Anti-coking reactor for coal tar processing

Abstract

The invention relates to the technical field of coal tar deep processing equipment, in particular to a coal tar processing anti-coking reactor which mainly comprises a reactor body, a feeding part, a discharger and an external separator. An inner kettle body is arranged in the reactor body, and the inner space of the inner kettle body is divided into a feeding cavity, a reaction area and a discharging area from top to bottom. A flow-equalizing turnover assembly is installed in the feeding cavity and used for receiving and distributing materials from the feeding part, a rotatable static mixer is installed in the reaction area, and strong turbulent flow is generated through a spiral piece structure nested inside and outside the static mixer, so that deep mixing is achieved. A temperature control unit wraps the periphery of the reactor, a plurality of heat conduction pipelines are wound in a parallel spiral mode to form a uniform honeycomb heat exchange surface, and the reaction temperature is accurately controlled. Through the synergistic effect of uniform flow turnover, dynamic mixing and uniform temperature control, the material mixing efficiency and the temperature field uniformity are remarkably improved, the local coking phenomenon is fundamentally and effectively inhibited, and the reaction efficiency and the product yield are improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of coal tar deep processing equipment, in particular to a coal tar processing anti-coking reactor. BACKGROUND

[0002] Coal tar is an important by-product produced in the process of coal dry distillation and gasification, which is extremely complex in composition and contains a large amount of aromatic hydrocarbons and heterocyclic compounds. It is a key raw material for obtaining high-value chemical products. In the processing of coal tar, especially in the process of thermal cracking, catalytic hydrogenation or condensation reaction, the reaction materials usually have the characteristics of high temperature, high viscosity and easy coking. Coking phenomenon refers to the process of polycondensation and deposition of heavy components on the inner wall of the reactor, the surface of the components or the catalyst bed, and finally forming solid coke. Once coking occurs, not only will it block the pipeline and reduce the heat transfer efficiency, but also will cause the reactor pressure to rise and the product selectivity to decrease, ultimately forcing the device to frequently shut down for decoking operation, causing huge economic losses and safety hazards.

[0003] At present, the reaction equipment widely used in the industry is mainly traditional kettle or tower reactor. Its typical structure includes a cylinder with a jacket, which may be provided with a mechanical stirrer or a fixed baffle to achieve mixing and heat transfer of the materials. However, these existing technologies have certain defects, especially uneven mixing of materials and poor temperature control accuracy, which together cause serious local coking problems. SUMMARY

[0004] The purpose of the present application is to provide a coal tar processing anti-coking reactor to solve the problems raised in the background.

[0005] To achieve the above purpose, the present application provides the following technical scheme:

[0006] A coal tar processing anti-coking reactor, comprising a reactor, a feeding part arranged at the feeding end of the reactor, an exhaust device arranged at the discharging end of the reactor, and an external separator, wherein the bottom of the reactor is provided with a reactor base;

[0007] The reactor comprises an equipment shell, an inner kettle body arranged in the equipment shell, and a discharge machine cylinder, wherein the discharge machine cylinder is installed at the bottom of the inner kettle body, the bottom of the discharge machine cylinder is provided with a multi-hole collector, and the output end of the multi-hole collector is connected with the conveying pipeline of the exhaust device; characterized in that:

[0008] The inner kettle body is sequentially provided with a feeding cavity, a reaction zone and a discharging zone from top to bottom, and the discharge machine cylinder is sleeved at the bottom of the discharging zone region;

[0009] The feeding cavity is located at the top of the inner kettle body and is internally provided with a uniform flow turnover assembly, and the input end of the feeding part is connected with the uniform flow turnover assembly;

[0010] The bottom of the flow equalizing turnover assembly is guided into a reaction zone, and a static mixer is arranged in the reaction zone;

[0011] The temperature control unit is mounted in the equipment shell and is wound around and attached to the periphery of the inner kettle body.

[0012] As a further scheme of the present application, the flow equalizing turnover assembly comprises a reaction introduction part and a material introduction part arranged on the top of the reaction introduction part, the reaction introduction part is located in the material cavity, the material introduction part is located in the reaction zone, the side edge of the reaction introduction part is supported and fixed to the inner wall of the inner kettle body through the support frame, and the bottom of the reaction introduction part is guided to the interval where the static mixer is located.

[0013] As a further scheme of the present application, the outer edge of the material introduction part is provided with a material outer ring, the material outer ring is provided with an introduction connection frame matched with the input end of the feeding part, and the material outer ring is provided with a material spiral track inside.

[0014] The inner edge of the material introduction part is provided with a reaction discharge cavity, the groove interval of the material spiral track is introduced into the reaction discharge cavity through the inner extension pipe body, the reaction discharge cavity is provided with a discharge spiral track inside, the discharge spiral track spirals towards the center position, and the center line position of the reaction discharge cavity is provided with a discharge hole communicated with the reaction introduction part.

[0015] As a further scheme of the present application, the inner cylinder of the reaction introduction part is provided with an inner cylinder plane, and the disc body of the inner cylinder plane is provided with a downflow port at the center line position.

[0016] The disc surface of the inner cylinder plane is provided with a plurality of support pads, the support pads are arranged at equal angles and are each provided with a baffle plate, a baffle interval is formed between the baffle plates, a middle supporting cylinder is further arranged in the baffle interval, a plurality of stepped guide pieces are arranged on the periphery of the middle supporting cylinder in a stepped annular manner.

[0017] As a further scheme of the present application, a circular center baffle is further arranged between the support pads, the circular center baffle is arranged on the upper edge of the downflow port and has a height difference with the inner cylinder plane to form an annular gap.

[0018] As a further scheme of the present application, the static mixer comprises a support shaft and support blocks arranged at both ends of the support shaft, the support blocks are mounted in the reaction zone through the support frame, and the support shaft is movably mounted and can rotate after being impacted by fluid.

[0019] The middle support rod is arranged at the center line position of the rod body of the support shaft, and end support rods are arranged at both ends of the rod body of the support shaft, and loop spiral blades are arranged between the rod ends of the support shaft and the middle support rod, two sections of loop spiral blades are wound outside the rod body of the support shaft to form an inner spiral mixing tool; four sections of inclined wing spiral blades are arranged between the end support rods and the middle support rod, the inclined wing spiral blades are connected to the opposite side of the middle support rod from one end of the end support rod in a slanting manner, and the four sections of inclined wing spiral blades form an outer spiral mixing tool outside the loop spiral blades.

[0020] As a further scheme of the present application: the temperature control unit comprises a heat exchanger arranged at the periphery of the reaction zone, a plurality of liquid delivery heads are arranged on the heat exchanger, each of the liquid delivery heads is connected with a heat conduction pipeline, the heat conduction pipeline is spirally wound downward at the peripheral region of the reaction zone to the discharge machine cylinder, a lateral interface is arranged on the heat exchanger, and a top valve is arranged on the lateral interface.

[0021] As a further scheme of the present application: the heat conduction pipeline is layered and wound in a spiral track to form a dense honeycomb-shaped shell, and the heat conduction pipelines are uniformly arranged without cross interference.

[0022] Compared with the prior art, the present application has the following beneficial effects:

[0023] The present application is dedicated to solving the coking problem caused by uneven material mixing and poor temperature control. A flow uniformization turnover assembly is arranged at the feeding end. The assembly utilizes a unique centrifugal and centripetal coupling flow channel design, so that the material undergoes pretreatment of separation first and then mixing before entering the main reaction zone, effectively breaking the plug flow, eliminating the flow dead zone, and realizing the preliminary homogenization of the material. Subsequently, the material enters the core reaction zone and is affected by a static mixer that can rotate with the fluid. The mixer generates strong radial cross-turbulence and shear through its special spiral blade structure nested inside and outside, realizes full-scale deep mixing, and greatly strengthens the mass transfer process. At the same time, the temperature control unit tightly wrapped around the outer wall of the reactor adopts a plurality of heat conduction pipelines layered and wound in a parallel and spiral manner to form a uniform and dense honeycomb-shaped heat exchange surface, ensuring that the reaction heat is precisely and uniformly removed or supplemented, completely eliminating the key coking cause of local overheating or overcooling. A highly uniform and stable ideal reaction environment is created, effectively inhibiting the occurrence of coking side reactions such as cracking and polycondensation from the source, thereby greatly extending the continuous operation period of the reaction device, reducing the frequency of parking and decoking, significantly reducing maintenance costs and production interruption losses, and providing reliable equipment support for the clean processing of coal tar with high added value.

[0024] It should be understood that the above general description and the following detailed description are only exemplary and explanatory, and cannot limit the present application. BRIEF DESCRIPTION OF DRAWINGS

[0025] 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. Furthermore, these drawings and textual descriptions are not intended to limit the scope of the concept in any way, but rather to illustrate the concepts of this application to those skilled in the art through reference to specific embodiments.

[0026] Figure 1 This is a schematic diagram of the overall structure of the anti-coking reactor for coal tar processing provided in an embodiment of the present invention.

[0027] Figure 2 This is a schematic cross-sectional view of the anti-coking reactor for coal tar processing provided in an embodiment of the present invention.

[0028] Figure 3 This is a schematic diagram of the flow equalization and turnover component provided in an embodiment of the present invention.

[0029] Figure 4 This is a schematic diagram of the internal structure of the reaction induction section provided in an embodiment of the present invention.

[0030] Figure 5 This is a schematic diagram of the structure of a static mixer provided in an embodiment of the present invention.

[0031] Figure 6 This is a schematic diagram of the temperature control unit provided in an embodiment of the present invention.

[0032] In the diagram: 1. Reactor; 2. Flow equalization and turnover assembly; 3. Static mixer; 4. Reactor base; 5. Temperature control unit; 7. Discharge device; 8. External separator; 9. Feeding component; 11. Equipment casing; 12. Inner vessel; 13. Discharge cylinder; 14. Reaction zone; 15. Feeding zone; 16. Feeding chamber; 17. Perforated collector; 21. Reaction inlet; 22. Support frame; 23. Feed inlet; 24. Inlet connecting frame; 25. Outer feed ring; 26. Feed spiral track; 27. Inner extension pipe 28. Feeding spiral track; 29. ​​Reaction feeding chamber; 20. Feeding hole; 31. Support shaft; 32. Middle support rod; 33. End support rod; 34. Annular spiral blade; 35. Inclined spiral blade; 36. Support block; 51. Heat exchanger; 52. Infusion head; 53. Heat conduction pipe; 54. Side interface; 55. Top valve; 61. Inner cylinder plane; 62. Support pad; 63. Baffle; 64. Circular center baffle; 65. Middle support cylinder; 66. Stepped guide plate; 67. Downflow port; 68. Annular gap. Detailed Implementation

[0033] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings, examples of which are illustrated in the drawings. In the following description relating to the drawings, unless otherwise indicated, the same numbers in different drawings represent the same or identical elements.

[0034] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to several embodiments. It should be understood that the specific embodiments described herein are for illustrative purposes only and are not intended to limit the invention.

[0035] Example 1; as Figure 1 and Figure 2 As shown, this embodiment provides a basic structure for a coal tar processing anti-coking reactor.

[0036] The reactor mainly comprises reactor 1, feeding device 9, discharge device 7, and external separator 8. Reactor 1 is fixedly installed via reactor base 4 at its bottom. The core shell structure of reactor 1 consists of equipment casing 11, inner vessel 12, and discharge cylinder 13. Inner vessel 12 is suspended inside equipment casing 11, and its bottom is fixedly connected to cylindrical discharge cylinder 13. A porous collector 17 is installed at the bottom outlet of discharge cylinder 13, which is connected to discharge device 7 via a pipe for discharging the reacted material. The internal space of inner vessel 12 is clearly divided into three functional areas: the top feeding chamber 16, the middle reaction zone 14, and the bottom discharge zone 15. Discharge cylinder 13 fits precisely around the discharge zone 15 of inner vessel 12, forming an extended and controllable discharge channel. The key improvement of this invention lies in the inclusion of a flow equalization and turnover assembly 2 within the feed chamber 16. The inlet of this assembly precisely aligns with the output end of the feeding component 9, while its outlet extends downwards to the reaction zone 14. Inside the reaction zone 14, a static mixer 3 is installed. Furthermore, a temperature control unit 5 is installed in the interlayer space between the equipment casing 11 and the inner vessel 12. This unit is formed by multiple pipes attached to the outer wall surface of the inner vessel 12, particularly around the reaction zone 14 and the discharge zone 15.

[0037] The coal tar raw material is driven by the feeding part 9 to enter the flow-distributing turnover assembly 2 first. After the preliminary distribution and flow guiding in the assembly, the raw material is uniformly sent to the reaction zone 14 below. In the reaction zone 14, the raw material flows through the static mixer 3 and is forced to be divided, sheared and recombined, so as to realize the sufficient mixing and reaction of the material. The mixture after completing the reaction continues to flow downward to enter the discharging zone 15, and then is collected by the multi-hole collector 17 at the bottom of the discharge cylinder 13, and finally is pumped to the external separator 8 by the discharger 7 for separation and purification of the product. During the whole process, the temperature control unit 5 continuously works to accurately absorb or release heat through the internally circulating heat-conducting medium, so as to ensure that the reaction temperature in the inner kettle body 12 is maintained in the preset optimal range.

[0038] The technical principle of the embodiment is to prevent coking through the three-stage synergistic effect of "pre-treatment-mixing reaction-accurate temperature control". The flow-distributing turnover assembly 2 breaks the "plug flow" that may be formed when the raw material enters the reactor, and avoids local material retention. The static mixer 3 greatly strengthens the mass transfer process by generating turbulent flow without moving parts, greatly increases the contact probability between reaction molecules, and avoids local overheating or incomplete reaction caused by uneven mixing. The temperature control unit 5 realizes efficient heat exchange with the reaction system through the design of large-area and closely fitted pipelines, eliminates the supercooling or overheating points on the inner kettle wall surface, and these temperature uneven points are the breeding ground for coke.

[0039] The embodiment ensures the uniformity of the material flow and mixing in the reaction zone through the combined action of the flow-distributing turnover assembly 2 and the static mixer 3, significantly improves the reaction efficiency and product yield. The fine design of the temperature control unit 5 fundamentally suppresses the occurrence of coking reaction, prolongs the continuous operation period and service life of the reactor.

[0040] Example Two, as shown in Figure 2 and Figure 3 The embodiment is based on example one, and the flow-distributing turnover assembly 2 is elaborated.

[0041] The flow equalization turnover assembly 2 is composed of an upper material inlet guide 23 and a lower reaction inlet guide 21. The reaction inlet guide 21 is fixed to the inner wall of the feed chamber 16 of the inner kettle body 12 through its side support frame column 22, and its bottom outlet is opposite to the static mixer 3 above the reaction zone 14. The material inlet guide 23 is located on the top of the reaction inlet guide 21. Specifically, the outer edge of the material inlet guide 23 is provided with an annular material outer ring 25, and the upper surface of the outer ring is provided with an inlet connection frame 24 which is connected to the outlet of the feeding member 9. The inside of the material outer ring 25 is processed with a downwardly inclined spiral material spiral track 26 which surrounds the whole ring. On the inner edge of the material inlet guide 23, a cylindrical reaction discharge chamber 29 is formed. The end of the material spiral track 26 is connected to the upper part of the reaction discharge chamber 29 through a plurality of radially arranged inner extension pipes 27. The inner wall of the reaction discharge chamber 29 is engraved with a discharge spiral track 28 which converges to the center. In the center of the bottom of the reaction discharge chamber 29, a discharge hole 20 is provided which is connected to the lower reaction inlet guide 21.

[0042] The raw materials enter the material spiral track 26 of the material outer ring 25 from the feeding member 9 through the inlet connection frame 24. Under the constraint of the spiral track, the raw materials make centrifugal motion and preliminarily separate the gas phase and the liquid phase. Then, the materials are transported to the periphery of the reaction discharge chamber 29 through the inner extension pipes 27. In the reaction discharge chamber 29, the materials flow downward along the centripetal discharge spiral track 28, which further mixes the materials while converging to the center. Finally, all the materials converge to the central discharge hole 20 and fall into the lower reaction inlet guide 21 as a concentrated column of materials, and then enter the main reaction zone 14.

[0043] The material spiral track 26 uses the centrifugal field to make the liquid droplets with larger density tend to the wall surface, and the gaseous and light components are more concentrated in the center, so as to preliminarily separate the gas and liquid phases, which can reduce the load of the main reaction zone. Then, the centripetal design of the discharge spiral track 28 forces the preliminarily separated materials to converge to the center point from the periphery, which is a strong shearing and mixing process, so as to ensure that all the components are homogenized again before entering the main reaction zone. The unique flow path design of "separation first and then mixing" greatly enhances the degree of fluid turbulence, and creates ideal conditions for subsequent deep reaction.

[0044] In this embodiment, the flow equalization and turnover component 2, through its ingenious flow channel design, achieves automatic material distribution, pre-separation, and pre-mixing without relying on any power components. It not only effectively eliminates the "piston flow" phenomenon during feeding and prevents the formation of dead zones, but its centripetal mixing mechanism also produces a mixing effect far exceeding that of conventional distributors, ensuring that the reactants reach a highly homogeneous state before entering the static mixer 3, thereby significantly improving the efficiency and stability of the entire reaction system. Simultaneously, the preliminary gas-liquid separation also helps reduce the gas phase load in the reaction zone, making the reaction more concentrated in the liquid phase and improving the selectivity of the target product.

[0045] Example 3, as Figure 3 and Figure 4 As shown, this embodiment focuses on the detailed structure of the reaction introduction section 21 in Embodiment 2.

[0046] The reaction inlet 21 has a horizontal inner cylinder plane 61 inside, with a downward flow port 67 at its center. Multiple support blocks 62 are arranged at equal angles along the circumference of the inner cylinder plane 61. Each support block 62 has a vertically mounted baffle 63, which forms an annular region above the inner cylinder plane 61. At the center of this annular region, a vertical central support cylinder 65 is fixed. The periphery of the central support cylinder 65 has several stepped guide plates 66 arranged in a stepped annular pattern; that is, the installation radius of these guide plates may gradually change from top to bottom, forming a stepped path similar to a spiral descent. Furthermore, a circular central baffle 64 is mounted above the support blocks 62, covering the downward flow port 67, but its diameter is smaller than the orifice of the downward flow port 67, creating an annular gap 68 between the edge of the central baffle 64 and the inner cylinder plane 61.

[0047] The material column falling from the upper discharge port 20 first impacts the top of the central support cylinder 65 and is then dispersed. Around the central support cylinder 65, the material flows downwards in a zigzag pattern along the stepped guide plates 66 arranged in a stepped pattern. During this process, the outer baffles 63 block and guide the fluid attempting radial diffusion, making its flow path more complex. When the material reaches the bottom and encounters the central baffle 64, the fluid is forced to change direction and flows radially out from the annular gap 68 at the edge of the central baffle 64. Subsequently, this radial flow collides and mixes with fluids from other directions below the central baffle 64 before finally exiting from the central outlet 67 and entering the static mixer 3.

[0048] The core principle of this structure is to create controllable turbulence and multiple flow direction changes. The combination of the stepped guide vanes 66 and the baffle 63 transforms the falling linear flow into a helical downward flow along a sinusoidal path, greatly increasing the flow path and shear rate. The central circular center baffle 64 and the annular gap 68 form a critical "redistributor". It forces all the fluid to pass through a narrow annular gap, generating high-speed radial jets that collide with each other in the central region, forming strong turbulence and mixing, ensuring extreme uniformity of temperature and concentration. This design allows the fluid to undergo sufficient micro-mixing before entering the static mixer.

[0049] The reaction introduction part 21 of this embodiment maximizes the conversion of kinetic energy of the fluid into mixing energy through its multi-stage baffle and central redistribution structure. It effectively breaks down any concentration gradient or temperature gradient that may exist, achieving "micro-premixing" of the materials and providing ideal feed conditions for the subsequent static mixer 3. This design can significantly suppress the condensation focusing reaction caused by excessive local concentration or low temperature, while ensuring sufficient exposure of reactive sites, thereby improving reaction rate and conversion, further strengthening the anti-coking ability of the reactor.

[0050] As shown in Examples Four, as shown in Figure 1 and Figure 5 This embodiment describes in detail the static mixer 3 described in Example One.

[0051] The mixer includes a support shaft 31, both ends of which are mounted on support blocks 36 through bearings, and the support blocks 36 are fixed to the inner wall of the reaction zone 14 through a support. The key is that the support shaft 31 and the mixing elements on it form an integral whole and are mounted movably, allowing free rotation under fluid impact. On the shaft body of the support shaft 31, three main fixed points are arranged axially: end support rods 33 at both ends, and a middle support rod 32 at the centerline position of the shaft body. In the two regions between the ends of the support shaft 31 and the middle support rod 32, the outer edge of the shaft body is tightly wound with loop spiral vanes 34, and the two loop spiral vanes 34 together form an "inner spiral mixing tool". In addition, between each end of the end support rod 33 and the middle support rod 32, four inclined wing spiral vanes 35 are arranged. The installation of these inclined wing spiral vanes 35 is particularly special: they start from one end of the end support rod 33, then extend obliquely and spirally, and finally connect to the other side of the middle support rod 32 opposite to the starting end. The four inclined wing spiral vanes 35 together form an "outer spiral mixing tool" on the periphery of the loop spiral vanes 34.

[0052] When fluid enters from the top and impacts the static mixer 3, it first acts on the inclined wing helix 35 and the ring helix 34. The kinetic energy of the fluid is converted into rotational torque on the mixer, driving the entire support shaft 31 to rotate. In the process, the fluid is divided and guided by the ring helix 34, generating strong internal vortex flow. At the same time, the inclined wing helix 35, with its unique inclined and intersecting design, not only pushes the fluid axially forward, but more importantly, performs cross displacement and shearing on the fluid in the radial direction. Fluid from one side is forced to be transported to the other side, and deeply mixed with another fluid. The entire mixing process is a combination of dynamic rotation and static mixing elements.

[0053] The technical principle of this mixer is the integration of passive rotation and multi-scale mixing. Traditional static mixers are fixed, while the active installation of this design allows the mixer to respond to fluid conditions, with its rotational speed self-adjusting with flow rate, which avoids the sharp decline in mixing effect at low flow rates. The ring helix 34 is responsible for basic division and generation of small-scale vortex flow. The "inclined" and "intersecting" design of the inclined wing helix 35 achieves large-scale, forced cross-flow of fluid in the pipe cross-section, which is the key to achieving radial uniform mixing. The inner and outer helix tools work together to achieve full-scale and efficient mixing from macro to micro.

[0054] The static mixer 3 of this embodiment, through its rotatable design and high-efficiency mixing elements, achieves mixing performance far superior to traditional static mixers. Its self-rotation feature allows it to adapt to a wider flow range, ensuring good mixing effect even at low load conditions. The radial cross-mixing capability brought by the inclined wing helix 35 completely solves the problem of possible temperature and concentration distribution unevenness in the radial direction of the fluid, greatly strengthening the mass and heat transfer process. This deep mixing ensures that the reaction proceeds quickly and uniformly, minimizing side reactions and coking phenomena caused by local accumulation of reactants, while its external power-free design also maintains the simplicity and reliability of the equipment.

[0055] As shown in Figure 1 and Figure 6 , this embodiment refines the temperature control unit 5 mentioned in embodiment one.

[0056] The unit includes a heat exchanger 51 (e.g. a ring-shaped header) disposed on the upper periphery of the reaction zone 14. The heat exchanger 51 is fitted with a plurality of downwardly extending fluid delivery heads 52. Each fluid delivery head 52 is connected to an individual heat transfer conduit 53. The heat transfer conduits 53 emanate from the heat exchanger 51 and are wound in a spiral trajectory down the outer wall of the inner kettle 12 at a precisely controlled pitch. They closely cover the entire reaction zone 14 and the discharge zone 15 up to the vicinity of the discharge machine cylinder 13. The plurality of heat transfer conduits 53 are wound in parallel, in layers, to form a dense honeycomb-like heat transfer shell that encloses the inner kettle 12 macroscopically. The heat exchanger 51 is also fitted with a lateral port 54 for the bulk input or output of heat transfer medium, which is fitted with a top valve 55 for control.

[0057] The heat transfer medium enters the heat exchanger 51 from the lateral port 54 and is evenly distributed to each of the fluid delivery heads 52. The heat transfer medium is then split into each of the individual heat transfer conduits 53, which flow along a spiral downward path. In the process, the heat transfer medium exchanges heat efficiently with the reaction mass in the inner kettle 12 through the metal tube walls. Finally, it is collected at the end of the conduits and flows out. By adjusting the temperature, flow rate and pressure of the heat transfer medium, the temperature of each zone in the reactor can be precisely controlled. The multiple parallel spiral flow paths ensure that even if a slight blockage occurs in one of the conduits, it will not have a fatal impact on the entire temperature control system.

[0058] The core technical principle of the design is distributed, parallel spiral winding heat exchange. Compared with the traditional single coil or jacket, the plurality of heat transfer conduits 53 are wound in layers in a spiral trajectory to form an even, dense heat exchange surface. This design brings a large specific surface area, significantly improving the overall heat transfer coefficient. The parallel multi-flow path design reduces the flow resistance in each conduit, ensuring the flow rate and heat exchange efficiency of the medium. It ensures that the heat flux density is extremely uniform on the outer wall of the reactor, eliminating the inevitable "hot spots" and "cold spots" in conventional designs. An even heat field is one of the most critical factors in suppressing local coking. The present embodiment ensures that the reaction system is in the best and stable thermal state, fundamentally eliminating cracking and coking caused by local overheating and condensation of heavy components caused by local overcooling.

[0059] It will be apparent to those skilled in the art that the application is not limited to the details of the above-described exemplary embodiments, and that the application can be implemented in other specific forms without departing from the spirit or essential characteristics of the application. Therefore, the embodiments should be considered in all respects as illustrative and not restrictive, and the scope of the application should be defined by the appended claims rather than the above description, and all changes falling within the meaning and range of equivalents of the elements of the claims are intended to be embraced therein.

[0060] Furthermore, it should be understood that although the specification is described in terms of embodiments, not every embodiment includes every feature described. The specification can include implicit combinations of explicitly mentioned features and / or explicit combinations of implicitely mentioned features. Each embodiment depends on the explicit combinations of features and / or the implicit combinations of features made specifically within that embodiment, and each such embodiment can be combined with every other such embodiment to create further embodiments.

Claims

1. A coal tar processing anti-coking reactor, comprising a reactor (1), a feeding device (9) disposed at the feeding end of the reactor (1), a discharge device (7) disposed at the discharge end of the reactor (1) and an external separator (8), and a reactor base (4) disposed at the bottom of the reactor (1); The reactor (1) includes a housing (11), an inner vessel (12) disposed within the housing (11), and a discharge cylinder (13). The discharge cylinder (13) is installed at the bottom of the inner vessel (12), and a porous collector (17) is provided at the bottom of the discharge cylinder (13). The output end of the porous collector (17) is connected to the conveying pipe of the discharger (7). Its characteristic is that: The inner vessel body (12) is provided with a feeding chamber (16), a reaction zone (14) and a discharging zone (15) arranged sequentially from top to bottom, and the discharge cylinder (13) is sleeved at the bottom of the discharging zone (15); The feeding chamber (16) is located at the top of the inner vessel body (12) and has a built-in flow equalization and turnover assembly (2), which is connected to the input end of the feeding component (9); The bottom of the flow equalization and turnover assembly (2) is guided into the reaction zone (14), where a static mixer (3) is provided; A temperature control unit (5) is installed inside the equipment housing (11), and the temperature control unit (5) is wrapped around and attached to the periphery of the inner vessel body (12).

2. The anti-coking reactor for coal tar processing according to claim 1, characterized in that, The flow equalization and turnover assembly (2) includes a reaction inlet (21) and a feed inlet (23) disposed on the top of the reaction inlet (21). The reaction inlet (21) is located in the feed chamber (16), and the feed inlet (23) is located in the reaction zone (14). The side edge of the reaction inlet (21) is supported and fixed to the inner wall of the inner vessel body (12) by a support frame (22), and the bottom of the reaction inlet (21) is guided to the area where the static mixer (3) is located.

3. The anti-coking reactor for coal tar processing according to claim 2, characterized in that, The outer edge of the feed inlet (23) is provided with a feed outer ring (25), the feed outer ring (25) is provided with an inlet connecting frame (24) that is connected to the input end of the feeding component (9), and the feed spiral track (26) is provided inside the feed outer ring (25). The inner edge of the feed inlet (23) is provided with a reaction discharge chamber (29). The groove section of the feed spiral track (26) is introduced into the reaction discharge chamber (29) through the inner extension tube (27). The reaction discharge chamber (29) is provided with a discharge spiral track (28). The discharge spiral track (28) spirals toward the center position. The center line of the reaction discharge chamber (29) is provided with a discharge hole (20) that communicates with the reaction inlet (21).

4. The anti-coking reactor for coal tar processing according to claim 3, characterized in that, The reaction inlet section (21) has an inner cylinder plane (61) inside its cylinder and a downflow port (67) is provided at the center line of the disc of the inner cylinder plane (61). The inner cylinder plane (61) has a plurality of support pads (62) arranged on the disk surface. The support pads (62) are arranged in an equiangular array and each support pad (62) is provided with a baffle plate (63). The baffle plates (63) form a baffle interval. A middle support cylinder (65) is also provided in the baffle interval. A plurality of stepped guide plates (66) are provided around the middle support cylinder (65). The stepped guide plates (66) are arranged in a stepped ring around the middle support cylinder (65).

5. The anti-coking reactor for coal tar processing according to claim 4, characterized in that, A circular central baffle (64) is also erected between the support pads (62). The circular central baffle (64) is erected on the upper edge of the outlet (67) and there is a height difference between it and the inner cylinder plane (61) to form an annular gap (68).

6. The anti-coking reactor for coal tar processing according to claim 1, characterized in that, The static mixer (3) includes a support shaft (31) and support blocks (36) disposed at both ends of the support shaft (31). The support blocks (36) are installed in the reaction zone (14) by a support frame and the support shaft (31) is movably installed and can rotate after being impacted by the fluid. A central support rod (32) is provided at the center line of the support shaft (31), and end support rods (33) are provided at both ends of the support shaft (31). A ring-shaped spiral blade (34) is provided between the end of the support shaft (31) and the central support rod (32). The two ring-shaped spiral blades (34) are wound around the outer edge of the support shaft (31) to form an inner spiral mixing tool. Four oblique spiral blades (35) are provided between the end support rods (33) and the central support rod (32). The oblique spiral blades (35) start from one end of the end support rod (33) and then obliquely spirally connect to the opposite side of the central support rod (32). The four oblique spiral blades (35) form an outer spiral mixing tool around the ring-shaped spiral blades (34).

7. The anti-coking reactor for coal tar processing according to claim 1, characterized in that, The temperature control unit (5) includes a heat exchanger (51) disposed around the reaction zone (14). Several infusion heads (52) are installed on the heat exchanger (51), and each infusion head (52) is connected to a heat conduction pipe (53). The heat conduction pipe (53) spirals downward around the outer area of ​​the reaction zone (14) until the discharge barrel (13). A side interface (54) is provided on the heat exchanger (51), and a top valve (55) is installed on the side interface (54).

8. The anti-coking reactor for coal tar processing according to claim 7, characterized in that, The heat conduction pipes (53) are wound in layers with a spiral trajectory to form a dense honeycomb shell. The gaps between the heat conduction pipes (53) are uniform and there is no cross interference.

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