CN221268054U - Multi-bed laminar flow reactor for organosilicon production - Google Patents
Multi-bed laminar flow reactor for organosilicon production Download PDFInfo
- Publication number
- CN221268054U CN221268054U CN202323158351.9U CN202323158351U CN221268054U CN 221268054 U CN221268054 U CN 221268054U CN 202323158351 U CN202323158351 U CN 202323158351U CN 221268054 U CN221268054 U CN 221268054U
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- Prior art keywords
- laminar flow
- flow reactor
- layer
- sieve
- bed
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 239000010410 layer Substances 0.000 claims abstract description 28
- 239000007790 solid phase Substances 0.000 claims abstract description 12
- 239000011229 interlayer Substances 0.000 claims abstract description 4
- 239000012071 phase Substances 0.000 claims description 10
- 229920001296 polysiloxane Polymers 0.000 claims description 6
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 abstract description 20
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 238000007086 side reaction Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 230000005465 channeling Effects 0.000 abstract description 2
- 239000012530 fluid Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 16
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 9
- 239000011863 silicon-based powder Substances 0.000 description 6
- 239000007787 solid Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 239000010703 silicon Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- LIKFHECYJZWXFJ-UHFFFAOYSA-N dimethyldichlorosilane Chemical compound C[Si](C)(Cl)Cl LIKFHECYJZWXFJ-UHFFFAOYSA-N 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229910021487 silica fume Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Abstract
The utility model discloses a multi-bed laminar flow reactor for organosilicon production, wherein a plurality of layers of sieve plates are equidistantly arranged in a shell, a heat exchanger is arranged on the lower side of each layer of sieve plate, and overflow pipes are arranged at staggered positions of two adjacent layers of sieve plates. The number of layers of the sieve plate is 3-5, and the interlayer spacing is 3-7 m. The tail end of the overflow pipe extends to the position of the heat exchanger arranged on the lower side of each layer of the sieve plate. The unique fluidized bed distributor and internal part design of the utility model effectively inhibit the generation of fluid return and bubbles, avoid channeling, enhance the mass transfer and heat transfer effects of gas and solid phases, and have high chloromethane conversion rate and less side reaction.
Description
Technical Field
The utility model belongs to the technical field of organosilicon production, and particularly relates to a multi-bed laminar flow reactor for organosilicon production.
Background
Fluidized bed reactors are one of the key devices for silicone production. In the fluidized bed reactor, gaseous chloromethane and solid silicon powder react under certain conditions to generate organic silicon monomers, and heat is released in the process. The chloromethane gas enters the reactor from the bottom of the reactor and reacts with the silicon powder in the reactor, so that the chloromethane gas in the fluidized bed reactor must reach a certain speed in order to improve the reaction efficiency of the silicon powder and chloromethane in the reactor, the silicon powder is ensured to be in a certain fluidization state, and the silicon powder and chloromethane can be fully contacted. Under the condition of ensuring the fluidization state of the silicon powder, the solid can rise from the central part of the bed layer, descend along the wall surface with gradually reduced air speed, and in the descending process, part of particles are radially mixed. The main air flow rises along the center of the bed layer, most of the air is separated from the bed layer through the central core part, but part of the air is turned around to flow downwards along the gap between the bed walls to be converged with the new air flow when approaching the bed surface. Although the back mixing is favorable for the temperature of the fluidized bed reactor to be uniform, the product dilutes the chloromethane gas due to the back mixing of the gas, so that the conversion rate is reduced, and the side reaction is increased.
Disclosure of utility model
Aiming at the problems that the conversion rate is reduced and the side reaction is increased due to back mixing of gas in the existing reactor, the utility model provides a multi-bed laminar flow reactor for producing organic silicon;
the technical scheme provided by the utility model is as follows:
a multi-bed laminar flow reactor for organosilicon production is characterized in that a plurality of layers of sieve plates are arranged in a shell at equal intervals, a heat exchanger is arranged on the lower side of each layer of sieve plate, and overflow pipes are arranged at staggered positions of two adjacent layers of sieve plates.
The number of layers of the sieve plate is 3-5, and the interlayer spacing is 3-7 m.
The tail end of the overflow pipe extends to the position of the heat exchanger arranged on the lower side of each layer of the sieve plate.
The shell is provided with a pressure gauge, a thermometer and a window at the opposite position of each layer of heat exchanger.
The upper part of the shell is provided with a solid phase inlet and a gas phase outlet; the bottom of the shell is provided with a solid phase outlet and a gas phase inlet.
The utility model has the beneficial effects that: the utility model effectively inhibits the generation of fluid return and bubbles, avoids channeling, enhances the mass transfer and heat transfer effects of gas and solid phases, and has high chloromethane conversion rate and less side reaction.
The utility model reduces the adverse effect caused by the back mixing of solid and gas, and ensures that the primary conversion rate of chloromethane is more than 70 percent and the selectivity of dimethyl dichlorosilane is more than 90 percent. Each layer of heat exchange tube has short path and high heat transfer efficiency, and is convenient for timely removing the heat exchanger, thereby improving the production stability.
Drawings
FIG. 1 is a schematic diagram of a multi-bed laminar flow reactor for producing silicone;
In the figure: the device comprises a shell 1, a heat exchange tube 2, a sieve plate 3, an overflow pipe 4, a solid phase inlet 5, a gas phase outlet 6, a gas phase inlet 7 and a solid phase outlet 8.
Detailed Description
The utility model is described in further detail below with reference to the drawings and the specific examples.
Example 1
A multi-bed laminar flow reactor for organosilicon production is provided, wherein a plurality of layers of sieve plates 3 are equidistantly arranged in a shell 1, a heat exchanger 2 is arranged on the lower side of each layer of sieve plate 3, and overflow pipes 4 are arranged at staggered positions of two adjacent layers of sieve plates.
The number of layers of the screen plate 3 is 5, and the interlayer spacing is 6 m.
The end of the overflow pipe 4 extends to the position of the heat exchanger 2 arranged on the lower side of each layer of screen plate 3.
The shell 1 is provided with a pressure gauge, a thermometer and a window at the opposite position of each layer of heat exchanger 2.
The upper part of the shell 1 is provided with a solid phase inlet 5 and a gas phase outlet 6; the bottom of the shell 1 is provided with a solid phase outlet 8 and a gas phase inlet 7.
Example 2
The multi-bed laminar flow reactor for producing the organic silicon of the embodiment 1 is adopted, and the implementation process is as follows: silica fume and catalyst enter the sieve plate 3 through the solid phase inlet 5, transversely enter the overflow pipe 4 through the sieve plate 3, then sequentially pass through the residual sieve plate and the overflow pipe, and the residual substances leave the reactor from the solid phase outlet 8. The chloromethane gas enters the gas phase inlet 7, passes through the sieve holes of each layer of sieve plate from bottom to top in sequence to fluidize with the solid and participate in the reaction, and finally leaves the reactor together with the reaction product through the gas phase outlet 6. The reaction process maintains the reaction temperature through four layers of heat exchange tubes 2.
The above embodiments are merely preferred embodiments of the present utility model, and should not be construed as limiting the present utility model, and the embodiments and features of the embodiments of the present utility model may be arbitrarily combined with each other without collision. The protection scope of the present utility model is defined by the claims, and the protection scope includes equivalent alternatives to the technical features of the claims. I.e., equivalent replacement modifications within the scope of this utility model are also within the scope of the utility model.
Claims (5)
1. A multi-bed laminar flow reactor for organosilicon production, characterized in that: inside equidistance of casing (1) sets up multilayer sieve (3), and every layer of sieve (3) downside sets up a heat exchanger (2), and the staggered position of adjacent two-layer sieve is provided with overflow pipe (4).
2. The multi-bed laminar flow reactor for producing silicone according to claim 1, characterized in that: the number of layers of the sieve plate (3) is 3-5, and the interlayer spacing is 3-7 m.
3. The multi-bed laminar flow reactor for producing silicone according to claim 1, characterized in that: the tail end of the overflow pipe (4) extends to the position of the heat exchanger (2) arranged at the lower side of each layer of the sieve plate (3).
4. The multi-bed laminar flow reactor for producing silicone according to claim 1, characterized in that: the shell (1) is provided with a pressure gauge, a thermometer and a window at the position opposite to each layer of heat exchanger (2).
5. The multi-bed laminar flow reactor for producing silicone according to claim 1, characterized in that: the upper part of the shell (1) is provided with a solid phase inlet (5) and a gas phase outlet (6); the bottom of the shell (1) is provided with a solid phase outlet (8) and a gas phase inlet (7).
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN221268054U true CN221268054U (en) | 2024-07-05 |
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| Date | Code | Title | Description |
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| GR01 | Patent grant |