CN114618398A - Air supplement device for fluidized bed - Google Patents
Air supplement device for fluidized bed Download PDFInfo
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- CN114618398A CN114618398A CN202011453476.2A CN202011453476A CN114618398A CN 114618398 A CN114618398 A CN 114618398A CN 202011453476 A CN202011453476 A CN 202011453476A CN 114618398 A CN114618398 A CN 114618398A
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- fluidized bed
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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
Abstract
The invention discloses an air supplement device for a fluidized bed, which comprises: the upper gas supplementing cabin and the lower gas supplementing cabin are both annular cavities and are sleeved outside the fluidized bed, the fluidized bed is sequentially provided with a large-diameter section lifting pipe, a diameter-variable section and a small-diameter section lifting pipe from top to bottom, the upper gas supplementing cabin is sleeved at the lower part of the large-diameter section lifting pipe, the upper part of the diameter-variable section is positioned in the upper gas supplementing cabin, the lower gas supplementing cabin is sleeved at the upper part of the small-diameter section lifting pipe, the lower part of the diameter-variable section is positioned in the lower gas supplementing cabin, a first gas supplementing inlet is formed in the upper gas supplementing cabin, and a second gas supplementing inlet is formed in the lower gas supplementing cabin; be provided with a plurality of first nozzles on the fluidized bed in last tonifying qi cabin, be provided with a plurality of second nozzles on the fluidized bed in tonifying qi cabin down, first nozzle and second nozzle all are located the reducing section, and this air supplement unit can fully solve circulating fluidized bed reaction inhomogeneous and the high backmixing scheduling problem of turbulent motion fluidized bed.
Description
Technical Field
The invention belongs to the technical field of circulating fluidized beds, and particularly relates to an air supplementing device for a fluidized bed.
Background
The fluidized bed has excellent mass transfer and heat transfer characteristics and high-efficiency and quick transport capacity, and is widely applied to various industries such as energy, chemical industry, pharmacy, food, environment and the like. However, the traditional circulating fluidized bed has low particle concentration, low gas-solid contact efficiency and uneven axial and radial flow characteristics, so that the reaction is insufficient and uneven, and the conversion rate of the product is low; although the concentration of particles in the high-density fluidized bed or turbulent fluidized bed is higher, the serious back-mixing phenomenon can occur in the fluidized bed reactor, so that the coking of the catalyst is serious, the catalyst is invalid, and the continuous reaction is adversely affected.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide the air supplement device for the fluidized bed, which can fully solve the problems of non-uniform reaction of the circulating fluidized bed, high back-mixing of a turbulent fluidized bed and the like.
The purpose of the invention is realized by the following technical scheme.
A gas supply for a fluidized bed, comprising: the upper gas supplementing cabin and the lower gas supplementing cabin are both annular cavities and are sleeved outside the fluidized bed, the fluidized bed is sequentially provided with a large-diameter section lifting pipe, a diameter-variable section and a small-diameter section lifting pipe from top to bottom, the upper gas supplementing cabin is sleeved at the lower part of the large-diameter section lifting pipe, the upper part of the diameter-variable section is positioned in the upper gas supplementing cabin, the lower gas supplementing cabin is sleeved at the upper part of the small-diameter section lifting pipe, the lower part of the diameter-variable section is positioned in the lower gas supplementing cabin, a first gas supplementing inlet is formed in the upper gas supplementing cabin, and a second gas supplementing inlet is formed in the lower gas supplementing cabin; the fluidized bed in the upper air supply cabin is provided with a plurality of first nozzles, the fluidized bed in the lower air supply cabin is provided with a plurality of second nozzles, and the first nozzles and the second nozzles are both positioned in the diameter-variable section.
In the technical scheme, a first air supply cabin ash discharge opening is formed in the upper air supply cabin, a cover body is installed on the first air supply cabin ash discharge opening, a second air supply cabin ash discharge opening is formed in the lower air supply cabin, and a cover body is installed on the second air supply cabin ash discharge opening.
In the above technical solution, a plurality of convex pyramids are formed on the inner wall of the variable diameter section.
In the above technical solution, the pyramid is a triangular pyramid.
In the technical scheme, the number of the first nozzles is 4-12 and the first nozzles are arranged on the fluidized bed along the circumferential direction, and the number of the second nozzles is 4-12 and the second nozzles are arranged on the fluidized bed along the circumferential direction.
In the technical scheme, an included angle theta between the inclined plane of the reducing section and the horizontal plane is 40-89 degrees.
In the technical scheme, an included angle between the most upper inclined plane of each pyramid and the inner wall of the diameter-variable section where the pyramid is located is 5-theta degrees.
In the technical scheme, the height of the upper air supplement cabin is 0.25-1 m, and the height of the lower air supplement cabin is 0.25-1 m.
In the technical scheme, the distance between the first nozzle and the central axis of the fluidized bed is R1, the distance between the second nozzle and the central axis of the fluidized bed is R2, and the radius of the large-diameter section riser is R, so that the ratio of 0.75< R1/R <1, and the ratio of 0.5< R2/R <0.75 are obtained.
The air supply device has the following beneficial effects:
1. under the action of the air supply device, the upper part of the small-diameter section lift pipe forms a negative pressure area, so that the pulling effect of gas-solid fluid in the lower part of the small-diameter section lift pipe is improved, the occurrence of choking in the lower part of the small-diameter section lift pipe is inhibited, and the gas-solid flow characteristic in the lower part of the small-diameter section lift pipe obtains the effects of higher particle concentration and uniform axial and radial flow;
2. the upper part of the large-diameter section of the lifting pipe provides a lifting effect for the gas-solid fluid in the upper part of the large-diameter section of the lifting pipe under the action of the gas supplementing device, so that the transportation of the gas-solid fluid is accelerated, and the gas-solid back mixing of the side wall area at the upper part of the large-diameter section of the lifting pipe is reduced.
3. Under the action of the air supplementing device, the solid-fluid flow pattern in the fluidized bed can be partitioned, the small-diameter section of the riser presents a turbulent fluidization flow pattern or a high-density fluidization flow pattern for realizing a dense phase region with a large solid-gas ratio, and the large-diameter section of the riser presents a rapid fluidization or pneumatic conveying flow pattern for presenting a dilute phase region with a small solid-gas ratio.
4. The air supplement device can flexibly control the large-diameter section lifting pipe and the small-diameter section lifting pipe respectively, so that the probability of side reaction and over reaction of the large-diameter section lifting pipe and the small-diameter section lifting pipe is reduced, and the yield of the total reaction target product is improved.
5. The tapered edges which are uniformly distributed are arranged on the inclined edge of the reducing section, so that a gas-solid mixture flowing downwards along the surface of the reducing section can form a blocking effect, the gas-solid mixture can be guided into a gas-solid main flow which is high-speed and upwards and arranged at the center of the lifting pipe of the large-diameter section, and the back mixing of the catalyst is effectively inhibited while the mixing of oil and the agent is accelerated.
Drawings
FIG. 1 is a schematic structural view of the novel combined small diameter section riser fluidized bed reactor of the present invention;
FIG. 2 is a schematic view of the gas supply device;
fig. 3 is a schematic structural view (with pyramid) of the air supply device.
Wherein, 1: compressor, 2: buffer tank, 3: relief valve, 4: first gas flow meter, 5: gas distributor, 6: small diameter section riser, 7: pressure sensor, 8: computer, 9: air supply device, 9-1: ash discharge port of the second air supply cabin, 9-2: a second air supply inlet, 9-3: a first air supply inlet, 9-4: first tonifying qi cabin ash discharge port, 10: fluidized bed, 10-1: first nozzle, 10-2: second nozzle, 11: companion bed, 12: first cyclone, 13: second cyclone, 14: absorbing device, 15: first pipe, 16: second pipe, 17: fifth pipe, 18: fourth pipe, 19: third pipe, 20: tenth pipe, 21: sixth pipe, 22: first valve, 23: eighth conduit, 24: ninth pipe, 25: a seventh conduit.
Detailed Description
The technical solution of the air supply device of the present invention is further described below with reference to the specific embodiments.
The gas distributor 5 can adopt a gas-solid distributor in CN 201210405627.6.
Example 1
The air supplement unit is applied to the fluidized bed, namely, a novel combined small-diameter section riser fluidized bed reaction device, as shown in fig. 1, comprises: fluidized bed 10, gas distributor 5, compressor 1, air supplement unit 9, companion's bed 11 and buffer tank 2, compressor 1 is through the air inlet intercommunication of first pipeline 15 and buffer tank 2, and gas distributor 5 sets up in fluidized bed 10, is provided with 2 gas vents on the buffer tank 2: the first exhaust port of the buffer tank 2 is communicated with a gas distributor 5 in the fluidized bed 10 through a second pipeline 16, the top of the fluidized bed 10 is communicated with a first inlet of the accompanying bed 11 through a tenth pipeline 20 and is used for introducing a catalyst and a gas product into the accompanying bed 11 through the tenth pipeline 20, a first outlet of the accompanying bed 11 is communicated with the fluidized bed 10 through a ninth pipeline 24 and is used for introducing the catalyst into the fluidized bed 10, a second outlet of the accompanying bed 11 is communicated with a gas inlet of a first cyclone separator 12 through a third pipeline 19 and is used for carrying out gas-solid separation on substances in the third pipeline 19, wherein the second outlet is positioned at the upper part of the accompanying bed 11, and the first outlet is positioned at the lower part of the accompanying bed 11.
An ash discharge port of the first cyclone separator 12 is communicated with an air inlet of a second cyclone separator 13 through a fourth pipeline 18 and is used for carrying out gas-solid separation on substances in the fourth pipeline 18, an ash discharge port of the second cyclone separator 13 is communicated with a second inlet of the accompanying bed 11 through a fifth pipeline 17 and is used for introducing a catalyst after the gas-solid separation into the accompanying bed 11, and exhaust ports of the first cyclone separator 12 and the second cyclone separator 13 are communicated with the outside;
a catalyst input port is arranged on the accompanying bed 11, and a cover body is arranged on the catalyst input port;
the air supply device 9 is arranged on the fluidized bed 10, and the second exhaust port of the buffer tank 2 is communicated with the air supply device 9 through an eighth pipeline 23.
The compressor conveys the raw material gas into the buffer tank, so that the raw material gas enters a gas distributor in the fluidized bed or enters an air supplementing device; after the reaction of the catalyst in the solid particle state and the feed gas in the fluidized bed is finished, the catalyst enters a tracing bed, most of the catalyst in the tracing bed is circularly fed back to the fluidized bed through a ninth pipeline 24, and a small part of the catalyst and the feed gas are subjected to gas-solid separation through a first cyclone separator and a second cyclone separator; in operation, the gas supplementing device can realize the partition regulation of the fluidized bed state, a dense phase region (the solid content ratio is between 0.25 and 0.3) with a large solid-gas ratio is formed in the small-diameter section riser 6, and a dilute phase region (the solid content ratio is between 0.03 and 0.08) with a small solid-gas ratio is formed in the large-diameter section riser.
The companion bed is the intermediate carrier of catalyst storage, and the setting of companion bed is higher than little diameter section riser in vertical direction, consequently provides power for the catalyst gets into little diameter section riser, and then has improved little diameter section riser circulation intensity, improves gas-solid contact efficiency, strengthens the radial homogeneity of little diameter section riser internal gas-solid flow axle, increases the productivity effect.
Example 2
As shown in fig. 2 and 3, on the basis of embodiment 1, the air supply device 9 includes: the upper air supplementing cabin and the lower air supplementing cabin are both annular cavities and are sleeved outside the fluidized bed 10, the fluidized bed 10 is sequentially provided with a large-diameter section lifting pipe, a diameter-changing section and a small-diameter section lifting pipe 6 from top to bottom, the upper air supplementing cabin is sleeved at the lower part of the large-diameter section lifting pipe, the upper part of the diameter-changing section is positioned in the upper air supplementing cabin, the lower air supplementing cabin is sleeved at the upper part of the small-diameter section lifting pipe 6, the lower part of the diameter-changing section is positioned in the lower air supplementing cabin, a first air supplementing inlet 9-3 is formed in the upper air supplementing cabin, and a second air supplementing inlet 9-2 is formed in the lower air supplementing cabin; a plurality of first nozzles 10-1 are arranged on the fluidized bed 10 in the upper air supply cabin, a plurality of second nozzles 10-2 are arranged on the fluidized bed 10 in the lower air supply cabin, and the first nozzles 10-1 and the second nozzles 10-2 are both positioned on the reducer section. The first nozzle and the second nozzle arranged in the gas supplementing device divide the upper flow pattern and the lower flow pattern of the fluidized bed, the small diameter section of the riser 6 presents a turbulent fluidization flow pattern or a high-density fluidization flow pattern for realizing a dense phase region with a large solid-gas ratio, and the large diameter section of the riser presents a fast fluidization or a pneumatic conveying flow pattern for realizing a dilute phase region with a small solid-gas ratio.
The gas firstly enters the upper gas supplementing cabin and the lower gas supplementing cabin through the eighth pipeline 23, and then enters the fluidized bed through the first nozzle and the second nozzle.
The number of the first nozzles 10-1 is 4-12 and the first nozzles are circumferentially arranged on the fluidized bed 10, and the number of the second nozzles 10-2 is 4-12 and the second nozzles are circumferentially arranged on the fluidized bed 10.
The distance between the first nozzle 10-1 and the central axis of the fluidized bed 10 is R1, the distance between the second nozzle 10-2 and the central axis of the fluidized bed 10 is R2, and the radius of the riser in the large-diameter section is R, so that 0.75< R1/R <1, and 0.5< R2/R < 0.75.
A first air supply cabin ash discharge port 9-4 is formed in the upper air supply cabin, a cover body is installed on the first air supply cabin ash discharge port 9-4, a second air supply cabin ash discharge port 9-1 is formed in the lower air supply cabin, and a cover body is installed on the second air supply cabin ash discharge port 9-1. The first air supply cabin ash discharge port 9-4 and the second air supply cabin ash discharge port 9-1 are arranged for discharging solid particles in the upper air supply cabin and the lower air supply cabin after meeting an emergency situation. In the air supply process, cover bodies on the ash discharge port 9-4 of the first air supply cabin and the ash discharge port 9-1 of the second air supply cabin are closed, air supply is stopped when abnormal conditions occur, and the cover bodies on the ash discharge port 9-4 of the first air supply cabin and the ash discharge port 9-1 of the second air supply cabin are opened for ash removal.
The inner wall of the variable-diameter section is provided with a plurality of convex pyramids. Preferably, the pyramid is a triangular pyramid. The included angle between the most upper inclined plane of each pyramid and the inner wall of the variable-diameter section where the pyramid is located is 5-theta degrees.
The inclined plane of reducing section and the contained angle theta of horizontal plane are 40 ~ 89.
The height of the upper air supply cabin is 0.25-1 m, and the height of the lower air supply cabin is 0.25-1 m.
The height of the first outlet of the bed 11 is higher than that of the small-diameter section of the riser 6, so that the catalyst discharged from the first outlet can be re-introduced into the fluidized bed under the action of gravity.
Example 3
On the basis of embodiment 2, the eighth conduit 23 is composed of two branch conduits, each branch conduit is provided with a second gas flow meter and a second valve, and the first supplemental gas inlet 9-3 and the second supplemental gas inlet 9-2 are respectively communicated with one branch conduit. The flow rate can be regulated and controlled by 2 branch pipelines independently.
A pressure sensor 7 is provided on the fluidized bed 10, a temperature sensor is provided on the fluidized bed 10, a catalyst concentration sensor is provided on the fluidized bed 10, and a velocity sensor for detecting the velocity of the catalyst is provided on the fluidized bed 10. The pressure sensor 7, the temperature sensor, the catalyst concentration sensor and the speed sensor are all electrically connected with the computer 8.
The exhaust ports of the first cyclone 12 and the second cyclone 13 are communicated with an absorption device 14, and the absorption device 14 is used for absorbing harmful gases and part of catalysts exhausted from the exhaust ports of the first cyclone 12 and the second cyclone 13. The absorption device 14 is communicated with the outside through a seventh pipe 25 for discharging the gas from which the harmful gas is removed and a part of the catalyst. The absorption device 14 is filled with modified fiber material, which can be recycled fiber balls in application No. 2018113390028, to realize the absorption of harmful gas and partial catalyst, thereby improving the environment.
The gas distributor 5 is disposed at the bottom of the small diameter section of the riser 6 of the fluidized bed 10.
The ash outlet of the second cyclone 13 is connected to the small diameter section of the riser 6 of the fluidized bed 10 via a fifth conduit 17.
A first gas flow meter 4 and a first valve 22 are arranged on the second line 16.
The buffer tank 2 has a vent connected to the absorber 14 via a sixth pipe 21, and the sixth pipe 21 is provided with a vent valve 3. The novel combined small-diameter section riser fluidized bed reaction device has the advantages that the vent valve 3 is opened before starting, so that the overlarge pressure of the buffer tank is avoided; when the novel combined small-diameter section riser fluidized bed reaction device operates, the air release valve 3 is regulated (when the first valve 22 and the second valve regulate large gas flow, the air release valve 3 is closed, when the first valve 22 and the second valve regulate small gas flow, the air release valve 3 is opened to avoid overlarge pressure of the buffer tank), and gas-solid flow in the fluidized bed reaches a specific flow pattern through the cooperation with the first valve 22 on the second pipeline 16; before the novel combined small-diameter section riser fluidized bed reaction device stops, the emptying valve 3 is opened again.
The invention has been described in an illustrative manner, and it is to be understood that any simple variations, modifications or other equivalent changes which can be made by one skilled in the art without departing from the spirit of the invention fall within the scope of the invention.
Claims (10)
1. A gas compensator for a fluidized bed, comprising: the upper air supplementing cabin and the lower air supplementing cabin are both annular cavities and are sleeved outside the fluidized bed (10), the fluidized bed (10) is sequentially provided with a large-diameter section lifting pipe, a diameter-variable section and a small-diameter section lifting pipe (6) from top to bottom, the upper air supplementing cabin is sleeved on the lower portion of the large-diameter section lifting pipe, the upper portion of the diameter-variable section is located in the upper air supplementing cabin, the lower air supplementing cabin is sleeved on the upper portion of the small-diameter section lifting pipe (6), the lower portion of the diameter-variable section is located in the lower air supplementing cabin, a first air supplementing inlet (9-3) is formed in the upper air supplementing cabin, and a second air supplementing inlet (9-2) is formed in the lower air supplementing cabin; a plurality of first nozzles (10-1) are arranged on the fluidized bed (10) in the upper air replenishing cabin, a plurality of second nozzles (10-2) are arranged on the fluidized bed (10) in the lower air replenishing cabin, and the first nozzles (10-1) and the second nozzles (10-2) are located in the diameter-changing section.
2. The air supplement device according to claim 1, wherein a first air supplement chamber ash discharge port (9-4) is formed on the upper air supplement chamber, and a cover body is mounted on the first air supplement chamber ash discharge port (9-4).
3. The air supplement device according to claim 2, wherein a second air supplement chamber ash discharge port (9-1) is formed on the lower air supplement chamber, and a cover body is mounted on the second air supplement chamber ash discharge port (9-1).
4. The gas compensator of claim 1, wherein the inner wall of the reducer section is formed with a plurality of convex pyramids.
5. The gas compensator of claim 4, wherein the pyramid is a triangular pyramid.
6. The air compensating device according to claim 4, characterized in that the angle between the most upper inclined surface of each pyramid and the inner wall of the tapered section where the pyramid is located is 5- θ °.
7. The gas supplementing device according to claim 1, wherein the number of the first nozzles (10-1) is 4 to 12 and arranged on the fluidized bed (10) in the circumferential direction, and the number of the second nozzles (10-2) is 4 to 12 and arranged on the fluidized bed (10) in the circumferential direction.
8. The gas supplementing device according to claim 1, wherein the first nozzle (10-1) is at a distance R1 from the central axis of the fluidized bed (10), the second nozzle (10-2) is at a distance R2 from the central axis of the fluidized bed (10), and the radius of the large diameter section riser is R, so that 0.75< R1/R <1, 0.5< R2/R < 0.75.
9. The gas supplementing device according to claim 1, wherein the inclined surface of the reducing section forms an included angle θ of 40-89 ° with the horizontal plane.
10. The air supplement device according to claim 1, wherein the upper air supplement compartment has a height of 0.25-1 m, and the lower air supplement compartment has a height of 0.25-1 m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011453476.2A CN114618398A (en) | 2020-12-11 | 2020-12-11 | Air supplement device for fluidized bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011453476.2A CN114618398A (en) | 2020-12-11 | 2020-12-11 | Air supplement device for fluidized bed |
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| Publication Number | Publication Date |
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| CN114618398A true CN114618398A (en) | 2022-06-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011453476.2A Pending CN114618398A (en) | 2020-12-11 | 2020-12-11 | Air supplement device for fluidized bed |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253934A (en) * | 2022-07-18 | 2022-11-01 | 中国石油大学(北京) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method |
-
2020
- 2020-12-11 CN CN202011453476.2A patent/CN114618398A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253934A (en) * | 2022-07-18 | 2022-11-01 | 中国石油大学(北京) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method |
| CN115253934B (en) * | 2022-07-18 | 2023-10-24 | 中国石油大学(北京) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method |
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