CN205323695U - Fixed fluidized bed reactor - Google Patents
Fixed fluidized bed reactor Download PDFInfo
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- CN205323695U CN205323695U CN201520905448.8U CN201520905448U CN205323695U CN 205323695 U CN205323695 U CN 205323695U CN 201520905448 U CN201520905448 U CN 201520905448U CN 205323695 U CN205323695 U CN 205323695U
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Abstract
The utility model relates to a fixed fluidized bed reactor, whole reactor can divide into by top -down: settling section, conversion zone, obconic's gas -liquid mixture section triplex has distributing plate, the sieve tray that can reciprocate, feeding atomizer and thermo -well in the conversion zone ware, scalable pipe is perpendicular to be connected at the sieve tray center, and through the position of flexible altitude control sieve tray, in the perpendicular insertion reaction ware of thermocouple sleeve pipe, the disconnection in the middle of reaction sequence of broken catalyst is opened the pipe and will be smashed the catalyst with catalyst uninstallation mouth and collect, and catalyst after the reaction on the sieve lets in through the pipe and gaseously blows off the recovery from pipes in a large number because the filter stops in the conversion zone, has guaranteed that all catalyst can both obtain the recovery.
Description
Technical field
This utility model relates to a kind of fixed fluidized-bed reactor for scientific experiment, particularly to a kind of fixed fluidized-bed reactor。
Background technology
Owing to hydrogenation is the usual process of Coal Chemical Industry and petrochemical industry, therefore, in decades, hydrogenation is always up an emphasis of coal chemical technology。But, it it is no matter the exploitation of technical process, or the exploitation of catalyst, or the reactivity worth of reaction mass and catalyst, all it be unable to do without and the coordinating of experimental provision, what comparison in field of hydrogenation was many generally have fixed bed reactors, fluidized-bed reactor, slurry bed system and fixed fluidized bed, wherein fixed fluidized bed taken into account fixing bed and fixed fluidized bed character, and becomes most widely used assay device；Wherein fixed bed reactors are the equipment of this assay device core the most。
The diversification of forms of current domestic conventional fixed fluidized-bed reactor, it can be common that the fixed fluidized-bed reactor of Luoyang petroleum chemical engineering company exploitation, it is provided with a housing；In housing, top is the cylindrical settling section being relatively large in diameter, and bottom is the cylindrical conversion zone that diameter is petite。The top of housing is provided with flange, blind flange, reaction mass delivery line that wherein blind flange is provided with and filter；It is provided with catalyst unloading mouth being positioned on the housing bottom conversion zone。This structure of reactor is simple, easy to operate, carries important function in current experiment。Have the drawback that, for the catalytic amount (5-50g) of trace, it is possible to even fluidizing。But, when catalytic amount is more than 100g, owing to gas-liquid mixed volume is relatively larger, the fluidisation linear velocity on conversion zone top is higher, a large amount of catalyst are entrained on the filter on settling section top by gas, not only make agent sinter, also have a large amount of catalyst to be entrained on the filter on settling section top, thus can affect catalyst burn the repeatability with test data。Affect experimental result, be unfavorable for the carrying out of reaction evaluating。Another conventional fluidized-bed reactor, is: in reactor enclosure body that top is cylindrical settling section, and bottom is obconic conversion zone with the main difference part of above-mentioned reactor。It is not provided with catalyst unloading mouth being positioned on the housing bottom conversion zone；Catalyst is blown out by reactor through unstripped gas entrance pipe after the completion of reaction。Adopt this blowout mode, be difficult to purge totally catalyst completely, also can affect the repeatability of experimental data。
Utility model content
For overcoming the defect of prior art, the purpose of this utility model is in that to provide a kind of fixed fluidized-bed reactor, it is possible to well adapting to current coal chemical technology high temperature, different catalysts type, high gas-liquid ratio, product fecund, catalyst reclaims the requirements such as convenient。
This utility model solves technical problem and adopts the following technical scheme that
A kind of fixed fluidized-bed reactor, wherein, including reactor body, described reactor includes settling section from top to bottom successively, conversion zone and gas-liquid mixed section, described settling section and gas-liquid mixed Duan Juncheng inverted cone-shaped structure, described settling section is positioned at reactor head, described gas-liquid mixed section is positioned at described reactor bottom, the cylindrical structure of described conversion zone, it is positioned at described reactor medium position, described reactor body is integral type structure, described reactor body top is provided with flange and blind flange, realize fixing at reactor body top by bolt between described flange and blind flange；Described blind flange is provided with catalyst addition tube, thermocouple sheath, reaction gas-liquid delivery line and scalable conduit, described scalable conduit is positioned at described blind flange center, described scalable conduit is in being vertically arranged, described catalyst addition tube and thermocouple sheath are positioned at described scalable conduit side, and described reaction gas-liquid delivery line is positioned at described scalable conduit opposite side；It is provided with filter bottom described reaction gas-liquid delivery line；
Being connected to sieve tray bottom described scalable conduit, described sieve tray is inside institute's conversion zone, and described sieve tray realizes moving up and down in conversion zone by the up and down motion of scalable conduit；Described reactor body sidewall is provided with the first conduit, the second conduit and the 3rd conduit, described first conduit and the second conduit set up separately in body both sides, it is and is obliquely installed, described first conduit and the second conduit are with scalable conduit for axis of symmetry, arranging axisymmetricly, described first conduit and the second conduit are positioned at above described sieve tray；Described 3rd conduit is positioned at below sieve tray, and described 3rd conduit is positioned at the first conduit side sidewall；
Described gas-liquid mixed section upper position is provided with by the distribution grid of powdered metallurgical material sintering, and described distribution plate orifices porosity is 20-50um；It is provided with catalyst unloading port bottom described gas-liquid mixed section, described catalyst unloading port is arranged over feed atomizer, material liquid pipeline and admission line it is connected to bottom described feed atomizer, described material liquid pipeline and admission line are all inclined to set, coupled reaction device body bottom described material liquid pipeline and admission line；Being positioned at described catalyst unloading port both sides bottom described material liquid pipeline and admission line, with reactor body center section view for datum level, described material liquid pipeline and the be included angle A of described admission line are 15-30 degree。
Above-mentioned a kind of fixed fluidized-bed reactor, wherein, reactor ratio of height to diameter is 1-8:1, the ratio of height to diameter of gas-liquid mixed section is 1-5:1, the diameter of conversion zone should be the minimum diameter of settling section, is also simultaneously the maximum gauge of gas-liquid mixed section, and the ratio of conversion zone height and this section of average diameter is 3-10:1。
Above-mentioned a kind of fixed fluidized-bed reactor, wherein, the percent opening in described sieve plate hole is 50-90%, and aperture is 0.05-2mm。
Above-mentioned a kind of fixed fluidized-bed reactor, wherein, scalable conduit is inserted perpendicularly into inside reactor along reactor center axis, and its insertion depth is the 50-95% of height for reactor, it is preferable that 75-85%。
Above-mentioned a kind of fixed fluidized-bed reactor, wherein, the ratio of height to diameter of described settling section is 1-10:1；The ratio of height to diameter of gas-liquid mixed section is 1-5:1。
Compared with the prior art, the beneficial effects of the utility model are embodied in:
1. the fixed fluidized-bed reactor that this utility model provides is connected with nebulizer after being respectively provided with by gas-liquid feed nozzle again, the impact on raw material preheating temperature of the inside reactor temperature can be avoided, make this temperature become a variable that can independently control in process of the test。
2. the fixed fluidized-bed reactor that this utility model provides changes traditional feeding manner, Venturi tube, trunnion etc. are had the gas-liquid injector of certain atomizing effect, and widened the raw material scope of application of this reactor, for instance reduced crude, decompression residuum etc. are suitable for this reactor。
3. the fixed fluidized-bed reactor that this utility model provides is provided with fluidized bed gas distribution grid。This distribution grid can make fluidizing gas be uniformly distributed in reactor, the flow regime of catalyst is played the effect of improvement, the turbulent flow of catalyst in reactor can be avoided to a certain extent and turbulent, simultaneously because it can move up and down, the position of sieve tray can be changed according to the amount of loading catalyst, so for the catalyst being applicable to difference filling quality widely of device, it is possible to change the upper-lower position of distribution grid according to the fluidized state of catalyst。Therefore, it is possible to better adapt to comparatively harsh reaction condition。
4. this utility model provides the feed tube of fixed fluidized-bed reactor and air inlet pipe front end are provided with atomizer, material liquid can be made fully to be atomized so that reactant liquor is better mixed with gas, the reaction efficiency of raising reactor。
Accompanying drawing explanation
Fig. 1 is sectional view of the present utility model。
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is described in further detail。
Embodiment
A kind of fixed fluidized-bed reactor, wherein, including reactor body 1, described reactor 1 includes settling section I from top to bottom successively, conversion zone II and gas-liquid mixed section III, described settling section I and gas-liquid mixed section III is all in inverted cone-shaped structure, described settling section I is positioned at reactor 1 top, described gas-liquid mixed section III is positioned at bottom described reactor 1, the described cylindrical structure of conversion zone II, it is positioned at described reactor 1 medium position, described reactor body 1 is integral type structure, described reactor body 1 top is provided with flange 12 and blind flange 13, gasket seal it is provided with between blind flange and flange, realize fixing at reactor body 1 top by bolt 18 between described flange 12 and blind flange 13；Described blind flange 13 is provided with catalyst addition tube 17, thermocouple sheath 7, reaction gas-liquid delivery line 16 and scalable conduit 11, described scalable conduit 11 is positioned at described blind flange 13 center, described scalable conduit 11 is in being vertically arranged, described catalyst addition tube 17 is positioned at described scalable conduit 11 side with thermocouple sheath 7, and described reaction gas-liquid delivery line 16 is positioned at described scalable conduit 11 opposite side；It is provided with filter 15 bottom described reaction gas-liquid delivery line 16；
Being connected to sieve tray 6 bottom described scalable conduit, described sieve tray 6 is for inside institute conversion zone II, and described sieve tray 6 realizes moving up and down in conversion zone II by the up and down motion of scalable conduit 11；Described reactor body 1 sidewall is provided with the first conduit the 9, second conduit 10 and the 3rd conduit 8, described first conduit 9 and the second conduit 10 set up separately in body 1 both sides, it is and is obliquely installed, described first conduit 9 and the second conduit 10 are with scalable conduit 11 for axis of symmetry, arranging axisymmetricly, described first conduit 9 and the second conduit position 10 are above described sieve tray 6；Described 3rd conduit 8 is positioned at below sieve tray 6, and described 3rd conduit 8 is positioned at the first conduit 1 homonymy sidewall；
Described gas-liquid mixed section III upper position is provided with by the distribution grid 4 of powdered metallurgical material sintering, and described distribution grid 4 porosity is 1.5mm；It is provided with catalyst unloading port 14 bottom described gas-liquid mixed section III, described catalyst unloading port 14 is arranged over feed atomizer 5, material liquid pipeline 19 and admission line 20 it is connected to bottom described feed atomizer 5, described material liquid pipeline 19 is all inclined to set with admission line 52, coupled reaction device body 1 bottom described material liquid pipeline 19 and admission line 52；Being positioned at described catalyst unloading port 14 both sides bottom described material liquid pipeline 19 and admission line 20, with reactor body 1 center section view for datum level, described material liquid pipeline 19 is 15-30 degree with described the be included angle A of admission line 20。
Reactor 1 ratio of height to diameter is 7:1, and the ratio of height to diameter of gas-liquid mixed section III is 5:1, and the diameter of conversion zone II should be the minimum diameter of settling section I, is also simultaneously the maximum gauge of gas-liquid mixed section III, and the ratio of conversion zone height and this section of average diameter is 7:1。The percent opening in described sieve plate hole is 70%, and aperture is 1mm。
It is internal that scalable conduit 11 is inserted perpendicularly into reactor 1 along reactor center axis, and its insertion depth is height for reactor 80%。
The ratio of height to diameter of described settling section is 8:1；The ratio of height to diameter of gas-liquid mixed section is 5:1。
Fixed fluidized-bed reactor provided by the utility model is operated as follows:
Below in conjunction with Fig. 1, specific operation process of the present utility model is described。Catalyst through weighing is sent in conversion zone II by catalyst addition tube 17, fluidizing gas is passed in reactor, such as, air, steam, nitrogen etc., send in reactor by admission line 20, first catalyst is fluidized in advance, entered in nebulizer by material liquid pipeline 19 after material liquid preheating and carry out mixed aerosol ejection with the gas in air inlet pipe 20, contact with the catalyst in conversion zone II and carry out catalytic reaction。Reaction generates entrained liquid partially catalyzed agent and is upwardly into settling section I, and catalyst free settling wherein separates。Afterwards, reaction generates gas after filter 15 filters, reaction gas-liquid delivery line 16 discharge reactor。In above-mentioned course of reaction, the gas-liquid that atomization gas-liquid and reaction generate is that the catalyst in conversion zone II fully fluidizes as fluidizing agent, in order to improve the flow regime of catalyst, it is possible to make to form uniform catalyst dense-phase bed in conversion zone by adjusting distribution grid and gas-liquid Feed space velocities；Thermocouple sheath 7 is inserted into thermocouple, is used for accurately measuring the reaction temperature of catalytic reaction。
After catalytic reaction terminates, stopping into material liquid, continue ventilation body, gas is sprayed by atomizer 5, and the catalyst in conversion zone II is stripped, the gas-liquid mixture after reaction in displacement catalyst。After stripping process terminates, stop air inlet, pass into Air for burning coke or oxygen through admission line 20。Air for burning coke or oxygen are sprayed by atomizer 5, enter in conversion zone II, catalyst therein is carried out roasting regeneration。Gas in above-mentioned stripping, burning process, steam stripped gas-liquid mixed gas etc., all discharged reactor by reaction gas-liquid delivery line 16 after filter 15 filters。Burning process opens conduit unloading port after terminating and broken catalyst is drawn off by the 3rd conduit 8, after closing the 3rd conduit 8 and unloading port, passes into a large amount of gas, open the second conduit 10 and reclaim catalyst in the first conduit 9。
In above-mentioned operating process, the operating condition of each step can be chosen routinely according to specific requirement。
Compared with the prior art, the beneficial effects of the utility model are embodied in:
1. the fixed fluidized-bed reactor that this utility model provides is connected with nebulizer after being respectively provided with by gas-liquid feed nozzle again, the impact on raw material preheating temperature of the inside reactor temperature can be avoided, make this temperature become a variable that can independently control in process of the test。
2. the fixed fluidized-bed reactor that this utility model provides changes traditional feeding manner, Venturi tube, trunnion etc. are had the gas-liquid injector of certain atomizing effect, and widened the raw material scope of application of this reactor, for instance reduced crude, decompression residuum etc. are suitable for this reactor。
3. the fixed fluidized-bed reactor that this utility model provides is provided with fluidized bed gas distribution grid。This distribution grid can make fluidizing gas be uniformly distributed in reactor, the flow regime of catalyst is played the effect of improvement, the turbulent flow of catalyst in reactor can be avoided to a certain extent and turbulent, simultaneously because it can move up and down, the position of sieve tray can be changed according to the amount of loading catalyst, so for the catalyst being applicable to difference filling quality widely of device, it is possible to change the upper-lower position of distribution grid according to the fluidized state of catalyst。Therefore, it is possible to better adapt to comparatively harsh reaction condition。
4. this utility model provides the feed tube of fixed fluidized-bed reactor and air inlet pipe front end are provided with atomizer, material liquid can be made fully to be atomized so that reactant liquor is better mixed with gas, the reaction efficiency of raising reactor。
The above; it is only this utility model preferably detailed description of the invention; but protection domain of the present utility model is not limited thereto; any those familiar with the art is in the technical scope that this utility model discloses; the change that can readily occur in or replacement, all should be encompassed in protection domain of the present utility model。Therefore, protection domain of the present utility model should be as the criterion with the protection domain of claims。
Claims (5)
1. a fixed fluidized-bed reactor, it is characterized in that, including reactor body, described reactor includes settling section from top to bottom successively, conversion zone and gas-liquid mixed section, described settling section and gas-liquid mixed Duan Juncheng inverted cone-shaped structure, described settling section is positioned at reactor head, described gas-liquid mixed section is positioned at described reactor bottom, the cylindrical structure of described conversion zone, it is positioned at described reactor medium position, described reactor body is integral type structure, described reactor body top is provided with flange and blind flange, realize fixing at reactor body top by bolt between described flange and blind flange；Described blind flange is provided with catalyst addition tube, thermocouple sheath, reaction gas-liquid delivery line and scalable conduit, described scalable conduit is positioned at described blind flange center, described scalable conduit is in being vertically arranged, described catalyst addition tube and thermocouple sheath are positioned at described scalable conduit side, and described reaction gas-liquid delivery line is positioned at described scalable conduit opposite side；It is provided with filter bottom described reaction gas-liquid delivery line；
Being connected to sieve tray bottom described scalable conduit, described sieve tray is inside institute's conversion zone, and described sieve tray realizes moving up and down in conversion zone by the up and down motion of scalable conduit；Described reactor body sidewall is provided with the first conduit, the second conduit and the 3rd conduit, described first conduit and the second conduit set up separately in body both sides, it is and is obliquely installed, described first conduit and the second conduit are with scalable conduit for axis of symmetry, arranging axisymmetricly, described first conduit and the second conduit are positioned at above described sieve tray；Described 3rd conduit is positioned at below sieve tray, and described 3rd conduit is positioned at the first conduit side sidewall；
Described gas-liquid mixed section upper position is provided with by the distribution grid of powdered metallurgical material sintering, and described distribution plate orifices porosity is 20-50um；It is provided with catalyst unloading port bottom described gas-liquid mixed section, described catalyst unloading port is arranged over feed atomizer, material liquid pipeline and admission line it is connected to bottom described feed atomizer, described material liquid pipeline and admission line are all inclined to set, coupled reaction device body bottom described material liquid pipeline and admission line；Being positioned at described catalyst unloading port both sides bottom described material liquid pipeline and admission line, with reactor body center section view for datum level, described material liquid pipeline and the be included angle A of described admission line are 15-30 degree。
2. a kind of fixed fluidized-bed reactor as claimed in claim 1, it is characterised in that reactor ratio of height to diameter is 1-8:1, and the ratio of height to diameter of gas-liquid mixed section is 1-5:1, and the diameter of conversion zone should be the minimum diameter of settling section, is also the maximum gauge of gas-liquid mixed section simultaneously。
3. a kind of fixed fluidized-bed reactor as claimed in claim 1, it is characterised in that the percent opening of described sieve tray is 50-90%, and aperture is 0.05-2mm。
4. a kind of fixed fluidized-bed reactor as claimed in claim 1, it is characterised in that scalable conduit is inserted perpendicularly into inside reactor along reactor center axis, and its insertion depth is the 50-95% of height for reactor。
5. a kind of fixed fluidized-bed reactor as claimed in claim 1, it is characterised in that the ratio of height to diameter of described settling section is 1-10:1；The ratio of height to diameter of gas-liquid mixed section is 1-5:1。
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520905448.8U CN205323695U (en) | 2015-11-16 | 2015-11-16 | Fixed fluidized bed reactor |
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| CN201520905448.8U CN205323695U (en) | 2015-11-16 | 2015-11-16 | Fixed fluidized bed reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107202320A (en) * | 2017-06-16 | 2017-09-26 | 天津科技大学 | A kind of adjustable fluid bed even distributing wind system and its control system |
| CN109100444A (en) * | 2018-10-11 | 2018-12-28 | 中触媒新材料股份有限公司 | A kind of fixed fluidized bed evaluating apparatus of MTO and method |
| CN111268884A (en) * | 2020-03-31 | 2020-06-12 | 浙江科茂环境科技有限公司 | Oil sludge treatment system and method |
| WO2022040844A1 (en) * | 2020-08-24 | 2022-03-03 | 中国科学院青岛生物能源与过程研究所 | Method and apparatus for extracting clean liquid from slurry reactor |
-
2015
- 2015-11-16 CN CN201520905448.8U patent/CN205323695U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107202320A (en) * | 2017-06-16 | 2017-09-26 | 天津科技大学 | A kind of adjustable fluid bed even distributing wind system and its control system |
| CN107202320B (en) * | 2017-06-16 | 2019-02-26 | 天津科技大学 | A kind of adjustable fluidized bed even distributing wind system and its control system |
| CN109100444A (en) * | 2018-10-11 | 2018-12-28 | 中触媒新材料股份有限公司 | A kind of fixed fluidized bed evaluating apparatus of MTO and method |
| CN111268884A (en) * | 2020-03-31 | 2020-06-12 | 浙江科茂环境科技有限公司 | Oil sludge treatment system and method |
| CN111268884B (en) * | 2020-03-31 | 2024-04-09 | 浙江科茂环境科技有限公司 | Oil sludge treatment system and method |
| WO2022040844A1 (en) * | 2020-08-24 | 2022-03-03 | 中国科学院青岛生物能源与过程研究所 | Method and apparatus for extracting clean liquid from slurry reactor |
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