Toluene-ethanol-water ternary azeotrope separation device
By utilizing a toluene-ethanol-water three-phase azeotropic separator, the complex process of separating toluene-ethanol-water ternary azeotropic mixtures is solved through the combination of a water-permeable membrane module and a toluene-permeable membrane module, thus simplifying the operation process and improving the separation efficiency.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- JIANGSU JIUMO HIGH TECH CO LTD
- Filing Date
- 2025-07-24
- Publication Date
- 2026-07-31
AI Technical Summary
Existing technologies for separating toluene-ethanol-water ternary azeotropic mixtures have complex processes, requiring the introduction of extractants and additional equipment, which increases operational complexity.
A toluene-ethanol-water three-phase azeotropic separator is used, which includes a water-permeable membrane module, a drainage unit, a distillation column, a separator, a toluene-permeable membrane module, and a material circulation module. Through the cooperation of the distillation column, the water-permeable membrane module, and the toluene-permeable membrane module, separation without the introduction of extractant is achieved.
The process for separating toluene-ethanol-water ternary azeotropic mixtures has been simplified, reducing the complexity of the equipment and improving the separation efficiency.
Smart Images
Figure CN224573245U_ABST
Abstract
Description
Technical Field
[0001] The embodiments disclosed herein relate to the field of chemical separation technology, specifically to a toluene-ethanol-water three-phase azeotrope separation device. Background Technology
[0002] Toluene and ethanol are widely used organic solvents in industries such as chemicals, pharmaceuticals, pesticides, and textiles, and they often form toluene-ethanol-water ternary azeotropes with water. Separating these azeotropes is crucial for the resource recovery and utilization of toluene and ethanol. Currently, extractive distillation units are commonly used industrially to separate toluene-ethanol-water ternary azeotropic mixtures.
[0003] However, when using the above method to separate toluene-ethanol-water ternary azeotropic mixtures, there are often technical problems with high process complexity.
[0004] The information disclosed in this background section is only intended to enhance the understanding of the background of the present disclosure concept, and therefore may contain information that does not constitute prior art known to those skilled in the art. Utility Model Content
[0005] The summary portion of this disclosure is intended to provide a brief overview of the concepts, which will be described in detail in the detailed description portion. This summary portion is not intended to identify key or essential features of the claimed technical solutions, nor is it intended to limit the scope of the claimed technical solutions.
[0006] Some embodiments of this disclosure provide a toluene-ethanol-water three-phase azeotrope separation device to solve one or more of the technical problems mentioned in the background section above.
[0007] Some embodiments of this disclosure provide a toluene-ethanol-water three-phase azeotrope separation device. The device includes a priority water-permeable membrane assembly, a drainage unit, a distillation column, a separator, a priority toluene-permeable membrane assembly, and a material circulation assembly. The permeate side of the priority water-permeable membrane assembly is connected to a first heater; the permeate side of the priority water-permeable membrane assembly is connected to a first vacuum pump; the drainage unit is connected to the permeate side of the priority water-permeable membrane assembly; the distillation column is connected to the permeate side of the priority water-permeable membrane assembly, and a second heater is provided between the distillation column and the priority water-permeable membrane assembly; the upper end of the distillation column is connected to the separator; the outlet of the separator is connected to the permeate side of the priority toluene-permeable membrane assembly, and a third heater is provided between the separator and the priority toluene-permeable membrane assembly; the inlet of the material circulation assembly is connected to the permeate side of the priority toluene-permeable membrane assembly, and the material in the material circulation assembly flows to the distillation column; the permeate side of the priority toluene-permeable membrane assembly is also connected to a second vacuum pump.
[0008] Optionally, the drainage unit includes a first condenser, a storage tank, and a drainage pump, wherein the first condenser is connected to the permeable side of the preferred permeable membrane assembly; the first vacuum pump is connected to the permeable side of the preferred permeable membrane assembly through the first condenser; the outlet of the first condenser is connected to the inlet of the storage tank; and the drainage pump is connected to the outlet of the storage tank.
[0009] Optionally, the permeable membrane assembly is further connected to a second condenser on its permeate side; the outlet of the second condenser is connected to a mixing tank, and the outlet of the mixing tank is equipped with a first booster pump; the second heater is disposed between the first booster pump and the distillation column; the outlet of the second heater is connected to the feed inlet in the middle of the distillation column.
[0010] Optionally, a product tank is connected to the lower end of the distillation column.
[0011] Optionally, a reboiler is also connected to the lower end of the distillation column.
[0012] Optionally, the upper end of the distillation column is provided with a top condenser; the liquid separator is connected to the outlet of the top condenser; and the outlet of the liquid separator is connected to a second booster pump.
[0013] Optionally, the second booster pump has two outlets; one outlet of the second booster pump is connected to the top of the distillation column; and the other outlet of the second booster pump is connected to the inlet of the third heater.
[0014] Optionally, the material circulation assembly includes a third condenser and an oil collection tank; the third condenser is connected to the permeation side of the preferred toluene membrane assembly; the outlet of the third condenser is connected to the inlet of the oil collection tank; the outlet of the oil collection tank is connected to the mixing tank; and the outlet of the oil collection tank is equipped with a liquid transfer pump.
[0015] Optionally, a second vacuum pump is also connected to the permeate side of the aforementioned preferred toluene permeate membrane module.
[0016] Optionally, the feed inlet of the distillation column is equipped with a temperature sensor; the detection end of the temperature sensor extends into the feed pipe, and the signal output end is connected to the first heater.
[0017] Some embodiments of this disclosure provide a toluene-ethanol-water three-phase azeotropic mixture separation apparatus, which can simplify the operation process of separating toluene-ethanol-water ternary azeotropic mixtures. Specifically, the reason why most processes for separating toluene-ethanol-water ternary azeotropic mixtures are highly complex is that an extractant needs to be introduced, and in order to ensure the purity of the product, additional equipment is required to separate the product from the extractant, which increases the complexity of the apparatus and thus makes the operation process more complicated. Based on this, some embodiments of this disclosure provide a toluene-ethanol-water three-phase azeotrope separation device. The toluene-ethanol-water three-phase azeotrope separation device includes a priority water-permeable membrane assembly, a drainage unit, a distillation column, a separator, a priority toluene-permeable membrane assembly, and a material circulation assembly. The permeate side of the priority water-permeable membrane assembly is connected to a first heater; the permeate side of the priority water-permeable membrane assembly is connected to a first vacuum pump; the drainage unit is connected to the permeate side of the priority water-permeable membrane assembly; the distillation column is connected to the permeate side of the priority water-permeable membrane assembly, and a second heater is provided between the distillation column and the priority water-permeable membrane assembly; the upper end of the distillation column is connected to the separator; the outlet of the separator is connected to the permeate side of the priority toluene-permeable membrane assembly, and a third heater is provided between the separator and the priority toluene-permeable membrane assembly; the inlet of the material circulation assembly is connected to the permeate side of the priority toluene-permeable membrane assembly, and the material in the material circulation assembly flows to the distillation column; the permeate side of the priority toluene-permeable membrane assembly is also connected to a second vacuum pump. By combining a distillation column, a water-permeable membrane module, and a toluene-permeable membrane module, a toluene-ethanol-water ternary azeotropic mixture can be separated without introducing an extractant. This simplifies the process flow for separating toluene-ethanol-water ternary azeotropic mixtures. Attached Figure Description
[0018] The above and other features, advantages, and aspects of the embodiments of this disclosure will become more apparent from the accompanying drawings and the following detailed description. Throughout the drawings, the same or similar reference numerals denote the same or similar elements. It should be understood that the drawings are schematic, and elements are not necessarily drawn to scale.
[0019] Figure 1 This is a schematic diagram of the structure of a toluene-ethanol-water three-phase azeotrope separation device according to some embodiments of this disclosure;
[0020] Figure 2 These are schematic diagrams of the drainage unit according to some embodiments of this disclosure;
[0021] Figure 3 This is a schematic diagram of the structure of a material recycling component according to some embodiments of this disclosure. Detailed Implementation
[0022] Embodiments of this disclosure will now be described in more detail with reference to the accompanying drawings. While some embodiments of this disclosure are shown in the drawings, it should be understood that this disclosure can be implemented in various forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided to provide a more thorough and complete understanding of this disclosure. It should be understood that the accompanying drawings and embodiments of this disclosure are for illustrative purposes only and are not intended to limit the scope of protection of this disclosure.
[0023] It should also be noted that, for ease of description, only the parts relevant to the invention are shown in the accompanying drawings. Unless otherwise specified, the embodiments and features described in this disclosure can be combined with each other.
[0024] It should be noted that the concepts of "first" and "second" mentioned in this disclosure are used only to distinguish different devices, modules or units, and are not used to limit the order of functions performed by these devices, modules or units or their interdependencies.
[0025] It should be noted that the terms "a" and "a plurality of" used in this disclosure are illustrative rather than restrictive, and those skilled in the art should understand that, unless otherwise expressly indicated in the context, they should be understood as "one or more".
[0026] The names of messages or information exchanged between multiple devices in the embodiments of this disclosure are for illustrative purposes only and are not intended to limit the scope of such messages or information.
[0027] This disclosure will now be described in detail with reference to the accompanying drawings and embodiments.
[0028] Figure 1 This is a schematic diagram of the structure of a toluene-ethanol-water three-phase azeotrope separation device according to some embodiments of this disclosure. Figure 1 It includes a first heater 1, a priority water-permeable membrane assembly 2, a mixing tank 3, a second heater 4, a separating tank 5, a third heater 6, a priority toluene-permeable membrane assembly 7, a second booster pump 12, a distillation column 13, and a first booster pump 14.
[0029] Figure 2 This is a schematic diagram of the structure of a drainage unit according to some embodiments of this disclosure. Figure 2 It includes a first heater 1, a priority water-permeable membrane assembly 2, a mixing tank 3, a second heater 4, a separating tank 5, a third heater 6, a priority toluene-permeable membrane assembly 7, a second booster pump 12, a distillation column 13, a first booster pump 14, a first condenser 15, a first vacuum pump 16, a drain pump 17, and a storage tank 18.
[0030] Figure 3 This is a schematic diagram of the structure of a material recycling component according to some embodiments of this disclosure. Figure 3It includes a first heater 1, a priority water-permeable membrane assembly 2, a mixing tank 3, a second heater 4, a separating tank 5, a third heater 6, a priority toluene-permeable membrane assembly 7, a second condenser 8, an oil collecting tank 9, a transfer pump 10, a second vacuum pump 11, a second booster pump 12, a distillation column 13, and a first booster pump 14.
[0031] In some embodiments, the toluene-ethanol-water three-phase azeotrope separation device may include a preferential water-permeable membrane module 2, a drainage unit, a distillation column 13, a separator 5, a preferential toluene-permeable membrane module 7, and a material circulation component. The preferential water-permeable membrane module 2 may have a cylindrical exterior and employ a preferential water-permeable membrane, such as a NaA molecular sieve membrane, a PVA membrane, or a silica membrane. The NaA molecular sieve membrane is a microporous inorganic membrane composed of NaA-type zeolite. The NaA-type zeolite is a synthetically produced zeolite molecular sieve belonging to the LTA (Linde Type A) structural type. The preferential water-permeable membrane module 2 can be composed of 1 to 200 membrane modules connected in series, parallel, or in a mixed configuration, which can be adjusted according to the actual throughput. The aforementioned membrane module can be an independent membrane separation unit. A single membrane module can consist of membrane material (such as NaA molecular sieve membrane, PVA membrane, etc.), a support (a structure for fixing the membrane material and providing physical support, such as a porous ceramic tube), a flow channel structure (a path design for guiding the flow of feed liquid (permeate side) and permeate, such as a tubular structure), and a sealing element (used for the connection interface between the various components of the membrane module to prevent leakage of feed liquid or permeate, such as a rubber gasket), and is cylindrical in shape externally. The aforementioned water-permeable membrane module 2 can separate the aqueous phase from the feed liquid. The feed liquid can be a toluene-ethanol-water three-phase azeotrope. The aforementioned drainage unit (refer to...) Figure 2 The above-mentioned drainage unit can be used to transport the aqueous permeate from the permeate side of the preferentially permeable membrane module 2. Therefore, the above-mentioned drainage unit can be connected to the permeate side of the preferentially permeable membrane module 2. The structure of the above-mentioned distillation column 13 can be a vertical cylindrical shape. The above-mentioned distillation column 13 can be used to separate toluene and ethanol in the residual liquid of the preferentially permeable membrane module 2, and achieve preliminary separation of the two through gas-liquid mass transfer. A toluene-ethanol azeotrope is obtained at the top of the column, and high-purity toluene is obtained at the bottom of the column. The above-mentioned separator 5 can be a horizontal cylindrical container, which can temporarily store the liquid phase mixture (containing toluene and ethanol) condensed at the top of the above-mentioned distillation column 13. The above-mentioned preferential toluene permeate membrane module 7 can use a preferential toluene permeate type membrane material (such as PDMS membrane or other hydrophobic membrane material), and can be composed of 1 to 200 membrane modules. In the above-mentioned preferential toluene permeate membrane module 7, toluene can preferentially permeate through the membrane to reach the permeate side. The above-mentioned material circulation component (see reference) Figure 3 The toluene condensate (toluene content of 45-60 wt%) on the permeate side of the preferential toluene membrane module 7 can be recovered and then returned to the distillation column 13 to achieve material recycling.
[0032] In some embodiments, a first heater 1 may be connected to the permeate side of the preferentially permeable membrane assembly 2. The first heater 1 may be a shell-and-tube heat exchanger. The first heater 1 may be used to heat the feed liquid. For example, it may be heated to a vaporized state, with a vapor pressure between 0.05 and 0.3 MPa, so that the feed liquid can pass through the preferentially permeable membrane assembly 2. A first vacuum pump 16 may be connected to the permeate side of the preferentially permeable membrane assembly 2. The first vacuum pump 16 may be a water ring vacuum pump, used to create a negative pressure on the permeate side, driving water molecules to preferentially permeate the preferentially permeable membrane assembly 2. The distillation column 13 may be a plate column, used to separate toluene and ethanol from the permeate of the preferentially permeable membrane assembly. A second heater 4 may be provided between the distillation column 13 and the preferentially permeable membrane assembly 2. The second heater 4 may be an electric heating rod, used to further heat the permeate of the preferentially permeable membrane assembly to a suitable temperature (e.g., 70–85°C). The upper end of the distillation column 13 may be connected to the separatory tank 5. The outlet of the separator 5 can be connected to the permeate side of the preferential toluene permeate membrane module 7. A third heater 6 can be provided between the separator 5 and the preferential toluene permeate membrane module 7. The third heater 6 can be a plate heat exchanger, which can be used to heat the liquid mixture (toluene-ethanol azeotrope) delivered from the separator 5 to a temperature (e.g., 50-70°C) for efficient separation. The inlet of the material circulation component can be connected to the permeate side of the preferential toluene permeate membrane module 7. The outlet of the material circulation component can be connected before the inlet of the distillation column 13 to form a circulation loop. A second vacuum pump 11 can also be connected to the permeate side of the preferential toluene permeate membrane module 7. The second vacuum pump 11 can be a rotary vane vacuum pump, which is used to maintain a low-pressure environment on the permeate side and improve the toluene permeation rate.
[0033] Optionally, such as Figure 1 and Figure 2 As shown, the drainage unit may include a first condenser 15, a storage tank 18, and a drainage pump 17. The first condenser 15 may be a shell-and-tube condenser, and the cooling medium may be circulating water. The first condenser 15 may be connected to the permeable side of the preferred permeable membrane assembly 2 to condense the permeated water vapor into liquid water. The first vacuum pump 16 may be connected to the permeable side of the preferred permeable membrane assembly 2 via the first condenser 15. The outlet of the first condenser 15 may be connected to the inlet of the storage tank 18. The storage tank 18 may be a stainless steel container with corrosion-resistant inner walls, used to temporarily store the condensed aqueous phase liquid. The drainage pump 17 may be a centrifugal pump, connected to the outlet of the storage tank 18, used to transport the aqueous phase liquid to a subsequent treatment unit or discharge system.
[0034] Optionally, a second condenser 8 can be connected to the permeate side of the aforementioned priority permeable membrane component 2. The second condenser 8 can be a finned condenser, used to cool the permeate from the priority permeable membrane component. The outlet of the second condenser 8 can be connected to a mixing tank 3, which can be a stainless steel container with an anti-corrosion inner wall, used to mix the permeate from the priority permeable membrane component with the toluene condensate transported from the aforementioned material circulation component. The outlet of the mixing tank 3 can be equipped with a first booster pump 14, which can be a gear pump, used to provide power for the material in the mixing tank 3 to enter the distillation column 13. A second heater 4 can be located between the first booster pump 14 and the distillation column 13, used to heat the pressurized material to improve the operating efficiency of the distillation column 13. The outlet of the second heater 4 can be connected to the middle feed inlet of the distillation column 13, allowing the material to participate in gas-liquid mass transfer in the middle section of the column, improving separation efficiency.
[0035] Optionally, a product tank can be connected to the lower end of the distillation column 13. The product tank can be a horizontal storage tank for collecting the toluene product (toluene purity of 99-99.9 wt%) discharged from the bottom of the distillation column 13.
[0036] Optionally, a reboiler may also be connected to the lower end of the distillation column 13. The reboiler may be a kettle-type reboiler, which can use steam or heat transfer oil to heat the liquid at the bottom of the column, provide the rising gas phase required for distillation, and maintain the gas-liquid balance in the distillation column 13.
[0037] Optionally, the upper end of the distillation column 13 may be equipped with a top condenser, which can be a shell-and-tube condenser used to condense the rising vapor at the top of the column. The separator 5 can be connected to the outlet of the top condenser to receive the condensed gas-liquid mixture. The outlet of the separator 5 can be connected to a second booster pump 12, which can be a plunger pump used to transport the mixture in the separator 5 to the next processing unit.
[0038] Optionally, the second booster pump 12 may have two outlets. One outlet of the second booster pump 12 may be connected to the top of the distillation column 13 to return a portion of the mixture (toluene-ethanol azeotrope) in the separatory tank 5 to the top of the distillation column 13 as reflux. The other outlet of the second booster pump 12 may be connected to the inlet of the third heater 6 to transport another portion of the mixture in the separatory tank 5 as the top product to the preferential toluene membrane assembly 7 for further separation.
[0039] Optionally, such as Figure 3As shown, the aforementioned material circulation assembly may include a third condenser and an oil collection tank 9. The third condenser may be a plate condenser, used to condense toluene vapor discharged from the permeate side of the preferential toluene membrane assembly 7. The outlet of the third condenser may be connected to the inlet of the oil collection tank 9. The oil collection tank 9 may be a container equipped with a level gauge, used to collect the condensed toluene condensate (toluene content of 45-60 wt%). The outlet of the oil collection tank 9 may be connected to the mixing tank 3, returning the toluene condensate to the mixing tank 3 to achieve material circulation. The outlet of the oil collection tank 9 may be equipped with a transfer pump 10 to provide driving force for the toluene condensate. The transfer pump 10 may be a centrifugal pump, and no specific limitation is made here.
[0040] Optionally, such as Figure 3 As shown, the permeation side of the aforementioned preferential toluene permeation membrane module 7 can also be connected to a second vacuum pump 11 to maintain the pressure difference across the membrane, thereby ensuring efficient toluene permeation to a certain extent. The second vacuum pump 11 can have the same design as the first vacuum pump 16.
[0041] Optionally, the feed inlet of the distillation column 13 may be equipped with a temperature sensor, which may be a thermocouple sensor with its sensing end extending into the feed pipe to monitor the feed temperature in real time. The signal output terminal of the temperature sensor may be connected to the first heater 1, and the heating power of the first heater 1 may be adjusted through feedback control to ensure that the temperature of the material entering the priority permeable membrane assembly 2 is stable within a suitable operating range (e.g., 70–85°C).
[0042] Optionally, the toluene-ethanol-water three-phase azeotropic separator may further include a pre-filtration unit and a backwashing system for pre-treating the feed liquid and maintaining the filtration device. It should be noted that the pre-filtration unit and the backwashing system are not shown in the accompanying drawings. The pre-filtration unit can be located before the first heater 1, and can be a three-stage series of cylindrical filters to form a gradient filtration structure. The first stage can be a sintered metal mesh, the second stage can be a polypropylene filter element, and the third stage can be a ceramic membrane filter element, equipped with a quick-release cover (such as a pull-rod type or a push-button type) for easy filter element replacement. The first stage of the pre-filtration unit has a pore size of 100–200 μm for trapping larger particulate impurities (such as rust and silt). The second stage of the pre-filtration unit has a filtration accuracy of 10–20 μm for removing medium-sized suspended solids (such as colloidal particles). The third stage of the aforementioned pre-filtration unit has a pore size of 0.5–1 μm to capture minute impurities (such as polymer debris), ensuring the cleanliness of the material entering the membrane module to a certain extent. The aforementioned backwashing system includes a backwash pipeline and a high-pressure water pump. One end of the backwash pipeline can be connected to the outlet of the aforementioned drain pump 17, using the separated clean water (stored in a water tank) as the backwashing medium; the other end can be connected to the aforementioned pre-filtration unit for reverse rinsing. The aforementioned high-pressure water pump can be connected to the aforementioned backwash pipeline, and the outlet pressure of the high-pressure water pump can be 0.5–2.0 MPa, providing sufficient power to flush away contaminants from the filter element surface. The backwash water flow rate of the aforementioned backwashing system can be 10–30% of the aforementioned raw material flow rate, and the backwashing cycle can be once every 2–4 hours. Timed backwashing prevents filter element clogging, extends the service life of the filter unit, and to a certain extent ensures the stable operation of the entire toluene-ethanol-water three-phase azeotropic separator.
[0043] The above-described optional embodiments, as an inventive point of this disclosure, solve the technical problem of "easy clogging of membrane modules and heaters". The specific factors leading to easy clogging of membrane modules and heaters are as follows: the feed liquid contains various impurities, and although current devices have filtration systems, they lack self-cleaning mechanisms, which greatly reduces the lifespan of the filtration system. Solving these factors can reduce the clogging of membrane modules and heaters. To achieve this effect, this disclosure also provides a pre-filtration unit and a backwashing system. The feed liquid is filtered in stages, and the pre-filtration unit is periodically cleaned by the backwashing system, achieving self-cleaning of the filtration system. This reduces the clogging of membrane modules and heaters. Furthermore, the backwashing system uses water from a storage tank for backwashing. The water in the storage tank is a byproduct already present in the system; its direct use for backwashing avoids the introduction of external cleaning water sources, reducing water consumption and costs. Moreover, the water in the storage tank has similar chemical compatibility (such as pH and temperature) with the feed liquid, which can, to some extent, avoid problems such as membrane swelling and corrosion caused by differences in water quality, protecting the integrity of the equipment.
[0044] Some embodiments of this disclosure provide a toluene-ethanol-water three-phase azeotropic mixture separation apparatus, which can simplify the operation process of separating toluene-ethanol-water ternary azeotropic mixtures. Specifically, the reason why most processes for separating toluene-ethanol-water ternary azeotropic mixtures are highly complex is that an extractant needs to be introduced, and in order to ensure the purity of the product, additional equipment is required to separate the product from the extractant, which increases the complexity of the apparatus and thus leads to a complex operation process. Based on this, some embodiments of this disclosure provide a toluene-ethanol-water three-phase azeotrope separation device. The toluene-ethanol-water three-phase azeotrope separation device includes a priority water-permeable membrane assembly, a drainage unit, a distillation column, a separator, a priority toluene-permeable membrane assembly, and a material circulation assembly. The permeate side of the priority water-permeable membrane assembly is connected to a first heater; the permeate side of the priority water-permeable membrane assembly is connected to a first vacuum pump; the drainage unit is connected to the permeate side of the priority water-permeable membrane assembly; the distillation column is connected to the permeate side of the priority water-permeable membrane assembly, and a second heater is provided between the distillation column and the priority water-permeable membrane assembly; the upper end of the distillation column is connected to the separator; the outlet of the separator is connected to the permeate side of the priority toluene-permeable membrane assembly, and a third heater is provided between the separator and the priority toluene-permeable membrane assembly; the inlet of the material circulation assembly is connected to the permeate side of the priority toluene-permeable membrane assembly, and the material in the material circulation assembly flows to the distillation column; the permeate side of the priority toluene-permeable membrane assembly is also connected to a second vacuum pump. By combining a distillation column, a water-permeable membrane module, and a toluene-permeable membrane module, a toluene-ethanol-water ternary azeotropic mixture can be separated without introducing an extractant. This simplifies the process flow for separating toluene-ethanol-water ternary azeotropic mixtures.
[0045] The above description is merely a selection of preferred embodiments of this disclosure and an explanation of the technical principles employed. Those skilled in the art should understand that the scope of the invention involved in the embodiments of this disclosure is not limited to technical solutions formed by specific combinations of the above-described technical features, but should also cover other technical solutions formed by arbitrary combinations of the above-described technical features or their equivalents without departing from the above-described inventive concept. For example, technical solutions formed by substituting the above-described features with (but not limited to) technical features with similar functions disclosed in the embodiments of this disclosure.
Claims
1. A toluene-ethanol-water ternary azeotrope separation apparatus, characterized by, The toluene-ethanol-water three-phase azeotrope separator includes a water-permeable membrane module, a drainage unit, a distillation column, a separator, a toluene-permeable membrane module, and a material circulation module. The permeable membrane assembly is connected to a first heater on its permeable side; The permeable membrane assembly is connected to a first vacuum pump on its permeation side; The drainage unit is connected to the permeable side of the preferred permeable membrane assembly; The distillation column is connected to the permeable side of the preferred permeable membrane assembly, and a second heater is provided between the distillation column and the preferred permeable membrane assembly; The upper end of the distillation column is connected to the separator; The outlet of the separator is connected to the permeate side of the preferred toluene permeate membrane assembly, and a third heater is provided between the separator and the preferred toluene permeate membrane assembly. The feed inlet of the material circulation component is connected to the permeate side of the preferential toluene membrane component, and the material in the material circulation component flows to the distillation column; The permeation side of the preferred toluene-permeable membrane module is also connected to a second vacuum pump.
2. The toluene-ethanol-water ternary azeotrope separation apparatus according to claim 1, characterized in that, The drainage unit includes a first condenser, a liquid storage tank, and a drainage pump, wherein the first condenser is connected to the permeable side of the preferred permeable membrane assembly. The first vacuum pump is connected to the permeable side of the preferred water-permeable membrane assembly via the first condenser; The outlet of the first condenser is connected to the inlet of the liquid storage tank; The drainage pump is connected to the outlet of the storage tank.
3. The toluene-ethanol-water ternary azeotrope separation apparatus of claim 1, wherein, The permeable membrane assembly is also connected to a second condenser on its permeable side; The outlet of the second condenser is connected to a mixing tank, and the outlet of the mixing tank is equipped with a first booster pump; The second heater is disposed between the first booster pump and the distillation column; The outlet of the second heater is connected to the feed inlet in the middle of the distillation column.
4. The toluene-ethanol-water ternary azeotrope separation apparatus of claim 1, wherein, The lower end of the distillation column is connected to a product tank.
5. The toluene-ethanol-water ternary azeotrope separation apparatus according to claim 4, wherein The lower end of the distillation column is also connected to a reboiler.
6. The toluene-ethanol-water ternary azeotrope separation apparatus of claim 1, wherein, The distillation column is equipped with a top condenser at its upper end; The separatory tank is connected to the outlet of the condenser at the top of the tower. The outlet of the separator is connected to a second booster pump.
7. The toluene-ethanol-water ternary azeotrope separation apparatus according to claim 6, characterized in that, The second booster pump has two discharge ports; One of the outlets of the second booster pump is connected to the top of the distillation column; The other outlet of the second booster pump is connected to the inlet of the third heater.
8. The toluene-ethanol-water ternary azeotrope separation apparatus of claim 3, wherein, The material circulation assembly includes a third condenser and an oil collection tank; The third condenser is connected to the permeate side of the preferred toluene permeate membrane assembly; The outlet of the third condenser is connected to the inlet of the oil collection tank; The outlet of the oil collecting tank is connected to the mixing tank; The oil collection tank is equipped with a transfer pump at its outlet.
9. The toluene-ethanol-water ternary azeotrope separation apparatus of claim 1, wherein, The feed inlet of the distillation column is equipped with a temperature sensor; The detection end of the temperature sensor extends into the feed pipe, and the signal output end is connected to the first heater.