CN204710289U - A kind of bubble tower gas-liquid reactor - Google Patents
A kind of bubble tower gas-liquid reactor Download PDFInfo
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- CN204710289U CN204710289U CN201520325634.4U CN201520325634U CN204710289U CN 204710289 U CN204710289 U CN 204710289U CN 201520325634 U CN201520325634 U CN 201520325634U CN 204710289 U CN204710289 U CN 204710289U
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Abstract
The utility model relates to a kind of bubble tower gas-liquid reactor, comprise tower body, vapor distributor and liquid phase distributor, it is characterized in that, also comprise the anti-medial rotation part being placed in and there is between vapor distributor and liquid phase distributor damping action, the gaseous phase outlet place of described tower body is provided with foam removal net, the liquid-phase outlet place of described tower body is provided with coalescent pack, dividing plate is provided with on described tower body top, the beneficial effects of the utility model are: adopt microvesicle generators can produce the minute bubbles of diameter 0.5-50mm, increase the contact area of gas-liquid two-phase, reduce the perturbation action that bubble produces; Arrange anti-medial rotation part, there is certain damping action in fluid flow direction, is conducive to the mass transfer enhancement between gas-liquid; Tower top dividing plate arranges static Disengagement zone, the third product of light component can be climbed over dividing plate, leaves standstill and separates, thus separate with bubble.
Description
Technical field
The utility model relates to a kind of bubble tower, belongs to the gas-liquid mass transfer (contact) equipment of chemical industry and environmental technology field, can be widely used in the technical process such as the distillation of the industries such as chemical industry, environmental protection, smelting, light industry, absorption, separation, washing, purification.
Background technology
Gas-liquid reaction process refers to that a reactant is in gas phase, and another is in liquid phase, and vapor-phase reactant need enter liquid phase and could react; Or two reactants are all in gas phase, but the catalyst exposure that need enter liquid phase and liquid phase could react.Very similar to MODEL OF CHEMICAL ABSORPTION PROCESS.
A large amount of equipment is had to adopt the mode of gas-liquid contact to complete chemical reaction process in petroleum chemical industry.Gas liquid phase reactor can be divided into by liquid phase contact form:
Gas is with bubble shape dispersion bubbling column reactor in the liquid phase, stirring bubbling tank reactor and plate-type reactor;
Liquid is with droplet-like dispersion spraying in the gas phase, injection and Wen's reactor etc.;
Liquid carries out the packed tower reactor and falling film reactor etc. that contact with membranaceous motion and gas phase.
Packed tower, plate column, spray tower etc. are applicable to moment, fast and the reaction of middling speed, and in tower, liquid phase disturbance is violent, is not suitable for slow reaction process, and cannot be separated producing in course of reaction the third product.In above-mentioned tower, solubility is not high in a liquid for gas, be difficult to accomplish that gas is to the efficient mass transfer in liquid, gas-liquid two-phase haptoreaction is usually run into abundant not in commercial Application, gas effciency is not high, the reason such as in liquid phase dissolved gases concentration is on the low side, thus making production cost higher, resource utilization is on the low side.
Traditional bubble tower utilizes simple tubular type punching type gas distributor, produces bubble diameter and reaches several even tens centimetres, although be applicable to slow reaction process, in tower, liquid dispersion is serious, and bubble easily produces coalescence, and reaction efficiency is lower.For slow reaction process, chemical reaction energy force rate diffusivity is low, and chemical reaction mainly carries out in liquid phase main body, is dynamics Controlling.
The way of a lot of strengthening gas-liquid mixed contacts of current research, as increased pressure in tower, adopt turbine-type mixer, mechanical impellor stirring etc. in tower, the method of these mechanical enhancers, energy consumption and expense larger, be difficult to extensive use, and need the chemical process keeping static reaction state to be separated third product can produce strong perturbation action to some, affect the separating effect of reaction result.Also have some to adopt the method for external force fields strengthening gas-liquid contacts mixing, as electric field-enhanced, ultrasonic wave excitation etc., be all wish in reactor, produce more minute bubbles, increase the contact area between gas-liquid, but equipment investment thus significantly will improve.
Bubble flow gas liquid reaction is widely used in gas-liquid two-phase reaction, removing harmful components, the chemical process such as utility in gas recovery in petroleum chemical industry.Bubble flow gas liquid reaction, not only at chemical field, also obtain at field of Environment Protection and applies widely, to process and ozone purification drinking water etc. as adopted By Bubble-floating Method to sewage.
In bubble tower, gas blasts liquid layer by distributor keyhole formation bubble.The empty tower gas velocity of gas determines the phase contact area of reaction, void fraction and back-mixing degree.Directly affect mass-and heat-transfer coefficient until reaction result.So the research size of bubble, the rate of climb, void fraction, disturbance and back-mixing degree, phase contact area and fluid resistance etc., have great significance to the analysis of bubbling column reactor, control and calculating.
Utility model content
For the present situation of above-mentioned prior art, technical problem to be solved in the utility model is to provide
A kind of gas that can improve is to the mass-transfer efficiency in liquid, raising gas liquid reaction speed, the equipment investment of reduction gas liquid reaction technique and the gas-liquid contact reaction device of operating cost.
The utility model solves the problems of the technologies described above adopted technical scheme: a kind of bubble tower gas-liquid reactor, comprise tower body, vapor distributor and liquid phase distributor, also comprise the anti-medial rotation part being placed in and there is between vapor distributor and liquid phase distributor damping action, the gaseous phase outlet place of described tower body is provided with foam removal net, the liquid-phase outlet place of described tower body is provided with coalescent pack, is provided with dividing plate on described tower body top.
Further, described vapor distributor comprises microvesicle generators and the support frame for fixing described microvesicle generators, the fixing orifice plate that described microvesicle generators comprises housing and offsets with described housing, described fixing orifice plate lower surface is provided with the micropore distribution grid be embedded in this fixing orifice plate, described housing cavity is provided with erosion control baffle plate, and described housing and support frame are threaded connection.
Further, described anti-medial rotation part comprises at least one group of transverse baffle and at least one group of longitudinal baffle and is interspersed and steppedly upwards arranges.
Further, check valve is equipped with in the gas phase import of described vapor distributor and blowing medium entrance location.
Further, hump gripper shoe is provided with in described housing.
Further, the described support frame anti-mixed baffle plate that is provided with that Open Side Down for preventing decline liquid back-mixing.
Further, described micropore distribution grid is silk screen sintering plate, powder sintered plate, boring steel plate, ceramic corundum sintered plate or high-molecular diaphragm.
Compared with prior art, the beneficial effects of the utility model are: adopt microvesicle generators can produce the minute bubbles of diameter 0.5-50mm, increase the contact area of gas-liquid two-phase, reduce the perturbation action that bubble produces; Arrange anti-medial rotation part, there is certain damping action in fluid flow direction, is conducive to the mass transfer enhancement between gas-liquid; Tower top dividing plate arranges static Disengagement zone, the third product of light component can be climbed over dividing plate, leaves standstill and separates, thus separate with bubble.
Accompanying drawing explanation
Fig. 1 is the overall structure schematic diagram of a kind of bubble tower gas-liquid reactor of the utility model;
Fig. 2 is the structural representation of the microvesicle generators of a kind of bubble tower gas-liquid reactor of the utility model;
Fig. 3 is the top view of the anti-medial rotation part of a kind of bubble tower of the utility model gas-liquid reactor;
Fig. 4 is the liquid phase dispensing arrangement schematic diagram of a kind of bubble tower gas-liquid reactor of the utility model;
Fig. 5 is the vapor distributor structural representation of a kind of bubble tower gas-liquid reactor of the utility model.
Detailed description of the invention
Below in conjunction with the accompanying drawing in the utility model embodiment, be clearly and completely described the technical scheme in the utility model embodiment, obviously, described embodiment is only the utility model part embodiment, instead of whole embodiments.Based in the utility model being embodiment, those of ordinary skill in the art are not making the every other embodiment obtained under creative work prerequisite, all belong to the scope of the utility model protection.
As Figure 1-5, a kind of bubble tower gas-liquid reactor, comprise tower body 1 and be placed in foam removal net 2 in tower body 1, vapor distributor 4, liquid phase distributor 3, anti-medial rotation part 7 and coalescent pack 5, the gaseous phase outlet place of tower body 1 is located at by described foam removal net 2, for removing the liquid phase of carrying secretly in divided gas flow, described anti-medial rotation part 7 is placed in the middle part of tower body 1, prevents the back-mixing in liquid phase descent and bubble uphill process, disturbance, and prevents the coalescence in bubble uphill process; The upper/lower terminal of described anti-medial rotation part 7 arranges liquid phase distributor 3 and vapor distributor 4 respectively.More even for making liquid phase spray, as shown in Figure 3, the nozzle of described liquid phase distributor 3 is equally spaced in tower body 1 cross section; Described vapor distributor 4 comprises microvesicle generators 41 and the support frame 42 for fixing described microvesicle generators 41, the fixing orifice plate 411 that described microvesicle generators 41 comprises housing 414 and offsets with described housing 414, described fixing orifice plate 411 lower surface is provided with the micropore distribution grid 412 be embedded in this fixing orifice plate 411, described housing 414 inner chamber is provided with erosion control baffle plate 415, be provided with hump gripper shoe 413 in described housing 414, described housing 414 is threaded connection with support frame 42.For preventing decline liquid back-mixing, at described support frame 42, be provided with that Open Side Down for anti-mixed baffle plate 43.
For ease of third product is separated separately, is provided with dividing plate 6 on described tower body 1 top, forms static Disengagement zone, the third product of light component can be climbed over dividing plate 6, leave standstill with bubble and separate, thus separate.
For promoting the mass transfer enhancement between gas-liquid, described anti-medial rotation part 7 comprises at least one group of transverse baffle 71 and at least one group of longitudinal baffle 72 and is interspersed and steppedly upwards arranges, have certain damping action at fluid flow direction, avoid central fluid flow velocity in void tower large, surrounding is little near tower wall flow velocity; Also by liquid in tower longitudinally separately, prevent from forming disturbance, avoid bubble coalescence, gas liquid interfacial area can not reduce anti-medial rotation part 7, increases the time of staying of bubble simultaneously, is conducive to the mass transfer enhancement between gas-liquid.
For preventing liquid phase from pouring in down a chimney to vapor delivery line, be equipped with check valve 44 in the gas phase import of described vapor distributor 4 and blowing medium position.
Described micropore distribution grid 412 is silk screen sintering plate, powder sintered plate, boring steel plate, ceramic corundum sintered plate or high-molecular diaphragm.
Last it is noted that above embodiment is only in order to illustrate technical scheme of the present invention, be not intended to limit; Although with reference to previous embodiment to invention has been detailed description, it will be understood by those of skill in the art that it still can be modified to the technical scheme described in foregoing embodiments, or wherein portion of techniques feature is replaced on an equal basis; And these amendments or replacement, do not make the essence of appropriate technical solution depart from spirit and the scope of various embodiments of the present invention technical scheme.
Claims (7)
1. a bubble tower gas-liquid reactor, comprise tower body (1), vapor distributor (4) and liquid phase distributor (3), it is characterized in that, also comprise the anti-medial rotation part (7) being placed in and there is between vapor distributor (4) and liquid phase distributor (3) damping action, the gaseous phase outlet place of described tower body (1) is provided with foam removal net (2), the liquid-phase outlet place of described tower body (1) is provided with coalescent pack (5), is provided with dividing plate (6) on described tower body (1) top.
2. a kind of bubble tower gas-liquid reactor according to claim 1, it is characterized in that, described vapor distributor (4) comprises microvesicle generators (41) and the support frame (42) for fixing described microvesicle generators, the fixing orifice plate (411) that described microvesicle generators (41) comprises housing (414) and offsets with described housing (414), described fixing orifice plate (411) lower surface is provided with the micropore distribution grid (412) be embedded in this fixing orifice plate (411), described housing (41) inner chamber is provided with erosion control baffle plate (415), described housing (41) and support frame (42) are threaded connection.
3. a kind of bubble tower gas-liquid reactor according to claim 1, it is characterized in that, described anti-medial rotation part (7) comprises at least one group of transverse baffle (71) and at least one group of longitudinal baffle (72) and is interspersed and steppedly upwards arranges.
4. a kind of bubble tower gas-liquid reactor according to claim 1, is characterized in that, is equipped with check valve (44) in the gas phase import of described vapor distributor (4) and blowing medium entrance location.
5. a kind of bubble tower gas-liquid reactor according to claim 2, is characterized in that, is provided with hump gripper shoe (413) in described housing (414).
6. a kind of bubble tower gas-liquid reactor according to claim 2, is characterized in that, described support frame (42) is provided with that Open Side Down for the anti-mixed baffle plate (43) preventing decline liquid back-mixing.
7. a kind of bubble tower gas-liquid reactor according to claim 2, is characterized in that, described micropore distribution grid (412) is silk screen sintering plate, powder sintered plate, boring steel plate, ceramic corundum sintered plate or high-molecular diaphragm.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520325634.4U CN204710289U (en) | 2015-08-08 | 2015-08-08 | A kind of bubble tower gas-liquid reactor |
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| CN201520325634.4U CN204710289U (en) | 2015-08-08 | 2015-08-08 | A kind of bubble tower gas-liquid reactor |
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| CN204710289U true CN204710289U (en) | 2015-10-21 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106622045A (en) * | 2016-11-30 | 2017-05-10 | 南京工业大学 | Method and device for improving reaction efficiency of bubble tower by micro-nano bubbles |
| CN106732308A (en) * | 2017-01-13 | 2017-05-31 | 浙江大学 | A kind of micro- bubbling gas-liquid reactor |
| CN107890758A (en) * | 2017-11-09 | 2018-04-10 | 中海油天津化工研究设计院有限公司 | A kind of outer circulation type electrochemistry sewage treatment plant deodoration system and method |
| CN108404699A (en) * | 2017-02-09 | 2018-08-17 | 埃尔微尘科技（北京）有限公司 | A kind of Liqiud-gas mixing device |
| CN110054768A (en) * | 2019-05-30 | 2019-07-26 | 上海欧勒奋生物科技有限公司 | A method of improving out-phase contacting efficiency |
| CN110183643A (en) * | 2019-05-30 | 2019-08-30 | 上海欧勒奋生物科技有限公司 | A kind of fluorinated systems of perfluoropolyether unstable end-group |
| CN110420609A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of micro/nano-scale multiphase flow process intensification reaction unit |
| CN113663635A (en) * | 2021-09-10 | 2021-11-19 | 中国石油大学(华东) | Gas-liquid mass transfer equipment for enhancing mass transfer rate of carbonization reaction |
| CN114854536A (en) * | 2022-06-14 | 2022-08-05 | 南京工业大学 | Micro-interface reinforced efficient bioreactor for synthesis gas conversion and application thereof |
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2015
- 2015-08-08 CN CN201520325634.4U patent/CN204710289U/en active Active
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106622045A (en) * | 2016-11-30 | 2017-05-10 | 南京工业大学 | Method and device for improving reaction efficiency of bubble tower by micro-nano bubbles |
| CN106732308A (en) * | 2017-01-13 | 2017-05-31 | 浙江大学 | A kind of micro- bubbling gas-liquid reactor |
| CN108404699A (en) * | 2017-02-09 | 2018-08-17 | 埃尔微尘科技（北京）有限公司 | A kind of Liqiud-gas mixing device |
| CN107890758B (en) * | 2017-11-09 | 2020-11-24 | 中海油天津化工研究设计院有限公司 | External circulation type electrochemical sewage treatment plant deodorization system and method |
| CN107890758A (en) * | 2017-11-09 | 2018-04-10 | 中海油天津化工研究设计院有限公司 | A kind of outer circulation type electrochemistry sewage treatment plant deodoration system and method |
| CN110183643B (en) * | 2019-05-30 | 2021-12-14 | 上海欧勒奋生物科技有限公司 | Fluorination system of unstable terminal group of perfluoropolyether |
| CN110183643A (en) * | 2019-05-30 | 2019-08-30 | 上海欧勒奋生物科技有限公司 | A kind of fluorinated systems of perfluoropolyether unstable end-group |
| CN110054768A (en) * | 2019-05-30 | 2019-07-26 | 上海欧勒奋生物科技有限公司 | A method of improving out-phase contacting efficiency |
| CN110054768B (en) * | 2019-05-30 | 2022-01-04 | 上海欧勒奋生物科技有限公司 | Method for improving heterogeneous contact efficiency |
| CN110420609A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of micro/nano-scale multiphase flow process intensification reaction unit |
| CN110420609B (en) * | 2019-09-02 | 2024-02-20 | 杭州烃能科技研究有限公司 | Micro-nano scale multiphase flow process strengthening reaction device |
| CN113663635A (en) * | 2021-09-10 | 2021-11-19 | 中国石油大学(华东) | Gas-liquid mass transfer equipment for enhancing mass transfer rate of carbonization reaction |
| CN114854536A (en) * | 2022-06-14 | 2022-08-05 | 南京工业大学 | Micro-interface reinforced efficient bioreactor for synthesis gas conversion and application thereof |
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