CN218131072U - Hollow fiber pervaporation membrane pilot plant - Google Patents
Hollow fiber pervaporation membrane pilot plant Download PDFInfo
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- CN218131072U CN218131072U CN202222506415.9U CN202222506415U CN218131072U CN 218131072 U CN218131072 U CN 218131072U CN 202222506415 U CN202222506415 U CN 202222506415U CN 218131072 U CN218131072 U CN 218131072U
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Abstract
The utility model provides a pilot plant for hollow fiber pervaporation membranes, which comprises a raw material storage tank, a hollow fiber pervaporation membrane assembly and a condenser which are connected in sequence, wherein the condenser comprises a tube layer and a heat exchange layer, the upper end of the tube layer is communicated with the hollow fiber pervaporation membrane assembly, and the heat exchange layer is communicated with a water chiller; the utility model discloses reduce equipment overall area, increase purification separation effect.
Description
Technical Field
The utility model relates to a purification splitter field especially relates to a hollow fiber pervaporation membrane pilot scale device.
Background
Pervaporation is a new membrane separation technology, realizes selective separation of materials by utilizing the difference of affinity and mass transfer resistance of a pervaporation membrane to different components in feed liquid, can be used for separation of azeotrope and near-boiling-point substances which are difficult to treat by the traditional separation means, removal of water and removal of trace organic matters in water, and has the advantages of high efficiency, energy conservation, simple process and environmental friendliness, thereby being widely applied. However, pervaporation technology and device architecture directly determine the separation efficiency and processing capacity of the overall pervaporation process.
The existing permeation device is usually connected with external storage tanks, condensers and other equipment, and needs to occupy a large area when being connected for use, and meanwhile, the final product effect can be influenced because the existing permeation device can have the condition of incomplete purification and separation after single permeation.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a reduce equipment overall area, increase the hollow fiber pervaporation membrane pilot scale device of purification separation effect.
In order to solve the technical problem, the utility model provides a hollow fiber pervaporation membrane pilot scale device, including raw material storage tank, hollow fiber pervaporation membrane module and the condenser that connects gradually, the condenser includes the tube layer and trades the heat layer, tube layer upper end and hollow fiber pervaporation membrane module intercommunication, trades heat layer and cold water machine intercommunication.
Furthermore, one side of the hollow fiber pervaporation membrane module close to the raw material storage tank is a concentration side, one side of the hollow fiber pervaporation membrane module close to the condenser is a permeation side, and a raw material pump is arranged between the concentration side and the raw material storage tank.
Further, the lower end of the middle tube layer of the condenser is communicated with the penetrating fluid collecting tank.
Furthermore, one side of the penetrating fluid collecting tank is connected with a vacuum pump.
Furthermore, a temperature measuring probe and a heating rod are arranged on the raw material storage tank and used for controlling the temperature of filtrate in the raw material storage tank.
Further, the hollow fiber pervaporation membrane module comprises an outer layer interface and an inner layer interface, wherein the outer layer interface is connected with the raw material storage tank, and the inner layer interface is connected with the condenser.
Furthermore, the raw material storage tank is provided with a feeding funnel and a sampling port.
Furthermore, a first pressure gauge and a liquid level display are arranged on the raw material storage tank.
Furthermore, a flow meter and a thermometer are connected between the raw material pump and the hollow fiber pervaporation membrane module.
Furthermore, the penetrating fluid collecting tank is provided with a second pressure gauge, and the bottom of the penetrating fluid collecting tank is provided with a water outlet.
The beneficial effects of the utility model reside in that:
1. the raw material storage tank, the hollow fiber pervaporation membrane module and the condenser are integrated into the same equipment, so that the floor area of the whole equipment is effectively reduced;
2. after the raw material pump drives the filtrate in the raw material storage tank to flow into the hollow fiber pervaporation membrane module for permeation, the purified filtrate flows back to the raw material storage tank, and then the purity of the filtrate in the raw material storage tank is increased through multiple times of permeation purification so as to ensure the permeation separation effect of the filtrate.
Drawings
Fig. 1 is a first schematic structural diagram of the present invention.
FIG. 2 is a schematic diagram of the present invention
Reference numerals: 1. a raw material storage tank; 2. a feedstock pump; 3. a hollow fiber pervaporation membrane module; 4. a condenser; 5. a water chiller; 6. a permeate collection tank; 7. a vacuum pump; 8. a master control console; 9. a charging hopper; 10. a first pressure gauge; 11. a temperature probe; 12. a heating rod; 13. a liquid level display; 14. a flow meter; 15. a thermometer; 16. an outer layer interface; 17. an inner layer interface; 18. a tube layer; 19. a heat exchange layer; 20. a second pressure gauge; 21. and a water outlet.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art all belong to the protection scope of the present invention.
It will be understood by those skilled in the art that in the present disclosure, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in a generic and descriptive sense only and not for purposes of limitation, as the terms are used in the description to indicate that the referenced device or element must have the specified orientation, be constructed and operated in the specified orientation, and not for the purposes of limitation.
It is understood that the terms "a" and "an" should be interpreted as meaning that a number of one element or element is one in one embodiment, while a number of other elements is one in another embodiment, and the terms "a" and "an" should not be interpreted as limiting the number.
As shown in fig. 1-2, the utility model provides a hollow fiber pervaporation membrane pilot scale unit, including raw materials storage tank 1, hollow fiber pervaporation membrane module 3 and the condenser 4 that connects gradually, condenser 4 includes pipe layer 18 and heat transfer layer 19, and pipe layer 18 upper end and hollow fiber pervaporation membrane module 3 intercommunication, heat transfer layer 19 and cold water machine 5 intercommunication.
Specifically, when the raw material needs to be separated, the raw material is placed in the raw material storage tank, then a valve between the raw material storage tank and the hollow fiber pervaporation membrane module is opened, so that the raw material flows into the hollow fiber pervaporation membrane module, and the raw material is subjected to pervaporation through the hollow fiber pervaporation membrane module, so that part of components in the raw material flows to a condenser after passing through the hollow fiber pervaporation membrane module, at the moment, the separated part of components is condensed and liquefied through the condenser and then collected to one position, the purified raw material at one side of the hollow fiber pervaporation membrane module, which is close to the raw material storage tank, returns to the raw material storage tank again, and then after multiple times of separation and purification processes are continuously performed, the purity of the raw material in the raw material storage tank is ensured, and the separation effect is improved.
The condenser comprises a pipe layer and a heat exchange layer, and the heat exchange layer is communicated with the water chiller, so that after part of components separated by the hollow fiber pervaporation membrane module enter the condenser, cooling water and cooling liquid can be provided for the heat exchange layer through the water chiller, the part of components in the pipe layer are fully condensed, and the problem that the part of components are mixed with the cooling water and the cooling liquid is solved.
In an embodiment of this scheme, the heat transfer layer parcel is in the outside of pipe layer to make cooling water, coolant liquid can effectually cool off the intraduct.
It should be noted that the hollow fiber pervaporation membrane module in the present embodiment includes a pervaporation membrane, which is the prior art and is not described herein in detail.
Preferably, the side of the hollow fiber pervaporation membrane module 3 close to the raw material tank 1 is a concentration side, the side of the hollow fiber pervaporation membrane module 3 close to the condenser 4 is a permeation side, and the raw material pump 2 is provided between the concentration side and the raw material tank 1.
Specifically, raw materials in a raw material storage tank are effectively conveyed to a hollow fiber pervaporation membrane module through a raw material pump, after pervaporation, a separated part of the components move to a permeation side and flow to a condenser, and raw materials which cannot undergo pervaporation still remain on a concentration side after purification, so that the purity of the raw materials on the concentration side is increased after subsequent purification for multiple times.
Wherein, the raw material pump adopts equipment such as water pump, suction pump.
Preferably, the lower end of the tube layer 18 in the condenser 4 communicates with the permeate collection tank 6.
Specifically, after components subjected to permeation separation enter a condenser to be condensed and liquefied, the components are collected through a penetrating fluid collecting tank so as to be conveniently subjected to subsequent unified treatment.
Preferably, a vacuum pump 7 is connected to one side of the permeate collection tank 6.
Specifically, the vacuum pump is used for sucking the permeation side of the condenser and the hollow fiber pervaporation membrane module, so that part of components which can be separated from the raw material can enter the permeation side from the concentration side more easily, the effect of pervaporation is improved, and meanwhile, due to the arrangement of the vacuum pump, the separated components cannot participate in new gas components, and the grouping stability is guaranteed.
Preferably, the raw material storage tank 1 is provided with a temperature probe 11 and a heating rod 12 for controlling the temperature of the filtrate in the raw material storage tank 1.
Specifically, heat the inside raw materials of raw materials storage tank through the heating rod, detect the temperature of raw materials in to the raw materials storage tank through the temperature probe simultaneously to guarantee that the temperature of this department raw materials is accurate, suitable.
Preferably, the hollow fiber pervaporation membrane module 3 comprises an outer layer interface 16 and an inner layer interface 17, wherein the outer layer interface 16 is connected with the raw material storage tank 1, and the inner layer interface 17 is connected with the condenser 4.
Specifically, through the setting of outer layer interface and inlayer interface for hollow fiber pervaporation membrane module when being connected with raw materials storage tank and condenser, can guarantee that concentrated side and infiltration side can not make mistakes, also guarantee simultaneously that some in the raw materials can get into in the condenser after complete infiltration separation.
Preferably, the raw material storage tank 1 is provided with an addition funnel 9 and a sampling port.
Specifically, by the inside raw materials that adds of feed hopper to raw materials storage tank, after the purification of certain number of times, the accessible sample connection takes out suitable raw materials simultaneously, and then conveniently detects the raw materials purity this moment to whether the judgement satisfies the purity demand or needs continue to purify.
In an embodiment of the scheme, the sampling opening is covered with a sealing cover, and the sealing cover is opened to sample when the sampling is needed.
Preferably, the raw material storage tank 1 is provided with a first pressure gauge 10 and a liquid level display 13.
Specifically, the pressure in the raw material storage tank is observed in real time through the first pressure gauge, and the raw material or the tank body is prevented from being influenced by overlarge pressure in the raw material storage tank.
Simultaneously because liquid level display's setting for raw materials storage liquid level in the raw materials storage tank can audio-visual demonstration on liquid level display, so that the user direct observation liquid level height, and then judge whether need add the raw materials.
In an embodiment of this scheme, liquid level display is connected with liquid level detector, through the liquid level height in the liquid level detector real time monitoring raw materials storage tank, and then shows on liquid level display.
Preferably, a flow meter 14 and a thermometer 15 are connected between the raw material pump 2 and the hollow fiber pervaporation membrane module 3.
Specifically, when the raw material pump delivers the raw material to the hollow fiber pervaporation membrane module, the flow and the temperature of the concentrated side of the hollow fiber pervaporation membrane module are respectively detected through a flow meter and a thermometer, so as to ensure the stability of the delivery of the raw material.
Preferably, the permeate collection tank 6 is provided with a second pressure gauge 20, and the bottom of the permeate collection tank 6 is provided with a water outlet 21.
Specifically, after a certain amount of permeate is collected in the permeate collection tank, the drain port is opened, and the permeate is discharged outward through the drain port.
Simultaneously, because the setting of second manometer for the pressure size in the penetrant collecting vat can real-time detection by the second manometer, when pressure is great, can in time open the outlet and carry out flowing back and pressure release.
Specially, this scheme still has master control platform 8, and equipment such as first manometer, second manometer, raw materials pump, heating rod are connected to master control platform department to supply power and control it through master control platform, increase the holistic stability of this scheme hollow fiber pervaporation membrane pilot scale device.
It is worth mentioning that the scheme adopts the following steps when the components are used for purifying and separating the raw materials:
step 1: storing the filtrate in a raw material storage tank, and heating according to the temperature characteristic of the filtrate, such as dehydrating ethanol and heating to 70 deg.C, dehydrating isopropanol and heating to 70-80 deg.C;
step 2: conveying the filtrate to a hollow fiber pervaporation membrane module for separation by using a raw material pump at a constant flow rate, wherein the flow rate of the filtrate at the concentration side is 500ml/min; the penetration side is connected with a condenser, a penetrating fluid collecting tank and a vacuum system, the vacuum degree of the penetration side is 8-9kpa, a heat exchange layer of the condenser is connected with a water chiller, and the set temperature of the water chiller is determined according to the liquefaction temperature of the penetrating fluid;
and 3, step 3: and returning the feed liquid on the concentrated side in the second step to the raw material storage tank to ensure that the concentration of the filtrate in the raw material storage tank is higher and higher until the requirement of a finished product meets the national standard.
The present scheme provides the following examples to clarify the manner of using the above-described hollow fiber pervaporation membrane pilot plant:
example 1-ethanol dehydration:
firstly, a hollow fiber pervaporation membrane component is checked to ensure that no yarn leakage and yarn breakage occur; feeding industrial grade ethanol (50% of water content, 50%) into a raw material storage tank 1, setting the temperature of the raw material storage tank 1 to be 70 ℃, and blowing air into the filtrate in the raw material storage tank 1 by using a raw material pump 2 to enable the filtrate to circularly flow so as to ensure that the temperature of the filtrate is uniform; starting a water chiller 5, adjusting according to the environmental temperature, wherein the temperature is set to be 3 ℃ in winter and is set to be-3 ℃ in summer; starting a vacuum pump 7 to clean the permeation side of the hollow fiber pervaporation membrane, wherein the vacuum degree is 8-9kpa; when the temperature of the filtrate reaches 70 ℃, introducing the filtrate into a hollow fiber pervaporation module assembly 3 for separation and purification by using a raw material pump at the flow rate of 500ml/min, returning the purified ethanol into a raw material storage tank 1, introducing the purified ethanol into a condenser 4 through the guide of a vacuum pump 7 on the permeation side for heat exchange, and condensing the pure water into a penetrating fluid collecting tank 6; 50% industrial grade ethanol can be purified to 99.9% by the operation of the device; and after the requirement is met, shutting down the machine, and cleaning the components and the pipeline.
Wherein, the water content of the ethanol purified in the example 1 is determined by a Karl Fischer titration method, the Karl Fischer consumes water by titration, and the purity of the ethanol is obtained by testing the water content, and the specific data are shown in a table 1.
TABLE 1
Example 2-dehydration of isopropanol:
firstly, a hollow fiber pervaporation membrane component is checked to ensure that no yarn leakage and yarn breakage occur; feeding a raw material of industrial grade isopropanol (50 percent and 50 percent of water) into a raw material storage tank 1, setting the temperature of the raw material storage tank 1 to be 80 ℃, and blowing air into the filtrate in the raw material storage tank 1 by using a raw material pump 2 to enable the filtrate to circularly flow so as to ensure that the temperature of the filtrate is uniform; starting a water chiller 5, adjusting according to the environmental temperature, wherein the temperature is set to be 3 ℃ in winter and is set to be-3 ℃ in summer; starting a vacuum pump 7 to clean the permeation side of the hollow fiber pervaporation membrane, wherein the vacuum degree is 8-9kpa; when the temperature of the filtrate reaches 80 ℃, the filtrate is guided into the hollow fiber pervaporation module assembly 3 for separation and purification by using the raw material pump 2 at the flow rate of 500ml/min, the purified ethanol returns to the raw material storage tank 1, the permeation side is guided by the vacuum pump 7 and is added with the condenser 4 for heat exchange, and the pure water is condensed into the penetrating fluid collecting tank 6; the 50% industrial grade isopropanol can be purified to 99.9% by the operation of the device; and after the requirement is met, shutting down the machine, and cleaning the components and the pipeline.
The water content of the isopropanol purified in example 2 was determined by karl fischer titration, the water content was measured by karl fischer titration to determine the purity of the isopropanol, and the specific data are shown in table 2.
TABLE 2
The present invention is not limited to the above preferred embodiments, and any person can obtain other products in various forms without changing the shape or structure of the product, and all the products having the same or similar technical solutions as the present invention fall within the protection scope of the present invention.
Claims (10)
1. A pilot plant for a hollow fiber pervaporation membrane is characterized in that: the water-cooling system comprises a raw material storage tank (1), a hollow fiber pervaporation membrane module (3) and a condenser (4) which are sequentially connected, wherein the condenser (4) comprises a tube layer (18) and a heat exchange layer (19), the upper end of the tube layer (18) is communicated with the hollow fiber pervaporation membrane module (3), and the heat exchange layer (19) is communicated with a water cooler (5).
2. The hollow fiber pervaporation membrane pilot plant according to claim 1, characterized in that: the side of the hollow fiber pervaporation membrane module (3) close to the raw material storage tank (1) is a concentration side, the side of the hollow fiber pervaporation membrane module (3) close to the condenser (4) is a permeation side, and a raw material pump (2) is arranged between the concentration side and the raw material storage tank (1).
3. The hollow fiber pervaporation membrane pilot plant according to claim 1, characterized in that: the lower end of a pipe layer (18) in the condenser (4) is communicated with a penetrating fluid collecting tank (6).
4. The hollow fiber pervaporation membrane pilot plant according to claim 3, characterized in that: one side of the penetrating fluid collecting tank (6) is connected with a vacuum pump (7).
5. The hollow fiber pervaporation membrane pilot plant according to claim 1, characterized in that: the raw material storage tank (1) is provided with a temperature probe (11) and a heating rod (12) for controlling the temperature of the filtrate in the raw material storage tank (1).
6. The hollow fiber pervaporation membrane pilot plant according to claim 1, characterised in that: the hollow fiber pervaporation membrane module (3) comprises an outer layer interface (16) and an inner layer interface (17), wherein the outer layer interface (16) is connected with the raw material storage tank (1), and the inner layer interface (17) is connected with the condenser (4).
7. The hollow fiber pervaporation membrane pilot plant according to claim 1, characterised in that: the raw material storage tank (1) is provided with a feeding funnel (9) and a sampling port.
8. The hollow fiber pervaporation membrane pilot plant according to claim 1, characterised in that: the raw material storage tank (1) is provided with a first pressure gauge (10) and a liquid level display (13).
9. The hollow fiber pervaporation membrane pilot plant according to claim 2, characterized in that: a flowmeter (14) and a thermometer (15) are connected between the raw material pump (2) and the hollow fiber pervaporation membrane module (3).
10. The hollow fiber pervaporation membrane pilot plant according to claim 3, characterized in that: the penetrating fluid collecting tank (6) is provided with a second pressure gauge (20), and the bottom of the penetrating fluid collecting tank (6) is provided with a water outlet (21).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222506415.9U CN218131072U (en) | 2022-09-19 | 2022-09-19 | Hollow fiber pervaporation membrane pilot plant |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222506415.9U CN218131072U (en) | 2022-09-19 | 2022-09-19 | Hollow fiber pervaporation membrane pilot plant |
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| CN218131072U true CN218131072U (en) | 2022-12-27 |
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| CN202222506415.9U Active CN218131072U (en) | 2022-09-19 | 2022-09-19 | Hollow fiber pervaporation membrane pilot plant |
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