CN111992146B - Axial and radial dehydrogenation reactor for vinyl toluene - Google Patents
Axial and radial dehydrogenation reactor for vinyl toluene Download PDFInfo
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- CN111992146B CN111992146B CN202010876711.0A CN202010876711A CN111992146B CN 111992146 B CN111992146 B CN 111992146B CN 202010876711 A CN202010876711 A CN 202010876711A CN 111992146 B CN111992146 B CN 111992146B
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- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 40
- HJWLCRVIBGQPNF-UHFFFAOYSA-N prop-2-enylbenzene Chemical compound C=CCC1=CC=CC=C1 HJWLCRVIBGQPNF-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 239000003054 catalyst Substances 0.000 claims abstract description 54
- 239000000463 material Substances 0.000 claims abstract description 46
- 239000002994 raw material Substances 0.000 claims abstract description 20
- 238000003860 storage Methods 0.000 claims abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims description 14
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims description 10
- 230000008676 import Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 5
- 238000000034 method Methods 0.000 description 3
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 229920000180 alkyd Polymers 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 229920006337 unsaturated polyester resin Polymers 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- 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
- B01J8/0257—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 in a cylindrical annular shaped bed
-
- 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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to a vinyltoluene axial-radial dehydrogenation reactor in the field of chemical equipment, wherein the upper end and the lower end of a reactor shell are provided with end sockets, the top of the upper end socket is provided with a raw material inlet, the bottom of the lower end socket is provided with a material outlet, a heat exchanger is arranged in the reactor shell, and the heat exchanger is provided with a plurality of heat exchange channels which can allow raw materials to downwards pass through the heat exchanger; a cylinder body comprising an inner cylinder and an outer cylinder is arranged below the heat exchanger, the tops and the bottoms of the inner cylinder and the outer cylinder are respectively connected through a top plate and a bottom plate, a gap is reserved between the outer cylinder and the inner wall of the reactor shell, and the bottom plate extends in the radial direction and closes the gap; the inner cavity of the inner cylinder vertically penetrates through the top plate and the bottom plate, the inner cylinder and the outer cylinder surround to form a catalyst storage cavity, a plurality of through holes are formed in the part of the bottom plate corresponding to the inner side of the outer cylinder, the upper part of the outer cylinder, the inner cylinder and the top plate, and the lower part of the outer cylinder is a non-porous closed cylinder. It can meet the requirements of raising catalyst activity and product yield, reducing energy consumption and further enlarging production capacity.
Description
Technical Field
The invention relates to a dehydrogenation reactor, in particular to a dehydrogenation reactor for vinyl toluene, and belongs to the technical field of chemical equipment.
Background
Vinyltoluene (VT) is an important chemical intermediate, and is generally produced by catalytic dehydrogenation of methylethylbenzene (ET). Vinyltoluene is a mixture of meta-and para-isomers, has the advantages of low toxicity, low volatility, good stability, high flash point, low odor and the like compared with Styrene (SM), can replace Styrene Monomer (SM) monomers, is mainly used for producing high-grade unsaturated polyester resin, modified alkyd resin, vinyl resin and the like, and the resin produced by the vinyltoluene is widely applied to the industries of impregnation type insulating paint, coating and composite materials.
At present, vinyltoluene produced by methyl ethyl benzene reported at home and abroad is mainly synthesized by a catalytic dehydrogenation method. In the presence of a Fe-K-Ce system catalyst, the catalytic reaction temperature is up to 580-640 ℃, methyl ethyl benzene is used as a raw material, and vinyl toluene is prepared by a feed vaporizer, a heat exchanger, a dehydrogenation reactor, a waste heat boiler, a dehydrogenation liquid cooler and an oil-water separator. The dehydrogenation reaction plays a key role in the process, so the requirements on the material, the structure and the working principle of the dehydrogenation reactor are higher.
The key technology of the vinyl toluene production device is to prepare vinyl toluene by dehydrogenating methyl ethylbenzene and ethyl benzene, wherein the core equipment is a first dehydrogenation reactor and a second dehydrogenation reactor in the vinyl toluene device, and a double-steam two-section adiabatic reactor is adopted. The traditional process has the problems of higher energy consumption, low once-through yield of dehydrogenation reaction, difficult capacity expansion of dehydrogenation reaction due to the limitation of the volume of a reactor, easy coking of a catalyst, shortened service life and the like. The design of the methyl ethyl benzene dehydrogenation reactor can not meet the requirement of expanded production, and simultaneously has the problems of reducing energy consumption and improving catalyst activity.
The existing methyl ethyl benzene dehydrogenation reactor is an axial adiabatic reactor, reaction gas passes through a catalyst bed layer of the reactor from top to bottom, high-temperature methyl ethyl benzene and accompanying high-temperature steam pass through a pipeline and a mixer and then enter the dehydrogenation reactor, the dehydrogenation reactor is internally provided with a dehydrogenation catalyst bed layer with a certain thickness, the reaction is a large amount of endothermic reaction, after the reaction gas enters the catalyst bed layer, the temperature of the catalyst bed layer is rapidly reduced, the activity of the catalyst is greatly influenced by the reaction temperature, and when the temperature of the catalyst bed layer is reduced to a certain degree, the reaction activity is poor, so that the height of the catalyst bed layer is fixed and cannot be increased, namely, the increase of the height of the bed layer does not help the yield of one-way reaction.
Disclosure of Invention
The invention aims to provide a vinyltoluene axial-radial dehydrogenation reactor, which meets the requirements of improving the activity of a catalyst and the yield of a product, reducing the energy consumption and further expanding the productivity.
The purpose of the invention is realized as follows: a vinyltoluene axial-radial dehydrogenation reactor comprises a reactor shell, wherein an upper end socket is arranged at the upper end of the reactor shell, a lower end socket is arranged at the lower end of the reactor shell, a raw material inlet is formed in the top of the upper end socket, a material outlet is formed in the bottom of the lower end socket, a heat exchanger is arranged below the raw material inlet in the reactor shell, and a medium inlet and a medium outlet of the heat exchanger are respectively connected to the outside of the reactor shell; a plurality of heat exchange channels for allowing the raw materials to downwards pass through the heat exchanger are arranged on the heat exchanger; a cylinder is vertically arranged below the heat exchanger and comprises an inner cylinder and an outer cylinder, the tops and the bottoms of the inner cylinder and the outer cylinder are respectively connected through a top plate and a bottom plate, a gap is reserved between the outer cylinder and the inner wall of the reactor shell, and the bottom plate extends in the radial direction and seals the gap; the inner cavity of the inner cylinder vertically penetrates through the top plate and the bottom plate, the inner cylinder and the outer cylinder surround to form a catalyst storage cavity, a plurality of through holes are formed in the part, the upper part of the outer cylinder, the inner cylinder and the top plate, corresponding to the inner side of the outer cylinder, on the bottom plate, and the lower part of the outer cylinder is a sealed cylinder without holes.
When the device works, catalyst particles are filled in the catalyst storage cavity, methyl ethyl benzene and high-temperature steam materials enter the reactor shell from the raw material inlet, after heat exchange by the heat exchanger, high-temperature steam material flow is divided into three parts, the first part of material flow enters along a gap between the reactor shell and the outer cylinder, then radially enters between the inner cylinder and the outer cylinder, contacts with the catalyst and carries out dehydrogenation reaction, and the material flow passing through the inner cylinder and the inner cylinder is converged; the second part of material flow axially enters between the inner cylinder and the outer cylinder from the top plate, and enters the inner cylinder after reaction; the third part of material flow directly enters the inner cylinder and moves downwards along the axial direction; in the three parts of material flows, the radial flow material flow and the axial flow material flow are converged and exchanged, so that the material flow direction shows the movement trend of the two aspects of the axial material flow and the radial material flow, and the material flow has more contact opportunities with the catalyst, thereby obtaining more reaction opportunities and improving the yield. Because the lower part of the outer cylinder is a closed cylinder without holes, the material flow passing through the area of the catalyst axially is relatively less along with the downward movement of the material flow, and the heat of the part of the catalyst is not easy to be taken away quickly, thereby ensuring that the catalyst still has high activity at the local part, and further ensuring that the dehydrogenation reaction still can be carried out stably. The third part of material flow directly enters the inner cylinder and moves downwards along the axial direction, the material flow does not actually participate in the reaction directly, the material flow has higher heat and is equivalent to a heat source, so that the temperature of the surrounding catalyst is not excessively reduced due to dehydrogenation heat absorption, and the high activity of the catalyst is ensured. Compared with the prior art, the invention has the beneficial effects that: the device can ensure high activity of the catalyst, improve the product yield and reduce energy consumption, thereby further enlarging the productivity. The device is specially used for vinyl toluene dehydrogenation.
The invention is further improved in that the inner cylinder and the outer cylinder are concentrically arranged cylinders. The inner cylinder and the outer cylinder are arranged concentrically, and the thickness of the catalyst is consistent, so that the material flow passes through the catalyst layer to obtain relatively equal reaction opportunities.
Furthermore, the outer cylinder is connected with the inner wall of the reactor shell through a telescopic support piece. The reactor shell can ensure that the radial relative position of the outer barrel and the inner wall of the reactor shell is stable, and the reactor shell can move adaptively after being heated, so that the temperature difference stress generated by the thermal expansion difference is eliminated, and the pulling-out of the supporting piece and the damage to the outer barrel are avoided.
As a further development of the invention, a jet flow controller is provided on the underside of the raw material inlet and above the heat exchanger. The injection flow controller enables the raw materials to enter the kettle in an injected mode, so that the material flow distribution is more uniform, and the effective reaction area is enlarged.
Furthermore, the heat exchange channels are a plurality of circular hole channels distributed in an array. The structure ensures that the pressure drop of material flow is small, the heat exchange of the material is uniform, and the generated vibration is small.
The catalyst storage cavity is characterized in that a catalyst unloading port is further formed in the lower end enclosure, and the catalyst unloading port is connected to the bottom of the catalyst storage cavity. The catalyst can be unloaded through the catalyst unloading port, so that the management is convenient.
In addition, the connection form of the perforated connecting pipe on the vinyl toluene dehydrogenation reactor can adopt a flexible structure, and a rigid structure is avoided, so that the stress concentration at a welding seam can be reduced.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a view from a-a in fig. 1.
Fig. 3 is a working principle diagram of the present invention.
In the figure, 1 raw material inlet, 2 medium inlet, 3 medium outlet, 4 jet flow controller, 5 upper end enclosure, 6 heat exchanger, 7 reactor shell, 8 top plate, 9 inner cylinder, 10 outer cylinder, 11 telescopic supporting piece, 12 catalyst storage cavity, 13 catalyst unloading port, 14 lower end enclosure, 15 material outlet, 16 bottom plate and 17 heat exchange channel.
Detailed Description
As shown in fig. 1-3, an axial-radial vinyltoluene dehydrogenation reactor is provided, in which an upper end enclosure 5 is disposed at an upper end of a reactor shell 7, a lower end enclosure 14 is disposed at a lower end of the reactor shell, a raw material inlet 1 is disposed at a top of the upper end enclosure 5, a material outlet 15 is disposed at a bottom of the lower end enclosure 14, a heat exchanger 6 is disposed below the raw material inlet 1 in the reactor shell 7, and a medium inlet 2 and a medium outlet 3 of the heat exchanger 6 are respectively connected to an outside of the reactor shell 7; the heat exchanger 6 is provided with a plurality of heat exchange channels 17 which can accommodate raw materials to downwards pass through the heat exchanger, and the heat exchange channels 17 are a plurality of circular hole channels distributed in an array; a jet flow controller 4 is arranged on the lower side of the raw material inlet 1 and above the heat exchanger 6; a cylinder is vertically arranged below the heat exchanger 6, the cylinder comprises an inner cylinder 9 and an outer cylinder 10, the inner cylinder 9 and the outer cylinder 10 are concentrically arranged cylinders, the tops and the bottoms of the inner cylinder 9 and the outer cylinder 10 are respectively connected through a top plate 8 and a bottom plate 16, a gap is reserved between the outer cylinder 10 and the inner wall of the reactor shell 7, and the bottom plate 16 radially extends and seals the gap, so that material flow can be blocked and only can bypass; the inner cavity of the inner cylinder 9 penetrates through the top plate 8 and the bottom plate 16 up and down, the inner cylinder 9 and the outer cylinder 10 enclose a catalyst storage cavity 12, a plurality of through holes are arranged on the part of the bottom plate 16 corresponding to the inner side of the outer cylinder 10, the upper part of the outer cylinder 10, the inner cylinder 9 and the top plate 8, the lower part of the outer cylinder 10 is a non-porous closed cylinder, and as shown in the figure 1, the dotted lines on the bottom plate 16, the outer cylinder 10, the inner cylinder 9 and the top plate 8 show the parts with the through holes.
The outer cylinder 10 is connected with the inner wall of the reactor shell 7 through a telescopic support 11. The lower end enclosure 14 is also provided with a catalyst unloading port 13, and the catalyst unloading port 13 is connected to the bottom of the catalyst storage cavity 12.
In addition, the perforated connecting pipe on the vinyl toluene dehydrogenation reactor adopts a flexible structure, and a rigid structure is avoided, so that the stress concentration at a welding seam can be reduced.
When the reactor works, catalyst particles are filled in the catalyst storage cavity 12, a catalyst layer is integrally formed, methyl ethyl benzene and high-temperature steam materials enter the reactor shell 7 from the raw material inlet 1, after heat exchange through the heat exchanger 6, a high-temperature steam material flow is divided into three parts, the first part of the material flow enters along a gap between the reactor shell 7 and the outer cylinder 10, then radially enters between the inner cylinder 9 and the outer cylinder 10, contacts with a catalyst and carries out dehydrogenation reaction, and the material flow passing through the inner cylinder 9 and the inner cylinder 9 is collected; the second part of material flow axially enters between the inner cylinder 9 and the outer cylinder 10 from the top plate 8, and enters into the inner cylinder 9 after dehydrogenation reaction; the third part of material flow directly enters the inner cylinder 9 and moves downwards along the axial direction; in the three-part flow, the radial flow and the axial flow are converged and exchanged, so that the flow direction shows the movement tendency of the two aspects of the axial flow and the radial flow, the contact chance of the flow and the catalyst is more, and therefore, more reaction opportunities can be obtained, and the yield is improved. Because the lower part of the outer cylinder 10 is a closed cylinder without holes, the material flow passing through the area of the catalyst axially is relatively less along with the downward movement of the material flow, and the heat of the part of the catalyst is not easy to be taken away quickly, thereby ensuring that the catalyst still has high activity at the local part, and further ensuring that the dehydrogenation reaction still can be carried out more stably. The third part of material flow directly enters the inner cylinder 9 and moves downwards along the axial direction, the part of material flow does not actually participate in the reaction directly, the material flow has higher heat and is equivalent to a heat source, so that the temperature of the surrounding catalyst is not excessively reduced due to dehydrogenation heat absorption, and the high activity of the catalyst is ensured. The device can ensure high activity of the catalyst, improve the product yield and reduce energy consumption, thereby further enlarging the productivity.
The present invention is not limited to the above-mentioned embodiments, and based on the technical solutions disclosed in the present invention, those skilled in the art can make some substitutions and modifications to some technical features without creative efforts according to the disclosed technical contents, and these substitutions and modifications are all within the protection scope of the present invention.
Claims (6)
1. The utility model provides a vinyltoluene axial radial dehydrogenation reactor, includes the reactor casing, and reactor casing upper end is equipped with the upper cover, and the lower extreme is equipped with the low head, and the upper cover top is equipped with the raw materials import, and the low head bottom is equipped with material export, its characterized in that: a heat exchanger is arranged below the raw material inlet in the reactor shell, and a medium inlet and a medium outlet of the heat exchanger are respectively connected to the outside of the reactor shell; a plurality of heat exchange channels for allowing the raw materials to downwards pass through the heat exchanger are arranged on the heat exchanger; a cylinder is vertically arranged below the heat exchanger and comprises an inner cylinder and an outer cylinder, the tops and the bottoms of the inner cylinder and the outer cylinder are respectively connected through a top plate and a bottom plate, a gap is reserved between the outer cylinder and the inner wall of the reactor shell, and the bottom plate extends in the radial direction and seals the gap; the inner cavity of the inner cylinder vertically penetrates through the top plate and the bottom plate, the inner cylinder and the outer cylinder surround to form a catalyst storage cavity, a plurality of through holes are formed in the part of the bottom plate corresponding to the inner side of the outer cylinder, the upper part of the outer cylinder, the inner cylinder and the top plate, and the lower part of the outer cylinder is a sealed cylinder without holes; during reaction, methyl ethyl benzene and high-temperature steam materials enter a reactor shell from a raw material inlet, after heat exchange by a heat exchanger, a high-temperature steam material flow is divided into three parts, the first part of the material flow enters along a gap between the reactor shell and an outer cylinder, then radially enters between an inner cylinder and an outer cylinder, contacts with a catalyst, performs dehydrogenation reaction, and then passes through the inner cylinder and is converged with the material flow in the inner cylinder; the second part of material flow axially enters between the inner cylinder and the outer cylinder from the top plate, and enters the inner cylinder after reaction; the third part of material flow directly enters the inner cylinder and moves downwards along the axial direction.
2. The vinyltoluene axial-radial dehydrogenation reactor according to claim 1, wherein: the inner cylinder and the outer cylinder are cylinders which are concentrically arranged.
3. The vinyltoluene axial-radial dehydrogenation reactor according to claim 1, wherein: the outer cylinder is connected with the inner wall of the reactor shell through a telescopic supporting piece.
4. A vinyltoluene axial-radial dehydrogenation reactor according to any one of claims 1-3, characterized in that: and a jet flow controller is arranged on the lower side of the raw material inlet and above the heat exchanger.
5. A vinyltoluene axial-radial dehydrogenation reactor according to any one of claims 1-3, characterized in that: the heat exchange channels are a plurality of circular hole channels distributed in an array.
6. A vinyltoluene axial-radial dehydrogenation reactor according to any one of claims 1-3, characterized in that: and the lower end enclosure is also provided with a catalyst unloading port, and the catalyst unloading port is connected to the bottom of the catalyst storage cavity.
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| CN202010876711.0A CN111992146B (en) | 2020-08-27 | 2020-08-27 | Axial and radial dehydrogenation reactor for vinyl toluene |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010876711.0A CN111992146B (en) | 2020-08-27 | 2020-08-27 | Axial and radial dehydrogenation reactor for vinyl toluene |
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| CN111992146B true CN111992146B (en) | 2022-08-09 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103721643A (en) * | 2014-01-10 | 2014-04-16 | 华东理工大学 | Z-type butane oxydehydrogenation static bed radial reactor |
| CN104248940A (en) * | 2014-09-24 | 2014-12-31 | 浙江大学 | Multistage radial stationary bed reaction system and method for producing propylene from oxy-compound as raw material |
| CN104645897A (en) * | 2015-02-11 | 2015-05-27 | 南京敦先化工科技有限公司 | Dual-seal-head controllable water heat removing reactor |
| DE102017208319A1 (en) * | 2017-05-17 | 2018-11-22 | Thyssenkrupp Ag | Radialstromeinsatzvorrichtung for predetermining at least one radial flow path in a bed reactor and assembly method and use |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102005020943A1 (en) * | 2005-05-04 | 2006-11-09 | Linde Ag | Process and reactor for carrying out endothermic catalytic reactions |
| GB201400805D0 (en) * | 2014-01-17 | 2014-03-05 | Johnson Matthey Plc | Method of loading a vessel |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103721643A (en) * | 2014-01-10 | 2014-04-16 | 华东理工大学 | Z-type butane oxydehydrogenation static bed radial reactor |
| CN104248940A (en) * | 2014-09-24 | 2014-12-31 | 浙江大学 | Multistage radial stationary bed reaction system and method for producing propylene from oxy-compound as raw material |
| CN104645897A (en) * | 2015-02-11 | 2015-05-27 | 南京敦先化工科技有限公司 | Dual-seal-head controllable water heat removing reactor |
| DE102017208319A1 (en) * | 2017-05-17 | 2018-11-22 | Thyssenkrupp Ag | Radialstromeinsatzvorrichtung for predetermining at least one radial flow path in a bed reactor and assembly method and use |
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