CN101653711A - Multilevel deflector-type bubble tower reactor and production process - Google Patents
Multilevel deflector-type bubble tower reactor and production process Download PDFInfo
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- CN101653711A CN101653711A CN200910307444A CN200910307444A CN101653711A CN 101653711 A CN101653711 A CN 101653711A CN 200910307444 A CN200910307444 A CN 200910307444A CN 200910307444 A CN200910307444 A CN 200910307444A CN 101653711 A CN101653711 A CN 101653711A
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Abstract
The invention relates to a multilevel deflector-type bubble tower reactor and a production process. A reaction section is formed by connecting a reaction column with a deflector; a liquid-phase distributor is arranged at the inner upper end of a tower body; a microbubble generator is arranged at the inner lower end of the tower body; a tower top is provided with an air outlet, and a tower bottom is provided with a liquid outlet; the upper end of the reaction section is provided with a liquid-phase feeding hole, the lower end of the reaction section is provided with an air-phase feeding hole; and more than two levels of reaction sections are arranged. The production process comprises the following steps: pumping liquid-phase raw materials into a tower through a pump by the liquid-phase distributor so that the liquid-phase raw materials sequentially flow downwards to all the levels of the reaction sections under the action of gravity; pumping gas-phase raw materials into the tower through a compressor by the microbubble generator; and enabling microvesicles to move upwards under the action of buoyancy and reversely contact and react with the liquid-phase raw materials under the leading action of the deflector so that liquid-phase reaction products flow out from the tower bottom, and gas-phase reaction products are exhausted from the tower top. The invention has the advantages ofsmall investment, little energy consumption, small floor area, high conversion rate and wide suitability.
Description
Technical field
The present invention relates to a kind of multilevel deflector-type bubble tower reactor and production technology, belong to the improvement of consersion unit and production technology in the chemical engineering unit operation.
Background technology
At present, the normal gas-liquid reaction apparatus that adopts is bubbling style reactor or stirred-tank reactor in the industrial production, this two quasi-traditions reactor reaction efficient is low, equipment is huger usually, floor space is big like this, one-time investment expense height, operating cost is also higher, and application is subjected to the restriction of reaction system.
The multi-stage circular flow reactor that comes based on the bubbling style reactor development, be multilevel deflector tube and the inner member that adopts different structure, make gas phase and liquid phase realize that big circulation overlaps flowing of little circulation, improve the two-phase flow situation, improve mass-transfer efficiency, but its defective is the arbitrary section place at body of the tower, gas phase and liquid phase have only formed one deck circulation, promptly only exist a big circulation to overlap little circulation, cause the annular space gas holdup still low, effectively mass transfer area is not very big, and the reactor utilization rate is low, and overall reactor efficient is low.
Summary of the invention
In order to overcome the above-mentioned deficiency of existing apparatus and technology, the object of the present invention is to provide a kind of multilevel deflector-type bubble tower reactor and production technology.
The present invention is realized by following technical proposals:
A kind of multilevel deflector-type bubble tower reactor of the present invention comprises conversion zone, deflector, liquid phase distributor and microvesicle generators; Conversion zone connects deflector by reaction column and constitutes; Liquid phase distributor is positioned at the tower body upper end, and microvesicle generators is positioned at the tower body lower end; Top of tower is provided with exhaust outlet, and tower bottom is provided with leakage fluid dram, is provided with the liquid phase feeding mouth in the conversion zone upper end, is provided with the gas-phase feed mouth in the conversion zone lower end; Conversion zone is more than the two-stage.Reaction column is structured packing, at least 3 on every order reaction post; The placement direction of adjacent two-stage reaction section internal reaction post is perpendicular.
The production technology of multilevel deflector-type bubble tower reactor of the present invention is squeezed into liquid phase feed in the tower via liquid phase distributor by pump, and under the effect of gravity, raw material flows through conversion zones at different levels downwards successively; Phase feed is squeezed in the tower via microvesicle generators by compressor, and under buoyancy function, microvesicle moves upward, with the liquid phase feed counter current contacting, and issue in the guide functions of deflector and to give birth to corresponding reaction, liquid-phase reaction product is discharged at the bottom of tower, and the gas-phase reaction product is discharged from cat head.
The progression of conversion zone decide according to conversion ratio and yield that reaction requires to reach, can be divided into two-stage, three grades or more, and conversion ratio and yield requirement are high more, and the progression of employing is many more.Every layer of interior evenly reaction column of the built-in structured packing of vertical parallel placement some of conversion zone, the concrete number of reaction column is decided according to conversion ratio and yield that reaction requires to reach, and conversion ratio and yield are high more, and the number of reaction column is many more.Every reaction column below correspondence is provided with a deflector, and the placement direction of adjacent two layers conversion zone internal reaction post is perpendicular;
Reacting gas enters conversion zone through microvesicle generators, under the effect of the jet power of gas and density contrast, microbubble drives surrounding liquid and moves upward, and carries out circulation movement fast round the space of differential responses post and intercolumniation, forms the flow regime that many big circulation overlap little circulation.
Multilevel deflector-type bubble tower reactor of the present invention, its advantage is: invest little, energy consumption is little, floor space is little; Hold the difference of holding tolerance in tolerance and the annular space in the reaction column of every layer of conversion zone and cause circulating of fluid, help phase feed and fully contact with liquid phase feed; The bubble diameter that adopts microvesicle generators to produce is little, and number is many, and therefore under same flow, specific area is bigger, and the probability increase with the liquid phase feed contact improves the outlet conversion ratio; Multilevel deflector-type bubble tower reactor provides higher reaction height, make the stroke of bubble in reaction tower long, the time of staying of raw material in reactor is longer, just can realize the abundant reaction of gas-liquid two-phase in less container, conversion ratio improves, the also corresponding raising of product outlet purity; Can satisfy the large-batch processing requirement preferably, because it is simple in structure, cost is low, has extensive applicability simultaneously.
Description of drawings
Fig. 1 is multilevel deflector-type bubble tower reactor and process chart thereof.
The specific embodiment
As shown in Figure 1, multilevel deflector-type bubble tower reactor of the present invention, mainly by microvesicle generators 5, liquid phase distributor 9, conversion zone 11 and deflector 7 constitute.The reaction column 8 of the even built-in structured packing of vertical parallel placement in every order reaction section, every reaction column below correspondence is provided with a deflector 7, and the placement direction of adjacent two layers conversion zone internal reaction post is perpendicular.Above conversion zone, be provided with liquid phase distributor, in succession material liquid inlet of liquid phase distributor, the equidistant level in the below of conversion zone is equipped with the microvesicle generators 5 of some, the microvesicle generators gas phase inlet 3 of ining succession.Be provided with gas vent 10 at the synthetic tower cat head, be provided with product outlet 6 at the bottom of the tower.
Material liquid inlet 1 is squeezed into liquid phase distributor 9 through feedstock pump 2, and the back that is evenly distributed evenly flows into conversion zone 11, all comprises the reaction column 8 of the built-in structured packing of some in every layer of conversion zone; Raw material is from entering the mouth 3, behind compressed machine 4, the microvesicle generators 5, squeeze in the tower, react under deflector 7 and certain reaction condition effect with the liquid phase feed liquid that flows from the top down, generate liquid product, the intact liquid phase feed of liquid product and unreacted is discharged from product outlet 6, and the intact phase feed of unreacted is discharged from gaseous phase outlet 10.
Introduce several specific embodiment of the present invention below, but do not limit to and these several reactions, multilevel deflector-type bubble tower reactor of the present invention is applicable to the normal gas-liquid system that adopts in the existing industrial production.
Embodiment 1: chlorine and toluene reaction generate benzotrichloride, and its reaction equation is toluene+chlorine → benzotrichloride.As shown in Figure 1, utilize multilevel deflector-type bubble tower reactor production technology of the present invention, at first under normal pressure, raw material toluene and catalyst ammonium chloride are mixed, and be heated to 140 ℃, squeeze into liquid phase distributor 9 through feedstock pump 2 from material liquid inlet 1, evenly inflow conversion zone 11 of back is evenly distributed, according to the reaction yield requirement, adopt the fourth-order reaction section, all comprise the reaction column 8 of three built-in structured packings in every order reaction section; Raw material chlorine is from entering the mouth 3, behind compressed machine 4, the microvesicle generators 5, squeeze in the tower, react under deflector 7 and catalyst action with the toluene that flows from the top down, generate benzotrichloride, the intact toluene of product and unreacted is discharged from product outlet 6, and the intact chlorine of byproduct hydrogen chloride and unreacted is discharged from gaseous phase outlet 10.The result shows: adopt multilevel deflector-type bubble tower reactor, the yield of raw material toluene improves about 10% than traditional multi-stage circular flow reactor.
Embodiment 2: p-nitroacetophenone synthetic, its reaction equation is to nitro ethylbenzene+air → p-nitroacetophenone.As shown in Figure 1, at first under 5atm, raw material nitro ethylbenzene and catalyst acetic acid salt are mixed, and be heated to 140 ℃, squeeze into liquid phase distributor 9 from material liquid inlet 1 through feedstock pump 2, the back that is evenly distributed evenly flows into conversion zone 11, according to the reaction yield requirement, adopt the third-order reaction section, all comprise the reaction column 8 of two built-in structured packings in every order reaction section; Raw air is from entering the mouth 3, behind compressed machine 4, the microvesicle generators 5, squeeze in the tower, react under deflector 7 and catalyst action with the nitro ethylbenzene that flows from the top down, generate p-nitroacetophenone, the intact nitro ethylbenzene of product and unreacted is discharged from product outlet 6, and the intact air of unreacted is discharged from gaseous phase outlet 10.The result shows: adopt multilevel deflector-type bubble tower reactor, the yield of raw material nitro ethylbenzene improves about 7% than traditional multi-stage circular flow reactor.
More than two embodiment prove: multilevel deflector-type bubble tower reactor has greater advantage than traditional circulation flow reactor really aspect gas liquid reaction, and, the reaction column radical is many more in the order of reaction and each level, feed stock conversion and yield are high more, but cost is also big more simultaneously, therefore should take all factors into consideration yield and cost two aspect factors in actual applications, find out the optimal value of reaction column radical in progression and each grade, make profit maximization.
A kind of multilevel deflector-type bubble tower reactor and production technology that the present invention proposes, be described in detail, person skilled obviously can be in not breaking away from content of the present invention, spirit and scope to technological process as herein described and equipment is changed or suitably change and combination, realize the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (3)
1. a multilevel deflector-type bubble tower reactor comprises conversion zone, deflector, liquid phase distributor and microvesicle generators; It is characterized in that conversion zone connects deflector by reaction column and constitutes; Liquid phase distributor is positioned at the tower body upper end, and microvesicle generators is positioned at the tower body lower end; Top of tower is provided with exhaust outlet, and tower bottom is provided with leakage fluid dram, is provided with the liquid phase feeding mouth in the conversion zone upper end, is provided with the gas-phase feed mouth in the conversion zone lower end; Conversion zone is more than the two-stage.
2. multilevel deflector-type bubble tower reactor as claimed in claim 1 is characterized in that reaction column is structured packing, at least 3 on every order reaction post; The placement direction of adjacent two-stage reaction section internal reaction post is perpendicular.
3. the production technology of claim 1 or 2 multilevel deflector-type bubble tower reactor is characterized in that liquid phase feed is squeezed in the tower via liquid phase distributor by pump, and under the effect of gravity, raw material flows through conversion zones at different levels downwards successively; Phase feed is squeezed in the tower via microvesicle generators by compressor, and under buoyancy function, microvesicle moves upward, with the liquid phase feed counter current contacting, and issue in the guide functions of deflector and to give birth to corresponding reaction, liquid-phase reaction product is discharged at the bottom of tower, and the gas-phase reaction product is discharged from cat head.
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| Application Number | Priority Date | Filing Date | Title |
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| CN200910307444A CN101653711A (en) | 2009-09-22 | 2009-09-22 | Multilevel deflector-type bubble tower reactor and production process |
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| CN200910307444A CN101653711A (en) | 2009-09-22 | 2009-09-22 | Multilevel deflector-type bubble tower reactor and production process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478698A (en) * | 2014-12-28 | 2015-04-01 | 甘肃银光聚银化工有限公司 | Method for continuously producing stearoyl acid chloride |
| WO2022056913A1 (en) * | 2020-09-21 | 2022-03-24 | 安徽金禾实业股份有限公司 | Preparation method for sucrose-6-carboxylate |
| CN114409686A (en) * | 2022-01-27 | 2022-04-29 | 上海化工研究院有限公司 | System and method for preparing boron trifluoride complex |
| CN115041106A (en) * | 2022-06-21 | 2022-09-13 | 湖北新轩宏新材料有限公司 | Reactor for preparing trichlorobenzene and preparation method |
-
2009
- 2009-09-22 CN CN200910307444A patent/CN101653711A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478698A (en) * | 2014-12-28 | 2015-04-01 | 甘肃银光聚银化工有限公司 | Method for continuously producing stearoyl acid chloride |
| WO2022056913A1 (en) * | 2020-09-21 | 2022-03-24 | 安徽金禾实业股份有限公司 | Preparation method for sucrose-6-carboxylate |
| CN114409686A (en) * | 2022-01-27 | 2022-04-29 | 上海化工研究院有限公司 | System and method for preparing boron trifluoride complex |
| CN114409686B (en) * | 2022-01-27 | 2023-11-07 | 上海化工研究院有限公司 | System and method for preparing boron trifluoride complex |
| CN115041106A (en) * | 2022-06-21 | 2022-09-13 | 湖北新轩宏新材料有限公司 | Reactor for preparing trichlorobenzene and preparation method |
| CN115041106B (en) * | 2022-06-21 | 2023-11-07 | 湖北新轩宏新材料有限公司 | Reactor for preparing trichlorotoluene and preparation method |
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Open date: 20100224 |