Stable tower coupling enhanced separation device and separation method

Abstract

The present application relates to the field of petrochemical separation, and discloses a stable column coupling enhanced separation device and a separation method, wherein the stable column coupling enhanced separation device comprises a stable column, a vortex tube module, the vortex tube module is composed of a plurality of vortex tube units in series, each vortex tube unit is composed of a plurality of vortex tubes in parallel, the vortex tube unit is provided with a feed pipe and a cold gas collecting pipe, the feed pipe is communicated with the feed end of the plurality of vortex tubes, the cold gas end of the plurality of vortex tubes is communicated with the cold gas collecting pipe, the cold gas collecting pipe of the vortex tube unit is communicated with the feed pipe of the next vortex tube unit in series, the vortex tube module is provided with a hot discharge pipe and a cold discharge pipe, the hot gas end of each vortex tube is communicated with the hot discharge pipe, and the cold discharge pipe is communicated with the stable column. By introducing the vortex tube module composed of a multi-stage series and parallel structure into the stable column, the energy consumption of the system is effectively reduced.

Description

Technical Field

[0001] This invention relates to the technical field of petrochemical separation, and in particular to a stabilizer tower coupled enhanced separation device and separation method. Background Technology

[0002] Absorption stabilization systems are widely used in petrochemical complexes, primarily for separating superheated steam streams generated by catalytic cracking units to obtain products such as dry gas, liquefied petroleum gas (LPG, C3-C4 components), and stabilized gasoline (C5+ components). Traditional absorption stabilization systems typically consist of multiple tower units, including an absorber, reabsorber, desorber, and stabilizer. Their complex processes and numerous components result in a high proportion of overall energy consumption in refining units, with the reboiling and condensation processes in the stabilizer tower being particularly demanding. In recent years, with the widespread application of new catalytic cracking processes such as high-efficiency catalytic cracking of heavy oil, the generation of C3-C4 light hydrocarbons in these units has significantly increased, leading to a continuous increase in the processing load of absorption stabilization systems and further amplifying the heat demand of the stabilizer towers. Against the backdrop of continuously rising energy prices and the "dual carbon" target (carbon diversification and carbon emission reduction), effectively reducing the overall energy consumption of absorption stabilization systems, especially the stabilizer tower unit, while ensuring product separation targets has become a critical technical issue that the petrochemical industry urgently needs to address.

[0003] To address the aforementioned issues, various energy-saving optimization schemes for absorption stabilization systems have been proposed in existing technologies. For example, some studies have introduced flash tanks into the gasoline absorption stabilization process and optimized the absorbent composition, thereby reducing system operating costs to some extent. Other literature combines process simulation and pinch analysis methods to modify the absorption stabilization system through process modification and thermal integration optimization, proposing to improve waste heat recovery efficiency by improving the condensation structure. Furthermore, in terms of optimizing operating conditions, related studies have systematically analyzed the influence of parameters such as tower operating pressure, absorbent circulation rate, and feed conditions on system energy consumption, achieving a certain degree of thermal energy saving through parameter adjustments. However, most existing energy-saving technologies focus on structural improvements and operating parameter optimization of single towers or local units, and their optimization approaches remain limited to the traditional framework of heat exchange and phase balance control. While these schemes have achieved some results in local energy saving, they generally suffer from the following shortcomings: on the one hand, they lack fundamental means to strengthen the energy-mass separation process of the stabilization tower, a high-energy-consuming core unit; on the other hand, they have not fully explored the technological potential of deeply coupling the stabilization tower with other non-traditional separation units to achieve system-level synergistic energy reduction. Therefore, existing absorption stabilization systems still have significant technical limitations and considerable room for improvement in reducing overall energy consumption.

[0004] Therefore, there is an urgent need for a new type of separation device and method that can enhance the stabilization tower separation process without significantly increasing system complexity and additional power consumption, and effectively couple it with the existing process, so as to meet the technical requirements of energy saving and consumption reduction of the absorption stabilization system under the current high load operation conditions. Summary of the Invention

[0005] The technical problem to be solved by this invention is to address the high overall energy consumption of the absorption stabilization system.

[0006] To address the aforementioned technical problems, this invention provides a stabilized tower coupling enhanced separation device, comprising: a stabilized tower; a vortex tube module, wherein the vortex tube module is composed of multiple vortex tube units connected in series, each vortex tube unit is composed of multiple vortex tubes connected in parallel, each vortex tube unit is provided with a feed pipe and a cold gas collecting pipe, the feed pipe being connected to the feed ends of the multiple vortex tubes, the cold gas ends of the multiple vortex tubes being connected to the cold gas collecting pipe, and the cold gas collecting pipe of the vortex tube unit being connected to the feed pipe of the next vortex tube unit connected in series; the vortex tube module is provided with a hot discharge pipe and a cold discharge pipe, the hot gas end of each vortex tube being connected to the hot discharge pipe, the cold discharge pipe being the cold gas collecting pipe of the vortex tube unit located at the end of the series connection, the cold discharge pipe being connected to the stabilized tower, and the vortex tube module being used for energy and mass separation of the raw material entering the stabilized tower or the overhead gas flow of the stabilized tower.

[0007] Furthermore, it also includes a feed flash tank, the input pipe of which is equipped with a feed heat exchanger, the gas output end of which is connected to the input end of the vortex tube module, the liquid output end of which is connected to the stabilizer tower, and both the hot discharge pipe and the cold discharge pipe are connected to the stabilizer tower.

[0008] Furthermore, the upper part of the stabilizing tower and the lower part of the stabilizing tower are respectively provided with an upper feed port and two lower feed ports. The liquid output end of the feed flash tank and the hot discharge pipe are respectively connected to the two lower feed ports, and the cold discharge pipe is connected to the upper feed port.

[0009] Furthermore, the liquid output end of the feed flash tank is connected to the feed inlet of the stabilizer tower body through a first pipeline, the first pipeline being equipped with a flow regulating valve. The gas output end of the feed flash tank is connected to the input end of the vortex tube module through a second pipeline, the second pipeline being equipped with a pressure monitoring instrument.

[0010] Furthermore, it also includes a condenser, a reflux tank, and a first reflux pump. The top of the stabilizer tower, the condenser, the reflux tank, and the first reflux pump are connected in sequence by pipelines. The reflux end of the first reflux pump is connected to the top of the stabilizer tower. The first reflux pump is provided with a product output pipeline for outputting liquefied petroleum gas.

[0011] Furthermore, the feed pipe is equipped with a separator, the cold air collection pipe is equipped with a mixer, and both the hot discharge pipe and the cold discharge pipe are equipped with pressure monitoring instruments.

[0012] Furthermore, each of the vortex tubes is provided with a throttle valve at its inlet end, which is used to regulate the feed flow rate and pressure of a single vortex tube.

[0013] Furthermore, it also includes a first cooler, a second cooler, a reflux tank, a first reflux pump, a second reflux pump, and a buffer tank. The top of the stabilizing tower is connected to the input end of the vortex tube module. The cold discharge pipe, the first cooler, the reflux tank, and the first reflux pump are connected in sequence through pipes. The reflux end of the first reflux pump is connected to the top of the stabilizing tower. The first reflux pump is equipped with a product output pipe for outputting liquefied petroleum gas. The hot discharge pipe, the second cooler, the buffer tank, the second reflux pump, and the top of the stabilizing tower are connected in sequence through pipes.

[0014] This invention also provides a stabilizer tower coupled enhanced separation method, employing the aforementioned stabilizer tower coupled enhanced separation device. The method includes: a mixture of liquefied petroleum gas (LPG) and stabilized gasoline undergoes heat exchange in the feed heat exchanger; the heat-exchanged mixture enters a feed flash tank for flash separation at a preset temperature and pressure to obtain a flash vapor phase and a flash liquid phase; the flash vapor phase enters the vortex tube module for energy-mass separation, resulting in a cold gas stream and a hot gas stream; the cold gas stream is fed into the feed inlet at the top of the stabilizer tower through the cold discharge pipe, and the hot gas stream is fed into the feed inlet at the bottom of the stabilizer tower through the hot discharge pipe; the flash liquid phase enters the feed inlet at the bottom of the stabilizer tower; the vapor phase at the top of the stabilizer tower is condensed and output as LPG product, and the stabilized gasoline product is output from the bottom of the stabilizer tower.

[0015] This invention also provides a stabilizer tower coupling enhanced separation method, employing the aforementioned stabilizer tower coupling enhanced separation device. The method includes: a mixture of liquefied petroleum gas (LPG) and stabilized gasoline feedstock directly enters the stabilizer tower; the gas phase at the top of the stabilizer tower enters the vortex tube module, and a cold discharge pipe outputs a cold gas stream, while a hot discharge pipe outputs a hot gas stream; the cold gas stream is cooled to a preset temperature by a first cooler and then enters a first reflux pump; one output end of the first reflux pump outputs LPG product, and the other output end of the first reflux pump inputs the cold gas stream into the stabilizer tower; the hot gas stream is cooled to a preset temperature by a second cooler and then returns to the top of the stabilizer tower via a buffer tank and the second reflux pump; stabilized gasoline product is output from the bottom of the stabilizer tower.

[0016] Compared with existing technologies, the beneficial effects of the stabilized tower coupling enhanced separation device of this invention are as follows: By introducing a vortex tube module composed of multi-stage series and single-stage parallel structures into the gas phase loop at the front end or top of the stabilized tower, the high-pressure mixed fluid entering the separation device can enter the vortex tube tangentially under its own pressure without external power, forming a high-speed rotating strong vortex field. Under the combined action of centrifugal force, radial pressure gradient, and axial backflow, significant differences in energy and component distribution are generated inside the fluid. The high-temperature, high-enthalpy, and high-density heavy components tend to move towards the tube wall region and are discharged along the outer vortex direction, forming a hot gas flow, while the low-temperature, low-enthalpy, and low-density light components gather towards the tube axis center and are discharged with the inner vortex, forming a cold gas flow. Through the series arrangement of multiple vortex tube units, the previous stage separation... The cooled airflow then enters the next stage of the vortex tube, achieving a step-by-step amplification of the energy-mass separation effect while maintaining fluid momentum and pressure gradient. This results in a more significant overall temperature drop and component enrichment. The parallel structure of multiple vortex tubes within a single stage effectively distributes the flow rate and reduces the load on individual tubes, ensuring stable swirling intensity and separation efficiency even under high-volume processing conditions. The material after the above energy-mass pre-separation then enters the stabilizer, optimizing the vapor-liquid balance conditions within the tower. This reduces the repeated vaporization and condensation of light components within the tower, significantly reducing the heat load on the reboiler and condensation system. Without altering the main structure of the stabilizer, the separation process is fundamentally enhanced, effectively reducing the overall energy consumption of the absorption stabilization system, improving separation efficiency and operational flexibility. This demonstrates excellent engineering adaptability and energy-saving application value. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the vortex tube module of the stabilizing tower coupling enhancement separation device provided by the present invention;

[0018] Figure 2 This is a process flow diagram of the stabilizer tower coupling enhancement separation device provided in Embodiment 1 of the present invention;

[0019] Figure 3 This is a process flow diagram of the stabilizing tower coupling enhancement separation device provided in Embodiment 2 of the present invention;

[0020] Figure 4 This is a flow chart of the conventional feed flash evaporation process for a stabilizer tower;

[0021] Figure 5 This is a flow chart of a conventional distillation mixing process in a stabilizer column;

[0022] Figure 6 This is a method for enhancing the separation of coupling in a stable tower, as provided in Embodiment 1 of the present invention;

[0023] Figure 7 This is a method for enhancing the separation of a stable tower coupling provided in Embodiment 2 of the present invention.

[0024] The correspondence between the reference numerals and the component names is as follows:

[0025] 1. Stabilizer; 11. Gasoline output pipe; 2. Vortex tube module; 21. Vortex tube unit; 211. Vortex tube; 212. Feed pipe; 213. Cold gas collection pipe; 22. Hot discharge pipe; 23. Cold discharge pipe; 3. Feed flash tank; 31. Feed heat exchanger; 301. Gas output end; 302. Liquid output end; 4. Condenser; 5. Reflux tank; 51. First reflux pump; 52. Second reflux pump; 6. Reboiler; 7. First cooler; 8. Second cooler; 9. Buffer tank. Detailed Implementation

[0026] The following description, in conjunction with the accompanying drawings, illustrates exemplary embodiments of the present invention, including various details to aid understanding. These details should be considered merely exemplary. Therefore, those skilled in the art will recognize that various changes and modifications can be made to the embodiments described herein without departing from the scope of the invention. Similarly, for clarity and brevity, descriptions of well-known functions and structures are omitted in the following description.

[0027] like Figures 1 to 5As shown in the figure, an embodiment of the present invention discloses a stabilizer tower coupling enhancement separation device, comprising: a stabilizer tower 1; a vortex tube module 2, wherein the vortex tube module 2 is composed of multiple vortex tube units 21 connected in series, and each vortex tube unit 21 is composed of multiple vortex tubes 211 connected in parallel. Each vortex tube unit 21 is provided with a feed pipe 212 and a cold gas collecting pipe 213. The feed pipe 212 is connected to the feed end of the multiple vortex tubes 211, and the cold gas ends of the multiple vortex tubes 211 are all connected to the cold gas collecting pipe 213. The cold gas collecting pipe 213 of 1 is connected to the feed pipe 212 of the next series-connected vortex tube unit 21; the vortex tube module 2 is provided with a hot discharge pipe 22 and a cold discharge pipe 23. The hot gas end of each vortex tube 211 is connected to the hot discharge pipe 22. The cold discharge pipe 23 is the cold gas collecting pipe 213 located at the end of the series-connected vortex tube unit 21. The cold discharge pipe 23 is connected to the stabilizer tower 1. The vortex tube module 2 is used to perform energy and mass separation on the raw material entering the stabilizer tower 1 or the top gas flow of the stabilizer tower 1.

[0028] The stabilized tower coupled enhanced separation device of this application introduces a vortex tube module 2, consisting of a multi-stage series and a single-stage parallel structure, into the gas phase loop at the front end or top of the stabilized tower 1. This allows the high-pressure mixed fluid entering the separation device to enter the vortex tube 211 tangentially under its own pressure without external power, forming a high-speed rotating strong vortex field. Under the combined action of centrifugal force, radial pressure gradient, and axial backflow, significant differences in energy and component distribution are generated within the fluid. The high-temperature, high-enthalpy, and high-density heavy components tend to move towards the tube wall region and are discharged along the outer vortex direction, forming a hot gas flow. Conversely, the low-temperature, low-enthalpy, and low-density light components gather towards the tube axis center and are discharged with the inner vortex, forming a cold gas flow. Through the series connection of multiple vortex tube units 21, the cold gas flow from the previous stage of separation further enters the next stage... The first-stage vortex tube 211, while maintaining fluid momentum and pressure gradient, achieves a step-by-step amplification of the energy-mass separation effect, thereby obtaining a more significant temperature drop and component enrichment effect overall. The parallel structure of multiple vortex tubes 211 within a single stage effectively distributes the flow rate and reduces the load on a single tube, ensuring stable swirling intensity and separation efficiency even under high-volume processing conditions. The material after the above-mentioned energy-mass pre-separation then enters the stabilizer tower 1, optimizing the vapor-liquid balance conditions within the tower, reducing the repeated vaporization and condensation processes of light components within the tower, and significantly reducing the heat load on the reboiler 6 and the condensation system. Without changing the main structure of the stabilizer tower 1, the separation process is essentially enhanced, thereby effectively reducing the overall energy consumption of the absorption stabilization system, improving separation efficiency and operational flexibility, and demonstrating good engineering adaptability and energy-saving application value.

[0029] The vortex tube module 2 of this application has significant advantages in terms of high economic efficiency, strong adaptability, and high process flexibility: its structure is simple and compact, it adopts a purely mechanical design and has no easily damaged parts, resulting in low investment cost, long service life, and extremely low operating and maintenance costs; at the same time, the number of vortex tube units connected in series and in parallel can be flexibly adjusted according to the raw material processing volume and separation accuracy requirements, the device has a compact structure, and is suitable for absorption stabilization systems of different scales and different separation accuracy requirements, especially suitable for operating conditions with high energy-saving requirements; in addition, the device can realize multiple process forms combining feed flash evaporation and vortex tube distillation, and can flexibly select the most suitable process scheme according to actual production conditions, thereby meeting diverse industrial application needs.

[0030] Specifically, the cold air ends of multiple scroll tubes 211 under the same scroll tube unit 21 are all connected to the cold air collection pipe 213. It should be noted that the scroll tube module 2, the scroll tube unit 21, and the scroll tube 211 all have an inlet end, a cold air outlet end, and a hot air outlet end; the input end of the scroll tube module 2 is the feed pipe 212 port of the first scroll tube unit 21, and the scroll tube module 2 has two output ends, namely the hot discharge pipe 22 and the cold discharge pipe 23.

[0031] Specifically, the number of vortex tube units 21 connected in series and the number of vortex tubes 211 connected in parallel in the vortex tube module 2 are selected according to the raw material processing volume. For example, according to the separation accuracy requirements, the number of vortex tube units 21 connected in series is 8.

[0032] like Figure 1 and Figure 2 As shown, in Embodiment 1 of the present invention, the stabilizer tower coupling enhanced separation device of this application further includes a feed flash tank 3. The input pipe of the feed flash tank 3 is provided with a feed heat exchanger 31. The gas output end 301 of the feed flash tank 3 is connected to the input end of the vortex tube module 2. The liquid output end 302 of the feed flash tank 3 is connected to the stabilizer tower 1. The hot discharge pipe 22 and the cold discharge pipe 23 are both connected to the stabilizer tower 1.

[0033] By installing a feed flash tank 3 on the feed side of stabilizer tower 1 and configuring a feed heat exchanger 31 on its input pipeline, the raw material is heated by heat exchange before entering stabilizer tower 1 and undergoes preliminary phase equilibrium separation in the flash tank. Some light components are pre-precipitated in gaseous form and directly enter vortex tube module 2 for further energy-mass separation, while the liquid phase enters stabilizer tower 1 with a lower content of light components, reducing the vaporization load of the feed to stabilizer tower 1 from the source. At the same time, the hot and cold gas streams separated by vortex tube module 2 are returned to the stabilizer tower 1 at different heat demand locations. This allows for the synergistic utilization of heat and cold within the tower, reducing ineffective energy consumption caused by repeated vaporization and condensation of light components. Through a multi-stage coupling structure involving feed heat exchange, flash pre-separation, and enhanced energy-mass separation via vortex tube 211, the feed state and mass transfer driving force of the stabilizer tower 1 are optimized as a whole. This further reduces the load on the reboiler 6 and condensation system without increasing additional power consumption, improving system energy utilization efficiency and operational stability. The overall energy-saving effect is more significant, making it suitable for in-depth energy-saving retrofitting of absorption stabilization systems under high-load conditions.

[0034] Specifically, the cold side channel of the feed heat exchanger 31 is connected to the raw material pipeline to be processed, and the hot side channel of the feed heat exchanger 31 is connected to the stable gasoline output pipeline at the bottom of the stabilizer tower 1. The stable gasoline output pipeline at the bottom of the stabilizer tower 1 is equipped with a feed flash tank 3.

[0035] like Figure 1 and Figure 2 As shown, in Embodiment 1 of the present invention, the upper part of the stabilizer tower 1 and the lower part of the stabilizer tower 1 are respectively provided with an upper feed port and two lower feed ports. The liquid output end 302 and the hot discharge pipe 22 of the feed flash tank 3 are respectively connected to the two lower feed ports, and the cold discharge pipe 23 is connected to the upper feed port.

[0036] By setting an upper feed inlet at the top of the stabilizer tower 1 and two lower feed inlets at the bottom, and introducing the liquid output end 302 of the feed flash tank 3 and the hot discharge pipe 22 of the vortex tube module 2 into the lower part of the stabilizer tower 1 respectively, while introducing the cold discharge pipe 23 obtained from the vortex tube module 2 into the upper part of the stabilizer tower 1, the streams with different temperatures, enthalpies, and component characteristics enter the tower at their thermodynamically optimal positions: the high-temperature, high-enthalpy streams rich in heavy components work synergistically with the reboiling zone in the lower part of the tower, enhancing the vaporization driving force and reducing the heating demand of the reboiler 6. The cold stream, which is low in temperature, low in enthalpy, and rich in light components, directly participates in the condensation and distillation process at the top of the column, reducing the condensation load at the top of the column and improving the separation conditions of light components. Through this arrangement of "staged feeding and heat utilization", the temperature gradient, gas-liquid load distribution and mass transfer driving force in the stabilizer column 1 are more reasonable, significantly reducing ineffective heat circulation and component backmixing in the column. Without increasing the system complexity and energy consumption, the separation efficiency and operational stability of the stabilizer column 1 are further improved, and the overall energy saving and consumption reduction effect is more prominent.

[0037] like Figure 1 and Figure 2 As shown, in Embodiment 1 of the present invention, the liquid output end 302 of the feed flash tank 3 is connected to the feed inlet of the stabilizer tower 1 through a first pipeline. The first pipeline is equipped with a flow regulating valve. The gas output end 301 of the feed flash tank 3 is connected to the input end of the vortex tube module 2 through a second pipeline. The second pipeline is equipped with a pressure monitoring instrument.

[0038] By introducing the liquid output end 302 of the feed flash tank 3 into the feed inlet of the stabilizer tower 1 through a first pipeline equipped with a flow regulating valve, the liquid feed rate into the stabilizer tower 1 can be finely controlled according to changes in the tower load, thereby stabilizing the risk of flooding in the tower 1 and optimizing the gas-liquid contact conditions. Simultaneously, the gas output end 301 of the feed flash tank 3 is introduced into the input end of the vortex tube module 2 through a second pipeline equipped with a pressure monitoring instrument, allowing for real-time monitoring and adjustment of the gas phase pressure entering the vortex tube 211. This ensures that the vortex tube 211 forms a stable vortex under suitable pressure differential conditions and maintains good energy-mass separation. Through the coordinated monitoring and adjustment of the liquid flow rate and gas phase pressure, the feed flash evaporation, vortex tube 211 separation, and stabilizer tower 1 distillation processes form a controllable and stable coupled operating state. This not only improves the system's operational safety and adaptability to different operating conditions but also ensures the long-term stable performance of the enhanced separation effect, providing strong support for overall energy saving and consumption reduction and reliable operation under high load conditions.

[0039] like Figure 1 and Figure 2 As shown, in Embodiment 1 of the present invention, the stabilizer tower coupling enhanced separation device of this application further includes a condenser 4, a reflux tank 5, and a first reflux pump 51. The top of the stabilizer tower 1, the condenser 4, the reflux tank 5, and the first reflux pump 51 are connected in sequence through pipelines. The reflux end of the first reflux pump 51 is connected to the top of the stabilizer tower 1. The first reflux pump 51 is provided with a product output pipeline for outputting liquefied petroleum gas.

[0040] By sequentially installing a condenser 4, a reflux tank 5, and a first reflux pump 51 at the top of the stabilizer tower 1, a stable and reliable top-of-tower condensation and reflux system is formed. This allows the light component gas phase separated by the stabilizer tower 1 to be efficiently condensed and separated into gas and liquid in the reflux tank 5. While ensuring a stable supply of reflux liquid required for distillation, liquefied petroleum gas (LPG) is continuously delivered as a product through the product output pipeline of the first reflux pump 51. This structure maintains a reasonable temperature and concentration distribution within the tower through a stable and adjustable reflux ratio, ensuring the stability of the separation effect and product quality of the stabilizer tower 1. On the other hand, it works synergistically with the front-end feed flash evaporation and the energy-mass separation process of the vortex tube 211 to reduce the ineffective circulating load and condensation heat demand of the light components at the top of the tower, thereby improving the operating efficiency of the condensation system. Without increasing additional power consumption and operational complexity, it achieves stable recovery of LPG products and further improves the overall energy efficiency of the system, exhibiting excellent continuous operation performance.

[0041] Specifically, the stabilizer tower 1 has 56 trays, a condenser 4, a top reflux tank 5, and a top first reflux pump 51 at the top, and a reboiler 6 at the bottom. A portion of the stream from the first reflux pump 51 is collected as LPG, and the remainder is returned to the top of the stabilizer tower 1. It should be noted that the first reflux pump 51 has an input end, a reflux end, and an output end. The input end of the first reflux pump 51 is connected to the reflux tank 5, and the output end of the first reflux pump 51 is used to output the LPG product.

[0042] like Figure 1 As shown, in an optional embodiment of the present invention, the feed pipe 212 is provided with a separator, the cold gas collection pipe 213 is provided with a mixer, and both the hot discharge pipe 22 and the cold discharge pipe 23 are provided with pressure monitoring instruments.

[0043] By installing a separator on the feed pipe 212 of the vortex tube module 2, the material entering the vortex tube 211 undergoes effective preliminary separation of gas, liquid, or impurities before entering the vortex separator. This avoids interference from droplet entrainment or uneven feeding on the stability of the vortex field, thereby ensuring the formation quality of the vortex structure inside the vortex tube 211 and the energy-mass separation effect. Simultaneously, a mixer is installed on the cold gas collection pipe 213, enabling uniform mixing and state integration of the cold gas flows from multiple parallel vortex tubes 211 during the collection process. This reduces temperature, pressure, and component fluctuations, preparing the material for subsequent processing. The stabilizing tower 1 or heat exchange unit provides a stable and controllable cold source material flow. In addition, pressure monitoring instruments are respectively configured on the hot discharge pipe 22 and the cold discharge pipe 23 to monitor the pressure status of the two material flows after separation by the vortex tube 211 in real time. This facilitates timely judgment of the operating conditions and separation effect of the vortex tube 211, and enables rapid early warning and adjustment of abnormal operating conditions of the system. Through the above structural settings, the stability, controllability and engineering reliability of the vortex tube module 2 are further improved, ensuring the continuous performance of enhanced separation and energy-saving effects during long-term operation.

[0044] In an optional embodiment of the present invention, each vortex tube 211 is provided with a throttle valve at its inlet end, the throttle valve being used to adjust the feed flow rate and pressure of a single vortex tube 211.

[0045] By independently installing a throttling valve at the inlet end of each vortex tube 211, the feed flow rate and pressure entering a single vortex tube 211 can be finely adjusted, ensuring that each vortex tube 211 maintains suitable and consistent differential pressure conditions in parallel operation. This forms a stable high-speed swirling flow field and fully utilizes the energy-mass separation effect. This structure effectively avoids the problem of decreased separation efficiency caused by uneven flow distribution or insufficient local differential pressure, improving the overall balance and reliability of the multi-vortex tube module 2. At the same time, the number of vortex tubes 211 in operation and the single-tube operating conditions can be flexibly adjusted according to changes in the unit load, enhancing the system's adaptability to different throughput and operating condition fluctuations. Without adding additional power equipment, the separation performance of the vortex tube 211 can be controllably enhanced, ensuring the long-term, stable, and efficient operation of the coupling separation process of the stabilizer tower 1, which is conducive to further improving the system's energy-saving effect and engineering application value.

[0046] like Figure 2 and Figure 3 As shown, in an optional embodiment of the present invention, the bottom of the stabilizing tower 1 is provided with a gasoline output pipe 11, and the gasoline output pipe 11 is provided with a reboiler 6.

[0047] By installing a gasoline output pipe 11 and a reboiler 6 at the bottom of the stabilizer tower 1, the stabilized gasoline at the bottom of the tower can receive controllable heat compensation while being continuously delivered, providing the necessary and stable vaporization driving force for the tower and ensuring that light components are fully removed from the gasoline at the bottom of the tower. The reboiler 6 works in synergy with the energy and mass separation effect of the front-end vortex tube module 2 on the feed or the gas flow at the top of the tower, so that the material entering the stabilizer tower 1 is in an optimized temperature and enthalpy state, thereby reducing the unit heat demand of the reboiler 6 and reducing the ineffective heating process. By concentrating the reboiling function in the gasoline loop at the bottom of the tower, it is not only beneficial to accurately control the quality of the product at the bottom of the tower and the temperature distribution in the tower, but also improves the overall stability and thermal efficiency of the stabilizer tower 1, achieving the dual effect of controllable stabilized gasoline quality and reduced system energy consumption.

[0048] like Figure 2 and Figure 6As shown in Embodiment 1, this application also provides a stabilizer tower coupled enhanced separation method, which adopts the above-mentioned stabilizer tower coupled enhanced separation device and feed flash evaporation process. The method includes: a mixture of liquefied petroleum gas and stabilized gasoline undergoes heat exchange after passing through a feed heat exchanger 31. The heat-exchanged mixture enters a feed flash evaporation tank 3 and undergoes flash separation at a preset temperature and pressure to obtain a flash vapor phase and a flash liquid phase. The flash vapor phase enters a vortex tube module 2 to achieve energy-mass separation, separating a cold gas flow and a hot gas flow. The cold gas flow is sent to the feed inlet at the top of the stabilizer tower 1 through a cold discharge pipe 23, and the hot gas flow is sent to the feed inlet at the bottom of the stabilizer tower 1 through a hot discharge pipe 22. The flash liquid phase enters the feed inlet at the bottom of the stabilizer tower 1. The gas phase at the top of the stabilizer tower 1 is treated by condensation and other processes to output liquefied petroleum gas products, and the bottom of the stabilizer tower 1 outputs stabilized gasoline products.

[0049] By organically combining feed heat exchange, flash pre-separation, energy-mass separation in vortex tube 211, and distillation in stabilizer tower 1, the mixed feedstock of liquefied petroleum gas and stabilized gasoline undergoes multi-stage thermodynamic state and component distribution optimization before entering stabilizer tower 1: the mixed feedstock recovers system waste heat through feed heat exchanger 31 and then enters feed flash tank 3, where light component gas phase is pre-precipitated under set temperature and pressure conditions, significantly reducing the subsequent distillation load; the flash vapor phase further enters vortex tube module 2, forming a strong swirling flow field under its own pressure without external power, achieving energy-mass separation of cold and hot gas streams, and introducing them into the upper and lower parts of stabilizer tower 1 according to their temperature and enthalpy characteristics, so that the heat and mass transfer driving force in the tower are utilized in a targeted manner; at the same time, the flash liquid phase directly enters the lower part of the tower to participate in distillation, reducing the repeated vaporization and condensation process of light components in the tower. Through the above methods, the reboiling and condensation loads of stabilizer tower 1 are significantly reduced, and the temperature gradient and gas-liquid load distribution within the tower are more reasonable. Under the premise of ensuring that the quality of liquefied petroleum gas and stabilized gasoline products meets the standards, the overall energy consumption of the system is effectively reduced, and the operational stability and adaptability to operating conditions are improved. It is especially suitable for energy-saving retrofitting and industrial application of high-load, high-energy-consumption absorption stabilization systems.

[0050] Specifically, in Example 1, the feed flow rate of stabilizer tower 1 is 330.6 t / h, the feed temperature is 124℃, and the feed pressure is 1.47 MPa. The liquefied petroleum gas (LPG) mass fraction is 21.5%, and the stabilized gasoline mass fraction is 78.5%. The feed to stabilizer tower 1 first enters the feed heat exchanger 31, where it exchanges heat with the stabilized gasoline discharged from the bottom of stabilizer tower 1. After the heat exchange, the feed temperature rises to 151℃, and then it enters the feed flash tank 3. Flash separation occurs in the feed flash tank 3 at a temperature of 151℃ and a pressure of 1.47 MPa, yielding a flash liquid phase and a flash vapor phase. The flash liquid phase, with a flow rate of 241.5 t / h, a temperature of 151℃, and a pressure of 1.47 MPa, enters stabilizer 1 from the 28th tray from the bottom. The flash vapor phase, with a flow rate of 89.1 t / h, a temperature of 151℃, and a pressure of 1.47 MPa, enters vortex tube module 2 for energy-mass separation. After separation by vortex tube module 2, two streams are obtained: a cold gas stream with a flow rate of 55.3 t / h, a temperature of 140℃, and a pressure of 1.37 MPa, introduced from the 26th tray from the bottom of stabilizer 1; and a hot gas stream with a flow rate of 33.8 t / h, a temperature of 160℃, and a pressure of 1.37 MPa, introduced from the 30th tray of stabilizer 1. By introducing gas streams with different temperatures and enthalpy characteristics to different heights within stabilizer 1, the heat and mass transfer driving force within the tower are utilized in a targeted manner. After the C3-C4 component-rich liquefied petroleum gas (LPG) vapor phase is discharged from the top of stabilizer tower 1, it is cooled into a liquid phase by condenser 4. A portion of this LPG is returned to the top of stabilizer tower 1 as reflux liquid via the first reflux pump 51, while the other portion is sent out as product. The mass fraction of C3-C4 component in the resulting LPG product is 99.0%. The stabilized gasoline, rich in C5+ component, is continuously discharged from the bottom of stabilizer tower 1 as product, with a C5+ component mass fraction of 98.7%. The specific parameters of stabilizer tower 1 are as follows: Stabilizer tower 1 has a total of 56 trays, a top pressure of 1.229 MPa, a top temperature of 64℃, and the top condenser 4 requires 3638 t / h of circulating water, corresponding to a cooling load of 21136 kW. The bottom pressure is 1.30 MPa, the bottom temperature is 187℃, and the bottom reboiler 6 uses 3.5 MPa medium-pressure steam as a heat source, with a steam consumption of 32 t / h and a corresponding reboiling load of 17537 kW. Through the above operating conditions, efficient separation of liquefied petroleum gas and stabilized gasoline is achieved, and the overall energy consumption of stabilizer tower 1 is effectively reduced while ensuring stable product quality.

[0051] like Figure 1 and Figure 3As shown, in Embodiment 2 of the present invention, the stabilizer tower coupling enhancement separation device of this application further includes a first cooler 7, a second cooler 8, a reflux tank 5, a first reflux pump 51, a second reflux pump 52, and a buffer tank 9. The top of the stabilizer tower 1 is connected to the input end of the vortex tube module 2. The cold discharge pipe 23, the first cooler 7, the reflux tank 5, and the first reflux pump 51 are connected in sequence through pipes. The reflux end of the first reflux pump 51 is connected to the top of the stabilizer tower 1. The first reflux pump 51 is provided with a product output pipe for outputting liquefied petroleum gas. The hot discharge pipe 22, the second cooler 8, the buffer tank 9, the second reflux pump 52, and the top of the stabilizer tower 1 are connected in sequence through pipes.

[0052] like Figure 3 and Figure 7 As shown in Embodiment 2, this application also provides a stabilizer tower coupled enhanced separation method, which uses the above-mentioned stabilizer tower coupled enhanced separation device and distillation mixing process for separation. The specific separation method steps are as follows: the liquefied petroleum gas and stabilized gasoline mixture to be separated directly enters the stabilizer tower coupled enhanced separation device in the stabilizer tower 1; the gas phase at the top of the stabilizer tower 1 enters the vortex tube module 2, and through the energy and mass separation effect of the vortex tube 211, the cold discharge pipe outputs a cold gas flow of C3-C4 light components, while the hot discharge pipe 22 outputs a gas flow containing less C3-C4 light components. The hot gas flow of C5+ heavy components is measured; the cold gas flow output from the cold discharge pipe 23 of the vortex tube module 2 is cooled to a reasonable temperature by the first cooler 7 and then enters the first reflux pump 51 at the top of the tower. Part of it is output as LPG product, and the other part is returned to the top of the stabilizer tower 1; the hot gas flow output from the hot discharge pipe 22 of the vortex tube module 2 is cooled to a reasonable temperature by the second cooler 8 and then returns to the top of the stabilizer tower 1 through the buffer tank 9 at the top of the tower and the second reflux pump 52 at the top of the tower; the stabilized gasoline product is collected from the bottom of the stabilizer tower 1.

[0053] By directly introducing the gas phase from the top of stabilizer tower 1 into vortex tube module 2, and subsequently setting up two independent cold and hot loops with corresponding cooling, buffering, and reflux systems, the gas phase from the top of the tower can complete energy and mass redistribution without increasing additional power consumption: After separation by vortex tube 211, the cold gas phase rich in C3-C4 light components is preferentially cooled by the first cooler 7 and enters the first reflux pump 51. Part of it is directly sent out as liquefied petroleum gas product, and the other part is refluxed back to the top of stabilizer tower 1 to maintain the necessary rectification reflux flow; while the hot gas phase containing a small amount of C5+ heavy components is cooled by the second cooler 8. All the gas is returned to the top of the stabilizer tower 1 through the buffer tank 9 and the second reflux pump 52 to participate in the re-separation, thereby effectively suppressing the entrainment of heavy components into the liquefied petroleum gas product. By implementing a closed-loop coupling method of energy and mass separation, branch cooling, and differentiated reflux of the gas phase at the top of the tower, the instantaneous load of the condensation system at the top of the tower is significantly reduced, the gas-liquid balance conditions in the tower are improved, and the ineffective circulation of light and heavy components in the top region of the tower is reduced. While ensuring that the quality of LPG and stabilized gasoline products meets the standards, the separation efficiency and operational stability at the top of the tower are improved, and the energy-saving potential of the stabilizer tower 1 system is further explored, which has good engineering application value.

[0054] Specifically, in Example 2, the feed flow rate of stabilization tower 1 is 330.6 t / h, the feed temperature is 124℃, and the feed pressure is 1.47 MPa. The liquefied petroleum gas (LPG) mass fraction is 21.5%, and the stabilized gasoline mass fraction is 78.5%. The feed is introduced into stabilization tower 1 at the 28th tray from bottom to top. After distillation separation within the tower, the stabilized gasoline rich in C5+ components is discharged from the bottom as the product, with a C5+ component mass fraction of 98.7%. The gas rich in C3-C4 components discharged from the top of the tower has a flow rate of 189.0 t / h, a temperature of 68℃, and a pressure of 1.229 MPa, and enters vortex tube module 2 for further energy-mass separation. After separation by vortex tube module 2, two streams of gas are obtained: a cold gas stream and a hot gas stream. The cold gas flow rate is 95.8 t / h, the temperature is 60℃, and the pressure is 1.129 MPa. After being cooled to 48℃ by the first cooler 7, it enters the first reflux pump 51 at the top of the column. Part of it is sent out as liquefied petroleum gas (LPG) product, and the other part is refluxed back to the top of the stabilizer column 1 to maintain the rectification reflux. The mass fraction of C3-C4 components in the obtained LPG product is 99.1%. The hot gas flow rate is 93.2 t / h, the temperature is 79℃, and the pressure is 1.129 MPa. After being cooled to 60℃ by the second cooler 8, it passes through the top buffer tank 9 and the second reflux pump 52 at the top of the column and is completely refluxed back to the top of the stabilizer column 1 to participate in the rectification. The specific parameters of the stabilizer column 1 are: a total of 56 trays, a top pressure of 1.229 MPa, and a top temperature of 72℃. The first cooler 7 and the second cooler 8 require a combined circulating water consumption of 3061 t / h, corresponding to a cooling load of 17776 kW. The bottom pressure is 1.3 MPa, the bottom temperature is 187℃, and the bottom reboiler 6 uses 3.5 MPa medium-pressure steam for heating, with a steam consumption of 47.6 t / h, corresponding to a reboiling load of 26223 kW. Through the above design and operating parameters, the vortex tube module 2 and the top reflux system of the stabilizer tower 1 work together to achieve enhanced separation and optimized reflux of the light components at the top of the tower. This not only ensures the high purity of the liquefied petroleum gas and stabilized gasoline products, but also effectively reduces the cooling load at the top of the tower and the reboiling load at the bottom, improving the overall energy efficiency and operational stability of the system.

[0055] like Figure 4As shown in Comparative Example 1, a conventional feed flash evaporation process for separating liquefied petroleum gas (LPG) and stabilized gasoline in a stabilizer tower operates under the following conditions: the feed flow rate of stabilizer tower 1 is 330.6 t / h, the feed temperature is 124℃, and the feed pressure is 1.47 MPa, with LPG comprising 21.5% by mass and stabilized gasoline comprising 78.5% by mass. The feed first enters the feed heat exchanger 31, where it exchanges heat with the stabilized gasoline discharged from the bottom of stabilizer tower 1, raising the feed temperature to 151℃. It then enters the feed flash tank 3 for flash separation. The flash liquid phase has a flow rate of 241.5 t / h, a temperature of 151℃, and a pressure of 1.47 MPa, and is introduced from the 28th tray from the bottom up in stabilizer tower 1; the flash vapor phase has a flow rate of 89.1 t / h, a temperature of 151℃, and a pressure of 1.47 MPa, and is introduced from the 26th tray in stabilizer tower 1.

[0056] After distillation and separation in the tower, liquefied petroleum gas (LPG) rich in C3-C4 components is discharged from the top of the tower. After being cooled into a liquid phase by condenser 4, a portion is refluxed back to the top of the tower by the first reflux pump 51, while the other portion is sent out as LPG product by the same reflux pump. The mass fraction of C3-C4 components in the product is 99.0%. Stabilized gasoline rich in C5+ components is discharged from the bottom of the tower as the product, with a C5+ component mass fraction of 98.7%. The stabilizer tower 1 has a total of 56 trays, a top pressure of 1.229 MPa, a top temperature of 64°C, and a circulating water consumption of condenser 4 at the top of the tower of 3728 t / h, corresponding to a cooling load of 21656 kW. The bottom pressure is 1.3 MPa, the bottom temperature is 187°C, and the reboiler 6 at the bottom of the tower uses 3.5 MPa medium-pressure steam with a steam consumption of 33 t / h, corresponding to a reboiling load of 17915 kW.

[0057] like Figure 5As shown in Comparative Example 2, a conventional distillation mixing process using a stabilizer tower for separating liquefied petroleum gas (LPG) and stabilized gasoline operates under the following conditions: the feed flow rate of stabilizer tower 1 is 330.6 t / h, the temperature is 124℃, and the pressure is 1.47 MPa. The LPG mass fraction in the feed is 21.5%, and the stabilized gasoline mass fraction is 78.5%. The feed is introduced into the stabilizer tower 1 from the 28th tray from the bottom. The LPG rich in C3-C4 components discharged from the top of the tower is cooled into a liquid phase by condenser 4. A portion of the liquid phase is refluxed back to the top of the tower, while the other portion is sent out as LPG product, with a C3-C4 component mass fraction of 99.0%. The stabilized gasoline rich in C5+ components is discharged from the bottom of the tower as product, with a C5+ component mass fraction of 98.7%. The stabilizer tower 1 has a total of 56 trays, a top pressure of 1.229 MPa, a top temperature of 59°C, a top condenser 4 with a circulating water consumption of 3098 t / h, and a cooling load of 18000 kW; the bottom pressure is 1.3 MPa, the bottom temperature is 187°C, the bottom reboiler 6 uses 3.5 MPa medium-pressure steam, the steam consumption is 49 t / h, and the corresponding reboiling load is 26926 kW.

[0058] The energy consumption comparison of Example 1 and Comparative Example 1 using the stabilizer tower feed flash evaporation process of the device of this application, and Example 2 and Comparative Example 2 using the distillation mixing process of the device of this application, is shown in the table below:

[0059] Table 1. Energy values ​​of the stabilizer tower feed flash evaporation process in Example 1

[0060]

[0061] Table 2 shows the energy values ​​of the conventional feed flash evaporation process in the stabilizer tower in Comparative Example 1.

[0062]

[0063] Table 3 Energy values ​​of the distillation-mixing process in Example 2

[0064]

[0065] Table 4. Energy values ​​of the conventional distillation-mixing process in Comparative Example 2

[0066]

[0067] Based on the energy consumption data comparison results in Tables 1-4 above, it can be concluded that the stabilizer-coupling enhanced separation device of this application exhibits significant energy-saving advantages and system enhancement effects under different process modes: under the feed flash evaporation process conditions, the total energy consumption of Example 1 is 51325 kW, significantly lower than the 52223 kW of the conventional stabilizer-coupling feed flash evaporation process in Comparative Example 1; under the distillation-mixing process conditions, the total energy consumption of Example 2 is 43999 kW, also significantly lower than the 44926 kW of the conventional distillation-mixing process in Comparative Example 2. This indicates that this application, through the coupled enhanced separation structure of the stabilizer and vortex tube module, achieves enhanced mass transfer process and improved phase separation efficiency, effectively reducing the system's dependence on energy units such as reboiling, condensation, and compression. While ensuring separation effect and product quality stability, it significantly reduces the overall system energy consumption, thus possessing outstanding energy-saving advantages, operational economy, and engineering promotion value in industrial applications.

[0068] It should be understood that the various forms of processes shown above can be used to reorder, add, or delete steps. For example, the steps described in this invention can be executed in parallel, sequentially, or in different orders, as long as the desired result of the technical solution disclosed in this invention can be achieved, and this is not limited herein.

[0069] The specific embodiments described above do not constitute a limitation on the scope of protection of this invention. Those skilled in the art should understand that various modifications, combinations, sub-combinations, and substitutions can be made according to design requirements and other factors. Any modifications, equivalent substitutions, and improvements made within the principles of this invention should be included within the scope of protection of this invention.

Claims

1. A stabilizer tower coupling enhancement separation device, characterized in that, include: Stabilizer tower; A vortex tube module, wherein the vortex tube module is composed of multiple vortex tube units connected in series, and each vortex tube unit is composed of multiple vortex tubes connected in parallel. The vortex tube unit is provided with a feed pipe and a cold air collection pipe. The feed pipe is connected to the feed end of multiple vortex tubes, and the cold air end of multiple vortex tubes is connected to the cold air collection pipe. The cold air collection pipe of the vortex tube unit is connected to the feed pipe of the next vortex tube unit connected in series. The vortex tube module is equipped with a hot discharge pipe and a cold discharge pipe. The hot gas end of each vortex tube is connected to the hot discharge pipe. The cold discharge pipe is a cold gas collection pipe located at the end of the vortex tube unit connected in series. The cold discharge pipe is connected to the stabilizer. The vortex tube module is used to perform energy and mass separation on the raw material entering the stabilizer or the top gas flow of the stabilizer. The feed flash tank has an input pipe equipped with a feed heat exchanger. The gas output end of the feed flash tank is connected to the input end of the vortex tube module, and the liquid output end of the feed flash tank is connected to the stabilizer tower. Both the hot discharge pipe and the cold discharge pipe are connected to the stabilizer tower. The upper part of the stabilizer tower and the lower part of the stabilizer tower are respectively provided with an upper feed port and two lower feed ports. The liquid output end of the feed flash tank and the hot discharge pipe are respectively connected to the two lower feed ports, and the cold discharge pipe is connected to the upper feed port. It also includes a condenser, a reflux tank, and a first reflux pump. The top of the stabilizer tower, the condenser, the reflux tank, and the first reflux pump are connected in sequence by pipelines. The reflux end of the first reflux pump is connected to the top of the stabilizer tower. The first reflux pump is provided with a product output pipeline for outputting liquefied petroleum gas.

2. The stabilizing tower coupling enhancement separation device according to claim 1, characterized in that, The liquid output end of the feed flash tank is connected to the feed inlet of the stabilizer tower body through a first pipeline, which is equipped with a flow regulating valve. The gas output end of the feed flash tank is connected to the input end of the vortex tube module through a second pipeline, which is equipped with a pressure monitoring instrument.

3. The stabilizing tower coupling enhancement separation device according to claim 1, characterized in that, The feed pipe is equipped with a separator, the cold air collection pipe is equipped with a mixer, and both the hot discharge pipe and the cold discharge pipe are equipped with pressure monitoring instruments.

4. The stabilizing tower coupling enhancement separation device according to claim 1, characterized in that, Each of the vortex tubes is equipped with a throttle valve at its inlet end, which is used to regulate the feed flow rate and pressure of a single vortex tube.

5. The stabilizing tower coupling enhancement separation device according to claim 1, characterized in that, It also includes a first cooler, a second cooler, a reflux tank, a first reflux pump, a second reflux pump, and a buffer tank. The top of the stabilizing tower is connected to the input end of the vortex tube module. The cold discharge pipe, the first cooler, the reflux tank, and the first reflux pump are connected in sequence through pipes. The reflux end of the first reflux pump is connected to the top of the stabilizing tower. The first reflux pump is equipped with a product output pipe for discharging liquefied petroleum gas. The hot discharge pipe, the second cooler, the buffer tank, the second reflux pump, and the top of the stabilizing tower are connected in sequence through pipes.

6. A method for enhancing separation through coupling in a stable tower, characterized in that, The method employing the stabilizing tower coupling enhancement separation device according to any one of claims 1 and 2, comprises: The mixture of liquefied petroleum gas and stabilized gasoline undergoes heat exchange in the feed heat exchanger. The heat-exchanged mixture then enters the feed flash tank, where it undergoes flash separation at a preset temperature and pressure to obtain a flash vapor phase and a flash liquid phase. The flash vapor phase enters the vortex tube module to achieve energy-mass separation, separating into cold gas flow and hot gas flow. The cold gas flow is sent to the feed inlet at the top of the stabilizer tower through the cold discharge pipe, and the hot gas flow is sent to the feed inlet at the bottom of the stabilizer tower through the hot discharge pipe. The flash liquid phase enters the feed inlet at the bottom of the stabilizer, the gas phase at the top of the stabilizer is condensed and output as liquefied petroleum gas, and the bottom of the stabilizer outputs as stabilized gasoline.

7. A method for enhancing separation through coupling in a stable tower, characterized in that, The method using the stabilizing tower coupling enhancement separation device as described in claim 5 includes: The liquefied petroleum gas and stabilized gasoline mixture feedstock is directly fed into the stabilization tower. After the gas phase at the top of the stabilization tower enters the vortex tube module, the cold discharge pipe outputs a cold gas flow and the hot discharge pipe outputs a hot gas flow. After the cold airflow is cooled to a preset temperature by the first cooler, it enters the first reflux pump. One output end of the first reflux pump outputs liquefied petroleum gas product, and the other output end of the first reflux pump inputs the cold airflow into the stabilizer. After the hot gas flow is cooled to a preset temperature by the second cooler, it passes through the buffer tank and the second reflux pump and returns to the top of the stabilizer tower. The stabilizer tower outputs stable gasoline products at the bottom of the tower.

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