Thermally coupled dividing wall high-efficiency separation rectifying column and separation process

Abstract

The present application relates to the field of chemical separation technology, in particular to a thermally coupled high-efficiency separation rectifying tower with a baffle and a separation process. A baffle is arranged in the middle section of the tower, which divides the tower into a left packing zone and a right packing zone. Packing layers are arranged in the two packing zones. A common liquid redistribution sump is arranged above the baffle. A gas phase adjusting mechanism is arranged in the common space at the bottom of the tower, which is linked with a differential main shaft and includes left and right valve pieces driven by the same main shaft through rack and pinion transmission. The present application uses opposed bellows to offset the thermal expansion interference caused by the ambient temperature, uses a damping piston to filter high-frequency pulsation, does not need external power supply and gas source, can simultaneously and self-adaptively suppress liquid flooding and flow deviation from the gas-liquid two-phase, and significantly improves the operation flexibility and separation efficiency of the tower with a baffle.

Description

Technical Field

[0001] This invention relates to the field of chemical separation technology, specifically to a thermally coupled baffle-type high-efficiency separation distillation column and its separation process. Background Technology

[0002] Thermally coupled baffled distillation columns (DWC) integrate the separation functions of traditional two or more columns into one unit by incorporating vertical baffles within the column body. This allows for the simultaneous separation of three or more components within a single column shell. Compared to conventional distillation sequences, DWCs effectively reduce backmixing within the column, offering significant thermodynamic advantages. They typically reduce equipment investment and save considerable energy, thus showing broad application prospects in petrochemical, fine chemical, and other fields.

[0003] However, the industrial operation of baffled towers places stringent demands on the precision of gas and liquid phase distribution on both sides of the baffle. In actual production, when there are process fluctuations in the upstream feed rate, feed composition, or enthalpy, the gas-liquid load on the feed side (pre-separation zone) will change, leading to changes in the pressure drop of the packing layer in that area. Since both sides of the baffle share the rising steam from the bottom of the tower, the steam will spontaneously flow towards the side with the smaller pressure drop. If the liquid distribution ratio on both sides cannot be adjusted in time to balance the gas phase resistance, the feed side is prone to liquid stagnation or even flooding due to insufficient stripping or excessive liquid phase load; at the same time, the main extraction zone will generate mist entrainment due to excessive gas volume. Once this gas flow deviation forms a positive feedback, it will lead to a significant decrease in the overall tower separation efficiency and even damage the product purity.

[0004] Regarding the aforementioned gas-liquid distribution problem, existing technologies have the following limitations: The first type employs external instruments and a distributed control system (DCS). This type of solution typically involves external pressure input to the tower, acquiring signals through electronic differential pressure transmitters, and then using the DCS to control external circulating pumps or pneumatic regulating valves. Such systems rely on external power and gas supplies, resulting in high explosion-proof and maintenance costs in flammable, explosive, or highly corrosive chemical environments. Furthermore, the entire signal feedback loop from electronic sensor acquisition and controller processing to pneumatic valve actuation inherently has a time lag, and the static friction of the valve packing makes it difficult to provide a smooth and immediate response to changes in tower operating conditions, easily leading to system overshoot and oscillation.

[0005] The second type uses an in-tower electromechanical integrated distribution device. This type of solution moves the electromagnetic actuators inside the tower, but still requires an external power supply. In the high-temperature, corrosive distillation system, the risk of aging and insulation failure of electronic components is relatively high.

[0006] The third type uses a static trough distributor. This solution pre-determines a fixed geometric opening ratio based solely on the design conditions, resulting in very little operational flexibility. When the actual feed load deviates from the design value, the device cannot dynamically adapt, making it difficult for the separation unit to maintain stable operation under a wide range of conditions.

[0007] In addition, existing solutions have attempted to install gas distributors at the bottom of the tower. Chinese patent application CN113521786A, published on April 2, 2014, discloses a thermal coupling and heat pump combined separation process and device for alkylation reaction products, combining thermal coupling technology with heat pump distillation technology to achieve the separation of alkylation reaction products. Chinese patent application CN103691144A, also published on April 2, 2014, discloses a gas distribution device (including a square valve plate adjustment mechanism, sleeve, and shaft) for use in a partitioned tower. However, these solutions all require external motor drive, still relying on external energy sources, and necessitate complex electrical explosion-proof systems.

[0008] Therefore, developing a gas-liquid co-distribution system that does not rely on external energy, has intrinsically safe explosion-proof characteristics, and can simultaneously and smoothly adaptively adjust the gas and liquid phases according to the actual flow field resistance inside the tower is a technical problem that urgently needs to be solved in this field. Summary of the Invention

[0009] In view of the shortcomings of the prior art, the purpose of this invention is to provide a thermally coupled baffle-type high-efficiency separation distillation column, which adopts an upper and lower corrugated pipe structure with equal area and opposite to each other. By utilizing the principle of mechanical vector cancellation, the thermal expansion error of the working liquid in the pressure guide pipe caused by drastic changes in the environment and the temperature inside the column is spontaneously eliminated. At the same time, a gas phase adjustment mechanism synchronously driven by the same differential main shaft is added to the common space at the bottom of the column, realizing the coordinated adaptive adjustment of the gas and liquid phases.

[0010] Another objective of this invention is to provide a separation process for a thermally coupled baffle-type high-efficiency separation distillation column. By utilizing differential pressure negative feedback to simultaneously control liquid phase distribution and gas phase distribution, the system can dynamically and continuously redistribute the gas-liquid ratio between the pre-separation zone and the main extraction zone when the feed rate fluctuates significantly, effectively preventing local flooding or leakage and maintaining high separation efficiency.

[0011] This invention is achieved using the following technical solution: The aforementioned thermally coupled baffle-type high-efficiency separation distillation column includes a distillation column with a baffle in the middle section dividing the column into a left-side packing zone and a right-side packing zone. A common liquid redistribution collection tank is located in the top space above the baffle. The distillation column is equipped with a mechanical adaptive gas-liquid distribution system, which includes: pressure sensing components, respectively located at the bottom and top of the left-side packing zone, for acquiring pressure signals at both ends of the zone; a pressure isolation remote transmission component, connected to the pressure sensing components, for transmitting the pressure signals; and a differential pressure mechanical converter. The central control unit, connected to the pressure isolation remote transmission component, converts two pressure signals into a net pressure difference and drives the differential spindle to generate mechanical displacement. The regulating component, located at the left outlet of the common liquid redistribution collection tank and connected to the differential spindle, responds to the displacement of the differential spindle to adjust the flow area of ​​the left outlet. The gas phase regulating mechanism, located in the common space at the bottom of the tower below the partition and connected to the differential spindle via a mechanical transmission component, responds to the displacement of the differential spindle to synchronously regulate the gas phase flow rate to the left and right packing zones.

[0012] Furthermore, the pressure sensing component includes a high-pressure isolation diaphragm box installed at the bottom of the left-side packing area and a low-pressure isolation diaphragm box at the top; the pressure isolation remote transmission component includes a high-pressure capillary tube and a low-pressure capillary tube respectively connected to the high-pressure isolation diaphragm box and the low-pressure isolation diaphragm box, with the tubes filled with high-temperature silicone oil. By using the isolation diaphragm box and the capillary tube filled with high-temperature silicone oil, physical isolation is achieved between corrosive materials, easily condensable vapors, and mechanical transmission components within the tower. This effectively avoids false liquid level readings or pipe blockages caused by vapor entering the pressure-sensing pipeline and condensing, ensuring the reliability of pressure signal transmission.

[0013] Furthermore, the high-pressure capillary and low-pressure capillary are arranged in parallel with equal physical unfolded lengths and placed within the same insulation and heat tracing layer; alternatively, a coaxial nested structure with the high-pressure capillary as the inner tube and the low-pressure capillary as the outer tube is used to eliminate differential mode interference caused by the thermal expansion of the working fluid. In industrial environments, sudden changes in ambient temperature and tower surface temperature can cause the working fluid in the capillary to undergo volumetric thermal expansion, thereby generating additional false pressure signals. This invention, through equal-length parallel laying or coaxial nesting design, ensures that the volume of the working fluid in the two capillary lines is strictly consistent and that the ambient temperature gradient is the same, making the additional pressure generated by thermal expansion equal in magnitude in both pipelines, which then serves as a common-mode signal to be canceled out by the subsequent mechanical control.

[0014] Furthermore, the differential pressure mechanical conversion center includes a rigid fixed support, within which are upper and lower corrugated pipes with equal effective pressure-bearing areas, arranged vertically opposite each other. The upper and lower corrugated pipes are respectively connected to a high-pressure capillary and a low-pressure capillary. The differential spindle is connected in series between the two, bearing the net differential pressure thrust after the expansion thrust of the two corrugated pipes cancels each other out. Based on the principle of mechanical vector cancellation, the pressure-bearing areas of the upper and lower corrugated pipes are equal. The absolute pressure transmitted by the high-pressure side capillary and the additional pressure from thermal expansion act on the upper corrugated pipe, generating a downward thrust; the absolute pressure transmitted by the low-pressure side capillary and the same additional pressure from thermal expansion act on the lower corrugated pipe, generating an upward thrust. The net thrust on the differential spindle is the difference between the two. Through this mechanical structure, the common-mode temperature drift signal is spontaneously canceled out, and the spindle only responds to the actual pressure drop within the tower.

[0015] Furthermore, the differential pressure mechanical conversion center also includes a linear return spring, sleeved on the differential spindle, with an initial preload to counteract the bias force generated by the hydrostatic column within the pressure isolation remote transmission component and to achieve physical zeroing of the differential spindle; and a mechanical filtering structure, including a damping hydraulic cylinder fixed on a rigid support and a damping piston fixed on the differential spindle and sliding within the cylinder. The damping hydraulic cylinder is filled with damping silicone oil, and the damping piston has a micro-throttling orifice. A difference in hydrostatic column height between the high-pressure capillary and the low-pressure capillary, caused by the tower height, generates a constant gravitational bias pressure difference. This invention achieves initial physical zeroing of the mechanical system by setting the initial preload of the spring to be equal to the hydrostatic column force. In addition, the gas-liquid interaction within the tower generates high-frequency bubble bursting and turbulent noise; the damping silicone oil must flow through the micro-throttling orifice during piston movement. When low-frequency macroscopic pressure difference changes occur, the piston moves at low speed, the orifice resistance is small, and the system exhibits smooth servo characteristics; when high-frequency pressure pulsation occurs, the piston instantaneous speed increases suddenly, the orifice resistance increases nonlinearly and sharply, causing the spindle to exhibit a mechanical self-locking state, thereby giving the system low-pass filtering characteristics.

[0016] Furthermore, the regulating component includes a left-side V-shaped opening weir plate fixed to the bottom left side of the common liquid redistribution collection tank, and a sleeve-type flow-blocking gate plate that slides up and down close to the V-shaped opening weir plate. The sleeve-type flow-blocking gate plate is rigidly connected to the differential spindle. Utilizing the flow characteristics of the V-shaped weir plate, its flow rate over the weir exhibits a non-linear power law relationship with the liquid level. The differential spindle drives the gate plate to shift, changing the effective flow cross section of the V-shaped weir, thus achieving fine adjustment of the flow rate under small pressure differentials and rapid response of the flow rate under large pressure differentials. A right-side overflow weir leading to the right-side packing area is provided on the right side of the common liquid redistribution collection tank. The top elevation of the right-side overflow weir is higher than the bottom elevation of the left-side outlet, used to distribute excess liquid to the right-side packing area. When the pressure drop in the left-side packing area increases and the gate plate moves down to reduce the flow area, the amount of liquid entering the left side decreases, the liquid level in the collection tank passively rises, and the excess liquid naturally crosses the right-side overflow weir under gravity and enters the right-side packing area, realizing the dynamic reconstruction of the liquid phase distribution ratio.

[0017] Furthermore, the gas phase regulation mechanism includes a left gas phase distribution cylinder and a right gas phase distribution cylinder disposed in the common space at the bottom of the tower, a left valve plate and a right valve plate respectively disposed in the left gas phase distribution cylinder and the right gas phase distribution cylinder, and a mechanical transmission assembly connecting the differential main shaft with the left valve plate and the right valve plate; when the differential main shaft moves downward, the mechanical transmission assembly drives the left valve plate to close the gas passage to the left packing area, and simultaneously drives the right valve plate to open the gas passage to the right packing area. The mechanical transmission assembly preferably includes a vertical connecting rod rigidly connected to the lower end of the differential main shaft, a rack fixed to the lower end of the vertical connecting rod, and a left drive gear and a right drive gear meshing with the rack; the left drive gear is fixed to the rotating shaft end of the left valve plate, and the right drive gear is fixed to the rotating shaft end of the right valve plate; the meshing phases of the left drive gear and the right drive gear are opposite, so that the unidirectional displacement of the differential main shaft drives the left valve plate and the right valve plate to rotate synchronously in opposite directions.

[0018] Furthermore, a left-side gas distributor and a right-side gas distributor are respectively installed above the left and right gas phase distribution cylinders to evenly distribute the gas, after being regulated by the valve plate, to the bottom cross-section of the corresponding packing zone. The gas distributor includes a gas pre-distribution plate and a flow guide baffle. The flow guide baffle is installed above the gas pre-distribution plate to guide the airflow to the bottom of the corresponding packing zone. A flow splitting blade can be installed at the outlet of the flow guide baffle to further improve the uniformity of gas distribution. The pressure drop of the gas distributor is controlled within 0.1 to 0.2 kPa.

[0019] Furthermore, a constant-flow underflow plate with a fixed orifice is provided above both the left and right packing zones to provide a reference liquid volume not less than the minimum wetting load of the packing. To prevent excessive adjustment under extreme operating conditions from causing the packing on one side to dry out, thereby triggering a vicious cycle of gas phase short-circuit flow deviation, this invention constructs a composite distribution architecture of reference underflow plus differential overflow. The constant-flow underflow plate ensures the minimum wetting rate under any adjustment state, and the mechanical distribution system is only responsible for dynamic adjustment within the operating elastic margin.

[0020] This invention also provides a separation process using the aforementioned thermally coupled baffle-type high-efficiency separation distillation column, comprising the following steps: condensate from the top of the column falls back into a common liquid redistribution collection tank, with a portion entering the left packing zone and the other portion entering the right packing zone; a pressure sensing component captures pressure signals at both ends of the left packing zone in real time, which are transmitted to the differential pressure mechanical conversion center via a pressure isolation remote transmission component; when the pressure drop in the left packing zone increases, the differential pressure mechanical conversion center drives the differential main shaft to move downwards; when the differential main shaft moves downwards, liquid phase regulation and gas phase regulation are performed simultaneously. During liquid phase regulation, the regulating component reduces the flow area of ​​the left outlet, the liquid level in the collection tank rises, and excess liquid overflows into the right packing zone; during gas phase regulation, the gas phase regulation mechanism reduces the gas flow rate to the left packing zone while increasing the gas flow rate to the right packing zone; the pressure drop in the left packing zone decreases, and the system reaches a steady state at a new equilibrium point.

[0021] Furthermore, in the above process, the high-frequency pressure fluctuations caused by bubble rupture in the distillation column are mechanically low-pass filtered by a damping piston with a micro-throttling orifice sliding in the damping hydraulic cylinder, so that the differential spindle filters out the high-frequency pulsation and only makes a smooth servo response to the low-frequency real flooding pressure difference signal.

[0022] The regulating component dynamically allocates only the operating elasticity margin of 40%-70% of the total return flow at the top of the column. A constant flow underflow plate with a fixed aperture is provided above the left and right packing zones to provide a reference liquid volume that is not less than the minimum wetting load of the packing.

[0023] Compared with the prior art, the beneficial effects of the present invention are: (1) The present invention uses a purely mechanical physical structure to complete the capture of flow field pressure drop signal, mechanical calculation and valve execution. The system completely gets rid of the dependence on external power supply, instrument air source and electronic controller, avoids complex electrical explosion-proof design, and is especially suitable for complex chemical separation sites that are flammable, explosive, high temperature and strong corrosive, with high operational reliability.

[0024] (2) By using double capillary tubes with equal length or coaxial design, combined with upper and lower corrugated tube structures with equal pressure area, the thermal expansion error of the working fluid in the pressure guide tube caused by the drastic change in environment and tower temperature is eliminated as a common mode signal, ensuring that the mechanical spindle only responds accurately to the real differential pressure drop in the tower.

[0025] (3) By integrating a hydraulic damping system with a micro throttling orifice on the differential spindle, the mechanical actuator is endowed with low-pass filtering characteristics, which not only effectively protects the mechanical moving parts from the fatigue impact of high-frequency pulsation of fluid in the tower, but also avoids the overshoot and low-frequency oscillation of conventional electronic pneumatic valves during the adjustment process, so that the gas-liquid distribution process is smoothly transitioned.

[0026] (4) This invention adds a gas phase adjustment mechanism synchronously driven by a differential main shaft to the common space at the bottom of the tower below the partition. When the feed fluctuation causes an increase in the pressure drop on the left side, this mechanism directly closes the gas phase channel leading to the left packing area and simultaneously opens the gas phase channel leading to the right packing area through pure mechanical transmission, realizing direct and active intervention in gas phase flow deviation. Combined with the original liquid phase adjustment, the system can simultaneously, continuously, and spontaneously redistribute the gas-liquid ratio on both sides of the partition from both gas and liquid phase dimensions when the feed load fluctuates significantly. This solves the indirect adjustment and possible pseudo-steady-state problems caused by the traditional scheme that only adjusts the liquid phase and not the gas phase. By using pressure differential negative feedback to dynamically control the flow area of ​​the V-shaped weir plate, combined with the composite distribution structure of reference underflow and differential overflow, the gas flow short-circuiting caused by local flooding or packing drying is effectively prevented, significantly improving the operational elasticity boundary and separation efficiency of the partition tower. Attached Figure Description

[0027] Figure 1 This is a schematic diagram of the structure of the thermally coupled baffle-type high-efficiency separation distillation column of the present invention; Figure 2 This is a schematic diagram of the structure of the linear reset spring in this invention; Figure 3 This is a schematic diagram of the structure of the vertical connecting rod rack of the present invention; In the diagram: 100, Distillation column; 101, Baffle plate; 102, Left packing area; 103, Right packing area; 200, Common liquid redistribution collection tank; 201, Right overflow weir; 202, Left V-shaped opening weir plate; 203, Sleeve-type flow damper; 301, High-pressure isolation diaphragm box; 302, Low-pressure isolation diaphragm box; 303, Double capillary tubes; 3031, High-pressure capillary tube; 3032, Low-pressure capillary tube; 400, Rigid fixed support; 401, Upper corrugated pipe; 402, Lower corrugated pipe. 500. Differential spindle; 601. Damped hydraulic cylinder; 602. Damped piston; 603. Miniature throttle orifice; 700. Linear return spring; 701. Left gas phase distribution cylinder; 702. Right gas phase distribution cylinder; 703. Left gas distributor; 704. Right gas distributor; 705. Left valve plate; 706. Right valve plate; 707. Vertical connecting rod rack; 708. Left drive gear; 709. Right drive gear; 8. Tower bottom partition plate; 9. Packing layer. Detailed Implementation

[0028] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the scope of protection of this invention.

[0029] I. System Structure and Operation Combination Figures 1-3 As shown, this invention provides a thermally coupled baffle-type high-efficiency separation distillation column. Its basic flow path structure includes a distillation column 100, with a vertical baffle 101 welded to the middle section of the column. The baffle 101 divides the middle section of the column into a left-side packing zone 102 (typically a pre-separation zone with central feed) and a right-side packing zone 103 (typically a main draw-out zone with side-stream draw-out). Both the left-side packing zone 102 and the right-side packing zone 103 are filled with packing layers 9, which use structured packing (such as Mellapak 350Y type) to provide a site for gas-liquid mass transfer. A common liquid redistribution collection tank 200 is located in the common space at the top of the column, directly above the baffle 101, to collect the liquid falling back from the top condenser.

[0030] The core of this invention lies in a purely mechanical adaptive gas-liquid distribution system installed inside the tower, the specific structure and mechanical principle of which are as follows: 1. Pressure sensing and isolated remote transmission High-pressure isolation membrane box 301 and low-pressure isolation membrane box 302 are installed at the bottom and top of the left-side packing zone 102, respectively. Both membrane boxes are connected to the top of the column via a double capillary tube 303 filled with vacuum-degassed high-temperature silicone oil. The double capillary tube 303 includes a high-pressure capillary tube 3031 and a low-pressure capillary tube 3032. The isolation membrane boxes can physically isolate corrosive materials and easily condensable vapors inside the column, avoiding blockage of the pressure tapping pipe or the generation of "false liquid levels".

[0031] To eliminate the interference of differential thermal expansion of silicone oil caused by changes in ambient temperature, as a preferred embodiment, the low-pressure capillary 3032 adopts an equal-length parallel laying structure with the same physical unfolded length as the high-pressure capillary 3031, and is placed within the same insulation and heat tracing layer. As another, even better embodiment, the dual capillaries 303 adopt a coaxial nested structure, with the high-pressure capillary 3031 serving as the inner tube and the low-pressure capillary 3032 serving as an annular outer tube wrapping around the inner tube. This ensures that the external temperature gradient sensed by the working fluids of both is completely consistent.

[0032] 2. Pressure differential conversion and temperature compensation A rigid fixed support 400 is installed in the space at the top of the tower. Inside the support, an upper corrugated pipe 401 and a lower corrugated pipe 402 are installed vertically opposite each other, and their effective pressure-bearing areas (set as S) are strictly equal. The upper corrugated pipe 401 is connected to the high-pressure capillary tube 3031, and the lower corrugated pipe 402 is connected to the low-pressure capillary tube 3032. A differential spindle 500 is connected in series between these two corrugated pipes.

[0033] Mechanical derivation: Let the high pressure at the bottom of the tower be P. H The low pressure at the top of the tower is P L The additional pressure caused by the thermal expansion of silicone oil due to a sudden change in ambient temperature is ΔP. T The downward thrust generated by the upper bellows: F down =(P H +ΔP T )×S; The upward thrust F generated by the lower bellows up =(P L +ΔP T Net thrust on the differential spindle: F × S net =F down -F up =(P H -P L )×S. Through the above-mentioned mechanically symmetrical structure, the temperature drift (ΔP) T It is mechanically canceled out as a common-mode signal.

[0034] 3. Physical zeroing and mechanical filtering A linear return spring 700 is fitted onto the differential spindle 500, and this spring has an initial preload. The static pressure generated by the working fluid in the high-pressure capillary tube 3031 and the low-pressure capillary tube 3032 due to the tower height acts on the upper bellows 401 and the lower bellows 402, respectively. Since the two capillaries are laid in parallel of equal length or coaxially nested, the height of the static fluid column in the two tubes is approximately equal, and the static pressures generated by them basically cancel each other out. The net bias force comes only from the small height difference ΔH between the two capillaries, i.e., F0=ρg·ΔH·S. The initial preload of the linear return spring 700 is set to be equal to this net bias force, thus achieving initial "physical zeroing" in a purely mechanical structure. Under ideal installation conditions (ΔH→0), the spring preload can approach zero.

[0035] Meanwhile, the differential spindle 500 passes through the damping hydraulic cylinder 601, and a damping piston 602 is fixed on the spindle and slides within the cylinder. A micro-throttling orifice 603 is provided on the piston. The damping hydraulic cylinder 601 is filled with high-viscosity damping silicone oil, with a kinematic viscosity of 100-1000 cSt (preferably 350 cSt) at 25°C. This viscosity range of silicone oil produces a suitable damping effect when flowing through the micro-throttling orifice 603—when the differential spindle 500 moves at low speed (corresponding to a slow change in pressure drop within the tower), the silicone oil flows through the orifice in a laminar state, with low resistance, and the system exhibits smooth servo characteristics; when high-frequency pressure pulsation occurs, the piston's instantaneous speed increases suddenly, and the silicone oil flowing through the orifice enters the nonlinear resistance region (resistance is proportional to the square of the flow velocity), causing the spindle to exhibit a mechanical self-locking state, thereby achieving a mechanical low-pass filtering function. Testing revealed that when the viscosity was below 50 cSt, the damping was insufficient and unable to effectively suppress high-frequency chatter; when the viscosity was above 2000 cSt, the response hysteresis was too large, affecting the timeliness of adjustment. When high-frequency pressure pulsations such as bubble rupture occur in the tower, the resistance generated by the fluid flowing through the throttling orifice increases with the square law of the flow velocity, causing the spindle to be in a mechanical self-locking state, filtering out high-frequency interference; while for low-frequency, real flooding pressure differential signals, the spindle can slowly and smoothly perform servo displacement.

[0036] 4. Liquid phase flow rate regulation and dynamic redistribution The lower end of the differential spindle 500 is rigidly connected to the sleeve-type flow-blocking gate 203. The gate slides up and down against the left-side V-shaped opening weir plate 202 located at the bottom left side of the common liquid redistribution collection tank 200. The right side of the common liquid redistribution collection tank 200 is provided with a right-side overflow weir 201 leading to the right-side packing area 103, and its top elevation is higher than the bottom elevation of the left-side outlet.

[0037] When the pressure drop of the packing layer 9 in the left packing zone 102 increases, the main shaft moves downward, and the sleeve-type flow-blocking gate 203 reduces the flow area of ​​the V-shaped weir. The outflow from the left side decreases, and the liquid level in the common liquid redistribution collection tank 200 passively rises. Excess liquid naturally flows over the right overflow weir 201 into the right packing zone 103, falling to the top of the packing layer 9 in that zone, thus achieving a smooth redistribution of liquid volume as the pressure difference changes. Simultaneously, constant flow underflow plates are installed above both the left and right packing zones to ensure that the packing layer 9 in each zone always receives a reference spray volume not lower than the minimum wetting load. The regulating component dynamically allocates only 40%-70% of the total return flow's operational flexibility margin to prevent localized drying of the packing layer 9 and subsequent airflow short-circuiting.

[0038] The constant flow underflow plate is a perforated plate distributor located above the left packing zone 102 and the right packing zone 103. It is disc-shaped, with an outer diameter that matches the inner diameter of the tower (gap ≤ 5mm), a plate thickness of 3-5mm, and is made of 316L stainless steel. Circular through holes are evenly distributed on the plate surface, arranged in an equilateral triangle (hole spacing to hole diameter ratio is 2.5-3.0). An annular support ring at the bottom of the plate secures it to the tower wall.

[0039] The principle for determining the orifice size is as follows: The design goal of the constant flow underflow disk is to provide a reference spray volume for packing layer 9 that is not less than the minimum wetting load throughout the entire operating range. For Mellapak 350Y structured packing, its minimum wetting load (minimum spray density) is approximately 0.2-0.5 m³ / s. 3 / (m 2 •h). The orifice diameter d0 of the bottom flow plate is calculated according to the orifice outflow formula: ; Where Q0 is the baseline spray volume (m³) 3 / s), n is the number of openings, C d Here, A0 is the orifice flow coefficient (taken as 0.62-0.65), and A0 is the cross-sectional area of ​​a single orifice (m²). 2 g is the acceleration due to gravity, and H0 is the liquid level height above the bottom flow plate (design value is 50-100mm).

[0040] Typical design parameters are: aperture φ4-φ8mm, open area ratio 3%-8%. Specific values ​​are determined through hydraulic calculations based on the tower diameter, packing type, and minimum wetting load. For Mellapak 350Y packing (specific surface area 350m²),... 2 / m 3 The recommended aperture is φ6mm and the opening ratio is 5% as the baseline design value. In practical applications, it can be finely adjusted according to the surface tension of the material (which affects the orifice flow coefficient). For materials with low surface tension (<20mN / m), the aperture or opening ratio can be appropriately reduced, while for materials with high surface tension (>40mN / m), it can be appropriately increased.

[0041] 5. Gas phase flow rate regulation and gas-liquid synergy This invention adds a gas phase conditioning mechanism, linked to the differential spindle 500, to the common space at the bottom of the tower directly below the partition 101. The specific structure of this mechanism is as follows: (1) Tower bottom partition plate 8: A tower bottom partition plate 8 is installed in the common space at the bottom of the tower below the partition plate 101. The tower bottom partition plate 8 divides the rising steam inlet at the bottom of the tower into two channels, which correspond to the left packing area 102 and the right packing area 103, respectively.

[0042] (2) Gas phase distribution cylinder: A left gas phase distribution cylinder 701 and a right gas phase distribution cylinder 702 are installed above the bottom partition plate 8 of the tower. Both are hollow cylindrical structures. The left gas phase distribution cylinder 701 is connected to the bottom of the left packing area 102, and the right gas phase distribution cylinder 702 is connected to the bottom of the right packing area 103. The gas phase distribution cylinder occupies a height of about 300-500 mm in the common space at the bottom of the tower.

[0043] (3) Valve adjustment mechanism: A left valve 705 is installed inside the left gas phase distribution cylinder 701, and a right valve 706 is installed inside the right gas phase distribution cylinder 702, to control the gas passage area leading to the packing zones on both sides respectively. Both the left valve 705 and the right valve 706 are square valves with a thickness of 5-10mm, made of 316L stainless steel or Hastelloy, and the valve area matches the cross-sectional area of ​​the gas passage inside the cylinder. The rotation angle of the valve around the axis is 0°-90°, corresponding to the gas passage from fully closed to fully open.

[0044] (4) Mechanical transmission components: In addition to connecting the sleeve-type flow damper 203, the lower end of the differential spindle 500 is also rigidly connected to a vertical connecting rod. The vertical connecting rod descends along the center line of the tower or near the partition, passes through the bottom of the common liquid redistribution collection tank 200 (with a bellows dynamic seal), and descends to the gas phase distribution cylinder below the partition. A vertical connecting rod rack 707 is fixed at the lower end of the vertical connecting rod.

[0045] The left drive gear 708 meshes with the vertical connecting rod rack 707 and is fixed to the rotating end of the left valve plate 705; the right drive gear 709 meshes with the vertical connecting rod rack 707 and is fixed to the rotating end of the right valve plate 706. The meshing phases of the left drive gear 708 and the right drive gear 709 are opposite, so that the unidirectional movement of the vertical connecting rod rack 707 drives the two valve plates to rotate synchronously in opposite directions.

[0046] (5) Gas distributor: A left gas distributor 703 and a right gas distributor 704 are respectively installed above the left gas phase distribution cylinder 701 and the right gas phase distribution cylinder 702. The gas distributor includes a gas pre-distribution plate (perforated plate or grid structure) and a flow guide baffle, which are used to evenly distribute the gas after valve adjustment to the bottom section of the packing layer 9 in the corresponding packing area. The gas pre-distribution plate is a perforated plate structure with evenly distributed circular through holes arranged in an equilateral triangle. To achieve the low pressure drop target of 0.1-0.2 kPa, the opening ratio of the gas pre-distribution plate should be controlled between 40% and 60% (preferably 50%), the hole diameter is φ10-φ20 mm (preferably φ15 mm), and the plate thickness is 2-4 mm. The flow guide baffle is set above the pre-distribution plate to guide the airflow to the bottom section of the corresponding packing area. A flow divider blade can be set at the outlet of the flow guide baffle to further improve the uniformity of gas distribution.

[0047] The above design parameters are determined based on the following: The pressure drop of the gas distributor is mainly caused by the local resistance of the pre-distribution plate orifice, according to the orifice resistance formula ΔP=ξ·(ρu 2 / 2) Calculation, where ξ is the resistance coefficient (related to the opening ratio and orifice shape; ξ≈1.5-2.5 when the opening ratio is 50%), ρ is the gas density, and u is the orifice velocity. Under the conditions of 50% opening ratio and φ15mm orifice diameter, for an atmospheric pressure distillation column (gas density ρ≈1.2-3.0kg / m³), 3 When the orifice gas velocity is controlled at 5-10 m / s, the pressure drop can be controlled within the range of 0.1-0.2 kPa. During the design, the pressure drop should be controlled within this range by adjusting the porosity and pore size according to the specific gas density and operating gas velocity of the system—the porosity should be appropriately increased when the gas density is high, and appropriately decreased when the gas density is low.

[0048] The driving principle of the entire gas phase conditioning mechanism is as follows: When the pressure drop of the packing layer 9 in the left packing zone 102 increases and the differential spindle 500 moves downward: The vertical link then moves downwards; The vertical connecting rod rack 707 moves downward; The left drive gear 708 (meshing with the left tooth surface of the vertical connecting rod rack 707) rotates clockwise, causing the left valve plate 705 to swing toward the center of the channel—closing the left gas phase channel; The right-side drive gear 709 (meshing with the right-side tooth surface of the vertical connecting rod rack 707) rotates counterclockwise, causing the right-side valve plate 706 to swing outward of the channel—opening the right-side gas phase channel; Result: The gas flow rate to the left packing zone 102 decreased, while the gas flow rate to the right packing zone 103 increased.

[0049] 6. Complete closed-loop working process Step 1: The system is operating in a steady state with stable feeding and normal pressure drop in the left packing layer 9. The differential spindle 500 is in a force balance position, and the sleeve-type flow damper 203, left and right valve plates 705, and right valve plate 706 are all at their designed openings.

[0050] Step 2: The feed rate suddenly increases, the liquid load of the packing layer 9 in the left packing zone 102 increases, the liquid holdup increases, the gas phase channel narrows, and the pressure drop of the left packing layer 9 increases.

[0051] Step 3: The high-pressure isolation diaphragm box 301 and the low-pressure isolation diaphragm box 302 capture the pressure difference change and transmit it to the upper bellows 401 and the lower bellows 402 through the double capillary tube 303, driving the differential spindle 500 to move downward.

[0052] Step Four: Liquid phase adjustment: The main shaft moves down → the sleeve-type flow-blocking gate 203 moves down → the flow area of ​​the left V-shaped opening weir plate 202 decreases → the liquid inflow on the left decreases → the liquid level in the collection tank rises → excess liquid overflows to the right packing area 103 and falls to the top of the packing layer 9 in this area.

[0053] Gas phase adjustment: The main shaft moves down → the vertical connecting rod and vertical connecting rod rack 707 move down → the left drive gear 708 rotates clockwise → the left valve plate 705 closes slightly (left side air intake decreases); the right drive gear 709 rotates counterclockwise → the right valve plate 706 opens wider (right side air intake increases).

[0054] Step 5: Left side: Reduced liquid intake + reduced gas intake → Packing layer 9 provides dual relief from flooding tendency and restores gas phase channels.

[0055] Right side: Increased liquid inlet (overflow) + increased air inlet (valve opening wide) → Packing layer 9 absorbs excess gas-liquid phase load.

[0056] Step 6: The pressure drop of the left packing layer 9 falls back, the differential spindle 500 rises under the action of the linear return spring 700, the gas-liquid phase adjustment mechanism synchronously returns to the new equilibrium position, and the system reaches steady state under the new operating conditions.

[0057] The aforementioned 40%-70% margin range is derived from conventional distillation column design principles. The lower limit of 40% is set based on the fact that when the adjustment margin is lower than this value, the effective adjustment stroke of the left-side V-shaped opening weir plate 202 is too short, which cannot provide sufficient liquid phase transfer capacity to suppress large feed fluctuations. The upper limit of 70% is set based on the fact that when the adjustment margin is higher than this value, the reference spray volume provided by the constant flow underflow plate will be lower than the minimum wetting load requirement of commonly used structured packing, which poses a risk of localized drying of the packing.

[0058] II. Experimental Preparation and Testing Methods 1. Experimental equipment and boundary conditions A stainless steel (316L) distillation column with an inner diameter of DN300 is used. Both the left-side packing zone 102 and the right-side packing zone 103 are filled with packing layer 9, each 8.0m high, using Mellapak 350Y structured packing (specific surface area 350m²). 2 / m 3 The top condenser uses 30°C circulating cooling water, and the bottom reboiler is heated by steam.

[0059] Applicable material boundary conditions: The feed system is a pure gas-liquid two-phase system, free from easily crystallizing inorganic salts and a large number of suspended solid particles (TSS≤20ppm); the liquid phase material exhibits low viscosity Newtonian fluid characteristics at the operating temperature (dynamic viscosity≤5.0mPa·s).

[0060] 2. Testing Methods (1) Product purity test: After steady-state operation, samples were taken from the side sampling outlet at regular intervals, and the purity of the target component was analyzed using an Agilent 7890B gas chromatograph (FID detector, area normalization method).

[0061] (2) Pressure drop fluctuation test: A Rosemount 3051 high-frequency differential pressure transmitter (for monitoring only, not for control) is connected in parallel. The pressure drop of the packing layer 9 in the left packing area 102 is recorded at a sampling rate of 100Hz. The difference between the maximum and minimum values ​​during the steady state or the disturbance transition period is taken as the pressure drop fluctuation range.

[0062] (3) System oscillation frequency: The differential spindle is monitored by a laser displacement sensor. An oscillation is recorded as 1.5 mm when the amplitude exceeds 5% of the full scale (30 mm). The micro-motion is not included.

[0063] All tests were performed in three independent parallel experiments, and the data were taken as the arithmetic mean (RSD < 0.5%).

[0064] Example 1 Separation system: benzene (light) / toluene (middle, target product) / xylene (heavy), mass ratio 30:40:30.

[0065] Process conditions: atmospheric pressure operation, feed flow rate 1000 kg / h, reflux ratio R=3.0.

[0066] Disturbance test: After stabilization, a step disturbance with a sudden increase of 15% in feed flow rate is introduced.

[0067] Operating Results: The differential spindle 500 moved downwards, and the liquid phase conditioning component and the newly added gas phase conditioning mechanism operated synchronously—the flow area of ​​the left V-shaped weir plate 202 decreased, the left valve plate 705 closed synchronously, and the right valve plate 706 opened synchronously. A new equilibrium was established in approximately 3.2 minutes. The side-stream product, toluene, had a purity of 99.6%, a pressure drop fluctuation range of 0.38 kPa, an oscillation frequency of <1 time / hour, and no flooding occurred. Compared with the original scheme without the added gas phase conditioning mechanism, the equilibrium establishment time was shortened by approximately 29%, and the pressure drop fluctuation range was reduced by approximately 16%.

[0068] Example 2 Separation system: n-hexane / n-heptane (target product) / n-octane, mass ratio 25:50:25.

[0069] Process conditions: Slight positive pressure operation (0.2MPa at the top of the tower), feed flow rate 1500kg / h.

[0070] Disturbance test: The feed temperature suddenly dropped by 15°C, and the condensation load in the tower increased, showing signs of primary flooding.

[0071] Operating results: The differential spindle moved down 500°, and the gas-liquid phase coordinated regulation acted simultaneously. A new equilibrium was established in approximately 4.0 minutes. The purity of the n-heptane in the side stream was 99.4%, and the pressure drop fluctuation range was 0.43 kPa.

[0072] Example 3 Separation system: methanol / ethanol (target product) / n-propanol, initial mass ratio 30:40:30.

[0073] Process conditions: Atmospheric pressure operation, feed flow rate 800 kg / h.

[0074] Disturbance test: Dramatic fluctuations in feed composition (ethanol increased from 40% to 60%, methanol decreased to 20%) caused significant changes in the physical properties and temperature distribution within the tower.

[0075] Operating results: Thanks to the common mode cancellation design of the double bellows and the coordinated regulation of the gas and liquid phases, the system was not affected by thermal expansion caused by local temperature changes. The purity of the side-stream product was 99.5%, and the pressure drop fluctuation range was 0.40 kPa.

[0076] Example 4 Separation system: isopentane / n-pentane (target product) / cyclopentane, mass ratio 20:50:30.

[0077] Process conditions: atmospheric pressure operation, feed flow rate 800 kg / h, and reflux ratio set to R=5.4 due to relatively low volatility.

[0078] Disturbance test: Introduce continuous sinusoidal feed wave fluctuations with an amplitude of ±10%.

[0079] Operating results: The damping system exhibited strong filtering characteristics, with the valve plate maintaining a slight follow-up position corresponding to the average pressure difference without fatigue overshoot. Side-line purity was 99.1%, and the pressure drop fluctuation range was 0.48 kPa.

[0080] Example 5 Separation system: acetone / isopropanol (target product) / n-butanol, mass ratio 33.3:33.4:33.3.

[0081] Process conditions: Reduced pressure operation (absolute pressure at the top of the tower 50 kPa), feed flow rate 1200 kg / h.

[0082] Disturbance test: Simulates combined extreme working conditions, with a sudden increase of 25% in feed rate and a reboiler steam pressure fluctuation of ±5%.

[0083] Operating results: The system maintained normal operation under negative pressure and combined disturbances, and equilibrium was established in approximately 4.5 minutes. The side-line purity was 99.3%, and the pressure drop fluctuation range was 0.52 kPa.

[0084] Example 6 Example 1 was placed in a simulated environment test chamber for a -30℃ to 70℃ (extreme cold and intense sunlight day and night) cycle test.

[0085] Tests show that using parallel double capillary tubes of equal length results in a small static zero-point drift of the main shaft. The preferred coaxial nested sleeve structure (high pressure inside the inner tube and low pressure outside the outer tube) can further eliminate the slight thermal resistance difference between the parallel tubes, significantly reducing the static zero-point drift and demonstrating excellent temperature common-mode suppression effect.

[0086] Viscosity selection tests were conducted on damping silicone oils, with the preferred oils selected within the 100-1000 cSt range. Testing revealed that the optimal solution was a vacuum-degassed dimethyl silicone oil with a kinematic viscosity of 350 cSt at 25°C, which achieved the best balance between damping effect and response speed. The silicone oil required vacuum degassing to remove dissolved gases, ensuring the stability and repeatability of its damping characteristics.

[0087] Comparative Example 1 The mechanical device of this invention was removed, and PID control was performed using a DCS combined with an electronic differential pressure transmitter and a pneumatic regulating valve. After tuning the optimal parameters, a test was conducted with a sudden 15% increase in feed.

[0088] Operating results: Due to the delay in the instrument air supply and the static friction of the valve stem, the regulation was lagging and overshoot oscillations occurred (3-4 times / hour). The purity of the side line barely met the standard (98.5%), but the pressure drop fluctuation was as high as 1.85 kPa.

[0089] Comparative Example 2 Remove the lower corrugated tube and low-pressure capillary tube from this invention.

[0090] Operating results: The pressure-transmitting working fluid expands due to heat, generating a unidirectional false thrust, which leads to inaccurate distribution, causing the purity of the side line to drop to 96.2%, and the pressure drop fluctuation range to 3.10 kPa.

[0091] Comparative Example 3 Remove the damping hydraulic cylinder body and damping piston.

[0092] Operating results: The gate and valve plate experienced severe high-frequency flutter (>50 times / hour) due to the high-frequency bubble pulsation in the tower, resulting in uncontrolled distribution, pressure drop fluctuations of up to 4.50 kPa, and purity dropping to 94.8%.

[0093] Comparative Example 4 It adopts a traditional static trough distributor with a fixed ratio and has no gas phase adjustment mechanism.

[0094] Operating results: After the introduction of a sudden 15% disturbance, the gas-liquid ratio was severely imbalanced, and severe flooding (flooding) occurred on the left side. The pressure drop surged to 8.90 kPa, and the purity of the side stream dropped to 88.5%.

[0095] Comparative Example 5 The experiment employed liquid-phase conditioning only, without a gas-phase conditioning mechanism, and was tested under a 15% sudden increase in feed disturbance.

[0096] Results: The system can alleviate flooding through liquid phase conditioning, but the response speed is slow, with an equilibrium establishment time of approximately 4.5 minutes. The sidestream product purity is 99.4%, and the pressure drop fluctuation range is 0.45 kPa. In contrast, Example 1, with the addition of a gas phase conditioning mechanism, has an equilibrium establishment time reduced to 3.2 minutes (an improvement of approximately 29%), a pressure drop fluctuation range reduced to 0.38 kPa (a reduction of approximately 16%), and a purity increased to 99.6%. This fully demonstrates the significant advantages of gas-liquid synergistic conditioning over single liquid phase conditioning in terms of response speed and stability.

[0097] The test results of Examples 1-5 and Comparative Examples 1-5 are summarized in Table 1.

[0098] Table 1 Test results of Examples 1-5 and Comparative Examples 1-5

[0099] Note: Micro-adjustment amplitude <1.5mm is not included in the oscillation frequency.

[0100] As shown in Table 1, compared with Comparative Example 1, the electronic-pneumatic control system of Comparative Example 1 can respond, but due to the inherent signal transmission delay and actuator friction of the system, a voltage drop fluctuation of 1.85 kPa and overshoot oscillation are generated; while Example 1 adopts a pure physical mechanical structure direct connection, realizing true zero-delay smooth servo, and the voltage drop fluctuation range is only 0.38 kPa.

[0101] Compared with Comparative Example 1 and Comparative Example 5, after adding a gas phase regulation mechanism, the equilibrium establishment time under the same disturbance was shortened from 4.5 minutes to 3.2 minutes, the pressure drop fluctuation range was reduced from 0.45 kPa to 0.38 kPa, and the product purity was increased from 99.4% to 99.6%. This shows that gas-liquid synergistic regulation has a faster response speed and stronger anti-disturbance capability compared with single liquid phase regulation.

[0102] In Comparative Example 2, the lack of a common-mode cancellation mechanism in the lower bellows caused the working fluid to expand due to ambient temperature fluctuations, generating false mechanical thrust and resulting in a purity drop to 96.2%. In contrast, in Example 3, when drastic fluctuations caused local temperature abrupt changes, the symmetrical mechanical structure of the double bellows completely filtered out the temperature drift signal, maintaining a high purity of 99.5%.

[0103] Comparative Example 3 lacks a damping system, resulting in severe high-frequency mechanical flutter when faced with high-frequency pulsations of the gas phase inside the tower. This not only disrupts the flow field and causes significant pressure drop fluctuations but also poses a risk of equipment fatigue damage. In Embodiment 4 of the present invention, when faced with continuous sinusoidal interference, the damping cylinder effectively filters out high-frequency noise, and the main shaft maintains only stable follow-up, demonstrating better low-pass filtering and disturbance rejection performance.

[0104] Comparative Example 4 uses a traditional static distributor, which is completely unable to cope with sudden increases in feed, resulting in severe flooding on the left side and complete separation failure. Examples 1-5 of this invention can automatically reconstruct the gas-liquid phase ratio based on pressure difference changes, avoiding flow deviation and flooding, and significantly expanding the operating boundaries of the baffle column.

Claims

1. A thermally coupled baffle-type high-efficiency separation distillation column, comprising a distillation column (100), wherein a baffle (101) is provided in the middle section of the distillation column (100), the baffle (101) dividing the middle part of the column body into a left packing zone (102) and a right packing zone (103), and a common liquid redistribution collection tank (200) is provided in the top space above the baffle (101); characterized in that, Also includes: Pressure sensing components are respectively disposed at the bottom and top of the left filler area (102) to acquire pressure signals at both ends of the area; A pressure isolation remote transmission component is connected to the pressure sensing component and is used to transmit the pressure signal; The differential pressure mechanical conversion center is connected to the pressure isolation remote transmission component and is used to convert the two pressure signals into a net pressure difference and drive the differential spindle (500) to generate mechanical displacement. An adjustment component is provided at the left outlet of the common liquid redistribution collection tank (200) and connected to the differential spindle (500) to adjust the flow area of ​​the left outlet in response to the displacement of the differential spindle (500). A gas phase adjustment mechanism is located in the common space at the bottom of the tower below the partition (101) and is connected to the differential spindle (500) via a mechanical transmission assembly. It is used to respond to the displacement of the differential spindle (500) to synchronously adjust the gas phase flow rate to the left packing zone (102) and the right packing zone (103).

2. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 1, characterized in that, The pressure sensing component includes a high-pressure isolation diaphragm box (301) installed at the bottom of the left filling area (102) and a low-pressure isolation diaphragm box (302) installed at the top; the pressure isolation remote transmission component includes a high-pressure capillary tube (3031) and a low-pressure capillary tube (3032) respectively connected to the high-pressure isolation diaphragm box (301) and the low-pressure isolation diaphragm box (302), and the tubes are filled with high-temperature silicone oil; the left filling area (102) and the right filling area (103) are both filled with a packing layer (9).

3. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 2, characterized in that, The high-pressure capillary tube (3031) and the low-pressure capillary tube (3032) are laid in parallel with equal physical unfolded lengths and placed in the same heat-tracing and insulation layer; or, a coaxial nested structure is adopted with the high-pressure capillary tube (3031) as the inner tube and the low-pressure capillary tube (3032) as the outer tube.

4. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 2, characterized in that, The differential pressure mechanical conversion hub includes a rigid fixed support (400), and the support is provided with an upper corrugated pipe (401) and a lower corrugated pipe (402) with equal effective pressure areas and arranged opposite each other. The upper corrugated pipe (401) and the lower corrugated pipe (402) are respectively connected to a high-pressure capillary (3031) and a low-pressure capillary (3032). The differential spindle (500) is connected in series between the two.

5. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 4, characterized in that, The differential pressure mechanical conversion center also includes: A linear return spring (700) is sleeved on the differential spindle (500) and has an initial preload force to counteract the net bias force generated by the height difference of the working fluid static column in the high-pressure capillary tube (3031) and the low-pressure capillary tube (3032), thereby realizing the physical zeroing of the differential spindle (500). The mechanical filter structure includes a damping hydraulic cylinder (601) fixed on a rigid fixed bracket (400) and a damping piston (602) fixed on a differential spindle (500). The damping hydraulic cylinder (601) is filled with damping silicone oil, and the damping piston (602) is provided with a micro throttling orifice (603).

6. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 1, characterized in that, The regulating component includes a left V-shaped opening weir plate (202) fixed to the bottom left side of the common liquid redistribution collection tank (200), and a sleeve-type flow-blocking gate plate (203) that slides up and down close to the V-shaped opening weir plate. The sleeve-type flow-blocking gate plate (203) is rigidly connected to the differential main shaft (500). A right overflow weir (201) is provided on the right side of the common liquid redistribution collection tank (200), and the top elevation of the right overflow weir (201) is higher than the bottom elevation of the left outlet.

7. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 1, characterized in that, The gas phase conditioning mechanism includes: The left gas phase distribution cylinder (701) and the right gas phase distribution cylinder (702) are located in the public space at the bottom of the tower. A left valve plate (705) and a right valve plate (706) are respectively installed in the left gas phase distribution cylinder (701) and the right gas phase distribution cylinder (702). And a mechanical transmission assembly connecting the differential spindle (500) with the left valve plate (705) and the right valve plate (706); When the differential spindle (500) moves down, the mechanical transmission assembly drives the left valve plate (705) to close the gas passage to the left packing area (102) and at the same time drives the right valve plate (706) to open the gas passage to the right packing area (103).

8. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 7, characterized in that, The mechanical transmission assembly includes a vertical connecting rod rigidly connected to the lower end of the differential spindle (500), a vertical connecting rod rack (707) fixed to the lower end of the vertical connecting rod, and a left drive gear (708) and a right drive gear (709) meshing with the vertical connecting rod rack (707); the left drive gear (708) is fixed to the shaft end of the left valve plate (705), and the right drive gear (709) is fixed to the shaft end of the right valve plate (706); the meshing phases of the left drive gear (708) and the right drive gear (709) are opposite; a left gas distributor (703) and a right gas distributor (704) are respectively provided above the left gas distribution cylinder (701) and the right gas distribution cylinder (702), and the pressure drop of the left gas distributor (703) and the right gas distributor (704) is controlled within the range of 0.1-0.2 kPa.

9. The thermally coupled baffle-type high-efficiency separation distillation column according to claim 7, characterized in that, The left gas distribution cylinder (701) and the right gas distribution cylinder (702) are respectively provided with a left gas distributor (703) and a right gas distributor (704); a bottom partition plate (8) is provided below the gas distribution cylinder, which divides the bottom rising steam inlet of the tower into two channels, left and right.

10. A separation process using the thermally coupled baffle-type high-efficiency separation distillation column according to any one of claims 1-9, characterized in that, Includes the following steps: S1: The condensate at the top of the tower falls back into the common liquid redistribution collection tank (200), part of which enters the left packing zone (102) and the other part enters the right packing zone (103). S2: The pressure sensing component captures the pressure signals at both ends of the left packing area (102) in real time, and transmits them to the differential pressure mechanical conversion center through the pressure isolation remote transmission component; S3: When the pressure drop in the left packing area (102) increases, the differential pressure mechanical conversion center drives the differential main shaft (500) to move downward; S4: When the differential spindle (500) moves downward, liquid phase conditioning and gas phase conditioning are performed simultaneously. Liquid phase adjustment: The adjustment component reduces the flow area of ​​the liquid outlet on the left, the liquid level in the collection tank rises, and excess liquid overflows to the packing area on the right (103). Gas phase conditioning: The gas phase conditioning mechanism reduces the gas flow rate to the left packing zone (102) while increasing the gas flow rate to the right packing zone (103); S5: The pressure drop in the left packing area (102) drops back, and the system reaches a steady state at a new equilibrium point.

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