CN220861402U - Hydrogenation reactor for preparing methyl propionate - Google Patents
Hydrogenation reactor for preparing methyl propionate Download PDFInfo
- Publication number
- CN220861402U CN220861402U CN202322687913.2U CN202322687913U CN220861402U CN 220861402 U CN220861402 U CN 220861402U CN 202322687913 U CN202322687913 U CN 202322687913U CN 220861402 U CN220861402 U CN 220861402U
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- CN
- China
- Prior art keywords
- hydrogenation reactor
- inlet
- methyl propionate
- catalyst bed
- cylindrical inlet
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 31
- RJUFJBKOKNCXHH-UHFFFAOYSA-N Methyl propionate Chemical compound CCC(=O)OC RJUFJBKOKNCXHH-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 229940017219 methyl propionate Drugs 0.000 title claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 64
- 239000000463 material Substances 0.000 claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 8
- -1 acrylic ester Chemical class 0.000 claims abstract description 6
- 238000006243 chemical reaction Methods 0.000 abstract description 22
- 239000010410 layer Substances 0.000 description 9
- 239000002994 raw material Substances 0.000 description 9
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 6
- 239000011344 liquid material Substances 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 125000001160 methoxycarbonyl group Chemical group [H]C([H])([H])OC(*)=O 0.000 description 3
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000013072 incoming material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000012827 research and development Methods 0.000 description 2
- 239000002356 single layer Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000005465 channeling Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model discloses a hydrogenation reactor for preparing methyl propionate, which comprises a shell, a material inlet and a material outlet which are arranged at two ends of the shell, and at least two catalyst beds which are positioned in the shell, wherein a material buffer cavity is arranged between every two adjacent catalyst beds to separate, and a gas-liquid distribution plate is arranged on the upper surface of each catalyst bed in a covering manner; the material inlet comprises an inner cylindrical inlet and an outer cylindrical inlet, wherein the inner cylindrical inlet is used for connecting a hydrogen gas source, the outer cylindrical inlet is used for connecting an acrylic ester feeding pipeline, and the inner cylindrical inlet and the outer cylindrical inlet are fixedly connected through a connecting rod. The utility model has the advantage of improving the reaction efficiency.
Description
Technical Field
The utility model relates to a hydrogenation reactor for preparing methyl propionate.
Background
Methyl propionate (molecular formula: CH 3CH2COOCH3) is a key intermediate in the process of synthesizing methyl methacrylate by using methyl acetate and methanol, and the reaction process involved is as follows:
CH3OH+1/2O2→HCHO+H2O
CH3- COOCH3+HCHO →CH2=HC-COOCH3+H2O
CH2=HC-COOCH3+H2→CH3CH2COOCH3
CH3CH2-COOCH3+HCHO→CH2=C(CH3)COOCH3+H2O
The methyl propionate is obtained by hydrogenation reaction of acrylic ester and hydrogen under the action of a catalyst, and the reaction efficiency is highly dependent on contact with the catalyst because the reaction raw material contains gas, and the catalyst in the existing single reactor is a single-layer catalytic bed, so that the catalyst consumption is high, the reaction efficiency is low, and a plurality of reactors are needed to be used alternately to improve the reaction efficiency.
The improvement mode adopted at present is to find a novel catalyst (CN 2018106762420) and adopt a physical-liquid circulation method to improve the conversion efficiency (CN 2014107842481). However, the improvement method has the problems of large research and development investment and complex equipment transformation.
Disclosure of Invention
The utility model provides a hydrogenation reactor for preparing methyl propionate, which aims to solve the problems of low reaction efficiency, complex equipment transformation and large research and development investment of the existing single reactor.
The hydrogenation reactor for preparing methyl propionate comprises a shell, a material inlet and a material outlet which are arranged at two ends of the shell, and at least two catalyst beds which are positioned in the shell, wherein a material buffer cavity is arranged between every two adjacent catalyst beds to separate, and a gas-liquid distribution plate is arranged on the upper surface of each catalyst bed in a covering manner.
The material inlet comprises an inner cylindrical inlet and an outer cylindrical inlet, wherein the inner cylindrical inlet is used for connecting a hydrogen gas source, the outer cylindrical inlet is used for connecting an acrylic ester feeding pipeline, and the inner cylindrical inlet and the outer cylindrical inlet are fixedly connected through a connecting rod.
After the material inlet is connected with the hydrogen gas source and the feeding pipeline, the hydrogen raw material enters from the inner cylindrical inlet, the liquid acrylic ester enters from the outer cylindrical inlet, the liquid raw material can form a certain degree of wrapping and clamping on the gas raw material, and the gas raw material can form good fusion at the initial stage of entering the catalyst bed layer, thereby being beneficial to improving the reaction efficiency. In addition, more catalyst beds are provided than in the prior art, thereby improving the reaction efficiency. The gas-liquid distribution plate can uniformly distribute incoming materials, so that the incoming materials uniformly enter the catalyst along the surface layer of the catalyst, and the phenomenon that channeling occurs in the middle of the catalyst bed body to affect the catalytic efficiency is avoided.
The inner cylindrical inlet and the outer cylindrical inlet each comprise a cylindrical part and a flare part connected to one end of the cylindrical part, the flare part is positioned in the shell, one side with a larger opening diameter faces the inside of the hydrogenation reactor, and the cylindrical part extends out of the shell. The larger side of horn mouth opening diameter is inside towards hydrogenation reactor, can reduce the inside speed of material especially liquid material entering reactor to a certain extent, and increases the area that the material contacted the catalyst, can improve catalytic reaction efficiency.
Further, a guide rib is provided on the inner wall of the flare portion of the cylindrical inlet, and an extension line of the guide rib intersects with the central axis of the cylindrical inlet. In this way, the flow guiding function can be achieved.
Further, the catalyst bed layers are two parallel layers, and are respectively used as a first catalyst bed layer and a second catalyst bed layer from top to bottom. The catalyst bed layer is optimally provided with two layers in view of comprehensive cost and reaction efficiency.
Further, the cross-sectional area of the first catalyst bed is smaller than the cross-sectional area of the second catalyst bed. Thus, a gap is reserved between the first catalyst bed and the inner wall of the hydrogenation reactor, so that gas-liquid materials can enter the lower material buffer cavity directly through the gap and contact with the second catalyst bed with larger cross-sectional area, and the overall conversion rate is improved.
Further, the gas-liquid distribution plate comprises a porous chassis, a short column vertically arranged on the upper surface of the porous chassis and a flow guide cap arranged at the upper end of the short column, and the top end of the flow guide cap is arc-shaped. In this way, the flow guiding function can be achieved.
Further, the flow guiding cap is in threaded connection with the short column. Thus, the disassembly and the maintenance are convenient.
Further, the material outlet is provided with a material collector. In this way, the flow guiding function can be achieved, and the discharge of products is promoted.
The beneficial effects are that: the hydrogenation reactor is provided with a plurality of gas-liquid distribution plates and a catalyst bed layer, so that the hydrogenation reactor has higher reaction efficiency compared with a single-layer catalyst bed layer in the prior art, the service life of the whole catalyst is longer, the main structure of the equipment is not modified, and the modification investment of the equipment is small; by providing the coaxial inner cylindrical inlet and outer cylindrical inlet, the gas-liquid raw material can be well fused at the initial stage of entering the catalyst bed, which contributes to the improvement of the reaction efficiency.
Drawings
FIG. 1 is a schematic diagram of a hydrogenation reactor according to the present utility model;
FIG. 2 is a bottom view of the material inlet structure of the hydrogenation reactor of the present utility model;
FIG. 3 is a schematic view of the structure of the gas-liquid distributor plate of the hydrogenation reactor of the present utility model;
In the figure, 1, a shell; 2. a material inlet; 21. an inner cylindrical inlet; 22. an outer cylindrical inlet; 23. a flare part; 24. a flow guiding convex strip; 3. a material outlet; 31. a material collector; 4. a gas-liquid distribution plate; 41. a porous chassis; 42. a short column; 43. a deflector cap; 5. a first catalyst bed; 6. a second catalyst bed; 7. the material is buffered in the cavity.
Detailed Description
The utility model will now be described in further detail with reference to the accompanying drawings. The drawings are simplified schematic representations which merely illustrate the basic structure of the utility model and therefore show only the structures which are relevant to the utility model.
As shown in fig. 1-3, a hydrogenation reactor for preparing methyl propionate comprises a vertical tower-shaped shell 1, a material inlet 2 and a material outlet 3 which are arranged at two ends of the shell 1, a first catalyst bed 5 and a second catalyst bed 6 which are positioned in the shell 1 from top to bottom, wherein a material buffer cavity 7 is arranged between the two catalyst beds to separate, and a gas-liquid distribution disc 4 is arranged on the upper surface of each catalyst bed in a covering manner. The catalyst beds are installed by adopting a conventional technology.
The material inlet 2 comprises an inner cylindrical inlet 21 for connecting a hydrogen gas source and an outer cylindrical inlet 22 for connecting an acrylic ester supply pipeline, which are coaxially arranged, wherein the inner cylindrical inlet 21 and the outer cylindrical inlet 22 are nested to form an annular inner channel and an annular outer channel, and the inner cylindrical inlet 21 and the outer cylindrical inlet 22 are welded by a connecting rod made of corrosion-resistant materials. Each cylindrical inlet comprises a cylindrical part and a flare part 23 welded at one end of the cylindrical part, the flare part 23 is positioned in the shell 1, one side with a larger opening diameter faces the inside of the hydrogenation reactor, the cylindrical part extends out of the shell 1, and the outermost outer wall of the cylindrical part is welded with the shell 1. When the material inlet 2 is installed, the detachable shell 1 can be detached, then the material inlet 2 is placed in the shell 1, and the cylindrical part extends out of the upper end opening of the shell for welding. Stainless steel guide ribs 24 are welded to the inner wall of the flare portion 23 of the cylindrical inlet, and the extension lines of the guide ribs 24 intersect with the central axis of the cylindrical inlet.
The thicknesses of the first catalyst bed 5 and the second catalyst bed 6 are the same, the cross-sectional area of the first catalyst bed 5 is smaller than the cross-sectional area of the second catalyst bed 6 (the volume of the first catalyst bed 5 is smaller than the volume of the second catalyst bed 6), namely a gap exists between the first catalyst bed 5 and the inner wall of the shell 1 (hydrogenation reactor), so that gas-liquid materials can directly enter the lower material buffer cavity 7 through the gap; the material buffer cavity 7 can contain gas-liquid materials which do not participate in the reaction, especially gas materials, and the gas-liquid materials enter the second catalyst bed 6 again uniformly under the action of the gas-liquid distribution plate 4 below to carry out the catalytic hydrogenation reaction. Specifically, in the first catalyst bed 5, the concentration of the raw materials is higher, the reaction is more intense, the reaction intensity of the part where the raw materials are located can be slowed down by the smaller volume, and then the raw materials are balanced by the second catalyst bed 6. The concentration of the materials participating in the reaction in the second catalyst bed 6 is relatively smaller, and the particles of the catalyst can be selected to be larger in size so as to facilitate the flow of the materials, and the gas-liquid materials which do not participate in the reaction can be fully received by setting the larger cross-sectional area, so that the overall conversion rate is improved.
The gas-liquid distribution plate 4 comprises a porous chassis 41, a short column 42 vertically arranged on the upper surface of the porous chassis 41 and a flow guide cap 43 arranged at the upper end of the short column 42 and bent towards the porous chassis 41, the top end of the flow guide cap 43 is arc-shaped, and the flow guide cap 43 is in threaded connection with the short column 42, so that the gas-liquid distribution plate is convenient to detach, overhaul and replace.
The material collector 31 is arranged at the material outlet 3, the material collector 31 is a conventional collector, and has a diversion function to promote the discharge of products.
The application scene of the hydrogenation reactor is as follows: the temperature of the reactor is controlled to be 80-150 ℃; the reaction pressure is controlled to be between normal pressure and 2.0MPa; the molar ratio of methyl acrylate to hydrogen is 1:2-1:10; the liquid volume space velocity is 0.5-10h -1; the catalyst is a selective hydrogenation catalyst, wherein the active component in the catalyst is Pt or Pd, and the carrier is one of SiO 2、Al2O3、TiO2; the catalyst particles used have a size of 3-8mm.
The hydrogenation reactor is used for producing methyl propionate by methyl acrylate hydrogenation, the conversion rate of methyl acrylate can reach more than 99.5 percent, and meanwhile, the service life of the catalyst can reach 3 to 5 years (the service life of the catalyst on the whole is longer because the second catalyst bed 6 shares the role of the first catalyst bed 5).
The abovementioned techniques not mentioned in particular refer to the prior art.
With the above-described preferred embodiments according to the present utility model as an illustration, the above-described descriptions can be used by persons skilled in the relevant art to make various changes and modifications without departing from the scope of the technical idea of the present utility model. The technical scope of the present utility model is not limited to the description, but must be determined according to the scope of claims.
Claims (8)
1. The hydrogenation reactor for preparing methyl propionate is characterized by comprising a shell, a material inlet and a material outlet which are arranged at two ends of the shell, and at least two catalyst beds which are positioned in the shell, wherein a material buffer cavity is arranged between every two adjacent catalyst beds to separate, and a gas-liquid distribution plate is arranged on the upper surface of each catalyst bed in a covering manner;
The material inlet comprises an inner cylindrical inlet and an outer cylindrical inlet, wherein the inner cylindrical inlet is used for connecting a hydrogen gas source, the outer cylindrical inlet is used for connecting an acrylic ester feeding pipeline, and the inner cylindrical inlet and the outer cylindrical inlet are fixedly connected through a connecting rod.
2. The hydrogenation reactor for producing methyl propionate according to claim 1, wherein the inner cylindrical introduction port and the outer cylindrical introduction port each comprise a cylindrical portion and a flare portion connected to one end of the cylindrical portion, the flare portion being located in the housing with a side having a larger opening diameter facing the inside of the hydrogenation reactor, and the cylindrical portion protruding from the housing.
3. The hydrogenation reactor for producing methyl propionate according to claim 2, wherein a diversion ridge is provided on an inner wall of a flare portion of the cylindrical introduction port.
4. A hydrogenation reactor for producing methyl propionate as claimed in claim 3 wherein the catalyst bed is two parallel layers, from top to bottom, as a first catalyst bed and a second catalyst bed respectively.
5. The hydrogenation reactor for producing methyl propionate as claimed in claim 4, wherein the cross-sectional area of the first catalyst bed is smaller than the cross-sectional area of the second catalyst bed.
6. The hydrogenation reactor for producing methyl propionate according to claim 5, wherein the gas-liquid distribution plate comprises a porous chassis, a short column vertically arranged on the upper surface of the porous chassis, and a deflector cap arranged on the upper end of the short column, and the top end of the deflector cap is arc-shaped.
7. The hydrogenation reactor for producing methyl propionate of claim 6 wherein the deflector cap is threaded with the stub.
8. The hydrogenation reactor for producing methyl propionate as claimed in claim 7, wherein the material outlet is provided with a material collector.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322687913.2U CN220861402U (en) | 2023-10-08 | 2023-10-08 | Hydrogenation reactor for preparing methyl propionate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322687913.2U CN220861402U (en) | 2023-10-08 | 2023-10-08 | Hydrogenation reactor for preparing methyl propionate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220861402U true CN220861402U (en) | 2024-04-30 |
Family
ID=90814589
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322687913.2U Active CN220861402U (en) | 2023-10-08 | 2023-10-08 | Hydrogenation reactor for preparing methyl propionate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220861402U (en) |
-
2023
- 2023-10-08 CN CN202322687913.2U patent/CN220861402U/en active Active
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| GR01 | Patent grant |