WO2022113423A1 - 酢酸アルケニル製造用固定床多管式反応器 - Google Patents
酢酸アルケニル製造用固定床多管式反応器 Download PDFInfo
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- WO2022113423A1 WO2022113423A1 PCT/JP2021/027393 JP2021027393W WO2022113423A1 WO 2022113423 A1 WO2022113423 A1 WO 2022113423A1 JP 2021027393 W JP2021027393 W JP 2021027393W WO 2022113423 A1 WO2022113423 A1 WO 2022113423A1
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- reaction
- tube
- acetate
- catalyst
- reactor
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- -1 alkenyl acetate Chemical compound 0.000 title claims abstract description 62
- 238000006243 chemical reaction Methods 0.000 claims abstract description 182
- 239000002994 raw material Substances 0.000 claims abstract description 46
- 229910052783 alkali metal Inorganic materials 0.000 claims abstract description 38
- 239000007864 aqueous solution Substances 0.000 claims abstract description 14
- 239000003595 mist Substances 0.000 claims abstract description 8
- SCVFZCLFOSHCOH-UHFFFAOYSA-M potassium acetate Chemical compound [K+].CC([O-])=O SCVFZCLFOSHCOH-UHFFFAOYSA-M 0.000 claims description 34
- 238000004519 manufacturing process Methods 0.000 claims description 27
- 235000011056 potassium acetate Nutrition 0.000 claims description 17
- ZOAIGCHJWKDIPJ-UHFFFAOYSA-M caesium acetate Chemical compound [Cs+].CC([O-])=O ZOAIGCHJWKDIPJ-UHFFFAOYSA-M 0.000 claims description 5
- 239000003054 catalyst Substances 0.000 abstract description 114
- 239000007789 gas Substances 0.000 abstract description 44
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 abstract description 40
- 150000001336 alkenes Chemical class 0.000 abstract description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 12
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 12
- 239000001301 oxygen Substances 0.000 abstract description 12
- 229910052760 oxygen Inorganic materials 0.000 abstract description 12
- 230000003197 catalytic effect Effects 0.000 abstract description 8
- 238000007254 oxidation reaction Methods 0.000 abstract description 7
- 238000011112 process operation Methods 0.000 abstract description 3
- 238000005259 measurement Methods 0.000 abstract description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 44
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 25
- 229910052737 gold Inorganic materials 0.000 description 25
- 239000010931 gold Substances 0.000 description 25
- 229910052763 palladium Inorganic materials 0.000 description 20
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- HVAMZGADVCBITI-UHFFFAOYSA-M pent-4-enoate Chemical compound [O-]C(=O)CCC=C HVAMZGADVCBITI-UHFFFAOYSA-M 0.000 description 15
- 150000001875 compounds Chemical class 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- 239000007795 chemical reaction product Substances 0.000 description 10
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 9
- 239000005977 Ethylene Substances 0.000 description 9
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 8
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 8
- 239000000377 silicon dioxide Substances 0.000 description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 6
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- 239000010949 copper Substances 0.000 description 6
- 229910052802 copper Inorganic materials 0.000 description 6
- 229910052700 potassium Inorganic materials 0.000 description 6
- 239000011591 potassium Substances 0.000 description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound 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 5
- 150000002736 metal compounds Chemical class 0.000 description 5
- 229910052708 sodium Inorganic materials 0.000 description 5
- 239000011734 sodium Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 4
- 239000012696 Pd precursors Substances 0.000 description 4
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 4
- 150000001340 alkali metals Chemical class 0.000 description 4
- 229910017052 cobalt Inorganic materials 0.000 description 4
- 239000010941 cobalt Substances 0.000 description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 4
- 239000003085 diluting agent Substances 0.000 description 4
- 229910001882 dioxygen Inorganic materials 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- PIBWKRNGBLPSSY-UHFFFAOYSA-L palladium(II) chloride Chemical compound Cl[Pd]Cl PIBWKRNGBLPSSY-UHFFFAOYSA-L 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- 239000002243 precursor Substances 0.000 description 4
- 229910052725 zinc Inorganic materials 0.000 description 4
- 239000011701 zinc Substances 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 150000001341 alkaline earth metal compounds Chemical class 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 239000011261 inert gas Substances 0.000 description 3
- 230000007774 longterm Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000758 substrate Substances 0.000 description 3
- GVNVAWHJIKLAGL-UHFFFAOYSA-N 2-(cyclohexen-1-yl)cyclohexan-1-one Chemical compound O=C1CCCCC1C1=CCCCC1 GVNVAWHJIKLAGL-UHFFFAOYSA-N 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 2
- 101150065749 Churc1 gene Proteins 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 102100038239 Protein Churchill Human genes 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- XXROGKLTLUQVRX-UHFFFAOYSA-N allyl alcohol Chemical compound OCC=C XXROGKLTLUQVRX-UHFFFAOYSA-N 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
- 238000009529 body temperature measurement Methods 0.000 description 2
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- OPQARKPSCNTWTJ-UHFFFAOYSA-L copper(ii) acetate Chemical compound [Cu+2].CC([O-])=O.CC([O-])=O OPQARKPSCNTWTJ-UHFFFAOYSA-L 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000010574 gas phase reaction Methods 0.000 description 2
- 150000004820 halides Chemical class 0.000 description 2
- IKDUDTNKRLTJSI-UHFFFAOYSA-N hydrazine hydrate Chemical compound O.NN IKDUDTNKRLTJSI-UHFFFAOYSA-N 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 125000000896 monocarboxylic acid group Chemical group 0.000 description 2
- 150000002823 nitrates Chemical class 0.000 description 2
- 230000001681 protective effect Effects 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 description 2
- NIXOWILDQLNWCW-UHFFFAOYSA-M Acrylate Chemical compound [O-]C(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-M 0.000 description 1
- 238000004438 BET method Methods 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000005909 Kieselgur Substances 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-M Methacrylate Chemical compound CC(=C)C([O-])=O CERQOIWHTDAKMF-UHFFFAOYSA-M 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 150000001242 acetic acid derivatives Chemical class 0.000 description 1
- 125000000218 acetic acid group Chemical group C(C)(=O)* 0.000 description 1
- MQRWBMAEBQOWAF-UHFFFAOYSA-N acetic acid;nickel Chemical compound [Ni].CC(O)=O.CC(O)=O MQRWBMAEBQOWAF-UHFFFAOYSA-N 0.000 description 1
- ZOIORXHNWRGPMV-UHFFFAOYSA-N acetic acid;zinc Chemical compound [Zn].CC(O)=O.CC(O)=O ZOIORXHNWRGPMV-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- HKNWKTRXBJXGMT-UHFFFAOYSA-N barium palladium Chemical compound [Pd].[Ba] HKNWKTRXBJXGMT-UHFFFAOYSA-N 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 229910052792 caesium Inorganic materials 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000006757 chemical reactions by type Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 229940011182 cobalt acetate Drugs 0.000 description 1
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 1
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 1
- QAHREYKOYSIQPH-UHFFFAOYSA-L cobalt(II) acetate Chemical compound [Co+2].CC([O-])=O.CC([O-])=O QAHREYKOYSIQPH-UHFFFAOYSA-L 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000007334 copolymerization reaction Methods 0.000 description 1
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 1
- NWFNSTOSIVLCJA-UHFFFAOYSA-L copper;diacetate;hydrate Chemical compound O.[Cu+2].CC([O-])=O.CC([O-])=O NWFNSTOSIVLCJA-UHFFFAOYSA-L 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000012770 industrial material Substances 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229910052901 montmorillonite Inorganic materials 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229940078494 nickel acetate Drugs 0.000 description 1
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- YJVFFLUZDVXJQI-UHFFFAOYSA-L palladium(ii) acetate Chemical compound [Pd+2].CC([O-])=O.CC([O-])=O YJVFFLUZDVXJQI-UHFFFAOYSA-L 0.000 description 1
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 229910052701 rubidium Inorganic materials 0.000 description 1
- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 235000019795 sodium metasilicate Nutrition 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 150000004685 tetrahydrates Chemical class 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004876 x-ray fluorescence Methods 0.000 description 1
- 239000004246 zinc acetate Substances 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/04—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
- C07C67/05—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation
- C07C67/055—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation in the presence of platinum group metals or their compounds
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- 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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
-
- 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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8946—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali or alkaline earth metals
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
- C07C69/02—Esters of acyclic saturated monocarboxylic acids having the carboxyl group bound to an acyclic carbon atom or to hydrogen
- C07C69/12—Acetic acid esters
- C07C69/14—Acetic acid esters of monohydroxylic compounds
- C07C69/145—Acetic acid esters of monohydroxylic compounds of unsaturated alcohols
- C07C69/155—Allyl acetate
-
- 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 fixed-bed multi-tube reactor used for producing alkenyl acetates such as allyl acetate and vinyl acetate from lower olefins, acetic acid and oxygen by vapor phase catalytic oxidation reaction.
- Allyl acetate is one of the important industrial raw materials used for manufacturing raw materials such as solvents and allyl alcohol.
- Patent Document 1 Japanese Patent Application Laid-Open No. 2-91045 (Patent Document 1) describes a method for producing allyl acetate using a catalyst in which palladium, potassium acetate, and copper are supported on a carrier.
- vinyl acetate is important as a raw material for vinyl acetate resin, a raw material for polyvinyl alcohol, or a monomer for copolymerization with ethylene, styrene, acrylate, methacrylate, etc., and is used in a wide range of fields such as paints, adhesives, and fiber treatment agents. Industrial material.
- Patent Document 2 Japanese Patent Application Laid-Open No. 2004-526553 describes a method for producing vinyl acetate using a catalyst in which palladium, gold, and potassium acetate are supported on a carrier.
- a fixed bed tube reactor is generally used as a reactor applied to the production of alkenyl acetate.
- the fixed-bed tube reactor is a reactor in which a catalyst (supported on a carrier) as a fixed bed is filled in the reaction tube.
- the fixed-bed multi-tube reactor includes a plurality of reaction tubes among the fixed-bed tube reactors.
- the reaction substrate is supplied to the reaction tube in a gas phase state, reacts in the catalyst layer, and the reaction product is discharged from the reaction tube.
- a straight tube type reaction tube is often used from the viewpoints of equipment manufacturing, equipment maintenance, workability at the time of filling and replacing the catalyst, removal of reaction heat, and the like.
- the reaction tube is often installed in the vertical direction (vertical type) from the viewpoint of workability of filling and extracting the catalyst.
- the catalyst layer temperature of these reactors is generally monitored to confirm the reaction state in the catalyst layer during the operation of the industrial manufacturing process.
- a method for measuring the catalyst layer temperature for example, as described in Japanese Patent Application Laid-Open No. 2002-121227 (Patent Document 3), some representatives of the entire fixed-bed multi-tube reactor before filling the catalyst.
- Patent Document 3 Japanese Patent Application Laid-Open No. 2002-121227
- the gas phase contact oxidation reaction is an exothermic reaction
- a heat medium for removing heat is generally supplied to the outside of the reaction tube.
- the temperature difference between the heat medium temperature (shell temperature) on the outside of the reaction tube and the catalyst layer temperature it is possible to observe at what position in the longitudinal direction of the catalyst layer and to what extent the reaction substrate reacts.
- the plant can be operated so that the gas phase contact oxidation reaction proceeds stably and with high efficiency by controlling the reaction based on the temperature uneven distribution.
- thermocouple inserted inside the reaction tube of the fixed bed tube reactor as described above can accurately measure the catalyst layer temperature when only gas is circulated as the process fluid.
- this temperature measurement method is applied to a fixed-bed multi-tube reactor for the production of alkenyl acetate and a long-term continuous reaction for several months is performed, the reaction of the fixed-bed multi-tube reactor as a whole is reacted. Proceeding to produce the desired reaction product (this is due to the generation of reaction heat, the catalyst layer temperature is the heat medium temperature (shell temperature) of the shell portion (heat medium flow region outside the reaction tube) during the continuous reaction. )
- the catalyst layer temperature that represents the entire fixed-bed multi-tube reactor is set. We have found that it cannot be monitored.
- the present invention has been made in view of the above circumstances, and a long-term process operation is carried out in producing alkenyl acetate by a gas phase catalytic oxidation reaction of lower olefin, acetic acid and oxygen using a fixed-bed multi-tube reactor. It is an object of the present invention to provide a reaction apparatus capable of accurately measuring the temperature of the catalyst layer inside the reaction tube even when the above is performed.
- thermometer protection in which a mist of an aqueous solution of an alkali metal acetate supplied to a fixed-bed multi-tube reactor for vinyl acetate production and allyl acetate production is inserted into the reactor.
- a reaction in which a thermometer protection tube is inserted by adhering to the tube, then forming droplets and flowing down through the thermometer protection tube, and selectively being supplied to the reaction tube into which the thermometer protection tube is inserted. It was found that the cause was that the amount of alkali metal acetate carried in the tube became excessive and the catalytic activity decreased.
- a reaction tube filled with a catalyst having a reduced catalytic activity that is, a reaction tube into which a thermocouple is inserted
- the amount of heat of reaction generated is small, so that the temperature of the catalyst layer and the shell temperature in these reaction tubes are different.
- the temperature difference becomes smaller.
- the catalyst layer temperature in these reaction tubes is correspondingly higher than the shell temperature, which is the catalyst layer of the plant. It is not reflected in the temperature measurement. Therefore, it may not be possible to properly operate the plant.
- the present inventors have determined that droplets of alkali metal acetate adhering to the thermometer protection tube are supplied to the reaction tube into which the thermometer protection tube is inserted through the thermometer protection tube. To prevent this, we found that by inserting the thermometer protection tube from the bottom of the reactor, it is possible to prevent the droplets of alkali metal acetate from being selectively supplied to the reaction tube into which the thermometer protection tube is inserted. The present invention has been completed.
- the present invention includes the following [1] to [4].
- a fixed-bed multi-tube reactor for the production of alkenyl acetate A plurality of reaction tubes to which a mist of an aqueous solution of a raw material gas and an aqueous solution of alkali metal acetate is supplied from the upper part of the fixed-bed multi-tube reactor.
- a thermometer protection tube inserted into at least one of the plurality of reaction tubes from the lower part of the fixed-bed multi-tube reactor. The thermometer inserted in the thermometer protection tube and Fixed-bed multi-tube reactor equipped with.
- the measured value of the temperature of the catalyst layer can be used for detecting hot spots and adjusting the supply amount of alkali metal acetate. It can be used as an index or the like. As a result, the production efficiency of alkenyl acetate can be maintained high for a long period of time.
- the fixed-bed multi-tube reactor for producing alkenyl acetate of one embodiment includes a plurality of reaction tubes to which a mist of a raw material gas and an aqueous solution of an alkali metal acetate is supplied from the upper part of the fixed-bed multi-tube reactor.
- a thermometer protection tube inserted into at least one of a plurality of reaction tubes from the lower part of the fixed-bed multi-tube reactor and a thermometer inserted into the thermometer protection tube are provided.
- FIG. 1 is a schematic vertical sectional view of a fixed-bed multi-tube reactor (hereinafter, also simply referred to as “reactor”) of one embodiment
- FIG. 1A is a plane AA of the reactor 1 of FIG. It is a bottom view of'.
- the reactor 1 includes a plurality of reaction tubes 2, a thermometer protection tube 3 inserted into at least one of the plurality of reaction tubes 2 from the lower part of the reactor 1, and a thermometer protection tube 3. It is equipped with a thermometer 4 inserted in.
- the thermometer protection tube 3 may be fixed by a holding device 5 for preventing the thermometer protection tube 3 from falling off downward.
- the holding device 5 preferably has as large an opening as possible so as to minimize the obstruction of the flow of the reaction gas.
- the inside of the reaction tube 2 is filled with a catalyst as a fixed bed (supported on a carrier, not shown).
- the reaction substrate is supplied as the raw material gas S in the gas phase state to the reaction tube 2 from the raw material gas supply unit 9 at the upper part of the reactor 1 through the supply pipe 8, and reacts in the catalyst layer to produce the reaction product R. Occurs.
- the reaction product R is collected in the reaction product discharge unit 10 at the lower part of the reactor 1 and discharged through the take-out pipe 11.
- the reaction tube 2 is preferably a straight tube type from the viewpoints of equipment manufacturing, equipment maintenance, workability at the time of filling and replacing the catalyst, removal of reaction heat, and the like.
- the reaction tube 2 is preferably installed in the vertical direction (vertical type) from the viewpoint of workability of filling and extracting the catalyst.
- the upper end and the lower end of the reaction tube 2 are fixed by the upper fixing plate 12 and the lower fixing plate 13, respectively.
- the inner diameter, outer diameter, length, material and reaction heat removing equipment of the reaction tube 2 and the reaction heat removing method are not particularly limited, but the reaction heat removing efficiency, the heat exchange area and the pressure loss inside the reaction tube are balanced.
- the inner diameter of the reaction tube 2 is preferably 10 to 40 mm, and the length is preferably 1 to 8 m. Since there is a limitation in increasing the inner diameter of the reaction tube 2 in order to remove the heat of reaction, the reactor 1 is configured as a multi-tube reactor including a plurality of reaction tubes 2.
- the number of reaction tubes 2 is preferably, for example, 1000 to 20000 from the viewpoint of securing the production amount.
- the material of the reaction tube is preferably SUS because it has excellent heat resistance and corrosion resistance.
- the reactor 1 includes a cylindrical or square tubular jacket 6 for cooling the reaction tube 2 (heating at the start of the reaction).
- a heat medium introduction port 14 is provided above the lower fixing plate 13 on the side surface of the jacket 6, and a heat medium discharge port 15 is provided below the upper fixing plate 12 on the side surface of the jacket 6.
- the space defined by the jacket 6, the upper fixing plate 12, the lower fixing plate 13, and the outside of the reaction tube 2 is called a shell SH.
- the heat medium HM for controlling the temperature of the reaction tube 2 is introduced from the heat medium introduction port 14, passes through the shell SH, and is discharged from the heat medium discharge port 15.
- one or more baffles may be provided to define the flow direction of the heat medium HM and to make the temperature distribution of the heat medium HM more uniform in the entire shell SH.
- the temperature of the heat medium HM flowing through the shell SH is measured by the shell thermometer 7.
- the shell thermometer 7 is preferably arranged so that the temperature measuring portion is located at the center of the reactor 1 (in the case of a cylindrical reactor, the center of the circle of cross section and the vicinity of the midpoint of the height of the cylinder).
- the heat medium HM is preferably water (steam).
- the raw material gas S and the mist of the aqueous solution of the alkali metal acetate SA are supplied to the reaction tube 2 through the supply pipe 8.
- the raw material gas S is a lower olefin such as ethylene and propylene, acetic acid and oxygen gas.
- the lower olefin is preferably ethylene or propylene.
- the mist of the aqueous solution of the alkali metal acetate SA can be formed by spraying the aqueous solution of the alkali metal acetate SA into the raw material gas S.
- the alkali metal acetate SA is preferably at least one selected from the group consisting of potassium acetate and cesium acetate.
- the concentration of the aqueous solution of the alkali metal acetate SA is preferably 0.1 to 20% by mass.
- the concentration of the aqueous solution of the alkali metal acetate SA may be increased or decreased according to the lapse of the total reaction time.
- the supply rate of the alkali metal acetate SA is preferably 2 to 200 mg / h per 1 L of the volume of the catalyst layer.
- an inert gas may be supplied to the reaction tube 2 through the supply pipe 8.
- the inert gas is preferably nitrogen gas, carbon dioxide, or a mixed gas thereof.
- the reaction product R, unreacted gas, etc. are extracted through the take-out pipe 11.
- the reaction product R is vinyl acetate when the raw material gas S is ethylene, and allyl acetate when the raw material gas S is propylene.
- thermometer protection tube 3 is inserted from the lower part of the reactor 1 into at least one of the reaction tubes 2.
- the thermometer protection tube 3 is preferably inserted up to the vicinity of the upper part of the reaction tube 2.
- the number of reaction tubes 2 into which the thermometer protection tube 3 is inserted is preferably 3 to 10.
- thermometer protection tubes 3 are evenly or symmetrically arranged inside the reactor 1.
- thermometer protection tube 3 is arranged in the center of the reactor 1. In FIG. 1A, the thermometer protection tube 3 is inserted into five reaction tubes 2 including the central reaction tube 2, and the thermometer 4 is inserted into each of the thermometer protection tubes 3.
- the diameter of the thermometer protection tube 3 is preferably 1/6 to 1/2 of the inner diameter of the reaction tube 2, and more preferably 1/4 to 1/2 of the inner diameter of the reaction tube 2. If the thermometer protection tube 3 is too thick, the catalyst filling amount of the reaction tube 2 decreases, the cross-sectional area through which the raw material gas S flows decreases, and the pressure loss increases. Therefore, the thermometer protection tube 3 is inserted.
- the reaction amount of the reaction tube 2 may be relatively reduced, that is, the temperature rise due to the reaction heat of the entire reactor 1 and the measured value of the thermometer 4 may deviate from each other.
- the material of the thermometer protection tube 3 is preferably SUS because it is excellent in heat resistance and corrosion resistance.
- thermometer 4 is inserted in the thermometer protection tube 3.
- the thermometer is preferably a thermocouple or resistance thermometer.
- thermocouple capable of multi-point measurement, the catalyst layer temperature can be measured at a plurality of positions (heights) of the reaction tube 2.
- the catalyst for producing alkenyl acetate filled in the reaction tube 2 is not particularly limited as long as it is a solid catalyst, and a conventionally known catalyst can be used depending on the reaction.
- a catalyst having palladium as a main catalyst component and an alkali metal or an alkaline earth metal compound supported on a carrier as a co-catalyst, as described in JP-A-2-91045 (Patent Document 1) described above, can be mentioned. Be done.
- the method for preparing such a catalyst is not particularly limited, and various conventionally well-known methods can be adopted.
- the raw material used for preparing the catalyst is not particularly limited, and nitrates, carbonates, acetates, ammonium salts, oxides, halides and the like of each element can be used in combination.
- the allyl acetate production catalyst used in one embodiment is a compound having at least one element selected from the group consisting of (a) palladium, (b) gold, (c) copper, nickel, zinc and cobalt, (. d) Includes alkali metal acetate and (e) carrier.
- the vinyl acetate production catalyst used in one embodiment includes (a) palladium, (b) gold, (d) alkali metal acetate, and (e) carrier.
- a) palladium (b) gold, (d) alkali metal acetate, and (e) carrier.
- Palladium may have any valence, but is preferably metallic palladium.
- the "metal palladium" in the present disclosure has a valence of 0.
- Metallic palladium can usually be obtained by reducing divalent or tetravalent palladium ions with a reducing agent such as hydrazine or hydrogen. In this case, not all palladium may be in the metallic state.
- the raw material of palladium that is, the compound containing palladium is not particularly limited, and metallic palladium or a palladium precursor that can be converted to metallic palladium can be used.
- the metallic palladium and the palladium precursor are collectively referred to as "palladium raw material".
- the palladium precursor include palladium chloride, palladium nitrate, palladium sulfate, sodium palladium chloride, potassium palladium chloride, barium palladium chloride, and palladium acetate.
- sodium chloride palladium is used.
- the palladium precursor a single compound may be used, or a plurality of types of compounds may be used in combination.
- Gold is supported on a carrier in the form of a compound containing a gold element, but it is preferable that substantially all of the gold is metallic gold in the end.
- the "metal gold" in the present disclosure has a valence of zero.
- Metallic gold can usually be obtained by reducing monovalent or trivalent gold ions with a reducing agent such as hydrazine or hydrogen gas. In this case, not all gold need to be in a metallic state.
- the raw material of gold that is, the compound containing gold is not particularly limited, and a metallic gold or a gold precursor that can be converted to metallic gold can be used.
- metallic gold and gold precursors are collectively referred to as "gold raw materials”.
- Gold precursors include, for example, chloroauric acid, sodium chloroauric acid, and potassium chloroauric acid. Preferably, chloroauric acid or sodium chloroauric acid is used.
- the gold precursor a single compound may be used, or a plurality of types of compounds may be used in combination.
- (C) A compound having at least one element selected from the group consisting of copper, nickel, zinc and cobalt also simply referred to as "(c) 4th period metal compound” in the present disclosure.
- soluble salts such as nitrates, carbonates, sulfates, organic acid salts and halides of at least one element selected from the group consisting of copper, nickel, zinc and cobalt are used.
- the organic acid salt include acetate. In general, easily available and water-soluble compounds are preferred. Preferred compounds include copper nitrate, copper acetate, nickel nitrate, nickel acetate, zinc nitrate, zinc acetate, cobalt nitrate, and cobalt acetate. Of these, copper acetate is most preferred from the viewpoint of raw material stability and availability.
- As the 4th period metal compound a single compound may be used, or a plurality of types of compounds may be used in combination.
- the alkali metal acetate is preferably an acetate of at least one alkali metal selected from the group consisting of lithium, sodium, potassium, rubidium, and cesium. Specifically, potassium acetate, sodium acetate, and cesium acetate are preferable, and potassium acetate and cesium acetate are more preferable.
- the carrier (e) is not particularly limited, and a porous substance generally used as a catalyst carrier can be used.
- Preferred carriers include, for example, silica, alumina, silica-alumina, diatomaceous earth, montmorillonite, titania and zirconia, with silica being more preferred.
- the silica content of the carrier is preferably at least 50% by mass, more preferably at least 90% by weight, based on the mass of the carrier.
- the carrier preferably has a specific surface area measured by the BET method in the range of 10 to 1000 m 2 / g, and more preferably in the range of 100 to 500 m 2 / g.
- the bulk density of the carrier is preferably in the range of 50 to 1000 g / L, more preferably in the range of 300 to 500 g / L.
- the water absorption rate of the carrier is preferably 0.05 to 3 g-water / g-carrier, and more preferably 0.1 to 2 g-water / g-carrier.
- the average pore diameter thereof is preferably in the range of 1 to 1000 nm, and more preferably in the range of 2 to 800 nm. When the average pore diameter is 1 nm or more, gas diffusion can be facilitated. On the other hand, when the average pore diameter is 1000 nm or less, the specific surface area of the carrier required for obtaining catalytic activity can be secured.
- the shape of the carrier There are no particular restrictions on the shape of the carrier. Specific examples thereof include, but are not limited to, powdery, spherical, and pelletized. The optimum shape can be selected according to the reaction type and reactor used.
- the particle size of the carrier there is no particular limitation on the particle size of the carrier.
- the carrier is spherical, its particle diameter is preferably in the range of 1 to 10 mm, more preferably in the range of 2 to 8 mm.
- the reaction tube 2 is filled with a catalyst and the reaction is carried out, if the particle diameter is 1 mm or more, it is possible to prevent an excessive increase in pressure loss when the gas is circulated and to effectively circulate the gas. ..
- the particle diameter is 10 mm or less, it becomes easy to diffuse the raw material gas to the inside of the catalyst, and the catalytic reaction can be effectively promoted.
- the reaction tube 2 of the reactor 1 may be uniformly filled with a catalyst for producing alkenyl acetate, and two or more catalyst layers containing catalysts for producing alkenyl acetate having different amounts of alkali metal salts are provided in the flow direction (reaction direction) of the raw material gas. ) May be arranged so that the amount of the alkali metal acetate carried on the carrier gradually decreases from the inlet side to the outlet side of the reactor 1.
- the reaction for producing an alkenyl acetate is carried out in a gas phase using lower olefins, acetic acid and oxygen as raw materials.
- the reaction formula is as shown in the formula (1)
- the reaction formula is as shown in the formula (2).
- CH 2 CHCH 3 + CH 3 COOH + 1 / 2O 2 ⁇
- CH 2 CHCH 2 OCOCH 3 + H 2 O (2)
- the lower olefin is ethylene
- acetic acid: propylene: oxygen 1: 1 to 12: 0.5 to 2 is preferable.
- the raw material gas contains a lower olefin, acetic acid and oxygen gas, and may further contain nitrogen gas, carbon dioxide, a rare gas or the like as a diluent, if necessary.
- the raw material gas preferably contains 0.5 to 25 mol% of water, and more preferably 1 to 20 mol%. Without being bound by any theory, it is believed that the presence of water in the reaction system reduces the outflow of (d) alkali metal acetate from the catalyst. Even if a large amount of water exceeding 25 mol% is present, the above effect is not improved, and the produced alkenyl acetate may be hydrolyzed.
- the raw material gas is preferably supplied to the reactor 1 at a space speed of 10 to 15000 hr -1 in a standard state, and more preferably supplied to the reactor 1 at a space speed of 300 to 8000 hr -1 .
- the space velocity By setting the space velocity to 10 hr -1 or more, the heat of reaction can be appropriately removed.
- equipment such as a compressor can be made into a practical size.
- the reaction temperature is preferably in the range of 100 to 300 ° C, more preferably in the range of 120 to 250 ° C. By setting the reaction temperature to 100 ° C. or higher, the reaction rate can be set within a practical range. By setting the reaction temperature to 300 ° C. or lower, the heat of reaction can be appropriately removed.
- the reaction pressure is preferably in the range of 0 to 3 MPaG (gauge pressure), more preferably in the range of 0.1 to 1.5 MPaG.
- the reaction pressure can be set within a practical range.
- lower olefins such as ethylene and propylene contained in the raw material gas.
- high-purity hydrocarbons are preferably used, but lower saturated hydrocarbons such as methane, ethane, and propane may be mixed.
- oxygen gas there are no particular restrictions on oxygen gas. It can be supplied in the form of an inert gas such as nitrogen gas or carbon dioxide gas, for example, in the form of air, but when the gas after the reaction is circulated, it is generally high-concentration oxygen, preferably 99% by volume. It is advantageous to use oxygen of the above purity.
- Process 1 4.1 L of an aqueous solution containing 199 g of sodium palladium chloride and 4.08 g of sodium chloroauric acid tetrahydrate was prepared and used as an A-1 solution. To this, 12 L of a silica carrier (bulk density 473 g / L, water absorption amount 402 g / L) was added, and the A-1 solution was impregnated to absorb the entire amount.
- a silica carrier bulk density 473 g / L, water absorption amount 402 g / L
- Step 2 427 g of sodium metasilicate nine hydrate was dissolved in pure water and diluted with pure water to a total volume of 8.64 L using a measuring cylinder to prepare an A-2 solution.
- the metal-supported carrier (A-1) obtained in step 1 was impregnated with the A-2 solution and allowed to stand at room temperature (23 ° C.) for 20 hours.
- Process 3 300 g of hydrazine monohydrate was added to the slurry of the alkali-treated silica carrier (A-2) obtained in step 2, and the mixture was gently stirred and then allowed to stand at room temperature for 4 hours. After filtering the obtained catalyst, the catalyst was transferred to a glass column equipped with a stop cock, and pure water was circulated for 40 hours for washing. Then, it was dried at 110 ° C. for 4 hours under an air flow to obtain a metal-supported catalyst (A-3).
- Step 4 624 g of potassium acetate and 90 g of copper acetate monohydrate were dissolved in pure water and diluted with pure water to a total volume of 3.89 L using a measuring cylinder.
- the metal-supported catalyst (A-3) obtained in step 3 was added thereto, and the entire amount was absorbed. Then, it was dried at 110 ° C. for 20 hours under an air flow to obtain a catalyst A for producing allyl acetate.
- the amount of potassium acetate which is an alkali metal acetate in the catalyst, is determined by crushing the catalyst into a uniform powder, molding it, using X-ray fluorescence analysis (XRF), and using the absolute calibration beam method to obtain K (potassium). It was quantified as the content of atoms (% by mass).
- step 4 the operation of Production Example 1 was repeated except that the amount of potassium acetate was changed from 624 g to 396 g to produce the catalyst B.
- Example 1 Allyl acetate was produced using the fixed-bed multi-tube reactor 1 as shown in FIG.
- the number of reaction tubes 2 was about 5000, and each reaction tube 2 was arranged in a hexagonal lattice.
- the length of the reaction tube 2 was about 6.3 m, and the inner diameter was 34 mm.
- inert balls are placed in order from the inlet side (upper side) to the outlet side of the raw material gas on the upstream side of the catalyst on the raw material gas inlet side.
- A was packed with a layer length of 3.3 m, and a catalyst B having a small potassium acetate carrier and low activity was filled with a layer length of 2.2 m.
- thermometer protection tube 3 having an outer diameter of 8 mm and an inner diameter of 6 mm was inserted into three of the reaction tubes 2 from the lower part of the reactor 1.
- a multi-point thermocouple capable of measuring the temperature at different heights (upper, middle and lower parts of the catalyst layer) is inserted into each thermometer protection tube 3 as a thermometer 4, and the catalyst during the reaction is being reacted.
- the layer temperature was monitored.
- the shell temperature was measured by a thermocouple arranged as a shell thermometer 7 in the center of the reactor 1.
- the raw material gas having the composition shown in Table 1 was circulated at a space velocity of 2000h -1 , and the reaction was carried out under the conditions of a reaction temperature of 160 ° C. and a reaction pressure of 0.75 MPaG (gauge pressure).
- An aqueous potassium acetate solution (1.5% by mass) was sprayed into the raw material gas from a spray nozzle at a supply amount of 24 g / h.
- FIG. 2A schematically shows the catalyst filling state of the reaction tube of Example 1 before and after the reaction.
- FIG. 2B schematically shows the catalyst filling state of the reaction tube of Comparative Example 1 before and after the reaction.
- FIG. 2C schematically shows the catalyst filling state of the reaction tube of Reference Example 1 before and after the reaction.
- 3A and 3B show the temperature difference (catalyst layer temperature-shell temperature) between the catalyst layer temperature and the shell temperature inside the reaction tube 2 in the central portion of the reactor 1 during the reaction in Example 1 and Comparative Example 1, respectively. Is shown. Since the gas-phase catalytic oxidation reaction for synthesizing allyl acetate is an exothermic reaction, if the reaction proceeds normally, the temperature of the catalyst layer becomes higher, that is, a positive temperature difference is observed.
- Example 1 in which the thermometer protection tube 3 was inserted into the reaction tube 2 from the lower part of the reactor 1, the temperature difference continued to be observed even after 1000 hours from the start of the reaction. From this, it can be seen that the catalyst layer temperature can be correctly and continuously monitored by inserting the thermometer protection tube into the reaction tube from the lower part of the reactor.
- Table 2 shows the potassium (K) loading amount of the catalysts of Example 1, Comparative Example 1, and Reference Example 1.
- the amount of K carried by catalyst A was 3.8% by mass, and the amount of K carried by catalyst B was 2.5% by mass.
- Example 1 the amount of K carried by the catalyst G extracted from the reaction tube 2 into which the thermometer protection tube 3 was inserted was 2.9% by mass, and the K of the catalyst H was K. The loading amount was 8.0% by mass.
- Comparative Example 1 the K-supported amount of the catalyst E extracted from the reaction tube 2 into which the thermometer protection tube 3 was inserted from the upper part of the reactor 1 was 12.6% by mass, and the K-supported amount of the catalyst F was 12.1% by mass. %, And excess potassium was carried.
- the K-supported amount of the catalyst C extracted from the reaction tube 2 into which the thermometer protection tube 3 was not inserted was 3.8% by mass, and the K-supported amount of the catalyst D was 8.5% by mass.
- the catalyst extracted from the reaction tube 2 into which the thermometer protection tube 3 is inserted from the upper part of the reactor 1 is mostly the reaction tube 2 in which the thermometer protection tube 3 is not inserted. It can be seen that the behavior is significantly different from that of the above, and the representativeness of the entire catalyst layer is not shown.
- the catalyst extracted from the reaction tube 2 into which the thermometer protection tube 3 is inserted from the lower part of the reactor 1 behaves similarly to most of the reaction tubes 2 in which the thermometer protection tube 3 is not inserted, and is a catalyst. It can be seen that it shows the representativeness of the layer.
- alkenyl acetate can be industrially stably produced.
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Abstract
Description
[1]
酢酸アルケニル製造用の固定床多管式反応器であって、
前記固定床多管式反応器の上部から原料ガス、及びアルカリ金属酢酸塩の水溶液のミストが供給される複数の反応管と、
前記固定床多管式反応器の下部から前記複数の反応管の少なくとも1本に挿入された温度計保護管と、
前記温度計保護管に挿入された温度計と、
を備えた固定床多管式反応器。
[2]
前記アルカリ金属酢酸塩が酢酸カリウム及び酢酸セシウムからなる群より選択される少なくとも1種である、[1]に記載の固定床多管式反応器。
[3]
前記温度計保護管が挿入された前記反応管の数が3~10である、[1]又は[2]のいずれかに記載の固定床多管式反応器。
[4]
前記温度計が熱電対又は抵抗温度計である、[1]~[3]のいずれかに記載の固定床多管式反応器。
一実施形態の酢酸アルケニル製造用の固定床多管式反応器は、固定床多管式反応器の上部から原料ガス、及びアルカリ金属酢酸塩の水溶液のミストが供給される複数の反応管と、固定床多管式反応器の下部から複数の反応管の少なくとも1本に挿入された温度計保護管と、温度計保護管に挿入された温度計とを備える。
反応管2に充填される酢酸アルケニル製造用触媒としては、固体触媒であれば特に限定されず、反応に応じて従来から知られている触媒を使用することができる。例えば、上述の特開平2-91045号公報(特許文献1)に記載されたような、パラジウムを主触媒成分とし、助触媒としてアルカリ金属又はアルカリ土類金属化合物を担体に担持させた触媒が挙げられる。
(a)パラジウムは、いずれの価数を持つものであってもよいが、好ましくは金属パラジウムである。本開示における「金属パラジウム」とは、0価の価数を持つものである。金属パラジウムは、通常、2価又は4価のパラジウムイオンを、還元剤であるヒドラジン、水素などを用いて還元することにより得ることができる。この場合、全てのパラジウムが金属状態になくてもよい。
(b)金は、金元素を含む化合物の形で担体に担持されるが、最終的には実質的にすべてが金属金であることが好ましい。本開示における「金属金」とは、0価の価数を持つものである。金属金は、通常、1価又は3価の金イオンを、還元剤であるヒドラジン、水素ガスなどを用いて還元することにより得ることができる。この場合、全ての金が金属状態になくてもよい。
(c)第4周期金属化合物としては、銅、ニッケル、亜鉛及びコバルトからなる群より選択される少なくとも1種の元素の硝酸塩、炭酸塩、硫酸塩、有機酸塩、ハロゲン化物などの可溶性塩を使用することができる。有機酸塩としては酢酸塩などが挙げられる。一般には、入手しやすく、水溶性である化合物が好ましい。好ましい化合物としては、硝酸銅、酢酸銅、硝酸ニッケル、酢酸ニッケル、硝酸亜鉛、酢酸亜鉛、硝酸コバルト、及び酢酸コバルトが挙げられる。これらの中では、原料の安定性、入手のしやすさの観点から、酢酸銅が最も好ましい。(c)第4周期金属化合物として、単独の化合物を用いてもよく、複数の種類の化合物を併用することもできる。
(d)アルカリ金属酢酸塩は、リチウム、ナトリウム、カリウム、ルビジウム、及びセシウムからなる群より選択される少なくとも1種のアルカリ金属の酢酸塩であることが好ましい。具体的には、酢酸カリウム、酢酸ナトリウム、及び酢酸セシウムが好ましく、酢酸カリウム、及び酢酸セシウムがより好ましい。
(e)担体として、特に制限はなく、触媒用担体として一般に用いられている多孔質物質を使用することができる。好ましい担体として、例えば、シリカ、アルミナ、シリカ-アルミナ、珪藻土、モンモリロナイト、チタニア及びジルコニアが挙げられ、より好ましくはシリカである。担体としてシリカを主成分とするものを用いる場合には、担体のシリカ含有量は、担体の質量に対して、好ましくは少なくとも50質量%、より好ましくは少なくとも90重量%である。
反応器1の反応管2に酢酸アルケニル製造用触媒を均一に充填してもよく、アルカリ金属塩量の異なる酢酸アルケニル製造用触媒を含む2以上の触媒層を、原料ガスの流れ方向(反応方向)に沿って、アルカリ金属酢酸塩の担体への担持量が反応器1の入口側から出口側に向かって順次低くなるように配置してもよい。
酢酸アルケニルを製造するための反応は、低級オレフィン、酢酸及び酸素を原料として気相で行われる。例えば、低級オレフィンがエチレンの場合、反応式は式(1)のとおりであり、プロピレンの場合、反応式は式(2)のとおりである。
CH2=CH2+CH3COOH+1/2O2→
CH2=CHOCOCH3+H2O (1)
CH2=CHCH3+CH3COOH+1/2O2→
CH2=CHCH2OCOCH3+H2O (2)
シリカ球状担体(球体直径5mm、比表面積155m2/g、吸水率0.85g-水/g-担体、以下単に「シリカ担体」という。)を用い、以下の手順で触媒Aの製造を行った。
塩化パラジウム酸ナトリウム199g及び塩化金酸ナトリウム四水和物4.08gを含有する水溶液4.1Lを調製し、A-1溶液とした。これにシリカ担体(嵩密度473g/L、吸水量402g/L)12Lを加え、A-1溶液を含浸させて、全量を吸収させた。
メタケイ酸ナトリウム九水和物427gを純水に溶解させ、メスシリンダーを用い、全量が8.64Lとなるように純水で希釈して、A-2溶液とした。工程1で得た金属担持担体(A-1)にA-2溶液を含浸させて、室温(23℃)で20時間静置した。
工程2で得られたアルカリ処理シリカ担体(A-2)のスラリーにヒドラジン一水和物300gを添加し、緩やかに撹拌した後、室温で4時間静置した。得られた触媒を濾過後、ストップコック付のガラスカラムに移し、40時間純水を流通させて洗浄した。次いで、空気気流下、110℃で4時間乾燥を行い、金属担持触媒(A-3)を得た。
酢酸カリウム624g、及び酢酸銅一水和物90gを純水に溶解させ、メスシリンダーを用い、全量が3.89Lとなるように純水で希釈した。これに工程3で得られた金属担持触媒(A-3)を加え、全量を吸収させた。次いで、空気気流下、110℃で20時間乾燥を行い、酢酸アリル製造用触媒Aを得た。
工程4において、酢酸カリウムの量を624gから396gに変更した以外は製造例1の操作を繰り返して、触媒Bの製造を行った。(a)、(b)、(c)及び(d)の質量比は、(a):(b):(c):(d)=1:0.024:0.39:5.4であった。(e)担体1gあたりの(d)アルカリ金属酢酸塩(酢酸カリウム)の担持量(g)は0.069g/gであった。
図1に示すような固定床多管式反応器1を用いて酢酸アリルの製造を行った。反応管2の数は約5000であり、各反応管2は六方格子状に配列されていた。反応管2の長さは約6.3m、内径は34mmであった。反応管2に、原料ガスの入口側(上方)から出口側に向かって順に、イナートボールを原料ガス入口側で触媒の上流側に層長0.8m、酢酸カリウム担持量が多く活性の高い触媒Aを層長3.3m、酢酸カリウム担持量が少なく活性の低い触媒Bを層長2.2mとなるように充填した。
温度計保護管3を反応管2に反応器1の上部から挿入したことを除き、実施例1と同様にして酢酸アリルの製造を行った。
実施例1において、反応終了後、温度計保護管3が挿入されていない反応管2から、触媒を原料ガスの入口側から3:2に分割して抜き出し、反応管2の入口側を触媒C、反応管2の出口側を触媒Dとした。図2Cに、反応前後の参考例1の反応管の触媒充填状態を模式的に示す。
2 反応管
3 温度計保護管
4 温度計
5 保持装置
6 ジャケット
7 シェル温度計
8 供給配管
9 原料ガス供給部
10 反応生成物排出部
11 取出配管
12 上側固定板
13 下側固定板
14 熱媒導入口
15 熱媒排出口
S 原料ガス
R 反応生成物
SA アルカリ金属酢酸塩
HM 熱媒
SH シェル
Claims (4)
- 酢酸アルケニル製造用の固定床多管式反応器であって、
前記固定床多管式反応器の上部から原料ガス、及びアルカリ金属酢酸塩の水溶液のミストが供給される複数の反応管と、
前記固定床多管式反応器の下部から前記複数の反応管の少なくとも1本に挿入された温度計保護管と、
前記温度計保護管に挿入された温度計と、
を備えた固定床多管式反応器。 - 前記アルカリ金属酢酸塩が酢酸カリウム及び酢酸セシウムからなる群より選択される少なくとも1種である、請求項1に記載の固定床多管式反応器。
- 前記温度計保護管が挿入された前記反応管の数が3~10である、請求項1又は2のいずれか一項に記載の固定床多管式反応器。
- 前記温度計が熱電対又は抵抗温度計である、請求項1~3のいずれか一項に記載の固定床多管式反応器。
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