CN205550236U - Synthetic fluidized bed reactor of methylchlorosilane monomer - Google Patents
Synthetic fluidized bed reactor of methylchlorosilane monomer Download PDFInfo
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- CN205550236U CN205550236U CN201620142512.6U CN201620142512U CN205550236U CN 205550236 U CN205550236 U CN 205550236U CN 201620142512 U CN201620142512 U CN 201620142512U CN 205550236 U CN205550236 U CN 205550236U
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Abstract
The utility model provides one kind has synthetic fluidized bed reactor of methylchlorosilane monomer, which comprises a tank body, respectively with the discharging pipe of jar body intercommunication, the silica flour inlet pipe, the chloromethane inlet pipe, advance oil pipe and arrange oil pipe, still including installing at internal many heat exchange tubes of jar and gas distributor base, be equipped with baffle and baffle down at jar internal interval, it personally experiences sth. Part of the body the jar at a distance from faling into the oil return cavity with lower baffle to go up the baffle, oil feed cavity and reaction cavity, advance oil pipe and oil feed cavity intercommunication, arrange oil pipe and oil return cavity intercommunication, gas distributor base installs in the reaction cavity, to react the cavity by gas distributor base separates to become and reacts the cavity and react the cavity under with, the chloromethane inlet pipe with react down the cavity and communicate, the silica flour inlet pipe passes down and reacts cavity and gas distributor base and last reaction cavity intercommunication, the heat exchange tube is located and reacts the cavity, and the both ends of heat exchange tube communicate with oil return cavity and oil feed cavity respectively, the discharging pipe passes oil return cavity and oil feed cavity and last reaction cavity intercommunication in proper order, the heat exchange tube is many U -shapeds pipe.
Description
Technical field
This utility model belongs to chemical industry technical field of organic silicon production, and relating to one has methyl chlorosilane monomer resultant current fluidized bed reactor.
Background technology
The features such as organosilicon material has the high-and low-temperature resistance of excellence, biocompatibility, can be widely applied to the fields such as industry, agricultural, military project, enjoy the good reputation of " industry monosodium glutamate " in industrial quarters.Fluidized-bed reactor is one of nucleus equipment of organosilicon production, under catalyst action, silica flour and gaseous chlorine methane synthesize gaseous organosilicon monomer under about 300 DEG C temperature conditionss, owing to silica flour is big with chloromethanes exothermic heat of reaction amount, in order to maintain reaction temperature condition constant, reaction is made to be smoothed out safely, it is necessary in time reaction heat to be removed fluid bed.
At present, organosilicon manufacturing enterprise all uses conduction oil as fluidized bed heat exchanger medium both at home and abroad, inside reactor is distributed a large amount of finger-type pipes (finger-type pipe is sleeve pipe, and in inner tube not contact bed, reaction mass, only outer tube wall are heat-transfer surfaces) or single U-tube to reach heat exchange purpose.Chinese patent CN
2623329Y describes a kind of fluidized-bed reactor, uses finger-type heat exchange tube, tube sheet and the heat exchange structure of conduction oil allotter composition, the centrally disposed syngas outlet of tube sheet.This fluidized-bed reactor fluidization quality is good, and installation, maintenance is convenient, but finger-type pipe only outer tube wall is direct and the heat-transfer surface of material-heat-exchanging in bed, heat transfer effect is undesirable, the finger-type pipe quantity needed is more, occupies reactor mass efficient reaction compartment, reduces the production capacity of reactor；Chinese patent CN 203598804U describes a kind of organic silicon monomer resultant current fluidized bed reactor, uses U-tube heat exchanger, with distributed rectangular device, heat-conducting oil pipes and oil tank joint is linked up, built-in primary cyclone etc. in the upper space dilute phase section of bed.Heat exchange efficiency is high, low cost of manufacture, and solve conventional u-shaped pipe and short tube dust stratification knot carbon, react the problem such as overheated, but owing to heat-conducting oil pipes and oil tank joint are linked up by needs at fluid bed top dilute phase section distributed rectangular device, technique is loaded down with trivial details, junction is also the most damaged, adds manufacture processing and maintenance maintenance difficulty.
Summary of the invention
The technical problems to be solved in the utility model is to provide one methyl chlorosilane monomer resultant current fluidized bed reactor, rational in infrastructure, and heat exchange efficiency is high, and the bed inner volume that heat exchanger tube takies is little, and in bed, " effective volume rate " is high, and organic silicon monomer production capacity is big.
In order to solve the problems referred to above, the technical solution of the utility model is: one has methyl chlorosilane monomer resultant current fluidized bed reactor, discharge nozzle, silica flour feed pipe, chloromethanes feed pipe, oil inlet pipe and the oil exit pipe including tank body, connected with tank body respectively, also include many heat exchanger tubes and the gas distribution grid being arranged in tank body
Upper spacer and lower clapboard it is interval with in tank body, upper spacer and lower clapboard by tank body every being divided into oil return cavity, oil-feed cavity and reaction cavity, oil inlet pipe connects with oil-feed cavity, oil exit pipe connects with oil return cavity, gas distribution grid is arranged in reaction cavity, by gas distribution grid, reaction cavity is separated into upper reaction cavity and lower reaction cavity, chloromethanes feed pipe connects with lower reaction cavity, silica flour feed pipe connects with upper reaction cavity through lower reaction cavity with gas distribution grid, heat exchanger tube is positioned at reaction cavity, and the two ends of heat exchanger tube connect with oil return cavity and oil-feed cavity respectively, discharge nozzle sequentially passes through oil return cavity and connects with upper reaction cavity with oil-feed cavity, described heat exchanger tube is many U-tube.
Further, the mouth of pipe of one end of heat exchanger tube connects through lower clapboard with oil-feed cavity, and the axis normal direction of the one end connected with oil-feed cavity is in lower clapboard；The other end of mouth of pipe of heat exchanger tube connects with oil return cavity through lower clapboard with upper spacer, and the axis normal direction of one end of oil return cavity connection is in upper spacer.
Further, the axis of discharge nozzle and the axis of tank body are parallel.
Further, gas distribution grid has two pieces, and two pieces of gas distribution grids are arranged in reaction cavity with the axis of tank body as line of symmetry, in " V " type.
Further, chloromethanes feed pipe has two, and two chloromethanes feed pipes and two pieces of gas distribution grids are corresponding.
Technique effect of the present utility model is:
1, many U heat exchange are used.When " than heat-transfer surface " (heat-transfer surface is divided by by the volume of heat exchange) is identical, the bed inner volume that many U heat exchange account for is little, and in bed, " effective volume rate " is high, improves the production intensity of fluid bed；Many U heat exchange heat exchange uniformity is high, good effect of heat exchange；Fluid bed effective reaction space is bigger, improves fluidization quality, enhances mass transfer effect.
2, heat exchanger tube normal direction is in upper spacer and lower clapboard.Make conduction oil flow resistance minimum, the settlement separate function of fluid bed dilute phase section can give full play to, and due to simple in construction, and the mouth of pipe of heat exchanger tube one end is directly inserted in oil-feed cavity and oil return cavity, make easy to maintenance, reduce heat exchanger tube little by damaged probability with dividing plate junction.
3, after product passes fuel tank center, the surface of self-fluidized type bed is discharged.In making fluid bed, fluidization is normal, good evenness, not bias current；Need not the useless height of bed increased because side goes out.
4, gas distribution grid is V-shaped is symmetrically mounted in reaction cavity, expands the surface area of gas distribution grid so that react more abundant.
Accompanying drawing explanation
Below in conjunction with the accompanying drawings this utility model is described further:
I master of the present utility model of Fig. 1 regards generalized section.
Detailed description of the invention
As shown in Figure 1: one has methyl chlorosilane monomer resultant current fluidized bed reactor, discharge nozzle 2, silica flour feed pipe 6, chloromethanes feed pipe 5, oil inlet pipe 3 and the oil exit pipe 4 including tank body 1, connected with tank body 1 respectively, also include many heat exchanger tubes 10 and the gas distribution grid 7 being arranged in tank body 1
nullUpper spacer 9 and lower clapboard 91 it is interval with in tank body 1，Upper spacer 9 and lower clapboard 91 by tank body 1 every being divided into oil return cavity 11、Oil-feed cavity 12 and reaction cavity，Oil inlet pipe 3 connects with oil-feed cavity 12，Oil exit pipe 4 connects with oil return cavity 11，Gas distribution grid 7 is arranged in reaction cavity，By gas distribution grid 7, reaction cavity is separated into upper reaction cavity 13 and lower reaction cavity 14，Chloromethanes feed pipe 5 connects with lower reaction cavity 14，Silica flour feed pipe 6 connects with upper reaction cavity 13 through lower reaction cavity 14 with gas distribution grid 7，Heat exchanger tube 10 is positioned at reaction cavity 13，And the two ends of heat exchanger tube 10 connect with oil return cavity 11 and oil-feed cavity 12 respectively，Discharge nozzle 2 sequentially passes through oil return cavity 11 and connects with upper reaction cavity 13 with oil-feed cavity 12，Many U-tube that described heat exchanger tube 10 is，Many U-tube are to be constituted by multiple U-tube are end to end，Shape is as shown in Figure 1.
Further, the mouth of pipe of one end of heat exchanger tube 10 connects through lower clapboard 91 with oil-feed cavity 12, and the axis normal direction of the one end connected with oil-feed cavity 12 is in lower clapboard 91；The other end of mouth of pipe of heat exchanger tube 10 connects with oil return cavity 11 through lower clapboard 91 with upper spacer 9, and the axis normal direction of one end of an oil return cavity 11 connection is in upper spacer 9.
Further, the axis of discharge nozzle 2 is parallel with the axis of tank body 1.
Further, gas distribution grid 7 has two pieces, and two pieces of gas distribution grids 7 are arranged in reaction cavity with the axis of tank body 1 as line of symmetry, in " V " type.
Further, chloromethanes feed pipe 5 has two, and two chloromethanes feed pipes 5 are corresponding with two pieces of gas distribution grids 7.
Time specifically used, silica flour enters in upper reaction cavity 13 from silica flour feed pipe 6, and methyl chloride gas is entered in lower reaction cavity 14 by chloromethanes feed pipe 5, after gas distribution grid 7, making the silica flour fluidization in reaction cavity 13, product is discharged from discharge nozzle 2；In course of reaction, reaction cavity 13 taken out of by produced heat oil exit pipe 4 after the heat exchange of many heat exchanger tubes 10, and wherein, conduction oil flow direction in reaction cavity is: oil inlet pipe 3, oil-feed cavity 12, heat exchanger tube 10, oil return cavity 11, oil exit pipe 4.
It is obvious to a person skilled in the art that this utility model is not limited to the details of above-mentioned one exemplary embodiment, and in the case of without departing substantially from spirit or essential attributes of the present utility model, it is possible to realize this utility model in other specific forms.Therefore, no matter from the point of view of which point, embodiment all should be regarded as exemplary, and be nonrestrictive, scope of the present utility model is limited by claims rather than described above, it is intended that all changes fallen in the implication of equivalency and scope of claim included in this utility model.Should not be considered as limiting involved claim by any reference in claim.
The above; it is only preferred embodiment of the present utility model; not in order to limit this utility model, every any trickle amendment, equivalent and improvement made above example according to technical spirit of the present utility model, within should be included in the protection domain of technical solutions of the utility model.
Claims (5)
1. one kind has methyl chlorosilane monomer resultant current fluidized bed reactor, discharge nozzle (2), silica flour feed pipe (6), chloromethanes feed pipe (5), oil inlet pipe (3) and the oil exit pipe (4) including tank body (1), connected with tank body (1) respectively, also include many heat exchanger tubes (10) and the gas distribution grid (7) being arranged in tank body (1), one circle heat tracing pipe (8) is installed outside tank body (1), it is characterised in that:
nullUpper spacer (9) and lower clapboard (91) it is interval with in tank body (1)，Upper spacer (9) and lower clapboard (91) by tank body (1) every being divided into oil return cavity (11)、Oil-feed cavity (12) and reaction cavity，Oil inlet pipe (3) connects with oil-feed cavity (12)，Oil exit pipe (4) connects with oil return cavity (11)，Gas distribution grid (7) is arranged in reaction cavity，By gas distribution grid (7), reaction cavity is separated into upper reaction cavity (13) and lower reaction cavity (14)，Chloromethanes feed pipe (5) connects with lower reaction cavity (14)，Silica flour feed pipe (6) connects with upper reaction cavity (13) through lower reaction cavity (14) with gas distribution grid (7)，Heat exchanger tube (10) is positioned at reaction cavity (13)，And the two ends of heat exchanger tube (10) connect with oil return cavity (11) and oil-feed cavity (12) respectively，Discharge nozzle (2) sequentially passes through oil return cavity (11) and connects with upper reaction cavity (13) with oil-feed cavity (12)，Described heat exchanger tube (10) is many U-tube.
One the most according to claim 1 has methyl chlorosilane monomer resultant current fluidized bed reactor, it is characterized in that: the mouth of pipe of one end of heat exchanger tube (10) connects through lower clapboard (91) with oil-feed cavity (12), and the axis normal direction of the one end connected with oil-feed cavity (12) is in lower clapboard (91)；Heat exchanger tube (10) the other end of mouth of pipe connects with oil return cavity (11) with upper spacer (9) through lower clapboard (91), and the axis normal direction of one end that an oil return cavity (11) connects is in upper spacer (9).
One the most according to claim 1 has methyl chlorosilane monomer resultant current fluidized bed reactor, it is characterised in that: the axis of discharge nozzle (2) is parallel with the axis of tank body (1).
One the most according to claim 1 has methyl chlorosilane monomer resultant current fluidized bed reactor, it is characterized in that: gas distribution grid (7) has two pieces, two pieces of gas distribution grids (7) are arranged in reaction cavity as line of symmetry, in " V " type with the axis of tank body (1).
One the most according to claim 4 has methyl chlorosilane monomer resultant current fluidized bed reactor, it is characterised in that: chloromethanes feed pipe (5) has two, and two chloromethanes feed pipes (5) are corresponding with two pieces of gas distribution grids (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620142512.6U CN205550236U (en) | 2016-02-25 | 2016-02-25 | Synthetic fluidized bed reactor of methylchlorosilane monomer |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201620142512.6U CN205550236U (en) | 2016-02-25 | 2016-02-25 | Synthetic fluidized bed reactor of methylchlorosilane monomer |
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| CN205550236U true CN205550236U (en) | 2016-09-07 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111655363A (en) * | 2017-12-21 | 2020-09-11 | 环球油品有限责任公司 | Method and apparatus for fluidizing a catalyst bed |
-
2016
- 2016-02-25 CN CN201620142512.6U patent/CN205550236U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111655363A (en) * | 2017-12-21 | 2020-09-11 | 环球油品有限责任公司 | Method and apparatus for fluidizing a catalyst bed |
| CN111655363B (en) * | 2017-12-21 | 2022-07-22 | 环球油品有限责任公司 | Method and apparatus for fluidizing a catalyst bed |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170503 Address after: The Yangtze River Road 443006 Hubei city of Yichang Province in Xiaoting District No. 29 Patentee after: HUBEI XINGRUI CHEMICAL CO., LTD. Address before: 443711 Yichang, Hubei, Xingshan Town, the ancient town of Hunan Road Patentee before: Hubei Xingfa Chemical Group Corp., Ltd. |
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| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 443007 No. 66-2 Ting Ting Road, Ting Ting District, Yichang, Hubei Patentee after: Hubei Xingrui silicon material Co., Ltd. Address before: 443006 No. 29 Changjiang Road, Ting Ting District, Yichang, Hubei Patentee before: HUBEI XINGRUI CHEMICAL CO., LTD. |