Stabilizer coupling enhanced separation device and separation method

Abstract

The invention relates to the field of petrochemical engineering separation, and discloses a stabilization tower coupling enhanced separation device and a separation method.The stabilization tower coupling enhanced separation device comprises a stabilization tower; the vortex tube module is formed by connecting a plurality of vortex tube units in series, each vortex tube unit is formed by connecting a plurality of vortex tubes in parallel, each vortex tube unit is provided with a feeding tube and a cold air collecting tube, the feeding tube is communicated with the feeding ends of the vortex tubes, and the cold air collecting tube is communicated with the cold air collecting tube. The cold air ends of the multiple vortex tubes are all communicated with the cold air collecting pipe, and the cold air collecting pipe of each vortex tube unit is communicated with the feeding pipe of the next vortex tube unit which is connected in series with the cold air collecting pipe; the vortex tube module is provided with a hot discharge tube and a cold discharge tube, the hot air end of each vortex tube is communicated with the hot discharge tube, and the cold discharge tube is communicated with the stabilizing tower. According to the invention, the vortex tube module formed by multi-stage series connection and parallel connection structures is introduced into the stabilizing tower, so that the energy consumption of the system is effectively reduced.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of petrochemical separation, and in particular to a stable tower coupling enhanced separation device and a separation method. BACKGROUND

[0002] The absorption stabilization system is widely used in petrochemical combined devices, and is mainly used for separating and treating the superheated steam flow generated by the catalytic cracking device to obtain dry gas, liquefied petroleum gas (LPG, C3-C4 components) and stable gasoline (C5+ components) and other products. The traditional absorption stabilization system is usually composed of multiple tower units such as an absorption tower, a reabsorption tower, a desorption tower and a stable tower, and has a complex process, a large number of equipment, and a high overall energy consumption in the oil refining device, among which the heat load of the reboiling and condensation process of the stable tower is the most prominent. In recent years, with the popularization and application of new catalytic cracking processes such as efficient catalytic cracking of heavy oil, the generation amount of C3-C4 light hydrocarbons in the device has significantly increased, resulting in a continuous increase in the processing load of the absorption stabilization system and a further increase in the heat demand of the stable tower. Under the background of the continuous rise in energy prices and the “double carbon” target, how to effectively reduce the comprehensive energy consumption of the absorption stabilization system, especially the stable tower unit, while ensuring the product separation index has become a key technical problem that needs to be solved in the petrochemical industry.

[0003] In view of the above problems, various energy-saving optimization schemes for the absorption stabilization system have been proposed in the prior art. For example, some research has introduced a flash tank into the gasoline absorption stabilization process and optimized the composition of the absorbent, thereby reducing the system operating cost to a certain extent; some literature has combined process simulation and pinch point analysis methods to reform and optimize the process of the absorption stabilization system, and has proposed improving the condensation structure to improve the waste heat recovery efficiency. In addition, in terms of operation condition optimization, related research has also systematically analyzed the influence law of parameters such as tower operating pressure, absorbent circulation amount and feed conditions on system energy consumption, and has realized a certain degree of heat energy saving through parameter adjustment. However, most of the existing energy-saving technical schemes are concentrated on the structure improvement and operation parameter optimization of a single tower or a local unit, and the optimization idea is still limited to the traditional heat exchange and phase equilibrium control framework. Although the above schemes have achieved certain results in local energy saving, they generally have the following shortcomings: on the one hand, there is a lack of essential strengthening means for the energy and mass separation process of the stable tower, which is a high-energy-consumption core unit; on the other hand, the technical potential of deeply coupling the stable tower with other non-traditional separation units to realize system-level collaborative energy saving has not been fully tapped. Therefore, the existing absorption stabilization system still has obvious technical limitations and great improvement space in terms of reducing overall energy consumption.

[0004] Therefore, there is an urgent need for a new separation device and method that can realize the intensification of the stable column separation process without significantly increasing the system complexity and additional power consumption, and effectively coupled with the existing process, to meet the technical needs of energy saving and consumption reduction of the absorption stabilization system under the current high load operation condition. SUMMARY

[0005] The technical problem to be solved by the present application is to solve the problem of high overall energy consumption of the absorption stabilization system.

[0006] To solve the above technical problems, the present application provides a stable column coupling and intensification separation device, comprising: a stable column; a vortex tube module, the vortex tube module is composed of a plurality of vortex tube units connected in series, each vortex tube unit is composed of a plurality of vortex tubes connected in parallel, the vortex tube unit is provided with a feed pipe and a cold gas collection pipe, the feed pipe is connected with the feed end of a plurality of vortex tubes, the cold gas end of a plurality of vortex tubes is connected with the cold gas collection pipe, the cold gas collection pipe of the vortex tube unit is connected with the feed pipe of the next series of vortex tube units; 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 connected with the hot discharge pipe, the cold discharge pipe is the cold gas collection pipe of the vortex tube unit connected in series at the end, the cold discharge pipe is connected with the stable column, the vortex tube module is used for energy and quality separation of the raw material entering the stable column or the overhead gas stream of the stable column.

[0007] Further, a feed flash tank is further included, an input pipeline of the feed flash tank is provided with a feed heat exchanger, a gas output end of the feed flash tank is connected with an input end of the vortex tube module, a liquid output end of the feed flash tank is connected with the stable column, the hot discharge pipe and the cold discharge pipe are both connected with the stable column.

[0008] Further, the upper part of the stable column and the lower part of the stable column are respectively provided with an upper feed inlet and two lower feed inlets, the liquid output end of the feed flash tank and the hot discharge pipe are respectively connected with two lower feed inlets, and the cold discharge pipe is connected with the upper feed inlet.

[0009] Further, the liquid output end of the feed flash tank is connected with the feed inlet of the stable column through a first pipeline, the first pipeline is provided with a flow regulating valve, the gas output end of the feed flash tank is connected with the input end of the vortex tube module through a second pipeline, and the second pipeline is provided with a pressure monitoring instrument.

[0010] Further, a condenser, a reflux tank and a first reflux pump are further included, the tower body top of the stabilizing tower, the condenser, the reflux tank, the first reflux pump are sequentially connected in communication through pipelines, the reflux end of the first reflux pump is connected in communication with the tower top of the stabilizing tower, and the first reflux pump is provided with a product output pipeline for outputting liquefied petroleum gas.

[0011] Further, the feed pipeline is provided with a separator, the cold gas collecting pipeline is provided with a mixer, and the hot discharge pipeline and the cold discharge pipeline are both provided with pressure monitoring instruments.

[0012] Further, the inlet end of each of the vortex tubes is provided with a throttle valve, and the throttle valve is used for adjusting the feed flow and pressure of the single vortex tube.

[0013] Further, a first cooler, a second cooler, a reflux tank, a first reflux pump, a second reflux pump and a buffer tank are further included, the tower top of the stabilizing tower is connected in communication with the input end of the vortex tube module, the cold discharge pipeline, the first cooler, the reflux tank and the first reflux pump are sequentially connected in communication through pipelines, the reflux end of the first reflux pump is connected in communication with the tower top of the stabilizing tower, the first reflux pump is provided with a product output pipeline for outputting liquefied petroleum gas, and the hot discharge pipeline, the second cooler, the buffer tank, the second reflux pump and the tower top of the stabilizing tower are sequentially connected in communication through pipelines.

[0014] The application further provides a stabilizing tower coupling enhanced separation method, which adopts the stabilizing tower coupling enhanced separation device, and the method comprises the following steps: after the mixed raw material of liquefied petroleum gas and stabilized gasoline is subjected to heat exchange through the feed heat exchanger, the mixed raw material after heat exchange is subjected to flash separation at a preset temperature and pressure to obtain a flash gas phase and a flash liquid phase; the flash gas phase is subjected to energy and mass separation through the vortex tube module to obtain a cold gas flow and a hot gas flow, the cold gas flow is sent into the upper feed inlet of the stabilizing tower through the cold discharge pipeline, and the hot gas flow is sent into the lower feed inlet of the stabilizing tower through the hot discharge pipeline; the flash liquid phase is sent into the lower feed inlet of the stabilizing tower, the gas phase in the tower top of the stabilizing tower is subjected to condensation treatment to output a liquefied petroleum gas product, and the tower bottom of the stabilizing tower outputs a stabilized gasoline product.

[0015] The application further provides a stable column coupling enhanced separation method, which adopts the stable column coupling enhanced separation device, and the method comprises the following steps: liquefied petroleum gas and stable gasoline mixed raw materials directly enter the stable column, after the gas phase at the top of the stable column enters the vortex tube module, the cold discharge pipe outputs cold gas flow and the hot discharge pipe outputs hot gas flow; after the cold gas flow is cooled to a preset temperature by the first cooler, the cold gas flow enters the first reflux pump, one output end of the first reflux pump outputs liquefied petroleum gas products, and the other output end of the first reflux pump inputs the cold gas flow into the stable column; after the hot gas flow is cooled to a preset temperature by the second cooler, the hot gas flow is returned to the inside of the top of the column body of the stable column through the buffer tank and the second reflux pump in sequence, and stable gasoline products are output from the bottom of the column body of the stable column.

[0016] Compared with the prior art, the stable column coupling enhanced separation device provided by the application has the following beneficial effects: by introducing the vortex tube module composed of multiple levels in series and single level in parallel into the gas phase loop at the front end or the top of the stable column, the high-pressure mixed fluid entering the separation device enters the vortex tube in a tangential manner and forms a high-speed rotating strong vortex flow field under the condition of no external power, and under the joint action of centrifugal force, radial pressure gradient and axial backflow, significant energy and component distribution differences are generated in the fluid, wherein the heavy components with high temperature, high enthalpy value and large density tend to the pipe wall area and are discharged along the outer spiral flow direction to form hot gas flow, and the light components with low temperature, low enthalpy value and small density gather to the pipe axis center and are discharged along the inner spiral flow to form cold gas flow; by the series connection of multiple vortex tube units, the cold gas flow after separation in the previous stage further enters the vortex tube in the next stage, the energy and mass separation effect is amplified step by step while the fluid momentum and pressure gradient are maintained, so that more significant temperature drop and component enrichment effects are obtained as a whole, and the parallel connection of multiple vortex tubes in the single stage effectively shares the flow and reduces the load of the single tube, so that stable vortex intensity and separation efficiency can be maintained under the condition of large processing capacity; after the above energy and mass pre-classification, the material enters the stable column again, so that the vapor-liquid balance condition in the column is optimized, the repeated vaporization and condensation process of the light components in the column is reduced, the heat load of the reboiler and the condensing system is significantly reduced, the separation process is essentially enhanced without changing the main structure of the stable column, and then the comprehensive energy consumption of the absorption and stabilization system is effectively reduced, the separation efficiency and operation flexibility are improved, and the stable column coupling enhanced separation device has good engineering adaptability and energy-saving application value. BRIEF DESCRIPTION OF DRAWINGS

[0017] Figure 1 FIG. 1 is a schematic diagram of a vortex tube module of the stable column coupling enhanced separation device provided by the application; Figure 2 FIG. 2 is a process flow diagram of the stable column coupling enhanced separation device provided by the first embodiment of the application; Figure 3is a process flow chart of the stable column coupled with the enhanced separation device provided in Embodiment Two of the present application; Figure 4 is a conventional feed flash process flow chart of a stable column; Figure 5 is a conventional rectification mixing process flow chart of a stable column; Figure 6 is a stable column coupled with an enhanced separation method provided in Embodiment One of the present application; Figure 7 is a stable column coupled with an enhanced separation method provided in Embodiment Two of the present application.

[0018] Correspondence between the reference signs and the component names is as follows: 1, stable column; 11, gasoline output pipeline; 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 DESCRIPTION

[0019] Exemplary embodiments of the present application are described herein below with reference to the accompanying drawings, which include various details of the embodiments of the present application to assist in the understanding thereof, and should be considered in connection with the following detailed description, and should be considered as merely illustrative. Thus, those skilled in the art will recognize that changes and modifications can be made thereto without departing from the scope of the present application. Also, in the following description, descriptions of well-known functions and constructions are omitted for clarity and conciseness.

[0020] As shown in the drawings, Figures 1 to 5 Embodiments of the present application disclose a stable column coupled with an enhanced separation device, comprising: a stable column 1; a vortex tube module 2, the vortex tube module 2 is composed of a plurality of vortex tube units 21 connected in series, each vortex tube unit 21 is composed of a plurality of vortex tubes 211 connected in parallel, the vortex tube unit 21 is provided with a feed pipe 212 and a cold gas collection pipe 213, the feed pipe 212 is connected with the feed end of the plurality of vortex tubes 211, the cold gas end of the plurality of vortex tubes 211 is connected with the cold gas collection pipe 213, the cold gas collection pipe 213 of the vortex tube unit 21 is connected with the feed pipe 212 of the next vortex tube unit 21 connected in series; 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 with the hot discharge pipe 22, the cold discharge pipe 23 is the cold gas collection pipe 213 of the vortex tube unit 21 located at the last end of the series, the cold discharge pipe 23 is connected with the stable column 1, and the vortex tube module 2 is used for energy and mass separation of raw materials entering the stable column 1 or the overhead gas stream of the stable column 1.

[0021] The stable column coupling enhanced separation device of the present application introduces a vortex tube module 2 composed of multiple levels in series or single level in parallel into the gas phase loop at the front end or top of the stable column 1, so that the high-pressure mixed fluid entering the separation device enters the inside of the vortex tube 211 in a tangential manner and forms a high-speed rotating strong vortex flow field under its own pressure without external power, and under the combined action of centrifugal force, radial pressure gradient and axial backflow, significant energy and component distribution differences are generated inside the fluid, in which the heavy components with high temperature, high enthalpy value and large density tend to the pipe wall area and are discharged along the outer spiral flow direction to form a hot gas stream, while the light components with low temperature, low enthalpy value and small density gather to the pipe axis center and are discharged along the inner spiral flow to form a cold gas stream; the series connection of multiple vortex tube units 21 enables the cold gas stream after separation of the previous stage to further enter the vortex tube 211 of the next stage, so as to realize the step-by-step amplification of the energy and quality separation effect while maintaining the fluid momentum and pressure gradient, thereby obtaining more significant temperature drop and component enrichment effect as a whole, and the parallel structure of multiple vortex tubes 211 in a single stage effectively shares the flow and reduces the load of a single tube, so as to ensure that the stable swirling intensity and separation efficiency can still be maintained under large processing capacity conditions; the material after the above energy and quality pre-classification enters the stable column 1 again, so that the vapor-liquid balance condition in the column is optimized, the repeated vaporization and condensation process of light components in the column is reduced, the heat load of the reboiler 6 and the condensing system is significantly reduced, the essence of the separation process is enhanced without changing the main structure of the stable column 1, thereby effectively reducing the comprehensive energy consumption of the absorption stabilization system, improving the separation efficiency and operation flexibility, and having good engineering adaptability and energy-saving application value.

[0022] The vortex tube module 2 of the present application has the remarkable features of high economic benefit, strong adaptability and high process flexibility: it has a simple and compact structure, adopts pure mechanical design and has no fragile parts inside, has low investment cost, long service life and extremely low operation and maintenance cost; at the same time, the series and parallel number of vortex tube units can be flexibly adjusted according to the raw material processing capacity and separation precision requirements, the device structure is compact, and it is suitable for absorption stabilization systems of different scales and different separation precision requirements, especially for working conditions with higher energy-saving requirements; in addition, the device can realize multiple process forms combining feed flash evaporation and vortex tube rectification, and the most suitable process scheme can be flexibly selected according to the actual production conditions, so as to meet the diversified industrial application requirements.

[0023] Specifically, the cold gas ends of multiple vortex tubes 211 under the same vortex tube unit 21 are connected with the cold gas collecting pipe 213. It should be noted that the vortex tube module 2, the vortex tube unit 21 and the vortex tube 211 all have an inlet end, a cold gas output end and a hot gas output end; the input end of the vortex tube module 2 is the feed pipe 212 port of the first vortex tube unit 21, and the vortex tube module 2 has two output ends, which are the hot discharge pipe 22 and the cold discharge pipe 23.

[0024] Specifically, the number of vortex tube units 21 in series, and the number of vortex tubes 211 in parallel in the vortex tube unit 21 are selected according to the raw material processing capacity, such as the number of vortex tube units 21 in series is 8 according to the separation precision requirement.

[0025] As shown in Figure 1 and Figure 2 In the first embodiment of the present application, the stable column coupling enhanced separation device further comprises a feed flash tank 3, the input pipeline 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 with the input end of the vortex tube module 2, the liquid output end 302 of the feed flash tank 3 is connected with the stable column 1, and the hot discharge pipe 22 and the cold discharge pipe 23 are both connected with the stable column 1.

[0026] By arranging the feed flash tank 3 on the feed side of the stable column 1 and configuring the feed heat exchanger 31 on the input pipeline thereof, the raw material is first heated by heat exchange and preliminarily separated by phase equilibrium in the flash tank before entering the stable column 1, part of the light components are separated out in the form of gas and directly enter the vortex tube module 2 for further energy and quality separation, and the liquid phase enters the stable column 1 with lower light component content, thereby reducing the vaporization load of the feed of the stable column 1 from the source; at the same time, the hot gas flow and the cold gas flow separated by the vortex tube module 2 are respectively sent back to different positions of the stable column 1 with different heat requirements, thereby realizing the collaborative use of heat and cold in the column and reducing the invalid energy consumption caused by repeated vaporization and condensation of light components in the column; through the multi-stage coupling structure of feed heat exchange, flash pre-separation and vortex tube 211 enhanced energy and quality separation, the feed state of the stable column 1 and the mass transfer driving force in the column are optimized as a whole, thereby further reducing the load of the reboiler 6 and the condensing system under the premise of not increasing additional power consumption, improving the energy utilization efficiency and operation stability of the system, and the overall energy saving effect is more significant, which is suitable for deep energy saving reconstruction of the absorption and stabilization system under high load conditions.

[0027] Specifically, the cold side channel of the feed heat exchanger 31 is connected with the pipeline of the raw material to be treated, the hot side channel of the feed heat exchanger 31 is connected with the stable gasoline output pipeline at the bottom of the column body of the stable column 1, and the stable gasoline output pipeline at the bottom of the column body of the stable column 1 is provided with the feed flash tank 3.

[0028] As shown in Figure 1 and Figure 2 In the first embodiment of the present application, the upper part of the stable column 1 and the lower part of the stable column 1 are respectively provided with an upper feed inlet and two lower feed inlets, the liquid output end 302 of the feed flash tank 3 and the hot discharge pipe 22 are respectively connected with the two lower feed inlets, and the cold discharge pipe 23 is connected with the upper feed inlet.

[0029] The liquid output end 302 of the feed flash tank 3 and the hot discharge pipe 22 of the vortex tube module 2 are introduced into the lower part of the stabilizing tower 1, and the cold discharge pipe 23 separated from the vortex tube module 2 is introduced into the upper part of the stabilizing tower 1, so that the streams with different temperatures, enthalpy values and component characteristics enter the tower at their thermodynamic optimal positions: the stream with high temperature, high enthalpy value and rich in heavy components cooperates with the reboiling zone at the lower part of the tower, so as to enhance the vaporization driving force and reduce the heat supply demand of the reboiler 6, and the cold stream with low temperature, low enthalpy value and rich in light components directly participates in the condensation and rectification process at the upper part of the tower, so as to weaken the condensation load at the top of the tower and improve the separation conditions of the light components; through the arrangement mode of “graded feeding and heat counterposition utilization”, the temperature gradient, gas-liquid load distribution and mass transfer driving force in the stabilizing tower 1 are more reasonable, the invalid heat circulation and component backmixing in the tower are significantly reduced, the separation efficiency and operation stability of the stabilizing tower 1 are further improved under the premise of not increasing the system complexity and energy consumption, and the overall energy saving and consumption reduction effect is more prominent.

[0030] As shown in Figure 1 and Figure 2 in the embodiment one of the present application, the liquid output end 302 of the feed flash tank 3 is connected with the feed port of the stabilizing tower 1 through the first pipeline, the first pipeline is provided with a flow regulating valve, and the gas output end 301 of the feed flash tank 3 is connected with the input end of the vortex tube module 2 through the second pipeline, and the second pipeline is provided with a pressure monitoring instrument.

[0031] By introducing the liquid output end 302 of the feed flash tank 3 into the feed port of the stabilizing tower 1 through the first pipeline provided with the flow regulating valve, the liquid phase feed amount entering the stabilizing tower 1 can be finely regulated according to the load change in the tower, so as to stabilize the risk of liquid flooding in the stabilizing tower 1 and optimize the gas-liquid contact conditions; at the same time, by introducing the gas output end 301 of the feed flash tank 3 into the input end of the vortex tube module 2 through the second pipeline provided with the pressure monitoring instrument, the gas phase pressure state entering the vortex tube 211 is monitored and regulated in real time, so as to ensure that the vortex tube 211 forms a stable vortex flow under the condition of appropriate pressure difference and maintains good energy-mass separation effect; through the coordinated monitoring and regulation of the liquid phase flow and the gas phase pressure, a controllable and stable coupled operation state is formed in the processes of feed flashing, separation of the vortex tube 211 and rectification of the stabilizing tower 1, which not only improves the system operation safety and working condition adaptability, but also ensures the long-term stable play of the enhanced separation effect, and provides strong support for the reliable operation under the overall energy saving and consumption reduction and high load working condition.

[0032] As shown in Figure 1 and Figure 2As shown in the embodiment one of the present application, the stable column coupling enhanced separation device of the present application further comprises a condenser 4, a reflux tank 5 and a first reflux pump 51, the top of the column body of the stable column 1, the condenser 4, the reflux tank 5 and the first reflux pump 51 are sequentially connected in communication through pipelines, the reflux end of the first reflux pump 51 is connected in communication with the top of the stable column 1, and the first reflux pump 51 is provided with a product output pipeline for outputting liquefied petroleum gas.

[0033] By sequentially arranging the condenser 4, the reflux tank 5 and the first reflux pump 51 at the top of the stable column 1, a stable and reliable column top condensation reflux system is formed, so that the light component gas phase separated by the stable column 1 can be efficiently condensed and realize gas-liquid separation in the reflux tank 5, thereby stably supplying reflux liquid required for rectification while continuously sending liquefied petroleum gas as a product out of the first reflux pump 51; on the one hand, the structure maintains a reasonable temperature and concentration distribution in the column through stable and adjustable reflux ratio, ensures the stability of the separation effect and product quality of the stable column 1, and on the other hand, cooperates with the front-end feed flash and vortex tube 211 to reduce the invalid circulation load and condensation heat demand of the light component at the top of the column, improve the operation efficiency of the condensation system, realize stable recovery of liquefied petroleum gas product and further improve the overall energy efficiency of the system without increasing additional power consumption and operation complexity, and has good continuous operation performance.

[0034] Specifically, the stable column 1 is provided with 56 trays, a condenser 4, a top reflux tank 5 and a first reflux pump 51 at the top, and a reboiler 6 at the bottom. A part of the outlet stream of the first reflux pump 51 is extracted as a product LPG, and a part is returned to the top of the column body of the stable column 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 in communication with the reflux tank 5, and the output end of the first reflux pump 51 is used to output liquefied petroleum gas product.

[0035] As shown in the embodiment one of the present application, the stable column coupling enhanced separation device of the present application further comprises a condenser 4, a reflux tank 5 and a first reflux pump 51, the top of the column body of the stable column 1, the condenser 4, the reflux tank 5 and the first reflux pump 51 are sequentially connected in communication through pipelines, the reflux end of the first reflux pump 51 is connected in communication with the top of the stable column 1, and the first reflux pump 51 is provided with a product output pipeline for outputting liquefied petroleum gas. Figure 1 As shown in an optional embodiment of the present application, the feed pipe 212 is provided with a separator, the cold gas collection pipe 213 is provided with a mixer, and the hot discharge pipe 22 and the cold discharge pipe 23 are each provided with a pressure monitoring instrument.

[0036] By setting the separator on the feed pipe 212 of the vortex tube module 2, the material entering the vortex tube 211 can be effectively preliminarily separated from gas or impurities before entering the cyclone separation, avoiding the interference of liquid droplet entrainment or uneven feed on the stability of the cyclone field, so as to ensure the formation quality and energy separation effect of the internal cyclone structure of the vortex tube 211; at the same time, the mixer is arranged on the cold gas collecting pipe 213, so that the cold gas streams from multiple parallel vortex tubes 211 can be uniformly mixed and state integrated during the collection process, reducing the temperature, pressure and component fluctuation, and providing a stable and controllable cold source stream for the subsequent stable tower 1 or heat exchange unit; in addition, the pressure monitoring instrument is arranged on the hot discharge pipe 22 and the cold discharge pipe 23 respectively, so that the pressure state of the two streams after the separation of the vortex tube 211 can be monitored in real time, so that the running condition and separation effect of the vortex tube 211 can be judged in time, and the rapid early warning and adjustment of abnormal working condition of the system can be realized; through the above structure, the stability, controllability and engineering reliability of the vortex tube module 2 are further improved, and the energy saving effect is ensured to be continuously played in the long-term running process.

[0037] In an optional embodiment of the present application, a throttle valve is arranged at the inlet end of each vortex tube 211, and the throttle valve is used to adjust the feed flow and pressure of the single vortex tube 211.

[0038] By independently arranging the throttle valve at the inlet end of each vortex tube 211, the feed flow and pressure entering the single vortex tube 211 can be finely adjusted, so that each vortex tube 211 can maintain appropriate and consistent pressure difference conditions in the parallel running state, so as to form a stable high-speed cyclone field and fully play the energy separation effect; this structure effectively avoids the problem of separation efficiency reduction caused by uneven flow distribution or insufficient local pressure difference, improves the balance and reliability of the overall operation of the multi-vortex tube module 2, and can flexibly adjust the number of vortex tubes 211 and the single tube working condition according to the device load change, thereby enhancing the adaptability of the system to different processing capacity and working condition fluctuation; without adding additional power equipment, the controllable strengthening of the separation performance of the vortex tube 211 is realized, the long-term, stable and efficient operation of the stable tower 1 coupling separation process is ensured, and the energy saving effect and engineering application value of the system are further improved.

[0039] As shown in Figure 2 and Figure 3 , in an optional embodiment of the present application, the stable tower 1 is provided with a gasoline output pipe 11, and the gasoline output pipe 11 is provided with a reboiler 6.

[0040] By setting the gasoline output pipeline 11 at the bottom of the stabilizing tower 1 and configuring the reboiler 6, the bottom stable gasoline is continuously sent out while obtaining controllable heat compensation, providing the necessary and stable vaporization driving force for the tower, ensuring that the light components are fully removed from the tower bottom gasoline; The reboiler 6 cooperates with the front-end vortex tube module 2 to separate the energy and quality of the feed or tower top gas stream, so that the material entering the stabilizing tower 1 is in an optimized temperature and enthalpy state, thereby reducing the unit heat supply requirement of the reboiler 6 and reducing the invalid heating process; By concentrating the reboiling function in the tower bottom gasoline circuit, not only is it beneficial to accurately control the tower bottom product quality and the temperature distribution in the tower, but also improves the stability and thermal efficiency of the stabilizing tower 1 operation as a whole, achieving the dual effects of controllable stable gasoline quality and reduced system energy consumption.

[0041] As shown in Figure 2 and Figure 6 In Example One, the application also provides a stabilizing tower coupled enhanced separation method, which uses the above-mentioned stabilizing tower coupled enhanced separation device and the feed flash process. The method comprises: the mixed raw material of liquefied petroleum gas and stable gasoline exchanges heat after passing through the feed heat exchanger 31, and the heat-exchanged mixed raw material enters the feed flash tank 3 to perform flash separation at a preset temperature and pressure, obtaining a flash gas phase and a flash liquid phase; The flash gas phase enters the vortex tube module 2 to realize energy and quality separation, and the separated cold gas stream and hot gas stream are obtained, the cold gas stream is sent into the upper feed inlet of the stabilizing tower 1 through the cold discharge pipe 23, and the hot gas stream is sent into the lower feed inlet of the stabilizing tower 1 through the hot discharge pipe 22; The flash liquid phase enters the lower feed inlet of the stabilizing tower 1, the gas phase in the top of the stabilizing tower 1 is treated by condensation and the like and then outputs the liquefied petroleum gas product, and the bottom of the stabilizing tower 1 outputs the stable gasoline product.

[0042] By combining feed heat exchange, flash pre-separation, vortex tube 211 energy separation and stable column 1 distillation process, the mixed feedstock of liquefied petroleum gas and stabilized gasoline is optimized and controlled in multiple levels of thermodynamic state and component distribution before entering the stable column 1: after recovering the system waste heat through the feed heat exchanger 31, the mixed feedstock enters the feed flash tank 3, and the light component gas phase is precipitated in advance under the set temperature and pressure conditions, significantly reducing the subsequent distillation load; the flash gas phase further enters the vortex tube module 2, and under the condition of no external power, it relies on its own pressure to form a strong vortex field, realizes the energy and quality separation of cold and hot gas streams, and introduces them into the upper and lower parts of the stable column 1 according to their temperature and enthalpy characteristics, so that the heat and mass transfer driving force in the column are utilized in place; at the same time, the flash liquid phase directly enters the lower part of the column to participate in the distillation, reducing the repeated vaporization and condensation process of light components in the column. Through the above method, the reboiling and condensation load of the stable column 1 is significantly reduced, and the temperature gradient and gas-liquid load distribution in the column are more reasonable, which effectively reduces the comprehensive energy consumption of the system, improves the operation stability and working condition adaptability, especially suitable for energy-saving reconstruction and industrial application of high-load and high-energy absorption stabilization system.

[0043] Specifically, in Example One, the feed flow rate of the stabilizing column 1 is 330.6 t / h, the feed temperature is 124℃, and the feed pressure is 1.47 MPa, wherein the mass fraction of liquefied petroleum gas is 21.5%, and the mass fraction of stabilized gasoline is 78.5%. The stabilizing column 1 feed first enters the feed heat exchanger 31 and exchanges heat with the stabilized gasoline discharged from the bottom of the stabilizing column 1. After heat exchange, the temperature of the feed increases to 151℃, and then the feed enters the feed flash tank 3. In the feed flash tank 3, flash separation is carried out at a temperature of 151℃ and a pressure of 1.47 MPa, to obtain a flash liquid phase and a flash gas phase. 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 into the stabilizing column 1 from the 28th tray of the stabilizing column 1 from bottom to top. The flash gas phase has a flow rate of 89.1 t / h, a temperature of 151℃, and a pressure of 1.47 MPa, and is introduced into the vortex tube module 2 for energy quality separation. After separation by the vortex tube module 2, two streams of cold gas flow and hot gas flow are obtained. The cold gas flow has a flow rate of 55.3 t / h, a temperature of 140℃, and a pressure of 1.37 MPa, and is introduced into the stabilizing column 1 from the 26th tray of the stabilizing column 1 from bottom to top. The hot gas flow has a flow rate of 33.8 t / h, a temperature of 160℃, and a pressure of 1.37 MPa, and is introduced into the stabilizing column 1 from the 30th tray of the stabilizing column 1. By introducing gas phase streams with different temperature and enthalpy characteristics into the stabilizing column 1 at different heights, the utilization of heat and mass transfer driving force in the column is optimized. The liquefied petroleum gas gas phase enriched in C3-C4 components is discharged from the top of the stabilizing column 1, cooled to a liquid phase by the condenser 4, and then part of the liquefied petroleum gas is returned to the top of the stabilizing column 1 as reflux liquid through the first reflux pump 51 at the top of the column, and the other part is sent out as product. The mass fraction of C3-C4 components in the obtained liquefied petroleum gas product is 99.0%. The stabilized gasoline enriched in C5+ components is continuously discharged from the bottom of the stabilizing column 1 as product, and the mass fraction of C5+ components in the product is 98.7%. The specific parameters of the stabilizing column 1 are as follows: the total number of trays of the stabilizing column 1 is 56, the pressure at the top of the column is 1.229 MPa, the temperature at the top of the column is 64℃, the condenser 4 at the top of the column requires 3638 t / h of circulating water, and the corresponding cooling load is 21136 kW; the pressure at the bottom of the column is 1.30 MPa, the temperature at the bottom of the column is 187℃, the reboiler 6 at the bottom of the column uses 3.5 MPa medium-pressure steam as heat source, and the steam consumption is 32 t / h, and the corresponding reboiling load is 17537 kW. Through the above working condition setting, efficient separation of liquefied petroleum gas and stabilized gasoline is realized, and while ensuring stable and qualified product quality, the overall energy consumption of the stabilizing column 1 is effectively reduced.

[0044] As 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.

[0045] 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.

[0046] By introducing the overhead gas phase of the stabilizer 1 directly into the vortex tube module 2, and setting two independent circuits of cold and hot respectively and the corresponding cooling, buffering and reflux systems, the overhead gas phase completes energy and mass redistribution without increasing additional power consumption: after separation by the vortex tube 211, the cold gas stream rich in C3-C4 light components is cooled by the first cooler 7 and enters the first reflux pump 51, part of which is directly sent out as liquefied petroleum gas product, and the other part is refluxed to the top of the stabilizer 1 to maintain the necessary rectification reflux amount; while the hot gas stream containing a small amount of C5+ heavy components is cooled by the second cooler 8, and then all of it is sent back to the top of the stabilizer 1 through the buffer tank 9 and the second reflux pump 52 to participate in the separation again, thereby effectively inhibiting the entrainment of heavy components into the liquefied petroleum gas product; by implementing the closed-circuit coupling mode of energy and mass separation, separate cooling and differential reflux on the overhead gas phase, the instantaneous load of the overhead condensing system is significantly reduced, the gas-liquid equilibrium conditions in the tower are improved, and the ineffective circulation of light and heavy components in the overhead region is reduced, thereby ensuring the quality of LPG and stabilized gasoline products to be stable and up to standard, improving the separation efficiency and operation stability of the overhead, further tapping the energy-saving potential of the stabilizer 1 system, and having good engineering application value.

[0047] 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.

[0048] 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.

[0049] 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.

[0050] 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.

[0051] 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: Table 1. Energy values ​​of the stabilizer tower feed flash evaporation process in Example 1 Table 2 shows the energy values ​​of the conventional feed flash evaporation process in the stabilizer tower in Comparative Example 1. Table 3 Energy values ​​of the distillation-mixing process in Example 2 Table 4. Energy values ​​of the conventional distillation-mixing process in Comparative Example 2 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.

[0052] 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.

[0053] 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 gas flow at the top of the stabilizer.

2. The stabilizing tower coupling enhancement separation device according to claim 1, characterized in that, 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.

3. The stabilizer tower coupling enhancement separation device according to claim 2, characterized in that, 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.

4. The stabilizing tower coupling enhancement separation device according to claim 2, 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.

5. The stabilizing tower coupling enhancement separation device according to claim 2, characterized in that, 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.

6. 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.

7. 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.

8. 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.

9. 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 2-5 includes: 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.

10. A method for enhancing separation through coupling in a stable tower, characterized in that, The method using the stabilizing tower coupling enhancement separation device according to any one of claims 8 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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