CN116078275A - High-efficiency gas distributor and vertical large-scale reactor - Google Patents
High-efficiency gas distributor and vertical large-scale reactor Download PDFInfo
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- CN116078275A CN116078275A CN202310001020.XA CN202310001020A CN116078275A CN 116078275 A CN116078275 A CN 116078275A CN 202310001020 A CN202310001020 A CN 202310001020A CN 116078275 A CN116078275 A CN 116078275A
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- 238000007789 sealing Methods 0.000 claims description 19
- 230000005540 biological transmission Effects 0.000 claims description 10
- 230000007704 transition Effects 0.000 claims description 10
- 238000000034 method Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 124
- 238000009826 distribution Methods 0.000 description 30
- 239000012495 reaction gas Substances 0.000 description 20
- 239000000376 reactant Substances 0.000 description 12
- 210000002445 nipple Anatomy 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
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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
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/02—Feed or outlet devices therefor
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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
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/04—Pressure vessels, e.g. autoclaves
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Abstract
The invention belongs to the technical field of pressure vessels, and particularly relates to a high-efficiency gas distributor and a vertical large-scale reactor. The technical proposal is as follows: the utility model provides a high-efficient gas distributor, includes the outer guide plate of tubaeform, and outer guide plate passes through first gusset to be connected in the upper end enclosure of vertical large-scale reactor, and outer guide plate is located the inlet connection pipe below of vertical large-scale reactor, and the upper segment diameter of outer guide plate is less than the internal diameter that the inlet connection was managed, is provided with tubaeform inlayer guide plate in the outer guide plate, is provided with spiral guide vane on the inlayer guide plate. The invention provides a high-efficiency gas distributor capable of converting the flow direction of gas into radial direction and a vertical large-scale reactor with the high-efficiency gas distributor.
Description
Technical Field
The invention belongs to the technical field of pressure vessels, and particularly relates to a high-efficiency gas distributor and a vertical large-scale reactor.
Background
Along with the development of economy and the progress of scientific technology in China, chemical equipment tends to be large-sized more and more, and various chemical reactors are more and more. The increased capacity of the device means increased flow, and for a reactor with gas inlet materials and non-distributed central area, the gas inlet connecting pipes are axially arranged at the center of the reactor, and high-flow-rate gas enters the reactor through the gas inlet connecting pipes and directly impacts a tube plate area without distributed tubes, so that the impact on the tube plate is not beneficial to the safety of the device. Meanwhile, uneven gas velocity distribution can occur in a cavity at the upper end of the reactor, so that the reaction efficiency is affected on one hand; on the other hand, gas vortex can be caused in the cavity, and the safety of equipment is endangered. The more uniform the gas distribution, the more favorable the stable progress and heat release of chemical reaction, and the higher the equipment reliability. The addition of a gas distributor at the lower end of the gas inlet enhances the uniform distribution of the gas. On the premise of continuously enlarging the reactor, the novel gas distributor structural design also needs to keep pace.
The traditional reactor gas distributor is generally a regular cone column or a reverse cone column, and holes are formed in the cone surface to strengthen gas distribution; there are also chinese patents which designed gas distributors with guide vanes, which utilize differential gas pressure to drive gas to be spirally distributed, so as to improve the uniformity of gas distribution at the inlet. The gas distributors have good application effect in small-sized equipment, however, when the equipment is large in scale and size, the structure can only influence the gas distribution in a certain area by taking a gas inlet as a center, and even distribution can not be ensured at the edge of the equipment and the area close to a reaction tube. Thus, the structural optimization of the gas distributor also has a large lifting space.
Disclosure of Invention
In order to solve the above problems in the prior art, an object of the present invention is to provide a high-efficiency gas distributor capable of converting a flow direction of gas into a radial direction and a vertical large-sized reactor with the high-efficiency gas distributor.
The technical scheme adopted by the invention is as follows:
the utility model provides a high-efficient gas distributor, includes the outer guide plate of tubaeform, and outer guide plate passes through first gusset to be connected in the upper end enclosure of vertical large-scale reactor, and outer guide plate is located the inlet connection pipe below of vertical large-scale reactor, and the upper segment diameter of outer guide plate is less than the internal diameter that the inlet connection was managed, is provided with tubaeform inlayer guide plate in the outer guide plate, is provided with spiral guide vane on the inlayer guide plate.
The outer-layer guide plate changes the speed direction of the gas which is split into the axial direction and the radial direction from the axial direction, so that the gas is more uniformly distributed at the outer edge part of the upper seal head. The surface of the inner-layer guide plate and the guide vanes form a spiral flow channel, when gas passes through the flow channel, the gas flow direction can be changed, radial force is generated, and when the gas leaves the flow channel, the gas continues to flow spirally. And the inner-layer guide plate can shield the middle part of the tube plate, so that the impact on the tube plate is reduced. The gas is radially diffused along the inner-layer guide plate, the gas distribution in the upper space of the tube plate non-tube distribution area is less, the safety of the reactor is facilitated, and the gas distribution in the tube plate tube distribution area can be more uniform due to the addition of spiral gas flow.
The diameter of the upper section of the outer guide plate is smaller than the inner diameter of the air inlet connecting pipe, so that an airflow channel between the outer side of the outer guide plate and the inner wall of the upper end socket is ensured, and the flow dead zone of the upper end socket is reduced.
As the preferable scheme of the invention, the air inlet pipe also comprises an outer magnet which is rotatably connected in the air inlet pipe, an inner magnet is arranged in the outer magnet, the inner magnet is connected with a shaft through a second rib plate and a third rib plate, and the lower end of the shaft is connected with an inner layer guide plate.
As a preferable mode of the invention, the external magnet is connected with a power device through a transmission mechanism. When the power equipment drives the outer magnet to rotate through the transmission mechanism, the inner magnet also rotates along with the outer magnet, and then the inner-layer guide plate fixed on the inner magnet also rotates synchronously. The higher the power of the external power equipment, the faster the inner-layer guide plate rotates. When the reaction gas contacts the inner-layer guide plate and the guide vane, the gas starts to change direction, flows along the formed spiral flow channel, and after leaving the guide vane, the reaction gas starts to be uniformly distributed in a spiral mode.
As a preferable scheme of the invention, the outer-layer guide plate and the inner-layer guide plate comprise an upper straight section, a middle circular arc transition section and a lower positive cone section.
As a preferable scheme of the invention, the diameter of the upper straight section of the outer-layer guide plate is 0.4-0.7 times of the inner diameter of the air inlet connecting pipe, and the height is 0.18-0.25 times of the height of the upper sealing head.
As a preferable scheme of the invention, the included angle between the bus of the lower positive cone section of the outer layer guide plate and the horizontal line is 0-45 ℃.
The vertical large-scale reactor comprises a cylinder body, wherein a tube plate is connected in the cylinder body, an upper sealing head is connected to the cylinder body, an air inlet connecting pipe is connected to the upper sealing head, and a connecting pipe flange is connected to the air inlet connecting pipe; the gas distributor is arranged in the upper sealing head and comprises a horn-shaped outer layer guide plate, the outer layer guide plate is connected in the upper sealing head through a first rib plate, the outer layer guide plate is positioned below the gas inlet connecting pipe, the diameter of the upper section of the outer layer guide plate is smaller than the inner diameter of the gas inlet connecting pipe, a horn-shaped inner layer guide plate is arranged in the outer layer guide plate, and spiral guide vanes are arranged on the inner layer guide plate.
The outer-layer guide plate changes the speed direction of the gas which is split into the axial direction and the radial direction from the axial direction, so that the gas is more uniformly distributed at the outer edge part of the upper seal head. The surface of the inner-layer guide plate and the guide vanes form a spiral flow channel, when gas passes through the flow channel, the gas flow direction can be changed, radial force is generated, and when the gas leaves the flow channel, the gas continues to flow spirally. And the inner-layer guide plate can shield the middle part of the tube plate, so that the impact on the tube plate is reduced. The gas is radially diffused along the inner-layer guide plate, the gas distribution in the upper space of the tube plate non-tube distribution area is less, the safety of the reactor is facilitated, and the gas distribution in the tube plate tube distribution area can be more uniform due to the addition of spiral gas flow.
The diameter of the upper section of the outer guide plate is smaller than the inner diameter of the air inlet connecting pipe, so that an airflow channel between the outer side of the outer guide plate and the inner wall of the upper end socket is ensured, and the air dead zone of the upper end socket is reduced.
As a preferable scheme of the invention, the air inlet connecting pipe is internally and rotatably connected with an outer magnet, an inner magnet is arranged in the outer magnet, the inner magnet is connected with a shaft through a second rib plate and a third rib plate, and the lower end of the shaft is connected with an inner layer guide plate.
As a preferable mode of the invention, the external magnet is connected with a power device through a transmission mechanism. When the power equipment drives the outer magnet to rotate through the transmission mechanism, the inner magnet also rotates along with the outer magnet, and then the inner-layer guide plate fixed on the inner magnet also rotates synchronously. The higher the power of the external power equipment, the faster the inner-layer guide plate rotates. When the reaction gas contacts the inner-layer guide plate and the guide vane, the gas starts to change direction, flows along the formed spiral flow channel, and after leaving the guide vane, the reaction gas starts to be uniformly distributed in a spiral mode.
As a preferable scheme of the invention, the outer-layer guide plate and the inner-layer guide plate comprise an upper straight section, a middle circular arc transition section and a lower positive cone section.
As a preferable scheme of the invention, the diameter of the upper straight section of the outer-layer guide plate is 0.4-0.7 times of the inner diameter of the air inlet connecting pipe, and the height is 0.18-0.25 times of the height of the upper sealing head.
As a preferable scheme of the invention, the included angle between the bus of the lower positive cone section of the outer layer guide plate and the horizontal line is 0-45 ℃.
The beneficial effects of the invention are as follows:
1. the outer-layer guide plate changes the speed direction of the gas which is split into the axial direction and the radial direction from the axial direction, so that the gas is more uniformly distributed at the outer edge part of the upper seal head. The surface of the inner-layer guide plate and the guide vanes form a spiral flow channel, when gas passes through the flow channel, the gas flow direction can be changed, radial force is generated, and when the gas leaves the flow channel, the gas continues to flow spirally. And the inner-layer guide plate can shield the middle part of the tube plate, so that the impact on the tube plate is reduced. The gas is radially diffused along the inner-layer guide plate, the gas distribution in the upper space of the tube plate non-tube distribution area is less, the safety of the reactor is facilitated, and the gas distribution in the tube plate tube distribution area can be more uniform due to the addition of spiral gas flow.
2. The diameter of the upper section of the outer-layer guide plate is smaller than the inner diameter of the air inlet connecting pipe, so that an airflow channel between the outer side of the outer-layer guide plate and the inner wall of the upper end socket is ensured, and the air flow dead zone of the upper end socket is reduced.
Drawings
FIG. 1 is a schematic view of a vertical large reactor;
FIG. 2 is a front view of a gas distributor;
fig. 3 is a top view of a gas distributor.
In the figure: 1-a cylinder; 2-an upper sealing head; 3-an air inlet connection pipe; 4-connecting pipe flanges; 5-gas distributor; 6-tube plate; 51-an outer deflector; 52-an inner baffle; 53-a first gusset; 54-second rib plates; 55-third rib plates; 56-axis; 57-guide vanes; 58-an inner magnet; 59-an external magnet.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the invention, as presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
Example 1:
as shown in fig. 1 to 3, the high-efficiency gas distributor 5 of the present embodiment includes a horn-shaped outer layer deflector 51, the outer layer deflector 51 is connected to the inside of the upper end enclosure 2 of the vertical large reactor through a first rib plate 53, the outer layer deflector 51 is located below the gas inlet connection pipe 3 of the vertical large reactor, the diameter of the upper section of the outer layer deflector 51 is smaller than the inner diameter of the gas inlet connection pipe 3, a horn-shaped inner layer deflector 52 is disposed in the outer layer deflector 51, and spiral guide vanes 57 are disposed on the inner layer deflector 52.
The outer-layer guide plate 51 changes the speed direction of the gas which is split into the axial direction and the radial direction, so that the gas is distributed more uniformly in the outer edge area of the upper sealing head 2. The surface of the inner baffle 52 and the guide vanes 57 form a spiral flow path, and when the gas passes through the flow path, the gas can change the direction of the gas flow to generate radial force, and when the gas leaves the flow path, the gas continues to flow spirally. And, the inner layer guide plate 52 can shelter from the middle part of the tube plate 6, thereby reducing the impact on the tube plate 6. The gas is radially diffused along the inner-layer guide plate 52, the gas distribution in the upper space of the area where the tube plate 6 is not distributed is less, the safety of the reactor is facilitated, and the gas distribution in the upper seal head 2 can be more uniform due to the addition of the spiral gas flow in the tube plate 6 distribution area.
The diameter of the upper section of the outer guide plate 51 is smaller than the inner diameter of the air inlet connecting pipe 3, so that an airflow channel between the outer side of the outer guide plate 51 and the inner wall of the upper seal head 2 is ensured, and the air flow dead zone of the upper seal head 2 is reduced.
Further, an outer magnet 59 is connected in a rotary manner to the air inlet connecting pipe 3 of the vertical large reactor, an inner magnet 58 is arranged in the outer magnet 59, the inner magnet 58 is connected with a shaft 56 through a second rib plate 54 and a third rib plate 55, and the lower end of the shaft 56 is connected with the inner deflector 52. The external magnet 59 is connected to a power device via a gear or a belt or other transmission mechanism. When the power device drives the outer magnet 59 to rotate through the transmission mechanism, the inner magnet 58 also rotates, and thus the inner baffle 52 fixed to the inner magnet 58 also rotates synchronously. The greater the power of the external power device, the faster the inner baffle 52 rotates. When the reactant gas contacts the inner baffle plate 52 and the guide vanes 57, the gas starts to change direction, flows along the spiral flow channel formed, and after leaving the guide vanes 57, the reactant gas starts to be uniformly distributed in a spiral shape.
Wherein the diameter of the cylinder body 1 is 6-12 m, the central area of the tube plate 6 is provided with an area without tube distribution, and the diameter of the area without tube distribution at the center of the tube plate 6 is 0.25-0.35 times of the diameter of the cylinder body 1.
Wherein, the outer layer guide plate 51 and the inner layer guide plate 52 each comprise an upper straight section, a middle circular arc transition section and a lower positive cone section. The upper straight section of the outer layer baffle 51 extends into the interior of the inlet nipple 3. The radius of the arc of the middle arc transition section of the outer-layer guide plate 51 and the middle arc transition section of the inner-layer guide plate 52 is 150-300 mm.
The diameter of the upper straight section of the outer layer guide plate 51 is 0.4-0.7 times of the inner diameter of the air inlet connecting pipe 3, and the height is 0.18-0.25 times of the height of the upper sealing head 2. The included angle between the bus of the lower positive cone section of the outer layer guide plate 51 and the horizontal line is 0-45 ℃.
The diameter of the bottom surface circle of the lower positive cone section of the inner layer guide plate 52 is 0.5-1 times of the inner diameter of the air inlet connecting pipe 3, and the height is 150-300 mm. The included angle between the lower positive cone section bus of the inner layer guide plate 52 and the horizontal line is 0-45 ℃. The flow passage formed between the guide vanes 57 is spiral, and the number of the guide vanes 57 is at least three.
Working principle:
for a certain tubular reactor, the inlet reaction gas is a mixture of air and a certain substance. The reaction gas enters the adapter flange 4 along the upstream pipeline and then enters the inlet adapter 3. The gas distributor 5 is disposed directly below the gas inlet nipple 3. In this embodiment, since the outer layer baffle 51 is disposed in the air inlet pipe 3, the air in the air inlet pipe is divided into two paths, and one path flows through the cavity formed by the upper end enclosure 2 and the outer layer baffle 51. When the reaction gas flows along the axial direction until contacting the outer surface of the outer guide plate 51, the reaction gas starts to flow along the outer surface of the outer guide plate 51, after leaving the outer surface of the outer guide plate 51, the gas speed continues to be divided into two directions, and flows downwards along the axial direction and outwards along the radial direction, the reaction gas can move farther along the radial direction before entering the tube plate 6, and the gas dead zone of the upper seal head 2 is small. The other path of reaction gas flows between the cavity formed by the outer layer baffle 51 and the inner layer baffle 52. When the reactant gas contacts the inner baffle plate 52 and the guide vanes 57, the gas starts to change direction, flows along the spiral flow channel formed, and after leaving the guide vanes 57, the reactant gas starts to be uniformly distributed in a spiral shape. When the outer magnet 59 is rotated by external power, the inner magnet 58 is rotated, and the inner baffle 52 fixed to the inner magnet 58 is rotated synchronously. The greater the power of the external motive force, the faster the inner baffle 52 rotates. Meanwhile, the reaction gas cannot directly impact the tube plate 6, the gas flow in the upper space of the tube plate 6 in the non-tube distribution area is extremely slow, and the flow path of the gas is reduced. The gas distributor 5 of the invention ensures that the reaction gas is distributed more uniformly in the upper seal head 2 after entering the upper seal head 2.
When no external power is applied, the inner magnet 58 is fixed, and the inner baffle 52 and the guide vane 57 are fixed. A spiral channel is formed between the inner guide plate 52 and the spiral inner guide vane 57. When the reactant gas contacts the inner baffle plate 52 and the guide vanes 57, the gas starts to change direction, flows along the spiral flow channel formed, and after leaving the guide vanes 57, the reactant gas starts to be uniformly distributed in a spiral shape.
Example 2:
as shown in fig. 1 to 3, the vertical large-scale reactor of the embodiment comprises a cylinder 1, wherein a tube plate 6 is connected in the cylinder 1, an upper sealing head 2 is connected to the cylinder 1, an air inlet connecting pipe 3 is connected to the upper sealing head 2, and a connecting pipe flange 4 is connected to the air inlet connecting pipe 3; the gas distributor 5 is arranged in the upper sealing head 2, the gas distributor 5 comprises a horn-shaped outer layer guide plate 51, the outer layer guide plate 51 is connected in the upper sealing head 2 through a first rib plate 53, the outer layer guide plate 51 is positioned below the air inlet connecting pipe 3, the diameter of the upper section of the outer layer guide plate 51 is smaller than the inner diameter of the air inlet connecting pipe 3, a horn-shaped inner layer guide plate 52 is arranged in the outer layer guide plate 51, and spiral guide vanes 57 are arranged on the inner layer guide plate 52.
The outer-layer guide plate 51 changes the speed direction of the gas which is split into the axial direction and the radial direction, so that the gas is distributed more uniformly at the outer edge of the upper sealing head 2. The surface of the inner baffle 52 and the guide vanes 57 form a spiral flow path, and when the gas passes through the flow path, the gas can change the direction of the gas flow to generate radial force, and when the gas leaves the flow path, the gas continues to flow spirally. And, the inner layer guide plate 52 can shelter from the middle part of the tube plate 6, thereby reducing the impact on the tube plate 6. The gas is radially diffused along the inner-layer guide plate 52, the gas distribution in the upper space of the area where the tube plate 6 is not distributed is less, the safety of the reactor is facilitated, and the gas distribution in the upper seal head 2 can be more uniform due to the addition of the spiral gas flow in the tube plate 6 distribution area.
The diameter of the upper section of the outer guide plate 51 is smaller than the inner diameter of the air inlet connecting pipe 3, so that an airflow channel between the outer side of the outer guide plate 51 and the inner wall of the upper seal head 2 is ensured, and the air flow dead zone of the upper seal head 2 is reduced.
Further, an outer magnet 59 is rotatably connected to the air inlet connection pipe 3, an inner magnet 58 is disposed in the outer magnet 59, the inner magnet 58 is connected to a shaft 56 through a second rib plate 54 and a third rib plate 55, and the lower end of the shaft 56 is connected to the inner deflector 52. The external magnet 59 is connected to a power device via a gear or a belt or other transmission mechanism. When the power device drives the outer magnet 59 to rotate through the transmission mechanism, the inner magnet 58 also rotates, and thus the inner baffle 52 fixed to the inner magnet 58 also rotates synchronously. The greater the power of the external power device, the faster the inner baffle 52 rotates. When the reactant gas contacts the inner baffle plate 52 and the guide vanes 57, the gas starts to change direction, flows along the spiral flow channel formed, and after leaving the guide vanes 57, the reactant gas starts to be uniformly distributed in a spiral shape.
Wherein the diameter of the cylinder body 1 is 6-12 m, the central area of the tube plate 6 is provided with an area without tube distribution, and the diameter of the area without tube distribution at the center of the tube plate 6 is 0.25-0.35 times of the diameter of the cylinder body 1.
Wherein, the outer layer guide plate 51 and the inner layer guide plate 52 each comprise an upper straight section, a middle circular arc transition section and a lower positive cone section. The upper straight section of the outer layer baffle 51 extends into the interior of the inlet nipple 3. The radius of the arc of the middle arc transition section of the outer-layer guide plate 51 and the middle arc transition section of the inner-layer guide plate 52 is 150-300 mm.
The diameter of the upper straight section of the outer layer guide plate 51 is 0.4-0.7 times of the inner diameter of the air inlet connecting pipe 3, and the height is 0.18-0.25 times of the height of the upper sealing head 2. The included angle between the bus of the lower positive cone section of the outer layer guide plate 51 and the horizontal line is 0-45 ℃.
The diameter of the bottom surface circle of the lower positive cone section of the inner layer guide plate 52 is 0.5-1 times of the inner diameter of the air inlet connecting pipe 3, and the height is 150-300 mm. The included angle between the lower positive cone section bus of the inner layer guide plate 52 and the horizontal line is 0-45 ℃. The flow passage formed between the guide vanes 57 is spiral, and the number of the guide vanes 57 is at least three.
Working principle:
for a certain tubular reactor, the inlet reaction gas is a mixture of air and a certain substance. The reaction gas enters the adapter flange 4 along the upstream pipeline and then enters the inlet adapter 3. The gas distributor 5 is disposed directly below the gas inlet nipple 3. In this embodiment, since the outer layer baffle 51 is disposed in the air inlet pipe 3, the air in the air inlet pipe is divided into two paths, and one path flows through the cavity formed by the upper end enclosure 2 and the outer layer baffle 51. When the reaction gas flows along the axial direction until contacting the outer surface of the outer guide plate 51, the reaction gas starts to flow along the outer surface of the outer guide plate 51, after leaving the outer surface of the outer guide plate 51, the gas speed direction continues to be divided into two directions, and flows downwards along the axial direction and outwards along the radial direction, the reaction gas can move farther along the radial direction before entering the tube plate 6, and the gas dead zone of the upper seal head 2 is small. The other path of reaction gas flows between the cavity formed by the outer layer baffle 51 and the inner layer baffle 52. When the reactant gas contacts the inner baffle plate 52 and the guide vanes 57, the gas starts to change direction, flows along the spiral flow channel formed, and after leaving the guide vanes 57, the reactant gas starts to be uniformly distributed in a spiral shape. When the outer magnet 59 is rotated by external power, the inner magnet 58 is rotated, and the inner baffle 52 fixed to the inner magnet 58 is rotated synchronously. The greater the power of the external motive force, the faster the inner baffle 52 rotates. Meanwhile, the reaction gas cannot directly impact the tube plate 6, the gas flow in the upper space of the tube plate 6 in the non-tube distribution area is extremely slow, and the flow path of the gas is reduced. The gas distributor 5 of the invention ensures that the reaction gas is distributed more uniformly in the upper seal head 2 after entering the upper seal head 2.
When no external power is applied, the inner magnet 58 is fixed, and the inner baffle 52 and the guide vane 57 are fixed. A spiral channel is formed between the inner baffle 52 and the spiral guide vane 57. When the reactant gas contacts the inner baffle plate 52 and the guide vanes 57, the gas starts to change direction, flows along the spiral flow channel formed, and after leaving the guide vanes 57, the reactant gas starts to be uniformly distributed in a spiral shape.
The invention is not limited to the above-described alternative embodiments, and any person who may derive other various forms of products in the light of the present invention, however, any changes in shape or structure thereof, all falling within the technical solutions defined in the scope of the claims of the present invention, fall within the scope of protection of the present invention.
Claims (10)
1. A high efficiency gas distributor, characterized in that: including tubaeform outer guide plate (51), outer guide plate (51) are connected in vertical large-scale reactor's upper end enclosure (2) through first gusset (53), outer guide plate (51) are located vertical large-scale reactor's inlet connection pipe (3) below, the upper segment diameter of outer guide plate (51) is less than the internal diameter of inlet connection pipe (3), be provided with tubaeform inlayer guide plate (52) in outer guide plate (51), be provided with helical guide vane (57) on inlayer guide plate (52).
2. A high efficiency gas distributor according to claim 1, wherein: the air inlet pipe is characterized by further comprising an outer magnet (59) rotatably connected in the air inlet pipe (3), an inner magnet (58) is arranged in the outer magnet (59), the inner magnet (58) is connected with a shaft (56) through a second rib plate (54) and a third rib plate (55), and the lower end of the shaft (56) is connected with an inner-layer guide plate (52).
3. A high efficiency gas distributor according to claim 2, wherein: the outer magnet (59) is connected with power equipment through a transmission mechanism.
4. A high efficiency gas distributor according to claim 1, wherein: the outer-layer guide plate (51) and the inner-layer guide plate (52) comprise an upper straight section, a middle circular arc transition section and a lower positive cone section.
5. A high efficiency gas distributor according to claim 4, wherein: the diameter of the upper straight section of the outer layer guide plate (51) is 0.4-0.7 times of the inner diameter of the air inlet connecting pipe (3), the height of the upper straight section is 0.18-0.25 times of the height of the upper sealing head (2), and the included angle between the bus of the lower positive cone section of the outer layer guide plate (51) and the horizontal line is 0-45 ℃.
6. The vertical large-scale reactor comprises a cylinder body (1), wherein a tube plate (6) is connected in the cylinder body (1), an upper sealing head (2) is connected to the cylinder body (1), an air inlet connecting pipe (3) is connected to the upper sealing head (2), and a connecting pipe flange (4) is connected to the air inlet connecting pipe (3); the method is characterized in that: be provided with gas distributor (5) in upper head (2), gas distributor (5) are including tubaeform outer guide plate (51), outer guide plate (51) are connected in upper head (2) through first gusset (53), outer guide plate (51) are located air inlet connection pipe (3) below, the upper segment diameter of outer guide plate (51) is less than the internal diameter of air inlet connection pipe (3), be provided with tubaeform inlayer guide plate (52) in outer guide plate (51), be provided with helical guide vane (57) on inlayer guide plate (52).
7. A vertical large scale reactor according to claim 6, wherein: the air inlet connecting pipe (3) is rotationally connected with an outer magnet (59), an inner magnet (58) is arranged in the outer magnet (59), the inner magnet (58) is connected with a shaft (56) through a second rib plate (54) and a third rib plate (55), and the lower end of the shaft (56) is connected with the inner-layer guide plate (52).
8. A vertical large scale reactor according to claim 7, wherein: the outer magnet (59) is connected with power equipment through a transmission mechanism.
9. A vertical large scale reactor according to claim 6, wherein: the outer-layer guide plate (51) and the inner-layer guide plate (52) comprise an upper straight section, a middle circular arc transition section and a lower positive cone section.
10. A vertical large scale reactor according to claim 9, wherein: the diameter of the upper straight section of the outer layer guide plate (51) is 0.4-0.7 times of the inner diameter of the air inlet connecting pipe (3), the height of the upper straight section is 0.18-0.25 times of the height of the upper sealing head (2), and the included angle between the bus of the lower positive cone section of the outer layer guide plate (51) and the horizontal line is 0-45 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310001020.XA CN116078275B (en) | 2023-01-03 | 2023-01-03 | High-efficiency gas distributor and vertical large-scale reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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Citations (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1529137A (en) * | 1966-10-28 | 1968-06-14 | Exxon Research Engineering Co | Fluid flow distributor |
| US4292274A (en) * | 1980-08-04 | 1981-09-29 | United Technologies Corporation | Catalytic reactor with improved burner |
| EP0413835A1 (en) * | 1989-08-08 | 1991-02-27 | Siemens Aktiengesellschaft | Container with a reaction vessel for chemical reactions, and process for operating this container |
| WO2002011877A1 (en) * | 2000-08-10 | 2002-02-14 | Totalfinaelf France | Novel method for homogeneous loading of solid particles in a chamber |
| CN1586703A (en) * | 2004-07-21 | 2005-03-02 | 清华大学 | Spherical high pressure multiple phase reactor |
| JP2011012945A (en) * | 2009-07-04 | 2011-01-20 | Ashida Mfg Co Ltd | Hot air circulation method and device for autoclave |
| CN203183918U (en) * | 2013-04-25 | 2013-09-11 | 甘肃蓝科石化高新装备股份有限公司 | Efficient gas distributor |
| CN103769011A (en) * | 2012-10-20 | 2014-05-07 | 中国石油化工股份有限公司 | Gas pre-distributor of fluidized bed reactor |
| CN203737214U (en) * | 2014-03-18 | 2014-07-30 | 兰州寰球工程公司 | Low-resistance combined type gas uniform distributor used in fixed bed reactor |
| WO2015007901A1 (en) * | 2013-07-19 | 2015-01-22 | Arkema France | Reactor for preparing hydrogen cyanide by the andrussow process, equipment comprising said reactor and process using such an equipment |
| CN204933414U (en) * | 2015-09-25 | 2016-01-06 | 石家庄波特无机膜分离设备有限公司 | A kind of full welding gas distributor |
| CN205032155U (en) * | 2015-10-09 | 2016-02-17 | 罗田广惠化工有限责任公司 | Axial fixity bed reaction gas redistributor |
| CN106040105A (en) * | 2016-07-04 | 2016-10-26 | 茂名重力石化机械制造有限公司 | Convex airflow distribution plate and reactor thereof |
| CN207805337U (en) * | 2017-12-29 | 2018-09-04 | 无锡海悦生化装备有限公司 | A kind of air sparger for air cooling de-watering apparatus |
| CN207941489U (en) * | 2017-12-29 | 2018-10-09 | 北京华和拓科技开发有限责任公司 | A kind of gas distributor |
| CN208003912U (en) * | 2018-01-19 | 2018-10-26 | 惠生工程（中国）有限公司 | A kind of axial entrance gas distributor |
| FR3083994A1 (en) * | 2018-07-19 | 2020-01-24 | IFP Energies Nouvelles | LOAD DISTRIBUTOR FOR AXIAL FLOW REACTOR |
| CN110801790A (en) * | 2019-10-17 | 2020-02-18 | 江苏华洋新思路能源装备股份有限公司 | Spiral jet type gas reaction pressure container |
| CN112023839A (en) * | 2020-08-10 | 2020-12-04 | 浙江大学 | Gas pre-distributor of fluidized bed reactor |
| CN216296266U (en) * | 2021-11-10 | 2022-04-15 | 东华工程科技股份有限公司 | Methyl acetate hydrogenation reactor |
| CN114505014A (en) * | 2022-04-19 | 2022-05-17 | 北京中科富海低温科技有限公司 | Pressure container |
| CN216756368U (en) * | 2022-02-22 | 2022-06-17 | 北京石油化工工程有限公司 | Reactor for producing methyl acrylate by using methanol and methyl acetate as raw materials |
-
2023
- 2023-01-03 CN CN202310001020.XA patent/CN116078275B/en active Active
Patent Citations (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1529137A (en) * | 1966-10-28 | 1968-06-14 | Exxon Research Engineering Co | Fluid flow distributor |
| US4292274A (en) * | 1980-08-04 | 1981-09-29 | United Technologies Corporation | Catalytic reactor with improved burner |
| EP0413835A1 (en) * | 1989-08-08 | 1991-02-27 | Siemens Aktiengesellschaft | Container with a reaction vessel for chemical reactions, and process for operating this container |
| WO2002011877A1 (en) * | 2000-08-10 | 2002-02-14 | Totalfinaelf France | Novel method for homogeneous loading of solid particles in a chamber |
| CN1586703A (en) * | 2004-07-21 | 2005-03-02 | 清华大学 | Spherical high pressure multiple phase reactor |
| JP2011012945A (en) * | 2009-07-04 | 2011-01-20 | Ashida Mfg Co Ltd | Hot air circulation method and device for autoclave |
| CN103769011A (en) * | 2012-10-20 | 2014-05-07 | 中国石油化工股份有限公司 | Gas pre-distributor of fluidized bed reactor |
| CN203183918U (en) * | 2013-04-25 | 2013-09-11 | 甘肃蓝科石化高新装备股份有限公司 | Efficient gas distributor |
| WO2015007901A1 (en) * | 2013-07-19 | 2015-01-22 | Arkema France | Reactor for preparing hydrogen cyanide by the andrussow process, equipment comprising said reactor and process using such an equipment |
| CN203737214U (en) * | 2014-03-18 | 2014-07-30 | 兰州寰球工程公司 | Low-resistance combined type gas uniform distributor used in fixed bed reactor |
| CN204933414U (en) * | 2015-09-25 | 2016-01-06 | 石家庄波特无机膜分离设备有限公司 | A kind of full welding gas distributor |
| CN205032155U (en) * | 2015-10-09 | 2016-02-17 | 罗田广惠化工有限责任公司 | Axial fixity bed reaction gas redistributor |
| CN106040105A (en) * | 2016-07-04 | 2016-10-26 | 茂名重力石化机械制造有限公司 | Convex airflow distribution plate and reactor thereof |
| CN207805337U (en) * | 2017-12-29 | 2018-09-04 | 无锡海悦生化装备有限公司 | A kind of air sparger for air cooling de-watering apparatus |
| CN207941489U (en) * | 2017-12-29 | 2018-10-09 | 北京华和拓科技开发有限责任公司 | A kind of gas distributor |
| CN208003912U (en) * | 2018-01-19 | 2018-10-26 | 惠生工程（中国）有限公司 | A kind of axial entrance gas distributor |
| FR3083994A1 (en) * | 2018-07-19 | 2020-01-24 | IFP Energies Nouvelles | LOAD DISTRIBUTOR FOR AXIAL FLOW REACTOR |
| CN110801790A (en) * | 2019-10-17 | 2020-02-18 | 江苏华洋新思路能源装备股份有限公司 | Spiral jet type gas reaction pressure container |
| CN112023839A (en) * | 2020-08-10 | 2020-12-04 | 浙江大学 | Gas pre-distributor of fluidized bed reactor |
| CN216296266U (en) * | 2021-11-10 | 2022-04-15 | 东华工程科技股份有限公司 | Methyl acetate hydrogenation reactor |
| CN216756368U (en) * | 2022-02-22 | 2022-06-17 | 北京石油化工工程有限公司 | Reactor for producing methyl acrylate by using methanol and methyl acetate as raw materials |
| CN114505014A (en) * | 2022-04-19 | 2022-05-17 | 北京中科富海低温科技有限公司 | Pressure container |
Also Published As
| Publication number | Publication date |
|---|---|
| CN116078275B (en) | 2024-06-07 |
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