CN110918006A - Multilayer inclined plate bed reactor - Google Patents
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- CN110918006A CN110918006A CN201911153652.8A CN201911153652A CN110918006A CN 110918006 A CN110918006 A CN 110918006A CN 201911153652 A CN201911153652 A CN 201911153652A CN 110918006 A CN110918006 A CN 110918006A
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- 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
- B01J8/04—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 passing successively through two or more beds
- B01J8/0446—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 passing successively through two or more beds the flow within the beds being predominantly vertical
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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
- B01J8/04—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 passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D201/00—Preparation, separation, purification or stabilisation of unsubstituted lactams
- C07D201/02—Preparation of lactams
- C07D201/04—Preparation of lactams from or via oximes by Beckmann rearrangement
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D223/00—Heterocyclic compounds containing seven-membered rings having one nitrogen atom as the only ring hetero atom
- C07D223/02—Heterocyclic compounds containing seven-membered rings having one nitrogen atom as the only ring hetero atom not condensed with other rings
- C07D223/06—Heterocyclic compounds containing seven-membered rings having one nitrogen atom as the only ring hetero atom not condensed with other rings with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D223/08—Oxygen atoms
- C07D223/10—Oxygen atoms attached in position 2
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The invention discloses a multilayer inclined plate bed reactor for improving the conversion rate of gas-phase Beckmann rearrangement cyclohexanone oxime, which comprises a reactor main body, wherein a main flow feeding channel, a main flow discharging channel and a combined bed layer between the main flow feeding channel and the main flow discharging channel are arranged in the reactor main body; the main flow feeding channel, the main flow discharging channel, the branch flow feeding channel and the branch flow discharging channel are all open at one end, the other end is closed, one side wall surface is inclined, and the channel width is gradually reduced from the open end to the closed end; the open end of the tributary feed channel of each layer of inclined plate bed structure unit is communicated with the main stream feed channel, and the open end of the tributary discharge channel is communicated with the main stream discharge channel.
Description
Technical Field
The invention relates to the technical field of fixed bed reactor design, in particular to a multilayer inclined plate bed reactor for improving the conversion rate of gas-phase Beckmann rearrangement cyclohexanone oxime.
Background
Epsilon-caprolactam is the most important raw material for producing nylon 6, and the industrial production thereof mainly depends on the Beckmann rearrangement reaction of cyclohexanone oxime. At present, the liquid phase Beckmann rearrangement process which takes oleum as a catalyst and a reaction medium is most widely applied to industrial production, the process is simple and has higher cyclohexanone oxime conversion rate and epsilon-caprolactam selectivity, but a large amount of ammonia needs to be added for neutralization in the separation process of the sulfuric acid, so the process has the main defects of generating a large amount of ammonium sulfate waste water, easily causing environmental pollution and having very high requirements on the corrosion resistance of equipment.
In recent years, a gas phase Beckmann rearrangement process using a molecular sieve as a catalyst is adopted in industrial production, the process does not produce ammonium sulfate as a byproduct, the cyclohexanone oxime conversion rate and the epsilon-caprolactam selectivity are high, and the product is simple to separate and purify, so that the method has a very good application prospect. The conversion rate of cyclohexanone-oxime and the selectivity of epsilon-caprolactam in gas phase Beckmann rearrangement reaction in a fluidized bed reactor can reach more than 95 percent and 90 percent by adopting a B-MFI molecular sieve catalyst.
The RBS-1 full-silicon molecular sieve catalyst with an MFI structure is prepared by a process scale mark and the like (process scale mark, Wangchun, Wu Wei, a gas-phase Beckmann rearrangement reaction [ J ] of cyclohexanone oxime on an RBS-1 catalyst, petroleum refining and chemical industry 2002,33(11):1-4.), and the conversion rate of cyclohexanone oxime and the selectivity of epsilon-caprolactam in a fixed bed reactor can reach more than 99.95 percent and 96.5 percent.
Because the molecular sieve catalyst is easy to generate carbon deposition inactivation and the heat effect in the reaction process is strong, a large amount of solvent and carrier gas are required to be added for diluting the reaction. Therefore, the most reasonable process should be that a fluidized bed and a fixed bed are connected in series, firstly, the cyclohexanone oxime conversion rate of more than 95% is achieved in the fluidized bed, most of reaction heat is released, the catalyst is easy to regenerate, and then the cyclohexanone oxime conversion rate is achieved in the fixed bed to reach more than 99.95%, so that the temperature in the fixed bed is close to isothermal, and the catalyst is not easy to inactivate. Due to the large gas volume of the fluidized bed, the direct introduction into the downstream conventional fixed bed reactor results in a high pressure drop, which is one of the major problems to be solved by the process.
Japanese Sumitomo chemical industries, Inc. discloses a method and apparatus for producing epsilon-caprolactam (publication No. CN 1273971A). The invention provides equipment for producing epsilon-caprolactam, which comprises a fluidized bed reactor filled with a solid catalyst and used for enabling cyclohexanone-oxime to carry out rearrangement reaction to obtain a product containing unreacted cyclohexanone-oxime, and a fixed bed reactor filled with the solid catalyst and used for enabling unreacted cyclohexanone-oxime to carry out rearrangement reaction to obtain a product mainly containing epsilon-caprolactam. However, the invention does not provide a reasonable fixed bed reactor configuration to reduce pressure drop and improve flow uniformity.
Disclosure of Invention
Aiming at the defects in the field, the invention provides a multilayer inclined plate bed reactor for improving the conversion rate of gas-phase Beckmann rearrangement cyclohexanone oxime, which can be used as a downstream fixed bed reactor of a fluidized bed reactor and adopts a multilayer distributed feeding and discharging channel structure and a thin bed layer to reduce the pressure drop; the flow uniformity is improved by adopting the inclined channel with non-uniform width, the influence of the inclination degree of the wall surface of the channel on the flow uniformity is simulated and researched by a computer, the size of the channel and the size of a bed layer are optimally designed, and the maximum catalyst filling amount is obtained under the condition of meeting the flow uniformity, so that the conversion rate of the cyclohexanone-oxime is ensured to be more than 99.95 percent, and the treatment capacity is improved.
A multilayer inclined plate bed reactor for improving the conversion rate of gas-phase Beckmann rearrangement cyclohexanone oxime comprises a reactor main body, wherein a main flow feeding channel, a main flow discharging channel and a combined bed layer between the main flow feeding channel and the main flow discharging channel are arranged in the reactor main body, the combined bed layer consists of a plurality of layers of parallel inclined plate bed structure units with the same inclination mode, and a branch feeding channel, a branch discharging channel and a catalyst filling bed layer between the branch feeding channel and the branch discharging channel are arranged in the inclined plate bed structure units;
the main flow feeding channel, the main flow discharging channel, the branch flow feeding channel and the branch flow discharging channel are all open at one end, the other end is closed, one side wall surface is inclined, and the channel width is gradually reduced from the open end to the closed end;
the open end of a branch feeding channel of each layer of inclined plate bed structure unit is communicated with the main flow feeding channel, and the open end of a branch discharging channel is communicated with the main flow discharging channel.
The multilayer inclined plate bed reactor adopts a distributed feeding and discharging channel structure, materials enter from a main flow feeding channel and then are shunted to enter a branch flow feeding channel of each layer of inclined plate bed structure unit, the shunted materials respectively enter each catalyst filling bed layer through the permeable wall surface of each branch flow feeding channel, the flowing direction of the materials in each catalyst filling bed layer is vertical to the inclined wall surface in the corresponding inclined plate bed structure unit, the materials after catalytic reaction enter each branch flow discharging channel through the permeable wall surface of each branch flow discharging channel and finally are converged to enter the main flow discharging channel to be discharged.
Preferably, the main flow feeding channel and the main flow discharging channel are longitudinal flow channels, and the branch flow feeding channel and the branch flow discharging channel are transverse flow channels, so that the flow uniformity is improved.
The influence of the inclination degree of the channel wall surface on the flow uniformity is researched through computer simulation, and preferably, the included angle between the inclined side wall surfaces of the main flow feeding channel and the main flow discharging channel and the vertical direction is 1-5 degrees;
the inclined side wall surfaces of the branch feeding channel and the branch discharging channel form an included angle of 1-5 degrees with the horizontal direction.
Optimally designing the size of a channel, wherein the length of the dry flow feeding channel and the dry flow discharging channel is 5-6 m, and the average width is 60-90 cm;
the length of tributary feedstock channel and tributary discharging channel is 2 ~ 2.5m, and the average width is 5 ~ 15 cm.
The size of the channels is optimally designed, and preferably, the longitudinal sections of all the channels are in a trapezoidal structure.
Optimally designing the size of a bed layer, wherein the contact surfaces of the catalyst filling bed layer and the adjacent branch feeding channel and the branch discharging channel are square, and the side length is equal to the length of the adjacent branch feeding channel and the length of the adjacent branch discharging channel;
the thickness of the catalyst filling bed layer is 50-80 cm, and cylindrical catalysts with the diameter of 1-2 mm are filled.
The catalyst packed bed can be filled with RBS-1 full-silicon molecular sieve catalyst with MFI structure, and has high activity.
In a preferred example, the inclined plate bed structure unit is inclined in an outer side manner, the side wall surfaces of the branch feeding channel and the branch discharging channel, which are far away from the catalyst packed bed layer, are inclined, and the longitudinal section of the catalyst packed bed layer is rectangular;
the inclination mode of the reactor main body is inner side inclination, and the side wall surface of the dry flow feeding channel and the dry flow discharging channel, which is close to the combined bed layer, is inclined.
In another preferred example, the inclined plate bed structure unit is inclined in the inner side, the side wall surfaces of the branch feeding channel and the branch discharging channel, which are close to the catalyst packed bed layer, are inclined, and the longitudinal section of the catalyst packed bed layer is a parallelogram;
the inclination mode of the reactor main body is outer side inclination, and the side wall surfaces of the main flow feeding channel and the main flow discharging channel, which are far away from the combined bed layer, are inclined.
The invention also provides the application of the multilayer inclined plate bed reactor in the preparation of epsilon-caprolactam, wherein the multilayer inclined plate bed reactor is used as a fixed bed reactor and arranged at the downstream of a fluidized bed reactor and is used for improving the conversion rate of cyclohexanone-oxime at the outlet of the fluidized bed reactor by about 95 percent to more than 99.95 percent.
Compared with the prior art, the invention has the main advantages that:
(1) the multilayer inclined plate bed reactor is a large-scale multilayer packed bed reactor, the catalyst loading is large, and the adoption of the high-activity RBS-1 full-silicon molecular sieve catalyst can ensure that the conversion rate of cyclohexanone-oxime reaches more than 99.95 percent, obviously improve the yield of epsilon-caprolactam and reduce the separation difficulty of products;
(2) the pressure drop can be effectively reduced by adopting a multi-layer distributed feeding and discharging channel structure and a thin bed layer under the condition of large gas quantity at the outlet of the fluidized bed;
(3) the flow uniformity is improved by adopting the inclined channel with non-uniform width, and the filling amount of the catalyst can be effectively improved under the condition of meeting the flow uniformity, so that the conversion rate of cyclohexanone-oxime is ensured and the treatment capacity is improved.
Drawings
FIG. 1 is a schematic structural view of a multilayer inclined plate bed reactor composed of inclined plate bed structural units inclined at the outer sides in example 1;
FIG. 2 is a schematic structural view of an outer inclined sloping plate bed structure unit of example 1;
FIG. 3 is a schematic structural view of the main body of a multilayer inclined plate bed reactor composed of inclined plate bed structural units inclined at the inner side of the reactor in example 2;
FIG. 4 is a schematic structural view of the inner inclined sloping plate bed structure unit of example 2;
fig. 5 is a schematic structural view of a multilayer inclined plate bed reactor main body of an application example, which is composed of 6 layers of inclined plate bed structural units inclined at the outer sides, and the unit of size: cm;
fig. 6 is a schematic structural view of a sloping plate bed structural unit of an application example, and the unit of dimensions: cm;
FIG. 7 is a graph showing a flow velocity distribution in the direction perpendicular to the inclined wall surface in the 6-layer catalyst-packed bed, wherein the abscissa is a dimensionless number representing different positions in the width direction of the catalyst bed.
Detailed Description
The invention is further described with reference to the following drawings and specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The following examples are conducted under conditions not specified, usually according to conventional conditions, or according to conditions recommended by the manufacturer.
Example 1
As shown in FIG. 1, the multi-layer inclined plate bed reactor of this embodiment comprises a reactor body inclined at the inner side, and a longitudinal dry flow feeding channel 106, a dry flow discharging channel 107 and a combined bed layer positioned between the dry flow feeding channel 106 and the dry flow discharging channel 107 are arranged in the reactor body. The main flow feed channel 106 and the main flow discharge channel 107 are inclined near one side wall surface 108 of the combined bed layer. The material flow direction is shown by the arrow.
The combined bed layer is composed of a plurality of layers of parallel inclined plate bed structural units inclined at the outer sides. As shown in fig. 2, a transverse branch feed channel 101, a branch discharge channel 102, and a catalyst packed bed layer 103 located between the branch feed channel 101 and the branch discharge channel 102 are provided in the sloping plate bed structure unit. The side wall surfaces 104 of the branch feeding channel 101 and the branch discharging channel 102 far away from the catalyst packed bed 103 are inclined, and the longitudinal section of the catalyst packed bed 103 is rectangular.
The main flow feed channel 106, the main flow discharge channel 107, the branch flow feed channel 101 and the branch flow discharge channel 102 are all open at one end, the other end is closed, one side wall surface is inclined, and the channel width is gradually reduced from the open end to the closed end.
The open end of the branch feeding channel 101 of each layer of inclined plate bed structure unit is communicated with the main flow feeding channel 106, and the open end of the branch discharging channel 102 is communicated with the main flow discharging channel 107.
Example 2
As shown in FIG. 3, the multi-layer inclined plate bed reactor of this embodiment comprises a reactor body inclined at the outer side, and a longitudinal dry flow feeding channel 106, a dry flow discharging channel 107 and a combined bed layer positioned between the dry flow feeding channel 106 and the dry flow discharging channel 107 are arranged in the reactor body. The side wall surfaces 109 of the main flow feeding channel 106 and the main flow discharging channel 107 far away from the combined bed layer are inclined. The material flow direction is shown by the arrow.
The combined bed layer is composed of a plurality of layers of parallel inclined plate bed structural units with inclined inner sides. As shown in fig. 4, a transverse branch feed channel 101, a branch discharge channel 102, and a catalyst packed bed layer 103 located between the branch feed channel 101 and the branch discharge channel 102 are provided in the sloping plate bed structural unit. The side wall surfaces 105 of the branch feeding channel 101 and the branch discharging channel 102 close to the catalyst packed bed 103 are inclined, and the longitudinal section of the catalyst packed bed 103 is a parallelogram.
The main flow feed channel 106, the main flow discharge channel 107, the branch flow feed channel 101 and the branch flow discharge channel 102 are all open at one end, the other end is closed, one side wall surface is inclined, and the channel width is gradually reduced from the open end to the closed end.
The open end of the branch feeding channel 101 of each layer of inclined plate bed structure unit is communicated with the main flow feeding channel 106, and the open end of the branch discharging channel 102 is communicated with the main flow discharging channel 107.
Application example
As shown in fig. 5, the multi-layer inclined plate bed reactor of this application example is similar to example 1, and comprises a reactor main body inclined at the inner side, and a longitudinal dry flow feeding channel 201, a dry flow discharging channel 210 and a combined bed layer positioned between the dry flow feeding channel 201 and the dry flow discharging channel 210 are arranged in the reactor main body. The combined bed layer consists of 6 layers of parallel inclined plate bed structural units with inclined outer sides. The side wall surfaces of the main flow feeding channel 201 and the main flow discharging channel 210 close to the combined bed layer are inclined. The material flow direction is shown by the arrow.
As shown in fig. 6, a transverse branch feed channel 202, a branch discharge channel 209, and catalyst packed beds 203 to 208 located between the branch feed channel 202 and the branch discharge channel 209 are provided in the sloping plate bed structural unit. The side wall surfaces of the branch feeding channel 202 and the branch discharging channel 209, which are far away from the catalyst filling beds 203-208, are inclined, and the longitudinal sections of the catalyst filling beds 203-208 are rectangular.
The main flow feed channel 201, the main flow discharge channel 210, the branch flow feed channel 202 and the branch flow discharge channel 209 are all open at one end, the other end is closed, one side wall surface is inclined, and the channel width is gradually reduced from the open end to the closed end.
The open end of the branch feeding channel 202 of each layer of inclined plate bed structure unit is communicated with the main flow feeding channel 201, and the open end of the branch discharging channel 209 is communicated with the main flow discharging channel 210.
The design goal of the multilayer inclined plate bed reactor of the application example is to improve the conversion rate of the cyclohexanone-oxime at 95 percent of the outlet of the fluidized bed reactor to 99.95 percent in the process of producing 30 ten thousand tons of epsilon-caprolactam annually.
In the operation process of the multilayer inclined plate bed reactor of the application example, reaction fluid longitudinally flows into the main flow feeding channel 201, transversely flows into the distributed multilayer branch feeding channel 202, flows into the catalyst packed bed layers 203-208 along the direction vertical to the inclined wall surface, and after the reaction is finished, flows into the main flow discharging channel 210 through the distributed multilayer branch discharging channel 209 and longitudinally flows out of the reactor.
The influence of the inclined wall surface of the channel and the inclination angle in the horizontal direction on the flow uniformity is analyzed through computer simulation, and the size parameters of the channel bed layer are optimally designed.
In the application example, the multilayer inclined plate bed reactor is used as a downstream fixed bed reactor of the preposed fluidized bed, and the inlet composition is determined by the inlet composition and the conversion rate of the fluidized bed. The fluidized bed adopts methanol as a solvent for liquid phase feeding, the mass fraction of cyclohexanone oxime in the solution is 35%, the methanol is mixed with nitrogen carrier gas after vaporization, the molar ratio of nitrogen to oxime is 2:1, and the mixture enters a multilayer inclined plate bed reactor after reaching 95% of cyclohexanone oxime conversion rate.
The operation condition of the multilayer inclined plate bed reactor is that the mass space velocity of cyclohexanone-oxime is 0.15h-1Normal pressure, inlet temperature 380 ℃.
As shown in FIG. 6, the inclined wall surface of the branch feeding and discharging channel in the inclined plate bed structure unit has an inclination angle of 3.6 degrees with the horizontal direction, the average width of the channel is 8.9cm, the width of the closed end is 1.3cm, the width of the open end is 16.4cm, and the length is 237 cm. The catalyst packed bed layer is 71cm thick and is filled
The RBS-1 full-silicon molecular sieve catalyst has the bed voidage of 38 percent and the bed permeability of 1.98 multiplied by 10-9m2。
As shown in FIG. 5, the main body of the multilayer inclined plate bed reactor is composed of 6 layers of inclined plate bed structural units in parallel, and has a total height of 531cm, a total width of 381cm, an inlet and outlet width of 89cm, and a width of 237cm in a direction perpendicular to the paper surface.
The reactor performance evaluation results obtained by carrying out numerical simulation on a two-dimensional model of a main body of the multilayer inclined plate bed reactor are as follows:
1) the flow velocity distribution in the direction of the vertical inclined wall surface in the 6 layers of catalyst packed beds is shown in figure 7, the bed flow velocity increases gradually from the inlet end to the outlet end, but the relative maximum deviation is less than 10 percent, and the requirement of flow uniform distribution is met;
2) the adiabatic temperature rise of the bed layer is not more than 5 ℃, the total pressure drop is 0.11atm, the conversion rate of the cyclohexanone oxime reaches more than 99.95 percent, the total treatment capacity of the cyclohexanone oxime reaches 2175kg/h, and the production requirement of the technical process of annual production of 30 ten thousand tons of epsilon-caprolactam is met.
Furthermore, it should be understood that various changes and modifications can be made by one skilled in the art after reading the above description of the present invention, and equivalents also fall within the scope of the invention as defined by the appended claims.
Claims (9)
1. A multilayer inclined plate bed reactor for improving the conversion rate of gas-phase Beckmann rearrangement cyclohexanone oxime comprises a reactor main body, wherein a main flow feeding channel, a main flow discharging channel and a combined bed layer between the main flow feeding channel and the main flow discharging channel are arranged in the reactor main body;
the main flow feeding channel, the main flow discharging channel, the branch flow feeding channel and the branch flow discharging channel are all open at one end, the other end is closed, one side wall surface is inclined, and the channel width is gradually reduced from the open end to the closed end;
the open end of a branch feeding channel of each layer of inclined plate bed structure unit is communicated with the main flow feeding channel, and the open end of a branch discharging channel is communicated with the main flow discharging channel.
2. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase beckmann rearrangement cyclohexanone oxime according to claim 1, wherein the main stream feed channel and the main stream discharge channel are longitudinal flow channels, and the subsidiary stream feed channel and the subsidiary stream discharge channel are transverse flow channels.
3. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase Beckmann rearrangement cyclohexanone oxime according to claim 2, wherein the inclined side wall surfaces of the main flow feed channel and the main flow discharge channel form an included angle of 1-5 degrees with the vertical direction;
the inclined side wall surfaces of the branch feeding channel and the branch discharging channel form an included angle of 1-5 degrees with the horizontal direction.
4. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase Beckmann rearrangement cyclohexanone oxime according to claim 1, wherein the lengths of the dry flow feeding channel and the dry flow discharging channel are 5-6 m, and the average width is 60-90 cm;
the length of tributary feedstock channel and tributary discharging channel is 2 ~ 2.5m, and the average width is 5 ~ 15 cm.
5. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase beckmann rearrangement cyclohexanone oxime according to claim 1, wherein the longitudinal sections of all the channels are in a trapezoidal structure.
6. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase Beckmann rearrangement cyclohexanone oxime according to claim 1, wherein the contact surfaces of the catalyst packed bed layer and the adjacent branch flow feed channel and branch flow discharge channel are both square, and the side length is equal to the length of the adjacent branch flow feed channel and branch flow discharge channel;
the thickness of the catalyst filling bed layer is 50-80 cm, and cylindrical catalysts with the diameter of 1-2 mm are filled.
7. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase Beckmann rearrangement cyclohexanone oxime according to any one of claims 1 to 6, wherein the inclined mode of the inclined plate bed structural unit is that the outer side is inclined, the side wall surfaces of the branch feeding channel and the branch discharging channel, which are far away from the catalyst packed bed layer, are inclined, and the longitudinal section of the catalyst packed bed layer is rectangular;
the inclination mode of the reactor main body is inner side inclination, and the side wall surface of the dry flow feeding channel and the dry flow discharging channel, which is close to the combined bed layer, is inclined.
8. The multilayer inclined plate bed reactor for improving the conversion rate of the gas-phase Beckmann rearrangement cyclohexanone oxime according to any one of claims 1 to 6, wherein the inclined mode of the inclined plate bed structure unit is that the inclined side is inclined, the side wall surfaces of the branch feeding channel and the branch discharging channel, which are close to the catalyst packed bed, are inclined, and the longitudinal section of the catalyst packed bed is a parallelogram;
the inclination mode of the reactor main body is outer side inclination, and the side wall surfaces of the main flow feeding channel and the main flow discharging channel, which are far away from the combined bed layer, are inclined.
9. The use of the multilayer inclined plate bed reactor according to any one of claims 1 to 8 in the preparation of epsilon-caprolactam, wherein the multilayer inclined plate bed reactor is arranged as a fixed bed reactor downstream of a fluidized bed reactor.
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| US2384874A (en) * | 1941-05-02 | 1945-09-18 | Standard Catalytic Co | Hydrocarbon synthesis reaction |
| US4604261A (en) * | 1984-06-29 | 1986-08-05 | Mobil Oil Corporation | Hydroprocessing reactor for catalytically dewaxing liquid petroleum feedstocks |
| EP0279060A2 (en) * | 1987-02-20 | 1988-08-24 | Uhde GmbH | Apparatus for the catalysis of sulphur dioxide into sulphur trioxide |
| CN109289710A (en) * | 2018-10-16 | 2019-02-01 | 中国科学院上海高等研究院 | A kind of radial two-dimentional flow reactor of gas-solid axis |
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2019
- 2019-11-22 CN CN201911153652.8A patent/CN110918006A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL124386C (en) * | ||||
| US2384874A (en) * | 1941-05-02 | 1945-09-18 | Standard Catalytic Co | Hydrocarbon synthesis reaction |
| US4604261A (en) * | 1984-06-29 | 1986-08-05 | Mobil Oil Corporation | Hydroprocessing reactor for catalytically dewaxing liquid petroleum feedstocks |
| EP0279060A2 (en) * | 1987-02-20 | 1988-08-24 | Uhde GmbH | Apparatus for the catalysis of sulphur dioxide into sulphur trioxide |
| CN109289710A (en) * | 2018-10-16 | 2019-02-01 | 中国科学院上海高等研究院 | A kind of radial two-dimentional flow reactor of gas-solid axis |
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Application publication date: 20200327 |