CN115160122A - Novel process for preparing glycollic acid by hydrolyzing methyl glycolate - Google Patents
Novel process for preparing glycollic acid by hydrolyzing methyl glycolate Download PDFInfo
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- CN115160122A CN115160122A CN202211037900.4A CN202211037900A CN115160122A CN 115160122 A CN115160122 A CN 115160122A CN 202211037900 A CN202211037900 A CN 202211037900A CN 115160122 A CN115160122 A CN 115160122A
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- glycolic acid
- methyl glycolate
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- AEMRFAOFKBGASW-UHFFFAOYSA-N Glycolic acid Chemical compound OCC(O)=O AEMRFAOFKBGASW-UHFFFAOYSA-N 0.000 title claims abstract description 119
- JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 title claims abstract description 50
- 230000003301 hydrolyzing effect Effects 0.000 title claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 12
- 238000000605 extraction Methods 0.000 claims abstract description 9
- 239000003054 catalyst Substances 0.000 claims abstract description 8
- 238000003808 methanol extraction Methods 0.000 claims abstract description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 21
- 239000000463 material Substances 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 13
- 238000000066 reactive distillation Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 3
- 238000005844 autocatalytic reaction Methods 0.000 claims description 2
- 239000012295 chemical reaction liquid Substances 0.000 claims description 2
- 230000000694 effects Effects 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 238000010079 rubber tapping Methods 0.000 claims description 2
- 229910021642 ultra pure water Inorganic materials 0.000 claims description 2
- 239000012498 ultrapure water Substances 0.000 claims description 2
- 238000002156 mixing Methods 0.000 abstract description 12
- 230000007062 hydrolysis Effects 0.000 abstract description 8
- 239000011347 resin Substances 0.000 abstract description 5
- 229920005989 resin Polymers 0.000 abstract description 5
- 239000000047 product Substances 0.000 description 16
- 239000007864 aqueous solution Substances 0.000 description 10
- 239000000243 solution Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 3
- LOMVENUNSWAXEN-UHFFFAOYSA-N Methyl oxalate Chemical compound COC(=O)C(=O)OC LOMVENUNSWAXEN-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- 238000005903 acid hydrolysis reaction Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000006315 carbonylation Effects 0.000 description 1
- 238000005810 carbonylation reaction Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- FOCAUTSVDIKZOP-UHFFFAOYSA-N chloroacetic acid Chemical compound OC(=O)CCl FOCAUTSVDIKZOP-UHFFFAOYSA-N 0.000 description 1
- 229940106681 chloroacetic acid Drugs 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- LTYRAPJYLUPLCI-UHFFFAOYSA-N glycolonitrile Chemical compound OCC#N LTYRAPJYLUPLCI-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 235000006408 oxalic acid Nutrition 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002522 swelling effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/09—Preparation of carboxylic acids or their salts, halides or anhydrides from carboxylic acid esters or lactones
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a novel process for preparing glycolic acid by hydrolyzing methyl glycolate, which comprises a complete mixing flow reactor, a reaction rectifying tower and a condenser, wherein an outlet of the complete mixing flow reactor is connected with an inlet of the reaction rectifying tower, a methanol extraction outlet is arranged at the top of the reaction rectifying tower, the methanol extraction outlet and a gas phase extraction outlet are respectively provided with the condenser, a feed liquid discharge port is arranged at the bottom of the reaction rectifying tower, and the feed liquid discharge port is connected with the inlet of the complete mixing flow reactor by a bypass pipe. According to the invention, by utilizing the characteristic of strong acidity of glycolic acid, glycolic acid is adopted to directly catalyze the hydrolysis of methyl glycolate, and no catalyst is needed, so that the production cost is reduced, and the influence of the crushing of the traditional resin catalyst on the purity of glycolic acid products is avoided.
Description
Technical Field
The invention belongs to the technical field of chemical production, and particularly relates to a novel process for preparing glycollic acid by hydrolyzing methyl glycolate.
Background
Glycolic acid, also known as glycolic acid, is an important fine organic synthetic intermediate and chemical product, and has been listed as a national primary chemical product for development in the fifteen program. At present, glycolic acid is widely applied in the fields of chemical cleaning, daily chemical industry, new biodegradable materials and the like, and can also be used in the field of fine medicine synthesis. A detergent composition comprising 2% of glycolic acid and 1% of formic acid, which is highly efficient and low in cost.
The traditional industrial production method comprises the following steps: chloroacetic acid hydrolysis, hydroxyacetonitrile hydrolysis, formaldehyde carbonylation, oxalic acid electrolysis, etc., but these methods produce glycolic acid at high cost and are not competitive in the market. A large amount of dimethyl oxalate can be produced as a byproduct in the process of preparing ethylene glycol from coal, the dimethyl oxalate is catalyzed and hydrogenated to generate methyl glycolate, and then glycolic acid can be obtained through hydrolysis. Therefore, the market prospect of glycolic acid production by the coal chemical industry route is wide. Patent CN105085227A discloses a process for hydrolyzing methyl glycolate to obtain glycolic acid, firstly, performing hydrolysis reaction of methyl glycolate and water in a hydrolysis reactor, and rectifying and purifying the reaction solution to obtain glycolic acid product. Patent CN104177250A discloses a process for producing glycolic acid from methyl glycolate, which comprises adding methyl glycolate and water into a rectifying column by using resin catalysts (such as 001 × 7, D072, NKC-9, a15, etc.), carrying out reactive rectification to obtain a low-concentration glycolic acid aqueous solution, evaporating, concentrating, and decolorizing to obtain a glycolic acid product with 70 wt%. The process has a large molar ratio of water to ester (1. In addition, methyl glycolate may also have a swelling action on the resin catalyst, so that the resin active site functional groups are detached and finally remain in the glycolic acid product, and these impurities may affect the quality of the product although they are in a slight amount. And finally, the product is filtered and decolored by active carbon, and the steps are complicated.
Therefore, it is necessary to develop a novel process for producing glycolic acid by hydrolyzing methyl glycolate.
Disclosure of Invention
Aiming at the problems, the invention provides a novel process for preparing glycolic acid by hydrolyzing methyl glycolate, and provides a method combining autocatalysis and reactive rectification, which realizes the complete hydrolysis of methyl glycolate under the condition of low water ester feed ratio to obtain a glycolic acid product, so as to solve the problems provided by the background technology, wherein the reaction process is as follows:
in order to achieve the purpose, the invention provides the following technical scheme: a new process for preparing glycollic acid by hydrolyzing methyl glycolate comprises a full mixed flow reactor, a reaction rectifying tower and a condenser, and the specific operation comprises the following steps:
step A, fully mixed flow reaction: mixing methyl glycolate and ultrapure water in a ratio, feeding the mixture and feed liquid extracted from the tower bottom of a subsequent reaction rectifying tower into a total mixed flow reactor, and performing partial hydrolysis reaction on the methyl glycolate and water under the self-catalysis action of glycolic acid to generate glycolic acid and methanol;
and B, reactive distillation: the pre-reaction liquid extracted from the full mixed flow reactor is sent into a reaction rectifying tower, methyl glycolate is continuously hydrolyzed under the self-catalysis of glycolic acid in the reaction rectifying tower, the generated methanol is timely removed from the reaction section under the rectification action and extracted from the top of the tower, the material extracted from the bottom of the tower returns to the inlet of the full mixed flow reactor to be used as a catalyst for hydrolyzing the methyl glycolate, and the material extracted from the gas phase side at the lower part of the reaction rectifying tower is condensed by a condenser to be used as a product glycolic acid for extracting.
Further, a full mixed flow reactor is adopted in the step A, the reaction temperature is 80-90 ℃, and the reaction time is 45-90min.
Further, in the step A, the feeding molar ratio of water to methyl glycolate is 3-5, and the feeding volume ratio of the feed liquid returned from the tower bottom of the reactive distillation tower to the water-ester mixture is 1:2-8.
Furthermore, the reaction rectifying tower in the step B is sequentially divided into a rectifying section and a reaction section from top to bottom, wherein the number of theoretical plates of the rectifying section is 20-40, the number of theoretical plates of the reaction section is 30-60, the feed inlet is positioned between the rectifying section and the reaction section, and a gas phase extraction port is arranged at a position close to 3-5 theoretical plates of the tower kettle.
Furthermore, the vapor-liquid mass transfer element in the reactive distillation column is one or two of a filler and a tower plate.
Furthermore, the operating pressure of the reactive distillation tower is 35-45kPa, the reflux ratio is 3-5, and the gas phase side tapping temperature is 83-89.5 ℃.
Further, the material in the tower bottom in the step B is mainly glycolic acid.
Further, the outlet of the complete mixing flow reactor is connected with the inlet of the reaction rectifying tower, the top of the reaction rectifying tower is provided with a methanol extraction outlet, the methanol extraction outlet and the gas phase extraction outlet are both provided with condensers, the bottom of the reaction rectifying tower is provided with a material liquid discharge port, and the material liquid discharge port is connected with the inlet of the complete mixing flow reactor by a bypass pipe.
The invention has the technical effects and advantages that:
1. according to the invention, by utilizing the characteristic of strong acidity of glycolic acid, glycolic acid is adopted to directly catalyze the hydrolysis of methyl glycolate, and no catalyst is needed, so that the production cost is reduced, and the influence of the crushing of the traditional resin catalyst on the purity of glycolic acid products is avoided.
2. The invention combines hydrolysis reaction and reactive distillation technology, glycolic acid extracted from the tower bottom of the reactive distillation tower is sent to the full mixed flow reactor, and trace unreacted methyl glycolate remained in the tower bottom of the reactive distillation tower can also return to the full mixed flow hydrolysis reactor, thereby ensuring the complete hydrolysis of the methyl glycolate.
3. According to the invention, the glycolic acid product is obtained through the gas phase outlet at the lower section of the reaction rectifying tower, so that the problem that an additional activated carbon decoloring process is needed for obtaining the glycolic acid product in the traditional process because the glycolic acid product is yellow is avoided.
4. The method is obtained by adopting a gas phase side extraction mode for the glycolic acid product, avoids the pollution of micro high-boiling-point substances contained in the raw material methyl glycolate to the product, and the tower bottom of the reaction rectifying tower is provided with a regular material liquid discharge port, when the color of the material liquid in the tower bottom is deepened or the temperature of the tower bottom is higher than the normal temperature by 1-2 ℃, the discharge is started, so that the product quality is ensured, and the refining and purifying operation of the methyl glycolate raw material can be saved.
Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by the practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and drawings.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 shows a process flow diagram of an embodiment of the invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1:
mixing a methyl glycolate raw material and water in a molar ratio of 1:4, entering a full mixed flow reactor after mixing, sending glycolic acid feed liquid extracted from the tower bottom of the subsequent reaction rectifying tower into the full mixed flow reactor, wherein the volume ratio of the returned glycolic acid aqueous solution to the fed methyl glycolate aqueous solution is 1. The mass fraction of glycolic acid at the outlet of the total mixed flow reactor was 27.9%, and the conversion of methyl glycolate was 36%. The number of theoretical plates of the rectifying section of the reactive rectifying tower is 20, the number of theoretical plates of the reactive rectifying tower is 60, the 20 th tower plate is fed, the operating pressure of the rectifying tower is 45kPa, the reflux ratio is 4, the temperature of the top of the tower is 67.6 ℃, the temperature of a side extraction opening is 89.5 ℃, 57.5 percent of methanol aqueous solution is extracted from the top of the tower, the mass fraction of the glycolic acid extracted from a gas phase side is 71 percent, and the conversion rate of the methyl glycolate is 99.6 percent.
Example 2:
mixing a methyl glycolate raw material and water in a molar ratio of 1:3, entering a full mixed flow reactor after mixing, sending glycolic acid feed liquid extracted from the tower bottom of the subsequent reaction rectifying tower into the full mixed flow reactor, wherein the volume ratio of the returned glycolic acid aqueous solution to the fed methyl glycolate aqueous solution is 1. The mass fraction of glycolic acid at the outlet of the total mixed flow reactor was 26.4%, and the conversion of methyl glycolate was 29%. The number of theoretical plates of the rectifying section of the reactive rectifying tower is 20, the number of theoretical plates of the reactive rectifying tower is 60, the 20 th tower plate is fed, the operating pressure of the rectifying tower is 45kPa, the reflux ratio is 5, the temperature of the top of the tower is 57.3 ℃, the temperature of a side extraction opening is 89.5 ℃, 81.9 percent of methanol aqueous solution is extracted from the top of the tower, the mass fraction of the glycolic acid extracted from a gas phase side is 72 percent, and the conversion rate of the methyl glycolate is 99.5 percent.
Example 3:
mixing a methyl glycolate raw material and water in a molar ratio of 1:5, mixing, then feeding the mixture into a full mixed flow reactor, feeding glycolic acid feed liquid extracted from the tower bottom of a subsequent reaction rectifying tower into the full mixed flow reactor, wherein the volume ratio of the returned glycolic acid aqueous solution to the fed methyl glycolate aqueous solution is 1. The mass fraction of glycolic acid at the outlet of the total mixed flow reactor was 28.6%, and the conversion of methyl glycolate was 36.2%. 15 theoretical plates are arranged on the rectification section of the reactive rectification tower, 40 theoretical plates are arranged on the reaction section, the 15 th tower plate is fed, the operating pressure of the rectification tower is 40kPa, the reflux ratio is 4, the temperature of the top of the tower is 67.8 ℃, the temperature of a side extraction port is 87.2 ℃, 42.6 percent of methanol aqueous solution is extracted from the top of the tower, the mass fraction of glycolic acid extracted from a gas phase side is 72 percent, and the conversion rate of methyl glycolate is 99.7 percent.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (8)
1. A new process for preparing glycollic acid by hydrolyzing methyl glycolate is characterized in that: the method comprises a full mixed flow reactor, a reaction rectifying tower and a condenser, and the specific operation comprises the following steps:
step A, fully mixed flow reaction: after being mixed in proportion, the methyl glycolate and the ultrapure water enter a full mixed flow reactor together with feed liquid extracted from a subsequent reaction rectifying tower kettle, and the methyl glycolate and the water undergo partial hydrolysis reaction under the autocatalysis effect of the glycolic acid to generate glycolic acid and methanol;
and B, reactive distillation: the pre-reaction liquid extracted from the full mixed flow reactor is sent into a reaction rectifying tower, methyl glycolate is continuously hydrolyzed under the self-catalysis of glycolic acid in the reaction rectifying tower, the generated methanol is timely removed from the reaction section under the rectification action and extracted from the top of the tower, the material extracted from the bottom of the tower returns to the inlet of the full mixed flow reactor to be used as a catalyst for hydrolyzing the methyl glycolate, and the material extracted from the gas phase side at the lower part of the reaction rectifying tower is condensed by a condenser to be used as a product glycolic acid for extracting.
2. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 1, characterized in that: in the step A, a full mixed flow reactor is adopted, the reaction temperature is 80-90 ℃, and the reaction time is 45-90min.
3. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 1, characterized in that: in the step A, the feeding molar ratio of water to methyl glycolate is 3-5, and the feeding volume ratio of feed liquid returned from the tower bottom of the reactive distillation tower to the water-ester mixture is 1:2-8.
4. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 1, characterized in that: and in the step B, the reaction rectifying tower is sequentially divided into a rectifying section and a reaction section from top to bottom, wherein the number of theoretical plates of the rectifying section is 20-40, the number of theoretical plates of the reaction section is 30-60, the feed inlet is positioned between the rectifying section and the reaction section, and a gas phase extraction outlet is arranged at a position close to 3-5 theoretical plates of the tower kettle.
5. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 4, characterized in that: the vapor-liquid mass transfer element in the reactive distillation column is one or two of a filler and a tower plate.
6. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 4, wherein: the operating pressure of the reactive distillation tower is 35-45kPa, the reflux ratio is 3-5, and the gas-phase side tapping temperature is 83-89.5 ℃.
7. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 1, characterized in that: and the material in the tower bottom in the step B is mainly glycolic acid.
8. The new process for preparing glycolic acid by hydrolyzing methyl glycolate according to claim 4, wherein: the outlet of the full mixed-flow reactor is connected with the inlet of the reaction rectifying tower, the top of the reaction rectifying tower is provided with a methanol extraction outlet, the methanol extraction outlet and the gas phase extraction outlet are respectively provided with a condenser, the bottom of the reaction rectifying tower is provided with a material liquid discharge outlet, and the material liquid discharge outlet is connected with the inlet of the full mixed-flow reactor by a bypass pipe.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211037900.4A CN115160122A (en) | 2022-08-26 | 2022-08-26 | Novel process for preparing glycollic acid by hydrolyzing methyl glycolate |
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| CN202211037900.4A CN115160122A (en) | 2022-08-26 | 2022-08-26 | Novel process for preparing glycollic acid by hydrolyzing methyl glycolate |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1066442A (en) * | 1992-05-25 | 1992-11-25 | 济南石油化工二厂 | Novel process with preparing aminic acid by methyl formate hydrolysis |
| CN103508878A (en) * | 2012-06-27 | 2014-01-15 | 上海浦景化工技术有限公司 | Method for preparing high-purity glycolic acid crystals from methyl glycolate |
| CN104177250A (en) * | 2014-09-16 | 2014-12-03 | 上海华谊（集团）公司 | Process for producing glycollic acid from methyl glycolate |
| CN104829445A (en) * | 2015-05-04 | 2015-08-12 | 上海华谊（集团）公司 | Method for producing aqueous solution of glycolic acid |
| CN104892389A (en) * | 2015-06-02 | 2015-09-09 | 福州大学 | Technique for preparing oxalic acid by performing continuous reaction rectification hydrolysis on dimethyl oxalate |
| US20190248724A1 (en) * | 2016-09-16 | 2019-08-15 | Johnson Matthey Davy Technologies Limited | Process for the production of glycolic acid |
-
2022
- 2022-08-26 CN CN202211037900.4A patent/CN115160122A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1066442A (en) * | 1992-05-25 | 1992-11-25 | 济南石油化工二厂 | Novel process with preparing aminic acid by methyl formate hydrolysis |
| CN103508878A (en) * | 2012-06-27 | 2014-01-15 | 上海浦景化工技术有限公司 | Method for preparing high-purity glycolic acid crystals from methyl glycolate |
| CN104177250A (en) * | 2014-09-16 | 2014-12-03 | 上海华谊（集团）公司 | Process for producing glycollic acid from methyl glycolate |
| CN104829445A (en) * | 2015-05-04 | 2015-08-12 | 上海华谊（集团）公司 | Method for producing aqueous solution of glycolic acid |
| CN104892389A (en) * | 2015-06-02 | 2015-09-09 | 福州大学 | Technique for preparing oxalic acid by performing continuous reaction rectification hydrolysis on dimethyl oxalate |
| US20190248724A1 (en) * | 2016-09-16 | 2019-08-15 | Johnson Matthey Davy Technologies Limited | Process for the production of glycolic acid |
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