WO2019000264A1 - Process for manufacture of ethylene glycol - Google Patents
Process for manufacture of ethylene glycol Download PDFInfo
- Publication number
- WO2019000264A1 WO2019000264A1 PCT/CN2017/090500 CN2017090500W WO2019000264A1 WO 2019000264 A1 WO2019000264 A1 WO 2019000264A1 CN 2017090500 W CN2017090500 W CN 2017090500W WO 2019000264 A1 WO2019000264 A1 WO 2019000264A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- process according
- catalyst
- reaction mixture
- water
- ethylene glycol
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 37
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 9
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000011541 reaction mixture Substances 0.000 claims abstract description 12
- 239000010457 zeolite Substances 0.000 claims abstract description 9
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 8
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000003054 catalyst Substances 0.000 claims description 19
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 17
- NQRYJNQNLNOLGT-UHFFFAOYSA-N Piperidine Chemical compound C1CCNCC1 NQRYJNQNLNOLGT-UHFFFAOYSA-N 0.000 claims description 6
- DBVJJBKOTRCVKF-UHFFFAOYSA-N Etidronic acid Chemical compound OP(=O)(O)C(O)(C)P(O)(O)=O DBVJJBKOTRCVKF-UHFFFAOYSA-N 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- ZSIQJIWKELUFRJ-UHFFFAOYSA-N azepane Chemical compound C1CCCNCC1 ZSIQJIWKELUFRJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 2
- 150000001412 amines Chemical class 0.000 claims description 2
- 239000011230 binding agent Substances 0.000 claims description 2
- 238000001125 extrusion Methods 0.000 claims description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 2
- 239000011707 mineral Substances 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- 239000000377 silicon dioxide Substances 0.000 claims description 2
- 239000002002 slurry Substances 0.000 claims description 2
- 239000003381 stabilizer Substances 0.000 claims description 2
- 238000006703 hydration reaction Methods 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000004817 gas chromatography Methods 0.000 description 4
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000005020 polyethylene terephthalate Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 2
- 230000003213 activating effect Effects 0.000 description 1
- 239000007798 antifreeze agent Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000006735 epoxidation reaction Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000009877 rendering Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/026—After-treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/09—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
- C07C29/10—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes
- C07C29/103—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes of cyclic ethers
- C07C29/106—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes of cyclic ethers of oxiranes
Definitions
- the present invention relates to a process for the manufacture of ethylene glycol starting from ethylene oxide (EO) .
- EO ethylene oxide
- Ethylene Glycol (Mono-Ethylene Glycol or MEG) is an important organic chemical raw material mainly used in the production of polyester (more precisely of PET or poly-ethylene-terephthalate) and as antifreeze agent.
- ethylene glycol production is generally made using a non-catalytic direct hydration method wherein ethylene oxide (EO) and water are reacted generally in a molar ratio of about 1: 20-22 (molar ratio) resulting in an ethylene glycol aqueous solution containing only about 10% (mass fraction) of MEG, the rest being water and by-products like diethylene glycol (DEG) and triethylene glycol (TEG) .
- EO ethylene oxide
- DEG diethylene glycol
- TEG triethylene glycol
- Increasing the amount of water used for this method can reduce the by-product formation and improve the conversion rate of ethylene oxide.
- Zeolites of the Ti-MWW type are known to be catalysts active in epoxidation reactions: see for instance US6759540 and US7323154.
- this kind of catalysts zeolite of the Ti-MWW type
- this type of catalyst also allows reducing the amount of water used (typically decreasing the water/EO ratio to about 5: 1) in said synthesis hence rendering it more economical and environmentally friendly.
- the present invention relates to a process for the manufacture of ethylene glycol starting from ethylene oxide (EO) , said process using a reaction mixture comprising EO, a Ti-MWW zeolite and water.
- EO ethylene oxide
- Preferred embodiments are those according to which:
- the zeolite is modified with an organic amine, preferably with piperidine or hexamethyleneimine as disclosed in CN101003376;
- the catalyst concentration in the reaction mixture is in the range of from 0.5 to 5 wt. %;
- the process is performed at a temperature from 20°C to 150°C;
- the molar ratio of water to EO is in the range of from 1 to 50.
- the molar ratio of hydrogen peroxide to EO is preferably in the range of from 0.01 to 10;
- the molar ratio of water to hydrogen peroxide is preferably in the range of from 5 to 50.
- said mixture when using hydrogen peroxide in the reaction mixture, also comprises a hydrogen peroxide stabilizer like a mineral acid, preferably nitric acid, and/or HEDP (1-hydroxy ethylidene-1, 1-diphosphonic acid) .
- a hydrogen peroxide stabilizer like a mineral acid, preferably nitric acid, and/or HEDP (1-hydroxy ethylidene-1, 1-diphosphonic acid
- the catalyst is preferably used as a slurry catalyst or a fixed bed catalyst.
- the zeolite is preferably mixed with a binder like silica, alumina or a mixture thereof and then shaped for instance by extrusion.
- a hydration reaction (HR) for producing ethylene glycol is carried out under vigorous stirring in an autoclave reactor equipped with a 45 mL Telfon-inner.
- the TS-1 catalyst was prepared according to the procedure described in U.S. Pat. No. 4,410,501.
- the reaction mixture is immediately immersed in a pre-heated oil bath to start the reaction.
- the reaction mixture is stirred at 40°C for 4 h, and then immediately cooled down in an ice bath to stop the reaction.
- Both the gas and the liquid phase samples are collected and analyzed by gas chromatography (GC) using isopropanol as an internal standard.
- GC gas chromatography
- the gases are vented into an acetonitrile solvent for GC analysis.
- the catalyst is removed from the reaction mixture by centrifugation and the supernatant is analyzed by GC for organic products.
- the hydration reaction is run according to the same procedure as Comparative Example 1 except that a Ti-MWW (0.1 g) is used as a catalyst instead of a TS-1 catalyst.
- the Ti-MWW was prepared according to a known literature procedure (Chemistry Letters, 2000: 774) .
- the hydration reaction is run according to the same procedure as Example 2 except that the Ti-MWW catalyst was chemically treated in an aqueous solution of piperidine according to a known literature procedure (Journal of Physical Chemistry C, 2008, 112, 6132) .
- the hydration reaction is run according to the same procedure as Example 2 except that the Ti-MWW catalyst was chemically treated in an aqueous solution of hexamethyleneimine according to a known literature procedure (Journal of Physical Chemistry C, 2008, 112, 6132) .
- the hydration reaction is run according to the same procedure as Example 2 except that the amount of Ti-MWW is 0.2 g.
- the hydration reaction is run according to the same procedure as Example 2 except that the amount of water is 2 g.
- the hydration reaction is run according to the same procedure as Example 3 except that the amount of water is 2.7 g.
- the hydration reaction is run according to the same procedure as Example 3 except that the amount of water is 2 g.
- the hydration reaction is run according to the same procedure as Example 2 except that the reaction temperature is at 60°C.
- the hydration reaction is run according to the same procedure as Example 2 except that 10 mmol of H2O2 is added into the reaction.
- the hydration reaction is run according to the same procedure as Example 3 except that the amount of catalyst and the reaction time are 0.05 g and 1 h, respectively.
- the hydration reaction is run according to the same procedure as Example 11 except that the reaction temperature is at 60°C.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
Abstract
Provided are process for the manufacture of ethylene glycol starting from ethylene oxide (EO) and said process using a reaction mixture comprising EO, a Ti-MWW zeolite and water.
Description
The present invention relates to a process for the manufacture of ethylene glycol starting from ethylene oxide (EO) .
Ethylene Glycol (Mono-Ethylene Glycol or MEG) is an important organic chemical raw material mainly used in the production of polyester (more precisely of PET or poly-ethylene-terephthalate) and as antifreeze agent.
At present, large-scale ethylene glycol production is generally made using a non-catalytic direct hydration method wherein ethylene oxide (EO) and water are reacted generally in a molar ratio of about 1: 20-22 (molar ratio) resulting in an ethylene glycol aqueous solution containing only about 10％ (mass fraction) of MEG, the rest being water and by-products like diethylene glycol (DEG) and triethylene glycol (TEG) . Increasing the amount of water used for this method can reduce the by-product formation and improve the conversion rate of ethylene oxide. However, it makes it necessary to set up multiple evaporators/distillation columns, increasing the equipment investment and energy consumption, which directly affects the production cost of ethylene glycol.
Zeolites of the Ti-MWW type are known to be catalysts active in epoxidation reactions: see for instance US6759540 and US7323154.
The inventors have now discovered that this kind of catalysts (zeolite of the Ti-MWW type) is also very active in the synthesis of MEG starting from EO and water (i.e. in the hydrolysis of EO to MEG) . Besides activating the reaction, this type of catalyst also allows reducing the amount of water used (typically decreasing the water/EO ratio to about 5: 1) in said synthesis hence rendering it more economical and environmentally friendly.
Therefore, the present invention relates to a process for the manufacture of ethylene glycol starting from ethylene oxide (EO) , said process using a reaction mixture comprising EO, a Ti-MWW zeolite and water.
Preferred embodiments are those according to which:
-the zeolite is modified with an organic amine, preferably with piperidine or hexamethyleneimine as disclosed in CN101003376；
-the catalyst concentration in the reaction mixture is in the range of from 0.5 to 5 wt. ％；
-the process is performed at a temperature from 20℃ to 150℃；
-the molar ratio of water to EO is in the range of from 1 to 50.
The use of hydrogen peroxide in the reaction mixture is preferred. In that embodiment:
-the molar ratio of hydrogen peroxide to EO is preferably in the range of from 0.01 to 10； and/or
-the molar ratio of water to hydrogen peroxide is preferably in the range of from 5 to 50.
Considering the fact that EO is extremely flammable and explosive, care should be taken to work in conditions outside the explosion zone.
In a preferred sub-embodiment, when using hydrogen peroxide in the reaction mixture, said mixture also comprises a hydrogen peroxide stabilizer like a mineral acid, preferably nitric acid, and/or HEDP (1-hydroxy ethylidene-1, 1-diphosphonic acid) .
In the invention, the catalyst is preferably used as a slurry catalyst or a fixed bed catalyst. Hence, the zeolite is preferably mixed with a binder like silica, alumina or a mixture thereof and then shaped for instance by extrusion.
The following Examples illustrate some embodiments of the present invention.
COMPARATIVE EXAMPLE 1
A hydration reaction (HR) for producing ethylene glycol is carried out under vigorous stirring in an autoclave reactor equipped with a 45 mL Telfon-inner. A TS-1 catalyst (0.1 g, Si/Ti＝50) , water (5 g) and ethylene oxide (0.44 g) are added into the reactor, and the pressure of the reactor is then raised to 1.5 MPa with nitrogen. The TS-1 catalyst was prepared according to the procedure described in U.S. Pat. No. 4,410,501. The reaction mixture is immediately immersed in a pre-heated oil bath to start the reaction. The reaction mixture is stirred at 40℃ for 4 h, and then immediately cooled down in an ice bath to stop the reaction.
Both the gas and the liquid phase samples are collected and analyzed by gas chromatography (GC) using isopropanol as an internal standard. The gases are vented into an acetonitrile solvent for GC analysis. The catalyst is removed from the reaction mixture by centrifugation and the supernatant is analyzed by GC for organic products.
EXAMPLE 2
The hydration reaction is run according to the same procedure as Comparative Example 1 except that a Ti-MWW (0.1 g) is used as a catalyst instead of a TS-1
catalyst. The Ti-MWW was prepared according to a known literature procedure (Chemistry Letters, 2000: 774) .
EXAMPLE 3
The hydration reaction is run according to the same procedure as Example 2 except that the Ti-MWW catalyst was chemically treated in an aqueous solution of piperidine according to a known literature procedure (Journal of Physical Chemistry C, 2008, 112, 6132) .
EXAMPLE 4
The hydration reaction is run according to the same procedure as Example 2 except that the Ti-MWW catalyst was chemically treated in an aqueous solution of hexamethyleneimine according to a known literature procedure (Journal of Physical Chemistry C, 2008, 112, 6132) .
EXAMPLE 5
The hydration reaction is run according to the same procedure as Example 2 except that the amount of Ti-MWW is 0.2 g.
EXAMPLE 6
The hydration reaction is run according to the same procedure as Example 2 except that the amount of water is 2 g.
EXAMPLE 7
The hydration reaction is run according to the same procedure as Example 3 except that the amount of water is 2.7 g.
EXAMPLE 8
The hydration reaction is run according to the same procedure as Example 3 except that the amount of water is 2 g.
EXAMPLE 9
The hydration reaction is run according to the same procedure as Example 2 except that the reaction temperature is at 60℃.
EXAMPLE 10
The hydration reaction is run according to the same procedure as Example 2 except that 10 mmol of H2O2 is added into the reaction.
EXAMPLE 11
The hydration reaction is run according to the same procedure as Example 3 except that the amount of catalyst and the reaction time are 0.05 g and 1 h, respectively.
EXAMPLE 12
The hydration reaction is run according to the same procedure as Example 11 except that the reaction temperature is at 60℃.
The results obtained in all these Examples are shown in Table 1 below.
Claims (10)
- A process for the manufacture of ethylene glycol starting from ethylene oxide (EO) ， said process using a reaction mixture comprising EO， a Ti-MWW zeolite and water.
- The process according to claim 1， wherein the zeolite is modified with an organic amine， preferably with piperidine or hexamethyleneimine.
- The process according to any of the preceding claims， wherein the catalyst concentration in the reaction mixture is in the range of from 0.5 to 5 wt. ％
- The process according to any of the preceding claims， wherein the process is performed at a temperature from 20℃ to 150℃.
- The process according to any of the preceding claims， wherein the molar ratio of water to EO is in the range of from 1 to 50.
- The process according to any of the preceding claims， wherein hydrogen peroxide in also present in the reaction mixture.
- The process according to the preceding claim， wherein the molar ratio of hydrogen peroxide to EO is preferably in the range of from 0.01 to 10.
- The process according to claim 6 or 7， wherein the reaction mixture also comprises a hydrogen peroxide stabilizer like a mineral acid， preferably nitric acid， and/or HEDP (1-hydroxy ethylidene-1， 1-diphosphonic acid) .
- The process according to any of the preceding claims， wherein the catalyst is a slurry catalyst or a fixed bed catalyst.
- The process according to the preceding claim， wherein the zeolite is mixed with a binder like silica， alumina or a mixture thereof and shaped by extrusion.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP17915315.0A EP3645489A4 (en) | 2017-06-28 | 2017-06-28 | PROCESS FOR PRODUCING ETHYLENE GLYCOL |
| PCT/CN2017/090500 WO2019000264A1 (en) | 2017-06-28 | 2017-06-28 | Process for manufacture of ethylene glycol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2017/090500 WO2019000264A1 (en) | 2017-06-28 | 2017-06-28 | Process for manufacture of ethylene glycol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO2019000264A1 true WO2019000264A1 (en) | 2019-01-03 |
Family
ID=64740222
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/CN2017/090500 WO2019000264A1 (en) | 2017-06-28 | 2017-06-28 | Process for manufacture of ethylene glycol |
Country Status (2)
| Country | Link |
|---|---|
| EP (1) | EP3645489A4 (en) |
| WO (1) | WO2019000264A1 (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020010378A1 (en) * | 2000-05-08 | 2002-01-24 | Yukihiko Kakimoto | Method for production of ethylene oxide |
| CN101003376A (en) * | 2006-09-30 | 2007-07-25 | 华东师范大学 | Method for synthesizing alkali modified molecular sieve containing titanium |
| CN102219642A (en) * | 2010-04-15 | 2011-10-19 | 中国石油化工股份有限公司 | Method for producing glycol by virtue of hydration of ethylene oxide |
| CN102951998A (en) * | 2011-08-24 | 2013-03-06 | 岳阳蓬诚科技发展有限公司 | Method of preparing glycol by using one-step ethylene method |
-
2017
- 2017-06-28 WO PCT/CN2017/090500 patent/WO2019000264A1/en unknown
- 2017-06-28 EP EP17915315.0A patent/EP3645489A4/en not_active Withdrawn
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020010378A1 (en) * | 2000-05-08 | 2002-01-24 | Yukihiko Kakimoto | Method for production of ethylene oxide |
| CN101003376A (en) * | 2006-09-30 | 2007-07-25 | 华东师范大学 | Method for synthesizing alkali modified molecular sieve containing titanium |
| CN102219642A (en) * | 2010-04-15 | 2011-10-19 | 中国石油化工股份有限公司 | Method for producing glycol by virtue of hydration of ethylene oxide |
| CN102951998A (en) * | 2011-08-24 | 2013-03-06 | 岳阳蓬诚科技发展有限公司 | Method of preparing glycol by using one-step ethylene method |
Non-Patent Citations (2)
| Title |
|---|
| LU, XINQING ET AL.: "Selective synthesis of ethylene oxide through liquid-phase epoxidation of ethylene with titanosilicate/H202 catalytic systems", APPLIED CATALYSIS A: GENERAL, vol. 515, 4 February 2016 (2016-02-04), pages 51 - 59, XP029451504 * |
| See also references of EP3645489A4 * |
Also Published As
| Publication number | Publication date |
|---|---|
| EP3645489A1 (en) | 2020-05-06 |
| EP3645489A4 (en) | 2020-12-09 |
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