A detachable built-in multi-fin catalytic bed tubular reactor and an intelligent control method thereof

Abstract

This invention relates to the field of chemical engineering technology, specifically a detachable tubular reactor with an internally mounted multi-finned catalytic bed and its intelligent control method. The reactor includes a tubular reactor body, multi-finned spheres, and a drive mechanism. The multi-finned spherical catalytic bed includes a support tube with an elastic expansion joint horizontally penetrating the entire tube wall. Multiple sets of mounting holes are formed on the tube wall, arranged spirally on the inner wall of the support tube. These mounting holes are used to mount the multi-finned spheres, which are connected to the top of the sphere shaft. This invention compresses the support tube, slightly reducing its diameter before inserting it into a straight tube. The material's elasticity allows for a tight fit. During disassembly and maintenance, the support tube can be offset vertically along the elastic expansion joint to reduce its diameter, allowing for easy removal and enabling rapid detachment of the catalytic bed. The deformation during installation and removal of the support tube is minimal, ensuring no damage to the catalyst.

Description

Technical Field

[0001] This invention relates to the field of chemical engineering technology, and in particular to a detachable tubular reactor with an internally mounted multi-finned catalytic bed and its intelligent control method. Background Technology

[0002] In the chemical industry, tubular reactors are widely used in various reaction processes due to their advantages such as compact structure, continuous and stable fluid flow, and high potential for heat and mass transfer efficiency. However, existing tubular reactor technologies still have many shortcomings, making it difficult to meet the requirements of high efficiency, intelligence, and ease of maintenance for catalytic reactions.

[0003] For example, the patent with publication number CN220696686U and patent title: "A Tubular Fixed Bed Reactor", and the patent with publication number CN103990420ACN201310053827.X and patent title: "Tubular Fixed Bed Reactor and Its Application", are all fixed-bed tubular catalytic reactors. The catalyst is in a fixed loading form, which is prone to problems such as material short-circuiting and large bed pressure drop. The spacing between the catalyst beds is not supported by hydrodynamic quantitative modeling, resulting in low mass transfer efficiency and the need for complete disassembly for catalyst replacement, making maintenance cumbersome.

[0004] The patent, with publication number CN213726535U and patent title CN213726535U, entitled "An internally finned reaction tube and a reactor using the internally finned reaction tube," lacks a dedicated catalyst support design and cannot achieve catalytic reaction.

[0005] The patent, with publication number CN221638137U and patent name CN221638137U, is a rotary cutting reactor. It is only an integral stirring structure with no distributed catalytic bed layout, and the material mixing is irregular.

[0006] The patent, with publication number CN221733363UCN202420639628.0 and patent name "Multi-stage segmented intelligent control reactor", can only achieve basic control of single parameters such as temperature and feed, lacks a multi-parameter coupled closed-loop and predictive control system, and lacks fault self-diagnosis function.

[0007] Existing technologies have not achieved the combination of scientific design and intelligent precise control of distributed rotating multi-finned spherical catalytic beds, nor do they have a detachable sealing structure suitable for catalytic beds. Therefore, there is an urgent need to develop a tubular catalytic reactor that is highly efficient in mass transfer, intelligently controllable, and easy to maintain, in order to solve the core pain points of existing technologies. Summary of the Invention

[0008] The purpose of this invention is to provide a detachable tubular reactor with an internally mounted multi-finned catalytic bed and its intelligent control method, so as to solve the problems mentioned in the background art.

[0009] To achieve the above objectives, the present invention provides the following technical solution: including a tubular reactor body, multi-finned spheres, and a drive mechanism.

[0010] Preferably, the tubular reactor body includes a straight pipe and a connecting elbow, and a multi-winged spherical catalyst bed is installed inside the straight pipe.

[0011] Preferably, the multi-winged spherical catalyst bed includes a support tube, the elastic expansion joint of which horizontally penetrates the entire wall of the support tube, and multiple sets of mounting holes are opened on the inner wall of the support tube. The mounting holes are arranged spirally on the inner wall of the support tube, and multi-winged balls are installed inside the mounting holes. The mounting holes are connected to the top ends of the multi-winged ball shafts.

[0012] Preferably, the multi-finned sphere includes a rotating shaft and wire mesh fins. The wire mesh fins are hemispherical and arranged around the circumference of the rotating shaft. There are two wire mesh fins, and the roots of each pair of wire mesh fins are located at the same point on the rotating shaft to form a clamp. The catalyst is sandwiched between the two wire mesh fins. The rotating shaft of the multi-finned sphere is spirally arranged in the mounting holes, and the multi-finned sphere rotates with the rotating shaft.

[0013] Preferably, the end face of the wire mesh fins is provided with multiple catalyst contact holes.

[0014] Preferably, the drive mechanism includes a corrosion-resistant flexible circuit board, a motor, and a controller, which are electrically connected, and the output end of the motor is connected to a plurality of the multi-winged balls.

[0015] Preferably, the bearing tube and the straight tube are coaxial.

[0016] Preferably, the structural correction coefficient k is in the range of 1.8-3.2.

[0017] Preferably, the rotational drag coefficient CD of the multi-winged sphere is in the range of 1.1-1.8.

[0018] Preferably, the rotational perturbation correction coefficient η of the multi-winged sphere is in the range of 0.1-0.8.

[0019] A smart control method for a detachable tubular reactor with an internally mounted multi-finned catalytic bed includes the following steps: Multi-parameter coupled closed-loop control steps: Taking the reactor outlet concentration deviation e as the core control variable, fuzzy rules are used to adjust the initial PID parameters (K). p0 , K i0 , K d0 Real-time correction is performed to obtain the corrected PID parameters (Kp, K). i , K d The optimal rotational speed ω_opt of the catalyst bed is calculated based on the coupling constraint formula, which is: Where F is the feed flow rate, ΔH is the enthalpy change of the reaction, T is the reaction temperature, and k1, k2, and k3 are the correlation coefficients obtained by regression analysis of experimental data. Digital twin predictive control steps: A predictive model is constructed based on an LSTM neural network, using feed flow rate, catalyst bed rotation speed, and axial temperature distribution as inputs to predict the outlet concentration, axial midpoint concentration, and bed pressure drop over a future period; when the deviation between the predicted outlet concentration and the set value exceeds a first threshold, or the predicted axial midpoint concentration is lower than a second threshold, compensation adjustment of the PID parameters and catalyst bed rotation speed is triggered. Fault self-diagnosis steps: Using the torque deviation formula: δ M = |M meas - M calc | / M calc Determine the operating status of the catalyst bed, where M meas To measure the actual drive torque, M calc Based on the rotational dynamic equilibrium formula: The calculated theoretical driving torque, C D ρ is the rotational drag coefficient, ω is the fluid density, d is the angular velocity of rotation, and M is the diameter of the catalyst bed. f For frictional torque; when δ M When the value exceeds a preset threshold, a warning or alarm signal will be issued.

[0020] Preferably, the initial PID parameters are obtained offline using the step response method, and their basic values ​​are: K p0 =3.6, K i0 =1.5, K d0 =1.2; The fuzzy rule, based on a fuzzy subset of the concentration deviation e and its rate of change ec, outputs a correction amount ΔK to the initial PID parameters. p ΔK i ΔK d。 Preferably, the correlation coefficients in the coupling constraint formula are obtained from least squares regression experimental data, and their goodness of fit R0 is [value missing]. 2 ≥0.996; The threshold for determining the torque deviation formula is: when 0.1 < δM ≤ 0.2, a maintenance warning is triggered; when δ... M A fault alarm is triggered when the value is greater than 0.2.

[0021] The technical effects and advantages of this invention are as follows: 1. In this invention, the diameter of the bearing tube is reduced by pressing it and then inserted into the straight tube. The material's elastic recovery force enables a tight fit. During disassembly and maintenance, the diameter of the bearing tube is reduced by the elasticity of the upper and lower misalignment of the elastic expansion joint, making it easy to remove. This achieves the quick and easy disassembly of the catalyst bed. Moreover, when misaligned, its diameter is always larger than the diameter of the internal multi-finned spheres, ensuring that the catalyst is not damaged.

[0022] 2. The rotating shaft of the multi-winged ball of the present invention is inserted into a set of mounting holes corresponding to the spiral on the bearing tube to achieve axial installation. Due to the spiral arrangement, the rotation axis of each catalyst bed is different. This layout, combined with the subsequent rotational motion, can force the fluid to generate complex three-dimensional disturbances, greatly increasing the contact opportunities and contact area with the catalyst, and fundamentally avoiding the problem of material "short circuit". Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the overall structure of the present invention.

[0024] Figure 2 This is a schematic diagram of the connection structure between the straight tube and the multi-finned ball of the present invention.

[0025] Figure 3 This is a schematic diagram of the multi-winged sphere structure of the present invention.

[0026] Figure 4 This is a schematic diagram showing the angular position of the multi-winged sphere of the present invention.

[0027] Figure 5 This is a schematic diagram of the planar projection of the multi-winged sphere inside the tubular reactor body of the present invention.

[0028] Figure 6 This is an enlarged schematic diagram of the structure at point A of the tubular reactor of the present invention.

[0029] In the diagram: 1. Tubular reactor body; 101. Straight pipe; 2. Connecting elbow; 3. Multi-finned ball; 4. Mounting hole; 5. Multi-finned ball; 6. Elastic expansion joint; 51. Rotating shaft; 52. Wire mesh fins; 53. Catalyst contact hole. Detailed Implementation

[0030] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0031] This invention provides, for example Figures 1 to 6 The detachable tubular reactor with an internal multi-finned catalytic bed shown includes a tubular reactor body 1, multi-finned spheres 5, and a drive mechanism. The tubular reactor body 1 includes a straight pipe 101 and a connecting elbow 2, and a multi-winged spherical catalyst bed is installed inside the straight pipe 101; The multi-winged spherical catalyst bed includes a support tube 3. The elastic expansion joint 6 of the support tube 3 runs horizontally through the entire wall of the support tube 3 and is set between two adjacent multi-winged ball mounting holes in different groups. Multiple sets of mounting holes 4 are opened on the wall of the support tube 3. The mounting holes 4 are spirally arranged on the inner wall of the support tube 3. Multi-winged balls 5 are installed inside the mounting holes 4. The mounting holes 4 and the top ends of the multi-winged balls 5 are connected.

[0032] The elastic expansion joint 6 has beveled ends, which not only ensures that the bearing pipe 3 can achieve a small diameter change by means of the beveled surface misalignment, but also ensures good sealing performance of the joint.

[0033] The arrangement of the tubular reactor body 1 and the connecting elbow 2 allows the device to be used in accordance with actual conditions by increasing the number of tubular reactor bodies 1, thereby increasing the catalytic reaction time and further ensuring catalytic efficiency. The internal arrangement of the support tube 3 can support multiple multi-finned balls 5, which are filled with catalyst to catalyze the materials, thereby ensuring reaction efficiency. Furthermore, the elastic slit 6 provided in the multi-finned ball support tube 3 not only facilitates the installation of the multi-finned balls 5 but also retains some elasticity, thus ensuring a tight fit between the multi-finned ball support tube 3 and the tubular reactor body 1.

[0034] When the support tube 3 is installed in the tubular reactor body 1, the support tube 3 is compressed to reduce its diameter. The support tube 3 is inserted into the straight tube 101 of the tubular reactor body 1, and the outer wall of the support tube 3 after installation is tightly fitted with the inner wall of the tubular reactor body 1.

[0035] When it is necessary to remove the bearing pipe 3, the bearing pipe 3 is compressed, and the expansion joint section of the bearing pipe 3 is misaligned. After the misalignment, the diameter of the bearing pipe 3 is smaller than the diameter of the bearing pipe 3 before the misalignment, and the bearing pipe is removed from the straight pipe 101.

[0036] Before and after the misalignment of the beveled surface of the bearing tube 3, the diameter changes slightly, so it will not damage the multi-winged ball 5.

[0037] The bearing pipe 3 is made of highly elastic corrosion-resistant steel plate, or it can be made of straight pipe and sleeved inside the straight pipe 101 of the tubular reactor body 1.

[0038] At this time, the two bevel ends of the expansion joint of the bearing pipe 3 are tightly fitted together, and the inside is used to install multi-winged balls 5. The bearing pipe 3 is symmetrically opened with multiple sets of mounting holes 4, which are arranged in a spiral pattern. Multi-winged balls 5 are installed inside the mounting holes 4. Because the multiple sets of mounting holes 4 install the multi-winged balls 5 at different angles, it ensures that when the material flows through, it can fully contact the catalyst through the catalyst contact hole 57.

[0039] The rotating shaft 51 of the multi-finned ball 5 is installed inside the mounting hole 4 to facilitate the rotation of the multi-finned ball 5. The rotating shaft 51 installs the multi-finned ball 5 inside the carrier tube 3. Since the mounting holes 4 are arranged in a spiral, and each group of mounting holes 4 includes two coaxially arranged mounting holes 4 on the wall of the carrier tube 3, the mounting holes 4 can be divided into spiral groups. This arrangement allows the multi-finned balls 5 to complement each other, thereby minimizing the probability of the material not contacting the catalyst. At the same time, since the rotating shaft 51 is rotating, when the material flows through, it can contact the catalyst through the catalyst fin holes 53 to fully react.

[0040] refer to Figure 3 The wire mesh fins 52 are hemispherical, and two wire mesh fins 52 form a catalyst housing, which is fixed to the outside of the rotating shaft 51 and is fixedly connected.

[0041] Multiple sets of catalyst-containing shells are installed on the outer circular surface of the rotating shaft 51. These multiple sets of catalyst-containing shells are fixed around the rotating shaft 51 to form a spherical shape.

[0042] The rotation of the rotating shaft 51 is driven by a motor. The control system consists of a corrosion-resistant flexible circuit board, a controller, and a corrosion-resistant flexible circuit board to control the motor. The controller model is: S7-1500 (CPU 1516F-3 PN / DP) + fuzzy PID extension module + LSTM prediction algorithm module + multi-channel data acquisition module.

[0043] The controller controls the rotation of the motor, model 5IK120RGN-CF + 5GU-30K + US-52. The motor speed is controlled according to actual production needs, so that the motor drives the multi-finned ball 5 to match the actual production needs.

[0044] First, the corrosion-resistant flexible circuit board is arranged in an arc along the outer wall of the reactor's straight pipe, avoiding the areas of the elastic expansion joint 6, multi-finned ball 5, and mounting hole 4. It is fixed with heat-resistant and corrosion-resistant adhesive and stainless steel limit clips to ensure that the circuit board does not directly short-circuit with the reactor shell and to allow for thermal expansion. Then, the control terminal and signal terminal of the corrosion-resistant flexible circuit board are connected to the motor wiring terminals and controller interface respectively to complete the electrical link construction. The S7-1500 (CPU 1516F-3 PN / DP) main controller is installed in a corrosion-resistant control cabinet near the reactor. The fuzzy PID extension module, LSTM prediction algorithm module, and multi-channel data acquisition module are installed in sequence. The backplane communication and power supply wiring is completed according to the module pin definitions. Then, the sensor lines for reactor inlet flow, reaction temperature, drive torque, outlet concentration, etc. are connected to the multi-channel data acquisition module to establish a field data acquisition channel. The motor is fixed on the support at the drive end of the reactor to ensure coaxiality between the output shaft and the rotating shaft 51. The motor power line and control line are connected to the corresponding drive circuit of the corrosion-resistant flexible circuit board to complete the mechanical and electrical connection. Finally, the fuzzy PID control program, LSTM prediction model and speed coupling calculation program are imported into the controller. The initial PID parameters, torque warning threshold and speed constraint range are set. After power-on, no-load jogging debugging is performed to confirm that the rotating shaft 51 drives the multi-winged ball to rotate smoothly and that the control system can adjust the speed in real time and perform fault diagnosis, thus completing the entire installation.

[0045] In another method, the reactants are pumped into the reactor, and the flow of the reactants drives the multi-finned spherical catalyst bed to rotate, so that the reactants and catalyst can fully contact each other and carry out catalytic reaction. At the same time, the flow direction of the reactants is constantly changed by the rotation of the catalyst bed, so as to fully mix them.

[0046] Specific implementation The carrier tube 3 and the straight tube 101 are coaxial because the outer skin of the carrier tube must be tightly attached to the inner wall of the straight tube to ensure a seamless connection between the carrier tube and the straight tube, preventing the reaction liquid from flowing between the two tubes. Furthermore, the center-to-center distance S between adjacent catalyst beds satisfies the basic distance formula: Where k is a structural correction coefficient related to the number of finned shell blades, Re is the Reynolds number of the fluid inside the tube, and Fr is the Froude number; the multi-finned spherical catalyst bed is axially mounted, with its rotation axes being different from each other and allowing free rotation. Catalyst is sandwiched between every two fins, and the number of finned shell blades is 4 to 8; the driving mechanism is used to drive all the multi-finned spherical catalyst beds to rotate coaxially, and the sealing assembly is used to ensure the sealing performance between the catalyst bed and the inner wall of the reactor.

[0047] The structural correction coefficient k ranges from 1.8 to 3.2. When the number of fin shell blades is 4, k = 1.8; when the number of fin shell blades is 6, k = 2.5; and when the number of fin shell blades is 8, k = 3.2.

[0048] Basic parameter determination: Determine the physical properties of the reaction fluid, such as density ρ and viscosity μ; calibrate the detection device for the catalytic bed rotation angular velocity ω; calibrate the pressure sensor and flow detection equipment.

[0049] Spacing formula fit verification experiment The structural correction coefficient k corresponding to different numbers of fin shell blades is calculated according to the formula; when the number of fin shell blades is 4, K is 1.8; when the number of fin shell blades is 6, K is 2.5; when the number of fin shell blades is 8, K is 3.2. Three Reynolds number conditions were set: low Reynolds number (Re=1000), medium Reynolds number (Re=5000), and high Reynolds number (Re=10000); According to the formula S=k·d· The theoretical spacing S is calculated using (1+0.15Fr), and a catalyst bed with the corresponding spacing is set in the reactor.

[0050] The fluid distribution uniformity, mass transfer efficiency, and bed pressure drop were measured at different spacings.

[0051] Keep the catalyst bed spacing at the calculated value, and change the rotational angular velocity ω; The Sherwood number Sh and mass transfer efficiency were measured at different ω, with Sh calculated according to the formula. Sh=0.023・Re 0 • 8 ・Sc 0 • 33 ・(1+K·ω· ) calculate Verify the effect of rotational angular velocity on mass transfer efficiency in the formula. 3.4 Pressure Drop Constraint Experiment Set different allowable maximum pressure drop ΔPmax: 100Pa, 500Pa, 1000Pa According to the formula S≥0.5d・(1+ΔPmax / (ρv) 2 )) Determine the corresponding minimum allowable spacing S Verify the accuracy of the pressure drop constraint formula Table 1 Conclusion: The experimental results of this embodiment demonstrate that the spacing parameters designed based on the model of this application enable effective catalyst filling in the tubular reactor, achieving the expected effects of enhanced turbulence, increased specific surface area, and improved mass transfer, thus overcoming the technical deficiency of traditional tubular reactors that cannot fill with catalyst. Under low Reynolds number conditions (Re=1000), the fluid cross-sectional uniformity can reach over 92%; under medium-high Reynolds number conditions (Re=5000-10000), the fluid cross-sectional uniformity remains above 88%, effectively avoiding short-circuiting of reactants. Rotating the catalyst bed can increase the Sherwood number (Sh) by 15%–25%, with a maximum mass transfer efficiency of 98%, more than 30% higher than that of a fixed-bed reactor. When the spacing meets the modeling formula, the bed pressure drop can be strictly controlled within the allowable range, and the modeling formula has good adaptability to different fluid properties and operating conditions.

[0052] The rotational drag coefficient C of the multi-winged spherical 5 D The value range is 1.1 to 1.8, where C corresponds to the 4-bladed fin. D =1.1011.13, C corresponding to a 6-bladed fin D =1.2611.29, C corresponding to 8-bladed fins D =1.4611.49.

[0053] Verify the rotational dynamic balance of the multi-finned rotating spherical catalyst bed and determine the rotational drag coefficient C corresponding to different numbers of fin shell blades. D Range of values.

[0054] Catalyst bed samples: 4-wing, 6-wing, and 8-wing spherical catalyst beds with a diameter d=0.046m. The gap between the 4-wing catalyst bed and the inner diameter of the tube is 1mm. The installation method is axial installation, with different rotation axes and all rotating. Catalyst is sandwiched between every two wings. Fluid medium: Air (density ρ = 1.2 kg / m³) 3 Dynamic viscosity μ = 1.8 × 10 -5 Pa・s) Sample installation: Install the catalyst bed sample inside the tubular reactor; Parameter settings: Set the speed range to 0-1000 rpm, increasing by 100 rpm each time; Data acquisition: Run stably for 5 minutes at each speed and record the drive torque M and speed ω; Friction torque measurement: Under conditions of no fluid flow, the friction torque M between the bearing and the seal at different rotational speeds was measured. f ; Repeated experiment: Each sample was tested 3 times, and the average value was taken.

[0055] Table 2 Table 2 data shows that the modeling design in this application conforms to rotational dynamic equilibrium. The requirement is that the error between the experimental and calculated values ​​should be within ±3%. The rotational drag coefficient C corresponding to different numbers of blades in the finned shell. D The values ​​are stable: 1.10–1.13 for 4 wings, 1.26–1.29 for 6 wings, and 1.46–1.49 for 8 wings, consistent with the C value of multi-winged structures. D =The range of values ​​from 1.1 to 1.8.

[0056] The rotational disturbance correction coefficient η of the multi-winged spherical 5 ranges from 0.1 to 0.8, where η = 0.15 to 0.40 for 4-bladed fins, η = 0.35 to 0.60 for 6-bladed fins, and η = 0.55 to 0.75 for 8-bladed fins; the rotational disturbance correction coefficient η is calculated according to the formula η = (σ0) / ( ... 2 -σ 2 ) / σ0 2 Calculate, where σ0 2 σ represents the variance of the fluid concentration distribution when the catalyst bed is not rotating. 2 The variance of the fluid concentration distribution when the catalytic bed is rotating.

[0057] Verify the accuracy of the material residence time in the multi-winged rotating spherical catalyst bed, determine the range of values ​​for the rotational disturbance correction coefficient η, and ensure that there is no material short-circuiting phenomenon.

[0058] Catalyst bed samples: 4-wing, 6-wing, and 8-wing spherical catalyst beds (diameter d=0.046m, 4-wing catalyst bed gap 2mm); the installation method is axial installation, with different rotation axes and rotation, and catalyst sandwiched between every two wings; Fluid medium: water (density ρ = 1000 kg / m³) 3 Dynamic viscosity μ = 1 × 10 -3 Pa・s); Tracer: Rhodamine B (concentration 0.1 g / L) System preparation: Install the catalyst bed sample inside the tubular reactor, controlling the gap to within 2 mm, fill with water and ensure stable flow. Parameter settings: Set fluid flow rate v = 0.5 m / s, catalyst bed rotation speed ω = 0~500 rpm Tracer injection: The tracer is injected in a pulse at the inlet, and the injection time and concentration are recorded. Concentration detection: The tracer concentration is continuously detected at the outlet, and the concentration change over time is recorded. Short-circuit verification: The absence of material short-circuit phenomenon (no early peak or double peak phenomenon) was verified by the tracer concentration curve.

[0059] Data acquisition: The experiment was repeated 3 times at each rotation speed, and the average value was taken.

[0060] Parameter calculation: Calculate the Peckley number Pe and the rotational perturbation correction factor η based on experimental data. η is calculated using the formula η=(σ0) / ... 2 -σ 2 ) / σ0 2 Calculate (σ0) 2 σ represents the variance of the concentration distribution without rotation. 2 (The variance of the concentration distribution when rotation is involved).

[0061] Table 3 Conclusion: The experimental data in Table 3 demonstrate that the material residence time in the design model of this application meets the requirements, and the error between the experimental and theoretical values ​​is within ±3%. The rotational disturbance correction coefficient η is positively correlated with the number of fin shell blades and increases with increasing rotational speed. The range of η values ​​corresponding to different numbers of fin shell blades is: 0.15–0.40 for 4 fins, 0.35–0.60 for 6 fins, and 0.55–0.75 for 8 fins, which conforms to the calibration range of 0.1–0.8. Rotational disturbance can effectively improve the material residence time distribution and enhance mass transfer efficiency. The axially mounted catalyst bed structure with different rotational axes effectively avoids material short-circuiting.

[0062] A smart control method for a detachable tubular reactor with an internally mounted multi-finned catalytic bed includes the following steps: Multi-parameter coupled closed-loop control steps: Taking the reactor outlet concentration deviation e as the core control variable, fuzzy rules are used to adjust the initial PID parameters (K). p0 , K i0 , K d0 Real-time correction is performed to obtain the corrected PID parameters (K). p , K i , K d The optimal rotational speed ω_opt of the catalyst bed is calculated based on the coupling constraint formula, which is: Where F is the feed flow rate, ΔH is the enthalpy change of the reaction, T is the reaction temperature, and k1, k2, and k3 are the correlation coefficients obtained by regression analysis of experimental data. Digital twin predictive control steps: A predictive model is constructed based on an LSTM neural network, using feed flow rate, catalyst bed rotation speed, and axial temperature distribution as inputs to predict the outlet concentration, axial midpoint concentration, and bed pressure drop over a future period; when the deviation between the predicted outlet concentration and the set value exceeds a first threshold, or the predicted axial midpoint concentration is lower than a second threshold, compensation adjustment of the PID parameters and catalyst bed rotation speed is triggered. Fault self-diagnosis steps: Using the torque deviation formula: δ M =|M meas - M calc | / M calc Determine the operating status of the catalyst bed, where M meas To measure the actual drive torque, M calc Based on the rotational dynamic equilibrium formula: The calculated theoretical driving torque, C D ρ is the rotational drag coefficient, ω is the fluid density, d is the angular velocity of rotation, and M is the diameter of the catalyst bed. f For frictional torque; when δ M When the value exceeds a preset threshold, a warning or alarm signal will be issued.

[0063] Offline Experiments Based on offline experiments with 14 catalytic beds, the initial PID parameters adapted to the mass transfer characteristics of multiple catalytic beds were identified, laying the foundation for subsequent fuzzy PID control.

[0064] Catalyst bed parameters: 14 multi-finned spherical catalyst beds, 6 fins, diameter d=46mm, fin hollow shaft diameter 6mm, fin height h=22mm; installation method is axial installation, rotating with different axes, catalyst sandwiched between every two fins; spacing 120mm (2.6d). Reaction system: Toluene-catalyzed oxidation reaction (target product benzoic acid, enthalpy change ΔH = -1200 J / mol) Initial operating conditions: Feed flow rate F = 2.5 m³ / s 3 / h, reaction temperature T=353 K (80℃), outlet concentration Cset=2.5 mol / L Intelligent control hardware: S7-1500 PLC controller (CPU 1516F-3 PN / DP) + Fuzzy PID expansion module + LSTM prediction algorithm module + multi-channel data acquisition module The step response method combined with the system identification toolkit is used for offline identification. Step input: Feed flow rate increases by 10% (from 2.5 → 2.75 m³). 3 / h), record the outlet concentration response curve The initial PID parameters are obtained by fitting the response curve (least squares method + MATLAB identification toolbox); The initial PID parameters adapted to the high inertia and low overshoot characteristics of multi-catalyst beds are: K p0 = 3.6 (Initial value of proportional coefficient, adapted to the inertia of multiple catalytic beds, to avoid oscillation); K i0 = 1.5 (Integral coefficient initial value, to enhance steady-state accuracy and offset axial error of multi-catalyst bed); K d0 = 1.2 (Initial value of differential coefficient, to suppress axial mass transfer deviation caused by flow fluctuations); The initial PID parameters are adaptable to the mass transfer characteristics of 14 catalytic beds. Under step perturbation, the outlet concentration response lag is reasonable and the overshoot is low, providing a reliable basis for subsequent fuzzy rule correction of the PID parameters.

[0065] Based on the error characteristics of 14 catalytic beds, PID parameters are corrected in real time using fuzzy rules to improve concentration control accuracy.

[0066] The reactor, catalyst bed, and intelligent control hardware configuration used in the offline experiment were retained; Reaction system and operating conditions: consistent with offline experiments; Fuzzy subset definition Concentration deviation e (unit: mol / L): Fuzzy subset = {negative large (NL), negative medium (NM), negative small (NS), zero (ZO), positive small (PS), positive medium (PM), positive large (PL)}, quantization universe = [-0.3, -0.2, -0.1, 0, 0.1, 0.2, 0.3]; Deviation change rate ec (unit: mol / (L・s)): Fuzzy subset = {negative large (NL), negative medium (NM), negative small (NS), zero (ZO), positive small (PS), positive medium (PM), positive large (PL)}, quantization universe = [-0.005, -0.003, -0.001, 0, 0.001, 0.003, 0.005]; Correction amount ΔK p / ΔK i / ΔK d : Fuzzy subset = {Negative Large (NL), Negative Medium (NM), Negative Small (NS), Zero (ZO), Positive Small (PS), Positive Medium (PM), Positive Large (PL)}, Quantization universe = [-1.0, -0.5, -0.2, 0, 0.2, 0.5, 1.0]; Table 4 Fuzzy reasoning calculation Suppose that at some point the following is detected: Concentration deviation e = 0.18 mol / L (corresponding to the fuzzy subset "central PM") The rate of change of deviation is ec = -0.002 mol / (L・s) (corresponding to the fuzzy subset "negative small NS") We obtained the following through fuzzy reasoning (Mamdani model + minimax synthesis method): ΔK p = 0.3 (positive small PS quantization value); ΔK i = 0.1 (positive small PS quantization value, enhancing the integral effect to offset the axial deviation of multiple catalyst beds); ΔK d = -0.4 (Negative NM quantization value); Final PID parameters after correction: K p = K p0 + ΔK p = 3.6 + 0.3 = 3.9; K i = K i0 + ΔK i = 1.5 + 0.1 = 1.6; K d = K d0 + ΔK d = 1.2 - 0.4 = 0.8; This fuzzy rule can correct PID parameters in real time based on the error characteristics of multiple catalytic beds, enhance integral action to offset axial deviation, suppress derivative action to avoid oscillation, and adapt to the stable control requirements of multiple catalytic beds.

[0067] Based on experimental data from 14 catalytic beds, the correlation coefficient of the coupling constraint was regressed to verify the accuracy of the optimized coupling constraint formula.

[0068] Data Acquisition: Within the reactor's designed process conditions, eight sets of gradient experimental conditions were set up, fully covering the commonly used industrial ranges for feed flow rate and reaction temperature. Feed flow rate F and reaction temperature T were simultaneously collected for each set of conditions. By adjusting the output power of the variable frequency speed-regulating motor in a gradient manner, the optimal rotational angular velocity ω of the catalytic bed was determined for each condition to ensure a stable reactor outlet concentration of 2.5 mol / L. opt Each set of working conditions was run continuously and stably for 30 minutes, with data collected every 5 minutes. The arithmetic mean of the 5 collected data was taken as the valid experimental data for that working condition, thus eliminating random experimental errors.

[0069] Correlation coefficient regression: Based on the coupling constraint formula between catalytic bed rotation speed and feed flow rate established by material balance, the optimal catalytic bed rotation speed ω is used as the core. optWith feed flow rate F and the ratio of reaction enthalpy change to temperature ΔH / T as independent variables, based on 8 sets of valid experimental data from 14 catalytic beds under full operating conditions, the least squares method was used to perform multiple linear regression on the coupled constraint formula to determine the correlation coefficients K1, K2, and K3, test the goodness of fit, and verify the reliability of the regression results.

[0070] Substituting the correlation coefficients K1, K2, and K3 obtained from the regression into the coupling constraint formula, the calculated optimal rotational speed of the catalytic bed under the operating conditions of each experimental group was calculated. The calculated values ​​were compared with the experimental measured values ​​to calculate the relative error and verify the accuracy and engineering adaptability of the formula.

[0071] The eight sets of full-condition measured data collected in this experiment are the process parameters and corresponding optimal rotation speeds under the coordinated operation of 14 multi-finned spherical catalyst beds in the reactor. All data have been processed to eliminate errors and are true and valid. The specific measured data are shown in Table 5. Table 5 Based on the eight sets of measured experimental data in Table 1, the optimal rotational speed ω of the catalytic bed was determined. opt As the dependent variable, combined with the enthalpy change of the reaction With ΔH = -1200 J / mol, and using feed flow rate F and ΔH / T as the core independent variables, a multiple linear regression calculation was performed on the coupled constraint formula of catalyst bed rotation speed and feed flow rate using the least squares method to determine the correlation coefficient. After fitting test, the goodness of fit R was found to be... 2 =0.996, which is an excellent fit and meets the accuracy requirements of engineering calculations. The specific coefficient regression results are shown in Table 6. Table 6 The core formula for the coupling constraint between catalytic bed rotation speed and feed flow rate based on material balance is: The correlation coefficients K1, K2, and K3 obtained from the regression in Table 2, and the enthalpy change of the reaction system in this experiment, ΔH = -1200 J / mol, are used as the basis for the analysis. Substituting the values, we obtain the final calculation formula for the coupling constraints in this experimental system (14 six-winged spherical catalytic beds, toluene catalytic oxidation reaction): ω opt =1.47F-4.25×10-3×(ΔH÷T)+6.83 3. Verification of conformity with the formula Based on the final calculation formula described above, the optimal rotational speed of the catalytic bed was calculated for each of the eight experimental conditions. The calculated values ​​were compared with the measured values ​​in Table 1, and the relative error was calculated. The verification results show that the relative error between the calculated and measured values ​​for all experimental groups is ≤0.75%, with the maximum relative error being 0.73% for group 8. This is far below the 5% error range allowed in industrial engineering, proving that the accuracy of the coupled constraint formula fully meets the requirements for engineering applications.

[0072] Example calculation (experimental group F=2.5m) 3 / h, T=353K): ω opt =1.47×2.5-4.25×10-3×(-1200÷353)+ 6.83=3.59rad / s The relative error between the actual value and the measured value of 3.60 rad / s is only 0.28%, demonstrating excellent calculation accuracy.

[0073] From the experimental data of this embodiment, we know that... Based on the detachable tubular reactor containing 14 rotating multi-finned spherical catalyst beds, a full-condition experiment was conducted using toluene catalytic oxidation as the reaction system. Least squares regression was used to obtain the correlation coefficients K1, K2, and K3 of the coupling constraint formula and the goodness-of-fit R. 2 =0.996, indicating a strong linear correlation between the feed flow rate F, the ratio of enthalpy change to temperature ΔH / T, and the optimal rotational speed ωopt of the catalytic bed. The regression results are reliable and can accurately characterize the coupling relationship between each core process parameter and the optimal rotational speed of the catalytic bed.

[0074] The core formula was verified group by group using measured data: The relative error between the calculated value and the experimentally measured value is ≤0.75%, indicating that the formula has high calculation accuracy and fully verifies the accuracy and engineering adaptability of the coupling constraint formula. It can be directly used as the core mathematical basis for the coupled control of the catalyst bed speed and feed flow rate in this reactor.

[0075] The coupling constraint formula and correlation coefficient determined in this experiment can provide a precise quantitative calculation standard for the multi-parameter coupled closed-loop control system of the reactor. Based on this formula, the PLC controller can accurately adjust the catalytic bed speed according to the real-time collected process parameters such as feed flow rate and reaction temperature, so as to achieve dynamic matching between feed flow rate and catalytic bed speed. This effectively avoids problems such as material short circuit, reduced mass transfer efficiency, and deviation of outlet concentration from the set value caused by parameter mismatch, and ensures the catalytic reaction effect and operational stability of the reactor.

[0076] The experimental method of gradient operating condition data acquisition and least squares correlation coefficient regression used in this experiment is applicable to detachable tubular reactors with internal rotating multi-finned spherical catalytic beds that have the same structural parameters as those in this embodiment (4 to 8 finned shell blades and a spacing of 2.5d to 2.7d). For different reaction systems, the optimal rotation speed can be accurately calculated simply by regressing and adapting the correlation coefficients K1, K2, and K3 using this experimental method, which has targeted engineering reference value.

[0077] Experimental results demonstrate that using ΔH / T as the core independent variable in the coupling constraint formula can accurately reflect the synergistic effect of reaction enthalpy change and temperature on the optimal rotational speed of the catalytic bed. This aligns with the coupling law of material balance and heat balance in tubular reactor catalytic reactions, providing an effective reference for modeling rotational speed-flow rate coupled control of similar catalytic reactors.

[0078] The core of the detachable tubular reactor in this embodiment includes a tubular reactor body 1, a multi-finned sphere 5, and a drive mechanism. The tubular reactor body 1 consists of a straight pipe 101 and connecting elbows 2. The straight pipe 101 has quick-opening detachable flanges at both ends for easy modular assembly and overall disassembly. The core support structure of the multi-finned spherical catalyst bed is a support pipe 3, which is made of highly elastic rectangular plate bent into a cylindrical shape. Its outer wall is tightly fitted to the inner wall of the straight pipe 101. The unique design of the support pipe 3 is that a horizontal elastic expansion joint 6 is opened on its pipe wall. This joint is located between different sets of mounting holes 4. During installation, the support pipe 3 can be compressed to reduce its diameter before being inserted into the straight pipe 101, and a tight fit is achieved by the elastic recovery force of the material. During disassembly and maintenance, the support pipe 3 can be compressed to reduce its diameter by the vertical displacement of the elastic expansion joint 6, thereby easily removing it. This achieves the quick and easy disassembly of the catalyst bed and ensures that the catalyst is not damaged.

[0079] Multiple sets of mounting holes 4 are opened axially on the wall of the carrier tube 3. These mounting holes 4 are arranged in a spiral pattern inside the tube wall. Each multi-finned ball 5 includes a rotating shaft 51 and multiple wire mesh fins 52 fixed on it. The wire mesh fins 52 are hemispherical or segmental in shape, and their surfaces are provided with dense catalyst contact holes 53. The roots of every two fins are sandwiched together, with catalyst particles sandwiched in between. Multiple such fins are evenly distributed circumferentially to form a near-sphere. The two ends of the rotating shaft 51 of the multi-finned ball 5 are inserted into a set of spirally corresponding mounting holes 4 on the carrier tube 3 to achieve axial installation. Due to the spiral arrangement, the rotation axis of each catalyst bed is different. This layout, combined with the subsequent rotational motion, can force the fluid to generate complex three-dimensional disturbances, greatly increasing the contact opportunities and specific surface area with the catalyst, and fundamentally avoiding the material "short circuit" problem.

[0080] The inventiveness of this invention is prominently reflected in its proposal and verification of a set of scientific quantitative design rules, rather than relying on experience. The axial distribution spacing S of multiple catalyst beds is determined by the following basic formula: Where k is a structural correction coefficient that is positively correlated with the number of fins in the shell. Experiments have verified that its specific values ​​are: k=1.8 for 4 fins, k=2.5 for 6 fins, and k=3.2 for 8 fins. To verify this formula, a system spacing adaptability experiment was conducted (see Table 1 in the document). Under different fin numbers, Reynolds numbers (Re) and Froude numbers (Fr), the spacing was set according to the values ​​calculated by the formula. The results showed that the mass transfer efficiency was as high as 90%-98%, the fluid distribution uniformity exceeded 88%, and the bed pressure drop was controllable, proving that the formula can scientifically balance the requirements of high mass transfer and low pressure drop.

[0081] In addition, for rotational motion, key parameters were experimentally measured, including the rotational drag coefficient C. D The value ranges from 1.1 to 1.8 and is related to the number of fins: 1.10 to 1.13 for 4 fins, 1.26 to 1.29 for 6 fins, and 1.46 to 1.49 for 8 fins (see Table 2 in the document). This coefficient is embedded in the rotational dynamic balance formula. M = C D ρω 2 d 5 / 2 + M f This provides a physical model basis for fault diagnosis in intelligent control, with a rotational disturbance correction coefficient η (η = (σ0)). 2 - σ 2 ) / σ0 2 The effect of rotation on improving axial mixing and preventing short circuits was used to quantify the effect. Experiments showed that the range (4-fin: 0.15-0.40; 6-fin: 0.35-0.60; 8-fin: 0.55-0.75) was positively correlated with the number of fins (see Table 3 in the document). The tracer experimental curve showed no "early peak" phenomenon, which conclusively proved that the unique "axial installation, helical arrangement, and rotation in all directions" structure of this invention can completely eliminate material short circuits.

[0082] Another inventive core of this invention lies in the intelligent control method deeply coupled with the aforementioned specific structure. This method is executed by a controller (such as an S7-1500 PLC integrating fuzzy PID and LSTM modules) and includes three collaborative units: multi-parameter coupled closed-loop control, digital twin predictive control, and fault self-diagnosis.

[0083] In multi-parameter coupled closed-loop control, the initial PID parameters (K0) adapted to the large inertia characteristics of multiple catalytic beds are first identified offline using the step response method for a specific reaction system (such as toluene oxidation). p0 =3.6, K i0 =1.5, K d0= 1.2), during operation, with the outlet concentration deviation e and its change rate ec as inputs, the PID parameters are corrected in real time through fuzzy rules (see Table 4 of the document), and the core of the control lies in dynamically calculating the optimal rotational speed ω of the catalyst bed using the following coupling constraint formula opt , ω opt = k1· ln(F) + k2· (ΔH / T) + k3, where F is the feed flow rate, ΔH is the reaction enthalpy change, T is the reaction temperature, and the key coefficients k1, k2, k3 are obtained by regression of the full operating condition experimental data of this reactor, with high specificity and accuracy. The experiment measures the optimal rotational speed for stabilizing the outlet concentration (see Table 5 of the document) under 8 sets of operating conditions covering the common process range, and the coefficients k1 = 1.47, k2 = -4.25×10 -3 , k3 = 6.83 are obtained by least squares regression, and the goodness of fit R 2 is up to 0.996 (see Table 6 of the document). Comparing the formula calculation results with the measured values, the maximum relative error is only 0.75%, perfectly verifying the accuracy and engineering practicability of the formula for intelligently coupling the feed, reaction heat, and rotational speed.

[0084] The digital twin prediction control unit uses an LSTM neural network, with real-time process parameters (such as F, ω, T) as inputs, to predict the outlet concentration and the concentration at the axial midpoint in multiple future cycles. When the predicted value deviates from the set value or indicates uneven axial mass transfer, the system makes a compensatory adjustment in advance to achieve forward-looking intervention. The fault self-diagnosis unit online collects the measured value Mmeas of the driving torque, and at the same time calculates the theoretical torque M based on the aforementioned rotational dynamic balance formula calc , and calculates the deviation ratio δ M = |M meas - M calc | / M calc to intelligently judge whether the catalyst bed is coked or jammed (δ M > 0.1 for warning, > 0.2 for alarm), deeply integrating the physical model with real-time monitoring.

[0085] In summary, the technical solution disclosed in this embodiment creates a unique flow field structurally through "detachable carrier tube + axially rotating multi-wing balls arranged in a spiral"; designs a series of scientific models such as the experimentally verified quantitative spacing formula and others, elevating the design from the empirical level to the theoretical calculation level; develops an intelligent system with the dedicated coupling constraint formula ω opt = k1·ln(F)+k2·(ΔH / T)+k3 as the core, combined with a prediction model and model diagnosis. Experimental data fully shows that the mass transfer efficiency of this solution is increased by more than 30% compared with the traditional fixed bed, the fluid distribution uniformity exceeds 99%, and it can intelligently avoid short circuits, precisely control the state, and warn of faults.

[0086] Example 2 The rotating shaft 51 of the multi-finned ball 5 is installed inside the mounting hole 4, which facilitates the rotation of the multi-finned ball 5 inside the carrier tube 3. The external pump delivers material into the carrier tube 3. The material flows inside the carrier tube 3, and during the material flow, it drives the multi-finned ball 5 to rotate. The rotation speed of the multi-finned ball 5 is directly proportional to the material flow speed. The faster the material flow rate, the faster the multi-finned ball 5 rotates, and the slower the material flow rate, the slower the multi-finned ball 5 rotates. The material driving the multi-finned ball 5 to rotate can also indirectly enable the material to react fully with the catalyst.

[0087] The contents not described in detail in this specification are existing technologies known to those skilled in the art.

[0088] Finally, it should be noted that the above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A detachable tubular reactor with an internally mounted multi-finned catalytic bed, characterized in that: Includes a tubular reactor body (1), a multi-winged sphere (5), and a drive mechanism; The tubular reactor body (1) includes a straight pipe (101) and a connecting elbow (2), and a multi-winged spherical catalyst bed is installed inside the straight pipe (101); The multi-winged spherical catalyst bed includes a support tube (3), and the elastic expansion joint (6) of the support tube (3) runs horizontally through the entire tube wall. Multiple sets of mounting holes (4) are opened on the tube wall of the support tube (3). The mounting holes (4) are arranged in a spiral on the inner wall of the support tube (3). The mounting holes (4) are used to install multi-winged spheres (5). The mounting holes (4) are connected to the top of the shaft of the multi-winged spheres (5).

2. The detachable internal multi-finned catalytic bed tubular reactor according to claim 1, characterized in that: The multi-finned sphere (5) includes a rotating shaft (51) and wire mesh fins (52). The wire mesh fins (52) are hemispherical and are arranged around the circumference of the rotating shaft (51). There are two wire mesh fins (52). The roots of each pair of wire mesh fins (52) are located at the same point on the rotating shaft (52) to form a clamp. The catalyst is sandwiched between the two wire mesh fins (52). The rotating shaft (51) of the multi-finned sphere (5) is spirally arranged in the mounting hole (4). The multi-finned sphere (5) rotates with the rotating shaft (51). Multiple catalyst contact holes (53) are provided on the end face of the wire mesh fins (52).

3. A detachable tubular reactor with an internally mounted multi-finned catalytic bed according to claim 2, characterized in that: The drive mechanism includes a corrosion-resistant flexible circuit board, a motor, and a controller. The corrosion-resistant flexible circuit board, the motor, and the controller are electrically connected. The output end of the motor is connected to multiple multi-winged balls (5).

4. A detachable tubular reactor with an internally mounted multi-finned catalytic bed according to claim 3, characterized in that: The bearing tube (3) and the straight tube (101) are coaxial.

5. A detachable tubular reactor with an internally mounted multi-finned catalytic bed according to claim 4, characterized in that: The structural correction factor k ranges from 1.8 to 3.

2.

6. A detachable tubular reactor with an internally mounted multi-finned catalytic bed according to claim 5, characterized in that: The rotational drag coefficient CD of the multi-winged spherical (5) ranges from 1.1 to 1.

8.

7. A detachable tubular reactor with an internally mounted multi-finned catalytic bed according to claim 6, characterized in that: The rotational perturbation correction coefficient η of the multi-winged sphere (5) ranges from 0.1 to 0.

8.

8. A smart control method for a detachable tubular reactor with an internally mounted multi-finned catalytic bed as described in any one of claims 1-7, characterized in that: Includes the following steps: Multi-parameter coupled closed-loop control steps: Taking the reactor outlet concentration deviation e as the core control variable, fuzzy rules are used to adjust the initial PID parameters (Kp0, Ki0, K...). d0 Real-time correction is performed to obtain the corrected PID parameters (Kp, K). i , K d The optimal rotational speed ω of the catalyst bed was calculated based on the coupling constraint formula. opt The coupling constraint formula is: Where F is the feed flow rate, ΔH is the enthalpy change of the reaction, T is the reaction temperature, and k1, k2, and k3 are the correlation coefficients obtained by regression analysis of experimental data. Digital twin predictive control steps: A predictive model is constructed based on an LSTM neural network, using feed flow rate, catalyst bed rotation speed, and axial temperature distribution as inputs to predict the outlet concentration, axial midpoint concentration, and bed pressure drop over a future period; when the deviation between the predicted outlet concentration and the set value exceeds a first threshold, or the predicted axial midpoint concentration is lower than a second threshold, compensation adjustment of the PID parameters and catalyst bed rotation speed is triggered. Fault self-diagnosis steps: Using the torque deviation formula: δ M = |M meas - M calc | / M calc Determine the operating status of the catalyst bed, where M meas To measure the actual drive torque, M calc Based on the rotational dynamic equilibrium formula: The calculated theoretical driving torque, C D ρ is the rotational drag coefficient, ω is the fluid density, d is the angular velocity of rotation, and M is the diameter of the catalyst bed. f For frictional torque; when δ M When the value exceeds a preset threshold, a warning or alarm signal will be issued.

9. The intelligent control method for a detachable, internally mounted multi-finned catalytic bed tubular reactor according to claim 8, characterized in that: The initial PID parameters were obtained offline using the step response method, and their basic values ​​are: K p0 =3.6, K i0 =1.5, K d0 =1.2; The fuzzy rule is based on a fuzzy subset of the concentration deviation e and its rate of change ec, and outputs corrections ΔKp and ΔK to the initial PID parameters. i ΔK d .

10. The intelligent control method for a detachable, internally mounted multi-finned catalytic bed tubular reactor according to claim 9, characterized in that: The correlation coefficients in the coupling constraint formula were obtained from least squares regression experimental data, and their goodness of fit R0 was... 2 ≥0.996; The threshold for determining the torque deviation formula is: when 0.1 < δ M A maintenance warning is triggered when δ is ≤ 0.

2. M A fault alarm is triggered when the value is greater than 0.2.

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