CN114984604B - Continuous double-tower distillation system - Google Patents
Continuous double-tower distillation system Download PDFInfo
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- CN114984604B CN114984604B CN202210766175.8A CN202210766175A CN114984604B CN 114984604 B CN114984604 B CN 114984604B CN 202210766175 A CN202210766175 A CN 202210766175A CN 114984604 B CN114984604 B CN 114984604B
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- 238000004821 distillation Methods 0.000 title claims abstract description 146
- 238000007789 sealing Methods 0.000 claims abstract description 8
- 238000007599 discharging Methods 0.000 claims abstract description 7
- 238000005194 fractionation Methods 0.000 claims description 57
- 230000001105 regulatory effect Effects 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 25
- 238000006073 displacement reaction Methods 0.000 claims description 4
- 239000012774 insulation material Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 2
- 239000007789 gas Substances 0.000 description 41
- 230000007246 mechanism Effects 0.000 description 11
- 238000011084 recovery Methods 0.000 description 9
- 230000007423 decrease Effects 0.000 description 7
- 230000005540 biological transmission Effects 0.000 description 5
- 238000009835 boiling Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000011810 insulating material Substances 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
- 210000003437 trachea Anatomy 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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, in particular 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 arranged 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 discharging base, and the first sealing end cover is connected with the discharging base through a pipeline; a plurality of sliding fractionating trays are arranged in the first distillation tower and the second distillation tower, and the positions of the fractionating trays are adjusted according to the internal temperature change of the first distillation tower or the second distillation tower; 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 steam in the first distillation tower, that is, the fractionating plate is always on a proper isothermal line, each component in the steam can be liquefied in a proper temperature interval, and the purity of the distilled product of 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 and the product concentration of the distillation towers, but also can improve the working efficiency of the distillation towers;
the continuous double-tower distillation system is also added 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, wherein the evaporation mechanism heats materials entering the continuous double-tower distillation system into steam, and during the rising process of the steam in a distillation tower, the steam flows in the distillation tower and rubs against the inner wall of the distillation tower and a liquid recovery mechanism, so that the steam does not uniformly rise in the distillation tower after being influenced by the inner wall of the distillation tower and the liquid recovery mechanism, and the temperature interval of the steam in the distillation tower is not fixed;
the position of the recovery liquid mechanism in the traditional distillation tower is fixed, but the temperature interval of the distillation tower is changed, if the isothermal line in the traditional distillation tower moves upwards, the temperature in the temperature interval corresponding to the recovery liquid mechanism is too high, the components which are liquefied on the recovery liquid mechanism are not liquefied or have very weak liquefying effect, other components with high boiling points are liquefied on the recovery liquid mechanism, the purity of the components is reduced, and if the isothermal line in the traditional distillation tower moves downwards, namely, the temperature in the temperature interval corresponding to the recovery liquid mechanism is too low, and other components with bottom boiling points are liquefied on the recovery liquid mechanism, the purity of the components is 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, wherein a sliding fractionating plate is arranged in a distillation tower, so that the position of the fractionating plate is matched with the change of the temperature interval of steam in a first distillation tower, that is, the fractionating plate is always on a proper isothermal line, each component in the steam can be liquefied in a proper temperature interval, and the purity of a distilled product of the first distillation tower is improved.
The technical scheme adopted 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 arranged 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 discharging base, and the first sealing end cover is connected with the discharging base through a pipeline;
the first distillation column and the second distillation column are internally provided with a plurality of sliding fractionation trays for collecting distilled liquid components, and the fractionation trays are adjusted in position according to the internal temperature change of the first distillation column or the second distillation column.
Preferably, a distillation tank is provided in the middle of the top surface of the fractionating plate for the circulation of steam in the first distillation tower or the second distillation tower, a baffle is fixedly connected to the bottom surface of the fractionating plate, which is close to the distillation tank, through a long rod, the top surface area of the baffle is larger than the sectional area of the distillation tank, the baffle is used for blocking the distillation tank, reducing the flow rate of steam, and increasing the contact area of the fractionating plate and 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 fractionation tray, and the limiting sliding grooves can also be other limiting mechanisms and are mainly used for limiting the displacement of the fractionation tray and playing a guiding role.
Preferably, the bottom of spacing spout is equipped with the supporting seat, the top surface of evaporimeter can be dismantled and be connected with the air pump, the air pump passes through the trachea and is connected with the supporting seat for the atmospheric pressure in the control cylinder pipe.
Preferably, a cylindrical pipe matched with the limiting chute is fixedly connected to the side surface of the fractionating plate close to the limiting chute.
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 the inner wall of cylinder pipe, and can follow the inner wall slip of cylinder pipe, and the pressure regulating stick is used for cooperating the cylinder pipe, makes the fractionation tray according to the temperature automatically regulated position in first distillation column or the second distillation column.
Preferably, the pressure regulating rod is internally penetrated with a gas transmission pipeline, and the supporting seat is communicated with the cylindrical pipe through the gas transmission pipeline.
Preferably, the pressure regulating rod is made of heat insulation materials, and a circle of vacuum cavity can be arranged on the outer side of the gas transmission pipeline for isolating heat transfer.
Preferably, the side walls of the first distillation tower and the second distillation tower are penetrated with liquid outlet pipelines, and the shape of the liquid outlet pipelines is L-shaped.
Preferably, a diversion pipeline is inserted in the position, close to the liquid outlet pipeline, of 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 beneficial effects of the invention are as follows:
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 steam in the first distillation tower, that is, the fractionating plate is always on a proper isothermal line, each component in the steam can be liquefied in a proper temperature interval, and the purity of the distilled product of the first distillation tower is improved.
2. According to the invention, the distillation tank is arranged on the top surface of the fractionation tray, the baffle plate is arranged on the bottom surface of the fractionation tray, the distillation tank arranged in the middle of the fractionation tray is used for circulating steam, the baffle plate fixedly connected with the bottom surface of the fractionation tray plays a role in inhibiting flow, the flow speed of the steam is reduced, the residence time of the steam in the first distillation tower is improved, the distillation product rate is improved, and the contact area between the baffle plate and the steam can be increased by the baffle plate, so that the steam is convenient to liquefy.
3. According to the invention, when the fractionating plate is installed, the fractionating plate can be directly put down aiming at the limiting chute, because the piston at the top of the pressure regulating rod can be inserted into the cylindrical pipe to form a cylinder structure when the fractionating plate descends to the position of the pressure regulating rod, the cylindrical pipe is filled with air originally, the gas transmission pipeline is connected with the gas pump through the pipeline, and after the piston is inserted into the cylindrical pipe, the gas transmission pipeline and the inner cavity of the cylindrical pipe form a closed space, so that the gas pressure in the closed space can be increased in the descending process of the fractionating plate, and meanwhile, the fractionating plate is supported by the pressure regulating rod, so that the fractionating plate is stopped stably, and a buffering effect is achieved.
Drawings
The invention will be further described with reference to the drawings and embodiments.
FIG. 1 is a perspective view of the present invention;
FIG. 2 is a perspective view of a first distillation column in accordance with the present invention;
FIG. 3 is a front view of a first distillation column in accordance with the present invention;
FIG. 4 is a cross-sectional view taken at E-E of FIG. 3;
FIG. 5 is a schematic view showing the structure of a first distillation column according to the present invention;
FIG. 6 is a perspective view of a pressure regulating rod in accordance with 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. limiting sliding grooves; 22. a support base; 23. a pressure regulating rod; 231. a piston; 232. a gas line; 24. a fractionation tray; 241. a distillation tank; 242. a baffle; 243. a cylindrical tube; 244. a diversion pipeline; 25. a liquid outlet pipe; 3. a first seal end cap; 4. a discharging base; 5. a second distillation column; 6. a second seal end cap; 7. a condenser; 8. an air pump.
Detailed Description
The invention is further described in connection with the following detailed description in order to make the technical means, the creation characteristics, the achievement of the purpose and the effect of the invention easy to understand.
As shown in fig. 1 to 7, the continuous double-column distillation system of the invention comprises an evaporator 1, a first distillation column 2 and a second distillation column 5, wherein the first distillation column 2 is detachably arranged on the top surface of the evaporator 1, the top surface of the first distillation column 2 is detachably connected with a first sealing end cover 3, the bottom surface of the second distillation column 5 is detachably connected with a discharge base 4, and the first sealing end cover 3 is connected with 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 trays 24 adjust positions 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 fractionating plate 24, a baffle 242 is fixedly connected to the bottom surface of the fractionating plate 24 close to the distillation tank 241 through a long rod, and the top surface area of the baffle 242 is larger than the sectional area of the distillation tank 241;
during operation, 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, so that the steam in the evaporator 1 can enter the first distillation tower 2, a fractionating plate 24 arranged in the first distillation tower 2 is arranged according to a temperature gradient in the first distillation tower 2, and the temperature in the first distillation tower 2 is gradually reduced from bottom to top, and the fractionating plate 24 is arranged at a proper height according to different boiling points of different components in the mixed liquid, so that components with corresponding high concentration can be obtained;
during the rising of the steam in the first distillation column 2, the steam is not uniformly rising due to the influence of the inner wall of the first distillation column 2 and the fractionation tray 24 in the flow of the steam in the first distillation column 2, so that the temperature interval of the steam in the first distillation column 2 is not fixed, the position of the fractionation tray 24 in the conventional distillation column is fixed, but the temperature interval of the distillation column is changed, if the inner isotherm of the conventional distillation column is shifted upwards, that is, the temperature in the temperature interval corresponding to the fractionation tray 24 is too high, the components which are liquefied in the fractionation tray 24 are not liquefied or the liquefying effect is very weak, and other components with high boiling points are liquefied in the fractionation tray 24, so that the purity of the components is reduced, and if the inner isotherm of the conventional distillation column is shifted downwards, that is, the temperature in the temperature interval corresponding to the fractionation tray 24 is too low, and other components with low boiling points are liquefied in the fractionation tray 24, so that the purity of the components is reduced;
the fractionating plate 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 plate 24 is matched with the change of the temperature interval of the steam in the first distillation tower 2, that is, the fractionating plate 24 is always on a proper isothermal line, each component in the steam can be liquefied in a proper temperature interval, and the purity of the distilled product of the first distillation tower 2 is improved;
the distillation tank 241 arranged in the middle of the fractionation tray 24 is used for circulating steam, and the baffle 242 fixedly connected with the bottom surface of the fractionation tray 24 plays a role in inhibiting flow, so that the flow speed of the steam is reduced, the residence time of the steam in the first distillation tower 2 is prolonged, the distillation product rate is improved, and the contact area between the baffle 242 and the steam can be increased, so that the steam is convenient to liquefy.
As an embodiment of the present invention, a plurality of limiting sliding grooves 21 are formed on the inner walls of the first distillation column 2 and the second distillation column 5, and the limiting sliding grooves 21 are used for limiting the displacement of the fractionation tray 24;
the bottom of the limiting 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 tube 243 matched with the limit chute 21 is fixedly connected to the side surface of the fractionation tray 24 close to the limit chute 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 matched with the inner wall of the cylindrical tube 243 and can slide along the inner wall of the cylindrical tube 243;
the pressure regulating rod 23 has a gas pipe 232 penetrating through the inside thereof, and the support base 22 is communicated with the cylindrical pipe 243 via the gas pipe 232;
in operation, as shown in fig. 4, 6 and 7, the fractionation tray 24 is limited in the first distillation column 2 or the second distillation column 5 through the limiting chute 21, since the cylindrical tube 243 fixedly connected to the side surface of the fractionation tray 24 is matched with the limiting chute 21, the limiting chute 21 can enable the fractionation tray 24 to slide in the first distillation column 2 more stably, and the fractionation tray 24 is detachable, so that the fractionation tray 24 can be detached when the first distillation column 2 is cleaned, the first distillation column 2 and the fractionation tray 24 can be cleaned respectively, the cleaning difficulty is reduced, and in addition, when the fractionation tray 24 is installed, the fractionation tray 24 can be aligned with the limiting chute 21 to be directly put down, because the piston 231 at the top of the pressure regulating rod 23 can be inserted into the cylindrical tube 243 when the fractionation tray 24 is lowered to the position of the pressure regulating rod 23, a cylinder structure is formed, and since the cylindrical tube 243 is filled with air, the air tube 232 is connected with the air pump 8 through the tube, after the piston 231 is inserted into the cylindrical tube, the inner cavity of the cylindrical tube 243 and the air pump, the air tube 232 and the air pump can be stably and the air pump is stably supported in the space of the cylindrical tube 243, and the pressure regulating rod is stably and the pressure regulating tray 24 is simultaneously reduced, and the pressure of the fractionation tray is stably and the pressure regulating tray is supported in the space 24;
when the first distillation column 2 is performing a distillation process, according to the van der Waals equation:
wherein p is the pressure of the gas, namely the gas pressure in the gas pipeline 232 and the cylindrical pipe 243;
a is a parameter for measuring intermolecular attraction;
b is the average occupied space size of each molecule;
t is the thermodynamic temperature, i.e. the temperature of the fractionation tray 24 corresponding to the temperature of the compartment within the first distillation column 2;
r is a universal gas constant;
m is the mass of the gas, namely the total mass of the gas in the gas pipeline 232 and the cylindrical pipe 243;
m is the molar mass, namely the molar mass of the gas in the gas pipeline 232 and the cylindrical pipe 243;
in actual calculation, because the caliber of the gas pipe 232 is small, the occupied gas is very small and can be ignored, but the gas pressure of the gas in the cylinder 243 can be read through an external barometer, then the gas pressure of the gas in the cylinder 243 is adjusted through the air pump 8 according to the interval temperature T in the first distillation tower 2, when the temperature is unchanged, the larger the gas pressure p is, the larger the volume V of the gas in the cylinder 243 is, the more the cylinder 243 is far away from the pressure regulating rod 23, the position of the pressure regulating rod 23 is fixed, the higher the position of the cylinder 243 is, the higher the position of the fractionation tray 24 is also ensured, and after the position of the fractionation tray 24 is adjusted, if the temperature of the temperature interval corresponding to the fractionation tray 24 is increased, namely T is increased, the volume V is also increased according to the Van's equation, so that the position of the fractionation tray 24 is increased, and the temperature interval is matched.
The pressure regulating rod 23 is made of heat insulation materials;
in operation, the pressure regulating rod 23 is made of heat insulating material, so that the gas in the gas pipeline 232 is not influenced by high-temperature steam at the bottom of the first distillation tower 2.
The side walls of the first distillation tower 2 and the second distillation tower 5 are penetrated with a liquid outlet pipeline 25, and the liquid outlet pipeline 25 is L-shaped;
a diversion pipeline 244 is inserted in the bottom surface of the fractionating plate 24 near the liquid outlet pipeline 25, and the outer diameter of the liquid outlet pipeline 25 is equal to the inner diameter of the diversion pipeline 244;
in operation, during the vertical sliding of the fractionation tray 24, the liquid outlet pipe 25 is inserted into the guide pipe 244, and during the vertical sliding of the fractionation tray 24, the liquid outlet pipe 25 and the guide pipe 244 are not separated from contact, so that the component liquefied in the fractionation tray 24 can always flow into the guide pipe 244 through the liquid outlet pipe 25, and the guide pipe 244 discharges the component.
Embodiment one:
when the temperature interval corresponding to one fractionation tray 24 in the first distillation column 2 or the second distillation column 5 increases, that is, the temperature at the position where the fractionation tray 24 is located increases above the original set point, according to the van der waals equation:
t represents the temperature at the fractionation tray 24, and when T increases, to ensure that the equation is satisfied, the pressure p of the gas in the cylindrical tube 243 or the volume V of the gas will increase, and the pressure p of the gas in the cylindrical tube 243 is mainly affected by the overall gravity of the fractionation tray 24, so that the pressure p of the gas in the cylindrical tube 243 is unchanged, the volume V of the gas in the cylindrical tube 243 will increase, and the height of the fractionation tray 24 will be raised during the increase of the volume V of the gas in the cylindrical tube 243, so that the fractionation tray 24 is in a new temperature interval, and the new temperature interval will be re-matched with the liquefaction temperature of the component.
Embodiment two:
when the temperature interval corresponding to one of the fractionation trays 24 in the first distillation column 2 or the second distillation column 5 decreases, that is, the temperature at the location where the tray 24 is located decreases below the original set point, according to the van der waals equation:
t represents the temperature at the fractionation tray 24, and when T decreases, to ensure that the equation is satisfied, the pressure p of the gas in the cylindrical tube 243 or the volume V of the gas will decrease, and the pressure p of the gas in the cylindrical tube 243 is mainly affected by the overall gravity of the fractionation tray 24, so that the pressure p of the gas in the cylindrical tube 243 is unchanged, the volume V of the gas in the cylindrical tube 243 will decrease, the height of the fractionation tray 24 will decrease during the decrease of the volume V of the gas in the cylindrical tube 243, and the fractionation tray 24 will be in a new temperature interval, and the new temperature interval will be re-matched with the liquefaction temperature of the component.
Claims (2)
1. The 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 arranged 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 discharging 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 discharging base (4) through a pipeline;
the method is characterized in that: a plurality of sliding fractionation trays (24) are arranged inside the first distillation column (2) and the second distillation column (5), and the fractionation trays (24) adjust positions according to the internal temperature change of the first distillation column (2) or the second distillation column (5);
a plurality of limit sliding grooves (21) are formed in the inner walls of the first distillation tower (2) and the second distillation tower (5), and the limit sliding grooves (21) are used for limiting the displacement of the fractionation tray (24);
the bottom of the limiting 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 limit chute (21) is fixedly connected to the side surface of the fractionation tray (24) close to the limit chute (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 matched with the inner wall of the cylindrical pipe (243) and can slide along the inner wall of the cylindrical pipe (243);
the pressure regulating rod (23) is internally penetrated with a gas pipeline (232), and the supporting seat (22) is communicated with the cylindrical pipe (243) through the gas pipeline (232);
the pressure regulating rod (23) is made of heat insulation materials;
the side walls of the first distillation tower (2) and the second distillation tower (5) are penetrated with liquid outlet pipelines (25), and the liquid outlet pipelines (25) are L-shaped;
the bottom surface of fractionation dish (24) is close to the position of drain pipe (25) and alternates there is water conservancy diversion pipeline (244), the external diameter of drain pipe (25) equals with the internal diameter of water conservancy diversion pipeline (244).
2. A continuous twin column distillation system according to claim 1 wherein: distillation tank (241) have been seted up to the top surface intermediate position of fractionating plate (24), the bottom surface of fractionating plate (24) is close to the position of distillation tank (241) and is connected with baffle (242) through stock fixedly, the top surface area of baffle (242) is greater than the sectional area of distillation tank (241).
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| CN202210766175.8A CN114984604B (en) | 2022-06-30 | 2022-06-30 | Continuous double-tower distillation system |
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| CN202210766175.8A CN114984604B (en) | 2022-06-30 | 2022-06-30 | Continuous double-tower distillation system |
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