WO2012157534A1 - Process for producing olefin oxide - Google Patents
Process for producing olefin oxide Download PDFInfo
- Publication number
- WO2012157534A1 WO2012157534A1 PCT/JP2012/062075 JP2012062075W WO2012157534A1 WO 2012157534 A1 WO2012157534 A1 WO 2012157534A1 JP 2012062075 W JP2012062075 W JP 2012062075W WO 2012157534 A1 WO2012157534 A1 WO 2012157534A1
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- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- metal
- olefin
- oxide
- particles
- Prior art date
Links
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 44
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 21
- 230000008569 process Effects 0.000 title claims abstract description 19
- 239000010931 gold Substances 0.000 claims abstract description 62
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 239000002245 particle Substances 0.000 claims abstract description 29
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229910052737 gold Inorganic materials 0.000 claims abstract description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 27
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 27
- 229910052751 metal Inorganic materials 0.000 claims abstract description 25
- 239000002184 metal Substances 0.000 claims abstract description 25
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims abstract description 24
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 8
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical group CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 claims description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 description 29
- 239000007789 gas Substances 0.000 description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- 229910044991 metal oxide Inorganic materials 0.000 description 12
- 150000004706 metal oxides Chemical class 0.000 description 12
- 238000010438 heat treatment Methods 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 9
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- -1 alkaline earth metal carbonate Chemical class 0.000 description 5
- 150000002366 halogen compounds Chemical class 0.000 description 5
- GGCZERPQGJTIQP-UHFFFAOYSA-N sodium;9,10-dioxoanthracene-2-sulfonic acid Chemical compound [Na+].C1=CC=C2C(=O)C3=CC(S(=O)(=O)O)=CC=C3C(=O)C2=C1 GGCZERPQGJTIQP-UHFFFAOYSA-N 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000004833 X-ray photoelectron spectroscopy Methods 0.000 description 4
- 230000004913 activation Effects 0.000 description 4
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 229910052786 argon Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 239000012018 catalyst precursor Substances 0.000 description 4
- 239000003638 chemical reducing agent Substances 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- GGKNTGJPGZQNID-UHFFFAOYSA-N (1-$l^{1}-oxidanyl-2,2,6,6-tetramethylpiperidin-4-yl)-trimethylazanium Chemical compound CC1(C)CC([N+](C)(C)C)CC(C)(C)N1[O] GGKNTGJPGZQNID-UHFFFAOYSA-N 0.000 description 3
- 101710194905 ARF GTPase-activating protein GIT1 Proteins 0.000 description 3
- 102100029217 High affinity cationic amino acid transporter 1 Human genes 0.000 description 3
- 101710081758 High affinity cationic amino acid transporter 1 Proteins 0.000 description 3
- IJKVHSBPTUYDLN-UHFFFAOYSA-N dihydroxy(oxo)silane Chemical compound O[Si](O)=O IJKVHSBPTUYDLN-UHFFFAOYSA-N 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000000465 moulding Methods 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- SQGYOTSLMSWVJD-UHFFFAOYSA-N silver(1+) nitrate Chemical compound [Ag+].[O-]N(=O)=O SQGYOTSLMSWVJD-UHFFFAOYSA-N 0.000 description 3
- WYTZZXDRDKSJID-UHFFFAOYSA-N (3-aminopropyl)triethoxysilane Chemical compound CCO[Si](OCC)(OCC)CCCN WYTZZXDRDKSJID-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical class [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 229910000288 alkali metal carbonate Inorganic materials 0.000 description 2
- 150000008041 alkali metal carbonates Chemical class 0.000 description 2
- AYJRCSIUFZENHW-UHFFFAOYSA-L barium carbonate Chemical compound [Ba+2].[O-]C([O-])=O AYJRCSIUFZENHW-UHFFFAOYSA-L 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 239000010431 corundum Substances 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- BDAGIHXWWSANSR-NJFSPNSNSA-N hydroxyformaldehyde Chemical compound O[14CH]=O BDAGIHXWWSANSR-NJFSPNSNSA-N 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 229910052709 silver Inorganic materials 0.000 description 2
- 239000004332 silver Substances 0.000 description 2
- 239000012279 sodium borohydride Substances 0.000 description 2
- 229910000033 sodium borohydride Inorganic materials 0.000 description 2
- 238000001228 spectrum Methods 0.000 description 2
- 229910000018 strontium carbonate Inorganic materials 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 description 1
- RBACIKXCRWGCBB-UHFFFAOYSA-N 1,2-Epoxybutane Chemical compound CCC1CO1 RBACIKXCRWGCBB-UHFFFAOYSA-N 0.000 description 1
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 description 1
- WHNBDXQTMPYBAT-UHFFFAOYSA-N 2-butyloxirane Chemical compound CCCCC1CO1 WHNBDXQTMPYBAT-UHFFFAOYSA-N 0.000 description 1
- SYURNNNQIFDVCA-UHFFFAOYSA-N 2-propyloxirane Chemical compound CCCC1CO1 SYURNNNQIFDVCA-UHFFFAOYSA-N 0.000 description 1
- 238000004438 BET method Methods 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 102100035959 Cationic amino acid transporter 2 Human genes 0.000 description 1
- 102100021391 Cationic amino acid transporter 3 Human genes 0.000 description 1
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- 229910004042 HAuCl4 Inorganic materials 0.000 description 1
- 108091006231 SLC7A2 Proteins 0.000 description 1
- 108091006230 SLC7A3 Proteins 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000003277 amino group Chemical group 0.000 description 1
- 229910002113 barium titanate Inorganic materials 0.000 description 1
- AYJRCSIUFZENHW-DEQYMQKBSA-L barium(2+);oxomethanediolate Chemical compound [Ba+2].[O-][14C]([O-])=O AYJRCSIUFZENHW-DEQYMQKBSA-L 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 239000011203 carbon fibre reinforced carbon Substances 0.000 description 1
- 239000002041 carbon nanotube Substances 0.000 description 1
- 229910021393 carbon nanotube Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- HRYZWHHZPQKTII-UHFFFAOYSA-N chloroethane Chemical compound CCCl HRYZWHHZPQKTII-UHFFFAOYSA-N 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000011258 core-shell material Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 229960003750 ethyl chloride Drugs 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 229910001676 gahnite Inorganic materials 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 229910052913 potassium silicate Inorganic materials 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 150000003377 silicon compounds Chemical class 0.000 description 1
- 229910001961 silver nitrate Inorganic materials 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000019795 sodium metasilicate Nutrition 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006557 surface reaction Methods 0.000 description 1
- 229910000299 transition metal carbonate Inorganic materials 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/48—Silver or gold
- B01J23/52—Gold
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/48—Silver or gold
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/0272—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing elements other than those covered by B01J31/0201 - B01J31/0255
- B01J31/0274—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing elements other than those covered by B01J31/0201 - B01J31/0255 containing silicon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0207—Pretreatment of the support
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/024—Multiple impregnation or coating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/16—Reducing
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/04—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen
- C07D301/08—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase
- C07D301/10—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase with catalysts containing silver or gold
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/08—Silica
Definitions
- the present invention relates to a process for producing an olefin oxide.
- WO 98/58921 Al and US 7319156 B2 disclose a process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a silver catalyst.
- the present invention provides a process for producing an olefin oxide related to the following:
- a process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a catalyst, wherein the catalyst comprises particles consisting of silver metal and gold metal, and a ratio of gold metal to silver metal of the particles ( [Au/Ag(bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1) :
- a catalyst for producing an olefin oxide which comprises particles consisting of silver metal and gold metal wherein a ratio of goldmetal to silver metal of the particles ( [Au/Ag (bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1):
- the present invention is a process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a catalyst, wherein the catalyst comprises particles consisting of silver metal and gold metal, and a ratio of gold metal to silver metal of the particles ( [Au/Ag (bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1) :
- the catalyst can be prepared according to the process described in Chem. Mater. 2009, 21, 410-418.
- the catalyst can be produced, for example, by the following steps (a) and (b) :
- step (b) the catalyst obtained may be heated under an atmosphere free from oxygen.
- the contacting temperature in the step (a) is usually 0 to 100°C.
- Examples of the silver salt include silver nitrate.
- Examples of the reducing agent include sodium borohydride .
- the temperature of the reduction is usually 0 to 100°C.
- the ratio of gold metal to silver metal of the particles ( [Au/Ag (bulk) ] ) can be calculated based on the used amount of gold particles and the used amount of the silver salt. Therefore, [Au/Ag (bulk) ] can be controlled by changing the used amount of gold particles and/or the used amount of the silver salt.
- [Au/Ag (bulk) ] is preferably 1 or more, and more preferably 3 or more.
- [Au/Ag (surface) ]/ [Au/Ag (bulk) ] is 0.9 or less, and preferably 0.7 or less.
- the ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) can be controlled by changing the temperature of heating after the step (b) .
- the particle size of the catalyst is usually 500 nm or less, preferably 100 nm or less and more preferably 50 nm or less.
- the catalyst supported on a carrier is preferably prepared.
- the catalyst supported on the carrier can be produced by the following steps (c) to (f) :
- step (f) a step of reducing the catalyst precursor.
- the contacting temperature in the step (c) is usually 0 to 50°C.
- the contact in the step (c) is usually conducted in water. After, contacting chloroauric acid with the carrier, the gold precursor obtained may be washed and/or dried before the step (d) .
- Examples of the reducing agent used in the steps (d) and (f) include the same as described in the above step (b) .
- the temperature of the reduction is usually 0 to 100°C.
- the contacting temperature in the step (e) is usually 0 to 50°C.
- the contact in the step (e) is usually conducted in water.
- the temperature of the reduction in the step (f) is usually 0 to 100°C.
- the reaction mixture obtained is usually filtrated to obtain the catalyst.
- the catalyst obtained can be washed with water.
- the catalyst obtained may be heated under an atmosphere free from oxygen in order to control [Au/Ag (surface) ] .
- [Au/Ag (surface) ] in the catalyst can be measured with XPS (X-ray photoelectron spectroscopy) analysis.
- the catalyst usually has a core-shell structure in which the core consists of gold particle and the shell consists of silver particle .
- the carrier is preferably one on which the catalyst can be supported and which does not change in property under the condition of the process of the present invention.
- the carrier include a metal carbonate, a metal oxide and carbon.
- the metal carbonate include an alkali metal carbonate, an alkaline earth metal carbonate and a transition metal carbonate, and the alkaline earth metal carbonate is preferable .
- Examples of the alkali metal carbonate include sodium carbonate and potassium carbonate .
- Examples of the alkaline earth metal carbonate include magnesium carbonate, calcium carbonate, strontium carbonate and barium carbonate, and calcium carbonate, strontium carbonate and barium carbonate are preferable.
- the alkaline earth metal carbonate having a specific surface area of 1 to 70 m 2 /g measured by nitrogen adsorption of the BET method is preferable.
- the metal carbonate may be used as it is or after fixing particles of the metal carbonate each other using a suitable binder.
- the metal carbonate may be mixed with a molding agent and molded by extrusion molding, press molding or the like to use the obtained product as the carrier. It is preferred that the metal carbonate is used as it is as the carrier.
- a metal oxide having a crystal form of a rock salt structure, a corundum structure, a spinel-type structure, a fluorite-type structure, a wurtzite-type structure, a rutile-type structure, a bixbite-type structure, an ilmenite-type structure, a pseudobrookite-type structure or a perovskite-type structure can be used.
- Examples of the metal oxide having a rock salt structure include TiO, VO, MnO and NiO.
- Examples of the metal oxide having a corundum structure include ⁇ - ⁇ 1 2 0 3 and a-Fe 2 0 3 .
- Examples of the metal oxide having a spinel-type structure include ZnAl 2 0 4 , y-Fe 2 0 3 and SnZn 2 0 4 .
- Examples of the metal oxide having a fluorite-type structure include Zr0 2 and Ce0 2 .
- Examples of the metal oxide having a wurtzite-type structure include ZnO.
- Examples of the metal oxide having a rutile-type structure include Sn0 2 , Ti0 2 and Ru0 2 .
- Examples of the metal oxide having a bixbite-type structure include p-Fe 2 0 3 .
- Examples of the metal oxide having an ilmenite-type structure include FeTi0 3 .
- Examples of the metal oxide having a pseudobrookite-type structure include FeTiOs.
- Examples of the metal oxide having a perovskite-type structure include CaTi0 3 , SrTi0 3 , BaTi0 3 , CaZr0 3 , SrZr0 3 , BaZr0 3 and LaA10 3 .
- Examples of the carbon include activated carbon, carbon black, graphite and carbon nanotubes, and graphite is preferred.
- a silicon compound can be also used, and examples thereof include a water-soluble silicate such as sodium metasilicate and potassium metasilicate, and a porous silicate having silica as a main component such as silica gel, zeolite and mesoporous silicate.
- a water-soluble silicate such as sodium metasilicate and potassium metasilicate
- a porous silicate having silica as a main component such as silica gel, zeolite and mesoporous silicate.
- a commercially available carrier may be used as it is, and such a commercially available carrier may also be used after purifying and molding by a well-known method.
- the used amount of the carrier is preferably 0.1 to 200 parts by mass per 1 part by mass of the catalyst.
- the catalyst is preferably activated before using for the process of the present invention.
- the activation of the catalyst is usually conductedby heating the catalyst prepared in the absence of oxygen.
- the heating temperature of the activation is usually 150 to 300°C.
- the process of the present invention comprises reacting an olefin and oxygen in the presence of the above-mentioned catalyst.
- the process of the present invention can be performed in a batch-wise reactor or a continuous reactor. From the viewpoint of an industrial process, it is preferably performed in a continuous reactor .
- the amount of the. catalyst is preferably 0.00005 mole or more relative to 1 mole of the olefin, and more preferably 0.0001 mole or more in a silver metal equivalent .
- the upper limit thereof is not limited, and while a larger amount of the olefin oxide can be produced if increasing the amount of the catalyst, the upper limit of the amount of the catalyst is usually adjusted by taking an economic efficiency such as the cost of catalyst into consideration.
- Oxygen can be used in combination with an inert gas such as nitrogen and carbon dioxide. Air can be used as oxygen.
- the amount of oxygen can be appropriately adjusted according to the reaction mode (continuous type or batch type) .
- the amount of oxygen is preferably in the range of 0.01 to 100 moles relative to 1 mole of the olefin, and more preferably in the range of 0.03 to 30 moles.
- the reaction temperature is preferably in the range of 100°C 400°C, and more preferably in the range of 120°C to 300°C.
- "olefin” means a hydrocarbon having one carbon-carbon double bond, and examples thereof include ethylene, propylene, butene, pentene and hexene, and propylene is preferable.
- the olefin can be used in combination with an inert organic gas such as a lower alkane such as methane and ethane.
- Olefin and oxygen gases can be fed in the form of their mixed gas.
- Olefin and oxygen gases may be fed with diluent gases .
- diluent gases include nitrogen, methane, ethane, propane, carbon dioxide and rare gases such as argon and helium.
- the reaction of the olefin and oxygen can be conducted in the presence of a halogen compound, particularly an organic halogenated compound.
- a halogen compound particularly an organic halogenated compound.
- the halogen compound include the halogen compounds disclosed in Japanese Unexamined Patent Application Publication No. 2008-184456, and it is preferably an organic chlorinated compound.
- the organic chlorinated compound include chloroethane , 1 , 2-dichloroethane , chloromethane and vinyl chloride.
- the halogen compound is preferably a compound existing in the form of a gas at the temperature and pressure condition in the reaction system of the reaction.
- the amount of the halogen compound is preferably 1 to 1000 ppm by volume, and more preferably 1 to 500 ppm by volume based on a total volume of the mixed gas other than steam, i.e. a mixed gas composed of oxygen, the olefin and a dilution gas added as necessary.
- the reaction pressure is not limited, and may be selected from those in reducedpressure conditions topressurized conditions .
- the pressure under pressurized conditions is preferable from the viewpoint of allowing sufficient contact of oxygen and the olefin with the catalyst, it may be a reaction pressure selected from the range of 0.01 to 3 MPa. in absolute pressure, and is more preferably selected from the range of 0.02 to 2 MPa.
- the reaction pressure is determined by also taking into consideration the pressure resistibility of the reaction device used in the present productionmethod.
- the reducedpressure condition means apressure lower than the atmospheric pressure.
- the pressurized condition means a pressure higher than the atmospheric pressure.
- the reaction can be carried out in the presence of water.
- water is preferably changed into steam by heating to use, and a mixed gas obtained by mixing steam, oxygen and the olefin is preferably contacted with the catalyst. It is preferable to use water as steam.
- the amount of water is preferably in the range of about 0.1 to about 20 moles relative to 1 mole of the olefin, more preferably in the range of 0.2 to 10 moles, and still more preferably in the range of 0.3 to 8 moles.
- the above-mentioned “amount of water” indicates an amount of water supplied separately from water contained in air in a case of supplying air as oxygen.
- the catalyst in a predetermined amount is filled into a reaction tower equipped with a gas supply port and a gas exhaust port.
- Suitable heating means may be provided in the reaction tower, and the inside of the reaction tower may be raised in temperature up to a predetermined reaction temperature by such heating means.
- a source gas containing the olefin and oxygen is supplied from the gas supply port into the reaction tower.
- the olefin and oxygen reacts in the presence of the catalyst, and the olefin oxide is generated.
- the product gas containing the olefin oxide thus generated is exhausted from the gas exhaust port .
- the linear velocity of the source gas that is passed through the inside of a reaction tower is determined so as to make a residence time that allows the source gas and the catalyst to sufficiently generate the olefin oxide.
- heating means being provided in the reaction tower
- the reaction tower may be maintained at ambient temperature, and the source gas may be supplied and then heated up to a predetermined reaction temperature by appropriate heating means, and then supplied into the reaction tower.
- suitable stirring means is provided in the reaction tower, and a source gas is supplied while stirring the catalyst that is present inside the reaction tower.
- the olefin oxide thus generated, unreacted olefin and oxygen, and byproducts such as carbon dioxide may be contained in the product gas passing through the reaction tower.
- an inert gas used for dilution may be incorporated.
- the olefin oxide, which is the objective can be removed by separation means such as distillation.
- olefin oxide examples include ethylene oxide, propylene oxide, butene oxide, pentene oxide and hexene oxide.
- X ray source Al non-monocromatic, lOkV, 50W
- a catalyst was prepared according to the method described in Chem. Mater. 2009, 21, 410-418.
- One (1) g of a commercial silica carrier (Scharlau, 500m 2 /gr) was added to a 50 mL of ethanol solution containing 2.5 g of APTES (H 2 N (CH 2 ) 3S1 (OE ' t) 3 ) .
- Themixture obtained was refluxed for 24 hours to graft APTES on the silica surface.
- the solid was dispersed in 16 g of water at room temperature, to which 4 mL of 1.88% by weight HAuCl 4 solution was added under stirring during 1.5 hours.
- the recovered solid was added into 10 g of water, to which 10 mL of 0.2 M NaBH 4 solution was added under vigorous stirring for reduction of AuCl 4 " . After 20 minutes, the solid was recovered by filtration and thoroughly washed with water to remove CI " for the subsequent Ag deposition. After dried at 60°C, the solid was dispersed in 16 g of H 2 0 at room temperature, to which . 4 mL of 0.277% by weight AgN0 3 solution was added under stirring. After filtration and washing, the recovered solid was added into 10 g of water, to which 10 mL of 0.2 MNaBH 4 solution was added under vigorous stirring . After 20 minutes, the solid was recovered by filtration and thoroughly washed with water and dried under vacuum (10 ⁇ 3 mbar) .
- the obtained catalyst is called as "CAT-1".
- CAT-1 was aged for 1 month to obtain a catalyst.
- This catalyst is called as “CAT-2” .
- CAT-1 was calcined at 500°C in air to obtain a catalyst.
- This catalyst is called as "CAT-3”.
- the nominal total metal loadings were 5% by weight. The results .are shown in Table 1.
- Table 1 Table 1
- Vacuum pressure 1*10 ⁇ 6 mbar during acquisition
- the catalysts weight was around 150 mg, diluted in CSi in a 1 : 1 weight ratio . The activation of the catalyst was conducted prior to the reaction.
- TPSR temperature programmed surface reaction
- propylene oxide which is useful as an intermediate material of manufactured products, can be produced from propylene and oxygen with superior propylene oxide selectivity (PO/C0 2 ) .
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Abstract
The present invention relates to a process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a catalyst, wherein the catalyst comprises particles consisting of silver metal and gold metal, and a ratio of gold metal to silver metal of the particles ([Au/Ag(bulk)]) and a ratio of gold metal to silver metal of the surfaces of the particles ([Au/Ag(surface)]) satisfy the following formula (1): 0≤[Au/Ag (surface)]/[Au/Ag (bulk)]≤0.9 (1)
Description
DESCRIPTION
PROCESS FOR PRODUCING OLEFIN OXIDE Technical Field
The present invention relates to a process for producing an olefin oxide.
Background Art
WO 98/58921 Al and US 7319156 B2 disclose a process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a silver catalyst.
Summary of Invention
The present invention provides a process for producing an olefin oxide related to the following:
[ 1 ] A process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a catalyst, wherein the catalyst comprises particles consisting of silver metal and gold metal, and a ratio of gold metal to silver metal of the particles ( [Au/Ag(bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1) :
0<[Au/Ag (surface) ]/ [Au/Ag (bulk)]<0.9 (1);
[2] The process according to [1], wherein the catalyst is supported on a carrier;
[3] The process according to [1] or [2], wherein the olefin is propylene and the olefin oxide is propylene oxide;
[4] A catalyst for producing an olefin oxide which comprises particles consisting of silver metal and gold metal wherein a ratio of goldmetal to silver metal of the particles ( [Au/Ag (bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1):
0<[Au/Ag (surface) ]/ [Au/Ag (bulk)]<0.9 (1)
Description of Embodiments
The present invention is a process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a catalyst, wherein the catalyst comprises particles consisting of silver metal and gold metal, and a ratio of gold metal to silver metal of the particles ( [Au/Ag (bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1) :
0<[Au/Ag (surface) ] / [Au/Ag (bulk) ] <0.9 (1)
The catalyst can be prepared according to the process described in Chem. Mater. 2009, 21, 410-418.
Specifically, the catalyst can be produced, for example, by the following steps (a) and (b) :
(a) a step of contacting gold particles with a silver salt to obtain a catalyst precursor,
(b) a step of reducing the catalyst precursor with a reducing agent .
After, step (b) , the catalyst obtained may be heated under an atmosphere free from oxygen.
The contacting temperature in the step (a) is usually 0 to 100°C.
Examples of the silver salt include silver nitrate. Examples of the reducing agent include sodium borohydride . The temperature of the reduction is usually 0 to 100°C.
The ratio of gold metal to silver metal of the particles ( [Au/Ag (bulk) ] ) can be calculated based on the used amount of gold particles and the used amount of the silver salt. Therefore, [Au/Ag (bulk) ] can be controlled by changing the used amount of gold particles and/or the used amount of the silver salt. In the catalyst, [Au/Ag (bulk) ] is preferably 1 or more, and more preferably 3 or more.
[Au/Ag (surface) ]/ [Au/Ag (bulk) ] is 0.9 or less, and preferably 0.7 or less.
The ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) can be controlled by changing the temperature of heating after the step (b) . The higher the temperature of the heating is, the more silver metal of the surfaces of the particles are diffused into the inside of the particles, and therefore, [Au/Ag (surface) ] becomes bigger. Therefore, the temperature of the heating is usually 0°C to 200°C, preferably 0°C to 150°C, and more preferably 0°C to 100°C.
The particle size of the catalyst is usually 500 nm or less, preferably 100 nm or less and more preferably 50 nm or less.
From the viewpoint of ease of the preparation of the catalyst having a small particle size, the catalyst supported on a carrier is preferably prepared. The catalyst supported on the carrier can be produced by the following steps (c) to (f) :
(c) a step of contacting chloroauric acid with a carrier functionalized by amino groups to obtain a gold precursor,
(d) a step of reducing the gold precursor with a reducing agent to obtain gold supported on the carrier,
(e) a step of contacting gold supported on the carrier with a silver salt to obtain a catalyst precursor,
(f) a step of reducing the catalyst precursor. The contacting temperature in the step (c) is usually 0 to 50°C. The contact in the step (c) is usually conducted in water. After, contacting chloroauric acid with the carrier, the gold precursor obtained may be washed and/or dried before the step (d) .
Examples of the reducing agent used in the steps (d) and (f) include the same as described in the above step (b) . The temperature of the reduction is usually 0 to 100°C.
The contacting temperature in the step (e) is usually 0 to 50°C. The contact in the step (e) is usually conducted in water.
The temperature of the reduction in the step (f) is usually 0 to 100°C.
After the step (f) , the reaction mixture obtained is usually filtrated to obtain the catalyst. The catalyst obtained can be washed with water.
As described above, the catalyst obtained may be heated under an atmosphere free from oxygen in order to control [Au/Ag (surface) ] .
[Au/Ag (surface) ] in the catalyst can be measured with XPS (X-ray photoelectron spectroscopy) analysis. The catalyst usually has a core-shell structure in which the core consists of gold particle and the shell consists of silver particle .
The carrier is preferably one on which the catalyst can be supported and which does not change in property under the condition of the process of the present invention. Examples of the carrier include a metal carbonate, a metal oxide and carbon.
Preferable examples of the metal carbonate include an alkali metal carbonate, an alkaline earth metal carbonate and a transition metal carbonate, and the alkaline earth metal carbonate is preferable .
Examples of the alkali metal carbonate include sodium carbonate and potassium carbonate . Examples of the alkaline earth metal carbonate include magnesium carbonate, calcium carbonate, strontium carbonate and barium carbonate, and calcium carbonate, strontium carbonate and barium carbonate are preferable. The alkaline earth metal carbonate having a specific surface area of 1 to 70 m2/g measured by nitrogen adsorption of the BET method is preferable.
As the carrier, the metal carbonate may be used as it is or after fixing particles of the metal carbonate each other using a suitable binder. The metal carbonate may be mixed with a molding agent and molded by extrusion molding, press molding or the like to use the obtained product as the carrier. It is preferred that the metal carbonate is used as it is as the carrier.
A metal oxide having a crystal form of a rock salt structure, a corundum structure, a spinel-type structure, a fluorite-type structure, a wurtzite-type structure, a rutile-type structure, a bixbite-type structure, an ilmenite-type structure, a pseudobrookite-type structure or a perovskite-type structure can be used.
Examples of the metal oxide having a rock salt structure include TiO, VO, MnO and NiO.
Examples of the metal oxide having a corundum structure include α-Α1203 and a-Fe203.
Examples of the metal oxide having a spinel-type structure include ZnAl204, y-Fe203 and SnZn204.
Examples of the metal oxide having a fluorite-type structure include Zr02 and Ce02.
Examples of the metal oxide having a wurtzite-type structure include ZnO.
Examples of the metal oxide having a rutile-type structure include Sn02, Ti02 and Ru02.
Examples of the metal oxide having a bixbite-type structure include p-Fe203.
Examples of the metal oxide having an ilmenite-type structure include FeTi03.
Examples of the metal oxide having a pseudobrookite-type structure include FeTiOs.
Examples of the metal oxide having a perovskite-type structure include CaTi03, SrTi03, BaTi03, CaZr03, SrZr03, BaZr03 and LaA103.
Examples of the carbon include activated carbon, carbon black, graphite and carbon nanotubes, and graphite is preferred.
As the carrier, a silicon compound can be also used, and examples thereof include a water-soluble silicate such as sodium metasilicate and potassium metasilicate, and a porous silicate having silica as a main component such as silica gel, zeolite and mesoporous silicate.
A commercially available carrier may be used as it is,
and such a commercially available carrier may also be used after purifying and molding by a well-known method.
The used amount of the carrier is preferably 0.1 to 200 parts by mass per 1 part by mass of the catalyst.
The catalyst is preferably activated before using for the process of the present invention. The activation of the catalyst is usually conductedby heating the catalyst prepared in the absence of oxygen. The heating temperature of the activation is usually 150 to 300°C.
Next, the process for producing an olefin oxide of the present invention will be illustrated. The process of the present invention comprises reacting an olefin and oxygen in the presence of the above-mentioned catalyst.
The process of the present invention can be performed in a batch-wise reactor or a continuous reactor. From the viewpoint of an industrial process, it is preferably performed in a continuous reactor .
The amount of the. catalyst is preferably 0.00005 mole or more relative to 1 mole of the olefin, and more preferably 0.0001 mole or more in a silver metal equivalent . The upper limit thereof is not limited, and while a larger amount of the olefin oxide can be produced if increasing the amount of the catalyst, the upper limit of the amount of the catalyst is usually adjusted by taking an economic efficiency such as the cost of catalyst into consideration.
Oxygen can be used in combination with an inert gas such as nitrogen and carbon dioxide. Air can be used as oxygen. The amount of oxygen can be appropriately adjusted according to the reaction mode (continuous type or batch type) . The amount of oxygen is preferably in the range of 0.01 to 100 moles relative to 1 mole of the olefin, and more preferably in the range of 0.03 to 30 moles.
The reaction temperature is preferably in the range of 100°C 400°C, and more preferably in the range of 120°C to 300°C.
In this specification, "olefin" means a hydrocarbon having one carbon-carbon double bond, and examples thereof include ethylene, propylene, butene, pentene and hexene, and propylene is preferable.
The olefin can be used in combination with an inert organic gas such as a lower alkane such as methane and ethane. Olefin and oxygen gases can be fed in the form of their mixed gas. Olefin and oxygen gases may be fed with diluent gases . Examples of diluent gases include nitrogen, methane, ethane, propane, carbon dioxide and rare gases such as argon and helium.
The reaction of the olefin and oxygen can be conducted in the presence of a halogen compound, particularly an organic halogenated compound. Examples of the halogen compound include the halogen compounds disclosed in Japanese Unexamined Patent Application Publication No. 2008-184456, and it is preferably an organic chlorinated compound. Examples of the organic chlorinated compound include chloroethane , 1 , 2-dichloroethane , chloromethane and vinyl chloride. The halogen compound is preferably a compound existing in the form of a gas at the temperature and pressure condition in the reaction system of the reaction.
The amount of the halogen compound is preferably 1 to 1000 ppm by volume, and more preferably 1 to 500 ppm by volume based on a total volume of the mixed gas other than steam, i.e. a mixed gas composed of oxygen, the olefin and a dilution gas added as necessary.
The reaction pressure is not limited, and may be selected from those in reducedpressure conditions topressurized conditions . The pressure under pressurized conditions is preferable from the viewpoint of allowing sufficient contact of oxygen and the olefin with the catalyst, it may be a reaction pressure selected from the range of 0.01 to 3 MPa. in absolute pressure, and is more preferably selected from the range of 0.02 to 2 MPa. The reaction pressure is determined by also taking into consideration the
pressure resistibility of the reaction device used in the present productionmethod. The reducedpressure condition means apressure lower than the atmospheric pressure. The pressurized condition means a pressure higher than the atmospheric pressure.
The reaction can be carried out in the presence of water. When the reaction is carried out in the presence of water, water is preferably changed into steam by heating to use, and a mixed gas obtained by mixing steam, oxygen and the olefin is preferably contacted with the catalyst. It is preferable to use water as steam.
The amount of water is preferably in the range of about 0.1 to about 20 moles relative to 1 mole of the olefin, more preferably in the range of 0.2 to 10 moles, and still more preferably in the range of 0.3 to 8 moles. The above-mentioned "amount of water" indicates an amount of water supplied separately from water contained in air in a case of supplying air as oxygen.
Hereinafter, an embodiment of the present production method of a continuous type, which is a favored reaction mode, will be explained .
First, the catalyst in a predetermined amount is filled into a reaction tower equipped with a gas supply port and a gas exhaust port. Suitable heating means may be provided in the reaction tower, and the inside of the reaction tower may be raised in temperature up to a predetermined reaction temperature by such heating means. Subsequently, using a compressor or the like, a source gas containing the olefin and oxygen is supplied from the gas supply port into the reaction tower. By contacting this source gas with the catalyst in the reaction tower, the olefin and oxygen reacts in the presence of the catalyst, and the olefin oxide is generated. Furthermore, the product gas containing the olefin oxide thus generated is exhausted from the gas exhaust port .
The linear velocity of the source gas that is passed through
the inside of a reaction tower is determined so as to make a residence time that allows the source gas and the catalyst to sufficiently generate the olefin oxide.
Although a case of heating means being provided in the reaction tower has been described in the above embodiment, it may be a mode in which the reaction tower may be maintained at ambient temperature, and the source gas may be supplied and then heated up to a predetermined reaction temperature by appropriate heating means, and then supplied into the reaction tower. It may be a mode in which suitable stirring means is provided in the reaction tower, and a source gas is supplied while stirring the catalyst that is present inside the reaction tower.
The olefin oxide thus generated, unreacted olefin and oxygen, and byproducts such as carbon dioxide may be contained in the product gas passing through the reaction tower. In addition, in a case of using the olefin and oxygen after dilution, an inert gas used for dilution may be incorporated. After having collected this product gas, the olefin oxide, which is the objective, can be removed by separation means such as distillation.
Examples of the olefin oxide include ethylene oxide, propylene oxide, butene oxide, pentene oxide and hexene oxide.
Examples
Hereinafter, Examples of the present invention will be described, but the present invention is not to be limited thereto.
[Au/Ag (surface) ] in the catalyst prepared was measured with XPS analysis: The XPS analysis was carried out under the following conditions; The spectra were energy calibrated by taking Si2p peak at 103 eV.
Producer: SPECS
Analyser: PHOIBOS 150MCD-9
X ray source: For BE determination: Al non-monocromatic, lOkV, 50W
Take off angle 0° versus normal
Diameter of the X ray beam 1 cm
No flood gun
Energy resolution: Ag3d5/2 at 368,14eV, FWHM l,22eV at 704Kcps with Pass Energy 20eV; for non monochromatic Al X ray source Vacuum pressure 1*10~9 mbar during spectra acquisition
Preparation Example
A catalyst was prepared according to the method described in Chem. Mater. 2009, 21, 410-418. One (1) g of a commercial silica carrier (Scharlau, 500m2/gr) was added to a 50 mL of ethanol solution containing 2.5 g of APTES (H2N (CH2) 3S1 (OE't) 3 ) . Themixture obtained was refluxed for 24 hours to graft APTES on the silica surface. After being washed with ethanol and dried at 60°C, the solid was dispersed in 16 g of water at room temperature, to which 4 mL of 1.88% by weight HAuCl4 solution was added under stirring during 1.5 hours. After filtration and washing, the recovered solid was added into 10 g of water, to which 10 mL of 0.2 M NaBH4 solution was added under vigorous stirring for reduction of AuCl4 " . After 20 minutes, the solid was recovered by filtration and thoroughly washed with water to remove CI" for the subsequent Ag deposition. After dried at 60°C, the solid was dispersed in 16 g of H20 at room temperature, to which.4 mL of 0.277% by weight AgN03 solution was added under stirring. After filtration and washing, the recovered solid was added into 10 g of water, to which 10 mL of 0.2 MNaBH4 solution was added under vigorous stirring . After 20 minutes, the solid was recovered by filtration and thoroughly washed with water and dried under vacuum (10~3 mbar) .
The obtained catalyst is called as "CAT-1". "CAT-1" was aged for 1 month to obtain a catalyst. This catalyst is called as "CAT-2" . "CAT-1" was calcined at 500°C in air to obtain a catalyst. This catalyst is called as "CAT-3". The nominal total metal loadings were 5% by weight. The results .are shown in Table 1.
Table 1
Examples 1 to 2 and Comparative Example 1
The reaction of propylene and oxygen was conducted using a microreactor connected to a mass spectrometer . The mass analysis was carried out under the following conditions:
MODEL: QMG 220 Ml (Telstar)
Filament current: 1.20 mA
Vacuum pressure: 1*10~6 mbar during acquisition
The reactant mixture was 5 ml/min. of propylene (C3H6) , 2.5 ml/min. of oxygen (O2) , and 22.5 ml/min. of argon (Ar) , which represent a molar ratio C3H6:02= 2:1. The catalysts weight was around 150 mg, diluted in CSi in a 1 : 1 weight ratio . The activation of the catalyst was conducted prior to the reaction.
In order to determine the onset temperature of reaction, product distribution and their evolution with the temperature, we performed temperature programmed surface reaction (TPSR) at a rate of 2°C/min. The activation of the catalyst was done under several conditions (argon or O2 at different temperatures) .
The results are shown in Table 2. In Table 2, "Ar" means argon, "PO" means propylene oxide, "C02" means carbon dioxide, and CO2 and PO are increment values measured relative to reference values of the reactant mixture.
Table 2
Industrial Applicability
According to the present invention, propylene oxide, which is useful as an intermediate material of manufactured products, can be produced from propylene and oxygen with superior propylene oxide selectivity (PO/C02) .
Claims
1. A process for producing an olefin oxide comprising reacting an olefin with oxygen in the presence of a catalyst, wherein the catalyst comprises particles consisting of silver metal and gold metal, and a ratio of gold metal to silver metal of the particles ( [Au/Ag (bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1) :
0<[Au/Ag (surface) ]/ [Au/Ag (bulk)]<0.9 (1)
2. The process according to claim 1 , wherein the catalyst is supported on a carrier.
3. The process according to claim 1, wherein the olefin is propylene and the olefin oxide is propylene oxide.
4. A catalyst for producing an olefin oxide which comprises particles consisting of silver metal and gold metal wherein a ratio of gold metal to silver metal of the particles ( [Au/Ag (bulk) ] ) and a ratio of gold metal to silver metal of the surfaces of the particles ( [Au/Ag (surface) ] ) satisfy the following formula (1) :
0<[Au/Ag (surface) ]/ [Au/Ag (bulk)]<0.9 (1)
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
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CN103706357A (en) * | 2014-01-08 | 2014-04-09 | 南京工业大学 | Preparation method and application of amine functional mesoporous silica-gel-loaded gold catalyst |
WO2018078567A1 (en) * | 2016-10-31 | 2018-05-03 | Sabic Global Technologies B.V. | Catalysts for soft oxidation coupling of methane to ethylene and ethane |
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US5780657A (en) * | 1997-06-23 | 1998-07-14 | Arco Chemical Technology, L.P. | Propylene epoxidation using chloride-containing silver catalysts |
WO1998058921A1 (en) | 1997-06-23 | 1998-12-30 | Arco Chemical Technology, L.P. | Propylene epoxidation using chloride-containing silver catalysts |
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CN103706357A (en) * | 2014-01-08 | 2014-04-09 | 南京工业大学 | Preparation method and application of amine functional mesoporous silica-gel-loaded gold catalyst |
WO2018078567A1 (en) * | 2016-10-31 | 2018-05-03 | Sabic Global Technologies B.V. | Catalysts for soft oxidation coupling of methane to ethylene and ethane |
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