CN111848348A - Isopropyl alcohol dehydration refining method - Google Patents
Isopropyl alcohol dehydration refining method Download PDFInfo
- Publication number
- CN111848348A CN111848348A CN202010614818.8A CN202010614818A CN111848348A CN 111848348 A CN111848348 A CN 111848348A CN 202010614818 A CN202010614818 A CN 202010614818A CN 111848348 A CN111848348 A CN 111848348A
- Authority
- CN
- China
- Prior art keywords
- isopropanol
- heat exchange
- raw material
- membrane separation
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides an isopropanol dehydration refining method, which comprises the following steps: conveying the water-containing isopropanol raw material to heat exchange equipment at a mass flow rate of 800-1200 kg/h for preheating, and introducing the raw material preheated to 70-90 ℃ into a membrane separation assembly for dehydration at a pressure of 0.2-0.4MPa and a temperature of 100-; and conveying the dehydrated isopropanol product steam to heat exchange equipment to exchange heat with the raw material, and then condensing and collecting the isopropanol product. The method of the invention is used for dehydrating and refining the hydrous isopropanol, and the design of the coupling loop effectively realizes the recycling of system energy, greatly reduces energy consumption and saves operation cost. And the advantages of the membrane separation technology can be fully exerted, and the traditional isopropanol dehydration rectifying tower is replaced. The whole device suitable for the method is simple and convenient to operate, stable in operation, capable of effectively realizing continuous operation and production, small in occupied area of related equipment and low in investment cost.
Description
Technical Field
The invention belongs to the field of organic solvent dehydration and refining, and particularly relates to a technology for dehydrating isopropanol by adopting a molecular sieve membrane technology.
Background
Isopropanol is an important chemical basic organic raw material, is mainly used as a chemical process solvent, an industrial cleaning agent and a fuel antifreeze, and has strict requirements on impurities, particularly water content in the isopropanol in the use process. Since the isopropanol and the water belong to an azeotropic system and have an azeotropic composition, the isopropanol and the water cannot be separated by a common separation method. The following methods are commonly used in industry: azeotropic distillation, extractive distillation, adsorptive separation, and the like. The azeotropic distillation needs to adopt an entrainer to separate water from isopropanol for recycling, the entrainer generally selected is benzene, the method has high energy consumption, benzene can be remained in the product to cause product pollution, and meanwhile, health hidden troubles are brought to operators and environmental pollution is caused. The extraction agent adopted in the extraction rectification is ethylene glycol, the principle of dissolution selectivity is utilized, and the water in the isopropanol is removed by combining the rectification, but the problems of product pollution, high energy consumption, low extraction agent recovery rate, complex operation and the like exist at the same time. The adsorption separation method utilizes the diameter difference between isopropanol and water, adopts a solid adsorbent to selectively adsorb the water, has the advantages that third component impurities are not introduced, and the quality of an isopropanol product is favorably improved, but the operation process of alternatively carrying out adsorption and desorption is not steady-state operation, a large amount of isopropanol-containing wastewater is generated by desorption liquid, and the comprehensive treatment performance is poor.
Pervaporation is a novel membrane technology for separating mixtures, has the outstanding advantages of high efficiency, high separation degree, low energy consumption and the like, is simple in process, does not need excessive matched treatment, is reliable and high in stability, does not introduce other components in the separation process, and belongs to a high-efficiency environment-friendly technology. Research on the application of pervaporation technology to the dehydration of aqueous isopropanol has been carried out for a long time, but the results of the existing research have many disadvantages for industrial scale application, including process efficiency, product purity or multi-angle process integration. Therefore, how to scale up the product while maintaining the dehydration level of the product, or how to further reduce the energy consumption while scaling up the product, has been an area of intense efforts by those skilled in the art.
Disclosure of Invention
The invention aims to provide a method for refining isopropanol by dehydration and discloses a set of low-energy-consumption integrated device for deep dehydration of water-containing isopropanol, which is suitable for the method.
The method for dehydrating and refining isopropanol comprises the following steps:
conveying the water-containing isopropanol raw material to heat exchange equipment at a mass flow rate of 800-1200 kg/h for preheating, and introducing the raw material preheated to 70-90 ℃ into a membrane separation assembly for dehydration at a pressure of 0.2-0.4MPa and a temperature of 100-; the dehydrated isopropanol product steam (namely the retentate) is conveyed to a heat exchange device to exchange heat with the raw material, and then is collected into an isopropanol product through condensation.
In order to fully implement the method for refining isopropanol by dehydration, the invention further provides a set of isopropanol pervaporation dehydration device suitable for the method, which comprises a raw material processing unit, a membrane separation unit, a retentate processing unit and a permeate processing unit, wherein: the raw material processing unit comprises a first storage tank, a first fluid conveying device and a first heat exchange device; wherein the first heat exchange equipment is provided with a raw material inlet, a raw material outlet, a heat exchange medium inlet and a heat exchange medium outlet; the membrane separation unit is provided with a raw material inlet, a retentate outlet and a permeate outlet; the heat exchange medium inlet of the first heat exchange device is connected with the retentate outlet of the membrane separation unit; the outlet of the heat exchange medium of the first heat exchange device is connected with a retentate treatment unit; and the permeate outlet of the membrane separation unit is connected with the permeate treatment unit. The method for dehydrating and purifying isopropanol by using the dehydration device comprises the following steps: the method comprises the following steps of buffering a raw material containing water isopropanol by a first storage tank, then feeding the raw material into first heat exchange equipment, preheating the raw material, wherein a heat source used for preheating is provided by a heat exchange medium; the preheated raw material enters the membrane separation unit in a steam or liquid state. And (3) enabling retentate isopropanol steam obtained by separation of the membrane separation unit to serve as a heat exchange medium to enter first heat exchange equipment, performing heat exchange with the raw material, and collecting and processing the retentate isopropanol by a retentate processing unit to finally form a qualified isopropanol product. The permeate (namely water vapor) obtained by the separation of the membrane separation unit enters a permeate treatment unit, and is discharged out of the system after condensation and buffering.
The method of the invention is used for dehydrating and refining the hydrous isopropanol, and the design of the coupling loop effectively realizes the cyclic utilization of system energy, greatly reduces energy consumption and saves operation cost. And the advantages of the membrane separation technology can be fully exerted, and the traditional isopropanol dehydration rectifying tower is replaced. The refining method based on the whole device has the advantages of simple and convenient operation, stable operation, effective realization of continuous operation and production, small occupied area of related equipment and low investment cost.
Drawings
FIG. 1 is a diagram of an apparatus for pervaporation dehydration of isopropyl alcohol according to the present invention, wherein:
1. a first storage tank; 2. a first fluid delivery device; 3. a first heat exchange device; 4. an evaporation apparatus; 5. a second heat exchanger; 6. a membrane separation module; 7. a pressure regulating device; 8. a second storage tank; 9. a second fluid delivery device; 10. a third heat exchanger; 11. a third storage tank; 12. a fourth fluid delivery device; 13. a third fluid delivery apparatus.
Detailed Description
The following detailed description of the invention refers to the accompanying drawings.
The invention provides an isopropanol dehydration refining method, which comprises the steps of conveying a hydrous isopropanol raw material to heat exchange equipment for preheating at a mass flow rate of 800-1200 kg/h, and introducing the raw material preheated to 70-90 ℃ into a membrane separation assembly for dehydration at a pressure of 0.2-0.4MPa and a temperature of 100-; the dehydrated isopropanol product steam (namely the retentate) is conveyed to a heat exchange device to exchange heat with the raw material, and then is collected into an isopropanol product through condensation. In order to ensure the product quality, in the isopropanol dehydration and refining method, the water content in the water-containing isopropanol raw material is not more than 10% by mass. The preheating temperature of the raw materials is preferably 80 +/-2 ℃.
In the loop design of the process, the design of the coupling loop effectively realizes the cyclic utilization of system energy, greatly reduces energy consumption and saves operation cost.
In order to better implement the method of the invention, in the specific embodiment of the invention, an isopropanol pervaporation dehydration device special for the method is provided, and the method is implemented by using the device. The isopropanol pervaporation dehydration device comprises a raw material processing unit, a membrane separation unit, a retentate processing unit and a permeate processing unit, wherein: the raw material processing unit comprises a first storage tank 1, a first fluid conveying device 2 and a first heat exchange device 3; wherein the first heat exchange device 3 is provided with a raw material inlet, a raw material outlet, a heat exchange medium inlet and a heat exchange medium outlet; the membrane separation unit is provided with a raw material inlet, a retentate outlet and a permeate outlet; the heat exchange medium inlet of the first heat exchange device 3 is connected with the retentate outlet of the membrane separation unit; the outlet of the heat exchange medium of the first heat exchange device 3 is connected with a retentate treatment unit; and the permeate outlet of the membrane separation unit is connected with the permeate treatment unit.
The raw material containing water isopropanol to be treated enters a membrane separation unit through a raw material treatment unit, and a membrane separation process is carried out. Water molecules penetrate through the molecular sieve membrane to form permeate, and the permeate is discharged out of the system by the permeate treatment unit. The isopropanol with larger molecular size is intercepted by the molecular sieve membrane to form an isopropanol product with ultralow water content, and the isopropanol product is collected by a retentate treatment unit to form the product. And in the system design, heat exchange is formed between the retentate and the raw material so as to recycle the retentate heat source to realize heating of the raw material.
In a specific embodiment, the raw material processing unit comprises a first storage tank 1, a first fluid conveying device 2 and a first heat exchange device 3, and can also comprise an evaporation device 4; the first heat exchange device 3 is provided with a raw material inlet, a raw material outlet, a heat exchange medium inlet and a heat exchange medium outlet; the membrane separation unit is provided with a raw material inlet, a retentate outlet and a permeate outlet; the heat exchange medium inlet of the first heat exchange device 3 is connected with the retentate outlet of the membrane separation unit, and a pressure regulating device 7 can be arranged between the heat exchange medium inlet and the retentate outlet; the outlet of the heat exchange medium of the first heat exchange device 3 is connected with a retentate treatment unit; the retentate treatment unit comprises a second heat exchanger 5, a second holding tank 8, a second fluid transport device 9. And the permeate outlet of the membrane separation unit is connected with the permeate treatment unit. The permeate treatment unit comprises a third heat exchanger 10, a third tank 11, a third fluid delivery device 13. Said third heat exchanger 10 is also connected to a fourth fluid transfer device 12 for vacuum generation.
In the isopropanol pervaporation dehydration device of the present invention, the following components:
the first storage tank 1 is used for buffer storage of the water-containing isopropanol raw material.
The first fluid transfer device 2 is used for transferring the liquid water-containing isopropanol raw material to the first heat exchange device 3, and a centrifugal pump and a positive displacement pump can be selected and used for realizing the purpose.
The first heat exchange means 3 provides a location for heat exchange of the aqueous isopropanol feed with the retentate, where the retentate from the membrane separation module 6 enters the first heat exchange means 3 as a heat exchange medium to exchange heat to the aqueous isopropanol feed which is heated and enters the evaporation means 4. According to the process requirements, the first heat exchange device 3 can be selected from, but not limited to, a fixed tube-plate type tube-and-tube heat exchanger, a floating head type tube-and-tube heat exchanger, a U-shaped tube-and-tube heat exchanger, a spiral plate type heat exchanger, a spiral tube wound heat exchanger and a plate type heat exchanger.
The vaporization apparatus 4 is adapted to receive the heated aqueous isopropanol feed from the first heat exchange apparatus and vaporize it. Frequently used evaporation apparatuses 4 include rising-film evaporators, falling-film evaporators, forced circulation evaporators, kettle reboiling evaporators, shell-and-tube evaporators, immersion evaporators.
The membrane separation unit is used for realizing the high-efficiency separation of isopropanol and water. For this purpose, the membrane separation unit is preferably an inorganic molecular sieve membrane separation unit, consisting of n (n is a positive integer) molecular sieve membrane modules 6. The membrane assembly can be a single tube pass or a plurality of tube passes, and the area of the single membrane assembly can be controlled between 5 square meters and 300 square meters. The number n of membrane modules arranged in each set is determined according to the separation purpose; when n is greater than 1, the membrane modules can be connected in series or in parallel according to the material condition, the separation target and the like. On the other hand, from the component structure, the present invention can adopt, but is not limited to, specific forms such as a thermostatic membrane component or a baffle-type membrane component. In the embodiment of the present invention, the molecular sieve membrane module may be specifically exemplified by, but not limited to, a plate-type, tubular-type, hollow fiber-type or spiral plate-type molecular sieve membrane module, preferably a tubular-type molecular sieve membrane module. Suitable types of molecular sieves include LTA, SOD, FAU, MOR, FER, MFI, PHI, BEA, CHA, ERI, and mixed crystal molecular sieve membranes thereof, preferably type A molecular sieve membranes.
Said second heat exchanger 5 receives the retentate, i.e. the isopropanol vapor, from the first heat exchange means 3 and further condenses it to obtain the product isopropanol. The second heat exchanger 5 can be selected from, but not limited to, a fixed tube-plate type tube-and-tube heat exchanger, a floating head type tube-and-tube heat exchanger, a U-shaped tube-and-tube heat exchanger, a spiral plate type heat exchanger, a spiral tube wound heat exchanger, and a plate type heat exchanger.
The second storage tank 8 is an isopropanol product buffer tank, and the buffered isopropanol product is output by the second fluid conveying equipment 9 and is an isopropanol qualified product. The second fluid transfer device 9 may be exemplified by, but not limited to, a centrifugal pump, a positive displacement pump.
The pressure regulating device 7 is disposed between the membrane separation module 6 and the first heat exchanger 3, and permanently adjusts the vapor pressure of isopropyl alcohol from the membrane separation module 6. Typically, pressure reducing valves, pressure regulating valves, and pressure maintaining valves are selected, but not limited to.
The third heat exchanger 10 is arranged to receive and condense permeate (i.e. separated water) from the membrane separation module 6. Generally, a fixed tube plate type tube heat exchanger, a floating head type tube heat exchanger, a U-shaped tube heat exchanger, a spiral plate type heat exchanger, a spiral tube wound heat exchanger and a plate type heat exchanger can be selected but not limited.
The third storage tank 11 is a permeate buffer tank, and the buffered water is output by a third fluid delivery device 13. The third fluid transfer device 13 may be exemplified by, but not limited to, a centrifugal pump, a positive displacement pump.
The fourth fluid transportation device 12 is a gas transportation device, and is used for generating system vacuum, and may be generally selected from, but not limited to, a liquid ring vacuum pump and unit, a dry vacuum pump and unit, a screw vacuum pump and unit, a roots liquid ring vacuum pump and unit, a roots screw vacuum pump and unit, a rotary vane vacuum pump, and a jet vacuum pump.
On the other hand, liquid foam droplets are entrained in the evaporation equipment 4 due to the rising of the isopropanol solvent vapor, and a liquid foam removing device can be arranged at the top of the evaporation equipment 4 for removing the liquid foam droplets. The liquid foam removing device can be a wire mesh foam remover which is arranged in the evaporation device, and can also be an external gas-liquid separator with a foam remover.
In the structural description of the above-mentioned device, the components that can be determined by those skilled in the art through the prior art in this field are not described, and these components can be exemplified but not limited to: piping for connecting the various devices, a feed tank for storing and/or supplying an aqueous solution containing isopropanol, a product tank for receiving/processing an isopropanol product, and the like. In addition, in combination with the above description, those skilled in the art can determine the most appropriate device selection and type according to the design requirements and requirements under the guidance of the prior art, and it is needless to describe this.
In combination with the isopropanol pervaporation dehydration device in the above embodiment, the method for dehydrating isopropanol purified by a molecular sieve membrane according to the present invention can be further described as comprising the following steps:
(1) after being buffered by the first storage tank 1, the water-containing isopropanol raw material is conveyed by the first fluid conveying pump 2 at the mass flow rate of 1000kg/h into the first heat exchange device 3 for preheating. The heat source adopted for preheating is isopropanol finished product steam from a membrane separation module, and the temperature of the preheated raw material is raised to 70-90 ℃, preferably to 80 +/-2 ℃;
(2) The preheated raw material enters an evaporation device 4 (through a pipeline), the isopropanol raw material containing 10 percent of water is vaporized in the evaporation device, the pressure after vaporization is 0.2-0.4MPa, the temperature is 100-;
the dehydrated isopropanol finished product steam (namely retentate) enters first heat exchange equipment 3 to preheat the raw material, recovers part of heat energy, is condensed and cooled by a second heat exchanger 5 to obtain an isopropanol product (with water purity meeting the requirement), enters a second storage tank 8, and is conveyed to be stored by second fluid conveying equipment 9;
the pressure of the vaporized raw material is 0.2-0.4MPa, and the temperature is 100-;
(3) the permeation side of the membrane separation assembly 6 is provided with vacuum by a fourth fluid conveying device 12 (a vacuum pump), and the pressure of the vacuum side is 0-30 kPa; the water vapor of the permeate is condensed by the third heat exchanger 10 to obtain liquid permeate, and the liquid permeate is buffered by the third storage tank 11 and then conveyed to be stored by the third fluid conveying equipment 13;
the whole process for purifying isopropanol and dehydrating by the molecular sieve membrane adopts continuous operation.
The optimization of the overall solution according to the invention should take into account the influence of the combination of technical features on the overall solution in addition to the application of the above-mentioned preferred technical features. The present invention provides the specific embodiment of the above-mentioned molecular sieve membrane purification isopropanol dehydration method to specifically illustrate the implementation mode and effect of the present invention. In this example, the method described herein uses an isopropanol pervaporation dehydration unit as illustrated in fig. 1, and the selection of the various devices in the unit is as follows:
the first storage tank 1 is a raw material buffer tank.
The first fluid conveying device 2 is a centrifugal pump.
The first heat exchange device 3 adopts a spiral pipe wound heat exchanger.
The evaporation equipment 4 adopts a shell and tube evaporator.
The membrane separation component 6 is a tubular molecular sieve membrane component; the molecular sieve membrane is an A-type molecular sieve membrane.
The second heat exchanger 5 is a spiral pipe wound heat exchanger.
The second storage tank 8 is a product buffer tank, and the second fluid conveying equipment 9 is a centrifugal pump.
The pressure regulating device 7 is a pressure regulating valve.
The third heat exchanger 10 is a spiral plate heat exchanger.
The third storage tank 11 is a penetrating fluid buffer tank, and the third fluid conveying device 13 is a centrifugal pump.
The fourth fluid transfer device 12 is a dry vacuum pump.
The method for dehydrating and refining the isopropanol by combining the device comprises the following steps:
(1) after an isopropanol crude product raw material containing 10% of water and 90% of isopropanol is buffered by a raw material buffer tank 1, the raw material is conveyed by a centrifugal pump 2 at a mass flow rate of 1000kg/h to enter a spiral tube winding heat exchanger 3 for preheating, a heat source adopted for preheating is finished product steam coming out of a tubular molecular sieve membrane component 6, the temperature of the preheated isopropanol raw material is raised, the preheating temperature is 80 ℃, and the water content of the finished product isopropanol steam for preheating is less than 0.5%;
(2) the crude isopropanol raw material preheated to 80 ℃ enters a tubular evaporator 4 through a pipeline, the liquid phase raw material is changed into a vapor phase (the vapor phase fraction is 1) in the tubular evaporator 4, and then the vapor phase raw material enters a tubular molecular sieve membrane component 6, the operating pressure of the material side of the membrane component is 0.4MPa, and the operating temperature is 130 ℃. The model of the molecular sieve membrane filled in the membrane component is NaA type, and the total membrane area is 120m2The configuration that 5 membrane assemblies are connected in series to form one group and two groups in total is adopted. Isopropanol finished product steam from the membrane module contains less than 0.5 percent of water, has the mass flow rate of 905kg/h, the pressure of 0.38MPa and the temperature of 125 ℃, enters a spiral tube winding heat exchanger 3 firstly, preheats raw material crude isopropanol, recovers partial heat energy, recovers the heat energy of 50kW, is equivalent to saving 86kg/h of steam consumption (saving 95kg of steam consumption per ton of product), is condensed and cooled to 40 ℃ by a finished product condenser 5 to obtain an isopropanol product with water purity meeting the requirement, enters a finished product buffer tank 8, and is conveyed by a centrifugal pump 9 for storage; the pressure and the temperature of the vaporized isopropanol raw material are 0.4MPa The temperature is 120 ℃, so that the isopropanol material entering the membrane separation assembly can be effectively dehydrated, and the dehydrated isopropanol vapor keeps proper temperature and pressure to meet the requirements of power and heat returning to the raw material preheater;
(3) the water obtained from the permeation side of the tubular molecular sieve membrane component 6 is in a vacuum steam state, and is condensed by the spiral plate type heat exchanger 10 to obtain liquid penetrating fluid, the mass flow rate of the penetrating fluid is 95kg/h, the water content is more than 99 percent, and the penetrating fluid is conveyed to be stored by the centrifugal pump 13 after being buffered by the penetrating fluid buffer tank 11; the vacuum side pressure is 0-30 kPa;
(4) the whole process for purifying isopropanol and dehydrating by the molecular sieve membrane adopts continuous operation.
(5) The comprehensive energy consumption of the device is shown in the table below, and compared with the existing water-containing isopropanol dehydration process, the device has the advantages of great energy consumption and cost in view of cost.
Claims (7)
1. The isopropanol dehydration and purification method is characterized by comprising the following steps: conveying the water-containing isopropanol raw material to heat exchange equipment at a mass flow rate of 800-1200 kg/h for preheating, and introducing the raw material preheated to 70-90 ℃ into a membrane separation assembly for dehydration at a pressure of 0.2-0.4MPa and a temperature of 100-;
and conveying the dehydrated isopropanol product steam to heat exchange equipment to exchange heat with the raw material, and then condensing and collecting the isopropanol product.
2. The process of claim 1 wherein the aqueous isopropanol feed contains no more than 10% by weight water.
3. The method of claim 1, wherein the membrane separation module permeate side pressure is 0-30kPa absolute.
4. The method of claim 1, wherein the feed preheat temperature is 80 ± 2 ℃.
5. The process of claim 1, wherein the process uses an isopropanol pervaporation dehydration unit comprising a feed processing unit, a membrane separation unit, a retentate processing unit, and a permeate processing unit, wherein: the raw material processing unit comprises a first storage tank (1), a first fluid conveying device (2) and a first heat exchange device (3);
wherein the first heat exchange device (3) is provided with a raw material inlet, a raw material outlet, a heat exchange medium inlet and a heat exchange medium outlet; the membrane separation unit is provided with a raw material inlet, a retentate outlet and a permeate outlet;
the heat exchange medium inlet of the first heat exchange device (3) is connected with the retentate outlet of the membrane separation unit; the outlet of the heat exchange medium of the first heat exchange device (3) is connected with a retentate treatment unit;
And the permeate outlet of the membrane separation unit is connected with the permeate treatment unit.
6. The method according to claim 5, wherein the isopropanol pervaporation dehydration unit comprises a raw material processing unit, a membrane separation unit, a retentate processing unit and a permeate processing unit, wherein the raw material processing unit comprises a first storage tank (1), a first fluid conveying device (2), a first heat exchange device (3) and an evaporation device (4); the membrane separation unit is provided with a raw material inlet, a retentate outlet and a permeate outlet; the retentate treatment unit comprises a second heat exchanger (5), a second storage tank (8) and a second fluid conveying device (9); the permeate treatment unit comprises a third heat exchanger (10), a third storage tank (11), and a third fluid delivery device (13); wherein the content of the first and second substances,
the first heat exchange device (3) is provided with a raw material inlet, a raw material outlet, a heat exchange medium inlet and a heat exchange medium outlet; the heat exchange medium inlet of the first heat exchange device (3) is connected with the retentate outlet of the membrane separation unit, and a pressure regulating device (7) is arranged between the heat exchange medium inlet and the retentate outlet; the outlet of the heat exchange medium of the first heat exchange device (3) is connected with the retentate treatment unit;
The membrane separation unit consists of one or more membrane separation modules (6), and A-type molecular sieve membranes are filled in the membrane separation modules (6);
the third heat exchanger (10) is also connected with a fourth fluid conveying device (12) for vacuum generation.
7. The method of claim 6, comprising the steps of:
(1) after being buffered by a first storage tank (1), the water-containing isopropanol raw material is conveyed by a first fluid conveying pump (2) at a mass flow rate of 800-1200 kg/h to enter first heat exchange equipment (3) for preheating, the heat source adopted for preheating is isopropanol finished product steam from a membrane separation module, and the temperature of the preheated raw material is raised to 70-90 ℃, preferably to 80 +/-2 ℃;
(2) the preheated raw material enters an evaporation device (4), the isopropanol raw material containing 10 percent of water is vaporized in the evaporation device, the pressure is 0.2-0.4MPa and the temperature is 100-; the dehydrated isopropanol finished product steam firstly enters first heat exchange equipment (3) to preheat raw materials, recovers partial heat energy, is condensed and cooled by a second heat exchanger (5) to obtain an isopropanol product, enters a second storage tank (8), and is conveyed to be stored by second fluid conveying equipment (9);
(3) The permeate side of the membrane separation assembly (6) is provided with vacuum by a fourth fluid conveying device (12), and the pressure of the vacuum side is 0-30 kPa; the water vapor of the permeate is condensed by a third heat exchanger (10) to obtain liquid permeate, and the liquid permeate is buffered by a third storage tank (11) and then is conveyed to be stored by a third fluid conveying device (13);
the whole process for purifying isopropanol and dehydrating by the molecular sieve membrane adopts continuous operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010614818.8A CN111848348A (en) | 2020-06-30 | 2020-06-30 | Isopropyl alcohol dehydration refining method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010614818.8A CN111848348A (en) | 2020-06-30 | 2020-06-30 | Isopropyl alcohol dehydration refining method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111848348A true CN111848348A (en) | 2020-10-30 |
Family
ID=72988874
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010614818.8A Pending CN111848348A (en) | 2020-06-30 | 2020-06-30 | Isopropyl alcohol dehydration refining method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111848348A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112843766A (en) * | 2020-12-29 | 2021-05-28 | 复榆(张家港)新材料科技有限公司 | Adsorption separation process for pressure swing adsorption separation solvent water binary azeotrope |
| CN114956935A (en) * | 2022-06-09 | 2022-08-30 | 南京佳华工程技术有限公司 | Coupling deep dehydration method and system for electronic-grade water-containing organic matters |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080216649A1 (en) * | 2007-03-06 | 2008-09-11 | Membrane Technology And Research, Inc. | Liquid-phase and vapor-phase dehydration of organic/water solutions |
| US20120152840A1 (en) * | 2009-09-02 | 2012-06-21 | Hitachi Zosen Corporation | Method for dewatering water-containing organic substance |
| CN103224456A (en) * | 2013-04-08 | 2013-07-31 | 江苏九天高科技股份有限公司 | Process and device for refining acetonitrile with a pervaporation method |
| CN103408514A (en) * | 2013-08-20 | 2013-11-27 | 江苏九天高科技股份有限公司 | Technique and device for recovering tetrahydrofuran by pervaporation method |
| CN103709016A (en) * | 2013-12-21 | 2014-04-09 | 江苏九天高科技股份有限公司 | Process and device for refining glycol dimethyl ether by using pervaporation method |
| CN103709022A (en) * | 2013-12-21 | 2014-04-09 | 江苏九天高科技股份有限公司 | Process and device for recovering butanone by pervaporation method |
| CN103910605A (en) * | 2013-12-27 | 2014-07-09 | 江苏九天高科技股份有限公司 | Pervaporation system and technology for refining biological n-butanol by pervaporation system |
| WO2015026161A1 (en) * | 2013-08-20 | 2015-02-26 | 주식회사 엘지화학 | Method for purifying isopropyl alcohol |
-
2020
- 2020-06-30 CN CN202010614818.8A patent/CN111848348A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080216649A1 (en) * | 2007-03-06 | 2008-09-11 | Membrane Technology And Research, Inc. | Liquid-phase and vapor-phase dehydration of organic/water solutions |
| US20120152840A1 (en) * | 2009-09-02 | 2012-06-21 | Hitachi Zosen Corporation | Method for dewatering water-containing organic substance |
| CN103224456A (en) * | 2013-04-08 | 2013-07-31 | 江苏九天高科技股份有限公司 | Process and device for refining acetonitrile with a pervaporation method |
| CN103408514A (en) * | 2013-08-20 | 2013-11-27 | 江苏九天高科技股份有限公司 | Technique and device for recovering tetrahydrofuran by pervaporation method |
| WO2015026161A1 (en) * | 2013-08-20 | 2015-02-26 | 주식회사 엘지화학 | Method for purifying isopropyl alcohol |
| CN103709016A (en) * | 2013-12-21 | 2014-04-09 | 江苏九天高科技股份有限公司 | Process and device for refining glycol dimethyl ether by using pervaporation method |
| CN103709022A (en) * | 2013-12-21 | 2014-04-09 | 江苏九天高科技股份有限公司 | Process and device for recovering butanone by pervaporation method |
| CN103910605A (en) * | 2013-12-27 | 2014-07-09 | 江苏九天高科技股份有限公司 | Pervaporation system and technology for refining biological n-butanol by pervaporation system |
Non-Patent Citations (2)
| Title |
|---|
| 王晴等: "渗透汽化膜技术回收含水异丙醇的工业研究", 《河北科技大学学报》 * |
| 白雪彬等: "渗透汽化回收制药废液中异丙醇", 《黑龙江医药科学》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112843766A (en) * | 2020-12-29 | 2021-05-28 | 复榆(张家港)新材料科技有限公司 | Adsorption separation process for pressure swing adsorption separation solvent water binary azeotrope |
| CN114956935A (en) * | 2022-06-09 | 2022-08-30 | 南京佳华工程技术有限公司 | Coupling deep dehydration method and system for electronic-grade water-containing organic matters |
| CN114956935B (en) * | 2022-06-09 | 2024-03-26 | 南京佳华科技股份有限公司 | Electronic-grade water-containing organic matter coupling deep dehydration method and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9266803B2 (en) | Liquid separation by membrane assisted vapor stripping process | |
| US6755975B2 (en) | Separation process using pervaporation and dephlegmation | |
| EP2421622B1 (en) | Combined vaporizing and absorption process and apparatus | |
| BRPI0812764B1 (en) | processes for separating a feed mix and processing facility | |
| CN103551036B (en) | A kind of ceramic molecular sieve membrane high-effective penetrating vaporising device and technique | |
| CN111848348A (en) | Isopropyl alcohol dehydration refining method | |
| KR101317571B1 (en) | Dehydration of glycols through the hollow fiber membranes | |
| CN212881891U (en) | Isopropanol pervaporation dehydration device | |
| CN111909120B (en) | Energy-saving separation process of water-containing ternary azeotropic system | |
| JP2020075865A (en) | Water-alcohol separation system and water-alcohol separation method for producing alcohol | |
| CN214004476U (en) | NMP device is refine in pervaporation membrane separation | |
| CN107198967A (en) | Multiple-effect membrane regeneration plant and method for gas purification solvent reclamation | |
| CN206940774U (en) | A kind of tetrahydrofuran dehydration device | |
| CN215610590U (en) | Organic solvent's edulcoration water trap | |
| CN102764559B (en) | Combined technique of separating and recycling VOCS (volatile organic compounds) from industrial waste gas by adsorption-desorption-rectification-pervaporation | |
| CN213680472U (en) | Tetrahydrofuran dehydration refining plant | |
| JPH02273519A (en) | Concentrate of volatile organic liquid aqueous solution | |
| CN214361095U (en) | Energy-saving separation device of water-containing ternary azeotropic system | |
| CN111943811A (en) | Energy-saving absolute ethyl alcohol membrane separation refining method | |
| CN110382068A (en) | A kind of crystallization apparatus and method | |
| CN106986769B (en) | Separation and integration system and separation and integration method of ethyl acetate-water system | |
| CN218944765U (en) | Zeolite membrane dewatering device for efficiently separating water in water-containing solvent | |
| CN214106479U (en) | High-efficient ethanol-water membrane separation device | |
| CN117085369A (en) | Gas-liquid dual-purpose organic matter fine dehydration device and process | |
| CN216171416U (en) | Membrane separation system of methyl acetate and/or ethyl acetate and methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20201030 |