Continuous bubbling type reaction device

Abstract

The utility model relates to a continuous bubbling type reaction device which comprises a reactor provided with a heat exchange assembly, the reactor is connected with a liquid phase feeding pipeline and a gas phase feeding pipeline, and a gas phase outlet of the gas phase feeding pipeline is connected with a micropore distributor in the reactor. During working, a reaction liquid-phase raw material is conveyed to the reactor from the liquid-phase feeding pipeline, meanwhile, raw material gas enters the reactor through the gas-phase feeding pipeline and the microporous distributor, reaction is started after two-phase cis / countercurrent contact, and internal members of the reactor tubes can promote dispersion of the gas raw material in a liquid phase and strengthen gas-liquid mixing; the reaction is promoted, the backmixing phenomenon is reduced, and the target product selectivity is improved. And meanwhile, the temperature required by the reaction can be maintained through a heat exchange medium introduced through a coil pipe in the reactor and a shell jacket, so that the reaction temperature is controlled, and a product with high yield is finally obtained. And different reaction conditions can be met through the combination of a plurality of reactors, so that the device has a wide production and application scene.

Description

Technical Field

[0001] The utility model relates to a continuous bubbling reaction device. Background Art

[0002] Gas-liquid reaction is a heterogeneous reaction, and the gas-liquid contact area and time are the key factors affecting the reaction rate. The bubbling reactor is a common device applied to gas-liquid reactions. In this reactor, the gas is the dispersed phase and the liquid is the continuous phase. The reaction gas is dispersed in the liquid phase layer in the form of bubbles to achieve the chemical reaction process. Such reactors are widely used in petrochemical industry, fine chemical industry, medicine and food industry, etc. According to different structural forms, the bubbling reactor can be divided into tower type and kettle type, namely bubbling tower and bubbling reaction kettle. In the traditional kettle-type reactor, the yield of gas-liquid reaction is relatively low. The gas-liquid contact can be enhanced by an internal stirring device, but it will cause gas overflow and problems such as slow heat transfer rate. The bubbling tower has excellent heat transfer performance, especially the tubular bubbling tower with higher heat transfer efficiency. However, it has problems such as short gas-liquid contact time, low equipment utilization rate, and difficulty in controlling the bubble size. Content of the Utility Model

[0003] In view of the deficiencies of the prior art, the technical problem to be solved by the utility model is to provide a continuous bubbling reaction device.

[0004] To solve the above technical problem, the technical solution of the utility model is: a continuous bubbling reaction device, including a reactor provided with a heat exchange component, a liquid phase feed pipe and a gas phase feed pipe are connected to the reactor, and a microporous distributor is connected to the gas phase outlet inside the reactor at the gas phase feed pipe.

[0005] Preferably, the microporous distributor includes a distributor housing, the air inlet end of the distributor housing is communicated with the gas phase outlet, and a plurality of microporous air outlets are arranged on the distributor housing.

[0006] Preferably, the heat exchange component includes a jacket on the outer shell of the reactor, and a heat exchange medium inlet and a heat exchange medium outlet are arranged on the jacket for connecting an external heat exchange medium.

[0007] Preferably, the heat exchange component includes an internal coil located inside the reactor, and a heat exchange medium inlet and a heat exchange medium outlet are arranged on the internal coil for connecting an external heat exchange medium.

[0008] Preferably, the shape of the internal coil is spiral.

[0009] Preferably, the internal coil is arranged at the raw material inlet.

[0010] Preferably, the reactor is a tubular reactor, and internal members for disturbing flow are arranged inside the tubes.

[0011] Preferably, a number of thermometers are provided at the bottom, middle and top of the reactor, and pressure gauges are provided at the bottom and top of the reactor.

[0012] Preferably, the heat exchange component includes a jacket on the outer shell of the reactor, and a number of baffles are arranged inside the outer shell from bottom to top, and the number of baffles are arranged in a staggered manner.

[0013] Preferably, liquid phase feed pipes are connected to both the bottom and top of the reactor, reaction liquid outlets are provided at both the bottom and top of the reactor, the gas phase feed pipe is connected to the bottom end of the reactor, and a vent outlet is provided at the top end of the reactor.

[0014] Compared with the prior art, the utility model has the following beneficial effects: During operation, the reaction liquid phase raw materials are transported to the reactor through the liquid phase feed pipe, and at the same time, the raw material gas enters the reactor through the gas phase feed pipe and the microporous distributor. After the two phases contact in a co-current / counter-current manner, the reaction starts. The internal components of the reactor tubes can promote the dispersion of the gas raw materials in the liquid phase, strengthen the gas-liquid mixing, promote the progress of the reaction, reduce the backmixing phenomenon, and improve the selectivity of the target product. At the same time, the temperature required for the reaction can be maintained by the heat exchange medium introduced into the coil inside the reactor and the jacket of the outer shell, so as to control the reaction temperature, and finally obtain a product with high yield. And through the combination of multiple reactors, different reaction conditions can be met, and it has a wide range of production application scenarios.

[0015] The following further describes the present utility model in detail with reference to the accompanying drawings and specific embodiments. Description of the Drawings

[0016] Figure 1 It is a schematic structural diagram of an embodiment of the present utility model.

[0017] Figure 2 It is a partial view of the tubes of an embodiment of the present utility model.

[0018] Figure 3 It is a partial view of the inner coil of an embodiment of the present utility model.

[0019] Figure 4 It is a schematic diagram of the co-current connection of a multi-stage continuous continuous bubble reaction device.

[0020] Figure 5 It is a schematic diagram of the counter-current connection of a multi-stage continuous continuous bubble reaction device.

[0021] In the figure: outer shell 1, reactor 2, liquid phase feed pipe 3, gas phase feed pipe 4, microporous distributor 5, inner coil 6, tubes 7, internal components 8, feed transfer pump 9, gas flowmeter 10, microporous gas outlet 11, thermometer 12, pressure gauge 13, baffle 14, reaction liquid outlet 15, vent outlet 16. Detailed implementation mode

[0022] The present utility model will be further described below in conjunction with the accompanying drawings and embodiments.

[0023] It should be noted that the following detailed description is exemplary and is intended to provide further description of the present application. Unless otherwise specified, all technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the technical field to which this application belongs.

[0024] It should be noted that the terms used herein are only for describing specific implementation modes and are not intended to limit the exemplary implementation modes according to the present application. As used herein, unless the context clearly indicates otherwise, the singular form is also intended to include the plural form. In addition, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0025] As Figures 1 to 3 As shown, the speed of the bubbling reaction depends on the degree of sufficient gas-liquid contact. Gas will form bubbles in the solution, and the bubbles will continuously accumulate and grow during the generation process, thus forming a mass of bubbles, which has an impact on the gas-liquid reaction contact and mixing. If the gas-liquid two-phase contact time is too short or the dispersion is not uniform enough, the gas-liquid contact surface is small, and the multi-stage bubbling effect is not obvious, which will affect the reaction efficiency and also the yield of the product. Therefore, the present utility model is proposed, mainly by strengthening the bubble breakage during the reaction to enhance the two-phase mixing and realizing the intensification of the reaction process. This embodiment provides a continuous bubbling reaction device, which includes a reactor 2 provided with a heat exchange component. A liquid-phase feed pipe 3 and a gas-phase feed pipe 4 are connected to the reactor. The gas-phase outlet of the gas-phase feed pipe is connected with a microporous distributor 5 inside the reactor.

[0026] The microporous distributor can disperse the gas through tiny apertures, which can effectively disperse the gas feed rate, thereby ensuring the gas-liquid contact area during the reaction process, ensuring the uniformity of the gas entering each internal tube of the reactor, and avoiding local reaction overheating or dead zones. The microporous distributor can be selected from an annular distributor, a single-hole nozzle, a perforated plate, etc.

[0027] In the embodiment of the present utility model, the microporous distributor includes a distributor housing. The air inlet end of the distributor housing is communicated with the gas-phase outlet, and a plurality of microporous air outlets 11 are arranged on the top surface of the distributor housing.

[0028] In the embodiment of the present utility model, the heat exchange component includes a jacket on the outer housing 1 of the reactor. The jacket is provided with a heat exchange medium inlet and a heat exchange medium outlet for connecting an external heat exchange medium. A heat exchange medium is introduced into the reactor jacket, so as to ensure that the heat released by the reaction can be removed in time and ensure that the reaction temperature is stable within a certain range.

[0029] In the embodiment of the present utility model, the heat exchange assembly includes an inner coil 6 located inside the reactor. The inner coil is provided with a heat exchange medium inlet and a heat exchange medium outlet for connecting to an external heat exchange medium. The inner coil is arranged in the region where liquid-phase mixing reaction occurs but there is no temperature control, further improving the functional area of the heat exchange assembly. At the same time, it ensures that a certain amount of reaction heat can be removed at the gas-liquid contact position, avoids too fast reaction at the moment of gas-liquid contact, and ensures the stability of the feed temperature, so that the two phases enter the tube bundle for full reaction.

[0030] In the embodiment of the present utility model, the shape of the inner coil is spiral.

[0031] In the embodiment of the present utility model, the inner coil is arranged at the raw material inlet.

[0032] In the embodiment of the present utility model, the reactor is a shell-and-tube reactor, and internal members 8 for disturbing flow are arranged inside each of its tubes 7.

[0033] Internal members are arranged inside the internal tubes, which can promote the dispersion of gaseous raw materials in the liquid phase, the fragmentation and distribution of gas-liquid, strengthen gas-liquid mixing, and promote the reaction process. At the same time, it reduces the backmixing phenomenon of the liquid and improves the selectivity of the target product. The internal members can be integral members or repeated internal parts. The integral member is installed as a whole into the tube, and the repeated internal parts are regularly stacked or randomly filled in the tube in large quantities. Integral members such as corrugated internal members, inserted sheet meshes, wire meshes, and spiral sheet internal members, and repeated internal parts such as randomly filled packings, and the shapes can be selected from saddle rings, Pall rings, cascade rings, Intalox saddles, hybrid saddles, Hiflow rings, conjugate rings, Raschig rings, Taylor flower rings, thorn flower rings, cross spherical rings, polyhedral hollow balls, Tellerette rings, etc. The material of the internal members can be selected from plastics, ceramics, metals, etc., mainly determined according to the corrosiveness of the reaction medium. The packing specifications are reasonably selected according to the inner diameter of the tower. In this embodiment, the inner diameter of the reactor is 32 mm, and a θ ring (also known as Dixon ring) with a size of Φ3 mm×3 mm is preferably selected. The θ ring is made of metal wire mesh. Due to the capillary action of the metal wire mesh, the liquid can be well dispersed into a film, which is beneficial for full mass transfer and heat transfer between the gas-liquid two phases, and can significantly eliminate unstable phenomena such as channeling.

[0034] In the embodiment of the present utility model, a number of thermometers 12 are provided at the bottom, middle and top of the reactor to monitor the reaction temperature in different regions of the reactor; pressure gauges 13 are provided at the bottom and top of the reactor to monitor the reaction pressure in different regions of the reactor.

[0035] In the embodiment of the present utility model, the heat exchange assembly includes a jacket on the outer shell of the reactor. A number of baffles 14 are arranged inside the outer shell from bottom to top, and the number of baffles is arranged in a staggered manner to form a curved gas-liquid mixing path, further strengthening the gas-liquid mixing process.

[0036] In an embodiment of the utility model, the bottom and top of the reactor are connected to a liquid-phase feed pipeline with a valve, the bottom and top of the reactor are provided with a reaction liquid outlet 15 with a valve, the gas-phase feed pipeline is connected to the bottom end of the reactor, and the top of the reactor is provided with a vent outlet 16.

[0037] In the embodiment of the utility model, a feed delivery pump 9 is provided on the liquid-phase feed pipeline, and a gas flow meter 10 is provided on the gas-phase feed pipeline.

[0038] The liquid raw material is fed into the reactor through one of the liquid feed pipes under the action of the feed delivery pump, and the gas raw material is fed into the reactor through the gas feed pipe. A gas flow meter is provided in the gas feed pipe to measure the intake amount of the gas raw material.

[0039] In the embodiment of the utility model, the working principle of the continuous bubbling reaction device is as follows: during operation, the reaction liquid phase raw material is transported to the reactor from the liquid phase feed pipeline, and the raw gas enters the reactor through the gas phase feed pipeline and the microporous distributor. The two phases start to react after the forward / countercurrent contact. The internal components of the reactor tube can promote the dispersion of the gas raw material in the liquid phase, strengthen the gas-liquid mixing, promote the reaction to reduce the back mixing phenomenon, and improve the selectivity of the target product. At the same time, the temperature required for the reaction can be maintained by the heat exchange medium introduced by the coil and the outer shell jacket in the reactor, thereby controlling the reaction temperature and finally obtaining a product with a high yield. And through the combination of multiple reactors, different reaction conditions can be met, with a wider production application scenario.

[0040] The utility model adopts a tubular reaction, the reaction process has little back mixing, the product concentration forms a concentration gradient, and the reaction is continuously and efficiently carried out in a positive direction. The bubbles are dispersed more evenly through the microporous distributor, the gas-liquid contact area is increased, and the reaction rate is improved.

[0041] In the embodiment of the utility model, when the utility model is applied in a specific application, in view of the situation that the reactor height is limited, a multi-stage continuous bubbling reaction device can be designed to be connected in actual application, and the gas phase feed pipelines between multiple parallel reactors are designed in parallel, and the raw gas is respectively passed into multiple reactors. After the reaction liquid is discharged, it enters the liquid phase feed pipeline of the next reactor, and continues to react after mixing with the raw gas. The raw materials are discharged from the reactor step by step to the next stage of reaction, and the unreacted raw materials can be fully utilized to improve the reaction yield. Among them:

[0042] like Figure 4As shown in the figure, the multi-stage continuous bubble column reactor is connected in co-current flow (the gas-liquid reaction is carried out in a co-current manner, and the gas and liquid phases flow in the same direction in the reactor). Specifically, the top reaction liquid outlet of the previous continuous bubble column reactor is connected to the bottom liquid phase feed pipeline of the next continuous bubble column reactor. When connected in co-current flow, the top liquid phase feed pipeline and the bottom reaction liquid outlet of the continuous bubble column reactor are not used.

[0043] As Figure 5 As shown in the figure, the multi-stage continuous bubble column reactor is connected in counter-current flow (the gas-liquid reaction is carried out in a counter-current manner, and the gas raw material and the liquid raw material are fed from both ends of the reactor respectively). Specifically, the bottom reaction liquid outlet of the previous continuous bubble column reactor is connected to the top liquid phase feed pipeline of the next continuous bubble column reactor. When connected in counter-current flow, the bottom liquid phase feed pipeline and the top reaction liquid outlet of the continuous bubble column reactor are not used.

[0044] The bubble column reactor provided by the present utility model can realize multi-stage continuous reaction, shorten the reaction time; adopt tubular reaction, with less backmixing in the reaction process, the product concentration forms a concentration gradient, and the reaction proceeds continuously and efficiently in the forward direction. The bubbles are dispersed more evenly through the microporous distributor, increasing the gas-liquid contact area and improving the reaction rate. At the same time, heat is continuously removed during the reaction process to maintain the reaction temperature, and finally a product with a high yield is obtained.

[0045] The above is only a preferred embodiment of the present utility model, and it is not intended to limit the present utility model in other forms. Any person skilled in the art may use the technical content disclosed above to make changes or modifications into equivalent embodiments with equivalent changes. However, any simple modification, equivalent change and modification made to the above embodiments based on the technical essence of the present utility model without departing from the technical solution content of the present utility model still belong to the protection scope of the technical solution of the present utility model.

Claims

1. A continuous bubbling reaction device, characterized in that: The invention comprises a reactor provided with a heat exchange component, wherein a liquid phase feed pipeline and a gas phase feed pipeline are connected to the reactor, and a gas phase outlet of the gas phase feed pipeline is connected with a microporous distributor inside the reactor.

2. The continuous bubbling reaction device according to claim 1, characterized in that: The microporous distributor comprises a distributor shell, the gas inlet end of the distributor shell is connected with the gas phase outlet, and the distributor shell is provided with a plurality of microporous gas outlets.

3. The continuous bubbling reaction device according to claim 1, characterized in that: The heat exchange component comprises a jacket on the outer shell of the reactor, and the jacket is provided with a heat exchange medium inlet and a heat exchange medium outlet for externally connecting the heat exchange medium.

4. The continuous bubbling reaction device according to claim 1, characterized in that: The heat exchange component comprises an inner coil located inside the reactor, and a heat exchange medium inlet and a heat exchange medium outlet are arranged on the inner coil for externally connecting the heat exchange medium.

5. The continuous bubbling reaction device according to claim 4, characterized in that: The inner coil is in a spiral shape.

6. The continuous bubbling reaction device according to claim 4, characterized in that: The inner coil is arranged at the raw material inlet.

7. The continuous bubbling reaction device according to claim 1, characterized in that: The reactor is a shell-and-tube reactor, and the interior of the shell and tube are all provided with internal components for flow disturbance. The internal components include integral components placed in the shell and tube or fillers scattered in the shell and tube. The shapes of the integral components include corrugated, inserted mesh, wire mesh, and spiral sheets. The shapes of the fillers include flat rings, ball rings, step rings, rectangular saddle rings, heterosaddle rings, Haier rings, conjugated rings, Raschig rings, Taylor wreaths, thorny wreaths, cross spherical rings, polyhedral hollow balls or Trared rings.

8. The continuous bubbling reaction device according to claim 1, characterized in that: A plurality of thermometers are arranged at the bottom, middle and top of the reactor, and a pressure gauge is arranged at the bottom and top of the reactor.

9. The continuous bubbling reaction device according to claim 1, characterized in that: The heat exchange component comprises a jacket on the outer shell of the reactor, and a plurality of baffles are arranged from bottom to top inside the outer shell, and the plurality of baffles are distributed in a staggered manner.

10. The continuous bubbling reaction device according to claim 1, characterized in that: The bottom and the top of the reactor are both connected with liquid-phase feed pipelines, the bottom and the top of the reactor are both provided with reaction liquid outlets, the gas-phase feed pipeline is connected to the bottom end of the reactor, and the top of the reactor is provided with a vent outlet.

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