WO2023276406A1 - アルコールの製造方法 - Google Patents
アルコールの製造方法 Download PDFInfo
- Publication number
- WO2023276406A1 WO2023276406A1 PCT/JP2022/017416 JP2022017416W WO2023276406A1 WO 2023276406 A1 WO2023276406 A1 WO 2023276406A1 JP 2022017416 W JP2022017416 W JP 2022017416W WO 2023276406 A1 WO2023276406 A1 WO 2023276406A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- acid
- catalyst
- reactor
- heteropolyacid
- reaction
- Prior art date
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 43
- 239000003054 catalyst Substances 0.000 claims abstract description 128
- 239000011964 heteropoly acid Substances 0.000 claims abstract description 65
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 150000001336 alkenes Chemical class 0.000 claims abstract description 45
- 150000003839 salts Chemical class 0.000 claims abstract description 33
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000011973 solid acid Substances 0.000 claims abstract description 25
- 230000000887 hydrating effect Effects 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims description 55
- 239000002253 acid Substances 0.000 claims description 52
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 40
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 31
- 239000005977 Ethylene Substances 0.000 claims description 31
- CGFYHILWFSGVJS-UHFFFAOYSA-N silicic acid;trioxotungsten Chemical compound O[Si](O)(O)O.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 CGFYHILWFSGVJS-UHFFFAOYSA-N 0.000 claims description 26
- 239000002994 raw material Substances 0.000 claims description 23
- 239000000377 silicon dioxide Substances 0.000 claims description 16
- IYDGMDWEHDFVQI-UHFFFAOYSA-N phosphoric acid;trioxotungsten Chemical compound O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.OP(O)(O)=O IYDGMDWEHDFVQI-UHFFFAOYSA-N 0.000 claims description 14
- 125000004432 carbon atom Chemical group C* 0.000 claims description 12
- DHRLEVQXOMLTIM-UHFFFAOYSA-N phosphoric acid;trioxomolybdenum Chemical compound O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.O=[Mo](=O)=O.OP(O)(O)=O DHRLEVQXOMLTIM-UHFFFAOYSA-N 0.000 claims description 4
- 238000006703 hydration reaction Methods 0.000 abstract description 38
- 238000000034 method Methods 0.000 abstract description 21
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- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 18
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical class [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 12
- -1 rare earth ions Chemical class 0.000 description 12
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- 239000012495 reaction gas Substances 0.000 description 11
- 239000006227 byproduct Substances 0.000 description 10
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 9
- 238000010521 absorption reaction Methods 0.000 description 8
- 150000001879 copper Chemical class 0.000 description 8
- 150000002258 gallium Chemical class 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical class [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 7
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- 229910003002 lithium salt Inorganic materials 0.000 description 7
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical class C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 6
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- 239000011734 sodium Chemical class 0.000 description 6
- SDKPSXWGRWWLKR-UHFFFAOYSA-M sodium;9,10-dioxoanthracene-1-sulfonate Chemical compound [Na+].O=C1C2=CC=CC=C2C(=O)C2=C1C=CC=C2S(=O)(=O)[O-] SDKPSXWGRWWLKR-UHFFFAOYSA-M 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical class [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 5
- 238000004458 analytical method Methods 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 229910052802 copper Inorganic materials 0.000 description 5
- 239000010949 copper Chemical class 0.000 description 5
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical class [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 5
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- 239000010931 gold Chemical class 0.000 description 5
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- 239000000047 product Substances 0.000 description 5
- 159000000000 sodium salts Chemical class 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 4
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- 238000005406 washing Methods 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 3
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- 239000002184 metal Substances 0.000 description 3
- 229910052758 niobium Inorganic materials 0.000 description 3
- 239000010955 niobium Substances 0.000 description 3
- GUCVJGMIXFAOAE-UHFFFAOYSA-N niobium atom Chemical compound [Nb] GUCVJGMIXFAOAE-UHFFFAOYSA-N 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 3
- 229910052721 tungsten Inorganic materials 0.000 description 3
- 239000010937 tungsten Substances 0.000 description 3
- 229910052720 vanadium Inorganic materials 0.000 description 3
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 3
- 229910002012 Aerosil® Inorganic materials 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052684 Cerium Inorganic materials 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 239000005909 Kieselgur Substances 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
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- ZMIGMASIKSOYAM-UHFFFAOYSA-N cerium Chemical compound [Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce] ZMIGMASIKSOYAM-UHFFFAOYSA-N 0.000 description 2
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- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
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- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
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- GUVRBAGPIYLISA-UHFFFAOYSA-N tantalum atom Chemical compound [Ta] GUVRBAGPIYLISA-UHFFFAOYSA-N 0.000 description 2
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- 235000010724 Wisteria floribunda Nutrition 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
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Images
Classifications
-
- 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
- C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
- C07C29/04—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
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- 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
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- 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
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/24—Chromium, molybdenum or tungsten
- B01J23/30—Tungsten
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B41/00—Formation or introduction of functional groups containing oxygen
- C07B41/02—Formation or introduction of functional groups containing oxygen of hydroxy or O-metal groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/08—Ethanol
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B61/00—Other general methods
Definitions
- the present invention relates to a method for producing alcohol through a hydration reaction of olefins using a heteropolyacid catalyst.
- the present invention is particularly suitable for producing ethanol from ethylene.
- Industrial ethanol is an important industrial chemical product that is widely used as an intermediate for organic solvents, raw materials for organic synthesis, disinfectants and chemicals.
- Industrial ethanol can be produced by adding liquid acids such as sulfuric acid, sulfonic acid, zeolite catalysts, metal oxide catalysts such as tungsten, niobium, tantalum, or heteropolyacids such as phosphotungstic acid, silicotungstic acid, or phosphoric acid to silica carriers, diatomaceous earth. It is known to be obtained by a hydration reaction of ethylene in the presence of a solid catalyst supported on a carrier or the like.
- Metal oxide catalysts are known as catalysts for ethylene hydration reactions that do not cause phosphoric acid to flow out, and include zeolite catalysts (Patent Document 1), metal oxide catalysts containing titanium oxide and tungsten oxide as essential components ( Patent Document 2), a metal oxide catalyst containing tungsten and niobium as essential components (Patent Document 3), and the like are known.
- Patent Document 1 metal oxide catalysts containing titanium oxide and tungsten oxide as essential components
- Patent Document 3 a metal oxide catalyst containing tungsten and niobium as essential components
- ethylene hydration reactions using these metal oxide catalysts are less active and less selective than those using phosphoric acid catalysts.
- a solid acid catalyst in which a heteropolyacid is supported on a carrier is known.
- a supported catalyst for ethanol production by a hydration reaction of ethylene with improved performance a catalyst in which a heteropolyacid is supported on fumed silica of a combustion method is disclosed (Patent Document 4).
- Patent Document 5 As a method for improving the performance of heteropolyacid-supported catalysts, use of catalysts in which a heteropolyacid is supported on a clay carrier treated with thermal acid has been proposed (Patent Document 5).
- a silica carrier with specified pore volume, specific surface area, and pore diameter is disclosed as a supported catalyst carrier suitable for the hydration reaction of olefins.
- a catalyst for ethanol production is also exemplified (Patent Document 6).
- An object of the present invention is to provide a method that enables the stable use of a catalyst over a long period of time in the production of alcohol through the hydration reaction of olefins using a heteropolyacid catalyst.
- the present invention relates to the following [1] to [10].
- [1] Using a solid acid catalyst in which a heteropolyacid or a salt thereof is supported on a carrier, a raw material gas containing water and an olefin having 2 to 5 carbon atoms is fed into a reactor equipped with a catalyst layer filled with the solid acid catalyst.
- a method for producing alcohol by continuously supplying and hydrating in the gas phase to obtain alcohol,
- a method for producing alcohol, wherein the pressure loss when the raw material gas passes through the catalyst layer is 350 kPa or less.
- the method for producing alcohol according to [1] wherein the reactor is a multitubular reactor.
- [3] The method for producing alcohol according to [2], wherein the solid acid catalyst is packed in the tube of the multitubular reactor.
- [4] The method for producing alcohol according to [3], wherein the tube of the multitubular reactor has an inner diameter of 40 mm or less.
- the superficial linear velocity of the source gas in the reactor is 0.1 to 1.0 m/s, and the gas hourly space velocity of the source gas in the reactor is 500 to 15000/h.
- [6] The method for producing alcohol according to any one of [1] to [5], wherein the conversion rate of the olefin having 2 to 5 carbon atoms is 2 to 6%.
- [7] The method for producing alcohol according to any one of [1] to [6], wherein the partial pressure of water in the source gas is 0.4 to 0.6 MPa.
- [8] The method for producing alcohol according to any one of [1] to [7], wherein the carrier is silica.
- the heteropolyacid is at least one selected from the group consisting of silicotungstic acid, phosphotungstic acid, phosphomolybdic acid, silicomolybdic acid, silicovanadotungstic acid, phosphovanadotungstic acid, and phosphovanadomolybdic acid [1]
- [10] The method for producing alcohol according to any one of [1] to [9], wherein the olefin having 2 to 5 carbon atoms is ethylene, and the alcohol is ethanol.
- coking of the heteropolyacid catalyst is suppressed in the production of alcohol through the hydration reaction of olefins using a heteropolyacid catalyst, and the catalyst can be used stably over a long period of time.
- the solid acid catalyst of one embodiment is a heteropolyacid or a salt thereof (collectively referred to as a "heteropolyacid catalyst") supported on a carrier, and a catalyst containing a heteropolyacid or a salt thereof as a main active component of the catalyst. is.
- heteropolyacid is an acid composed of a central element and peripheral elements to which oxygen is bonded.
- the central element is usually silicon or phosphorus, but can be selected from any one of the many elements of Groups 1 to 17 of the Periodic Table of the Elements.
- Examples of the central element constituting the heteropolyacid include cupric ions; divalent ions of beryllium, zinc, cobalt, or nickel; trivalent ions of boron, aluminum, gallium, iron, cerium, arsenic, antimony, Ions of phosphorus, bismuth, chromium, or rhodium; ions of tetravalent silicon, germanium, tin, titanium, zirconium, vanadium, sulfur, tellurium, manganese, nickel, platinum, thorium, hafnium, cerium, and other rare earth ions pentavalent phosphorus, arsenic, vanadium, antimony ions; hexavalent tellurium ions; and heptavalent iodine ions, but are not limited thereto.
- peripheral elements include tungsten, molybdenum, vanadium, niobium, and tantalum, but are not limited to these.
- heteropolyacids are known as “polyoxoanions”, “polyoxometal salts", or “metal oxide clusters”.
- Some structures of well-known anions are named after researchers in the field, e.g., Keggin-type structures, Wells-Dawson type structures, and Anderson-Evans-Perloff type structures are known.
- Keggin-type structures e.g., Keggin-type structures
- Wells-Dawson type structures e.g., and Anderson-Evans-Perloff type structures are known.
- Heteropolyacids are usually of high molecular weight, eg, having a molecular weight in the range of 700-8500, and include not only their monomers but also dimer complexes.
- the heteropolyacid salt is not particularly limited as long as it is a metal salt or onium salt in which some or all of the hydrogen atoms of the above heteropolyacid are substituted.
- Examples include, but are not limited to, metal salts of lithium, sodium, potassium, cesium, magnesium, barium, copper, gold, and gallium, and onium salts such as ammonium salts.
- Heteropolyacids have a relatively high solubility in water or other polar solvents such as oxygenated solvents, especially when the heteropolyacid is in the form of the free acid or some salt.
- the solubility of heteropolyacids can be controlled by choosing appropriate counterions.
- heteropolyacids that can be used as catalysts include, but are not limited to: Silicotungstic acid H 4 [SiW 12 O 40 ].xH 2 O Phosphotungstic acid H 3 [PW 12 O 40 ].xH 2 O Phosphomolybdic acid H 3 [PMo 12 O 40 ].xH 2 O Silicomolybdic acid H4[ SiMo12O40 ] .xH2O Sivanadotungstic acid H 4+n [SiV n W 12-n O 40 ].xH 2 O Phosphorvanadotungstic acid H 3+n [PV n W 12-n O 40 ].xH 2 O Phosphovanadomolybdate H 3+n [PV n Mo 12-n O 40 ].xH 2 O Sivanadomolybdate H 4+n [SiV n Mo 12-n O 40 ].xH 2 O Silicomolybdotungstic acid H 4 [SiMo n W 12-n O 40 ].xH 2 O Sil
- the heteropolyacid is preferably silicotungstic acid, phosphotungstic acid, phosphomolybdic acid, silicomolybdic acid, silicobanadotungstic acid, phosphovanadotungstic acid, or phosphovanadomolybdic acid, and silicotungstic acid, phosphotungstic acid, silicobanadotungstic acid More preferred are acids or phosphovanadotungstic acid.
- a method for synthesizing such a heteropolyacid is not particularly limited, and any method may be used.
- a heteropolyacid can be obtained by heating an acidic aqueous solution (about pH 1 to pH 2) containing a salt of molybdic acid or tungstic acid and a heteroatom simple oxygen acid or a salt thereof.
- the heteropolyacid compound can be isolated, for example, by crystallization and separation as a metal salt from the produced heteropolyacid aqueous solution.
- heteropolyacids A specific example of the production of heteropolyacids can be found in 1413 of "New Experimental Chemistry Course 8 Synthesis of Inorganic Compounds (III)" (edited by The Chemical Society of Japan, published by Maruzen Co., Ltd., August 20, 1984, 3rd edition). page, but is not limited to this.
- the structure of the synthesized heteropolyacid can be confirmed by X-ray diffraction, UV, or IR measurement as well as chemical analysis.
- heteropolyacid salts include lithium salts, sodium salts, potassium salts, cesium salts, magnesium salts, barium salts, copper salts, gold salts, gallium salts, and ammonium salts of the above preferred heteropolyacids.
- heteropolyacid salts include lithium silicotungstic acid, sodium silicotungstic acid, cesium silicotungstic acid, copper silicotungstic acid, gold silicotungstic acid, and gallium silicotungstic acid.
- heteropolyacid salts include lithium silicotungstic acid, sodium silicotungstic acid, cesium silicotungstic acid, copper silicotungstic acid, gold silicotungstic acid, gallium silicotungstic acid; Lithium salt of acid, sodium salt of phosphotungstic acid, cesium salt of phosphotungstic acid, copper salt of phosphotungstic acid, gold salt of phosphotungstic acid, gallium salt of phosphotungstic acid; Sodium salt of tungstic acid, cesium salt of siliconvanadotungstic acid, copper salt of siliconvanadotungstic acid, gold salt of siliconvanadotungstic acid, gallium salt of siliconvanadotungstic acid; lithium salt of phosphovanadotungstic acid, phosphovanadotungstic acid , the cesium salt of phosphovanadotungstic acid, the copper salt of phosphovanadotungstic acid, the gold salt of phosphovanadotungstic acid, or the gallium salt of phosphovanadotungstic acid.
- lithium silicotungstic acid As the heteropolyacid salt, lithium silicotungstic acid, cesium silicotungstic acid, lithium phosphotungstic acid, or cesium phosphotungstic acid is particularly suitable.
- the heteropolyacid catalyst can be used as it is, it is preferably supported on a carrier.
- the carrier is preferably at least one selected from the group consisting of silica, diatomaceous earth, titania, activated carbon, alumina, and silica-alumina, more preferably silica.
- the shape of the carrier is not particularly limited.
- spherical, columnar, hollow columnar, plate, elliptical, sheet, and honeycomb shapes can be mentioned. It is preferably spherical, cylindrical, hollow cylindrical or ellipsoidal, more preferably spherical or cylindrical, which facilitates filling the reactor and supporting the catalytically active components.
- the size of the carrier is not particularly limited, but it affects the handling of the solid acid catalyst on which the catalytically active component is supported during production or when the catalyst is filled, the differential pressure after filling the reactor, and the reaction performance of the catalytic reaction. Therefore, it is desirable to have a size that takes these into account.
- the thickness is preferably 1 to 20 mm, more preferably 2 to 10 mm.
- the crushing strength of the carrier is preferably 5 N or more, and 10 N or more. is more preferred.
- the crushing strength is a value when a load is applied to the carrier using a KHT-40N digital hardness tester manufactured by Fujiwara Seisakusho Co., Ltd. and the carrier breaks.
- the specific surface area of the carrier is not limited, but the higher the specific surface area, the higher the activity of the catalyst. preferable.
- the method for supporting the heteropolyacid or its salt on the carrier there is no particular limitation on the method for supporting the heteropolyacid or its salt on the carrier.
- a solution or suspension obtained by dissolving or suspending a heteropolyacid or a salt thereof in a solvent is absorbed into a carrier, and the solvent is evaporated.
- the amount of the heteropolyacid or its salt supported on the carrier can be adjusted, for example, by dissolving the heteropolyacid or its salt in distilled water corresponding to the water absorption amount of the carrier and impregnating the carrier with the solution.
- the amount of the heteropolyacid or its salt supported on the carrier is determined by immersing the carrier in a solution of an excess amount of the heteropolyacid or its salt while moving it moderately, and then filtering the excess heteropolyacid or its salt. It can also be adjusted by removing the salt.
- the volume of the solution or suspension varies depending on the carrier used, the supporting method, etc.
- a solid acid catalyst supported on a carrier can be obtained by placing the carrier impregnated with a heteropolyacid or a salt thereof in a heating oven for several hours to evaporate the solvent.
- the drying method is not particularly limited, and various methods such as a stationary method and a belt conveyor method can be used.
- the amount of the heteropolyacid or its salt supported on the carrier can be accurately measured by chemical analysis such as ICP and XRF.
- the amount of the heteropolyacid or its salt supported on the carrier is preferably 10 to 300 parts by mass, preferably 20 to 200 parts by mass, based on 100 parts by mass of the carrier. more preferred.
- the alcohol is obtained by using a solid acid catalyst in which a heteropolyacid or a salt thereof is supported on a carrier, and a raw material gas containing water and an olefin having 2 to 5 carbon atoms is provided with a catalyst layer filled with a solid acid catalyst. It can be obtained by continuously supplying it to a reactor and causing a hydration reaction in the gas phase.
- R 1 to R 4 each independently represent a hydrogen atom or an alkyl group having 1 to 3 carbon atoms, and the total number of carbon atoms of R 1 to R 4 is 0 to 3.
- the olefins having 2 to 5 carbon atoms that can be used are not particularly limited.
- Examples of olefins having 2 to 5 carbon atoms include ethylene, propylene, n-butene, isobutene, pentene, or mixtures of two or more thereof. Among them, ethylene is more preferable.
- a preferred format is the fixed bed format from the viewpoint of high reaction efficiency and requiring the least energy for separation from the catalyst.
- a solid acid catalyst of one embodiment is packed in a fixed-bed reactor to form a catalyst layer.
- a multi-tubular reactor with good heat removal efficiency is preferable as a fixed bed reactor.
- a reactor with poor heat removal efficiency is not preferable because the temperature difference in the catalyst layer increases.
- a shell-and-tube reactor is equipped with a plurality of tubes as reaction tubes, and the solid acid catalyst can be filled in these tubes to form a catalyst layer.
- the inner diameter of the tubes of the multitubular reactor is preferably 40 mm or less. Moreover, from the viewpoint of uniformly circulating the raw material gas in each tube, it is preferable that the inner diameter and length of each tube are uniform.
- the number of tubes depends on the size of the reactor and can range from a few to thousands.
- a reactor other than a multitubular reactor is used as the fixed bed reactor
- a plurality of small adiabatic reactors and heat exchangers are alternately combined in series to reduce the temperature difference in the catalyst layer. can be made smaller.
- liquid water used as the coolant used to remove heat from the reactor.
- the heat of vaporization of the coolant can efficiently remove heat from the process fluid in the reactor.
- the superficial linear velocity of the source gas flowing through the reactor is preferably 0.1 to 1.0 m/s. If it is 0.1 m/s or more, the overall heat transfer coefficient does not decrease too much, and heat removal efficiency is maintained. If it is 1.0 m/s or less, the pressure loss in the reactor does not become too large, and the collapse of the catalyst or the load increase of the circulating gas compressor hardly occurs.
- the gas space velocity in the reactor is not particularly limited, it is preferably 500 to 15000/hr, more preferably 1000 to 4000/hr from the viewpoint of energy and reaction efficiency. If the gas space velocity is 500/hr or more, the amount of catalyst used can be effectively reduced, and if it is 15000/hr or less, the amount of gas circulation can be reduced. If so, the production of alcohol can be carried out more efficiently.
- reaction pressure in the olefin hydration reaction using a heteropolyacid catalyst there is no limit to the reaction pressure in the olefin hydration reaction using a heteropolyacid catalyst. Since the hydration reaction of olefins is a reaction that reduces the number of molecules, it is generally advantageous to carry it out at high pressure.
- a preferable reaction pressure is 0.5 to 7.0 MPaG, more preferably 1.5 to 4.0 MPaG. "G" means gauge pressure. If the reaction pressure is 0.5 MPaG or more, a sufficient reaction rate can be obtained. Installation is no longer required, and further energy costs can be further reduced.
- the partial pressure of water in the source gas is preferably 0.4-0.6 MPa.
- the pressure loss when the raw material gas passes through the catalyst layer of the reactor is the differential pressure between the static pressure of the raw material gas at the catalyst layer inlet and the static pressure of the post-reaction gas (reactant gas) at the catalyst layer outlet.
- the value of the pressure loss when the raw material gas passes through the catalyst layer of the reactor is 350 kPa or less, more preferably 200 kPa or less, and even more preferably 50 kPa or less.
- the pressure loss value is 350 kPa or less, the difference in partial pressure of each raw material component in the vertical direction of the catalyst layer can be reduced.
- the pressure is the pressure difference between the static pressure of the chamber that distributes the raw material gas to multiple tubes, which are reaction tubes, and the static pressure of the chamber that collects the reaction gas from the multiple tube outlets. loss.
- the reaction temperature for the olefin hydration reaction using a heteropolyacid catalyst is not particularly limited, and can be carried out at a wide range of temperatures.
- a preferable reaction temperature is 100 to 550°C, more preferably 150 to 350°C, considering the thermal stability of the heteropolyacid or its salt and the temperature at which water, one of the raw materials, does not condense.
- the hydration reaction of olefins using a heteropolyacid catalyst is an equilibrium reaction, and the maximum conversion rate of olefins is the equilibrium conversion rate.
- the equilibrium conversion rate in the production of ethanol by hydration of ethylene is calculated to be 7.5% at a temperature of 200°C and a pressure of 2.0 MPaG. Therefore, in the process of alcohol production by hydration of olefins, the maximum conversion is determined by the equilibrium conversion.
- the olefin conversion rate in the olefin hydration reaction is preferably 2 to 6%.
- a conversion rate of 2% or more is economically advantageous because the amount of unreacted ethylene circulated can be reduced.
- the conversion rate is 6% or less, the difference from the equilibrium conversion rate can be made to the extent necessary to maintain the reaction rate, and severe conditions such as high pressure are not essential. Therefore, it is advantageous from the economic and facility aspects.
- the loss of olefin can be reduced by recycling unreacted olefin to the reactor.
- the olefins may be isolated from the process fluid leaving the reactor and recycled, or may be recycled together with other inert components.
- Technical grade olefins often contain very small amounts of paraffins.
- ethylene gas a portion of the recovered reaction gas (ethylene gas) is should be purged out of the system.
- the product alcohols undergo a dehydration reaction, and an ether compound may be produced as a by-product.
- an ether compound may be produced as a by-product.
- diethyl ether is produced as a by-product. This diethyl ether is considered to be produced by a dehydration reaction from two molecules of ethanol, and when ethanol is produced by a hydration reaction of ethylene, it significantly reduces the yield of the reaction.
- diethyl ether is converted to ethanol, and ethanol can be produced from ethylene with extremely high efficiency.
- the method of recycling the by-produced ether compound to the reactor is not particularly limited. There is a method of recycling to the reactor as a component.
- the alcohol produced is dissolved in a large amount of water that has not been converted as a reaction raw material, and is sent to the separation and purification process along with other by-products.
- the separation and purification process alcohol, water, and other by-products are separated, and the alcohol whose purity reaches a certain level or higher through purification becomes the product.
- the water obtained at the same time may be disposed of as waste water, but from the perspective of environmental impact and load, it is desirable to recycle it within the process and use it again as a raw material for the reaction.
- silica carrier Fumed silica: Aerosil (trademark) 300 (Nippon Aerosil Co., Ltd.) 40 parts by mass Silica gel: CARiACT G6 (Fuji Silysia Chemical Co., Ltd.) 60 parts by mass Colloidal silica: Snowtex O (Nissan Chemical Co., Ltd.) After kneading 40 parts by mass in a kneader, methyl cellulose: Metolose (registered trademark) SM-4000 (Shin-Etsu Chemical Co., Ltd.) as water and additives, and Celander (registered trademark) YB-132A (Yuken) as a resin binder. Kogyo Co., Ltd.) was put into a kneader and further kneaded to prepare a kneaded product.
- the kneaded material was put into an extruder equipped with a die having a circular hole of 3 mm ⁇ at the tip.
- the kneaded product was extruded from an extruder, and the extruded intermediate product was cut with a cutter to a size of 3 mm to obtain a cylindrical pre-fired compact.
- the obtained pre-fired compact was formed into a spherical shape using Marumerizer (registered trademark) and pre-dried at 70° C. for 24 hours or longer.
- a sintering treatment was performed at 820° C. in an air atmosphere and cooled to obtain a silica carrier.
- the water absorption of the obtained silica carrier was measured by the following method. (1) About 5 g of the carrier was weighed (W1 (g)) with a balance and placed in a 100 mL beaker. (2) About 15 mL of pure water (ion-exchanged water) was added to the beaker so as to completely cover the carrier. (3) Leave for 30 minutes. (4) The carrier and pure water were poured over the wire mesh, the pure water was drained off by the wire mesh, and the carrier was taken out. (5) Water adhering to the surface of the carrier was removed by lightly pressing with a paper towel until the surface became dull.
- the total mass of the carrier obtained in (5) and pure water was measured (W2 (g)).
- the aqueous solution of silicotungstic acid is transferred to a 200 mL volumetric flask, then 100 mL of the weighed silica carrier is added to the 200 mL volumetric flask, and the volumetric flask is stirred so that the aqueous solution of silicotungstic acid spreads over the entire carrier.
- the contents were mixed to support the silicotungstic acid on the silica carrier.
- the silica carrier supporting silicotungstic acid was transferred to a magnetic dish, air-dried for 1 hour, and then dried for 5 hours in a hot-air dryer adjusted to 150°C. After drying, it was transferred into a desiccator and cooled to room temperature to obtain a heteropolyacid catalyst (solid acid catalyst).
- reaction liquid After the reaction started, hot water was circulated on the shell side of the double-tube reactor to remove the heat of reaction.
- the reaction gas after passing through the reactor was cooled, and the condensed reaction liquid, the reaction gas passed through the scrubber after removing the condensate (reaction liquid), and the washing water of the scrubber were each sampled for a certain period of time.
- the sampled reaction solution, reaction gas, and washing water were analyzed using a gas chromatography analyzer and a Karl Fischer analyzer by the method described below, and the reaction results were calculated.
- Ethylene conversion rate and acetaldehyde selectivity were determined by the following equations.
- Ethylene conversion rate (mol%) (number of moles of ethylene reacted/number of moles of ethylene supplied) x 100
- Acetaldehyde selectivity (mol%) (number of moles of acetaldehyde produced/number of moles of ethylene supplied) x 100
- Example 1 A double-tube reactor (made of SUS316, inner diameter 34 mm, length 6.7 m) was filled with 3.1 L of a heteropolyacid catalyst (solid acid catalyst). At this time, the height of the catalyst layer was 3.6 m. After replacing the inside of the reactor with nitrogen gas, the pressure was increased to 2.4 MPaG. Then, the reactor is heated to 180° C., and when the temperature is stabilized, the amount of water vaporized by the evaporator is such that the GHSV (gas hourly space velocity) is 3000/hr and the molar ratio of water to ethylene is 0.3. and ethylene, diethyl ether (3% by volume) in a balanced amount before and after the reactor, and nitrogen gas (13% by volume) as an inert gas were fed into the reactor to carry out a hydration reaction of ethylene.
- GHSV gas hourly space velocity
- the pressure of the raw material gas at the inlet of the reaction tube was maintained at 2.4 MPaG by automatic control of the pressure regulating valve. After the raw material gas was fed and the temperature stabilized, the average temperature of the catalyst layer was adjusted so that the ethylene conversion rate was 4.1%. The average temperature was 190°C. The superficial linear velocity of the source gas was 0.20 m/s. Moreover, the partial pressure of water in the source gas was 0.48 MPa.
- reaction liquid, cleaning liquid, and reaction gas from which the reaction liquid had been removed were sampled.
- the obtained reaction liquid, cleaning liquid, and reaction gas were each analyzed by the above methods, and the reaction performance of the catalyst was calculated from the mass, gas flow rate, and analysis results.
- Example 2 A hydration reaction of ethylene was carried out in the same manner as in Example 1, except that 5.7 L of the heteropolyacid catalyst (solid acid catalyst) was charged. The average temperature of the catalyst layer was adjusted so that the conversion of ethylene was 4.1%. The average temperature was 190°C. As in Example 1, the GHSV (gas hourly space velocity) was set to 3000/hr, and the superficial linear velocity of the source gas was 0.37 m/s. The pressure loss of the source gas was 200 kPa. In addition, the reaction results were calculated in the same manner as in Example 1, and the transition of the reaction results over a period of one year (change over time in selectivity of acetaldehyde, a typical by-product) was predicted. The results are shown in Table 1 and FIG.
- Example 1 A hydration reaction of ethylene was carried out in the same manner as in Example 1, except that 6.6 L of the heteropolyacid catalyst (solid acid catalyst) was charged. The pressure loss of the source gas was 400 kPa. The average temperature of the catalyst layer was 190° C., the GHSV (gas hourly space velocity) was 3000/hr, and the superficial linear velocity was 0.43 m/s.
- the reaction results were calculated in the same manner as in Example 1, and the transition of the reaction results over a period of one year (change over time in selectivity of acetaldehyde, a typical by-product) was predicted. The results are shown in Table 1 and FIG.
- the present invention reduces the pressure loss when the raw material gas passes through the catalyst layer in the production of alcohol by the hydration reaction of olefins using a heteropolyacid catalyst, so that the catalyst can be used stably for a long period of time, It is industrially useful because it is economically advantageous.
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Abstract
Description
[1]
ヘテロポリ酸又はその塩が担体に担持された固体酸触媒を用い、前記固体酸触媒が充填された触媒層を備えた反応器へ、水と炭素原子数2~5のオレフィンとを含む原料ガスを連続的に供給し、気相中で水和反応させてアルコールを得るアルコールの製造方法であって、
前記原料ガスが前記触媒層を通過する際の圧力損失が350kPa以下である、アルコールの製造方法。
[2]
前記反応器は、多管式反応器である、[1]に記載のアルコールの製造方法。
[3]
前記固体酸触媒は、前記多管式反応器のチューブに充填されている、[2]に記載のアルコールの製造方法。
[4]
前記多管式反応器の前記チューブの内径は、40mm以下である、[3]に記載のアルコールの製造方法。
[5]
前記原料ガスの前記反応器内における空塔線速度は、0.1~1.0m/sであり、かつ前記原料ガスの前記反応器内におけるガス空間速度は、500~15000/hである、[1]~[4]のいずれか一態様に記載のアルコールの製造方法。
[6]
前記炭素原子数2~5のオレフィンの転化率は、2~6%である、[1]~[5]のいずれか一態様に記載のアルコールの製造方法。
[7]
前記原料ガスにおける水の分圧は、0.4~0.6MPaである、[1]~[6]のいずれか一態様に記載のアルコールの製造方法。
[8]
前記担体は、シリカである、[1]~[7]のいずれか一態様に記載のアルコールの製造方法。
[9]
前記ヘテロポリ酸は、ケイタングステン酸、リンタングステン酸、リンモリブデン酸、ケイモリブデン酸、ケイバナドタングステン酸、リンバナドタングステン酸、及びリンバナドモリブデン酸からなる群より選ばれる少なくとも一種である、[1]~[8]のいずれか一態様に記載のアルコールの製造方法。
[10]
前記炭素原子数2~5のオレフィンはエチレンであり、前記アルコールはエタノールである、[1]~[9]のいずれか一態様に記載のアルコールの製造方法。
一実施形態の固体酸触媒は、ヘテロポリ酸又はその塩(併せて「ヘテロポリ酸触媒」という)が担体に担持されたものであり、触媒の主要な活性成分として、ヘテロポリ酸又はその塩を含む触媒である。
ヘテロポリ酸とは、中心元素、及び酸素が結合した周辺元素からなる酸である。中心元素は、通常ケイ素又はリンであるが、元素の周期表の第1族~第17族の多種の元素から選ばれる任意の一つから選択することができる。
ケイタングステン酸 H4[SiW12O40]・xH2O
リンタングステン酸 H3[PW12O40]・xH2O
リンモリブデン酸 H3[PMo12O40]・xH2O
ケイモリブデン酸 H4[SiMo12O40]・xH2O
ケイバナドタングステン酸 H4+n[SiVnW12-nO40]・xH2O
リンバナドタングステン酸 H3+n[PVnW12-nO40]・xH2O
リンバナドモリブデン酸 H3+n[PVnMo12-nO40]・xH2O
ケイバナドモリブデン酸 H4+n[SiVnMo12-nO40]・xH2O
ケイモリブドタングステン酸 H4[SiMonW12-nO40]・xH2O
リンモリブドタングステン酸 H3[PMonW12-nO40]・xH2O
(式中、nは1~11の整数であり、xは1以上の整数である。)
ヘテロポリ酸触媒はそのままでも使用することができるが、担体に担持して使用することが好ましい。担体は、シリカ、珪藻土、チタニア、活性炭、アルミナ、及びシリカアルミナからなる群より選ばれる少なくとも一種であることが好ましく、シリカであることがより好ましい。
次に、ヘテロポリ酸触媒を用いたオレフィンの水和反応によるアルコールの製造方法について説明する。アルコールは、ヘテロポリ酸又はその塩が担体に担持された固体酸触媒を用いて、水と炭素原子数2~5のオレフィンとを含む原料ガスを、固体酸触媒が充填された触媒層を備えた反応器へ連続的に供給し、気相中で水和反応させることで得ることができる。
反応器内を流れる原料ガスの空塔線速度は、0.1~1.0m/sであることが好ましい。0.1m/s以上であれば、総括伝熱係数が低下しすぎることがなく、除熱効率が保たれる。1.0m/s以下であれば、反応器内の圧力損失が大きくなりすぎず、触媒の圧壊又は循環ガス圧縮機の負荷増加が起こりにくい。なお、空塔線速度は、下記計算式(1)により得られる。
(空塔線速度[m/s])=(実ガス流量[m3/s])÷(反応器断面積[m2]) (1)
(ガス空間速度[/s])=(ガス流量[Nm3/s])÷(触媒充填量[m3]) (2)
フュームドシリカ:Aerosil(商標)300(日本アエロジル株式会社) 40質量部、シリカゲル:CARiACT G6(富士シリシア化学株式会社) 60質量部、コロイダルシリカ:スノーテックスO(日産化学株式会社) 40質量部を、ニーダーにて混練した後、水及び添加剤としてメチルセルロース:メトローズ(登録商標)SM-4000(信越化学工業株式会社)と、樹脂系バインダーとしてセランダー(登録商標)YB-132A(ユケン工業株式会社)をニーダーに適量入れて更に混練し、混練物を調製した。
得られたシリカ担体につき、以下の方法でその吸水率を測定した。
(1)担体約5gを天秤で計量(W1(g))し、100mLのビーカーに入れた。
(2)担体を完全に覆うように、純水(イオン交換水)約15mLをビーカーに加えた。
(3)30分間放置した。
(4)金網の上に担体と純水とを流して、金網によって純水をきり、担体を取り出した。
(5)担体の表面に付着した水を、表面の光沢がなくなるまで紙タオルで軽く押して除去した。
(6)(5)で得られた担体+純水の合計質量を測定した(W2(g))。
(7)以下の式を用いて、担体の吸水率を算出した。
吸水率(g-水/g-担体)(%)=(W2-W1)/W1×100
したがって、担体の吸水量(g)は、「担体の吸水率(g-水/g-担体)(%)×使用した担体の質量(g)」により計算できる。
市販のKeggin型ケイタングステン酸・26水和物(H4SiW12O40・26H2O;日本無機化学工業株式会社) 40.7gを、100mLのビーカーにはかりとり、少量の蒸留水を加えてケイタングステン酸を溶解させた後、200mLのメスシリンダーに移液した。次いで、メスシリンダーのケイタングステン酸溶液の液量が、担持するシリカ担体の吸水率の95%になるように蒸留水を加え、全体が均一になるように撹拌した。撹拌後、ケイタングステン酸の水溶液を、200mLのメスフラスコに移液し、次いで、秤量したシリカ担体 100mLを200mLメスフラスコに投入し、ケイタングステン酸の水溶液が担体全体に行きわたるように、メスフラスコ内を混合し、ケイタングステン酸をシリカ担体に担持させた。ケイタングステン酸が担持されたシリカ担体を磁性皿に移し、1時間風乾させた後、150℃に調節した熱風乾燥器で5時間乾燥させた。乾燥後、デシケーター内に移し、室温になるまで冷却し、ヘテロポリ酸触媒(固体酸触媒)を得た。
実際の多管式反応器を想定したサイズの二重管式反応器(SUS316製、内径34mm、長さ6.7m)に、所定量の前記ヘテロポリ酸触媒(固体酸触媒)を充填した。二重管式反応器のシェル側にスチームコンデンセート(高圧の熱水)をポンプにて送給し、チューブ側の触媒層を所定の温度とした。所定の圧力まで昇圧したのち、蒸発器により気化した所定量の水、及び所定量のエチレンを、反応器に導入した。
サンプリングした反応ガスは、ガスクロマトグラフィー装置(装置名:7890、アジレント(Agilent)・テクノロジー社)を使用し、複数のカラムと二つの検出器によるシステムプログラムにて、以下の条件で分析した。
・ガスクロマトグラフィー条件:
オーブン:40℃で3分間保持後、20℃/分で200℃まで昇温
キャリアガス:ヘリウム
スプリット比:10:1
・使用カラム:アジレント・テクノロジー社
HP-1:2m
GasPro:30m×320μm
DB-624:60m×320μm×1.8μm
・検出器:
フロント検出器:FID(ヒーター:230℃、水素流量40mL/分、空気流量400L/分)
バック検出器:FID(ヒーター:230℃、水素流量40mL/分、空気流量400L/分)
Aux検出器:TCD(ヒーター:230℃、リファレンス流量45mL/分、メークアップ流量2mL/分)
サンプリングした反応液及び洗浄水は、ガスクロマトグラフィー装置(装置名:6850、アジレント(Agilent)・テクノロジー社)を使用して分析した。
・使用カラム:PoraBONDQ 25m×0.53mmID×10μm
・オーブン温度:100℃で2分間保持後、5℃/分で240℃まで昇温
・インジェクション温度:250℃
・検出器温度:300℃
・検出器:FID
反応液中の水濃度は、カールフィッシャー分析装置(三菱化学株式会社)で分析した。
エチレン転化率、及びアセトアルデヒド選択率は、次の式にて求めた。
エチレン転化率(モル%)=(反応したエチレンのモル数/供給したエチレンのモル数)×100
アセトアルデヒド選択率(モル%)=(生成したアセトアルデヒドのモル数/供給したエチレンのモル数)×100
ヘテロポリ酸触媒(固体酸触媒)3.1Lを、二重管式反応器(SUS316製、内径34mm、長さ6.7m)に充填した。このとき、触媒層の高さは3.6mであった。反応器内を窒素ガスで置換した後、2.4MPaGまで昇圧した。次いで、反応器を180℃に加熱し、温度が安定した段階で、GHSV(ガス空間速度)が3000/hr、エチレンに対する水のモル比が0.3となる量の、蒸発器により気化した水とエチレン、及び反応器前後でバランスする量のジエチルエーテル(3体積%)、並びに不活性ガスとして窒素ガス(13体積%)を、反応器にフィードして、エチレンの水和反応を行った。
ヘテロポリ酸触媒(固体酸触媒)5.7Lを充填した以外は、実施例1と同様にして、エチレンの水和反応を行った。エチレンの転化率が4.1%となるよう、触媒層の平均温度を調整した。平均温度は190℃であった。実施例1と同様にGHSV(ガス空間速度)を3000/hrとし、原料ガスの空塔線速度は0.37m/sとなった。原料ガスの圧力損失は200kPaであった。また、実施例1と同様に、反応成績を算出するとともに、1年間の反応成績の推移(代表的な副生物であるアセトアルデヒド選択率の経時変化)を予測した。その結果を、表1及び図1に示す。
ヘテロポリ酸触媒(固体酸触媒)6.6Lを充填した以外は、実施例1と同様にして、エチレンの水和反応を行った。原料ガスの圧力損失は400kPaであった。触媒層の平均温度は190℃、GHSV(ガス空間速度)は3000/hr、空塔線速度は0.43m/sであった。また、実施例1と同様に、反応成績を算出するとともに、1年間の反応成績の推移(代表的な副生物であるアセトアルデヒド選択率の経時変化)を予測した。その結果を、表1及び図1に示す。
比較例1では、触媒層を通過する際の原料ガスの圧力損失が400kPaと高く、副生物であるアセトアルデヒドの選択率が高くなっている。アセトアルデヒドが生成すると、触媒表面上において重合してコークとなり、触媒の反応活性を低下させたり選択性を悪化させたりするため、触媒を長期間にわたって安定的に使用することができなくなる。実施例1~2の結果から、原料ガスが触媒層を通過する際の圧力損失を低減することで、アセトアルデヒド選択率が低減されており、本条件は触媒を長期間にわたって安定して使用するために有利であることがわかる。
実施例1~2では、1年間を通して低いアセトアルデヒド選択率を維持でき、アルコールを長期間にわたって安定的に製造できるといえる。比較例1では、アセトアルデヒド選択率の上昇速度が大きく、触媒を安定して使用できる目安であるアセトアルデヒド選択率1%を超えてしまう。
Claims (10)
- ヘテロポリ酸又はその塩が担体に担持された固体酸触媒を用い、前記固体酸触媒が充填された触媒層を備えた反応器へ、水と炭素原子数2~5のオレフィンとを含む原料ガスを連続的に供給し、気相中で水和反応させてアルコールを得るアルコールの製造方法であって、
前記原料ガスが前記触媒層を通過する際の圧力損失が350kPa以下である、アルコールの製造方法。 - 前記反応器は、多管式反応器である、請求項1に記載のアルコールの製造方法。
- 前記固体酸触媒は、前記多管式反応器のチューブに充填されている、請求項2に記載のアルコールの製造方法。
- 前記多管式反応器の前記チューブの内径は、40mm以下である、請求項3に記載のアルコールの製造方法。
- 前記原料ガスの前記反応器内における空塔線速度は、0.1~1.0m/sであり、かつ前記原料ガスの前記反応器内におけるガス空間速度は、500~15000/hである、請求項1~4のいずれか一項に記載のアルコールの製造方法。
- 前記炭素原子数2~5のオレフィンの転化率は、2~6%である、請求項1~4のいずれか一項に記載のアルコールの製造方法。
- 前記原料ガスにおける水の分圧は、0.4~0.6MPaである、請求項1~4のいずれか一項に記載のアルコールの製造方法。
- 前記担体は、シリカである、請求項1~4のいずれか一項に記載のアルコールの製造方法。
- 前記ヘテロポリ酸は、ケイタングステン酸、リンタングステン酸、リンモリブデン酸、ケイモリブデン酸、ケイバナドタングステン酸、リンバナドタングステン酸、及びリンバナドモリブデン酸からなる群より選ばれる少なくとも一種である、請求項1~4のいずれか一項に記載のアルコールの製造方法。
- 前記炭素原子数2~5のオレフィンはエチレンであり、前記アルコールはエタノールである、請求項1~4のいずれか一項に記載のアルコールの製造方法。
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JP2010179923A (ja) * | 2009-02-03 | 2010-08-19 | Sumitomo Chemical Co Ltd | 貯留容器 |
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