CN114984604A - Continuous double-tower distillation system - Google Patents
Continuous double-tower distillation system Download PDFInfo
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- CN114984604A CN114984604A CN202210766175.8A CN202210766175A CN114984604A CN 114984604 A CN114984604 A CN 114984604A CN 202210766175 A CN202210766175 A CN 202210766175A CN 114984604 A CN114984604 A CN 114984604A
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- 238000004821 distillation Methods 0.000 title claims abstract description 163
- 238000005194 fractionation Methods 0.000 claims abstract description 30
- 238000007789 sealing Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 27
- 230000001105 regulatory effect Effects 0.000 claims description 26
- 230000005540 biological transmission Effects 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 8
- 238000006073 displacement reaction Methods 0.000 claims description 4
- 239000011810 insulating material Substances 0.000 claims description 4
- 210000003437 trachea Anatomy 0.000 claims description 2
- 230000009977 dual effect Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 description 41
- 230000007246 mechanism Effects 0.000 description 11
- 238000011084 recovery Methods 0.000 description 9
- 238000009835 boiling Methods 0.000 description 5
- 230000003247 decreasing effect Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 230000003139 buffering effect Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention belongs to the technical field of distillation, and particularly relates to a continuous double-tower distillation system which comprises an evaporator, a first distillation tower and a second distillation tower, wherein the first distillation tower is detachably mounted on the top surface of the evaporator, the top surface of the first distillation tower is detachably connected with a first sealing end cover, the bottom surface of the second distillation tower is detachably connected with a discharge base, and the first sealing end cover is connected with the discharge base through a pipeline; a plurality of sliding fractionation trays are arranged inside the first distillation column and the second distillation column, and the positions of the fractionation trays are adjusted according to the internal temperature change of the first distillation column or the second distillation column; according to the invention, the sliding fractionation tray is arranged in the distillation tower, so that the position of the fractionation tray is matched with the change of the temperature interval of the steam in the first distillation tower, namely the fractionation tray is always positioned on a proper isotherm, all components in the steam can be liquefied in the proper temperature interval, and the purity of the distillation product in the first distillation tower is improved.
Description
Technical Field
The invention belongs to the technical field of distillation, and particularly relates to a continuous double-tower distillation system.
Background
The continuous double-tower distillation system is characterized in that two distillation towers are connected in series to realize the distillation function, and compared with a single-tower distillation system, the continuous double-tower distillation system not only can further improve the yield of the distillation towers and the concentration of products, but also can improve the working efficiency of the distillation towers;
the continuous double-tower distillation system can also be additionally provided with a waste heat recovery system, so that the heat of the system is recovered, and the energy loss is reduced;
the continuous double-tower distillation system comprises an evaporation mechanism, the evaporation mechanism heats materials entering the continuous double-tower distillation system into steam, and in the process that the steam rises in the distillation tower, because the steam flows in the distillation tower and can rub against the inner wall of the distillation tower and the liquid recovery mechanism, the steam does not rise uniformly in the distillation tower after being influenced by the inner wall of the distillation tower and the liquid recovery mechanism, so that the temperature interval of the steam in the distillation tower is not fixed and constant;
the position of a liquid recovery mechanism in a traditional distillation tower is fixed, but the temperature range of the distillation tower can be changed, if the isotherm in the traditional distillation tower moves upwards, the temperature in the temperature range corresponding to the liquid recovery mechanism is too high, components which are originally liquefied on the liquid recovery mechanism cannot be liquefied or the liquefaction effect is very weak, other components with high boiling points can be liquefied on the liquid recovery mechanism, and the purity of the components is reduced, if the isotherm in the traditional distillation tower moves downwards, namely the temperature in the temperature range corresponding to the liquid recovery mechanism is too low, and the components with other bottom boiling points can be liquefied on the liquid recovery mechanism, and the purity of the components can also be reduced.
Disclosure of Invention
In order to make up for the defects of the prior art, the invention provides a continuous double-tower distillation system, a sliding fractionation tray is arranged in a distillation tower, so that the position of the fractionation tray is matched with the change of the temperature interval of steam in a first distillation tower, namely the fractionation tray is always positioned on a proper isotherm, all components in the steam can be liquefied in the proper temperature interval, and the purity of a distillation product in the first distillation tower is improved.
The technical scheme adopted by the invention for solving the technical problems is as follows: the invention relates to a continuous double-tower distillation system which comprises an evaporator, a first distillation tower and a second distillation tower, wherein the first distillation tower is detachably mounted on the top surface of the evaporator, the top surface of the first distillation tower is detachably connected with a first sealing end cover, the bottom surface of the second distillation tower is detachably connected with a discharge base, and the first sealing end cover is connected with the discharge base through a pipeline;
the first and second distillation columns are internally provided with a plurality of sliding fractionation trays for collecting the distilled liquid components, the fractionation trays being positionally adjusted according to a change in internal temperature of the first or second distillation column.
Preferably, a distillation tank is arranged in the middle of the top surface of the fractionation tray and used for circulation of steam in the first distillation tower or the second distillation tower, a baffle is fixedly connected to the bottom surface of the fractionation tray, which is close to the distillation tank, through a long rod, the top area of the baffle is larger than the sectional area of the distillation tank, and the baffle is used for blocking the distillation tank, reducing the flow rate of the steam and increasing the contact area of the fractionation tray and the steam.
Preferably, the inner walls of the first distillation tower and the second distillation tower are provided with a plurality of limiting sliding grooves, the limiting sliding grooves are used for limiting the displacement of the fractionating plate, and the limiting sliding grooves can be other limiting mechanisms and are mainly used for limiting the displacement of the fractionating plate and playing a role in guiding.
Preferably, the bottom of spacing spout is equipped with the supporting seat, the top surface of evaporimeter can be dismantled and is connected with the air pump, the air pump passes through the trachea and is connected with the supporting seat for the intraductal atmospheric pressure of control cylinder.
Preferably, a cylindrical pipe matched with the limiting sliding groove is fixedly connected to the side surface of the fractionating plate, which is close to the limiting sliding groove.
Preferably, the top surface fixedly connected with pressure regulating stick of supporting seat, the top surface fixedly connected with piston of pressure regulating stick, the piston agrees with mutually with the inner wall of cylinder pipe, and can slide along the inner wall of cylinder pipe, and the pressure regulating stick is used for cooperating the cylinder pipe, makes the fractionating tray according to the temperature automatically regulated position in first distillation column or the second distillation column.
Preferably, a gas pipeline penetrates through the pressure regulating rod, and the supporting seat is communicated with the cylindrical pipe through the gas pipeline.
Preferably, the pressure regulating rod is made of heat insulating materials, and a circle of vacuum cavity can be arranged on the outer side of the gas transmission pipeline to isolate heat transfer.
Preferably, liquid outlet pipelines are inserted into the side walls of the first distillation tower and the second distillation tower, and the liquid outlet pipelines are L-shaped.
Preferably, a diversion pipeline is inserted in a position, close to the liquid outlet pipeline, on the bottom surface of the fractionating plate, and the outer diameter of the liquid outlet pipeline is equal to the inner diameter of the diversion pipeline.
The invention has the following beneficial effects:
1. according to the invention, the sliding fractionating plate is arranged in the distillation tower, so that the position of the fractionating plate is matched with the change of the temperature interval of the steam in the first distillation tower, namely the fractionating plate is always positioned on a proper isotherm, all components in the steam can be liquefied in the proper temperature interval, and the purity of the distillation product in the first distillation tower is improved.
2. The distillation tray is provided with the distillation groove on the top surface and the baffle on the bottom surface, the distillation groove arranged in the middle of the distillation tray is used for the circulation of steam, the baffle fixedly connected with the bottom surface of the distillation tray plays a role in flow inhibition, the flow speed of the steam is reduced, the retention time of the steam in the first distillation tower is prolonged, the distillation product rate is improved, and the contact area of the steam and the baffle can be increased, so that the steam is convenient to liquefy.
3. According to the invention, through the arranged pressure regulating rod, when the fractionating tray is installed, the fractionating tray can be directly put down by aiming at the limiting sliding chute, because when the fractionating tray descends to the position of the pressure regulating rod, the piston at the top of the pressure regulating rod can be inserted into the cylindrical pipe to form a cylinder structure, the cylindrical pipe is originally filled with air, the air transmission pipeline is connected with the air pump through a pipeline, and after the piston is inserted into the cylindrical pipe, the air transmission pipeline and the inner cavity of the cylindrical pipe can form a closed space, so that the air pressure in the closed space can be increased in the descending process of the fractionating tray, and meanwhile, the fractionating tray is supported by the pressure regulating rod, so that the fractionating tray is stably stopped, and a buffering effect is achieved.
Drawings
The invention is further described with reference to the following figures and embodiments.
FIG. 1 is a perspective view of the present invention;
FIG. 2 is a perspective view of a first distillation column in the present invention;
FIG. 3 is a front view of a first distillation column in the present invention;
FIG. 4 is a cross-sectional view taken at E-E of FIG. 3;
FIG. 5 is a schematic view of the structure of a first distillation column in the present invention;
FIG. 6 is a perspective view of a pressure regulating bar of the present invention;
fig. 7 is a perspective view of a fractionation tray according to the present invention.
In the figure: 1. an evaporator; 2. a first distillation column; 21. a limiting chute; 22. a supporting seat; 23. a pressure regulating rod; 231. a piston; 232. a gas pipeline; 24. a fractionating tray; 241. a distillation tank; 242. a baffle plate; 243. a cylindrical tube; 244. a diversion pipeline; 25. a liquid outlet pipeline; 3. a first end seal cap; 4. a discharge base; 5. a second distillation column; 6. a second end seal cap; 7. a condenser; 8. an air pump.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further described with the specific embodiments.
As shown in fig. 1 to 7, the continuous double-column distillation system according to the present invention includes an evaporator 1, a first distillation column 2 and a second distillation column 5, wherein the first distillation column 2 is detachably mounted on a top surface of the evaporator 1, a first sealing end cap 3 is detachably connected to the top surface of the first distillation column 2, a discharge base 4 is detachably connected to a bottom surface of the second distillation column 5, and the first sealing end cap 3 is connected to the discharge base 4 through a pipeline;
a plurality of sliding fractionation trays 24 are arranged inside the first distillation column 2 and the second distillation column 5, and the positions of the fractionation trays 24 are adjusted according to the internal temperature change of the first distillation column 2 or the second distillation column 5;
a distillation tank 241 is arranged in the middle of the top surface of the fractionation tray 24, a baffle 242 is fixedly connected to the position, close to the distillation tank 241, of the bottom surface of the fractionation tray 24 through a long rod, and the top area of the baffle 242 is larger than the sectional area of the distillation tank 241;
when the distillation device works, a mixed liquid to be distilled is injected into the evaporator 1 through a pipeline to be heated and evaporated to form steam, the evaporator 1 is communicated with the first distillation tower 2 to ensure that the steam in the evaporator 1 can enter the first distillation tower 2, and the fractionating tray 24 arranged in the first distillation tower 2 is arranged according to the temperature gradient in the first distillation tower 2, so that the temperature in the first distillation tower 2 is gradually reduced from bottom to top, and the fractionating tray 24 is arranged at a proper height according to different boiling points of different components in the mixed liquid, so that the components with corresponding high concentrations can be obtained;
in the process of the steam rising in the first distillation tower 2, because the steam flowing in the first distillation tower 2 is affected by the inner wall of the first distillation tower 2 and the fractionating tray 24, the steam does not rise uniformly, so that the temperature range of the steam in the first distillation tower 2 is not fixed, but the position of the fractionating tray 24 in the conventional distillation tower is fixed, but the temperature range of the distillation tower changes, if the isotherm in the conventional distillation tower moves upwards, i.e. the temperature in the temperature range corresponding to the fractionating tray 24 is too high, the component which is liquefied in the fractionating tray 24 will not be liquefied or the liquefaction effect is very weak, while other components with high boiling points will be liquefied in the fractionating tray 24, so that the purity of the component will decrease, if the isotherm in the conventional distillation tower moves downwards, i.e. the temperature in the temperature range corresponding to the fractionating tray 24 passes through the bottom, and other components with bottom boiling points will be liquefied in the fractionating tray 24, this also leads to a reduction in the purity of the component;
the fractionating tray 24 arranged in the first distillation tower 2 can slide, and the position is adjusted according to the temperature change in the first distillation tower 2, so that the position of the fractionating tray 24 is matched with the change of the temperature interval of the steam in the first distillation tower 2, that is, the fractionating tray 24 is always positioned on a proper isotherm, all components in the steam can be liquefied in the proper temperature interval, and the purity of the distillation product in the first distillation tower 2 is improved;
the distillation groove 241 provided in the middle of the fractionation tray 24 is used for the circulation of steam, and the baffle 242 fixedly connected to the bottom of the fractionation tray 24 plays a role of flow inhibition, thereby reducing the flow velocity of the steam, increasing the residence time of the steam in the first distillation tower 2, increasing the distillation yield, and the baffle 242 can increase the contact area with the steam, so that the steam is convenient for liquefaction.
As an embodiment of the present invention, the inner walls of the first distillation column 2 and the second distillation column 5 are provided with a plurality of limiting chutes 21, and the limiting chutes 21 are used for limiting the displacement of the fractionating plate 24;
the bottom of the limiting sliding chute 21 is provided with a supporting seat 22, the top surface of the evaporator 1 is detachably connected with an air pump 8, and the air pump 8 is connected with the supporting seat 22 through an air pipe;
a cylindrical pipe 243 matched with the limiting sliding groove 21 is fixedly connected to the side surface of the fractionating plate 24 close to the limiting sliding groove 21;
the top surface of the supporting seat 22 is fixedly connected with a pressure regulating rod 23, the top surface of the pressure regulating rod 23 is fixedly connected with a piston 231, and the piston 231 is fit with the inner wall of the cylindrical tube 243 and can slide along the inner wall of the cylindrical tube 243;
a gas transmission pipeline 232 penetrates through the pressure regulating rod 23, and the supporting seat 22 is communicated with the cylindrical pipe 243 through the gas transmission pipeline 232;
in operation, as shown in fig. 4, 6 and 7, the fractionating tray 24 is limited in the first distillation tower 2 or the second distillation tower 5 by the limiting sliding groove 21, since the cylindrical tube 243 fixedly connected to the side of the fractionating tray 24 fits with the limiting sliding groove 21, the limiting sliding groove 21 can make the fractionating tray 24 slide in the first distillation tower 2 more smoothly, and the fractionating tray 24 is detachable, therefore, when cleaning the first distillation tower 2, the fractionating tray 24 can be detached, so that the first distillation tower 2 and the fractionating tray 24 can be cleaned separately, thereby reducing the difficulty of cleaning, and, when installing the fractionating tray 24, the fractionating tray 24 can be directly lowered down by aligning to the limiting sliding groove 21, because when the fractionating tray 24 is lowered to the position of the pressure regulating rod 23, the piston 231 at the top of the pressure regulating rod 23 can be inserted into the cylindrical tube 243 to form a cylinder structure, since the cylindrical tube 243 is filled with air, the gas transmission pipeline 232 is connected with the gas pump 8 through a pipeline, and after the piston 231 is inserted into the cylindrical pipe 243, the gas transmission pipeline 232 and the inner cavity of the cylindrical pipe 243 form a closed space, so that the gas pressure in the closed space can be increased in the descending process of the fractionating tray 24, and meanwhile, the fractionating tray 24 is supported by the pressure regulating rod 23, so that the fractionating tray 24 is stably stopped, and a buffering effect is achieved;
when the first distillation column 2 is performing the distillation process, according to the van der waals equation:
wherein p is the pressure of the gas, i.e., the pressure in the gas transmission pipeline 232 and the cylindrical pipe 243;
a is a parameter for measuring intermolecular attraction;
b is the average size of the occupied space per molecule;
t is the thermodynamic temperature, i.e. the temperature in the interval of the fractionation tray 24 corresponding to the first distillation column 2;
r is a universal gas constant;
m is the mass of the gas, which is the total mass of the gas in the gas transmission pipeline 232 and the cylindrical pipe 243;
m is the molar mass, that is, the molar mass of the gas in the gas transmission line 232 and the cylindrical pipe 243;
in actual calculation, because the caliber of the gas transmission pipeline 232 is thin, the occupied gas is very little and can be ignored, but the gas pressure of the gas in the cylindrical pipe 243 can be read by an external barometer, then, according to the temperature interval T in the first distillation column 2, the gas pressure of the gas in the cylindrical tube 243 is adjusted by the gas pump 8, at a constant temperature, the larger the gas pressure p, the larger the volume V of the gas in the cylindrical tube 243, which ensures that the cylindrical tube 243 is further away from the pressure regulating rod 23, the position of the pressure regulating rod 23 is fixed, which results in a higher position of the cylindrical tube 243, therefore, the position of the fractionating plate 24 is ensured to be higher, and if the temperature of the temperature zone corresponding to the fractionating plate 24 is increased, that is, T is increased, the volume V also increases according to the van der waals equation, and the position of the fractionating plate 24 is raised to fit the temperature range.
The pressure regulating rod 23 is made of a heat insulating material;
during operation, the pressure regulating rod 23 is made of heat insulating material, so that the gas in the gas transmission pipeline 232 is not affected by the high-temperature steam at the bottom of the first distillation tower 2.
a guide pipeline 244 is inserted in the position, close to the liquid outlet pipeline 25, of the bottom surface of the fractionating tray 24, and the outer diameter of the liquid outlet pipeline 25 is equal to the inner diameter of the guide pipeline 244;
during operation, in the process of the fractionation tray 24 sliding up and down, the liquid outlet pipe 25 is inserted into the guide pipe 244, and when the fractionation tray 24 slides up and down, the liquid outlet pipe 25 and the guide pipe 244 are not separated from contact, so that the components liquefied in the fractionation tray 24 can always flow into the guide pipe 244 through the liquid outlet pipe 25, and the components are discharged by the guide pipe 244.
The first embodiment is as follows:
when the temperature zone corresponding to one of the fractionation trays 24 in the first distillation column 2 or the second distillation column 5 rises, that is, the temperature at which the fractionation tray 24 is located rises above the original set value, according to the van der waals equation:
t represents the temperature at the fractionating tray 24, and when T is increased, if the equation is satisfied, the pressure p of the gas in the cylindrical pipe 243 or the volume V of the gas is increased, the pressure p of the gas in the cylindrical pipe 243 is mainly affected by the gravity of the whole fractionating tray 24, so that the pressure p of the gas in the cylindrical pipe 243 is unchanged, the volume V of the gas in the cylindrical pipe 243 is increased, the height of the fractionating tray 24 is increased in the process that the volume V of the gas in the cylindrical pipe 243 is increased, the fractionating tray 24 is in a new temperature range, and the new temperature range is matched with the liquefaction temperature of the component again.
Example two:
when the temperature zone corresponding to one of the fractionation trays 24 in the first distillation column 2 or the second distillation column 5 is lowered, that is, the temperature at the position where the fractionation tray 24 is located is lowered below the preset value, according to the van der waals equation:
t represents the temperature at the fractionating tray 24, and when T is decreased, the equation is ensured to be satisfied, the pressure p of the gas in the cylindrical pipe 243 or the volume V of the gas is decreased, the pressure p of the gas in the cylindrical pipe 243 is mainly affected by the gravity of the whole fractionating tray 24, therefore, the pressure p of the gas in the cylindrical pipe 243 is not changed, the volume V of the gas in the cylindrical pipe 243 is decreased, the height of the fractionating tray 24 is decreased in the process that the volume V of the gas in the cylindrical pipe 243 is decreased, the fractionating tray 24 is in a new temperature range, and the new temperature range is matched with the liquefaction temperature of the component again.
Claims (10)
1. A continuous double-tower distillation system comprises an evaporator (1), a first distillation tower (2) and a second distillation tower (5), wherein the first distillation tower (2) is detachably mounted on the top surface of the evaporator (1), a first sealing end cover (3) is detachably connected to the top surface of the first distillation tower (2), a discharge base (4) is detachably connected to the bottom surface of the second distillation tower (5), and the first sealing end cover (3) is connected with the discharge base (4) through a pipeline;
the method is characterized in that: the first distillation column (2) and the second distillation column (5) are internally provided with a plurality of sliding fractionation trays (24), and the fractionation trays (24) are adjusted in position according to the internal temperature change of the first distillation column (2) or the second distillation column (5).
2. A continuous two-column distillation system according to claim 1, wherein: the distillation tray is characterized in that a distillation groove (241) is formed in the middle of the top surface of the distillation tray (24), a baffle (242) is fixedly connected to the position, close to the distillation groove (241), of the bottom surface of the distillation tray (24) through a long rod, and the top area of the baffle (242) is larger than the sectional area of the distillation groove (241).
3. A continuous two-column distillation system according to claim 1, wherein: the inner walls of the first distillation tower (2) and the second distillation tower (5) are provided with a plurality of limiting sliding grooves (21), and the limiting sliding grooves (21) are used for limiting the displacement of the fractionating plate (24).
4. A continuous two-column distillation system as claimed in claim 3, wherein: the bottom of spacing spout (21) is equipped with supporting seat (22), the top surface of evaporimeter (1) can be dismantled and is connected with air pump (8), air pump (8) are connected with supporting seat (22) through the trachea.
5. A continuous two-column distillation system as claimed in claim 3, wherein: the side surface of the fractionating plate (24) close to the position of the limiting sliding groove (21) is fixedly connected with a cylindrical pipe (243) which is matched with the limiting sliding groove (21).
6. A continuous two-column distillation system according to claim 4 or 5, wherein: the top surface of the supporting seat (22) is fixedly connected with a pressure regulating rod (23), the top surface of the pressure regulating rod (23) is fixedly connected with a piston (231), and the piston (231) is matched with the inner wall of the cylindrical pipe (243) and can slide along the inner wall of the cylindrical pipe (243).
7. A continuous two-column distillation system as claimed in claim 6, wherein: a gas transmission pipeline (232) penetrates through the pressure regulating rod (23), and the supporting seat (22) is communicated with the cylindrical pipe (243) through the gas transmission pipeline (232).
8. A continuous two-column distillation system as claimed in claim 7, wherein: the pressure regulating rod (23) is made of heat insulating materials.
9. A continuous two-column distillation system as claimed in claim 1, wherein: liquid outlet pipelines (25) are inserted into the side walls of the first distillation tower (2) and the second distillation tower (5), and the liquid outlet pipelines (25) are L-shaped.
10. A continuous dual column distillation system as claimed in claim 9, wherein: a flow guide pipeline (244) is inserted in a position, close to the liquid outlet pipeline (25), of the bottom surface of the fractionating plate (24), and the outer diameter of the liquid outlet pipeline (25) is equal to the inner diameter of the flow guide pipeline (244).
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