WO2015008819A1 - 不均一系触媒および1,2-ジクロロエタンの製造用触媒システム - Google Patents
不均一系触媒および1,2-ジクロロエタンの製造用触媒システム Download PDFInfo
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- WO2015008819A1 WO2015008819A1 PCT/JP2014/069004 JP2014069004W WO2015008819A1 WO 2015008819 A1 WO2015008819 A1 WO 2015008819A1 JP 2014069004 W JP2014069004 W JP 2014069004W WO 2015008819 A1 WO2015008819 A1 WO 2015008819A1
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- Prior art keywords
- catalyst
- chloride
- adsorption
- dichloroethane
- diluent
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- 239000003054 catalyst Substances 0.000 title claims abstract description 199
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000002638 heterogeneous catalyst Substances 0.000 title claims abstract description 14
- 238000000034 method Methods 0.000 claims abstract description 126
- 238000001179 sorption measurement Methods 0.000 claims abstract description 111
- 239000003085 diluting agent Substances 0.000 claims abstract description 46
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000005977 Ethylene Substances 0.000 claims abstract description 32
- 238000003795 desorption Methods 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 59
- 239000007789 gas Substances 0.000 claims description 59
- 239000001301 oxygen Substances 0.000 claims description 59
- 229910052760 oxygen Inorganic materials 0.000 claims description 59
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 56
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 42
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 35
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 30
- 239000001103 potassium chloride Substances 0.000 claims description 28
- 235000011164 potassium chloride Nutrition 0.000 claims description 28
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 claims description 27
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 26
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 24
- 150000002736 metal compounds Chemical class 0.000 claims description 24
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 20
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 20
- 229910052757 nitrogen Inorganic materials 0.000 claims description 18
- 239000000377 silicon dioxide Substances 0.000 claims description 16
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 14
- 239000011780 sodium chloride Substances 0.000 claims description 13
- AIYUHDOJVYHVIT-UHFFFAOYSA-M caesium chloride Chemical compound [Cl-].[Cs+] AIYUHDOJVYHVIT-UHFFFAOYSA-M 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 229910001510 metal chloride Inorganic materials 0.000 claims description 10
- 229910002804 graphite Inorganic materials 0.000 claims description 8
- 239000010439 graphite Substances 0.000 claims description 8
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 7
- 150000004820 halides Chemical class 0.000 claims description 6
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 6
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 claims description 4
- 239000000395 magnesium oxide Substances 0.000 claims description 4
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 4
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 4
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 3
- 229910021536 Zeolite Inorganic materials 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims description 3
- 230000000737 periodic effect Effects 0.000 claims description 3
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims description 3
- 239000010457 zeolite Substances 0.000 claims description 3
- 229910001928 zirconium oxide Inorganic materials 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 108
- 230000000052 comparative effect Effects 0.000 description 74
- 239000007788 liquid Substances 0.000 description 36
- 238000006243 chemical reaction Methods 0.000 description 35
- 238000002336 sorption--desorption measurement Methods 0.000 description 35
- 238000007654 immersion Methods 0.000 description 34
- 229910021591 Copper(I) chloride Inorganic materials 0.000 description 33
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 description 33
- 239000010949 copper Substances 0.000 description 30
- 238000011156 evaluation Methods 0.000 description 27
- 239000000203 mixture Substances 0.000 description 20
- 239000011148 porous material Substances 0.000 description 18
- 239000002994 raw material Substances 0.000 description 15
- 230000003197 catalytic effect Effects 0.000 description 14
- 239000007864 aqueous solution Substances 0.000 description 12
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 239000000243 solution Substances 0.000 description 8
- 239000011261 inert gas Substances 0.000 description 7
- 239000011777 magnesium Substances 0.000 description 6
- 239000011734 sodium Substances 0.000 description 6
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 5
- 229910052786 argon Inorganic materials 0.000 description 5
- 238000009826 distribution Methods 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 230000002902 bimodal effect Effects 0.000 description 4
- 238000001035 drying Methods 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
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 4
- FGDZQCVHDSGLHJ-UHFFFAOYSA-M rubidium chloride Chemical compound [Cl-].[Rb+] FGDZQCVHDSGLHJ-UHFFFAOYSA-M 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 3
- 238000007598 dipping method Methods 0.000 description 3
- 238000010304 firing Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000178 monomer Substances 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000990 Ni alloy Inorganic materials 0.000 description 2
- 239000003570 air Substances 0.000 description 2
- QVQLCTNNEUAWMS-UHFFFAOYSA-N barium oxide Chemical compound [Ba]=O QVQLCTNNEUAWMS-UHFFFAOYSA-N 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229960003280 cupric chloride Drugs 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004445 quantitative analysis Methods 0.000 description 2
- 229940102127 rubidium chloride Drugs 0.000 description 2
- NDVLTYZPCACLMA-UHFFFAOYSA-N silver oxide Chemical compound [O-2].[Ag+].[Ag+] NDVLTYZPCACLMA-UHFFFAOYSA-N 0.000 description 2
- 229910001631 strontium chloride Inorganic materials 0.000 description 2
- AHBGXTDRMVNFER-UHFFFAOYSA-L strontium dichloride Chemical compound [Cl-].[Cl-].[Sr+2] AHBGXTDRMVNFER-UHFFFAOYSA-L 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 1
- 239000005751 Copper oxide Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- -1 For example Substances 0.000 description 1
- 229910021607 Silver chloride Inorganic materials 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- WDIHJSXYQDMJHN-UHFFFAOYSA-L barium chloride Chemical compound [Cl-].[Cl-].[Ba+2] WDIHJSXYQDMJHN-UHFFFAOYSA-L 0.000 description 1
- 229910001626 barium chloride Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- KOPBYBDAPCDYFK-UHFFFAOYSA-N caesium oxide Chemical compound [O-2].[Cs+].[Cs+] KOPBYBDAPCDYFK-UHFFFAOYSA-N 0.000 description 1
- 229910001942 caesium oxide Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 229910000431 copper oxide Inorganic materials 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 229940045803 cuprous chloride Drugs 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000001747 exhibiting effect Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- FUJCRWPEOMXPAD-UHFFFAOYSA-N lithium oxide Chemical compound [Li+].[Li+].[O-2] FUJCRWPEOMXPAD-UHFFFAOYSA-N 0.000 description 1
- 229910001947 lithium oxide Inorganic materials 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000000691 measurement method Methods 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000006082 mold release agent Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- CHWRSCGUEQEHOH-UHFFFAOYSA-N potassium oxide Chemical compound [O-2].[K+].[K+] CHWRSCGUEQEHOH-UHFFFAOYSA-N 0.000 description 1
- 229910001950 potassium oxide Inorganic materials 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000012552 review Methods 0.000 description 1
- 229910001952 rubidium oxide Inorganic materials 0.000 description 1
- CWBWCLMMHLCMAM-UHFFFAOYSA-M rubidium(1+);hydroxide Chemical compound [OH-].[Rb+].[Rb+] CWBWCLMMHLCMAM-UHFFFAOYSA-M 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- HKZLPVFGJNLROG-UHFFFAOYSA-M silver monochloride Chemical compound [Cl-].[Ag+] HKZLPVFGJNLROG-UHFFFAOYSA-M 0.000 description 1
- 229910001923 silver oxide Inorganic materials 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 150000008053 sultones Chemical class 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Images
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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/06—Halogens; Compounds thereof
- B01J27/138—Halogens; Compounds thereof with alkaline earth metals, magnesium, beryllium, zinc, cadmium or mercury
-
- 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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/06—Halogens; Compounds thereof
- B01J27/08—Halides
- B01J27/122—Halides of copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
-
- B01J35/40—
-
- B01J35/50—
-
- B01J35/51—
-
- B01J35/60—
-
- B01J35/647—
-
- B01J35/69—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0207—Pretreatment of the support
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/15—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination
- C07C17/152—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons
- C07C17/156—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons of unsaturated hydrocarbons
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00513—Controlling the temperature using inert heat absorbing solids in the bed
-
- 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
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
-
- B01J35/30—
-
- B01J35/56—
-
- B01J35/66—
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- B01J35/67—
Definitions
- the present invention relates to a novel heterogeneous catalyst, and more particularly, a catalyst used in the production of petrochemical products and organic chemical products, particularly 1,2-dichloroethane useful as a raw material for vinyl chloride monomer from ethylene.
- the present invention relates to a novel oxychlorination catalyst produced with high activity and high selectivity, and a method for producing 1,2-dichloroethane.
- Heterogeneous catalysts can be easily separated from gas-phase or liquid-phase reaction fluids, and are constantly held in the reactor and can function as catalysts, producing many petrochemical processes and organic chemicals. Used in the process.
- a supported copper chloride catalyst is used for the production of 1,2-dichloroethane (hereinafter abbreviated as EDC) by oxychlorination using ethylene, hydrogen chloride and oxygen as raw materials, and is one of the typical ultra-large petrochemical processes. It is. EDC production facilities are becoming larger and 100,000 tons / year large-scale facilities are operating. In terms of production, ethylene conversion and EDC selectivity are important factors, and even a difference of 0.1% appears as a large economic difference.
- EDC 1,2-dichloroethane
- Japanese Unexamined Patent Publication No. 56-141842 Japanese Unexamined Patent Publication No. 57-136828 Japan Special Table 2007-508134 Japanese Unexamined Patent Publication No. 2000-254507
- EDC production facilities include the air method process (ethylene, HCl, air as the main raw material), the oxygen enrichment method process (ethylene, HCl, air as the main raw material, and a small amount of oxygen added) and the oxygen method process (ethylene, HCl).
- Oxygen is the main raw material).
- the air method and the oxygen enrichment process there is a problem in improving unconverted ethylene.
- the oxygen method process there is a problem in improving productivity with a highly active catalyst, but in the oxychlorination catalyst proposed in Patent Document 1, The catalyst activity and EDC selectivity are not yet satisfactory, and a catalyst that greatly improves the catalyst activity and EDC selectivity is expected.
- the diluent used for hot spot suppression also has the problem of increasing pressure loss in the case of an irregularly shaped diluent by mechanical grinding, or in a size much smaller than the diameter and length of the catalyst.
- problems caused by such an increase in pressure loss are economically disadvantageous, such as reduced productivity due to pressure loss and the need for high-pressure reaction equipment.
- a pressure loss can be suppressed by using a diluent having a large diameter or length, the heat removal effect is lowered, and thus a satisfactory heat removal effect cannot be obtained. Therefore, the material, shape, and dimensions of the selected diluent must be optimized in consideration of the balance between pressure loss and heat removal effect.
- the present invention has been made in view of the above problems, and an object thereof is to provide a heterogeneous catalyst, particularly an oxychlorination catalyst, which exhibits high catalytic activity and EDC selectivity.
- a catalyst having a specific pore shape defined by the gas adsorption method has high activity and high selectivity, particularly in oxychlorination.
- a catalyst system for producing EDC characterized by exhibiting an active and high EDC selectivity, and comprising the catalyst and a diluent selected from a spherical shape, a cylindrical shape or a hollow cylindrical shape, and the same A manufacturing method was found and the present invention was completed.
- the catalyst characterized by being 19% or less with respect to a value.
- the porous carrier is alumina, silica, silica-alumina, zeolite, titanium oxide, zirconium oxide or magnesium oxide.
- a catalyst system for the production of 2-dichloroethane. [16] The catalyst system for production of 1,2-dichloroethane as described in [14] or [15] above, wherein the outer diameter D of the diluent having a spherical shape is the dimension (mm) of the following general formula (1).
- the outer diameter De 1 of the cylinder of the diluent having a cylindrical shape is the dimension (mm) of the following general formula (2), and the side length L 1 is the dimension (mm) of the following general formula (3).
- the dimensions of the hollow cylindrical outer diameter De 2 is represented by the following general formula of the hollow cylinder of the diluent with (4) (mm), the dimensions of the inner diameter Di by the following general formula (5) (mm), the side length 1,2-dichloroethane as described in [14] or [15] above, wherein the thickness L 2 is the dimension (mm) of the following general formula (6), and the relationship between the outer diameter De 2 and the inner diameter Di is the following general formula (7) Catalyst system for the production of
- novel heterogeneous catalyst and catalyst system of the present invention exhibit high ethylene conversion and EDC selectivity, especially when used for oxychlorination of ethylene, and high productivity of EDC useful as a raw material for vinyl chloride monomer. It is also extremely useful industrially as a method of manufacturing with
- Hysteresis ratio (desorption side adsorption isotherm area ⁇ adsorption side adsorption tower hot spring area) / (adsorption side adsorption isotherm area).
- the catalyst of the present invention is a heterogeneous catalyst in which a metal compound is supported on a porous carrier, and an integral value of hysteresis generated between an adsorption isotherm and a desorption isotherm in the gas adsorption method is an adsorption isotherm. 19% or less of the total integral value.
- the gas adsorption method is Shimadzu review Vol. 48 No. 1 (1991.6.), which is a technique for measuring specific surface area and pore distribution from condensation of gas molecules by adsorbing gas molecules having a known adsorption area on the surface of catalyst particles.
- Nitrogen and argon are mentioned as a gas molecule, Among these, nitrogen is preferable.
- the adsorption isotherm is a plot of the relative pressure on the horizontal axis, the number of gas molecules adsorbed on the vertical axis, or the volume of gas in the standard state, with the relative pressure changed from low to high.
- the adsorption isotherm is called the desorption isotherm.
- Hysteresis is considered to be caused by capillary condensation due to the pore shape (cylinder, cone, slit, ink bottle, etc.) and refers to a mismatch between the adsorption isotherm on the adsorption side and the desorption side. (See FIG. 1).
- the integral value of hysteresis is defined as the difference between the integral value of the adsorption isotherm and the integral value of the desorption isotherm in the relative pressure range under the measurement conditions.
- the integral value of hysteresis generated between the adsorption isotherm and desorption isotherm in the gas adsorption method is 19% or less with respect to the total integral value of the adsorption isotherm.
- 19% or less it is considered that the pore shape of the catalyst changes, the pores of the ink bottle shape decrease, and at the same time, the straight pores increase. Due to this shape change, an effect of improving catalytic activity and selectivity is exhibited.
- the integral value of hysteresis generated between the adsorption isotherm and desorption isotherm in the gas adsorption method is 17.5% or less with respect to the total integral value of the adsorption isotherm. Preferably there is.
- the catalyst of the present invention enables operation over a long period of time without impairing activity and selectivity, it can be used for oxidation reaction, reduction reaction, hydrogenation reaction, dehydrogenation reaction, alkylation reaction, etc.
- a high effect can be expected for an EDC production method from hydrogen chloride and oxygen.
- the effect of improving the catalyst activity is remarkable, and the activity of the catalyst according to the present invention is improved by 10% or more. Therefore, as a catalyst for an oxygen process requiring high productivity, and in an air process and an oxygen enrichment process. It can be used to improve the conversion rate of unconverted ethylene.
- the shape of the pore distribution is not particularly limited, and examples thereof include a unimodal pore distribution and a bimodal pore distribution.
- the shape of bimodal pores is preferable because the catalytic activity and selectivity are improved.
- the pore diameter of the bimodal pore is not particularly limited, but a bimodal type having a pore having a pore diameter in the range of 3 to less than 15 nm and a pore having a pore diameter in the range of 15 to 50 nm is preferable. Further activity and selectivity can be improved.
- the catalyst of the present invention is a heterogeneous catalyst in which a metal compound is supported on a porous carrier, and is preferably a granule.
- the porous carrier is not particularly limited, and examples thereof include alumina, silica, silica-alumina, zeolite, titanium oxide, zirconium oxide, and magnesium oxide. Of these, alumina is preferred because of its high affinity with the metal compound serving as the catalytically active component, and among these, a porous alumina carrier having pores is preferred.
- the porous alumina carrier may be mixed with silicon or iron derived from the alumina raw material, carbon such as a mold release agent, or additive such as silica or titanium, as long as it does not interfere with the catalytic reaction.
- Such an alumina carrier can be formed by any method, and can be formed by, for example, an extrusion method or a compression method.
- the hollow cylinder has an outer diameter of 3 to 6 mm, an inner diameter of less than 1 to 3 mm, and a side length of 3 to 6 mm. It is preferable that the outer diameter is 5 to 6 mm, the inner diameter is less than 2 to 3 mm, and the length is 4 to 6 mm.
- carrier For example, periodic table group 1, 2 or 11 is preferable, although it does not specifically limit as a metal compound, An oxide or a halide is mentioned.
- Metal chlorides are preferred.
- the metal oxide include lithium oxide, sodium oxide, potassium oxide, rubidium oxide, cesium oxide, magnesium oxide, calcium oxide, sultone oxide, barium oxide, copper oxide, and silver oxide.
- the halide include lithium chloride, sodium chloride, potassium chloride, rubidium chloride, magnesium chloride, calcium chloride, strontium chloride, barium chloride, copper chloride, silver chloride and the like.
- copper chloride is preferred because of its particularly high activity in oxychlorination.
- examples of the copper chloride include cuprous chloride and / or cupric chloride. Among them, cupric chloride is preferable because it becomes an oxychlorination catalyst having particularly excellent stability.
- the supported amount of the metal compound is not particularly limited as long as the oxychlorination catalyst acts as a catalyst, and among them, it is preferably 1 to 30% by weight because it becomes an oxychlorination catalyst having excellent catalytic activity. Further, it is preferably 2 to 28% by weight.
- the supported amount of copper chloride is preferably 3 to 25% by weight, and more preferably 8 to 20% by weight, since it becomes an oxychlorination catalyst having excellent catalytic activity. preferable.
- metal chloride on copper chloride as the metal compound.
- metal chlorides include, but are not limited to, lithium chloride, sodium chloride, potassium chloride, rubidium chloride, cesium chloride, magnesium chloride, calcium chloride, strontium chloride, etc.
- oxychlorination catalyst Potassium chloride, cesium chloride, sodium chloride and magnesium chloride are preferred because of increased stability.
- the amount of metal chloride supported is not limited as long as the oxychlorination catalyst acts as a catalyst. Among them, the oxychlorination catalyst contributes to the stability of copper chloride and has excellent catalytic activity. It is preferably ⁇ 20% by weight, more preferably 0.1 to 10% by weight.
- the loading ratio of copper chloride and other metal chlorides in the oxychlorination catalyst of the present invention is not limited as long as the oxychlorination catalyst acts as a catalyst, and among them, oxychlorine excellent in catalytic activity and stability. From the standpoint of forming a catalyst, a ratio of 0.1 to 3 moles of chloride per mole of copper chloride is preferable, and 0.1 to 1.3 moles is more preferable.
- the oxychlorination catalyst of the present invention may have any shape, and examples thereof include a spherical shape, a honeycomb shape, and a hollow cylindrical shape. Of these, a hollow cylindrical shape is preferable from the viewpoint of excellent fracture strength. There is no particular limitation on the shape and dimension, and among them, since it has excellent catalytic activity, a cylindrical shape with an outer diameter of 2 to 8 mm, an inner diameter of 1 to 7 mm, and a length of 2 to 8 mm is preferable, and an outer diameter of 3 to It is preferably 6 mm, an inner diameter of 1 to less than 3 mm, and a length of 3 to 6 mm.
- the catalyst of the present invention can be produced by any method, and examples thereof include a method of producing a catalyst by supporting a metal compound on a porous carrier.
- Examples of the supporting method at that time include a dipping method, an impregnation method, a coprecipitation method, and the like. Among these, the operation is simple and the productivity is excellent. preferable.
- the dipping method is to immerse the porous carrier in a solution (immersion solution) containing a metal compound, and after the dipping treatment, after separating the porous carrier and the solution, the porous carrier to which the metal compound is adhered is dried.
- a solution immersion solution
- the porous carrier to which the metal compound is adhered is dried.
- the concentration of the aqueous copper chloride solution is particularly Although not limited, it is preferably 50 to 300 g / L, more preferably 70 to 270 g / L because of high catalytic activity.
- the concentration of the aqueous potassium chloride solution is not particularly limited, but is preferably 10 to 280 g / L, more preferably 20 to 260 g / L because of high catalytic activity.
- the concentration of the aqueous cesium chloride solution is not particularly limited, but is preferably 30 to 180 g / L, more preferably 50 to 150 g / L because of its high catalytic activity.
- the concentration of the aqueous sodium chloride solution is not particularly limited, but is preferably 10 to 130 g / L, more preferably 20 to 100 g / L because of high catalytic activity.
- the concentration of the magnesium chloride aqueous solution is not particularly limited, but is preferably 50 to 220 g / L, and more preferably 80 to 200 g / L because of its high catalytic activity.
- the temperature at the time of immersion is not particularly limited, and is, for example, 0 to 80 ° C., preferably 10 to 50 ° C.
- the reaction pressure is not particularly limited, but is usually normal pressure.
- the immersion time depends on the temperature and the concentration of the immersion liquid and cannot be generally determined, but is usually 1 to 10 hours.
- the atmosphere during the reaction is not particularly limited, but it can be substituted with an inert gas such as nitrogen, argon or helium.
- the supporting order of the metal compounds in the case of producing the oxychlorination catalyst by the immersion method is not particularly limited, but it may be supported at one time or may be supported separately.
- the metal compound can be supported in the state of each aqueous solution as required.
- the drying temperature is not particularly limited, but is preferably 0 to 250 ° C, more preferably 30 to 200 ° C.
- the drying time is not particularly limited, but is preferably 1 to 20 hours, and more preferably 2 to 10 hours.
- the atmosphere during drying is not particularly limited, but is usually performed in air. Further, it can be substituted with an inert gas such as nitrogen, argon or helium and dried.
- the firing temperature is not particularly limited, but is preferably 0 to 500 ° C, more preferably 100 to 400 ° C.
- the firing time is not particularly limited, but is preferably 1 to 20 hours, and more preferably 2 to 10 hours. Moreover, it can replace with an inert gas such as nitrogen, argon or helium, and can be fired.
- the integral value of the hysteresis generated between the adsorption isotherm and desorption isotherm in the gas adsorption method of the catalyst of the present invention is controlled by treatment of the carrier with hydrochloric acid and subsequent high-temperature calcination.
- the amount of hydrochloric acid is not particularly limited, but is preferably 10 to 1000 ml, more preferably 20 to 200 ml, per 50 g of carrier.
- the immersion time is not particularly limited, but is preferably 1 to 20 hours, and more preferably 2 to 10 hours.
- the temperature at the time of immersion is not particularly limited and is, for example, 0 to 80 ° C., preferably 10 to 50 ° C.
- EDC can be produced by performing an oxychlorination reaction using ethylene, hydrogen chloride and oxygen as raw materials in the presence of the oxychlorination catalyst.
- the reaction format for producing EDC by oxychlorination reaction using ethylene, hydrogen chloride and oxygen as raw materials is not particularly limited, and can be performed in any reaction format, for example, fixed bed flow type Or it can carry out by a fluid bed circulation type. Among these, it is preferable to carry out by a fixed bed flow type because the apparatus is simple.
- the reaction temperature is not particularly limited, but is preferably 100 ° C. to 400 ° C., more preferably 150 ° C. to 350 ° C., because it can be efficiently converted to EDC.
- the reaction pressure is not particularly limited, but is usually 0.01 to 2 MPa in absolute pressure, preferably 0.05 to 1 MPa.
- the gas hourly space velocity (GHSV) during a fixed bed flow reaction because it can efficiently converted to EDC, preferably 10 hr -1 ⁇ 10,000 -1, more preferably 30hr -1 ⁇ 8,000hr -1 .
- the gas hourly space velocity (GHSV) represents the amount of ethylene supplied per unit time (hr) per unit catalyst volume.
- ethylene, hydrogen chloride, and oxygen may be used as they are, or may be diluted with an inert gas.
- an inert gas For example, nitrogen, helium, or argon etc. are mentioned, These inert gases can be used not only independently but in mixture of 2 or more types. It is.
- the so-called air method using air as oxygen as one of the raw materials, the oxygen enrichment method using oxygen added to the air, and the oxygen method using no inert gas such as nitrogen are industrial processes. Widely adopted and implemented.
- the oxychlorination catalyst of the present invention can be suitably used for any process.
- the material of the reaction tower is not particularly limited, and examples thereof include nickel, nickel alloy, and stainless steel. Of these, nickel and nickel alloys are preferred because of their excellent corrosion resistance to hydrogen chloride.
- a diluent may be mixed in the catalyst layer to form a catalyst system for producing EDC including the oxychlorination catalyst and the diluent.
- the shape of the diluent is not particularly limited and includes, for example, a spherical shape, a cylindrical shape, a hollow cylindrical shape, and the like, but since a good heat removal effect and a low pressure loss are possible, a spherical shape, a cylindrical shape, or a hollow cylindrical shape A diluent having is preferred.
- a hollow cylindrical shape if the outer diameter is D, the following dimensions (mm); 4.5 ⁇ D ⁇ 7.0 (1) It is preferable that In the case of a cylindrical shape, if the diameter is De 1 and the side length is L 1 , the dimension (mm) is 4.5 ⁇ De 1 ⁇ 7.0 (2) 4.0 ⁇ L 1 ⁇ 7.0 (3) It is preferable that In the case of a hollow cylindrical shape, a circular cylinder having a diameter smaller than the diameter of the circle is formed in parallel with the side surface from the circular surface of one column, and the outer diameter of the hollow cylinder of the diluent is De 2 , the inner diameter Di, the side length L 2 , and the relationship between the outer diameter De 2 and the inner diameter Di in dimensions (mm) 4.5 ⁇ De 2 ⁇ 7.0 (4) 1.5 ⁇ Di ⁇ 4.0 (5) 4.0 ⁇ L 2 ⁇ 7.0 (6) De 2/3 ⁇ Di (7 ) It is preferable that Among them, a hollow cylindrical shape is preferable because
- the material of the diluent is at least one selected from the group consisting of alumina, silica, alumina-silica, silicon carbide, aluminum nitride and graphite.
- a sintered body having a specific surface area of 5 m 2 / g or less is preferable for alumina, silica, alumina-silica, silicon carbide, and aluminum nitride. Is preferably a sintered body of 20 m 2 / g or less.
- the mixing ratio of the oxychlorination catalyst and the diluent can be changed in the range of 5:95 to 95: 5 in consideration of the calorific value.
- the oxychlorination catalyst can be used in the presence of a high concentration of the diluent at a high raw material concentration, such as the reaction bed inlet, and at a small amount or all at the outlet side.
- hysteresis was measured using a nitrogen adsorption specific surface area / pore distribution measuring device (trade name: ASAP2400, manufactured by Micromeritics) under conditions of liquid nitrogen temperature and nitrogen relative pressure of 0.001 to 0.995. .
- the integral value of hysteresis is the difference obtained by calculating the integral values of the adsorption isotherm and desorption isotherm in the range of relative pressures 0.001 to 0.995, and subtracting the former from the latter.
- ⁇ Reaction method> For the reaction evaluation of the oxychlorination catalyst, a fixed bed gas phase flow reactor using a glass reaction tube (inner diameter 22 mm, length 600 mm) was used. The middle stage of a glass reaction tube was filled with an oxychlorination catalyst, and ethylene, hydrogen chloride, molecular oxygen and nitrogen for dilution were supplied to the catalyst layer.
- the raw material compositions in Examples 1 to 8, 29 to 35 and Comparative Examples 1 to 4 and 15 to 16 are pneumatic compositions (ethylene 32 ml / min, hydrogen chloride 64 ml / min, oxygen 13 ml / min, nitrogen 91 ml / min) and did.
- Example 9 to 18 and Comparative Examples 5 to 9 the oxygen enrichment composition (ethylene 24 ml / min, hydrogen chloride 44 ml / min, oxygen 20 ml / min, nitrogen 413 ml / min) was used.
- the oxygen method composition ethylene 190 ml / min, hydrogen chloride 30 ml / min, oxygen 8 ml / min, nitrogen 122 ml / min was used.
- the specific activities in Examples 1 to 8, 29 to 35 and Comparative Examples 1 to 4 and 15 to 16 were controlled when 2 cm before the entrance of the catalyst layer was controlled to 220 ° C. and the top temperature of the catalyst layer was controlled to 270 ° C.
- Each ethylene conversion rate was determined, and the average value of the ethylene conversion rate with respect to the filling rate was set as activity.
- the specific activity was determined from the ethylene conversion when 2 cm before the catalyst layer entrance was controlled at 220 ° C.
- the EDC selectivity was determined by controlling 2 cm before the entrance of the catalyst layer to 220 ° C.
- the outlet gas and the reaction solution under each reaction condition were collected, and the gas component and the liquid component were individually analyzed using a gas chromatograph.
- the gas component was analyzed using a gas chromatograph (manufactured by Shimadzu Corporation, trade name: GC-14A).
- PorapakQ (trade name) manufactured by Waters and MS-5A (trade name) manufactured by GL Science were used.
- the liquid component was analyzed using a gas chromatograph (manufactured by Shimadzu Corporation, trade name: GC-1700).
- a capillary column (manufactured by GL Science, trade name: TC-1) was used.
- Example 1 After immersing 50 g of hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in 100 ml of 1N hydrochloric acid for 2 hours, drained, 120 A hollow cylindrical shape in which the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method is 12.5% with respect to the integrated value of the adsorption isotherm An alumina support was obtained.
- hollow cylindrical alumina carrier trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 14.0% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 142, and the EDC selectivity was 99.4%.
- the specific activity was set to 100 in Comparative Example 2.
- Example 3 After immersing 50 g of hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in 100 ml of 1N hydrochloric acid for 2 hours, drained, 120 A hollow cylindrical shape in which the area ratio of the adsorption / desorption isotherm hysteresis in the gas adsorption method is 14.4% with respect to the integral value of the adsorption isotherm is performed by drying at 700 ° C. and firing at 700 ° C. in air for 5 hours. An alumina support was obtained.
- hollow cylindrical alumina carrier trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm
- An oxychlorination catalyst of 80 was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 18.9% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 120 and the EDC selectivity was 99.2%.
- the specific activity was set to 100 in Comparative Example 2.
- Comparative Example 1 After immersing 50 g of hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in pure water for 1 hour, drained, 120 ° C. Hollow cylindrical alumina that is dried and calcined in air at 500 ° C. for 5 hours, and the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method is 15.2% with respect to the integral value of the adsorption isotherm A carrier was obtained.
- hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in pure water for 1 hour, drained, 120 ° C. Hollow cylindrical alumina that is dried and calcined in air at 500 ° C. for 5
- Comparative Example 2 After immersing 50 g of hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in pure water for 1 hour, drained, 120 ° C. Hollow cylindrical alumina that is dried and calcined in air at 700 ° C. for 5 hours, and the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method is 16.2% with respect to the integral value of the adsorption isotherm A carrier was obtained.
- hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in pure water for 1 hour, drained, 120 ° C. Hollow cylindrical alumina that is dried and calcined in air at 700 ° C. for 5
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.1% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 251 and the EDC selectivity was 99.3%.
- the specific activity was set to 100 in Comparative Example 2.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.6% with respect to the integral value of the adsorption isotherm.
- the specific activity was 234 and the EDC selectivity was 99.1%.
- the specific activity was set to 100 in Comparative Example 2.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 17.2% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 226, and the EDC selectivity was 99.0%.
- the specific activity was set to 100 in Comparative Example 2.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 18.4% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 212 and the EDC selectivity was 98.8%.
- the specific activity was set to 100 in Comparative Example 2.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 23.9% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 199, and the EDC selectivity was 98.6%.
- the specific activity was set to 100 in Comparative Example 2.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 24.1% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 192 and the EDC selectivity was 98.4%.
- the specific activity was set to 100 in Comparative Example 2.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.2% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 119.
- the specific activity was set to 100 in Comparative Example 5.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.5% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 118.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.3% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 177.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst of 0.50 was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.1% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 260.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst having a (Na + Mg) / Cu ratio of 0.50 was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 13.4% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 198.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 15.0% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 117.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 15.1% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 115.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 15.3% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 184.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst of 0.50 was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 14.8% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 254.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst having a (Na + Mg) / Cu ratio of 0.50 was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 14.8% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 194.
- the specific activity was set to 100 in Comparative Example 5.
- An oxychlorination catalyst of 0.50 was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 23.8% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 98.
- the specific activity was set to 100 in Comparative Example 5.
- a catalyst was prepared.
- the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method was 23.8% with respect to the integrated value of the adsorption isotherm.
- the specific activity was 148.
- the specific activity was set to 100 in Comparative Example 5.
- Example 19 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 9, the specific activity was 374. The specific activity was set to 100 in Comparative Example 10.
- Example 20 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 10, the specific activity was 364. The specific activity was set to 100 in Comparative Example 10.
- Example 21 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 11, the specific activity was 340. The specific activity was set to 100 in Comparative Example 10.
- Example 22 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 12, the specific activity was 259. The specific activity was set to 100 in Comparative Example 10.
- Example 23 As a result of evaluating using the catalyst prepared in Example 13 under oxygen method conditions, the specific activity was 312. The specific activity was set to 100 in Comparative Example 10.
- Example 24 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 14, the specific activity was 202. The specific activity was set to 100 in Comparative Example 10.
- Example 25 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 15, the specific activity was 197. The specific activity was set to 100 in Comparative Example 10.
- Example 26 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 16, the specific activity was 184. The specific activity was set to 100 in Comparative Example 10.
- Example 27 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 17, the specific activity was 144. The specific activity was set to 100 in Comparative Example 10.
- Example 28 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Example 18, the specific activity was 168. The specific activity was set to 100 in Comparative Example 10.
- Comparative Example 10 As a result of evaluation using the catalyst prepared in Comparative Example 5 under oxygen method conditions, the specific activity was 100. The specific activity was set to 100 in Comparative Example 10.
- Comparative Example 11 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Comparative Example 6, the specific activity was 98. The specific activity was set to 100 in Comparative Example 10.
- Comparative Example 12 As a result of evaluation using the catalyst prepared in Comparative Example 7 under oxygen method conditions, the specific activity was 91. The specific activity was set to 100 in Comparative Example 10.
- Comparative Example 13 As a result of evaluation using the catalyst prepared in Comparative Example 8 under oxygen method conditions, the specific activity was 71. The specific activity was set to 100 in Comparative Example 10.
- Comparative Example 14 As a result of evaluating under the oxygen method conditions using the catalyst prepared in Comparative Example 9, the specific activity was 76. The specific activity was set to 100 in Comparative Example 10.
- Example 29 After immersing 50 g of hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in 100 ml of 1N hydrochloric acid for 2 hours, drained, 120 A hollow cylindrical shape in which the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method is 12.5% with respect to the integrated value of the adsorption isotherm An alumina support was obtained.
- hollow cylindrical alumina carrier trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm
- Example 30 Evaluation was performed in the same manner as in Example 29 except that a cylindrical graphite diluent having a diameter of 5.0 mm, a side length of 5.0 mm, and a specific surface area of 1.7 m 2 / g was used as the diluent.
- Example 31 Except for using a hollow cylindrical alumina-silica diluent having a hollow cylinder outer diameter of 6.4 mm, an inner diameter of 3.5 mm, a side length of 5.0 mm, and a specific surface area of 0.094 m 2 / g as a diluent. Evaluation was performed in the same manner as in Example 29.
- Example 32 Except for using a hollow cylindrical alumina-silica diluent having a hollow cylinder outer diameter of 6.4 mm, an inner diameter of 3.5 mm, a side length of 6.4 mm, and a specific surface area of 0.094 m 2 / g as the diluent. Evaluation was performed in the same manner as in Example 29.
- Example 33 Except for using a hollow cylindrical alumina-silica diluent having a hollow cylinder outer diameter of 5.0 mm, an inner diameter of 2.5 mm, a side length of 5.0 mm, and a specific surface area of 0.094 m 2 / g as a diluent. Evaluation was performed in the same manner as in Example 29.
- Example 34 Except for using a hollow cylindrical graphite diluent having a hollow cylinder outer diameter of 5.0 mm, an inner diameter of 2.0 mm, a side length of 5.0 mm, and a specific surface area of 1.7 m 2 / g as a diluent. Evaluation was conducted in the same manner as in No. 29.
- Example 35 Example except that a hollow cylindrical graphite diluent having a hollow cylinder outer diameter of 6.0 mm, an inner diameter of 2.5 mm, a side length of 5.0 mm, and a specific surface area of 1.7 m 2 / g was used as the diluent. Evaluation was conducted in the same manner as in No. 29.
- Comparative Example 15 In the same manner as in Example 29, except that an amorphous graphite diluent having a diameter of 5.0 mm, a side length of 1.0 to 8.0 mm, and a specific surface area of 1.7 m 2 / g was used as the diluent. evaluated.
- Comparative Example 16 After immersing 50 g of hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in pure water for 1 hour, drained, 120 ° C. Hollow cylindrical alumina that is dried and calcined in air at 700 ° C. for 5 hours, and the area ratio of adsorption / desorption isotherm hysteresis in the gas adsorption method is 16.2% with respect to the integral value of the adsorption isotherm A carrier was obtained.
- hollow cylindrical alumina carrier (trade name N611N3, outer diameter 4.9 mm, inner diameter 1.8 mm, length 3.9 mm) manufactured by JGC Catalysts & Chemicals Co., Ltd. in pure water for 1 hour, drained, 120 ° C. Hollow cylindrical alumina that is dried and calcined in air at 700 ° C. for 5
- Example 29 As a result of quantitative analysis, it was 12.7% CuCl 2 -5.6% KCl / alumina catalyst.
- Example 29 except that 15 ml of this catalyst was mixed with 15 ml of hollow cylindrical graphite diluent having an outer diameter of 5.0 mm, an inner diameter of 2.0 mm, a side length of 5.0 mm, and a specific surface area of 1.7 m 2 / g. Evaluation was made in the same manner.
- the heterogeneous catalyst of the present invention can be used as a catalyst for producing 1,2-dichloroethane particularly useful as a raw material for vinyl chloride monomer from ethylene.
- the dichloroethane selectivity is extremely high and the economy is excellent. In addition, since stable production is possible, it is excellent in safety.
- Hysteresis 2 Desorption side 3: Adsorption side
Abstract
Description
[1] 多孔質担体上に金属化合物が担持された不均一系触媒であって、ガス吸着法の吸着等温線と脱着等温線との間に生じるヒステリシスの積分値が、吸着等温線の全積分値に対して19%以下であることを特徴とする触媒。
[2] 多孔質担体がアルミナ、シリカ、シリカ―アルミナ、ゼオライト、酸化チタン、酸化ジルコニウム又は酸化マグネシウムであることを特徴とする、上記[1]に記載の触媒。
[3] 金属化合物の金属が、周期表1族、2族又は11族であることを特徴とする上記[1]又は[2]に記載の触媒。
[4] 金属化合物が、酸化物またはハロゲン化物であることを特徴とする上記[1]~[3]のいずれかに記載の触媒。
[5] 金属化合物が塩化銅であることを特徴とする上記[1]~[4]のいずれかに記載の触媒。
[6] 金属化合物が、塩化銅並びに塩化カリウム、塩化セシウム、塩化ナトリウムおよび塩化マグネシウムからなる群から選択される1種以上の金属塩化物であることを特徴とする上記[1]~[5]のいずれかに記載の触媒。
[7] 塩化銅の担持量が3~25重量%であることを特徴とする上記[5]又は[6]に記載の触媒。
[8] 金属塩化物の担持量が、0.1~20重量%であることを特徴とする上記[6]又は[7]に記載の触媒。
[9] ガス吸着法が窒素吸着法であることを特徴とする上記[1]~[8]のいずれかに記載の触媒。
[10] 不均一系触媒が中空円筒形状であることを特徴とする上記[1]~[9]のいずれかに記載の触媒。
[11] 外径3~6mm、内径1~3mm未満、長さ3~6mmの中空円筒形状であることを特徴とする上記[10]に記載の触媒。
[12] 触媒がエチレンのオキシ塩素化用途に使用される上記[1]~[11]のいずれかに記載の触媒。
[13] 上記[1]~[12]のいずれかに記載の触媒の存在下、エチレン、塩化水素及び酸素のオキシ塩素化を行うことを特徴とする1,2-ジクロロエタンの製造方法。
[14] 上記[1]~[12]のいずれかに記載の触媒及び球形状、円柱形状または中空円筒形状を有する希釈剤を含むことを特徴とする、エチレン、塩化水素および酸素から1,2-ジクロロエタンの製造用触媒システム。
[15] 希釈剤が、アルミナ、シリカ、アルミナ-シリカ、炭化ケイ素、窒化アルミニウム、炭素及びグラファイトからなる群より選択される少なくとも1種であることを特徴とする上記[14]に記載の1,2-ジクロロエタンの製造用触媒システム。
[16] 球形状を有する希釈剤の外径Dが下記一般式(1)の寸法(mm)である上記[14]又は[15]に記載の1,2-ジクロロエタンの製造用触媒システム。
[17] 円柱形状を有する希釈剤の円柱の外径De1が下記一般式(2)の寸法(mm)、側面の長さL1が下記一般式(3)の寸法(mm)である上記[14]又は[15]に記載の1,2-ジクロロエタンの製造用触媒システム。
4.0≦L1≦7.0 (3)
[18] 中空円筒形状を有する希釈剤の中空円筒の外径De2が下記一般式(4)の寸法(mm)、その内径Diが下記一般式(5)の寸法(mm)、側面の長さL2が下記一般式(6)の寸法(mm)、外径De2と内径Diの関係が下記一般式(7)である上記[14]又は[15]に記載の1,2-ジクロロエタンの製造用触媒システム。
1.5≦Di≦4.0 (5)
4.0≦L2≦7.0 (6)
De2/3≦Di (7)
[19] 希釈剤の外径がオキシ塩素化触媒の長さと等しい長さである上記[14]~[18]のいずれかに記載の1,2-ジクロロエタンの製造用触媒システム。
[20] 上記[14]~[19]のいずれかに記載の1,2-ジクロロエタンの製造用触媒システムの存在下で、エチレン、塩化水素および酸素を反応させることを特徴とする1,2-ジクロロエタンの製造方法。
4.5≦D≦7.0 (1)
であることが好ましい。円柱形状の場合には、その径をDe1、側面の長さをL1とすると寸法(mm)が、
4.5≦De1≦7.0 (2)
4.0≦L1≦7.0 (3)
であることが好ましい。中空円筒形状の場合には、1個の円柱の円状面よりその円の径より小さい径を有する円柱を側面と平行に貫通した形状を成しており、希釈剤の中空円筒の外径をDe2、その内径をDi、側面の長さをL2、そして外径De2と内径Diの関係を寸法(mm)で示すと、
4.5≦De2≦7.0 (4)
1.5≦Di≦4.0 (5)
4.0≦L2≦7.0 (6)
De2/3≦Di (7)
であることが好ましい。その中でも、圧力損失の低減が可能になることから、中空円筒形状が好ましい。寸法が大きいと圧力損失は小さいが除熱効果が小さくなり不利である。また、寸法が小さいと除熱効果は大きいが、圧力損失は大きくなり不利になる。
ヒステリシスの測定は、窒素吸着法比表面積・細孔分布測定装置(マイクロメリティクス社製 商品名:ASAP2400)を用い、液体窒素温度および0.001~0.995の窒素相対圧の条件で行った。ヒステリシスの積分値は、相対圧0.001~0.995の範囲において吸着等温線、及び脱着等温線それぞれの積分値を求め、後者から前者を引いた差分である。
塩化銅、及び塩化物の定量は、走査型蛍光X線分析装置(理学製、(商品名)ZSX PrimusII)を用い、触媒約3gを粉砕、次いで加圧プレスで試料プレートを作製し、このプレートをRh管球、管電圧/管電流50kV/60mAの条件で測定した。得られたCu、及びK濃度は、各々CuCl2、KClに換算して、表1に記載した。
オキシ塩素化触媒の反応評価は、ガラス製反応管(内径22mm、長さ600mm)を用いた固定床気相流通式反応装置を用いた。ガラス製反応管の中段に、オキシ塩素化触媒を充填し、エチレン、塩化水素、分子状酸素および希釈用窒素を触媒層に供給した。原料組成は実施例1~8、29~35及び比較例1~4、15~16において、空気法組成(エチレン32ml/min、塩化水素64ml/min、酸素13ml/min、窒素91ml/min)とした。実施例9~18及び比較例5~9においては、酸素富化法組成(エチレン24ml/min、塩化水素44ml/min、酸素20ml/min、窒素413ml/min)とした。実施例19~28及び比較例10~14においては、酸素法組成(エチレン190ml/min、塩化水素30ml/min、酸素8ml/min、窒素122ml/min)とした。比活性は、実施例1~8、29~35及び比較例1~4、15~16において、触媒層の入口手前2cmを220℃に制御した場合と、触媒層のトップ温度を270℃に制御した場合の各々のエチレン転化率を求め、充填率に対するエチレン転化率の平均値を活性と設定した。実施例9~28及び比較例5~14においては、触媒層入口手前2cmを220℃に制御した場合のエチレン転化率から比活性を求めた。また、EDC選択率は、触媒層の入口手前2cmを220℃になるよう制御し求めた。各反応条件での出口ガス及び反応液を採取し、ガスクロマトグラフを用い、ガス成分および液成分を個別に分析した。ガス成分は、ガスクロマトグラフ(島津製作所製、商品名:GC-14A)を用いて分析した。充填剤は、Waters社製PorapakQ(商品名)およびGLサイエンス社製MS-5A(商品名)を用いた。液成分は、ガスクロマトグラフ(島津製作所製、商品名:GC-1700)を用いて分析した。分離カラムは、キャピラリーカラム(GLサイエンス社製、商品名:TC-1)を用いた。
日揮触媒化成株式会社製の中空円筒形状のアルミナ担体(商品名N611N3、外径4.9mm、内径1.8mm、長さ3.9mm)50gを1N塩酸100mlに2時間浸した後、水切り、120℃乾燥、および、空気中500℃での5時間の焼成を行い、ガス吸着法における吸脱着等温線ヒステリシスの面積比率が吸着等温線の積分値に対して12.5%である中空円筒形状のアルミナ担体を得た。このアルミナ担体30gに水を十分に吸収させた後、CuCl2=174g/L、KCl=136g/Lの水溶液80mLに4時間浸漬させた。浸漬液からアルミナ担体を取り出し、マッフル炉を用いて120℃で2時間乾燥させた。その後、250℃で4時間焼成し、K/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.6%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は159、EDC選択率は99.6%であった。なお、比活性は比較例2の活性を100とした。
CuCl2=255g/L、KCl=140g/Lの水溶液80mLに2時間浸漬させたこと以外は実施例1と同様の条件でK/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して、14.0%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は142、EDC選択率は99.4%であった。なお、比活性は比較例2を100とした。
日揮触媒化成株式会社製の中空円筒形状のアルミナ担体(商品名N611N3、外径4.9mm、内径1.8mm、長さ3.9mm)50gを1N塩酸100mlに2時間浸した後、水切り、120℃乾燥、および、空気中700℃での5時間の焼成を行い、ガス吸着法における吸脱着等温線ヒステリシスの面積比率が吸着等温線の積分値に対して14.4%である中空円筒形状のアルミナ担体を得た。このアルミナ担体30gに水を十分に吸収させた後、CuCl2=174g/L、KCl=136g/Lの水溶液80mLに4時間浸漬させた。浸漬液からアルミナ担体を取り出し、マッフル炉を用いて120℃で2時間乾燥させた。その後、420℃で4時間焼成し、K/Cu比が0.80であるオキシ塩素化触媒を調製した。 ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して、17.3%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は134、EDC選択率は99.3%であった。なお、比活性は比較例2を100とした。
CuCl2=255g/L、KCl=140g/Lの水溶液80mLに2時間浸漬させたこと、および、300℃で4時間焼成したこと以外は実施例3と同様の条件でK/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して、18.9%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は120、EDC選択率は99.2%であった。なお、比活性は比較例2を100とした。
日揮触媒化成株式会社製の中空円筒形状のアルミナ担体(商品名N611N3、外径4.9mm、内径1.8mm、長さ3.9mm)50gを純水に1時間浸した後、水切り、120℃乾燥、および、空気中500℃での5時間の焼成を行い、ガス吸着法における吸脱着等温線ヒステリシスの面積比率が吸着等温線の積分値に対して15.2%である中空円筒形状のアルミナ担体を得た。このアルミナ担体30gに水を十分に吸収させた後、CuCl2=270g/L、KCl=150g/Lの水溶液80mLに30分浸漬させた。浸漬液からアルミナ担体を取り出し、マッフル炉を用いて120℃で2時間乾燥させた。その後、420℃で6時間焼成し、K/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して、23.4%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は107、EDC選択率は99.1%であった。なお、比活性は比較例2を100とした。
日揮触媒化成株式会社製の中空円筒形状のアルミナ担体(商品名N611N3、外径4.9mm、内径1.8mm、長さ3.9mm)50gを純水に1時間浸した後、水切り、120℃乾燥、および、空気中700℃での5時間の焼成を行い、ガス吸着法における吸脱着等温線ヒステリシスの面積比率が吸着等温線の積分値に対して16.2%である中空円筒形状のアルミナ担体を得た。このアルミナ担体30gに水を十分に吸収させた後、CuCl2=255g/L、KCl=140g/Lの水溶液80mLに2時間浸漬させた。浸漬液からアルミナ担体を取り出し、マッフル炉を用いて120℃で2時間乾燥させた。その後、420℃で6時間焼成し、K/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して、24.5%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は100、EDC選択率は98.9%であった。なお、比活性は比較例2を100とした。
浸漬液の濃度をCuCl2=207g/L、KCl=22g/Lとしたこと以外は実施例1と同様の条件で、K/Cu比が0.15であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.1%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は251、EDC選択率は99.3%であった。なお、比活性は比較例2を100とした。
浸漬液の濃度をCuCl2=250g/L、KCl=30g/Lとしたこと以外は実施例2と同様の条件で、K/Cu比が0.15であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.6%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は234、EDC選択率は99.1%であった。なお、比活性は比較例2を100とした。
浸漬液の濃度をCuCl2=207g/L、KCl=22g/Lとしたこと以外は実施例3と同様の条件で、K/Cu比が0.15であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して17.2%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は226、EDC選択率は99.0%であった。なお、比活性は比較例2を100とした。 実施例8
浸漬液の濃度をCuCl2=250g/L、KCl=30g/Lとしたこと以外は実施例4と同様の条件で、K/Cu比が0.15であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して18.4%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は212、EDC選択率は98.8%であった。なお、比活性は比較例2を100とした。
CuCl2=295g/L、KCl=32g/Lの水溶液80mLに1時間浸漬させたこと以外は比較例1と同様の条件で、K/Cu比が0.15であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して23.9%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は199、EDC選択率は98.6%であった。なお、比活性は比較例2を100とした。
浸漬液の濃度をCuCl2=250g/L、KCl=30g/Lとした以外は比較例2と同様の条件で、K/Cu比が0.15であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して24.1%であった。この触媒を用いて空気法条件下で評価を行った結果、比活性は192、EDC選択率は98.4%であった。なお、比活性は比較例2を100とした。
浸漬液の組成をCuCl2=161g/L、KCl=98g/Lとした以外は実施例1と同様の条件で、K/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.2%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は119であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、CsCl=221g/Lとした以外は実施例1と同様の条件で、Cs/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.5%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は118であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、NaCl=77g/Lとしたこと及び400℃で2時間焼成したこと以外は実施例1と同様の条件で、Na/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.3%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は177であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、MgCl2・2H2O=267g/Lとしたこと及び400℃で2時間焼成したこと以外は実施例1と同様の条件で、Mg/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.1%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は260であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、NaCl=26g/L、MgCl2・2H2O=180g/Lとしたこと及び400℃で2時間焼成したこと以外は実施例1と同様の条件で、(Na+Mg)/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.4%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は198であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、KCl=98g/Lとしたこと及び250℃で4時間焼成したこと以外は実施例3と同様の条件で、K/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して15.0%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は117であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、CsCl=221g/Lとしたこと及び250℃で4時間焼成したこと以外は実施例3と同様の条件で、Cs/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して15.1%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は115であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、NaCl=77g/Lとしたこと及び400℃で2時間焼成したこと以外は実施例3と同様の条件で、Na/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して15.3%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は184であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、MgCl2・2H2O=267g/Lとしたこと及び400℃で2時間焼成したこと以外は実施例3と同様の条件で、Mg/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して14.8%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は254であった。なお、比活性は比較例5を100とした。
浸漬液の組成をCuCl2=161g/L、NaCl=26g/L、MgCl2・2H2O=180g/Lとしたこと及び400℃で2時間焼成したこと以外は実施例3と同様の条件で、(Na+Mg)/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して14.8%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は194であった。なお、比活性は比較例5を100とした。
液組成がCuCl2=240g/L、KCl=105g/Lの浸漬液に1時間浸漬させたこと及び420℃で6時間焼成したこと以外は比較例2と同様の条件で、K/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して23.6%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は100であった。なお、比活性は比較例5を100とした。
液組成がCuCl2=240g/L、CsCl=238g/Lの浸漬液に1時間浸漬させたこと及び420℃で6時間焼成したこと以外は比較例2と同様の条件で、Cs/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して23.8%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は98であった。なお、比活性は比較例5を100とした。
液組成がCuCl2=255g/L、NaCl=91g/Lの浸漬液に30分浸漬させたこととした以外は比較例2と同様の条件で、Na/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して23.8%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は148であった。なお、比活性は比較例5を100とした。
液組成がCuCl2=255g/L、MgCl2・2H2O=293g/Lの浸漬液に30分浸漬させたこと及び250℃で4時間焼成したこと以外は比較例23と同様の条件で、Mg/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して23.7%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は217であった。なお、比活性は比較例5を100とした。
液組成がCuCl2=255g/L、NaCl=32g/L、MgCl2・2H2O=220g/Lの浸漬液に30分浸漬させたこと及び250℃で4時間焼成したこととした以外は比較例2と同様の条件で、(Na+Mg)/Cu比が0.50であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して23.9%であった。この触媒を用いて酸素富化法条件下で評価を行った結果、比活性は166であった。なお、比活性は比較例5を100とした。
実施例9で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は374であった。なお、比活性は比較例10を100とした。
実施例10で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は364であった。なお、比活性は比較例10を100とした。
実施例11で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は340であった。なお、比活性は比較例10を100とした。
実施例12で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は259であった。なお、比活性は比較例10を100とした。
実施例13で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は312であった。なお、比活性は比較例10を100とした。
実施例14で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は202であった。なお、比活性は比較例10を100とした。
実施例15で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は197であった。なお、比活性は比較例10を100とした。
実施例16で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は184であった。なお、比活性は比較例10を100とした。
実施例17で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は144であった。なお、比活性は比較例10を100とした。
実施例18で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は168であった。なお、比活性は比較例10を100とした。
比較例5で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は100であった。なお、比活性は比較例10を100とした。
比較例6で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は98であった。なお、比活性は比較例10を100とした。
比較例7で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は91であった。なお、比活性は比較例10を100とした。
比較例8で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は71であった。なお、比活性は比較例10を100とした。
比較例9で調製した触媒を用い、酸素法条件下で評価を行った結果、比活性は76であった。なお、比活性は比較例10を100とした。
日揮触媒化成株式会社製の中空円筒形状のアルミナ担体(商品名N611N3、外径4.9mm、内径1.8mm、長さ3.9mm)50gを1N塩酸100mlに2時間浸した後、水切り、120℃乾燥、および、空気中500℃での5時間の焼成を行い、ガス吸着法における吸脱着等温線ヒステリシスの面積比率が吸着等温線の積分値に対して12.5%である中空円筒形状のアルミナ担体を得た。このアルミナ担体30gに水を十分に吸収させた後、CuCl2=174g/L、KCl=136g/Lの水溶液80mLに4時間浸漬させた。浸漬液からアルミナ担体を取り出し、マッフル炉を用いて120℃で2時間乾燥させた。その後、250℃で4時間焼成し、K/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して13.6%であった。定量分析の結果、12.9%CuCl2-5.7%KCl/アルミナ触媒であった。この触媒と径5.0mm、比表面積0.1m2/gの球形状のアルミナ―シリカ希釈剤を混合して空気法条件の反応方法に従って評価した。
希釈剤として、径5.0mm、側面の長さ5.0mm、比表面積1.7m2/gの円柱形状のグラファイト希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
希釈剤として、中空円筒の外径6.4mm、内径3.5mm、側面の長さ5.0mm、比表面積0.094m2/gの中空円筒形状のアルミナ―シリカ希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
希釈剤として、中空円筒の外径6.4mm、内径3.5mm、側面の長さ6.4mm、比表面積0.094m2/gの中空円筒形状のアルミナ―シリカ希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
希釈剤として、中空円筒の外径5.0mm、内径2.5mm、側面の長さ5.0mm、比表面積0.094m2/gの中空円筒形状のアルミナ―シリカ希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
希釈剤として、中空円筒の外径5.0mm、内径2.0mm、側面の長さ5.0mm、比表面積1.7m2/gの中空円筒形状のグラファイト希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
希釈剤として、中空円筒の外径6.0mm、内径2.5mm、側面の長さ5.0mm、比表面積1.7m2/gの中空円筒形状のグラファイト希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
希釈剤として、径5.0mm、側面の長さ1.0~8.0mm、比表面積1.7m2/gの不定形状のグラファイト希釈剤を用いたこと以外は実施例29と同様の方法で評価した。
日揮触媒化成株式会社製の中空円筒形状のアルミナ担体(商品名N611N3、外径4.9mm、内径1.8mm、長さ3.9mm)50gを純水に1時間浸した後、水切り、120℃乾燥、および、空気中700℃での5時間の焼成を行い、ガス吸着法における吸脱着等温線ヒステリシスの面積比率が吸着等温線の積分値に対して16.2%である中空円筒形状のアルミナ担体を得た。このアルミナ担体30gに水を十分に吸収させた後、CuCl2=255g/L、KCl=140g/Lの水溶液80mLに2時間浸漬させた。浸漬液からアルミナ担体を取り出し、マッフル炉を用いて120℃で2時間乾燥させた。その後、420℃で6時間焼成し、K/Cu比が0.80であるオキシ塩素化触媒を調製した。ガス吸着法における吸脱着等温線ヒステリシスの面積比率は、吸着等温線の積分値に対して、24.5%であった。定量分析の結果、12.7%CuCl2-5.6%KCl/アルミナ触媒であった。この触媒15mlと、外径5.0mm、内径2.0mm、側面の長さ5.0mm、比表面積1.7m2/gの中空円筒形状グラファイト希釈剤15mlを混合したこと以外は実施例29と同様の方法で評価した。
2:脱着側
3:吸着側
Claims (20)
- 多孔質担体上に金属化合物が担持された不均一系触媒であって、ガス吸着法の吸着等温線と脱着等温線との間に生じるヒステリシスの積分値が、吸着等温線の全積分値に対して19%以下であることを特徴とする触媒。
- 多孔質担体がアルミナ、シリカ、シリカ―アルミナ、ゼオライト、酸化チタン、酸化ジルコニウム又は酸化マグネシウムであることを特徴とする、請求項1に記載の触媒。
- 金属化合物の金属が、周期表1族、2族又は11族であることを特徴とする請求項1又は2に記載の触媒。
- 金属化合物が、酸化物またはハロゲン化物であることを特徴とする請求項1~3のいずれかに記載の触媒。
- 金属化合物が塩化銅であることを特徴とする請求項1~4のいずれかに記載の触媒。
- 金属化合物が、塩化銅並びに塩化カリウム、塩化セシウム、塩化ナトリウムおよび塩化マグネシウムからなる群から選択される1種以上の金属塩化物であることを特徴とする請求項1~5のいずれかに記載の触媒。
- 塩化銅の担持量が3~25重量%であることを特徴とする請求項5又は6に記載の触媒。
- 金属塩化物の担持量が、0.1~20重量%であることを特徴とする請求項6又は7に記載の触媒。
- ガス吸着法が窒素吸着法であることを特徴とする請求項1~8のいずれかに記載の触媒。
- 不均一系触媒が中空円筒形状であることを特徴とする請求項1~9のいずれかに記載の触媒。
- 外径3~6mm、内径1~3mm未満、長さ3~6mmの中空円筒形状であることを特徴とする請求項10に記載の触媒。
- 触媒がエチレンのオキシ塩素化用途に使用される請求項1~11のいずれかに記載の触媒。
- 請求項1~12のいずれかに記載の触媒の存在下、エチレン、塩化水素及び酸素のオキシ塩素化を行うことを特徴とする1,2-ジクロロエタンの製造方法。
- 請求項1~12のいずれかに記載の触媒及び球形状、円柱形状または中空円筒形状を有する希釈剤を含むことを特徴とする、エチレン、塩化水素および酸素から1,2-ジクロロエタンの製造用触媒システム。
- 希釈剤が、アルミナ、シリカ、アルミナ-シリカ、炭化ケイ素、窒化アルミニウム、炭素及びグラファイトからなる群より選択される少なくとも1種であることを特徴とする請求項14に記載の1,2-ジクロロエタンの製造用触媒システム。
- 球形状を有する希釈剤の外径Dが下記一般式(1)の寸法(mm)である請求項14又は15に記載の1,2-ジクロロエタンの製造用触媒システム。
4.5≦D≦7.0 (1) - 円柱形状を有する希釈剤の円柱の外径De1が下記一般式(2)の寸法(mm)、側面の長さL1が下記一般式(3)の寸法(mm)である請求項14又は15に記載の1,2-ジクロロエタンの製造用触媒システム。
4.5≦De1≦7.0 (2)
4.0≦L1≦7.0 (3) - 中空円筒形状を有する希釈剤の中空円筒の外径De2が下記一般式(4)の寸法(mm)、その内径Diが下記一般式(5)の寸法(mm)、側面の長さL2が下記一般式(6)の寸法(mm)、外径De2と内径Diの関係が下記一般式(7)である請求項14又は15に記載の1,2-ジクロロエタンの製造用触媒システム。
4.5≦De2≦7.0 (4)
1.5≦Di≦4.0 (5)
4.0≦L2≦7.0 (6)
De2/3≦Di (7) - 希釈剤の外径がオキシ塩素化触媒の長さと等しい長さである請求項14~18のいずれかに記載の1,2-ジクロロエタンの製造用触媒システム。
- 請求項14~19のいずれかに記載の1,2-ジクロロエタンの製造用触媒システムの存在下で、エチレン、塩化水素および酸素を反応させることを特徴とする1,2-ジクロロエタンの製造方法。
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US9687824B2 (en) | 2017-06-27 |
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TWI642481B (zh) | 2018-12-01 |
EP3023149A4 (en) | 2017-03-15 |
JP6379781B2 (ja) | 2018-08-29 |
CN105392561B (zh) | 2018-04-03 |
CN105392561A (zh) | 2016-03-09 |
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TW201513936A (zh) | 2015-04-16 |
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