Ether after carbon four raw material pretreatment device and method thereof

Abstract

The present application relates to the technical field of chemical raw material pretreatment and automatic control, in particular to an ether post-C4 raw material pretreatment device and method thereof, which comprises a pre-stabilization tank, a slow mixing drum, a layered drum, a protective filter drum, a double drying drum, a finished product buffer tank and a parameter detection and control unit; the system core is to set upper, middle and lower density pressure tapping ports at different heights on the side wall of the layered drum to detect the static pressure of multiple layers, convert the phase change into pressure gradient characteristics, and dynamically adjust the flow proportion of the variable shear mixing section in the slow mixing drum according to the static pressure signal; the present application effectively solves the problem that the conventional liquid level meter is easily interfered by the emulsion layer and fails to judge, can accurately distinguish between thick emulsion layer and real water layer, reduces the probability of misdischarge of target material, and at the same time inhibits the thickening of the emulsion layer and maintains the stability of the liquid phase.

Description

Technical Field

[0001] This invention relates to the field of chemical raw material pretreatment and automatic control technology, specifically to a device and method for pretreatment of C4 raw materials after etherification. Background Technology

[0002] In the purification and pretreatment process of post-etherification C4 feedstock, the separation and purification unit is fundamental to ensuring the stable operation of subsequent processes. Existing pretreatment schemes generally employ series-connected physical purification equipment, using conventional level gauges and fixed parameter thresholds to control liquid-liquid separation and drying / dehydration operations. Although this scheme has a certain separation capability under stable operating conditions, its high dependence on fixed threshold control and limited physical state detection methods make it highly susceptible to local flash evaporation and emulsion layer thickening when faced with dynamic fluctuations in feedstock composition, temperature, and pressure. Furthermore, conventional level measurements are easily affected by changes in emulsion layer thickness, often leading to inaccurate identification of the true interface and mis-discharge of materials. Moreover, existing drying bed monitoring relies solely on total pressure difference, failing to effectively distinguish between adsorbent capacity decay and fluid deviation. The multiphase characteristics within the fluid are often unmeasurable in dynamic continuous flow systems, resulting in rapid degradation of purification efficiency and delayed system control response.

[0003] Therefore, improving the accuracy of multiphase interface identification and the timeliness of dynamic physical control during the separation and pretreatment of C4 feedstock after etherification has become an urgent technical problem to be solved. Summary of the Invention

[0004] To solve the above-mentioned technical problems, the present invention provides a device and method for pretreatment of C4 feedstock after etherification. Specifically, the technical solution of the present invention is as follows: A post-etherification C4 feedstock pretreatment device, comprising: Pre-stabilizing tank, slow mixing tank, stratification tank, protective filter tank, finished product buffer tank and double drying tank; The dual drying cylinder includes a first drying cylinder and a second drying cylinder arranged in parallel, with a pressure equalization pipe connected between them, equipped with a pressure equalization valve; The feed inlet of the pre-stabilizing tank is connected to the upstream raw material pipeline, and its bottom liquid outlet is connected to the finished product buffer tank via a slow mixing cylinder, a stratification cylinder, a protective filter cylinder, a first drying cylinder, and a second drying cylinder. The slow mixing cylinder is equipped with a guide core, a variable shear mixing section, and a vortex reduction and settling section along the flow direction. The layered cylinder consists of a primary coalescing layer, a low-disturbance deceleration chamber, and a secondary coalescing layer from top to bottom; the device includes control valves and electrical connections, as well as a control unit and parameter detection unit. The control unit is connected to the control valves on the pre-stabilizing tank, slow mixing tank, stratification tank, protective filter tank, and dual drying tank; The parameter detection unit converts the detected operating parameters into signals and transmits them to the control unit to control the valve; The parameter detection unit includes upper density pressure taps, middle density pressure taps, and lower density pressure taps on the side wall of the layered cylinder, inlet pressure taps, middle pressure taps, and outlet pressure taps on the protective filter cylinder, and upper, middle, and lower pressure taps on the outer walls of the first and second drying cylinders.

[0005] In some embodiments, the parameter detection unit is a density detection unit. The density detection unit detects the static pressure at different heights inside the layered cylinder, converts it into a corresponding static pressure signal, and then transmits it to the control unit. The control unit controls the control valve according to the static pressure signal. The upper density tap is located above the primary coalescing layer, the middle density tap is located between the primary coalescing layer and the secondary coalescing layer, and the lower density tap is located below the secondary coalescing layer.

[0006] In some embodiments, the variable shear mixing section is composed of a first spiral blade, a second spiral blade, and a third spiral blade. The blade twist angle of the first spiral blade is smaller than that of the second spiral blade, and the blade twist angle of the third spiral blade is smaller than that of the second spiral blade. The first spiral blade, the second spiral blade, and the third spiral blade all have straight tube slow-release sections without internal obstructions. The protective filter cartridge has an inlet distribution cap, a coarse filter basket, a fine filter cartridge, and an outlet collection chamber arranged sequentially from top to bottom. An annular buffer volume is provided between the coarse filter basket and the fine filter cartridge.

[0007] In some embodiments, the interior of both the first drying cylinder and the second drying cylinder is arranged from top to bottom as follows: an upper distribution plate, a main adsorption layer, a buffer inert layer, a support grid plate, and a bottom confluence cone; the upper pressure tap is located on the upper part of the main adsorption layer, the middle pressure tap is located in the middle of the main adsorption layer, and the lower pressure tap is located above the buffer inert layer.

[0008] A control method for a post-etherification C4 feedstock pretreatment device includes the following steps: S1. Obtain the operating parameters of the C4 raw material pretreatment device after etherification. The operating parameters include the static pressure parameters at different heights in the layered cylinder, as well as the multi-stage differential pressure parameters of the protective filter cylinder and the double drying cylinder. S2. Compare the operating parameters with preset parameter thresholds; generate corresponding control signals based on the comparison results; S3. Based on the control signal, control the opening and closing of the corresponding control valve, dynamically adjust the flow rate ratio of the variable shear mixing section, the liquid phase pulse emission cycle or the switching state of the dual drying cylinder, or generate cleaning and replacement prompts.

[0009] In some embodiments, obtaining the operating parameters of the post-ether C4 feedstock pretreatment device includes: obtaining the static pressure signals corresponding to the upper density tap, the middle density tap, and the lower density tap; comparing the operating parameters with preset parameter thresholds includes: calculating the first static pressure difference between the upper and middle density taps and the second static pressure difference between the middle and lower density taps, determining whether the ratio of the first static pressure difference to the second static pressure difference is within a preset smoothing range, determining whether the static pressure change rate corresponding to the middle density tap is lower than a preset fluctuation threshold, and determining whether the difference between the real-time static pressure corresponding to the lower density tap and the reference drainage boundary static pressure exceeds a preset static pressure increment threshold. The step of generating corresponding control signals based on the comparison results includes: generating a normal stratification control signal when the static pressure difference changes smoothly in the order of liquid density; generating an emulsification control signal when the static pressure change rate corresponding to the medium density pressure tap is lower than a preset fluctuation threshold; and generating a restricted pulse emission control signal when the real-time static pressure corresponding to the lower density pressure tap exceeds a preset static pressure increment threshold. The step of controlling the opening and closing of the control valve according to the control signal includes: controlling the maintenance of the current flow rate ratio of the variable shear mixing section according to the normal stratification control signal; controlling the reduction of the flow rate ratio of the variable shear mixing section according to the emulsification control signal; and controlling the transition to restricted pulse emission according to the restricted pulse emission control signal.

[0010] In some embodiments, obtaining the operating parameters of the C4 feedstock pretreatment device after etherification includes: obtaining the total pressure difference and drainage frequency of the layered cylinder; comparing the operating parameters with preset parameter thresholds includes: determining that the total pressure difference is greater than, equal to or less than a preset pressure difference threshold, and determining that the drainage frequency is greater than, equal to or less than a preset frequency threshold. The step of generating a corresponding control signal based on the comparison result includes: generating a mismatch control signal when the total pressure difference is greater than or equal to the preset pressure difference threshold and the drainage frequency is less than the preset frequency threshold; and generating a high-efficiency coalescence control signal when the total pressure difference is less than the preset pressure difference threshold and the drainage frequency is greater than or equal to the preset frequency threshold. When the total pressure difference is greater than or equal to the preset pressure difference threshold and the drainage frequency is greater than or equal to the preset frequency threshold, or when the total pressure difference is less than the preset pressure difference threshold and the drainage frequency is less than the preset frequency threshold, the current operating state is maintained; the step of controlling the opening and closing of the control valve according to the control signal includes: controlling the reduction of the total flow rate and the reduction of the flow ratio of the variable shear mixing section according to the mismatch control signal; and controlling the increase of the total flow rate according to the high-efficiency coalescence control signal.

[0011] In some embodiments, obtaining the operating parameters of the C4 feedstock pretreatment device after etherification includes: obtaining the rate of change of the flow resistance coefficient from the inlet-side pressure tap to the intermediate-side pressure tap, and the rate of change of the flow resistance coefficient from the intermediate-side pressure tap to the outlet-side pressure tap. The step of comparing the operating parameters with preset parameter thresholds includes: determining that the rate of change of the front-end flow resistance coefficient is greater than, equal to or less than the rate of change of the rear-end flow resistance coefficient; the step of generating a corresponding control signal based on the comparison result includes: generating a particle trapping control signal when the rate of change of the front-end flow resistance coefficient is greater than or equal to the rate of change of the rear-end flow resistance coefficient. When the rate of change of the flow resistance coefficient in the front section is less than the rate of change of the flow resistance coefficient in the rear section, a microdroplet penetration control signal is generated; the step of controlling the opening and closing of the control valve according to the control signal includes: controlling and adjusting the working state of the stratification cylinder according to the microdroplet penetration control signal; and generating a prompt for cleaning or replacing the coarse filter basket according to the particle retention control signal.

[0012] In some embodiments, obtaining the operating parameters of the C4 feedstock pretreatment device after etherification includes: obtaining the pressure difference percentages corresponding to the upper pressure tap, the middle pressure tap, and the lower pressure tap of the first drying cylinder and the second drying cylinder; comparing the operating parameters with preset parameter thresholds includes: determining that the middle pressure difference percentage corresponding to the middle pressure tap is greater than, equal to, or less than a preset middle percentage threshold, and determining that the lower pressure difference percentage corresponding to the lower pressure tap is greater than, equal to, or less than a preset lower percentage threshold. The step of generating a corresponding control signal based on the comparison result includes: generating a load reduction control signal when the proportion of the middle section pressure difference is greater than or equal to the preset middle section proportion threshold; and generating a switching control signal when the proportion of the lower section pressure difference is greater than or equal to the preset lower section proportion threshold. The step of controlling the opening and closing of the control valve according to the control signal includes: controlling the reduction of the flow rate shared by the corresponding drying cylinder according to the load reduction control signal; and controlling the switch to the standby drying cylinder in advance and controlling the pressure equalization valve to open according to the switching control signal.

[0013] In some embodiments, the control to switch to the standby drying cylinder in advance includes: controlling the inlet valve of the drying cylinder to be put into operation to open and the outlet valve to close for pre-filling; controlling the equalizing valve to open so that the top pressures of the first drying cylinder and the second drying cylinder gradually approach each other; controlling the outlet valve of the drying cylinder to be put into operation to open and gradually increasing the opening of the inlet valve for segmented flow connection. Determine whether the differential pressure development sequence of the drying cylinder to be put into operation is consistent with or inconsistent with the preset reference timing characteristics; if the differential pressure development sequence is consistent with the preset reference timing characteristics, control the inlet valve of the drying cylinder to be taken out of operation to reduce its opening first, and control its outlet valve to reduce its opening to complete the unloading at the tail end; if the differential pressure development sequence is inconsistent with the preset reference timing characteristics, stop the switching.

[0014] The present invention has the following beneficial effects: 1. This invention detects multi-layer static pressure by setting upper, middle, and lower density pressure taps at different heights on the side wall of the layered cylinder, converting phase changes into pressure gradient characteristics. This design effectively solves the problem in the background technology where conventional level gauges are easily affected by emulsion layers and fail to make judgments. It can accurately distinguish between thick emulsion layers and real water layers, reducing the probability of mis-discharge of target materials. At the same time, the system can dynamically adjust the flow rate ratio of the variable shear mixing section according to the static pressure signal, suppressing the thickening of the emulsion layer and maintaining the stability of the liquid phase.

[0015] 2. This invention sets multiple pressure taps on the protective filter cartridge and the dual drying cartridge respectively. By monitoring the rate of pressure drop change and the percentage of pressure difference in different sections, a resistance characteristic with spatial resolution is formed. This solution overcomes the defect of the prior art that cannot distinguish the type of equipment failure by relying solely on the total pressure difference. It can effectively identify the retention of solid particles and droplet penetration in the filter cartridge, as well as the capacity decay and fluid deviation in the drying bed, thereby triggering load reduction or early switching operations in a timely manner and improving the accuracy of dynamic control of the system. Attached Figure Description

[0016] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. In the drawings: Figure 1 This is a schematic diagram of the overall structure of the device; Figure 2 This is a schematic diagram of the overall elevation structure of the device; Figure 3 This is a schematic diagram of the internal structure of the device's slow mixing cylinder, stratification cylinder, and protective filter cylinder; Figure 4 This is a schematic diagram of the device's flow guide core and variable shear mixing section. Figure 5 This is a schematic diagram of the structure of the first spiral plate, the second spiral plate, and the third spiral plate of the device; Figure 6 This is a flowchart of the method of the present invention.

[0017] In the diagram: 1. Pre-stabilizing tank; 2. Slow mixing cylinder; 3. Layering cylinder; 4. Protective filter cylinder; 5. Finished product buffer tank; 6. First drying cylinder; 7. Second drying cylinder; 8. Pressure equalization pipe; 9. Pressure equalization valve; 10. Guide core; 11. Variable shear mixing section; 12. Anti-swirl settling section; 13. Primary coalescing layer; 14. Low-disturbance deceleration chamber; 15. Secondary coalescing layer; 16. Upper density pressure tap; 17. Middle density pressure tap; 18. Lower density pressure tap; 19. Inlet side pressure tap; 20. Middle side pressure tap; 21. Outlet side pressure tap; 22. First spiral vane; 23. Second spiral vane; 24. Third spiral vane; 25. Inlet distribution cap; 26. Coarse filter basket; 27. Fine filter cylinder; 28. Liquid collection chamber; 29. ​​Annular buffer volume; 30. Double drying cylinder. Detailed Implementation

[0018] To enable those skilled in the art to better understand the present invention, 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. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort should fall within the scope of protection of the present invention.

[0019] Example 1: Combination Figure 1 and Figure 2 As shown, a post-etherification C4 feedstock pretreatment device includes: Pre-stabilizing tank 1, slow mixing tank 2, stratification tank 3, protective filter tank 4, finished product buffer tank 5, and double drying tank 30; The double drying cylinder 30 includes a first drying cylinder 6 and a second drying cylinder 7 arranged in parallel, with a pressure equalization pipe 8 connected between them and equipped with a pressure equalization valve 9; The inlet of the pre-stabilizing tank 1 is connected to the upstream raw material pipeline, and its bottom outlet is connected to the finished product buffer tank 5 via the slow mixing cylinder 2, the stratification cylinder 3, the protective filter cylinder 4, the first drying cylinder 6, and the second drying cylinder 7. like Figure 3 As shown, the slow mixing cylinder 2 is provided with a guide core 10, a variable shear mixing section 11, and a vortex-reducing settling section 12 along the material flow direction. The layered cylinder 3 is provided with a primary coalescing layer 13, a low-disturbance deceleration chamber 14, and a secondary coalescing layer 15 from top to bottom; the device includes control valves and electrical connection control units and parameter detection units; The control unit is connected to the control valves on the pre-stabilizing tank 1, the slow mixing tank 2, the stratification tank 3, the protective filter tank 4, and the double drying tank 30; The parameter detection unit converts the detected operating parameters into signals and transmits them to the control unit to control the valve; The parameter detection unit includes an upper density pressure tap 16, a middle density pressure tap 17, and a lower density pressure tap 18 on the side wall of the layered cylinder 3; an inlet side pressure tap 19, a middle side pressure tap 20, and an outlet side pressure tap 21 on the protective filter cylinder 4; and upper, middle, and lower pressure taps on the outer walls of the first drying cylinder 6 and the second drying cylinder 7.

[0020] Existing technologies for processing post-etherified C4 raw materials mostly rely on physical purification units connected in series with fixed thresholds. When the composition, temperature, and pressure of the raw materials fluctuate, problems such as local flash evaporation and thickening of the emulsion layer can easily occur. To solve this problem, this embodiment proposes a pretreatment device for post-etherified C4 raw materials. The device includes a pre-stabilizing tank 1, a slow mixing tank 2, a layering tank 3, a protective filter tank 4, a double drying tank 30, and a finished product buffer tank 5. The dual drying cylinder 30 includes a first drying cylinder 6 and a second drying cylinder 7 arranged in parallel. A pressure equalization pipe 8 is connected between the first drying cylinder 6 and the second drying cylinder 7, and a pressure equalization valve 9 is installed on the pressure equalization pipe 8. The inlet of the pre-stabilizing tank 1 is connected to the upstream raw material pipeline. The bottom outlet of the pre-stabilizing tank 1 is connected to the inlet of the slow mixing cylinder 2. The outlet of the slow mixing cylinder 2 is connected to the inlet of the stratification cylinder 3. The outlet of the stratification cylinder 3 is connected to the inlet of the protective filter cylinder 4. The outlet of the protective filter cylinder 4 is connected to the inlet of the first drying cylinder 6 and the second drying cylinder 7. The outlets of the first drying cylinder 6 and the second drying cylinder 7 are connected to the inlet of the finished product buffer tank 5. The slow mixing cylinder 2 is arranged with a guide core 10, a variable shear mixing section 11, and a vortex reduction and settling section 12 in sequence along the flow direction. The layered cylinder 3 is arranged with a primary coalescing layer 13, a low-disturbance deceleration chamber 14, and a secondary coalescing layer 15 in sequence from top to bottom. The device also includes control valves, an electrical control unit, and a parameter detection unit. The control unit is electrically connected to the control valves on the pre-stabilizing tank 1, the slow mixing cylinder 2, the layered cylinder 3, the protective filter cylinder 4, and the dual drying cylinder 30, respectively. The parameter detection unit is used to detect the working parameters of the C4 raw material pretreatment device after etherification, convert them into corresponding detection signals, and transmit them to the control unit. The control unit controls the control valves according to the received detection signals. The parameter detection unit includes an upper density pressure tap 16, a middle density pressure tap 17 and a lower density pressure tap 18 disposed on the side wall of the layered cylinder 3, an inlet side pressure tap 19, a middle side pressure tap 20 and an outlet side pressure tap 21 disposed on the protective filter cylinder 4, and an upper section pressure tap, a middle section pressure tap and a lower section pressure tap disposed on the outer wall of the first drying cylinder 6 and the second drying cylinder 7. Through the above structural arrangement, mixing enhancement and demulsification are sequentially separated and processed in the same flow channel. By utilizing the multi-stage pressure tapping structure of the layered cylinder 3, the protective filter cylinder 4, and the double drying cylinder 30, the phase and flow state changes are transformed into measurable pressure gradient characteristics, laying a physical basis for subsequent dynamic control.

[0021] The parameter detection unit is a density detection unit. The density detection unit detects the static pressure at different heights inside the layered cylinder 3, converts it into a corresponding static pressure signal, and then transmits it to the control unit. The control unit adjusts and controls the valve according to the static pressure signal. Among them, the upper density pressure tap 16 is located above the primary coalescing layer 13, the middle density pressure tap 17 is located between the primary coalescing layer 13 and the secondary coalescing layer 15, and the lower density pressure tap 18 is located below the secondary coalescing layer 15.

[0022] In the liquid-liquid separation process of C4 after etherification, the change in the thickness of the emulsion layer often causes the interface judgment of conventional level gauges to fail. In order to accurately identify the true stratification state, the parameter detection unit is a density detection unit. The density detection unit detects the static pressure at different heights in the stratification cylinder 3, converts it into the corresponding static pressure signal, and then transmits it to the control unit. The control unit adjusts the control valve according to the static pressure signal. The upper density pressure tap 16 is located above the primary coalescing layer 13, the middle density pressure tap 17 is located between the primary coalescing layer 13 and the secondary coalescing layer 15, and the lower density pressure tap 18 is located below the secondary coalescing layer 15. This spatial distribution means that the static pressure corresponding to the upper density pressure tap 16 represents the characteristics of the main flow zone, the static pressure corresponding to the middle density pressure tap 17 represents the characteristics of the emulsification-prone zone, and the static pressure corresponding to the lower density pressure tap 18 represents the characteristics of the aqueous phase enrichment zone. By transforming a single liquid level measurement into a multi-layer static pressure gradient measurement, it is possible to distinguish between thick emulsion layers and real water layers, reducing the probability of misclassifying emulsion layers as water layers and causing incorrect C4 discharge. This ability to distinguish between different phases stems from the characterization of density differences in the static pressure gradient: in the true stratified state, the static pressure difference between adjacent pressure taps is determined by the product of the average density of the fluid in that interval and the height difference. The pure C4 layer and the pure water layer correspond to their respective characteristic static pressure difference values, and there is a measurable difference between the two. The density of the emulsion layer is between that of C4 and water and varies with the degree of emulsification. When the emulsion layer covers the density tap 17, the two static pressure differences formed by the tap and the upper and lower taps will deviate from their respective pure phase characteristic values ​​at the same time, and the direction of deviation is consistent. By monitoring this synchronous deviation characteristic, the existence of the emulsion layer and its coverage range can be determined. It should be noted that in a continuous flow environment, the dynamic pressure and turbulent fluctuations of the fluid can disrupt the above-mentioned ideal static assumption of hydrostatic pressure. To eliminate dynamic interference, this embodiment uses a low-disturbance deceleration cavity 14 to reduce the local flow velocity in terms of physical structure, making the dynamic pressure component much smaller than the static pressure component. In terms of algorithm logic, the density detection unit performs a moving average filter on the collected instantaneous pressure signal to filter out the periodic fluctuations caused by the upstream pump pulsation, thereby extracting the true static pressure signal. The control unit has a pre-stored reference static pressure difference corresponding to pure C4 obtained through calibration, as well as a pure water characteristic static pressure difference; specifically, the quantitative calculation is as follows: when the C4 layer is pure, the static pressure difference between the upper and middle pressure taps is stable at the reference static pressure difference. When the emulsion covers the medium density pressure tap 17, due to the increase in the average density of the emulsion, the static pressure difference between the upper density pressure tap 16 and the medium density pressure tap 17 deviates from the reference static pressure difference and approaches the characteristic static pressure difference of pure water. The system can accurately quantify the degree of emulsification by identifying the deviation amplitude, thus overcoming the technical defect that the internal state is unmeasurable when conventional hydrodynamic formulas are applied to dynamic continuous flow systems.

[0023] like Figure 4 and Figure 5 As shown, the variable shear mixing section 11 is composed of a first spiral blade 22, a second spiral blade 23, and a third spiral blade 24. The blade twist angle of the first spiral blade 22 is smaller than that of the second spiral blade 23, and the blade twist angle of the third spiral blade 24 is smaller than that of the second spiral blade 23. The first spiral blade 22, the second spiral blade 23, and the third spiral blade 24 all have straight tube slow-release sections without internal obstructions. The inside of the protective filter cartridge 4 is arranged from top to bottom as follows: an inlet distribution cap 25, a coarse filter basket 26, a fine filter cartridge 27, and an outlet collection chamber 28. An annular buffer volume 29 is left between the coarse filter basket 26 and the fine filter cartridge 27.

[0024] To achieve a balance between mass transfer enhancement and emulsification inhibition within the same flow channel, the variable shear mixing section 11 is composed of a first helical blade 22, a second helical blade 23, and a third helical blade 24. The blade twist angle of the first helical blade 22 is smaller than that of the second helical blade 23, and the blade twist angle of the third helical blade 24 is smaller than that of the second helical blade 23. The first helical blade 22, the second helical blade 23, and the third helical blade 24 all have straight tube slow-release sections without internal obstructions. When the fluid passes through the first spiral vane 22 and the second spiral vane 23, the interfacial stretching enhances mass transfer. When it passes through the third spiral vane 24, the swirling flow weakens, causing droplets to coalesce. The filter cartridge 4 is protected by an inlet distribution cap 25, a coarse filter basket 26, a fine filter cartridge 27, and an outlet collection chamber 28 arranged sequentially from top to bottom. An annular buffer volume 29 is left between the coarse filter basket 26 and the fine filter cartridge 27. This structure prevents the occasional microdroplets and fine powder carried out from the front stage from directly impacting the surface of the fine filter cartridge 27. The flow resistance changes in the coarse and fine filtration sections can be characterized independently, providing a structural basis for distinguishing between particle retention and microdroplet penetration.

[0025] The interior of both the first drying cylinder 6 and the second drying cylinder 7 is arranged from top to bottom as follows: an upper distribution plate, a main adsorption layer, a buffer inert layer, a support grid plate, and a bottom confluence cone; the upper pressure tap is located on the upper part of the main adsorption layer, the middle pressure tap is located in the middle of the main adsorption layer, and the lower pressure tap is located above the buffer inert layer.

[0026] To identify the failure type of the drying bed, the interior of both the first drying cylinder 6 and the second drying cylinder 7 is arranged from top to bottom as follows: an upper distribution plate, a main adsorption layer, a buffer inert layer, a support grid plate, and a bottom confluence cone; the upper pressure tap is located above the main adsorption layer, the middle pressure tap is located in the middle of the main adsorption layer, and the lower pressure tap is located above the buffer inert layer. Existing technologies rely on total pressure difference to determine bed condition, which cannot distinguish between capacity decay and fluid deviation. By dividing the bed into three pressure tapping zones along the material flow direction, the accumulation and blockage of microdroplets at the inlet end, capacity decay in the middle of the bed, and rearrangement of the flow channel at the bottom are manifested as changes in the pressure difference ratio of different zones, forming a bed resistance characteristic with spatial resolution.

[0027] Example 2: Combination Figure 6 As shown, a control method for a post-etherification C4 feedstock pretreatment device includes the following steps: S1. Obtain the operating parameters of the C4 raw material pretreatment device after etherification. The operating parameters include the static pressure parameters at different heights in the layered cylinder, as well as the multi-stage differential pressure parameters of the protective filter cylinder and the double drying cylinder. S2. Compare the operating parameters with preset parameter thresholds; generate the corresponding control signal based on the comparison result; S3. Based on the control signal, control the opening and closing of the corresponding control valve, dynamically adjust the flow rate ratio of the variable shear mixing section, the liquid phase pulse emission cycle or the switching status of the dual drying cylinder, or generate cleaning and replacement prompts.

[0028] To address the issue of purification efficiency degradation caused by raw material fluctuations, a control method for a post-etherification C4 raw material pretreatment device is proposed. This method involves acquiring the operating parameters of the device, comparing these parameters with preset threshold values, generating corresponding control signals based on the comparison results, and controlling the opening and closing of control valves according to these signals to dynamically adjust the flow rate ratio of the variable shear mixing section, the liquid phase pulse emission cycle, or the switching state of the dual drying cylinders. This method utilizes the characteristic parameters of each treatment unit to dynamically adjust fluid distribution and operating cycle, maintaining liquid phase stability and suppressing efficiency degradation.

[0029] The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the static pressure signals corresponding to the upper density pressure tap 16, the middle density pressure tap 17 and the lower density pressure tap 18; The working parameters are compared with preset parameter thresholds, including: calculating the first static pressure difference between the upper density pressure tap 16 and the middle density pressure tap 17, and the second static pressure difference between the middle density pressure tap 17 and the lower density pressure tap 18; determining whether the ratio of the first static pressure difference to the second static pressure difference is within a preset smoothing range; determining whether the static pressure change rate corresponding to the middle density pressure tap 17 is lower than a preset fluctuation threshold; and determining whether the difference between the real-time static pressure corresponding to the lower density pressure tap 18 and the benchmark drainage boundary static pressure exceeds a preset static pressure increment threshold. Based on the comparison results, corresponding control signals are generated, including: generating a normal stratification control signal when the static pressure difference changes smoothly according to the liquid density sequence; generating an emulsification control signal when the static pressure change rate corresponding to the medium density pressure tap 17 is lower than the preset fluctuation threshold; and generating a restricted pulse emission control signal when the real-time static pressure corresponding to the lower density pressure tap 18 exceeds the preset static pressure increment threshold. Based on the control signals, the opening and closing of the control valves are controlled, including: based on the normal stratification control signal, maintaining the current flow ratio of the variable shear mixing section; based on the emulsification control signal, reducing the flow ratio of the variable shear mixing section 11; and based on the restricted pulse emission control signal, switching to restricted pulse emission.

[0030] Determine whether the static pressure difference between the upper density pressure tap 16, the middle density pressure tap 17 and the lower density pressure tap 18 changes smoothly in the order of liquid density; determine whether the static pressure change rate corresponding to the middle density pressure tap 17 is lower than the preset fluctuation threshold; and determine whether the difference between the real-time static pressure corresponding to the lower density pressure tap 18 and the benchmark drainage boundary static pressure exceeds the preset static pressure increment threshold. When the static pressure difference changes smoothly according to the liquid density sequence, a normal stratification control signal is generated; when the static pressure change rate corresponding to the medium density pressure tap 17 is lower than the preset fluctuation threshold, an emulsification control signal is generated; when the difference between the real-time static pressure corresponding to the lower density pressure tap 18 and the reference drainage boundary static pressure exceeds the preset static pressure increment threshold, a restricted pulse discharge control signal is generated; based on the normal stratification control signal, the flow rate ratio of the current variable shear mixing section is maintained; based on the emulsification control signal, the flow rate ratio of the variable shear mixing section 11 is reduced; based on the restricted pulse discharge control signal, the system switches to restricted pulse discharge. The actual interface location is determined by multi-layer pressure characteristics. The specific determination logic is as follows: The input source is the static pressure signal collected in real time from three density pressure taps; Step 1: Calculate the first static pressure difference between the upper density pressure tap 16 and the middle density pressure tap 17, and the second static pressure difference between the middle density pressure tap 17 and the lower density pressure tap 18. Step 2: Compare the ratio of the first static pressure difference to the second static pressure difference with the preset smoothing interval. If it is within the interval, it is determined that the static pressure difference changes smoothly according to the liquid density order, which means that the current pressure gradient is consistent with the normal stratification characteristics. Step 3: Calculate the static pressure change rate of the medium density pressure tap 17 per unit time. If the change rate is less than the preset fluctuation threshold and the aforementioned ratio deviates from the smooth range, it is determined that the static pressure change rate is lower than the preset fluctuation threshold, which means that the emulsion layer has thickened and covered the medium density pressure tap 17 area. Step 4: Compare the real-time static pressure at the lower density pressure tap 18 with the reference drainage boundary static pressure. If it exceeds the preset static pressure increment threshold, it is determined that the lower static pressure has increased, indicating that the drainage of the water phase enrichment area is blocked. The above states serve as logic trigger signals. When the thickening of the emulsion layer is detected and an emulsion control signal is generated, the controller commands to reduce the flow rate ratio of the variable shear mixing section to transfer the emulsion load. When the obstruction of the lower drainage is detected and a restricted pulse discharge control signal is generated, the continuous discharge mode is changed to restricted pulse discharge to ensure the discharge of the water phase in the interface collection chamber. Considering the periodic pulsation of the upstream raw material pump and the transient water hammer effect caused by valve action, directly calculating the static pressure change rate in the dynamic environment would cause the judgment result to exceed the allowable error range, thus destroying the ideal assumption of a stable interface. Therefore, before executing the above judgment logic, the control unit introduces steady-state judgment logic: static pressure signal is collected only within the steady-state time window when the total flow fluctuation rate of the layered cylinder 3 is less than the set threshold and each regulating valve does not exceed the preset opening change range within the set time. The specific data flow and calculation rules are as follows: the time series within the steady-state window is divided into multiple sub-intervals, the static pressure mean of each sub-interval is calculated, and the static pressure change rate per unit time is obtained based on the change in the mean of adjacent sub-intervals; this effectively isolates the destruction of static density stratification characteristics by high-frequency interference such as vibration generated by the operation of mechanical parts, and ensures the reliability of multi-layer pressure characteristic judgment. During the commissioning and calibration phase of the unit, samples were collected under the following conditions: the interface between the C4 phase and the aqueous phase was clear; the emulsion with a known proportion covered the density pressure tap 17; and the aqueous phase gradually accumulated in the lower part. The smoothing range, fluctuation threshold, reference drainage boundary static pressure, and static pressure increment threshold were determined. Each threshold was divided into several working condition groups according to the raw material temperature and the pressure of the layered cylinder 3. During operation, a set of thresholds corresponding to the current working condition was called. To avoid actions triggered by random deviations within a single stable window, a corresponding control signal is generated only when the same judgment result appears consecutively to reach a preset number of confirmations. When the state recovers, a recovery threshold below the trigger boundary is used to form a hysteresis. The static pressure change rate of the medium density pressure tap 17 is lower than the preset fluctuation threshold and is not used as an emulsification criterion on its own. Only when its ratio with the first static pressure difference and the second static pressure difference deviates from the smooth range can it be determined that the emulsion layer covers the central region. As an implementation method to reduce the flow rate ratio of the variable shear mixing section 11, the liquid inlet distribution pipe of the slow mixing cylinder 2 is configured to pass through the main branch of the variable shear mixing section 11 and the low shear bypass branch connected in parallel with it. The two branches converge before the swirl reduction and settling section 12, and are respectively equipped with regulating valves controlled by the control unit. After generating the emulsification control signal, the control unit gradually reduces the valve opening of the main branch and correspondingly increases the valve opening of the low-shear bypass branch to keep the total flow rate change within the allowable range; after the pressure gradient recovers to the recovery range corresponding to normal stratification and continues to reach the preset time, the flow rate ratio of the main branch is gradually restored. The restricted pulse discharge uses preset maximum single opening degree, opening duration and minimum interval between adjacent pulses, and stops when the static pressure at the lower density pressure tap 18 drops back to the recovery threshold. If the number of pulses reaches the upper limit and the lower static pressure has not recovered, the drain valve remains closed and a manual inspection signal is output, thereby limiting the accidental discharge of carbon four phases during the drainage process.

[0031] The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the total pressure difference and drainage frequency of the layered cylinder 3; comparing the operating parameters with preset parameter thresholds, including: determining the relationship between the total pressure difference and the preset pressure difference threshold, and determining whether the drainage frequency is greater than, equal to or less than the preset frequency threshold; Based on the comparison results, corresponding control signals are generated, including: generating a mismatch control signal when the total pressure difference is greater than or equal to a preset pressure difference threshold and the drainage frequency is less than a preset frequency threshold; and generating a high-efficiency coalescence control signal when the total pressure difference is less than a preset pressure difference threshold and the drainage frequency is greater than or equal to a preset frequency threshold. When the total differential pressure is greater than or equal to the preset differential pressure threshold and the drainage frequency is greater than or equal to the preset frequency threshold, or when the total differential pressure is less than the preset differential pressure threshold and the drainage frequency is less than the preset frequency threshold, the current operating state is maintained; according to the control signal, the opening and closing of the control valve are controlled, including: according to the mismatch control signal, controlling the reduction of the total flow and the reduction of the flow ratio of the variable shear mixing section 11; according to the high-efficiency coalescence control signal, controlling the increase of the total flow.

[0032] Obtain the total pressure difference and drainage frequency of the layered cylinder 3; determine the relationship between the total pressure difference and the preset pressure difference threshold, and determine whether the drainage frequency is greater than, equal to or less than the preset frequency threshold; generate a mismatch control signal when the total pressure difference is greater than or equal to the preset pressure difference threshold and the drainage frequency is less than the preset frequency threshold; generate a high-efficiency coalescence control signal when the total pressure difference is less than the preset pressure difference threshold and the drainage frequency is greater than or equal to the preset frequency threshold. Based on the mismatch control signal, the total flow rate is reduced and the flow rate ratio of the variable shear mixing section 11 is reduced; the coalescence performance is decomposed into droplet formation and discharge capacity; among them, the preset differential pressure threshold is a safety indicator characterizing the upper limit of the flow resistance of the coalescence layer in the layered cylinder 3, which is obtained by multiplying the benchmark differential pressure measured by the system under full load of pure C4 raw materials by a safety factor; the preset frequency threshold is an indicator characterizing the normal aqueous phase separation capacity per unit time, which is derived from the average drainage frequency during the historical stable operation phase; The controller collects the inlet and outlet pressures of the layered cylinder 3 in real time to calculate the total pressure difference and counts the number of times the drain valve opens per unit time as the drainage frequency. When the total pressure difference is greater than or equal to the preset pressure difference threshold and the drainage frequency is less than the preset frequency threshold, this state is used as a mismatch trigger condition, indicating that the fine droplets are blocked at the front end of the coalescing layer and the system enters a mismatch state. At this time, by reducing the flow rate and front-end shear, the droplets are promoted to re-coalesce and conditions are created to reduce the latent degradation of the coalescing material due to changes in the wetting state.

[0033] The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the rate of change of the flow resistance coefficient of the front section from the inlet pressure tap 19 to the intermediate pressure tap 20, and the rate of change of the flow resistance coefficient of the rear section from the intermediate pressure tap 20 to the outlet pressure tap 21; comparing the operating parameters with preset parameter thresholds, including: determining whether the rate of change of the flow resistance coefficient of the front section is greater than, equal to or less than the rate of change of the flow resistance coefficient of the rear section. Based on the comparison results, corresponding control signals are generated, including: generating a particle retention control signal when the rate of change of the flow resistance coefficient in the front section is greater than or equal to the rate of change of the flow resistance coefficient in the rear section; generating a droplet penetration control signal when the rate of change of the flow resistance coefficient in the front section is less than the rate of change of the flow resistance coefficient in the rear section; and controlling the opening and closing of the control valves according to the control signals, including: controlling the working state of the adjusting layering cylinder 3 according to the droplet penetration control signal; and generating a prompt for cleaning or replacing the coarse filter basket according to the particle retention control signal.

[0034] The system acquires the rate of change of the flow resistance coefficient from the inlet-side pressure tap 19 to the intermediate-side pressure tap 20, and the rate of change of the flow resistance coefficient from the intermediate-side pressure tap 20 to the outlet-side pressure tap 21; it determines whether the rate of change of the flow resistance coefficient in the inlet section is greater than, equal to, or less than the rate of change of the flow resistance coefficient in the outlet section; if the rate of change of the flow resistance coefficient in the inlet section is greater than or equal to the rate of change of the flow resistance coefficient in the outlet section, it generates a particle retention control signal; if the rate of change of the flow resistance coefficient in the inlet section is less than the rate of change of the flow resistance coefficient in the outlet section, it generates a droplet penetration control signal. According to the microdroplet penetration control signal, the working state of the layered cylinder 3 is controlled and adjusted. Since the coarse filter basket 26 and the fine filter cylinder 27 correspond to the front and rear resistance respectively, when the pressure drop in the front section rises rapidly, it indicates that solid particles are mainly retained. When the pressure drop in the rear section rises rapidly, it indicates that fine droplets have penetrated the front layered cylinder 3, causing the fine filter layer droplets to accumulate and block the filter. By separating the two resistance change rates, the type of contamination can be identified, thereby adjusting the pre-stage stratification state when microdroplet penetration occurs, and avoiding premature replacement of the fine filter layer. This distinction is based on the difference in resistance accumulation mechanisms between solid particles and droplets during the filtration process: the coarse filter basket 26 adopts a pore structure with a larger pore size than the fine filter cartridge 27, forming a surface interception of solid particles. The particles accumulate layer by layer on the surface of the coarse filter basket 26, causing the flow channel cross-section to shrink, and the pressure drop in the front section continues to increase with the accumulation of particles. The fine filter cartridge 27 adopts a fine pore structure. When the front-stage stratification is insufficient, droplets with a diameter lower than the preset particle size threshold that have not fully aggregated will pass through the coarse filter basket 26 and enter the interior of the fine filter layer. Under capillary action, the droplets are adsorbed into the pores of the fine filter material, gradually forming a liquid film and increasing the pore resistance, which increases the rate of pressure drop growth in the later stage. Therefore, the dominant change rate of the flow resistance coefficient in the front stage indicates that particle retention is dominant, while the dominant change rate of the flow resistance coefficient in the later stage indicates that the risk of microdroplet penetration is dominant. In the pre-processing mode, dynamic fluctuations in flow rate can cause pressure drop to momentarily exceed the set threshold. If the absolute pressure drop rate is used directly, it will disrupt the resistance accumulation calculation based on a fixed flow rate, resulting in distorted judgment results. To solve this problem, the control unit acquires the real-time flow rate signal simultaneously with the pressure drop signal, and divides the front-end pressure drop and the back-end pressure drop by the square of the real-time flow rate to convert them into a normalized flow resistance coefficient used to eliminate the influence of flow fluctuations. Because there is a spatial distance between the pressure tap and the flow meter in the physical pipeline, and the response time constants of the two types of sensors are different, directly dividing the instantaneous pressure drop signal by the square of the instantaneous flow signal will produce a false spike in the calculation due to the time misalignment of the signal when the flow fluctuates drastically, interfering with the subsequent slope calculation. To eliminate this conflict, in terms of data flow and calculation rules, before performing the division operation, the control unit determines the physical transmission delay time of the material corresponding to the flow signal reaching the pressure tap based on the pipeline volume and average flow velocity, and performs time shifting and alignment on the flow signal; the same low-pass filtering algorithm is used to smooth the synchronized pressure drop signal and flow signal, filter out high-frequency noise, and ensure that the numerator and denominator participating in the division operation are matched in the time domain and frequency domain. The slope of the increase of the front flow resistance coefficient with time is calculated as the rate of change of the front flow resistance coefficient, and the slope of the increase of the rear flow resistance coefficient with time is calculated as the rate of change of the rear flow resistance coefficient. Through the definition of the above data flow and calculation rules, the dynamic flow interference and sensor spatial distribution differences are removed, and the resistance change trend corresponding to the particle accumulation on the surface of the coarse filter basket 26 and the micro-droplet blockage inside the fine filter cartridge 27 is restored, so as to realize the identification of pollution type. Under initial clean conditions, calibration materials containing known particle load and free water content below the set value, and calibration materials containing known droplet load and particle content below the set value were introduced under the same flow rate and temperature conditions. The growth slope of the flow resistance coefficient in the front and back sections was recorded to form the particle retention sample interval and the droplet penetration sample interval. During operation, the control unit first deducts the baseline drift corresponding to the clean filter cartridge. When the difference in the rate of change of the flow resistance coefficient between the current section and the subsequent section is within the preset uncertainty range, the original control state is maintained and no new pollution type control signal is generated. Only when the difference crosses the corresponding boundary and is continuously maintained for a preset confirmation time is a particle interception control signal or droplet penetration control signal generated. This avoids directly interpreting the measurement difference between the two sections with slopes below the preset error range as a difference in pollution type. After generating the droplet penetration control signal, the working state of the layered cylinder 3 is adjusted in the following ways: the opening of the inlet regulating valve of the layered cylinder 3 is reduced by a preset step size to reduce the unit cross-sectional flow velocity, the residence time in the low disturbance deceleration chamber 14 is extended, and the discharge rhythm of the drain valve is adjusted according to the static pressure state of the lower density pressure tap 18; if the total pressure difference of the layered cylinder 3 does not exceed the safety upper limit, this adjustment state is maintained until the rate of change of the flow resistance coefficient in the later section falls back to the recovery threshold. If the rate of change of the flow resistance coefficient in the downstream section continues to increase after the preset duration of adjustment, a check signal is output to the fine filter cartridge 27. The increase in downstream resistance is no longer attributed solely to the penetration of microdroplets in the upstream stage, thus ensuring that the control action corresponds to the pollution type judgment.

[0035] The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the pressure difference ratios corresponding to the upper, middle and lower pressure taps of the first drying cylinder 6 and the second drying cylinder 7; comparing the operating parameters with preset parameter thresholds, including: determining that the middle pressure difference ratio corresponding to the middle pressure tap is greater than, equal to or less than the preset middle ratio threshold, and determining that the lower pressure difference ratio corresponding to the lower pressure tap is greater than, equal to or less than the preset lower ratio threshold. Based on the comparison results, corresponding control signals are generated, including: generating a load reduction control signal when the middle section pressure difference ratio is greater than or equal to a preset middle section ratio threshold; and generating a switching control signal when the lower section pressure difference ratio is greater than or equal to a preset lower section ratio threshold. Based on the control signal, control the opening and closing of the control valve, including: based on the load reduction control signal, controlling the reduction of the flow rate shared by the corresponding drying cylinder; based on the switching control signal, controlling the early switching to the standby drying cylinder and controlling the pressure equalization valve to open.

[0036] Obtain the pressure difference percentages corresponding to the upper, middle, and lower pressure taps of the first drying cylinder 6 and the second drying cylinder 7; determine whether the middle pressure difference percentage corresponding to the middle pressure tap is greater than, equal to, or less than a preset middle percentage threshold, and determine whether the lower pressure difference percentage corresponding to the lower pressure tap is greater than, equal to, or less than a preset lower percentage threshold. When the pressure difference ratio in the middle section is greater than or equal to the preset middle section ratio threshold, a load reduction control signal is generated; when the pressure difference ratio in the lower section is greater than or equal to the preset lower section ratio threshold, a switching control signal is generated; according to the load reduction control signal, the flow rate of the corresponding drying cylinder is reduced; according to the switching control signal, the switch to the standby drying cylinder is controlled and the pressure equalization valve 9 is opened. The risk of accumulated wet load in the middle of the main adsorption layer and the risk of abnormal flow channel in the lower part of the bed are distinguished by the percentage of segmented pressure difference. When the percentage of resistance in the middle section continues to increase, it indicates that the liquid distribution or wetting state in the middle of the main adsorption layer has changed relative to the healthy baseline. The local resistance can be suppressed by reducing the load and the available operating time can be extended. When the proportion of the lower section resistance increases abnormally, it indicates that particle settling, debris migration, or local velocity redistribution has occurred near the buffer inert layer and support grid. At this time, the switching logic is activated to prevent the abnormal flow channel from developing further. The pressure difference ratio is used to characterize the spatial migration of bed resistance. It does not directly equate the single pressure difference ratio with the chemical saturation of the adsorbent, thereby avoiding the exaggeration of the effect caused by inferring the adsorption capacity based solely on the bed pressure difference. Specifically, the inlet pressure of the drying cylinder is used as the upstream reference pressure. The pressures of the upper, middle and lower pressure taps and the outlet pressure of the drying cylinder are used to determine the segmented pressure difference along the logistics direction. The pressure difference ratio is formed by the proportion of each segmented pressure difference to the total pressure difference. All pressure signals are collected using the same sampling period and timestamp. Zero-point correction and moving average with the same window are performed before calculating the ratio. When the total pressure difference of the drying cylinder is less than the effective resolution lower limit of the instrument, or the inlet flow fluctuation rate exceeds the set threshold, the percentage judgment is paused and the original control state is maintained. In order to eliminate the percentage migration caused by changes in the processing flow rate, the preset middle section percentage threshold and the preset lower section percentage threshold are established according to the flow range and the raw material temperature range, respectively, and the threshold that matches the current working condition is selected during operation. During the commissioning and calibration phase of the unit, the flow rate is first increased in stages under the condition that the bed is properly filled, the adsorbent is dry, and the flow rate distribution is uniform, to obtain the baseline range of the pressure difference ratio of each section of the bed under normal operating conditions; by gradually increasing the inlet water content and periodically detecting the outlet water content, the load reduction warning range corresponding to the change in the middle section ratio and the trend of the outlet water content is obtained; by shutting down for inspection, filling and settling simulation, or abnormal bed data of the same model, the switching warning range corresponding to the abnormal change in the lower section ratio is obtained. During operation, a control signal is generated only when the percentage of differential pressure in the middle section or the percentage of differential pressure in the lower section reaches the corresponding threshold for multiple consecutive judgment windows. The recovery judgment adopts the hysteresis boundary below the trigger threshold. After the percentage of differential pressure in the middle section reaches the threshold, the control unit reduces the opening of the inlet valve of the corresponding drying cylinder by a preset step size and transfers the reduced flow to another drying cylinder. At the same time, the outlet water content detection result is used as the operation effect verification parameter. If the outlet water content still exceeds the product control limit after the load is reduced, the system directly enters the switching preparation state. Once the lower section pressure difference reaches the threshold, the control unit executes the pre-filling, pressure equalization, and segmented flow connection procedures for the backup drying cylinder. Thus, the segmented pressure difference provides a real-time basis for triggering risks, and the effluent content and calibration sample form a basis for verifying the effect, so that the load reduction and switching actions correspond to the bed purification status.

[0037] Controlling the early switching to the standby drying cylinder includes: controlling the inlet valve of the drying cylinder to be put into operation to open and the outlet valve to close for pre-filling; controlling the equalizing valve 9 to open so that the top pressure of the first drying cylinder 6 and the second drying cylinder 7 gradually approach each other; controlling the outlet valve of the drying cylinder to be put into operation to open and gradually increasing the opening of the inlet valve for segmented flow connection. Determine whether the differential pressure development sequence of the drying cylinder to be put into operation is consistent with or inconsistent with the preset reference timing characteristics; if the differential pressure development sequence is consistent with the preset reference timing characteristics, control the inlet valve of the drying cylinder to be taken out of operation to reduce its opening first, and control its outlet valve to reduce its opening to complete the unloading at the tail end; if the differential pressure development sequence is inconsistent with the preset reference timing characteristics, stop the switching.

[0038] The inlet valve of the drying cylinder to be put into the dryer is opened and the outlet valve is closed for pre-filling; the equalizing valve 9 is opened to gradually bring the top pressure of the first drying cylinder 6 and the second drying cylinder 7 closer together; the outlet valve of the drying cylinder to be put into the dryer is opened and the opening of the inlet valve is gradually increased for segmented flow connection. Determine whether the differential pressure development sequence of the drying cylinder to be put into operation is consistent with or inconsistent with the preset reference timing characteristics; if the differential pressure development sequence is consistent with the preset reference timing characteristics, control the inlet valve of the drying cylinder to be taken out of operation to reduce its opening first, and control its outlet valve to reduce its opening to complete the unloading at the tail end; if the differential pressure development sequence is inconsistent with the preset reference timing characteristics, stop the switching; the three-segment differential pressure development path of the newly put into bed layer is used as the physical verification standard for successful connection during the switching process; Among them, the preset reference time sequence feature is a standard time sequence feature that characterizes the pressure difference of the upper, middle and lower sections of the drying cylinder in a stepwise increase over time when the flow is connected in sections under normal and unbiased flow conditions. It is derived from the pressure difference dynamic response sequence measured when the same type of drying cylinder is calibrated under the best operating conditions. During the segmented connection phase, the controller's judgment logic is as follows: the input source is the real-time differential pressure signal and time collected from the pressure taps of the upper, middle, and lower sections of the drying cylinder to be put into operation; the preset pressure threshold is an empirical differential pressure value set based on the characteristic inflection point value of the initial rise of differential pressure in each section under historical normal switching conditions. Step 1: The controller extracts the time points when the pressure difference in the upper, middle, and lower sections reaches the preset pressure threshold. Step 2: Calculate the time difference between the pressure differential responses of two adjacent segments; Step 3: Compare the calculated time difference with the standard time difference interval in the preset benchmark time series characteristics; In industrial environments, the mechanical action of control valves in gradually increasing the inlet valve opening inevitably involves mechanical clearance, valve stem jamming, and nonlinear flow characteristics. These inherent errors in mechanical action cause the fluid entry rate into the bed to change nonlinearly, directly causing the absolute time point at which the differential pressure reaches the pressure threshold to deviate beyond the allowable error range. If only absolute time difference is relied upon for comparison, the uncertainty of mechanical action will cause high-precision time-series comparison algorithms to fail, resulting in frequent misjudgments. To resolve the conflict between mechanical action and algorithm accuracy, this embodiment performs structured dimensionality reduction on the algorithm model: while extracting the time point, the control unit simultaneously reads the real-time opening signal of the inlet valve with position feedback; the calculation time difference in step two is converted into the opening increment of the inlet valve when calculating the differential pressure response of two adjacent segments; in step three, the calculated opening increment is compared with the standard opening increment interval in the preset benchmark time sequence characteristics. By mapping the characteristics of the time dimension to the mechanical action dimension, and using relative opening changes to replace absolute time differences, the signal-to-noise ratio degradation caused by uneven valve movement speed is isolated. If the calculated opening increments all fall within the standard opening increment range, they are considered consistent. This consistency state serves as a safety trigger signal, allowing the original drying cylinder to be withdrawn and the tail end unloading to be completed. If any opening increment deviates from the standard range, it is considered inconsistent, and the stop switching plan is immediately triggered, reducing the risk of flow channel deviation induced by the switching action and maintaining the continuous stability of the purification system.

[0039] It should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit it. Although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can be made to the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.

Claims

1. A pretreatment device for C4 feedstock after etherification, comprising: Pre-stabilizing tank (1), slow mixing tank (2), stratification tank (3), protective filter tank (4), finished product buffer tank (5) and double drying tank (30); The double drying cylinder (30) includes a first drying cylinder (6) and a second drying cylinder (7) arranged in parallel, with an equalizing pipe (8) connected between them with an equalizing valve (9); The inlet of the pre-stabilizing tank (1) is connected to the upstream raw material pipeline, and its bottom outlet is connected to the finished product buffer tank (5) via the slow mixing cylinder (2), the stratification cylinder (3), the protective filter cylinder (4), the first drying cylinder (6), and the second drying cylinder (7). The slow mixing cylinder (2) is provided with a guide core (10), a variable shear mixing section (11), and a swirl reduction and settling section (12) along the material flow direction. The layered cylinder (3) is provided with a primary coalescing layer (13), a low-disturbance deceleration chamber (14), and a secondary coalescing layer (15) from top to bottom; the device includes control valves and control units and parameter detection units with electrical connections; The control unit is connected to the control valves on the pre-stabilizing tank (1), the slow mixing tank (2), the stratification tank (3), the protective filter tank (4), and the double drying tank (30); The parameter detection unit converts the detected operating parameters into signals and transmits them to the control unit to control the valve; The parameter detection unit includes the upper density pressure tap (16), middle density pressure tap (17), and lower density pressure tap (18) on the side wall of the layered cylinder (3), the inlet side pressure tap (19), middle side pressure tap (20), and outlet side pressure tap (21) of the protective filter cylinder (4), and the upper, middle, and lower pressure taps on the outer walls of the first drying cylinder (6) and the second drying cylinder (7).

2. The C4 feedstock pretreatment device according to claim 1, characterized in that, The parameter detection unit is a density detection unit. The density detection unit detects the static pressure at different heights inside the layered cylinder (3), converts it into a corresponding static pressure signal, and then transmits it to the control unit. The control unit adjusts the control valve according to the static pressure signal. The upper density tap (16) is located above the primary coalescing layer (13), the middle density tap (17) is located between the primary coalescing layer (13) and the secondary coalescing layer (15), and the lower density tap (18) is located below the secondary coalescing layer (15).

3. The C4 feedstock pretreatment device according to claim 1, characterized in that, The variable shear mixing section (11) is composed of a first spiral blade (22), a second spiral blade (23) and a third spiral blade (24). The blade twist angle of the first spiral blade (22) is smaller than that of the second spiral blade (23), and the blade twist angle of the third spiral blade (24) is smaller than that of the second spiral blade (23). The first spiral blade (22), the second spiral blade (23) and the third spiral blade (24) all have straight tube slow release sections without internal obstructions. The inside of the protective filter cylinder (4) is arranged from top to bottom as follows: inlet distribution cap (25), coarse filter basket (26), fine filter cylinder (27) and liquid collection chamber (28). An annular buffer volume (29) is left between the coarse filter basket (26) and the fine filter cylinder (27).

4. The C4 feedstock pretreatment device after etherification according to claim 1, characterized in that, The interior of the first drying cylinder (6) and the second drying cylinder (7) are arranged from top to bottom as follows: an upper distribution plate, a main adsorption layer, a buffer inert layer, a support grid plate and a bottom confluence cone; the upper pressure tap is located on the upper part of the main adsorption layer, the middle pressure tap is located in the middle of the main adsorption layer and the lower pressure tap is located above the buffer inert layer.

5. A control method applied to the C4 feedstock pretreatment device after etherification according to any one of claims 1-4, comprising the following steps: S1. Obtain the operating parameters of the C4 raw material pretreatment device after etherification. The operating parameters include the static pressure parameters at different heights in the layered cylinder, as well as the multi-stage differential pressure parameters of the protective filter cylinder and the double drying cylinder. S2. Compare the operating parameters with preset parameter thresholds; generate corresponding control signals based on the comparison results; S3. Based on the control signal, control the opening and closing of the corresponding control valve, dynamically adjust the flow rate ratio of the variable shear mixing section, the liquid phase pulse emission cycle or the switching state of the dual drying cylinder, or generate cleaning and replacement prompts.

6. The control method according to claim 5, characterized in that, The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the static pressure signals corresponding to the upper density pressure tap (16), the middle density pressure tap (17) and the lower density pressure tap (18); comparing the operating parameters with preset parameter thresholds, including: calculating the first static pressure difference between the upper density pressure tap (16) and the middle density pressure tap (17), and the second static pressure difference between the middle density pressure tap (17) and the lower density pressure tap (18), determining whether the ratio of the first static pressure difference to the second static pressure difference is within the preset smoothing range, determining whether the static pressure change rate corresponding to the middle density pressure tap (17) is lower than the preset fluctuation threshold, and determining whether the difference between the real-time static pressure corresponding to the lower density pressure tap (18) and the benchmark drainage boundary static pressure exceeds the preset static pressure increment threshold; Based on the comparison results, corresponding control signals are generated, including: generating a normal stratification control signal when the static pressure difference changes smoothly in the order of liquid density; generating an emulsification control signal when the static pressure change rate corresponding to the medium density pressure tap (17) is lower than the preset fluctuation threshold; and generating a restricted pulse emission control signal when the real-time static pressure corresponding to the lower density pressure tap (18) exceeds the preset static pressure increment threshold. According to the control signal, control the opening and closing of the control valve, including: according to the normal stratification control signal, control to maintain the flow ratio of the current variable shear mixing section; according to the emulsification control signal, control to reduce the flow ratio of the variable shear mixing section (11); according to the restricted pulse emission control signal, control to switch to restricted pulse emission.

7. The control method according to claim 5, characterized in that, The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the total pressure difference and drainage frequency of the layered cylinder (3); comparing the operating parameters with the preset parameter threshold, including: determining the relationship between the total pressure difference and the preset pressure difference threshold, and determining whether the drainage frequency is greater than, equal to or less than the preset frequency threshold. Based on the comparison results, corresponding control signals are generated, including: generating a mismatch control signal when the total pressure difference is greater than or equal to a preset pressure difference threshold and the drainage frequency is less than a preset frequency threshold; and generating a high-efficiency coalescence control signal when the total pressure difference is less than a preset pressure difference threshold and the drainage frequency is greater than or equal to a preset frequency threshold. When the total differential pressure is greater than or equal to the preset differential pressure threshold and the drainage frequency is greater than or equal to the preset frequency threshold, or when the total differential pressure is less than the preset differential pressure threshold and the drainage frequency is less than the preset frequency threshold, the current operating state is maintained; according to the control signal, the opening and closing of the control valve are controlled, including: according to the mismatch control signal, controlling the reduction of the total flow rate and the reduction of the flow rate ratio of the variable shear mixing section (11); according to the high-efficiency coalescence control signal, controlling the increase of the total flow rate.

8. The control method according to claim 5, characterized in that, The operating parameters of the C4 feedstock pretreatment device after etherification are obtained, including: obtaining the change rate of the flow resistance coefficient of the front section from the inlet pressure tap (19) to the intermediate pressure tap (20), and the change rate of the flow resistance coefficient of the rear section from the intermediate pressure tap (20) to the outlet pressure tap (21); comparing the operating parameters with preset parameter thresholds, including: determining whether the change rate of the flow resistance coefficient of the front section is greater than, equal to or less than the change rate of the flow resistance coefficient of the rear section; Based on the comparison results, corresponding control signals are generated, including: generating a particle retention control signal when the rate of change of the front flow resistance coefficient is greater than or equal to the rate of change of the rear flow resistance coefficient; generating a droplet penetration control signal when the rate of change of the front flow resistance coefficient is less than the rate of change of the rear flow resistance coefficient; controlling the opening and closing of the control valve according to the control signals, including: controlling the working state of the adjustment layering cylinder (3) according to the droplet penetration control signal; generating a prompt for cleaning or replacing the coarse filter basket according to the particle retention control signal.

9. The control method according to claim 5, characterized in that, The operating parameters of the C4 raw material pretreatment device after etherification are obtained, including: obtaining the pressure difference ratios corresponding to the upper, middle and lower pressure taps of the first drying cylinder (6) and the second drying cylinder (7); comparing the operating parameters with preset parameter thresholds, including: determining that the middle pressure difference ratio corresponding to the middle pressure tap is greater than, equal to or less than the preset middle ratio threshold, and determining that the lower pressure difference ratio corresponding to the lower pressure tap is greater than, equal to or less than the preset lower ratio threshold; Based on the comparison results, corresponding control signals are generated, including: generating a load reduction control signal when the middle section pressure difference ratio is greater than or equal to the preset middle section ratio threshold; generating a switching control signal when the lower section pressure difference ratio is greater than or equal to the preset lower section ratio threshold; controlling the opening and closing of the control valve according to the control signals, including: controlling the reduction of the flow share of the corresponding drying cylinder according to the load reduction control signal; controlling the early switching to the standby drying cylinder and controlling the pressure equalization valve (9) to open according to the switching control signal.

10. The control method according to claim 9, characterized in that, Controlling the early switching to the standby drying cylinder includes: controlling the inlet valve of the drying cylinder to be put into operation to open and the outlet valve to close, and pre-filling with liquid; controlling the equalization valve (9) to open, so that the top pressure of the first drying cylinder (6) and the second drying cylinder (7) gradually approach each other; controlling the outlet valve of the drying cylinder to be put into operation to open, and gradually increasing the opening of the inlet valve to perform segmented flow connection; Determine whether the differential pressure development sequence of the drying cylinder to be put into operation is consistent with or inconsistent with the preset reference timing characteristics; if the differential pressure development sequence is consistent with the preset reference timing characteristics, control the inlet valve of the drying cylinder to be taken out of operation to reduce its opening first, and control its outlet valve to reduce its opening to complete the unloading at the tail end; if the differential pressure development sequence is inconsistent with the preset reference timing characteristics, stop the switching.

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