CN114053961B - Feeding distributor and reactor - Google Patents
Feeding distributor and reactor Download PDFInfo
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- CN114053961B CN114053961B CN202010766896.XA CN202010766896A CN114053961B CN 114053961 B CN114053961 B CN 114053961B CN 202010766896 A CN202010766896 A CN 202010766896A CN 114053961 B CN114053961 B CN 114053961B
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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
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
Abstract
The invention discloses a feeding distributor and a reactor, relating to the technical field of reactors, wherein the feeding distributor comprises: the included angle between the first gas distribution pipe and the horizontal direction is 30-90 degrees; the second gas distribution pipe is communicated with the first gas distribution pipe and is annularly arranged on a horizontal plane; one end of the air inlet pipe is communicated with the second gas distribution pipe; a plurality of gas distribution holes opened on the first gas distribution pipe and/or the second gas distribution pipe; this feeding distributor can realize the distribution of feeding in the reactor, improves the feeding effect of reactor.
Description
Technical Field
The invention belongs to the technical field of reactors, and particularly relates to a feeding distributor and a reactor.
Background
With the aggravation of the heavy and inferior crude oil trend in China, how to process inferior residual oil efficiently becomes a focus of attention. At present, about 2 hundred million tons of domestic processed residual oil are processed every year, and the main means for processing the inferior residual oil are delayed coking, fixed bed residual oil hydrogenation, fluidized bed hydrogenation, slurry bed residual oil hydrogenation and other processing technologies. The slurry bed residual oil hydrogenation technology is almost not limited by reaction raw materials, the conversion rate of the raw materials is high and can reach 90%, the liquid yield is high, the operation period is long, the method is one of important ways for lightening inferior residual oil, is expected to replace a delayed coking device, and is an important technical means for transformation development of modern refineries. Therefore, slurry bed residuum hydrogenation technology has received much attention and has been vigorously developed in recent years.
The slurry bed reactor is the core equipment of the slurry bed residual oil hydrogenation technology. In recent years, with the rapid development of coal chemical industry and petrochemical industry, researchers and engineers at home and abroad develop corresponding treatment processes and reactors for specific reaction systems through continuous research, development and improvement.
In the existing slurry bed reactor technology, a large amount of research and development work is carried out on the aspects of gas-liquid distribution uniformity, liquid reflux, catalyst or solid particle deposition, system coking and the like, and partial problems are solved, but the problems that how to improve the primary conversion rate of the raw materials of the reactor, the bubble coalescence at the middle upper part of the reactor, the large thickness of the laminar boundary layer near the wall of the reactor and the like are solved, the stable operation of the device is ensured, and the problems that the technical personnel in the field need to solve urgently are solved.
Disclosure of Invention
The invention aims to solve the problems in the prior art, and provides a feeding distributor and a reactor, which realize the distribution of feeding in the reactor and improve the feeding effect of the reactor.
In order to achieve the above object, the present invention provides a feed distributor comprising:
the first gas distribution pipe forms an included angle of 30-90 degrees with the horizontal direction;
the second gas distribution pipe is communicated with the first gas distribution pipe and is annularly arranged on a horizontal plane;
one end of the air inlet pipe is communicated with the second gas distribution pipe;
a plurality of gas distribution holes opened on the first gas distribution pipe and/or the second gas distribution pipe.
Optionally, the first gas distribution pipe is provided in plurality, and the plurality of first gas distribution pipes are parallel to each other.
Optionally, the second gas distribution pipe is provided with a plurality of, and a plurality of the second gas distribution pipes are respectively arranged on planes parallel to each other.
Optionally, the equivalent diameter of the gas distribution holes gradually decreases along the feed distributor from bottom to top, and the equivalent diameter of the gas distribution holes is 1mm to 15mm.
Optionally, the aperture ratio of the gas distribution holes on the first gas distribution pipe and/or the second gas distribution pipe is 0.05% -45%, and the range of the included angle between the axis of the gas distribution hole and the horizontal direction is-80 ° to 80 °.
Optionally, the distance between adjacent first gas distribution pipes is 3 to 50 times the diameter of the first gas distribution pipes, and the distance between adjacent second gas distribution pipes is 3 to 50 times the diameter of the second gas distribution pipes.
The present invention also provides a reactor comprising:
a reactor body;
the liquid phase feed inlet is arranged at the bottom of the reactor body;
the gas feed inlet is arranged on the side wall of the reactor body;
a reaction product outlet disposed at the top of the reactor body;
the feeding distributor is arranged inside the reactor body;
the other end of the air inlet pipe is communicated with the gas feed port.
Optionally, the reactor body is cylindrical, the second gas distribution pipe is annular, a vertical axis of the ring is collinear with a vertical axis of the reactor body, and a ratio of the radius of the ring to the radius of the cylinder is 0.5-0.95.
Optionally, 3 feeding distributors are sequentially arranged in the reactor body from top to bottom, and each feeding distributor is communicated with an independent gas feeding hole.
Optionally, the reactor further comprises a partition plate, the partition plate is arranged inside the reactor body, a fluid distributor is arranged on the partition plate, the fluid distributor can allow fluid to pass through, one of the lowest feed distributors is arranged below the partition plate, and the other two feed distributors are arranged above the partition plate.
The invention provides a feeding distributor and a reactor, which have the beneficial effects that:
1. the reactor is internally provided with the feeding distributor which is coaxial with the reactor body, the equivalent diameter of a gas distribution hole on the feeding distributor is gradually reduced along the direction from bottom to top of the feeding distributor, the larger the hole diameter is, the lower the gas flow velocity is, the pressure drop of the gas passing through a large hole is small, the large hole is arranged at the position close to the bottom of the reactor, and the small hole is arranged at the position close to the top of the reactor, so that the gas content in a liquid phase can be increased, and the liquid phase conversion rate can be improved;
2. the feeding distributor provided by the invention improves the uniform distribution degree of gas and liquid in the reactor, the equivalent diameter of the gas distribution holes is gradually reduced along the direction from bottom to top of the feeding distributor, the flow velocity of gas sprayed by the gas distribution holes is gradually increased from bottom to top, and the gas and liquid phase disturbance degree near the wall of the reactor is favorably increased and the thickness of the laminar boundary layer near the wall of the reactor is reduced through the specific opening rate and opening orientation on the first gas distribution pipe and/or the second gas distribution pipe, so that the coalescence of bubbles in the process that the gas and liquid phases in the reactor flow from the bottom to the top is avoided, more liquid phase substances near the wall of the reactor participate in the reaction, and the reaction effect is improved.
3. The feeding distributor is arranged above and below the partition plate and the fluid distributor in the reactor, so that the uniform mixing of gas and liquid phases in the reactor is fundamentally ensured, no dead zone exists in the whole reactor, the reaction conversion efficiency is improved, and the deposition of solid particles at the bottom of the reactor can be reduced;
4. the reactor with the feeding distributor provided by the invention realizes multi-point gas injection through the plurality of gas feeding holes, and has the advantages of large liquid phase treatment capacity, strong applicability, stable device operation, flexible operation, large operation elasticity and the like.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings, wherein like reference numerals generally represent like parts in the exemplary embodiments of the present invention.
Fig. 1 shows a schematic structural diagram of a feed distributor according to a first embodiment of the present invention.
Fig. 2 is a schematic sectional view of the structure of fig. 1 taken along the direction a according to a first embodiment of the present invention.
Fig. 3 shows a schematic structural diagram of a reactor according to a first embodiment of the invention.
Fig. 4 shows a schematic structural view of gas distribution holes on a first gas distribution pipe of a feed distributor according to a first embodiment of the present invention.
Fig. 5 shows a schematic structural view of gas distribution holes on a second gas distribution pipe of a feed distributor according to a first embodiment of the present invention.
Fig. 6 shows a schematic structural view of gas distribution holes on a first gas distribution pipe of a feed distributor according to a second embodiment of the present invention.
Fig. 7 shows a schematic view of the structure of the gas distribution holes on the second gas distribution pipe of a feed distributor according to the second embodiment of the present invention.
Fig. 8 shows a schematic structural view of gas distribution holes on a first gas distribution pipe of a feed distributor according to a third embodiment of the present invention.
Fig. 9 shows a schematic structural view of gas distribution holes on a second gas distribution pipe of a feed distributor according to a third embodiment of the present invention.
Fig. 10 shows a schematic view of the structure of the gas distribution holes on the first gas distribution pipe of a feed distributor according to a fourth embodiment of the present invention.
Fig. 11 shows a schematic view of the structure of the gas distribution holes on the second gas distribution pipe of a feed distributor according to a fourth embodiment of the present invention.
Fig. 12 shows a schematic structural diagram of a feed distributor according to example five of the present invention.
Fig. 13 shows a schematic view of the structure of the gas distribution holes on the second gas distribution pipe of a feed distributor according to example five of the present invention.
Description of reference numerals:
1. a first gas distribution pipe; 2. a second gas distribution pipe; 3. an air inlet pipe; 4. a gas distribution aperture; 5. a reactor body; 6. a liquid phase feed inlet; 7. a gas feed port; 8. a reaction product outlet; 9. a partition plate; 10. a fluid distributor.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
The present invention provides a feed distributor comprising:
the included angle between the first gas distribution pipe and the horizontal direction is 30-90 degrees;
the second gas distribution pipe is communicated with the first gas distribution pipe and is annularly arranged on a horizontal plane;
one end of the air inlet pipe is communicated with the second gas distribution pipe;
a plurality of gas distribution holes opened on the first gas distribution pipe and/or the second gas distribution pipe.
Specifically, the gas materials enter the first gas distribution pipe and the second gas distribution pipe of the feeding distributor through the gas inlet pipe, and can be distributed in the reactor through the gas distribution holes distributed in the first gas distribution pipe and/or the second gas distribution pipe, so that the feeding effect of the reactor is improved.
Optionally, the first gas distribution pipe is provided in plurality, and the plurality of first gas distribution pipes are parallel to each other.
Specifically, the lengths of the first gas distribution pipes arranged in parallel in the vertical direction are equal, the upper end and the lower end of each first gas distribution pipe are communicated with the second gas distribution pipes, and a plurality of second gas distribution pipes can be arranged between the upper second gas distribution pipe and the lower second gas distribution pipe.
In one example, the gas distribution holes open on the first gas distribution pipe.
Optionally, the second gas distribution pipes are provided in plurality, and the plurality of second gas distribution pipes are respectively provided on planes parallel to each other.
Specifically, a plurality of second gas distribution pipes are arranged in a stacked mode in the vertical direction at intervals, and the plurality of second gas distribution pipes are communicated with each other through the vertical first gas distribution pipe.
In one example, the gas distribution holes open on the second gas distribution pipe.
Further, the feeding distributor is communicated with the feeding hole through a gas connecting pipeline, the number and the size of the connecting pipeline are determined according to the actual gas consumption, and the number of the connecting pipelines is generally 2-8, preferably 2-4.
Further, in order to realize the gas circulation in each gas distribution pipe, the first gas distribution pipe 1 is in fluid communication through at least one second gas communication pipeline, and second gas communication pipes may be respectively disposed at the center and both ends of the first gas distribution pipe; when the second gas distribution pipes are a plurality of pipes, the preferred arrangement mode is that the second gas distribution pipes are arranged at equal intervals, and the second gas distribution pipes are in fluid communication through at least one first gas communication pipe arranged in the circumferential direction of the second gas distribution pipes; when the first gas distribution pipes are multiple, the preferred arrangement is that the first gas communication pipes are arranged at equal intervals in the circumferential direction of the annular second gas distribution pipe.
Optionally, the equivalent diameter of the gas distribution holes is gradually reduced along the direction from bottom to top of the feed distributor, and the equivalent diameter of the gas distribution holes is 1mm to 15mm.
Specifically, in order to realize uniform distribution of gas and liquid phases and increase the gas content and the turbulence degree of the liquid phase, because the static pressures at different heights in the reactor are different, the gas distribution holes on the first gas distribution pipe and the second gas distribution pipe are gradually reduced from bottom to top, and the equivalent diameter of the gas distribution hole at the top is 0.03-0.99 times, preferably 0.1-0.9 times of the equivalent diameter of the bottom distribution hole.
Further, the shape of the gas distribution holes may be at least one of circular, triangular, rectangular, oval, and regular polygonal, and for ease of processing and reduction of production cost, the circular, triangular, and rectangular distribution holes are preferred, and the circular shape is most preferred.
Optionally, the aperture ratio of the gas distribution holes on the first gas distribution pipe and/or the second gas distribution pipe is 0.05% -45%, and the included angle between the axis of the gas distribution hole and the horizontal direction ranges from-80 ° to 80 °.
Specifically, in order to realize the uniform distribution of the gas-liquid phase at the upper part of the reactor, the opening rate of the first gas distribution pipe and the second gas distribution pipe is 0.05-45%, preferably 0.3-30%, and the lower the opening rate is, the less the gas throughput is; in order to increase the turbulence degree of the liquid and reduce the thickness of the laminar boundary layer near the wall of the device, the included angle alpha between the gas distribution holes on the first gas distribution pipe and the horizontal plane is between-80 degrees and alpha is between 80 degrees, and the preferred included angle alpha is between-60 degrees and alpha is between 60 degrees and alpha; the included angle alpha between the gas distribution holes on the second gas distribution pipe and the horizontal plane is between minus 80 degrees and alpha is between minus 60 degrees and alpha is between 60 degrees and alpha is preferred.
Optionally, the distance between adjacent first gas distribution pipes is 3-50 times the diameter of the first gas distribution pipes and the distance between adjacent second gas distribution pipes is 3-50 times the diameter of the second gas distribution pipes.
Specifically, in order to reduce the influence of the addition of the feeding distributor on the gas-liquid phase flow field in the reactor and simultaneously take the reinforcing effect of the feeding distributor into consideration, the distance between the adjacent first gas distribution pipes in the circumferential direction of the second gas distribution pipe is 3 times to 50 times of the diameter of the first gas distribution pipe, and the optimal distance is 5 times to 30 times of the diameter of the first gas distribution pipe; the distance between the adjacent second gas distribution pipes in the vertical direction is 3 to 50 times of the diameter of the second gas distribution pipes, and the preferable distance is 5 to 30 times of the diameter of the second gas distribution pipes; the material of the first and second distribution pipes is not specifically limited, and may be a metal material, such as: 316 stainless steel, carbon steel, etc.; but also can be non-metal materials, such as: the polymer composite material, the ceramic material and the like can meet the performance requirements of the distributor such as mechanical strength, corrosion resistance, gas distribution and the like.
The present invention also provides a reactor comprising:
a reactor body;
the liquid phase feed inlet is arranged at the bottom of the reactor body;
the gas feed inlet is arranged on the side wall of the reactor body;
the reaction product outlet is arranged at the top of the reactor body;
the feeding distributor is arranged inside the reactor body;
the other end of the air inlet pipe is communicated with the air inlet.
In one example, the reactor is a slurry bed reactor, the gas feed inlets of the reactor body comprise a # 1 gas feed inlet, a # 2 gas feed inlet and a # 3 gas feed inlet, a liquid-phase reactant enters from the bottom of the reactor body and starts to react after being mixed with a gas-phase medium sent out from the # 3 feed distributor, the gas-liquid-phase material flow enters the upper space of the partition plate after passing through the fluid distributor on the partition plate and being uniformly distributed again, and a reaction product leaves the reactor body from the top of the reactor after the reinforcing action of the # 2 feed distributor and the # 1 feed distributor in the whole reactor.
Optionally, the reactor body is cylindrical, the second gas distribution pipe is annular, a vertical axis of the ring is collinear with a vertical axis of the reactor body, and a ratio of a radius of the ring to a radius of the cylinder is 0.5-0.95.
Optionally, a feed distributor consisting of the first gas distribution pipe and/or the second gas distribution pipe is coaxial with the reactor, the ratio R of the inner diameter (R1) of the feed distributor to the inner diameter (R2) of the reactor is 0.5-0.95, and the preferable ratio R is 0.7-0.85; the axial height of the feed distributor is from 0.2 to 0.9 times the tangential length of the reactor barrel, preferably from 0.3 to 0.7 times the tangential length of the reactor barrel.
Specifically, in order to realize the uniform distribution of the gas-liquid phase at the upper part of the reactor and simultaneously facilitate the installation, the manufacture and the mechanical stability of the feeding distributor, the feeding distributor consisting of the first distribution pipe and/or the second gas distribution pipe is coaxial with the reactor.
Optionally, 3 feeding distributors are sequentially arranged in the reactor body from top to bottom, and each feeding distributor is communicated with an independent gas feeding hole.
Specifically, in order to improve the conversion rate of the liquid phase reactant and simultaneously prevent the solid-containing materials from depositing at the bottom of the reactor and from being in a gas-poor phase region, a 2# feed distributor and a 3# feed distributor are further arranged at the lower part of the 1# feed distributor, the 2# feed distributor is in fluid communication with the 2# feed inlet, the 3# feed distributor is in fluid communication with the 3# feed inlet, the 2# feed distributor is the same as the gas medium distributed by the 3# feed distributor, and the gas medium distributed by the 2# feed distributor and the 3# feed distributor can also be the same as the gas medium in the 1# feed distributor; in addition, when the reactor has temperature runaway, a cooling medium can be injected into the reactor through a cooling medium pipeline preset outside the reactor through a No. 1 feeding hole, the selection of the cooling medium is closely related to the reaction system, and generally, for a residual oil hydrogenation system, the cooling medium adopts liquid-phase quenching oil, such as vacuum wax oil, heavy diesel oil and the like, and can also be quenching hydrogen.
Optionally, the reactor further comprises a partition plate, the partition plate is arranged inside the reactor body, the partition plate is provided with a fluid distributor, the fluid distributor can allow fluid to pass through, one feed distributor positioned at the lowest part is arranged below the partition plate, and the other two feed distributors are arranged above the partition plate.
Specifically, the No. 2 feeding distributor is positioned at the upper part of the partition plate, the No. 3 feeding distributor is positioned at the lower part of the partition plate, and the partition plate is provided with a fluid distributor for fluid to pass through, so that the gas-liquid phase is uniformly distributed; the fluid distributor can be a common bubble cap structure or a specific fluid distributor, and the structure, the material and the like of the fluid distributor are not particularly limited as long as the gas-liquid phase is uniformly distributed, the strength, the corrosion resistance, the long-period stable operation and the low price are met; the fluid distributor is arranged on the partition plate, the upper space and the lower space of the partition plate in the reactor body can only be communicated through a flow channel in the fluid distributor, the partition plate is a plate which is well known by a person skilled in the art and divides the reactor body into two sections of cavities, and the details of the disclosure are omitted; further, the structure and form of the # 2 feed distributor and the # 3 feed distributor are not particularly limited as long as the uniform distribution of the reaction gas in the bottom region of the reactor is satisfied.
Example one
As shown in fig. 1 to 5, the present invention provides a feed distributor comprising:
the first gas distribution pipe 1, the included angle of the first gas distribution pipe 1 and the horizontal direction is 90 degrees;
the second gas distribution pipe 2 is communicated with the first gas distribution pipe 1, and the second gas distribution pipe 2 is annularly arranged on a horizontal plane;
one end of the air inlet pipe 3 is communicated with the second gas distribution pipe 2;
a plurality of gas distribution holes 4 opened on the first gas distribution pipe 1 and/or the second gas distribution pipe 2.
In the present embodiment, the first gas distribution pipes 1 are provided in plurality, and the plurality of first gas distribution pipes 1 are parallel to each other.
In the present embodiment, the second gas distribution pipes 2 are provided in plurality, and the plurality of second gas distribution pipes 2 are respectively provided on planes parallel to each other.
In this embodiment, the equivalent diameter of the gas distribution holes 4 is gradually reduced from the bottom to the top of the feed distributor, and the equivalent diameter of the gas distribution holes is 1mm to 15mm.
In this embodiment, the aperture ratio of the gas distribution holes 4 on the first gas distribution pipe 1 and/or the second gas distribution pipe 2 is 0.05% -45%, and the included angle between the axis of the gas distribution hole 4 and the horizontal direction ranges from-80 ° to 80 °.
In the present embodiment, the distance between adjacent first gas distribution pipes 1 is 3 to 50 times the diameter of the first gas distribution pipes 1, and the distance between adjacent second gas distribution pipes 2 is 3 to 50 times the diameter of the second gas distribution pipes 2.
The present invention also provides a reactor comprising:
a reactor body 5;
a liquid phase feed inlet 6 arranged at the bottom of the reactor body 5;
a gas feed port 7 provided on the side wall of the reactor body 5;
a reaction product outlet 8 disposed at the top of the reactor body 5;
the above-mentioned feed distributor is arranged inside the reactor body 5;
the other end of the air inlet pipe 3 is communicated with the air inlet 7.
In this embodiment, the reactor body 5 is cylindrical, the second gas distribution pipe 2 is annular, the vertical axis of the ring is collinear with the vertical axis of the reactor body 5, and the ratio of the radius of the ring to the radius of the cylinder is 0.5-0.95.
In this embodiment, 3 feeding distributors are sequentially arranged in the reactor body 5 from top to bottom, and each feeding distributor is communicated with an independent gas feeding port 7.
In this embodiment, the reactor further comprises a partition 9, the partition 9 is disposed inside the reactor body 5, a fluid distributor 10 is disposed on the partition 9, the fluid distributor 10 can allow fluid to pass through, one feed distributor located at the lowest position is disposed below the partition 9, and the other two feed distributors are disposed above the partition 9.
Further, the feed reactor in this embodiment is provided with 4 first gas distribution pipes 1 and 7 second gas distribution pipes 2, the length of the first gas distribution pipe 1 is 25m, the diameter is 40mm, the diameter of the circular ring of the second gas distribution pipe 2 of the feed distributor is 3.8m, and the distance between two adjacent second gas distribution pipes 2 is 350mm. The structure of the gas distribution holes 4 is shown in fig. 4 and 5, the gas distribution holes 4 are circular holes, the diameter of the gas distribution hole 4 at the bottom is 12mm, the diameter of the gas distribution hole 4 at the top is 9mm, and the aperture ratio is 5.3%. The feed distributor was installed in a reactor main body 5, the reactor main body 5 had an inner diameter of 4.8m and a height of 40m, and gas-liquid distribution function of bubble caps were provided on a partition 9, and the number of bubble caps was 1150.
In conclusion, when the reactor provided by the invention is used, the reactor is applied to the hydrogenation reaction of inferior residual oil, and the reactor body 5 and the feeding distributor are both made of 2.25Cr-Mo-V materials. The average reaction temperature in the reactor is 435 ℃, the reaction pressure is 18.5MPa, and the space velocity is 0.18h -1 And the media introduced into the three feeding distributors are all hydrogen. Through actual measurement, the difference between the highest temperature and the lowest temperature in the reactor is 0.3 ℃, which shows that the gas-liquid phase is uniformly distributed; the liquid phase one-time pass conversion rate of the reactor reaches 92 percent, and after the test of 8400h long-period reaction, the reaction is carried outThe existing feed distributor, the baffle 9 and the inner wall of the reactor body 5 have no obvious change. Compared with the conventional slurry bed reactor, the gas-liquid phase in the reactor is uniformly distributed, the temperature difference of each point of the reactor is obviously smaller, the conventional slurry bed is generally higher than 5 ℃, the primary conversion rate of the conventional slurry bed is not more than 85 percent, and the coking is easy to occur. The long-period industrial test result shows that the feeding distributor and the reactor provided by the invention have reasonable structures, and the gas-liquid phase mass transfer effect of the reactor is obvious. In addition, the feed distributor provided by the embodiment can also be used for other gas-liquid phase reaction systems, such as: fischer-Tropsch synthesis reaction, gas-liquid-solid three-phase systems and the like; the feeding distributor provided by the invention has the advantages of large treatment capacity, strong applicability, flexible operation, high raw material conversion rate, stable device operation and the like.
The difference between the feed distributor and the reactor provided in example two, example three and example four and example one is that: the structure of the gas distribution holes 4 on the first gas distribution pipe 1 and the structure of the gas distribution holes 4 on the second gas distribution pipe 2 are different, and the structures of the gas distribution holes 4 on the first gas distribution pipe 1 and the second gas distribution pipe 2 of the feed distributor provided in examples two, three and four are shown in fig. 6 to 11.
The difference between the feed distributor and the reactor provided in example five and example one is that: the included angle between the first gas distribution pipe 1 and the horizontal plane is 75 degrees, the second gas distribution pipe adopts holes opened along the central line direction of the ring pipe, the included angle between the holes and the horizontal plane is 45 degrees, the structure of the distributor and the structure of the gas distribution holes 4 on the second gas distribution pipe 2 are shown in figures 12 and 13.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (6)
1. A reactor, comprising:
a reactor body;
the liquid phase feed inlet is arranged at the bottom of the reactor body;
the gas feed inlet is arranged on the side wall of the reactor body;
a reaction product outlet disposed at the top of the reactor body;
a feed distributor disposed inside the reactor body; the feed distributor comprises:
the first gas distribution pipe forms an included angle of 30-90 degrees with the horizontal direction;
the second gas distribution pipe is communicated with the first gas distribution pipe, and the second gas distribution pipe is annularly arranged on a horizontal plane;
one end of the air inlet pipe is communicated with the second gas distribution pipe;
a plurality of gas distribution holes opened on the first gas distribution pipe and/or the second gas distribution pipe;
the equivalent diameter of the gas distribution holes is gradually reduced along the direction from bottom to top of the feed distributor, and the equivalent diameter of the gas distribution holes is 1mm to 15mm;
3 feeding distributors are sequentially arranged in the reactor body from top to bottom, and each feeding distributor is communicated with an independent gas feeding hole; the baffle is arranged in the reactor body, the baffle is provided with a fluid distributor, the fluid distributor can be used for fluid to pass through, the lowest feeding distributor is arranged below the baffle, and the other two feeding distributors are arranged above the baffle;
the other end of the air inlet pipe is communicated with the gas feed port.
2. The reactor of claim 1, wherein the first gas distribution pipe is provided in plurality, and a plurality of the first gas distribution pipes are parallel to each other.
3. The reactor according to claim 1, wherein the second gas distribution pipe is provided in plurality, and the plurality of second gas distribution pipes are respectively provided on planes parallel to each other.
4. The reactor according to claim 1, wherein the opening ratio of the gas distribution holes on the first gas distribution pipe and/or the second gas distribution pipe is 0.05-45%, and the included angle between the axis of the gas distribution holes and the horizontal direction ranges from-80 ° to 80 °.
5. The reactor of claim 1, wherein a distance between adjacent first gas distribution pipes is 3-50 times a diameter of the first gas distribution pipes and a distance between adjacent second gas distribution pipes is 3-50 times a diameter of the second gas distribution pipes.
6. The reactor of claim 1, wherein the reactor body is cylindrical, the second gas distribution tube is annular, a vertical axis of the annular ring is collinear with a vertical axis of the reactor body, and a ratio of a radius of the annular ring to a radius of the cylinder is 0.5-0.95.
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| CN202010766896.XA CN114053961B (en) | 2020-08-03 | 2020-08-03 | Feeding distributor and reactor |
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| CN202010766896.XA CN114053961B (en) | 2020-08-03 | 2020-08-03 | Feeding distributor and reactor |
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| CN114053961B true CN114053961B (en) | 2023-01-03 |
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| CN105056844B (en) * | 2015-08-07 | 2017-04-12 | 北京华福工程有限公司 | Gas distributor for acetylene hydrogenation to ethylene slurry reactor and application thereof |
| CN105854530A (en) * | 2016-06-19 | 2016-08-17 | 张罡 | Casting-type liquid distributor |
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| CN206121712U (en) * | 2016-10-20 | 2017-04-26 | 王潇 | Preparation hydrogenation dicyclopentadiene petroleum resin's hydrogenation cauldron |
| CN108786669B (en) * | 2017-04-27 | 2021-01-12 | 中国科学院大连化学物理研究所 | Fluidized bed gas distributor, reactor using same and method for co-producing p-xylene and low-carbon olefin |
| CN206935363U (en) * | 2017-06-14 | 2018-01-30 | 上海凌凯医药科技有限公司 | A kind of chemical laboratory reactor |
| CN108085067A (en) * | 2017-12-28 | 2018-05-29 | 新奥科技发展有限公司 | A kind of gas distributor of fludized bed, fluidized-bed reactor and its gasification process |
| CN208390000U (en) * | 2018-04-20 | 2019-01-18 | 漯河美迪康生物科技有限公司 | A kind of reaction unit of furans chlorination |
| CN208865611U (en) * | 2018-06-29 | 2019-05-17 | 中国石油化工股份有限公司 | Bubbled gas distributor and bubbling bed reactor |
| CN109134233B (en) * | 2018-10-19 | 2019-08-30 | 兖矿鲁南化工有限公司 | A kind of process units and production method of synthesizing acetic acid by methanol low-voltage carbonylation |
| CN210079510U (en) * | 2019-04-26 | 2020-02-18 | 安徽诺全药业有限公司 | Ticagrelor raw material medicine synthesis reaction kettle |
| CN211133865U (en) * | 2019-07-04 | 2020-07-31 | 华东理工大学 | Fractal bubble configuration controllable slurry bed reactor |
| CN110433509A (en) * | 2019-08-30 | 2019-11-12 | 浙江工业大学 | A kind of inert particles fluidized bed liquid distribution trough |
| CN110652941A (en) * | 2019-11-01 | 2020-01-07 | 中国科学院过程工程研究所 | Micro-bubbling hydrogenation reactor and application thereof |
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2020
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