WO2006042659A1 - Reaktor und verfahren zur synthese von vinylacetat in der gasphase - Google Patents
Reaktor und verfahren zur synthese von vinylacetat in der gasphase Download PDFInfo
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- WO2006042659A1 WO2006042659A1 PCT/EP2005/010883 EP2005010883W WO2006042659A1 WO 2006042659 A1 WO2006042659 A1 WO 2006042659A1 EP 2005010883 W EP2005010883 W EP 2005010883W WO 2006042659 A1 WO2006042659 A1 WO 2006042659A1
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- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims description 43
- 239000007792 gaseous phase Substances 0.000 title 1
- 239000003054 catalyst Substances 0.000 claims abstract description 107
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 30
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 27
- 239000010931 gold Substances 0.000 claims abstract description 26
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 22
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000005977 Ethylene Substances 0.000 claims abstract description 18
- 229910052737 gold Inorganic materials 0.000 claims abstract description 17
- 239000001301 oxygen Substances 0.000 claims abstract description 17
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 238000007036 catalytic synthesis reaction Methods 0.000 claims abstract description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 29
- 229910052763 palladium Inorganic materials 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 239000011230 binding agent Substances 0.000 claims description 12
- 239000002360 explosive Substances 0.000 claims description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 8
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 8
- 229910044991 metal oxide Inorganic materials 0.000 claims description 7
- 150000004706 metal oxides Chemical class 0.000 claims description 7
- 239000000377 silicon dioxide Substances 0.000 claims description 6
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims description 5
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 5
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 5
- GEIAQOFPUVMAGM-UHFFFAOYSA-N ZrO Inorganic materials [Zr]=O GEIAQOFPUVMAGM-UHFFFAOYSA-N 0.000 claims description 5
- 239000002585 base Substances 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 229910052684 Cerium Inorganic materials 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 4
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 4
- 229910052910 alkali metal silicate Inorganic materials 0.000 claims description 4
- 235000012216 bentonite Nutrition 0.000 claims description 4
- 239000012876 carrier material Substances 0.000 claims description 4
- 229920002678 cellulose Polymers 0.000 claims description 4
- 239000001913 cellulose Substances 0.000 claims description 4
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 4
- 229910017052 cobalt Inorganic materials 0.000 claims description 4
- 239000010941 cobalt Substances 0.000 claims description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 4
- 229910052802 copper Inorganic materials 0.000 claims description 4
- 239000010949 copper Substances 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 229910052747 lanthanoid Inorganic materials 0.000 claims description 4
- 150000002602 lanthanoids Chemical class 0.000 claims description 4
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 claims description 4
- 229920000609 methyl cellulose Polymers 0.000 claims description 4
- 235000010981 methylcellulose Nutrition 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 229910052700 potassium Inorganic materials 0.000 claims description 4
- 239000011591 potassium Substances 0.000 claims description 4
- 235000019353 potassium silicate Nutrition 0.000 claims description 4
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 239000010935 stainless steel Substances 0.000 claims description 4
- 229910052720 vanadium Inorganic materials 0.000 claims description 4
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 2
- 150000001339 alkali metal compounds Chemical class 0.000 claims description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 2
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 2
- 150000002739 metals Chemical class 0.000 claims description 2
- 235000010980 cellulose Nutrition 0.000 claims 2
- 230000004913 activation Effects 0.000 claims 1
- 239000012267 brine Substances 0.000 claims 1
- 230000003197 catalytic effect Effects 0.000 claims 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims 1
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 15
- 238000002474 experimental method Methods 0.000 description 15
- 239000006227 byproduct Substances 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 239000000203 mixture Substances 0.000 description 10
- 239000013590 bulk material Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 6
- 238000011068 loading method Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000012360 testing method Methods 0.000 description 6
- 241000282326 Felis catus Species 0.000 description 4
- 239000001307 helium Substances 0.000 description 4
- 229910052734 helium Inorganic materials 0.000 description 4
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 4
- 239000011261 inert gas Substances 0.000 description 4
- SCVFZCLFOSHCOH-UHFFFAOYSA-M potassium acetate Chemical compound [K+].CC([O-])=O SCVFZCLFOSHCOH-UHFFFAOYSA-M 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- 150000001340 alkali metals Chemical class 0.000 description 3
- 238000000465 moulding Methods 0.000 description 3
- 239000010970 precious metal Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910004373 HOAc Inorganic materials 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 229910052793 cadmium Inorganic materials 0.000 description 2
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 235000011056 potassium acetate Nutrition 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- 238000001228 spectrum Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- JNBLCHLVUYMNLH-UHFFFAOYSA-N 1-acetyloxyethenyl acetate Chemical group CC(=O)OC(=C)OC(C)=O JNBLCHLVUYMNLH-UHFFFAOYSA-N 0.000 description 1
- GOKCJCODOLGYQD-UHFFFAOYSA-N 4,6-dichloro-2-imidazol-1-ylpyrimidine Chemical compound ClC1=CC(Cl)=NC(N2C=NC=C2)=N1 GOKCJCODOLGYQD-UHFFFAOYSA-N 0.000 description 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 150000001242 acetic acid derivatives Chemical class 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- VEVRNHHLCPGNDU-MUGJNUQGSA-O desmosine Chemical compound OC(=O)[C@@H](N)CCCC[N+]1=CC(CC[C@H](N)C(O)=O)=C(CCC[C@H](N)C(O)=O)C(CC[C@H](N)C(O)=O)=C1 VEVRNHHLCPGNDU-MUGJNUQGSA-O 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 229910052735 hafnium Inorganic materials 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/44—Palladium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
- B01J19/249—Plate-type reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/48—Silver or gold
- B01J23/52—Gold
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0215—Coating
- B01J37/0225—Coating of metal substrates
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00085—Plates; Jackets; Cylinders
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00783—Laminate assemblies, i.e. the reactor comprising a stack of plates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
- B01J2219/00835—Comprising catalytically active material
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00873—Heat exchange
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2461—Heat exchange aspects
- B01J2219/2462—Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2476—Construction materials
- B01J2219/2477—Construction materials of the catalysts
- B01J2219/2479—Catalysts coated on the surface of plates or inserts
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2476—Construction materials
- B01J2219/2483—Construction materials of the plates
- B01J2219/2485—Metals or alloys
- B01J2219/2486—Steel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2491—Other constructional details
- B01J2219/2497—Size aspects, i.e. concrete sizes are being mentioned in the classified document
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/58—Platinum group metals with alkali- or alkaline earth metals
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/66—Silver or gold
Definitions
- the invention is directed to a synthesis reactor for the production of monomeric vinyl acetate (VAM), in which gaseous ethylene and gaseous acetic acid and oxygen or oxygen-containing gases catalytically react, wherein the synthesis reactor is a wall reactor in which the catalytic synthesis in a plurality of reaction spaces takes place which, with respect to the free flow cross-section, are smaller than 2000 ⁇ m, preferably smaller than 1000 ⁇ m, at least in one dimension and whose indirectly cooled walls are coated with a palladium-gold catalyst.
- VAM monomeric vinyl acetate
- ethylene, acetic acid and molecular oxygen or O 2 -containing gases optionally with the addition of inert gases such as CO 2 , at temperatures of 100 0 C to 250 0 C and elevated pressure in the presence of a catalyst is reacted. This is done by passing the process gas over a catalyst bed.
- a catalyst is usually used which contains palladium, gold and alkali metals on an oxidic support.
- the catalyst is in the form of shaped bodies, such as, for example, spheres, granules, tablets or extrudates, on which the catalytically active substances are applied in a shell-shaped outer zone.
- EP 1 106 247 B1 describes such a process and a suitable catalyst, wherein the supported catalyst has an ideal Pd content of 0.3 to 4.0% by weight and an Au content of 0.1 to 2.0 % By weight.
- the catalyst thickness on the support is given with a maximum of 1 mm and preferably less than 0.5 mm.
- EP 1 106 247 B1 mentions productivities (referred to in the document as activity) which amount to a maximum of 225.5 gV A iv / kgK at * h. Although a high selectivity is mentioned in the document, it is not described or quantified as a function of the selected supported catalyst or the preparation process.
- EP 0 987 058 B1 describes a supported catalyst based on silicon dioxide, which has a special carrier geometry.
- DE 199 14 066 discloses a catalyst in which barium or cadmium are used as doping elements and different metal oxides in the carrier body.
- Cadmium is disadvantageous from an environmental point of view.
- EP 196 19 961, EP 0 916 402 A1 or EP 0 997 192 B1 to optimize carrier bodies with regard to their external shape. Pressings, cylinders, rings and other forms which are used in VAM synthesis are known.
- EP 1 323 469 A3 describes a shaped body which has special open structures as the pyrogenically produced silicon dioxide body.
- EP 1 106 247 B1 specifies external dimensions of 2-15 mm for such molded articles. The loading is given as 0.2-1.5% by weight of Au, 0.3-4.0% by weight of Pd and 3.5-10% by weight of potassium acetate.
- EP 0 997 291 B1 mentions support materials which consist of at least two components of the group SiO 2 , Al 2 O 3 , TiO 2 and ZrO 2 . According to the aforementioned document, these carrier materials can be present in any desired form, for example as cylinders, spheres or rings, which are produced as extrudates, extrudates or tablets.
- EP 0 723 810 B1 also discloses a support material which contains the elements zirconium and titanium. As an advantage of the invention is shown in the examples mac ⁇ that a productivity of 225 GM AM / kg ⁇ a t * h is achieved. It is further known and described in the art that a number of by-products are formed in VAM synthesis.
- EP 0 072 484 discloses a process which results in improved dewatering by adding small amounts of H 2 O to a vinyl acetate recycle stream and introducing it into the distillation.
- DE 198 25 254 an analogous makesver ⁇ drive is described, in which in addition to water and acetic acid is added to this reflux stream, whereby a reduction in the ethyl acetate content is achieved.
- These methods are downstream of the synthesis process steps and reduce the formation of by-products by additional measures. There continues to be a lack of a method which allows both a high produc tivity and a high selectivity of the catalyst.
- the object of the invention is thus to remedy the deficiency in the prior art and to reduce the formation of by-products and at the same time to achieve high selectivity and productivity.
- the productivity is determined as the formed mass of vinyl acetate per catalyst mass and time unit with the unit gv AM / kg ⁇ a t * h, wherein the mass of the catalyst was calculated without binder.
- the device according to the invention and the method according to the invention solve this problem in the prior art by using a synthesis reactor for use in the production of vinyl acetate, in which gaseous ethylene and acetic acid and oxygen or oxygen-containing gases catalytically react, wherein a wall reactor is used as the synthesis reactor is used.
- This wall reactor has a multiplicity of reaction spaces in which the catalytic reaction takes place. At least one wall in each of these reaction spaces is coated with a catalyst and indirectly cooled.
- the dimensioning of the reaction chamber is selected such that the free flow cross section in each of these reaction chambers is smaller than 2000 ⁇ m, preferably smaller than 1000 ⁇ m, at least in one dimension.
- the reaction chambers consist of a multiplicity of tubes or of stacked plates which have a large number of gaps, wherein the tubes or gaps can have any desired orientation relative to one another and ideally run parallel to one another.
- the device of the invention comprises a catalyst containing palladium, gold and alkali metal compounds on an oxidic support material and is applied by means of a binder adhering to the wall surfaces of the reaction spaces.
- the palladium content of the catalyst according to the invention is 0.3 to 10% by weight.
- the metals can be distributed throughout the catalyst layer since, owing to the small layer thickness and the high porosity of the support material, there are no mass transfer resistances in the reaction which have a negative effect on the activity.
- the local selenium metal concentration in the catalyst layer is not locally excessive due to this largely homogeneous distribution, so that the catalytically active metal surface as a surface is optimal and correspondingly high activities are achieved.
- a catalyst verwen ⁇ det which has an alkali metal content of 0.4 to 6, preferably 1 to 4 wt .-% Alkali ⁇ metal.
- the alkali metal used is primarily potassium, which is preferably present in the form of its acetate.
- the catalyst used contains one or more elements from the group of Erdal ⁇ kalimetalle, lanthanides, vanadium, iron, manganese, cobalt, nickel, copper, cerium, platinum, wherein the total content of these elements 3 wt .-% does not exceed.
- a catalyst in the synthesis thesereaktor which contains an oxidic support material having as main component an oxide from the group SiO 2 , Al 2 O 3 , TiO 2 and ZrO 2 .
- the support material contains further oxides as secondary components.
- bentonites can be used as natural mixed oxides.
- an advantageous embodiment of the device according to the invention is that the base material of the reaction chambers be ⁇ at least partially made of stainless steel be ⁇ , and the catalyst is applied using an oxidic or organic binder on the stainless steel walls to be coated.
- binders from the groups of the metal oxide sols, cellulose derivatives or alkali metal silicates, for example silica sols, methylcelluloses or waterglass.
- the invention also includes a method using the above-described reactor, wherein the reactor is operated almost isothermally, and the maximum temperature increase between the inlet and outlet of the synthesis reactor 5 K, preferably 2 K.
- This small increase in temperature is not only due to the difference in inlet and outlet temperatures, but equally applies to all areas within the reactor.
- the inventive method is further characterized in that in the reaction chambers, a temperature of 100 to 250 0 C and preferably from 150 to 200 0 C is present, wherein the pressure in the range of 1 to 12 bar and preferably 6 to 10 absolute bar.
- the method according to the invention can be carried out in explosive process states, and no restrictions must be accepted with regard to the optimal operating parameters, which therefore result in explosive states being reached.
- Explosive conditions are understood as meaning gas mixtures having a composition which can be exploded under the conditions present in the process, such as pressure and temperature, in a defined volume.
- the lower explosive limit for oxygen is quantified in US 3,855,280 with typically 8%.
- Processes according to the invention include process states in which an O 2 content of more than 7% by volume is present in the process gas.
- the invention comprises a catalyst for use in a reactor for vinyl acetate synthesis, which is characterized in that the palladium content of the catalyst is from 0.5 to 10% by weight and preferably from 0.8 to 5% by weight .-% is.
- the gold content of the catalyst is 0.25 to 5% by weight and preferably 0.4 to 2.5% by weight.
- the potassium content of the catalyst is 0.5 to 10% by weight and preferably 1 to 4% by weight.
- the support material of the catalyst according to the invention comprises an oxidic material with an oxide from the group SiO 2 , Al 2 O 3 , TiO 2 and ZrO 2 , wherein in an advantageous embodiment the support material comprises further oxides as secondary components includes.
- Bentonites for example, can be used as natural mixed oxides.
- the catalyst layer applied by means of an oxidic or organic binder on the walls of the reaction spaces is, wherein the proportion of the binder in the catalyst layer is 0-50 wt .-% and preferably to be used binders from the groups metal oxide sols, cellulose derivatives or alkali metal silicates such as silica sols, methylcelluloses or waterglass.
- An optimized embodiment of the catalyst according to the invention consists in that all the aforementioned doping and activating elements are distributed homogeneously in the entire volume of the catalyst layer and there is no stratification, as is usual in the case of the coated catalysts known from the prior art.
- the catalyst was prepared analogously to the preparation in EP 1 008 385 A1, a powdered SiO 2 -containing carrier being used which is identical in composition to a customary bulk material catalyst carrier. Subsequently, the catalyst was applied to two stainless steel plates with Ste ⁇ conditions and activated with potassium acetate. The plate pairs are connected to one another in such a way that the catalyst layers lie opposite each other and a gap of approximately 500 ⁇ m is formed. This pair of plates is placed in a pressure-resistant reactor, which was heated with oil and operated almost completely isothermally at 155 0 C. The temperature rise was less than 1 K, with 5 measuring points measured along the course of the flow.
- the pressure in the reactor was in the range of 5 bar to 9 bar absolute. Ethylene, oxygen, methane and helium were metered in gaseous form, with methane as the internal standard for the analysis.
- the acetic acid was metered in liquid and evaporated in front of the reactor.
- the gas mixture entering the reactor had the following composition, expressed in volume percent: 63.2% ethylene, 5.7% oxygen, 4.2% methane, 9.6% helium and 17.2% acetic acid.
- the system is initially deoxygenated, but the oxygen content can be quickly increased to the standard level over an hour.
- the analysis is carried out by gas chromatography and a CO 2 detector.
- an advantage of the invention is to operate the process at a gas load of up to about 12,000 l / kg * h.
- the pressure loss in the reactor according to the invention is markedly lower owing to the deflection and low-interference flow guidance than in the known tubular reactor which has a catalyst bed.
- a further increase in gas load above 12,000 l / kg * h does not significantly increase productivity.
- test conditions 3 and 4 are in the explosive range with respect to the O 2 -C 2 H 4 ratios. It's the Advantage of the invention is to be seen in that to increase the productivity explosive process States to optimize the process can be set very specific.
- a Pd-Au catalyst was used, which was prepared on the basis of the method described in EP 0 723 810 A1.
- standing experiments described particles with a particle size of 50-150 microns used.
- the base material is identical to that of the moldings.
- the ethylene concentration in the reactant stream was reduced in comparison to the tests 1 to 6 and replaced by a corresponding volume fraction of inert gas and a small proportion of steam.
- a change in the ethylene content in the starting material stream to the extent has negligible influence on the synthesis reaction.
- the wall catalyst prepared by the aforementioned method was used, which contained 2.5% by weight of Pd and 1.1% by weight of Au.
- a gas temperature of 155 ° C and a pressure of 9 bar was set.
- the composition of the educt gas was chosen as follows:
- experiment 8 the process known from the prior art was investigated by using a bulk material catalyst in the tubular reactor in comparison with the process according to the invention using a microreactor.
- the wall catalyst prepared by the aforementioned method was used, which likewise contained 1.1% by weight. % Au.
- the gas temperature was 155 ° C and the pressure 9 bar, with a gas load of 12,000 l / kg ⁇ at * h was selected.
- composition of the educt gas was chosen as follows:
- the wall catalyst also exhibits a higher VAM selectivity with respect to ethylene than the bulk catalyst at elevated C 2 H 4 conversion. Overall, this leads to a productivity of the wall catalyst of 2050 gV AM / kg Ka t * n compared to 720 gV AM / kg cat * h of the bulk material catalyst.
- the wall catalyst it was possible to choose a metal coating which can not be implemented on the bulk material catalyst, since such a high loading with Pd and Au leads to such strong local overheating, so-called "hot spots".
- the respective value for the productivity after 10 hours was taken as the base value and the relative change to this base value is shown in Table 10.
- the measured data show the surprising result that the wall catalyst barely deactivates during a period of 100 hours in comparison to the bulk material catalyst despite significantly higher productivity. This is a considerable advantage of the wall catalyst over the known bulk material catalyst for industrial use.
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Abstract
Description
Claims
Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2005297591A AU2005297591A1 (en) | 2004-10-15 | 2005-10-10 | Reactor and method for synthesising vinyl acetate in the gaseous phase |
MX2007004497A MX2007004497A (es) | 2004-10-15 | 2005-10-10 | Reactor y metodo para la sintesis de acetato de vinilo en fase gaseosa. |
US11/665,079 US20090054683A1 (en) | 2004-10-15 | 2005-10-10 | Reactor and method for synthesising vinyl acetate in the gaseous phase |
JP2007536062A JP2008516906A (ja) | 2004-10-15 | 2005-10-10 | 気相で酢酸ビニルを合成するための反応器及び方法 |
EP05798523.6A EP1804963B1 (de) | 2004-10-15 | 2005-10-10 | Reaktor und verfahren zur synthese von vinylacetat in der gasphase |
CA002584173A CA2584173A1 (en) | 2004-10-15 | 2005-10-10 | Reactor and method for synthesising vinyl acetate in the gaseous phase |
BRPI0516508-3A BRPI0516508A (pt) | 2004-10-15 | 2005-10-10 | reator e método para sìntese de acetato de vinila em fase gasosa |
IL182479A IL182479A0 (en) | 2004-10-15 | 2007-04-11 | Reactor and method for synthesising vinyl acetate in the gaseous phase |
NO20072450A NO20072450L (no) | 2004-10-15 | 2007-05-10 | Reaktor og fremgangsmate for a syntetisere vinylacetat i gassfasen |
Applications Claiming Priority (2)
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DE102004050585A DE102004050585A1 (de) | 2004-10-15 | 2004-10-15 | Mikroreaktor und Verfahren zur Synthese von Vinylacetat-Monomer (VAM) in der Gasphase |
DE102004050585.3 | 2004-10-15 |
Publications (1)
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WO2006042659A1 true WO2006042659A1 (de) | 2006-04-27 |
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PCT/EP2005/010883 WO2006042659A1 (de) | 2004-10-15 | 2005-10-10 | Reaktor und verfahren zur synthese von vinylacetat in der gasphase |
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Country | Link |
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US (1) | US20090054683A1 (de) |
EP (2) | EP1804963B1 (de) |
JP (1) | JP2008516906A (de) |
KR (1) | KR20070100692A (de) |
CN (1) | CN101056699A (de) |
AU (1) | AU2005297591A1 (de) |
BR (1) | BRPI0516508A (de) |
CA (1) | CA2584173A1 (de) |
DE (1) | DE102004050585A1 (de) |
IL (1) | IL182479A0 (de) |
MX (1) | MX2007004497A (de) |
NO (1) | NO20072450L (de) |
RU (1) | RU2007117920A (de) |
SG (3) | SG149035A1 (de) |
TW (1) | TW200626229A (de) |
WO (1) | WO2006042659A1 (de) |
ZA (1) | ZA200702978B (de) |
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WO2010094660A1 (de) | 2009-02-19 | 2010-08-26 | Wacker Chemie Ag | Verfahren und vorrichtung zur herstellung von vinylacetat |
DE102011081786A1 (de) | 2011-08-30 | 2013-02-28 | Wacker Chemie Ag | Verfahren zur Acetoxylierung von Olefinen in der Gasphase |
WO2024030440A1 (en) | 2022-08-05 | 2024-02-08 | Celanese International Corporation | Zone catalyst loading and processes for the acetoxylation of olefins using the same |
WO2024030439A1 (en) | 2022-08-05 | 2024-02-08 | Celanese International Corporation | Catalyst for olefin acetoxylation |
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DE10361893A1 (de) * | 2003-12-19 | 2005-07-21 | Degussa Ag | Spezielles Verfahren zur Herstellung von Fluoralkylgruppen tragenden Siliciumverbindungen durch Hydrosilylierung |
US7468455B2 (en) * | 2004-11-03 | 2008-12-23 | Velocys, Inc. | Process and apparatus for improved methods for making vinyl acetate monomer (VAM) |
DE102007023762A1 (de) * | 2006-08-10 | 2008-02-14 | Evonik Degussa Gmbh | Anlage und Verfahren zur kontinuierlichen industriellen Herstellung von 3-Glycidyloxypropylalkoxysilanen |
DE102007023763A1 (de) * | 2006-08-10 | 2008-02-14 | Evonik Degussa Gmbh | Anlage, Reaktor und Verfahren zur kontinuierlichen industriellen Herstellung von Polyetheralkylalkoxysilanen |
DE102007047430A1 (de) * | 2007-10-04 | 2009-04-09 | Evonik Degussa Gmbh | Katalysator |
ES2691384T3 (es) | 2008-09-02 | 2018-11-27 | Basf Se | Procedimiento para la fabricación de papel, cartón y cartulina usando endo-beta-1,4-glucanasas como agente de drenaje |
FR2975777B1 (fr) * | 2011-05-26 | 2014-03-14 | Arkema France | Procede de caracterisation d'un copolymere d'ethylene et d'acetate de vinyle |
CN102381966A (zh) * | 2011-11-11 | 2012-03-21 | 天津大学 | 一种醋酸乙烯生产方法 |
DE102012205444A1 (de) | 2012-04-03 | 2013-10-10 | Wacker Chemie Ag | Verfahren zur Herstellung von Vinylacetat |
CN106582871B (zh) * | 2015-10-19 | 2020-07-03 | 中国石油化工股份有限公司 | 醋酸烯丙酯生产所用的催化剂 |
CN106582868B (zh) * | 2015-10-19 | 2019-06-11 | 中国石油化工股份有限公司 | 醋酸烯丙酯制备所用的催化剂 |
US20240342676A1 (en) * | 2020-11-27 | 2024-10-17 | Resonac Corporation | Fixed bed multi-tubular reactor for producing alkenyl acetate |
DE102022116221A1 (de) | 2022-06-29 | 2024-01-04 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung eingetragener Verein | Verfahren zur Herstellung eines Katalysatorelements zur Verwendung in einem chemischen Reaktor, Katalysatorelement und chemischer Reaktor |
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- 2005-10-10 KR KR1020077008020A patent/KR20070100692A/ko not_active Application Discontinuation
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- 2005-10-10 EP EP05798523.6A patent/EP1804963B1/de active Active
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WO2010094660A1 (de) | 2009-02-19 | 2010-08-26 | Wacker Chemie Ag | Verfahren und vorrichtung zur herstellung von vinylacetat |
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Also Published As
Publication number | Publication date |
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JP2008516906A (ja) | 2008-05-22 |
BRPI0516508A (pt) | 2008-09-16 |
DE102004050585A1 (de) | 2006-04-20 |
SG182195A1 (en) | 2012-07-30 |
IL182479A0 (en) | 2007-07-24 |
KR20070100692A (ko) | 2007-10-11 |
CN101056699A (zh) | 2007-10-17 |
EP2241373A1 (de) | 2010-10-20 |
US20090054683A1 (en) | 2009-02-26 |
NO20072450L (no) | 2007-06-27 |
RU2007117920A (ru) | 2008-11-20 |
EP1804963A1 (de) | 2007-07-11 |
SG182196A1 (en) | 2012-07-30 |
EP1804963B1 (de) | 2015-09-09 |
MX2007004497A (es) | 2007-05-10 |
ZA200702978B (en) | 2009-07-29 |
TW200626229A (en) | 2006-08-01 |
CA2584173A1 (en) | 2006-04-27 |
AU2005297591A1 (en) | 2006-04-27 |
SG149035A1 (en) | 2009-01-29 |
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