A gas-liquid reactor

Abstract

The application discloses a gas-liquid reactor, which comprises a reactor shell, a heat exchange jacket device arranged outside the reactor shell, a liquid phase inlet, a gas phase inlet and a gas-liquid phase outlet arranged on the reactor shell. An electric dispersion gas distributor is arranged inside the reactor shell and communicates with the gas phase inlet, and a needle electrode is arranged on the electric dispersion gas distributor. A tube bank is arranged above the electric dispersion gas distributor, the lower end of the tube bank is grounded, and the upper end of the tube bank is located below the gas-liquid phase outlet. The gas-liquid reactor can be used for continuous production of gas-liquid reaction, the needle electrode is used to disperse the gas phase material to form micron-scale bubbles, the gas phase material is premixed with the liquid phase material, then the mixture stably flows through the tube bank, the gas-liquid mass transfer area is greatly increased, the reaction process is strengthened, the reaction efficiency is improved, meanwhile, the reactor provides a large enough heat transfer area, and the removal of the reaction heat of the material is effectively promoted.

Description

Technical Field

[0001] This invention relates to a novel gas-liquid reaction device, and more particularly to a gas-liquid reactor for enhancing mass and heat transfer between the gas and liquid phases, which can be widely applied to gas-liquid heterogeneous exothermic reaction processes such as ozonation, sulfonation, and chlorination. Background Technology

[0002] In chemical production and other fields, gas-liquid mass transfer is a common technique. The purpose of gas-liquid mass transfer is to increase the gas-liquid contact area, thereby increasing the gas-liquid reaction rate. Based on the different gas-liquid contact methods, gas-liquid reactors can be mainly divided into: bubble type (such as bubble column, plate column, mechanically stirred tank), droplet type (such as spray column, jet reactor, Venturi reactor), and liquid film type (such as packed column, wet wall column).

[0003] For strongly exothermic gas-liquid heterogeneous reactions such as ozonation, sulfonation, and chlorination, mass transfer is usually the controlling step of the entire gas-liquid reaction process, mainly limited by the interphase area between the gas and liquid phases. Simultaneously, the large amount of heat generated during the reaction needs to be removed promptly to avoid "runaway temperatures." However, existing bubbling towers, spray towers, packed towers, jet reactors, and Venturi reactors still suffer from problems such as small gas-liquid interphase area, low heat transfer efficiency, high energy consumption, and difficulty in control. Summary of the Invention

[0004] This invention aims to overcome the shortcomings of the prior art by providing a novel gas-liquid reactor with a simple and reasonable structure, large phase interface area, high mass transfer efficiency, fast heat transfer rate, and low energy consumption. The purpose of this invention is to enhance the gas-liquid phase mass and heat transfer processes by coupling electric field dispersion technology with tubular reactor technology, thereby achieving enhanced reaction and heat transfer processes.

[0005] A gas-liquid reactor, characterized in that it includes a reactor shell and a heat exchange jacket disposed outside the reactor shell. The bottom and top of the reactor shell are respectively provided with a liquid phase inlet and a gas / liquid phase outlet. The lower middle part of the reactor shell is provided with a gas phase inlet, and an electrodispersive gas distributor communicating with the gas phase inlet is provided inside the lower middle part of the reactor shell. The upper surface of the electrodispersive gas distributor is provided with a plurality of needle-shaped electrodes, and a gas hole is provided in the center of the needle-shaped electrodes. A tube is provided above the electrodispersive gas distributor, and the lower end of the tube is grounded. The needle-shaped electrodes are connected to a high-voltage electrode. The gas phase material enters the internal cavity of the electrodispersive gas distributor through the gas phase inlet, and is dispersed by the needle-shaped electrodes and mixed with the liquid phase material. Then it flows stably through the tube and finally flows out through the gas / liquid phase outlet.

[0006] The gas-liquid reactor is characterized in that: the electrodispersed gas distributor has a circular tube cavity structure, and a plurality of needle-shaped electrodes are uniformly distributed on the upper surface of the electrodispersed gas distributor. The tubes and needle-shaped electrodes correspond one-to-one, and the central axes of the corresponding tubes and needle-shaped electrodes are located on the same vertical line.

[0007] The gas-liquid reactor is characterized in that: the reactor shell includes an upper end cap, an intermediate shell and a lower end cap, the gas phase inlet is disposed at the lower part of the side wall of the intermediate shell, and an insulating layer is provided on the side wall of the intermediate shell above and below the gas phase inlet, with the upper insulating layer disposed between the high voltage electrode and the ground electrode.

[0008] The gas-liquid reactor is characterized in that the diameter of the tube array is 5 to 100 times the diameter of the needle electrode.

[0009] The gas-liquid reactor is characterized in that the tubes and needle electrodes are made of conductive metal.

[0010] The gas-liquid reactor is characterized in that the interior of the tubes is filled with packing material.

[0011] The gas-liquid reactor is characterized in that: the heat exchange jacket device includes a heat exchange jacket layer disposed on the outside of the intermediate shell, and the lower end and upper end of the heat exchange jacket layer are respectively provided with a heat exchange medium inlet and a heat exchange medium outlet.

[0012] The beneficial effects of this invention are:

[0013] 1. The gas-liquid reactor disclosed in this invention can be used for continuous production of gas-liquid heterogeneous strongly exothermic reactions. The electric field dispersion technology is organically integrated with tubular reactor technology, resulting in a reactor with advantages such as large phase interface area, low energy consumption, high heat and mass transfer efficiency, stable and controllable bubbles that are not prone to coalescence, and ease of continuous production.

[0014] 2. By using electric field dispersion technology to directionally act on the gas phase, the gas phase is autonomously and efficiently dispersed into "micron-sized" charged bubbles of different diameters. For bubbles with a diameter of 400 micrometers, the volumetric surface area (6 / d) can reach 15,000 m². 2 / m 3 This significantly increases the interphase area required for gas-liquid mass transfer. Compared to traditional reactors such as jet reactors and Venturi reactors that utilize high-speed liquid flow to achieve gas dispersion, it can substantially reduce energy consumption.

[0015] 3. By combining electric field dispersion technology and tubular reactor technology, stable and efficient dispersion of charged microbubbles is achieved, enhancing the heat and mass transfer efficiency of the reactor. On the one hand, the electric field disperser generates micron-sized bubbles with the same charge. Under the repulsive force of the like charges, the micron-sized bubbles can flow stably through the tubular reactor without coalescence, while also enhancing liquid turbulence and further improving the heat and mass transfer efficiency of the tubular reactor. On the other hand, while achieving rapid removal of reaction heat, the tubular reactor, through the turbulence and redispersion of the packing material, increases the residence time of microbubbles, enhances the turbulence of the liquid film on the microbubble surface, and strengthens the mass transfer process of microbubbles.

[0016] 4. The gas-liquid reactor disclosed in this invention has a simple structure, is easy to start and stop, is easy to scale up industrially, and has good versatility. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the gas-liquid reactor of the present invention;

[0018] Figure 2 This is a schematic diagram showing the correspondence between the mass transfer coefficient and the enhanced mass transfer device in Example 1;

[0019] Figure 3 This is a schematic diagram of the bubble dispersion in Example 1;

[0020] Figure 4 This is a bubble size distribution diagram of Example 1;

[0021] Figure 5 This is a graph showing the conversion rate of the ozonation reaction versus temperature in Example 2;

[0022] Figure 6 This is a graph showing the conversion rate of oxygen cracking reaction versus temperature in Example 3;

[0023] In the figure: 1-lower end cap, 2-electrodispersed gas distributor, 3-insulating layer, 4-heat exchange medium inlet, 5-intermediate shell, 6-upper end cap, 7-gas and liquid phase outlet, 8-heat exchange medium outlet, 9-tube shell, 10-heat exchange jacket, 11-gas phase inlet, 12-lower end of tube shell, 13-needle electrode, 14-liquid phase inlet. Detailed Implementation

[0024] The present invention will be further described below with reference to specific embodiments, but the scope of protection of the present invention is not limited thereto.

[0025] Example: Comparison Figure 1

[0026] A gas-liquid reactor includes a reactor shell and a heat exchange jacket device disposed outside the reactor shell. The reactor shell includes an upper end cap 6, an intermediate shell 5 and a lower end cap 1. The heat exchange jacket device includes a heat exchange interlayer 10 disposed outside the intermediate shell 5. The lower end and the upper end of the heat exchange interlayer 10 are respectively provided with a heat exchange medium inlet 4 and a heat exchange medium outlet 8.

[0027] Comparison Figure 1 The upper end cap 6 has a gas and liquid phase outlet 7 at the top, and a liquid phase inlet 14 at the bottom of the lower end cap 1. The lower part of the side wall of the middle shell 5 has a gas phase inlet 11. The lower part of the middle shell 5 has an electrodispersed gas distributor 2 that communicates with the gas phase inlet 11. The electrodispersed gas distributor 2 has a cylindrical cavity structure. Several needle-shaped electrodes 13 are evenly distributed on the upper surface of the electrodispersed gas distributor 2. A gas hole is set in the center of the needle-shaped electrodes 13. The middle shell 5 also has a column of tubes 9, which are located above the electrodispersed gas distributor 2.

[0028] Comparison Figure 1 In this configuration, the tubes 9 and needle electrodes 13 are positioned one-to-one, with their central axes aligned vertically. The lower end 12 of the tubes is positioned close to the upper part of the needle electrodes 13. The lower end 12 of the tubes is grounded, and the needle electrodes 13 are connected to the high-voltage electrode. The gaseous material enters the internal cavity of the electrodispersive gas distributor 2 through the gas inlet 11 and is uniformly transported by the internal cavity of the electrodispersive gas distributor 2 to the needle electrodes 13 at the top of the electrodispersive gas distributor 2 for dispersion and mixing with the liquid material. The mixture then flows stably through the tubes 9 and finally exits through the gas / liquid outlet 7.

[0029] Comparison Figure 1 In the middle, an insulating layer 3 is provided on the side wall of the intermediate shell 5 above and below the gas phase inlet 11, and the upper insulating layer 3 is located between the high voltage electrode and the ground electrode.

[0030] The diameter of the tube 9 is much larger than the diameter of the needle electrode 13, ranging from 5 to 100 times. A non-uniform electrostatic field is formed in the region between the needle electrode 13 and the lower end 12 of the tube, dispersing the gaseous material and achieving mixing of the gas and liquid phases. Both the tube 9 and the needle electrode 13 are made of conductive metal. The interior of the tube 9 is filled with filler.

[0031] Example 1

[0032] Oxygen mass transfer experiments were conducted in a reactor, comparing and analyzing the electrodispersive reactor (i.e., the gas-liquid reactor of this invention) under different voltages with a traditional bubble reactor. The gas-liquid reactor used tubes with a diameter of 15 mm, filled with 3 mm glass spring packing, and needle electrodes with an orifice diameter of 0.5 mm. All flow patterns were gas-liquid upflow. The apparent gas velocity through the tubes was 0.0008–0.004 m / s, and the apparent liquid velocity was 0.0001 m / s. The experimental temperature was 20 °C, and the oxygen mass transfer coefficient K was measured using the dynamic oxygen concentration method. La The oxygen mass transfer coefficient of the electrodispersive reactor under different voltages is as follows: Figure 2 As shown, when using this method and apparatus for dissolved oxygenation in water, the oxygen mass transfer coefficient of the electrodispersive reactor increased from 0.0025–0.013 at 0 kV to 0.028–0.062 at 15 kV. Under the same operating conditions, the oxygen mass transfer coefficient of the conventional bubble column reactor is 0.002–0.01, which is comparable to that of the 0 kV electrodispersive reactor. The oxygen mass transfer coefficient of the 15 kV electrodispersive reactor is at least 6.2 times that of the bubble column reactor.

[0033] like Figure 3 , Figure 4 The image shows bubble dispersion in different regions of the electrodispersion reactor under different voltages, specifically including bubble images and particle size distribution maps at 7.5 kV and 15 kV in the electrodispersion zone and at the reactor outlet. Figure 3 The photographs show that the bubble dispersion is relatively uniform in size, with minimal aggregation within each region. From Figure 4 Bubble size distribution analysis showed that under electrodispersion, the bubble size exhibited a narrow peak distribution with a standard deviation of 0.017–0.018, further indicating a relatively uniform bubble size distribution and controllable electrodispersion. Furthermore, the bubble size distribution was highly consistent between the electrodispersion zone and the reactor outlet zone. At 15 kV, the average bubble size in the electrodispersion zone was 0.428 mm, while in the reactor outlet zone it was 0.435 mm; at 7.5 kV, the average bubble size in the electrodispersion zone was 0.900 mm, while in the reactor outlet zone it was 0.920 mm. This also demonstrates that due to the repulsive effect of like charges, the bubbles can flow stably through the tube shell without significant aggregation.

[0034] Example 2

[0035] The reaction performance of this invention was determined using an ozone oxidation process for oleic acid. The process parameters for ozone oxidation were as follows: reaction temperature 30℃, oleic acid:acetic acid mass ratio 1:4, ozone flow rate 20 g / h, oleic acid-acetic acid mixture flow rate 10 mL / min, apparent gas velocity through the tube was 0.002 m / s, and apparent liquid velocity was 0.0001 m / s. After dispersion, the ozone fully reacted with the oleic acid-acetic acid mixture. Under the conditions of a liquid feed temperature of 30℃ and an applied voltage of 15 kV for electrodispersion, the average particle size of the dispersed gaseous material was measured to be approximately 400 micrometers using a high-speed camera. Figure 5 The results of the ozone oxidation reaction in the electrodispersive reactor show that the conversion rate of oleic acid at the liquid outlet reaches and is maintained at 96% for a short time during the continuous reaction process in the electrodispersive reactor, and the reaction temperature is stable at 30℃.

[0036] Example 3

[0037] The reaction performance of this invention was determined using an oxygen oxidative cracking process. The process parameters for the oxygen oxidative cracking process are as follows: reaction temperature 90℃; the liquid product of ozone oxidation in Example 2 was used as the liquid feedstock for oxygen oxidative cracking; oxygen flow rate 0.3 L / min; liquid feedstock flow rate 10 mL / min; apparent gas velocity through the tube was 0.003 m / s; and apparent liquid velocity was 0.0001 m / s. The oxygen, after dispersion, fully contacts and reacts with the liquid feedstock. Under the conditions of a liquid feedstock feed temperature of 90℃ and an electrodispersion applied voltage of 15 kV, the average particle size of the dispersed gaseous material was measured to be approximately 400 micrometers using a high-speed camera. Figure 6 The results of the oxygen cracking reaction in the electrodispersive reactor show that the conversion rate of oleic acid ozonides in the liquid outlet reaches and is maintained at 96% for a short time during the continuous reaction process in the electrodispersive reactor, and the reaction temperature is stable at 90℃.

[0038] The results of the oleic acid ozone oxidation pyrolysis reaction show that this invention effectively enhances the oleic acid ozone oxidation pyrolysis reaction process and the heat transfer process. During the continuous reaction in the electrodispersive reactor, oleic acid and oleic acid ozonides reach and maintain a high conversion rate in a short time, the reaction temperature is stable, and the final azelaic acid yield reaches over 85%. The above examples demonstrate that this invention can be used for the continuous production of azelaic acid from oleic acid ozone oxidation pyrolysis.

[0039] The contents described in this specification are merely an enumeration of the implementation forms of the inventive concept, and the scope of protection of this invention should not be regarded as limited to the specific forms described in the embodiments.

Claims

1. A gas-liquid reactor, characterized in that: The reactor includes a reactor shell and a heat exchange jacket device located outside the reactor shell. The bottom and top of the reactor shell are respectively provided with a liquid phase inlet (14) and a gas and liquid phase outlet (7). The lower middle part of the reactor shell is provided with a gas phase inlet (11), and the lower middle part of the reactor shell is provided with an electrodispersive gas distributor (2) that communicates with the gas phase inlet (11). The upper surface of the electrodispersive gas distributor (2) is provided with several needle-shaped electrodes (13). The needle-shaped electrodes (13) are provided with air holes in the center. The electrodispersive gas distributor (2) is provided with a tube (9) above it. The lower end (12) of the tube is grounded. The needle-shaped electrodes (13) are connected to the high-voltage electrode. The gas phase material enters the internal cavity of the electrodispersive gas distributor (2) through the gas phase inlet (11), and is dispersed by the needle-shaped electrodes (13) and mixed with the liquid phase material. Then it flows steadily through the tube (9) and finally flows out through the gas and liquid phase outlet (7). The electrodispersive gas distributor (2) has a cylindrical cavity structure. Several needle-shaped electrodes (13) are evenly distributed on the upper surface of the electrodispersive gas distributor (2). The tubes (9) and the needle-shaped electrodes (13) correspond one-to-one, and the central axes of the corresponding tubes (9) and the needle-shaped electrodes (13) are located on the same vertical line. The tubes (9) and needle electrodes (13) are both made of conductive metal; The tube (9) is filled with filler.

2. A gas-liquid reactor as described in claim 1, characterized in that: The reactor shell includes an upper end cap (6), an intermediate shell (5) and a lower end cap (1). The gas inlet (11) is located on the lower part of the side wall of the intermediate shell (5), and an insulating layer (3) is provided on the side wall of the intermediate shell (5) above and below the gas inlet (11). The upper insulating layer (3) is located between the high voltage electrode and the ground electrode.

3. A gas-liquid reactor as described in claim 1, characterized in that: The diameter of the tube (9) is 5 to 100 times the diameter of the needle electrode (13).

4. A gas-liquid reactor as described in claim 2, characterized in that: The heat exchange jacket device includes a heat exchange jacket (10) disposed on the outside of the intermediate shell (5), and the lower end and upper end of the heat exchange jacket (10) are respectively provided with a heat exchange medium inlet (4) and a heat exchange medium outlet (8).

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