CN103394310B - Fluidized bed reactor and application thereof to production of organosilicone monomer - Google Patents
Fluidized bed reactor and application thereof to production of organosilicone monomer Download PDFInfo
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- CN103394310B CN103394310B CN201310319627.9A CN201310319627A CN103394310B CN 103394310 B CN103394310 B CN 103394310B CN 201310319627 A CN201310319627 A CN 201310319627A CN 103394310 B CN103394310 B CN 103394310B
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Abstract
The invention discloses a fluidized bed reactor which comprises a vertically arranged cylinder body, a heat extracting pipe bundle arranged in the cylinder body and extending along the height direction of the cylinder body, and a material distributor arranged in the cylinder body and positioned below the heat extracting pipe bundle, wherein a material inlet and a catalyst inlet are formed in the bottom of the cylinder body; a product outlet, a heat conduction oil inlet and a heat conduction oil outlet are formed in the upper part of the cylinder body, especially, the heat extracting pipe bundle is of a single-return stroke heat extracting pipe bundle structure formed by a plurality of parallelly-arranged finger-shaped pipes; each finger-shaped pipe forms an independent heat extracting unit and comprises an inner pipe with openings in two ends, and an outer pipe arranged outside the inner pipe; an opening is formed in the upper end of the outer pipe, the lower end of the outer pipe is closed, two ends of the inner pipe are respectively communicated with the outer pipe and the heat conduction oil inlet, and the opening in the upper end of the outer pipe is communicated with the heat conduction oil outlet. Compared with a conventional reactor, the reactor disclosed by the invention has the advantages that the heat transfer efficiency is increased by 3-6 percent, and the catalyst loss is reduced. The fluidized bed reactor is suitable for large-scale production.
Description
Technical field
The present invention relates to a kind of fluidized-bed reactor, particularly one and be suitable for Coal Chemical Industry gasification and synthesis, produce the fluidized-bed reactor of organosilicon, polysilicon monomer.
Background technology
Fluidized-bed reactor is a kind of important chemical reactor being easy to maximization and producing, and is specially adapted to strong exothermic reaction or the endothermic reaction.In order to take out reaction liberated heat in time or in time heating maintains the stability of reaction, fluidized-bed reactor domestic at present researched and analysed two kinds of reaction fluidizing reactors, one is poly-formula reactor, and one is loose formula reactor.Poly-formula reactor bed is stablized, and all arrange a large amount of heat-obtaining tube banks in fluid bed inside at present, heat removing tube is U-tube or thimble tube, is multitube group heat-obtaining structure.In use, conduction oil from interior pipe down to low side, then from low side upwards heat-obtaining, and then to next root dactylethrae, according to the fluid interchange in the dactylethrae of more than a group of the identical type of flow.Take the heat removing tube of this structure, due to the extension along with flowing, the temperature of conduction oil itself, in continuous rising, causes the temperature field in bed uneven, and have impact on reaction efficiency.In addition due to the mode of this kind of heat transfer, side is gas heat convection, and side is convective heat transfer liquid, and from heat-transfer mechanism, what affect heat transfer efficiency is the convection recuperator coefficient of gas phase in bed, thus have impact on the production capacity of respond and separate unit reactor.Again, in a fluidized bed reactor, the reactivity of catalyst is the principal element affecting reaction efficiency.And current fluidized-bed reactor, all there is the problem that catalyst taking-out amount is larger, this not only larger life-span that have impact on reactor exit separator, also have influence on the amplification of separate unit production capacity.If improve separate unit production capacity, certainly will the drag-out of catalyst can be more many, the load of a second-stage separator of reactor outlet can be more large, the solid silicon powder particles extreme hardness of catalyst, load is large can produce serious wearing and tearing, shortens the service life of separator.In addition, if the non-complete reaction of the catalyst reaction in fluid bed and being taken out of, then the primary first-order equation rate of catalyst can be had influence on.
Summary of the invention
Technical problem to be solved by this invention overcomes the deficiencies in the prior art, provides a kind of fluidized-bed reactor of improvement.
For solving above technical problem, the present invention takes following technical scheme:
A kind of fluidized-bed reactor, it comprises the upright cylindrical shell arranged, be arranged on the heat-obtaining tube bank extended in cylindrical shell and along the short transverse of cylindrical shell, to be arranged in cylindrical shell and to be positioned at the material distributor of heat-obtaining tube bank below, the bottom of cylindrical shell offers material inlet and catalyst inlet, top offers products export, heat conductive oil inlet and conduction oil outlet, particularly, the single backhaul heat-obtaining Pipe bundle structure be made up of the many dactylethraes be arranged in parallel is taked in described heat-obtaining tube bank, every root dactylethrae forms independently heat-obtaining unit, dactylethrae comprises the interior pipe of both ends open, be arranged on the outer tube outside described interior pipe, the upper end open of described outer tube, lower end closed, the two ends of interior pipe are connected with outer tube with heat conductive oil inlet respectively, the upper end open of outer tube exports with conduction oil and is connected.
Preferably, described dactylethrae evenly gathers in cylindrical shell.
According to a preferred aspect, the outer surface of described outer tube is evenly arranged multiple fin extending longitudinally along its circumference.Fin provides the expanding surface of gas phase side, and heat transfer temperature difference has increased significantly, and heat-transfer effect improves greatly, realizes the homogenising of bed interior reaction temperature field.
According to a concrete and preferred aspect of the present invention, cylindrical shell is followed successively by feeding section, conversion zone, expanding section and heat conduction fuel tank section from bottom to top, be provided with upper perforated plate in the cylindrical shell of heat conduction fuel tank section correspondence and be positioned at the lower perforated plate below upper perforated plate, the upper end of interior pipe is fixed on upper perforated plate, the upper end of outer tube is fixed on lower perforated plate, heat conductive oil inlet is positioned at the top of upper perforated plate, on the cylindrical shell of conduction oil outlet between upper perforated plate and lower perforated plate; Material inlet and catalyst inlet are positioned on cylindrical shell corresponding to feeding section, and dactylethrae extends to conversion zone from heat conduction fuel tank section.Further, described products export is arranged on cylindrical shell corresponding to expanding section.The cylindrical shell that described conversion zone is corresponding comprises the straight drum part of the conical section that upwards broadens gradually from the feeding section cylindrical shell corresponding with expanding section with being connected this conical section.The outer surface of described outer tube is evenly arranged multiple fin extending longitudinally along its circumference.Usually, the concentrated phase area of the bottom forming reactions of described conversion zone, top is the dilute-phase zone of reaction, preferably, the outer surface being positioned at the part of dilute-phase zone of described outer tube is provided with described fin, and the outer surface being positioned at the part of concentrated phase area of outer tube does not establish described fin.Install fin additional at dilute-phase zone, heat transfer temperature difference has increased significantly, and heat-transfer effect improves greatly, realizes the homogenising of bed interior reaction temperature field.Do not install fin additional in concentrated phase area, the circulating ratio that concentrated phase area is reacted is improved, and substantially increases W-response efficiency.Usually, the height ratio of concentrated phase area, cylindrical shell that dilute-phase zone is corresponding is 1:1 ~ 4.
Further preferably, described fluidized-bed reactor also comprises the separator being arranged on products export place, and this separator comprises the separating plate of multiple V-shape, spaced apart on the direction of the plurality of separating plate at products export and the direction perpendicular to products export.Separator effectively can reduce the carrying amount of fine particle catalyst, and the time that catalyst is stopped inside reactor is long, reduces the loss of catalyst, improves reaction efficiency, also mitigates the load of reactor rear portion three-stage cyclone separator simultaneously.
Further, described fluidized-bed reactor also comprises the catalyst returning charge mouth of the bottom being arranged on cylindrical shell, and this catalyst returning charge mouth is positioned at the bottom of the conical section of described cylindrical shell, for being turned back in reactor by the catalyst taken out of.
Fluidized-bed reactor of the present invention is particularly suitable for Coal Chemical Industry gasification and synthesis, produces organosilicon, polysilicon monomer.For this reason, the invention still further relates to fluidized-bed reactor for Coal Chemical Industry gasification and synthesis, produce purposes, the particularly fluidized-bed reactor application in production organic silicon monomer of organosilicon, polysilicon monomer.
Due to the enforcement of above technical scheme, the present invention compared with prior art tool has the following advantages:
Temperature field is uneven is the key factor affecting reaction efficiency, the defect of existing multitube distance structure itself exacerbates the uneven of temperature field, the single tube journey structure that the present invention adopts thoroughly overcomes this defect, take single tube journey structure that stringing can be made more intensive, there is provided good condition for creating uniform temperature reaction, thus effectively improve reaction efficiency; This structure improves about 2 ~ 3% to the reaction efficiency of equipment, and heat transfer efficiency improves about 3 ~ 6%, and adopts not knowing of single tube journey structure, the reaction zone that has been the equal of refinement, prevents material to occur Teng Yong and channel at fluidized state, keeps the activity of reactor.In addition, owing to being the heat removing tube of single backhaul, the maximization of reactor obtains good development space.
Accompanying drawing explanation
Below in conjunction with accompanying drawing and concrete embodiment, the present invention will be further described in detail;
Fig. 1 is the structural representation according to fluidized-bed reactor of the present invention;
Fig. 2 is the structural representation according to dactylethrae of the present invention;
Fig. 3 be in Fig. 2 A-A direction analyse and observe enlarged diagram;
Fig. 4 is the distribution schematic diagram of dactylethrae in cylindrical shell;
Fig. 5 is the structural representation of separators according to the present invention;
Wherein: 1, cylindrical shell; 10, feeding section; 10a, catalyst inlet; 10b, material inlet; 11, conversion zone; 11a, concentrated phase area; 11b, dilute-phase zone; 110, catalyst returning charge mouth; 12, expanding section; 120, products export; 13, heat conduction fuel tank section; 13a, heat conductive oil inlet; 13b, conduction oil export; 2, heat-obtaining tube bank; 20a, interior pipe; 20b, outer tube; 21, fin; 3, material distributor; 4, upper perforated plate; 5, lower perforated plate; 6, separator; 60, separating plate;
Detailed description of the invention
As shown in Figures 1 to 5, this example provides a kind of fluidized-bed reactor, it comprise upright arrange cylindrical shell 1, be arranged on extends in cylindrical shell 1 and along the short transverse of cylindrical shell 1 heat-obtaining tube bank 2, be arranged in cylindrical shell 1 and be positioned at heat-obtaining and restrain material distributor 3 below 2.Single backhaul heat-obtaining Pipe bundle structure that heat-obtaining tube bank 2 is made up of the many dactylethraes be arranged in parallel 20, every root dactylethrae 20 forms independently heat-obtaining unit.Dactylethrae 20 comprises the interior pipe 20a of both ends open, the outer tube 20b be arranged on outside described interior pipe 20a, the upper end open of outer tube 20b, lower end closed.Cylindrical shell 1 is followed successively by feeding section 10, conversion zone 11, expanding section 12 and heat conduction fuel tank section 13(conversion zone 11, expanding section 12 from bottom to top and forms fluid bed), be provided with upper perforated plate 4 and lower perforated plate 5 in the cylindrical shell 1 of wherein heat conduction fuel tank section 13 correspondence.The upper end of interior pipe 20a is fixed on upper perforated plate 4, and the upper end of outer tube 20b is fixed on lower perforated plate 5.Be provided with heat conductive oil inlet 13a at the top of the cylindrical shell 1 of heat conduction fuel tank section 13 correspondence, the cylindrical shell 1 between upper perforated plate 4 and lower perforated plate 5 be provided with conduction oil outlet 13b.The two ends of interior pipe 20a are connected with outer tube 20b with heat conductive oil inlet 13 respectively, and upper end open and the conduction oil of outer tube 20b export 13b and be connected.Catalyst inlet 10a and material inlet 10b is provided with in the bottom of the cylindrical shell 1 of feeding section 10 correspondence.The bottom of conversion zone 11 is conical section, and top is straight drum part, is provided with catalyst returning charge mouth 110 in the bottom of conical section.The bottom of conversion zone 11 is concentrated phase area 11a of reaction, top is the dilute-phase zone 11b of reaction, the outer surface being positioned at the part of dilute-phase zone 11b of outer tube 20b is provided with the fin 21 extended longitudinally, and the outer surface being positioned at the part of concentrated phase area of outer tube 20b does not establish fin.Install fin 21 additional at dilute-phase zone, heat transfer temperature difference has increased significantly, and heat-transfer effect improves greatly, realizes the homogenising of bed interior reaction temperature field.Do not install fin additional in concentrated phase area, the circulating ratio that concentrated phase area is reacted is improved, and substantially increases W-response efficiency.Be provided with products export 120 on the top of expanding section 12, and products export 120 place is provided with separator 6.Separator 6 comprises the separating plate 60 of multiple V-shape, spaced apart on the plurality of direction of separating plate 60 at products export and the direction perpendicular to products export.Separator 6 effectively can reduce the carrying amount of fine particle catalyst, and the time that catalyst is stopped inside reactor is long, reduces the loss of catalyst, improves reaction efficiency, also mitigates the load of reactor rear portion three-stage cyclone separator simultaneously.
Reactor of the present invention is mainly used in the reaction that this reactor is mainly used between gas and graininess (or powdery) solid.
Operation principle of the present invention is as follows:
The endothermic reaction during beginning due to this reaction, first the conduction oil with certain heat to be passed into heat conduction fuel tank section 13 from heat conductive oil inlet 12a when starting, enter the pipe 20a be positioned on upper perforated plate 4, until the end of interior pipe 20a, outer tube 20b is entered at end, upwards flow between upper perforated plate 4 and lower perforated plate 5 along outer tube 20b, then by flowing to outside liquefied bed from conduction oil outlet 13b.Through this process, the conduction oil carrying heat fully can heat the material in bed, reaches and keeps the reaction temperature in fluid bed.
Reactant feed, through material inlet 10b, enters feeding section 10, is evenly entered bed by material distributor 3, carries out ciculation fluidized, is heated to reaction temperature by conduction oil to it simultaneously.The catalyst of preheating and relevant intermediate, realization response in fluid bed is entered through material distributor 12 and conical section by catalyst inlet 10a, reactant flows from bottom to top in fluid bed inside, and at formation concentrated phase area, the bottom 11a of fluid bed, dilute-phase zone 11b is formed at middle part, through expanding section 12, enter separator 6, export 18 by separator 6 and enter next technological process.
Because course of reaction is exothermic reaction, after reaction starts, the temperature in fluid bed raises rapidly, temperature required in order to maintain reaction, conduction oil in pipe stops heating and starting absorption reaction heat, and heat takes reactor out of by conduction oil, realizes the even of bed interior reaction temperature field.When reactant flows through finned outer tube, fin can enhanced heat exchange, and heat is taken away by conduction oil substantially.When reactant flows through dilute-phase zone, heat is removed, and reactant flow velocity reduces, and is convenient to the sedimentation of an inner catalyst, can improves the utilization rate of catalyst.
Fluidized-bed reactor of the present invention has following features:
(1) inside reactor heat removing tube adopts regular intensive one way heat-obtaining structure, instead of traditional multitube group heat-obtaining mechanism: traditional reactor heat-obtaining tube bank is generally the structures such as multitube distance pipe group structure, U-tube pipe group structure, upper lower header convection bank.The pipe group of multitube distance and U-tube bundle are all upper and lower multiple tube sides in reactor, and the first tube side and the temperature difference in last tube side and bed are comparatively large, are unfavorable for the carrying out of main reaction, and generating accessory substance increases, and causes reaction efficiency low.The form of upper and lower convection bank is better, but header wearing and tearing in lower end are relatively serious, easily cause potential safety hazard; Comparatively large owing to restraining in this structure in addition, lifting exists the problem that cannot overcome, be difficult to realize maximizing.Therefore adopting rational heat-obtaining to restrain is the key improving reaction efficiency and realize equipment enlarging.The intensive one way heat-obtaining structure that the present invention takes overcomes above defect, providing good condition for creating uniform temperature reaction, improve reaction efficiency; This structure improves about 2 ~ 3% to the reaction efficiency of equipment, and heat transfer efficiency improves about 3 ~ 6%.
The present invention installs the longitudinal fin of augmentation of heat transfer additional in the outside of heat removing tube, be distributed on around dactylethrae, provide the expanding surface of gas phase side, this longitudinal fin installs additional at the dilute-phase zone of reaction, heat transfer temperature difference has increased significantly, heat-transfer effect improves greatly, realizes the homogenising of bed interior reaction temperature field.Hinder the raising of reaction cycle multiplying power owing to installing fin additional, help not install fin additional in concentrated phase area, the circulating ratio that concentrated phase area is reacted is improved, and substantially increases W-response efficiency.
For Chemical Manufacture, the feature of particularly polysilicon and organosilicon manufacturing condition and reaction, maintains inside reactor temperature stabilization and ensures the uniform and stable of reaction zone internally-powered field and temperature field, is the emphasis improving reactor activity.In a fluidized bed reactor, reactant enters the bottom of cylindrical shell from material inlet, and through the material distributor of cylinder body bottom, uniform and catalyst mix, carries out gas-solid phase reaction process, and release a large amount of heat; Reactant is in fluidized state when gas-solid phase reaction, and traditional reactor is all that fluidized state easily forms turbulent or vortex phenomenon, and cause reaction zone unstable, temperature field is uneven, and reaction efficiency is declined.
Adopt the layout of the intensive heat removing tube of one way, be equivalent to refinement reaction zone, in reactor shell internal-response district, material is prevented to occur turbulent and channel at fluidized state, keep the activity of reactor, simultaneously fin also can suppress the formation of channel, reaches inside reactor power and the stable object of uniform temperature fields, improves reaction efficiency.
In addition, owing to being the heat removing tube of single backhaul, the maximization of reactor obtains good development space.
(2) reactor heat removing tube installs longitudinal fin additional, fin is multiple, longitudinally arrange at the outer surface of heat removing tube, circumference is uniform, for providing expanding surface in bed, and the heat exchange area of increase, improve the convection recuperator coefficient of gas phase side, enhance the heat convection of gas phase side, the ability taking away heat improves, and also improves reaction efficiency simultaneously.
(3) products export arranges multistage V-type separator, reduce the carrying amount of fine particle catalyst, the time that catalyst is stopped inside reactor is long, reduces catalyst loss, improve reaction efficiency, also mitigate the load of reactor rear portion three-stage cyclone separator simultaneously.
(4) in the amplification section that the envisaged underneath of lower perforated plate is made up of two centrums and a cylindrical shell by, and products export is located at amplification section place, reduces the flow velocity of catalyst, and then reduce drag-out.
application example
In September, 2012, this fluidized-bed reactor used in annual output 80000 tons of organic silicon monomer projects.The reaction raw materials that this project uses is Si powder and CH
3cl, catalyst is copper powder, and reaction equation is as follows:
This reaction needed reactant CH in early stage
3cl etc. heat, conduction oil is carried out preheating by the outer coil pipe of dactylethrae and equipment to reaction bed, reactant carries out pre-fluidisation in bed, and by the temperature and pressure in thermocouple and Pressure gauge monitoring bed, when being preheating to 250 DEG C, catalyst is entered in fluid bed by lower inlet, start reaction, by the time when the temperature in bed starts raise and reach predetermined temperature, system stops heating, the heat-obtaining tube bank be made up of dactylethrae starts heat in absorbent bed, and take system out of by conduction oil in pipe, to maintain reaction temperature suitable in bed.Temperature in on-line monitoring bed, when temperature reaches predetermined temperature (280 DEG C), reactor outlet equipment is started working.Whole equipment runs to now, equipment operational excellence, the single driving cycle reaches 45 days, be far longer than like product in industry (the like product single driving cycle is generally about 30 days), substantially increase the annual driving time, make the cycle average conversion of dimethyl monomer improve 3 percentage points, occupy silicone industry in China industry prostatitis.This fluidized-bed reactor has following characteristics: one is, improves the cycle of operation, thus improves organic silicon monomer annual production, reduces production cost; Two are, the conversion ratio of dimethyl monomer is high; Three are, prevented from caking in bed, decrease the number of times of parking maintenance.
Above to invention has been detailed description, but the invention is not restricted to the embodiments described.The equivalence change that all Spirit Essences according to the present invention are done or modification, all should be encompassed in protection scope of the present invention.
Claims (8)
1. a fluidized-bed reactor, comprise the upright cylindrical shell arranged, be arranged on the heat-obtaining tube bank extended in described cylindrical shell and along the short transverse of cylindrical shell, to be arranged in described cylindrical shell and to be positioned at the material distributor of described heat-obtaining tube bank below, the bottom of described cylindrical shell offers material inlet and catalyst inlet, top offers products export, heat conductive oil inlet and conduction oil outlet, it is characterized in that: the single backhaul heat-obtaining Pipe bundle structure be made up of the many dactylethraes be arranged in parallel is taked in described heat-obtaining tube bank, dactylethrae described in every root forms independently heat-obtaining unit, described dactylethrae comprises the interior pipe of both ends open, be arranged on the outer tube outside described interior pipe, the upper end open of described outer tube, lower end closed, the two ends of described interior pipe are connected with described outer tube with described heat conductive oil inlet respectively, the upper end open of described outer tube exports with described conduction oil and is connected, the outer surface of described outer tube is evenly arranged multiple fin extending longitudinally along its circumference, described fluidized-bed reactor also comprises the separator being arranged on described products export place, this separator comprises the separating plate of multiple V-shape, spaced apart on the described direction of multiple separating plate at described products export and the direction perpendicular to products export.
2. fluidized-bed reactor according to claim 1, is characterized in that: described dactylethrae evenly gathers in described cylindrical shell.
3. fluidized-bed reactor according to claim 1, it is characterized in that: described cylindrical shell is followed successively by feeding section, conversion zone, expanding section and heat conduction fuel tank section from bottom to top, be provided with upper perforated plate in the cylindrical shell of described heat conduction fuel tank section correspondence and be positioned at the lower perforated plate below upper perforated plate, the upper end of described interior pipe is fixed on described upper perforated plate, the upper end of described outer tube is fixed on described lower perforated plate, described heat conductive oil inlet is positioned at the top of described upper perforated plate, on the cylindrical shell of described conduction oil outlet between described upper perforated plate and described lower perforated plate; Described material inlet and catalyst inlet are positioned on cylindrical shell corresponding to described feeding section, and described dactylethrae extends to described conversion zone from described heat conduction fuel tank section.
4. fluidized-bed reactor according to claim 3, is characterized in that: described products export is arranged on cylindrical shell corresponding to described expanding section.
5. fluidized-bed reactor according to claim 3, is characterized in that: the cylindrical shell that described conversion zone is corresponding comprises the straight drum part of the conical section that upwards broadens gradually from the described feeding section cylindrical shell corresponding with described expanding section with being connected this conical section.
6. the fluidized-bed reactor according to claim 3 or 5, it is characterized in that: the outer surface of described outer tube is evenly arranged multiple fin extending longitudinally along its circumference, the concentrated phase area of the bottom forming reactions of described conversion zone, top is the dilute-phase zone of reaction, the outer surface being positioned at the part of described dilute-phase zone of described outer tube is provided with described fin, and the outer surface being positioned at the part of described concentrated phase area of described outer tube does not establish described fin.
7. fluidized-bed reactor according to claim 6, is characterized in that: the height ratio of described concentrated phase area, cylindrical shell that described dilute-phase zone is corresponding is 1:1 ~ 4.
8. the application in organic silicon monomer produced by the fluidized-bed reactor any one of claim 1 to 7 as described in claim.
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| CN201310319627.9A CN103394310B (en) | 2013-07-26 | 2013-07-26 | Fluidized bed reactor and application thereof to production of organosilicone monomer |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1680013A (en) * | 2005-01-26 | 2005-10-12 | 浙江大学 | Reactor of organic silicon fluidized bed with cyclone separator |
| CN203389627U (en) * | 2013-07-26 | 2014-01-15 | 张家港市江南锅炉压力容器有限公司 | Fluidized bed reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1680013A (en) * | 2005-01-26 | 2005-10-12 | 浙江大学 | Reactor of organic silicon fluidized bed with cyclone separator |
| CN203389627U (en) * | 2013-07-26 | 2014-01-15 | 张家港市江南锅炉压力容器有限公司 | Fluidized bed reactor |
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Address after: 215635 No. 139 Gangfeng Road, Yangtze River International Chemical Industrial Park, Zhangjiagang, Suzhou, Jiangsu Patentee after: Jiangsu Jiangguo Intelligent Equipment Co.,Ltd. Address before: 215635 No. 139 Gangfeng Road, Yangtze River International Chemical Industrial Park, Zhangjiagang, Suzhou, Jiangsu Patentee before: Jiangnan Boilers & Pressure Vessels (Zhangjiagang) Co.,Ltd. |