CN113083162A - Large-scale propane dehydrogenation propylene preparation reactor - Google Patents

Large-scale propane dehydrogenation propylene preparation reactor Download PDF

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Publication number
CN113083162A
CN113083162A CN202110474939.1A CN202110474939A CN113083162A CN 113083162 A CN113083162 A CN 113083162A CN 202110474939 A CN202110474939 A CN 202110474939A CN 113083162 A CN113083162 A CN 113083162A
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reactor
barrel
outlet
combined
inlet
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Inventor
孙中心
张万尧
马建强
何德强
梁元月
王慧
张晓阳
冯小朋
郭雨
王建刚
徐澍
董富荣
秦云龙
巩乐
崔建航
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Tianhua Institute of Chemical Machinery and Automation Co Ltd
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Tianhua Institute of Chemical Machinery and Automation Co Ltd
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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
    • B01J3/006—Processes utilising sub-atmospheric pressure; Apparatus therefor
    • 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
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0292—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds with stationary packing material in the bed, e.g. bricks, wire rings, baffles
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
    • C07C5/333—Catalytic processes

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention provides a large-scale reactor for preparing propylene by propane dehydrogenation, which is a horizontal reactor and comprises a cylinder body, wherein a heat-insulating layer is arranged on the inner wall of the cylinder body, an arch bridge type reaction bed layer is arranged in the cylinder body and divides the interior of the cylinder body into an upper reaction zone and a lower reaction zone, a process channel is arranged on the reaction bed layer and communicates the upper reaction zone with the lower reaction zone, two ends of the cylinder body are respectively provided with an end enclosure, an external reinforcing ring I is arranged at the straight edge of the end enclosure, and at least two external reinforcing rings II are arranged on the outer wall of the cylinder body. The reactor provided by the invention has the advantages of large volume, high reaction efficiency, high reaction conversion rate and stable and reliable performance, and can realize continuous large-scale production.

Description

Large-scale propane dehydrogenation propylene preparation reactor
Technical Field
The invention relates to the technical field of new energy and chemical equipment, in particular to a large-scale reactor for preparing propylene by propane dehydrogenation.
Background
Propylene is an important chemical raw material and also a direct raw material for producing polypropylene, and the demand of polypropylene is rising year by year in recent years, so that the supply of the propylene raw material is short. The preparation of propylene by propane dehydrogenation is a relatively popular propylene production technology in recent years, a reactor of the technology is a key device of a device for preparing propylene by propane dehydrogenation, raw material propane is gasified and then heated to about 600 ℃ to enter the reactor, the operating temperature of the reactor is about 590-650 ℃, and dehydrogenation reaction is carried out in the reactor under the action of a catalyst to convert the raw material propane into propylene and hydrogen.
Disclosure of Invention
Based on the above, the invention aims to provide a fixed bed propane dehydrogenation propylene preparation reactor which is large in size, high in yield, high in reaction conversion rate, safe and stable.
The reactor is a horizontal reactor and comprises a cylinder body, wherein a heat-insulating layer is arranged on the inner wall of the cylinder body, an arch bridge type reaction bed layer is arranged in the cylinder body and divides the interior of the cylinder body into an upper reaction zone and a lower reaction zone, a process channel is arranged on the reaction bed layer and communicates the upper reaction zone with the lower reaction zone, two ends of the cylinder body are respectively provided with an end enclosure, an external reinforcing ring I is arranged at the straight edge of each end enclosure, and at least two external reinforcing rings II are arranged on the outer wall of the cylinder body.
Specifically, the heat-insulating layer can control the heat loss of the reactor and ensure that the dehydrogenation reaction is carried out at the environmental temperature required by the process; after the catalyst falls onto the arch bridge type reaction bed layer, the catalyst is distributed more uniformly due to the fact that the shape of the reaction bed layer is beneficial to the dispersion of the catalyst, the external reinforcing ring I and the external reinforcing ring II can reinforce the strength and rigidity of the end socket and the cylinder body, and the end socket and the cylinder body can be guaranteed not to be deformed unstably under the negative pressure state; the roundness of the cylinder can be controlled by the external reinforcing ring II, so that the cross section of the cylinder is prevented from being changed from a circle to an ellipse. Through the arrangement of the components, the invention aims to provide a large-scale reactor for preparing propylene by propane dehydrogenation.
In the reactor of the present invention, preferably, the heat insulating layer is built by heat insulating refractory bricks, and an oil gas blocking ring is disposed between the heat insulating layer and the inner wall of the cylinder.
In the reactor of the present invention, it is preferable that a crotch-shaped combined inlet is provided at the top of the barrel, and the combined inlet includes a steam and reducing gas inlet, an air inlet, and a hydrocarbon inlet; catalyst loading and unloading ports are arranged on two sides of the combined inlet at the top of the cylinder body; an h-shaped combined outlet is formed in one side of the bottom of the cylinder body and comprises an air outlet and an air suction opening, and a sampling opening is formed in the pipe wall of the air outlet; a hydrocarbon outlet is formed in the other side of the bottom of the cylinder body, and a sampling port is formed in the pipe wall of the hydrocarbon outlet; the top and the bottom of the cylinder body are respectively provided with at least one manhole for internal part installation, internal construction and maintenance.
In the reactor of the present invention, preferably, the diameter of the cylinder is greater than 7 meters, the total external length of the cylinder including the left and right end sockets is greater than 19 meters, the distance between the flange sealing surface of the combined inlet and the center line of the cylinder is greater than 10 meters, the distance between the bottom of the combined outlet and the center line of the cylinder is greater than 6 meters, and the volume of the reactor is greater than 900 cubic meters.
Specifically, due to the arrangement of the components such as the heat-insulating layer, the external reinforcing ring and the like, the main body material of the large-scale reactor cylinder adopts Q345R, and the wall thickness is about 25 mm. The pipe orifice flange is made of Cr-Mo steel forgings, and the material of the contact surface of the pipe orifice and the material can be finished by adopting the lining S310S material, so that the equipment investment cost is reduced to the maximum extent.
In the reactor of the present invention, preferably, at least one surface temperature measuring port is disposed on an inner wall of the combined inlet, pipe orifice supporting portions are disposed at joints of the combined inlet, the combined outlet, and the hydrocarbon outlet with the cylinder, respectively, and pipe orifice external reinforcing rings are disposed on the combined inlet, the combined outlet, and the hydrocarbon outlet, respectively.
In the reactor of the present invention, it is preferable that the combined inlet, the combined outlet, and the hydrocarbon outlet have lining connecting pipes on inner sides thereof, gaps are respectively formed between the lining connecting pipes and the combined inlet, between the lining connecting pipes and the combined outlet, and between the lining connecting pipes and the hydrocarbon outlet, and the gaps are completely filled with a heat insulating refractory material to form a heat insulating refractory layer.
In the reactor of the present invention, preferably, the width of the gap is 80mm to 120mm, and the lining pipe is made of heat-resistant stainless steel.
In the reactor of the present invention, it is preferable that the process channel is disposed directly below the combined inlet, and a steam inlet distributor is disposed above the process channel.
In the reactor of the invention, preferably, the reaction bed layer is built by heat-insulating refractory bricks; the end socket is a butterfly end socket, and the manufacturing cost of the end socket is lower than that of an elliptical end socket.
In the reactor of the present invention, it is preferable that the cylinder is provided with at least one thermocouple port for monitoring the temperature of the reaction bed, the upper part in the cylinder and the lower part in the cylinder; the barrel is provided with at least one pressure measuring port for monitoring the operating pressure inside the reactor.
Compared with the prior art, the invention has the following advantages:
1. the reactor provided by the invention has the advantages of large volume, high reaction efficiency, high reaction conversion rate and stable and reliable performance, the volume of a single reactor is more than 900 cubic meters, the propylene yield of the single reactor is more than 10 ten thousand tons/year, and the propane dehydrogenation reaction rate is more than or equal to 90 percent. In continuous scale production, 3-8 reactors are generally required to be matched for production. For example, 3 reactors are used for the project of preparing propylene by propane dehydrogenation of 30 ten thousand tons/year, and 8 reactors are used for the project of preparing propylene by propane dehydrogenation of 90 ten thousand tons/year.
2. The inner wall of the reactor barrel is provided with the heat-insulating layer, and the pipe orifice adopts a lining heat-insulating structure, so that the heat loss of the reactor can be controlled to the maximum extent, and the dehydrogenation reaction is ensured to be at the environmental temperature required by the process.
3. The inner wall of the reactor cylinder body is provided with the arch bridge type reaction bed layer, and the catalyst can be freely spread and dispersed from the top of the arch bridge during loading and unloading, so that the workload of manual spreading is reduced compared with the traditional plane bed layer.
4. The invention designs a plurality of groups of external reinforcing rings, which can ensure the strength and rigidity of equipment under the operating pressure and reduce the equipment investment cost on the premise of not increasing the wall thickness of the cylinder body.
5. The invention adopts the combined inlet and the combined outlet, the three outlets and the two outlets are respectively converged into the pipe orifice assembly to be welded with the cylinder body, the whole pipe orifice assembly is favorably processed in a factory workshop, the processing quality can be ensured, meanwhile, a section of connecting pipe is reserved to be welded with the cylinder body, only 1 butt-joint circular seam for field welding is reserved, and the field workload can be reduced.
6. The hydrocarbon outlet and the air outlet are respectively provided with 1 sampling port, so that the purity and the reaction rate of propylene can be sampled, detected and analyzed.
Drawings
FIG. 1 is an axial cross-sectional view of a propane dehydrogenation to propylene reactor of the present invention;
FIG. 2 is a radial cross-sectional view of a reactor for producing propylene by dehydrogenation of propane according to the present invention.
Wherein:
1. steam and reducing gas inlets; 2. an air inlet; 3. a hydrocarbon inlet; 4. an outer reinforcement ring I; 5. a catalyst loading and unloading port; 6. an outer reinforcement ring II; 7. a thermally insulating refractory layer; 8. a steam inlet distributor; 9. a barrel; 10. a thermocouple interface; 11. a manhole; 12. a butterfly-shaped end socket; 13. an oil-gas blocking ring; 14. an air extraction opening; 15. an air outlet; 16. a hydrocarbon outlet; 17. a sampling port; 18. a hydrocarbon outlet baffle; 19. a pressure measuring port; 20. a pipe orifice supporting part; 21. a temperature measuring port; 22. a pipe orifice outer reinforcing ring; 23. a lining adapter; 24. a heat-insulating layer; 25. a reaction bed layer; 26. a process channel.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. The present invention may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.
As shown in FIGS. 1 and 2, the present invention provides a large fixed bed reactor for producing propylene by propane dehydrogenation, which is a horizontal reactor and comprises a cylindrical body 9, in an axial sectional view and a radial sectional view. The left end and the right end of the cylinder 9 are respectively provided with a butterfly-shaped end enclosure 12, the straight edges of the butterfly-shaped end enclosures 12 are respectively provided with an external reinforcing ring I4, and the outside of the cylinder 9 is provided with 4 external reinforcing rings II 6. The outer reinforcing ring I4 and the outer reinforcing ring II 6 have two functions: the first step, the strength and rigidity of the cylinder and the end socket are enhanced, and the end socket can not be deformed in a destabilization manner under a negative pressure state; secondly, the device is used for controlling the roundness of the cylinder body, and the cylinder body is easy to generate elliptical deformation because of belonging to a cylinder body with a large diameter and a thin wall.
The middle position of the top of the cylinder 9 is provided with a crotch-shaped combined inlet consisting of a steam and reducing gas inlet 1, an air inlet 2 and a hydrocarbon inlet 3. A hydrocarbon outlet 16 is arranged on one side of the bottom of the cylinder 9, and a sampling port 17 is arranged on a connecting pipe of the hydrocarbon outlet 16. The other side of the bottom of the cylinder 9 is provided with an h-shaped combined outlet consisting of an air outlet 15 and an air suction port 14, and a sampling port 17 is arranged on a connecting pipe of the air outlet 15.
The left and right symmetrical positions of the top of the cylinder body 9 are respectively provided with a catalyst loading and unloading port 5, the outer side of each catalyst loading and unloading port 5 is provided with a manhole 11, and two sides of the bottom of the cylinder body 9 are respectively provided with a manhole 11, so that personnel can conveniently enter a dispersed catalyst or a maintenance device. A steam inlet distributor 8 is arranged below the fork-shaped combined inlet in the barrel 9.
The inner wall of the barrel 9 is provided with a heat preservation layer 24 built by refractory bricks, the inside of the barrel 9 is provided with an arch bridge type reaction bed layer 25 built by refractory bricks, the inside of the barrel 9 is divided into an upper reaction zone and a lower reaction zone by the reaction bed layer 25, the top cambered surface of the reaction bed layer 25 is used for stacking catalysts, a cylindrical process channel 26 built by refractory bricks is arranged right below a crotch type combined inlet on the reaction bed layer 25, and the upper reaction zone is communicated with the lower reaction zone by the process channel 26. The outer diameter of the cylindrical process channel 26 is close to the diameter of the pipe orifice of the crotch-shaped combined inlet, the outer wall of the cylindrical process channel is provided with a plurality of holes, and the upper part of the cylindrical process channel is used for placing the steam inlet distributor 8. The oil gas blocking ring 13 is arranged between the inner wall of the cylinder 9 and the heat insulation layer 24, distributed between each layer of refractory bricks of the heat insulation layer 24 and welded with the cylinder 9, and has the function of preventing reactants from flowing away along the inner wall of the cylinder through gaps of the refractory bricks, so that the reactants cannot be in full contact with a catalyst on a bed layer, and further insufficient reaction is caused.
The top of the cylinder 9 is provided with a plurality of thermocouple interfaces 10 which are distributed at various positions and are respectively used for monitoring the bed temperature, the temperature of the upper part in the cylinder 9 and the temperature of the lower part in the cylinder 9.
The cylinder 9 is provided with a plurality of pressure measuring ports 19 which are distributed at different height positions of the cylinder 9.
The inner side of the crotch-shaped combined inlet is provided with a lining connecting pipe 23, a gap of 80-120 mm is formed between the lining connecting pipe 23 and the crotch-shaped combined inlet, the gap is completely filled with heat-insulating and refractory materials to form a heat-insulating refractory layer 7, and the lining connecting pipe 23 is made of heat-resistant stainless steel. The inner wall and the outer wall of the crotch-shaped combined inlet are provided with a plurality of temperature measuring ports 21, the joint of the crotch-shaped combined inlet and the barrel body 9 is provided with a pipe orifice supporting part 20, and the crotch-shaped combined inlet is also provided with a pipe orifice external reinforcing ring 22.
The pipe orifice of the hydrocarbon outlet 16 faces downwards, the pipe orifice supporting part 20 is also arranged at the joint of the hydrocarbon outlet 16 and the cylinder 9, the hydrocarbon outlet 16 is provided with an external reinforcing ring 22, the inner side of the hydrocarbon outlet 16 is provided with an inner lining connecting pipe 23, a gap of 80mm-120mm exists between the inner lining connecting pipe 23 and the inner wall of the hydrocarbon outlet 16, the gap is completely filled with heat-insulating refractory materials to form a heat-insulating refractory layer, and the material of the inner lining connecting pipe 23 is heat-resistant stainless steel. A hydrocarbon outlet baffle plate 18 is arranged in the cylinder 9 opposite to the hydrocarbon outlet 16.
The H-shaped combined outlet formed by the air outlet 15 and the air suction opening 14 has a downward pipe orifice, a pipe orifice supporting part is arranged at the joint of the H-shaped combined outlet and the cylinder body 9, an external reinforcing ring is arranged on the combined outlet, a lining connecting pipe is also arranged on the inner side of the combined outlet, a gap of 80mm-120mm exists between the lining connecting pipe and the inner wall of the combined outlet, the gap is completely filled with heat-insulating refractory materials to form a heat-insulating refractory layer 7, and the lining connecting pipe 23 is made of heat-resistant stainless steel.
When the reactor works, a catalyst is added through the catalyst loading and unloading port 5, the catalyst falls on the reaction bed layer 25, high-temperature air (about 650 ℃) enters from the air inlet 2 and flows out from the air outlet 15, the heat exchange is carried out inside the reactor to ensure that the temperature of the reactor reaches the working temperature environment (590 ℃ -650 ℃) of dehydrogenation reaction, then the air outlet 15 and the air inlet 2 are closed, the air is pumped through the air pumping port 14 to ensure that the inside of the reactor reaches the vacuum state, then the high-temperature gasified propane (540 ℃ -590 ℃) is injected through the hydrocarbon inlet 3, and the dehydrogenation reaction is completed on the bed layer inside the reactor under the action of the catalyst and the high-temperature environment (590 ℃ -650 ℃):
Figure BDA0003047073700000061
after the reaction is finished, the hydrocarbon outlet 16 is opened, the products of propylene and hydrogen are produced from the hydrocarbon outlet 16, and the reactor is vacuumized again by suction so that the reacted gas completely enters the next process. The steam and reducing gas inlet 1 is used for introducing steam and reducing gas to restore the activity of the catalyst after the reaction is completed.
The invention generally needs a plurality of identical reactors to be matched for recycling. The continuous scale production generally needs 3-8 reactors for production, and the propylene yield of a single reactor is more than 10 ten thousand tons per year. For example, 3 reactors can be used for the project of preparing propylene by dehydrogenating propane for 30 ten thousand tons/year, and 8 reactors can be used for the project of preparing propylene by dehydrogenating propane for 90 ten thousand tons/year.
It should be noted that the above preferred embodiments are only for illustrating the present invention, but the present invention is not limited to the above embodiments, and variations and modifications within the spirit of the present invention, which are made by those skilled in the art, are included in the protection scope of the present invention.

Claims (10)

1. The utility model provides a large-scale propane dehydrogenation system propylene reactor, this reactor is horizontal reactor, includes the barrel, its characterized in that, be equipped with the heat preservation on the inner wall of barrel, be equipped with the reaction bed layer of arch bridge type in the barrel will barrel inside is cut apart into upper portion reaction zone and lower part reaction zone, it will to be equipped with the process channel on the reaction bed layer upper portion reaction zone with lower part reaction zone intercommunication, the both ends of barrel respectively are equipped with a head, the straight flange department of head is equipped with outside reinforcing ring I, be equipped with two at least outside reinforcing rings II on the outer wall of barrel.
2. The reactor of claim 1, wherein the heat insulating layer is made of heat insulating refractory bricks, and an oil and gas blocking ring is arranged between the heat insulating layer and the inner wall of the cylinder body.
3. The reactor according to claim 1, characterized in that the top of the shell is provided with a crotch-type combined inlet comprising a steam and reducing gas inlet, an air inlet and a hydrocarbon inlet; catalyst loading and unloading ports are arranged on two sides of the combined inlet at the top of the cylinder body; an h-shaped combined outlet is formed in one side of the bottom of the cylinder body and comprises an air outlet and an air suction opening, and a sampling opening is formed in the pipe wall of the air outlet; a hydrocarbon outlet is formed in the other side of the bottom of the cylinder body, and a sampling port is formed in the pipe wall of the hydrocarbon outlet; the top and the bottom of the cylinder body are respectively provided with at least one manhole.
4. The reactor of claim 1 wherein the diameter of the barrel is greater than 7 meters and the barrel has a left and right head overall profile length greater than 19 meters, the distance between the flange seal surface of the combined inlet and the barrel centerline is greater than 10 meters, the distance between the combined outlet bottom and the barrel centerline is greater than 6 meters, and the reactor volume is greater than 900 cubic meters.
5. The reactor of claim 1, wherein the inner wall of the combined inlet is provided with at least one surface temperature measuring port, the joints of the combined inlet, the combined outlet and the hydrocarbon outlet with the cylinder are respectively provided with a pipe orifice supporting part, and the combined inlet, the combined outlet and the hydrocarbon outlet are respectively provided with a pipe orifice external reinforcing ring.
6. The reactor of claim 1, wherein the combined inlet, the combined outlet and the hydrocarbon outlet are provided with lining connecting pipes on the inner sides, gaps are respectively formed among the lining connecting pipes, the combined inlet, the combined outlet and the hydrocarbon outlet, and the gaps are completely filled with heat-insulating refractory materials to form heat-insulating refractory layers.
7. The reactor of claim 6, wherein the width of the gap is 80mm-120mm, and the inner lining pipe is made of heat-resistant stainless steel.
8. The reactor of claim 1 wherein the process channel is disposed below the combined inlet and a steam inlet distributor is disposed above the process channel.
9. The reactor of claim 1 wherein the reaction bed is built of insulating refractory bricks; the seal head is a butterfly seal head.
10. The reactor of claim 1 wherein said barrel is provided with at least one thermocouple junction for monitoring the temperature of said reaction bed, the upper portion of said barrel interior and the lower portion of said barrel interior; the barrel is provided with at least one pressure measuring port for monitoring the operating pressure inside the reactor.
CN202110474939.1A 2021-04-29 2021-04-29 Large-scale propane dehydrogenation propylene preparation reactor Pending CN113083162A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN117582897A (en) * 2024-01-18 2024-02-23 山东神驰石化有限公司 Large-scale propane dehydrogenation system propylene reactor

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN117582897A (en) * 2024-01-18 2024-02-23 山东神驰石化有限公司 Large-scale propane dehydrogenation system propylene reactor
CN117582897B (en) * 2024-01-18 2024-04-16 山东神驰石化有限公司 Large-scale propane dehydrogenation system propylene reactor

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