CN201962078U

CN201962078U - Disproportionation reaction device

Info

Publication number: CN201962078U
Application number: CN2010206314531U
Authority: CN
Inventors: 张松林; 丁显波; 周勇
Original assignee: BYD Co Ltd
Current assignee: BYD Co Ltd
Priority date: 2010-11-27
Filing date: 2010-11-27
Publication date: 2011-09-07
Anticipated expiration: 2020-11-27

Abstract

The utility model provides a disproportionation reaction device. The disproportionation reaction device comprises a reaction device main body, a catalysis bed, a heating device, a waste material outlet and a raw material input device, wherein the catalysis bed comprises a helix tube structure and filler arranged in the helix tube structure; the raw material input device comprises a raw material pipeline and an atomization device; and the atomization device comprises an inlet port and an outlet port, the inlet port of the atomization device is connected with the raw material pipeline, and the outlet port of the atomization device is arranged in the reaction device main body. By adopting the disproportionation reaction device, the technical problems that a common disproportionation reaction device is high in energy consumption and unstable when raw material is evaporated and is low in primary reaction conversion rate can be solved. In the catalysis bed of the disproportionation reaction device, HSiCl3 is completely disproportioned in a gas state, the reaction process is stable in pressure, and the reaction residence time of the reaction raw material HSiCl3 is longer in the catalysis bed, so that the disproportionation reaction device can achieve a higher primary conversion rate.

Description

A kind of disproportionation reactor

Technical field

The utility model relates to the disproportionation reactor that a kind of trichlorosilane disproportionation prepares dichloro hydrogen silicon.

Background technology

H ₂SiCl ₂Be a kind of used in electronic industry raw material of high value, be widely used in fields such as epitaxial silicon crystalline chemical vapor deposition (CVD) and high performance solar cells.H ₂SiCl ₂Synthetic three kinds of discrimination method, chlorination process and the hydride processs that mainly contain of industry.Discrimination method prepares H ₂SiCl ₂Main reaction as follows:

2HSiCl ₃→H ₂SiCl ₂+SiCl ₄

This reaction is a reversible reaction, at HSiCl ₃Gas, liquid all can react down, but under gas phase condition, and fast many of speed of reaction are example with 60 ℃ of reaction conditionss, fast about 100 times than liquid phase reaction of gas-phase reactions.In existing technology, prepare H by discrimination method ₂SiCl ₂Reactor, take more the bottom heating evaporation mode, slowly evaporate HSiCl ₃Liquid is to reach gas-phase reaction, and vaporator rate is low, and consumption of calorie is more, and owing to exists HSiCl ₃The mutual conversion of gas-liquid phase makes that pressure has fluctuation in the reaction process; And what catalytic bed was often taked is through type, and the reaction time of reactant is shorter, and the primary first-order equation transformation efficiency is on the low side, and the length of lengthening catalytic bed can cause the catalytic bed front and back end to exist bigger pressure again and fall.

The utility model content

The above-mentioned feed vaporization process energy consumption of mentioning is big in order to solve for the utility model, instability and the low technical problem of primary first-order equation transformation efficiency, and a kind of disproportionation reactor is provided.

A kind of disproportionation reactor comprises reactor body, catalytic bed, heating unit, waste material relief outlet and raw material input device; Wherein, catalytic bed is positioned at reactor body top, and heating unit is positioned at around the reactor body, and waste material relief outlet and raw material input device are positioned at the reactor body bottom;

Catalytic bed comprises spiral tube structure and is positioned at the filler of spiral tube structure; Raw material input device comprises raw material pipeline and atomisation unit; Atomisation unit comprises inlet end and exit end, and its inlet end links to each other with the raw material pipeline, and exit end places reactor body.

In the disproportionation reactor that the utility model provides, spiral tube structure can be various spiral pipes such as coil pipe, and the internal diameter of coil pipe is preferably 50-200mm, and the diameter that spirals is preferably 150-300mm;

There is screen cloth at the spiral tube structure two ends, and filler is between two screen clothes; There is fixed terminal the screen cloth both sides, are fixed in the spiral tube structure; Screen sizes is consistent with the coil pipe internal diameter, and thickness is preferably 2-10mm, and the aperture is preferably 0.5-3mm; Filler can be resin catalyst, molecular sieve catalyst or activated-carbon catalyst.

In the disproportionation reactor that the utility model provides, atomisation unit be the technician known various can be with the device of the atomization of liquid; Under the preferable case, can be spray header, spray header utilizes the high-pressure liquid raw material to be ejected into by the pore spray header and realizes atomizing heating vaporization in the heated cavity.Be distributed with some apertures on the spray header, the aperture of aperture is enough little, can be vaporized fully after guaranteeing that raw material has under certain flow condition, will making raw material enter into reactor simultaneously.Under the preferable case, the aperture of spray header is 0.5-2mm; Further preferred, the aperture of spray header is 1.5mm.

In the disproportionation reactor that the utility model provides, the reactor body height is preferably 1000-4000mm; Internal diameter is preferably 150-400mm.The internal diameter of raw material pipeline is preferably 10-100mm.

Also has the oil bath thermal insulation layer around the disproportionation reactor that the utility model provides.

The disproportionation reactor that adopts the utility model to provide has solved in the general disproportionation reactor that raw material vaporescence energy consumption is big, instability and the low technical problem of primary first-order equation transformation efficiency.Raw material HSiCl ₃Through raw material pipeline and atomisation unit, enter into reactor body with the form of " atomizing ", can be fast in reactor, the sufficient vaporization, enter into catalytic bed with the form of complete gas phase disproportionation reaction takes place, can keep pressure stable in the reaction process; Catalytic bed adopts the coil tube type filler simultaneously, makes HSiCl ₃Flow velocity in catalytic bed slows down, and under same vertical height condition, coil tube type has longer catalytic bed length, makes reaction raw materials HSiCl ₃Long reaction time is arranged in catalytic bed, thereby a higher transformation efficiency is arranged.

Description of drawings

Fig. 1 is the structural representation of disproportionation reactor in the utility model embodiment;

Fig. 2 is the structural representation of spray header in the utility model embodiment;

Fig. 3 is the structural representation of catalytic bed two ends screen cloth in the utility model embodiment;

Fig. 4 is the structural representation of catalytic bed in the utility model embodiment.

Embodiment

Clearer for technical problem, technical scheme and beneficial effect that the utility model is solved, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein only in order to explanation the utility model, and be not used in qualification the utility model.

As shown in Figure 1 and Figure 4, the disproportionation reactor that provides in this example comprises reactor body 11, catalytic bed 4, heating unit 3, waste material relief outlet 5 and raw material input device; Wherein, catalytic bed 4 is positioned at reactor body top, and heating unit 3 is positioned at around the reactor body, and waste material relief outlet 5 and raw material input device are positioned at the reactor body bottom; Catalytic bed 4 comprises spiral tube structure 13 and is positioned at the filler 12 of spiral tube structure; Raw material input device comprises raw material pipeline 1 and atomisation unit; Atomisation unit comprises inlet end 10 and exit end 2, and its inlet end 10 links to each other with raw material pipeline 1, and exit end 2 places reactor body.

In the disproportionation reactor that provides in this example, exit end 2 is a spray header, as shown in Figure 2.

There is screen cloth 6 at the spiral tube structure two ends, as shown in Figure 3; Filler 12 is between two screen clothes; There is fixed terminal 7 the screen cloth both sides, are fixed in the spiral tube structure 13; Spiral tube structure 13 is connected with export pipeline 8.

Oil bath thermal insulation layer 9 is be provided around the disproportionation reactor that provides in this example.

Adopt the disproportionation reactor that provides in this example, HSiCl ₃Raw material is preheated in raw material pipeline 1, successively by behind inlet end 10 and the spray header 2, enters into reactor body 11 with the form of " atomizing ", under the effect of reactor heating unit 3, whole reactor main body 11 comprises that 4 sections of catalytic beds are heated to 80 ℃, and this temperature has surpassed HSiCl ₃Boiling point, make HSiCl ₃Vaporization enters into catalytic bed 4 then fully, through screen cloth 6, with filler 12 disproportionation reaction takes place in spiral tube structure 13, HSiCl ₃Part be transformed into H ₂SiCl ₂And SiCl ₄, the three leaves catalytic bed 4 with the gasiform form by export pipeline 8, enters in the knockout tower.In the entire reaction course, keep temperature of reaction in the reactor by oil bath thermal insulation layer 9; The impurity that the solid waste that is produced after some solid catalyst fragmentations and some other liquid state can not heat vaporization is discharged by waste material relief outlet 5.

The above only is a better embodiment of the present utility model; not in order to restriction the utility model; all any modifications of within spirit of the present utility model and principle, being done, be equal to and replace and improvement etc., all should be included within the protection domain of the present utility model.

Claims

1. a disproportionation reactor comprises reactor body, catalytic bed, heating unit, waste material relief outlet and raw material input device; Described catalytic bed is positioned at reactor body top, and described heating unit is positioned at around the reactor body, and described waste material relief outlet and described raw material input device are positioned at the reactor body bottom;

It is characterized in that: described catalytic bed comprises spiral tube structure and is positioned at the filler of spiral tube structure;

Described raw material input device comprises raw material pipeline and atomisation unit;

Described atomisation unit comprises inlet end and exit end, and its inlet end links to each other with the raw material pipeline, and exit end places reactor body.

2. disproportionation reactor as claimed in claim 1 is characterized in that: described spiral tube structure is a coil pipe, and the internal diameter of described coil pipe is 50-200mm, and the diameter that spirals of described coil pipe is 150-300mm.

3. disproportionation reactor as claimed in claim 1 is characterized in that: there is screen cloth at described spiral tube structure two ends, and described filler is between two screen clothes.

4. disproportionation reactor as claimed in claim 3 is characterized in that: described screen sizes is consistent with the coil pipe internal diameter, and the thickness of described screen cloth is 2-10mm, and the aperture of described screen cloth is 0.5-3mm.

5. disproportionation reactor as claimed in claim 1 is characterized in that: described exit end is a spray header.

6. disproportionation reactor as claimed in claim 5 is characterized in that: be distributed with some apertures on the described spray header, the aperture of described aperture is 0.5-2mm.

7. disproportionation reactor as claimed in claim 1 is characterized in that: the height of described reactor body is 1000-4000mm; The internal diameter of described reactor body is 150-400mm.

8. disproportionation reactor as claimed in claim 1 is characterized in that: the internal diameter of described raw material pipeline is 10-100mm.

9. disproportionation reactor as claimed in claim 1 is characterized in that: the oil bath thermal insulation layer is arranged around the described disproportionation reactor.