CN101721962B - Three-phase fluidized bed reactor - Google Patents
Three-phase fluidized bed reactor Download PDFInfo
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- CN101721962B CN101721962B CN2008102284144A CN200810228414A CN101721962B CN 101721962 B CN101721962 B CN 101721962B CN 2008102284144 A CN2008102284144 A CN 2008102284144A CN 200810228414 A CN200810228414 A CN 200810228414A CN 101721962 B CN101721962 B CN 101721962B
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Abstract
The invention discloses a three-phase fluidized bed reactor. The three-phase fluidized bed reactor comprises a reactor shell and a three-phase separator, wherein the reactor shell comprises an expansion section and a straight-tube section from top to bottom; the three-phase separator is arranged in the expansion section; the upper part of the straight tube section on the reactor shell is provided with a guide port which has an annular passage structure; the outer side of the guide port is tightly connected with the inner wall of the straight tube section on the reactor shell; and the inner diameter of the guide port is 50 to 95 percent of the inner diameter of the straight tube section on the reactor shell. The fluidized bed reactor organically combines the expansion section, the guide port and the three-phase separator to enhance the operation elasticity of the reactor and ensure efficient separation of the three-phase separator. The reactor is mainly suitable for carrying out a chemical reaction under the condition that different types of liquid and gas substances contact with solid particles, and has the advantages of large catalyst inventory, high reactor utilization rate, simple structure, easy operation and the like.
Description
Technical field
The present invention relates to the solid three-phase fluidized bed reactor of a kind of novel gas-liquid, specifically be used for variety classes liquids and gases material and flow to upward contacting a kind of improved three-phase fluidized bed hydrogenation reactor that carries out chemical reaction 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, adopted the mode of operation of oil circulating pump, but this process is not enough below in practical application, existing: 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 that device is compelled stops 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 and 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; Be prone to take place gas phase crossfire phenomenon; Influence the separating effect of three phase separator, and the catalyst easy blocking downstream unit of taking out of, be 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; The wall zone on the 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 possibly 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
To the problem that prior art exists, the present 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.
Three-phase fluidized bed reactor of the present invention comprises reactor shell and three phase separator; Said reactor shell comprises expanding reach and direct tube section from top to bottom, and three phase separator is arranged in the expanding reach, on the top of reactor shell direct tube section targeting port is set; Targeting port is an annular channel structure; The targeting port outside closely is connected with reactor shell direct tube section inwall, and the targeting port internal diameter is 50%～95% of a reactor shell direct tube section internal diameter, is preferably 60%～85%.
In the fluidized bed reactor of the present invention, the targeting port height accounts for 0.1%～20%, preferred 0.2%～10% of reactor direct tube section height.Targeting port is preferably disposed on the position near expanding reach of reactor direct tube section; Targeting port is an annular channel structure; The best top and bottom of targeting port are the taper diffusion structure; The stage casing is straight cylindrical channel structure (diameter of targeting port refers to the diameter of the straight cylindrical channel part of targeting port), and promptly the longitudinal profile of targeting port is preferably trapezoidal, and the long limit of trapezoidal two parallel edges is near reactor shell.
In the fluidized bed reactor of the present invention, the diameter of reactor shell expanding reach is 1.2～2 times of direct tube section diameter, and the diameter of expanding reach is 0.3:1～2.0:1 with the ratio of height.
In the fluidized bed reactor of the present invention, described three phase separator is located in the expanding reach, and three phase separator is the tube-in-tube structure of two concentric drums comprising that internal diameter is different: inner core and urceolus.The whole openings in two ends up and down of said inner core and urceolus; Inner core and urceolus include epimere and hypomere; The epimere of inner core and urceolus is direct tube section; The hypomere of inner core and urceolus is the taper diffuser, and the open upper end of urceolus is higher than the open upper end 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, be provided with feed(raw material)inlet and gas-liquid distributor at reactor bottom.Be provided with gas vent at reactor expanding reach top, expanding reach top shell wall is provided with liquid outlet, and the position of liquid outlet is between three phase separator urceolus open upper end and the lower ending opening, and being respectively applied for derives gas that is separated out and liquid.
In the fluidized bed reactor of the present invention; (all inner cores of mentioning all refer to the integral body that the taper diffuser by the direct tube section of inner core epimere and hypomere constitutes to the inner core of said three phase separator among the application; Mention that urceolus is also like this) constitute the central tube of three phase 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 a supernatant liquid product collecting region, and the diffuser opening of said inner core is the logistics introducing port.The concrete dimension scale and the relative position of each building block of three phase separator all can be confirmed through calculating perhaps simple test according to specific requirements such as employed catalyst size, reactor for treatment amount, reaction condition and separating effects by this area designer.
In the fluidized bed reactor of the present invention, the reactor shell expanding reach adopts inversion taper type structure to be connected with direct tube section.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 0.3:1～2:1 with the ratio of height.The blade diameter length ratio scope of direct tube section is between 0.01:1～0.1:1.
The top of fluidized bed reactor three phase separator of the present invention 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.
Fluidized bed reactor of the present invention also comprises at least one parts and at least one parts toward said reactor fresh makeup catalyst from said reactor discharge catalyst usually.The parts of said fresh makeup catalyst are arranged at the position of said reactor head usually, and the parts of discharge catalyst are usually located near the said 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 and inner core of three phase separator, and the fresh catalyst that adds like this can get into beds downwards along with the logistics here.Described catalyst exchange system and method for using can be any suitable equipment or method, for example can carry out with reference to free and public technology such as US3398085 or the described method of US4398852.
For make reaction raw materials in reactor with the catalyst even contact, generally also should distributor be set in the bottom in the said reactor shell, 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.Preferably adopt efficient multistage arrangement bubble cap distributor.The bubble cap distributor that is provided with is that percent opening is generally 0.1%～10%.
In the fluidized bed reactor of the present invention, reactor shell direct tube section middle part can be provided with inner member, promotes the distribution of continuous phase and decentralized photo; Air pocket is carried out fragmentation, improve fluidization quality, make fluid radial velocity more even distribution; Simultaneously strong turbulent flow is disturbed, improved mass transfer rate.
Said inner member can be pyramidal structure or cylindrical structure; In reactor, can be provided with 2～8; Horizontal sectional area (total) accounts for 0.1%～20% of reactor level sectional area; Arrangement mode can be arranged above and below, about arrange, also can be equilateral triangle, square and other arrangement modes.Said inner member can lead by convection cell, promotes the distribution of continuous phase and decentralized photo, suppresses the formation and the coalescence of air pocket.
Fluidized bed reactor of the present invention can load the catalyst granules of different-grain diameter, as wherein loading the catalyst of wide region particle diameter, like 0.1mm～1.0mm; Also can load the catalyst of close limit particle diameter, like 0.4mm～0.5mm.
Compared with prior art, the advantage of fluidized bed reactor of the present invention is:
(1) in the reactor shell suitable location targeting port is set; Three phase separator, targeting port and expanding reach structure combine; Improved the operating flexibility of three phase separator; Guaranteed the high efficiency separation of three phase separator, significantly reduced the drag-out of catalyst, avoided 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.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.Can suitably reduce the position of product export mouth, reduce internal circulating load, prevent the generation of condensation coking reaction at the lower high-temperature region liquid stream of catalyst concn.
(4) increased targeting port, made fluid upwards directly get into separator region, strengthened the separating effect of three phase separator, the solid phase after separating is simultaneously gone back to the reactor body district along the targeting port landing again well.
(5) suitable inner member is set, can leads by convection cell, promote the distribution of continuous phase and decentralized photo; Suppress the formation and the coalescence of air pocket, improve fluidization quality, make fluid radial velocity more even distribution; 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.
The specific embodiment
For further setting forth concrete characteristic of the present invention, will combine accompanying drawing explanation.In conjunction with accompanying drawing 1, the architectural feature and the operation principle of reactor of the present invention are following:
Reaction raw materials mixes the back and gets into reactor by charging aperture 1, uniformly through beds 7, in the reactor inner member 16 can be set 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.Gas and liquid charging stock carry out hydrogenation reaction in reaction zone; Reacted oil gas is carried the enlarged area 8 that the part catalyst granules surrounded through expanding reach 4 after through the guide effect of targeting port 15 again secretly and is got into three phase separators 11; Carrying out gas-liquid-solid three-phase separates: gas at first is separated; Discharge reactor through 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 basically discharged reactors through liquid outlet 12.Discharge reactor for timely fresh makeup catalyst with the catalyst of inactivation; Can add pipe 9 through the catalyst on reactor top and in reaction system, replenish fresh catalyst, and can the part decaying catalyst be discharged reaction system through the delivery pipe 14 of reactor lower part.
The lower end of expanding reach 4 can be an inverted uncovered round platform, can certainly be other suitable geometry.The expanding reach angle is an acute angle, is preferably 45 degree to 60 degree.
Three phase separator 11 is to be made up of inner core 5, urceolus 6, brings into play the centrifugation of gas, liquid, solid jointly together with the inner walls of reactor expanding reach 4.The direct tube section of 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; The opening of above-mentioned central tube lower end diffuser is the logistics introducing port, and the circular opening that the opening of this diffuser 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 diffuser conical apex angle is generally than inner core diffuser 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
According to the structure of boiling bed hydrogenation reactor according to the 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 (diameter of reactor direct tube section housing; Down together)=and 160mm, the targeting port internal diameter is 120mm, height 80mm; Height=the 3000mm of reactor shell (wherein reactor shell direct tube section height is 2100mm), housing dischargeable capacity 60L, separator height=500mm; Separator central tube column part diameter=135mm, the base diameter=190mm of inner core lower taper opening, the height=35mm of inner core bottom conical section; Urceolus column part diameter=160mm; Base diameter=the 285mm of its tapering part opening, the height=30mm of tapering part, 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, the vertical range of separator urceolus upper opening and reactor shell top tangent line is 200mm, the vertical range of fluid product tube center distance reactor head tangent line is 120mm.The expanding reach section diameter is 300mm, and the widening angle is 45 degree.Select for use aviation kerosine as liquid medium during operation, 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 is seen 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.Promptly after having increased the expanding reach structure, further improve the separating effect of three phase separator, greatly reduced the drag-out of catalyst.
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, and experimental condition and result see table 2.
Comparative example-1
The basic structure of reactor is with embodiment 1, and difference is not to be provided with in the reactor flow-guiding mouth structure.Reaction condition and test raw material are with embodiment 2, and wherein concrete experimental condition and result see table 2.
The relation of table 1 60L cold model unit oil inlet quantity, air inflow and catalyst drag-out
1000 hours result of the tests of the medium-sized hot-die device of table 2 60L
Claims (10)
1. three-phase fluidized bed reactor; Comprise reactor shell and three phase separator, it is characterized in that: said reactor shell comprises expanding reach and direct tube section from top to bottom, and three phase separator is arranged in the expanding reach; Top at the reactor shell direct tube section is provided with targeting port; Targeting port is an annular channel structure, and the targeting port outside closely is connected with reactor shell direct tube section inwall, and the targeting port internal diameter is 50%～95% of a reactor shell direct tube section internal diameter.
2. according to the described reactor of claim 1, it is characterized in that: described targeting port internal diameter is 60%～85% of a reactor shell direct tube section internal diameter.
3. according to the described reactor of claim 1, it is characterized in that: the targeting port height accounts for 0.1%～20% of reactor direct tube section height.
4. according to the described reactor of claim 1, it is characterized in that: the targeting port height accounts for 0.2%～10% of reactor direct tube section height.
5. according to the described reactor of claim 1, it is characterized in that: the diameter of reactor shell expanding reach is 1.2～2 times of direct tube section diameter, and the diameter of expanding reach is 0.3: 1～2.0: 1 with the ratio of height.
6. according to the described reactor of claim 1; It is characterized in that: three phase separator is the tube-in-tube structure of two concentric drums comprising that internal diameter is different: inner core and urceolus, and the whole openings in two ends up and down of said inner core and urceolus, inner core and urceolus include epimere and hypomere; The epimere of inner core and urceolus is direct tube section; The hypomere of inner core and urceolus is the taper diffuser, and the open upper end of urceolus is higher than the open upper end of inner core, and the lower ending opening of urceolus is higher than the lower ending opening of inner core.
7. according to the described reactor of claim 1; It is characterized in that: be provided with feed(raw material)inlet and gas-liquid distributor at reactor bottom; Be provided with gas vent at reactor expanding reach top; Expanding reach top shell wall is provided with liquid outlet, and the position of liquid outlet is between three phase separator urceolus open upper end and the lower ending opening.
8. according to the described reactor of claim 1, it is characterized in that: the reactor shell expanding reach adopts inversion taper type structure to be connected with direct tube section, and inversion frustum that expanding reach is connected with direct tube section and direct tube section extended line angle are acute angle.
9. according to the described reactor of claim 1; It is characterized in that: fluidized bed reactor comprises at least one parts from said reactor discharge catalyst; With at least one parts toward said reactor fresh makeup catalyst; The parts of said fresh makeup catalyst are arranged at said reactor head, and the parts of discharge catalyst are positioned at said reactor bottom.
10. according to the described reactor of claim 1; It is characterized in that: inner member is set at reactor shell direct tube section middle part; Inner member is pyramidal structure or cylindrical structure, in reactor, is provided with 2～8, and horizontal sectional area accounts for 0.1%～20% of reactor level sectional area.
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| CN101721962B true CN101721962B (en) | 2012-04-04 |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102451652B (en) * | 2010-10-15 | 2014-01-01 | 中国石油化工股份有限公司 | Boiling-bed reactor |
| CN102451650A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Suspension bed hydrogenation reactor |
| CN102728285B (en) * | 2012-07-10 | 2014-05-28 | 四川大学 | System and device for three-phase complete mixed flow carbon dioxide ammoniation mineralization reaction |
| 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 |
| CN104560157B (en) * | 2013-10-22 | 2016-06-22 | 中国石油化工股份有限公司 | A kind of residual hydrogenation method |
| CN104560158B (en) * | 2013-10-22 | 2016-07-20 | 中国石油化工股份有限公司 | A kind of residual hydrogenation method |
| CN108554330B (en) * | 2018-05-25 | 2024-04-02 | 北京中科诚毅科技发展有限公司 | Internal flow guiding process of hydrogenation reactor and design method and application thereof |
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| 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 |
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2008
- 2008-10-29 CN CN2008102284144A patent/CN101721962B/en active Active
Patent Citations (4)
| 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 |
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