CN1425494A - Large fluidized bed reactor for wide sieving fluidized particles - Google Patents
Large fluidized bed reactor for wide sieving fluidized particles Download PDFInfo
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- CN1425494A CN1425494A CN 03100605 CN03100605A CN1425494A CN 1425494 A CN1425494 A CN 1425494A CN 03100605 CN03100605 CN 03100605 CN 03100605 A CN03100605 A CN 03100605A CN 1425494 A CN1425494 A CN 1425494A
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- bed
- bed reactor
- fluidized
- reactor
- fluidized bed
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- 239000002245 particle Substances 0.000 title claims description 22
- 238000007873 sieving Methods 0.000 title 1
- 238000009826 distribution Methods 0.000 claims description 9
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 13
- 239000007787 solid Substances 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- 238000005243 fluidization Methods 0.000 description 8
- 239000003921 oil Substances 0.000 description 7
- 230000003321 amplification Effects 0.000 description 6
- 238000003199 nucleic acid amplification method Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000178 monomer Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 4
- YGZSVWMBUCGDCV-UHFFFAOYSA-N chloro(methyl)silane Chemical compound C[SiH2]Cl YGZSVWMBUCGDCV-UHFFFAOYSA-N 0.000 description 4
- 235000013312 flour Nutrition 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000000377 silicon dioxide Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 235000013339 cereals Nutrition 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 239000011863 silicon-based powder Substances 0.000 description 2
- 239000011343 solid material Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 238000013316 zoning Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010574 gas phase reaction Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to chemical equipment technology. The large fluidized bed reactor consists of main bed, conic bed, internal finger-shaped tube heat-exchange member and gad distributor, and features the inner cone structure in the conic bed and sectional introduction of heat-exchange medium to the heat exchange pipe. Using the fluidized bed reactor of the present invention can regulate effectively the fluidizing cross-section area, improve fluidizing quality and realize industrial application easily.
Description
Technical field
The present invention relates to a kind of large-scale fluidized bed reactor that is applicable to the wide-size distribution fluidized particles, being particularly useful for solid particle is the gas-solid reaction system of reaction raw materials, belongs to technical field of chemical.
Background technology
In chemical process, in order to reach the purpose of effective heat and mass, a lot of production carried out in fluidized-bed reactor usually.Wherein relate to a lot of solid material particle diameters again and distribute very wide or solid particle is the system of reaction raw materials, such as the ore roast in coal dust gasification, the metallurgical industry etc.For this class system, because particle diameter gradually changes in the wide distribution character of the solid grain size of itself or the course of reaction, require reactor to have higher operating flexibility, when the particle diameter that can guarantee solid particle changed within the specific limits, system still had good fluidizing performance.Therefore, design the large-scale fluidized-bed reactor of such class, have very high industrial applicibility.Below with the synthetic feature that this class system is described of producing of organic silicon monomer.
Organosilicon material is a kind of macromolecular material of excellent performance, is obtained by the hydrolysis of methylchlorosilane monomer usually.Methylchlorosilane adopts the Rochow direct method synthetic, and this reaction is strong exothermal reaction (280kJ/mol); Solid material in the synthetic reaction is a silicon powder particle, and its Surface Renewal is to the reaction important influence.Based on above 2 points, the industrial production of all adopting fluidized-bed reactor to realize the methylchlorosilane monomer.Silicon powder particle itself just has very wide particle diameter and distributes, and in process of production, silica flour is constantly consumed, and particle diameter changes, and constantly replenishes fresh silica flour to reactor simultaneously.In addition, the average grain diameter of raw material silica flour and particle size range also can frequent the changing because of the actual conditions of silica flour production.Therefore, it is wide that the principal character of solid particle is exactly the particle diameter distribution in fluidized-bed reactor, contains more fine powder.For the fluidisation system of such complexity, the engineering of fluidized-bed reactor is amplified the technological core that has just become the methylchlorosilane monomer to realize economic scale production.
Except organic silicon monomer production, other similar system also exists engineering to amplify the problem of difficulty.Traditional way all is only to add conical bed under main bed, as shown in Figure 1.This fluid bed is made up of main bed 4, dactylethrae heat exchange inner member 5, conical bed 7, circle distributor 11.Though this fluid bed can improve fluidization quality to a certain extent, if but the fluidized-bed reactor scale further enlarges, structural parameters such as the semi-cone angle of conical bed, fluid bed ratio of height to diameter then can not satisfy the requirement of chemical reaction process, and existing fluidized-bed structure has limited the large-scale engineering of this class reactor process is amplified.Therefore, be necessary to design a kind of rational structure more, realize the amplification of this class reactor, especially the amplification of large-scale fluidized bed reactor.
Summary of the invention
The purpose of this invention is to provide a kind of large-scale fluidized bed reactor that is applicable to wide-size distribution particle diameter distributed granule, be particularly useful for the system that solid particle is a reaction raw materials.This reactor can effectively be adjusted fluidizing cross-section area according to actual conditions, improves fluidization quality, is easy to realize industrial amplification requirement.
Large-scale fluidized bed reactor of the present invention is made up of main bed, conical bed, dactylethrae heat exchange inner member, gas distributor, it is characterized in that introducing the inner cone structure in conical bed, and the heat transferring medium subregion enters heat exchanger tube.After in conical bed, introducing the inner cone structure, under the certain situation of throughput, can effectively change fluidizing cross-section area, with regard to relative bigger, be beneficial to the initial fluidisation of particle, thereby improve fluidization quality in the gas speed of bed bottom.Another advantage of introducing the inner cone structure is exactly the amplification design that helps such reactor.If the simple conical bed structure that in design, only adds, if the scale of fluidized-bed reactor further enlarges so, for half inclination angle that guarantees conical bed within the specific limits, the height of conical bed part will inevitably be very big, bring difficulty so just for the appropriate design and the processing of whole reactor, even can not satisfy the chemical technology condition.By introducing the inner cone structure, just the height of conical bed can well be controlled within the specific limits.Simultaneously, be added with double-deck end socket in the bed bottom, so just can the more effective appearance of avoiding the fluidisation dead band.Can reach optimized mode of operation by above design and the concrete parameter of local adjustment.
The design form that described heat transferring medium adopts subregion to add, desalted water or heat exchange oil enter the dactylethrae heat exchange component from reactor head by several different subregions, and (heat exchange oil still flows out with liquid state) discharged in vaporization after heat exchange.Number of partitions can be decided to be 1～8 according to the fluid bed diameter, and the discharge of steam or heat exchange oil concentrates on an outlet.By such zoning design, heat transferring medium evenly can be distributed, also made things convenient for the amplification design of reactor simultaneously.
Owing in conical bed, introduced the inner cone structure,, improved fluidization quality so fluidized-bed reactor of the present invention can effectively be adjusted fluidizing cross-section area.Simultaneously because the design form that heat transferring medium takes subregion to add is easy to realize industrial amplification requirement.
Description of drawings
Fig. 1 is for being usually used in the fluidized-bed reactor structural representation of solid with wide range particle at present.
Fig. 2 is a large-scale fluidized bed reactor structural representation of the present invention.
Fig. 3 is a dactylethrae heat exchange inner member structural representation of the present invention.
Fig. 4 is a dactylethrae heat exchange inner member subregion distribution design schematic diagram of the present invention.
The specific embodiment
Describe concrete structure of the present invention and mode of operation in detail below in conjunction with accompanying drawing:
Large-scale fluidized bed reactor Fig. 2 of the present invention is made up of main bed 4, conical bed 7, annular gas distributor 10 and dactylethrae heat exchange inner member 5.Main bed diameter D can be between 2.0～6.0m, height H
1Can be between 8～15m; The height H of conical bed
2Can be between 1.8～4.5m, semi-cone angle α can be between 7～13 °; Introduce inner cone structure 8 in conical bed, its semi-cone angle β can be between 5～13 °.Below all can select as the case may be.By conical bed and inner cone structure cross-sectional area is carried out dual adjustment, on suitable conical bed height, gas speed is effectively regulated, the problem of having avoided simple employing conical bed can't large-scale engineering to amplify.In the reactor bottom design double-seal head 11 is arranged, further avoid the appearance in fluidisation dead band.
Described gas distributor is 2～5 circle tubular type annular gas distributors, and the distributor nozzle evenly distributes on endless tube.The concrete parameter of distributor comprises percent opening, perforate number etc., designs in conjunction with the parameter of leading bed, conical bed and inner cone structure, uses variable mass stream principle and is optimized calculating, guarantees that fluidized-bed reactor is in optimized mode of operation.Reacting gas enters from gas reactor inlet 10, effectively distributes by the gas distributor that goes in ring then, and the solid reaction raw material adds reactor continuously from particle inlet 9, reacts by bringing into after gas fluidized in the main bed.The gas-phase reaction product is discharged from reactor product outlet 3.
Described fluidized-bed reactor is used to shift out reaction heat at the inner dactylethrae heat exchange components that many vertical arrangements are installed of main bed.The introducing of dactylethrae heat exchange component can be so that this fluidized-bed reactor be specially adapted to the reaction system of those strong heat releases.The distribution mode of dactylethrae adopts positive triangle capable or square uniform.Simultaneously, reasonably the dactylethrae distribution mode can effectively play the effect of bubble crushing, raising fluidizing performance.Heat exchange can be adopted the mode of desalted water vaporization, perhaps adopts the mode of conduction oil heat exchange.Can adjust the number of heat exchange component according to actual exchange capability of heat.Fig. 3 is the dactylethrae structural representation.Heat transferring medium (desalted water or heat exchange oil) 13 enters and manages 14 in the heat exchanger tube from entering the mouth, and the coolant outlet 17 from interior pipe flows out then, flows into heat exchanger tube outer tube 16 and carries out heat exchange.Through after the heat exchange, steam or heat exchange oil are discharged from heat exchanger tube outlet 15.Dactylethrae heat exchange inner member is uniform according to triangle or square, and the top is fixed by welding on the ring flange of reactor head, and the bottom is adopted the 3-8 layer to support flower stand 6 and located diametrically.
In the present invention, the form of zoning design is taked in the adding of heat transferring medium, as shown in Figure 4.Be decided to be 1～8 (being exemplified as three among the figure: I, II and III district) according to the bed diameter.Heat transferring medium enters each subregion from the inlet 1 of reactor head, and then enters dactylethrae heat exchange inner member.Steam after the heat exchange or heat exchange oil are finally discharged from the outlet 2 of reactor.
Claims (4)
1. a large-scale fluidized bed reactor that is applicable to the wide-size distribution fluidized particles is made up of main bed, conical bed, dactylethrae heat exchange inner member, gas distributor, it is characterized in that introducing the inner cone structure in conical bed, and the heat transferring medium subregion enters heat exchanger tube.
2. according to the described large-scale fluidized bed reactor of claim 1, it is characterized in that: the height of main bed is between 8～15m, and diameter is between 2～6m.
3. according to the described large-scale fluidized bed reactor of claim 1, it is characterized in that: the height of conical bed between 1.8～4.5m, semi-cone angle α=7～13 °.
4. according to the described large-scale fluidized bed reactor of claim 1, it is characterized in that: the inner cone structure of introducing in the conical bed, its semi-cone angle β=5～13 °.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03100605 CN1194805C (en) | 2003-01-17 | 2003-01-17 | Large fluidized bed reactor for wide sieving fluidized particles |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03100605 CN1194805C (en) | 2003-01-17 | 2003-01-17 | Large fluidized bed reactor for wide sieving fluidized particles |
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| Publication Number | Publication Date |
|---|---|
| CN1425494A true CN1425494A (en) | 2003-06-25 |
| CN1194805C CN1194805C (en) | 2005-03-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03100605 Expired - Fee Related CN1194805C (en) | 2003-01-17 | 2003-01-17 | Large fluidized bed reactor for wide sieving fluidized particles |
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| Country | Link |
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| CN (1) | CN1194805C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101708449A (en) * | 2005-06-03 | 2010-05-19 | 塞巴斯蒂安·崔玛 | Fluidized bed reaction tower |
| CN102031132A (en) * | 2010-12-30 | 2011-04-27 | 东北林业大学 | Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass |
-
2003
- 2003-01-17 CN CN 03100605 patent/CN1194805C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101708449A (en) * | 2005-06-03 | 2010-05-19 | 塞巴斯蒂安·崔玛 | Fluidized bed reaction tower |
| CN102031132A (en) * | 2010-12-30 | 2011-04-27 | 东北林业大学 | Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass |
| CN102031132B (en) * | 2010-12-30 | 2013-08-21 | 东北林业大学 | Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1194805C (en) | 2005-03-30 |
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