CN102513038B - Double-layer fluidized bed reactor - Google Patents
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Abstract
The invention discloses a double-layer fluidized bed reactor comprising a reaction section and an expansion section, wherein the reaction section is divided into a double-layer structure including an upper layer and a lower layer by a pored baffle; the lower layer of the reactor is connected with an air distributor; the upper layer of the reactor is connected with the expansion section; and the upper layer and the lower layer are connected by an external overflow pipe with a valve. Both the upper layer and the lower layer of the reactor are respectively provided with catalyst inlets; as long as a pipeline is divided into two branch pipes and the two branch pipes are respectively connected with the two catalyst inlets, the reactor can be in operation; and a valve is arranged on the pipeline. When the inlet on the lower layer of the reactor is enabled, the reactor is in operation in a common single-layer fluidized bed; and when the inlet on the upper layer of the reactor is enabled, the reactor is in operation in the double-layer fluidized bed to adjust the stability of the catalyst bed. The double-layer fluidized bed reactor adopts a more flexible convertible double-layer fluidized bed form.
Description
Technical field
The present invention relates to chemical industry equipment field, relate to a kind of double-layer fluidized bed bioreactor.
Background technology
Fluid bed is to utilize fluid to pass through granular solids bed, and when the resistance that fluid flows through bed is greater than the weight of bed particle, solid particle is in suspended motion state, the bed form that can flow as fluid.The reactor corresponding with it is exactly fluidized-bed reactor.In version, fluidized-bed reactor has circulating fluid bed reactor and fixed fluidized-bed reactor.Recirculating fluidized bed has solid material continuous feed and discharging, is used in the course of reaction of solid phase processing and the easy inactivation of catalyst.Fixed fluidized bed without solid material continuous feed and discharging, in solid particle is long-time, there is not significant change.
Compared with fixed bed reactors, the particle in fluidized-bed reactor is the same with fluid can be freely mobile, has following major advantage: bed has efficient heat transfer property, and bed internal temperature is even, is easy to control, and is specially adapted to strong exothermal reaction system; Can realize successive reaction and the regeneration cycle operation of catalyst, be applicable to catalysqt deactivation and react faster; Can realize the continuous input and output of solid material by separation system.Based on above advantage, fluidized-bed reactor has development faster at petrochemical industry, and particularly there is more ripe application petroleum catalytic cracking aspect.
Due to the characteristic of fluidization technology, the influence factor that fluidized-bed reaction process is subject to is a lot.Physical property, the reaction time distribution, two of catalyst is separated, distribution of gas etc. all has influence on fluid bed stable operation.Can improve by fluid bedreactors, as add macropore distribution grid to 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, expand the range of application of fluidized-bed reactor.Patent CN200610113710.0 utilizes multiple stage fluidized-bed reactor to prepare vinyl chloride, fluid bed without axial height place, gas distribution grid with holes is set, fluid bed is separated into two or more catalyst buildup district, to improve the selective of vinyl chloride.Patent ZL200610114092.1 utilizes multistage fluidized bed reactor to prepare acrylic acid by propylene oxidation, adopts the better gas distributor of distribution effect and active catalyst preferably, strengthens the contact effect of gas-solid, and propylene conversion is better.Patent CN200920234619.3 utilizes two-stage fluidized hydrogen making, by middle air distribution plate, reactor is divided into two-layerly up and down, and outside is connected by overflow pipe.
Above bilayer or multicompartment fluidized bed reactor by adding gas distribution grid to realize bilayer or sandwich construction in reactor, but this structure is to controlling upper strata catalyst inventory, there is defect in rugged catalyst fluidized state, and structure of reactor complexity, can not realize according to response situation the switching of individual layer bilayer or multi-layered reactors to reactor.
Summary of the invention
For the problems of the prior art, the invention provides a kind of double-layer fluidized bed bioreactor, solve the problem that can not realize according to response situation the switching of individual layer bilayer or multi-layered reactors in prior art to reactor.
The present invention is achieved through the following technical solutions:
A kind of double-layer fluidized bed bioreactor, comprise reactor shell, described reactor shell is made up of conversion zone and expanding reach two parts, described conversion zone comprises reactor upper strata and reactor lower floor, and the gas distributor that reactor lower floor is connected by gas access and the lower floor's emulsion zone above gas distributor and lower floor's dilute-phase zone form; Reactor upper strata is made up of the upper strata emulsion zone on macropore distribution grid and macropore distribution grid and upper strata dilute-phase zone; Respectively there are a catalyst inlet in reactor upper strata and reactor lower floor, are second to be connected respectively two catalyst inlets with the 3rd pipeline by the first pipe branch, and second pipe is provided with the second valve, and the 3rd pipeline is provided with the 3rd valve; Upper strata emulsion zone is connected by outside overflow pipe with lower floor emulsion zone, catalyst can by outside overflow pipe realize catalyst from upper strata to lower floor flow, realize the balance of two-layer catalyst inventory, overflow pipe middle part is provided with the first valve and can regulates by convective flux.
The gas vent of described expanding reach connects cyclone separator or filter, separates gas-solid two-phase, and relatively fine particle is separated, and prevents from taking reactor out of with gas phase.
Valve on described the first pipeline, second pipe, the 3rd pipeline and overflow pipe is guiding valve or control valve, can realize control and the adjusting to catalyst stream flux in pipeline by automatic or manual.
Described gas distributor is positioned at reactor bottom, any in bubble cap formula distributor, pipe distributor, multiaperture-type distributor and float-valve type distributor.
The percent opening of described macropore distribution grid is 1%-10%, and the number of openings is 20-50.
Described 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.
On catalyst transport the first pipeline, second pipe, the 3rd pipeline, reactor lower floor and upper strata, pressure transmitter, pressure difference transmitter and thermocouple are housed.
Described reactor inductor material is carbon steel or stainless steel, and inside reactor adds wear resistance lining.
A kind of method of operating of double-layer fluidized bed bioreactor, gas phase enters reactor by gas access, catalyst is passed into from the first pipeline, regulate the valve on second pipe, the 3rd pipeline and overflow pipe, catalyst is the spheroidal catalyst after granulating and forming, the average grain diameter of catalyst is 60-150 μ m, and has certain anti-wear performance, damages with the race that reduces catalyst.The active component of catalyst is Y type or SAPO-34 molecular sieve or loaded catalyst, and catalyst is 0.1-3 times of catalyst general reserve in the internal circulating load of recirculating fluidized bed.
Described gas phase inlet gas can be inert gas, air or through gasification after reactant, and they part mixture, in reactor, gas speed is 0.01-2.0m/s.
Each locations of structures of reactor arranges pressure temperature measuring instrument, and operating temperature is room temperature-600 DEG C, and reaction pressure is 0MPa-0.4MPa.
Catalyst is by second pipe and two entrances of the 3rd pipeline, enter into respectively the upper and lower of fluidized-bed reactor middle part baffle of porous baffle, in the time enabling lower floor's entrance, catalyst enters into lower floor's emulsion zone of reactor, and reactor operates under common single-layer fluidized bed form; In the time enabling upper strata entrance, catalyst flows into upper strata emulsion zone, operates under two-stage fluidized form; In the time that two entrances operate adjusting simultaneously, can play a role beds is stable.
Compare with technology with existing equipment, have the following advantages:
(1) reactor is provided with upper and lower two-layer two catalyst inlets, reactor can operate under common single-layer fluidized bed form, not changing under the condition of structure of reactor, also can under two-stage fluidized form, operate, is 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 within the specific limits gas speed, and can there is not significant change in height of dense phase and pressure drop thereof, improve the regulating power of fluidized bed process.
(3) due to horizontal macropore distributor being set in fluid bed inside, just on axial height, there are two or more emulsion zones.Due to the existence of multiple close phases, for the process that needs Temperature Distribution or CONCENTRATION DISTRIBUTION has been created condition.And owing to having limited the axial backmixing of gas, make flowing closer to laminar flow form of gas, be conducive to improve conversion ratio.
The form design of (4) two entrances is simple, easy to prepare, invests lessly, installs easily, and transformation is convenient.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of the double-layer fluidized bed bioreactor of the present invention.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is further illustrated.
Primary structure of the present invention and operating process are as follows.
(a) catalyst is entered by entrance the first pipeline 1, is divided into two-way pipeline, and, there is the second valve 2V101 on second pipe 5 coupled reaction device upper stratas on second pipe 5, controls pipeline flow and switch; , there is the 3rd valve 3V102 in the 3rd pipeline 6 coupled reaction device lower floors on the 3rd pipeline 6, control pipeline flow and switch.In the time that on the 3rd pipeline 6, the 3rd valve 3V102 opens, catalyst buildup is to gas distributor (9) upper end.
(b) gas phase enters reactor by gas access 8, then after being uniformly distributed by gas distributor 9, blows afloat catalyst, and catalyst is in fluidized state.
(c) in the time that the second valve 2V101 closes, when the 3rd valve 3V102 opens, reactor belongs to single-layer fluidized bed, and reactor only has lower floor to be divided into catalyst emulsion zone 10 and dilute-phase zone 11.The catalyst entering from entrance directly flow to lower floor's emulsion zone position, in the time having partially catalyzed agent on macropore distribution grid 12, can, by regulating the first valve 4V103, control catalyst stream and get back to lower floor's emulsion zone.
(d) in the time that the second valve 2V101 opens, when the 3rd valve 3V102 closes, the catalyst entering from entrance directly flow to the emulsion zone 13 macropore distribution grid, form emulsion zone 13 and the dilute-phase zone 14 on upper strata, by regulating the first valve 4V103 on outside overflow pipe 7 to regulate gas flow, control catalyst stream stable in the reserve of levels.
(e) gas is carried partially catalyzed agent secretly and is entered the expanding reach 15 being connected with conversion zone 17 upper ends, low at expanding reach gas prompt drop, the most of sedimentation of catalyst is returned in conversion zone, gas vent 18 at expanding reach connects cyclone separator 16 or filter, and part relatively fine particle catalyst enters cyclone separator 16 with gas.
(f) cyclone separator separates gas-solid two-phase, and relatively fine particle is separated, and prevents from taking reactor out of with gas phase.
(g) work off one's feeling vent one's spleen phase composition and admittedly containing of analysis reactor.
Embodiment 1
Adopt the two-stage fluidized cold model with two catalyst inlets, reaction unit operates at normal temperatures and pressures, and gas phase adopts air, and catalyst is catalytic cracking catalyst, and mean particle size is 84 μ m.Fluidized-bed reactor diameter 0.7m, expanding reach diameter 1.2m, the diameter of entrance inclined tube, outside overflow pipe is all 80mm.Conversion zone straight tube adds expanding reach height overall 12.5m, and upper and lower two-layer height of dense phase is 3m, and upper dilute phase section height is that 5m(comprises expanding reach), lower dilute phase section height 1.5m.Reactor catalyst reserve 1.5t.Reactor material is carbon steel, wall thickness 6mm.On two pipelines of catalyst inlet and outside overflow pipe be provided with three single-linkage sliding valve controlled pressure balances and catalyst and flow.In expanding reach outlet, efficient three grades of whirlwind are housed, in order to separating catalyst.Gas phase entrance is equipped with gas distributor.Macropore distribution grid is installed at reactor middle part, and the number of openings is 36, and percent opening is 5%.Operating process is as follows.Catalyst is entered by inlet duct from regenerator, has the 3rd valve V102 to open on the 3rd pipeline, and catalyst buildup is to gas distributor upper end.Air enters reactor by gas access, and air mass flow is 1500Nm
3/ h, then after being uniformly distributed by gas distributor, take up catalyst, catalyst is in fluidized state.When the second valve V101 opens, when the 3rd valve V102 closes, the catalyst entering from entrance directly flow to the emulsion zone macropore distribution grid, forms the emulsion zone on upper strata, by regulating the first valve V103 and gas flow, control catalyst stream stable in the reserve of levels.After fluidisation is stable, reactor is in bunk beds mode of operation.Catalyst inventory is measured by pressure difference transmitter, and upper strata catalyst inventory is 7KPa, and lower floor's catalyst inventory is 15KPa, the aperture of by-pass valve control V101, and catalyst circulation amount is at 1.5t/h.Detection reaction device outlet catalyst concn is 150mg/m
3.
Embodiment 2
Adopt the two-stage fluidized cold model with two catalyst inlets, reaction unit operates at normal temperatures and pressures, and gas phase adopts air, and catalyst is methanol-to-olefins catalyst, and mean particle size is 87 μ m.Fluidized-bed reactor diameter 0.7m, expanding reach diameter 1.2m, the diameter of entrance inclined tube, outside overflow pipe is all 80mm.Conversion zone straight tube adds expanding reach height overall 12.5m, and upper and lower two-layer height of dense phase is 3m, and upper dilute phase section height is that 5m(comprises expanding reach), lower dilute phase section height 1.5m.Reactor catalyst reserve 1.3t.Reactor material is carbon steel, wall thickness 6mm.On two pipelines of catalyst inlet and outside overflow pipe be provided with three single-linkage sliding valve controlled pressure balances and catalyst and flow.In expanding reach outlet, efficient three grades of whirlwind are housed, in order to separating catalyst.Gas phase entrance is equipped with gas distributor.Macropore distribution grid is installed at reactor middle part, and the number of openings is 36, and percent opening is 5%.Operating process is as follows.Catalyst is entered by inlet duct from regenerator, has the 3rd valve V102 to open on the 3rd pipeline, and catalyst buildup is to gas distributor upper end.Air enters reactor by gas access, and air mass flow is 1300Nm
3/ h, then after being uniformly distributed by gas distributor, take up catalyst, catalyst is in fluidized state.When the second valve V101 closes, the 3rd valve V102 opens, and reactor belongs to single-layer fluidized bed, and reactor only has lower floor's catalyst emulsion zone.The catalyst entering from entrance directly flow to lower floor's emulsion zone position, in the time having partially catalyzed agent on macropore distribution grid, can, by regulating the first valve V103, control catalyst stream and get back to lower floor's emulsion zone.After fluidisation is stable, reactor is in individual layer bed mode of operation.Catalyst inventory is measured by pressure difference transmitter, and catalyst inventory is 22KPa, controls the aperture of the second valve V101, and catalyst circulation amount is at 1.2t/h.Detection reaction device outlet catalyst concn is 130mg/m
3.
Embodiment 3
Adopt the hot reactor of two-stage fluidized with two catalyst inlets, reaction unit operates at normal temperatures and pressures, and gas phase adopts the postindustrial methyl alcohol of gasification, and catalyst is methanol-to-olefins catalyst, and mean particle size is 87 μ m.Fluidized-bed reactor diameter 0.35m, expanding reach diameter 0.55m, the diameter of entrance inclined tube, outside overflow pipe is all 20mm.Conversion zone straight tube adds expanding reach height overall 2.0m, reactor catalyst reserve 150kg.Reactor material is carbon steel, wall thickness 4mm.On two pipelines of catalyst inlet and outside overflow pipe be provided with three automatic regulating valve controlled pressure balances and catalyst and flow.In expanding reach outlet, filter is housed, in order to separating catalyst.Gas phase entrance is equipped with gas distributor.Macropore distribution grid is installed at reactor middle part, and the number of openings is 36, and percent opening is 10%.Operating process is as follows.Catalyst is entered by inlet duct from regenerator, has the 3rd valve V102 to open on the 3rd pipeline, and catalyst buildup is to gas distributor upper end.Gas enters reactor by gas access, and gas flow is 30Nm
3/ h, then after being uniformly distributed by gas distributor, take up catalyst, catalyst is in fluidized state.When the second valve V101 closes, the 3rd valve V102 opens, and reactor belongs to single-layer fluidized bed, and reactor only has lower floor's catalyst emulsion zone.The catalyst entering from entrance directly flow to lower floor's emulsion zone position, in the time having partially catalyzed agent on macropore distribution grid, can, by regulating the first valve V103, control catalyst stream and get back to lower floor's emulsion zone.After fluidisation is stable, reactor is in individual layer bed mode of operation.Catalyst inventory is measured by pressure difference transmitter, and catalyst inventory is 10KPa, controls the aperture of the second valve V101, and catalyst circulation amount is at 50kg/h.Detection reaction device outlet catalyst concn is 110mg/m
3, methanol conversion 97%.Open the second valve V101, while closing the 3rd valve V102, the catalyst entering from entrance directly flow to the emulsion zone macropore distribution grid, by regulating the first valve V103 and gas flow, controls catalyst stream stable in the reserve of levels.After fluidisation is stable, reactor is in bunk beds mode of operation.Upper strata catalyst inventory is 4KPa, and lower floor's catalyst inventory is 6KPa, controls the aperture of the second valve V101, and catalyst circulation amount is at 50kg/h.Detection reaction device outlet catalyst concn is 110mg/m
3, methanol conversion 98%.
Claims (10)
1. a double-layer fluidized bed bioreactor, comprise reactor shell, it is characterized in that, described reactor shell is made up of conversion zone (17) and expanding reach (15) two parts, described conversion zone (17) comprises reactor upper strata and reactor lower floor, and gas distributor (9) and gas distributor (9) lower floor's emulsion zone (10) and lower floor's dilute-phase zone (11) above that reactor lower floor is connected by gas access (8) form; Reactor upper strata is made up of the upper strata emulsion zone (13) on macropore distribution grid (12) and 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, second pipe (5) and the 3rd pipeline (6) are attached thereto, the first pipeline (1) connects respectively second pipe (5) and the 3rd pipeline (6), second pipe (5) is provided with the second valve (2), and the 3rd pipeline (6) is provided with the 3rd valve (3); Upper strata emulsion zone (13) is connected by outside overflow pipe (7) with lower floor's emulsion zone (10), and the first valve (4) is installed on described outside overflow pipe (7); The gas vent (18) of described expanding reach connects cyclone separator (16) or filter.
2. double-layer fluidized bed bioreactor according to claim 1, it is characterized in that, the valve on described the first pipeline (1), second pipe (5) and the 3rd pipeline (6) and outside overflow pipe (7) is guiding valve or control valve.
3. double-layer fluidized bed bioreactor according to claim 1, is characterized in that, described gas distributor (9) is positioned at reactor bottom, any in bubble cap formula distributor, pipe distributor, multiaperture-type distributor and float-valve type distributor.
4. double-layer fluidized bed bioreactor according to claim 1, is characterized in that, the percent opening of described macropore distribution grid (12) is 1%-10%, and the number of openings is 20-50.
5. double-layer fluidized bed bioreactor according to claim 1, it is characterized in that, described cyclone separator (16) is connected with the top of reactor shell, the outlet of cyclone separator (16) is the outlet of reactor, and cyclone separator (16) adopts one or more levels version.
6. double-layer fluidized bed bioreactor according to claim 1, is characterized in that, on second pipe, the 3rd pipeline, reactor lower floor and upper strata, pressure transmitter, pressure difference transmitter and thermocouple is housed.
7. double-layer fluidized bed bioreactor according to claim 1, is characterized in that, described reactor material is carbon steel or stainless steel, and inside reactor adds wear resistance lining.
8. the method for operating of double-layer fluidized bed bioreactor according to claim 1, it is characterized in that, gas phase enters reactor by gas access (8), catalyst is passed into from the first pipeline (1), regulate the valve on second pipe (5) and the 3rd pipeline (6) and outside overflow pipe (7), catalyst is the spheroidal catalyst after granulating and forming, the average grain diameter of catalyst is 60-150 μ m, and there is certain anti-wear performance, the active component of catalyst is Y type or SAPO-34 molecular sieve or loaded catalyst, catalyst is 0.1-3 times of catalyst general reserve in the internal circulating load of recirculating fluidized bed.
9. the using method of double-layer fluidized bed bioreactor according to claim 8, it is characterized in that, described gas access (8) gas can be inert gas, air or reactant after gasification, and the mixture of their part, in reactor, gas speed is 0.01-2.0m/s.
10. the using method of double-layer fluidized bed bioreactor according to claim 8, is characterized in that, each locations of structures of reactor arranges pressure temperature measuring instrument, and operating temperature is room temperature-600 DEG C, and reaction pressure is 0MPa-0.4MPa.
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| CN103868327A (en) * | 2014-01-01 | 2014-06-18 | 杨胜妹 | Multilayer fluidized bed |
| CN104801242B (en) * | 2015-04-27 | 2016-08-31 | 华中科技大学 | A kind of fluidized-bed reactor and application thereof |
| CN106902712A (en) * | 2017-03-30 | 2017-06-30 | 中国神华能源股份有限公司 | Reactor |
| CN107281981B (en) * | 2017-06-26 | 2021-06-29 | 清华大学 | Inner member, fluidized bed reactor and application method |
| CN109585796A (en) * | 2017-09-29 | 2019-04-05 | 横店集团东磁股份有限公司 | A kind of fluidized bed and its method for coating processing |
| CN111686659A (en) * | 2019-03-13 | 2020-09-22 | 洛阳瑞泽石化工程有限公司 | Combined gas distributor for two-stage fluidized bed reactor |
| CN110893333B (en) * | 2019-12-19 | 2021-11-12 | 靖江神驹容器制造有限公司 | O-chlorobenzonitrile fluidized bed reactor |
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| CN101121635A (en) * | 2007-07-19 | 2008-02-13 | 新疆天业（集团）有限公司 | Method for preparing vinyl chloride by circulating fluidized bed reactor and device thereof |
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| CN202460598U (en) * | 2011-12-31 | 2012-10-03 | 中国天辰工程有限公司 | Double-layer fluidized bed reactor |
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| KR101103594B1 (en) * | 2009-08-07 | 2012-01-10 | 한국에너지기술연구원 | Multi fluidized bed water-gas shift reactor and the hydrogen production method by using syngas from waste gasification |
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| US3905336A (en) * | 1973-09-28 | 1975-09-16 | Foster Wheeler Corp | Apparatus and method for generating heat |
| CN101121635A (en) * | 2007-07-19 | 2008-02-13 | 新疆天业（集团）有限公司 | Method for preparing vinyl chloride by circulating fluidized bed reactor and device thereof |
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