A reactor for intensifying the gas-liquid mass transfer process of high viscosity fluid

Abstract

The application relates to the technical field of chemical reaction equipment, and discloses a reactor for intensifying the gas-liquid mass transfer process of high-viscosity fluid, which comprises a reactor shell, spiral fillers, a high-viscosity fluid distributor and a reactor base. The core innovation of the reactor lies in the spiral structure which, under the support of equidistant spiral lines, promotes the condensation of high-viscosity fluid to form liquid bridges and makes the liquid bridges flow downward along spiral tracks, thereby constructing a unique semi-restrained liquid flow mode. In this mode, the gas-phase reactants realize high-efficiency gas-liquid mass transfer reaction at the gas-liquid interfaces on the inner and outer sides of the spiral liquid bridges. Through the unique design of the spiral structure, the application effectively solves the problems existing in the gas-liquid mass transfer reaction of high-viscosity fluid, such as uneven distribution, local liquid film thickening, poor wettability of high-viscosity fluid leading to the reduction of gas-liquid contact area and the like, significantly improves the mass transfer efficiency and reaction absorption rate, reduces the system pressure drop, and realizes the uniform distribution of gas-liquid fluid and the significant inhibition of flow backmixing.

Description

Technical Field

[0001] This invention relates to the field of chemical reaction equipment technology, specifically to a reactor using spiral liquid bridge falling film structured packing, suitable for high-viscosity fluid gas-liquid phase mass transfer reaction processes. Background Technology

[0002] With the increasing prominence of global climate change, CO2 capture has become a crucial component of CCUS (Carbon Dioxide, Gas, and Gas) technology. Among existing CO2 capture technologies, chemical absorption based on alkanolamine absorbents is considered one of the most promising industrial application routes due to its high capture efficiency, technological maturity, and adaptability. However, traditional chemical absorption methods still suffer from high energy consumption and operating costs, limiting their further large-scale application.

[0003] In chemical absorption methods, high energy consumption during absorbent regeneration is a significant factor contributing to the high system cost. Taking a conventional 30 wt.% ethanolamine aqueous solution as an example, its regeneration process requires not only significant sensible heat for temperature rise but also latent heat consumption due to the vaporization of a large amount of water. To reduce regeneration energy consumption, researchers have proposed using organic solvents instead of water as the absorbent solvent. Compared to traditional water-based systems, non-aqueous absorbents show greater potential in reducing heat consumption and increasing circulation capacity.

[0004] However, non-aqueous absorbents generally suffer from high viscosity, and the solution viscosity often increases further after CO2 absorption. High liquid viscosity not only worsens flow conditions but also weakens liquid dispersibility and gas-liquid mass transfer performance. For example, studies have shown that in certain low-water systems, the viscosity of the CO2-rich solution can be significantly higher than that of a conventional 30 wt.% MEA aqueous solution. This high viscosity characteristic has become one of the important factors restricting the industrial application of non-aqueous absorbents.

[0005] Liquid viscosity is a key factor affecting fluid distribution, liquid film morphology, and gas-liquid mass transfer efficiency. For high-viscosity fluids, problems such as uneven distribution, localized liquid film thickening, and poor wettability are prone to occur in conventional mass transfer equipment. This leads to a decrease in the actual gas-liquid contact area, an increase in mass transfer resistance, and further weakens the performance advantages of the absorbent itself.

[0006] To address the aforementioned problems, existing technologies primarily improve the flow and mass transfer performance of high-viscosity fluids by optimizing the structure of structured packing materials. For example:

[0007] CN103182241B proposes a process for absorbing CO2 with a high-viscosity amine solution. This method involves the high-viscosity absorbent solution contacting the gas in a counter-current or co-current flow within a structured packing material on a vertical plate in a straight channel, thereby enhancing gas-liquid mass transfer. The patent disclosure defines the high-viscosity absorbent solution as an amine absorbent solution with a viscosity greater than 3 mPa·s. The DEA solution used in the embodiments has a viscosity range of 1-15 mPa·s, and it shows that the liquid-phase mass transfer coefficient can be improved within a certain viscosity range. However, this method mainly relies on the liquid film flow on the plate surface, and the liquid distribution still largely depends on top spraying and wall wetting. For high-viscosity systems, especially those where the viscosity further increases after CO2 loading, problems such as insufficient local wetting and liquid film thickening are still likely to occur.

[0008] CN103191692A discloses a structured packing material with alternating walled and wallless liquid films adapted to viscous absorbents. This material improves the film formation and mass transfer behavior of viscous absorbents in structured packings by constructing a structure where attached and free films flow alternately. However, it essentially still belongs to the reinforcement concept of sheet-like structured packings, where liquid flow and gas-liquid contact mainly rely on the alternating interactions between inter-plate channels, wall regions, and free films in pores. Further improvements are still needed to achieve a stable, continuous, and renewable liquid flow interface for high-viscosity liquids in open spaces, while simultaneously considering a longer gas-liquid contact path and lower pressure drop.

[0009] Therefore, developing a novel gas-liquid phase mass transfer reactor that can effectively alleviate problems such as uneven distribution of high-viscosity fluids, thickening of liquid films, and insufficient interface renewal, and achieve stable continuous flow of liquid and efficient gas-liquid contact under low pressure drop conditions, has important application value. Summary of the Invention

[0010] To address the shortcomings and deficiencies of existing technologies, the present invention aims to provide a reactor for enhancing the gas-liquid phase mass transfer process of high-viscosity fluids. By utilizing the excellent liquid self-distribution performance of the internal spiral liquid bridge falling film structure, uniform liquid distribution is achieved, significantly enhancing mass transfer efficiency while maintaining a low pressure drop. This solves the bottleneck problems of severe backmixing of high-viscosity fluids in the internal components of the tower, uneven gas-liquid distribution, and difficulties in reactor scale-up.

[0011] This invention is achieved through the following technical solution:

[0012] A reactor for enhancing gas-liquid phase mass transfer processes of high-viscosity fluids, comprising:

[0013] Reactor shell: Vertically placed, it is a cylindrical sleeve structure with inner and outer jackets, which provides a mass transfer reaction site for gas-liquid phase contact; its inner and outer jacket design provides conditions for isothermal operation of the reaction system.

[0014] The spiral packing assembly is vertically installed in the internal cavity of the reactor shell, and its upper end is fixed to the inner sleeve of the high viscosity fluid distributor. The spiral packing assembly is formed by continuously winding a single rectangular cross-section metal wire along a spiral trajectory with equal diameter and equal spiral gap to form a vertical spiral structure with uniform spiral gap.

[0015] A high-viscosity fluid distributor is installed above the reactor shell and is sealed to the upper end of the reactor shell via a flange connection. The high-viscosity fluid distributor has an outer sleeve and an inner sleeve. The outer sleeve has a liquid inlet on its side and is structured as a liquid storage tank. When a certain liquid level is reached in the outer sleeve, the overflow liquid flows downward along the wall of the inner sleeve, providing a stable liquid flow rate for the inner sleeve. The inner sleeve has a liquid distribution port on its wall, through which the overflow liquid is guided and distributed to the surface of the spiral packing assembly. The upper part of the inner sleeve has a gas phase inner outlet, and the bottom side of the outer sleeve has a gas phase outer outlet.

[0016] Reactor base: Located below the reactor shell, it is sealed to the lower end of the reactor shell through a flange connection. The reactor base is a semi-closed tubular structure with an open top. Its side wall has an outer gas phase inlet, the center of the reactor base has an inner gas phase inlet, and the bottom has a liquid phase outlet.

[0017] In the above technical solution, the spiral packing assembly is formed by continuously winding a single rectangular cross-section metal wire along a spiral trajectory with equal diameter and equal spiral gap, thus forming a vertical spiral structure with uniform spiral gap.

[0018] In the above technical solution, the wire width of the spiral packing assembly is 1.0mm to 2.5mm, the spiral outer diameter is 10mm, the spiral gap is 1.0mm to 2.5mm, and the height is 350mm to 450mm.

[0019] In the above technical solution, the ratio of the height of the reactor shell to its outer cross-sectional diameter is 35:9 to 45:9; the ratio of the diameter of the internal cavity cross-section of the reactor shell to its outer cross-sectional diameter is 3:9 to 5:9.

[0020] In the above technical solution, the ratio of the outer diameter of the inner sleeve of the high viscosity fluid distributor to the inner diameter of its outer sleeve is 1:2.5 to 1:3.5; the opening diameter of the inner gas phase outlet and the outer gas phase outlet is 5 mm to 7 mm; and the opening diameter of the liquid phase inlet is 2 mm to 4 mm.

[0021] In the above technical solution, the opening diameter of the outer gas phase inlet and the inner gas phase inlet is 5mm to 7mm; the opening diameter of the liquid phase outlet is 5mm to 7mm.

[0022] On the other hand, the above-mentioned method of using a reactor for enhancing the gas-liquid phase mass transfer process of high-viscosity fluid includes the following steps: gaseous reactants enter from the outer gas phase inlet and the inner gas phase inlet of the reactor base and enter the reactor shell; high-viscosity fluid enters from the liquid phase inlet of the high-viscosity fluid distributor, and after a certain liquid level is formed in the outer sleeve of the high-viscosity fluid distributor, the liquid overflow flows downward along the pipe wall of the inner sleeve and is guided and distributed to the surface of the spiral packing assembly; the high-viscosity fluid flows downward along the spiral line of the spiral packing assembly under the action of gravity, forming a stable and uniform liquid bridge; the downward flowing high-viscosity fluid and the upward flowing gaseous reactants undergo gas-liquid countercurrent contact in the gaps and surfaces of the spiral packing assembly, and a mass transfer reaction occurs; the tail gas after the reaction leaves the reactor from the inner gas phase outlet and the outer gas phase outlet of the high-viscosity fluid distributor; the high-viscosity fluid product after the reaction leaves the reactor from the liquid phase outlet of the reactor base.

[0023] Compared with the prior art, the present invention has the following main advantages:

[0024] (1) The spiral packing used in this invention has strong fluid self-distribution performance within the equidistant spiral gaps, enabling high-viscosity fluids to form uniform and stable liquid bridges along the spiral due to gravity. Furthermore, the packing adopts an independent modular structure design, effectively ensuring the uniform distribution of the gas and liquid phases on the reactor, overcoming the problems of uneven distribution and thick liquid films that easily occur with traditional packing for high-viscosity fluids. Especially for working fluids with a viscosity of 30 mPa·s or higher at the operating temperature, and for systems where the viscosity further increases to 60 mPa·s or higher due to gas absorption, this invention can still maintain a relatively stable liquid distribution and continuous liquid bridge flow, thereby maintaining a high gas-liquid mass transfer efficiency.

[0025] (2) Compared with traditional corrugated structured packing, the spiral packing used in this invention significantly reduces the flow resistance of the gas phase when passing through the packing, thus achieving a lower system pressure drop.

[0026] (3) The spiral packing used in this invention makes both its external surface and internal gaps highly efficient gas-liquid contact areas. Compared with traditional packings of the same specifications, its effective gas-liquid contact area is significantly increased, which greatly promotes the mass transfer and heat transfer process.

[0027] (4) In the process of the liquid phase flowing downward along the spiral trajectory in the device of the present invention, compared with vertical downward flow, the flow length per unit height of the spiral increases, which effectively prolongs its residence time in the packing. Furthermore, the residence time of the reactants in the reactor can be precisely controlled by adjusting the height of the packing. Attached Figure Description

[0028] Figure 1 This is the front view of the present invention;

[0029] Figure 2 This is a cross-sectional view of the high-viscosity fluid distributor of the present invention along the AA direction;

[0030] Figure 3 This is a diagram showing the specifications of the spiral packing of the present invention; the parameters are as follows: spiral height (H), diameter (D), spiral gap (W), line width (L), line thickness (B), and spiral inclination angle (θ).

[0031] in:

[0032] 1. Reactor shell; 2. Helical packing assembly; 3. High viscosity fluid distributor; 4. Liquid phase distribution port; 5. Gas phase inner outlet; 6. Liquid phase inlet; 7. Gas phase outer outlet; 8. Gas phase outer inlet; 9. Reactor base; 10. Liquid phase outlet; 11. Gas phase inner inlet. Detailed Implementation

[0033] The following is in conjunction with the appendix Figures 1 to 3 The present invention will be further described in detail below with reference to specific embodiments. It should be noted that the following embodiments are for illustrative purposes only and are not intended to limit the scope of protection of the present invention.

[0034] The reactor shell mentioned in the following embodiments is made of plexiglass, which facilitates observation of the phenomena during the experiment; the spiral packing assembly, the high-viscosity fluid distributor and the reactor base are all made of 304 stainless steel.

[0035] A reactor for enhancing the gas-liquid phase mass transfer process of high-viscosity fluid includes a reactor shell 1, a helical packing assembly 2, a high-viscosity fluid distributor 3, and a reactor base 9. The reactor shell 1 is vertically positioned and has an inner and outer jacketed cylindrical tube structure, providing a mass transfer reaction site for gas-liquid phase contact. The high-viscosity fluid distributor 3 is located above the reactor shell 1 and is sealed to the upper end of the reactor shell 1 via a flange connection. The high-viscosity fluid distributor 3 has an outer sleeve and an inner sleeve. A liquid inlet 6 is provided on the side of the outer sleeve. The outer sleeve structure is a liquid storage tank. When a certain liquid level is reached in the outer sleeve, the liquid overflows and flows downwards along the wall of the inner sleeve, providing a stable liquid flow rate to the inner sleeve. The tube wall is provided with a liquid phase distribution port 4, through which overflow liquid is guided and distributed to the surface of the spiral packing assembly 2; the upper part of the inner sleeve is provided with a gas phase inner outlet 5, and the bottom side of the outer sleeve is provided with a gas phase outer outlet 7; the reactor base 9 is located below the reactor shell 1 and is sealed to the lower end of the reactor shell 1 through a flange connection. The reactor base 9 is a semi-closed tubular structure with an open upper end, and its side wall is provided with a gas phase outer inlet 8. The center of the reactor base is provided with a gas phase inner inlet 11, and the bottom is provided with a liquid phase outlet 10.

[0036] The spiral packing assembly 2 is vertically arranged in the internal cavity of the reactor shell 1, and its upper end is fixed to the inner sleeve of the high viscosity fluid distributor 3. The spiral packing assembly 2 is formed by continuously winding a single rectangular cross-section metal wire along a spiral trajectory with equal diameter and equal spiral gap, forming a vertical spiral structure with uniform spiral gap.

[0037] The gaseous reactants enter the reactor base 9 through the outer gas phase inlet 8 and the inner gas phase inlet 11, and then enter the reactor shell 1. The high-viscosity fluid enters through the liquid phase inlet 6 of the high-viscosity fluid distributor 3. After a certain liquid level is formed in the outer sleeve of the high-viscosity fluid distributor 3, the liquid overflows and flows downward along the wall of the inner sleeve, and is guided and distributed to the surface of the spiral packing assembly 2. Under the action of gravity, the high-viscosity fluid flows downward along the spiral line of the spiral packing assembly 2, forming a stable and uniform liquid bridge. The downward flowing high-viscosity fluid and the upward flowing gaseous reactants undergo gas-liquid countercurrent contact in the gaps and on the surface of the spiral packing assembly 2, resulting in a mass transfer reaction. The tail gas after the reaction leaves the reactor through the inner gas phase outlet 5 and the outer gas phase outlet 7 of the high-viscosity fluid distributor 3. The high-viscosity fluid product after the reaction leaves the reactor through the liquid phase outlet 10 of the reactor base 9.

[0038] The non-aqueous amine working solution in the following examples was prepared using ethanolamine (MEA) and ethylene glycol (EG), with MEA comprising 30% by mass. At 25°C, the initial viscosity of this working solution was 29.4 mPa·s, and the viscosity could further increase to over 60 mPa·s with increasing CO2 loading during the gas-liquid phase mass transfer absorption process. The working solution could still form a relatively stable spiral liquid bridge downflow within the reactor of this invention, achieving continuous gas-liquid countercurrent contact mass transfer. The gas phase consisted of nitrogen (N2) and CO2 mixed in a gas buffer tank, with CO2 comprising 20% ​​by volume.

[0039] In the following embodiments, the CO2 capture performance uses CO2 absorption rate as the main evaluation index. Specifically, after the device reaches a stable operating state, the changes in CO2 concentration in the gas phase at the reactor inlet and outlet are measured, and the CO2 absorption rate is calculated based on the gas phase concentration change results. Simultaneously, the CO2 absorption in the liquid phase sample at the reactor outlet is measured using the acid titration-closed drainage method, and the gas phase calculation results are verified to characterize the device's CO2 absorption effect. Since the inert gas N2 does not participate in mass transfer during the absorption process, the CO2 absorption rate can be calculated based on the change in the molar ratio of CO2 to inert gas in the inlet and outlet gases.

[0040]

[0041] in, ΦIndicates CO2 absorption rate, % V 0 This represents the molar flow rate of CO2 at the reactor inlet, in mol·(L·min). -1 ;in, G g Expressed as the molar flow rate of the inert gas N2 (mol·(L·min)). -1 ; Y 0 and Y 1 These represent the molar ratios of CO2 and inert gas in the gas phase at the reactor inlet and reactor outlet, respectively.

[0042] Example 1:

[0043] The spiral structured packing is made of 304 stainless steel rectangular cross-section wire machined along a helical trajectory of equal diameter. The cross-section is a solid rectangle, the helix width is 2 mm, the helical gap is 2 mm, the outer diameter is 10 mm, and the packing height is 0.4 m. It is installed in a reactor with an inner diameter of 20 mm. The working liquid is fed from the top of the reactor at 6 ml / min, and the mixed gas phase is fed from the bottom of the reactor at 500 mL / min. The non-aqueous absorbent and CO2 undergo a countercurrent contact reaction process in the reactor. The reactor operates at atmospheric pressure, and the reaction temperature is 25 °C. The reaction products are collected from the liquid phase outlet. After 30 minutes of reaction, the CO2 concentration at the gas phase outlet remains stable, and the measured CO2 absorption rate is 97.4%.

[0044] Example 2:

[0045] The spiral structured packing is made of 304 stainless steel rectangular cross-section wire machined along a helical trajectory of equal diameter. The cross-section is a solid rectangle with a spiral width of 2mm, a spiral gap of 1.5mm, an outer diameter of 10mm, and a packing height of 0.4m. It is installed in a reactor with an inner diameter of 20mm. The working liquid is fed from the top of the reactor at a rate of 6ml / min, and the mixed gas phase is fed from the bottom of the reactor at a rate of 500mL / min. The non-aqueous absorbent and CO2 undergo a countercurrent contact reaction process in the reactor. The reactor operates at atmospheric pressure, and the reaction temperature is 25℃. The reaction products are collected from the liquid phase outlet. After 30 minutes of reaction, the CO2 concentration at the gas phase outlet remains stable, and the measured CO2 absorption rate is 92%.

[0046] Example 3:

[0047] The spiral structured packing is made of 304 stainless steel rectangular cross-section wire machined along a helical trajectory of equal diameter. The cross-section is a solid rectangle, the helix width is 1.5 mm, the helical gap is 1.5 mm, the outer diameter is 10 mm, and the packing height is 0.4 m. It is installed in a reactor with an inner diameter of 20 mm. The working liquid is fed from the top of the reactor at 6 ml / min, and the mixed gas phase is fed from the bottom of the reactor at 500 mL / min. The non-aqueous absorbent and CO2 undergo a countercurrent contact reaction process in the reactor. The reactor operates at atmospheric pressure, and the reaction temperature is 25 °C. The reaction products are collected from the liquid phase outlet. After 30 minutes of reaction, the CO2 concentration at the gas phase outlet remains stable, and the measured CO2 absorption rate is 99.4%.

[0048] Example 4:

[0049] The spiral structured packing is made of 304 stainless steel rectangular cross-section wire machined along a helical trajectory of equal diameter. The cross-section is a solid rectangle, the helix width is 1.5 mm, the helical gap is 1 mm, the outer diameter is 10 mm, and the packing height is 0.4 m. It is installed in a reactor with an inner diameter of 20 mm. The working liquid is fed from the top of the reactor at 6 ml / min, and the mixed gas phase is fed from the bottom of the reactor at 500 mL / min. The non-aqueous absorbent and CO2 undergo a countercurrent contact reaction process in the reactor. The reactor operates at atmospheric pressure, and the reaction temperature is 25 °C. The reaction products are collected from the liquid phase outlet. After 30 minutes of reaction, the CO2 concentration at the gas phase outlet remains stable, and the measured CO2 absorption rate is 98.7%.

[0050] Example 5:

[0051] The spiral structured packing is made of 304 stainless steel rectangular cross-section wire machined along a helical trajectory of equal diameter. The cross-section is a solid rectangle, the helix width is 2.5 mm, the helical gap is 2 mm, the outer diameter is 10 mm, and the packing height is 0.4 m. It is installed in a reactor with an inner diameter of 20 mm. The working liquid is fed from the top of the reactor at 6 ml / min, and the mixed gas phase is fed from the bottom of the reactor at 500 mL / min. The non-aqueous absorbent and CO2 undergo a countercurrent contact reaction process in the reactor. The reactor operates at atmospheric pressure, and the reaction temperature is 25 °C. The reaction products are collected from the liquid phase outlet. After 30 minutes of reaction, the CO2 concentration at the gas phase outlet remains stable, and the measured CO2 absorption rate is 93%.

[0052] The above description is only a preferred embodiment of the present invention. It should be noted that for those skilled in the art, several modifications and improvements can be made without departing from the inventive concept, and these all fall within the protection scope of the present invention.

Claims

1. An intensified gas-liquid mass transfer process reactor for high viscosity fluids, characterized in that, include: The reactor shell (1) is placed vertically and is a cylindrical sleeve structure with inner and outer layers, which provides a mass transfer reaction site for gas-liquid phase contact. The spiral packing assembly (2) is vertically arranged in the internal cavity of the reactor shell (1), and its upper end is fixed to the inner sleeve of the high viscosity fluid distributor (3); the spiral packing assembly (2) is formed by continuously winding a single rectangular cross-section metal wire along a spiral trajectory with equal diameter and equal spiral gap to form a vertical spiral structure with uniform spiral gap. A high-viscosity fluid distributor (3) is installed above the reactor shell (1) and is sealed to the upper end of the reactor shell (1) through a flange connection. The high-viscosity fluid distributor (3) has an outer sleeve and an inner sleeve. The outer sleeve has a liquid inlet (6) on its side. The outer sleeve is a liquid storage tank. When the outer sleeve reaches a certain liquid level, the liquid overflows and flows downward along the pipe wall of the inner sleeve to provide a stable liquid flow rate for the inner sleeve. The inner sleeve has a liquid distribution port (4) on its pipe wall. The overflow liquid is guided and distributed to the surface of the spiral packing assembly (2) through the liquid distribution port (4). The inner sleeve has a gas phase inner outlet (5) at the top and the outer sleeve has a gas phase outer outlet (7) at the bottom side. The reactor base (9) is located below the reactor shell (1) and is sealed to the lower end of the reactor shell (1) through a flange connector. The reactor base (9) is a semi-closed tubular structure with an open upper end. Its side wall is provided with an outer gas phase inlet (8), the center of the reactor base is provided with an inner gas phase inlet (11), and the bottom is provided with a liquid phase outlet (10).

2. The reactor for enhancing high-viscosity fluid gas-liquid phase mass transfer process according to claim 1, characterized in that: The spiral packing assembly (2) has a wire width of 1.0 mm to 2.5 mm, a spiral outer diameter of 10 mm, a spiral gap of 1.0 mm to 2.5 mm, and a height of 350 mm to 450 mm.

3. The reactor for enhancing high-viscosity fluid gas-liquid phase mass transfer process according to claim 1, characterized in that: The ratio of the height of the reactor shell (1) to its outer cross-sectional diameter is 35:9 to 45:9; the ratio of the diameter of the internal cavity cross-section of the reactor shell (1) to its outer cross-sectional diameter is 3:9 to 5:

9.

4. The reactor for enhancing high-viscosity fluid gas-liquid phase mass transfer process according to claim 1, characterized in that: The ratio of the outer diameter of the inner sleeve to the inner diameter of the outer sleeve of the high viscosity fluid distributor (3) is 1:2.5 to 1:3.5; the opening diameter of the inner gas phase outlet (5) and the outer gas phase outlet (7) is 5 mm to 7 mm; and the opening diameter of the liquid phase inlet (6) is 2 mm to 4 mm.

5. The reactor for enhancing high-viscosity fluid gas-liquid phase mass transfer process according to claim 1, characterized in that: The opening diameter of the outer gas phase inlet (8) and the inner gas phase inlet (11) is 5 mm to 7 mm; the opening diameter of the liquid phase outlet (10) is 5 mm to 7 mm.

6. A method of using a reactor for enhanced high-viscosity fluid gas-liquid phase mass transfer process according to any one of claims 1 to 5, characterized in that, Includes the following steps: The gaseous reactants enter from the outer gas phase inlet (8) and the inner gas phase inlet (11) of the reactor base (9) and enter the interior of the reactor shell (1); the high viscosity fluid enters from the liquid phase inlet (6) of the high viscosity fluid distributor (3), and after a certain liquid level is formed in the outer sleeve of the high viscosity fluid distributor (3), the liquid overflow flows downward along the pipe wall of the inner sleeve and is guided to be distributed to the surface of the spiral packing assembly (2); the high viscosity fluid flows downward along the spiral line of the spiral packing assembly (2) under the action of gravity, forming a stable and uniform liquid bridge; the downward flowing high viscosity fluid and the upward flowing gaseous reactants make gas-liquid countercurrent contact in the gaps and surfaces of the spiral packing assembly (2) and a mass transfer reaction occurs; the tail gas after the reaction leaves the reactor from the inner gas phase outlet (5) and the outer gas phase outlet (7) of the high viscosity fluid distributor (3); the high viscosity fluid product after the reaction leaves the reactor from the liquid phase outlet (10) of the reactor base (9).

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