CN103657540A - Gas-liquid distributor for fluidized bed reactor - Google Patents
Gas-liquid distributor for fluidized bed reactor Download PDFInfo
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- CN103657540A CN103657540A CN201210344233.4A CN201210344233A CN103657540A CN 103657540 A CN103657540 A CN 103657540A CN 201210344233 A CN201210344233 A CN 201210344233A CN 103657540 A CN103657540 A CN 103657540A
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Abstract
The invention provides a gas-liquid distributor for a three-phase fluidized bed reactor. The gas-liquid distributor is mainly composed of a central pipe, a bell cap, connection legs and a distribution plate, wherein the central pipe is divided into upper and lower sections; a material inlet of the central pipe is formed in the end part of the lower section and a material outlet of the central pipe is formed in the end part of the upper section; a pipe wall which is close to the material inlet is provided with a vertical seam which is communicated with the material inlet; a pore plate mixer is arranged on the lower section of the central pipe; three vertical strip-shaped holes are formed in the upper section of the central pipe; the three connection legs which are arrayed vertically are arranged along the peripheral direction of the inner wall of the bell cap; each connection leg comprises a long arm and a short arm and forms an angle rule shape; the short arms of the connection legs are embedded in the vertical strip-shaped holes and can move up and down along the vertical strip-shaped holes; the bell cap is connected with the upper section of the central pipe by the three connection legs and covers the material outlet; the periphery of the bottom of the bell cap can be fitted with the distribution plate. According to the gas-liquid distributor for the three-phase fluidized bed reactor, gas can be crushed into continuous micro air bubbles in liquid and is uniformly distributed; the problem of reverse flowing and blocking of materials can be effectively solved or relieved.
Description
Technical field
The present invention relates to reactor inner member field, relate in particular to a kind of gas-liquid distributor for three-phase fluidized bed reactor.
Background technology
Gas-liquid-solid three-phase fluidized bed reactor is widely applied in industrial reaction process, for the very large course of reaction of reaction heat, use three-phase fluidized bed reactor can effectively remove reaction heat, the isothermal operation of realization response device, guarantees the normal operation of reactor.In three-phase fluidized bed reactor, gas-liquid distributor is to guarantee gas equally distributed important inner member in bed, directly affects even running and the reaction efficiency of reactor.
At present both at home and abroad in publication, ebullated bed gas-liquid distributor divides and has two large classes according to functional characteristic: the type that dams (US4874583 for example, 200910012453.5 and 201020636320.3 etc.) and the non-type that dams (for example 200910012498.2), existing document shows the bubble cap formula gas-liquid distributor US4874583 with reverse stopping ball that has substantially adopted U.S. Texaco company on current commercial plant, Fu Yan institute of China Petrochemical Industry utilize catalyst buildup angle feature development non-section of flow-type gas-liquid distributor, can prevent a large amount of adverse currents of catalyst, but the adverse current that cannot avoid dividing plate top logistics completely, very easily stop up, generally should not adopt.
When in fluidized bed reactor, liquid phase gas holdup is identical, bubble diameter is less, and gas liquid film is long-pending larger, and mass transfer rate is faster, is conducive to improve reaction effect and utilization rate.The rate of climb of air pocket in liquid phase, higher than minute bubbles, also can cause the time of staying of gas in reactor to shorten simultaneously, or can say that air pocket does not have and liquid phase contact mass transfer portion gas in reactor, forms short circuit to a certain extent.These all can affect the mass transfer effect between reactant, and reduce the conversion ratio of reaction.Therefore how academia's major concern gas-liquid distributor makes distribution of gas even present stage, produces more less bubbles, should possess the logistics generation adverse current preventing above reactor dividing plate with catalyst simultaneously.Gas-solid-liquid three phase materials effectively evenly mixing, mass-transfer efficiency and operating flexibility in reactor are the important performance indexes of fluidized bed reactor, and therefore, the gas-liquid distributor of excellent performance is the crucial inner member of fluidized bed reactor.
The patent US4874583 of U.S. Texaco company has introduced a kind of gas-liquid distributor for fluidized bed reactor, is bubble cap distributor, mainly parts such as bubble cap, tedge, reverse stopping ball and spools, consists of.The bottom of bubble cap cylindrical shell is provided with bar seam, and tedge top and spool middle part are provided with fluid issuing, and spool bottom is provided with valve seat.The bottom of tedge is with the gas-liquid premixed structure of air inlet duct (bar seam), is provided with the orifice mixer for gas-liquid mixed in tedge.A plurality of bubble cap distributors are arranged on distribution grid equably.In use mainly there are the following problems for this gas-liquid distributor: (1), although adopt described gas-liquid mixed structure can play certain gas-liquid mixed effect, disconnected plug flow and Pulsating Flow easily appear in gas-liquid.And the top of valve core cavity is sealed, enter into the reverse stopping ball top of floating, the gas-liquid of valve core cavity top dead can form swirling flow (gas-liquid downwards convolution flows).Therefore, reverse stopping ball can be in gas-liquid logistics bob, cause the collsion damage of reverse stopping ball and spool.(2) reverse stopping ball is when normally floating position, if gas-liquid charging is interrupted suddenly or pressure decreased, the material in ebullated bed will enter the valve core cavity of reverse stopping ball below from fluid issuing; The reverse stopping ball sealing station that can not fall back rapidly because below adverse current material instantaneous pressure is excessive is realized sealing.(3) because bubble-cap is columned, and its top has nut to be connected with center-pole, whole bubble-cap can only be to maintain static, it is more that simultaneously the area of bubble-cap is greater than the area of distribution plate perforate, therefore the possibility that the solid particle in material deposits on bubble-cap is also larger, and this also likely causes coking.In actual motion, find, part bubble-cap has the phenomenon of being surrounded by solid deposits.
The structure that the patent 200910012453.5 of Fu Yan institute of China Petrochemical Industry is introduced has been done a large amount of improvement in gas-liquid mixed structure, and gas-liquid mixed charging is steady.But the oblique top of top perforate, the baffling that simultaneously there is no bubble cap structure, catalyst easy deposition above dividing plate, may cause fluidized bed reactor over-heat at the bottom and burn out catalyst, owing to lacking fragmentation and the diffusion bubble of bubble cap, gas range of scatter is less, and bubble is larger, because export distributor does not have the baffling barrier effect of bubble cap, during adverse current, logistics is by moment adverse current, central feed tube flow velocity is larger, and reverse stopping ball is difficult for rapid return, needs an of short duration return process.
The patent 201020636320.3 of Firing Shenhua Coal liquefaction company application has conical bubble-cap, and this circular cone bubble-cap is connected with this distribution plate by a plurality of angle square supporting legs.The feature of this structure be by the characteristic structure of float valve simple, easy operating, closely, when fluid flow is zero, cone has covered the perforate of distribution plate completely, has completely cut off the material on distribution plate and has entered under distribution plate in sealing.The problem that this gas-liquid distributor in use exists: (1) lacks gas-liquid mixed structure, the logistics of distribution plate below enters bed when bubble cap floats, and bubble is larger, and bubble wake coverage is larger, directly cause the fluctuation of bed bottom larger, distribute uneven; (2) bubble-cap is connected with this distribution plate by angle square supporting leg, can freely move up and down, in running, there is rotation simultaneously, rotatablely move in bubble crushing and prevent that catalyst from depositing certain effect on bubble-cap, but rotation very easily causes the wearing and tearing of angle square supporting leg and distribution plate perforate for a long time, reliability reduces, and meaning and the benefit of the safe handling of petrochemical equipment long period are larger, so bubble cap should not rotate freely.
Summary of the invention
The technical problem that is prone to disconnected plug flow and Pulsating Flow, reverse stopping ball sealing sluggishness and distribution plate perforate wearing and tearing existing in order to solve prior art, the invention provides a kind of gas-liquid distributor for three-phase fluidized bed reactor, within this minute, gas-liquid distributor has been strengthened gas-liquid mixed, realized the continuous homogeneous state charging of gas-liquid, movable part is stable, catalyst at reactor bottom and bubble-cap upper wall surface without deposition.
Gas-liquid distributor for three-phase fluidized bed reactor provided by the invention is mainly by central tube, bubble cap, connection leg and distribution plate form: central tube is through the perforate on distribution plate, be assigned with plate and be divided into two sections, the material inlet of pipe centered by the end of hypomere, the material outlet of pipe centered by the end of epimere, near having the longitudinal bar seam connecting with material inlet on the tube wall of material inlet, at central tube hypomere, near longitudinal bar, sew in the central tube of end and be provided with an orifice mixer, central tube epimere is near along the circumferential direction having equably three longitudinal bar holes on the tube wall of distribution plate, bubble cap is the uncovered hood-like thing in a bottom, bubble cap inwall is along the circumferential direction provided with the connection leg of three longitudinal arrangements equably, connection leg comprises a long-armed and galianconism, be angle square shape, the circumscribed circle at connection leg place is less than inner diameter of centerpipe from footpath, the galianconism of connection leg be embedded in longitudinal bar hole and longitudinally bar hole move up and down, bubble cap is flexibly connected and covers on material outlet top by three connection legs and central tube epimere, the bottom periphery of bubble cap can fit with distribution plate.
Described orifice mixer center has an orifice mixer big hole, the uniform a plurality of orifice mixer small sircle holes of orifice mixer big hole surrounding.
Described bubble cap is cone barrel or taper, and cone barrel bubble cap divides up and down, two parts, and top is taper, and bottom is cylindrical shape.
For gas-liquid is realized better, mix, can also be on the central tube tube wall between distribution plate and orifice mixer, along the circumferential direction symmetrically have a plurality of central tube small sircle holes of oblique top from outside to inside.
In order to realize better sealing effectiveness, effectively prevent the generation of adverse current, can also on distribution plate, set up trapezoidal annulus platform, when there is adverse current, bubble cap bottom periphery can fit tightly with the upper bottom surface of trapezoidal annulus platform, realizes good sealing.
In order to improve the intensity of angle square shape connection leg, prevent that connection leg from deforming under high-temperature condition, affect the operation of connection leg, also can increase annular reinforcement in connection leg inner side.
Tool of the present invention has the following advantages:
(1) the present invention has perfect gas-liquid mixed unit, can make gas-liquid evenly mix and flow, and prevents disconnected plug flow and Pulsating Flow.And, when bubble cap floats, enter the gas-liquid of central tube epimere, can back down hole and side-wall hole outflow (to circular passage) through central tube, can not form swirling flow at central tube, Liquid Flow keeps comparatively stablely, bubble cap can be in gas-liquid logistics bob, its suspended state is stable, can not cause the collsion damage of angle square shape connection leg and the longitudinal bar hole of central tube epimere, guarantees inner member long-term operation;
(2) bubble cap adopts three angle square shape connection legs to be embedded in central tube epimere bar hole, and three legs are more stable, be difficult for stuck, nimbly and freely.By the restriction of longitudinal bar hole, the bubble cap space that only moves up and down, Bu Huiyin strenuous exercise causes wearing and tearing, and life cycle is longer;
(3) central tube except a porous plate blender after, there is not other loaded down with trivial details structures, central tube upper end and sidewall all have hole, circulation area is large, can reduce the Pressure Drop of gas-liquid charging when the gas-liquid distributor, is difficult for occurring catalyst simultaneously and stops up.
Accompanying drawing explanation
Fig. 1 is the structural representation of the first embodiment of the gas-liquid distributor for three-phase fluidized bed reactor of the present invention;
Fig. 2 is the structural representation of the second embodiment of the gas-liquid distributor for three-phase fluidized bed reactor of the present invention;
Fig. 3 is the structural representation that connection leg is connected with annular reinforcement;
Fig. 4 is that the A of Fig. 3 is to view;
Fig. 5 is trapezoidal annulus platform structural representation;
Fig. 6 is that the B of Fig. 5 is to view.
In figure, 1-central tube, the longitudinal bar seam of 11-, 12-orifice mixer, 13-orifice mixer big hole, 14-orifice mixer small sircle hole, 15-central tube small sircle hole, the longitudinal bar hole of 16-, 2-cone barrel bubble cap, 21-taper bubble cap, 3-connection leg, 31-annular reinforcement, 4-distribution plate, the trapezoidal annulus platform of 41-, the perforate of 42-distribution plate, 5-material inlet, 6-material outlet.
The specific embodiment
Below in conjunction with accompanying drawing, the gas-liquid distributor for three-phase fluidized bed reactor of the present invention is further described.
Embodiment 1
Fig. 1 is the structural representation of the first embodiment of the gas-liquid distributor for three-phase fluidized bed reactor of the present invention, and as shown in the figure, gas-liquid distributor provided by the invention is mainly comprised of central tube 1, cone barrel bubble cap 2, connection leg 3 and distribution plate 4.
Central tube 1 is through the distribution plate perforate on distribution plate 4 (representing with distribution plate perforate 42 in figure), be assigned with plate 4 and be divided into two sections, the upper surface of distribution plate 4 of take between epimere and hypomere is boundary, central tube 1 can be processed by whole pipe, epimere diameter is generally than the large 2-8mm of hypomere diameter, between epimere and hypomere, form an annular table, be mainly used in location and the installation of central tube 1 and distribution plate 4.
Central tube hypomere is mainly used in gas-liquid charging, realizes gas-liquid two-phase and mixes.The material inlet 5 of pipe centered by the end of central tube 1 hypomere, material inlet 5 is the main gas-liquid feeding-passages of central tube 1, the material outlet 6 of pipe centered by the end of epimere, near having the longitudinal bar seam 11 connecting with material inlet 5 on the tube wall of material inlet 5, longitudinally bar seam 11 is generally 2-8 bar, uniform along central tube circumferencial direction, preferred 4-6 bar, bar seam width is 2-5mm.Longitudinally the Main Function of bar seam 11 be tolerance when excessive gas can stitch 11 places at longitudinal bar and carry and enter central tube 1 by liquid.
At central tube hypomere, near longitudinal bar, stitch in the central tube of 11 upper ends and be provided with an orifice mixer 12, orifice mixer 12 centers have an orifice mixer big hole 13, the diameter of orifice mixer big hole 13 is generally the 50%-80% of central tube 1 internal diameter, the uniform a plurality of orifice mixer small sircle holes 14 of orifice mixer big hole 13 surrounding, the diameter of orifice mixer small sircle hole 14 is generally the 3%-15% of central tube 1 internal diameter, quantity is generally 4-8, be uniformly distributed, the thickness of orifice mixer 12 equals central tube hypomere wall thickness.
For being realized better, gas-liquid mixes, on the central tube tube wall between distribution plate 4 and orifice mixer 12, along the circumferential direction symmetrically have a plurality of central tube small sircle holes 15 of oblique top from outside to inside, central tube small sircle hole 15 is storied placement along the circumferential direction, be traditionally arranged to be 1-4 layer, every one deck is containing 4-8 central tube small sircle hole 15, and aperture is generally 2-5mm, and the angle of inclination axially becoming with horizontal direction of central tube small sircle hole 15 is 20-60 °.
Central tube 1 epimere is near along the circumferential direction having equably three longitudinal bar holes 16 on the tube wall of distribution plate 4, for the location of cone barrel bubble cap 2 and the stroke space of restriction cone barrel bubble cap 2, three longitudinal bar holes 16 make cone barrel bubble cap 2 more stable, be difficult for occurring stuck phenomenon, operate steadily, longitudinally the width of bar hole 16 is generally 5-15mm, and longitudinally the longitudinal length of bar hole 16 is generally the 40%-60% of central tube epimere height.
Cone barrel bubble cap 2 is the uncovered hood-like thing in a bottom, be cone barrel, divide upper and lower two parts, top is taper, bottom is cylindrical shape, the cone angle of the pyramidal structure on top generally should be less than the stocking angle of catalyst, be generally 45-70 °, can prevent the depositional phenomenon of catalyst on bubble cap, the external diameter of bottom cylinder is generally 1.8-2.5 times of central tube external diameter, and bubble cap bottom is set to cylindrical shape, can reduce the radial space that taper bubble cap occupies, thereby can reduce the spacing between many bubble caps, improve the percent opening of distribution plate.On cone barrel bubble cap 2 conical inboard walls, be along the circumferential direction provided with equably the connection leg 3 of three longitudinal arrangements, connection leg 3 comprises a long-armed and galianconism, be angle square shape, the circumscribed circle diameter at three angle square shape connection leg 3 places is less than central tube 1 internal diameter, angle square shape connection leg 3 is mainly used in the motion of guiding and restriction cone barrel bubble cap 2, the galianconism of angle square shape connection leg 3 be embedded in longitudinal bar hole 16 and longitudinally bar hole 16 move up and down, the width of galianconism matches with the width of longitudinal bar hole 16, general wide 5-15mm; The length of galianconism is greater than the wall thickness of central tube 1 epimere, is generally 5-15mm, and the long-armed length of angle square shape connection leg 3 is generally determined according to the size of bubble cap and central tube; In order to improve the intensity of angle square shape connection leg 3, prevent that connection leg 3 from deforming under high-temperature condition, affect the operation up and down of connection leg 3, in connection leg 3 inner sides, be provided with annular reinforcement 31, the situation that connection leg 3 is connected with annular reinforcement 31 as shown in Figure 3 and Figure 4.
Cone barrel bubble cap 2 is flexibly connected and covers on material outlet 6 tops by three angle square shape connection legs 3 with central tube 1 epimere, and the bottom periphery of cone barrel bubble cap 2 can fit tightly with the upper bottom surface of the trapezoidal annulus platform 41 that arranges on distribution plate 4.The size shape of trapezoidal annulus platform 41 and cone barrel bubble cap 2 match, trapezoidal annulus platform 41 is set is mainly the poorly sealed phenomenon that on distribution plate 4, a small amount of deposited catalyst causes when preventing that cone barrel bubble cap 2 from falling, trapezoidal annulus platform 41 is more easily for 2 sealings of cone barrel bubble cap provide a sealing plane.Trapezoidal annulus platform 41 adopts fine finishining, can improve sealing effectiveness, effectively prevents the generation of adverse current, and the trapezoidal base angle of trapezoidal annulus platform 41 is generally 50-70 °, the general 5-15mm of trapezoidal height, and upper bottom width is 2-6mm, the general 4-10mm of lower bottom width.The structure of trapezoidal annulus platform 41 as shown in Figure 5 and Figure 6.
Fig. 2 is the structural representation of the second embodiment of the gas-liquid distributor for three-phase fluidized bed reactor of the present invention, and embodiment 2 and the difference of embodiment 1 are, in the different and embodiment 2 of the structure of bubble cap, trapezoidal annulus platform is not set, and all the other structures are all identical.Certainly, embodiment 2 also can arrange trapezoidal annulus platform, to improve sealing property, better prevents that adverse current from occurring.In embodiment 2, taper bubble cap 21 is similarly the uncovered hood-like thing in bottom, and tapered, the cone angle of pyramidal structure generally should be less than the stocking angle of catalyst, and the stocking angle of catalyst is generally 45-70 °.With respect to embodiment 1, taper bubble cap 21 structures are simpler, but can reduce the percent opening of distribution plate.In embodiment 2, taper bubble cap 21 bottom periphery can be directly and distribution plate 4 fit.
As shown in Figure 1, gas-liquid distributor of the present invention in normal operation, the equal phase materials of gas-liquid enters central tube by the material inlet 5 of central tube 1 hypomere end, the central tube small sircle hole 15 of part gaseous phase materials on central tube 1 tube wall enters central tube, gaseous phase materials enters in the interior material flow of central tube 1 with the form of bubble, in the situation that air inflow increases, longitudinal bar seam bar seam 11 that part gaseous phase materials also can connect through central tube 1 hypomere and material inlet 5 enters central tube, gas-liquid mixed material therefrom core barrel hypomere enters central tube after the up arrival central tube of central tube epimere, small part material enters into the annular space space between central tube 1 epimere and cone barrel bubble cap 2 through the longitudinal bar hole 16 of central tube, most of material is gone out through the material outlet 6 of central tube 1 epimere end, the percussion of material flow is floated cone barrel bubble cap 2, gas-liquid two-phase material flow is under the barrier effect of cone barrel bubble cap 2, baffling enters the annular space space between central tube 1 epimere and cone barrel bubble cap 2 from cone barrel bubble cap 2 lower edge, and then enter in reactor bed.Once occur in the situation of charging interruption, cone barrel bubble cap 2 can fall rapidly, trapezoidal annulus platform 41 upper bottom surfaces on cone barrel bubble cap 2 bottom periphery and distribution plate 4 fit, thereby blocking-up material channel makes distribution plate 4 tops adverse current can not occur containing the material of catalyst; Or as shown in Figure 2, taper bubble cap 21 bottom periphery directly fit with distribution plate 4, thereby prevent adverse current generation.
In addition, longitudinally bar hole 16 is except the travel limits space as connection leg 3, make cone barrel bubble cap 2 (or taper bubble cap 21, see Fig. 2) only there is a upper and lower free degree, the free degree that there is no rotation, guarantee cone barrel bubble cap 2 (or taper bubble caps 21, see Fig. 2) in the situation that charging occurs interrupting, fall after rise rapidly outside, longitudinally bar hole 16 has played part shunting action on the other hand, excessive material flow is slowed down to some extent before arriving material outlet, thereby material outlet place flow velocity situation excessive and that cause bubble cap to be difficult to falling sealing rapidly single in the time of can effectively preventing adverse current generation occurs.
The present invention is in conjunction with the characteristic of technological process, gas-liquid mixed and the biphase gas and liquid flow of ebullated bed, provide a kind of simple and reasonable, the gas-liquid distributor of safe and reliable three-phase fluidized bed reactor, both can guarantee that gas was broken for continuous microbubble in liquid, be uniformly distributed, can effectively solve or alleviate again the adverse current blockage problem of carrying the material of catalyst when gas-liquid pressure shakiness or gas-liquid charging are interrupted suddenly.
Claims (18)
1. for a gas-liquid distributor for three-phase fluidized bed reactor, it is characterized in that: mainly by central tube, bubble cap, connection leg and distribution plate, formed, central tube is through the perforate on distribution plate, be assigned with plate and be divided into two sections, the material inlet of pipe centered by the end of hypomere, the material outlet of pipe centered by the end of epimere, near having the longitudinal bar seam connecting with material inlet on the tube wall of material inlet, at central tube hypomere, near longitudinal bar, sew in the central tube of end and be provided with an orifice mixer, central tube epimere is near along the circumferential direction having equably three longitudinal bar holes on the tube wall of distribution plate, bubble cap is the uncovered hood-like thing in a bottom, bubble cap inwall is along the circumferential direction provided with the connection leg of three longitudinal arrangements equably, connection leg comprises a long-armed and galianconism, be angle square shape, the circumscribed circle diameter at connection leg place is less than inner diameter of centerpipe, the galianconism of connection leg be embedded in longitudinal bar hole and longitudinally bar hole move up and down, bubble cap is flexibly connected and covers on material outlet top by three connection legs and central tube epimere, the bottom periphery of bubble cap can fit with distribution plate.
2. gas-liquid distributor according to claim 1, is characterized in that, on described distribution plate and the central tube tube wall between orifice mixer, along the circumferential direction symmetrically have a plurality of central tube small sircle holes of oblique top from outside to inside.
3. gas-liquid distributor according to claim 1, is characterized in that, described bubble cap is cone barrel, minute upper and lower two parts, and top is taper, bottom is cylindrical shape.
4. gas-liquid distributor according to claim 1, is characterized in that, described bubble cap is tapered.
5. gas-liquid distributor according to claim 1, is characterized in that, described distribution plate is provided with trapezoidal annulus platform, and bubble cap bottom periphery can fit tightly with the upper bottom surface of trapezoidal annulus platform.
6. gas-liquid distributor according to claim 1, is characterized in that, described connection leg inner side is provided with annular reinforcement.
7. gas-liquid distributor according to claim 1, is characterized in that, described longitudinal bar seam is for 2-8 bar, uniform along central tube circumferencial direction.
8. gas-liquid distributor according to claim 1, is characterized in that, the width of the galianconism of described connection leg matches with the width of longitudinal bar hole, and the length of galianconism is greater than the wall thickness of central tube epimere.
9. according to the arbitrary gas-liquid distributor described in claim 1-8, it is characterized in that, described orifice mixer center has an orifice mixer big hole, the uniform a plurality of orifice mixer small sircle holes of orifice mixer big hole surrounding.
10. gas-liquid distributor according to claim 9, is characterized in that, the 50%-80% of bore centered by the diameter of described orifice mixer big hole, and the 3%-15% of bore centered by the diameter of orifice mixer small sircle hole, quantity is 4-8.
11. gas-liquid distributors according to claim 2, is characterized in that, described central tube small sircle hole is storied placement along the circumferential direction, is set to 1-4 layer, and every one deck is containing 4-8 central tube small sircle hole.
12. gas-liquid distributors according to claim 11, is characterized in that, the aperture of described central tube small sircle hole is 2-5mm, and the angle of inclination axially becoming with horizontal direction of central tube small sircle hole is 20-60 °.
13. gas-liquid distributors according to claim 11, is characterized in that, described bubble cap is cone barrel, minute upper and lower two parts, and top is taper, and bottom is cylindrical shape, and the cone angle of pyramidal structure is less than the stocking angle of catalyst.
14. gas-liquid distributors according to claim 13, is characterized in that, described distribution plate is provided with trapezoidal annulus platform, and bubble cap bottom periphery can fit tightly with the upper bottom surface of trapezoidal annulus platform.
15. gas-liquid distributors according to claim 3, is characterized in that, the cone angle of the pyramidal structure of described bubble cap is less than the stocking angle of catalyst.
16. gas-liquid distributors according to claim 4, is characterized in that, the cone angle of the pyramidal structure of described bubble cap is less than the stocking angle of catalyst.
17. gas-liquid distributors according to claim 5, is characterized in that, the trapezoidal base angle of described trapezoidal annulus platform is 50-70 °, and trapezoidal height is 5-15mm, and upper bottom width is 2-6mm, lower bottom width 4-10mm.
18. according to the arbitrary gas-liquid distributor described in claim 1-8 and claim 11-17, it is characterized in that, manages the 40%-60% of epimere height centered by the longitudinal length of described longitudinal bar hole.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105582862A (en) * | 2014-10-22 | 2016-05-18 | 中国石油化工股份有限公司大连石油化工研究院 | Gas-liquid distribution disk for up-flow reactor |
| CN105582861A (en) * | 2014-10-22 | 2016-05-18 | 中国石油化工股份有限公司 | Gas-liquid distributor for fluidized bed |
| CN107661735A (en) * | 2017-09-30 | 2018-02-06 | 北京中科诚毅科技发展有限公司 | A kind of hydrogenation reactor feed distributor and its feeding process, design method and purposes |
| CN114130051A (en) * | 2021-12-08 | 2022-03-04 | 常州大学 | Floating valve mass transfer element |
| CN115151321A (en) * | 2020-02-25 | 2022-10-04 | 雅苒国际集团 | Distribution chamber for liquid flow |
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| CN201493093U (en) * | 2009-08-31 | 2010-06-02 | 湖北侨光石化机械有限责任公司 | Gas-liquid partition tray |
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| ES2019809A6 (en) * | 1990-02-13 | 1991-07-01 | Antolin Giraldo Gregorio | Bubbling cap (bubble cap) |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105582862A (en) * | 2014-10-22 | 2016-05-18 | 中国石油化工股份有限公司大连石油化工研究院 | Gas-liquid distribution disk for up-flow reactor |
| CN105582861A (en) * | 2014-10-22 | 2016-05-18 | 中国石油化工股份有限公司 | Gas-liquid distributor for fluidized bed |
| CN105582862B (en) * | 2014-10-22 | 2018-03-16 | 中国石油化工股份有限公司大连石油化工研究院 | A kind of gas-liquid partition tray for up-flow reactor |
| CN105582861B (en) * | 2014-10-22 | 2018-06-15 | 中国石油化工股份有限公司 | A kind of gas-liquid distributor for fluid bed |
| CN107661735A (en) * | 2017-09-30 | 2018-02-06 | 北京中科诚毅科技发展有限公司 | A kind of hydrogenation reactor feed distributor and its feeding process, design method and purposes |
| CN115151321A (en) * | 2020-02-25 | 2022-10-04 | 雅苒国际集团 | Distribution chamber for liquid flow |
| CN115151321B (en) * | 2020-02-25 | 2024-02-06 | 雅苒国际集团 | Distribution chamber for liquid flow |
| CN114130051A (en) * | 2021-12-08 | 2022-03-04 | 常州大学 | Floating valve mass transfer element |
| CN114130051B (en) * | 2021-12-08 | 2022-10-21 | 常州大学 | Floating valve mass transfer element |
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| CN103657540B (en) | 2015-12-16 |
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