WO2022165662A1 - 甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 - Google Patents
甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 Download PDFInfo
- Publication number
- WO2022165662A1 WO2022165662A1 PCT/CN2021/075023 CN2021075023W WO2022165662A1 WO 2022165662 A1 WO2022165662 A1 WO 2022165662A1 CN 2021075023 W CN2021075023 W CN 2021075023W WO 2022165662 A1 WO2022165662 A1 WO 2022165662A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- acidic
- catalyst
- molecular sieve
- acid
- methyl
- Prior art date
Links
- AEMRFAOFKBGASW-UHFFFAOYSA-N Glycolic acid Chemical compound OCC(O)=O AEMRFAOFKBGASW-UHFFFAOYSA-N 0.000 title claims abstract description 77
- RMIODHQZRUFFFF-UHFFFAOYSA-N methoxyacetic acid Chemical compound COCC(O)=O RMIODHQZRUFFFF-UHFFFAOYSA-N 0.000 title claims abstract description 63
- ICPWFHKNYYRBSZ-UHFFFAOYSA-M 2-methoxypropanoate Chemical compound COC(C)C([O-])=O ICPWFHKNYYRBSZ-UHFFFAOYSA-M 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 53
- JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 title claims abstract description 30
- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 23
- 230000007062 hydrolysis Effects 0.000 title claims abstract description 17
- 239000003054 catalyst Substances 0.000 claims abstract description 104
- 238000006243 chemical reaction Methods 0.000 claims abstract description 78
- 239000002994 raw material Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 230000003197 catalytic effect Effects 0.000 claims abstract description 15
- 239000003377 acid catalyst Substances 0.000 claims abstract description 13
- 239000011973 solid acid Substances 0.000 claims abstract description 8
- 239000007787 solid Substances 0.000 claims abstract description 7
- 230000002378 acidificating effect Effects 0.000 claims description 114
- 239000002808 molecular sieve Substances 0.000 claims description 105
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 105
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000007864 aqueous solution Substances 0.000 claims description 12
- 239000002585 base Substances 0.000 claims description 10
- 239000011347 resin Substances 0.000 claims description 10
- 229920005989 resin Polymers 0.000 claims description 10
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 9
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 8
- 239000003729 cation exchange resin Substances 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- -1 hydrogen ions Chemical class 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 claims description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 6
- 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 claims description 6
- 229910001701 hydrotalcite Inorganic materials 0.000 claims description 6
- 229960001545 hydrotalcite Drugs 0.000 claims description 6
- 229910052588 hydroxylapatite Inorganic materials 0.000 claims description 6
- XYJRXVWERLGGKC-UHFFFAOYSA-D pentacalcium;hydroxide;triphosphate Chemical compound [OH-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O XYJRXVWERLGGKC-UHFFFAOYSA-D 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 229910052680 mordenite Inorganic materials 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 230000008929 regeneration Effects 0.000 claims description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 3
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 claims description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 239000003957 anion exchange resin Substances 0.000 claims description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 229920001577 copolymer Polymers 0.000 claims description 3
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 3
- 239000000347 magnesium hydroxide Substances 0.000 claims description 3
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 3
- 229910017604 nitric acid Inorganic materials 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 229910052814 silicon oxide Inorganic materials 0.000 claims description 3
- 125000000542 sulfonic acid group Chemical group 0.000 claims description 3
- 229940023913 cation exchange resins Drugs 0.000 claims description 2
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 2
- 239000011261 inert gas Substances 0.000 claims description 2
- 229910021536 Zeolite Inorganic materials 0.000 claims 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims 1
- 238000002156 mixing Methods 0.000 claims 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims 1
- 239000010457 zeolite Substances 0.000 claims 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 16
- NKDDWNXOKDWJAK-UHFFFAOYSA-N dimethoxymethane Chemical compound COCOC NKDDWNXOKDWJAK-UHFFFAOYSA-N 0.000 abstract description 13
- 238000005810 carbonylation reaction Methods 0.000 abstract description 10
- 230000006315 carbonylation Effects 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 239000000126 substance Substances 0.000 abstract description 7
- 239000003245 coal Substances 0.000 abstract description 5
- 238000009833 condensation Methods 0.000 abstract description 2
- 230000005494 condensation Effects 0.000 abstract description 2
- 238000010924 continuous production Methods 0.000 abstract description 2
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 abstract 1
- 229960004275 glycolic acid Drugs 0.000 description 31
- 239000000047 product Substances 0.000 description 18
- 229910052799 carbon Inorganic materials 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 9
- 238000006555 catalytic reaction Methods 0.000 description 7
- RMIODHQZRUFFFF-UHFFFAOYSA-M methoxyacetate Chemical compound COCC([O-])=O RMIODHQZRUFFFF-UHFFFAOYSA-M 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 5
- 229920000954 Polyglycolide Polymers 0.000 description 4
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 239000004633 polyglycolic acid Substances 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- FOCAUTSVDIKZOP-UHFFFAOYSA-N chloroacetic acid Chemical compound OC(=O)CCl FOCAUTSVDIKZOP-UHFFFAOYSA-N 0.000 description 3
- 229940106681 chloroacetic acid Drugs 0.000 description 3
- 150000002148 esters Chemical class 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- ICPWFHKNYYRBSZ-UHFFFAOYSA-N 2-methoxypropanoic acid Chemical compound COC(C)C(O)=O ICPWFHKNYYRBSZ-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000005903 acid hydrolysis reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
- 238000004811 liquid chromatography Methods 0.000 description 2
- 238000004895 liquid chromatography mass spectrometry Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 238000007493 shaping process Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- ALRHLSYJTWAHJZ-UHFFFAOYSA-N 3-hydroxypropionic acid Chemical compound OCCC(O)=O ALRHLSYJTWAHJZ-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 229910014497 Ca10(PO4)6(OH)2 Inorganic materials 0.000 description 1
- FHKPLLOSJHHKNU-INIZCTEOSA-N [(3S)-3-[8-(1-ethyl-5-methylpyrazol-4-yl)-9-methylpurin-6-yl]oxypyrrolidin-1-yl]-(oxan-4-yl)methanone Chemical compound C(C)N1N=CC(=C1C)C=1N(C2=NC=NC(=C2N=1)O[C@@H]1CN(CC1)C(=O)C1CCOCC1)C FHKPLLOSJHHKNU-INIZCTEOSA-N 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 229920006238 degradable plastic Polymers 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000004310 lactic acid Substances 0.000 description 1
- 235000014655 lactic acid Nutrition 0.000 description 1
- 238000003760 magnetic stirring Methods 0.000 description 1
- 238000004949 mass spectrometry Methods 0.000 description 1
- 238000001819 mass spectrum Methods 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Natural products C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 125000001453 quaternary ammonium group Chemical group 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000002407 tissue scaffold Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/347—Preparation of carboxylic acids or their salts, halides or anhydrides by reactions not involving formation of carboxyl groups
- C07C51/377—Preparation of carboxylic acids or their salts, halides or anhydrides by reactions not involving formation of carboxyl groups by splitting-off hydrogen or functional groups; by hydrogenolysis of functional groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/30—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group
- C07C67/31—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by introduction of functional groups containing oxygen only in singly bound form
Definitions
- the application relates to a method for preparing glycolic acid and methyl glycolate by hydrolysis of methyl methoxyacetate and methoxyacetic acid, and belongs to the technical field of chemical product preparation.
- Glycolic acid also known as hydroxyacetic acid
- Methyl glycolate can not only be hydrogenated to produce ethylene glycol, but also easily hydrolyzed to produce glycolic acid under mild conditions. Because the molecular structure of glycolic acid contains both hydroxyl and carboxyl groups, it can polymerize itself to form polyglycolic acid (PGA).
- PGA polyglycolic acid
- Polyglycolic acid not only has good biocompatibility, but also has safe biodegradability. Therefore, it is not only widely used in medical surgical sutures, drug release materials, degradable human tissue scaffolds, etc., but also can produce commonly used plastic products.
- Glycolic acid can also be copolymerized with lactic acid, hydroxypropionic acid and other monomers to form polymer materials with excellent performance and wide application.
- glycolic acid is also an excellent chemical cleaning agent and cosmetic raw material.
- the production and preparation methods of glycolic acid mainly include chloroacetic acid hydrolysis method, formaldehyde carbonylation method, oxalate ester hydrogenation/hydrolysis method, etc.
- Chloroacetic acid hydrolysis method is not only polluted in the preparation process of raw material chloroacetic acid, but also produces a large amount of waste salt in the hydrolysis process, causing serious pollution and poor product quality, which is basically eliminated at present.
- the formaldehyde carbonylation method although the raw materials are cheap and easy to obtain, needs to be carried out under the conditions of high temperature, high pressure, strong liquid acid, and organic solvent; the equipment is easy to corrode, and the product purification is difficult, resulting in high industrial production costs.
- the oxalate hydrogenation/hydrolysis method is to partially hydrogenate the oxalate to methyl glycolate, and then hydrolyze the methyl glycolate to produce glycolic acid.
- the oxalate partial hydrogenation catalyst is immature, with low conversion efficiency and poor stability; on the other hand, the oxalate production process is long and the cost is high; these problems seriously restrict the application of the oxalate hydrogenation/hydrolysis method. develop.
- methyl methoxyacetate a product of methylal carbonylation
- the methoxyacetic acid after the hydrolysis of the ester bond of methyl methoxyacetate has relatively few uses, resulting in waste of raw materials.
- a method for preparing glycolic acid and methyl glycolate by hydrolysis of methyl methoxyacetate and methoxyacetic acid is provided, and the method of the present invention is particularly suitable for the methylal produced by coal chemical industry.
- the carbonylation reaction produces methyl methoxyacetate, which is then hydrolyzed to produce glycolic acid and methyl glycolate. Through this reaction process, it can be combined with the carbonylation of methylal to produce methyl methoxyacetate, and the methylal in the coal chemical platform can be converted into glycolic acid and methyl glycolate efficiently, greenly and economically.
- the use of methoxyacetate and methoxyacetic acid has been achieved, and beneficial effects have been achieved.
- the catalyst is selected from any of a solid acid catalyst, a liquid acid catalyst, a solid base catalyst, and a liquid base catalyst.
- glycolic acid, methyl glycolate and methoxyacetic acid can be obtained by hydrolysis of ether bond and ester bond of methyl methoxyacetate. Because methoxyacetic acid has relatively few uses, it can be returned to the reactor for co-hydrolysis with methyl methoxyacetate, which becomes a green and economical production route for glycolic acid and methyl glycolate.
- the solid acid catalyst is selected from at least one of an acidic molecular sieve catalyst, an acidic resin catalyst, and an acidic alumina catalyst;
- the acidic molecular sieve catalyst contains acidic molecular sieve.
- the acidic molecular sieve is selected from at least one of acidic MFI structural molecular sieves, acidic FAU structural molecular sieves, acidic FER structural molecular sieves, acidic BEA structural molecular sieves, acidic MOR structural molecular sieves, and acidic MWW structural molecular sieves.
- the acidic molecular sieve is selected from any one of acidic MFI molecular sieves and acidic FER structural molecular sieves.
- the acidic molecular sieve is selected from at least one of acidic ZSM-5 molecular sieves, acidic Y molecular sieves, acidic ZSM-35 molecular sieves, acidic beta molecular sieves, acidic mordenite molecular sieves, and acidic MCM-22 molecular sieves.
- the acidic molecular sieve is at least one of acidic ZSM-5 molecular sieve and acidic ZSM-35 molecular sieve.
- the acidic molecular sieve is selected from at least one of hydrogen-type ZSM-5 molecular sieve, hydrogen-type Y molecular sieve, hydrogen-type ZSM-35 molecular sieve, hydrogen-type beta molecular sieve, hydrogen-type mordenite molecular sieve, and hydrogen-type MCM-22 molecular sieve. kind.
- the acidic molecular sieve is at least one of hydrogen type ZSM-5 molecular sieve and hydrogen type ZSM-35 molecular sieve.
- the Si/Al atomic ratio Si/Al in the acidic molecular sieve is 3-500.
- the upper limit of the silicon-aluminum atomic ratio in the acidic molecular sieve is selected from 20, 10, 50, 100, 500; the lower limit of the silicon-aluminum atomic ratio in the acidic molecular sieve is selected from 3, 10, 20, 50, 100 .
- the Si/Al atomic ratio Si/Al in the acidic molecular sieve is 20-500.
- the content of the acidic molecular sieve in the acidic molecular sieve catalyst is 50-100 wt %.
- the acidic molecular sieve catalyst further contains a forming agent; the forming agent is an oxide; the oxide is selected from one of alumina and silicon oxide.
- the content of the forming agent in the acidic molecular sieve catalyst is m, and the value range of m is 0 ⁇ m ⁇ 50wt%.
- the acidic molecular sieve catalyst is a fresh acidic molecular sieve catalyst and/or a regenerated acidic molecular sieve catalyst; the fresh acidic molecular sieve catalyst is an unused acidic molecular sieve catalyst.
- the method for regenerating the acidic molecular sieve catalyst comprises: treating the deactivated acidic molecular sieve catalyst with a regeneration gas containing oxygen at 400-800° C. for 0.5-24 hours, so as to obtain the regenerated acidic molecular sieve catalyst;
- the volume fraction of oxygen is 0.5-50%.
- the acidic resin catalyst is selected from any one of strongly acidic cation exchange resins.
- the skeleton structure in the strongly acidic cation exchange resin is a copolymer of styrene and divinylbenzene;
- the acidic group in the strongly acidic cation exchange resin is a sulfonic acid group.
- the acidic alumina catalyst is ⁇ -structure alumina.
- the liquid acid catalyst is selected from any of acidic liquids.
- the liquid acid catalyst is selected from at least one of sulfuric acid, hydrochloric acid, nitric acid, and phosphoric acid.
- the concentration of hydrogen ions H + contained in the liquid acid catalyst is 0.01-10 mol/L.
- the solid base catalyst is selected from at least one selected from hydrotalcite, anion exchange resin, and hydroxyapatite.
- the liquid base catalyst is selected from any one of liquids with basicity.
- the liquid alkali catalyst is selected from any one of sodium hydroxide aqueous solution, potassium hydroxide aqueous solution, calcium hydroxide aqueous solution, and magnesium hydroxide aqueous solution.
- the concentration of hydroxide ions OH - contained in the liquid alkali catalyst is 0.01-10 mol/L.
- the conditions of the reaction are:
- the reaction pressure is 0.1 ⁇ 10MPa
- methyl methoxyacetate and methoxyacetic acid are not limited.
- the upper limit of the reaction temperature is selected from 130°C, 160°C, 200°C, and 260°C; the lower limit of the reaction temperature is selected from 60°C, 130°C, 160°C, and 200°C.
- the upper limit of the reaction pressure is selected from 0.3 MPa, 1 MPa, 5 MPa, and 10 MPa; the lower limit of the reaction pressure is selected from 0.1 MPa, 0.3 MPa, 1 MPa, and 5 MPa.
- the upper limit of the ratio of the total moles of methyl methoxyacetate and methoxyacetic acid to the moles of water is selected from 1:3, 1:6, 1:8, 1:10, 1:15, 1:20;
- the lower limit of the ratio of the total moles of methyl methoxyacetate and methoxyacetic acid to the moles of water is selected from 1:2, 1:3, 1:6, 1:8, 1:10, 1:15.
- the conditions of the reaction are:
- the reaction pressure is 0.1 ⁇ 0.3MPa
- the molar ratio of the methyl methoxyacetate to the methoxyacetic acid is 4:1 to 9:1.
- the upper limit of the molar ratio of methyl methoxyacetate to methoxyacetic acid is selected from 5:1 and 9:1; the lower limit of the molar ratio of methyl methoxyacetate to methoxyacetic acid is selected from 4:1 , 5:1.
- the reaction is carried out in a reactor
- the reactor is selected from any one of a fixed bed reactor, a tank reactor, and a catalytic rectification reactor.
- the reactor comprises a fixed bed reactor, or a plurality of fixed bed reactors connected in series and/or parallel; or,
- the reactor comprises one tank reactor, or a plurality of tank reactors connected in series and/or in parallel; or,
- the reactor includes one catalytic rectification reactor, or a plurality of catalytic rectification reactors connected in series and/or in parallel.
- the mass space velocity of methyl methoxyacetate and methoxyacetic acid in the raw material is 0.1-3 h -1 .
- the upper limit of the mass space velocity of methyl methoxyacetate and methoxyacetic acid is 0.6h -1 , 1h -1 , 3h -1 ; the upper limit of the mass space velocity of methyl methoxyacetate and methoxyacetic acid is The lower limit is 0.1h -1 , 0.6h -1 , 1h -1 .
- the stirring rate is 250-350 rpm; the reaction time is 1-3 days.
- the reaction time is 8-15 h; the stirring speed is 350-650 rpm; and the reflux ratio is 1-3.
- the methyl methoxyacetate in the raw material is newly added raw material and/or unreacted methyl methoxyacetate after product separation; and/or,
- the methoxyacetic acid in the described raw material is the newly added raw material and/or the unreacted methoxyacetic acid after product separation; and/or,
- the water in the raw material is newly added raw material and/or unreacted water after product separation.
- methyl methoxyacetate, methoxyacetic acid and water in the raw materials are newly added raw materials and/or unreacted materials after product separation.
- reaction is carried out in an inert atmosphere
- the inert atmosphere includes any one of nitrogen gas and inert gas.
- the method for producing glycolic acid and methyl glycolate in the present invention can be realized by using a traditional fixed bed reactor, a kettle type reactor or a catalytic rectification reactor under normal pressure, and is very suitable for continuous production.
- the method in the present invention is combined with methanol and formaldehyde condensation to prepare methylal reaction, and methylal carbonylation to prepare methyl methoxyacetate reaction, so that methanol, which is a coal chemical industry platform, can be efficiently, greenly and economically converted into Glycolic acid and methyl glycolate.
- FIG. 1 is a mass spectrum diagram of glycolic acid anion in the reaction product analyzed by liquid chromatography-mass spectrometry in Example 1 of the application.
- the present invention develops a method for preparing glycolic acid and methyl glycolate by hydrolysis of methoxyacetate and methoxyacetic acid. Moreover, the method of the invention is especially suitable for methylal produced by coal chemical industry, and methyl methoxyacetate is generated through carbonylation reaction, and then glycolic acid and methyl glycolate are prepared by hydrolysis.
- the present invention provides a method for preparing glycolic acid and methyl glycolate by hydrolysis of methoxyacetate and methoxyacetic acid.
- the raw materials methoxyacetate, methoxyacetic acid and water are passed through
- the reaction zone carrying the catalyst is reacted to produce glycolic acid and methyl glycolate under certain reaction conditions;
- the catalyst is any one or a mixture of a solid acid catalyst, a liquid acid catalyst, a solid base catalyst and a liquid base catalyst;
- the reaction zone contains one fixed bed reactor, or multiple fixed bed reactors connected in series and/or parallel, or one tank reactor, or multiple tank reactors connected in series and/or parallel
- a reactor either containing one catalytic rectification reactor, or a plurality of catalytic rectification reactors connected in series and/or in parallel;
- reaction conditions are as follows: the reaction temperature is 60-260° C., the molar ratio (methyl methoxyacetate+methoxyacetic acid) in the raw material: water is 1:20 ⁇ 1:2, and the molar ratio in the raw material is methyl methoxyacetic acid.
- Ester:Methoxyacetic acid is in any ratio, and the reaction pressure is 0.1-10MPa.
- the methoxyacetic acid in the reaction (3) continues to be hydrolyzed to generate glycolic acid under the same catalyst and reaction conditions:
- the solid acid catalyst is one or a mixture of an acidic molecular sieve catalyst, an acidic resin catalyst or an acidic alumina catalyst.
- the acidic molecular sieve-containing catalyst also contains 0-50% by weight of a catalyst shaping agent, and the catalyst shaping agent is one of alumina and silicon oxide.
- the acidic molecular sieve-containing catalyst is a freshly prepared acidic molecular sieve catalyst and/or a regenerated acidic molecular sieve catalyst.
- the preparation method of the regenerated acidic molecular sieve catalyst is as follows: the acidic molecular sieve catalyst after the deactivation of the hydrolysis reaction of methoxyacetate and methoxyacetic acid is used, and the gas containing 0.5-50% volume fraction of oxygen is used at 400 ⁇ 800°C for 0.5 ⁇ 24h.
- the acidic resin catalyst is a strongly acidic cation exchange resin.
- the skeleton structure of the strongly acidic cation exchange resin is a copolymer of styrene and divinylbenzene, and the acidic group is a sulfonic acid group.
- the acidic alumina catalyst is ⁇ -structure alumina.
- the ⁇ -structure alumina is prepared by calcining SB powder at 400-800°C.
- the liquid acid catalyst is an acidic liquid.
- the liquid acid catalyst is one or more of sulfuric acid, hydrochloric acid, nitric acid and phosphoric acid.
- the concentration of hydrogen ions H + contained in the liquid acid catalyst is 0.01-10 mol/L.
- the solid base catalyst is one or more of hydrotalcite, anion exchange resin and hydroxyapatite.
- composition of the hydrotalcite can be expressed as [Mg 1-x Al x (OH) 2 ] x+ [CO 3 2- ] x/2 ⁇ n H 2 O, the value of x is 0.1-0.34, and the value of n is 0- An integer of 4.
- Mg can be isomorphically substituted by Zn, Fe, Co, Ni and Cu, while Al can be substituted by Cr, Fe, In.
- the hydroxyapatite composition can be represented as Ca 10-x (HPO 4 ) x (PO 4 ) 6-x (OH) 2-x , and the value of x is 0-1.
- the liquid alkali catalyst is an alkaline liquid.
- the liquid alkali catalyst is one or more of sodium hydroxide aqueous solution, potassium hydroxide aqueous solution, calcium hydroxide aqueous solution and magnesium hydroxide aqueous solution.
- the concentration of hydroxide ions OH - contained in the liquid alkali catalyst is 0.01-10 mol/L.
- the reaction conditions are as follows: the reaction temperature is 130-200° C., the molar ratio (methyl methoxyacetate+methoxyacetic acid) in the raw material: water is 1:8 to 1:3, and the molar ratio in the raw material is methyl methoxyacetic acid.
- the ratio of ester:methoxyacetic acid is 4:1 ⁇ 9:1, and the reaction pressure is 0.1 ⁇ 0.3MPa.
- the mass space velocity of methyl methoxyacetate and methoxyacetic acid in the raw material is 0.1-3h ⁇ 1 .
- the raw materials methoxyacetate, methoxyacetic acid and water are newly added raw materials and/or unreacted raw materials after product separation.
- the raw material contains one of nitrogen and argon inert carrier gases in the process of passing through the reaction zone carrying the acidic molecular sieve catalyst.
- Agilent7890B gas chromatograph to analyze products other than glycolic acid and unreacted raw materials. Its FID detector is connected to DB-FFAP capillary column, and its TCD detector is connected to Porapak Q packed column. Glycolic acid was analyzed by liquid chromatography, the separation column was a C 18 column, and the detector was an ultraviolet detector.
- conversion and selectivity are calculated based on the number of moles of carbon:
- Conversion rate of methoxyacetic acid [(carbon moles of methoxyacetic acid in feed)-(carbon moles of methoxyacetic acid in discharge)] ⁇ (carbon moles of methoxyacetic acid in feed) ⁇ 100%
- the acidic molecular sieve catalyst especially the H-ZSM-5 molecular sieve catalyst, has high raw material conversion rate and long life in the hydrolysis reaction.
- Example 1 The catalyst in Example 1 was replaced with a DB757 strongly acidic sulfonic acid-based exchange resin commercially purchased by Dandong Pearl Company with an exchange degree of 3.2 mmol/g, and activated with 50 mL/min nitrogen at 100 ° C for 4 h. Other conditions were the same as the operation.
- the reaction results are shown in Table 3.
- Example 10 The catalyst in Example 10 was replaced with ⁇ -alumina whose ammonia adsorption capacity was 0.29 mmol/g purchased by Beijing Yanxin Technology Company, and other operating conditions were the same as those in Example 10, and the reaction results were shown in Table 3.
- Example 10 The catalyst in Example 10 was replaced with a 202FC type strongly basic quaternary ammonium-based exchange resin with an exchange degree of 3.5 mmol/g purchased from Dandong Pearl Company, and other operating conditions were the same as in Example 10, and the reaction results were shown in Table 3.
- Example 10 The catalyst in Example 10 was replaced with a composition of [Mg 0.8 Al 0.2 (OH) 2 ] 0.2+ [CO 3 2- ] 0.1 2H 2 O hydrotalcite, other operating conditions were the same as those in Example 10, and the reaction results were shown in the table 3.
- Example 10 The catalyst in Example 10 was replaced with a composition of Ca 10 (PO 4 ) 6 (OH) 2 hydroxyapatite, and other operating conditions were the same as those in Example 10. The reaction results are shown in Table 3.
- solid acids such as strongly acidic resin, ⁇ -alumina, basic resin, hydrotalcite, hydroxyapatite, etc., can also catalyze the hydrolysis of methyl methoxyacetate and methoxyacetic acid to produce ethanol.
- the acid reacts with methyl glycolate.
- the liquid acid can also catalyze the reaction of methyl methoxyacetate and methoxyacetic acid to hydrolyze glycolic acid and methyl glycolate.
- the hydrolysis reaction of methyl methoxyacetate and methoxyacetic acid was tested by batch catalytic distillation.
- the column body of the rectification tower is a glass column with a diameter of 30mm, and an inert annular packing with a size of 3.0mm ⁇ 3.0mm is installed inside, and the height of the packing is 2.0m.
- the distillation still is heated by a heating jacket, and the temperature of the top condenser is -15°C.
- the reaction temperature was 150° C.
- the reaction pressure was 0.1 MPa
- the magnetic stirring speed was 500 rpm
- the reflux ratio was 2.
- the conversion rates of methyl methoxyacetate and methoxyacetic acid were both about 100%
- the selectivity of glycolic acid was 43.5%
- the selectivity of methyl glycolate was 13.0%.
- the reacted catalyst can be basically restored to the reaction performance of the fresh catalyst after being calcined and regenerated in a mixed atmosphere of oxygen/nitrogen.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
Abstract
Description
Claims (30)
- 一种甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法,其特征在于,包括将含有甲氧基乙酸甲酯、甲氧基乙酸和水的原料,与催化剂接触、反应,即可得到乙醇酸和乙醇酸甲酯;所述催化剂选自固体酸催化剂、液体酸催化剂、固体碱催化剂、液体碱催化剂中的任一种。
- 根据权利要求1所述的方法,其特征在于,所述固体酸催化剂选自酸性分子筛催化剂、酸性树脂催化剂、酸性氧化铝催化剂中的至少一种;其中,所述酸性分子筛催化剂中含有酸性分子筛。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛选自酸性MFI结构分子筛、酸性FAU结构分子筛、酸性FER结构分子筛、酸性BEA结构分子筛、酸性MOR结构分子筛、酸性MWW结构分子筛中的至少一种。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛选自酸性ZSM-5分子筛、酸性Y分子筛、酸性ZSM-35分子筛、酸性β分子筛、酸性丝光沸石分子筛、酸性MCM-22分子筛中的至少一种。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛选自氢型ZSM-5分子筛、氢型Y分子筛、氢型ZSM-35分子筛、氢型β分子筛、氢型丝光沸石分子筛、氢型MCM-22分子筛中的至少一种。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛中的硅铝原子比Si/Al为3~500。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛在所述酸性分子筛催化剂中的含量为50~100wt%。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛催化剂中还含有成型剂;所述成型剂为氧化物;所述氧化物选自氧化铝、氧化硅中的一种。
- 根据权利要求8所述的方法,其特征在于,所述成型剂在所述酸性分子筛催化剂中的含量为m,m的取值范围为0<m≤50wt%。
- 根据权利要求2所述的方法,其特征在于,所述酸性分子筛催化剂为新鲜的酸性分子筛催化剂和/或再生后的酸性分子筛催化剂;所述新鲜的酸性分子筛催化剂为未使用过的酸性分子筛催化剂。
- 根据权利要求10所述的方法,其特征在于,所述酸性分子筛催化剂的再生方法包括:将失活的酸性分子筛催化剂,利用含氧气的再生气,在400~800℃下处理0.5~24h,即可得到再生后的酸性分子筛催化剂;其中,在所述再生气中,氧气的体积分数为0.5~50%。
- 根据权利要求2所述的方法,其特征在于,酸性树脂催化剂选自强酸性阳离子交换树脂中的任一种。
- 根据权利要求12所述的方法,其特征在于,所述强酸性阳离子交换树脂中的骨架结构为苯乙烯与二乙烯苯的共聚物;所述强酸性阳离子交换树脂中的酸性基团为磺酸基。
- 根据权利要求2所述的方法,其特征在于,所述酸性氧化铝催化剂为γ结构氧化铝。
- 根据权利要求1所述的方法,其特征在于,所述液体酸催化剂选自具有酸性的液体中的任一种。
- 根据权利要求15所述的方法,其特征在于,所述液体酸催化剂选自硫酸、盐酸、硝酸、磷酸中的至少一种。
- 根据权利要求15所述的方法,其特征在于,所述液体酸催化剂中含有氢离子H +的浓度为0.01~10mol/L。
- 根据权利要求1所述的方法,其特征在于,所述固体碱催化剂选自选自水滑石、阴离子交换树脂、羟基磷灰石中的至少一种。
- 根据权利要求1所述的方法,其特征在于,所述液体碱催化剂选自具有碱性的液体中的任一种。
- 根据权利要求19所述的方法,其特征在于,所述液体碱催化剂选自氢氧化钠水溶液、氢氧化钾水溶液、氢氧化钙水溶液、氢氧化镁水溶液中的任一种。
- 根据权利要求19所述的方法,其特征在于,所述液体碱催化剂中含有氢氧根离子OH -的浓度为0.01~10mol/L。
- 根据权利要求1所述的方法,其特征在于,所述反应的条件为:反应温度60~260℃;反应压力为0.1~10MPa;在所述原料中,甲氧基乙酸甲酯和甲氧基乙酸的总摩尔数与水的摩尔数之比为:(甲氧基乙酸甲酯+甲氧基乙酸):水=1:2~1:20。
- 根据权利要求22所述的方法,其特征在于,所述反应的条件为:反应温度130~200℃;反应压力为0.1~0.3MPa;在所述原料中,甲氧基乙酸甲酯和甲氧基乙酸的总摩尔数与水的摩尔数之比为:(甲氧基乙酸甲酯+甲氧基乙酸):水=1:3~1:8;所述甲氧基乙酸甲酯与甲氧基乙酸的摩尔比为4:1~9:1。
- 根据权利要求1所述的方法,其特征在于,所述反应在反应器中进行;所述反应器选自固定床反应器、釜式反应器、催化精馏反应器中的任一种。
- 根据权利要求24所述的方法,其特征在于,所述反应器包括一个固定床反应器,或通过串联和/或并联方式连接的多个固定床反应器;或者,所述反应器包括一个釜式反应器,或通过串联和/或并联方式连接的多个釜式反应器;或者,所述反应器包括一个催化精馏反应器,或通过串联和/或并联方式连接的多个催化精馏反应器。
- 根据权利要求24所述的方法,其特征在于,采用固定床反应器时,原料中甲氧基乙酸甲酯和甲氧基乙酸的质量空速为0.1~3h -1。
- 根据权利要求24所述的方法,其特征在于,采用釜式反应器时,搅拌速率为250~350转/分;反应时间为1~3天。
- 根据权利要求24所述的方法,其特征在于,采用催化精馏反应器时;反应时间为8~15h;搅拌转速为350~650转/分;回流比为1~3。
- 根据权利要求1所述的方法,其特征在于,所述原料中的甲氧基乙酸甲酯为新加入的原料和/或经过产物分离后未反应完的甲氧基乙酸甲酯;和/或,所述原料中的甲氧基乙酸为新加入的原料和/或经过产物分离后未反应完的甲氧基乙酸;和/或,所述原料中的水为新加入的原料和/或经过产物分离后未反应完的水。
- 根据权利要求1所述的方法,其特征在于,所述反应在非活性气氛中进行;所述非活性气氛包括氮气、惰性气体中的任一种。
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP21923690.8A EP4279477A4 (en) | 2021-02-03 | 2021-02-03 | PROCESS FOR PRODUCING GLYCOLIC ACID AND METHYL GLYCOLATE BY HYDROLYSIS OF METHYL METHOXYACETATE AND METHOXYACETIC ACID |
PCT/CN2021/075023 WO2022165662A1 (zh) | 2021-02-03 | 2021-02-03 | 甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 |
JP2023546202A JP2024504821A (ja) | 2021-02-03 | 2021-02-03 | メトキシ酢酸メチル及びメトキシ酢酸の加水分解によるグリコール酸及びグリコール酸メチルの製造方法 |
US18/275,444 US20240109833A1 (en) | 2021-02-03 | 2021-02-03 | Method for preparing glycolic acid and methyl glycolate through hydrolysis of methyl methoxyacetate and methoxyacetic acid |
ZA2023/07576A ZA202307576B (en) | 2021-02-03 | 2023-07-31 | Method for preparing glycolic acid and methyl glycolate through hydrolysis of methyl methoxyacetate and methoxyacetic acid |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/CN2021/075023 WO2022165662A1 (zh) | 2021-02-03 | 2021-02-03 | 甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2022165662A1 true WO2022165662A1 (zh) | 2022-08-11 |
Family
ID=82740671
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CN2021/075023 WO2022165662A1 (zh) | 2021-02-03 | 2021-02-03 | 甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 |
Country Status (5)
Country | Link |
---|---|
US (1) | US20240109833A1 (zh) |
EP (1) | EP4279477A4 (zh) |
JP (1) | JP2024504821A (zh) |
WO (1) | WO2022165662A1 (zh) |
ZA (1) | ZA202307576B (zh) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN116239472A (zh) * | 2022-11-22 | 2023-06-09 | 中国科学院青岛生物能源与过程研究所 | 由乙醛和乙酸甲酯制备3-羟基丁酸甲酯的方法及该方法中采用的催化剂 |
CN116328825A (zh) * | 2023-02-22 | 2023-06-27 | 中国科学院青岛生物能源与过程研究所 | 一种催化剂,其制备方法以及采用其催化甲醇和乙酸甲酯制备3-甲氧基丙酸甲酯的方法 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1130431B (de) * | 1958-08-27 | 1962-05-30 | Degussa | Verfahren zur Herstellung von wasserfreien kristallisierten ª‡-Oxycarbonsaeuren aus ihren Estern |
CN1180067A (zh) * | 1997-07-11 | 1998-04-29 | 清华大学 | 同时合成羟基乙酸甲酯和甲氧基乙酸甲酯的方法 |
JP2003300926A (ja) * | 2002-04-08 | 2003-10-21 | Nippon Shokubai Co Ltd | α−ヒドロキシカルボン酸又はα−オキソカルボン酸の製造方法 |
WO2013148482A1 (en) * | 2012-03-27 | 2013-10-03 | Eastman Chemical Company | Hydrocarboxylation of formaldehyde in the presence of a higher order carboxylic acid and a heterogeneous catalyst |
CN106554250A (zh) * | 2015-09-30 | 2017-04-05 | 中国科学院大连化学物理研究所 | 一种乙二醇单甲醚水解制备乙二醇的方法 |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107602388B (zh) * | 2017-09-12 | 2020-10-30 | 沈阳化工大学 | 一种制备乙醇酸甲酯并副产卤代烷烃的方法 |
-
2021
- 2021-02-03 EP EP21923690.8A patent/EP4279477A4/en active Pending
- 2021-02-03 US US18/275,444 patent/US20240109833A1/en active Pending
- 2021-02-03 WO PCT/CN2021/075023 patent/WO2022165662A1/zh active Application Filing
- 2021-02-03 JP JP2023546202A patent/JP2024504821A/ja active Pending
-
2023
- 2023-07-31 ZA ZA2023/07576A patent/ZA202307576B/en unknown
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1130431B (de) * | 1958-08-27 | 1962-05-30 | Degussa | Verfahren zur Herstellung von wasserfreien kristallisierten ª‡-Oxycarbonsaeuren aus ihren Estern |
CN1180067A (zh) * | 1997-07-11 | 1998-04-29 | 清华大学 | 同时合成羟基乙酸甲酯和甲氧基乙酸甲酯的方法 |
JP2003300926A (ja) * | 2002-04-08 | 2003-10-21 | Nippon Shokubai Co Ltd | α−ヒドロキシカルボン酸又はα−オキソカルボン酸の製造方法 |
WO2013148482A1 (en) * | 2012-03-27 | 2013-10-03 | Eastman Chemical Company | Hydrocarboxylation of formaldehyde in the presence of a higher order carboxylic acid and a heterogeneous catalyst |
CN106554250A (zh) * | 2015-09-30 | 2017-04-05 | 中国科学院大连化学物理研究所 | 一种乙二醇单甲醚水解制备乙二醇的方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP4279477A4 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN116239472A (zh) * | 2022-11-22 | 2023-06-09 | 中国科学院青岛生物能源与过程研究所 | 由乙醛和乙酸甲酯制备3-羟基丁酸甲酯的方法及该方法中采用的催化剂 |
CN116239472B (zh) * | 2022-11-22 | 2024-04-26 | 中国科学院青岛生物能源与过程研究所 | 由乙醛和乙酸甲酯制备3-羟基丁酸甲酯的方法及该方法中采用的催化剂 |
CN116328825A (zh) * | 2023-02-22 | 2023-06-27 | 中国科学院青岛生物能源与过程研究所 | 一种催化剂,其制备方法以及采用其催化甲醇和乙酸甲酯制备3-甲氧基丙酸甲酯的方法 |
Also Published As
Publication number | Publication date |
---|---|
US20240109833A1 (en) | 2024-04-04 |
EP4279477A4 (en) | 2024-04-03 |
EP4279477A1 (en) | 2023-11-22 |
ZA202307576B (en) | 2023-12-20 |
JP2024504821A (ja) | 2024-02-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN108236955B (zh) | 一种草酸二甲酯加氢合成乙醇用催化剂的制备方法以及由此得到的催化剂和其应用 | |
EP1740525B1 (en) | Process for preparing acetic acid and derivatives thereof | |
JP5530437B2 (ja) | 二重反応区域プロセスを用いる酢酸からのエチレンの製造 | |
WO2022165662A1 (zh) | 甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 | |
TWI402253B (zh) | 製備羰基化產物的方法 | |
EP2138478A1 (en) | Process for producing hydrogenolysis products of polyhydric alcohols | |
TW201113250A (en) | Process for the production of acetic acid and dimethyl ether | |
WO2010014152A1 (en) | Process for catalytically producing ethylene directly from acetic acid in a single reaction zone | |
CN104245651A (zh) | 用于生产乙酸和二甲醚的方法 | |
CN100503534C (zh) | 一种异丙醇的合成方法 | |
TW201012781A (en) | Two-stage, gas phase process for the manufacture of alkylene glycol | |
CN112479841A (zh) | 一种丙烯氢甲酰化合成丁醛的工艺 | |
CN114853592B (zh) | 一种烷氧基乙酸酯水解制取乙醇酸的方法 | |
US8574522B2 (en) | Process for selective oxidative dehydrogenation of a hydrogen-containing CO mixed gas | |
CN114853605B (zh) | 甲氧基乙酸甲酯和甲氧基乙酸水解制取乙醇酸和乙醇酸甲酯的方法 | |
CN115745751A (zh) | 在固定床反应器上用苯酚和甲醇原料连续生产苯甲醚的液固相反应方法 | |
CN103842322A (zh) | 用于制备一种醇类混合物的方法 | |
WO2022165663A1 (zh) | 一种烷氧基乙酸酯水解制取乙醇酸的方法 | |
RU2422203C1 (ru) | Катализатор, способ его приготовления и способ получения метилацетата | |
CN114425318A (zh) | 复合氧化物及其制备方法和应用 | |
Jérôme et al. | Selective conversion of glycerol into functional monomers via catalytic processes | |
JPS63225335A (ja) | α−(3−ベンゾイルフエニル)プロピオン酸またはそのエステルの製造方法 | |
CN114380659B (zh) | 一种由异丁烯-甲醇制备异戊二烯的方法 | |
JP2014043415A (ja) | ジベンジルアミンの製造方法 | |
JPH0136448B2 (zh) |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 21923690 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2023546202 Country of ref document: JP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 18275444 Country of ref document: US |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112023015333 Country of ref document: BR |
|
WWE | Wipo information: entry into national phase |
Ref document number: 202392058 Country of ref document: EA |
|
ENP | Entry into the national phase |
Ref document number: 2021923690 Country of ref document: EP Effective date: 20230817 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 112023015333 Country of ref document: BR Kind code of ref document: A2 Effective date: 20230731 |