A jet loop reactor

Abstract

The embodiment of the application provides a kind of jet loop reactor, it is related to the technical field of chemical equipment, including the reactor body and the loop reactor of jet device.The reactor body is equipped with reaction liquid feed inlet, gas discharge port and reaction liquid discharge port.Jet device is longitudinally arranged along the reaction liquid feed inlet and is interconnected with each other mixing channel, contraction channel and expansion channel, mixing channel is equipped with liquid circulating feed inlet and reaction liquid nozzle, and separated liquid enters mixing channel and mixes with reaction liquid by circulating feed inlet, contraction channel gradually shrinks along the material flow direction, and expansion channel gradually expands along the flow direction, by the synergistic effect of mixing channel, contraction channel and expansion channel in jet device, combined with the double circulation flow channel formed by flow guide piece, the gas-liquid-solid three-phase mixing effect is strengthened, effectively prevent solid deposition and bubble coalescence, with the advantages of uniform mixing, high reaction efficiency and stable operation.

Description

Technical Field

[0001] This application relates to the technical field of chemical equipment, and more particularly to a jet-type circulating reactor. Background Technology

[0002] Chemical reactors are key core equipment in modern chemical production and are widely used in chemical, oil refining, and metallurgical fields.

[0003] A circulating reactor is a common type of chemical reactor, mainly consisting of a reactor body, flow guides, and a feed system. The flow guides are coaxially installed inside the reactor body, forming an annular flow channel. Solid-liquid two-phase feed pipes and gaseous feed pipes are located on both sides of the bottom of the reactor. Gas nozzles and reaction liquid nozzles are configured at the bottom of the flow guides. The gaseous material is directly connected to the gas nozzles through the feed pipes, while the liquid material is connected to the reaction liquid nozzles through the other feed pipe.

[0004] However, the above-mentioned circulating reactor is mainly suitable for gas-liquid reactions. When applied to gas-liquid-solid reactions, the single circulating flow formed by the guide element cannot provide sufficient shear force, making it difficult for solid particles to be uniformly suspended. This results in the formation of a deposition zone at the bottom of the annular channel, reducing the effective reaction volume and significantly lowering the catalyst utilization rate. It also leads to excessive bubble aggregation in the high solid content system, significantly reducing the gas-liquid contact area and decreasing the mass transfer efficiency. This results in uneven three-phase mixing, forming local concentration differences, which affects the reaction selectivity and product yield.

[0005] Therefore, there is an urgent need for a jet-type circulating reactor that can maintain a high gas holdup and a stable circulation state, enhance the contact between the gas, liquid, and solid phases, improve mass and heat transfer, increase reaction efficiency, shorten reaction time, provide mild reaction conditions, ensure good safety, and enable continuous production. Utility Model Content

[0006] This application provides a jet-type circulating reactor, which can fully mix the reaction liquid, enhance the contact between the gas, liquid, and solid phases, improve the mass and heat transfer effect, greatly improve the reaction efficiency, shorten the reaction time, provide mild reaction conditions, and ensure good safety, enabling continuous production.

[0007] In a first aspect, embodiments of this application provide a jet-type circulating reactor, comprising: a reactor body having a reaction liquid inlet, a gas outlet, and a reaction liquid outlet; and a jetting device having interconnected mixing channels, contraction channels, and expansion channels along the longitudinal direction of the reaction liquid inlet. The mixing channel has a liquid circulation inlet and a reaction liquid nozzle for jetting the reaction liquid. Liquid separated from the gas outlet enters the mixing channel through the liquid circulation inlet and mixes with the reaction liquid. The contraction channel gradually contracts along the material flow direction, and the expansion channel gradually expands along the material flow direction.

[0008] In one possible implementation, the spray direction of the reaction liquid nozzle is perpendicular to the axial direction of the liquid circulation inlet.

[0009] In one possible implementation, a flow guide is provided inside the reactor body, forming an upward channel for the reaction liquid to flow from bottom to top, and a downward channel for the reaction liquid to flow from top to bottom is formed between the outer wall of the flow guide and the inner wall of the reactor body.

[0010] In one possible implementation, a flow-rectifying baffle is provided inside the flow guide and between the inner wall of the reactor body and the outer wall of the flow guide to break up bubbles in the reaction liquid.

[0011] In one possible implementation, the outer wall of the reactor body is provided with a first heat exchange jacket, and the outer wall of the flow guide is provided with a second heat exchange jacket.

[0012] In one possible implementation, a gas injection device is also included, which is used to inject gas into the rising channel to drive a portion of the reaction liquid into the rising channel and to drive a portion of the reaction liquid to circulate between the falling channel and the rising channel.

[0013] In one possible implementation, the gas injection device includes a gas feed pipe and a horizontally arranged annular pipe. The annular pipe has multiple gas outlet holes evenly arranged on its wall, and the gas feed pipe is used to supply gas to the annular pipe.

[0014] In one possible implementation, the reactor body has an internal collector located above the flow guide and used to capture the gas-containing reaction liquid, and the collector is connected to the gas outlet.

[0015] In one possible implementation, a gas-liquid separation device is also included, which includes a condenser and a separator. The gas discharged from the gas outlet enters the condenser and the separator. The separator delivers the separated gas to the gas inlet pipe through a gas feed pump, and the separator delivers the separated liquid to the liquid circulation inlet through a liquid feed pump.

[0016] In one possible implementation, the reaction feed inlet, reaction feed nozzle, loop pipe, flow guide, and reactor body are coaxially arranged.

[0017] This application provides a jet-type circulating reactor, which, through a longitudinally arranged mixing channel, contraction channel, expansion channel, and liquid circulation inlet, allows the liquid separated from the gas outlet to enter the mixing channel through the liquid circulation inlet and mix with the reaction liquid. The directional fluid shear force generated by the liquid effectively solves the technical problem of solid-phase accumulation. Combined with the variable-speed flow design of the contraction-expansion channel, a stable vortex-enhanced mixing mechanism is formed, which can maintain a high gas holdup and a stable circulation state. The reaction liquid can be fully mixed, enhancing the contact between the gas, liquid, and solid phases, resulting in good mass and heat transfer, greatly improving reaction efficiency, shortening reaction time, and providing mild reaction conditions with good safety, enabling continuous production. Attached Figure Description

[0018] The accompanying drawings, which are incorporated in and form part of this specification, illustrate embodiments consistent with this application and, together with the description, serve to explain the principles of this application.

[0019] Figure 1 A schematic diagram of the jet-type circulating reactor provided in this application;

[0020] Figure 2 This is a schematic diagram of the structure of the reaction liquid nozzle of the jet-type circulating reactor provided in this application;

[0021] Figure 3 A schematic diagram of the ring structure of the jet-type circulating reactor provided in this application;

[0022] Figure 4 This is a schematic diagram of the jetting device of the jet-type circulating reactor provided in this application.

[0023] Reference numerals: 1. Reactor body heat exchange jacket; 2. Reactor body; 3. Flow guide; 4. Rectifying baffle; 5. Collector; 6. Reaction liquid outlet; 7. Gas outlet; 8. Condenser; 9. Separator; 10. Gas feed pump; 11. Liquid feed pump; 12. Liquid circulation inlet; 13. Reaction liquid inlet; 14. Reaction liquid nozzle; 15. Gas injection device; 16. Reaction liquid inlet; 17. Gas feed pipe; 18. Liquid circulation feed pipe; 19. Reaction liquid feed pipe; 20. Ring pipe; 21. Gas outlet; 22. Mixing channel; 23. Contraction channel; 24. Expansion channel; 25. Removable flange; 26. Reaction liquid injection device; 27. Separation device.

[0024] The accompanying drawings illustrate specific embodiments of this application, which will be described in more detail below. These drawings and descriptions are not intended to limit the scope of the concept in any way, but rather to illustrate the concept of this application to those skilled in the art through reference to particular embodiments. Detailed Implementation

[0025] Exemplary embodiments will now be described in detail, examples of which are illustrated in the accompanying drawings. When the following description relates to the drawings, unless otherwise indicated, the same numbers in different drawings denote the same or similar elements. The embodiments described in the following exemplary embodiments do not represent all embodiments consistent with this application. Rather, they are merely examples of apparatuses and methods consistent with some aspects of this application as detailed in the appended claims.

[0026] In related technologies, circulating reactors are widely used in gas-liquid reaction systems, but they have significant drawbacks when handling three-phase reactions involving gas, liquid, and solid. Traditional structures employ a single circulating flow pattern. In the annular channel formed by the guide elements and the reactor body, solid particles easily deposit at the bottom, creating dead zones and reducing catalyst utilization. High solids content environments exacerbate bubble coalescence, reducing the gas-liquid contact area and decreasing mass transfer efficiency. These defects result in uneven three-phase mixing, making it difficult to control reaction selectivity and product yield, thus limiting the reactor's application in complex systems.

[0027] To address these issues, researchers observed that traditional reactors lack multi-stage mixing mechanisms, failing to generate sufficient turbulence intensity. Analysis of material flow characteristics revealed that solid particle suspension requires stronger shear forces, while bubble dispersion necessitates a dynamically changing pressure environment. Based on fluid mechanics principles, an energy conversion device was introduced into the feeding system, employing a multi-stage flow channel structure to alter the fluid motion state. Further integration with a circulation system design creates a continuously enhanced mixing process, thereby resolving the problems of particle deposition and bubble coalescence.

[0028] Therefore, this application proposes a circulating reactor comprising a reactor body and an injection device. The reactor body is provided with a reactant inlet, a gas outlet, and a reactant outlet. The injection device is longitudinally arranged with interconnected mixing channels, contraction channels, and expansion channels along the reactant inlet. The mixing channel is provided with a liquid circulation inlet and a reactant nozzle. The separated liquid enters the mixing channel through the circulation inlet and mixes with the reactant. The contraction channel gradually contracts along the material flow direction, and the expansion channel gradually expands along the flow direction. Through the synergistic effect of the mixing channel, contraction channel, and expansion channel in the injection device, combined with the double circulation flow channel formed by the guide element, the gas-liquid-solid three-phase mixing effect is enhanced, effectively preventing solid phase deposition and bubble aggregation. At the same time, through the optimized configuration of the heat exchange jacket and the gas injection device, the mass transfer efficiency and temperature control capability are improved, resulting in advantages such as uniform mixing, high reaction efficiency, and stable operation.

[0029] The technical solution of this application and how the technical solution of this application solves the above-mentioned technical problems are described in detail below with specific embodiments. These specific embodiments can be combined with each other, and the same or similar concepts or processes may not be described again in some embodiments. The embodiments of this application will now be described with reference to the accompanying drawings.

[0030] Combination Figures 1 to 4 This application provides a jet-type circulating reactor, which includes a reactor body 2 and a jetting device. The reactor body 2 has a reaction liquid inlet 16, a gas outlet 7 and a reaction liquid outlet 6. The jetting device is provided with a mixing channel 22, a contraction channel 23 and an expansion channel 24 that are interconnected. The mixing channel 22 is provided with a liquid circulation inlet 12 and a reaction liquid nozzle 14.

[0031] The reactor body 2 includes an outer cylinder for providing reaction space and a pressurized environment. A reaction liquid outlet 6 is located near the middle of the reactor body 2. The reaction liquid flowing out of the reaction liquid outlet 6 flows into the separation device 27 for the next process. A reaction feed inlet 16 is located at the bottom of the reactor body 2. The reaction feed liquid enters the reactor body 2 through the expansion channel 24 to react and form a reaction liquid. A gas outlet 7 is located at the top of the reactor body 2. Excess gas inside the reactor body 2 is discharged outside the reactor body 2 through the gas outlet 7 to avoid gas accumulation inside the reactor body 2, which would cause fluctuations in operating pressure.

[0032] The injection device includes a housing. Along the longitudinal direction of the reaction liquid inlet 16, the housing is longitudinally arranged a mixing channel 22, a contraction channel 23, and an expansion channel 24 that are interconnected. The mixing channel 22 is a tubular structure that achieves the initial mixing of liquid and gaseous materials, and its side wall has a liquid circulation inlet 12. The contraction channel 23 is a tapered pipe with a gradually decreasing cross-sectional area, which can be implemented using a conical or stepped contraction structure, used to accelerate fluid movement. The expansion channel 24 is a diffusion pipe with a gradually increasing cross-sectional area, which can be implemented using a funnel-shaped flaring structure, used to create a local negative pressure zone. The reaction liquid nozzle 14 is an open structure that generates a high-speed jet, used to inject the reaction liquid into the mixing channel 22, and can be a Venturi nozzle.

[0033] Specifically, the contraction channel 23 is a channel formed by the gradual contraction of the cylinder along the material flow direction, and the ratio of the channel outlet width to the channel inlet width of the contraction channel is 1:5 to 1:2. The expansion channel 24 is a channel formed by the gradual expansion of the cylinder along the material flow direction, and the ratio of the channel outlet width to the channel inlet width of the expansion channel is 10:1 to 2:1.

[0034] Specifically, the reaction liquid enters the mixing channel 22 as a high-speed jet through a nozzle, colliding and mixing with the separated liquid introduced through the circulating feed inlet. The contraction channel 23 converts the kinetic energy of the mixed fluid into velocity energy, increasing the flow shear strength. The expansion channel 24 creates a pressure gradient through cross-sectional expansion, causing bubbles to break up and disperse. After the mixed material enters the reactor body 2, it is continuously subjected to turbulence during the circulation process. Solid particles are suspended by shear force, bubbles remain dispersed in the dynamic pressure field, and the separated liquid re-participates in the mixing through the circulation system, forming a continuously enhanced mass transfer process.

[0035] Traditional circulating reactors rely solely on the guide element 3 to form a single circulating flow pattern, while this scheme constructs a dual mixing mechanism through an injection device and a liquid circulation system. In related technologies, bubble dispersion relies on a static flow field; this scheme actively controls bubble size using dynamic pressure changes generated by a contraction-expansion structure. In related technologies, solid-phase suspension relies on natural fluid turbulence; this scheme generates a high-intensity shear field through forced mixing of a high-speed jet and the circulating liquid.

[0036] Through the above technical solutions, this application effectively prevents solid particles from depositing at the bottom of the reactor, maintains uniform dispersion of the catalyst, suppresses bubble aggregation, significantly increases the gas-liquid contact area, achieves continuous mixing of three-phase materials during circulation, reduces local concentration differences, improves reaction selectivity and product yield, and the synergistic effect of the dynamic pressure field and circulation system enables the reactor to maintain stable operation in systems with high solid content.

[0037] This application further proposes a configuration in which the spray direction of the reaction liquid nozzle 14 is perpendicular to the axial direction of the liquid circulation inlet 12.

[0038] The spray direction of the reaction liquid nozzle 14 refers to the trajectory direction of the fluid jet at the nozzle outlet. This can be achieved using a conical nozzle structure with a specific outlet angle, ensuring the jet flow is orthogonal to the axial direction. The axial direction of the liquid circulation inlet 12 refers to the direction in which the centerline of the feed pipe extends. This can be achieved using a structure where a straight pipe section is coaxially arranged with the mixing channel 22, maintaining the circulating liquid flow in a single direction. The vertically positioned spray direction and the axial flow form a momentum exchange interface, generating a shear force field within the mixing channel 22, promoting the dispersion of solid particles.

[0039] Specifically, within mixing channel 22, the reactant liquid is injected laterally into the axially flowing circulating liquid through vertically positioned nozzles, creating a cross-flow pattern between the two fluid streams. The axially flowing circulating liquid carries the reactant liquid and suspended particles, while the laterally injected fresh liquid impacts the main fluid at high speed, disrupting the original laminar boundary layer and generating a three-dimensional vortex structure. This impact disperses solid particles from their aggregated state and enhances bubble breakage, ensuring that the three-phase materials are fully premixed before entering contraction channel 23.

[0040] Compared to related technologies, the reaction feed nozzles 14 of traditional circulating reactors are usually arranged in the same direction as the circulating liquid, relying solely on velocity differences for mixing, resulting in a mixing dead zone. This solution generates forced turbulence through orthogonal injection, significantly improving mixing efficiency, effectively enhancing the uniformity of solid particle suspension, and eliminating bottom sedimentation.

[0041] Through the above technical solution, this application solves the technical problem of uneven suspension of solid particles in a gas-liquid-solid three-phase system. By using the turbulent shearing effect generated by orthogonal jetting, the solid particles are uniformly dispersed in the mixing channel 22, avoiding the formation of sedimentation zones. At the same time, it enhances the gas-liquid contact area, providing a material basis for sufficient mixing in the subsequent reaction zone.

[0042] This application further proposes that the reactor body 2 is provided with a flow guide 3 inside, the inside of the flow guide 3 forms an upward channel for the reaction liquid to flow from bottom to top, and the outer wall of the flow guide 3 and the inner wall of the reactor body 2 form a downward channel for the reaction liquid to flow from top to bottom.

[0043] The flow guide 3 is a structural component installed inside the reactor body 2 to guide the flow of the reaction liquid. It can be cylindrical or conical in shape, and its axial height can cover the main reaction area inside the reactor body 2. The upward channel is a vertical flow channel formed inside the flow guide 3, specifically through a cavity enclosed by the inner wall of the flow guide 3, used to promote the upward flow of the gas-liquid-solid three-phase mixture. The downward channel is an annular space between the outer wall of the flow guide 3 and the inner wall of the reactor body 2, specifically formed by adjusting the ratio of the diameter of the flow guide 3 to the diameter of the reactor body 2, used to guide the reaction liquid downward under gravity.

[0044] Specifically, the flow guide 3 forms a dual-channel circulation system by separating the internal space of the reactor. In the ascending channel, as the reaction liquid flows upward from the bottom, bubbles and solid particles are continuously entrained by vertical convection, making it difficult for the solid particles to settle due to the increased flow velocity. In the descending channel, as the reaction liquid flows downward from top to bottom, the friction between the liquid flow and the outer wall of the flow guide 3 generates shear force, causing large bubbles to break into smaller bubbles. The density difference between the ascending and descending channels forms a circulation driving force, causing the reaction liquid to continuously circulate between the two channels. The solid particles remain suspended during the circulation process, increasing bubble dispersion and expanding the gas-liquid contact area.

[0045] In order to maintain a stable circulation state and enhance the mass and heat transfer effect, the ratio of the height of the outer cylinder to its diameter is set to 1-10, the ratio of the height of the guide 3 to its diameter is set to 1-10, and the ratio of the diameter of the guide 3 to the diameter of the outer cylinder is set to 0.2-0.8.

[0046] Traditional circulating reactors achieve liquid-phase circulation through a single annular channel, with a fixed channel width between the guide element 3 and the reactor body 2, which cannot simultaneously meet the requirements of vertical particle suspension and horizontal bubble dispersion. This solution utilizes a dual-channel structure constructed with the guide element 3 to spatially separate the upward and downward flows, optimizing for solid-phase suspension and bubble dispersion respectively, thus overcoming the technical deficiency of uneven shear force distribution under a single flow pattern.

[0047] Through the above technical solution, this application solves the problem of uneven three-phase mixing caused by solid particle deposition and bubble aggregation in traditional reactors, realizes full contact between gas, liquid and solid phases, improves the mass transfer efficiency and mixing uniformity of the reaction system, thereby improving reaction selectivity and product yield.

[0048] This application further proposes to install a flow-rectifying baffle 4 inside the flow guide 3 and between the inner wall of the reactor body 2 and the outer wall of the flow guide 3 to break up bubbles in the reaction liquid, thereby eliminating bubble coalescence and the resulting turbulence and local backmixing.

[0049] The rectifying baffle 4 refers to the physical structure installed within the flow channel. It applies mechanical shear force to the bubbles by altering the fluid flow path. Specifically, it can be implemented using an alternating plate-like structure, with its edges designed to be serrated or wavy to enhance the turbulence effect. The rectifying baffle 4 inside the guide member 3 acts on the rising channel, forcing the bubbles to deform and rupture by cutting off their continuous rising path. The rectifying baffle 4 between the outer wall of the guide member 3 and the reactor body 2 acts on the descending channel, utilizing the kinetic energy of the fluid as it descends to perform secondary breakup of the bubbles.

[0050] Specifically, in the upward channel formed inside the guide member 3, rectifier baffles 4 are vertically fixed to the inner wall of the channel at intervals. When the gas-liquid mixture flows upward, the bubbles are cut into smaller sizes at the edges of the baffles. In the annular downward channel formed by the outer wall of the guide member 3 and the inner wall of the reactor body 2, the rectifier baffles 4 are installed at an inclined angle, which generates a vortex flow field when the fluid flows downward, and the bubbles are further broken up under the vortex shearing action. The rectifier baffles 4 in the upward and downward channels work together to continuously apply a breaking force throughout the entire circulation path of the bubbles, avoiding bubble coalescence caused by pressure changes or flow velocity differences.

[0051] Compared to related technologies, traditional circulating reactors rely solely on turbulence within a single channel for bubble dispersion, without designing differentiated breakup structures to address the fluid characteristic differences between the rising and falling channels. This solution utilizes a dual-rectifying baffle layout to actively cut bubbles in the rising section and enhance secondary breakup in the falling section, thus resolving the issue of decreased mass transfer efficiency caused by bubble coalescence in high-solids-content systems.

[0052] Through the above technical solution, this application effectively suppresses the excessive aggregation of bubbles in the gas-liquid-solid three-phase reaction, maintains the high dispersion state of the gas and liquid phases, improves the gas-liquid contact area and mass transfer efficiency, and promotes the uniform suspension of solid particles, reduces local concentration differences, thereby improving reaction selectivity and product yield.

[0053] This application further proposes to provide a first heat exchange jacket on the outer wall of the reactor body 2 and a second heat exchange jacket on the outer wall of the flow guide 3.

[0054] The first heat exchange jacket is a sandwich structure covering the outer wall of the reactor body 2. Specifically, it can be implemented by a ring cavity structure formed by a double shell. The cavity is configured to allow the heat exchange medium to circulate. The overall temperature of the reaction liquid flowing in the descending channel inside the reactor body 2 is controlled by adjusting the temperature of the medium.

[0055] The second heat exchange jacket refers to the jacket structure covering the outer wall of the guide member 3. Specifically, it can be implemented by a sleeve structure coaxially installed with the guide member 3. The internal medium flow channel is independent of the first heat exchange jacket. The gas-liquid mixture in the rising channel inside the guide member 3 is locally controlled by adjusting the medium flow rate and temperature.

[0056] Specifically, the first heat exchange jacket is configured to exchange heat with the outer wall of the reactor body 2. By introducing a temperature-controlled heat exchange medium, such as circulating cooling water or heat transfer oil, into the jacket, heat is exchanged with the high-density reaction liquid flowing in the descending channel, thereby maintaining the overall temperature uniformity of the reactor. The second heat exchange jacket is configured to independently exchange heat with the outer wall of the flow guide 3. By adjusting the flow rate and temperature of the heat exchange medium within the jacket, for example using a segmented temperature control strategy, targeted heat removal is performed on the exothermic process of the gas-liquid mixture in the ascending channel. The medium circulation systems of the two heat exchange jackets can operate independently, ensuring that the temperature control of the reactor body 2 and the flow guide 3 regions does not interfere with each other, thereby eliminating local temperature gradients caused by differences in the exothermic effects of the three-phase reaction.

[0057] Compared with related technologies, traditional circulating reactors only have a single heat exchange structure in the reactor body 2, which cannot implement differentiated temperature control between the internal rising channel and the external descending channel of the guide member 3. This application increases the heat exchange area of ​​the guide member 3 region by adding a second heat exchange jacket, thereby improving the effective heat exchange area. At the same time, it allows for more precise temperature regulation of the rising channel through which the gas-liquid mixture flows, thus overcoming the deficiency of a single heat exchange device that cannot simultaneously optimize gas-liquid mass transfer and solid-phase suspension thermodynamic conditions.

[0058] Through the above technical solution, this application achieves independent temperature control in the reactor body 2 and the flow guide 3 region, effectively eliminating the uneven temperature distribution caused by insufficient heat transfer efficiency in the gas-liquid-solid three-phase reaction system. At the same time, through the synergistic effect of the double heat exchange jacket, the negative impact of local overheating on catalyst activity is avoided, ensuring the thermodynamic stability of the reaction system.

[0059] This application further proposes a gas injection device 15, which is used to inject gas into the rising channel to drive a portion of the reaction liquid into the rising channel and to drive a portion of the reaction liquid to circulate between the falling channel and the rising channel.

[0060] Among them, the gas injection device 15 refers to a device that generates kinetic energy through gas injection to drive fluid circulation. Specifically, it can be realized by a combination structure of ring pipe 20 and air outlet 21. The ring pipe 20 is horizontally arranged at the bottom of the rising channel, and the air outlet 21 is evenly distributed around the ring pipe 20. The gas forms a uniform jet through the air outlet 21, thereby forming a stable gas-liquid mixture flow in the rising channel.

[0061] To maintain a high gas holdup and a fine, uniform gas distribution within the reactor, numerous uniformly distributed gas outlets 21 are provided on the annular pipe 20. Depending on the reaction system, the diameter of the gas outlets 21 ranges from 500 to 5000 μm, and the number of outlets 21 ranges from 50 to 500. Depending on the viscosity of the reaction medium, the angle between the extension of the opening direction of the gas outlets 21 and the perpendicular line passing through the center of the annular pipe 20 and perpendicular to the plane of the annular pipe 20 is set between 0 and 30°.

[0062] The rising channel is a vertical flow channel formed inside the flow guide 3. Specifically, it can be achieved through a flow guide tube structure. The flow guide tube is arranged coaxially with the reactor body 2. Its internal space is defined as the rising channel, and its external annular space is defined as the falling channel. The gas jet acts directly on the bottom of the rising channel and drives the fluid to move upward through momentum transfer.

[0063] Among them, the circulating flow refers to the closed loop path formed by the reaction liquid between the rising channel and the falling channel. Specifically, it is achieved by the superposition of forced convection generated by the gas jet and natural convection caused by density difference. The kinetic energy generated by the gas jet drives the fluid in the rising channel to accelerate, while the density of the gas-liquid mixture decreases to form buoyancy. The dual effect drives the fluid to continuously circulate between the rising channel and the falling channel.

[0064] Specifically, the gas injection device 15 is configured to inject gas into the bottom of the rising channel. The gas enters the rising channel in jet form and mixes with the reaction liquid. The jet's kinetic energy is directly converted into fluid kinetic energy, propelling the reaction liquid upwards. At the top of the rising channel, the gas-liquid mixture generates buoyancy due to density differences, accelerating the fluid into the descending channel. Within the descending channel, the fluid moves downwards under gravity and re-enters the rising channel at the bottom, thus forming a closed loop. The turbulent shearing effect generated by the gas jet breaks up bubbles, inhibits bubble coalescence, and simultaneously enhances the suspension and dispersion of solid particles. Continuous gas injection within the rising channel creates a local gas holdup gradient, promoting full contact between the gas, liquid, and solid phases during the circulation process.

[0065] Compared to related technologies, traditional circulating reactors rely on a single circulating flow pattern, maintaining mixing solely through the natural circulation formed by the guide element 3, which cannot overcome the problems of particle deposition and bubble coalescence in high solids content systems. This scheme, by adding a gas injection device 15, superimposes forced convection and natural convection within the rising channel, forming a dual-drive mechanism that significantly enhances fluid turbulence intensity. The gas jet directly acts on key nodes of the circulation path, optimizing circulation stability through kinetic energy input, while simultaneously utilizing the jet shear effect to improve bubble dispersion and particle suspension.

[0066] Through the above technical solutions, this application can effectively prevent solid particles from depositing at the bottom of the reactor, maintain the uniform suspension distribution of catalyst particles, suppress the aggregation of bubbles in high solid content systems, increase the gas-liquid contact area, enhance the mixing efficiency of the gas-liquid-solid three phases, eliminate local concentration differences, and thus improve reaction selectivity and product yield.

[0067] This application further proposes a gas injection device 15 including a gas feed pipe 17 and a horizontally arranged annular pipe 20. The annular pipe 20 has a plurality of gas outlet holes 21 evenly arranged on its wall. The gas feed pipe 17 is used to supply gas to the annular pipe 20.

[0068] The ring pipe 20 refers to a ring-shaped pipe extending horizontally, which can be made of stainless steel or corrosion-resistant alloy material, and its diameter can match the cross-sectional dimensions of the rising channel inside the guide member 3. This structure, through its ring-shaped layout, covers the internal space of the guide member 3, ensuring a uniform radial distribution of gas in the reaction liquid.

[0069] The vent 21 refers to a through hole opened on the wall of the annular pipe 20. Specifically, it can adopt a circular or elliptical hole structure with equal spacing, and the hole diameter range is, for example, 0.5-3 mm. The uniformly distributed vent 21 forms multiple independent bubble flows, avoiding local turbulence zones caused by concentrated gas injection.

[0070] The gas feed pipe 17 refers to the gas supply pipe that is perpendicularly connected to the ring pipe 20. It can be connected by a flange or thread, and its inner diameter is, for example, 1 / 3 to 1 / 2 of the diameter of the ring pipe 20. This design balances the gas supply pressure at various points of the ring pipe 20 through the vertical connection structure, eliminating uneven gas distribution caused by differences in pipe length.

[0071] Specifically, the horizontal annular pipe 20 extends along the cross-sectional direction of the rising channel inside the guide member 3. When gas enters the annular pipe 20 through the gas feed pipe 17, it is evenly distributed to each outlet 21 along the circumference of the annular pipe 20. The gas is released simultaneously from multiple outlets 21 in the form of tiny bubbles, forming a uniformly distributed bubble group within the rising channel. Because the outlets 21 are evenly spaced and the annular pipe 20 covers the entire cross-sectional area, the bubbles maintain a symmetrical distribution in both the radial and axial directions, effectively suppressing bubble aggregation. The vertical connection between the gas feed pipe 17 and the annular pipe 20 ensures that the gas supply pressure is uniformly transmitted along the circumference of the annular pipe 20, preventing a reduction in the gas output from the distal outlets 21 due to pressure loss.

[0072] Compared to related technologies, traditional gas injection devices use single-point nozzles or asymmetrically arranged gas supply pipes, resulting in gas being released concentrated in the central area of ​​the guide element 3. This causes bubbles to collide and coalesce into large bubbles during their ascent. This solution, through a combination of annular pipes and porous structures, expands the gas dispersion area in the reaction liquid to the entire cross-section of the guide element 3. The initial bubble size and distribution density tend to be uniform, significantly reducing the probability of bubble coalescence.

[0073] Through the above technical solution, this application achieves three-dimensional uniform dispersion of gas in the reaction liquid, forming a stable and dense bubble flow. The uniformly distributed bubble cluster provides continuous and uniform fluid shear force to the solid particles, promoting full contact of the three-phase materials and eliminating local concentration differences. The contact area between the bubbles and the liquid is significantly increased, enhancing the gas-liquid mass transfer efficiency, while avoiding reaction volume loss caused by bubble coalescence.

[0074] This application further proposes to install a collector 5 inside the reactor body 2, located above the flow guide 3, for capturing the reaction liquid containing gas, and the collector 5 is connected to the gas outlet 7.

[0075] The trap 5 refers to a gas-liquid separation device installed in the space above the guide member 3. Specifically, it can be implemented using a porous plate structure or a cyclone separation structure, and its pore size range can be adapted according to the bubble diameter distribution. This device forcibly retains incompletely reacted bubbles through physical interception, causing the gas and liquid phases to form a turbulent state within the trap 5.

[0076] The area above the guide tube 3 refers to the region between the top of the guide tube inside the reactor body 2 and the reactor top cover. This can be achieved by adjusting the ratio of the guide tube height to the total height of the reactor. This location effectively intercepts the rising gas bubbles at the top of the reactor, preventing gas from directly entering the discharge pipe.

[0077] Specifically, after initial mixing in the rising channel formed by the guide element 3, the gas-containing reaction liquid enters the collector 5 for secondary separation. The separation structure inside the collector 5 creates a velocity difference between the bubbles and the liquid, trapping the bubbles and forming a gas-liquid mixture layer. At this time, the gas outlet 7 is directly connected to the gas phase space of the collector 5, forcing the trapped gas to come into contact with the fresh reaction liquid again within the collector 5. When the unseparated microbubbles enter the descending channel with the liquid, due to the high static pressure in the annular space between the guide element 3 and the reactor body 2, the bubbles are compressed, broken, and redispersed into the liquid phase.

[0078] Compared to related technologies, traditional circulating reactors without a gas trap result in low gas holdup due to unreacted gas being directly discharged with the liquid. This solution addresses this by installing a gas trap 5 above the guide vane 3, creating a forced gas-liquid separation zone and extending the residence time of bubbles within the trap 5 by approximately 30-60 seconds. In related technologies, bubbles tend to coalesce and form large bubbles during their ascent; however, this solution, through the multi-stage separation action of the trap 5, can control the average bubble diameter within the range of 0.5-2 mm.

[0079] Through the above technical solutions, this application effectively improves the gas holdup of the reaction system, increasing the gas dispersion in the liquid phase by approximately 40%. Bubble aggregation is suppressed, and the gas-liquid contact area increases by approximately 25%. The uniformity of three-phase mixing is improved, the suspension stability of solid particles is increased by approximately 35%, and the catalyst utilization rate is increased by approximately 20%. The circulation disturbance of the reaction liquid within the collector 5 reduces local concentration differences by approximately 30%, and the reaction selectivity is increased by approximately 15%.

[0080] This application further proposes a gas-liquid separation device, which includes a condenser 8 and a separator 9. The gas discharged from the gas outlet 7 enters the condenser 8 and the separator 9. The separator 9 transports the separated gas to the gas inlet pipe 17 through the gas feed pump 10, and the separator 9 transports the separated liquid to the liquid circulation inlet 12 through the liquid feed pump 11.

[0081] The condenser 8 is used to cool the reaction tail gas. Specifically, it can be achieved by using a shell-and-tube heat exchanger or a plate heat exchanger. Heat exchange is achieved through indirect contact between the cooling medium and the high-temperature gas, which promotes the phase change liquefaction of condensable components.

[0082] Among them, the liquid separator 9 refers to the container used to achieve gas-liquid two-phase separation. Specifically, it can be implemented by gravity settling separator. By setting baffles or cyclone separation structure, the separation efficiency is enhanced, so that the gas phase and liquid phase form a stable stratification in the tank.

[0083] Among them, the gas feed pump 10 is a device used to pressurize and transport the separated gas. Specifically, it can be implemented by using a diaphragm compressor or a screw gas booster to increase the gas pressure through mechanical work to meet the gas intake requirements of the reactor.

[0084] Among them, the liquid feed pump 11 refers to the equipment used to circulate and transport the separated liquid. Specifically, it can be implemented by a centrifugal pump or a gear pump. The liquid is pressurized and injected into the reaction system by the centrifugal force generated by the rotation of the impeller.

[0085] Specifically, the gas generated during the reaction is discharged from the gas outlet 7 and first enters the condenser 8 for cooling. The condensable components in the gas liquefy under low temperature conditions, forming a gas-liquid mixture that flows into the separatory tank 9. Inside the separatory tank 9, the gas and liquid phases naturally separate due to their density difference. The upper gas layer is pressurized by the gas feed pump 10 and returned to the gas feed pipe 17 to participate in the reaction process again; the lower liquid layer is pressurized by the liquid feed pump 11 and transported to the liquid circulation inlet 12, where it mixes with the fresh reaction liquid and re-enters the reactor. This design allows unreacted gaseous materials to form a closed-loop circulation within the system, while the liquid phase maintains the material balance within the reaction system through continuous reflux.

[0086] Compared to related technologies, traditional gas-liquid reaction systems typically discharge unreacted gases directly or perform only simple washing, resulting in low raw material utilization and environmental pollution risks. This solution achieves efficient separation and directional circulation of the gas and liquid phases through the synergistic action of condenser 8 and separator 9, avoiding material loss caused by open exhaust. Simultaneously, a pumping device maintains pressure balance within the reaction system, resolving the problem of reaction kinetic fluctuations caused by gas phase escape.

[0087] Through the above technical solutions, this application realizes the recovery and reuse of unreacted components in the reaction tail gas, reducing raw material consumption and waste gas emissions; the closed-loop circulation of gas and liquid phases enhances the mass transfer efficiency in the reaction system, avoiding the negative impact of local concentration differences on reaction selectivity; the continuous reflux design of the liquid circulation inlet 12 further optimizes the three-phase mixing state in the reactor, providing stable conditions for the uniform conduction of gas-liquid-solid reactions.

[0088] This application further proposes that the reaction liquid inlet 16, the reaction liquid nozzle 14, the ring pipe 20, the flow guide 3 and the reactor body 2 are arranged coaxially.

[0089] The coaxiality of the reaction liquid inlet 16 and the reaction liquid nozzle 14 means that their central axes coincide. This can be achieved through a flange connection to ensure axial positioning and that the reaction liquid injection direction is perpendicular to the circulating liquid flow. The coaxiality of the annular pipe 20 and the guide pipe 3 means that the axis of the gas distribution annular pipe 20 coincides with the center line of the guide pipe 3. This can be achieved through a ring-shaped support frame to ensure concentric positioning and uniform gas distribution across the cross-section of the rising channel. The coaxiality of the guide pipe 3 and the reactor body 2 means that the outer wall of the guide pipe and the inner wall of the reactor form an equidistant annular space. This can be achieved by welding and fixing the bottom positioning ring of the guide pipe 3, forming a symmetrical annular channel.

[0090] Specifically, the reaction liquid forms a vertical jet through the coaxially arranged inlet and nozzle, generating high-intensity shear force with the circulating liquid flow within the mixing channel 22, causing solid particles to detach from the deposition state. The gas outlet 21 of the annular pipe 20 is uniformly distributed along the axis of the guide member 3, allowing gas to enter the rising channel in a symmetrical flow pattern, preventing bubble aggregation in localized areas. The coaxial structure of the guide member 3 and the reactor body 2 forms a symmetrical circulation path, enabling the reaction liquid to form a stable circulating flow between the rising and falling channels, eliminating dead zones. The synergistic effect of the coaxial superposition of various components causes the gas and liquid phases to form a uniformly dispersed microbubble cluster within the expansion channel 24, keeping the solid particles suspended in the symmetrical flow field.

[0091] Compared to related technologies, the traditional circulating reactor's guide element 3 is eccentrically installed with the reactor body 2, resulting in uneven velocity distribution within the annular channel and the formation of a solid-phase deposition zone at the bottom. When the gas nozzle is positioned off-axis from the guide element 3, bubbles deflect and coalesce during their ascent, reducing gas-liquid contact efficiency. This solution, through a coaxial design of the entire system, creates a spatially symmetrical structure between the reaction liquid jet, gas distribution, and the circulating channel, eliminating particle settling caused by velocity gradients and suppressing bubble coalescence.

[0092] Through the above technical solution, this application achieves uniform mixing of gas, liquid and solid phases in the reactor, solid particles remain in a stable suspended state in a symmetrical flow field, microbubble clusters are uniformly dispersed in the liquid phase, the gas-liquid contact area is significantly increased, the mass transfer efficiency is effectively improved, and the concentration gradient in the reaction system is eliminated.

[0093] The working principle and process of this utility model are as follows: The reaction liquid enters the reaction liquid inlet 13 and the reaction liquid nozzle 14 through the reaction liquid inlet pipe 19, and the circulating liquid enters the liquid circulation inlet 12 through the liquid circulation inlet pipe 18. After mixing in the mixing channel 22, the two enter the circulating reactor through the contraction channel 23, the reaction liquid inlet 16, and the expansion channel 24. The gas enters the gas injection device 15 through the gas inlet pipe 17, and at the same time, it pushes the gas-liquid-solid multiphase flow reaction liquid to flow from bottom to top in the guide member 3. After passing through the collector 5 at the top of the guide member 3, gas separation is performed. Part of the gas is discharged through the gas outlet 7, and the other part of the gas is entrained by the reaction liquid into the descending channel between the reactor body 2 and the guide member 3 to continue to participate in the reaction. The gas discharged from the gas outlet 7 enters the condenser 8 and the separator 9 in sequence for gas-liquid separation. The obtained gas is returned to the gas injection device 15 by the gas feed pump 10, and the obtained liquid is returned to the liquid circulation inlet 12 by the liquid feed pump 11 to continue to participate in the reaction. Finally, the solid and liquid materials obtained from the reaction are discharged from the reaction liquid outlet 6 and enter the subsequent separation unit. The heat of polymerization is removed by the heat exchange jacket 1 of the reactor body, the heat exchange jacket of the flow guide 3, and the condenser 8, so the whole process can be carried out continuously.

[0094] Finally, it should be noted that other embodiments of this application will readily conceive of by those skilled in the art upon consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of this application that follow the general principles of this application and include common knowledge or customary techniques in the art not disclosed herein, and is not limited to the precise structures described above and shown in the accompanying drawings, and various modifications and alterations may be made without departing from its scope. The scope of this application is limited only by the appended claims.

Claims

1. A jet-type circulating reactor, characterized in that: include: The reactor body (2) has a reaction liquid inlet (16), a gas outlet (7) and a reaction liquid outlet (6) for discharging the reaction liquid. The spraying device (26) is provided with a mixing channel (22), a contraction channel (23) and an expansion channel (24) connected to each other along the longitudinal direction of the reaction liquid inlet (16). The mixing channel (22) is provided with a liquid circulation inlet (12) and a reaction liquid nozzle (14) for spraying the reaction liquid. The liquid separated from the gas outlet (7) enters the mixing channel (22) through the liquid circulation inlet (12) and mixes with the reaction liquid. The contraction channel (23) gradually contracts along the material flow direction, and the expansion channel (24) gradually expands along the material flow direction.

2. The jet-type circulating reactor according to claim 1, characterized in that: The spraying direction of the reaction liquid nozzle (14) is perpendicular to the axial direction of the liquid circulation inlet (12).

3. The jet-type circulating reactor according to claim 1, characterized in that: The reactor body (2) is provided with a flow guide (3) inside. The flow guide (3) forms an upward channel for the reaction liquid to flow from bottom to top. The outer wall of the flow guide (3) and the inner wall of the reactor body (2) form a downward channel for the reaction liquid to flow from top to bottom.

4. A jet-type circulating reactor according to claim 3, characterized in that: A flow-rectifying baffle (4) for breaking up bubbles in the reaction liquid is provided both inside the flow guide (3) and between the inner wall of the reactor body (2) and the outer wall of the flow guide (3).

5. A jet-type circulating reactor according to claim 3, characterized in that: The outer wall of the reactor body (2) is provided with a first heat exchange jacket (1), and the outer wall of the flow guide (3) is provided with a second heat exchange jacket (1).

6. A jet-type circulating reactor according to claim 3, characterized in that: It also includes a gas injection device (15) for injecting gas into the rising channel to drive a portion of the reaction liquid into the rising channel and to drive a portion of the reaction liquid to circulate between the falling channel and the rising channel.

7. A jet-type circulating reactor according to claim 6, characterized in that: The gas injection device (15) includes a gas feed pipe (17) and a horizontally arranged ring pipe (20). The ring pipe (20) has a plurality of gas outlet holes (21) evenly arranged on its wall. The gas feed pipe (17) is used to supply gas to the ring pipe (20).

8. A jet-type circulating reactor according to claim 7, characterized in that: The reactor body (2) is provided with a collector (5) located above the flow guide (3) and used to collect the reaction liquid containing gas. The collector (5) is connected to the gas outlet (7).

9. A jet-type circulating reactor according to claim 8, characterized in that: It also includes a gas-liquid separation device, which includes a condenser (8) and a separator (9). The gas discharged from the gas outlet (7) enters the condenser (8) and the separator (9). The separator (9) transports the separated gas to the gas inlet pipe (17) through a gas feed pump (10). The separator (9) transports the separated liquid to the liquid circulation inlet (12) through a liquid feed pump (11).

10. A jet-type circulating reactor according to claim 7, characterized in that: The reaction liquid inlet (16), reaction liquid nozzle (14), ring pipe (20), flow guide (3) and reactor body (2) are coaxially arranged.

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