CN101618305B - Fluidized bed reactor - Google Patents
Fluidized bed reactor Download PDFInfo
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- CN101618305B CN101618305B CN 200810012191 CN200810012191A CN101618305B CN 101618305 B CN101618305 B CN 101618305B CN 200810012191 CN200810012191 CN 200810012191 CN 200810012191 A CN200810012191 A CN 200810012191A CN 101618305 B CN101618305 B CN 101618305B
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Abstract
The invention discloses an improved fluidized bed reactor, which comprises a reactor shell and a three-phase separator, wherein the reactor shell comprises an expanding section and a straight cylinder section from up to bottom; the three-phase separator is arranged in the expanding section; the diameter of the expanding section is 1.2 to 2 times larger than that of the straight cylinder section, and the ratio of the diameter to the height of the expanding section is 0.3-2.0:1. The expanding section and the three-phase separator of the reactor are organically combined, so that the operational flexibility of the three-phase separator is improved, and the highly-efficient separation of the three-phase separator is ensured. The reactor is mainly used for the chemical reaction of various liquids and gases under a condition of contacting solid particles, and has the advantages of large catalyst reserve, high utilization rate of the reactor, 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 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
Fluidized bed reactor is the gas, liquid, solid three phase fluidized beds; Can handle weight, the inferior feedstock oil of high metal, high asphalt content, have pressure little, uniformity of temperature profile is fallen, can keep whole service cycle the inner catalyst activity constant, 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, 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.
Chinese patent 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 be attached on the catalyst feed opening and the feed opening place has the phenomenon of collaborating to take place easily; Influence the separating effect of three phase separator; And the catalyst easy blocking downstream unit of taking out of is unfavorable for the long-term operation of device.
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.
Fluidized bed reactor provided by the invention comprises 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 successively; Described three phase separator is arranged in the expanding reach; The diameter of expanding reach is 1.2～2 times of direct tube section diameter, and the diameter of expanding reach is 0.3～2.0: 1 with the ratio of height.
The concrete structure of fluidized bed reactor of the present invention is:
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 being respectively applied for derives gas that is separated out and liquid.Described three phase separator is located in the expanding reach, comprises two concentric drums that internal diameter is different: inner core and urceolus.The whole openings in two ends up and down of said inner core and urceolus, the epimere of inner core and urceolus is direct tube section, and the hypomere that is attached thereto is the taper diffuser, and the open upper end of urceolus and lower ending opening are higher than the open upper end and the lower ending opening of inner core respectively.The lower ending opening diameter of inner core (being the opening diameter of diffuser) is less than the internal diameter of reactor expanding reach; The lower ending opening diameter of urceolus (being the opening diameter of diffuser) also should be less than the internal diameter of reactor expanding reach.
(all inner cores of mentioning all refer to the integral body that is made up of inner core direct tube section and diffuser to the inner core of said three phase separator among the application; Mention that urceolus is also like this) constitute 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 diffuser opening of said inner core is the logistics introducing port; The circular opening that the diffuser opening of inner core and reactor expanding reach inwall constitute is the catalyst feed opening of this three phase separator, and isolated solia particle catalyst turns back in the beds along the reactor shell wall herein again.
The concrete dimension scale and the relative position of described 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.
Described expanding reach is the annular enlarged configuration that is arranged at the reactor upper end.The angle (angle originates in axis, ends at the tangent line at intersection point place) that the tangent line at expanding reach and direct tube section intersection point place and reactor axis form is called the widening angle, and this widening angle is an acute angle, is preferably 45 degree to 60 degree.The expanding reach diameter (referring to internal diameter) of said reactor 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.
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 open upper end and lower ending opening of three phase separator urceolus.
The top of said 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.
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 U.S. Pat 3398085 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.
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, like 0.1mm～0.5mm; 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) reactor content outlet and three phase separator and expanding reach structure combine; More increased the operating flexibility of three phase separator; Guarantee the high efficiency 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.
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; 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.Gas and liquid charging stock carry out hydrogenation reaction in reaction zone; Reacted oil gas is carried the part catalyst granules secretly and is got into three phase separator 11 through the enlarged area 8 that expanding reach 4 is surrounded; Carrying out gas-liquid-solid three-phase separates: gas at first is separated; Discharge reactors 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 widening angle that the tangent line at expanding reach and direct tube section intersection point place and reactor axis form is an acute angle, is preferably 45 degree to 60 degree.
Three phase separator 11 is to be made up of jointly together with the inner walls of reactor expanding reach 4 inner core 5, urceolus 6.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=160mm of reactor shell; Height=the 3000mm of reactor shell, 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 widening angle that the tangent line at expanding reach structure and reactor wall intersection point place, bottom and reactor wall radial level line form is 45 degree, and the expanding reach section 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 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 expanding reach 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 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
Claims (6)
1. fluidized bed reactor; Comprise reactor shell and three phase separator; It is characterized in that; Described reactor shell comprises expanding reach and direct tube section from top to bottom successively, is connected through inverted taper type structure between described expanding reach and the direct tube section, and the angle that the hypotenuse of frustum and reactor axis form is an acute angle; Described three phase separator is arranged in the expanding reach, and the diameter of expanding reach is 1.2～2 times of direct tube section diameter, and the diameter of expanding reach is 0.3～2.0: 1 with the ratio of height; 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;
Wherein said three phase separator comprises two concentric drums inner cores and the urceolus that internal diameter is different, the whole openings in two ends up and down of inner core and urceolus, and direct tube section and the diffuser by epimere constitutes respectively; 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; The lower ending opening diameter of said inner core is less than the internal diameter of reactor expanding reach, and the lower ending opening diameter of said urceolus is less than the internal diameter of reactor expanding reach.
2. according to the described fluidized bed reactor of claim 1, it is characterized in that the diameter of said expanding reach is 1.4～1.6 times of direct tube section diameter.
3. according to the described fluidized bed reactor of claim 1, it is characterized in that the conical apex angle of the diffuser of said urceolus is than the conical apex angle of the diffuser of inner core to 20 degree when young.
4. according to the described fluidized bed reactor of claim 1, it is characterized in that the conical apex angle of the diffuser of said urceolus is than little 40～80 degree of conical apex angle of the diffuser of inner core.
5. according to the described fluidized bed reactor of claim 1, it is characterized in that said fluidized bed reactor comprises that also at least one catalyst discharge pipe and at least one catalyst add pipe.
6. according to the described fluidized bed reactor of claim 5, it is characterized in that said catalyst adds the projected position of pipe between the urceolus and inner core of three phase separator.
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| CN 200810012191 CN101618305B (en) | 2008-07-04 | 2008-07-04 | Fluidized bed reactor |
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| CN 200810012191 CN101618305B (en) | 2008-07-04 | 2008-07-04 | Fluidized bed reactor |
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| CN101618305A CN101618305A (en) | 2010-01-06 |
| CN101618305B true CN101618305B (en) | 2012-05-30 |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102463077A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Three-phase boiling bed reactor |
| CN103769010B (en) * | 2012-10-19 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| CN103920430B (en) * | 2014-04-21 | 2016-03-23 | 河南百优福生物能源有限公司 | The fluidized bed reactor of biomass coke tar |
| WO2018136849A1 (en) * | 2017-01-20 | 2018-07-26 | Gas Technology Institute | System and method to synthesize ammonia |
| CN109529731B (en) * | 2018-12-07 | 2021-04-23 | 淮阴工学院 | Organosilicon fluidized bed reactor |
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 |
| CN1214959A (en) * | 1998-09-25 | 1999-04-28 | 清华大学 | Dense-phase circulating fluidized bed reactor for strong exothermal reaction process |
| CN1448212A (en) * | 2002-04-04 | 2003-10-15 | 中国石油化工股份有限公司 | Boiling bed reactor |
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2008
- 2008-07-04 CN CN 200810012191 patent/CN101618305B/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 |
| CN1214959A (en) * | 1998-09-25 | 1999-04-28 | 清华大学 | Dense-phase circulating fluidized bed reactor for strong exothermal reaction process |
| CN1448212A (en) * | 2002-04-04 | 2003-10-15 | 中国石油化工股份有限公司 | Boiling bed reactor |
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