CN104667831A - Gas-liquid distributor of trickle bed reaction device - Google Patents
Gas-liquid distributor of trickle bed reaction device Download PDFInfo
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- CN104667831A CN104667831A CN201510060815.3A CN201510060815A CN104667831A CN 104667831 A CN104667831 A CN 104667831A CN 201510060815 A CN201510060815 A CN 201510060815A CN 104667831 A CN104667831 A CN 104667831A
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Abstract
The invention relates to a gas-liquid distributor of a trickle bed reaction device. The gas-liquid distributor mainly includes a horizontal plate, a cap cover combination structure, liquid inlets, a liquid distribution cap, a liquid distribution tube, a liquid distribution baffle, and a liquid distribution cap bottom margin, wherein a plurality of cap cover combination structures are uniformly arranged on the horizontal plate, and each cap cover combination structure is characterized in that an inner layer cap cover is embedded into the horizontal plate; an outer layer cap cover is arranged outside the inner layer cap cover; a plurality of sieve pores are respectively arranged on the inner layer cap cover and the outer layer cap cover; the liquid inlets are arranged on the inner layer cap cover and correspondingly equipped with the liquid distribution baffle; the liquid distribution cap is arranged at the bottom of the liquid distribution baffle; the sieve pores are arranged on the liquid distribution cap; the liquid distribution baffle is arranged on the corresponding position of each liquid inlet; a plurality of liquid distribution tubes are arranged at the bottom of the liquid distribution cap. According to the gas-liquid distributor, gas and liquid can fully contact, the liquid flows in the sieve pore region and is driven to disperse and jet by gas, and one part of the liquid flows into the bottom of the liquid distribution cap for redistribution, thus the gas-liquid distributor is large in operation elasticity, low in resistance, good in liquid distribution effect, and low in anti-clogging and levelness requirements.
Description
Technical field
The present invention relates to a kind of trickle bed reaction unit gas-liquid distributor, be specially the gas-liquid distributor of the biphase gas and liquid flow distribution in a kind of fixed bed reactors, be widely used in the industries such as Coal Chemical Industry, oil refining, petrochemical industry, fine chemistry industry, pharmacy, grease.
Background technology
The hydrogenation process that what industrial application trickle bed was largest is in petroleum refining industry, as the hydrofinishing etc. of the hydrodesulfurization of heavy oil or residual oil, hydrocracking and diesel oil, lubricating oil.In bed, liquid distribution situation is one of key property parameter of trickle bed reactor, industrial reactor is very responsive to liquid distribution, liquid distribution inequality can cause catalyst irrigation incomplete, channel and focus etc. is formed at bed, the utilization ratio of catalyst can be reduced, reduction of service life, and cause product property to be deteriorated.In clean fuel oil production process, the effect adopting an inner member technology (such as gas-liquid distributor) packaged to obtain never is second to uses a kind of active better catalyst instead.
As everyone knows, the factor affecting liquid distribution mainly contains: the ratio of the pre-distribution situation of liquid, gas/liquid service speed, liquid property, shape of catalyst, bed diameter and particle diameter and solid particle and reactor material wettability etc.Along with the promotion and application in the whole world of the increasingly stringent of environmental protection law regulation in world wide, clean fuel and following requirement of producing ultra-low-sulphur diesel, traditional oil Refining Technologies must carry out the technological improvement upgraded.Wherein one of key technology is exactly that reactor must have the peak use rate distributing to realize catalyst between good liquid, gas initial distribution and bed again, otherwise can not produce ultra-low-sulphur diesel.
On beds, usual layout inlet diffuser, distributing disc, gas-liquid distributor, the Main Function of diffuser and distributing disc is rough segmentation cloth and reduces gas-liquid flow at high speed to the impact of gas-liquid distributor, and the distributor performance of the gas-liquid distributor directly over beds is most important.For rectifying and absorption tower, gas-liquid counter current is more common, conventional gas-liquid distributor has Box-type Gas-liquid Distributor, calandria gas-liquid distributor, tank type liquid distributor, disc type liquid distribution trough etc., the most fluid flow of operating mode that these distributors use is relatively large, stable, the uniform distributed effect of easy formation, for the operating mode of gas and liquid flowing, should gas-liquid mixed is even, also two-phase to be evenly distributed simultaneously, also will have good operating flexibility, anti-stifled and anti-dirt performance simultaneously.
Along with the expansion of unit scale, the diameter of reactor is continuing to increase, and gas-liquid distribution is more and more important.Gas-liquid skewness can have a strong impact on reactor operating characteristics, directly affects the efficiency of trickle bed reactor.The several important indicators evaluating gas-liquid distributor performance comprise: 1, within the scope of larger gas-liquid load, keep stable, good performance; 2, the spacing of cloth liquid point is little, quantity is abundant; 3, low to distributor levelness sensitiveness; 4, pressure drop is little; 5, be not easy blocked; Distributor used both at home and abroad has various ways at present: liquid flow type distributor, sieve-board type distributor, funnel-shaped distributing disc, length pipe distributor, angle pipe distributor, v-notch distributor, bubble-cap type distributor, air lift type distributor etc., these distributors are updated in operating flexibility, anti-clogging, but the space be still improved; Still deficiency is had in the quantity, density increase of cloth liquid point.In the face of the trend that device constantly maximizes, under the equally distributed prerequisite of gas-liquid, gas-liquid formation spray regime how is made to become the focus of research and development.
Document US4708852 describes a kind of trickle bed reactor.This reactor comprises an import pre-distributor, a gas-liquid distributor, porcelain ball bed, beds.The gas-liquid distributor of the document adopts the structure of perforate corrugated plating, certain liquid level is kept in trough, the all perforates of the lowest point, brae, summit, liquid passes from the hole of the lowest point and the hole be in subsurface brae, form laterally stream, gas then passes from summit and the hole of brae that is on liquid level.Gas and liquid, at corrugated plating lower contact, improve enterprise object uniformity.This gas-liquid distributor can provide gas-liquid at the distributing homogeneity of different angles, but the liquid level in paddy can not control, if initial gas or liquid distribution uneven, then this gas-liquid distributor is difficult to form liquid level in uniform paddy, do not reach equally distributed object, inside reactor drip poor effect, affects the reaction efficiency of trickle bed reactor.
Chinese patent CN101279229A discloses a kind of trickle bed reactor, distribution grid is provided with gas passage pipe and fluid passage pipe, gas passage pipe is made up of circular cone top cover and upright short tube, fluid passage pipe is vertical short tube, 10-100 millimeter above distribution grid is stretched out in the upper end of vertical short tube, 200-1000mm below distribution grid is stretched out in lower end, and the cross section of diverse location vertically has aperture equably.CN103212345A discloses a kind of gas-liquid distributor of hanging structure, distributor is made up of outer tube and interior pipe, outer tube is connected by gripper shoe with interior pipe, outer tube makes its top closure by cover plate, outer tube wall has the duct as gas-liquid fluid entrance, and outer tube is stay pipe, be arranged on distributor tower tray, interior pipe is hanging structure, and in its underpart, the distance of tower tray is 30-50 millimeter, is placed on outer tube by gripper shoe; Gripper shoe is one piece of annular slab between interior pipe and outer tube, is fixed by interior pipe, is hanging structure, and stops fluid to flow downward along the annular space between interior pipe and outer tube.The defect of this distributor is to belong to the application under applicable low pressure, large gas liquid ratio working condition, and for high pressure reaction assembly, in most cases the kinetic energy of gas is lower, cannot realize pumping function well and spray divergent function.
It is uniform that the gas-liquid of above-mentioned trickle bed reactor obtains to a certain extent, but interaction of gas and liquid is less, and liquid distribution mainly rill stock concentrates flowing, cannot spray with drop state, and then liquid cannot realize the initial ideal of beds is uniform.
Summary of the invention
The object of the present invention is to provide a kind of novel trickle bed reaction unit gas-liquid distributor, the defect of prior art can be overcome.The present invention is based on the combination of some calottes, the uniform design of multistage liquid, provide a kind of cost low, structure is simple, the trickle bed reaction unit gas-liquid distributor that distributed effect is good.
Gas-liquid distributor provided by the invention mainly comprises level board, calotte combining structure, inlet opening, cloth liquid cover, liquid distributor, cloth liquid baffle plate, cloth liquid cover base; Uniform some calotte combining structures on horizontal plate, calotte combining structure is that internal layer calotte embeds in level board, the outer calotte of internal layer calotte peripheral hardware, and internal layer calotte, outer calotte all have some sieve apertures, and internal layer calotte is without top cover, and outer calotte has top cover; Internal layer calotte is in the position near level board, and internal layer calotte arranges some inlet openings; Cloth liquid baffle plate bottom arranges cloth liquid cover, and cloth liquid cover arranges sieve aperture; The height of the distance from bottom level board of internal layer calotte arranges inlet opening, and the position that inlet opening is corresponding arranges cloth liquid baffle plate; If the bottom of cloth liquid cover arranges individual liquid distributor (such as at least 3), decrease doing of cloth liquid cover centre, be conducive to the even drippage of liquid.
Interior installation 3-12 liquid distributor of described cloth liquid cover.Described liquid distributor is straight tube, bend pipe or the combination of the two.
Described internal layer calotte and outer calotte are vertical vertical sieve tray.
Described cloth liquid cover base is serration type base.Sawtooth is circumferentially respectively to interior and outwards open, and angle is 30-60 °, is conducive to, from the dispersion of the liquid of cloth liquid cover outer wall landing and even drippage, gas-liquid fully being mixed and reaching equally distributed effect.
The invention provides novel trickle bed reaction unit gas-liquid distributor conveniently mounting means installation (comprising brace summer, clamp, bolt and pressing plate etc. to be arranged in trickle bed reactor).
The gas-liquid distributor of trickle bed reaction unit provided by the invention can directly apply to the technique of castor oil hydrogenation, obtains excellent effect.The present invention is widely used in the fields such as Coal Chemical Industry, oil refining, petrochemical industry, fine chemistry industry, pharmacy, grease equally.
The substantial advantage that the present invention gives prominence to and effect are described below:
1, the present invention can make gas-liquid distribute to reach good result, and resistance drop is less, can control within the scope of 150Pa-300Pa, and cloth liquid point is close, be evenly distributed, and reduces without liquid zone, thus improves the efficiency of beds, minimizing hot localised points.
2, the present invention adopts multistage liquid uniform, take into account multiple Liquid Flow and Interactions Mode, and the operating flexibility of gas-liquid is larger.
3, the present invention is because liquid distribution is mainly by liquid layer pressure, and the requirement for horizontality thus for distributor installation is lower, and enlarge-effect is less.
4, internal layer calotte of the present invention is vertical sieve aperture with outer calotte, and anti-clogging is higher, is suitable for the operating mode that liquid property is comparatively severe.
5, the present invention is easy to installation, convenient disassembly.
In a word, the present invention can overcome the defect of prior art.The present invention is based on some inside and outside calotte combinations, design concept that Liquid inject dispersion, liquid distributor secondary divide uniform, liquid drip to distribute, provide that a kind of resistance is low, anti-clogging, cost are low, structure is simple, the trickle bed reaction unit gas-liquid distributor that distributed effect is good, be widely used, there is huge economic benefit and social benefit.
Accompanying drawing explanation
Figure 1A is gas-liquid distributor structural representation of the present invention.
The inlet opening local gas-liquid state flow that Figure 1B is gas-liquid distributor shown in Figure 1A is to schematic diagram.
Fig. 1 C is gas-liquid distributor of the present invention installation site and general structure generalized section in the reactor.
Fig. 1 D is cloth liquid cover, liquid distributor and deflector locus in gas-liquid distributor of the present invention, according to Fig. 1 C E-E generalized section.
Fig. 2 A is document US4708852 drip-flow reactor schematic diagram.
Fig. 2 B is for the gas-liquid state flow of the gas-liquid distributor of the drip-flow reactor shown in Fig. 2 A is to schematic diagram.
Fig. 3 A is the trickle bed reactor schematic diagram of domestic current.
Fig. 3 B is for the gas-liquid state flow of the gas-liquid distributor of trickle bed reactor shown in Fig. 3 A is to schematic diagram.
Detailed description of the invention
The present invention is elaborated further below in conjunction with specific embodiment and accompanying drawing.The experiment of unreceipted actual conditions in embodiment, method of testing, usually conveniently condition and the condition described in handbook, or according to the condition that manufacturer advises; Equipment used, material, reagent etc., if no special instructions, all can obtain from commercial channels.
As shown in the figure, 1, outer calotte; 2, internal layer calotte; 3, cloth liquid plate washer; 4, cloth liquid cover; 5, liquid distributor; 6, serration type deflector; 7, inlet opening; 8, level board; 9 is reactor, and 10 is porcelain ball bed, and 11 is charging aperture, and 12 is beds, and 13 is discharging opening; 14 is the gas-liquid distributor of document US4708852 trickle bed reactor, and 15 is the gas-liquid distributor of existing trickle bed reactor.
Described gas-liquid distributor mounting means as shown in Figure 1 C, comprises outer calotte 1, internal layer calotte 2, cloth liquid plate washer 3, cloth liquid cover 4, liquid distributor 5, serration type deflector 6, reactor 9, charging aperture 11.
Described cloth liquid cover structure as shown in figure ip, is provided with gas-liquid distributor in reactor 9, and some cloth liquid cover 4 at distributor routed underneath, cloth liquid cover 4 connects liquid distributor 5, serration type deflector 6.
Uniform some calotte combining structures on level board 8, calotte combining structure is that internal layer calotte 2 embeds in level board 8, and arrange outer calotte 1 outside internal layer calotte 2, internal layer calotte 2, outer calotte 1 all have some sieve apertures; Internal layer calotte 2 is in the position near level board 8, and internal layer calotte 2 arranges some inlet openings 7, and cloth liquid baffle plate 3 bottom arranges cloth liquid cover 4, and cloth liquid cover 4 arranges sieve aperture; The height of the distance from bottom level board 8 of internal layer calotte 2 arranges inlet opening 7, and the position of inlet opening 7 correspondence arranges cloth liquid baffle plate 3; If the bottom of cloth liquid cover 4 arranges individual liquid distributor 5(such as at least 3), decrease doing of cloth liquid cover 4 centre, be conducive to the even drippage of liquid.
3-12 root liquid distributor is installed in cloth liquid cover
.
Described internal layer calotte and outer calotte are vertical vertical sieve tray, and internal layer calotte is without top cover, and outer calotte has top cover;
Described cloth liquid cover base is processed to serration type deflector, and the shape of every bar deflector can be triangle, trapezoidal, strip.Sawtooth respectively to interior and outside stretching, extension, is conducive to the dispersion from the liquid of cloth liquid cover outer wall landing and even drippage according to odd and even number.
Described internal layer calotte 2 to embed on level board and welds.
Described inlet opening can be 2-8.
Distance between described internal layer calotte 2 and outer calotte 1 is 10-50mm.
Described sieve aperture is 2-9 row, and often arrange 4-20, sieve diameter is 4-12 mm.
The workflow of gas-liquid distributor provided by the invention is described in detail as follows:
The gas-liquid mixture fallen from reactor 9 top falls: a part directly falls into horizontal plate 8, enters in internal layer calotte 2 by the inlet opening of internal layer calotte 2; A part drops on above outer calotte 1, liquid is by the downward landing of sidewall of outer calotte 1, the gas entered with the sieve aperture by outer layer cover 1 interacts, gas-liquid mixed, transverse injection, to flow downward, the gas-liquid mixture of part transverse injection is ejected on internal layer calotte 2, secondary impact, fragmentation, Surface Renewal occur, and most of liquid is fallen on horizontal plate 8, and a small amount of liquid enters internal layer cover 2 with drop state and flows down in cloth liquid cover 4.
Inlet opening 7 is set, the liquid in inflow internal layer calotte 2 is made to pass through (cloth liquid baffle plate 3) water conservancy diversion, liquid is made to enter into cloth liquid cover 4 along internal layer calotte 2 bottom, and flow downward along the sieve aperture of cloth liquid cover 4, be divided into three parts and fall: gas drives a part of Liquid inject, dispersion and going out at sieve aperture place; Part liquid falls along cloth liquid cover 4 inwall; Part liquid is along the landing of cloth liquid cover 4 outer wall, and after flowing to serration type deflector, liquid stream is guided separately, forms multiply liquid stream and flows along the surface of deflector, be scattering into beds.
Multitube secondary liquid distributor is set bottom cloth liquid cover 4, namely at the multiple liquid distributor of cloth liquid cover 4 bottom design, makes to fall liquid bottom cloth liquid cover by liquid distributor 5 water conservancy diversion, be evenly distributed in beds from liquid distributor 5 lower end, reduce without liquid zone.
The effect test of gas-liquid distributor provided by the invention:
Adopt one-level castor oil hydrogenation as the technique of performance test, under identical technological parameter, with same reactor and catalyst, change dissimilar gas-liquid distributor, after detection hydrogenation, the iodine number of product, both can verify the distributed effect of distributor to gas-liquid two-phase.
The present invention is applied to the process conditions of castor oil hydrogenation: system hydrogen exchange, and catalyst is Raney's nickel catalyst, and the diatomite of use amount is carrier.Selecting catalyst consumption is 2%, and at 1.15MPa (G) pressure, reaction temperature is 150-180 DEG C.
Application Example 1
Shown in Figure 1A, 1B, 1C, 1D, the iodine number of initial castor oil is greater than 85 grams of I
2/ 100 grams of Oil, hydrogen equals 320 with hydrogen-oil ratio and enters trickle bed reactor, adopt copper nickel binary catalyst, employing diatomite is carrier, hydrogenation reactor adopts gas-liquid distributor of the present invention, outer layer cover diameter is 80mm, and percent opening is 20%, and internal layer cover diameter is 60mm, percent opening is 15%, inlet opening number is 4, and diameter is 3mm, and cloth liquid cover diameter is identical with internal layer cover, the percent opening 10% of cloth liquid cover, 3 liquid distributors are installed in the bottom of cloth liquid cover, and 8 serration type deflectors are designed in cloth liquid cover lower end, and experiment proves that the castor oil iodine number after hydrogenation is≤2.8 grams of I
2/ 100 grams of Oil.
Application Example 2
Shown in Figure 1A, 1B, 1C, 1D, the iodine number of initial castor oil is greater than 85 grams of I
2/ 100 grams of Oil, hydrogen equals 320 with hydrogen-oil ratio and enters trickle bed reactor, adopt copper nickel binary catalyst, employing diatomite is carrier, hydrogenation reactor adopts gas-liquid distributor of the present invention, outer layer cover diameter is 100mm, percent opening is 20%, internal layer cover diameter is 80mm, percent opening is 15%, inlet opening number is 6, diameter is 2mm, cloth liquid cover diameter is identical with internal layer cover, the percent opening 12% of cloth liquid cover, 4 liquid distributors are installed in the bottom of cloth liquid cover, 10 serration type deflectors are designed in cloth liquid cover lower end, experiment proves that the castor oil iodine number after hydrogenation is≤2.3 grams of I
2/ 100 grams of Oil.
Application Example 3
By Figure 1A, 1B, 1C, shown in 1D, the iodine number of initial castor oil is greater than 85 grams of I2/100 gram of Oil, hydrogen equals 320 with hydrogen-oil ratio and enters trickle bed reactor, adopt copper nickel binary catalyst, employing diatomite is carrier, hydrogenation reactor adopts gas-liquid distributor of the present invention, outer layer cover diameter is 70mm, percent opening is 20%, internal layer cover diameter is 40mm, percent opening is 15%, inlet opening number is 3, diameter is 2mm, cloth liquid cover diameter is identical with internal layer cover, the percent opening 15% of cloth liquid cover, 3 liquid distributors are installed in the bottom of cloth liquid cover, 6 serration type deflectors are designed in cloth liquid cover lower end, experiment proves that the castor oil iodine number after hydrogenation is≤2.5 grams of I
2/ 100 grams of Oil.
Comparative example 1
Shown in Fig. 2 A, 2B, the iodine number of initial castor oil is greater than 85 grams of I
2/ 100 grams of Oil, hydrogen equals 320 with hydrogen-oil ratio and enters trickle bed reactor, catalyst adopts copper nickel binary catalyst to adopt diatomite to be carrier, adopts the trickle bed reactor of document US 4708852, and the castor oil iodine number after experiment proves hydrogenation is :≤3.0 grams of I
2/ 100 grams of Oil.
Comparative example 2
Shown in Fig. 3 A, 3B, the iodine number of initial castor oil is greater than 85 grams of I
2/ 100 grams of Oil, hydrogen equals 320 with hydrogen-oil ratio and enters trickle bed reactor, and adopt copper nickel binary catalyst, employing diatomite is carrier, adopts the trickle bed reactor of domestic current, and the castor oil iodine number after experiment proves hydrogenation is :≤3.5 grams of I
2/ 100 grams of Oil.
Proved by test, castor oil iodine number sequence after hydrogenation is: comparative example 2 > comparative example 1 > embodiment 1 > embodiment 3 > embodiment 2, and then illustrate that distributor performance is on the impact of hydrogenation effect, the cloth liquid better performances of gas-liquid distributor of the present invention, illustrate for the present invention, the number of suitable liquid distributor and the number of serration type deflector play an important role equally simultaneously.Therefore, the present invention is that a kind of resistance is low, anti-clogging, cost are low, and structure is simple, the trickle bed reaction unit gas-liquid distributor that distributed effect is good.
Claims (10)
1. a gas-liquid distributor, is characterized in that mainly comprising horizontal plate, calotte combining structure, inlet opening, cloth liquid cover, liquid distributor, cloth liquid baffle plate, cloth liquid cover base; Uniform some calotte combining structures on horizontal plate, calotte combining structure is that internal layer calotte embeds in level board, the outer calotte of internal layer calotte peripheral hardware, and internal layer calotte, outer calotte all have some sieve apertures, and internal layer calotte is without top cover, and outer calotte has top cover; Internal layer calotte is in the position near horizontal plate, and internal layer calotte arranges some inlet openings, and inlet opening place correspondence is established and installed cloth liquid baffle plate, and cloth liquid baffle plate bottom arranges cloth liquid cover, and cloth liquid cover arranges sieve aperture; The certain altitude of the distance from bottom level board of internal layer calotte arranges inlet opening, and the position corresponding with inlet opening arranges cloth liquid baffle plate; If the bottom of cloth liquid cover arranges individual liquid distributor.
2. gas-liquid distributor according to claim 1, is characterized in that described internal layer calotte and outer calotte are vertical vertical sieve tray.
3. gas-liquid distributor according to claim 1, is characterized in that interior installation 3-12 liquid distributor of described cloth liquid cover; Liquid distributor is straight tube, bend pipe or the combination of the two.
4. gas-liquid distributor according to claim 1, is characterized in that described cloth liquid cover base is serration type deflector, and the shape of every bar deflector can be triangle, trapezoidal, strip.
5. gas-liquid distributor according to claim 4, it is characterized in that described sawtooth circumferentially respectively to interior and outwards open, angle is 30-60 °.
6. gas-liquid distributor according to claim 1, is characterized in that described internal layer calotte to embed on level board and to weld.
7. gas-liquid distributor according to claim 1, it is characterized in that the height of described inlet opening distance level board is 5-50mm, its number is 3-12.
8. gas-liquid distributor according to claim 1, is characterized in that the distance between described internal layer calotte and outer calotte is 10-50mm.
9. gas-liquid distributor according to claim 1, it is characterized in that described sieve aperture is 2-9 row, often arrange 4-20, diameter is 4-12 mm.
10. an application for gas-liquid distributor as claimed in claim 1, is characterized in that it is applied to the technique of castor oil hydrogenation.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510060815.3A CN104667831B (en) | 2015-02-05 | 2015-02-05 | Trickle bed reaction unit gas-liquid distributor |
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| CN201510060815.3A CN104667831B (en) | 2015-02-05 | 2015-02-05 | Trickle bed reaction unit gas-liquid distributor |
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| CN104667831B CN104667831B (en) | 2016-08-24 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1186451A (en) * | 1995-06-02 | 1998-07-01 | 国际壳牌研究有限公司 | Horizontal tray and column for contacting gas and liquid |
| CN101279229A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Trickle bed reactor |
| CN101954263A (en) * | 2010-04-20 | 2011-01-26 | 南通泰禾化工有限公司 | Trickle bed equipment for preparing m-Metaxylenediamine |
| CN205042449U (en) * | 2015-02-05 | 2016-02-24 | 天津奥展兴达化工技术有限公司 | Trickle bed reaction unit gas -liquid distributor |
-
2015
- 2015-02-05 CN CN201510060815.3A patent/CN104667831B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1186451A (en) * | 1995-06-02 | 1998-07-01 | 国际壳牌研究有限公司 | Horizontal tray and column for contacting gas and liquid |
| CN101279229A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Trickle bed reactor |
| CN101954263A (en) * | 2010-04-20 | 2011-01-26 | 南通泰禾化工有限公司 | Trickle bed equipment for preparing m-Metaxylenediamine |
| CN205042449U (en) * | 2015-02-05 | 2016-02-24 | 天津奥展兴达化工技术有限公司 | Trickle bed reaction unit gas -liquid distributor |
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