CN218636644U - Device for separating dimethyl carbonate and methanol azeotrope with low energy consumption - Google Patents
Device for separating dimethyl carbonate and methanol azeotrope with low energy consumption Download PDFInfo
- Publication number
- CN218636644U CN218636644U CN202221578421.9U CN202221578421U CN218636644U CN 218636644 U CN218636644 U CN 218636644U CN 202221578421 U CN202221578421 U CN 202221578421U CN 218636644 U CN218636644 U CN 218636644U
- Authority
- CN
- China
- Prior art keywords
- membrane module
- pervaporation membrane
- dimethyl carbonate
- tower
- pressure
- 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.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a device of low energy consumption separation dimethyl carbonate and methyl alcohol azeotrope, wherein, the entry of the surplus side exit linkage second pervaporation membrane module of first pervaporation membrane module, the entry of the infiltration side exit linkage high pressure rectification tower of first pervaporation membrane module, the entry of the surplus liquid exit linkage ordinary pressure rectifying column of infiltration of second pervaporation membrane module, the top of the tower fraction exit linkage of high pressure rectifying column the entry of ordinary pressure rectifying column. The utility model has the advantages of the purification of dimethyl carbonate and methyl alcohol is realized to the method that uses two rectifying columns and membrane system second grade separation to combine, and the energy consumption is low, and safety, environmental protection, pollution-free can realize cleaner production.
Description
Technical Field
The utility model belongs to the chemical industry separation field, concretely relates to device of low energy consumption separation dimethyl carbonate and methyl alcohol azeotrope.
Background
Dimethyl carbonate (DMC) is a green solvent with excellent performance, and can be completely mixed with most of solvents such as ketone, alcohol, ether, etc. DMC is nontoxic and contains functional groups such as methyl, carbonyl and the like in the structure, can replace highly toxic dimethyl sulfate, methyl chloroformate and phosgene to carry out methylation reaction to synthesize a plurality of downstream products with high added values, eliminates the pollution of the highly toxic chemicals to the environment, is an environment-friendly organic chemical intermediate, and becomes 'new cornerstone' in organic synthesis in a new period. With the rapid development of new energy fields at home and abroad, the electrolyte is used as a main solvent for the composition of the electrolyte, and the market demand is gradually expanding. Meanwhile, DMC can be used for preparing high and new material polycarbonate through ester exchange, polymerization and other processes, becomes an important chemical raw material in the field of new production of polycarbonate, and can greatly promote the growth of industrial scale. The gasoline additive has a high oxygen content in the molecular structure, has a good octane number improving effect, and is considered to be one of the most potential gasoline additives.
The main production routes of DMC include phosgene process, methanol oxidation and carbonylation process, CO 2 Direct synthesis, urea alcoholysis and ester exchange synthesis. The phosgene method uses strong corrosive and virulent radioactive phosgene, the production process seriously pollutes the environment and has serious potential safety hazard, and the method is gradually eliminated. At present, CO 2 Both the direct synthesis and the urea alcoholysis process remain limited to the laboratory or to the pilot-scale research phase of kilotons/year. Oxidative carbonylation processes include direct oxidative carbonylation of methanol and indirect oxidative carbonylation. The indirect oxidation carbonylation method is that methanol and NOx firstly generate methyl nitrite, and the methyl nitrite generates carbonylation reaction to obtain DMC and N 2 O，N 2 The O is reoxidized to NOx. The advantage of this process is the low cost of the starting material, but the disadvantages are equally evident, N 2 O is known as laughing gas, has neurotoxicity and has a greenhouse effect of CO 2 300 times of the amount of the product, and simultaneously produces water as a byproduct and industrial wastewater, so the method is not environment-friendly. The DMC prepared by the method has lower purity, a large amount of byproducts (such as dimethyl oxalate and the like) of oxygen-containing compounds are generated, the byproducts of oxidation reaction are mostly common diseases, and the process difficulty of separating the byproducts into electronic-grade chemicals is higher. And the route adopts the noble metal catalyst, the catalyst price is higher, and along with the popularization of the technology, the price of the noble metal catalyst can be greatly increased. Meanwhile, a small amount of nitric acid with strong corrosiveness is generated in the continuous operation process of the technology. The liquid phase oxidation carbonylation method mainly uses cuprous chloride as a catalyst. The cuprous chloride in the reaction system has high corrosivity and high requirement on equipment, so the investment cost is high, the catalyst is easy to inactivate, and the service life is short.
Whether methanol oxidation carbonylation method or CO method is adopted 2 The direct synthesis, urea alcoholysis and transesterification synthesis all suffer from the problem of separation of methanol and DMC azeotropes. Under normal pressure, the azeotropic temperature of methanol and DMC is 63.7 ℃, the azeotropic composition of methanol and DMC is 70wt% and 30wt%, and the common rectification process is difficult to realize the product refining requirement. For the separation of methanol and DMC, the main technological techniques studied at present are extractive distillation, pressure swing separation, recrystallization andand a membrane separation method, and the most widely industrialized application is an extractive distillation method and a pressure swing separation method. The entrainer with high boiling point outside the system is often introduced in the extraction and rectification, the complete separation and recovery in the later period are difficult, the product quality is influenced, and the process operation is complicated. Pressure swing separation is realized by changing the volatility of azeotrope components by utilizing pressure change in the process, but the high-pressure rectification process has relatively high operation temperature and large energy consumption and heat loss, and the separation process needs to be enhanced and upgraded urgently.
The patent CN 104370698A and CN 104370699A disclose that dimethyl carbonate and methanol are separated, only a pressurized tower or an atmospheric tower is used on the membrane permeation side, the fraction at the top of the tower also comprises dimethyl carbonate, the fraction at the top of the tower directly returns to a reaction rectifying tower, the yield of the dimethyl carbonate is lower, the steam energy consumption is high, and a methanol product is not obtained. Patent CN 110404422A discloses an organic composite membrane for separating methanol and dimethyl carbonate, which has a much shorter service life than inorganic composite membranes in industrial applications. The patent CN 101143803A only considers the separation of dimethyl carbonate and methanol by using a membrane, does not consider the separation of components at the top of the atmospheric distillation column and components at the retentate side of the membrane, and does not circulate among streams, which results in low yield of dimethyl carbonate, high energy consumption, and is not beneficial to industrial popularization. The patents CN 201823480U and CN107206286A disclose that the front of dimethyl carbonate and methanol is atmospheric tower, and the bottom of the tower is methanol product, which violates the scientific principle, the azeotropic mixture between the atmospheric tower and the methanol can not be separated theoretically, the tower still can not obtain any pure product, and if the front end of the membrane is provided with a rectifying tower, the front end of the membrane must be high pressure tower. The azeotrope contains 70wt% of methanol, the heat of vaporization of methanol is very large, and if a membrane which is permeable to methanol preferentially is selected, the energy consumption is relatively high.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a device that is fit for industrial popularization's low energy consumption separation dimethyl carbonate and methyl alcohol azeotrope adopts the method that the preferential dimethyl carbonate membrane separation technique of passing through and rectifying column combine to separate, can obtain two kinds of products of high-purity dimethyl carbonate and methyl alcohol simultaneously, improves separation effect and product yield, reduces the energy consumption.
In order to achieve the above object, the utility model adopts the following technical scheme:
a device for separating dimethyl carbonate and methanol is characterized in that an outlet at the permeation side of a first pervaporation membrane module is connected with an inlet of a second pervaporation membrane module, an outlet at the permeation side of the first pervaporation membrane module is connected with an inlet of a high-pressure rectifying tower, an outlet at the permeation side of the second pervaporation membrane module is connected with an inlet of an atmospheric rectifying tower, and an outlet at the top of the high-pressure rectifying tower is connected with an inlet of the atmospheric rectifying tower.
Further, the first pervaporation membrane module and the second pervaporation membrane module adopt a pervaporation membrane which preferentially permeates dimethyl carbonate.
Further, the preferential penetration dimethyl carbonate pervaporation membrane is a tubular organic-inorganic composite membrane, the carrier of the preferential penetration dimethyl carbonate pervaporation membrane is alumina, corundum or mullite, and the upper layer of the preferential penetration dimethyl carbonate pervaporation membrane is alumina, titanium oxide or zirconium oxide; the organic film layer is an organic silicon hybrid film with controllable aperture formed by co-condensation of propyl trimethoxy silane and 1, 3-bis (triethoxysilyl) propane.
Further, the outlet of the permeation side of the second pervaporation membrane module is connected with the inlet of the first pervaporation membrane module.
Further, a heater is arranged at the inlet of the first pervaporation membrane module.
Further, an overhead fraction outlet of the atmospheric distillation tower is connected with an inlet of the first pervaporation membrane module.
Furthermore, the heat of the top of the high-pressure rectifying tower is connected with the reboiler of the normal-pressure rectifying tower through a heat exchanger to supply heat for the reboiler of the normal-pressure rectifying tower.
Further, an outlet at the permeation side of the first pervaporation membrane module is connected with a first condenser, and an outlet at the permeation side of the second pervaporation membrane module is connected with a second condenser.
Further, the first pervaporation membrane module and the second pervaporation membrane module are connected with a vacuum system, and a driving force is provided by the vacuum system.
The utility model can be operated by adopting a common method.
To achieve a better separation effect, the following method can also be used:
raw materials enter a first pervaporation membrane module, a first penetrating fluid obtained after pervaporation treatment enters a high-pressure rectifying tower for rectification treatment, and a first residual liquid enters a second pervaporation membrane module; the second residual liquid obtained by the second pervaporation membrane module enters a normal pressure rectifying tower for rectification; obtaining dimethyl carbonate at the bottom of the high-pressure rectifying tower; and obtaining methanol at the bottom of the atmospheric distillation tower.
Preferably, the operating temperature of the first pervaporation membrane module is 40 to 60 ℃.
Preferably, the operating temperature of the second pervaporation membrane module is 40 to 60 ℃.
Preferably, the concentration of the dimethyl carbonate in the raw material is 20 to 30wt%, and the raw material enters the first pervaporation membrane module in a gas phase or liquid phase mode.
The concentration of dimethyl carbonate in the first penetrating fluid is 40 to 90wt%. The concentration of dimethyl carbonate in the penetrating fluid obtained by the second membrane module is 20 to 40wt%. The concentration of the dimethyl carbonate in the second residual solution is 0.5-20wt%.
Preferably, the absolute pressure of the vacuum system is 1000 to 10000Pa.
Preferably, the reflux ratio of the high-pressure rectifying tower is 0.5 to 5, the operating pressure is 0.2 to 0.7MPa, and the tower top temperature is 90 to 130 ℃.
Preferably, the reflux ratio of the atmospheric distillation tower is 0.5 to 5, the operating pressure is 0.01 to 0.1MPa, and the tower top temperature is 60 to 70 ℃.
The utility model discloses following beneficial effect has:
1. the utility model discloses a preferentially pass through dimethyl carbonate's organic inorganic complex film, this complex film can effectively break methyl alcohol-dimethyl carbonate azeotropic bottleneck, changes the relative volatility of azeotrope, reduces substantially the steam energy consumption, and the membrane is higher to dimethyl carbonate's selectivity, and the steam energy consumption is lower more, the utility model discloses the selectivity and the stability of the membrane of chooseing for use are superior to the membrane of document data report.
2. The utility model discloses a device set up two-stage membrane separation system, the high-tension column is advanced to the one-level penetrant, and the mixed back one-level membrane system of second grade penetrant and raw materials. The top heat of high-pressure column is used for the tower cauldron heating of atmospheric tower, matches each other through membrane separation system and high-low pressure rectifying column, and every ton dimethyl carbonate's steam consumption is about 7.2 tons under the condition of heat retrieval and utilization in traditional pressure swing rectifying technology, the utility model discloses a steam energy consumption only has 30 of traditional pressure swing rectifying technology to 50%, and the handling capacity of high-pressure column only has 40% of traditional pressure swing rectifying technology high-pressure column, and the handling capacity of atmospheric tower only has 60% of traditional pressure swing rectifying technology atmospheric tower.
3. The device and the process of the utility model can reduce the operating pressure and the treatment capacity of the high-pressure tower, improve the yield of dimethyl carbonate and further reduce the separation difficulty and the tower load.
4. The utility model adopts continuous operation, can simultaneously obtain two products of dimethyl carbonate and methanol with the purity of more than or equal to 99.5wt percent, and has the advantages of high yield and no three wastes in the cyclic separation of all materials in the system.
5. The utility model provides a technology of rectifying column and membrane has comprehensively considered investment and working costs, is fit for the industrialization and promotes.
Drawings
FIG. 1 is a schematic diagram of an apparatus for separating dimethyl carbonate and methanol.
Wherein, 1 is a first pervaporation membrane component, 2 is a second pervaporation membrane component, 3 is a high-pressure rectifying tower, 4 is an atmospheric rectifying tower, 5 is a first condenser, 6 is a second condenser, 7 is a reboiler of the high-pressure rectifying tower, 8 is the reboiler of the atmospheric rectifying tower, 9 is a heater, and 10 is a vacuum system. In the figure, the realized arrows represent the material flow direction, and the dotted arrows represent the heat supply direction.
Detailed Description
The present invention will be further explained with reference to the following examples. The following examples are provided only for illustrating the present invention and are not intended to limit the scope of the present invention.
As shown in fig. 1, in the apparatus for separating dimethyl carbonate and methanol, an outlet on a retentate side of a first pervaporation membrane module 1 is connected to an inlet of a second pervaporation membrane module 2, an outlet on a permeate side of the first pervaporation membrane module 2 is connected to an inlet of a high-pressure rectification column 3, an outlet on a retentate side of the second pervaporation membrane module 2 is connected to an inlet of an atmospheric rectification column 4, and an outlet of a fraction on a top of the high-pressure rectification column 3 is connected to an inlet of the atmospheric rectification column 4.
The first pervaporation membrane module 1 and the second pervaporation membrane module 2 adopt a pervaporation membrane which permeates dimethyl carbonate preferentially.
And the outlet at the permeation side of the second pervaporation membrane module 2 is connected with the inlet of the first pervaporation membrane module 1.
A heater 9 is arranged at the inlet of the first pervaporation membrane module 1.
And the top fraction outlet of the atmospheric distillation tower 4 is connected with the inlet of the first pervaporation membrane module 1.
The heat of the high-pressure rectifying tower 3 supplies heat to a reboiler 8 of the normal-pressure rectifying tower 4.
The outlet of the permeation side of the first pervaporation membrane module 1 is connected with a first condenser 5, and the outlet of the permeation side of the second pervaporation membrane module 2 is connected with a second condenser 6.
The first pervaporation membrane module 1 and the second pervaporation membrane module 2 are driven by a vacuum system 10.
Example 1
The raw material containing 30wt% of dimethyl carbonate and methanol is heated to 50 ℃ by adopting the device and then enters the membrane component, and the raw material is separated by the two-stage membrane component through the organosilicon hybrid membrane/alumina ceramic which adopts the cocondensation of propyl trimethoxy silane and 1, 3-bis (triethoxy silicon-based) propane and preferentially permeates the dimethyl carbonate pervaporation membrane. The downstream side of the membrane adopts a vacuum pumping and condensation mode to form the vapor partial pressure difference of components on the upstream side and the downstream side of the membrane. Penetrating fluid steam enters a first condenser and a second condenser respectively under the suction of 5000Pa absolute pressure of a vacuum unit to obtain a first penetrating fluid and a second penetrating fluid, the concentration of dimethyl carbonate in the first penetrating fluid is 50wt%, and the first penetrating fluid enters a high-pressure rectifying tower for treatment. The concentration of the dimethyl carbonate in the second penetrating fluid is 28wt percent, and the raw material containing 30wt percent of dimethyl carbonate and methanol is mixed and then returned to the first pervaporation membrane module for circular treatment.
The first penetrating fluid is conveyed to the middle part of a high-pressure rectifying tower by a tower feeding pump, the high-pressure rectifying tower is operated under the pressure of 0.2MPa, the reflux ratio is 1, the temperature at the top of the tower is 130 ℃, a reboiler at a tower kettle is heated and vaporized, after the full-reflux stabilizing operation, part of the first penetrating fluid is condensed and refluxed to the top of the high-pressure rectifying tower, a methanol mixture containing 20 percent of dimethyl carbonate is extracted from the top of the tower, and 99.8 percent of DMC product by weight is extracted from the tower kettle. And the product at the top of the tower enters an atmospheric tower for treatment. The heat of the tower top product is provided for a tower kettle reboiler of the atmospheric distillation tower.
The second residual solution and the product on the top of the high-pressure rectifying tower are conveyed to the middle part of the normal-pressure rectifying tower by a tower feeding pump, the normal-pressure rectifying tower is operated under the pressure of 0.05MPa, the reflux ratio is 1, the temperature on the top of the tower is 65 ℃, a reboiler at the bottom of the tower is heated and vaporized, after the full-reflux stabilizing operation, the second residual solution is condensed by a condenser at the top of the tower, part of the second residual solution reflows to the top of the normal-pressure rectifying tower, the methanol mixture containing 25wt% DMC is partially extracted, and the methanol product with the concentration of 99.5wt% is extracted from the bottom of the tower. And the product at the top of the tower circularly enters a first pervaporation membrane module to be treated. The heat of the tower bottom comes from the heat of the tower top of the high-pressure rectifying tower.
Example 2
The device is adopted to make the gas phase raw material of 28wt% dimethyl carbonate and methanol with the temperature of 60 ℃ enter a membrane component, and an organic silicon hybrid membrane/alumina ceramic which is co-condensed by propyl trimethoxy silane and 1, 3-bis (triethoxy silicon base) propane is adopted to preferentially permeate a dimethyl carbonate pervaporation membrane and is separated by a two-stage membrane component. The downstream side of the membrane adopts a vacuum pumping and condensation mode to form the vapor partial pressure difference of components on the upstream side and the downstream side of the membrane. Penetrating fluid steam enters a first condenser and a second condenser respectively under the suction of 10000Pa absolute pressure of a vacuum unit to obtain a first penetrating fluid and a second penetrating fluid, wherein the concentration of dimethyl carbonate in the first penetrating fluid is 60wt%, and the first penetrating fluid enters a high-pressure rectifying tower for treatment. The dimethyl carbonate with the concentration of 32wt% in the second penetrating fluid is heated and vaporized, and then mixed with raw materials containing 28wt% of dimethyl carbonate and methanol, and then returned to the first pervaporation membrane module for circular treatment.
The first penetrating fluid is conveyed to the middle part of a high-pressure rectifying tower by a tower feeding pump, the high-pressure rectifying tower is operated under the pressure of 0.4MPa, the reflux ratio is 5, the temperature at the top of the tower is 90 ℃, a reboiler at the bottom of the tower is heated and vaporized, after the full-reflux stabilizing operation, part of the first penetrating fluid is condensed and refluxed to the top of the high-pressure rectifying tower, a methanol mixture containing 20 percent of dimethyl carbonate is extracted from a gas phase part and enters a normal pressure tower for treatment, and 99.7 percent of DMC products by weight are extracted from the bottom of the tower.
The second residual solution and the tower top product of the high-pressure rectifying tower are conveyed to the middle part of the normal-pressure rectifying tower by a tower feeding pump, the normal-pressure rectifying tower is operated under the pressure of 0.01MPa, the reflux ratio is 5, the temperature at the tower top is 70 ℃, a reboiler of a tower kettle is heated and vaporized, after the full reflux stabilizing operation, part of the second residual solution flows back to the top part of the normal-pressure rectifying tower, a methanol mixture containing 26wt% DMC is extracted from a gas phase, the methanol mixture enters a first pervaporation membrane component for treatment, and a methanol product with the concentration of 99.5wt% is extracted from the tower kettle.
Example 3
The raw materials of 20wt% dimethyl carbonate and methanol are heated to 40 ℃ by adopting the device, enter a membrane component, and are separated by a two-stage membrane component by adopting an organosilicon hybrid membrane/alumina ceramic which is co-condensed by propyl trimethoxy silane and 1, 3-bis (triethoxy silicon-based) propane and preferentially permeating the dimethyl carbonate pervaporation membrane. The downstream side of the membrane adopts a vacuum pumping and condensing mode to form the vapor partial pressure difference of components on the upstream side and the downstream side of the membrane. Penetrating fluid steam enters a first condenser and a second condenser respectively under the suction of 1000Pa of absolute pressure of a vacuum unit to obtain a first penetrating fluid and a second penetrating fluid, wherein the concentration of dimethyl carbonate in the first penetrating fluid is 40wt%, and the first penetrating fluid enters a high-pressure rectifying tower for treatment. The concentration of the dimethyl carbonate in the second penetrating fluid is 32wt percent, and the second penetrating fluid is heated and gasified, mixed with the raw material containing 20wt percent of dimethyl carbonate and methanol and returned to the first pervaporation membrane module for circular treatment.
The first penetrating fluid is conveyed to the middle part of a high-pressure rectifying tower by a tower feeding pump, the high-pressure rectifying tower is operated under the pressure of 0.7MPa, the reflux ratio is 0.5, the temperature at the top of the tower is 128 ℃, a reboiler at the bottom of the tower is heated and vaporized, after the full reflux stabilizing operation, part of the first penetrating fluid is condensed and refluxed to the top of the high-pressure rectifying tower, a methanol mixture containing 20 percent of dimethyl carbonate is extracted from a gas phase part and enters a normal pressure tower for treatment, and 99.7 percent of DMC products by weight are extracted from the bottom of the tower.
The second residual liquid and the tower top product of the high-pressure rectifying tower are conveyed to the middle part of the normal-pressure rectifying tower by a tower feeding pump, the normal-pressure rectifying tower is operated under the pressure of 0.1MPa, the reflux ratio is 0.5, the temperature at the top of the tower is 60 ℃, a reboiler at the tower bottom is heated and vaporized, after the full reflux stabilizing operation, part of the mixture flows back to the top of the normal-pressure rectifying tower, a methanol mixture containing 26wt% of DMC is extracted from a gas phase, the methanol mixture enters a first pervaporation membrane component for treatment, and a methanol product with the concentration of 99.5wt% is extracted from the tower bottom.
Claims (8)
1. The device for separating dimethyl carbonate and methanol azeotrope with low energy consumption is characterized in that an outlet on the permeation side of a first pervaporation membrane module is connected with an inlet of a second pervaporation membrane module, an outlet on the permeation side of the first pervaporation membrane module is connected with an inlet of a high-pressure rectifying tower, a retentate outlet of the second pervaporation membrane module is connected with an inlet of an atmospheric rectifying tower, and an overhead fraction outlet of the high-pressure rectifying tower is connected with an inlet of the atmospheric rectifying tower.
2. The low-energy-consumption device for separating dimethyl carbonate from methanol azeotrope, according to claim 1, wherein the first pervaporation membrane module and the second pervaporation membrane module adopt a permselective dimethyl carbonate pervaporation membrane.
3. The low energy consumption apparatus for separating dimethyl carbonate from methanol azeotrope according to claim 1, wherein the outlet of the second pervaporation membrane module on the permeation side is connected with the inlet of the first pervaporation membrane module.
4. The low-energy-consumption device for separating dimethyl carbonate from methanol azeotrope according to claim 1, wherein the inlet of the first pervaporation membrane module is provided with a heater.
5. The device for separating dimethyl carbonate from methanol azeotrope with low energy consumption as claimed in claim 1, wherein the overhead fraction outlet of the atmospheric distillation tower is connected with the inlet of the first pervaporation membrane module.
6. The device for separating dimethyl carbonate from methanol azeotrope with low energy consumption according to claim 1, wherein the overhead heat of the high pressure distillation column is connected with the reboiler of the atmospheric distillation column through a heat exchanger.
7. The low-energy-consumption device for separating dimethyl carbonate from methanol azeotrope according to claim 1, wherein the outlet of the first pervaporation membrane module on the permeation side is connected with a first condenser, and the outlet of the second pervaporation membrane module on the permeation side is connected with a second condenser.
8. The low-energy-consumption device for separating dimethyl carbonate from methanol azeotrope according to claim 1, wherein the first pervaporation membrane module and the second pervaporation membrane module are connected with a vacuum system, and the driving force is provided by the vacuum system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221578421.9U CN218636644U (en) | 2022-06-23 | 2022-06-23 | Device for separating dimethyl carbonate and methanol azeotrope with low energy consumption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221578421.9U CN218636644U (en) | 2022-06-23 | 2022-06-23 | Device for separating dimethyl carbonate and methanol azeotrope with low energy consumption |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218636644U true CN218636644U (en) | 2023-03-17 |
Family
ID=85488745
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221578421.9U Active CN218636644U (en) | 2022-06-23 | 2022-06-23 | Device for separating dimethyl carbonate and methanol azeotrope with low energy consumption |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218636644U (en) |
-
2022
- 2022-06-23 CN CN202221578421.9U patent/CN218636644U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9169186B2 (en) | System and method for continuously producing polyoxymethylene dimethyl ethers | |
| CN101143803B (en) | Method for separating dimethyl carbonate and methanol azeotrope | |
| US8845863B2 (en) | Alkylene oxide purification processes and systems | |
| CN106431812B (en) | A kind of method and device of separation of extractive distillation toluene-methanol-water azeotropic mixture | |
| CN112225650B (en) | Refining method for obtaining high-purity methylal by purifying industrial-grade methylal | |
| US10377689B2 (en) | Process for preparing polyoxymethylene dimethyl ethers from formaldehyde and methanol in aqueous solutions | |
| CN101289389B (en) | Production process of ethyl acetate | |
| CN114949907A (en) | Device and method for separating dimethyl carbonate and methanol azeotrope with low energy consumption | |
| CN110743372A (en) | Device and process for preparing methanol and butyl acetate | |
| EP2307112B1 (en) | System and process for alkylene oxide purification | |
| CN101092365A (en) | Technical method for associated producing carbonic allyl ester, methyl carbonate, and propylene glycol | |
| CN218636644U (en) | Device for separating dimethyl carbonate and methanol azeotrope with low energy consumption | |
| CN114591155A (en) | Methylal rectification process | |
| CN104370699B (en) | The technique of the integrated separating dimethyl carbonate of a kind of infiltration evaporation-atmospheric distillation and methyl alcohol | |
| CN111100004B (en) | Method and integrated device for refining dimethyl carbonate | |
| CN114315522A (en) | Method for purifying cyclohexanol and method for producing cyclohexanone | |
| CN218553168U (en) | Device for separating methanol and dimethyl carbonate azeotrope by membrane separation coupled rectification | |
| CN115282913A (en) | Reaction system and method for preparing methyl propionate | |
| CN113200820B (en) | Method for separating dimethyl carbonate and methanol by using imidazole ionic liquid | |
| CN113698371A (en) | Method and device for recovering tetrahydrofuran by rectification-membrane separation coupling method | |
| CN220513452U (en) | Piperidine separation and purification system | |
| CN114163332B (en) | Process for preparing dimethyl carbonate by removing methanol from near-azeotropic-concentration dimethyl carbonate-methanol mixture | |
| CN112174816B (en) | Method and device for reactive distillation and membrane coupling in backpack tower | |
| CN115572215B (en) | Separation method of methanol and dimethyl carbonate azeotrope through coupling and rectification of membrane separation | |
| CN219848214U (en) | Recovery device for dimethyl carbonate as byproduct of dimethyl oxalate synthesis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |