CN105582857A - Gas-liquid-solid three-phase reactor and application method thereof - Google Patents
Gas-liquid-solid three-phase reactor and application method thereof Download PDFInfo
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- CN105582857A CN105582857A CN201410563140.XA CN201410563140A CN105582857A CN 105582857 A CN105582857 A CN 105582857A CN 201410563140 A CN201410563140 A CN 201410563140A CN 105582857 A CN105582857 A CN 105582857A
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Abstract
The invention discloses a gas-liquid-solid three-phase reactor and an application method thereof. The reactor comprises a top material inlet, a bottom material outlet, a pre-distributor, a plurality layers of gas-liquid distribution disks, and two annular baffle plates which are arranged on the inner wall of the reactor, and a plurality of catalyst bed layers. In the reactor, gas and liquid are fully contacted with each other in both radial and axial directions, so that the gas liquid distribution status in the reactor is significantly improved. The gas and liquid are distributed uniformly in the reactor, so that adverse effect caused by wall flow is reduced and reaction efficiency of a trickle bed is increased. The reactor is suitable for gas-liquid-solid three-phase reactions, such as C3 liquid-phase hydrogenation and the like.
Description
Technical field
The invention belongs to petrochemical industry, relate to a kind of fixed bed reactors, more particularly, relate to onePlant and adopt the distribution of segmentation gas-liquid and deflection plate to eliminate trickle bed reactor and the application of wall stream, bias current.
Background technology
Trickle bed reactor is one of main several reactors. Because it had both had simple in structure, equipment throwingProvide low advantage, there is again the feature easy to operate, operating flexibility is large; Therefore, trickle bed reactor is in refiningOil, chemical field is used widely, particularly in fields such as oil hydrogenation cracking, hydrocarbons hydrogenation are refining,Trickle bed is one of the most basic reactor.
One of feature of trickle bed reactor is that the interior gas of reactor and liquid also flow by beds, itsMiddle liquid is with the drip mode beds of flowing through, and gas is that mode with continuous-flow is by catalysisAgent bed; Therefore, can liquid form drip in reactor, whether distribution of gas is evenly called trickle bedThe major influence factors of reactor design. Along with the expansion of unit scale, the diameter of reactor is continuing to increase,Gas-liquid distributes more and more important; Gas-liquid skewness can have a strong impact on reactor operating characteristics, directly impactThe efficiency of trickle bed reactor also can cause in bed temperature distributing disproportionation even simultaneously, destroys catalyst stableProperty.
On fixed bde catalyst, the phase reaction of liquid and gas is through being used for chemical process; Chemistry is anti-The conversion ratio of answering and the selective fluid dynamic that not only depends on kinetics but also especially depend on reactorLearn; Reaction process is necessary uniformly, and this just requires gas and liquid, i.e. two kinds of reactants, in reactionOn device radial and axial, can be uniformly distributed; The problem of skewness is particularly prominent in large scale industry reactorGo out.
Patent US4708852 has introduced a kind of trickle bed reactor, and this reactor comprises import pre-distributor,Gas-liquid distributor, porcelain ball bed, beds; Its gas-liquid distributor adopts perforate corrugated board structures,Keep certain liquid level in trough, the lowest point, brae, summit are all provided with perforate, liquid from the hole of the lowest point andHole on subsurface brae passes, and forms cross-current, and gas is from summit and the paddy on liquid levelHole on slope is passed; Gas contacts below corrugated plating with liquid, has improved uniform gas-liquid distribution. This gasLiquid distributor can improve the distributing homogeneity of gas-liquid in different angles, but liquid level in paddy is difficult to control, asFruit initial gas or liquid distribution are inhomogeneous, and this gas-liquid distributor is difficult to form liquid level in uniform paddy, reachesLess than equally distributed object, inside reactor drip poor effect, the reaction that affects trickle bed reactor is imitatedRate.
Adopt at present more trickle bed reactor mainly to adopt following structure: charging aperture, gas-liquid partition tray,Porcelain ball bed, beds; But distribute because liquid and gas only have axial flow, be difficult to form allEven gas-liquid distributes, the especially conplane reaction result difference in reactor middle and lower part, and this explanation is existingThe gas-liquid of reactor distributes and does not also reach and be satisfied with requirement.
Patent CN101279229B introduces a kind of trickle bed reactor, this invention by adopt by charging aperture,Reactor shell, gas-liquid distributor, porcelain ball bed, beds and discharging opening composition trickle bed reactor;Wherein gas-liquid distributor is that gas passage pipe and fluid passage pipe composition, gas passage are installed on distribution gridPipe is made up of circular cone top cover and upright short tube; Fluid passage pipe is vertical short tube, and stretch out the upper end of vertical short tube10～100 millimeters of distribution grid tops, 200～1000 millimeters of distribution grid belows are stretched out and vertically not in lower endOn the cross section of co-located, have equably aperture, solved preferably gas-liquid initial distribution inequality, drip effectThe problem that fruit is not good, can be applicable in various gas-liquid-solid phase reaction devices.
Although the trickle bed reactor described in above-mentioned document has good gas-liquid initial distribution, along with reactionCarrying out, in the time that gas-liquid flows to reactor middle and lower part, gas-liquid cannot reach mixed uniformly effect, and wall streamIncrease, cause the reaction efficiency of trickle bed reactor to be difficult to improve.
Summary of the invention
In order to solve problems of the prior art, improve the reaction effect of trickle bed reactor, reduce wallThe situation of the gas-liquid skewness such as stream, bias current, the invention provides a kind of gas-liquid-solid phase reaction device and shouldUse method.
A kind of gas-liquid-solid phase reaction device of the present invention is achieved in that
A kind of gas-liquid-solid phase reaction device, described reactor comprises cylindrical shell 1, along described cylindrical shell 1 axially from upperTo under be disposed with predistribution device 2, at least 2 layers of gas-liquid partition tray 3 and be arranged on described gas-liquid partition trayThe beds 4 of 3 belows, and be arranged on the outlet liquid trap 9 of described cylindrical shell 1 bottom.
In the specific implementation, on the inwall of the described cylindrical shell 1 of described beds 4 correspondences, be provided with annularDeflection plate 5, does not have space between ring baffle plate 5 and described cylindrical shell 1 inwall, its cross section in the vertical directionBe the vertical isosceles triangle in base. The angle on described isosceles triangle summit is 45-75 degree, preferably 60 degree;The difference of the interior outer radius of described ring baffle plate 5 is the 3%-20% of described cylindrical shell 1 inside radius; At described catalystDescribed cylindrical shell 1 inwall of bed 4 correspondences, is uniformly distributed the described ring baffle plate 5 of 1-10 layer is set, preferably1-5 layer, more preferably 1-2 layer. Described reactor inside diameter is 0.5-3 rice, and reactor ratio of height to diameter is 2-9, annularDeflection plate [5] is uniformly distributed on the inwall of described cylindrical shell [1], and spacing is between 0.5 meter-3 meters, preferred distanceFor 1-2 rice.
In the specific implementation, described reactor arranges 2～4 layers of described gas-liquid partition tray 3 and described catalystBed 4, preferably 2 layers; First floor gas-liquid partition tray 3 is positioned at the top of described reactor.
The application process of a kind of gas-liquid-solid phase reaction device of the present invention is achieved in that
Adopt gas-liquid-solid phase reaction device of the present invention, after liquid phase material mixes with gaseous phase materials, by described cylinderThe entrance on body 1 top enters, and through 2, at least 2 layers of described gas-liquid partition tray 3 of described predistribution device, evenly dividesLiquid phase material and gaseous phase materials described in cloth, and carry out gas-liquid-solid phase reaction by described beds 4;Product is discharged reactor by described outlet liquid trap 9.
In the specific implementation, described gas-liquid-solid phase reaction device removes first for liquid phase selective hydrogenation of C 3 hydrocarbonsEthyl-acetylene and allene; 0～500 DEG C of the temperature of described hydrogenation reaction, pressure 0.1～3.0MPa.
The present invention arranges multilayer gas-liquid allotter and deflection plate in gas-liquid-solid phase reaction device; Impel gas-liquid to fillPoint contact, improves the gas-liquid distribution situation of inside reactor, have gas-liquid radially, axially on fully contact,Gas-liquid is evenly distributed in reactor, the effective feature of drip in reactor, and it is raw to have reduced wall miscarriageIll effect, improved the reaction efficiency of trickle bed, be applicable to the gas-liquid-solid three-phase such as carbon three liquid-phase hydrogenatins anti-Should.
Brief description of the drawings
Fig. 1 is trickle bed reactor schematic diagram of the present invention;
Fig. 2 is current conventional trickle bed reactor schematic diagram;
Wherein: 1-reactor shell, 2-predistribution device, 3,6-gas-liquid partition tray, 4,7-beds, 5,8-deflection plate, 9-exports collector.
Detailed description of the invention
Be described in further detail technical scheme of the present invention, protection scope of the present invention below in conjunction with embodiment and accompanying drawingBe not limited to following detailed description of the invention.
Embodiment 1
Reactor as shown in Figure 1. Gas-liquid-solid phase reaction device axially sets gradually from top to bottom along cylindrical shell 1There are predistribution device 2, gas-liquid partition tray 3/6, beds 4/7, outlet collector 9, and at catalystThe inwall of the cylindrical shell 1 of bed 4/7 correspondence is provided with ring baffle plate 5/8.
Reactor shell internal diameter is 0.8 meter, and Catalyst packing total height is 3 meters, wherein beds 4/7Height be respectively 1.5 meters. Beds 4/7 is respectively equipped with ring baffle plate 5/8, and ring baffle plate existsThe cross section of vertical direction is the vertical isosceles triangle in base, and the angle on its summit is 60 degree, ring baffle plateThe difference of interior outer radius is 10% of described cylindrical shell inside radius.
This trickle bed reactor removes allylene and allene for liquid phase selective hydrogenation of C 3 hydrocarbons; ReactionIn the carbon 3 material of device entrance, MAPD content is 2.5mol%, and the air speed of hydrogenation reaction is in 50-60hr-1, pressurePower 2.4MPa, the mole that hydrogen is allocated into is 1.3 times of MAPD, 38 DEG C of reactor inlet temperatures, urgeAgent adopts general palladium series hydrocatalyst; Carbon three raw materials pass through in the material after hydrogenation reactorMAPD content is less than 50ppm.
Comparative example 1
Reactor as shown in Figure 2. Gas-liquid-solid phase reaction device axially sets gradually from top to bottom along cylindrical shell 1There are predistribution device 2, gas-liquid partition tray 3, beds 4, outlet collector 9.
Reactor inside diameter is 0.8 meter, and catalyst packing height is 3 meters. This trickle bed reactor heats up in a steamer for carbon threeDivide liquid phase to select hydrogenation and removing allylene and allene; MAPD content in the carbon 3 material of reactor inletFor 2.5mol%, the air speed of hydrogenation reaction is at 50-60hr-1, pressure 2.4MPa, and the mole that hydrogen is allocated into is1.3 times of MAPD, 38 DEG C of reactor inlet temperatures, catalyst adopts general palladium series hydrocatalyst;MAPD content in the material of carbon three raw materials after by hydrogenation reactor is 1000ppm.
Compared with prior art, layering of the present invention arranges gas-liquid partition tray and beds, and in catalysisAgent bed arranges ring baffle plate, has obviously improved the gas-liquid distribution situation of inside reactor, makes gas-liquid in footpathTo, axially upper fully contact, gas-liquid is evenly distributed in reactor, has reduced the raw ill effect of wall miscarriage,Improve the reaction effect of trickle bed; Be applied to the gas-liquid-solid phase reactions such as carbon three liquid-phase hydrogenatins, remaining formerIn the constant situation of the loadings of catalyst and operation condition, can meet in hydrogenation reaction productMAPD is less than the requirement of 50ppm.
Claims (8)
1. a gas-liquid-solid phase reaction device, described reactor comprises cylindrical shell [1], along described cylindrical shell [1] axially from upperTo under be disposed with predistribution device [2], at least 2 layers of gas-liquid partition tray [3] and be arranged on described gas-liquid and distributeThe beds [4] of dish [3] below, and be arranged on the outlet liquid trap [9] bottom described cylindrical shell [1].
2. reactor according to claim 1, is characterized in that:
On the inwall of described cylindrical shell [1] corresponding to described beds [4], be provided with ring baffle plate [5], annularBetween deflection plate [5] and described cylindrical shell [1] inwall, there is no space, it is vertical that its cross section is in the vertical direction baseIsosceles triangle.
3. reactor according to claim 2, is characterized in that:
The angle on described isosceles triangle summit is 45-75 degree; The interior outer radius of described ring baffle plate [5] poorFor the 3%-20% of described cylindrical shell [1] inside radius;
At described cylindrical shell [1] inwall corresponding to described beds [4], be uniformly distributed the described ring of 1-10 layer is setShape deflection plate [5].
4. reactor according to claim 3, is characterized in that:
The angle on described isosceles triangle summit is 60 degree;
At described cylindrical shell [1] inwall corresponding to described beds [4], be uniformly distributed the described ring of 1-5 layer is setShape deflection plate [5]; Distance between described ring baffle plate [5] is 0.5 meter～3.0 meters.
5. reactor according to claim 4, is characterized in that:
Distance between described ring baffle plate [5] is 1.0 meters～2.0 meters.
6. reactor according to claim 1, is characterized in that:
Described reactor inside diameter is 0.5 meter-3 meters, and ratio of height to diameter is 2-9; Described reactor arranges described in 2～4 layersGas-liquid partition tray [3].
7. according to the application process of one of claim 1-6 described reactor;
Adopt described gas-liquid-solid phase reaction device, after liquid phase material mixes with gaseous phase materials, by described cylindrical shell [1]The entrance on top enters, and through described predistribution device [2], at least 2 layers of described gas-liquid partition tray [3], is uniformly distributedDescribed liquid phase material and gaseous phase materials, and carry out gas-liquid-solid phase reaction by described beds [4]; InsteadAnswer product to discharge reactor by described outlet liquid trap [9].
8. application process according to claim 7, is characterized in that:
Described hydrogenation reactor removes allylene and allene for liquid phase selective hydrogenation of C 3 hydrocarbons; Described0～500 DEG C of the temperature of hydrogenation reaction, pressure 0.1～3.0MPa.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110023460A (en) * | 2016-11-09 | 2019-07-16 | Ifp 新能源公司 | It will be used for the new equipment for being used for gas-liquid separation of such as three-phase fluid bed reactor of those used in the H-oil technique |
| CN112295510A (en) * | 2019-08-01 | 2021-02-02 | 中国石油化工股份有限公司 | Reactor and application |
| CN112546968A (en) * | 2020-12-02 | 2021-03-26 | 中国科学院广州能源研究所 | Three-phase reactor and method applied to hydrodeoxygenation refining of biological aviation oil |
| CN113736514A (en) * | 2020-05-28 | 2021-12-03 | 中国石油化工股份有限公司 | Automatic control method of multilayer structure carbon three-liquid phase hydrogenation reactor and reactor |
| CN115400697A (en) * | 2021-05-27 | 2022-11-29 | 中国石油化工股份有限公司 | Automatic control method and system for double-layer structure carbon-three-liquid phase hydrogenation reactor and hydrogenation reactor |
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| CN101450884A (en) * | 2007-12-07 | 2009-06-10 | 中国石油化工股份有限公司 | High unsaturated hydrocarbon selective hydrogenation method in cracking gas |
| CN201632171U (en) * | 2010-03-17 | 2010-11-17 | 上海融新能源环境科技有限公司 | Washing tower |
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| US4708852A (en) * | 1985-04-08 | 1987-11-24 | Texaco Inc. | Uniform flow distributing means for a trickle bed flow reactor |
| CN1915482A (en) * | 2006-06-21 | 2007-02-21 | 中国石油集团工程设计有限责任公司抚顺分公司 | No wall flow technique and equipment for hydrogenation reaction chamber |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110023460A (en) * | 2016-11-09 | 2019-07-16 | Ifp 新能源公司 | It will be used for the new equipment for being used for gas-liquid separation of such as three-phase fluid bed reactor of those used in the H-oil technique |
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| CN113736514A (en) * | 2020-05-28 | 2021-12-03 | 中国石油化工股份有限公司 | Automatic control method of multilayer structure carbon three-liquid phase hydrogenation reactor and reactor |
| CN112546968A (en) * | 2020-12-02 | 2021-03-26 | 中国科学院广州能源研究所 | Three-phase reactor and method applied to hydrodeoxygenation refining of biological aviation oil |
| CN115400697A (en) * | 2021-05-27 | 2022-11-29 | 中国石油化工股份有限公司 | Automatic control method and system for double-layer structure carbon-three-liquid phase hydrogenation reactor and hydrogenation reactor |
| CN115400697B (en) * | 2021-05-27 | 2024-02-13 | 中国石油化工股份有限公司 | Automatic control method and control system for double-layer structure carbon three-liquid-phase hydrogenation reactor and hydrogenation reactor |
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| CN105582857B (en) | 2019-05-31 |
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