CN114478250A - Preparation method of methyl ethyl carbonate and co-production of diethyl carbonate - Google Patents
Preparation method of methyl ethyl carbonate and co-production of diethyl carbonate Download PDFInfo
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- JBTWLSYIZRCDFO-UHFFFAOYSA-N ethyl methyl carbonate Chemical compound CCOC(=O)OC JBTWLSYIZRCDFO-UHFFFAOYSA-N 0.000 title claims abstract description 35
- OIFBSDVPJOWBCH-UHFFFAOYSA-N Diethyl carbonate Chemical compound CCOC(=O)OCC OIFBSDVPJOWBCH-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000002360 preparation method Methods 0.000 title claims abstract description 14
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims abstract description 61
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 239000000463 material Substances 0.000 claims abstract description 24
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 22
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 18
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000000047 product Substances 0.000 claims abstract description 9
- 238000000066 reactive distillation Methods 0.000 claims abstract description 8
- 239000012043 crude product Substances 0.000 claims abstract description 4
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 239000000376 reactant Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 20
- 239000002994 raw material Substances 0.000 claims description 11
- 150000002148 esters Chemical group 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 230000014759 maintenance of location Effects 0.000 claims 1
- 239000000203 mixture Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 5
- 229910001416 lithium ion Inorganic materials 0.000 description 5
- -1 sodium alkoxide Chemical class 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000003792 electrolyte Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000005886 esterification reaction Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 3
- 235000017557 sodium bicarbonate Nutrition 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 description 2
- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 238000005809 transesterification reaction Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000006315 carbonylation Effects 0.000 description 1
- 238000005810 carbonylation reaction Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- GDVKFRBCXAPAQJ-UHFFFAOYSA-A dialuminum;hexamagnesium;carbonate;hexadecahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Al+3].[Al+3].[O-]C([O-])=O GDVKFRBCXAPAQJ-UHFFFAOYSA-A 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 229960001545 hydrotalcite Drugs 0.000 description 1
- 229910001701 hydrotalcite Inorganic materials 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 229910003002 lithium salt Inorganic materials 0.000 description 1
- 159000000002 lithium salts Chemical class 0.000 description 1
- 229910001960 metal nitrate Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005832 oxidative carbonylation reaction Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C68/00—Preparation of esters of carbonic or haloformic acids
- C07C68/06—Preparation of esters of carbonic or haloformic acids from organic carbonates
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C68/00—Preparation of esters of carbonic or haloformic acids
- C07C68/08—Purification; Separation; Stabilisation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to a preparation method of ethyl methyl carbonate and co-production of diethyl carbonate, belonging to the technical field of chemical industry. The invention discloses a preparation method of ethyl methyl carbonate and diethyl carbonate, which comprises the following steps: putting dimethyl carbonate and ethanol into a pre-reaction kettle, mixing, and then dripping a catalyst concentrated sulfuric acid into the pre-reaction kettle to perform pre-reaction; the reacted materials enter a reaction rectifying tower to continue, after a light component dimethyl carbonate/methanol azeotrope separated from the tower top passes through a rectifying tower I, a methanol finished product is obtained at the tower top, and the tower kettle materials return to a pre-reaction kettle; feeding the heavy component reactant crude product obtained from the tower kettle of the reactive distillation tower into a dealcoholization tower; the rest materials enter a continuous rectification section; firstly, the mixture enters a rectification tower II, light components at the tower top are partially applied to a dealcoholization tower, ethyl methyl carbonate is extracted from the side, the rest kettle material continuously flows into a rectification tower III, the light components at the tower top are sleeved back to the rectification tower II, diethyl carbonate is extracted from the side, and the rest materials in the rectification tower III are recovered and applied to a pre-reaction kettle.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and relates to a preparation method for co-producing diethyl carbonate from methyl ethyl carbonate.
Background
Ethyl Methyl Carbonate (EMC) is an environmentally friendly carbonate, is chemically active and is a common organic synthetic intermediate. EMC has excellent thermal conductivity and electrochemical stability, and can be used as an environment-friendly solvent; meanwhile, due to the structural advantages, the lithium ion battery electrolyte is an important lithium ion battery electrolyte composition, and the lithium ion battery electrolyte has an asymmetric structure and small steric hindrance, so that the solubility of lithium salt can be improved, and the energy density and the discharge capacity of the battery can be further improved. After China establishes new energy automobiles to be specially researched and developed, the lithium ion battery has excellent performances of high energy density, high voltage, long cycle life, good safety, environmental friendliness, no pollution and the like, and the demand of the electrolyte is continuously increased, so that the lithium ion battery drives the EMC to have very wide market prospect. The main production methods of EMC include phosgene method, oxidative carbonylation method and ester exchange method. The phosgene method has the disadvantages of complicated process flow, high operation requirement, harsh reaction conditions of the oxidation and carbonylation method and serious pollution. The transesterification method has the advantages of simple process flow, mild reaction conditions, low cost and relatively low pollution, is a mainstream industrial production method at present, takes dimethyl carbonate as a raw material, and performs transesterification with ethanol under the action of a catalyst to obtain EMC, but the EMC is easy to further react to continuously generate diethyl carbonate, and EMC disproportionation per se can also generate dimethyl carbonate and diethyl carbonate under the same conditions, so that the ethyl methyl carbonate is removed from a reaction system in time during the reaction to prevent the EMC from being excessively converted. However, the current process route is generally limited by the low conversion and selectivity of the catalyst. In addition, the traditional industrial production of methyl ethyl carbonate mainly uses an alkaline catalyst mainly comprising sodium alkoxide, water in a reaction system reacts with diethyl carbonate to generate a small amount of carbonic acid, the sodium alkoxide and the carbonic acid react to generate sodium bicarbonate and sodium carbonate, the sodium bicarbonate and the sodium carbonate are separated out in a solid form to cause catalyst inactivation and influence the activity and the service life of the catalyst, and excessive catalyst is often required to be added to meet the production requirement, so that resource waste is caused.
Chinese patent application document CN201710593249.1 discloses a method for preparing methyl ethyl carbonate by ester exchange, which adopts a fixed bed reaction process of ester exchange of dimethyl carbonate and diethyl carbonate, uses metal nitrate and hydrochloride as active component sources of a catalyst, adopts an impregnation method to load alkaline or acidic metal oxide, and has esterification catalytic efficiency of more than 20g/gh, reaction temperature of 200 ℃, airspeed of 30h-1Under the condition, the conversion rate of the product diethyl carbonate is 69.17 percent. The active components of the catalyst are easy to lose in the reaction process, and the conversion rate is low. Chinese patent CN201611057992.7 discloses a method for synthesizing methyl ethyl carbonate by calcium-magnesium-aluminum composite oxide catalysis, wherein the catalyst is obtained by roasting calcium-magnesium-aluminum hydrotalcite at the temperature of 400-600 ℃ for 2-8 h; the catalyst has low price and easy separation, but has general catalytic activity, low conversion rate and easy loss of active components. Chinese patent application CN 201810708682.X discloses a production process of methyl ethyl carbonate, which takes dimethyl carbonate and ethanol as raw materials to synthesize methyl ethyl carbonate under the catalytic action of sodium methoxide. However, sodium alkoxide reacts with carbonic acid generated in the reaction to generate sodium bicarbonate and sodium carbonate, which are precipitated to cause catalyst deactivation, and the catalyst has low activity and short service life.
The esterification reaction is a reversible reaction, the prior art is difficult to achieve the optimal equilibrium state of the reaction, and the prior catalyst generally has the problems of low conversion rate and selectivity and poor stability. Therefore, the selection of a catalyst which has high activity, high selectivity and good stability and is easy to separate and recycle and the improvement of the product conversion rate have important significance.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a preparation method of ethyl methyl carbonate and diethyl carbonate, wherein sulfuric acid is used as a catalyst, so that the ethyl methyl carbonate and the diethyl carbonate have high purity.
The invention adopts the following technical scheme: a preparation method of ethyl methyl carbonate and diethyl carbonate, which comprises the following steps:
putting dimethyl carbonate and ethanol into a pre-reaction kettle, mixing, dripping catalyst concentrated sulfuric acid, and heating for pre-reaction; the reacted materials enter a reaction rectifying tower to continue ester exchange, after a light component dimethyl carbonate/methanol azeotrope separated from the tower top passes through a rectifying tower I, a methanol finished product is obtained at the tower top, and the tower kettle materials return to a pre-reaction kettle; the heavy component reactant crude product obtained from the tower bottom of the reactive distillation tower enters a dealcoholization tower, unreacted raw materials of ethanol and dimethyl carbonate are removed from the tower top, and the raw materials are returned to the pre-reaction kettle again to participate in the reaction; the rest materials enter a continuous rectification section; after the material enters a continuous rectification working section, the material firstly enters a rectification tower II, light components on the tower top are partially applied to a dealcoholization tower, ethyl methyl carbonate is extracted laterally, the rest kettle material continuously flows into a rectification tower III, the light components on the tower top are sleeved and returned to the rectification tower II, diethyl carbonate is extracted laterally, and the rest materials in the rectification tower III are recycled and applied to a pre-reaction kettle.
Preferably, the mass ratio of the dimethyl carbonate to the ethanol is (6-10): 1.
Preferably, the mass of the concentrated sulfuric acid catalyst accounts for 0.5-20% of the total mass of the raw materials.
Preferably, the heating speed in the pre-reaction kettle is 4-6 ℃/min, the reaction temperature is 50-90 ℃, the reaction time is 6-10h, and the operation pressure is 10-200 kPa.
Further preferably, the reaction temperature in the pre-reaction kettle is 60-80 ℃ and the time is 7-8 h.
Preferably, the 1 to 6 reactive distillation columns are used in series.
Further preferably, the operating pressure of the reactive distillation column is 0-50kPa, the reaction temperature is 80-100 ℃, and the reaction time is 9-11 h.
Preferably, the reaction temperature of the rectification tower I is 60-75 ℃, the pressure is 0-0.1MPa, and the reaction time is 4-5 h.
Preferably, the operating temperature of the dealcoholization tower is 80-100 ℃, and the operating pressure is 0.01-0.03 MPa.
Preferably, the rectification II tower is operated under normal pressure, the operation temperature is 80-110 ℃, and the time is 3-6 h.
Preferably, the operation temperature of the rectifying column III is 60-95 ℃, the operation pressure is-0.08-0 MPa, and the time is 3-6 h.
Further preferably, in the continuous rectification reaction, the reflux ratio is 6 to 10.
Further preferably, the mass percentage of EMC in the product is 55-65%, the mass percentage of DEC is 15-25%, and the mass percentage of the byproduct methanol is 20-30%.
Compared with the prior art, the invention has the following beneficial effects:
1. the method can be used for preparing Ethyl Methyl Carbonate (EMC) and co-producing diethyl carbonate (DEC).
2. The invention adopts a reaction rectification mode, and the methanol generated in the system is continuously evaporated out, so that the reaction balance moves forward; and sulfuric acid is used as a catalyst for ester exchange reaction, and the reaction conversion rate reaches 92%.
3. The EMC purity of the product prepared by the method is more than or equal to 99.99%, and the DEC purity is more than or equal to 99.99%.
4. The invention adopts the sulfuric acid as the catalyst, so that the cost can be saved, and the sulfuric acid has water absorption and can absorb water generated in the dealcoholization esterification reaction, thereby overcoming the defects of low catalyst activity and low conversion rate caused by the reaction of the traditional alkaline catalyst in water.
5. The sulfuric acid, the middle distillate and the heavy components of the sulfuric acid can be recycled.
Drawings
FIG. 1 is a flow chart of the present invention.
Detailed Description
The following are specific examples of the present invention and further describe the technical solutions of the present invention, but the present invention is not limited to these examples.
Example 1
Putting dimethyl carbonate and ethanol with the mass ratio of 6:1 into a pre-reaction kettle, mixing, dropwise adding 4% concentrated sulfuric acid, heating to 70 ℃ at the speed of 5 ℃/min, and pre-reacting for 7.5 h; the reacted materials enter a reaction rectifying tower, ester exchange is continuously carried out at 90 ℃ for 10h under the operation pressure of 40kPa, light component dimethyl carbonate/methanol azeotrope separated from the tower top continuously flows into a rectifying tower I through a pipeline, reaction is carried out at 70 ℃ for 4h under the pressure of 0.05MPa, a methanol finished product is obtained at the tower top, and the tower kettle materials return to a pre-reaction kettle; the heavy component reactant crude product obtained from the tower kettle of the reactive distillation tower enters a dealcoholization tower, reacts for 3 hours at 90 ℃ under the operating pressure of 0.02MPa, and unreacted raw materials, namely ethanol and DMC, are removed from the tower top and then return to the pre-reaction kettle again to participate in the reaction; the rest material enters a continuous rectification working section through a pipeline, and then enters a rectification II tower at first, the rectification II tower is operated under normal pressure, after the reaction at 100 ℃ for 4 hours, the light components at the tower top are partially applied to a dealcoholization tower, side extraction is performed to obtain Ethyl Methyl Carbonate (EMC), the rest kettle material continuously flows into a rectification III tower, the rectification III tower reacts at 90 ℃ for 4 hours under the operating pressure of-0.05 Mpa, the light components at the tower top are applied to the rectification II tower in a sleeved mode, side extraction is performed to obtain diethyl carbonate (DEC), and the rest material in the rectification III tower is recovered and applied to a pre-reaction kettle
Examples 2-39 ethyl methyl carbonate was synthesized with co-production of diethyl carbonate using the raw materials and parameters of the examples in table 1 in accordance with the procedure of example 1.
TABLE 1 feed parameters and results for examples 1-39
In conclusion, the method can realize the recycling of the raw materials and the catalyst, and the EMC and DEC purity of the prepared product is more than or equal to 99.99 percent.
The specific embodiments described herein are merely illustrative of the spirit of the invention. Various modifications or additions may be made to the described embodiments, or alternatives may be employed, by those skilled in the art, without departing from the spirit or ambit of the invention as defined in the appended claims.
Claims (10)
1. A preparation method of ethyl methyl carbonate and diethyl carbonate is characterized by comprising the following steps:
putting dimethyl carbonate and ethanol into a pre-reaction kettle, mixing, dripping catalyst concentrated sulfuric acid, and heating for pre-reaction; the reacted materials enter a reaction rectifying tower to continue ester exchange, after a light component dimethyl carbonate/methanol azeotrope separated from the tower top passes through a rectifying tower I, a methanol finished product is obtained at the tower top, and the tower kettle materials return to a pre-reaction kettle; the heavy component reactant crude product obtained from the tower bottom of the reactive distillation tower enters a dealcoholization tower, unreacted raw materials of ethanol and dimethyl carbonate are removed from the tower top, and the raw materials are returned to the pre-reaction kettle again to participate in the reaction; the rest materials enter a continuous rectification section; after the material enters a continuous rectification working section, the material firstly enters a rectification tower II, light components on the tower top are partially applied to a dealcoholization tower, ethyl methyl carbonate is extracted laterally, the rest kettle material continuously flows into a rectification tower III, the light components on the tower top are sleeved and returned to the rectification tower II, diethyl carbonate is extracted laterally, and the rest materials in the rectification tower III are recycled and applied to a pre-reaction kettle.
2. The preparation method according to claim 1, wherein the mass ratio of the dimethyl carbonate to the ethanol is (9-16): 1.
3. The preparation method according to claim 1, wherein the mass of the concentrated sulfuric acid catalyst is 0.5-20% of the total mass of the raw materials.
4. The preparation method according to claim 1, wherein the heating speed in the pre-reaction kettle is 4-6 ℃/min, the reaction temperature is 50-90 ℃, the reaction time is 6-10h, and the operation pressure is 10-200 kPa.
5. The method according to claim 1, wherein the 1 to 6 reactive distillation columns are used in series.
6. The preparation method according to claim 1 or 5, wherein the operating pressure of the reactive distillation column is 0 to 50kPa, the reaction temperature is 80 to 100 ℃, and the reaction time is 9 to 11 hours.
7. The preparation method according to claim 1, wherein the reaction temperature of the rectification column I is 60-80 ℃, the pressure is 0-0.1MPa, and the retention time is 4-5 h.
8. The method of claim 1, wherein the dealcoholization column is operated at 80 to 100 ℃ and at 0.01 to 0.03 MPa.
9. The method according to claim 1, wherein the rectification column II is operated at normal pressure, the operation temperature is 80-120 ℃ and the operation time is 3-6 h.
10. The preparation method according to claim 1, wherein the operating temperature of the rectifying column III is 60-120 ℃, the operating pressure is-0.08-0 MPa, and the time is 3-6 h.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114835583A (en) * | 2022-05-31 | 2022-08-02 | 天津科技大学 | Process method for producing high-purity methyl ethyl carbonate and diethyl carbonate |
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| CN101381308A (en) * | 2008-10-22 | 2009-03-11 | 天津大学 | Preparation method of diethyl carbonate and methyl ethyl carbonate mixed ester |
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| CN107032998A (en) * | 2017-04-28 | 2017-08-11 | 山东海容电源材料股份有限公司 | A kind of methyl ethyl carbonate method for continuously synthesizing without catalyst |
| CN109503375A (en) * | 2018-12-06 | 2019-03-22 | 沈阳化工大学 | A kind of production technology for the heterogeneous catalysis methyl ethyl carbonate that is coupled |
| CN111773755A (en) * | 2020-07-16 | 2020-10-16 | 河北工业大学 | Method and device for preparing methyl ethyl carbonate by using bulkhead reaction rectifying tower |
| CN113354540A (en) * | 2021-07-26 | 2021-09-07 | 华东理工大学 | Method for efficiently and continuously preparing methyl ethyl carbonate |
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Patent Citations (6)
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| CN101381308A (en) * | 2008-10-22 | 2009-03-11 | 天津大学 | Preparation method of diethyl carbonate and methyl ethyl carbonate mixed ester |
| CN102134191A (en) * | 2010-12-22 | 2011-07-27 | 河北工业大学 | Process method for producing ethyl acetate by catalytic rectification |
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| CN109503375A (en) * | 2018-12-06 | 2019-03-22 | 沈阳化工大学 | A kind of production technology for the heterogeneous catalysis methyl ethyl carbonate that is coupled |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114835583A (en) * | 2022-05-31 | 2022-08-02 | 天津科技大学 | Process method for producing high-purity methyl ethyl carbonate and diethyl carbonate |
| CN114835583B (en) * | 2022-05-31 | 2024-05-10 | 天津科技大学 | Process method for producing high-purity methyl ethyl carbonate and diethyl carbonate |
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