Fluid mass transfer device and method using reverse single-cyclone enhanced bubbles

Abstract

The present application relates to a kind of fluid mass transfer device and method of bubble strengthening using reverse single vortex, the device includes reverse cyclone and cyclone liquid storage chamber, reverse cyclone includes the cylindrical cavity part and cyclone cavity part that inside is cavity;Method is: liquid and gas are mixed in reverse cyclone Contact, and generate the cyclone field by bubble group;Liquid and bubble form liquid cyclone to side wall and bubble cyclone to the state of gas-liquid reverse flow to center;After cyclone, gas and liquid discharge;Using equipment measures the discharged liquid and gas, judges mass transfer effect.Compared with prior art, the present application has high gas rate using gas-liquid reverse cyclone, greatly improve the gas-liquid mass transfer area of unit space, strengthen gas-liquid mass transfer effect;It can realize larger gas-liquid mass transfer area and gas-liquid mass transfer coefficient under the premise of smaller pressure drop loss;Cyclone field structure is suitable for different liquid of larger range viscosity etc. Advantage.

Description

Technical Field

[0001] This invention relates to the fields of chemical reaction and gas-liquid mass transfer technology, and in particular to a fluid mass transfer device and method that utilizes counter-current single swirl to enhance bubble flow. Background Technology

[0002] Currently, China's three major oil and petrochemical companies primarily use air stripping to remove hydrogen sulfide, employing air-based equipment. Air stripping, a common gas-liquid mass transfer separation method in chemical industrial production, utilizes a carrier gas to reduce the partial pressure of dissolved gases in the liquid, stripping the gases to be removed from the liquid phase and transferring them to the carrier gas, achieving stable separation efficiency. Unheated air stripping is suitable for hydrogen sulfide removal from liquid sulfur. However, the lower temperature introduces a disadvantage related to thermodynamic diffusion mass transfer: the desorption and mass transfer rate of dissolved gases is slow, and liquid sulfur needs to remain in the gravity stripping tank for 12–24 hours to meet the hydrogen sulfide removal requirements. For a 40,000-ton / year sulfur plant, this consumes 120 standard cubic meters of air per hour, resulting in insufficient gas-liquid mass transfer, leading to huge carrier gas consumption, excessive tail gas emissions, and excessively long residence times. Gas-liquid mass transfer plays a major role in hydrogen sulfide separation; therefore, constructing a low-consumption, high-efficiency gas-liquid mass transfer method is a necessity for high-quality liquid sulfur production in the chemical industry.

[0003] A search revealed CN101108299A, which discloses a highly efficient gas-liquid mass transfer device. Specifically, the device comprises a demister, a liquid distributor, and a multi-stage gas-liquid exchange mechanism arranged from top to bottom within a tower. The bottom of the tower is a liquid collection chamber, and the top is a gas outlet. Direct gas-liquid contact is employed, enabling dynamic contact and turbulent mass transfer, significantly increasing the contact area between gas and liquid, allowing the gas to achieve thorough mixing and contact with the liquid in a very short time. However, problems such as agglomeration, deformation, and uneven distribution of bubbles can occur when they enter a large-scale tower reactor, resulting in certain limitations in gas-liquid mass transfer.

[0004] Application publication number CN109589879A discloses a gas-liquid mass transfer device, specifically comprising: a tower body, two or more mass transfer unit groups, an independent liquid collector, an independent liquid receiving tray, and a gas barrier plate; the top of the tower body has a gas phase outlet and a liquid phase inlet, and the bottom has a liquid phase outlet and a gas phase inlet; the mass transfer unit group includes, from top to bottom, a liquid collector, a liquid receiving tray, a liquid distributor, and a mass transfer zone. However, this device has a large overall footprint, a relatively large pressure drop, high energy consumption, and only moderate mass transfer efficiency.

[0005] Application publication number CN109482131A discloses a gas-liquid enhanced mass transfer device based on a porous ceramic membrane. Specifically, it comprises a housing containing several membrane elements, a perforated plate at each end of the housing, a liquid inlet at the head, a gas-liquid outlet at the tail, and an axial gas inlet on one side. This device is simple to operate and can achieve efficient dispersion and mixing of gas and liquid phases with low energy consumption. However, the numerous tiny pores and channels are easily blocked by particles or precipitates, affecting the mass transfer effect; it is not suitable for high-viscosity liquids, as it affects the gas-liquid interface renewal rate.

[0006] In conclusion, it is of great significance to find a new method to enhance gas-liquid mass transfer and overcome the problems of instability, low mass transfer efficiency, easy clogging, and unsuitability for high-viscosity liquids in existing technologies for bubbles in large-scale tower reactors. Summary of the Invention

[0007] The purpose of this invention is to overcome the defects of the prior art by providing a fluid mass transfer device and method that enhances bubble flow using reverse single swirl.

[0008] The objective of this invention can be achieved through the following technical solutions:

[0009] According to one aspect of the present invention, a fluid mass transfer device for enhancing bubbles using counter-current single swirling is provided, comprising a counter-current swirler and a swirling liquid storage chamber. The counter-current swirler includes a cylindrical cavity portion and a swirling cavity portion, both of which are hollow. The cylindrical cavity portion is provided with a liquid inlet and a counter-current swirler gas channel. The swirling cavity portion is provided with a gas outlet, a liquid tangential outlet, and a gas axial inlet. The cylindrical cavity portion is located within the cavity of the swirling cavity portion, with one end having the liquid inlet extending out of the swirling cavity portion. The counter-current swirler is connected to the swirling liquid storage chamber. The liquid to be transferred enters from the liquid inlet, and the gas after mass transfer exits from the gas outlet.

[0010] As a preferred technical solution, the gas channel of the reverse cyclone is located at the end of the reverse cyclone without a liquid inlet, guiding the gas tangentially into the reverse cyclone.

[0011] As a preferred technical solution, the swirling liquid storage chamber includes a side wall and a bottom plate, and the side wall is connected to the counter-swirling device.

[0012] As a preferred technical solution, the swirling cavity is generally in the shape of an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-swirling cavity. The gas outlet is located on the side wall of the upper cylinder, the liquid tangential outlet is located on the side wall of the lower cylinder, and the gas axial inlet is located on the bottom surface of the lower cylinder.

[0013] As a preferred technical solution, the structural characteristic parameter S of the fluid mass transfer device is set to characterize the mass transfer effect:

[0014]

[0015] Set S to a range of 5 to 15, D1 to a range of 320 to 420 mm, the ratio of P1 to P2 to a range of 0.7 to 1.0, and the ratio of d1 to D1 to a range of 0.01 to 0.1. a With d l The ratio ranges from 0.2 to 0.8; where P1 is the pressure value at the liquid inlet, D1 is the diameter of the gas-liquid counter-vortex chamber, and d a P2 is the equivalent diameter of the gas axial inlet, P2 is the pressure value of the gas-liquid counter-swirling chamber, and d is the equivalent diameter of the gas axial inlet. l This is the equivalent diameter of the liquid inlet.

[0016] As a preferred technical solution, the ratio of P1 to P2 ranges from 0.8 to 0.9, and the d l The ratio to D1 ranges from 0.05 to 0.1; the d a With d l The ratio ranges from 0.5 to 0.7.

[0017] As a preferred technical solution, the swirling liquid storage cavity is a cylinder with a liquid outlet on the bottom plate. The ratio of the diameter D1 of the gas-liquid counter-swirling cavity to the diameter D2 of the swirling liquid storage cavity is 0.6 to 1.0; the ratio of the height H1 of the swirling liquid storage cavity to the diameter D1 of the swirling liquid storage cavity is 0.4 to 0.8.

[0018] As a preferred technical solution, the ratio of the diameter D1 of the gas-liquid countercurrent swirling cavity to the diameter D2 of the swirling liquid storage cavity is 0.8 to 1.0, and the ratio of the height H1 of the swirling liquid storage cavity to the diameter D1 of the swirling liquid storage cavity is 0.5 to 0.7.

[0019] According to another aspect of the present invention, a fluid mass transfer method employing a fluid mass transfer device is provided, specifically comprising the following steps:

[0020] Step S1: Liquid enters the counter-cyclone separator through the liquid inlet;

[0021] In step S2, the gas enters through the gas axial inlet and mixes with the liquid, generating a swirling field composed of a group of bubbles at the gas-liquid counter-swirling cavity;

[0022] Step S3: In the gas-liquid countercurrent swirling chamber, the liquid swirls from the center to the side wall and generates a centrifugal field. Under the action of the centrifugal field, the bubbles move towards the center, forming a state of gas-liquid countercurrent flow where the liquid swirls towards the side wall and the bubbles swirl towards the center.

[0023] In step S4, the swirling gas moves upward and is discharged through the gas outlet; the swirling liquid flows into the swirling liquid storage chamber through the liquid tangential outlet and is discharged through the liquid outlet.

[0024] Step S5: Use equipment to measure the discharged liquid and gas to determine the mass transfer effect.

[0025] As a preferred technical solution, in step S3, the rotational acceleration of the liquid during swirling flow is 40 to 1000 times the acceleration due to gravity; the pressure drop of the liquid in the swirling region ranges from 0.01 to 0.25 MPa; the gas-liquid separation efficiency is 70% to 95%; the volumetric flow rate ratio of the liquid to the gas in the swirling cavity is 1 to 50; the velocity of the liquid entering the liquid inlet is 4 to 20 m / s; the velocity of the liquid exiting the liquid outlet is 1 to 10 m / s; the average flow velocity of the gas at the gas axial inlet ranges from 1 to 8 m / s; and the average flow velocity of the gas at the gas outlet ranges from 1 to 5 m / s.

[0026] Compared with the prior art, the present invention has the following advantages:

[0027] 1) The swirling cavity provided by this invention has sufficient space for gas-liquid mass transfer; and the swirling field structure is suitable for liquids of different viscosities over a wide range, allowing for full gas-liquid contact, longer residence time, and achieving a more efficient gas-liquid mass transfer effect.

[0028] 2) This invention utilizes counter-current gas-liquid swirling to achieve high gas content, significantly increasing the gas-liquid mass transfer area per unit space. Numerous liquid microparticles are constantly renewed near the gas-liquid interface. The vortex effect greatly shortens the residence time of liquid microparticles at the gas-liquid interface, increasing the gas-liquid surface renewal rate, thereby enhancing the gas-liquid mass transfer effect.

[0029] 3) This invention occupies a small area and can achieve a large gas-liquid mass transfer area and gas-liquid mass transfer coefficient with a small pressure drop loss. It utilizes the swirling flow to cause bubble interface oscillation, thereby enhancing the mass transfer coefficient. Attached Figure Description

[0030] Figure 1 This is a schematic diagram of the overall structure of a fluid mass transfer device for enhancing bubbles using reverse single swirl flow, according to the present invention.

[0031] Figure 2 This is a cross-sectional view of the cylindrical cavity portion of the present invention;

[0032] Figure 3 This is a top view of the cylindrical cavity portion of the present invention;

[0033] Figure 4 This is a cross-sectional view of the swirling cavity of the present invention;

[0034] Figure 5This is a top view of the vortex cavity section of the present invention;

[0035] Figure 6 This is a schematic diagram of the overall structure of the vortex liquid storage chamber of the present invention;

[0036] Figure 7 This is a flowchart illustrating the working process of a fluid mass transfer device for enhancing bubbles using reverse single swirl flow, as described in this invention.

[0037] Figure 1 As indicated by the standard number:

[0038] 1. Reverse cyclone separator; 10. Cylindrical cavity section; 11. Cyclone cavity section; 110. Gas outlet; 1110. Tangential liquid outlet; 2. Cyclone storage chamber; 210. Liquid outlet.

[0039] Figure 2 As indicated by the standard number:

[0040] 100. Liquid import;

[0041] Figure 3 As indicated by the standard number:

[0042] 101. Gas passage for the reverse cyclone separator;

[0043] Figure 4 As indicated by the standard number:

[0044] 111. Gas-liquid counter-current swirling chamber; 1111. Gas axial inlet;

[0045] Figure 6 As indicated by the standard number:

[0046] 20. Side wall; 21. Base plate. Detailed Implementation

[0047] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort should fall within the scope of protection of the present invention.

[0048] Traditional swirling flow generation methods rely on liquid being injected from the cylindrical sidewall 20 to create a certain tangential velocity. The liquid flows from the sidewall 20 to the center, forming a swirling flow field, which is a swirling flow from the sidewall 20 to the center. This invention provides a fluid mass transfer device and method that enhances bubble flow using a counter-current single swirling flow.

[0049] The principle of this invention is as follows:

[0050] After the liquid enters the counter-cyclone 1 through the axially downward liquid inlet 100 near the center of the cyclone, it flows from the center to the side wall 20 due to the pre-swirl of the liquid in the central region, forming a liquid vortex in the middle region. This induces the surrounding liquid, and even the liquid on the side wall 20, to form a swirling flow from the center to the side wall 20. Inside the cyclone cavity, the liquid flows in a swirling motion from the center to the side wall 20, generating a centrifugal field. Gas enters the counter-cyclone layer through several axial gas inlets 1111, mixes and contacts with the liquid, and moves towards the center under the action of the centrifugal field. Finally, a counter-current gas-liquid flow is formed in the cyclone cavity, with the liquid swirling towards the side wall 20 and the bubbles swirling towards the center. Several tangential liquid outlets 1110 near the cyclone side wall 20 flow into the cyclone storage chamber 2 and finally exit through several liquid outlets 210 on the bottom plate 21, achieving a multi-stage enhanced gas-liquid mass transfer effect using bubbles. On the one hand, the counter-current flow of gas and liquid can achieve a high gas content and keep the bubbles small, which can greatly increase the gas-liquid mass transfer area per unit space. On the other hand, the oscillation of the bubble interface caused by the swirling flow can improve the counter-current mass transfer effect, thereby enhancing the mass transfer coefficient.

[0051] like Figure 1 As shown, the fluid mass transfer device for enhancing bubbles using counter-current single swirl according to the present invention includes a counter-current cyclone 1 and a swirl storage chamber 2. The counter-current cyclone 1 includes a cylindrical cavity portion 10 and a swirl cavity portion 11, both of which are hollow.

[0052] like Figure 2 and Figure 3 As shown, the cylindrical cavity 10 is provided with a liquid inlet 100 that is close to the swirling center and vertically downward in the axial direction, and a reverse swirling gas channel 101. There are multiple reverse swirling gas channels 101, eight of which are shown in the figure. They are evenly distributed around the bottom of the cylindrical cavity 10, guiding the gas tangentially into the reverse swirling gas channel 1.

[0053] like Figure 4 and Figure 5 As shown, the swirling cavity section 11 is generally shaped like an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-swirling cavity 111. A gas outlet 110 is provided on the side wall of the upper cylinder, and a liquid tangential outlet 1110 is provided on the side wall of the lower cylinder. A gas axial inlet 1111 is provided on the bottom surface of the lower cylinder. There are multiple liquid tangential outlets 1110 and gas axial inlets 1111. In the figure, there are 8 liquid tangential outlets 1110 and 4 gas axial inlets 1111, all circumferentially distributed on the lower cylinder of the swirling cavity section 11.

[0054] like Figure 6As shown, the swirling liquid storage chamber 2 consists of a cylindrical curved side wall 20 and a bottom plate 21. The side wall 20 of the swirling liquid storage chamber 2 is connected to the gas-liquid counter-swirling chamber 111 of the swirling chamber body 11. The bottom plate 21 of the swirling liquid storage chamber 2 is provided with several liquid outlets 210 for measuring the dissolved oxygen mass transfer effect and deoxygenation mass transfer effect of the device.

[0055] To achieve better dissolved oxygen mass transfer, this device is equipped with a structural characteristic parameter S:

[0056]

[0057] The structural characteristic parameter S ranges from 5 to 15, where D1 is the diameter of the gas-liquid counter-swirling cavity 111; d a d is the equivalent diameter of the gas axial inlet 1111; l P1 is the equivalent diameter of the liquid inlet 100; P2 is the pressure value of the liquid inlet 100; P3 is the pressure value of the gas-liquid counter-vortex chamber 111. If the diameter D1 of the gas-liquid counter-vortex chamber 111 is too large, the bubble vortex effect will be insignificant; if it is too small, the outermost bubble fluid of the vortex chamber will contact the sidewall 20 during counter-vortexing, weakening the mass transfer effect of the counter-vortex generator 1 on the bubble fluid. To achieve better vortexing and mass transfer effects, the diameter D1 of the gas-liquid counter-vortex chamber 111 is in the range of 320–420 mm, verified through multiple experimental tests and case studies. When the diameter D1 of the gas-liquid counter-vortex chamber 111 is 370 mm, the device utilizing counter-vortexing to enhance bubble fluid mass transfer exhibits good vortexing and mass transfer effects.

[0058] The pressure value P1 of the liquid inlet 100 is 0.7-1.0, preferably 0.8-0.9, relative to the pressure value of the gas-liquid counter-vortex chamber 111; the equivalent diameter d of the liquid inlet 100 is... l The ratio of the diameter D1 of the gas-liquid counter-swirling cavity 111 to the diameter of the nozzle is 0.01 to 0.1, preferably 0.05 to 0.1; the equivalent diameter d of the nozzle is... a The equivalent diameter d of the liquid inlet 100 l The ratio is 0.2 to 0.8, preferably 0.5 to 0.7.

[0059] The gas-liquid countercurrent swirling cavity 111 has a liquid circulation function and realizes gas-liquid mass transfer function through bubble swirling. The ratio of the diameter D1 of the gas-liquid countercurrent swirling cavity 111 to the diameter D2 of the swirling liquid storage cavity 2 is 0.6 to 1.0, preferably 0.8 to 1.0; the ratio of the height H1 of the swirling liquid storage cavity 2 to the diameter D1 of the swirling liquid storage cavity 2 is 0.4 to 0.8, preferably 0.5 to 0.7.

[0060] like Figure 7As shown, the present invention discloses a fluid mass transfer method for enhancing bubbles using reverse single swirl flow, employing a fluid mass transfer device for enhancing bubbles using reverse single swirl flow. The specific process is as follows:

[0061] First, liquid enters the counter-cyclone separator 1 through liquid inlet 100; gas enters the gas-liquid counter-cyclone chamber 111 through gas axial inlet 1111 and mixes with the liquid, generating a swirling field composed of bubble clusters at the gas-liquid counter-cyclone chamber 111. Inside the cyclone storage chamber 2, the liquid swirls from the center towards the side wall 20, generating a centrifugal field; the bubbles move towards the center under the influence of the centrifugal field, ultimately forming a counter-current gas-liquid flow where the liquid swirls towards the side wall 20 and the bubbles swirl towards the center. The swirling gas moves upwards and is discharged through gas outlet 110; the swirling liquid flows into the cyclone storage chamber 2 through the tangential liquid outlet 1110 near the cyclone side wall 20, and finally exits through liquid outlet 210 of the bottom plate 21. Finally, the separation efficiency of the discharged liquid and gas is measured using a separation detection device, and the dissolved oxygen mass transfer effect and deoxygenation mass transfer effect are measured using a dissolved oxygen meter.

[0062] The rotational acceleration of the liquid in the counter-swirling layer is 40 to 1000 times the acceleration due to gravity, and the pressure drop of the liquid in the swirling region ranges from 0.01 to 0.25 MPa; the gas-liquid separation efficiency is 70% to 95%; excessive pressure drop may lead to poor gas-liquid separation efficiency and insignificant bubble swirling effect. The swirling region in this invention requires both low pressure drop and high separation efficiency, as well as good dissolved oxygen mass transfer, thus there exists an optimizable range for both pressure drop and separation efficiency. The dissolved oxygen mass transfer coefficient of this device ranges from 0.01 to 0.05; in the swirling chamber 11, the volumetric flow rate ratio of the liquid to the gas is 1 to 50. The velocity of liquid injection at liquid inlet 100 is 4–20 m / s; the velocity of liquid discharge at liquid outlet 210 is 1–10 m / s; the average flow velocity of gas at the gas axial inlet is within the range of 1–8 m / s; the average flow velocity of gas at gas outlet 110 is within the range of 1–5 m / s; the gas content enhancement efficiency ranges from 25% to 50%; the device for enhancing bubble fluid mass transfer using counter-swirling flow can be heated or condensed to achieve a more efficient mass transfer process.

[0063] Example 1

[0064] This invention provides a fluid mass transfer device that enhances bubble flow using a counter-current single swirling flow. The device includes a counter-current swirler 1 and a swirling liquid storage chamber 2. The counter-current swirler 1 includes a cylindrical cavity 10 and a swirling cavity 11. The cylindrical cavity 10 is provided with a liquid inlet 100 and a counter-current swirler gas channel 101. The swirling cavity 11 is generally shaped as an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-current swirling cavity 111. The upper cylinder sidewall is provided with a gas outlet 110, the lower cylinder sidewall is provided with a liquid tangential outlet 1110, and the lower cylinder bottom surface is provided with a gas axial inlet 1111. The swirling liquid storage chamber 2 is composed of a cylindrical curved sidewall 20 and a bottom plate 21. The bottom plate 21 is provided with a plurality of liquid outlets 210.

[0065] An oxygenation experiment was conducted using an air-water system to fill low-oxygen water, testing the enhanced mass transfer effect of the device from gas to liquid. In this example, the diameter D1 of the gas-liquid counter-vortex chamber 111 was fixed at 370 mm; the equivalent diameter d of the liquid inlet 100 was... l The inlet diameter is 30 mm; the pressure value P1 at the liquid inlet is 0.28 MPa. The dissolved oxygen concentration of the low-oxygen water is 3 mg / L.

[0066] The device utilizing counter-vortex flow to enhance bubble-fluid mass transfer can increase the dissolved oxygen concentration in low-oxygen water to 6 mg / L, significantly improving the dissolved oxygen rate in the water; it achieves high separation efficiency; and it significantly improves the gas-to-liquid mass transfer effect, making it a closed and highly efficient gas-liquid mass transfer method. Experimental parameters and results are shown in Table 1.

[0067] Table 1

[0068]

[0069]

[0070] Example 2

[0071] This invention provides a fluid mass transfer device that enhances bubble flow using a counter-current single swirling flow. The device includes a counter-current swirler 1 and a swirling liquid storage chamber 2. The counter-current swirler 1 includes a cylindrical cavity 10 and a swirling cavity 11. The cylindrical cavity 10 is provided with a liquid inlet 100 and a counter-current swirler gas channel 101. The swirling cavity 11 is generally shaped as an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-current swirling cavity 111. The upper cylinder sidewall is provided with a gas outlet 110, the lower cylinder sidewall is provided with a liquid tangential outlet 1110, and the lower cylinder bottom surface is provided with a gas axial inlet 1111. The swirling liquid storage chamber 2 is composed of a cylindrical curved sidewall 20 and a bottom plate 21. The bottom plate 21 is provided with a plurality of liquid outlets 210.

[0072] Using the same air-water system, an oxygenation experiment was conducted on low-oxygen water to test the enhanced mass transfer effect of the device from gas to liquid. This example compares with Example 1 to show the effect of a smaller diameter D1 of the gas-liquid counter-vortex chamber 111 on separation efficiency and dissolved oxygen mass transfer. The dissolved oxygen concentration of the low-oxygen water was 3 mg / L. The experimental parameters and results are shown in Table 2.

[0073] Table 2

[0074]

[0075] Example 3

[0076] This invention provides a fluid mass transfer device that enhances bubble flow using a counter-current single swirling flow. The device includes a counter-current swirler 1 and a swirling liquid storage chamber 2. The counter-current swirler 1 includes a cylindrical cavity 10 and a swirling cavity 11. The cylindrical cavity 10 is provided with a liquid inlet 100 and a counter-current swirler gas channel 101. The swirling cavity 11 is generally shaped as an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-current swirling cavity 111. The upper cylinder sidewall is provided with a gas outlet 110, the lower cylinder sidewall is provided with a liquid tangential outlet 1110, and the lower cylinder bottom surface is provided with a gas axial inlet 1111. The swirling liquid storage chamber 2 is composed of a cylindrical curved sidewall 20 and a bottom plate 21. The bottom plate 21 is provided with a plurality of liquid outlets 210.

[0077] Using the same air-water system, an oxygenation experiment was conducted on low-oxygen water to test the enhanced mass transfer effect of the device from gas to liquid. This example compares with Example 1 to show the effect of a larger diameter D1 of the gas-liquid counter-vortex chamber 111 on the separation efficiency and dissolved oxygen mass transfer effect. The dissolved oxygen concentration of the low-oxygen water was 3 mg / L. The experimental parameters and results are shown in Table 3.

[0078] Table 3

[0079]

[0080]

[0081] Example 4

[0082] This invention provides a fluid mass transfer device that enhances bubble flow using a counter-current single swirling flow. The device includes a counter-current swirler 1 and a swirling liquid storage chamber 2. The counter-current swirler 1 includes a cylindrical cavity 10 and a swirling cavity 11. The cylindrical cavity 10 is provided with a liquid inlet 100 and a counter-current swirler gas channel 101. The swirling cavity 11 is generally shaped as an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-current swirling cavity 111. The upper cylinder sidewall is provided with a gas outlet 110, the lower cylinder sidewall is provided with a liquid tangential outlet 1110, and the lower cylinder bottom surface is provided with a gas axial inlet 1111. The swirling liquid storage chamber 2 is composed of a cylindrical curved sidewall 20 and a bottom plate 21. The bottom plate 21 is provided with a plurality of liquid outlets 210.

[0083] A nitrogen-water system was used to conduct deoxygenation experiments on highly oxygenated water to test the enhanced mass transfer effect of the device from liquid to gas. This example is compared with Example 1. With the cyclone diameter D1 fixed at 370 mm, the effect of changing the gas velocity at the axial inlet 1111 of the counter-cyclone layer on the separation efficiency and the liquid-to-gas deoxygenation mass transfer effect was compared. The dissolved oxygen concentration of the highly oxygenated water was 9 mg / L. The experimental parameters and results are shown in Table 4.

[0084] Table 4

[0085]

[0086]

[0087] Traditional gas-liquid co-current swirl-enhanced mass transfer technology can achieve a single equilibrium within a very small volume. However, its mass transfer limit is a first-order theoretical equilibrium, and it cannot achieve multi-order theoretical equilibrium. The mass transfer flux of dissolved gases is equal to the product of the mass transfer coefficient, the mass transfer area, and the concentration difference. Only by achieving countercurrent contact and reducing the consumption of carrier gas or solvent can it be more widely applied in chemical processes and improve economic efficiency in the field of liquid sulfur desulfurization. Employing gas-liquid counter-swirl to achieve a reasonable distribution of the concentration gradient is one of the effective means to overcome the above-mentioned bottlenecks in gas-liquid counter-swirl-enhanced gas lift mechanisms.

[0088] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any person skilled in the art can easily conceive of various equivalent modifications or substitutions within the technical scope disclosed in the present invention, and these modifications or substitutions should all be covered within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A fluid mass transfer device that enhances bubble flow using counter-current single swirl, characterized in that, The device includes a reverse cyclone separator (1) and a cyclone storage chamber (2). The reverse cyclone separator (1) includes a cylindrical cavity (10) and a cyclone cavity (11) with the interior being hollow. The cylindrical cavity (10) is provided with a liquid inlet (100) and a reverse cyclone separator gas channel (101). The cyclone cavity (11) is provided with a gas outlet (110), a liquid tangential outlet (1110), and a gas axial inlet (1111). The cylindrical cavity (10) is located in the cavity of the cyclone cavity (11) and one end of the cylindrical cavity (100) extends out of the cyclone cavity (11). The reverse cyclone separator (1) is connected to the cyclone storage chamber (2). The liquid to be transferred enters from the liquid inlet (100), and the gas after mass transfer is discharged from the gas outlet (110).

2. The fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 1, characterized in that, The gas passage (101) of the reverse cyclone is located at the end of the reverse cyclone (1) without a liquid inlet (100), guiding the gas tangentially into the reverse cyclone (1).

3. The fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 1, characterized in that, The swirling liquid storage chamber (2) includes a side wall (20) and a bottom plate (21), and the side wall (20) is connected to the counter-swirling device (1).

4. The fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 1, characterized in that, The swirling cavity (11) is generally in the shape of an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-swirling cavity (111). The gas outlet (110) is located on the side wall of the upper cylinder, the liquid tangential outlet (1110) is located on the side wall of the lower cylinder, and the gas axial inlet (1111) is located on the bottom surface of the lower cylinder.

5. A fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 4, characterized in that, Set the structural characteristic parameter S of the fluid mass transfer device to characterize the mass transfer effect: Set S to a range of 5 to 15, D1 to a range of 320 to 420 mm, and the ratio of P1 to P2 to a range of 0.7 to 1.0, d l The ratio to D1 ranges from 0.01 to 0.1, d a With d l The ratio ranges from 0.2 to 0.8; Where P1 is the pressure value of the liquid inlet (100), D1 is the diameter of the gas-liquid counter-vortex chamber (111), and d a P2 is the equivalent diameter of the gas axial inlet (1111), P2 is the pressure value of the gas-liquid counter-swirling chamber (111), and d l The equivalent diameter of the liquid inlet (100).

6. A fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 5, characterized in that, The ratio of P1 to P2 is in the range of 0.8 to 0.9, and the d l The ratio to D1 ranges from 0.05 to 0.1; the d a With d l The ratio ranges from 0.5 to 0.

7.

7. A fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 6, characterized in that, The swirling liquid storage chamber (2) is a cylinder, and a liquid outlet (210) is provided on the bottom plate (21). The ratio of the diameter D1 of the gas-liquid counter-swirling chamber (111) to the diameter D2 of the swirling liquid storage chamber (2) is 0.6 to 1.0; the ratio of the height H1 of the swirling liquid storage chamber (2) to the diameter D1 of the swirling liquid storage chamber (2) is 0.4 to 0.

8.

8. A fluid mass transfer device for enhancing bubbles using counter-current single swirl as described in claim 7, characterized in that, The ratio of the diameter D1 of the gas-liquid countercurrent swirling cavity (111) to the diameter D2 of the swirling liquid storage cavity (2) is 0.8 to 1.0, and the ratio of the height H1 of the swirling liquid storage cavity (2) to the diameter D1 of the swirling liquid storage cavity (2) is 0.5 to 0.

7.

9. A fluid mass transfer method using the fluid mass transfer device of claim 1, characterized in that, Specifically, the following steps are included: In step S1, the liquid enters the reverse cyclone separator (1) through the liquid inlet (100); In step S2, the gas enters through the gas axial inlet (1111) and mixes with the liquid, generating a swirling field composed of a group of bubbles at the gas-liquid counter-swirling chamber (111); Step S3: In the gas-liquid countercurrent swirling chamber (111), the liquid swirls from the center to the side wall (20) and generates a centrifugal field. Under the action of the centrifugal field, the bubbles move towards the center, forming a state of gas-liquid countercurrent flow where the liquid swirls towards the side wall (20) and the bubbles swirl towards the center. In step S4, the swirling gas moves upward and is discharged through the gas outlet (110); the swirling liquid flows into the swirling liquid storage chamber (2) through the liquid tangential outlet (1110) and is discharged through the liquid outlet (210). Step S5: Use equipment to measure the discharged liquid and gas to determine the mass transfer effect.

10. The fluid mass transfer method according to claim 9, characterized in that, The rotational acceleration of the liquid during the swirling flow in step S3 is 40 to 1000 times the acceleration due to gravity. The pressure drop of the liquid in the swirling region is 0.01 to 0.25 MPa, and the gas-liquid separation efficiency is 70% to 95%. In the swirling cavity (11), the volumetric flow rate ratio of the liquid to the gas is 1 to 50. The velocity of the liquid entering the liquid inlet (100) is 4 to 20 m / s. The velocity of the liquid exiting the liquid outlet (210) is 1 to 10 m / s. The average flow velocity of the gas at the gas axial inlet (1111) is 1 to 8 m / s. The average flow velocity of the gas at the gas outlet (110) is 1 to 5 m / s.

Images