CN202460598U - Double-layer fluidized bed reactor - Google Patents
Double-layer fluidized bed reactor Download PDFInfo
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- CN202460598U CN202460598U CN 201120573116 CN201120573116U CN202460598U CN 202460598 U CN202460598 U CN 202460598U CN 201120573116 CN201120573116 CN 201120573116 CN 201120573116 U CN201120573116 U CN 201120573116U CN 202460598 U CN202460598 U CN 202460598U
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Abstract
The utility model discloses a double-layer fluidized bed reactor. The reactor comprises a reaction section and an expanding section, wherein the reaction section is divided into an upper layer and a lower layer by a perforated baffle; the lower layer of the reaction section is connected with a gas distributor; the upper layer of the reaction section is connected with the expanding section; the upper layer and the lower layer are connected through an external overflow pipe with a valve; a catalyst inlet is formed on each of the upper layer and the lower layer of the reaction section; one pipeline is branched into two pipelines connected with the two inlets respectively; and valves are arranged on the pipelines. When the inlet of the lower layer is opened, the reactor is operated in the common single-layer fluidized bed form; and when the inlet of the upper layer is opened, the reactor is operated in a double-layer fluidized bed form, an effect of adjusting the stability of a catalyst bed is achieved, and the double-layer fluidized bed form is flexible and switchable.
Description
Technical field
The utility model relates to the chemical industry equipment field, relates to a kind of double-layer fluidized bed bioreactor.
Background technology
Fluid bed is to utilize fluid to pass through the granular solids bed, and the resistance that fluid flows through bed is during greater than the weight of bed particle, and solid particle is in the suspended motion state, the bed form that can flow as fluid.The reactor corresponding with it is exactly fluidized-bed reactor.Fluidized-bed reactor has circulating fluid bed reactor and fixed fluidized-bed reactor on the version.Recirculating fluidized bed has solid material continuous feed and discharging, is used in the course of reaction that solid phase processing and catalyst are prone to inactivation.Significant change does not take place in solid particle is long-time in fixed fluidized bed no solid material continuous feed and discharging.
Compare with fixed bed reactors, the particle in the fluidized-bed reactor is the same with fluid freely to flow, and following major advantage is arranged: bed has heat transfer property efficiently, and the bed internal temperature is even, is easy to control, is specially adapted to the strong exothermal reaction system; Can realize the successive reaction and the regeneration cycle operation of catalyst, be applicable to that catalysqt deactivation reacts faster; Can realize the continuous input and output of solid material through separation system.Based on above advantage, fluidized-bed reactor has development, particularly petroleum catalytic cracking aspect faster that the application of maturation is arranged at petrochemical industry.
Because the characteristic of fluidization technology, the influence factor that the fluidized-bed reaction process receives is a lot.The physical property of catalyst, reaction time distribution, two are separated, distribution of gas etc. all has influence on fluid bed stable operation.Can improve through fluid bedreactors; As add the macropore distribution grid and form bilayer or multi-layered reactors; The gas distributor of design distribution better effects and if efficiently cyclone separator etc. improve the reactivity worth of fluid bed, enlarge the range of application of fluidized-bed reactor.Patent CN200610113710.0 utilizes multiple stage fluidized-bed reactor to prepare vinyl chloride, fluid bed without the axial height place gas distribution grid with holes is set, fluid bed is separated into two or more catalyst buildup district, to improve the selectivity of vinyl chloride.Patent ZL200610114092.1 utilizes multistage fluidized bed reactor to prepare acrylic acid by propylene oxidation, adopts better gas distributor of distribution effect and activity catalyst preferably, strengthens the contact effect of gas-solid, and propylene conversion is better.Patent CN200920234619.3 utilizes two-stage fluidized to produce hydrogen, and two-layer about through middle air distribution plate reactor being divided into, the outside is connected by overflow pipe.
Above bilayer or multicompartment fluidized bed reactor are realized bilayer or sandwich construction through in reactor, adding gas distribution grid; But this structure is to control upper strata catalyst inventory; There is defective in the rugged catalyst fluidized state; And structure of reactor is complicated, can not realize the switching of individual layer bilayer or multi-layered reactors according to response situation to reactor.
The utility model content
To the problems of the prior art, the utility model provides a kind of double-layer fluidized bed bioreactor, solves the problem that can not realize the switching of individual layer bilayer or multi-layered reactors in the prior art according to response situation to reactor.
The utility model is realized through following technical scheme:
A kind of double-layer fluidized bed bioreactor; Comprise reactor shell; Said reactor shell is made up of conversion zone and expanding reach two parts; Said conversion zone comprises reactor upper strata and reactor lower floor, and gas distributor that reactor lower floor is connected by the gas access and the lower floor's emulsion zone above the gas distributor and lower floor's dilute-phase zone are formed; The reactor upper strata is made up of upper strata emulsion zone on macropore distribution grid and the macropore distribution grid and upper strata dilute-phase zone; Respectively there are a catalyst inlet in reactor upper strata and reactor lower floor; Upper strata inlet duct and lower floor's inlet duct are attached thereto; The inlet total pipeline connects upper strata inlet duct and lower floor's inlet duct respectively, and the upper strata inlet duct is provided with the upper strata valve, and lower floor's inlet duct is provided with lower floor's valve; The upper strata emulsion zone is connected through outside overflow pipe with the lower floor emulsion zone, on the said outside overflow pipe control valve is installed; The gas vent of said expanding reach connects cyclone separator or filter.
The gas vent of said expanding reach connects cyclone separator or filter, separates gas-solid two phases, will separate than fine grained, prevents to take reactor out of with gas phase.
Said upper strata valve, lower floor's valve and control valve are guiding valve or control valve, can realize control and adjusting to catalyst stream flux in the pipeline through automatic or manual.
Said gas distributor is positioned at reactor bottom, any in bubble cap formula distributor, pipe distributor, multiaperture-type distributor and the float-valve type distributor.
The percent opening of said macropore distribution grid is 1%-10%, and perforate quantity is 20-50.
Said cyclone separator is connected with the top of reactor shell, and the outlet of cyclone separator is the outlet of reactor, and cyclone separator adopts one or more levels version.
Each all is equipped with pressure transmitter, pressure difference transmitter and thermocouple on inlet total pipeline, reactor lower floor and upper strata.
Said reactor inductor material is carbon steel or stainless steel, and adds wear resistance lining.
A kind of method of operating of double-layer fluidized bed bioreactor; Gas phase gets into reactor through the gas access, and catalyst is fed from pipeline, regulates the valve on pipeline and the overflow pipe; Catalyst is the spheroidal catalyst behind the granulating and forming; The average grain diameter of catalyst is 60-150 μ m, and has certain anti-wear performance, decreases with the race that reduces catalyst.The activity of such catalysts composition is Y type or SAPO-34 molecular sieve or loaded catalyst, catalyst the internal circulating load of recirculating fluidized bed be the catalyst general reserve 0.1-3 doubly.
Said gas phase inlet can be inert gases such as nitrogen, air or warp gasification afterreaction thing etc., and the mixture of their part, and gas speed is 0.01-2.0m/s in the reactor.
Each locations of structures of reactor is provided with the pressure temperature measuring instrument, and operating temperature is a room temperature-600 ℃, and reaction pressure is 0MPa-0.4MPa.
Catalyst enters into the upper and lower of fluidized-bed reactor middle part baffle plate with holes respectively through two entrances, and when launching lower floor's inlet, catalyst enters into lower floor's emulsion zone of reactor, and reactor operates under the common single-layer fluidized bed form; When launching the upper strata inlet, catalyst flows into the upper strata emulsion zone, promptly operates under the two-stage fluidized form; When two inlets simultaneously during adjusted, can play effect to beds is stable.
With existing equipment and compared with techniques, have the following advantages:
(1) reactor is provided with two-layer two catalyst inlets up and down; Reactor can be operated under common single-layer fluidized bed form; Under the condition that does not change structure of reactor, also can under the two-stage fluidized form, operate, be a kind of fluidized bed process mode that can flexible conversion.
(2) two catalyst inlets and outside overflow pipe have improved the operational stability of fluid bed, strengthen the poised state of two-layer catalyst.Change gas speed within the specific limits, and significant change can not take place in close phase height and pressure drop thereof, improve the regulating power of fluidized bed process.
(3) owing to, just on axial height, have two or more emulsion zones at the horizontal macropore distributor of fluid bed set inside.Because the existence of a plurality of close phases is for the process that needs Temperature Distribution or CONCENTRATION DISTRIBUTION has been created condition.And owing to limited the axial backmixing of gas, make gas flow more approach the laminar flow form, help improving conversion ratio.
The form simplicity of design of (4) two inlets, preparation is convenient, invest lessly, installs easily, transforms conveniently.
Description of drawings
Fig. 1 is the schematic flow sheet of the double-layer fluidized bed bioreactor of the utility model.
The specific embodiment
Below in conjunction with specific embodiment the utility model is further described.
The primary structure and the operating process of the utility model are following.
(a) catalyst is got into by inlet duct 1, is divided into the two-way pipeline, and there is upper strata valve 2V101 on inlet duct 5 coupled reaction device upper stratas in upper strata on the upper strata inlet duct 5, control pipeline flow and switch; There is the valve 3V102 of lower floor in lower floor's inlet duct 6 coupled reaction device lower floors on lower floor's inlet duct 6, control pipeline flow and switch.When valve 3V102 opened on lower floor's inlet duct 6, catalyst buildup was to gas distributor (9) upper end.
(b) gas phase gets into reactor through gas access 8, after evenly distributing through gas distributor 9, blows afloat catalyst again, and catalyst is in fluidized state.
(c) when upper strata valve 2V101 closes, when the valve 3V102 of lower floor opened, reactor belonged to single-layer fluidized bed, and reactor has only lower floor to be divided into catalyst emulsion zone 10 and dilute-phase zone 11.The catalyst that gets into from inlet directly flow to lower floor emulsion zone position, when on the macropore distribution grid 12 the part catalyst being arranged, can pass through control valve 4V103, and the control catalyst stream is got back to lower floor's emulsion zone.
(d) when upper strata valve 2V101 opens; When the valve 3V102 of lower floor closes; The catalyst that gets into from inlet directly flow to the emulsion zone 13 on the macropore distribution grid; Form the emulsion zone 13 and dilute-phase zone 14 on upper strata, through the control valve 4V103 that regulates on the outside overflow pipe 7 gas flow is regulated, the control catalyst stream is stable in the reserve of levels.
(e) gas is carried the part catalyst secretly and is got into the expanding reach 15 that is connected with conversion zone 17 upper ends; Low at expanding reach gas prompt drop; The most of sedimentation of catalyst is returned in the conversion zone; Gas vent 18 at expanding reach connects cyclone separator 16 or filter, and part gets into cyclone separator 16 than finely grained catalyst with gas.
(f) cyclone separator separates gas-solid two phases, will separate than fine grained, prevents to take reactor out of with gas phase.
(g) work off one's feeling vent one's spleen phase composition and containing admittedly of analysis reactor.
Embodiment 1
Employing has the two-stage fluidized cold conditions model of two catalyst inlets, and reaction unit is operated at normal temperatures and pressures, and gas phase adopts air, and catalyst is a catalytic cracking catalyst, and mean particle size is 84 μ m.The about 0.7m of fluidized-bed reactor diameter, expanding reach diameter 1.2m, the diameter of inlet inclined tube, outside overflow pipe all is 80mm.The straight tube of conversion zone adds expanding reach height overall 12.5m, and two-layer up and down close phase highly is 3m, and last dilute phase section highly is 5m (comprising expanding reach), following dilute phase section height 1.5m.Reactor catalyst reserve 1.5t.Reactor material is a carbon steel, wall thickness 6mm.On two pipelines of catalyst inlet, being provided with three single-linkage sliding valve controlled pressure balances and catalyst with outside overflow pipe flows.In the expanding reach outlet efficient three grades of whirlwind are housed, in order to separating catalyst.The gas phase inlet is equipped with gas distributor.The macropore distribution grid is installed at the reactor middle part, and perforate quantity is 36, and percent opening is 5%.Operating process is following.Catalyst is got into by inlet duct from regenerator, has valve V102 to open on the pipeline, and catalyst buildup is to the gas distributor upper end.Air gets into reactor through the gas access, and air mass flow is 1500 Nm
3/ h after evenly distributing through gas distributor, takes up catalyst again, and catalyst is in fluidized state.When V101 opens, when V102 closes, directly flow to the emulsion zone on the macropore distribution grid from the catalyst that gets into that enters the mouth, form the emulsion zone on upper strata, through control valve V103 and gas flow, the control catalyst stream is stable in the reserve of levels.After fluidisation was stable, reactor was in the bunk beds mode of operation.Catalyst inventory is measured through pressure difference transmitter, and the upper strata catalyst inventory is 7KPa, and lower floor's catalyst inventory is 15 KPa, the aperture of by-pass valve control V101, and the catalyst circulation amount is at 1.5t/h.Detection reaction device outlet catalyst concn is 150mg/ m
3
Employing has the two-stage fluidized cold conditions model of two catalyst inlets, and reaction unit is operated at normal temperatures and pressures, and gas phase adopts air, and catalyst is the methanol-to-olefins catalyst, and mean particle size is 87 μ m.The about 0.7m of fluidized-bed reactor diameter, expanding reach diameter 1.2m, the diameter of inlet inclined tube, outside overflow pipe all is 80mm.The straight tube of conversion zone adds expanding reach height overall 12.5m, and two-layer up and down close phase highly is 3m, and last dilute phase section highly is 5m (comprising expanding reach), following dilute phase section height 1.5m.Reactor catalyst reserve 1.3t.Reactor material is a carbon steel, wall thickness 6mm.On two pipelines of catalyst inlet, being provided with three single-linkage sliding valve controlled pressure balances and catalyst with outside overflow pipe flows.In the expanding reach outlet efficient three grades of whirlwind are housed, in order to separating catalyst.The gas phase inlet is equipped with gas distributor.The macropore distribution grid is installed at the reactor middle part, and perforate quantity is 36, and percent opening is 5%.Operating process is following.Catalyst is got into by inlet duct from regenerator, has valve V102 to open on the pipeline, and catalyst buildup is to the gas distributor upper end.Air gets into reactor through the gas access, and air mass flow is 1300 Nm
3/ h after evenly distributing through gas distributor, takes up catalyst again, and catalyst is in fluidized state.When V101 closed, V102 opened, and reactor belongs to single-layer fluidized bed, and reactor has only lower floor's catalyst emulsion zone.The catalyst that gets into from inlet directly flow to lower floor emulsion zone position, when on the macropore distribution grid part catalyst being arranged, can pass through control valve V103, and the control catalyst stream is got back to lower floor's emulsion zone.After fluidisation was stable, reactor was in individual layer bed mode of operation.Catalyst inventory is measured through pressure difference transmitter, and catalyst inventory is 22KPa, the aperture of by-pass valve control V101, and the catalyst circulation amount is at 1.2t/h.Detection reaction device outlet catalyst concn is 130mg/ m
3
Embodiment 3
Employing has the hot reactor of two-stage fluidized of two catalyst inlets, and reaction unit is operated at normal temperatures and pressures, and gas phase adopts the postindustrial methyl alcohol of gasification, and catalyst is the methanol-to-olefins catalyst, and mean particle size is 87 μ m.The about 0.35m of fluidized-bed reactor diameter, expanding reach diameter 0.55m, the diameter of inlet inclined tube, outside overflow pipe all is 20mm.The straight tube of conversion zone adds expanding reach height overall 2.0m, reactor catalyst reserve 150kg.Reactor material is a carbon steel, wall thickness 4mm.On two pipelines of catalyst inlet, being provided with three automatic regulating valve controlled pressure balances and catalyst with outside overflow pipe flows.In the expanding reach outlet filter is housed, in order to separating catalyst.The gas phase inlet is equipped with gas distributor.The macropore distribution grid is installed at the reactor middle part, and perforate quantity is 36, and percent opening is 10%.Operating process is following.Catalyst is got into by inlet duct from regenerator, has valve V102 to open on the pipeline, and catalyst buildup is to the gas distributor upper end.Gas gets into reactor through the gas access, and gas flow is 30 Nm
3/ h after evenly distributing through gas distributor, takes up catalyst again, and catalyst is in fluidized state.When V101 closed, V102 opened, and reactor belongs to single-layer fluidized bed, and reactor has only lower floor's catalyst emulsion zone.The catalyst that gets into from inlet directly flow to lower floor emulsion zone position, when on the macropore distribution grid part catalyst being arranged, can pass through control valve V103, and the control catalyst stream is got back to lower floor's emulsion zone.After fluidisation was stable, reactor was in individual layer bed mode of operation.Catalyst inventory is measured through pressure difference transmitter, and catalyst inventory is 10KPa, the aperture of by-pass valve control V101, and the catalyst circulation amount is at 50kg/h.Detection reaction device outlet catalyst concn is 110mg/ m
3, methanol conversion 97%.Open V101, when closing V102, the catalyst that gets into from inlet directly flow to the emulsion zone on the macropore distribution grid, and through control valve V103 and gas flow, the control catalyst stream is stable in the reserve of levels.After fluidisation was stable, reactor was in the bunk beds mode of operation.The upper strata catalyst inventory is 4KPa, and lower floor's catalyst inventory is 6 KPa, the aperture of by-pass valve control V101, and the catalyst circulation amount is at 50kg/h.Detection reaction device outlet catalyst concn is 110mg/ m
3, methanol conversion 98%.
Claims (7)
1. double-layer fluidized bed bioreactor; Comprise reactor shell; It is characterized in that; Said reactor shell is made up of conversion zone (17) and expanding reach (15) two parts, and said conversion zone (17) comprises reactor upper strata and reactor lower floor, and reactor lower floor is made up of gas distributor (9) and top lower floor's emulsion zone (10) and the lower floor's dilute-phase zone (11) of gas distributor (9) that gas access (8) connect; The reactor upper strata is made up of upper strata emulsion zone (13) on macropore distribution grid (12) and the macropore distribution grid (12) and upper strata dilute-phase zone (14); Respectively there are a catalyst inlet in reactor upper strata and reactor lower floor; Upper strata inlet duct (5) and lower floor's inlet duct (6) are attached thereto; Inlet total pipeline (1) connects upper strata inlet duct (5) and lower floor's inlet duct (6) respectively; Upper strata inlet duct (5) is provided with upper strata valve (2), and lower floor's inlet duct (6) is provided with lower floor's valve (3); Upper strata emulsion zone (13) is connected through outside overflow pipe (7) with lower floor's emulsion zone (10), and control valve (4) is installed on the said outside overflow pipe (7); The gas vent of said expanding reach (18) connects cyclone separator (16) or filter.
2. according to the said double-layer fluidized bed bioreactor of claim 1, it is characterized in that said upper strata valve (2), lower floor's valve (3) and control valve (4) are guiding valve or control valve.
3. according to the said double-layer fluidized bed bioreactor of claim 1, it is characterized in that said gas distributor (9) is positioned at reactor bottom, any in bubble cap formula distributor, pipe distributor, multiaperture-type distributor and the float-valve type distributor.
4. according to the said double-layer fluidized bed bioreactor of claim 1, it is characterized in that the percent opening of said macropore distribution grid (12) is 1%-10%, perforate quantity is 20-50.
5. according to the said double-layer fluidized bed bioreactor of claim 1; It is characterized in that; Said cyclone separator (16) is connected with the top of reactor shell, and the outlet of cyclone separator (16) is the outlet of reactor, and cyclone separator (16) adopts one or more levels version.
6. according to the said double-layer fluidized bed bioreactor of claim 1, it is characterized in that each all is equipped with pressure transmitter, pressure difference transmitter and thermocouple respectively on inlet total pipeline, reactor lower floor and upper strata.
7. according to the said double-layer fluidized bed bioreactor of claim 1, it is characterized in that said reactor inductor material is carbon steel or stainless steel, and add wear resistance lining.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201120573116 CN202460598U (en) | 2011-12-31 | 2011-12-31 | Double-layer fluidized bed reactor |
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| CN 201120573116 CN202460598U (en) | 2011-12-31 | 2011-12-31 | Double-layer fluidized bed reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102513038A (en) * | 2011-12-31 | 2012-06-27 | 中国天辰工程有限公司 | Double-layer fluidized bed reactor |
| WO2020078414A1 (en) * | 2018-10-17 | 2020-04-23 | 中国石油化工股份有限公司 | Di-trapezoidal component, fluidization device, and hydrogenation method for nitro compound |
| RU2802870C2 (en) * | 2018-10-17 | 2023-09-05 | Чайна Петролиум & Кемикал Корпорейшн | Element in form of two trapeziums, unit with fluidized bed, and method for carrying out reaction of nitro compound hydrogenation |
-
2011
- 2011-12-31 CN CN 201120573116 patent/CN202460598U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102513038A (en) * | 2011-12-31 | 2012-06-27 | 中国天辰工程有限公司 | Double-layer fluidized bed reactor |
| CN102513038B (en) * | 2011-12-31 | 2014-09-24 | 中国天辰工程有限公司 | Double-layer fluidized bed reactor |
| WO2020078414A1 (en) * | 2018-10-17 | 2020-04-23 | 中国石油化工股份有限公司 | Di-trapezoidal component, fluidization device, and hydrogenation method for nitro compound |
| RU2802870C2 (en) * | 2018-10-17 | 2023-09-05 | Чайна Петролиум & Кемикал Корпорейшн | Element in form of two trapeziums, unit with fluidized bed, and method for carrying out reaction of nitro compound hydrogenation |
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Granted publication date: 20121003 Effective date of abandoning: 20140924 |
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| RGAV | Abandon patent right to avoid regrant |