CN211800723U - U-shaped tubular methyl chlorosilane fluidized bed reactor - Google Patents
U-shaped tubular methyl chlorosilane fluidized bed reactor Download PDFInfo
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- CN211800723U CN211800723U CN201922357439.0U CN201922357439U CN211800723U CN 211800723 U CN211800723 U CN 211800723U CN 201922357439 U CN201922357439 U CN 201922357439U CN 211800723 U CN211800723 U CN 211800723U
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Abstract
The utility model relates to a U-shaped tubular methyl chlorosilane fluidized bed reactor, which comprises a middle shell, an upper end socket arranged at the upper part of the middle shell and a lower end socket arranged at the lower part of the middle shell, wherein a gas distributor is arranged at the lower part of the inner part of the middle shell, a plurality of heat exchange tubes are arranged in the upper cavity and are divided into an inner heat exchange tube and a peripheral heat exchange tube, the peripheral heat exchange tube is formed by connecting three U-shaped heat exchange tubes end to end, the inner heat exchange tube is formed by connecting two U-shaped heat exchange tubes end to end, the peripheral heat exchange tubes are radially arranged to form a circular ring enclosure, the inner heat exchange tubes are positioned in the circular ring enclosure, the inner heat exchange tubes are arranged in a rectangular array at equal intervals, the straight tube sections of the U-shaped heat exchange tubes of the inner heat exchange tubes and the peripheral heat exchange tubes, the two ends of the inner heat exchange tube and the outer heat exchange tube which are connected in parallel are respectively connected with the heat medium inlet tube and the heat medium outlet tube, so that the fluidization state of the silicon powder in the reactor is effectively improved.
Description
Technical Field
The utility model belongs to the technical field of fluidized bed reactor, concretely relates to U type tubular methyl chlorosilane fluidized bed reactor.
Background
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be taken as an acknowledgement or any form of suggestion that this information constitutes prior art that is already known to a person skilled in the art.
Methyl chlorosilane is a raw material for producing 107 glue, methyl silicone oil, a cross-linking agent, an end-capping agent (hexamethyldisiloxane) and the like. The key equipment for producing methyl chlorosilane is a fluidized bed synthesis reactor. At present, methyl chlorosilane is produced in a fluidized bed synthesis reactor by using methyl chloride and silicon powder as raw materials through a direct method in the organic silicon industry. The heat exchange effect of the fluidized bed synthesis reactor, the fluidization state of the silicon powder and the uniform distribution of HCl gas directly influence the yield of the methyl chlorosilane.
At present, the organosilicon industry mainly adopts a fluidized bed synthesis reactor with a finger-shaped tube structure, namely, an internal and external heat exchange member is arranged in the reactor. The fluidized bed synthesis reactor of this structure has disadvantages in that the distance between the outer diameter of the tube and the tube is relatively large, and the gas tends to form short circuits and channeling in the solid phase distribution, and a good fluidized state cannot be formed, with the result that uniform reaction and heat dissipation cannot be achieved. In addition, the fluidized bed reactor mainly utilizes gas to enable the silicon powder to be in a uniform fluidized state, the height of the silicon powder is 5-12 m, and all reaction gas needs to be introduced from the bottom of the reactor, so that the gas cannot be uniformly distributed in the reactor, and the silicon powder cannot form a good fluidized state.
SUMMERY OF THE UTILITY MODEL
To the problem that exists among the above-mentioned prior art, the utility model aims at providing a U type tubular methyl chlorosilane fluidized bed reactor. The reactor can effectively improve the uniformity distribution of gas in the bed and improve the fluidization state of silicon powder in the bed.
In order to solve the technical problem, the technical scheme of the utility model is that:
a U-shaped tubular methyl chlorosilane fluidized bed reactor comprises a middle shell, an upper end socket on the upper part of the middle shell and a lower end socket arranged on the lower part of the middle shell, wherein a gas distributor is arranged on the lower part inside the middle shell, the middle shell is divided into an upper cavity and a lower cavity by the gas distributor, a plurality of heat exchange tubes are arranged in the upper cavity and are divided into inner heat exchange tubes and peripheral heat exchange tubes, the peripheral heat exchange tubes are formed by connecting three U-shaped heat exchange tubes end to end, the inner heat exchange tubes are formed by connecting two U-shaped heat exchange tubes end to end, the peripheral heat exchange tubes are radially arranged to form a circular ring-shaped enclosure, the inner heat exchange tubes are positioned inside the circular ring-shaped enclosure, the inner heat exchange tubes are arranged in a rectangular array at equal intervals, the straight tube sections of the U-shaped heat exchange tubes of the inner heat exchange tubes and the peripheral heat exchange tubes are, one end of each heat medium pipe is fixedly connected with the side wall of the middle shell, each group of heat medium pipes comprises a heat medium inlet pipe and a heat medium outlet pipe, a plurality of groups of heat medium pipes are arranged on the outer side wall of the middle shell in the circumferential direction, two ends of every three groups of inner heat exchange pipes are connected in parallel, two ends of the top of every three groups of peripheral heat exchange pipes are connected in parallel, and two ends of the inner heat exchange pipes or the peripheral heat exchange pipes after being connected in parallel are respectively connected with the heat medium inlet pipes and the heat medium outlet pipes.
The utility model discloses the U type pipe quantity that sets up peripheral heat exchange tube and interior heat exchange tube is different, and its reason is for importing and exporting the difference in temperature calculation through the resistance and the heat medium of conduction oil velocity of flow, heat exchange tube, can be balanced middle casing inside and outside heat transfer temperature difference, make central point the same with the heat transfer effect of peripheral part.
As a further technical scheme, the number of the inner heat exchange tubes is 384, the number of the outer heat exchange tubes is 126, and the number of the heat medium tubes is 39-45.
As a further technical scheme, the outer diameter of the U-shaped heat exchange tube is 20-700 mm, and the distance between the outer walls of the adjacent straight tube sections of the U-shaped heat exchange tube is 100-1500 mm. The adjacent straight pipe sections refer to adjacent straight pipe sections of the same U-shaped heat exchange pipe and adjacent straight pipe sections among different U-shaped heat exchange pipes.
As a further technical scheme, the gas distributor is a plate body with a funnel-shaped structure, the bottom and the top of the gas distributor are both of an open structure, and a plurality of through holes which are radially arranged are formed in the gas distributor.
The specification setting of the gas distributor and the U-shaped heat exchange tube can effectively transmit the heat energy generated by the reaction out of the reactor under the condition of ensuring the sufficient flow of materials.
As a further technical scheme, the inside of middle casing sets up the gallows, the structure of gallows is by taut bolt and nut, the cushion, the round steel is constituteed, the top of middle casing sets up the crossbeam, the lower part of upper cover sets up the arc roof beam, connect through the steel sheet between arc roof beam and the crossbeam, the lower part of middle casing sets up the flower disc, taut bolt's top and crossbeam are connected, round steel and flower disc fixed connection are passed through to taut bolt's bottom, taut bolt's top is passed through the cushion and the nut is connected with the crossbeam, the flower disc is passed through to U type heat exchange tube.
The U-shaped heat exchange tube is fixed in the shell by the flower disc, and the position height of the flower disc can be adjusted by the tensioning bolt and the nut, so that the U-shaped heat exchange tube is more flexible to install and replace.
As a further technical scheme, a section of circular side wall at the upper part of the upper cavity body extends outwards to form a protruding part. After the bulge is formed, the sedimentation of the silicon powder is facilitated, the air speed is reduced after the air rises to the expansion part, the pushing effect on the silicon powder is weakened, the silicon powder is changed into a descending state from a rising state and is distributed again, so that the distribution of the silicon powder in the reactor is more uniform, and compared with a fluidized state formed by forcibly pushing the silicon powder by air flow, the design of arranging the expansion part can effectively improve the fluidized state of the silicon powder in the reactor.
As a further technical scheme, a gas phase discharging pipe communicated with the upper cavity is arranged on the upper end enclosure; and a gas inlet pipe and a powder inlet and outlet pipe communicated with the upper cavity are arranged on the lower end enclosure, and the powder inlet and outlet pipe penetrates through the gas distributor from bottom to top and is communicated with the upper cavity.
As a further technical scheme, a safety valve interface is arranged on the upper end enclosure.
The utility model has the advantages that:
the utility model discloses a fluidized bed reactor compares in present finger tube structure fluidized bed synthesis reactor and has improved gaseous evenly distributed, makes silica flour form good fluidization state, has designed the mode of arranging of U type heat exchange tube, has improved even radiating effect and has improved material fluidity.
Drawings
The accompanying drawings, which form a part of the specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention and not to limit the invention unduly.
FIG. 1 is a schematic view of a fluidized bed according to the present invention;
FIG. 2 is a schematic layout view of U-shaped heat exchange tubes inside the upper cavity;
FIG. 3 is a view of the upper part of a fluidized bed reactor;
FIG. 4 is a top view of a gas distributor;
the device comprises an upper end enclosure 1, a lower end enclosure 2, a lower end enclosure 3, a middle shell 4, a gas distributor 5, an upper cavity 6, a lower cavity 7, a heat medium inlet pipe 8, a heat medium outlet pipe 9, a U-shaped heat exchange pipe 10, through holes 11, a gas phase outlet pipe 12, a powder inlet pipe 13, a gas inlet pipe 14, a tension bolt 15, a flower disc 16, a safety valve interface 17, an arc beam 18, a steel plate 19, a nut 20, a cushion block 21, round steel 22 and a cross beam.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
As shown in fig. 1 and 2, the fluidized bed reactor of the utility model has set up the gas distributor 4 made by the perforated plate in the shell, and set up the heat transfer part that adopts U type heat exchange tube 9 as the reactor, the straight tube section of U type heat exchange tube 9 is parallel to each other, and extend along the axis direction of middle casing, the curved dispersion of U-shaped of U type heat exchange tube 9 is arranged, every three group of inner heat exchange tubes or peripheral heat exchange tube are parallelly connected, the both ends at its top respectively with heat medium import pipe 7, heat medium outlet pipe 8 are connected, the quantity that leads to the U-shaped of being located the lower part is bent will be more than the quantity that is located the U-shaped of upper portion, so can furthest reduce the U-shaped and bend the hindrance that reciprocates. When the finger-type heat exchange tube is adopted, the connecting ends among the branch tubes of the finger-type heat exchange tube are positioned at the upper ends of the branch tubes, the finger-type heat exchange tube is of a sleeve structure, so that the finger-type heat exchange tube is thick in appearance, the radius and the distance between the connecting elbows among the branch tubes are large, and the dual factors are overlapped to ensure that the fluidization state is poor. Therefore, after the U-shaped heat exchange tube 9 with multiple tube passes is adopted, the fluidity of the materials in the reaction zone can be effectively improved, and the fluidization state of the materials in the reactor is improved.
The outer diameter of the U-shaped heat exchange tube 9 is 20-700 mm, and the distance between the outer walls of the adjacent straight tube sections of the U-shaped heat exchange tube 9 is 100-1500 mm. The adjacent straight pipe sections refer to the adjacent straight pipe sections of the same U-shaped heat exchange pipe 9 and also refer to the adjacent straight pipe sections between different U-shaped heat exchange pipes 9. The arrangement of the space between the U-shaped heat exchange tubes 9 improves the fluidization state of the silicon powder in the reactor.
As shown in fig. 4, the gas distributor 4 is provided with a plurality of through holes 10, which have the function of uniformly distributing the air, and contribute to improving the uniformity of the silicon powder. The gas distributor is fixedly connected with the inner side wall of the middle shell.
As shown in fig. 3, a hanger is provided inside the middle housing 4, and the hanger is composed of a tension bolt 14, a nut 19, a spacer 20, and a round bar 21. Steel plates 18 are welded between the arc beam 17 and the cross beam 22, the upper portion of the tensioning bolt 14 is fixed on the cross beam 22 inside the upper end enclosure, the cushion block 20 is placed between the nut 19 and the cross beam 22 to prevent the nut 19 from sliding, round steel 21 on the lower portion is welded with the flower disc 15, the arc beam 17 is fixed on the lower portion of the upper end enclosure, the cross beam 22 is located at the top of the middle shell, and the flower disc 15 is located below the cross beam 22. The U-shaped heat exchange tube is fixed in the shell by the flower disc 15, and the position height of the flower disc can be adjusted by the tension bolt 14 and the nut 19, so that the U-shaped heat exchange tube is more flexible to install and replace.
As shown in fig. 1, a section of the circular sidewall of the upper portion of the upper cavity 5 extends outward to form a protrusion. Is beneficial to the sedimentation of the silicon powder.
A gas phase discharge pipe 11 communicated with the upper cavity 5 is arranged on the upper end enclosure 1; and a powder inlet and outlet pipe 12 communicated with the upper cavity 5 and a gas inlet pipe 13 communicated with the lower cavity 6 are arranged on the lower end enclosure 2, and the powder inlet and outlet pipe 12 penetrates through the gas distributor 4 from bottom to top and is communicated with the upper cavity 5.
Silicon powder enters from a powder inlet and outlet pipe 12 of the lower end enclosure 2, methyl chloride gas enters from a gas inlet pipe 13, then the silicon powder is mixed with methyl chloride and enters the middle shell 3 to react, and the reacted mixed gas flows out from a gas phase outlet pipe 11 of the upper end enclosure. Unreacted powder directly enters the gas distributor 4 through the powder inlet and outlet pipe, then is mixed with inlet gas, and reacts again, and waste contact bodies are discharged from an outlet at the lower part.
The upper end enclosure 1 is provided with a safety valve interface 16. A safety valve may be attached to the safety valve port 16, and the safety valve is actuated to release the pressure in the reactor when the pressure in the reactor exceeds a set pressure.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A U type tubular methyl chlorosilane fluidized bed reactor which is characterized in that: the heat exchanger comprises a middle shell, an upper end socket on the upper part of the middle shell and a lower end socket arranged on the lower part of the middle shell, wherein a gas distributor is arranged on the lower part of the inner part of the middle shell, the gas distributor divides the middle shell into an upper cavity and a lower cavity, a plurality of heat exchange tubes are arranged in the upper cavity and are divided into an inner heat exchange tube and a peripheral heat exchange tube, the peripheral heat exchange tube is formed by connecting three U-shaped heat exchange tubes end to end, the inner heat exchange tube is formed by connecting two U-shaped heat exchange tubes end to end, the peripheral heat exchange tubes are radially arranged to form a circular surrounding ring, the inner heat exchange tubes are positioned in the circular surrounding ring, the inner heat exchange tubes are arranged in a rectangular array at equal intervals, straight tube sections of the U-shaped heat exchange tubes of the inner heat exchange tubes and the peripheral heat exchange tubes are parallel to the axis of the middle shell, two ends of the tops of each three, The heat medium outlet pipe is connected.
2. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: the number of the inner heat exchange tubes is 384, the number of the outer heat exchange tubes is 126, and the number of the heat medium tubes is 39-45.
3. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: the outer diameter of the U-shaped heat exchange tube is 20-700 mm, and the distance between the outer walls of the adjacent straight tube sections of the U-shaped heat exchange tube is 100-1500 mm.
4. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: the gas distributor is the plate body of funnel-shaped structure, and bottom and top are open structure, and the last a plurality of through-holes that set up to be radial arrangement of gas distributor.
5. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: the inside of middle casing sets up the gallows, the structure of gallows is by taut bolt and nut, the cushion, the round steel is constituteed, the top of middle casing sets up the crossbeam, the lower part of upper cover sets up the arc roof beam, connect through the steel sheet between arc roof beam and the crossbeam, the lower part of middle casing sets up the flower disc, taut bolt's top and crossbeam are connected, round steel and flower disc fixed connection are passed through to taut bolt's bottom, taut bolt's top is passed through the cushion and the nut is connected with the crossbeam, the flower disc is passed through to U type heat exchange tube.
6. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: a section of circular side wall on the upper part of the upper cavity extends outwards to form a convex part.
7. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: a gas phase discharging pipe communicated with the upper cavity is arranged on the upper sealing head; and a gas inlet pipe and a powder inlet and outlet pipe communicated with the upper cavity are arranged on the lower end enclosure, and the powder inlet and outlet pipe penetrates through the gas distributor from bottom to top and is communicated with the upper cavity.
8. The U-tube methylchlorosilanes fluidized bed reactor of claim 1, wherein: the upper end enclosure is provided with a safety valve interface.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922357439.0U CN211800723U (en) | 2019-12-23 | 2019-12-23 | U-shaped tubular methyl chlorosilane fluidized bed reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922357439.0U CN211800723U (en) | 2019-12-23 | 2019-12-23 | U-shaped tubular methyl chlorosilane fluidized bed reactor |
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| CN211800723U true CN211800723U (en) | 2020-10-30 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114832730A (en) * | 2022-05-06 | 2022-08-02 | 聊城市鲁西化工工程设计有限责任公司 | Fluidized bed reaction device and method for synthesizing organochlorosilane monomer |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114832730A (en) * | 2022-05-06 | 2022-08-02 | 聊城市鲁西化工工程设计有限责任公司 | Fluidized bed reaction device and method for synthesizing organochlorosilane monomer |
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