Heat exchanger for hydrogenation reaction and system thereof

Abstract

The invention provides a heat exchanger for hydrogenation reaction and a system thereof, and relates to the field of heat exchangers, the heat exchanger comprises an outer tank body structure and an operation tank body structure, the outer tank body structure and the operation tank body structure are internally provided with a safety protection module a and a safety protection module b respectively, and the safety protection module a and the safety protection module b comprise sensor groups and reaction pipelines. The system further comprises an equipment space, a hydrogen separation precooling module is arranged in the equipment space, the system further comprises a monitoring and management interaction platform, and the monitoring and management interaction platform further comprises a heat exchange efficiency prediction module which obtains a heat exchange prediction model based on equipment data training. And the heat exchange prediction module is used for importing monitoring data in each device of the heat exchanger into a heat exchange prediction model, the hydrogenation temperature is dynamically adjusted on the basis of an XGBoost / LightGBM model feedback unit host, the hydrogenation reaction temperature control precision is further intelligently improved, and the problem that an existing heat exchange system is inconvenient to intelligently improve the hydrogenation reaction heat exchange temperature control precision by using a prediction model is solved.

Description

Technical Field

[0001] The present invention relates to the technical field of heat exchangers, and in particular to a heat exchanger and a system thereof for hydrogenation reaction. Background Art

[0002] During the synthesis of steroidal drugs, heat exchange is required between the hydrogen (H2) and reaction solvent (such as methanol), catalyst, and API in the hydrogenation reactor to remove the heat from the exothermic hydrogenation reaction and prevent reaction runaway (thermal runaway), product quality degradation, and process parameter runaway. Hydrogen can not only continue to dissolve and participate in the reaction, preventing separation from interrupting the process, but can also be used to improve heat exchange efficiency. The heat transfer coefficient is low during heat exchange in a gas-liquid mixed state: In a gas-liquid two-phase flow, the gas forms an insulating layer, reducing the overall heat transfer efficiency. Flow inhomogeneity: Gas-liquid mixing can easily lead to unstable flow patterns (such as stratified flow and annular flow), and large fluctuations in local thermal resistance. This may cause the local gas content to be too high, resulting in a sharp deterioration in heat transfer. Increased pressure drop: The friction resistance of two-phase flow is usually higher than that of single-phase flow, which may increase pump power consumption.

[0003] Existing heat exchangers need to control the temperature of the hydrogenation process in real time when dealing with the synthesis of steroid drugs. For example, the hydrogenation reaction of common drugs can easily reach above 100°C. For example, the optimal hydrogenation temperature range of hydrocortisone is 70±5°C, so it is necessary to effectively control its temperature. When using heat exchangers for pharmaceutical work, if a plate heat exchanger is used, it is easy to get clogged. If a spiral tube type is used, the heat transfer efficiency is low, the space occupied is large, and it is not easy to disassemble and replace the pipeline individually when a regional failure occurs. The existing heat exchange system is not convenient for using predictive models to intelligently improve the heat exchange temperature control accuracy of the hydrogenation reaction. Summary of the Invention

[0004] The object of the present invention is to provide a heat exchanger and a system thereof for hydrogenation reaction to solve the problems raised in the above background technology.

[0005] To achieve the above-mentioned purpose, the present invention provides the following technical solutions: a heat exchanger for hydrogenation reaction and its system, specifically including an outer tank structure and an operating tank structure, wherein the outer tank structure and the operating tank structure are respectively provided with a safety protection module a and a safety protection module b, the safety protection module a and the safety protection module b include a sensor group and a reaction pipeline, the sensor group includes a methanol sensor, a hydrogen sensor, a temperature sensor and an air pressure sensor, the reaction pipeline includes an anti-soluble foam fire extinguishing agent pipeline and a carbon dioxide pipeline driven by a high-pressure pump; an operating tank structure, wherein the operating tank structure is fixed to the inner side of the outer tank structure by bolts, the top of the operating tank structure is connected to a top cover by a flange, and through an inner and outer two-layer shell structure, the unit main unit is installed on the right side of the outer tank structure through a flange pipe at the left end, and the end of the flange pipe at the left end of the unit main unit extends to the On the inside of the operating tank structure, a control system is provided in the unit host, and an environmental sensor is installed on the inside of the flange pipe. The unit host is connected to the lines of the safety protection module a and the safety protection module b through the flange pipe. The unit host is connected to the monitoring and management interactive platform through wireless data, and the monitoring and management interactive platform is connected to several mobile terminal data. The environment in the double-layer area can be monitored through the safety protection module a and the safety protection module b. When a leak occurs in the operating tank or the outer tank structure, when solvents such as methanol and flammable substances such as hydrogen flow out, the alarm signal can be sent to the online platform through the unit host at the first time through monitoring. The maintenance personnel can quickly know the leakage of the hydrogenation reactor or the heat exchanger through the mobile terminal, and can remotely control the anti-solubility foam fire extinguishing agent pipeline and the carbon dioxide pipeline at the faulty container through the mobile terminal to discharge them, so that they fill the tank interlayer space for timely flame retardancy.

[0006] Preferably, it also includes an equipment space and an acceleration cabin, the equipment space is arranged in the upper half of the inner side of the working tank body structure, the hydrogen separation pre-cooling module is located inside the equipment space, and it also includes a finished product tank, the finished product tank is located inside the working tank body structure, the top of the finished product tank is connected to the top of the reaction chamber through a pipeline with a control valve and an air pressure sensor, the bottom of the finished product tank is connected to a discharge pump connected to the unit host control circuit through a flange, and the pump body outlet of the discharge pump is connected to the finished product pipe through a flange.

[0007] Preferably, the top of the outer tank structure is connected to a hemispherical head through a flange, the top of the hemispherical head on the top of the outer tank structure is connected to a flange cover through a flange, the top of the flange cover is connected to a three-way pipe through a flange, the rear end of the three-way pipe is connected to a secondary reflux pipe through a flange, the front end of the flange cover is connected to a soluble raw material liquid pipeline through a flange, the front end of the soluble raw material liquid pipeline is connected to a one-way valve a through a flange, the front end of the three-way pipe is connected to a one-way valve b through a flange, a one-way valve c is provided at the connection between the secondary reflux pipe and the three-way pipe, a methanol raw material pipeline is provided on the side of the three-way pipe, the top right end of the methanol raw material pipeline is connected to a one-way valve d through a flange, the right end of the one-way valve d is connected to the left end of the three-way pipe through a flange, a hydrogen raw material pipeline is provided on the rear side of the flange cover, the front end of the hydrogen raw material pipeline is connected to a one-way valve e through a flange, and a feed mist is provided under the flange cover. A feed atomization module includes an umbrella tube a and an umbrella tube b. The umbrella tube a is connected to the bottom of the trifurcated tube through a flange. An ultrasonic nozzle is installed at the bottom of the umbrella tube a. The umbrella tube b is connected to the bottom of the downward bend of the front end pipeline of the one-way valve e. Electric valves are respectively provided in the middle sections of the umbrella tube a and the umbrella tube b. The electric valves of the umbrella tube a and the umbrella tube b and the flow valve control circuits of various raw material pipelines are connected to the unit host. A catalyst can be installed through the flange under the flange cover as needed, so that the liquid raw material can continuously react by flushing the catalyst during the downward flow. The maintenance personnel can remotely adjust the feed amount through the mobile terminal. Through the pipeline setting, when methanol or raw material liquid is introduced, part of the liquid can be separated and atomized through the ultrasonic nozzle. A part of the liquid is atomized so that hydrogen, liquid medicine and methanol are atomized and fused.

[0008] Preferably, the hydrogen separation precooling module includes a separation tank, which is connected to the right side of the vertical pipe in the middle section of the acceleration cabin through a flange, and the left end of the separation tank is connected to a bent cone tube through a flange. A dome cover can be installed on the top of the bent cone tube as needed to disperse the liquid flow so that the liquid flow is dispersed to the surrounding areas to the adjustment hole. The separation tank is fixedly connected to an air distribution pipe, and the right end of the air distribution pipe is fixedly connected to a horizontal branch pipe. The inner curved surface of the separation tank is provided with a spiral guide plate, and the horizontal inclination angle of the spiral guide plate gradually increases from top to bottom. The inner side of the separation tank is fixedly connected to a condensation screen. , the front side of the separation tank is connected to a connecting pipe through a flange, the rear end of the connecting pipe is at the same height as the flange connection between the separation tank and the bent conical tube, a through hole is provided in the tapered part at the lower end of the acceleration cabin, and a negative pressure pipe is connected to the front lower part of the connecting pipe through a flange, and the convergence acceleration cooling catalytic module also includes a nickel, palladium, and platinum alloy spiral tube, which is a multi-layer structure, and the cross section of the nickel, palladium, and platinum alloy spiral tube is an inverted water drop shape, and low-pressure drainage surfaces are provided on both sides of the bottom of the nickel, palladium, and platinum alloy spiral tube. The multi-layer nickel, palladium, and platinum alloy disc A bridge bend is installed between the spiral tubes at the inner center and the outer edge. The through hole opened in the tapered part of the lower end of the negative pressure pipe is connected by a flange. The acceleration cabin is hourglass-shaped and consists of a middle vertical pipe and tapered parts at its upper and lower ends. The equipment space is located in the gap between the outside of the acceleration cabin and the inner side of the working tank structure. The acceleration cabin includes an adjustable separation module and a convergence acceleration cooling catalytic module. The convergence acceleration cooling catalytic module includes the vertical pipe part in the middle section of the acceleration cabin. When the atomized droplets flow downward with gravity, The pressurized injection of the upper feed pipeline and the negative pressure absorption of the tapered part at the lower end of the acceleration chamber cause the air flow in the acceleration chamber to form a vertical high-speed flow from top to bottom. When passing through the hourglass-shaped acceleration chamber, accompanied by the Bernoulli principle, the flow velocity in the narrower diameter pipe in the middle section increases, and the mist flow and liquid flow are accelerated through the nickel, palladium, and platinum alloy spiral tube. When the vertically downward fluid passes through the evenly distributed nickel, palladium, and platinum alloy spiral tube with an inverted water droplet-shaped cross-section, the flow velocity of the droplet in the lower half of the spiral tube is further increased, which further improves the contact efficiency of the spiral tube with catalytic effect with the raw liquid and hydrogen.

[0009] Preferably, the adjustable separation module includes a conical ring cover, an adjustable cone frame and a side pipe, the conical ring cover is fixedly connected to the inner side of the acceleration cabin, the outer curved surface of the conical ring cover is fixedly connected to a plane bearing, a plurality of adjustment holes are opened on the surface of the conical ring cover, the adjustable cone frame is rotatably connected to the outer side of the conical ring cover, the top of the adjustable cone frame is connected to the plane bearing, the outer curved surface of the adjustable cone frame is fixedly connected to a tooth portion, the side pipe is fixedly connected to the right side of the vertical pipe in the middle section of the acceleration cabin, the inner curved surface of the side pipe is fixedly connected to a C-ring in the vertical direction, the left side of the C-ring is fixedly connected to a sleeve by bolts, the inner side of the sleeve is rotatably connected to a worm gear mechanism, the turbine top of the worm gear mechanism is coaxially connected to a transmission gear, the transmission gear The wheel is meshed with the tooth part, and magnetic couplings are respectively provided on the left and right sides of the flange blind plate at the right end of the sleeve. The right end of the worm of the worm gear mechanism is coaxially connected to the left half of the magnetic coupling. A steel frame is fixedly installed on the inside of the equipment space, and a servo motor is provided in the steel frame. The double-head pump is installed in the equipment space, and the working chamber inlet at the front end of the double-head pump is connected to the bottom end of the separation tank through a flange. The bottom of the secondary return pipe is connected to the working chamber outlet at the rear end of the double-head pump. The servo motor shaft is coaxially connected to the right half of the magnetic coupling, and the servo motor control circuit is connected to the unit host. The vertical pipe in the middle section of the acceleration cabin and the tapered parts at the upper and lower ends are equidistantly installed on the inner surface with temperature sensors connected to the unit host. Sensors and pressure sensors, maintenance personnel receive data through the mobile terminal to obtain the current reaction status. When the temperature needs to be adjusted, the servo motor can be controlled by the remote control unit host to make its shaft drive the magnetic coupler to non-contact control the worm gear mechanism to operate, and the transmission gear coaxial with the worm gear cooperates with its meshing teeth to drive the adjustment cone frame to rotate, and the size of the adjustment hole can be adjusted to adjust the initial air intake into the hydrogen separation pre-cooling module. The double-head pump drives the bent cone tube to perform downward negative pressure absorption, so that the atomized droplets and hydrogen flow are absorbed into the gas distribution pipe. The droplets flow through the spiral blade drainage transmission process to separate the liquid and gas. Part of the separated air flow can be separately introduced into the pipeline inside the heat exchange box a through the pump body to connect with the liquid The flow is pre-cooled in advance, and the low-temperature hydrogen that has been cooled in advance is introduced into the pressurized tank A for storage through the pump. The monitoring and management interactive platform processing system adjusts the venting of the pressurized tank A in time according to the current temperature in the reaction chamber, so that it can fill the pre-stored appropriate amount of low-temperature hydrogen into the mixed liquid through the sieve tube, so that it can always maintain the optimal hydrogenation temperature range of 70±5℃ for hydrocortisone. Sensor equipment for detecting the solvent content can be installed in the reaction chamber as needed. The control system measures the data of the pump, sensor and flow valve before and after the reaction in real time, and at the same time, according to the gas data feedback, the consumed hydrogen is stoichiometrically determined in real time and then the gas heat exchange is supplemented for the second time. It can automatically adjust the optimal amount of hydrogen required for the reaction chamber without personnel control, and cooperate with the air pressure sensor.Reduce the occurrence of inadequate responses.

[0010] Preferably, the reaction chamber is connected to the inner side of the working tank structure through a flange, the reaction chamber is located below the acceleration cabin, a hexagonal frame is installed inside the reaction chamber, a liquid circulation module is provided at the bottom of the reaction chamber, the liquid circulation module includes a circulation pipe, the circulation pipe is provided at the bottom of the reaction chamber through a flange connection, the working chamber inlet at the rear end of the double-head pump is connected to the top of the circulation pipe, the pipelines and containers of each equipment of the heat exchanger are also respectively installed with temperature, pressure, catalyst concentration, flow rate, pH value, product chromatographic purity sensors, a temperature sensor and a radar-type liquid volume sensor connected to the unit host circuit are installed at the bottom of the inner side of the reaction chamber, a return pipe, the return pipe is installed on the outside of the hexagonal frame through a clamp, the top of the return pipe is connected to the exhaust pipe of the pressurized tank A through a flange, the pressurized tank A is located on the inside of the equipment space, a vertical air pipe, and the vertical air pipe is installed in the middle of the hexagonal frame through a clamp. The top of the vertical air pipe is connected to the pressurized tank B through a drain pipe with a pressure sensor and a control valve. A pressurized tank B is provided on the inside of the equipment space, and several groups of sieve tubes are connected to the bottom of the vertical air pipe. The exhaust pipe of the pressurized tank A is installed with a pressure sensor and a control valve. The rear side of the pressurized tank A is connected to an air inlet pipe with a one-way valve. The air inlet pipe of the pressurized tank A is connected to the outlet of the working chamber at the front end of the double-head pump. The double-head pump is operated to make the liquid inside the reaction chamber flow upward to the feed atomization module, so that the drug liquid that has not fully reacted can be refluxed for circulation and cooling. The continuous impact of the vertical fluid and the gas filling can prevent the drug crystals from adhering to the inner wall of the equipment while cooling the solvent of the hydrogenation reaction.

[0011] Preferably, it also includes a gasket pipe heat exchange system, which is arranged inside the operating tank structure, and the gasket pipe heat exchange system includes a heat exchange box a and a heat exchange box b, and the working chamber outlet at the front end of the double-head pump is connected to the heat box a pipeline, and the heat exchange box a and the heat exchange box b are respectively installed on the left and right sides of the equipment space, and two sets of line cabins are installed on the upper and lower sides of the heat exchange box a, and the heat exchange box a and the heat exchange box b are provided with pipeline area compensation monitoring modules, and the bottom and left side of the heat exchange box a are respectively connected to the top of the pressurized tank B and the horizontal branch pipe at the right end of the air distribution pipe, and the gasket pipe heat exchange system also includes mutually nested vertical hexagonal tube a, vertical hexagonal tube b and vertical hexagonal tube c, and the vertical hexagonal tube a, vertical hexagonal tube b and vertical hexagonal tube c are provided with chamfers at the upper and lower edges, and the left and right sides of the end of the vertical hexagonal tube c are symmetrically provided with fitting slopes a, and the left and right sides of the end of the vertical hexagonal tube b are respectively provided with two sets of asymmetric fitting slopes b, the vertical hexagonal tube a, the vertical hexagonal tube b and the vertical hexagonal tube c are vertically slidably nested with each other, a hexagonal space is provided between the vertical hexagonal tube a, the vertical hexagonal tube b and the vertical hexagonal tube c, the monitoring control tube is slidably connected to the inner side of the hexagonal space, after the vertical hexagonal tube c is vertically aligned, the vertical hexagonal tube a and the vertical hexagonal tube b can be butt-jointed and spliced ​​from their upper and lower sides respectively, the vertical hexagonal tube c is connected to the high-temperature pipeline separately, so that the vertical hexagonal tube a and the vertical hexagonal tube c are After b is connected to the low-temperature pipeline, the vertical-grained hexagonal tube a and the vertical-grained hexagonal tube b can make high-density contact with the vertical-grained hexagonal tube c, so that the high-temperature pipeline can always be wrapped in the low-temperature pipeline, which can fully cool it. At the same time, the inner and outer walls of the vertical-grained hexagonal tube are stamped with vertical grooves, and various fitting inclined surfaces cooperate closely with each other to enable each group of vertical-grained hexagonal tubes to cross-slide and assemble, solving the problem of large space occupation of spiral tube heat exchangers. The structure of the vertical-grained hexagonal tube solves the problem of easy blockage of plate heat exchangers while improving heat transfer efficiency.

[0012] Preferably, the pipeline area compensation monitoring module includes several groups of monitoring and control tubes, and several groups of the monitoring and control tubes are equidistantly fixed on the surface of the circuit cabin. The cross section of the monitoring and control tube is a regular hexagon, and the vertical facade of the monitoring and control tube is provided with a square hole. A circuit tube is installed on the inside of the monitoring and control tube, and a temperature sensor and a semiconductor refrigeration plate are installed inside the square hole respectively. After assembling the vertical hexagonal tubes, the upper and lower parts of the circuit cabin with the monitoring and control tubes are docked, so that the monitoring and control tubes are inserted into the hexagonal space of the upper and lower parts, so that a honeycomb structure with sliding contact can be formed. Separate vertical hexagonal tubes can be assembled by flanges or welding. While supported by the equidistantly distributed monitoring and control tubes, they can monitor the local temperature changes of the heat exchange pipeline in real time, and cooperate with the monitoring and management interactive platform to assist in adjusting the temperature of the heat exchange pipeline. The working process of the above-mentioned pipeline area compensation monitoring module includes the following steps:

[0013] Step 1: Liquid and gas are heat exchanged through the curved hexagonal tube.

[0014] Step 2: Monitor each area of ​​the pipeline through sensors of the monitoring control pipe distributed equally in the hexagonal space to establish a temperature change model.

[0015] Step 3: It is normal when the temperature change of the entire pipeline is evenly distributed.

[0016] Step 4: When the abnormality of the regional pipeline temperature change data is less than the model warning value, the regional pipeline temperature is corrected through the semiconductor cooling plate.

[0017] Step 5: When the abnormality of the regional pipeline temperature change data exceeds the model warning value, an early warning is issued, and the regional pipeline fault location is sent. Maintenance personnel can quickly find the heat exchanger pipeline fault location by monitoring the control pipe data, facilitating rapid repair and replacement.

[0018] Preferably, the heat exchanger system for hydrogenation reaction also includes two groups of external machines, a monitoring and management interactive platform, a processing system, a mobile terminal, a heat exchange equipment database, a heat exchange prediction module and a real-time interactive module. The two groups of external machines are arranged on the rear side of the outer tank structure, and the two groups of external machines are connected to the heat exchange box a and the heat exchange box b respectively through pipelines. The two groups of external machine control circuits are connected to the unit host. The monitoring and management interactive platform is used to collect and summarize the real-time data of the unit host of each heat exchanger through a network protocol; the mobile terminal is used to connect to the monitoring and management interactive platform data in real time, for maintenance personnel to monitor equipment data and make feedback instructions based on data information. The database stores multiple groups of internal equipment data of the heat exchanger, and obtains a heat exchange prediction model based on equipment data training; the heat exchange prediction module is used to integrate the monitoring data in each device of the heat exchanger into the heat exchange prediction model; the real-time interactive module is used to connect the unit host control circuit and the mobile terminal, for maintenance personnel to remotely monitor and control.

[0019] The present invention provides a heat exchanger and system for hydrogenation reaction, which have the following beneficial effects:

[0020] 1. According to the structures of various embodiments of the present invention, the distance between hydrogen gas molecules is large and the interaction between molecules is weak, so the heat transfer is faster than that of liquid. The hydrogen that has been previously heat-exchanged is used, filtered, and then re-filled into the liquid phase that has not been completely heat-exchanged to utilize the residual heat, so that the gas that has been previously heat-exchanged assists the liquid in heat exchange, avoiding heat energy waste, reducing pump labor consumption, and improving heat exchange efficiency.

[0021] 2. A heat exchange prediction model is obtained based on equipment data training. The heat exchange prediction module is used to integrate the monitoring data in each device of the heat exchanger into the heat exchange prediction model. Based on the XGBoost / LightGBM model feedback unit host, the hydrogenation temperature is dynamically adjusted, which can further intelligently improve the temperature control accuracy of the hydrogenation reaction.

[0022] 3. Utilizing the Bernoulli principle, when the fast-flowing gas and liquid pass through multiple layers of evenly distributed spiral tubes, the pressure change causes the spiral tubes containing the catalyst components to undergo high-intensity friction with the raw gas and liquid, allowing the raw materials to fully mix and react, further improving the contact efficiency while preventing process temperature from getting out of control.

[0023] 4. The double-layer tank design not only ensures safety, but also has reserved space for equipment to be installed around it. The surround layout and integrated closed design improve space utilization.

[0024] 5. The double-head pump is operated to return the liquid inside the reaction chamber upward to the feed atomization module, so that the drug liquid that has not fully reacted can be refluxed for circulation and cooling. The continuous impact of vertical fluid and gas filling can cool the solvent of the hydrogenation reaction while preventing drug crystals from adhering to the inner wall of the equipment.

[0025] 6. The control system measures the data of the pump station, solvent sensor and flow valve before and after the reaction in real time. At the same time, it measures the stoichiometric amount of hydrogen consumed in real time based on the gas data feedback and then performs secondary gas heat exchange replenishment. It can automatically adjust the optimal amount of hydrogen required for the reaction chamber without human control, and reduce the occurrence of insufficient reaction by cooperating with the air pressure sensor.

[0026] 7. The vertical hexagonal tube a and the vertical hexagonal tube b make high-density contact with the vertical hexagonal tube c, so that the high-temperature pipeline can always be wrapped in the low-temperature pipeline, which can fully cool it. At the same time, the vertical hexagonal tubes are stamped with vertical grooves on the inner and outer walls, and various fitting inclined surfaces cooperate closely with each other to enable each group of vertical hexagonal tubes to cross-slide and assemble, solving the problem of large space occupation of spiral tube heat exchangers. At the same time, the structure of the vertical hexagonal tubes improves the heat transfer efficiency while solving the problem of easy blockage of plate heat exchangers.

[0027] 8. When the abnormality of regional pipeline temperature change data exceeds the model warning value, an early warning will be sent. Maintenance personnel can quickly find the location of the heat exchanger pipeline failure through monitoring and control pipe data. The cross-docking structure facilitates disassembly and assembly, making it easy to quickly repair and replace the heat exchanger failure pipeline.

[0028] 9. The control system measures the data in real time, and at the same time, it determines the stoichiometric amount of hydrogen consumed in real time based on the gas data feedback, and then performs secondary gas heat exchange replenishment. It can automatically adjust the optimal amount of hydrogen required by the reaction chamber without human control to avoid the occurrence of insufficient reaction. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings of the embodiments are briefly introduced below.

[0030] The drawings described below only relate to some embodiments of the present invention, but are not intended to limit the present invention.

[0031] In the attached figure:

[0032] Figure 1 It is a structural diagram of the system of embodiment 1 of the present invention.

[0033] Figure 2 It is a schematic diagram of the system structure of the monitoring and management interactive platform of the first embodiment of the present invention.

[0034] Figure 3 It is a schematic diagram of the three-dimensional structure of the rear side of the first embodiment of the present invention.

[0035] Figure 4 It is a schematic three-dimensional cross-sectional view of the entire embodiment of the present invention.

[0036] Figure 5 yes Figure 4 A partial enlarged schematic diagram of the middle A.

[0037] Figure 6 It is a three-dimensional cross-sectional schematic diagram of the acceleration cabin of the first embodiment of the present invention.

[0038] Figure 7 yes Figure 6 A partial enlarged schematic diagram of B in the figure.

[0039] Figure 8 It is a three-dimensional cross-sectional schematic diagram of the reaction chamber of Example 1 of the present invention.

[0040] Figure 9 It is a three-dimensional cross-sectional schematic diagram of the heat exchange box a according to the first embodiment of the present invention.

[0041] Figure 10 It is a three-dimensional disassembled schematic diagram of the wiring compartment of the first embodiment of the present invention.

[0042] Figure 11 1 is a top perspective schematic diagram of hexagonal tube a, hexagonal tube b, and hexagonal tube c according to the first embodiment of the present invention.

[0043] Figure 12 It is a three-dimensional cross-sectional schematic diagram of the nickel, palladium and platinum alloy spiral tube according to the first embodiment of the present invention.

[0044] Figure 13 It is a three-dimensional disassembly schematic diagram of the working tank structure of Example 1 of the present invention.

[0045] Figure 14 It is a three-dimensional disassembled schematic diagram of hexagonal tube a, hexagonal tube b, and hexagonal tube c in Example 1 of the present invention.

[0046] Figure 15 It is a side perspective schematic diagram of the acceleration cabin according to the first embodiment of the present invention.

[0047] Figure 16 It is a three-dimensional disassembled schematic diagram of the monitoring and control tube of the first embodiment of the present invention.

[0048] Figure 17 It is a front top perspective schematic diagram of the outer tank structure of the first embodiment of the present invention.

[0049] Figure 18 1 is a top perspective schematic diagram of hexagonal tube a, hexagonal tube b, and hexagonal tube c according to the first embodiment of the present invention.

[0050] Figure 19 Schematic diagram of the working steps of the pipeline area compensation monitoring module in the first embodiment of the present invention.

[0051] Figure 20 1 is a top perspective schematic diagram of hexagonal tube a, hexagonal tube b, and hexagonal tube c according to the fourth embodiment of the present invention.

[0052] Reference Signs List

[0053] 1. Outer tank structure; 101. Flange cover; 102. Trident pipe; 1021. Secondary reflux pipe; 1022. Check valve a; 1023. Check valve b; 1024. Check valve c; 103. Umbrella pipe a; 1031. Ultrasonic nozzle; 104. Umbrella pipe b; 2. Soluble API liquid pipeline; 3. Methanol raw material pipeline; 301. Check valve d; 4. Hydrogen raw material pipeline; 401. Check valve e; 5. Working tank structure Structure; 501, top cover; 6, equipment space; 7, acceleration chamber; 701, conical ring cover; 702, plane bearing; 703, adjustment hole; 704, adjustment cone frame; 7041, tooth portion; 705, side pipe; 706, C-ring; 707, sleeve; 708, worm gear mechanism; 709, transmission gear; 710, magnetic coupling; 8, separation tank; 801, curved cone pipe; 802, gas distribution pipe; 803, condensation screen; 80 4. Connecting pipe; 8041. Negative pressure pipe; 9. Double-head pump; 10. Reaction chamber; 1001. Hexagonal rack; 1002. Circulation pipe; 11. Liquid return pipe; 1101. Pressurized tank A; 12. Vertical air pipe; 1201. Pressurized tank B; 1202. Sieve tube; 13. Heat exchange box a; 1301. Line compartment; 1302. Monitoring and control pipe; 1303. Square hole; 1304. Line pipe; 1305. Temperature and humidity sensor; 130 6. Semiconductor refrigeration plate; 1307. Hexagonal space; 14. Vertical hexagonal tube a; 15. Vertical hexagonal tube b; 1501. Fitting slope a; 16. Vertical hexagonal tube c; 1601. Fitting slope b; 17. Heat exchange box b; 18. Nickel, palladium, and platinum alloy spiral tube; 1801. Low-pressure drainage surface; 1802. Bridge bend; 19. Finished product tank; 1901. Discharge pump; 20. Finished product pipe; 21. Unit host; 22. External unit. DETAILED DESCRIPTION

[0054] The embodiments of the present invention are described in further detail below with reference to the accompanying drawings and examples.

[0055] See also Figure 1-19, Embodiment 1 provided by the present invention: The present invention provides a heat exchanger for hydrogenation reaction and its system, including an outer tank structure 1 and an operating tank structure 5, wherein the outer tank structure 1 and the operating tank structure 5 are respectively provided with a safety protection module a and a safety protection module b, the safety protection module a and the safety protection module b include a sensor group and a reaction pipeline, the sensor group includes a methanol sensor, a hydrogen sensor, a temperature sensor and an air pressure sensor, the reaction pipeline includes an anti-solvent foam fire extinguishing agent pipeline and a carbon dioxide pipeline driven by a high-pressure pump, the operating tank structure 5, the operating tank structure 5 is fixed to the inner side of the outer tank structure 1 by bolts, the top of the operating tank structure 5 is connected to a top cover 501 by a flange, a unit host 21, and the unit host 21 is connected to the outer tank structure 1 by a flange. The flange pipe passing through the left end is installed on the right side of the outer tank structure 1. The end of the flange pipe at the left end of the unit host 21 extends to the inside of the operating tank structure 5. An environmental sensor is installed on the inside of the flange pipe. It also includes an equipment space 6. The equipment space 6 is set in the upper half of the inside of the operating tank structure 5. The unit host 21 is connected to the lines of the safety protection module a and the safety protection module b through the flange pipe. The unit host 21 is connected to the monitoring and management interactive platform through wireless data. The monitoring and management interactive platform is connected to several mobile terminal data. The double-layer tank design ensures safety while the equipment space 6 reserved inside it is convenient for various equipment components to be installed around it. The surround layout solves the problem of large space occupation of existing heat exchangers.

[0056] Furthermore, the top of the outer tank structure 1 is connected to a hemispherical head through a flange, the top of the hemispherical head on the top of the outer tank structure 1 is connected to a flange cover 101 through a flange, the top of the flange cover 101 is connected to a three-way pipe 102 through a flange, the rear end of the three-way pipe 102 is connected to a secondary return pipe 1021 through a flange, the front end of the flange cover 101 is connected to a soluble raw material drug liquid pipeline 2 through a flange, the front end of the soluble raw material drug liquid pipeline 2 is connected to a one-way valve a1022 through a flange, the front end of the three-way pipe 102 is connected to a one-way valve b1023 through a flange, a one-way valve c1024 is provided at the connection between the secondary reflux pipe 1021 and the three-way pipe 102, and a methanol raw material pipeline 3 is provided on the side of the three-way pipe 102. The right end of the top of the methanol raw material pipeline 3 is connected to a one-way valve d301 through a flange, and the right end of the one-way valve d301 is connected to the left end of the three-way pipe 102 through a flange. A hydrogen raw material pipeline 4 is arranged on the rear side of the flange cover 101, and the front end of the hydrogen raw material pipeline 4 is connected to a one-way valve e401 through a flange. The bottom of the three-way pipe 102 is connected to an umbrella pipe a103 through a flange, and an ultrasonic nozzle 1031 is installed at the bottom of the umbrella pipe a103. The front end pipeline of the one-way valve e401 is bent downward, and an umbrella pipe b104 is arranged at the bottom. Electric valves are respectively provided in the middle sections of the umbrella pipe a103 and the umbrella pipe b104. Through the processing and control system in the unit host 21, the material entry amount can be adjusted according to the model.

[0057] Furthermore, it also includes an acceleration cabin 7, an equipment space 6 is arranged in the upper half of the inner side of the working tank structure 5, and the hydrogen separation pre-cooling module is located inside the equipment space 6. The acceleration cabin 7 is hourglass-shaped and consists of a middle vertical pipe and tapered parts at its upper and lower ends. The equipment space 6 is located in the gap between the outer side of the acceleration cabin 7 and the inner side of the working tank structure 5. The acceleration cabin 7 includes an adjustable separation module and a convergence acceleration cooling catalytic module. The convergence acceleration cooling catalytic module includes a vertical pipe part in the middle section of the acceleration cabin 7, and the adjustable separation module includes a conical ring cover 701, a volume adjustment cone frame 704 and a side pipe 705. The conical ring cover 701 The cone ring cover 701 is fixedly connected to the inside of the acceleration chamber 7, and the outer curved surface of the cone ring cover 701 is fixedly connected to the plane bearing 702. The surface of the cone ring cover 701 is provided with a plurality of adjustment holes 703. The adjustment cone frame 704 is rotatably connected to the outside of the cone ring cover 701. The top of the adjustment cone frame 704 is connected to the plane bearing 702. The outer curved surface of the adjustment cone frame 704 is fixedly connected to a tooth portion 7041. The side pipe 705 is fixedly connected to the right side of the vertical pipe in the middle section of the acceleration chamber 7. The inner curved surface of the side pipe 705 is fixedly connected to a C-shaped ring 706 in the vertical direction. The left side of the C-shaped ring 706 is fixedly connected to a sleeve 707 by bolts. The sleeve 707 The inner side is connected to the worm gear mechanism 708, and the top of the turbine of the worm gear mechanism 708 is coaxially connected to the transmission gear 709, which is engaged with the tooth portion 7041. The left and right sides of the flange blind plate at the right end of the sleeve 707 are respectively provided with magnetic couplers 710. The right end of the worm of the worm gear mechanism 708 is coaxially connected to the left half of the magnetic coupler 710. A steel frame is fixedly installed inside the equipment space 6, and a servo motor is arranged in the steel frame. The servo motor shaft is coaxially connected to the right half of the magnetic coupler 710. The control circuit of the servo motor is connected to the unit host 21, and the acceleration Temperature sensors and pressure sensors connected to the unit main unit 21 are installed equidistantly on the inner surface of the vertical pipe in the middle section of the cabin 7 and the tapered parts at its upper and lower ends. The unit main unit 21 controls the operation of the servo motor so that its shaft drives the magnetic coupler 710 to non-contactly control the operation of the worm gear mechanism 708. The transmission gear 709 coaxial with the worm gear cooperates with the tooth portion 7041 meshing with it to drive the adjustment cone frame 704 to rotate, and the opening size of the adjustment hole 703 can be adjusted, thereby adjusting the initial air intake volume entering the hydrogen separation pre-cooling module, so that the unit main unit 21 can automatically adjust the low-temperature hydrogen volume as needed.

[0058] Furthermore, the hydrogen separation precooling module includes a separation tank 8, which is connected to the right side of the vertical pipeline in the middle section of the acceleration cabin 7 through a flange, and the left end of the separation tank 8 is connected to a bent conical tube 801 through a flange, and a gas distribution pipe 802 is fixedly connected inside the separation tank 8, and the right end of the gas distribution pipe 802 is fixedly connected to a horizontal branch pipe. The inner curved surface of the separation tank 8 is provided with a spiral guide plate, and the horizontal inclination angle of the spiral guide plate gradually increases from top to bottom. A condensation screen 803 is fixedly connected to the inside of the separation tank 8, and a connecting pipe 804 is connected to the front side of the separation tank 8 through a flange. The rear end of the connecting pipe 804 is at the same height as the flange connection between the separation tank 8 and the bent conical tube 801. A through hole is provided in the conical part at the lower end of the acceleration cabin 7, and a negative pressure pipe 8041 is connected to the front and lower part of the connecting pipe 804 through a flange. The through hole opened in the conical part at the lower end of the acceleration cabin 7 is connected by a flange. The negative pressure pipe 8041 is connected to the through hole in the conical part at the lower end of the acceleration cabin 7 through a flange. The flow velocity of the gas and liquid in the equipment can be further enhanced through negative pressure absorption, which can enhance the heat exchange efficiency.

[0059] Furthermore, it also includes a double-head pump 9, which is installed in the equipment space 6, and the working chamber inlet at the front end of the double-head pump 9 is connected to the bottom end of the separation tank 8 through a flange, and the bottom of the secondary reflux pipe 1021 is connected to the working chamber outlet at the rear end of the double-head pump 9, and a reaction chamber 10. The reaction chamber 10 is connected to the inner side of the working tank structure 5 through a flange, and the reaction chamber 10 is located below the acceleration cabin 7. A hexagonal frame 1001 is installed on the inner side of the reaction chamber 10, and a liquid circulation module is provided at the bottom of the reaction chamber 10. The liquid circulation module includes a circulation pipe 1002, and the circulation pipe 1002 is provided at the bottom of the reaction chamber 10 through a flange connection. The working chamber inlet at the rear end of the double-head pump 9 is connected to the top of the circulation pipe 1002, and a temperature sensor and a radar-type liquid volume sensor connected to the circuit of the unit host 21 are installed at the bottom inside the reaction chamber 10, and the sensor circuit is connected to the unit host 21. Through the collected data of the sensor, the control and processing system in the host performs intelligent allocation and processing according to the model data.

[0060] Furthermore, it also includes a return liquid pipe 11, which is installed on the outside of the hexagonal frame 1001 through a clamp, and the top of the return liquid pipe 11 is connected to the exhaust pipe of the pressurized tank A1101 through a flange, and the pressurized tank A1101 is located inside the equipment space 6. The exhaust pipe of the pressurized tank A1101 is installed with a pressure sensor and a control valve. The rear side of the pressurized tank A1101 is connected to an air inlet pipe with a one-way valve, and the air inlet pipe of the pressurized tank A1101 is connected to the working chamber outlet at the front end of the double-head pump 9, a vertical air pipe 12, and the vertical air pipe 12 is installed in the middle of the hexagonal frame 1001 through a clamp, and the top of the vertical air pipe 12 is connected to the pressurized tank B1201 through a discharge pipe with a pressure sensor and a control valve. The pressurized tank B1201 is arranged inside the equipment space 6, and the bottom of the vertical air pipe 12 is connected to several groups of sieve tubes 1202. It also includes a pad tube heat exchange system, which is arranged inside the working tank structure 5. The pad tube heat exchange system includes a heat exchange box a13 and a heat exchange box b17. The heat exchange box a13 and the heat exchange box b17 are respectively installed on the left and right sides of the equipment space 6. Two sets of line cabins 1301 are installed on the upper and lower sides of the heat exchange box a13. The heat exchange box a13 and the heat exchange box b17 are provided with a pipeline area compensation monitoring module. The pipeline area compensation monitoring module includes several groups of monitoring control pipes 1302, and the several groups of monitoring control pipes 1302 are fixedly installed at equal distances. On the surface of the circuit cabin 1301, the cross-section of the monitoring and control tube 1302 is a regular hexagon. A square hole 1303 is opened on the vertical surface of the monitoring and control tube 1302. A circuit tube 1304 is installed inside the monitoring and control tube 1302. A temperature and humidity sensor 1305 and a semiconductor refrigeration plate 1306 are installed inside the square hole 1303. The bottom and left side of the heat exchange box a13 are connected to the top of the pressurized tank B1201 and the horizontal branch pipe at the right end of the gas distribution pipe 802 respectively. The working process of the above-mentioned pipeline area compensation monitoring module includes the following steps:

[0061] Step 1: Liquid and gas are heat exchanged through the curved hexagonal tube.

[0062] Step 2: Monitor each area of ​​the pipeline through sensors of the monitoring control tube 1302 in the equally distributed hexagonal space 1307 to establish a temperature change model.

[0063] Step 3: It is normal when the temperature change of the entire pipeline is evenly distributed.

[0064] Step 4: When the abnormality of the regional pipeline temperature change data is less than the model warning value, the regional pipeline temperature is corrected through the semiconductor cooling plate 1306.

[0065] Step 5: When the abnormality of the regional pipeline temperature change data exceeds the model warning value, an early warning is sent and the regional pipeline fault location is sent.

[0066] Furthermore, the pad tube heat exchange system also includes vertical hexagonal tubes a14, b15 and c16 nested with each other. The vertical hexagonal tubes a14, b15 and c16 are provided with chamfers at the upper and lower ends. The left and right sides of the end of the vertical hexagonal tube b15 are symmetrically provided with fitting slopes a1501. The left and right sides of the end of the vertical hexagonal tube c16 are provided with two sets of asymmetrical fitting slopes b1601. The vertical hexagonal tubes a14, b15 and c16 are nested with each other in a vertical sliding manner. The vertical hexagonal tubes a14, b15 and c16 are nested with each other in a vertical sliding manner. A hexagonal space 1307 is provided between the tube b15 and the vertical-striped hexagonal tube c16, and the monitoring and control tube 1302 is slidably connected to the inner side of the hexagonal space 1307. After the vertical-striped hexagonal tube c16 is vertically aligned, the vertical-striped hexagonal tube a14 and the vertical-striped hexagonal tube b15 can be docked and inserted for splicing from the upper and lower sides thereof respectively. The vertical-striped hexagonal tube c16 is connected to the high-temperature pipeline alone. After the vertical-striped hexagonal tube a14 and the vertical-striped hexagonal tube b15 are connected to the low-temperature pipeline, the vertical-striped hexagonal tube a14 and the vertical-striped hexagonal tube b15 can be made to make high-density contact with the vertical-striped hexagonal tube c16, so that the high-temperature pipeline can always be wrapped in the low-temperature pipeline.

[0067] Furthermore, the convergent accelerated cooling catalytic module also includes a nickel, palladium, platinum alloy spiral tube 18, which is a multi-layer structure. The cross section of the nickel, palladium, platinum alloy spiral tube 18 is in the shape of an inverted water droplet. Low-pressure drainage surfaces 1801 are provided on both sides of the bottom of the nickel, palladium, platinum alloy spiral tube 18. Bridge bends 1802 are installed between the multi-layer nickel, palladium, platinum alloy spiral tubes 18 through the inner center and the outer edge. When the atomized droplets flow downward with gravity, the pressurized injection of the upper feed pipeline and the negative pressure absorption of the conical part at the lower end of the acceleration cabin 7 form a vertical high-speed flow in the acceleration cabin 7. When passing through the hourglass-shaped acceleration cabin 7, the middle The flow rate in the narrower diameter pipe increases, and the mist flow and liquid flow are accelerated through the nickel, palladium, and platinum alloy spiral tube 18. When the vertically downward fluid passes through the evenly distributed nickel, palladium, and platinum alloy spiral tube 18 with an inverted water droplet-shaped cross section, the flow rate of the droplets in the lower half of the spiral tube is further increased. When the droplets and gas are accelerated downward to impact the high-pressure surface of the upper half of the spiral tube, the pressure increases and the flow rate slows down. When flowing downward through the low-pressure drainage surfaces 1801 on both sides, the pressure increases again. When the gas and liquid pass through multiple layers of evenly distributed spiral tubes, the pressure change causes the spiral tubes with catalyst components to undergo high-density friction with the raw gas and liquid, further improving the contact efficiency while preventing the process temperature from getting out of control.

[0068] Furthermore, it also includes a finished product tank 19, which is located inside the operating tank structure 5. The top of the finished product tank 19 is connected to the top of the reaction chamber 10 through a pipe with a control valve and an air pressure sensor. The bottom of the finished product tank 19 is connected to a discharge pump 1901 connected to the control circuit of the unit host 21 through a flange, and the pump body outlet of the discharge pump 1901 is connected to the finished product pipe 20 through a flange. The heat exchange system also includes two groups of external machines 22, which are arranged on the rear side of the outer tank structure 1. The two groups of external machines 22 are connected to the heat exchange box a13 and the heat exchange box b17 through pipelines respectively. The control circuits of the two groups of external machines 22 are connected to the unit host 21. The control circuits of the two groups of external machines 22 are connected to the unit host 21. The monitoring and management interactive platform is used to collect and summarize the real-time data of the unit host 21 of each heat exchanger through a network protocol to establish a database. The mobile terminal is used to connect to the data of the monitoring and management interactive platform in real time. The monitoring and management interactive platform is connected to the data of several unit hosts 21 for maintenance personnel to monitor the equipment. Prepare data and make feedback instructions based on the data information. The database stores temperature, pressure, catalyst concentration, flow rate, pH value, product chromatographic purity and other data extracted by sensors from multiple groups of internal equipment of the heat exchanger. The monitoring and management interactive platform also includes a heat exchange efficiency prediction module, which derives a heat exchange prediction model based on equipment data training. The heat exchange prediction module is used to integrate the monitoring data in each device of the heat exchanger into the heat exchange prediction model. Based on the XGBoost / LightGBM model feedback unit host 21 sends an adjustment control signal to dynamically adjust the hydrogenation temperature, thereby further intelligently improving the temperature control accuracy of the hydrogenation reaction.

[0069] Example 2: Based on Example 1, containers with catalysts are installed below the ultrasonic nozzle 1031 and inside the reaction chamber 10, respectively. A product chromatography detection module is installed in the finished product tank 19. Catalyst concentration sensors, flow rate sensors, pH sensors, and product chromatography purity sensors are also installed in each module container and pipeline included in the embodiment as a whole.

[0070] Example 3: On the basis of Example 1, one-way valves and control valves are installed on the pipes connecting the separation tank 8 and each device as needed, and the pressurized tank A1101 is separately installed with an outward discharge pipe with a pressure relief valve as needed, and the outward discharge pipe is connected to the hydrogen raw material pipeline 4. At the same time, separate valves and sensors are installed at both ends of the hydrogen raw material pipeline 4 at the connection with the outward discharge pipe to prevent the excessive air pressure in the tank from causing abnormalities in the tank body.

[0071] Example 4: Figure 20 As shown, the arrangement of the vertical hexagonal tube a14, the vertical hexagonal tube b15 and the vertical hexagonal tube c16 can be as follows: Figure 19By combining in the manner shown, the number of hexagonal spaces 1307 can be reduced by half, and at the same time, the number of monitoring and control tubes 1302 can be reduced by half, so that the contact of the heat exchange pipelines is more compact, the heat exchange efficiency is improved, and the circuit cabin 1301 is set to be installed on one side, thereby further saving floor space.

[0072] The specific usage and function of this embodiment: When the present invention is used, first, raw materials such as hydrogen, methanol, and pharmaceuticals are driven by a pump body that is separately connected to the unit host 21 data. When they enter the working tank structure 5 from above through the pipeline, part of their liquid components are atomized by the feed atomization module. When the atomized droplets flow downward with gravity, the pressurized injection of the upper feed pipeline and the negative pressure absorption of the conical part at the lower end of the acceleration cabin 7 form a vertical high-speed flow from top to bottom in the acceleration cabin 7. When passing through the hourglass-shaped acceleration cabin 7, the flow velocity in the pipe with a narrower diameter in the middle section increases along with the Bernoulli principle. The gas meets the liquid phase and is accelerated through the nickel, palladium, and platinum alloy spiral tube 18. When the vertically downward fluid passes through the nickel, palladium, and platinum alloy spiral tube 18 with a uniformly distributed cross-section in the shape of an inverted water droplet, the droplets further increase their flow velocity in the lower half of the spiral tube and then contact the high-pressure surface below to circulate back and forth, through the pressure difference change The contact efficiency between the spiral tube with catalyst components and the raw liquid and hydrogen is further improved. The convergence accelerated cooling catalytic module and the hydrogen pre-cooling module are heat exchanged through the pad tube heat exchange system. Part of the hydrogen is separated into the hydrogen pre-cooling module through the adjustable separation module and then cooled and cached in the pressurized tank A1101. The cooled raw materials are converged downward in the reaction chamber 10 for hydrogenation reaction. The control system controls the injection of an appropriate amount of pre-cooled hydrogen into the bottom of the reaction chamber 10 for secondary heat exchange of the solvent according to the heat exchange prediction model and existing data. Part of the liquid solvent is refluxed upward to the feed atomization module through the liquid circulation module for re-atomization, and circulating heat exchange is carried out to control the temperature while preventing product crystallization from adhering to the inner wall of the reaction chamber 10. The maintenance personnel of the monitoring and management interactive platform monitor the heat exchange system through the mobile terminal, and the finished product is cached in the finished product tank 19 and then discharged through the discharge pump 1901.

Claims

1. A heat exchanger for hydrogenation reaction, comprising: The outer tank structure (1) and the operating tank structure (5) are characterized in that a safety protection module a and a safety protection module b are respectively provided inside the outer tank structure (1) and the operating tank structure (5), the safety protection module a and the safety protection module b comprising a sensor group and a reaction pipeline, the sensor group comprising a methanol sensor, a hydrogen sensor, a temperature sensor and an air pressure sensor, the reaction pipeline comprising an anti-solvent foam fire extinguishing agent pipeline and a carbon dioxide pipeline driven by a high-pressure pump; An operating tank structure (5), wherein the operating tank structure (5) is fixed to the inner side of the outer tank structure (1) by means of bolts, and a top cover (501) is connected to the top of the operating tank structure (5) by means of a flange; A unit host (21), the unit host (21) is installed on the right side of the outer tank structure (1) through a flange pipe at the left end, the end of the flange pipe at the left end of the unit host (21) extends to the inside of the operating tank structure (5), an environmental sensor is installed inside the flange pipe, the unit host (21) is connected to the lines of the safety protection module a and the safety protection module b through the flange pipe, the unit host (21) is connected to the monitoring and management interactive platform through wireless data, the monitoring and management interactive platform is connected to several groups of mobile terminal data, and a control system is set in the unit host (21); The top of the outer tank structure (1) is connected to a hemispherical head via a flange, the top of the hemispherical head at the top of the outer tank structure (1) is connected to a flange cover (101) via a flange, the top of the flange cover (101) is connected to a three-pronged pipe (102) via a flange, and the rear end of the three-pronged pipe (102) is connected to a secondary return pipe (1021) via a flange.

2. A heat exchanger for hydrogenation reaction according to claim 1, characterized in that: The front end of the flange cover (101) is connected to a soluble bulk drug liquid pipeline (2) via a flange, the front end of the soluble bulk drug liquid pipeline (2) is connected to a one-way valve a (1022) via a flange, the front end of the three-way pipe (102) is connected to a one-way valve b (1023) via a flange, a one-way valve c (1024) is provided at the connection between the secondary reflux pipe (1021) and the three-way pipe (102), a methanol raw material pipeline (3) is provided on the side of the three-way pipe (102), the top right end of the methanol raw material pipeline (3) is connected to a one-way valve d (301) via a flange, the right end of the one-way valve d (301) is connected to the left end of the three-way pipe (102) via a flange, and the flange A hydrogen raw material pipeline (4) is provided at the rear side of the cover (101), and a one-way valve e (401) is connected to the front end of the hydrogen raw material pipeline (4) through a flange. A feed atomization module is provided below the flange cover (101), and the feed atomization module includes an umbrella tube a (103) and an umbrella tube b (104). The umbrella tube a (103) is connected to the bottom of the three-pronged pipe (102) through a flange, and an ultrasonic nozzle (1031) is installed at the bottom of the umbrella tube a (103). The umbrella tube b (104) is connected to the bottom of the downward bend of the front end pipeline of the one-way valve e (401), and electric valves are respectively provided in the middle sections of the umbrella tube a (103) and the umbrella tube b (104).

3. A heat exchanger for hydrogenation reaction according to claim 1, characterized in that: It also includes an equipment space (6) and an acceleration chamber (7), wherein the equipment space (6) is arranged in the upper inner half of the working tank structure (5), and a hydrogen separation pre-cooling module is arranged inside the equipment space (6); The acceleration chamber (7) is an hourglass-shaped structure, consisting of a middle vertical pipe and tapered parts at its upper and lower ends. The equipment space (6) is located in the gap between the outside of the acceleration chamber (7) and the inside of the working tank structure (5). The acceleration chamber (7) includes an adjustable separation module and a convergence acceleration cooling catalytic module. The convergence acceleration cooling catalytic module includes the middle vertical pipe part of the acceleration chamber (7). The convergence acceleration cooling catalytic module also includes a nickel, palladium, and platinum alloy spiral tube (18). The nickel, palladium, and platinum alloy spiral tube (18) is a multi-layer structure. The cross section of the nickel, palladium, and platinum alloy spiral tube (18) is in the shape of an inverted water drop. Low-pressure drainage surfaces (1801) are provided on both sides of the bottom of the nickel, palladium, and platinum alloy spiral tube (18). Bridge bends (1802) are installed between the multiple layers of the nickel, palladium, and platinum alloy spiral tube (18) through the inner center and the outer edge.

4. A heat exchanger for hydrogenation reaction according to claim 3, characterized in that: The adjustable separation module comprises a conical ring cover (701), an adjustable cone frame (704) and a side pipe (705), wherein the conical ring cover (701) is fixedly connected to the inner side of the acceleration cabin (7), the outer curved surface of the conical ring cover (701) is fixedly connected to a plane bearing (702), a plurality of adjustment holes (703) are provided on the surface of the conical ring cover (701), the adjustable cone frame (704) is rotatably connected to the outer side of the conical ring cover (701), the top of the adjustable cone frame (704) is connected to the plane bearing (702), and the outer curved surface of the adjustable cone frame (704) is fixedly connected to a tooth portion (7041).

5. A heat exchanger for hydrogenation reaction according to claim 4, characterized in that: The side pipe (705) is fixedly connected to the right side of the vertical pipe in the middle section of the acceleration cabin (7). A C-shaped ring (706) is fixedly connected to the inner curved surface of the side pipe (705) in the vertical direction. A sleeve (707) is fixedly connected to the left side of the C-shaped ring (706) by bolts. A worm gear mechanism (708) is rotatably connected to the inner side of the sleeve (707). The turbine top of the worm gear mechanism (708) is coaxially connected to a transmission gear (709). The transmission gear (709) is meshed with the tooth portion (7041). The left and right sides of the flange blind plate at the right end of the sleeve (707) are connected to the transmission gear (709). A magnetic coupler (710) is provided on each side, the right end of the worm of the worm gear mechanism (708) is coaxially connected to the left half of the magnetic coupler (710), a steel frame is fixedly installed inside the equipment space (6), a servo motor is provided inside the steel frame, the servo motor shaft is coaxially connected to the right half of the magnetic coupler (710), the control circuit of the servo motor is connected to the unit main unit (21), and the vertical pipe in the middle section of the acceleration cabin (7) and the tapered parts at the upper and lower ends thereof are equidistantly installed on the inner surface with a temperature sensor and a pressure sensor connected to the unit main unit (21).

6. A heat exchanger for hydrogenation reaction according to claim 3, characterized in that: The hydrogen separation precooling module includes a separation tank (8), which is connected to the right side of the vertical pipe in the middle section of the acceleration cabin (7) through a flange, and the left end of the separation tank (8) is connected to a bent cone pipe (801) through a flange, and the separation tank (8) is fixedly connected to a gas distribution pipe (802) inside, and the right end of the gas distribution pipe (802) is fixedly connected to a horizontal branch pipe, and the inner curved surface of the separation tank (8) is provided with a spiral guide plate, and the horizontal inclination angle of the spiral guide plate gradually increases from top to bottom. A condensation screen (803) is fixedly connected to the side of the separation tank (8), a connecting pipe (804) is connected to the front side of the separation tank (8) through a flange, the rear end of the connecting pipe (804) is at the same height as the flange connection between the separation tank (8) and the bent conical pipe (801), a through hole is opened in the conical portion at the lower end of the acceleration chamber (7), a negative pressure pipe (8041) is connected to the front lower part of the connecting pipe (804) through a flange, and the negative pressure pipe (8041) is connected to the through hole opened in the conical portion at the lower end of the acceleration chamber (7) through a flange.

7. A heat exchanger for hydrogenation reaction according to claim 6, characterized in that: It also includes a double-head pump (9), which is installed in the equipment space (6), the working chamber inlet at the front end of the double-head pump (9) is connected to the bottom end of the separation tank (8) through a flange, and the bottom of the secondary return pipe (1021) is connected to the working chamber outlet at the rear end of the double-head pump (9); A reaction chamber (10), wherein the reaction chamber (10) is connected to the inner side of the working tank structure (5) via a flange, the reaction chamber (10) is located below the acceleration chamber (7), a hexagonal frame (1001) is installed on the inner side of the reaction chamber (10), a liquid circulation module is provided at the bottom of the reaction chamber (10), the liquid circulation module includes a circulation pipe (1002), the circulation pipe (1002) is provided at the bottom of the reaction chamber (10) via a flange connection, the working chamber inlet at the rear end of the double-head pump (9) is connected to the top end of the circulation pipe (1002), and a temperature sensor and a radar-type liquid volume sensor connected to the circuit of the unit host (21) are installed at the inner bottom of the reaction chamber (10); a liquid return pipe (11), the liquid return pipe (11) being mounted on the outside of the hexagonal frame (1001) via a clamp, the top of the liquid return pipe (11) being connected to the exhaust pipe of the pressurized tank A (1101) via a flange, the pressurized tank A (1101) being located inside the equipment space (6), the exhaust pipe of the pressurized tank A (1101) being installed with a pressure sensor and a control valve, the rear side of the pressurized tank A (1101) being connected to an air intake pipe with a one-way valve, the air intake pipe of the pressurized tank A (1101) being connected to the outlet of the working chamber at the front end of the double-head pump (9); A vertical air pipe (12) is installed in the middle of the hexagonal frame (1001) through a clamp, the top of the vertical air pipe (12) is connected to the pressure tank B (1201) through a discharge pipe with a pressure sensor and a control valve, the pressure tank B (1201) is provided inside the equipment space (6), and the bottom of the vertical air pipe (12) is connected to a plurality of groups of sieve tubes (1202).

8. A heat exchanger for hydrogenation reaction according to claim 7, characterized in that: It also includes a gasket heat exchange system, which is arranged inside the working tank structure (5). The gasket heat exchange system includes a heat exchange box a (13) and a heat exchange box b (17). The heat exchange box a (13) and the heat exchange box b (17) are respectively installed on the left and right sides of the equipment space (6). The working cavity outlet at the front end of the double-head pump (9) is connected to the pipeline of the heat box a (13). Two sets of line cabins (1301) are installed on the upper and lower sides of the heat exchange box a (13). The heat exchange box a (13) and the heat exchange box b (17) are provided with pipeline area compensation monitoring modules. The pipeline area compensation monitoring module includes a plurality of groups of monitoring control tubes (1302), which are fixedly installed at equal intervals on the surface of the circuit cabin (1301), the cross section of the monitoring control tube (1302) is a regular hexagon, the vertical surface of the monitoring control tube (1302) is provided with a square hole (1303), the inner side of the monitoring control tube (1302) is provided with a circuit tube (1304), the interior of the square hole (1303) is provided with a temperature and humidity sensor (1305) and a semiconductor refrigeration plate (1306), and the bottom and left side of the heat exchange box a (13) are connected to the top of the pressurized tank B (1201) and the horizontal branch pipe at the right end of the gas distribution pipe (802) respectively; The gasket heat exchange system further comprises a vertical hexagonal tube a (14), a vertical hexagonal tube b (15) and a vertical hexagonal tube c (16) nested with each other, wherein the vertical hexagonal tube a (14), the vertical hexagonal tube b (15) and the vertical hexagonal tube c (16) are provided with chamfers at their upper and lower ends, and the left and right sides of the end of the vertical hexagonal tube b (15) are symmetrically provided with fitting inclined surfaces a (1501), and the left and right sides of the end of the vertical hexagonal tube c (16) are symmetrically provided with fitting inclined surfaces a (1501). Two sets of asymmetric fitting inclined surfaces b (1601) are respectively provided, and the vertical hexagonal tube a (14), the vertical hexagonal tube b (15) and the vertical hexagonal tube c (16) are vertically slidably nested with each other, and a hexagonal space (1307) is provided between the vertical hexagonal tube a (14), the vertical hexagonal tube b (15) and the vertical hexagonal tube c (16), and the monitoring control tube (1302) is slidably connected to the inner side of the hexagonal space (1307).

9. A heat exchanger for hydrogenation reaction according to claim 8, characterized in that: It also includes a finished product tank (19), the finished product tank (19) is located inside the operating tank structure (5), the top of the finished product tank (19) is connected to the top of the reaction chamber (10) through a pipeline with a control valve and an air pressure sensor, the bottom of the finished product tank (19) is connected to a discharge pump (1901) connected to the control circuit of the unit main unit (21) through a flange, and the pump body outlet of the discharge pump (1901) is connected to the finished product pipe (20) through a flange; Two groups of external machines (22), the two groups of external machines (22) are arranged on the rear side of the outer tank structure (1), the two groups of external machines (22) are respectively connected to the heat exchange box a (13) and the heat exchange box b (17) through pipelines, and the control circuits of the two groups of external machines (22) are connected to the unit host (21).

10. A heat exchanger system for hydrogenation reaction, characterized in that: The invention comprises a heat exchanger for hydrogenation reaction as described in any one of claims 1 to 9, and also comprises a monitoring and management interactive platform and a mobile terminal. Temperature, pressure, catalyst concentration, flow rate, pH value, and product chromatographic purity sensors are also installed in the pipelines and containers of each device of the heat exchanger. The monitoring and management interactive platform is used to collect and summarize the real-time data of the unit host (21) of each heat exchanger through a network protocol to establish a database. The mobile terminal is used to connect to the monitoring and management interactive platform data in real time. The monitoring and management interactive platform is connected to the data of several unit hosts (21) for maintenance personnel to monitor the equipment data and make feedback instructions based on the data information. The database stores the temperature, pressure, catalyst concentration, flow rate, pH value, product chromatographic purity and other data extracted by sensors of multiple groups of internal devices of the heat exchanger. The monitoring and management interactive platform also comprises a heat exchange efficiency prediction module. A heat exchange prediction model is obtained based on equipment data training. The heat exchange prediction module is used to integrate the monitoring data in each device of the heat exchanger into the heat exchange prediction model and dynamically adjust the hydrogenation temperature based on the XGBoost / LightGBM model.

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