; Fig. When shooting down, that is, when the swirl tube 5 is shooting down obliquely, α should not be too large. If α is too large, it is also not conducive to the shearing of the air bubbles in the area near the center of the tube. After simulation and experiments, when the swirl tube 5 shoots down, when α is within 0°～45°, the shearing effect of the swirl tube 5 on the air bubbles is the best; thus, when α is between -45°～20° , the swirl tube 5 has the best shearing effect on the bubbles, wherein, when α is greater than zero, the swirl tube 5 shoots upwards, and when α is less than zero, the swirl tube 5 shoots down.

As shown in Figures 2 and 7, a swirl tube 5 is also provided at the connection between the cylinder wall of the second gas distribution plate 22 and the first gas distribution plate 21. The solid particles in this area are in a continuous flow state under the comprehensive action of shear stress, gas buoyancy and their own gravity, which strengthens the flow field in this area, ensures that there is no flow dead angle in this area, improves the fluidization effect in this area, and avoids flow in this area. Insufficient fluidization of the bed material will affect the discharge of slag, and finally ensure that the slag generated by the reaction smoothly enters the slag discharge pipeline 8 to be discharged from the reaction chamber 300 .

Through simulation and experiments, when the α angle of the swirl tube 5 at the connection between the cylinder wall of the second gas distribution plate 22 and the first gas distribution plate 21 ranges from 0° to 45°, the fluidization of this area can be achieved. The effect is better, and it is more conducive to the discharge of slag.

In order to further improve the shear effect of the swirl tube 5 on the bubbles, as shown in Figure 2, along the height direction of the second gas distribution plate 22, a plurality of swirl tubes 5 are distributed in multiple horizontal planes, as shown in Figure 4, Multiple pairs of swirl tubes 5 are arranged in each horizontal plane, and the two swirl tubes 5 in each pair are symmetrical about the cylinder center O of the second gas distribution plate 22 . By setting the two swirl tubes 5 in each pair in this way, the airflows that can be ejected in opposite directions can form a better shearing effect, which is conducive to more sufficient contact between the gas and the bed particles, and then improves the flow rate of the bed. effect.

In the fluidized bed gas distributor provided by the embodiment of the utility model, the shape of the first gas distribution plate 21 is not unique, for example, as shown in Figure 2 and Figure 6, the first gas distribution plate 21 can be a tapered cylinder structure , and the large mouth end of the first gas distribution plate 21 is connected to the lower end of the second gas distribution plate 22 located at the bottom. The first gas distribution plate 21 is designed as a cone structure, which can facilitate the slag generated by the reaction in the reaction chamber 300 to enter the slag discharge pipeline 8 at the lower end of the first gas distribution plate 21 . The first gas distribution plate 21 of this shape is suitable for fluidized bed processes with chemical reactions such as coal gasification.

In addition, as shown in FIG. 7 and FIG. 8 , the first gas distribution plate 21 may also be a flat plate structure. Since the flat first gas distribution plate 21 is not conducive to the discharge of slag, the first gas distribution plate 21 of this shape is suitable for processes without chemical reactions such as fluidized bed drying, or processes with chemical reactions at low temperature.

As shown in Figure 6, in the first gas distribution plate 21 of the conical cylinder structure, the cone angle θ of the first gas distribution plate 21 is an important parameter, and the cone angle θ should not be too large or too small. If the cone angle θ is too large, it is unfavorable for the slag generated by the reaction to be discharged from the slag discharge pipeline 8; if the cone angle θ is too small, the space in the cylinder of the first gas distribution plate 21 is small, which reduces the flow rate of the fluidized bed. The cloth area of the bed material. Through simulation and experiments, when the cone angle θ of the first gas distribution plate 21 is 60°-120°, it will neither affect the discharge of slag nor make the material distribution area of the fluidized bed too small. Wherein, when the cone angle θ of the first gas distribution plate 21 is 90°, the optimal point of facilitating the discharge of slag and the size of the distribution area is reached.

There are also a plurality of first through holes on the first gas distribution plate 21, which is similar to the opening method of the through holes 221 on the second gas distribution plate 22. The first through holes can be opened perpendicular to the first gas distribution plate 21, or can be It is set at a certain angle with the first gas distribution plate 21 , and the above two methods can also be combined to ensure that the gas can enter the reaction chamber 300 from different directions and fully contact with the bed.

The range of diameters of the plurality of first through holes is preferably within 0.5-5mm, and by controlling the diameter of the first through holes and other parameters such as gas, the velocity range of the gas when passing through the through holes 221 is between 25-50m/s preferably within 30-40m/s, so as to ensure that the gas enters the reaction chamber 300 through the first gas distribution plate 21 and can be dispersed more uniformly, thereby optimizing the flow field in the reaction chamber 300 and improving The fluidization effect of the bed.

When the first gas distribution plate 21 is a cone-shaped cylinder structure, on the cylinder wall of the first gas distribution plate 21, the diameters of the plurality of first through holes gradually decrease from bottom to top, so that the gas can be distributed evenly through the first gas distribution plate 21. The plate 21, so that the gas can be distributed more evenly in the bed layers of different heights, and the fluidization effect in the reaction chamber 300 can be further improved.

When the first gas distribution plate 21 is a tapered cylinder structure, a plurality of swirl tubes 5 can also be arranged on the cylinder wall of the first gas distribution plate 21, and the arrangement of the plurality of swirl tubes 5 is the same as that of the second gas distribution system. The arrangement of the swirl tubes 5 on the plate 22 is the same, and the effect achieved is the same as that achieved by the swirl tubes 5 on the second gas distribution plate 22 , which will not be repeated here.

As shown in Figure 2, the small opening end of the first gas distribution plate 21 is connected to the slag discharge pipeline 8 through the transition cylinder 9, and the cylinder wall of the transition cylinder 9 separates the first gas chamber 31 from the interior of the transition cylinder 9, and also That is, there is no hole connecting the interior of the transition cylinder 9 with the first air chamber 31 on the cylinder wall of the transition cylinder 9, so that the gas in the first air chamber 31 can be prevented from entering the interior of the transition cylinder 9 from the cylinder wall of the transition cylinder 9. The slag in the transition cylinder 9 interferes, thereby ensuring a smoother slag discharge; since the transition cylinder 9 has a certain volume, it can accommodate a certain amount of slag, thereby increasing the amount of slag held in this area.

Wherein, the shape of the transition cylinder 9 is not unique, such as the transition cylinder 9 can be a cylindrical tube; 21 are connected to each other, and the small mouth end of the transition cylinder 9 is connected to the slag discharge pipeline 8. Compared with the cylindrical barrel, when the transition barrel 9 is a conical barrel, the slag is easier to enter the slag discharge pipeline 8 along the inner wall of the transition barrel 9, so that the smooth progress of the discharge can be ensured, and the flow of the slag in the transition barrel can be reduced. 9 stacks.

When the transition cylinder 9 is a tapered cylinder, as shown in Figure 2, the cone angle δ of the transition cylinder 9 is an important parameter, and the cone angle δ of the transition cylinder 9 should not be too large or too small. If the cone angle δ is too large, the gas distribution area of the first gas distribution plate 21 will be reduced, resulting in a larger dead zone in the central area and a decrease in fluidization quality; if the cone angle δ of the transition cylinder 9 is too small, then the transition cylinder 9 The volume is also small, thereby reducing the amount of slag held in this area, which affects the smooth entry of slag into the slag discharge pipeline 8 . Through calculation and experimental research, when the cone angle δ of the transition cylinder 9 is between 12° and 24°, the transition cylinder 9 can not only maintain a certain amount of slag held, but also allow the slag to enter the slag discharge smoothly. Line 8 exits.

As shown in FIG. 2 , a jet tube 81 is coaxially arranged inside the slag discharge pipeline 8 , and the upper end of the jet tube 81 extends into the interior of the transition cylinder 9 . The upper end of jet tube 81 is stretched into the inside of transition tube 9, so that when the upper end of jet tube 81 does not stretch into the inside of transition tube 9, the air flow ejected by jet tube 81 will slag in transition tube 9 Jack up, thus affecting the discharge of slag.

Wherein, as shown in Figure 2, the length a of the jet tube 81 extending into the inside of the transition cylinder 9 should not be too large or too small. If a is too large, the air flow ejected by the jet tube 81 will directly enter the reaction In the chamber 300, an obvious gas-solid fluidization transition zone is not formed inside the transition cylinder 9, which is unfavorable to the smoother discharge of the slag; if a is too small, the airflow injected by the jet tube 81 will be It has a greater impact on the slag in the transition cylinder 9, and is also unfavorable for smoother discharge of the slag. Through simulation and experiments, when the height of a and the transition cylinder 9 is b and satisfies a=(0.5-0.7)b, the slag can be discharged more smoothly.

As shown in FIG. 2 , there is a gap channel 82 between the slag discharge pipeline 8 and the jet pipe 81 , and the gap channel 82 is used for slag discharge. While discharging slag, superheated steam at 450-600°C is passed from bottom to top in the gap channel 82, so that the amount of slag discharge can be adjusted by controlling the amount of steam introduced; the jet tube 81 is passed from bottom to top The mixture of superheated steam and oxygen (the concentration of oxygen is controlled at 15-30%) can strengthen the gas-solid turbulence in the central area of the bed, thereby ensuring more sufficient fluidization in the central area of the bed.

In the fluidized bed gas distributor provided by the embodiment of the utility model, the shape of the second gas distribution plate 22 is not unique, for example, as shown in Figure 2 and Figure 7, the second gas distribution plate 22 can be a cylindrical structure ; In addition, as shown in Figure 6 and Figure 8, the second gas distribution plate 22 can also be a cone structure, and between two adjacent second gas distribution plates 22, the second gas distribution plate 22 located below The large mouth end of is connected with the lower end of the second gas distribution plate 22 located above. The second gas distribution plate 22 is designed as a conical barrel structure, and it is arranged as an inverted cone, so that the cross-sectional area of the second gas distribution plate 22 near the lower end is smaller, and the gas below passes through it at a faster speed. The gas can bring up the larger bed particles located in the lower part, so as to ensure that the bed layer located in the lower part is fully fluidized.

Wherein, a plurality of second gas distribution plates 22 can be all cylindrical barrel structures (such as shown in Figure 7), also can be all conical barrel structures (such as shown in Figure 8), also can be cylindrical barrel structure and conical barrel structure The combination of structures is not specifically limited here.

In the second gas distribution plate 22 of the tapered cylinder structure, as shown in Figure 6, the cone angle of the second gas distribution plate 22 is an important parameter, its cone angle should not be too large, if the cone angle If it is too large, the slag generated by the reaction is easy to accumulate on the second gas distribution plate 22, which is not conducive to downward slag discharge. Through simulation and experiments, when the cone angle of the second gas distribution plate 22 When the angle is less than 20°, the slag is not easy to accumulate on the second gas distribution plate 22, which can ensure the smooth progress of slag discharge.

After further simulation and experiments, when the cone angle of the second gas distribution plate 22 When the angle is less than 14°, the slag is less likely to accumulate on the second gas distribution plate 22, and the slag discharge can be carried out more smoothly.

Example 2

As shown in Figure 1, the embodiment of the utility model provides a fluidized bed reactor, including a cylindrical second shell 200 with a sealed upper end and an open lower end, and the fluidized bed gas distribution described in Embodiment 1 device 100, the lower end of the second housing 200 is sealed with the upper end of the first housing 1 of the fluidized bed gas distributor 100, so that the gas distribution plate 2 between the second housing 200 and the fluidized bed gas distributor 100 A reaction chamber 300 is formed between them.

Wherein, the first housing 1 and the second housing 200 can be integrally formed (such as shown in FIG. 1 ), or the lower end of the second housing 200 and the upper end of the first housing 1 can be sealed and connected through a connection structure. No specific limitation is made here.

Since the fluidized bed gas distributor 100 included in the fluidized bed reactor provided by the embodiment of the utility model is the same as the fluidized bed gas distributor 100 described in Example 1, the same technical problem is also solved, The same technical effect is achieved. Other structures of the fluidized bed reactor are well known to those skilled in the art and will not be repeated here.

The above are only specific embodiments of the present utility model, but the scope of protection of the present utility model is not limited thereto. Anyone familiar with the technical field can easily think of changes or replacements within the technical scope disclosed in the present utility model. All should be covered within the protection scope of the present utility model. Therefore, the protection scope of the present utility model should be based on the protection scope of the claims.

Claims (15)

1. A fluidized bed gas distributor, comprising a cylindrical shell with an open upper end and a lower end seal, a gas distribution plate is provided in the first shell, and the gas distribution plate and the first shell An air chamber is enclosed between the bodies, and it is characterized in that the air chamber includes a first air chamber and a plurality of second air chambers, and in the first air chamber and the plurality of second air chambers, adjacent The two gas chambers are isolated from each other; the gas distribution plate includes a first gas distribution plate and a plurality of cylindrical and vertically arranged second gas distribution plates, and the plurality of second gas distribution plates are arranged along the vertical direction Distributed and connected in sequence, the first gas distribution plate is connected to the lower end of the second gas distribution plate located at the bottom, the first gas distribution plate corresponds to the first gas chamber, each of the A second gas distribution plate corresponds to at least one of said second gas chambers. 2. The fluidized bed gas distributor according to claim 1, wherein the cylinder wall on the second gas distribution plate has a plurality of through holes, and the diameter of the plurality of through holes gradually increases from bottom to top. decrease. 3. The fluidized bed gas distributor according to claim 1, wherein the cylinder wall of the second gas distribution plate has a plurality of through holes, and the maximum diameter of the plurality of through holes is n, The gap value between the second gas distribution plate and the first housing is m, and m and n satisfy: m=(3-10)n; wherein, the gap value is the second gas distribution plate The average value of the gap in the vertical direction with the first shell. 4. The fluidized bed gas distributor according to claim 1, characterized in that, when a plurality of the second gas distribution plates are circular cylinder structures, the second gas distribution plate located at the bottom The diameter of the barrel opening at the lower end is d, the sum of the heights of the plurality of second gas distribution plates is h, and h and d satisfy: h=(0.5-3)d. 5. The fluidized bed gas distributor according to claim 1, wherein a plurality of swirl tubes are arranged on the cylinder wall of the second gas distribution plate, and a plurality of the swirl tubes run through the The cylinder wall of the second gas distribution plate is set, and the end of each swirl tube away from the second gas distribution plate is located in the second air chamber. 6 . The fluidized bed gas distributor according to claim 5 , wherein the swirl tube is arranged on the cylinder wall of the second gas distribution plate located at the bottom. 7. The fluidized bed gas distributor according to claim 5, characterized in that, in the first plane, the included angle between the incident direction of the swirl tube and the first straight line is β, and the range of β is 20 °～60°; the included angle between the swirl tube and the first plane is α, and the range of α is -45°～20°; wherein, the first plane is perpendicular to the second gas distribution plate The central axis of the cylinder, and the plane passing through the incident point of the swirl tube; the first straight line is the line between the central point of the cylinder of the second gas distribution plate and the incident point of the swirl tube . 8. The fluidized bed gas distributor according to any one of claims 1-7, characterized in that, the first gas distribution plate is a conical cylinder structure, and the large opening end of the first gas distribution plate It is connected to the lower end of the second gas distribution plate located at the bottom; or the first gas distribution plate is a flat plate structure. 9. The fluidized bed gas distributor according to claim 8, characterized in that, when the first gas distribution plate is a conical cylinder structure, the small mouth end of the first gas distribution plate passes through the transition cylinder and exhaust The slag pipeline is connected, and the cylinder wall of the transition cylinder separates the first air chamber from the interior of the transition cylinder. 10. The gas distributor for a fluidized bed according to claim 9, wherein the transition cylinder is a conical cylinder, and the large mouth end of the transition cylinder is connected to the small mouth end of the first gas distribution plate, The small opening end of the transition cylinder is connected with the slag discharge pipeline. 11. The fluidized bed gas distributor according to claim 10, characterized in that, the cone angle of the transition cylinder is 12°-24°. 12 . The fluidized bed gas distributor according to claim 9 , wherein a jet tube is coaxially arranged in the slag discharge line, and the upper end of the jet tube extends into the interior of the transition cylinder. 13 . 13. The fluidized bed gas distributor according to claim 12, wherein the length of the jet tube extending into the interior of the transition cylinder is a, the height of the transition cylinder is b, and a and b satisfy : a=(0.5～0.7)b. 14. The fluidized bed gas distributor according to any one of claims 1-7, characterized in that, the second gas distribution plate is a cylindrical tube structure; or the second gas distribution plate is a conical tube structure, and between two adjacent second gas distribution plates, the large mouth end of the lower second gas distribution plate is connected to the lower end of the upper second gas distribution plate. 15. A fluidized bed reactor, characterized in that it comprises a cylindrical second shell with a sealed upper end and an open lower end and the fluidized bed gas distributor according to any one of claims 1 to 14, wherein The lower end of the second housing is sealingly connected to the upper end of the first housing of the fluidized bed gas distributor, so that a gap is formed between the second housing and the gas distribution plate of the fluidized bed gas distributor. reaction chamber.