CN101564665A - Fluidized bed reactor - Google Patents
Fluidized bed reactor Download PDFInfo
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- CN101564665A CN101564665A CNA2009100272861A CN200910027286A CN101564665A CN 101564665 A CN101564665 A CN 101564665A CN A2009100272861 A CNA2009100272861 A CN A2009100272861A CN 200910027286 A CN200910027286 A CN 200910027286A CN 101564665 A CN101564665 A CN 101564665A
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- conduction oil
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Abstract
The invention relates to a fluidized bed reactor, in particular to a fluidized bed reactor suitable for synthesizing methyl chlorosilane. The fluidized bed reactor is characterized in that a conduction oil inlet distribution box (3) is connected with the upper end of an inner tube of a finger-shaped sleeve bundle, and a conduction oil outlet box (4) is connected with the upper end of an outer tube of the finger-shaped sleeve bundle; a feed gas side inlet is provided with a gas guiding device (12); and a feed gas bottom inlet is provided with a gas distribution plate (13) which is arranged on the lower end of the finger-shaped sleeve bundle (9). The fluidized bed reactor can save the energy consumption and improve the reaction yield.
Description
Technical field
The present invention relates to the fluidized-bed reactor of a kind of fluidized-bed reactor, particularly suitable for synthesizing methyl chlorosilane.
Background technology
Methylchlorosilane is a field of organic silicon material commonly used, the direct method synthesizing methyl-chloro-silane is a strong exothermal reaction, for in time getting rid of liberated heat, U type pipe or thimble tube generally all are set as heat exchange structure in fluid bed, and the every pipe that present U type pipe that uses or thimble tube have is connected with outer tube separately, what have organizes with several Guan Weiyi, is connected with outer tube then.But, because reaction is lumpd easily, cause fluidized state to worsen, product quality descends, and reaction selectivity reduces.During the fluid unit maintenance, need other equipment such as top cylindrical shell and upper cover are unloaded, it is very inconvenient to operate.
For very big large-scale fluidized bed of exothermic heat of reaction amount, dozens or even hundreds of heat exchanger tube arranged, the adding of heating surface bank, significantly reduced the net sectional area of bed body, for equal cylinder fluid beds straight, container causes empty tower gas velocity too high, thereby makes the granularity smaller particles be blown a body easily, thereby influences course of reaction.
Distribution grid is an important component part of industrial fluidized bed equipment.The fluidization quality of whole fluid bed and the operating characteristics of reactor all had important effect.The distributing plate structure that existing fluid bed uses is comparatively simple, stephanoporate steel plate just, and each aperture also is covered with one section angle steel, makes air-flow along the ejection of distribution grid level and prevent that particle from falling under the plate.
In addition, the bottom section of general fluid bed adopts conical bed, improves all abundant fluidisation of material that fluidizing velocity makes different-grain diameter.
Summary of the invention
The object of the present invention is to provide a kind of fluidized-bed reactor.This fluidized-bed reactor is particularly suitable for synthesizing methyl-chloro-silane.
Purpose of the present invention realizes in the following manner:
Fluidized-bed reactor of the present invention, comprise conduction oil turnover fuel tank, conduction oil import and export, expanding reach cylindrical shell, straight cylinder body, unstrpped gas import and syngas outlet, wherein conduction oil oil-feed distributor box 3 with go out fuel tank 4 and be connected with thimble tube bundle 9 and place expanding reach cylindrical shell 7 and straight cylinder body 10, wherein conduction oil oil-feed distributor box 3 is connected with pipe upper end in the thimble tube bundle, and conduction oil goes out fuel tank 4 and is connected with thimble tube bundle outer tube upper end; The unstripped gas side inlet is equipped with air flow guiding device 12, and the unstripped gas bottom inlet is equipped with gas distribution grid 13, and gas distribution grid 13 is installed in thimble tube bundle 9 lower ends.
Wherein syngas outlet is evenly distributed on outer ring, expanding reach cylindrical shell 7 top.Syngas outlet is 2-10, and nozzle diameter is 50-500mm, highly is 50-3000mm.
Wherein expanding reach cylindrical shell crown center is provided with conduction oil oil-feed distributor box and conduction oil goes out fuel tank, and conduction oil flows in the thimble tube bundle pipe via distributor box and converges after via chuck flow out fluid bed after conduction oil goes out fuel tank.
Gas distribution grid and air flow guiding device are installed in thimble tube bundle below.Air flow guiding device is installed in the gas distribution grid top.The unstripped gas side circle of contact and bottom vertical air inlet enter fluid bed, make unstrpped gas and solid particle form whirlpool in bed and rise.
The course of work of fluidized-bed reactor of the present invention is, under certain temperature and pressure, partial raw gas enters in the fluid bed by air flow guiding device 12 from unstripped gas sidepiece charging aperture 11, partial raw gas enters in the fluid bed through gas distribution grid 13 from unstripped gas bottom feed mouth 14, with the solid particle reaction that enters from charge door 8, the product that generates is derived by syngas outlet 6, and the residue that reaction finishes in the post-reactor is discharged by slag-drip opening 16.
Fluidized-bed reactor of the present invention following advantages are arranged:
1) mode that adopts gas distribution grid and air flow guiding device to combine, the unstripped gas circle of contact and bottom inflow from the side enters, strengthened the inner lateral flow of bed, make that the interior gas-solid of bed is horizontal mutually and axial flow is more even, and forming whirlpool in fluid bed rises, prevent the deposition of solid particle, strengthened the heat and mass in the course of reaction, improved reaction yield.
2) adopt this heat exchange structure, thimble tube is connected with the conduction oil distributor box, and is simple in structure, is convenient to maintenance is installed, and increased an interior heat transfer sheet area, improved the fluidized state of whole bed, makes the easy control of temperature of gas phase section.
3) the expanding reach cylindrical shell is adopted on fluid bed top, makes the gas prompt drop low, and material is easy to deposit, and is difficult for being taken out of by gas, has reduced the load of subsequent separation system, improves the fluid bed conversion per pass, and energy efficient.
4) the fluid bed bottom section adopts the circle straight barrel, has increased the cylindrical shell volume, makes solid particle and unstrpped gas in abundant fluidisation of this stage, and the flow velocity of reduction material and minimizing are to the wearing and tearing of finger-type tube bank.
Description of drawings
Fig. 1 is the structural representation of fluidized-bed reactor of the present invention (wherein 1. heat conductive oil inlets, 2. conduction oil exhaust outlet, 3. conduction oil oil-feed distributor box, 4. conduction oil goes out fuel tank, 5. conduction oil outlet, 6. syngas outlet, 7. expanding reach cylindrical shell, 8. feed particles charge door, 9. thimble tube bundle, 10. straight cylinder body, 11. unstripped gas sidepiece charging apertures, 12. air flow guiding devices, 13. gas distribution grid, 14. unstripped gas bottom feed mouth, 15. discharging holes, 16. slag-drip openings.)
The specific embodiment
Fluidized-bed reactor
Fluidized-bed reactor of the present invention as shown in Figure 1 has conduction oil oil-feed distributor box 3 and conduction oil to go out fuel tank 4, conduction oil import and export 1,5, expanding reach cylindrical shell 7, straight cylinder body 10 and unstrpped gas import 11,14.Expanding reach cylindrical shell 7 tops are equipped with conduction oil and go out fuel tank 4, conduction oil oil-feed distributor box 3, conduction oil outlet 5 and heat conductive oil inlet 1.Conduction oil oil-feed distributor box 3 is connected with pipe upper end in the thimble tube bundle, and conduction oil goes out fuel tank 4 and is connected with thimble tube bundle outer tube upper end.Conduction oil oil-feed distributor box 3 tops are provided with exhaust outlet 2, outer ring, expanding reach cylindrical shell 7 top is equipped with syngas outlet 6, feed particles charge door 8 is at straight cylinder body 10 middle parts, and thimble tube bundle 9 is installed in the middle of expanding reach cylindrical shell 7 and the straight cylinder body 10, and is connected with the heat conduction fuel tank.Air flow guiding device 12 is connected with unstripped gas sidepiece charging aperture 11, and air flow guiding device 12 is installed in thimble tube bundle 9 belows, the top of gas distribution grid 13.The fluid bed bottom is provided with unstripped gas bottom feed mouth 10, slag-drip opening 16 and discharging hole 15.
Synthesizing methyl-chloro-silane
As the fluidized-bed reactor of embodiment 1,2 of syngas outlet, diameter is 200mm.Regulate 75% (mass ratio of unstrpped gas chloromethanes, enter from fluid bed bottom air inlet 14 down together), gas flow rate is 0.38m/s, form the air-flow of axial flow, remain 25% methyl chloride gas by 11 air inlets of unstripped gas sidepiece air inlet, gas flow rate is 28m/s, make air-flow on original axial velocity basis, add tangential velocity, when temperature is 285 ℃, with raw silicon powder particles and copper catalyst and co-catalyst (aluminium powder, zinc powder and/or glass putty) add from fluid bed raw materials mouth 8, thereby cause the shape rising in the shape of a spiral of unstrpped gas entrained solids particle, entire reaction course feed particles and catalyst etc. prolong with unstrpped gas time of contact, the chloromethanes conversion per pass is 35%, and the dimethyldichlorosilane selectivity is 88%.
Claims (4)
1, a kind of fluidized-bed reactor, comprise that conduction oil oil-feed distributor box and conduction oil go out fuel tank, conduction oil import and export, expanding reach cylindrical shell, straight cylinder body, unstrpped gas import and syngas outlet, wherein conduction oil oil-feed distributor box (3) and conduction oil go out fuel tank (4) and are connected with thimble tube bundle (9) and place expanding reach cylindrical shell (7) and straight cylinder body (10), it is characterized in that conduction oil oil-feed distributor box (3) is connected with pipe upper end in the thimble tube bundle, conduction oil goes out fuel tank (4) and is connected with thimble tube bundle outer tube upper end; The unstripped gas side inlet is equipped with air flow guiding device (12), and the unstripped gas bottom inlet is equipped with gas distribution grid (13), and gas distribution grid (13) is installed in thimble tube bundle (9) lower end.
2, fluidized-bed reactor according to claim 1 is characterized in that syngas outlet is arranged on expanding reach cylindrical shell (7) outer ring, top.
3, fluidized-bed reactor according to claim 2 is characterized in that syngas outlet is 2-10, and nozzle diameter is 50-500mm, highly is 50-3000mm.
4, fluidized-bed reactor according to claim 1 is characterized in that air flow guiding device installs the top of thimble tube bundle below, gas distribution grid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100272861A CN101564665A (en) | 2009-05-27 | 2009-05-27 | Fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100272861A CN101564665A (en) | 2009-05-27 | 2009-05-27 | Fluidized bed reactor |
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| CN101564665A true CN101564665A (en) | 2009-10-28 |
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| CNA2009100272861A Pending CN101564665A (en) | 2009-05-27 | 2009-05-27 | Fluidized bed reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109179545A (en) * | 2018-08-30 | 2019-01-11 | 浙江工业大学 | A kind of apparatus system using power-plant flue gas Heat Treatment desulfurization wastewater |
| CN110496573A (en) * | 2019-09-11 | 2019-11-26 | 哈尔滨理工大学 | A kind of dock fluidized-bed reactor |
| CN112791671A (en) * | 2020-12-10 | 2021-05-14 | 青岛科技大学 | Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor |
-
2009
- 2009-05-27 CN CNA2009100272861A patent/CN101564665A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109179545A (en) * | 2018-08-30 | 2019-01-11 | 浙江工业大学 | A kind of apparatus system using power-plant flue gas Heat Treatment desulfurization wastewater |
| CN109179545B (en) * | 2018-08-30 | 2021-06-01 | 浙江工业大学 | Device system for treating desulfurization wastewater by using flue gas waste heat of power plant |
| CN110496573A (en) * | 2019-09-11 | 2019-11-26 | 哈尔滨理工大学 | A kind of dock fluidized-bed reactor |
| CN112791671A (en) * | 2020-12-10 | 2021-05-14 | 青岛科技大学 | Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor |
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Open date: 20091028 |