CN101721960A - Fluidized bed reactor - Google Patents
Fluidized bed reactor Download PDFInfo
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- CN101721960A CN101721960A CN 200810228412 CN200810228412A CN101721960A CN 101721960 A CN101721960 A CN 101721960A CN 200810228412 CN200810228412 CN 200810228412 CN 200810228412 A CN200810228412 A CN 200810228412A CN 101721960 A CN101721960 A CN 101721960A
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Abstract
The invention discloses a fluidized bed reactor which comprises a reactor shell and a three-phase separator, the three-phase separator is arranged at the upper part inside the reactor shell and is of a sleeve structure comprising an inner sleeve and an outer sleeve, the upper ends and lower ends of the inner sleeve and the outer sleeve are both of opening structures, the inner sleeve and the outer sleeve are respectively composed of an upper section and a lower section, the upper sections of the inner sleeve and the outer sleeve are in reverse frustum structures, and the lower sections of the inner sleeve and the outer sleeve are in frustum structures. By designing a novel three-phase separating structure, the invention can further improve separating effect, reduce catalyst carrying-out amount, and enhance the operation elasticity of the three-phase separator. The reactor is mainly applicable to chemical reactions between liquid and gas substances of different types and solid particles under contact condition, and has the advantages of large catalyst inventory, high reactor use ratio, simple structure, easy operation and the like.
Description
Technical field
The present invention relates to a kind of gas-liquid-solid three-phase fluidized bed reactor, specifically be used for the liquids and gases material and flow to upward contacting a kind of improved three-phase fluidized bed reactor that carries out chemistry or physical reactions under the situation with solid particle.
Background technology
Heavy oil boiling bed hydrogenation reactor belongs to the gas, liquid, solid three-phase fluid bed reactor, can handle weight, the inferior feedstock oil of high metal, high asphalt content, have pressure fall little, uniformity of temperature profile, can keep the active homogeneous of whole catalyst in reactor service cycle, can on-stream adding fresh catalyst and take out characteristics such as dead catalyst.
Described typical ebullated bed technology among the US Re 25,770, adopt the mode of operation of oil circulating pump, but this process has the following disadvantages in actual applications: the catalyst in reactor reserve is less, and the space reactor utilization rate is low; Oil circulating pump maintaining expense is higher, in case and oil circulating pump work is not normal and damage, will cause catalyst to sink to assembling, the result forces device to be forced to stop work; Fluid product overstand under the on-catalytic hydroconversion condition in the reactor at high temperature is easy to carry out the coking of secondary heat scission reaction and reduces product quality.
CN02109404.7 has introduced a kind of novel fluidized bed reactor, compares with typical fluidized bed reactor, has characteristics such as simple in structure, processing ease and reactor utilization rate height.But owing to use particle diameter is the microspherical catalyst of 0.1～0.2mm, and catalyst is taken reactor out of with reaction oil gas easily.Guarantee the normal stable operation of this kind fluidized bed reactor, key is the internal structure of requirement appropriate design reactor, make it to match with the three phase separator efficiently on top, the catalyst separation that reaction oil gas carries is come out, avoid catalyst from reactor, to take out of causing damage and downstream unit is impacted.The feed opening and the reactor outlet position operation elasticity of the three phase separator that this patent is introduced are little, the catalyst that is separated by three phase separator can stick to catalyst feed opening and feed opening place, gas phase crossfire phenomenon easily takes place, influence the separating effect of three phase separator, and the easy clog downstream device of the catalyst of taking out of is unfavorable for the long-term operation of device.
Simultaneously, in the fluidized bed reactor, material flow is skewness diametrically, and in the central area, flow velocity is higher; In wall zone, limit, flow velocity is lower, even the possibility that flows downward is arranged.Flow velocity difference increases along with the increase of reactor diameter, and this just may cause bubble coalescence, and the formation of air pocket contacts insufficiently between gas phase and the liquid phase, and fluid effect is relatively poor.
Summary of the invention
At the problem that prior art exists, the invention provides a kind of novel bubbling bed reactor that can operation steady in a long-term.This structure of reactor is simple, processing ease, and operating flexibility is big, can satisfy the needs of long period steady running.
Fluidized bed reactor provided by the invention comprises reactor shell and three phase separator, and described three phase separator is arranged on the reactor shell internal upper part, and three phase separator is the tube-in-tube structure that comprises inner core and urceolus.The two ends up and down of described inner core and urceolus are hatch frame, inner core is formed by epimere that links to each other and hypomere with urceolus, the epimere of inner core and urceolus is inverted taper type structure, the hypomere of inner core and urceolus is the taper type structure of just putting, the upper end open of urceolus is higher than the upper end open of inner core, and the lower ending opening of urceolus is higher than the lower ending opening of inner core.
In the fluidized bed reactor of the present invention, three phase separator urceolus epimere frustum face and the horizontal plane angle (angle on the plumb cut, be designated as angle P) be 35～70 degree, three phase separator inner core epimere frustum face and the horizontal plane angle (angle on the plumb cut, be designated as angle Q) be 40～80 degree, preferred P＜Q.
In the fluidized bed reactor of the present invention, described reactor shell can be the straight barrel type reactor, preferably comprises the reactor of expanding reach and direct tube section from top to bottom.When reactor shell comprises expanding reach, described three phase separator is arranged in the expanding reach, expanding reach adopts inversion taper type structure to be connected with direct tube section, and the sleeve lower ending opening that three phase separator inner core and urceolus form is right against the place, inversion taper type inclined-plane of reactor shell expanding reach and direct tube section junction.Inversion frustum structure that expanding reach is connected with direct tube section and direct tube section extended line angle (title widening angle) are acute angle, and the widening angle is preferably 45～60 degree.Expanding reach diameter (referring to internal diameter) is preferably 1.4～1.6 times for 1.2～2 times of direct tube section diameter (referring to internal diameter).The diameter of expanding reach is 0.3～2 with the ratio of height.The blade diameter length ratio scope of direct tube section is between 0.01～0.1.
In the fluidized bed reactor of the present invention, can be in reactor shell under the three phase separator optional position material distributor is set, the quantity of material distributor is specifically determined according to the height of reactor, is generally 1～3 and gets final product.The material distributor is the slab construction that some circular holes are set.
In the fluidized bed reactor of the present invention, the inner core of described three phase separator constitutes the central tube of separator, annulus between inner core and the urceolus is formed the baffling district of three phase separator, and the annulus between urceolus and the reactor wall is the supernatant liquid product collecting region of this three phase separator; The hypomere opening of described inner core is the logistics introducing port, the circular opening that the hypomere opening of inner core and reactor wall constitute is the catalyst feed opening of this three phase separator, and isolated solia particle catalyst turns back in the beds again along the reactor shell wall herein.
The concrete dimension scale and the relative position of described each building block of three phase separator all can be given specifically determining by calculating or simply testing according to specific requirements such as employed catalyst size, reactor for treatment amount, reaction condition and separating effects by this area designer.
Described gas discharge outlet generally is positioned at the reactor head center.Described liquid outlet operated by rotary motion is on the top of reactor expanding reach shell wall, and its position should be between the upper end open and lower ending opening of three phase separator urceolus.
The top of described three phase separator should be provided with certain cushion space usually, and the gaseous product after being separated is discharged reactor in this enrichment and from gas discharge outlet.
Described fluidized bed reactor middle part is provided with the material distributor, the material distributor is the circular distribution flat board that has certain percent opening, the distribution platen area account for reactor cross section long-pending 30%～80%, percent opening is 0.2～0.6, the distribution plate diameter is less than reactor diameter, the fastest because of the central area flow velocity, the opening diameter of general central area is less than the opening diameter away from the central area.The adding of material distributor promotes the distribution of continuous phase and decentralized photo, suppresses the formation and the coalescence of air pocket, improves fluidization quality, and it is more even to make that the fluid radial velocity distributes, and simultaneously strong turbulent flow is disturbed, and improves mass-and heat-transfer efficient.
Compared with prior art, the advantage of fluidized bed reactor of the present invention is:
(1) reactor content outlet and three phase separator and expanding reach structure combine, more increased the operating flexibility of three phase separator, guarantee the efficient separation of three phase separator, significantly reduced the drag-out of catalyst, avoid taking out of in a large number of catalyst catalyst.
(2) increased the expanding reach structure, can suitably reduce the position of product export mouth, reduced internal circulating load, prevented the generation of condensation coking reaction at the lower high-temperature region liquid stream of catalyst concn.
(3) increase the expanding reach structure, can suitably amplify the size of three phase separator feed opening, helped the smooth return catalizer bed of isolated catalyst, can prevent effectively that simultaneously gas from going here and there from feed opening, influenced separating effect.
(4) increased the expanding reach structure, strengthened the operating flexibility and the effect of three phase separator, can load the catalyst of different-grain diameter scope as required flexibly, strengthened adaptability different catalysts.
(5) along with the shortening of supernatant liquid product collecting region to liquid phase outlet distance, flow velocity is accelerated, and has shortened the time of staying of product, makes product leave reactor rapidly, has reduced the possibility of coking.
(6) expansion in catalyst feed opening zone has increased the sedimentation time of catalyst in liquid phase, better promotes isolated solia particle catalyst to turn back in the beds again along the reactor shell wall herein.
(7) be provided with inner member (material distributor) in the middle part of the described fluidized bed reactor, for having the circular quadratic distribution flat board of certain percent opening, the distribution platen area account for reactor cross section long-pending 0.3～0.8, percent opening is 0.2～0.6, diameter is less than reactor diameter, promote the distribution of continuous phase and decentralized photo, suppress the formation and the coalescence of air pocket, improve fluidization quality, it is more even to make that the fluid radial velocity distributes, simultaneously strong turbulent flow is disturbed, improved mass-and heat-transfer efficient.
Description of drawings
Fig. 1 is the structural representation of a kind of embodiment of reactor of the present invention.
Fig. 2 is that the A-A of Fig. 1 reactor band material distributor is to view.
The specific embodiment
Fluidized bed reactor of the present invention is a kind of specifically to be become: be provided with feed(raw material)inlet and gas-liquid distributor at reactor bottom.The reactor middle part is provided with the material distributor, promotes the distribution of continuous phase and decentralized photo, improves fluidization quality, and it is more even to make that the fluid radial velocity distributes, and simultaneously strong turbulent flow is disturbed, and improves mass transfer rate.Be provided with gas vent at reactor expanding reach top, expanding reach top shell wall is provided with liquid outlet, and being respectively applied for derives isolated gas and liquid.
Fluidized bed reactor of the present invention also comprises at least one parts and at least one parts toward described reactor fresh makeup catalyst from described reactor discharge catalyst usually.The parts of described fresh makeup catalyst are arranged at the position of described reactor head usually, and the parts of discharge catalyst are usually located near the described reactor bottom.Catalyst for example is set at the reactor shell top adds pipe, and the catalyst discharge pipe is set in the bottom.The catalyst on reactor top adds pipe, and its projected position is between the urceolus of three phase separator and the sleeve position between the inner core, and the fresh catalyst of Jia Ruing can enter beds downwards along with logistics herein like this.Described catalyst exchange system and using method can be any suitable equipment or method, for example can carry out with reference to free and public technology US3398085 or the described method of US4398852.
For make reaction raw materials in reactor with the catalyst even contact, generally also should gas-liquid distributor be set in the bottom in the described reactor shell, gas-liquid distributor can be selected for use and anyly can make gas or the equally distributed structure of liquid stream, for example can adopt the bubble cap structure.
Employing has in the fluidized bed reactor of this expanding reach structure, can load the catalyst granules of different-grain diameter, as wherein loading the catalyst of wide region particle diameter, as 0.1mm～0.5mm; Also can load the catalyst of close limit particle diameter, as 0.4mm～0.5mm.
For further setting forth concrete feature of the present invention, will be illustrated in conjunction with the accompanying drawings.In conjunction with the accompanying drawings 1, the architectural feature and the operation principle of reactor of the present invention are as follows:
Reaction raw materials mixes the back and enters reactor by charging aperture 1, pass through beds 7 uniformly through gas-liquid distributor 2 backs, catalyst loading amount in the reactor direct tube section 3 is at least 20% of reactor dischargeable capacity, is generally 40%～70%, is preferably 50%～60%.In gas-liquid mutually and flow under the up effect, beds expand into certain height, and its back volume that expands is bigger by 20%～70% than its static volume usually.Material distributor 15 is set in the middle of reactor.Gas and liquid charging stock carry out hydrogenation reaction in reaction zone, reacted oil gas is carried the part catalyst granules secretly and is entered three phase separator 11 by the enlarged area 8 that expanding reach 4 is surrounded, carrying out gas-liquid-solid three-phase separates: gas at first is separated, discharge reactor by gas discharge outlet 10, the catalyst that separates returns reaction zone through feed opening 13, and the supernatant liquid logistics that does not contain catalyst granules is substantially discharged reactors by liquid outlet 12.Discharge reactor for timely fresh makeup catalyst with the catalyst of inactivation, can add pipe 9 by the catalyst on reactor top and in reaction system, replenish fresh catalyst, and the part decaying catalyst can be discharged reaction system by the delivery pipe 14 of reactor lower part.The lower end of expanding reach 4 can be an inverted frustum drum body structure, can certainly be other suitable geometry.
Three phase separator 11 is to be made of inner core 5, urceolus 6.Inner core 5 constitutes the central tube of this three phase separator, annulus between inner core 5 and the urceolus 6 is formed the baffling tube of this three phase separator, annulus between urceolus 6 and reactor expanding reach 4 inner walls is a supernatant liquid product collecting region, above-mentioned central tube lower ending opening is the logistics introducing port, and the circular opening that this opening and reactor expanding reach 4 inner walls constitute is the catalyst feed opening.For baffling tube inner fluid speed is accelerated, improve separating effect, urceolus hypomere conical apex angle generally than inner core hypomere conical apex angle to 20 degree when young, preferably little 40～80 degree.
Further the structure and the result of use of reactor of the present invention are described below in conjunction with specific embodiment.
Embodiment-1
Structure according to boiling bed hydrogenation reactor of the present invention, carried out the medium-sized reactor cold model experiment of three phase separator ebullated bed, cold mould middle-scale device is of a size of: the internal diameter=160mm of reactor shell direct tube section, the height=3000mm of reactor shell direct tube section, housing dischargeable capacity 60L.Three phase separator height=500mm, the separator inner core minimum diameter diameter=135mm of place, diameter=the 190mm of inner core lower taper opening, height=the 35mm of inner core bottom conical section, urceolus smallest diameter portion diameter=160mm, urceolus hypomere opening diameter=285mm, urceolus hypomere height=30mm, the urceolus upper opening is higher than the inner core upper opening, the bottom position of urceolus lower taper opening is higher than the bottom position of inner core lower taper opening, both difference in height=25mm, angle P are 45 degree, and angle Q is 55 degree.The vertical range of separator urceolus upper opening and reactor shell top tangent line is 200mm.The widening angle is 45 degree, and the expanding reach diameter is 300mm.Select for use aviation kerosine as liquid medium, oil inlet quantity is 30～180L/hr; Gas phase is selected nitrogen for use, and air inflow is 0.5～3.6Nm
3/ hr.It is the microspherical catalyst of 0.1～0.2mm that solid phase is selected particle diameter for use, and the catalyst buildup reserve is 50% of a reactor dischargeable capacity.Result of the test sees Table 1.
Find out from result of the test, the catalyst buildup reserve up to 50% situation under, inlet amount changes in quite wide scope, the catalyst drag-out is all extremely low, three-phase fluidization is even, effect is better.
Embodiment-2
On the cold model experiment basis, on the 60L middle-scale device, carried out the test of isolated island reduced crude HDM.Wherein the size of reactor is identical with embodiment 1, experimental condition and the results are shown in Table 2.
Comparative example-1
The basic structure of reactor is with embodiment 1, and difference is that the epimere of interior three phase separator urceolus of reactor and inner core is the cylindrical drum structure.Reaction condition and test raw material be with embodiment 2, wherein concrete experimental condition and the results are shown in Table 2.
The relation of table 160L cold model unit oil inlet quantity, air inflow and catalyst drag-out
1000 hours result of the tests of the table medium-sized hot-die device of 260L
Embodiment-3
Operating condition is identical with embodiment-1, fluidized bed reactor direct tube section middle part is provided with the material distributor, the material distributor is the circular quadratic distribution flat board that has certain percent opening, the distribution platen area account for reactor cross section long-pending 0.6, percent opening is 0.5, diameter is less than reactor diameter, promote the distribution of continuous phase and decentralized photo, the formation and the coalescence that suppress air pocket, improve fluidization quality, it is more even to make that the fluid radial velocity distributes, and simultaneously strong turbulent flow is disturbed, improve mass-and heat-transfer efficient, process is strengthened.As can be seen, mass transfer rate increased when inner member was arranged, and better improved fluidization quality.
Table 3 has or not the inner member comparing result
Claims (10)
1. fluidized bed reactor, comprise reactor shell and three phase separator, described three phase separator is arranged on the reactor shell internal upper part, three phase separator is the tube-in-tube structure that comprises inner core and urceolus, the two ends up and down of the inner core of described three phase separator and urceolus are hatch frame, inner core is formed by epimere that links to each other and hypomere with urceolus, it is characterized in that: the epimere of inner core and urceolus is inverted taper type structure, the hypomere of inner core and urceolus is the taper type structure of just putting, the upper end open of urceolus is higher than the upper end open of inner core, and the lower ending opening of urceolus is higher than the lower ending opening of inner core.
2. according to the described reactor of claim 1, it is characterized in that: three phase separator urceolus epimere frustum face and horizontal plane angle are 35～70 degree, and three phase separator inner core epimere frustum face and horizontal plane angle are 40～80 degree.
3. according to the described reactor of claim 2, it is characterized in that: three phase separator urceolus epimere frustum face and horizontal plane angle are less than inner core epimere frustum face and horizontal plane angle.
4. according to the described reactor of claim 1, it is characterized in that: described reactor shell is the straight barrel type reactor.
5. according to the described reactor of claim 1, it is characterized in that: described reactor shell is for comprising the structure of reactor of expanding reach and direct tube section from top to bottom.
6. according to the described reactor of claim 5, it is characterized in that: reactor shell comprises expanding reach, described three phase separator is arranged in the expanding reach, expanding reach adopts inversion taper type structure to be connected with direct tube section, and the sleeve lower ending opening that three phase separator inner core and urceolus form is right against the place, inversion taper type inclined-plane of reactor shell expanding reach and direct tube section junction.
7. according to the described reactor of claim 6, it is characterized in that: inversion frustum structure that expanding reach is connected with direct tube section and direct tube section extended line angle are acute angle, the expanding reach diameter is 1.2～2 times of direct tube section diameter, the diameter of expanding reach is 0.3～2 with the ratio of height, and the blade diameter length ratio scope of direct tube section is between 0.01～0.1.
8. according to the described reactor of claim 1, it is characterized in that: the optional position is provided with the material distributor under the three phase separator in reactor shell.
9. according to the described reactor of claim 8, it is characterized in that: the material distributor is the circular distribution flat board with suitable percent opening, the distribution platen area account for reactor cross section long-pending 30%～80%, percent opening is 0.2～0.6.
10. according to the described reactor of claim 1, it is characterized in that: the gas discharge outlet of fluidized bed reactor is positioned at reactor head, and liquid outlet is arranged on reactor between the upper end open and lower ending opening of three phase separator urceolus.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102453527A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Catalyst grading suspension bed hydrogenation process |
| CN102453525A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Multi-stage boiling bed hydrogenation process |
| CN102453526A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Multi-section suspension bed hydrogenation process |
| CN103769007A (en) * | 2012-10-19 | 2014-05-07 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| CN104549070B (en) * | 2013-10-12 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| CN105983377A (en) * | 2015-01-30 | 2016-10-05 | 中国科学院上海高等研究院 | Airlift internal loop slurry-bed reactor |
| CN107107018A (en) * | 2014-12-11 | 2017-08-29 | 阿克森斯公司 | Technique and device that the solid particle in the exit for limiting three phase fluidized bed is carried under one's arms |
| CN108607476A (en) * | 2016-12-09 | 2018-10-02 | 中国石油化工股份有限公司 | Fluidized-bed reactor and its application and the method for adsorbing desulfurization for hydrocarbon ils |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4645520A (en) * | 1984-07-20 | 1987-02-24 | Huettlin Herbert | Filter assembly for dust removal from gases, especially in fluidized bed apparatus |
| US5063028A (en) * | 1990-05-18 | 1991-11-05 | Mobil Oil Corporation | Process and apparatus for regeneration of FCC catalyst |
| CN1078492C (en) * | 1998-09-25 | 2002-01-30 | 清华大学 | Dense-phase circulating fluidized bed reactor for strong exothermal reaction process |
| CN1185047C (en) * | 2002-04-04 | 2005-01-19 | 中国石油化工股份有限公司 | Boiling bed reactor |
| CN100512941C (en) * | 2007-01-31 | 2009-07-15 | 华东理工大学 | Slurry bubble columun reactor having internal circulation and external heat-exchanging and the application |
-
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- 2008-10-29 CN CN2008102284125A patent/CN101721960B/en active Active
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| CN102453525B (en) * | 2010-10-15 | 2014-07-23 | 中国石油化工股份有限公司 | Multi-stage boiling bed hydrogenation process |
| CN102453525A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Multi-stage boiling bed hydrogenation process |
| CN102453526A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Multi-section suspension bed hydrogenation process |
| CN102453527B (en) * | 2010-10-15 | 2014-04-02 | 中国石油化工股份有限公司 | Catalyst grading suspension bed hydrogenation process |
| CN102453527A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Catalyst grading suspension bed hydrogenation process |
| CN102453526B (en) * | 2010-10-15 | 2014-05-21 | 中国石油化工股份有限公司 | Multi-section suspension bed hydrogenation process |
| CN103769007A (en) * | 2012-10-19 | 2014-05-07 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| CN103769007B (en) * | 2012-10-19 | 2015-11-25 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| CN104549070B (en) * | 2013-10-12 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| CN107107018A (en) * | 2014-12-11 | 2017-08-29 | 阿克森斯公司 | Technique and device that the solid particle in the exit for limiting three phase fluidized bed is carried under one's arms |
| CN107107018B (en) * | 2014-12-11 | 2021-02-23 | 阿克森斯公司 | Process and apparatus for limiting solid particle entrainment at the outlet of a three-phase fluidized bed |
| CN105983377A (en) * | 2015-01-30 | 2016-10-05 | 中国科学院上海高等研究院 | Airlift internal loop slurry-bed reactor |
| CN105983377B (en) * | 2015-01-30 | 2020-07-28 | 上海睿碳能源科技有限公司 | Air lift type internal circulation slurry bed reactor |
| CN108607476A (en) * | 2016-12-09 | 2018-10-02 | 中国石油化工股份有限公司 | Fluidized-bed reactor and its application and the method for adsorbing desulfurization for hydrocarbon ils |
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