WO2022230791A1 - プロピレンの製造方法 - Google Patents
プロピレンの製造方法 Download PDFInfo
- Publication number
- WO2022230791A1 WO2022230791A1 PCT/JP2022/018666 JP2022018666W WO2022230791A1 WO 2022230791 A1 WO2022230791 A1 WO 2022230791A1 JP 2022018666 W JP2022018666 W JP 2022018666W WO 2022230791 A1 WO2022230791 A1 WO 2022230791A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- silica
- catalyst
- propylene
- alumina
- alumina catalyst
- Prior art date
Links
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 96
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 80
- 239000003054 catalyst Substances 0.000 claims abstract description 167
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 112
- 239000002994 raw material Substances 0.000 claims abstract description 51
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 claims abstract description 50
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 238000010304 firing Methods 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims description 25
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 23
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims description 22
- 150000001336 alkenes Chemical class 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 10
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 27
- 239000000377 silicon dioxide Substances 0.000 abstract description 12
- 229910052681 coesite Inorganic materials 0.000 abstract 1
- 229910052593 corundum Inorganic materials 0.000 abstract 1
- 229910052906 cristobalite Inorganic materials 0.000 abstract 1
- 235000012239 silicon dioxide Nutrition 0.000 abstract 1
- 229910052682 stishovite Inorganic materials 0.000 abstract 1
- 229910052905 tridymite Inorganic materials 0.000 abstract 1
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 1
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 62
- 239000007788 liquid Substances 0.000 description 32
- 239000000843 powder Substances 0.000 description 30
- 238000006243 chemical reaction Methods 0.000 description 29
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 27
- 239000007789 gas Substances 0.000 description 25
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 20
- 239000011521 glass Substances 0.000 description 16
- 238000001354 calcination Methods 0.000 description 14
- 239000000499 gel Substances 0.000 description 14
- 208000005156 Dehydration Diseases 0.000 description 13
- 230000018044 dehydration Effects 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 12
- 238000004817 gas chromatography Methods 0.000 description 12
- 239000006200 vaporizer Substances 0.000 description 12
- 238000010438 heat treatment Methods 0.000 description 11
- 239000000203 mixture Substances 0.000 description 11
- WWUVJRULCWHUSA-UHFFFAOYSA-N 2-methyl-1-pentene Chemical compound CCCC(C)=C WWUVJRULCWHUSA-UHFFFAOYSA-N 0.000 description 10
- 238000004458 analytical method Methods 0.000 description 10
- 239000012535 impurity Substances 0.000 description 10
- 238000002354 inductively-coupled plasma atomic emission spectroscopy Methods 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 239000006227 byproduct Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 9
- 238000011049 filling Methods 0.000 description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 8
- XNDZQQSKSQTQQD-UHFFFAOYSA-N 3-methylcyclohex-2-en-1-ol Chemical compound CC1=CC(O)CCC1 XNDZQQSKSQTQQD-UHFFFAOYSA-N 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- BOTDANWDWHJENH-UHFFFAOYSA-N Tetraethyl orthosilicate Chemical compound CCO[Si](OCC)(OCC)OCC BOTDANWDWHJENH-UHFFFAOYSA-N 0.000 description 7
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- 239000011230 binding agent Substances 0.000 description 6
- -1 polypropylene, propylene Polymers 0.000 description 6
- 229910052573 porcelain Inorganic materials 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- 229910052782 aluminium Inorganic materials 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 238000000465 moulding Methods 0.000 description 5
- 241000209094 Oryza Species 0.000 description 4
- 235000007164 Oryza sativa Nutrition 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 235000009566 rice Nutrition 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- 239000006259 organic additive Substances 0.000 description 3
- 230000002194 synthesizing effect Effects 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N Diisopropyl ether Chemical compound CC(C)OC(C)C ZAFNJMIOTHYJRJ-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- MRELNEQAGSRDBK-UHFFFAOYSA-N lanthanum(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[La+3].[La+3] MRELNEQAGSRDBK-UHFFFAOYSA-N 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 150000003377 silicon compounds Chemical class 0.000 description 2
- 238000003980 solgel method Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- DNIAPMSPPWPWGF-VKHMYHEASA-N (+)-propylene glycol Chemical compound C[C@H](O)CO DNIAPMSPPWPWGF-VKHMYHEASA-N 0.000 description 1
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 description 1
- DNIAPMSPPWPWGF-GSVOUGTGSA-N (R)-(-)-Propylene glycol Chemical compound C[C@@H](O)CO DNIAPMSPPWPWGF-GSVOUGTGSA-N 0.000 description 1
- YPFDHNVEDLHUCE-UHFFFAOYSA-N 1,3-propanediol Substances OCCCO YPFDHNVEDLHUCE-UHFFFAOYSA-N 0.000 description 1
- BEQGRRJLJLVQAQ-UHFFFAOYSA-N 3-methylpent-2-ene Chemical compound CCC(C)=CC BEQGRRJLJLVQAQ-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- ZZSNKZQZMQGXPY-UHFFFAOYSA-N Ethyl cellulose Chemical compound CCOCC1OC(OC)C(OCC)C(OCC)C1OC1C(O)C(O)C(OC)C(CO)O1 ZZSNKZQZMQGXPY-UHFFFAOYSA-N 0.000 description 1
- 239000001856 Ethyl cellulose Substances 0.000 description 1
- XOBKSJJDNFUZPF-UHFFFAOYSA-N Methoxyethane Chemical compound CCOC XOBKSJJDNFUZPF-UHFFFAOYSA-N 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- 235000010724 Wisteria floribunda Nutrition 0.000 description 1
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- OWBTYPJTUOEWEK-UHFFFAOYSA-N butane-2,3-diol Chemical compound CC(O)C(C)O OWBTYPJTUOEWEK-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 229910052570 clay Inorganic materials 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 1
- 150000002009 diols Chemical class 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 229920001249 ethyl cellulose Polymers 0.000 description 1
- 235000019325 ethyl cellulose Nutrition 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 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
- 238000005470 impregnation Methods 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000691 measurement method Methods 0.000 description 1
- DNIAPMSPPWPWGF-UHFFFAOYSA-N monopropylene glycol Natural products CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 238000006384 oligomerization reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920000166 polytrimethylene carbonate Polymers 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- WHFQAROQMWLMEY-UHFFFAOYSA-N propylene dimer Chemical group CC=C.CC=C WHFQAROQMWLMEY-UHFFFAOYSA-N 0.000 description 1
- 235000013772 propylene glycol Nutrition 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 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
- 238000001291 vacuum drying Methods 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
- C07C1/24—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by elimination of water
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B61/00—Other general methods
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/12—Silica and alumina
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a method for producing propylene by dehydrating propanol using a catalyst.
- Propylene is used as a raw material for polypropylene, propylene oxide, aromatic hydrocarbons, aromatic alcohols, etc.
- a method for producing propylene a method of dehydrating isopropanol (IPA) or normal propanol (NPA) is known.
- IPA isopropanol
- NPA normal propanol
- Patent Document 1 discloses a method for producing propylene using silica gel supporting 1000 to 10000 ppm by mass of aluminum element as an IPA dehydration catalyst.
- Non-Patent Document 1 discloses that when propylene is produced using silica-alumina as an IPA dehydration catalyst, the presence of a large amount of water in IPA, which is a raw material, reduces the dehydration rate of IPA. .
- the present invention has been made in view of the above problems, and aims to provide a method for efficiently producing propylene from propanol containing a large amount of water.
- the present inventors have made intensive studies and found that propanol containing a large amount of water can be obtained by using a catalyst containing silica alumina containing Al 2 O 3 and SiO 2 in a specific ratio. can be efficiently converted into propylene by a dehydration reaction, leading to the completion of the present invention.
- the present invention includes the following configurations.
- ⁇ 3> The method for producing propylene according to ⁇ 1> or ⁇ 2>, wherein the temperature of the catalyst layer containing the catalyst in the dehydration reaction step is 450° C. or less.
- ⁇ 4> In the fluid produced in the dehydration reaction step, at least one of the olefins represented by the following general formula (1) or (2) is present in a molar ratio with respect to the amount of propylene contained in the fluid: The method for producing propylene according to any one of ⁇ 1> to ⁇ 3>, wherein the amount is 0.1 or less.
- R 1 , R 2 and R 3 are a methyl group and the rest are hydrogen.
- a method for producing propylene according to an embodiment of the present invention uses a catalyst containing silica alumina having a SiO 2 content of 3 to 80 in molar ratio to Al 2 O 3 to prepare a raw material containing propanol and water.
- the catalyst containing silica-alumina is produced by a production method including a step of calcining at a calcination temperature of 400° C. or higher and 950° C. or lower. It can also be said that the molar ratio of SiO 2 to Al 2 O 3 in the silica alumina is 3-80.
- the method for producing propylene according to one embodiment of the present invention is also referred to as the present production method.
- a catalyst containing silica-alumina is also called a silica-alumina catalyst.
- the silica-alumina catalyst is used as a dehydration catalyst in the present production method.
- the silica-alumina catalyst By using the silica-alumina catalyst, propanol can be efficiently dehydrated to produce propylene even when propanol as a raw material contains a large amount of water.
- the use of the silica-alumina catalyst enables the dehydration reaction of propanol at low temperatures, thereby suppressing the production of by-products such as olefins having 6 carbon atoms (C6 olefins). The resulting carbon deposition during propylene production can be suppressed.
- the raw material contains water, it serves as a heat carrier for the heat of reaction, making it possible to make the temperature in the reaction system more uniform during the production of propylene (relaxation of temperature distribution), thereby improving industrial usability. .
- IPA isopropanol
- IPA isopropanol
- IPA may be converted to propylene by either intramolecular dehydration or intermolecular dehydration.
- Propylene is produced directly from IPA when intramolecular dehydration of IPA is performed.
- DIPE diisopropyl ether
- the silica-alumina catalyst used in the dehydration reaction step of this production method is produced by a production method including a step of firing at a firing temperature of 400° C. or higher and 950° C. or lower.
- the method for producing propylene may include a step of calcining the raw material of the silica-alumina catalyst at a calcination temperature of 400° C. or more and 950° C. or less to obtain a silica-alumina catalyst.
- the method for producing a silica-alumina catalyst may include other production steps than the calcination step.
- the silica-alumina contained in the catalyst used in the dehydration reaction step of the present production method has a SiO 2 content of 3 to 80, preferably 4 to 70 in molar ratio to Al 2 O 3 , and more It is preferably 4-60, more preferably 4-50.
- the above molar ratio can be measured, for example, by the inductively coupled plasma atomic emission spectrometry (ICP-AES method) described in the examples below.
- the above catalyst can be used together with a molding agent (binder).
- a molding agent binder
- the molar ratio of SiO 2 and Al 2 O 3 measured by the ICP-AES method is the silica and/or alumina added as the binder.
- a value including the amount of SiO 2 and Al 2 O 3 contained in that is, when the catalyst is used in combination with the binder, the molar ratio of SiO 2 and Al 2 O 3 is measured based on the total amount of SiO 2 and Al 2 O 3 contained in the catalyst and the binder. be done. This is the same when alumina or the like is used together with the silica-alumina catalyst as a co-catalyst.
- the ratio of Al 2 O 3 contained in the catalyst is larger than that of conventional silica-alumina. Therefore, by ensuring a sufficient amount of acid during the dehydration reaction of propanol, the catalyst becomes highly active and propylene can be produced efficiently even if the raw propanol contains a large amount of water. .
- the silica-alumina catalyst may contain, in addition to Al 2 O 3 and SiO 2 , trace amounts of metal elements derived from impurities in the raw material. Examples of such metal elements include Ca, Fe, Mg, Na, Ti and Zr.
- metal elements include Ca, Fe, Mg, Na, Ti and Zr.
- As the silica-alumina catalyst a commercially available product or a chemically synthesized product may be used as long as the molar ratio of SiO 2 to Al 2 O 3 is within the above range.
- a silicon compound and an aluminum compound can be used as raw materials.
- raw materials containing silicon include tetraethylorthosilicate, silica gel, and sodium silicate.
- the raw material containing aluminum is preferably water-soluble, and specific examples thereof include aluminum nitrate, aluminum sulfate, and aluminum phosphate. Further, these aluminum-containing compounds may be a single substance or a hydrate.
- the method for synthesizing the silica-alumina catalyst may be, for example, either an impregnation method or a sol-gel method.
- a method for synthesizing the silica-alumina catalyst by a sol-gel method is shown below.
- First, the raw material containing silicon and the raw material containing aluminum are stirred in the presence of a solvent and an organic additive to obtain a gel.
- This reaction is usually carried out by adding a silicon compound to an aqueous solution containing an aluminum compound.
- the obtained gel is dried in air or by an evaporator or the like to be powdered.
- the silica-alumina catalyst can be obtained by calcining the obtained powder.
- Organic additives include citric acid, ethylene glycol, 1,2-propanediol, 1,3-propanediol, 1,4-butanediol, 2,3-butanediol, and 2-methyl-2,4-pentane A diol or the like can be used.
- the firing temperature of the powder is 400° C. or higher and 950° C. or lower.
- the lower limit of the firing temperature is 400° C. or higher, preferably 500° C. or higher, and more preferably 600° C. or higher.
- the upper limit of the firing temperature is 950° C. or lower, preferably 900° C. or lower, and more preferably 850° C. or lower.
- the firing temperature of the powder may be 200° C. or higher or 300° C. or higher.
- the firing time is preferably 1 hour to 10 hours, more preferably 2 hours to 9 hours. Firing of the powder may be performed in multiple steps. When firing is performed multiple times, the heating temperature and heating time may be the same or different.
- the heating method is also not particularly limited, but it can be carried out by using, for example, a muffle furnace, a tubular furnace, a rotary kiln, a shaft kiln, or the like.
- the silica-alumina catalyst By performing calcination during the production of the silica-alumina catalyst, Si--O--Al chemical bonds are formed in the resulting silica-alumina catalyst. As a result, the resulting silica-alumina catalyst has a stronger acid point than SiO 2 or Al 2 O 3 alone or a mixture thereof, resulting in high activity. Further, when the calcination temperature is within the above range, the resulting silica-alumina catalyst becomes more active, so that the yield of propylene is improved when used for dehydration of propanol. Moreover, if the calcination temperature is 400° C. or higher, the organic additives used in the preparation of the silica-alumina catalyst can be sufficiently removed. Therefore, the silica-alumina catalyst can obtain sufficient acid sites and also has improved moldability, so that it can be suitably used as a catalyst for dehydration of propanol.
- the raw material to be dehydrated contains water and propanol.
- Propanol includes isopropanol (IPA), normal propanol (NPA), or any mixture of IPA and NPA.
- the mass of water in the raw material is 0.01 to 2 times, preferably 0.1 to 2 times, more preferably 0.5 to 2 times the mass of propanol in the raw material. Yes, and particularly preferably 1.0 to 2 times.
- the raw material preferably contains 33 to 99% by mass, more preferably 33 to 90% by mass, and still more preferably 33 to 50% by mass of propanol when the entire raw material is 100% by mass. If the content of propanol in the raw material is 99% by mass or less, the raw material can contain water, so that the above-described effect of containing water can be obtained. Further, when the content of propanol in the raw material is 33% by mass or more, the production amount of propylene is improved.
- this raw material may further contain other components such as impurities that may be mixed in during the process of manufacturing this raw material.
- Other components such as impurities include, for example, unreacted raw materials used in the production of the present raw material, by-products produced in the production process of the present raw material, and the like.
- impurities include, for example, acetone, methanol, ethylene glycol, dimethyl ether, methyl ethyl ether, dimethyl carbonate, and the like.
- the content of impurities in the raw material is not particularly limited as long as it does not affect the production of propylene, but it is preferably 5% by mass or less, more preferably 1% by mass or less, and ideally no impurity. Not included.
- the production method includes a dehydration reaction step of dehydrating the raw material using the silica-alumina catalyst.
- the silica-alumina catalyst may be used as a catalyst layer filled in a reactor or the like.
- the type of reactor used in the dehydration reaction step is not particularly limited, and may be, for example, batch type, semi-batch type, or continuous flow type.
- the form of the dehydration reaction step is not particularly limited, and it can be carried out in any form of liquid phase, gas phase, or gas-liquid mixed layer.
- the packing method for forming the catalyst into the catalyst layer is not particularly limited, and packing can be performed by any method such as fixed bed, fluidized bed, suspended bed, and tray fixed bed.
- a gaseous component that does not interfere with the dehydration reaction step may be added.
- gaseous components include, for example, nitrogen, carbon dioxide, argon, helium, methane, ethane and propane.
- the silica-alumina catalyst may be used alone, or may be used in combination with a catalyst or molding agent (binder) that can be used for dehydration reaction.
- a catalyst or molding agent binder
- the above silica-alumina catalyst is used together with a molding agent, it may be used in the form of a molded product having increased mechanical strength by kneading and extruding them.
- catalysts or forming agents that can be used for dehydration reactions include silica, alumina, clay, titania, zirconia, zinc oxide, ceria, lanthana, graphite, and ethyl cellulose.
- the temperature of the catalyst layer during the dehydration reaction step is preferably 450° C. or lower, more preferably 400° C. or lower, even more preferably 300° C. or lower, and 200° C. or lower. Especially preferred.
- the lower limit of the temperature is not particularly limited as long as it is at least the temperature at which the dehydration reaction step can be carried out, but from the viewpoint of enhancing the activity of the resulting catalyst, it can be 160° C. or higher, or 180° C. or higher.
- the temperature of the catalyst layer can be appropriately adjusted by changing the temperature of the device used for the dehydration treatment.
- the dehydration reaction can be carried out at a relatively low temperature, so the energy required for the reaction can be reduced.
- propylene oligomerization and heavy weighting are accelerated in a high temperature environment. Therefore, by carrying out the reaction at a lower temperature than before, the production of by-products is suppressed and the yield of propylene is improved.
- the reaction pressure during the dehydration reaction step is not particularly limited, but is preferably 0 to 100000 KPa (gauge pressure), more preferably 0 to 5000 KPa (gauge pressure), and still more preferably 0 to 4000 KPa (gauge pressure). be.
- the ratio (W/F) of the catalyst weight g to the propanol flow rate mol ⁇ h ⁇ 1 during the dehydration reaction step is not particularly limited, but is preferably 0.01 to 10000 g ⁇ h ⁇ mol ⁇ 1 , more preferably 0.00 g ⁇ h ⁇ mol ⁇ 1 . 1 to 5000 g ⁇ h ⁇ mol ⁇ 1 , still more preferably 1 to 200 g ⁇ h ⁇ mol ⁇ 1 .
- the activity of the catalyst may be recovered using a known method.
- two or more reactors are arranged in parallel, and while one reactor is recovering the activity of the catalyst, another reactor is used for the dehydration reaction. It doesn't matter.
- two or more reactors in which the activity of the catalyst has not been recovered may be connected in series to reduce variations in production.
- the reactor system is a fluidized bed circulation reaction system or a moving bed reaction system, continuously or intermittently withdraw part or all of the catalyst from the reactor, and an amount equivalent to the amount withdrawn By replenishing the catalyst, it is possible to maintain constant catalytic activity.
- the product propylene may be taken out in a gas-liquid separation step and then purified by distillation or the like.
- the products in this production method may contain impurities other than propylene.
- impurities include water, unreacted propanol, and by-products.
- by-products include C6 olefins.
- the content of the impurities is preferably 0.1 or less, more preferably 0.05 or less, and still more preferably 0.01 or less in molar ratio to the propylene content in the product. is.
- the impurities should ideally be completely absent from the product.
- At least one of the olefins represented by the following general formula (1) or (2) may be contained in the fluid produced in the dehydration reaction step of the production method.
- olefins represented by the following general formula (1) or (2) include 3-methyl-2-pentene, 2-methyl-1-pentene and the like.
- the lower limit of the content of the olefin may be contained in an amount of 0.00000001 or more in a molar ratio with respect to the amount of propylene in the fluid, and may be contained in an amount of 0.0000001 or more in a molar ratio, It may be contained in an amount of 0.000001 or more in terms of molar ratio.
- the upper limit may be included in an amount of 0.1 or less in a molar ratio, may be included in an amount of 0.05 or less in a molar ratio, or 0.01 in a molar ratio with respect to the amount of propylene in the fluid. May contain the following amounts:
- the olefin represented by the following general formula (1) or (2) corresponds to an olefin having a main chain of 5 carbon atoms and a methyl group. Ideally, the olefin should not be contained in the fluid at all, but the lower limit of the amount of the olefin contained may be greater than 0, for example in terms of molar ratio. If the olefin is contained in the fluid, carbon may deposit on the catalyst. Carbon deposited on the catalyst causes a decrease in the acid sites of the catalyst, which may reduce catalytic activity.
- R 1 , R 2 and R 3 are a methyl group and the rest are hydrogen.
- oligomers and the like can be mixed as by-products in the method of producing propylene by propanol dehydration.
- the structure of the oligomer was not known, and in particular, the C6 olefin having a branch in the carbon skeleton represented by the above formula (1) or (2) was not known as a by-product.
- propylene obtained by this production method is not particularly limited, but it can be suitably used as a raw material for polypropylene, propylene oxide, plastics, aromatic hydrocarbons, aromatic alcohols, and the like.
- Propylene yield (%) [(supplied propanol [mol/min] - unreacted propanol [mol/min])/supplied propanol [mol/min]] x [3 x amount of propylene produced [mol/min]/ (Total amount of carbon-based production of each product [mol/min])] ⁇ 100 (4) ⁇ Example 1> (a. Method for producing silica-alumina catalyst (A)) 60.14 g of pure water, 23.16 g of aluminum nitrate nonahydrate and 13.05 g of citric acid were placed in a 200 ml glass beaker and stirred at room temperature for 5 minutes.
- silica-alumina catalyst (A) had a SiO 2 /Al 2 O 3 molar ratio of 11.
- silica-alumina catalyst (A) was pressurized at 60 MPa (gauge pressure) for 20 minutes using a press to obtain a silica-alumina catalyst (A) compact. After that, the obtained compact was pulverized in an agate mortar, passed through 10-mesh and 26-mesh sieves, and taken out from between the two sieves to obtain silica-alumina catalyst (A) compact powder. 3.08 g of the powder of the silica-alumina catalyst (A) compact thus obtained was packed into a SUS reaction tube with an inner diameter of 1.4 cm, including a SUS tube with an outer diameter of 3 mm containing a thermocouple, and the filling volume was 5.
- a catalyst layer of 0.77 ml was formed. After that, the temperature of the catalyst layer was raised from room temperature to 200° C. over 45 minutes in a reaction tube heating furnace while flowing nitrogen at 136.7 Nml/min. Under nitrogen flow, a hydrous IPA raw material containing 1-fold mass of water relative to IPA is introduced into a vaporizer heated to 110°C at a flow rate of 0.298 ml/min with a liquid feed pump, and then connected to the latter stage of the vaporizer. It was introduced into the reaction tube with After that, the temperature of the reaction tube heating furnace was adjusted so that the temperature at the center of the catalyst layer was about 200°C.
- the liquid from the reaction tube was collected in two glass trap containers containing 26 g of methanol for 36 minutes, and the liquid component was analyzed by gas chromatography. rice field.
- the gas components emitted from the outlets of the two glass trap containers containing methanol were collected with a gas bag, and the gas components were analyzed by gas chromatography.
- the silica-alumina catalyst (B) had a SiO 2 /Al 2 O 3 molar ratio of 404.
- the silica-alumina catalyst (B) corresponds to the catalyst described in Example 4 of Patent Document 1.
- Example 2> (a. Method for producing silica-alumina catalyst (C)) 59.73 g of pure water, 5.11 g of aluminum nitrate nonahydrate, and 12.95 g of citric acid were placed in a 200 ml glass beaker and stirred at room temperature for 5 minutes. While continuing to stir the mixture in the beaker at room temperature, 71.63 g of tetraethyl orthosilicate was added dropwise from the dropping buret over 1 hour to obtain a gel. This gel was transferred to a porcelain dish, dried in the atmosphere at room temperature for 24 hours, and then dried in an evaporator under reduced pressure of 160 hPa at a water bath temperature of 50° C.
- C silica-alumina catalyst
- silica-alumina catalyst (C) had a SiO 2 /Al 2 O 3 molar ratio of 51.
- a silica-alumina catalyst (C) molded powder was obtained from the silica-alumina catalyst (C) using a press and a sieve in the same manner as in Example 1. Same as Example 1, except that the silica-alumina catalyst (C) compact was vacuum-dried at 200°C for 2 hours to form a catalyst layer with a filling volume of 5.77 ml, and the temperature of the vaporizer was 210°C. Propylene was produced by the method of Example 1, and the liquid component and gas component were analyzed in the same manner as in Example 1.
- Example 3> (a. Method for producing silica-alumina catalyst (D)) 60.03 g of pure water, 3.67 g of aluminum nitrate nonahydrate and 13.06 g of citric acid were placed in a 200 ml glass beaker and stirred at room temperature for 5 minutes. While continuing to stir the mixture in the beaker at room temperature, 71.54 g of tetraethyl orthosilicate was added dropwise from the dropping buret over 1 hour to obtain a gel. This gel was transferred to a porcelain dish, dried in the atmosphere at room temperature for 24 hours, and then dried in an evaporator under reduced pressure of 160 hPa at a water bath temperature of 50° C. to obtain 47.25 g of powder.
- D silica-alumina catalyst
- silica-alumina catalyst (D) As a result of analysis by inductively coupled plasma atomic emission spectrometry (ICP-AES method), the silica-alumina catalyst (C) had a SiO 2 /Al 2 O 3 molar ratio of 69.
- a silica-alumina catalyst (D) molded powder was obtained from the silica-alumina catalyst (D) using a press and a sieve in the same manner as in Example 1. Same as Example 1, except that the silica-alumina catalyst (D) molded body was vacuum-dried at 200°C for 2 hours to form a catalyst layer with a filling volume of 5.77 ml, and the temperature of the vaporizer was set to 210°C. Propylene was produced by the method of Example 1, and the liquid component and gas component were analyzed in the same manner as in Example 1.
- ⁇ Comparative Example 2> (Method for producing silica-alumina catalyst (E)) 59.88 g of pure water, 23.17 g of aluminum nitrate nonahydrate, and 13.07 g of citric acid were placed in a 200 ml glass beaker and stirred at room temperature for 5 minutes. While continuing to stir the mixture in the beaker at room temperature, 71.67 g of tetraethyl orthosilicate was added dropwise from the dropping buret over 1 hour to obtain a gel. This gel was transferred to a porcelain dish, dried in the atmosphere at room temperature for 24 hours, and then dried in an evaporator under reduced pressure of 160 hPa at a water bath temperature of 50° C.
- silica-alumina catalyst (E) was colored brown because the organic components contained in the raw materials for preparation had not been removed. Further, molding was attempted using a press in the same manner as in Example 1, but molding was not possible.
- Example 4> (a. Method for producing silica-alumina catalyst (F)) 12.30 g of silica-alumina catalyst (E) was placed in the muffle furnace again and calcined at 500° C. for 2 hours to obtain 10.11 g of silica-alumina catalyst (F).
- Example 2 A silica-alumina catalyst (F) molded powder was obtained from the silica-alumina catalyst (F) using a press and a sieve in the same manner as in Example 1. The same procedure as in Example 1 was carried out, except that a catalyst layer with a filling volume of 5.77 ml was formed after drying the silica-alumina catalyst (F) compact at 200°C for 2 hours, and the temperature of the vaporizer was set at 210°C. Propylene was produced in the same manner as in Example 1, and liquid and gas components were analyzed in the same manner as in Example 1.
- Example 5> (a. Method for producing silica-alumina catalyst (G)) 60.79 g of pure water, 23.17 g of aluminum nitrate nonahydrate and 13.02 g of citric acid were placed in a 200 ml glass beaker and stirred at room temperature for 5 minutes. While continuing to stir the mixture in the beaker at room temperature, 72.21 g of tetraethyl orthosilicate was added dropwise from the dropping buret over 1 hour to obtain a gel. This gel was transferred to a porcelain dish, dried in the atmosphere at room temperature for 24 hours, and then dried in an evaporator under reduced pressure of 160 hPa at a water bath temperature of 50° C. to obtain 62.75 g of powder. 30.52 g of this powder was calcined in a muffle furnace at 900° C. for 1 hour to obtain 11.35 g of silica-alumina catalyst (G).
- Example 2 A silica-alumina catalyst (G) molded powder was obtained from the silica-alumina catalyst (G) using a press and a sieve in the same manner as in Example 1. The same procedure as in Example 1 was carried out, except that a catalyst layer with a filling volume of 5.77 ml was formed after drying the silica-alumina catalyst (G) compact at 200°C for 2 hours, and the temperature of the vaporizer was set at 210°C. Propylene was produced in the same manner as in Example 1, and liquid and gas components were analyzed in the same manner as in Example 1.
- a hydrous IPA raw material containing 1-fold mass of water relative to IPA is introduced into a vaporizer heated to 210°C at a flow rate of 0.237 ml/min with a liquid feed pump, and then connected to the latter stage of the vaporizer. It was introduced into the reaction tube with After that, the temperature of the reaction tube heating furnace was adjusted so that the temperature at the center of the catalyst layer was about 200°C. Thirty minutes after the temperature of the catalyst layer was adjusted, the liquid from the reaction tube was collected in two glass trap containers containing 25 g of methanol for 35 minutes, and the liquid component was analyzed by gas chromatography. rice field. Thirty-four minutes after the collection of the liquid, the gas components emitted from the outlets of the two glass trap containers containing methanol were collected with a gas bag, and the gas components were analyzed by gas chromatography.
- Example 6> Manufacture of propylene
- a catalyst layer having a filling volume of 5.77 ml was formed.
- the temperature of the catalyst layer was raised from room temperature to 300° C. over 70 minutes in a reaction tube heating furnace while flowing nitrogen at 136.7 Nml/min.
- a hydrous NPA raw material containing one mass of water to NPA is introduced into a vaporizer heated to 210°C at a flow rate of 0.298 ml/min by a liquid feed pump, and then connected to the latter stage of the vaporizer.
- the temperature of the reaction tube heating furnace was adjusted so that the temperature at the center of the catalyst layer was about 300°C.
- the liquid from the reaction tube was collected in two glass trap containers containing 26 g of methanol for 36 minutes, and the liquid component was analyzed by gas chromatography. rice field.
- the gas components emitted from the outlets of the two glass trap containers containing methanol were collected with a gas bag, and the gas components were analyzed by gas chromatography.
- Example 7> (a. Method for producing silica-alumina catalyst (I)) 59.88 g of pure water, 23.17 g of aluminum nitrate nonahydrate, and 13.07 g of citric acid were placed in a 200 ml glass beaker and stirred at room temperature for 5 minutes. While continuing to stir the mixture in the beaker at room temperature, 71.67 g of tetraethyl orthosilicate was added dropwise from the dropping buret over 1 hour to obtain a gel. This gel was transferred to a porcelain dish, dried in the atmosphere at room temperature for 24 hours, and then dried in an evaporator under reduced pressure of 160 hPa at a water bath temperature of 50° C. to obtain 65.67 g of powder. 30.40 g of this powder was calcined in a muffle furnace at 800° C. for 2 hours to obtain 10.11 g of silica-alumina catalyst (I).
- silica-alumina catalyst (I) molded powder was obtained from the silica-alumina catalyst (I) using a press and a sieve in the same manner as in Example 1. Propylene production was carried out in the same manner as in Example 6, except that a catalyst layer having a filling volume of 5.77 ml was formed after drying the silica alumina catalyst (I) molded body at 200 ° C. for 2 hours. Analysis of the liquid component and the gas component was performed in the same manner as in 6.
- Example 8> Manufacture of propylene
- the powder of the silica-alumina catalyst (A) compact was packed in a SUS reaction tube to form a catalyst layer with a packed volume of 5.77 ml. After that, the temperature of the catalyst layer was raised from room temperature to 180° C. over 40 minutes in a reaction tube heating furnace while flowing nitrogen at 267.0 Nml/min. After introducing a hydrous IPA raw material containing 0.2 times the mass of water to IPA under nitrogen flow into a vaporizer heated to 110 ° C.
- the latter stage of the vaporizer was introduced into a reaction tube connected to After that, the temperature of the reaction tube heating furnace was adjusted so that the temperature at the center of the catalyst layer was about 180°C.
- the liquid from the reaction tube was collected in two glass trap containers containing 25 g of methanol for 34 minutes, and the liquid component was analyzed by gas chromatography. rice field.
- the gas components emitted from the outlets of the two glass trap containers containing methanol were collected with a gas bag, and the gas components were analyzed by gas chromatography.
- Example 9 Manufacture of propylene
- Propylene was produced in the same manner as in Example 8 except that the was used, and the liquid and gas components were analyzed in the same manner as in Example 8.
- Table 1 shows the propylene yield calculated by gas chromatography analysis of the SiO 2 /Al 2 O 3 ratio, calcination temperature, liquid component, and gaseous component of the catalysts of Examples 1-5 and Comparative Examples 1-3.
- Table 2 shows the propylene yield calculated by gas chromatography analysis of the SiO 2 /Al 2 O 3 ratio, calcination temperature, liquid component, and gas component of the catalysts of Examples 6 to 7 and Comparative Examples 4 and 5.
- Table 3 shows the propylene yield calculated by gas chromatography analysis of the SiO 2 /Al 2 O 3 ratio, the liquid component, and the gas component of the silica-alumina catalyst (A) shaped bodies of Examples 8 and 9.
- the silica-alumina catalyst (A) compact of Example 1 the silica-alumina catalyst (C) compact of Example 2, the silica-alumina catalyst (D) compact of Example 3, and the silica-alumina of Example 4 It can be seen that most of the IPA was converted to propylene when the catalyst (F) compact and the silica-alumina catalyst (G) compact of Example 5 were used.
- the silica-alumina catalyst (B) having a high SiO 2 molar ratio of Comparative Example 1 was used, the amount of propylene produced was below the detection limit, and IPA was not converted to propylene at all.
- the yield of propylene was 81.35% when a hydrous IPA raw material containing 0.2 times the mass of the IPA of Example 8 was used.
- the propylene yield The rate was 53.66%.
- the molar ratio of 2-methyl-1-pentene to propylene obtained in Example 9 was 0.04.
- the present invention can be suitably used as a method for producing propylene.
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Abstract
Description
<1>
SiO2の含有量がAl2O3に対するモル比で3~80であるシリカアルミナを含む触媒を用いて、プロパノールと水とを含む原料を脱水する脱水反応工程を含み、前記シリカアルミナを含む触媒は400℃以上、950℃以下の焼成温度で焼成する工程を含む製造方法により製造される、プロピレンの製造方法。
<2>
上記原料中の水の質量が、上記原料中のプロパノールの質量に対して、0.01~2倍である、<1>に記載のプロピレンの製造方法。
<3>
上記脱水反応工程における上記触媒を含む触媒層の温度が450℃以下である、<1>または<2>に記載のプロピレンの製造方法。
<4>
上記脱水反応工程において生成される流体中に、下記一般式(1)または(2)で表されるオレフィンの内、少なくとも1種類が、当該流体中に含まれるプロピレンの量に対してモル比で0.1以下の量含まれる、<1>~<3>のいずれかに記載のプロピレンの製造方法。
本発明の一実施形態に係るプロピレンの製造方法は、SiO2の含有量がAl2O3に対するモル比で3~80であるシリカアルミナを含む触媒を用いて、プロパノールと水とを含む原料を脱水する脱水反応工程を含み、前記シリカアルミナを含む触媒は400℃以上、950℃以下の焼成温度で焼成する工程を含む製造方法により製造される。上記シリカアルミナ中のAl2O3に対するSiO2のモル比が3~80であるとも言える。以下、本発明の一実施形態に係るプロピレンの製造方法を、本製造方法とも称する。また、シリカアルミナを含む触媒をシリカアルミナ触媒とも称する。上記シリカアルミナ触媒は、本製造方法において、脱水触媒として使用される。
本製造方法において、プロパノールとして、イソプロパノール(IPA)を用いる場合は、IPAは分子内脱水、あるいは分子間脱水のいずれによってもプロピレンへと転化されてもよい。IPAの分子内脱水が行われる場合、IPAから直接プロピレンが製造される。一方、IPAの分子間脱水が行われる場合、ジイソプロピルエーテル(DIPE)を経由して、プロピレンが製造される。
本製造方法の脱水反応工程において使用されるシリカアルミナ触媒は、400℃以上、950℃以下の焼成温度で焼成する工程を含む製造方法によって製造される。換言すれば、プロピレンの製造方法は400℃以上、950℃以下の焼成温度で、シリカアルミナ触媒の原料の焼成を行ってシリカアルミナ触媒を得る工程を含んでもよい。また、シリカアルミナ触媒を製造する方法は、前記焼成する工程以外のその他の製造工程を含んでいてもよい。
本製造方法において、脱水される原料(以下、本原料とも称する。)は、水とプロパノールとを含む。プロパノールはイソプロパノール(IPA)、またはノルマルプロパノール(NPA)、またはIPAとNPAを任意の割合で混合したものを含む。
本製造方法は、上記シリカアルミナ触媒を用いて本原料を脱水する、脱水反応工程を含む。上記脱水反応工程において、上記シリカアルミナ触媒は、反応器等に充填された触媒層としてから使用されてもよい。
本製造方法の脱水反応工程において、プロパノールを含む本原料の脱水が行われ、プロピレンを含む生成物が生成される。
実施例のプロピレンの製造において、反応器出口から出る液体成分、気体成分の分析はガスクロマトグラフィーにより行い、プロピレン収率を以下の式(4)により算出した。
<実施例1>
(a.シリカアルミナ触媒(A)の製造方法)
ガラス製200mlビーカーに純水60.14g、硝酸アルミニウム9水和物23.16g、クエン酸13.05gを入れて、室温で5分間撹拌した。室温でのビーカー内の混合物の撹拌を継続しつつ、テトラエチルオルトシリケート71.90gを1時間かけて滴下ビュレットから滴下し、ゲルを得た。このゲルを磁製皿に移し、室温にて24時間、大気中で乾燥後、エバポレーターにて160hPaの減圧下、水浴温度50℃で乾燥させて95.67gの粉末を得た。この粉末43.86gをマッフル炉にて500℃、5時間焼成した後、マッフル炉から取り出し、11.35gの粉末を得た。取り出した粉末10.02gを再度マッフル炉に入れて600℃にて2時間焼成し、シリカアルミナ触媒(A)10.11gを得た。誘導結合プラズマ発光分析法(ICP-AES法)による分析の結果、シリカアルミナ触媒(A)のSiO2/Al2O3のモル比率は11であった。
上記シリカアルミナ触媒(A)を、プレス機を用いて60MPa(ゲージ圧)で20分間加圧して、シリカアルミナ触媒(A)成形体を得た。その後、得られた成形体をメノウ乳鉢で粉砕し、10メッシュ、および26メッシュの篩を通過させ、2つの篩の間から取り出すことによりシリカアルミナ触媒(A)成形体の粉末を得た。得られた3.08gの上記シリカアルミナ触媒(A)成形体の粉末を、熱電対の入った外径3mmのSUS管を含む、内径1.4cmのSUS反応管中に充填して充填体積5.77mlの触媒層を形成した。その後、窒素136.7Nml/min流通下で、触媒層の温度を反応管加熱炉にて、45分かけて室温から200℃まで昇温した。窒素流通下でIPAに対して1質量倍の水を含む含水IPA原料を送液ポンプにて、0.298ml/minの流量で110℃に加熱した気化器に導入後、気化器の後段に連結された反応管に導入した。その後、触媒層中心の温度が約200℃となるように反応管加熱炉の温度を調整した。触媒層の温度を調整してから30分経過後に、反応管からの液を26gのメタノールの入った2つのガラス製トラップ容器に36分間捕集し、ガスクロマトグラフィーにて液体成分の分析を行った。液の捕集後35分経過後に、メタノールの入った2つのガラス製トラップ容器の出口から出る気体成分をガスバッグにて捕集し、ガスクロマトグラフィーにて気体成分の分析を行った。
(a)シリカアルミナ触媒(B)の製造方法
ガラス製ビーカー100ml内に純水19.31g、および硝酸アルミニウム9水和物0.55gの混合物を調製し、パスツールピペットを用いてガラス製ビーカー500ml内の富士シリシア製キャリアクト(Q-30)20gに室温にて一滴ずつ滴下した。この混合物を120℃で3時間乾燥させた後、混合物19.85gをマッフル炉に入れて500℃にて6時間焼成し、シリカアルミナ触媒(B)19.67gを得た。ICP-AES法による分析の結果、シリカアルミナ触媒(B)のSiO2/Al2O3のモル比率は404であった。なお、シリカアルミナ触媒(B)は、特許文献1の実施例4に記載されている触媒に相当する。
上記シリカアルミナ触媒(B)2.12gを使用して充填体積5.77mlの触媒層を形成させたことを除き、実施例1と同様の方法にてプロピレンの製造を実施し、実施例1と同様の方法にて液体成分、および気体成分の分析を行った。
(a.シリカアルミナ触媒(C)の製造方法)
ガラス製200mlビーカーに純水59.73g、硝酸アルミニウム9水和物5.11g、クエン酸12.95gを入れて、室温で5分間撹拌した。室温でのビーカー内の混合物の撹拌を継続しつつ、テトラエチルオルトシリケート71.63gを1時間かけて滴下ビュレットから滴下し、ゲルを得た。このゲルを磁製皿に移し、室温にて24時間、大気中で乾燥後、エバポレーターにて160hPaの減圧下、水浴温度50℃で乾燥させて41.55gの粉末を得た。この粉末35.83gをマッフル炉にて600℃、2時間焼成し、シリカアルミナ触媒(C)23.10gを得た。誘導結合プラズマ発光分析法(ICP-AES法)による分析の結果、シリカアルミナ触媒(C)のSiO2/Al2O3のモル比率は51であった。
上記シリカアルミナ触媒(C)から実施例1と同様にプレス機と篩を用いてシリカアルミナ触媒(C)成形体の粉末を得た。シリカアルミナ触媒(C)成形体を200℃で2時間真空乾燥した後に充填体積5.77mlの触媒層を形成したこと、および気化器の温度を210℃としたことを除き、実施例1と同様の方法にてプロピレンの製造を実施し、実施例1と同様の方法にて液体成分、および気体成分の分析を行った。
(a.シリカアルミナ触媒(D)の製造方法)
ガラス製200mlビーカーに純水60.03g、硝酸アルミニウム9水和物3.67g、クエン酸13.06gを入れて、室温で5分間撹拌した。室温でのビーカー内の混合物の撹拌を継続しつつ、テトラエチルオルトシリケート71.54gを1時間かけて滴下ビュレットから滴下し、ゲルを得た。このゲルを磁製皿に移し、室温にて24時間、大気中で乾燥後、エバポレーターにて160hPaの減圧下、水浴温度50℃で乾燥させて47.25gの粉末を得た。この粉末46.44gをマッフル炉にて600℃、2時間焼成し、シリカアルミナ触媒(D)20.79gを得た。誘導結合プラズマ発光分析法(ICP-AES法)による分析の結果、シリカアルミナ触媒(C)のSiO2/Al2O3のモル比率は69であった。
上記シリカアルミナ触媒(D)から実施例1と同様にプレス機と篩を用いてシリカアルミナ触媒(D)成形体の粉末を得た。シリカアルミナ触媒(D)成形体を200℃で2時間真空乾燥した後に充填体積5.77mlの触媒層を形成したこと、および気化器の温度を210℃としたことを除き、実施例1と同様の方法にてプロピレンの製造を実施し、実施例1と同様の方法にて液体成分、および気体成分の分析を行った。
(シリカアルミナ触媒(E)の製造方法)
ガラス製200mlビーカーに純水59.88g、硝酸アルミニウム9水和物23.17g、クエン酸13.07gを入れて、室温で5分間撹拌した。室温でのビーカー内の混合物の撹拌を継続しつつ、テトラエチルオルトシリケート71.67gを1時間かけて滴下ビュレットから滴下し、ゲルを得た。このゲルを磁製皿に移し、室温にて24時間、大気中で乾燥後、エバポレーターにて160hPaの減圧下、水浴温度50℃で乾燥させて65.67gの粉末を得た。この粉末30.40gをマッフル炉にて300℃、2時間焼成した後、マッフル炉から取り出し、シリカアルミナ触媒(E)12.47gの粉末を得た。このシリカアルミナ触媒(E)は調製原料に含まれる有機成分が除去されておらず茶色に着色していた。また、実施例1と同様にプレス器で成形を試みたが、成形することができなかった。
(a.シリカアルミナ触媒(F)の製造方法)
シリカアルミナ触媒(E)12.30gを再度マッフル炉に入れて500℃にて2時間焼成し、シリカアルミナ触媒(F)10.11gを得た。
上記シリカアルミナ触媒(F)から実施例1と同様にプレス機と篩を用いてシリカアルミナ触媒(F)成形体の粉末を得た。シリカアルミナ触媒(F)成形体を200℃で2時間乾燥した後に充填体積5.77mlの触媒層を形成したこと、および気化器の温度を210℃としたことを除き、実施例1と同様の方法にてプロピレンの製造を実施し、実施例1と同様の方法にて液体成分、および気体成分の分析を行った。
(a.シリカアルミナ触媒(G)の製造方法)
ガラス製200mlビーカーに純水60.79g、硝酸アルミニウム9水和物23.17g、クエン酸13.02gを入れて、室温で5分間撹拌した。室温でのビーカー内の混合物の撹拌を継続しつつ、テトラエチルオルトシリケート72.21gを1時間かけて滴下ビュレットから滴下し、ゲルを得た。このゲルを磁製皿に移し、室温にて24時間、大気中で乾燥後、エバポレーターにて160hPaの減圧下、水浴温度50℃で乾燥させて62.75gの粉末を得た。この粉末30.52gをマッフル炉にて900℃、1時間焼成し、シリカアルミナ触媒(G)11.35gを得た。
上記シリカアルミナ触媒(G)から実施例1と同様にプレス機と篩を用いてシリカアルミナ触媒(G)成形体の粉末を得た。シリカアルミナ触媒(G)成形体を200℃で2時間乾燥した後に充填体積5.77mlの触媒層を形成したこと、および気化器の温度を210℃としたことを除き、実施例1と同様の方法にてプロピレンの製造を実施し、実施例1と同様の方法にて液体成分、および気体成分の分析を行った。
(a.シリカアルミナ触媒(H)の製造方法)
シリカアルミナ触媒(A)成形体の粉末4.57gをマッフル炉に入れて1000℃にて1時間焼成し、シリカアルミナ触媒(H)成形体4.18gを得た。
4.00gの上記シリカアルミナ触媒(H)成形体の粉末を、熱電対の入った外径3mmのSUS管を含む、内径1.4cmのSUS反応管中に充填して充填体積4.62mlの触媒層を形成した。その後、窒素110.0Nml/min流通下で、触媒層の温度を反応管加熱炉にて、45分かけて室温から200℃まで昇温した。窒素流通下でIPAに対して1質量倍の水を含む含水IPA原料を送液ポンプにて、0.237ml/minの流量で210℃に加熱した気化器に導入後、気化器の後段に連結された反応管に導入した。その後、触媒層中心の温度が約200℃となるように反応管加熱炉の温度を調整した。触媒層の温度を調整してから30分経過後に、反応管からの液を25gのメタノールの入った2つのガラス製トラップ容器に35分間捕集し、ガスクロマトグラフィーにて液体成分の分析を行った。液の捕集後34分経過後に、メタノールの入った2つのガラス製トラップ容器の出口から出る気体成分をガスバッグにて捕集し、ガスクロマトグラフィーにて気体成分の分析を行った。
(プロピレンの製造)
シリカアルミナ触媒(A)成形体の粉末を200℃で2時間真空乾燥した後に充填体積5.77mlの触媒層を形成した。その後、窒素136.7Nml/min流通下で、触媒層の温度を反応管加熱炉にて、70分かけて室温から300℃まで昇温した。窒素流通下でNPAに対して1質量倍の水を含む含水NPA原料を送液ポンプにて、0.298ml/minの流量で210℃に加熱した気化器に導入後、気化器の後段に連結された反応管に導入した。その後、触媒層中心の温度が約300℃となるように反応管加熱炉の温度を調整した。触媒層の温度を調整してから30分経過後に、反応管からの液を26gのメタノールの入った2つのガラス製トラップ容器に36分間捕集し、ガスクロマトグラフィーにて液体成分の分析を行った。液の捕集後34分経過後に、メタノールの入った2つのガラス製トラップ容器の出口から出る気体成分をガスバッグにて捕集し、ガスクロマトグラフィーにて気体成分の分析を行った。
(プロピレンの製造)
シリカアルミナ触媒(B)を200℃で2時間真空乾燥した後に充填体積5.77mlの触媒層を形成したことを除き、実施例6と同様の方法にてプロピレンの製造を実施し、実施例6と同様の方法にて液体成分、および気体成分の分析を行った。
(a.シリカアルミナ触媒(I)の製造方法)
ガラス製200mlビーカーに純水59.88g、硝酸アルミニウム9水和物23.17g、クエン酸13.07gを入れて、室温で5分間撹拌した。室温でのビーカー内の混合物の撹拌を継続しつつ、テトラエチルオルトシリケート71.67gを1時間かけて滴下ビュレットから滴下し、ゲルを得た。このゲルを磁製皿に移し、室温にて24時間、大気中で乾燥後、エバポレーターにて160hPaの減圧下、水浴温度50℃で乾燥させて65.67gの粉末を得た。この粉末30.40gをマッフル炉にて800℃、2時間焼成し、シリカアルミナ触媒(I)10.11gを得た。
上記シリカアルミナ触媒(I)から実施例1と同様にプレス機と篩を用いてシリカアルミナ触媒(I)成形体の粉末を得た。シリカアルミナ触媒(I)成形体を200℃で2時間乾燥した後に充填体積5.77mlの触媒層を形成したことを除き、実施例6と同様の方法にてプロピレンの製造を実施し、実施例6と同様の方法にて液体成分、および気体成分の分析を行った。
(プロピレンの製造)
シリカアルミナ触媒(H)成形体を200℃で2時間乾燥した後に充填体積5.77mlの触媒層を形成したことを除き、実施例6と同様の方法にてプロピレンの製造を実施し、実施例6と同様の方法にて液体成分、および気体成分の分析を行った。
(プロピレンの製造)
上記シリカアルミナ触媒(A)成形体の粉末をSUS反応管中に充填して充填体積5.77mlの触媒層を形成した。その後、窒素267.0Nml/min流通下で、触媒層の温度を反応管加熱炉にて、40分かけて室温から180℃まで昇温した。窒素流通下でIPAに対して0.2質量倍の水を含む含水IPA原料を送液ポンプにて、0.193ml/minの流量で110℃に加熱した気化器に導入後、気化器の後段に連結された反応管に導入した。その後、触媒層中心の温度が約180℃となるように反応管加熱炉の温度を調整した。触媒層の温度を調整してから30分経過後に、反応管からの液を25gのメタノールの入った2つのガラス製トラップ容器に34分間捕集し、ガスクロマトグラフィーにて液体成分の分析を行った。液の捕集後33分経過後に、メタノールの入った2つのガラス製トラップ容器の出口から出る気体成分をガスバッグにて捕集し、ガスクロマトグラフィーにて気体成分の分析を行った。
(プロピレンの製造)
窒素流量を270.0Nml/minとしたこと、およびIPAに対して0.2質量倍の水、およびオレフィンである2-メチル-1-ペンテンをIPAに対して0.058質量倍含む含水IPA原料を使用したことを除き、実施例8と同様の方法にてプロピレンの製造を実施し、実施例8と同様の方法にて液体成分、および気体成分の分析を行った。
実施例1~5、および比較例1~3の触媒のSiO2/Al2O3比率、焼成温度、液体成分、および気体成分のガスクロマトグラフィー分析によって算出したプロピレン収率を表1に示す。
Claims (4)
- SiO2の含有量がAl2O3に対するモル比で3~80であるシリカアルミナを含む触媒を用いて、プロパノールと水とを含む原料を脱水する脱水反応工程を含み、前記シリカアルミナを含む触媒は400℃以上、950℃以下の焼成温度で焼成する工程を含む製造方法により製造される、プロピレンの製造方法。
- 上記原料中の水の質量が、上記原料中のプロパノールの質量に対して、0.01~2倍である、請求項1に記載のプロピレンの製造方法。
- 上記脱水反応工程における上記触媒を含む触媒層の温度が450℃以下である、請求項1または2に記載のプロピレンの製造方法。
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US20150011813A1 (en) * | 2013-07-02 | 2015-01-08 | Ut-Battelle, Llc | Catalytic conversion of alcohols having at least three carbon atoms to hydrocarbon blendstock |
CN104549436A (zh) * | 2013-10-12 | 2015-04-29 | 中国石油化工股份有限公司 | 一种氢型zsm-5分子筛催化剂及其制备方法和应用 |
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US20150011813A1 (en) * | 2013-07-02 | 2015-01-08 | Ut-Battelle, Llc | Catalytic conversion of alcohols having at least three carbon atoms to hydrocarbon blendstock |
CN104549436A (zh) * | 2013-10-12 | 2015-04-29 | 中国石油化工股份有限公司 | 一种氢型zsm-5分子筛催化剂及其制备方法和应用 |
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