EP2501473A1 - Kugelförmiger, zeolithischer katalysator zur umsetzung von methanol zu olefinen - Google Patents
Kugelförmiger, zeolithischer katalysator zur umsetzung von methanol zu olefinenInfo
- Publication number
- EP2501473A1 EP2501473A1 EP10776743A EP10776743A EP2501473A1 EP 2501473 A1 EP2501473 A1 EP 2501473A1 EP 10776743 A EP10776743 A EP 10776743A EP 10776743 A EP10776743 A EP 10776743A EP 2501473 A1 EP2501473 A1 EP 2501473A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- catalyst according
- binder
- diameter
- olefins
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 113
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 16
- 239000011230 binding agent Substances 0.000 claims abstract description 32
- 238000000034 method Methods 0.000 claims description 77
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 44
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 36
- 238000006243 chemical reaction Methods 0.000 claims description 31
- 238000001354 calcination Methods 0.000 claims description 15
- 239000011148 porous material Substances 0.000 claims description 14
- 238000002360 preparation method Methods 0.000 claims description 11
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 10
- 238000000465 moulding Methods 0.000 claims description 10
- 238000005469 granulation Methods 0.000 claims description 9
- 230000003179 granulation Effects 0.000 claims description 9
- 238000001694 spray drying Methods 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 5
- 239000002915 spent fuel radioactive waste Substances 0.000 claims description 3
- 229910052809 inorganic oxide Inorganic materials 0.000 claims description 2
- 239000000376 reactant Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 abstract description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 abstract description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 22
- 239000010457 zeolite Substances 0.000 description 22
- 229910021536 Zeolite Inorganic materials 0.000 description 20
- 239000000203 mixture Substances 0.000 description 19
- 239000003513 alkali Substances 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 230000003197 catalytic effect Effects 0.000 description 12
- 239000000047 product Substances 0.000 description 12
- 239000011541 reaction mixture Substances 0.000 description 11
- 239000000243 solution Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 229910052782 aluminium Inorganic materials 0.000 description 10
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 10
- 239000000843 powder Substances 0.000 description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 9
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 8
- 230000015572 biosynthetic process Effects 0.000 description 8
- 229910052710 silicon Inorganic materials 0.000 description 8
- 239000010703 silicon Substances 0.000 description 8
- 238000003756 stirring Methods 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 7
- 239000002253 acid Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000012736 aqueous medium Substances 0.000 description 5
- 239000006185 dispersion Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000012065 filter cake Substances 0.000 description 5
- 238000005342 ion exchange Methods 0.000 description 5
- 150000002500 ions Chemical class 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 239000000725 suspension Substances 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- 239000013078 crystal Substances 0.000 description 4
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 238000001879 gelation Methods 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- -1 tetrapropylammonium compound Chemical class 0.000 description 4
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000012431 aqueous reaction media Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000011159 matrix material Substances 0.000 description 3
- 229910017604 nitric acid Inorganic materials 0.000 description 3
- 150000007524 organic acids Chemical class 0.000 description 3
- 238000005453 pelletization Methods 0.000 description 3
- 238000001935 peptisation Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000007858 starting material Substances 0.000 description 3
- BGQMOFGZRJUORO-UHFFFAOYSA-M tetrapropylammonium bromide Chemical compound [Br-].CCC[N+](CCC)(CCC)CCC BGQMOFGZRJUORO-UHFFFAOYSA-M 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 238000004438 BET method Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000032683 aging Effects 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000008119 colloidal silica Substances 0.000 description 2
- 150000002170 ethers Chemical class 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003349 gelling agent Substances 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 239000004005 microsphere Substances 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 150000007522 mineralic acids Chemical class 0.000 description 2
- 239000006199 nebulizer Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000002459 porosimetry Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000007493 shaping process Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000012798 spherical particle Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- LPSKDVINWQNWFE-UHFFFAOYSA-M tetrapropylazanium;hydroxide Chemical compound [OH-].CCC[N+](CCC)(CCC)CCC LPSKDVINWQNWFE-UHFFFAOYSA-M 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- QSAMQSXFHVHODR-UHFFFAOYSA-N Cl.C=CC#N Chemical compound Cl.C=CC#N QSAMQSXFHVHODR-UHFFFAOYSA-N 0.000 description 1
- 235000013162 Cocos nucifera Nutrition 0.000 description 1
- 244000060011 Cocos nucifera Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 229920001328 Polyvinylidene chloride Polymers 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 229910052910 alkali metal silicate Inorganic materials 0.000 description 1
- 150000004645 aluminates Chemical class 0.000 description 1
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical class O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000007900 aqueous suspension Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001493 electron microscopy Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 229920005615 natural polymer Polymers 0.000 description 1
- 229910000484 niobium oxide Inorganic materials 0.000 description 1
- URLJKFSTXLNXLG-UHFFFAOYSA-N niobium(5+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[Nb+5].[Nb+5] URLJKFSTXLNXLG-UHFFFAOYSA-N 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 150000004831 organic oxygen compounds Chemical class 0.000 description 1
- 150000002927 oxygen compounds Chemical class 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- 229920001184 polypeptide Polymers 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 229920000131 polyvinylidene Polymers 0.000 description 1
- 239000005033 polyvinylidene chloride Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000004626 scanning electron microscopy Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000010414 supernatant solution Substances 0.000 description 1
- 229920005613 synthetic organic polymer Polymers 0.000 description 1
- 230000002123 temporal effect Effects 0.000 description 1
- 125000005207 tetraalkylammonium group Chemical group 0.000 description 1
- 238000007669 thermal treatment Methods 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
Classifications
-
- 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
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0018—Addition of a binding agent or of material, later completely removed among others as result of heat treatment, leaching or washing,(e.g. forming of pores; protective layer, desintegrating by heat)
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
-
- B01J35/40—
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- B01J35/51—
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- B01J35/615—
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- B01J35/617—
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- B01J35/633—
-
- B01J35/635—
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- 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
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/42—Addition of matrix or binder particles
-
- 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
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
-
- 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
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0063—Granulating
-
- 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
- B01J37/0072—Preparation of particles, e.g. dispersion of droplets in an oil bath
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a catalyst based on pentasil aluminosilicates, in the form of spheres having an average diameter between 0.3 and 7 mm, the BET surface area of the catalyst being between 300 and 600 m 2 / g and a binder is included. Furthermore, the invention relates to a process for the preparation of the catalyst according to the invention, and its use for the conversion of methanol into olefins, in particular to propylene. The present invention also relates to a process for the production of olefins from methanol.
- zeolite catalysts are used on an industrial scale. Catalysts based on crystalline aluminosilicates prepared from an aluminum source, a silicon source, an alkali source, a template (e.g., a tetrapropylammonium compound), and water are known, for example, from U.S. Patent 3,702,886.
- the size of the primary crystallites of catalysts is considered to be important for the life of the catalysts. Usually, however, these primary crystallites are not used directly as a fine powder but are formed into larger particles to be more suitable for use in catalytic processes. It is of great importance here that the reaction parameters in the reactor, for example a fixed bed reactor, can be optimally adjusted.
- the reaction parameters are of the properties of the catalysts, in particular their catalytic
- EP-A-173 901 relates to a process for the preparation of small zeolite crystallites from the ZSM-5 Type having a SiO 2 / Al 2 O 3 molar ratio of more than 5, corresponding to an Si / Al atomic ratio of more than 2.5. The smallest dimension of the crystallites is below 0.3 pm.
- the crystallites are subjected to an ion exchange reaction and formed into larger particles after mixing with a matrix material. These are dried and calcined to give catalysts for various hydrocarbon conversion reactions.
- EP 1 424 128 relates to catalysts of crystalline aluminosilicate with Primärkristaiiiten having an average diameter of at least 0.01 pm and less than 0.1 pm, which are combined into agglomerates of 5 to 500 pm, wherein the primary crystallites or agglomerates by finely divided Alumina are interconnected.
- the catalyst material thus obtained is then extruded in a commercial extruder into moldings having a diameter of about 1.5 mm and a length of 3 mm.
- EP 0 369 364 B1 relates to catalysts based on crystalline aluminosilicates of the pentasil type having an Si / Al atomic ratio of at least 10, which are composed of primary crystals having an average diameter of at least 0.1 ⁇ m and at most 0.9 ⁇ m.
- EP-A-123 449 describes a process for the conversion of alcohol or ethers into olefins using steam-treated zeolite catalysts; these have a crystal size of less than 1 pm and can be incorporated into a matrix.
- the matrix materials indicated are clays, silicic acid and / or metal oxides.
- US-A-4 025 572 relates to a process for the preparation of certain hydrocarbon mixtures, wherein the catalyst bed and the like. contains a zeolite. The synthesis of the zeolite is carried out in the presence of sulfuric acid and using Al 2 (SO 4 ) 3 .xH 2 O. As an example, the zeolite catalyst is mixed with 90 wt% alumina and pelletized.
- This object is achieved by the catalysts defined in the claims and the inventive use of the catalysts for the conversion of methanol to olefins, in particular to propylene.
- the catalyst of the invention based on pentasil type aluminosilicates is used in the form of spheres having a mean diameter between 0.3 to 7 mm, preferably between 0.5 and 5 mm, more preferably between 1 and 3.5 mm, more preferably between 2 and 3 mm, and more preferably between 2.2 and 2.8 mm.
- At least 20%, more preferably at least 40%, more preferably at least 60%, even more preferably at least 80%, more preferably at least 90% and most preferably at least 98% of the spheres have a diameter between 0.3 and 7 mm, preferably between 0.5 and 5, more preferably between 1 and 3 mm, more preferably between 2 and 3 mm and most preferably between 2.2 and 2.8 mm. More preferably, at least 40%, more preferably at least 60%, even more preferably at least
- aluminosilicate which is suitable according to the invention can be prepared in any desired manner, for example in an aqueous reaction mixture containing a silicon source, an aluminum source, an alkali source and optionally a template.
- an alkaline aluminosilicate gel is produced at elevated temperature and optionally at elevated pressure in a conventional manner and converted into a crystalline aluminosilicate, but the reaction is stopped when the resulting primary crystallites have an average diameter of at least 0.01 pm, but less than 0.1 pm, preferably from 0.01 to 0.06 pm, in particular from 0.015 to 0.05 pm.
- a process for producing crystalline aluminosilicate is known, for example, from EP 1 424 128.
- the primary crystallites may partially combine to form agglomerates, which, however, are only loosely bound to each other, such as in filter cake. From this, the primary crystallites can be relatively easily, if necessary, e.g. by dispersing the filter cake in an aqueous medium and stirring the dispersion.
- the average diameter of the primary crystallites is defined as the arithmetic mean, averaged over a plurality of crystallites, between the largest and smallest diameters of a single crystallite as determined by scanning electron microscopy at a magnification of 20,000 (magnifications of, for example, 80,000 or even 10,000 also used, see the method section below).
- This definition has its significance in crystallites with an irregular crystal habit, eg in rod-shaped crystallites. In the case of spherical or approximately spherical crystallites, the largest and the smallest diameter coincide. The method for determining the diameters of the primary crystallites is described in the Methods section.
- the thus-obtained primary crystallites or agglomerates thereof may then be shaped into spheres using a binder and optionally a burnout agent.
- Processes for this purpose are known to the person skilled in the art and include, for example, processes for granulation (for example in a pelletizing dish or Eirich mixer), spray-drying processes, gelling processes such as, for example, the oil-drop process and molding processes using press extruders.
- a preferred method of manufacturing balls is granulation in the pelletizer or Eirich mixer. When produced in an Eirich mixer, powdery ingredients (eg, zeolite powder and burnout) are contacted with a liquid component (eg, binder suspension) and mixed thoroughly to form spherical granules. Subsequently, the obtained balls are dried and calcined.
- the so-called oil-drop method can be used.
- droplet coagulation takes place starting from a metastable sol which is suspended in a different liquid phase, with simultaneous gelation, aging and shaping.
- a usually aqueous sol is converted by means of a nebulizer into droplet form, wherein the size of the nebulizer nozzles is selected according to the desired ball diameter.
- the generated droplets are passed through a heated, water-immiscible solvent (e.g., 100 ° C oil) and settle therein due to immiscibility. Due to the surface tension, gel balls are formed, which are dried after aging.
- a heated, water-immiscible solvent e.g. 100 ° C oil
- Aluminum oxide microspheres used in the "Thermofor Catalytic Cracking" TCC process are, in particular Composition of the sol, nature of the continuous phase (where, inter alia, the density and the surface tension of importance), temperature, pH and contact time. Depending on the specific gravity, the injection may be from the top or bottom of the column and, accordingly, the process is also referred to as “oil-drop” or “oil-up”.
- the molding process can be used with two-shell press extruders for ball production.
- powdery ingredients eg, zeolite powder and burnout material
- a liquid component eg, binder suspension and / or release agent
- Suitable binders for producing the spherical catalysts according to the invention are, for example, inorganic oxides, preferably aluminum oxide, magnesium oxide, titanium oxide, zinc oxide, niobium oxide, zirconium oxide or silicon oxide, and mixtures thereof, as well as amorphous aluminosilicates and non-oxidic binders such as, for example, aluminum phosphates.
- alumina is used.
- Modified alumina such as phosphorus-modified alumina may also be used.
- Particularly preferred is the use of finely divided alumina binder, which is preferably obtained by hydrolysis of aluminum trialkyls or aluminum alcoholates, or used in the form of peptisable alumina hydrate. Very particular preference is given to using peptisable alumina hydrate as binder. More preferably, at least 95% of the particles of the peptisable alumina hydrate (based on the average diameter) ⁇ 55 pm.
- the binder in an amount of 5 to 60% by weight, more preferably 10 to 40% by weight, based on the total weight of aluminosilicate and binder.
- burnout materials are preferably used.
- Ausbrennstoffen are pore-forming substances by which the porosity and pore structure of shaped catalysts can be adjusted in a known manner by the so-called temporary additives (burnout) are added to the plasticized catalyst composition prior to shaping, which then by thermal treatment of the molding again be removed.
- pore-forming substances are, for example, natural and synthetic organic polymers, polypeptides, polysaccharides such as wood chips, coconut shells, waxes, polystyrene or polyvinylidene chloride.
- Graphite, sugar, starch and urea can be mentioned as further pore-forming additives or burnout substances (D. Kerner, M. Rochina, in Handbook of Heterogenous Catalysis, G. Ertl, H. Knoeginger, F. Schuith, J. Weitkamp (Edts.) , Second Edition, Vol. 1, p 286).
- the structure of the balls of the finished catalyst of primary crystallites, agglomerates and binders also determines the BET surface area, the pore volume and the pore diameter.
- the BET surface of the finished catalyst of primary crystallites, agglomerates and binders also determines the BET surface area, the pore volume and the pore diameter.
- Catalyst in the form of spheres is determined as described in the Methods section and is between 300 and 600 m 2 / g, more preferably 330 to 450 m 2 / g, particularly preferably between 350 and 420 m 2 / g - Das Pore volume of the final catalyst in the form of spheres is determined as described in the Methods section, and is preferably between 0.2 and 0.8 cm 3 / g, more preferably between 0.25 and 0.7 cm 3 / g, and more preferably between 0.28 and 0.6 cm 3 / g - Furthermore, additionally preferably at least 10%, preferably at least 20%, and in particular at least 60%, of the pores of the finished catalyst in the form of spheres have a diameter of 14 to 1750 nm, preferably 80 up to 1750 nm.
- the average diameter of the catalyst balls is defined as the arithmetic mean averaged over a plurality of balls.
- the BET surface area, pore volume, and diameter of the catalyst spheres described above, optionally in combination with the pore diameter, are an optimum selection to obtain catalysts with high activity, selectivity, and lifetime.
- the present invention also relates to a process for the preparation of the catalyst according to the invention, wherein primary crystallites having an average diameter of at least 0.01 .mu.m and less than 0.1 .mu.m or agglomerates thereof are mixed with a binder and optionally with a spent fuel and into spheres with an average diameter between 0.3 and 7 mm are formed, and then followed by drying and calcination of the catalyst is carried out.
- Suitable processes for the formation of spherical particles include, in particular, processes for granulation (for example in a pelletizing dish or Eirich mixer), spray-drying processes, gelling processes such as, for example,
- an alkaline aluminosilicate gel is produced at elevated temperature and optionally at elevated pressure in a conventional manner and converted into a crystalline aluminosilicate, but the Reaction is terminated if the resulting primary crystallites have an average diameter of at least 0.01 pm, but less than 0.1 pm, preferably from 0.01 to 0.06 pm, in particular from 0.015 to 0.05 pm;
- step (c) the product of step (b) is reacted to separate the alkali ions in aqueous medium with a proton-containing or proton-generating substance, separated, dried, and optionally recombined
- step (d) the powder of step (c) is mixed with a binder, preferably alumina hydrate, and optionally a burnout material, and by a suitable process, preferably granulation processes (for example in the pelletizer or Eirich mixer)
- a binder preferably alumina hydrate, and optionally a burnout material
- Spray drying, gelation method such as the oil-drop method and molding method using press extruders converted into balls with the diameter according to the invention
- step (e) the product of step (d) is subjected to drying and a
- step (a) first an aqueous reaction mixture containing a silicon source (for example colloidal silica or an alkali silicate), an alkali and an aluminum source (alkali aluminate, especially sodium aluminate) and a template are prepared.
- a silicon source for example colloidal silica or an alkali silicate
- alkali and an aluminum source alkali aluminate, especially sodium aluminate
- a template aqueous reaction mixture containing a silicon source (for example colloidal silica or an alkali silicate), an alkali and an aluminum source (alkali aluminate, especially sodium aluminate) and a template are prepared.
- a silicon source for example colloidal silica or an alkali silicate
- alkali and an aluminum source alkali aluminate, especially sodium aluminate
- a template for example colloidal silica or an alkali silicate
- alkali and an aluminum source alkali
- the catalyst is to be used in a CMO or MTP process, in particular a process according to DE 100 27 159 A1, the disclosure of which is hereby included in the description, the weight fractions between silicon source and aluminum source is selected such that crystalline aluminosilicates having a Si / Al atomic ratio between about 50 and 250, preferably about 50 and 150, in particular about 75 to 120 are obtained.
- an alkaline aluminosilicate gel is produced at elevated temperature and optionally at elevated pressure in a manner known per se. You can already work at temperatures above 90 ° C, but in this case, the reaction times are relatively long (about 1 week). It is therefore preferably at temperatures of 90 to 190 ° C, in particular of
- Aluminosilicate If the temperature of the reaction mixture is higher than 190 ° C, the growth of the aluminosilicate primary crystallites becomes too fast and it easily obtain too large primary crystallites, while at the same time still aluminosilicate gel is present in the reaction mixture.
- the template employed are tetraalkylammonium compounds, preferably tetrapropylammonium hydroxide (TPAOH) or tetrapropylammonium bromide (TPABr). It is also possible to use mixtures of ammonia or an organic amine and another organic compound from the group of the alcohols, preferably butanol, as the template.
- the aqueous reaction batch of step (a) preferably has a pH of 10 to 13. At a pH of less than 10, the conversion of the aluminosilicate gel to the crystalline aluminosilicate proceeds relatively slowly. At higher pH's than 13, the aluminosilicate crystals may re-dissolve in some cases.
- Formation of the crystalline aluminosilicate primary crystallites can be controlled by proper selection of the source of silicon, the source of aluminum, the source of alkali, and the template, as well as by appropriate selection of temperature and pH and stirring rate. It is essential that the reaction is stopped when the primary crystallites have reached the desired mean diameter.
- a new reaction mixture does not always have to be prepared. Rather, to produce the aluminosilicate gel, the
- Silicon source, the alkali source, the aluminum source, the template and the water from the mother liquors of previous syntheses used and by the for the synthesis of aluminosilicate gel required amounts of said compounds are added.
- the formation of the aluminosilicate primary crystallites of step (a) is preferably carried out at a pH between 10 and 13, with the reaction mixture being stirred. In this way, the size distribution of the primary crystallites is homogenized.
- the stirring speed should, however, preferably not be more than 900 rpm. For larger stirring speeds, the proportion of smaller primary crystallites is higher, which may be advantageous, as long as it is ensured that the average diameter of all primary crystallites is at least 0.01 pm.
- step (b) the primary crystallites are separated from the aqueous reaction medium as pre-agglomerates, i. not as single crystallites.
- a flocculant to the aqueous reaction medium.
- a cationic organic macromolecular compound is used as a flocculating agent.
- the flocculant not only facilitates the separation of the primary crystallites from the reaction medium (improved filterability), but also causes the primary crystallites to assemble into pre-agglomerates which already largely resemble the agglomerates formed in the following step in terms of size, structure and attachment of the primary crystallites.
- the pre-agglomerates are dried and subjected to an intermediate calcination, which is preferably carried out first in an inert atmosphere at about 200 to 350 ° C, in particular at about 250 ° C, wherein a portion of the template is decomposed.
- the intermediate calcination can then be completed in an oxidizing atmosphere at about 350 to 600 ° C, with any remaining amount of template being burned off.
- the pre-agglomerates are calcined for about 1 to 20 hours in the inert atmosphere and about 1 to 30 hours in the oxidizing atmosphere.
- step (c) the product of step (b) is reacted to exchange the alkali ions in an aqueous medium with a proton-containing or proton-producing substance upon heating.
- the ion exchange may be carried out with the aid of a dilute mineral acid (eg hydrochloric acid, nitric acid or sulfuric acid) or an organic acid (eg acetic acid).
- the ion exchange is preferably carried out with stirring for at least one hour at temperatures between 25 and 100 ° C, wherein at least a portion of the alkali ions are exchanged in the Voragglomeraten the primary crystallites by hydrogen ions. If necessary, the ion exchange can be repeated under the same conditions.
- the proton-containing product (H-zeolite) is separated (for example by filtration), dried and optionally subjected to intermediate calcination.
- the insects is carried out at temperatures of 400 to 800 ° C, preferably at about 600 ° C over a period of 5 to 20 hours.
- the ion exchange can also be carried out with the aid of an ammonium salt solution under comparable conditions.
- the alkali ions are exchanged by ammonium ions.
- ammonia is removed to give a proton-containing product.
- the pulverulent product obtained after drying and optionally intermediate calcining contains, on the one hand, agglomerates> 500 ⁇ m and, on the other hand, dust contents of ⁇ 5 ⁇ m. It will therefore be a
- the Agglomerate fraction separated from about 5 to 500 pm is mixed in step (d) with the binder and optionally the burn-out agent, wherein of the particles of the binder are preferably at least 95% ⁇ 55 pm and at least 30%> 35 pm. These values are, averaged over a plurality of particles, in each case based on the average diameter, which is defined as the average diameter of the primary crystallites.
- the binder preferably the alumina, typically has the following grain spectrum: 99% ⁇ 90 ⁇ m; 95% ⁇ 45 pm; 55% ⁇ 25 pm.
- the binder is essentially responsible for the adjustment of the pore volume of the catalyst according to the invention.
- the amount of the finely divided alumina hydrate binder to be used is preferably about 5 to 60% by weight based on the total weight of the product (mixture) of step (d).
- the finely divided alumina hydrate binder is peptizable alumina which is particularly low in Na and Fe.
- an acid concentration of 0.01 to 2.5 mol H + / mol Al 2 O 3 preferably from 0.02 to 1.5 mol H + / mol Al 2 O 3 , more preferably from 0, 05 to 1.0 mol H + / mol Al 2 0 3 and in particular from 0.1 to 0.8 mol H + / mol Al 2 0 3 set.
- the peptization can in principle be carried out with organic or inorganic acids in a concentration range of the acid of 0.1% to 100%.
- organic acids such as 100% acetic acid or dilute inorganic acids such as 52% nitric acid, etc. may be used.
- step (d) The mixture of the agglomerate fraction and the binder is converted into spheres in step (d) by methods known to those skilled in the art.
- Processes include, in particular, processes for granulation (for example in a pelletizing dish or Eirich mixer), spray-drying processes, gelling processes such as, for example, the oil-drop process and molding methods using press extruders as discussed in detail above.
- step (e) The product of step (d) is then subjected to drying and final calcination in step (e). This may generally be carried out at temperatures between about 350 ° C and 850 ° C, preferably between about 500 ° C and 850 ° C, for 1 to 12 hours. However, it has also surprisingly been found in the context of the present invention that the final calcination is carried out particularly advantageously at a temperature of 660 ° C. to 850 ° C. for less than 5 hours, in particular from 680 ° C. to 800 ° C. for 1 to 4 hours.
- the end product thus obtained can, as mentioned above, be used particularly advantageously in CMO processes, particularly preferably MTP processes.
- the present invention also relates to a process for the preparation of
- oxygenates are understood as meaning oxygen compounds, in particular organic oxygen compounds, such as
- the gaseous starting material may also contain, in addition to oxygenate and water vapor.
- the reactant gas in a catalytic cycle of over 370 hours over a directed catalyst of the invention.
- the process according to the invention for the production of olefins from methanol takes place at temperatures in the reactor between 380 ° C and 550 ° C, more preferably between 420 ° C and 510 ° C, wherein preferably the WHSV (weight hourly space velocity) in the range of 0.25 to 5 h "1 , more preferably 0.4 to 3 h " 1 , and particularly preferably in the range of 0.5 to 1.5 h "1 .
- WHSV weight hourly space velocity
- Figure 1 shows the catalytic properties of the spherical catalysts according to the invention in comparison with catalysts in the form of extrudates.
- the reported values for the primary crystallites are the average dimensions (arithmetic mean of the largest and the smallest dimension, averaged over a plurality of crystallites, preferably at least 25 crystallites are used). These values are measured using a LEO Field Emission Scanning Electron Microscope (LEO Electron Microscopy Inc., USA) using powder samples of the
- Catalyst which had previously been redispersed in acetone, ultrasonicated for 30 seconds and then applied to a support (Sample Current Range: 4 pA to 10 nA).
- the measurement usually at 20000x magnification (magnifications of 80,000 or even 10,000 are also suitable). The values could be confirmed at 253,000 times magnification.
- the pore diameter results from the mercury porosimetry
- the pore volume is determined using the
- a catalyst was prepared according to Example 1 of EP 1 424 128 with an average diameter of the primary crystallites of about 0.03 ⁇ m (Si / Al ratio 105). The process and the physical and chemical properties of the product specified therein are expressly incorporated by reference into the present specification.
- aluminosilicate zeolites having a primary crystallite size of ⁇ 1 ⁇ m were produced.
- the catalysts were prepared with the addition of alumina as a binder.
- a reaction mixture was prepared by intimately mixing two solutions at room temperature in a 40 liter autoclave.
- the two solutions were designated solution A and solution B.
- Solution A was prepared by dissolving 2218 g of TPABr in 11 kg of deionized water. In this solution, 5000 g of a commercial silica were added.
- Solution B was prepared by dissolving 766 g of NaOH and then 45.6 g of NaAlO 2 in 5.5 liters of deionized water. The still warm solution B was added to solution A.
- the autoclave was then closed and stirred at about 60 rpm. immediately brought to the reaction temperature. The reaction was stopped as soon as the average diameter of the primary crystallites was 0.03 ⁇ m.
- the filter cake was slurried in about 40 liters of deionized water, added with about 5 liters of a 0.4 wt% aqueous suspension of a commercially available flocculant, and decanted after stirring and settling the pre-agglomerates of the solid.
- the described washing process was repeated until the wash water had a pH of 7 to 8 and a Br concentration of less than 1 ppm.
- Filter cake was then dried at 120 ° C for 12 hours.
- the dried filter cake was comminuted with a commercial granulator to a grain size of 2 mm.
- the granules were brought at a heating rate of 1 ° C / min under nitrogen (1000 Nl / h) to 350 ° C and calcined at 350 ° C for 15 hours under nitrogen (1000 Nl / h). Then, the temperature was raised to 540 ° C at a heating rate of 1 ° C / min, and the granules were calcined in air at this temperature for 24 hours to burn off the remaining template.
- the calcined Na zeolite was suspended in a 5-fold amount of a 1-molar HCI aqueous solution and brought to 80 °. At this Temperature was stirred for one hour. Then, about 1 liter of a 0.4% by weight suspension of the flocculant was added and the supernatant was decanted off after the solid had settled. The process thus described was repeated once more.
- the solid was suspended in about 10 washings in 60 liters of deionized water with stirring and mixed with an average of 100 ml of a 0.4 wt .-% suspension of the flocculant. After the zeolite had settled, the supernatant solution was decanted. When the content of CI " in the washing water ⁇ was 5 ppm, the suspension was filtered off and dried at 120 ° C for 15 hours.
- the dried H-zeolite was crushed with a commercial granulator to 2 mm and placed under air at a heating rate of 1 ° C / min to 540 ° C and calcined at this temperature under air for 10 hours.
- This mixture was kneaded for about 30 minutes until plating and extruded in a commercial extruder into cylindrical shaped articles having a diameter of about 1.5 mm and a length of about 3 mm.
- the final calcination was carried out at 650 ° C for 3 hours.
- Example B The composition of the cylindrical extrudate of Comparative Example A is shown in Table I.
- Example B The composition of the cylindrical extrudate of Comparative Example A is shown in Table I.
- composition of the spherical catalyst of Example B according to the invention is given in Table I.
- composition of the spherical catalyst of Example C according to the invention is given in Table I.
- the catalytic activity of the spherical catalyst according to the invention from Example C is shown on the basis of experimental data in Figure 1.
- the methanol / water feed was with a WHSV of 3 (kg / (kgxh), ie Kilogram of total feed per kilogram of catalyst and per hour at a pressure of 1 bar for the conversion of methanol over the CMO catalyst in an isothermal fixed-bed tubular reactor .
- Gas phase and liquid phase at the outlet of the CMO catalyst reactor were determined by the usual gas chromatographic analysis method.
- the catalysts (also the catalyst according to the invention) can be regenerated after completion of a first cycle by first stopping the MeOH flow. Nitrogen is then fed to displace residual MeOH. Finally, oxygen is slowly added to the nitrogen in gradually increasing concentrations to burn off the hydrocarbon deposited on the catalysts. The regeneration of the catalysts is complete when the oxygen content of the nitrogen stream at the inlet and outlet of the catalyst bed is the same.
Abstract
Description
Claims
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DE102009053922A DE102009053922A1 (de) | 2009-11-19 | 2009-11-19 | Kugelförmiger, zeolithischer Katalysator zur Umsetzung von Methanol zu Olefinen |
PCT/EP2010/067587 WO2011061196A1 (de) | 2009-11-19 | 2010-11-16 | Kugelförmiger, zeolithischer katalysator zur umsetzung von methanol zu olefinen |
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DE102010026880A1 (de) * | 2010-07-12 | 2012-01-12 | Süd-Chemie AG | Verfahren zur Herstellung von Katalysatoren auf Zeolithbasis zur Umsetzung von Oxygenaten zu niederen Olefinen |
DE102011013909A1 (de) | 2011-03-15 | 2012-09-20 | Süd-Chemie AG | Verfahren zur Herstellung eines Katalysators auf Zeolithbasis zur Umwandlung von Methanol in Olefine |
RU2518091C1 (ru) * | 2012-10-26 | 2014-06-10 | Федеральное государственное бюджетное учреждение науки Ордена Трудового Красного Знамени Институт нефтехимического синтеза им. А.В. Топчиева Российской академии наук (ИНХС РАН) | Катализатор и способ синтеза олефинов из диметилового эфира в его присутствии |
JP2023510094A (ja) | 2019-12-11 | 2023-03-13 | ビーエーエスエフ ソシエタス・ヨーロピア | ゼオライト触媒の成形品を調製する方法 |
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GB1601915A (en) | 1977-05-25 | 1981-11-04 | Mobil Oil Corp | Method of preparation of large crystal alumino-silicate zeolite catalyst |
DE3228269A1 (de) | 1982-07-29 | 1984-02-02 | Degussa Ag, 6000 Frankfurt | Katalysator fuer die konvertierung von alkoholen und/oder aliphatischen aethern zu ungesaettigten kohlenwasserstoffen und das verfahren zu dessen herstellung |
NZ207523A (en) | 1983-04-22 | 1986-03-14 | Mobil Oil Corp | Catalytic production of olefin mixtures from alcohols and/or ethers |
AU579656B2 (en) | 1984-09-04 | 1988-12-01 | W.R. Grace & Co.-Conn. | Process to make small crystallites of zsm-5 |
DE3838710A1 (de) | 1988-11-15 | 1990-05-17 | Sued Chemie Ag | Katalysator auf der basis von kristallinen alumosilikaten |
DE4009459A1 (de) | 1990-03-23 | 1991-09-26 | Metallgesellschaft Ag | Verfahren zur erzeugung von niederen olefinen |
EP0507122B1 (de) | 1991-03-11 | 1995-01-11 | Mitsubishi Oil Co., Ltd. | Verfahren zur Herstellung von sphärischen Zeolithkatalysatoren und Vorrichtung zur Herstellung derselben |
US5365003A (en) * | 1993-02-25 | 1994-11-15 | Mobil Oil Corp. | Shape selective conversion of hydrocarbons over extrusion-modified molecular sieve |
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CA2374739A1 (en) * | 1999-05-20 | 2000-11-30 | Wilfried J. Mortier | Hydrocarbon conversion process and catalyst useful therein |
DE10027159A1 (de) | 2000-05-31 | 2001-12-13 | Mg Technologies Ag | Verfahren zum Erzeugen von Propylen aus Methanol |
KR100413692B1 (ko) * | 2002-01-21 | 2004-01-03 | 삼성전자주식회사 | 채널명 자동 완성 기능을 이용한 채널 선국 방법 및텔레비전 수상기 |
ATE419062T1 (de) * | 2002-12-01 | 2009-01-15 | Sued Chemie Ag | Verwendung eines katalysators auf der basis von kristallinem alumosilicat |
DE10356184A1 (de) * | 2003-12-02 | 2005-07-07 | Basf Ag | Zeolithisches Material vom Pentasil-Strukturtyp, seine Herstellung und seine Verwendung |
DE102004029544A1 (de) * | 2004-06-18 | 2006-01-05 | Basf Ag | Formkörper enthaltend ein mikroporöses Material und mindestens ein siliciumhaltiges Bindemittel, Verfahren zu seiner Herstellung und seine Verwendung als Katalysator, insbesondere in einem Verfahren zur Herstellung von Triethylendiamin (TEDA) |
US7414167B2 (en) * | 2005-01-14 | 2008-08-19 | Uop Llc | Conversion of oxygenate to propylene using moving bed technology and a separate heavy olefin interconversion step |
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EP2082801A1 (de) | 2008-01-25 | 2009-07-29 | Total Petrochemicals Research Feluy | Verfahren zur Gewinnung modifizierter molekularer Siebe |
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