A fluid mass transfer device and method using multi-stage reverse single-cyclone to strengthen bubbles

Abstract

The application relates to a fluid mass transfer device and method for strengthening bubbles by using a multistage reverse single-cyclone, which comprises at least two reverse cyclone units connected in series, wherein each reverse cyclone unit comprises a reverse cyclone and a cyclone liquid storage cavity, the reverse cyclone comprises a cylindrical cavity part and a cyclone cavity part, the cylindrical cavity part is provided with a liquid inlet and a reverse cyclone gas channel, the cyclone cavity part is provided with a gas outlet, a liquid tangential outlet and a gas axial inlet; the liquid to be mass transferred is fed into the liquid inlet of the uppermost reverse cyclone unit, and the gas after mass transfer is discharged from the gas outlet. Compared with the prior art, the application has the advantages that the gas-liquid contact time is prolonged by connecting the reverse cyclone units in series, the mass transfer efficiency is improved, the gas is sucked and reversely contacted and mixed by fluid negative pressure, the gas is further broken into smaller scales, the mass transfer area and the mass transfer coefficient are improved, the energy consumption is low, the gas-liquid mass transfer efficiency is high, and the overall device has the advantages of small land occupation and the like.

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 multi-stage counter-current single swirl to enhance bubble flow. Background Technology

[0002] In many industrial processes, liquids are often entrained with microbubbles and dissolved gases. Swirl-flow enhanced gas-liquid mass transfer methods offer advantages such as compactness, high efficiency, and low operation and maintenance costs, making them suitable for numerous gas-liquid mass transfer processes. However, current research on swirl-flow enhanced gas-liquid mass transfer is insufficient. It neglects the migration and coalescence patterns of bubbles during swirl degassing and lacks research on the influence of centrifugal force and pressure gradient fields on dissolved gas mass transfer. Only by gaining a deeper understanding of the mechanisms of swirl-flow enhanced gas-liquid mass transfer can we design more rational and efficient swirl-flow enhanced gas-liquid mass transfer devices with appropriate dimensions and structures, thus promoting the development of economical and efficient liquid mass transfer technologies.

[0003] Application publication number CN115845423A discloses a device and method for enhancing gas-liquid mass transfer using local circulation and bubble swirling. Specifically, it discloses a mass transfer unit comprising several stages connected in series. Each stage includes a swirling negative pressure chamber and a bubble swirling chamber that are interconnected and axially perpendicular. The swirling negative pressure chamber has a liquid inlet tangentially, a gas inlet at one axial end, and a jet port tangentially connected to the bubble swirling chamber at the other end. The bubble swirling chamber has a liquid outlet tangentially and a gas outlet axially, with the gas outlet connected to the gas inlet via a circulation pipeline. However, this device occupies a large area and consumes a lot of energy.

[0004] Authorization announcement number CN201342249Y discloses a disc-type gas-liquid mass transfer device, specifically comprising a gas-liquid distribution disc, a liquid seal disc, a cylinder, upper and lower end caps, a gas phase inlet / outlet, and a liquid phase inlet / outlet. The gas-liquid distribution disc consists of an annular gas distribution box and several inlet pipes; the annular gas distribution box consists of a cylinder, a conical guide plate, and an annular base plate; several serrated grooves are formed along the upper edge of the cylinder of the annular gas distribution box; an annular gap is formed between the conical guide plate and the annular base plate; the gas-liquid distribution disc can be manufactured into a vertical multi-stage series structure. However, this device exhibits a high degree of gas aggregation, uneven dispersion, relatively short gas-liquid contact time, high resistance, and a small mass transfer area.

[0005] Authorization announcement number CN102350294B discloses a counter-current mass transfer, heat transfer, and reaction device based on an ejector. Specifically, it discloses, from top to bottom, a sealed upper separator, a mass transfer, heat transfer, or reaction unit, and a lower separator. The upper separator has a light medium outlet at its top, and the lower separator has a heavy medium outlet at its bottom. The unit is divided into multiple connected sections, with an ejector mounted on a partition at the connection between each pair of adjacent sections to isolate the fluid. The ejector's suction chamber is connected to an ejector suction pipe, and the other end of the ejector suction pipe passes through the partition and connects to the preceding unit. It also includes a power flow inlet located at the top or bottom of the unit, which is connected to the ejector nozzle via a pipe. However, the mass transfer region of this device mostly occurs in the central mixing region, and the gas-liquid separation region still uses the principle of gravity sedimentation to separate the heavy and light media into layers. The required separation area is too large, and the separation area is still under the influence of gravity, lacking the effect of intense contact.

[0006] In summary, existing technologies suffer from problems such as large volume, uneven gas-liquid dispersion, small mass transfer area, and insufficient gas-liquid contact. Therefore, a device capable of solving these problems is a technical issue that needs to be addressed. Summary of the Invention

[0007] The purpose of this invention is to overcome the defects of the prior art and provide a fluid mass transfer device and method that utilizes multi-stage counter-current single swirl to enhance bubble flow.

[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 multi-stage counter-current single swirl is provided, comprising at least two counter-current units connected in series in the vertical direction to form a multi-stage structure. Each counter-current unit includes a counter-current cyclone and a swirl reservoir. The counter-current cyclone includes a cylindrical cavity portion and a swirl cavity portion, both of which are hollow. The cylindrical cavity portion is provided with a liquid inlet and a gas channel for the counter-current cyclone. The swirl cavity portion is provided with a gas outlet, a tangential liquid outlet, and an axial gas inlet. In the series-connected counter-current units, the counter-current cyclone of the lower-level counter-current unit is located in the swirl reservoir of the upper-level counter-current unit. The liquid to be transferred enters from the liquid inlet of the uppermost swirl unit, and the gas after mass transfer is discharged from the gas outlet.

[0010] 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.

[0011] As a preferred technical solution, in the reverse swirling unit, the reverse swirling device is connected to the swirling liquid storage chamber; the cylindrical cavity is located in the cavity of the swirling cavity and one end of which is provided with a liquid inlet extends out of the swirling cavity.

[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 swirling characteristic parameter K of the fluid mass transfer device is set as follows:

[0014]

[0015] K is set to a range of 25 to 150, where D1 is the diameter of the gas-liquid counter-swirling cavity; d a d is the equivalent diameter of the gas axial inlet. l V is the equivalent diameter of the liquid inlet. m V1 is the velocity of the liquid inlet of the m-th stage; V2 is the velocity of the gas axial inlet of the first-stage counter-swirling unit; n is the number of stages connected in series in the counter-swirling unit.

[0016] As a preferred technical solution, each stage of the interconnected counter-swirling units has a gas circulation function, and the structural characteristic parameter S characterizing the mass transfer effect of the counter-swirling units is set as follows:

[0017]

[0018] 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 and P2 is the pressure value of the gas-liquid counter-vortex chamber.

[0019] As a preferred technical solution, the dissolved oxygen mass transfer coefficient of the device ranges from 0.01 to 0.05; and the volumetric flow rate ratio of liquid to gas in the swirling cavity is from 1 to 50.

[0020] According to another aspect of the present invention, a fluid mass transfer method is provided using a multi-stage counter-current single swirling enhanced bubble fluid mass transfer device, specifically comprising the following steps:

[0021] Step S1: Liquid enters the counter-cyclone separator through the liquid inlet;

[0022] 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;

[0023] Step S3: In the gas-liquid counter-current 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 counter-current flow where the liquid swirls towards the side wall and the bubbles swirl towards the center.

[0024] Step S4: The swirled gas is discharged through the gas outlet, and the discharged gas is detected by the equipment; if the swirled liquid has reached the last stage of the counter-swirling unit, then proceed to step S5; otherwise, return to step S1.

[0025] In step S5, the liquid after swirling is discharged through the liquid outlet of the last stage counter-swirling unit, and the discharged liquid is detected by the equipment.

[0026] As a preferred technical solution, the rotational acceleration of the liquid in the gas-liquid counter-current swirling chamber is 40 to 1000 times the acceleration due to gravity, and the pressure drop of the liquid ranges from 0.01 to 0.25 MPa; the gas-liquid separation efficiency is 70% to 95%.

[0027] As a preferred technical solution, in each stage of the counter-swirling unit, the average velocity of the liquid injection at the liquid inlet is 4 to 20 m / s; the velocity of the liquid discharge at the liquid outlet is 1 to 10 m / s; the average flow velocity of the gas at the gas axial inlet is within the range of 1 to 8 m / s; and the average flow velocity of the gas at the gas outlet is within the range of 1 to 5 m / s.

[0028] Compared with the prior art, the present invention has the following advantages:

[0029] 1) This invention extends the gas-liquid contact time by connecting multiple counter-swirling units in series, optimizes the volume dispersion of bubbles, and improves the mass transfer efficiency; multiple counter-swirling units are a kind of concentration gradient optimized hypergravity mass transfer unit, with a more reasonable concentration gradient, and the mass transfer coefficient and mass transfer area are effectively enhanced at the same time.

[0030] 2) This invention uses fluid negative pressure and a special flow field structure to form a strong negative pressure region, which draws in another gas and mixes it in reverse contact, thereby breaking the gas into a smaller scale, increasing the mass transfer area and mass transfer coefficient. It is a highly efficient mass transfer method.

[0031] 3) The present invention is a self-priming structure that draws gas into the swirling unit, resulting in low energy consumption, high gas-liquid mass transfer efficiency, and a small overall footprint. Attached Figure Description

[0032] Figure 1This is a schematic diagram of the overall structure of a fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl, as described in one embodiment of the present invention.

[0033] Figure 2 This is a schematic diagram of the overall structure of the reverse swirl unit of the present invention;

[0034] Figure 3 This is a schematic diagram of the overall structure of the reverse cyclone separator of the present invention;

[0035] Figure 4 This is a cross-sectional view of the reverse cyclone separator of the present invention;

[0036] Figure 5 This is a top view of the cylindrical cavity portion of the present invention;

[0037] Figure 6 This is a cross-sectional view of the swirling cavity of the present invention;

[0038] Figure 7 This is a schematic diagram of the overall structure of the vortex liquid storage chamber of the present invention;

[0039] Figure 8 This is a flowchart of a fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl, as described in this invention.

[0040] Figure 1 As indicated by the index number:

[0041] 1000, Liquid Inlet; 1011, First-stage Gas Outlet; 1012, Second-stage Gas Outlet; 1013, Third-stage Gas Outlet; 1014, Fourth-stage Gas Outlet; 1015, Liquid Tangential Outlet; 11, First-stage Countercurrent Cyclone; 12, Second-stage Countercurrent Cyclone; 13, Third-stage Countercurrent Cyclone; 14, Fourth-stage Countercurrent Cyclone; 21, First-stage Cyclone Storage Chamber; 22, Second-stage Cyclone Storage Chamber; 23, Third-stage Cyclone Storage Chamber; 24, Fourth-stage Cyclone Storage Chamber; 2010, Liquid Outlet;

[0042] Figure 2 As indicated by the index number:

[0043] 10. Reverse cyclone separator; 101. Cyclone chamber; 1010. Gas outlet; 1016. Gas axial inlet; 20. Cyclone storage chamber.

[0044] Figure 4 As indicated by the index number:

[0045] 100. Cylindrical cavity section;

[0046] Figure 5 As indicated by the index number:

[0047] 1001. Gas passage for the reverse cyclone separator;

[0048] Figure 6 As indicated by the index number:

[0049] 1017. Gas-liquid counter-current swirling chamber;

[0050] Figure 7 As indicated by the index number:

[0051] 200. Sidewall; 201. Base plate. Detailed Implementation

[0052] 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.

[0053] This invention provides a fluid mass transfer device and method for enhancing bubbles using multi-stage counter-current single swirl. The device includes at least two counter-current units connected in series in the vertical direction, forming a multi-stage structure. Gas and liquid flow through the device, and it is necessary to ensure good overall airtightness.

[0054] like Figure 1 As shown, the fluid mass transfer device of the present invention, which utilizes multi-stage counter-current single swirling to enhance bubble flow, can be configured with four counter-current units. These four units are vertically installed from top to bottom. The next-stage counter-current swirler 10 is placed within the swirling liquid storage chamber 20 of the previous stage. The liquid, after four stages of processing, is discharged from the liquid outlet 2010 on the bottom plate 201 of the last stage, i.e., the fourth-stage swirling liquid storage chamber 24. Due to the multi-stage stacked structure of this device, with the next-stage counter-current swirler 10 placed within the previous-stage swirling liquid storage chamber 20, gas discharge holes need to be opened on the side wall 200 of the previous-stage swirling liquid storage chamber 20 for discharge. These holes are shown as the second-stage gas outlet 1012, the third-stage gas outlet 1013, and the fourth-stage gas outlet 1014 in the figure. The mass transfer effect of the device can be measured by the gas difference at the gas outlets 1010 at different locations.

[0055] like Figure 2 , Figure 3 and Figure 4 As shown, each reverse swirling unit includes a reverse swirling device 10 and a swirling liquid storage chamber 20. The reverse swirling device 10 includes a cylindrical cavity portion 100 with an internal cavity and a swirling cavity portion 101. The cylindrical cavity portion 100 is located in the swirling cavity portion 101 and one end extends upward through the swirling cavity portion 101.

[0056] like Figure 5As shown, the cylindrical cavity 100 has a liquid inlet 1000 at one end that extends out of the swirling cavity 101 and is located near the center of the swirling flow and axially downward. The other end has a reverse swirling gas channel 1001, which is the area where the gas and liquid come into contact in reverse flow at the first moment. There are multiple reverse swirling gas channels 1001, eight of which are shown in the figure. They are evenly distributed around the bottom of the cylindrical cavity 100 and guide the gas tangentially into the reverse swirling gas channel 10.

[0057] like Figure 6 As shown, the swirling cavity 101 is generally shaped as an upper cylinder and a lower cylinder stacked together. The cavity inside the lower cylinder is a gas-liquid counter-swirling cavity 1017. A gas outlet 1010 is provided on the side wall of the upper cylinder, and a liquid tangential outlet 1015 is provided on the side wall of the lower cylinder. A gas axial inlet 1016 is provided on the bottom surface of the lower cylinder. There are multiple liquid tangential outlets 1015 and gas axial inlets 1016, which are evenly distributed circumferentially on the lower cylinder of the swirling cavity 101.

[0058] like Figure 7 As shown, the swirling liquid storage chamber 20 consists of a cylindrical curved sidewall 200 and a bottom plate 201. The sidewall 200 of the swirling liquid storage chamber 20 is connected to the gas-liquid counter-swirling chamber 1017 of the swirling chamber body 101. The bottom plate 201 of the swirling liquid storage chamber 20 is provided with several liquid outlets 2010 for measuring the dissolved oxygen mass transfer effect and deoxygenation mass transfer effect of the device.

[0059] To achieve better dissolved oxygen mass transfer, a structural characteristic parameter S is set for the counter-swirling unit:

[0060]

[0061] The structural characteristic parameter S ranges from 5 to 15, where D1 is the diameter of the gas-liquid counter-swirling cavity 1017; d a The equivalent diameter of the gas axial inlet is 1016; d l P1 is the equivalent diameter of the liquid inlet 1000; P2 is the pressure value of the liquid inlet 1000; P3 is the pressure value of the gas-liquid counter-vortex chamber 1017. If the diameter D1 of the gas-liquid counter-vortex chamber 1017 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 200 during counter-vortexing, weakening the mass transfer effect of the counter-vortex generator 10 on the bubble fluid. To achieve better vortexing and mass transfer effects, the diameter D1 of the gas-liquid counter-vortex chamber 1017 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 1017 is 370 mm, the device utilizing counter-vortexing to enhance bubble fluid mass transfer exhibits good vortexing and mass transfer effects.

[0062] The ratio of the pressure value P1 at the liquid inlet 1000 to the pressure value at the gas-liquid counter-vortex chamber 1017 is 0.7 to 1.0, preferably 0.8 to 0.9; the equivalent diameter d of the liquid inlet 1000 is... l The ratio of the diameter D1 of the gas-liquid counter-swirling cavity 1017 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 1000 l The ratio is 0.2 to 0.8, preferably 0.5 to 0.7.

[0063] The gas-liquid countercurrent swirling cavity 1017 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 1017 to the diameter D2 of the swirling liquid storage cavity 20 is 0.6 to 1.0, preferably 0.8 to 1.0; the ratio of the height H1 of the swirling liquid storage cavity 20 to the diameter D1 of the swirling liquid storage cavity 20 is 0.4 to 0.8, preferably 0.5 to 0.7.

[0064] This device is configured with a swirling characteristic parameter:

[0065]

[0066] K ranges from 25 to 150, where D1 is the diameter of the gas-liquid counter-swirling cavity 1017; d a d is the equivalent diameter of the gas inlet. l P1 is the equivalent diameter of the liquid inlet 1000; P2 is the pressure value of the liquid inlet 1000; P3 is the pressure value of the gas-liquid counter-vortex chamber 1017; V m V1 is the velocity of the liquid inlet of the m-th stage (1000); V2 is the velocity of the gas axial inlet of the first-stage counter-swirling unit (1016); n is the number of stages connected in series in the counter-swirling unit.

[0067] like Figure 7 As shown, the present invention discloses a fluid mass transfer method for enhancing bubbles using multi-stage counter-current single swirl, employing a fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl. The specific process is as follows:

[0068] Liquid enters the first-stage counter-cyclone unit 11 through the liquid inlet 1000; gas enters the first-stage counter-cyclone layer through the gas axial inlet 1016, and then mixes with the liquid in the counter-cyclone gas channel 1001 of the first-stage counter-cyclone unit 11, generating a swirling field composed of bubble clusters in the gas-liquid counter-cyclone chamber 1017. This swirling field utilizes the pre-swirl of liquid in the central region, with the liquid flowing from the center towards the sidewall 200, forming a liquid vortex, inducing swirling flow in the surrounding liquid and even the sidewall 200, thereby causing bubble interface oscillation, similar to particle interface oscillation, which can improve the convective mass transfer effect and enhance the mass transfer coefficient. The swirled gas is discharged through the first-stage gas outlet 1011 above the counter-cyclone layer; the swirled liquid is discharged into the first-stage cyclone storage chamber 21 through the liquid tangential outlet 1015 near the swirling sidewall 200 of the first cyclone layer.

[0069] The liquid in the first-stage swirling storage chamber 21 then enters the second-stage counter-swirling unit through the liquid inlet 1000, and the gas enters the second-stage counter-swirling unit 12 through the gas inlet. Similarly, a swirling field composed of bubble clusters is generated in the second-stage counter-swirling layer. The swirled gas is discharged through the second-stage gas outlet 1012; the swirled liquid is discharged into the second-stage swirling storage chamber 22 through several tangential liquid outlets 1015 near the swirling sidewalls 200 of the second-stage swirling layer.

[0070] The number of stages of the fluid mass transfer device that enhances bubble flow by multi-stage counter-current single swirl can be adjusted according to experimental requirements. Each stage of the swirl unit then performs the swirl process described above for the first and second stage swirl units. Several liquid outlets 2010 are provided at the bottom of the swirl storage chamber 20 of the last stage for measuring the separation efficiency, gas content enhancement efficiency, dissolved oxygen mass transfer effect, and deoxygenation mass transfer effect of the device.

[0071] 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 101, the volumetric flow rate ratio of liquid to gas is 1 to 50. The velocity of liquid injection at liquid inlet 1000 is 4–20 m / s; the velocity of liquid discharge at liquid outlet 2010 is 1–10 m / s; the average flow velocity of gas at gas axial inlet 1016 is within the range of 1–8 m / s; the average flow velocity of gas at gas outlet 1010 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.

[0072] Example 1

[0073] This invention provides a fluid mass transfer device that enhances bubbles using multi-stage counter-current single swirl. The device includes two counter-current units connected in series vertically, forming a multi-stage structure. Each counter-current unit includes a counter-current cyclone separator 10 and a swirl storage chamber 20. The counter-current cyclone separator 10 includes a cylindrical cavity portion 100 and a swirl cavity portion 101, both of which are hollow. The cylindrical cavity portion 100 is provided with a liquid inlet 1000 and a counter-current cyclone gas channel 1001. The swirl cavity portion 101 is provided with a gas outlet 1010, a tangential liquid outlet 1015, and an axial gas inlet 1016. In the series-connected counter-current units, the counter-current cyclone separator 10 of the lower-stage counter-current unit is located within the swirl storage chamber 20 of its upper-stage counter-current unit.

[0074] An oxygenation experiment was conducted on low-oxygen water using an air-water system to test the enhanced mass transfer effect from gas to liquid in this device with a two-stage counter-cyclone unit. The dissolved oxygen concentration of the low-oxygen water was 3 mg / L. The first-stage counter-cyclone unit increased the dissolved oxygen concentration to 6 mg / L, while the second-stage counter-cyclone unit increased it to 7.2 mg / L, thus improving the dissolved oxygen rate in the water and enhancing the mass transfer effect from gas to liquid. The experimental parameters and results are shown in Table 1.

[0075] Table 1

[0076]

[0077]

[0078] Example 2

[0079] This invention provides a fluid mass transfer device that enhances bubbles using multi-stage counter-current single swirl. The device comprises four counter-current units connected in series vertically, forming a multi-stage structure. Each counter-current unit includes a counter-current cyclone separator 10 and a swirl storage chamber 20. The counter-current cyclone separator 10 includes a cylindrical cavity portion 100 and a swirl cavity portion 101, both of which are hollow. The cylindrical cavity portion 100 is provided with a liquid inlet 1000 and a counter-current cyclone gas channel 1001. The swirl cavity portion 101 is provided with a gas outlet 1010, a tangential liquid outlet 1015, and an axial gas inlet 1016. In the series-connected counter-current units, the counter-current cyclone separator 10 of the lower-level counter-current unit is located within the swirl storage chamber 20 of its upper-level counter-current unit.

[0080] An oxygenation experiment was conducted on low-oxygen water using an air-water system to test the enhanced mass transfer effect from gas to liquid in this device with a four-stage counter-cyclone unit. The dissolved oxygen concentration of the low-oxygen water was 3 mg / L. The first-stage counter-cyclone unit increased the dissolved oxygen concentration to 6 mg / L, while the fourth-stage counter-cyclone unit increased it to 8.4 mg / L, significantly improving the dissolved oxygen rate in the water and thus the gas-to-liquid mass transfer effect. The experimental parameters and results are shown in Table 2.

[0081] Table 2

[0082]

[0083]

[0084] Example 3

[0085] This invention provides a fluid mass transfer device that enhances bubbles using multi-stage counter-current single swirl. The device comprises four counter-current units connected in series vertically, forming a multi-stage structure. Each counter-current unit includes a counter-current cyclone separator 10 and a swirl storage chamber 20. The counter-current cyclone separator 10 includes a cylindrical cavity portion 100 and a swirl cavity portion 101, both of which are hollow. The cylindrical cavity portion 100 is provided with a liquid inlet 1000 and a counter-current cyclone gas channel 1001. The swirl cavity portion 101 is provided with a gas outlet 1010, a tangential liquid outlet 1015, and an axial gas inlet 1016. In the series-connected counter-current units, the counter-current cyclone separator 10 of the lower-level counter-current unit is located within the swirl storage chamber 20 of its upper-level counter-current unit.

[0086] A nitrogen-water system was used to conduct deoxygenation experiments on highly oxygenated water, testing the enhanced mass transfer effect from gas to liquid in this apparatus with a four-stage counter-cyclone unit. The dissolved oxygen concentration of the highly oxygenated water was 9 mg / L.

[0087] The first-stage counter-cyclone unit reduced the dissolved oxygen concentration of high-oxygen water to 6 mg / L, while the fourth-stage counter-cyclone unit reduced the dissolved oxygen concentration of low-oxygen water to 3.6 mg / L, significantly improving the mass transfer effect from liquid to gas. The experimental parameters and results are shown in Table 3.

[0088] Table 3

[0089]

[0090]

[0091] Since the discovery and description of turbulence, rotating turbulence has become a research hotspot. The centrifugal field and pressure gradient field formed by rotating turbulence have been continuously explored and enriched, expanding research on separation, mixing, and reactions. With the increasing refinement and greening of industrial production, attention has been paid to the effects of rotating turbulence on heterogeneous separation, gas-liquid interface mass transfer, and soft fluid deformation. Compared to laminar flow, rotating turbulence has complex velocity distribution characteristics, making it difficult to quantitatively study the migration of bubbles and dissolved gases under rotating turbulence. Improving the migration mechanisms of bubbles and dissolved gases under centrifugal and pressure gradient fields will help to better understand the momentum and mass transfer laws under turbulence, which is of great significance for promoting the advancement of industrial production technologies.

[0092] 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.

[0093] 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 multi-stage counter-current single swirl, characterized in that, The system comprises at least two counter-swirling units connected in series vertically to form a multi-stage structure. Each counter-swirling unit includes a counter-swirling device (10) and a swirling liquid storage chamber (20). The counter-swirling device (10) includes a cylindrical cavity (100) and a swirling cavity (101) with the interior being hollow. The cylindrical cavity (100) is provided with a liquid inlet (1000) and a counter-swirling device gas channel (1001). The swirling cavity (101) is provided with a gas outlet (1010), a liquid tangential outlet (1015), and a gas axial inlet (1016). In the series-connected counter-swirling units, the counter-swirling device (10) of the lower-level counter-swirling unit is located in the swirling liquid storage chamber (20) of its upper-level counter-swirling unit. The liquid to be transferred enters from the liquid inlet (1000) of the uppermost swirling unit, and the gas after mass transfer is discharged from the gas outlet (1010). In the reverse swirling unit, the reverse swirling device (10) is connected to the swirling liquid storage chamber (20); the cylindrical cavity part (100) is located in the cavity of the swirling cavity part (101) and one end of the cylindrical cavity part (1000) extends out of the swirling cavity part (101). The swirling cavity (101) 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 (1017). The gas outlet (1010) is located on the side wall of the upper cylinder, the liquid tangential outlet (1015) is located on the side wall of the lower cylinder, and the gas axial inlet (1016) is located on the bottom surface of the lower cylinder.

2. The fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl as described in claim 1, characterized in that, The swirling liquid storage chamber (20) includes a side wall (200) and a bottom plate (201), and the side wall (200) is connected to the reverse swirler (10).

3. The fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl as described in claim 1, characterized in that, Set the swirling characteristic parameters of the fluid transfer device K : ， Set K to a range of 25 to 150, where The diameter of the gas-liquid counter-vortex chamber (1017); The equivalent diameter of the gas axial inlet (1016); The equivalent diameter of the liquid inlet (1000); Let m be the velocity of the liquid inlet (1000) at stage m; The velocity of the gas at the axial inlet (1016) of the first-stage counter-swirling unit; The number of stages connected in series in the counter-swirling unit.

4. The fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl as described in claim 3, characterized in that, Each stage of the interconnected counter-swirling units has a gas circulation function, and structural characteristic parameters characterizing the mass transfer effect of the counter-swirling units are set. : ， set up The range is 5 to 15. The range is 320 to 420 mm. and The ratio ranges from 0.7 to 1.

0. and The ratio ranges from 0.01 to 0.

1. and The ratio ranges from 0.2 to 0.8; among which, This is the pressure value at the liquid inlet (1000). The pressure value is the gas-liquid counter-current swirling chamber (1017).

5. The fluid mass transfer device for enhancing bubbles using multi-stage counter-current single swirl as described in claim 1, characterized in that, The dissolved oxygen mass transfer coefficient of the device ranges from 0.01 to 0.05; the volumetric flow rate ratio of liquid to gas in the swirling cavity (101) is from 1 to 50.

6. A fluid mass transfer method using the multi-stage counter-current single swirling enhanced bubble fluid mass transfer device as described in claim 1, characterized in that, Specifically, the following steps are included: In step S1, the liquid enters the reverse cyclone separator (10) through the liquid inlet (1000); In step S2, the gas enters through the gas axial inlet (1016) and mixes with the liquid, generating a swirling field composed of a group of bubbles in the gas-liquid countercurrent swirling chamber (1017); Step S3: In the gas-liquid countercurrent swirling chamber (1017), the liquid swirls from the center to the side wall (200) 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 (200) and the bubbles swirl towards the center. Step S4: The swirled gas is discharged through the gas outlet (1010), and the discharged gas is detected by the equipment. If the swirled liquid has reached the last stage of the reverse swirling unit, then proceed to step S5; otherwise, return to step S1. In step S5, the swirled liquid is discharged through the liquid outlet (2010) of the last stage counter-swirling unit, and the discharged liquid is detected by the equipment.

7. The fluid mass transfer method according to claim 6, characterized in that, The rotational acceleration of the liquid in the gas-liquid counter-current swirling chamber (1017) is 40 to 1000 times the acceleration due to gravity, and the pressure drop of the liquid ranges from 0.01 to 0.25 MPa; the gas-liquid separation efficiency is 70% to 95%.

8. The fluid mass transfer method according to claim 6, characterized in that, In each stage of the counter-swirling unit, the average velocity of the liquid injection liquid inlet (1000) is 4 to 20 m / s; the velocity of the liquid discharge liquid outlet (2010) is 1 to 10 m / s; the average flow velocity of the gas at the gas axial inlet (1016) is within the range of 1 to 8 m / s; and the average flow velocity of the gas at the gas outlet (1010) is within the range of 1 to 5 m / s.

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