CA2211043C - Hydrocarbon treatment and catalyst therefor - Google Patents
Hydrocarbon treatment and catalyst therefor Download PDFInfo
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- CA2211043C CA2211043C CA002211043A CA2211043A CA2211043C CA 2211043 C CA2211043 C CA 2211043C CA 002211043 A CA002211043 A CA 002211043A CA 2211043 A CA2211043 A CA 2211043A CA 2211043 C CA2211043 C CA 2211043C
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- Prior art keywords
- molecular sieve
- silicon
- core
- olefin
- surface layer
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Links
- 239000003054 catalyst Substances 0.000 title claims description 26
- 150000002430 hydrocarbons Chemical class 0.000 title description 10
- 229930195733 hydrocarbon Natural products 0.000 title description 8
- 239000004215 Carbon black (E152) Substances 0.000 title description 4
- 239000002808 molecular sieve Substances 0.000 claims abstract description 33
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 33
- 150000001336 alkenes Chemical class 0.000 claims abstract description 28
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000010457 zeolite Substances 0.000 claims abstract description 23
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 21
- 238000006384 oligomerization reaction Methods 0.000 claims abstract description 20
- 239000000203 mixture Substances 0.000 claims description 36
- 230000015572 biosynthetic process Effects 0.000 claims description 31
- 238000000034 method Methods 0.000 claims description 30
- 238000003786 synthesis reaction Methods 0.000 claims description 29
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 26
- 229910052710 silicon Inorganic materials 0.000 claims description 23
- 239000010703 silicon Substances 0.000 claims description 23
- 239000013078 crystal Substances 0.000 claims description 18
- 239000004411 aluminium Substances 0.000 claims description 17
- 229910052782 aluminium Inorganic materials 0.000 claims description 17
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 17
- 239000002344 surface layer Substances 0.000 claims description 16
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 claims description 14
- 229910052733 gallium Inorganic materials 0.000 claims description 14
- 229910052742 iron Inorganic materials 0.000 claims description 13
- 239000010410 layer Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 125000004432 carbon atom Chemical group C* 0.000 claims description 7
- 238000002425 crystallisation Methods 0.000 claims description 7
- 230000008025 crystallization Effects 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 4
- 150000001767 cationic compounds Chemical class 0.000 claims description 2
- 229910001411 inorganic cation Inorganic materials 0.000 claims description 2
- 239000011162 core material Substances 0.000 description 28
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 25
- 229910001868 water Inorganic materials 0.000 description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- 239000000243 solution Substances 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000002253 acid Substances 0.000 description 10
- -1 ammonium ions Chemical class 0.000 description 7
- 238000001354 calcination Methods 0.000 description 7
- NAQMVNRVTILPCV-UHFFFAOYSA-N hexane-1,6-diamine Chemical compound NCCCCCCN NAQMVNRVTILPCV-UHFFFAOYSA-N 0.000 description 7
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 5
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000000843 powder Substances 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical group CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000011230 binding agent Substances 0.000 description 3
- 239000008119 colloidal silica Substances 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 3
- 150000002500 ions Chemical group 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000002441 X-ray diffraction Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 235000013844 butane Nutrition 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 2
- 239000000539 dimer Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical group CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- OIDIRWZVUWCCCO-UHFFFAOYSA-N 1-ethylpyridin-1-ium Chemical compound CC[N+]1=CC=CC=C1 OIDIRWZVUWCCCO-UHFFFAOYSA-N 0.000 description 1
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 description 1
- VILCJCGEZXAXTO-UHFFFAOYSA-N 2,2,2-tetramine Chemical compound NCCNCCNCCN VILCJCGEZXAXTO-UHFFFAOYSA-N 0.000 description 1
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- TYSIILFJZXHVPU-UHFFFAOYSA-N 5-methylnonane Chemical compound CCCCC(C)CCCC TYSIILFJZXHVPU-UHFFFAOYSA-N 0.000 description 1
- 229910002012 Aerosil® Inorganic materials 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical compound NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- OFOBLEOULBTSOW-UHFFFAOYSA-N Malonic acid Chemical compound OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 159000000013 aluminium salts Chemical class 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 229910000329 aluminium sulfate Inorganic materials 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- HOPRXXXSABQWAV-UHFFFAOYSA-N anhydrous collidine Natural products CC1=CC=NC(C)=C1C HOPRXXXSABQWAV-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 150000004982 aromatic amines Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- JBANFLSTOJPTFW-UHFFFAOYSA-N azane;boron Chemical compound [B].N JBANFLSTOJPTFW-UHFFFAOYSA-N 0.000 description 1
- HQABUPZFAYXKJW-UHFFFAOYSA-N butan-1-amine Chemical compound CCCCN HQABUPZFAYXKJW-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 229910052792 caesium Inorganic materials 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- UTBIMNXEDGNJFE-UHFFFAOYSA-N collidine Natural products CC1=CC=C(C)C(C)=N1 UTBIMNXEDGNJFE-UHFFFAOYSA-N 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- HPNMFZURTQLUMO-UHFFFAOYSA-N diethylamine Chemical compound CCNCC HPNMFZURTQLUMO-UHFFFAOYSA-N 0.000 description 1
- 238000006471 dimerization reaction Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000007037 hydroformylation reaction Methods 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 239000003701 inert diluent Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(III) nitrate Inorganic materials [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000003606 oligomerizing effect Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 125000004817 pentamethylene group Chemical class [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000008707 rearrangement Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- GFYHSKONPJXCDE-UHFFFAOYSA-N sym-collidine Natural products CC1=CN=C(C)C(C)=C1 GFYHSKONPJXCDE-UHFFFAOYSA-N 0.000 description 1
- FAGUFWYHJQFNRV-UHFFFAOYSA-N tetraethylenepentamine Chemical compound NCCNCCNCCNCCN FAGUFWYHJQFNRV-UHFFFAOYSA-N 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 229960001124 trientine Drugs 0.000 description 1
- 230000004580 weight loss Effects 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
- C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
- C07C2/08—Catalytic processes
- C07C2/12—Catalytic processes with crystalline alumino-silicates or with catalysts comprising molecular sieves
-
- 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
-
- 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
-
- 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
-
- B01J35/19—
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
-
- 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
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
-
- 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
- C07C2529/80—Mixtures of different zeolites
Abstract
A crystalline molecular sieve, especially a zeolite, each crystallite having a core and an outer layer of the same structure, the Si:Al molar ratio in the core being greater than that in the outer layer, gives lower branching in olefin oligomerization products.
Description
"Hydrocarbon Treatment and Catalyst Therefor"
This invention relates to the treatment of hydro-carbons, especially olefinic hydrocarbons, to effect oligomerization, and to catalysts for use in such treatment.
Olefinic hydrocarbons are employed as starting materials in the hydroformylation, or oxo, process, for the eventual manufacture of numerous valuable products, e.g., alcohols, esters and ethers derived therefrom, aldehydes, and acids. In many of these end uses, linear or lightly branched hydrocarbon chains have advantages compared with more heavily branched chains.
In the oxo process itself, moreover, olefins with heavily branched chains are less reactive than those with linear or lightly branched structures and, for a given degree of branching, certain isomers are less reactive than others.
Olefinic feedstocks, especially in the C4.to C20, and more particularly in the C~ to C15 range, are frequently produced by oligomerization of lower molecular weight original starting materials, a process that, because of rearrangements that take p1_ace during the reaction, may produce an undesirably high proportion of multiply branched olefins, even if the original materials are linear. Also, the locations of the branches, at sites close to each other on the hydrocarbon chain, or in the central region of the chain, or both, resulting from , the oligomerization further reduce the reactivity of the molecules in the oxo reaction.
There are other areas in which a less highly branched hydrocarbon has advantages; these include the alkylation of aromatic hydrocarbons by reaction with olefins in the manufacture of surfactants and polyolefin stabilizers.
There is accordingly a need to provide a method to produce an olefin oligoner having a reduced degree of branching of a hydrocarbon material.
U.S. Patent No. 5,234,939 (Apelian, et al, assigned to Mobil Oil Corporation) describes the use of a medium pore size shape-selective acid crystalline zeolite in the catalytic oligomerization of olefinic hydrocarbons, and discusses the factors influencing the linearity or degree of branching of the products. Acid activity at the zeolite particle surface is said to favour the production of branched products, and reference is made to de-alumination of zeolite surfaces to reduce surface acidity, or the ratio of surface acidity to intracrystalline acid site activity. Other reduction methods mentioned in an extensive prior art review in the patent include the use of bulky amines to inactivate acid ' sites; the invention to which the patent is directed is the use of a dicarboxylic acid to inactivate the surface acid sites.
In U.S. Patent No. 5,250,484 (Beck et al., also assigned to Mobil), surface acidity is reduced by contacting the catalyst with an ammonia-borane solution and calcining to form an inactive ceramic layer on the surface. In U.S. Patent No. 4,788,374 (Chu et al;., also assigned to Mobil), surface acidity is reduced by forming a silica shell on a metallosilicate core by crystallizing silica on the surface of the core in the presence of fluoride.
The present invention provides a process for the oligomerization of an olefin, which comprises contacting under oligomerization conditions a feed comprising at least one olefin with an olefin oligomerization catalyst comprising a particulate molecular sieve, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon: selected element ratio than that of the core.
The invention also provides a particulate molecular sieve, capable of catalysing olefin oligomerization, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon:selected element ratio than that of the core.
The invention further provides the use of a particulate molecular sieve, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon:selected element ratio than that of the core, as an olefin oligomerization catalyst to reduce the degree of branching of the oligcmer product. , The invention still further provides a process for the manufacture of a particulate molecular sieve, which comprises heating an aqueous synthesis mixture comprising a source of silicon, a source of an element selected from aluminium, gallium and iron, a source of monovalent inorganic cations, and, if desired or required, an organic structure directing agent, the synthesis mixture having dispersed therein crystals of a molecular sieve containing silicon and an element selected from aluminium, gallium, and iron, the molar ratio of silicon to selected element i.n the crystals being lower than the molar ratio of :~ilico~n to selected element in their respective sources in the synthesis mixture, to cause crystallization of a molecular sieve layer from the synthesis mixture onto the surfaces of the crystals.
In each of the above-mentioned aspects of the invention, the selected element is advantageously aluminium. The elements selected for the core and for the outer layer are advantageously, but not necessarily, the same. For example, a gallium-containing outer layer may surround an aluminiu~:~-containing core.
Advantageously, t:he resulting crystalline product is ion exchanged with ammonium ions or protons, and calcined to yield the acid form of the molecular sieve.
Advantageously, calcination takes place at a temperature of at most 600°C,. preferably at most 500°C.
Certain features of the process for the manufacture of the molecular sieve of the present invention are shared with processes ,known in the art as commonly practised or as described in the literature.
These may be described briefly, as follows: .
This invention relates to the treatment of hydro-carbons, especially olefinic hydrocarbons, to effect oligomerization, and to catalysts for use in such treatment.
Olefinic hydrocarbons are employed as starting materials in the hydroformylation, or oxo, process, for the eventual manufacture of numerous valuable products, e.g., alcohols, esters and ethers derived therefrom, aldehydes, and acids. In many of these end uses, linear or lightly branched hydrocarbon chains have advantages compared with more heavily branched chains.
In the oxo process itself, moreover, olefins with heavily branched chains are less reactive than those with linear or lightly branched structures and, for a given degree of branching, certain isomers are less reactive than others.
Olefinic feedstocks, especially in the C4.to C20, and more particularly in the C~ to C15 range, are frequently produced by oligomerization of lower molecular weight original starting materials, a process that, because of rearrangements that take p1_ace during the reaction, may produce an undesirably high proportion of multiply branched olefins, even if the original materials are linear. Also, the locations of the branches, at sites close to each other on the hydrocarbon chain, or in the central region of the chain, or both, resulting from , the oligomerization further reduce the reactivity of the molecules in the oxo reaction.
There are other areas in which a less highly branched hydrocarbon has advantages; these include the alkylation of aromatic hydrocarbons by reaction with olefins in the manufacture of surfactants and polyolefin stabilizers.
There is accordingly a need to provide a method to produce an olefin oligoner having a reduced degree of branching of a hydrocarbon material.
U.S. Patent No. 5,234,939 (Apelian, et al, assigned to Mobil Oil Corporation) describes the use of a medium pore size shape-selective acid crystalline zeolite in the catalytic oligomerization of olefinic hydrocarbons, and discusses the factors influencing the linearity or degree of branching of the products. Acid activity at the zeolite particle surface is said to favour the production of branched products, and reference is made to de-alumination of zeolite surfaces to reduce surface acidity, or the ratio of surface acidity to intracrystalline acid site activity. Other reduction methods mentioned in an extensive prior art review in the patent include the use of bulky amines to inactivate acid ' sites; the invention to which the patent is directed is the use of a dicarboxylic acid to inactivate the surface acid sites.
In U.S. Patent No. 5,250,484 (Beck et al., also assigned to Mobil), surface acidity is reduced by contacting the catalyst with an ammonia-borane solution and calcining to form an inactive ceramic layer on the surface. In U.S. Patent No. 4,788,374 (Chu et al;., also assigned to Mobil), surface acidity is reduced by forming a silica shell on a metallosilicate core by crystallizing silica on the surface of the core in the presence of fluoride.
The present invention provides a process for the oligomerization of an olefin, which comprises contacting under oligomerization conditions a feed comprising at least one olefin with an olefin oligomerization catalyst comprising a particulate molecular sieve, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon: selected element ratio than that of the core.
The invention also provides a particulate molecular sieve, capable of catalysing olefin oligomerization, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon:selected element ratio than that of the core.
The invention further provides the use of a particulate molecular sieve, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon:selected element ratio than that of the core, as an olefin oligomerization catalyst to reduce the degree of branching of the oligcmer product. , The invention still further provides a process for the manufacture of a particulate molecular sieve, which comprises heating an aqueous synthesis mixture comprising a source of silicon, a source of an element selected from aluminium, gallium and iron, a source of monovalent inorganic cations, and, if desired or required, an organic structure directing agent, the synthesis mixture having dispersed therein crystals of a molecular sieve containing silicon and an element selected from aluminium, gallium, and iron, the molar ratio of silicon to selected element i.n the crystals being lower than the molar ratio of :~ilico~n to selected element in their respective sources in the synthesis mixture, to cause crystallization of a molecular sieve layer from the synthesis mixture onto the surfaces of the crystals.
In each of the above-mentioned aspects of the invention, the selected element is advantageously aluminium. The elements selected for the core and for the outer layer are advantageously, but not necessarily, the same. For example, a gallium-containing outer layer may surround an aluminiu~:~-containing core.
Advantageously, t:he resulting crystalline product is ion exchanged with ammonium ions or protons, and calcined to yield the acid form of the molecular sieve.
Advantageously, calcination takes place at a temperature of at most 600°C,. preferably at most 500°C.
Certain features of the process for the manufacture of the molecular sieve of the present invention are shared with processes ,known in the art as commonly practised or as described in the literature.
These may be described briefly, as follows: .
A source of silica is required; this may be, for example, a colloidal silica suspension, e.g., one sold under the trade-mark Ludox, or may be a finely divided solid, e.g., one sold under the trade-mark Aerosil.
An appropriate source of aluminium may be an alumina introduced into the synthesis mixture as, e.g., A12o3.3H20 previously dissolved in alkali or an aluminium salt, e.g., A12(S04)3.18H20, dissolved in an alkali solution. An appropriate source of gallium is, e.g., Ga203, also dissolved in an alkali solution, while for iron Fe(N03)3 is preferred. In the following description, re:Eerence will be made only to aluminium for the sake of clarity.
The synthesis mi:rcture contains a source of a monovalent cation, fo:r example, an alkali metal, e.g., sodium, potassium or caesium, or a source of ar,,monium ions. This nay advantageously be provided in the form of a hydroxide, thereby providing an alkaline solution in which the alumina may be introduced.
The organic: strucaure directing agent if present directs the formation of a given molecular sieve by the so-called templating effect. The role of organic molecules in molecular- sieve synthesis is well-knocan and discussed in, for example, e.g. Lok et al, Zeolites 1933, Volume 3, pages 282 to 291 and Moretti et al, Chim. Ind.
(Milan) G7, No. 1 to 2, 21 to 34 (1985). The effect of an organic structure directing agent is that in the 7 PCTlEP96/00395 -production of the crystalline framework the organic compound acts as a template around which the crystalline framework grows, or which causes the crystallization to be directed to form a particular crystalline framework.
Preferred agents for the manufacture of ZSM-22 sieves are mono- and di-aminoalkanes having up to 12 carbon atoms, particularly 4, 6, 8, 10 or 12 carbon atoms, e.g. 1,6-diaminohexane (which is preferred), diethylamine, 1-aminobutane or 2,2'-diaminodiethylamine; arylamines containing up to 8 carbon atoms, heterocyclic organic compounds, e.g., as N-ethylpyridinium; poly-alkylenepolyamines, e.g. triethylene tetramine or tetraethylene pentamine, and alkanolamines, e.g.
ethanolamine or diethanolamine.
A preferred quantity of template R, based on the preferred template of 1,6-diaminohexane, is a molar ratio of R/Si02 in the synthesis mixture of 0.025 to 0.4.
The Si02/A1203 molar ratio in the synthesis mixture is generally at least 150:1, preferably at least 250:1, and may be as high as 1500:1. Ratios between 3.00:1 and 900:1, especially between 300:1 and 600:1, are especially preferred.
The Si02/A1203 molar ratio in the zeolite layer after crystallization may be up to 30% lower than the molar ratio in the synthesis mixture; this reduction may be taken into account in selecting the proportions of components in the synthesis mixture, to ensure the _ g _ required relationship between core and outer layer ratios. The Si02/A1203 molar ratio in the core crystals dispersed in the synthesis mixture is advantageously at most 120:1, is more advantageously in the range 40:1 to 120:1, and preferably in the range 60 to 100:1.
The proportions of reactants in the synthesis mixture are generally lower than in the normal synthesis mixture, i.e., in addition to the lower aluminium content, the synthesis mixture should be highly diluted, for example, with water. The synthesis mixture including the core material may contain, for example, up to 850, advantageously from 50 to 80% by weight, of diluent, especially water.
Advantageously, crystallization is effected at 120 to 180°C, preferably 140 to 170°C. The crystallization time may be from 10 to 72 hours, typically 15 to 48 hours.
After crystallization the zeolite may be washed with deionized water or with acidified water, and then, optionally after a drying or calcining-step, ion exchanged to yield the acidic form.
The zeolite is preferably exchanged with ammonium ions and subjected to conditions under which the ammonium ions decompose, with the formation of ammonia and a proton, thus producing the acidic form of the zeolite.
Alternatively the acid form may be obtained by acid exchange with, for ea:ample, hydrochloric acid.
_ g _ The exchange with ammonium ions may be carried out by any suitable method, for example, by treating the crystals with an aqueous solution of ammonium chloride, ammonium nitrate or ammonium hydroxide. Exchange with protons is advantageously carried out by contacting the crystals with a dilute acid solution, e.g., HC1.
After exchange with ammonium ions or protons, the crystals may be calcined, advantageously at a temperature of from 120° to 600°C, preferably from 150° to 500°C.
Suitable calcination 'times range from 1 hour to several days, the temperatures in the upper part of the specified temperature range corresponding to the shorter heating times and the temperatures in the lower part of the specified temperature range corresponding to the longer heating times.
Thus, for example, crystals may be calcined at a temperature of 400°C l:or from 1 to 20 hours. At a temperature of 120°C, longer calcination times of at least 2 days and preferably from 3 to 5 days will generally be necessary to achieve adequate voiding of the pores.
The sieve may be post-treated, as by steaming, or may be caused to contain other cations either by incorporation during preparation or by subsequent ion-exchange, examples of suitable cations being Ni, Cd, Cu, Zn, Pd, Ca, B and Ti.and rare earth metals.
Advantageously, the molecular sieve of the invention has a refined constraint index (as hereinafter defined) , greater than 2, and advantageously greater than 10.
The refined constraint index, CI°, is defined in J.A. Martens, M. Tielen, P.A. Jacobs and J. Weitkamp, Zeolites, 1984, p. 9E., and P.A. Jacobs & J.A. Martens, Pure and Applied Chem., 1986, Vol. 58, p. 1329, as the ratio of 2-meth:ylnonane to 5-methylnonane produced at 50 conversion in the hydro-isomerization of n-decane.
Examples o:E molecular sieves having a CI° between 2 and 10 include ZSM-5, 11, 12, 35, 38, 48, and 57, SAPO-11, MCM-22 and E~rionite, those having a CI° between 5 and presently being preferred. Examples of molecular sieves having a CI° g:reater than l0, and accordingly most preferred, include ZS1~I-22, ZSM-23, and certain ferrierites.
It is within the scope of the oligomerization process of the invention to employ mixtures containing two or more molecular sieves.
The molecular sieve or zeolite catalyst is advantageously ZSM-22, described in U.S. Patent No.
4556477 and in V.'O 93/254'75.
A molecular sieve: crystallite size advantageously up to 5 ~cm, prefera:bly within the range of from 0.05 to 5 ~cm, more especially from 0.05 to 2 Vim, and most preferably from 0. 1 to~ ~1.0 ~cm, may be employed.
The proportion by weight represented by the surface layer, based on the total weight of the molecular sieve of the invention, may, for example, be within the range of 5% to 20%, conveniently from 8% to 15%, after calcination.
The molecular sieve may be used in the form of granules, powder or other shaped form, e.g., an extrudate. The extrudate advantageously contains the molecular sieve, and a binder, for example alumina, silica, an aluminosilicate, or clay, advantageously in a proportion of from 10:90 to 90:10, preferably 20:80 to 80:20, by weight of sieve to binder. The sieve and binder may be composited by, for example, intimately mixing them together in the presence of water, and extruding or otherwise shaping, e.g., by pelletizing.
The feed olefin advantageously contains from 2 to 12 carbon atoms, and preferably from 2 to G carbon atoms;
more preferably, the olefin feed advantageously contains propene, butenes and/or pentenes.
Reaction conditions for the oligomerization process of the invention may be, with the exception of the use of the novel catalyst, in accordance with conditions operative for prior art processes oligomerizing the same olefin.
The olefin may, for example, be fed to the catalyst in admixture with an inert diluent, e.g., a saturated hydrocarbon, in the liquid or, preferably, the gaseous WO 96/24567 PCTlEP96/00395 phase. For a feed comprising propene, a suitable diluent is propane, advantageously in proportions of propene:propane from 90:10 to 10:90, preferably from 10:90 to 60:40, especially about 50:50 by weight.
Correspondingly, for a butene feed, a suitable diluent is butane, advantageously in proportions from 90:10 to 10:90, preferably from 75:25 to 50:50, especially about 2:1, by weight olefin: saturate. The feed is advantageously hydrated; preferably it contains from 0.05% to 2a by weight water. The desired proportion of water may be incorporated by saturating the feed at an appropriate temperature, e.g., from 25 to 60°C, or by injecting water through a pump.
The oligomerization may take place at a temperature advantageously in the range of from 160°C to 300°C, preferably from 170°C to 260°C, and most preferably from 180°C to 260°C, at a pressure advantageously in the range of from 5 to 10 MPa, preferably from 6 to 8 MPa, and at an olefin hourly space velocity advantageously in the range 0.1 to 20, preferably from 0.5 to 10, and most preferably 0.75 to 3.5, :ahsv.
In olefin oligomerizations employing a normal prior art catalyst, e.g., ZSI~i-22, it was found that with a r, decrease in conversion rate, selectivity to dimer, e.g., from butene to octene, increased but the degree of branching increased also. Using the catalyst of the present invention, however, it his surprisingly been R'O 96/24567 PCTIEP96/00395 found that, at lower conversion rates, the selectivity to - dimeris retained and is accompanied by a decrease in the degree of branching. Accordingly, oligomerization may be carried out at a lower conversion rate, unreacted monomer separated from oligomer, and recycled, resulting in a high dimer selectivity without loss of linearity in the product.
Further, the catalyst of the present invention has the additional advantage over the bulky-amine treated material of the prior art that it may readily be regenerated, as by calcining, without requiring a subsequent amine treatment. The catalyst of the present invention will moreover not differ on regeneration in its ability to oligomerize olefins to a less highly branched product from the catalyst of the invention as originally prepared.
The following examples, in which parts and percentages are by weight unless otherwise stated, illustrate the invention:
WO 96/24567 PCTlEP96/00395 Examples 1 to 3 Preparation of Catalyst Example 1 Preparation of synthesis mixture:
Solution A:
COMPONENT PARTS
H20 229.64 A12(S04)3 18H20 0.6538 NaOH (98.4%) 2.11 1,6-diaminohexane 12.85 The ingredients were dissolved in the ~~:ater in the order shown.
Solution B:
COMPONENT PARTS
Ludox AS-40 54.81 (Colloidal Silica) Solutions A and B were mixed for about 3 minutes, producing a smooth whitish gel (synthesis mixture).
Mixture C:
COMPONENT PARTS
ZSM-22 (H20 content 1.18%), 50.00 Si02/A1203 molar ratio 73:1 H20 50.09 Particle size of ZSM-22 < 1 um.
The components of Mixture C were mixed for 5 minutes, producing a very viscous paste. 72.54 parts of the synthesis mixture (Solutions A & B) were added and mixed for 15 minutes. An easily pourable and homogenous mass was obtained.
The molar composition of the final synthesis mixture (excluding the crystals) was:
2G.4 Na20/112.G R/A1203/372 Si02/2G580 H20 where R is 1,6-diaminohexane.
The mixture contained 28.70 preformed ZSM-22 crystals.
80.87 parts of the synthesis mixture were transferred to a stainless steel autoclave and heated to 160°C over a period of 2 hours, and kept at this temperature for 48 hours.
The product was filtered and washed three times with 500 parts water to pH 9.4 and subsequently dried at 125°C; 25.88 parts of dried product were recovered. The product after drying had an intense yellowish appearance, indicating that the core crystals were covered with a silica-rich ZSM-22 outer layer or shell. The weight ratio of the shell to core was calculated as follows:
Parts of synthesis mixture x Fraction preformed crystals (80.87 x 0.287) 23.21 Parts of Dried Product 25.88 Gain 2.67 Ratio shell/uncalcined core 2.67/23.21, i.e., 0.12 On the assumption that on calcination there is a shell weight loss of about 12%, the expected weight ratio of calcined shell to core is about 0.10:1.
X-ray diffraction (XRD) on the dried product showed a structure of ZSM-22 very slightly contaminated with crystobalite.
~xampla 2 Following the procedure of Example 1 a final synthesis mixture of molar composition 53.0 Na20/226 R/A1203/746 Si02/61045 H20 where R is 1,6-diaminohexane, was obtained, containing 29. 32 o preformed ZSI~I-22 crystals.
111.24 parts of the crystallite-containing synthesis mixture were transferred to a stainless steel autoclave, which was placed in an oven at room temperature. The oven was heated to 153°C over a period of 2 hours and maintained at that temperature for 24 hours.
WO 96124567 PCTlEP96/00395 The resulting crystalline product was repeatedly washed with water and dried at 125°C for 40 hours. 35.8 parts of dry product were recovered. By a calculation as described in Example 1, the weight ratio of uncalcined shell: core was found to be 0.10:1 and the expected calcined shell:core ratio was about 0.09:1. XRD showed a pure crystalline ZSM-22 structure.
Example 3 Preparation of synthesis mixture:
Solution A:
COMPONENT PARTS
A12(S04)3 18H20 0.2193 NaOH (98.4%) 2.10 1,6-diaminohexane 12.87 H20 175.00 The first three components were dissolved in the order shown in the 175 parts of water. 54.82 parts of colloidal silica (Ludox AS40) Solution B were placed in a mixer, solution A was poured over the mixer contents, and the vessel in which solution A was prepared was rinsed with 54.67 parts water, the rinse water then being poured into the mixer. The contents ~,aere then stirred for 3 minutes to provide Mixture C. To 40.46 parts of water were added 44.13 parts of Mixture C, the diluted material then being mixed with 35.02 parts of ZSM-22 crystals.
After mixing for 5 minutes a viscous but pourable mass D , resulted, with a molar composition of:
78.9 Na20/336 R/A1203/1112 Si02/85320 H20 R being 1,6-diaminohexane; with 29.0% dry weight content of ZSM-22 seeds.
110.05 parts of the mass D were transferred to a stainless steel autoclave, which was placed in an oven at room temperature. The oven was then heated to 150°C over 3 hours and maintained at that temperature for 24 hours.
After the separated crystalline product was washed three times to reach a pH (last wash water) of 9.4, it was dried overnight at 120°C, yielding 35.75 parts of dried product. Calculation as described in Example 1 showed a weight ratio of uncalcined shell:core of 0.12:1, and a predicted calcined shell: core of 0.10:1.
In each of Examples 1 to 3, the product ~~~as cation exchanged with a 0.5N NH4C1 solution, ~~~ashed, and calcined at 400°C for 16 hours.
Examples 4 and 5 and Comparative Examples A, B and C
Olefin Oliaomerization The following examples were carried out to illustrate the effectiveness of catalysts produced according to the invention in oligomerization of an olefin. In each case, the feed was a mixed butene feed, diluted with butanes, in proportions of approximately 65%
olefins and 35% saturates, saturated with water vapour at 40°C. Reactor temperature was maintained in the region of 205 to 235°C, increasing in each case with the number of days on stream. The reactor pressure was maintained at about 7 MPa.
Prior art catalysts used were (a) the ZSM-22 catalyst employed as core crystals in Examples 1 to 3 above (termed "Parent" in Tables 1 and 2 below), and (b) collidine treated ZSM-22; both catalysts (a) and (b) were formed into extrudates of 5 mm diameter; the catalysts according to the invention and catalyst (a) were used as powders. Table 1 shows the catalytic activity in terms of butene conversion at 205°C, 7 MPa and weight hourly space velocity of 1.3 g olefin/g catalyst/hour.
Table 1 Ex. No. Catalyst Conversion, Comp. A (a) Parent, powder 97.0 Comp. B (a) Parent, extrudate 80.3.
Comp. C (b) Collidine-Treated, g l extrudate .
Example 1, powder 91.3 Example 2, powder 84.9 R'O 96/24567 PCT/EP96I00395 Examples 6 to 13 and Comparative Examples D to H .
In these Examples, the catalysts of Examples 1 and 2 and of Comparison Examples B and C were used in butene dimerization and the degree of branching of the resulting octenes was compared. The feed and conditions used were as described above with reference to Examples 4 and 5 above, but feed rates and hence space velocities were varied to give different conversion rates. The results are summarized in Table 2 below.
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SUBSTITUTE SHEET (RULE 26~
An appropriate source of aluminium may be an alumina introduced into the synthesis mixture as, e.g., A12o3.3H20 previously dissolved in alkali or an aluminium salt, e.g., A12(S04)3.18H20, dissolved in an alkali solution. An appropriate source of gallium is, e.g., Ga203, also dissolved in an alkali solution, while for iron Fe(N03)3 is preferred. In the following description, re:Eerence will be made only to aluminium for the sake of clarity.
The synthesis mi:rcture contains a source of a monovalent cation, fo:r example, an alkali metal, e.g., sodium, potassium or caesium, or a source of ar,,monium ions. This nay advantageously be provided in the form of a hydroxide, thereby providing an alkaline solution in which the alumina may be introduced.
The organic: strucaure directing agent if present directs the formation of a given molecular sieve by the so-called templating effect. The role of organic molecules in molecular- sieve synthesis is well-knocan and discussed in, for example, e.g. Lok et al, Zeolites 1933, Volume 3, pages 282 to 291 and Moretti et al, Chim. Ind.
(Milan) G7, No. 1 to 2, 21 to 34 (1985). The effect of an organic structure directing agent is that in the 7 PCTlEP96/00395 -production of the crystalline framework the organic compound acts as a template around which the crystalline framework grows, or which causes the crystallization to be directed to form a particular crystalline framework.
Preferred agents for the manufacture of ZSM-22 sieves are mono- and di-aminoalkanes having up to 12 carbon atoms, particularly 4, 6, 8, 10 or 12 carbon atoms, e.g. 1,6-diaminohexane (which is preferred), diethylamine, 1-aminobutane or 2,2'-diaminodiethylamine; arylamines containing up to 8 carbon atoms, heterocyclic organic compounds, e.g., as N-ethylpyridinium; poly-alkylenepolyamines, e.g. triethylene tetramine or tetraethylene pentamine, and alkanolamines, e.g.
ethanolamine or diethanolamine.
A preferred quantity of template R, based on the preferred template of 1,6-diaminohexane, is a molar ratio of R/Si02 in the synthesis mixture of 0.025 to 0.4.
The Si02/A1203 molar ratio in the synthesis mixture is generally at least 150:1, preferably at least 250:1, and may be as high as 1500:1. Ratios between 3.00:1 and 900:1, especially between 300:1 and 600:1, are especially preferred.
The Si02/A1203 molar ratio in the zeolite layer after crystallization may be up to 30% lower than the molar ratio in the synthesis mixture; this reduction may be taken into account in selecting the proportions of components in the synthesis mixture, to ensure the _ g _ required relationship between core and outer layer ratios. The Si02/A1203 molar ratio in the core crystals dispersed in the synthesis mixture is advantageously at most 120:1, is more advantageously in the range 40:1 to 120:1, and preferably in the range 60 to 100:1.
The proportions of reactants in the synthesis mixture are generally lower than in the normal synthesis mixture, i.e., in addition to the lower aluminium content, the synthesis mixture should be highly diluted, for example, with water. The synthesis mixture including the core material may contain, for example, up to 850, advantageously from 50 to 80% by weight, of diluent, especially water.
Advantageously, crystallization is effected at 120 to 180°C, preferably 140 to 170°C. The crystallization time may be from 10 to 72 hours, typically 15 to 48 hours.
After crystallization the zeolite may be washed with deionized water or with acidified water, and then, optionally after a drying or calcining-step, ion exchanged to yield the acidic form.
The zeolite is preferably exchanged with ammonium ions and subjected to conditions under which the ammonium ions decompose, with the formation of ammonia and a proton, thus producing the acidic form of the zeolite.
Alternatively the acid form may be obtained by acid exchange with, for ea:ample, hydrochloric acid.
_ g _ The exchange with ammonium ions may be carried out by any suitable method, for example, by treating the crystals with an aqueous solution of ammonium chloride, ammonium nitrate or ammonium hydroxide. Exchange with protons is advantageously carried out by contacting the crystals with a dilute acid solution, e.g., HC1.
After exchange with ammonium ions or protons, the crystals may be calcined, advantageously at a temperature of from 120° to 600°C, preferably from 150° to 500°C.
Suitable calcination 'times range from 1 hour to several days, the temperatures in the upper part of the specified temperature range corresponding to the shorter heating times and the temperatures in the lower part of the specified temperature range corresponding to the longer heating times.
Thus, for example, crystals may be calcined at a temperature of 400°C l:or from 1 to 20 hours. At a temperature of 120°C, longer calcination times of at least 2 days and preferably from 3 to 5 days will generally be necessary to achieve adequate voiding of the pores.
The sieve may be post-treated, as by steaming, or may be caused to contain other cations either by incorporation during preparation or by subsequent ion-exchange, examples of suitable cations being Ni, Cd, Cu, Zn, Pd, Ca, B and Ti.and rare earth metals.
Advantageously, the molecular sieve of the invention has a refined constraint index (as hereinafter defined) , greater than 2, and advantageously greater than 10.
The refined constraint index, CI°, is defined in J.A. Martens, M. Tielen, P.A. Jacobs and J. Weitkamp, Zeolites, 1984, p. 9E., and P.A. Jacobs & J.A. Martens, Pure and Applied Chem., 1986, Vol. 58, p. 1329, as the ratio of 2-meth:ylnonane to 5-methylnonane produced at 50 conversion in the hydro-isomerization of n-decane.
Examples o:E molecular sieves having a CI° between 2 and 10 include ZSM-5, 11, 12, 35, 38, 48, and 57, SAPO-11, MCM-22 and E~rionite, those having a CI° between 5 and presently being preferred. Examples of molecular sieves having a CI° g:reater than l0, and accordingly most preferred, include ZS1~I-22, ZSM-23, and certain ferrierites.
It is within the scope of the oligomerization process of the invention to employ mixtures containing two or more molecular sieves.
The molecular sieve or zeolite catalyst is advantageously ZSM-22, described in U.S. Patent No.
4556477 and in V.'O 93/254'75.
A molecular sieve: crystallite size advantageously up to 5 ~cm, prefera:bly within the range of from 0.05 to 5 ~cm, more especially from 0.05 to 2 Vim, and most preferably from 0. 1 to~ ~1.0 ~cm, may be employed.
The proportion by weight represented by the surface layer, based on the total weight of the molecular sieve of the invention, may, for example, be within the range of 5% to 20%, conveniently from 8% to 15%, after calcination.
The molecular sieve may be used in the form of granules, powder or other shaped form, e.g., an extrudate. The extrudate advantageously contains the molecular sieve, and a binder, for example alumina, silica, an aluminosilicate, or clay, advantageously in a proportion of from 10:90 to 90:10, preferably 20:80 to 80:20, by weight of sieve to binder. The sieve and binder may be composited by, for example, intimately mixing them together in the presence of water, and extruding or otherwise shaping, e.g., by pelletizing.
The feed olefin advantageously contains from 2 to 12 carbon atoms, and preferably from 2 to G carbon atoms;
more preferably, the olefin feed advantageously contains propene, butenes and/or pentenes.
Reaction conditions for the oligomerization process of the invention may be, with the exception of the use of the novel catalyst, in accordance with conditions operative for prior art processes oligomerizing the same olefin.
The olefin may, for example, be fed to the catalyst in admixture with an inert diluent, e.g., a saturated hydrocarbon, in the liquid or, preferably, the gaseous WO 96/24567 PCTlEP96/00395 phase. For a feed comprising propene, a suitable diluent is propane, advantageously in proportions of propene:propane from 90:10 to 10:90, preferably from 10:90 to 60:40, especially about 50:50 by weight.
Correspondingly, for a butene feed, a suitable diluent is butane, advantageously in proportions from 90:10 to 10:90, preferably from 75:25 to 50:50, especially about 2:1, by weight olefin: saturate. The feed is advantageously hydrated; preferably it contains from 0.05% to 2a by weight water. The desired proportion of water may be incorporated by saturating the feed at an appropriate temperature, e.g., from 25 to 60°C, or by injecting water through a pump.
The oligomerization may take place at a temperature advantageously in the range of from 160°C to 300°C, preferably from 170°C to 260°C, and most preferably from 180°C to 260°C, at a pressure advantageously in the range of from 5 to 10 MPa, preferably from 6 to 8 MPa, and at an olefin hourly space velocity advantageously in the range 0.1 to 20, preferably from 0.5 to 10, and most preferably 0.75 to 3.5, :ahsv.
In olefin oligomerizations employing a normal prior art catalyst, e.g., ZSI~i-22, it was found that with a r, decrease in conversion rate, selectivity to dimer, e.g., from butene to octene, increased but the degree of branching increased also. Using the catalyst of the present invention, however, it his surprisingly been R'O 96/24567 PCTIEP96/00395 found that, at lower conversion rates, the selectivity to - dimeris retained and is accompanied by a decrease in the degree of branching. Accordingly, oligomerization may be carried out at a lower conversion rate, unreacted monomer separated from oligomer, and recycled, resulting in a high dimer selectivity without loss of linearity in the product.
Further, the catalyst of the present invention has the additional advantage over the bulky-amine treated material of the prior art that it may readily be regenerated, as by calcining, without requiring a subsequent amine treatment. The catalyst of the present invention will moreover not differ on regeneration in its ability to oligomerize olefins to a less highly branched product from the catalyst of the invention as originally prepared.
The following examples, in which parts and percentages are by weight unless otherwise stated, illustrate the invention:
WO 96/24567 PCTlEP96/00395 Examples 1 to 3 Preparation of Catalyst Example 1 Preparation of synthesis mixture:
Solution A:
COMPONENT PARTS
H20 229.64 A12(S04)3 18H20 0.6538 NaOH (98.4%) 2.11 1,6-diaminohexane 12.85 The ingredients were dissolved in the ~~:ater in the order shown.
Solution B:
COMPONENT PARTS
Ludox AS-40 54.81 (Colloidal Silica) Solutions A and B were mixed for about 3 minutes, producing a smooth whitish gel (synthesis mixture).
Mixture C:
COMPONENT PARTS
ZSM-22 (H20 content 1.18%), 50.00 Si02/A1203 molar ratio 73:1 H20 50.09 Particle size of ZSM-22 < 1 um.
The components of Mixture C were mixed for 5 minutes, producing a very viscous paste. 72.54 parts of the synthesis mixture (Solutions A & B) were added and mixed for 15 minutes. An easily pourable and homogenous mass was obtained.
The molar composition of the final synthesis mixture (excluding the crystals) was:
2G.4 Na20/112.G R/A1203/372 Si02/2G580 H20 where R is 1,6-diaminohexane.
The mixture contained 28.70 preformed ZSM-22 crystals.
80.87 parts of the synthesis mixture were transferred to a stainless steel autoclave and heated to 160°C over a period of 2 hours, and kept at this temperature for 48 hours.
The product was filtered and washed three times with 500 parts water to pH 9.4 and subsequently dried at 125°C; 25.88 parts of dried product were recovered. The product after drying had an intense yellowish appearance, indicating that the core crystals were covered with a silica-rich ZSM-22 outer layer or shell. The weight ratio of the shell to core was calculated as follows:
Parts of synthesis mixture x Fraction preformed crystals (80.87 x 0.287) 23.21 Parts of Dried Product 25.88 Gain 2.67 Ratio shell/uncalcined core 2.67/23.21, i.e., 0.12 On the assumption that on calcination there is a shell weight loss of about 12%, the expected weight ratio of calcined shell to core is about 0.10:1.
X-ray diffraction (XRD) on the dried product showed a structure of ZSM-22 very slightly contaminated with crystobalite.
~xampla 2 Following the procedure of Example 1 a final synthesis mixture of molar composition 53.0 Na20/226 R/A1203/746 Si02/61045 H20 where R is 1,6-diaminohexane, was obtained, containing 29. 32 o preformed ZSI~I-22 crystals.
111.24 parts of the crystallite-containing synthesis mixture were transferred to a stainless steel autoclave, which was placed in an oven at room temperature. The oven was heated to 153°C over a period of 2 hours and maintained at that temperature for 24 hours.
WO 96124567 PCTlEP96/00395 The resulting crystalline product was repeatedly washed with water and dried at 125°C for 40 hours. 35.8 parts of dry product were recovered. By a calculation as described in Example 1, the weight ratio of uncalcined shell: core was found to be 0.10:1 and the expected calcined shell:core ratio was about 0.09:1. XRD showed a pure crystalline ZSM-22 structure.
Example 3 Preparation of synthesis mixture:
Solution A:
COMPONENT PARTS
A12(S04)3 18H20 0.2193 NaOH (98.4%) 2.10 1,6-diaminohexane 12.87 H20 175.00 The first three components were dissolved in the order shown in the 175 parts of water. 54.82 parts of colloidal silica (Ludox AS40) Solution B were placed in a mixer, solution A was poured over the mixer contents, and the vessel in which solution A was prepared was rinsed with 54.67 parts water, the rinse water then being poured into the mixer. The contents ~,aere then stirred for 3 minutes to provide Mixture C. To 40.46 parts of water were added 44.13 parts of Mixture C, the diluted material then being mixed with 35.02 parts of ZSM-22 crystals.
After mixing for 5 minutes a viscous but pourable mass D , resulted, with a molar composition of:
78.9 Na20/336 R/A1203/1112 Si02/85320 H20 R being 1,6-diaminohexane; with 29.0% dry weight content of ZSM-22 seeds.
110.05 parts of the mass D were transferred to a stainless steel autoclave, which was placed in an oven at room temperature. The oven was then heated to 150°C over 3 hours and maintained at that temperature for 24 hours.
After the separated crystalline product was washed three times to reach a pH (last wash water) of 9.4, it was dried overnight at 120°C, yielding 35.75 parts of dried product. Calculation as described in Example 1 showed a weight ratio of uncalcined shell:core of 0.12:1, and a predicted calcined shell: core of 0.10:1.
In each of Examples 1 to 3, the product ~~~as cation exchanged with a 0.5N NH4C1 solution, ~~~ashed, and calcined at 400°C for 16 hours.
Examples 4 and 5 and Comparative Examples A, B and C
Olefin Oliaomerization The following examples were carried out to illustrate the effectiveness of catalysts produced according to the invention in oligomerization of an olefin. In each case, the feed was a mixed butene feed, diluted with butanes, in proportions of approximately 65%
olefins and 35% saturates, saturated with water vapour at 40°C. Reactor temperature was maintained in the region of 205 to 235°C, increasing in each case with the number of days on stream. The reactor pressure was maintained at about 7 MPa.
Prior art catalysts used were (a) the ZSM-22 catalyst employed as core crystals in Examples 1 to 3 above (termed "Parent" in Tables 1 and 2 below), and (b) collidine treated ZSM-22; both catalysts (a) and (b) were formed into extrudates of 5 mm diameter; the catalysts according to the invention and catalyst (a) were used as powders. Table 1 shows the catalytic activity in terms of butene conversion at 205°C, 7 MPa and weight hourly space velocity of 1.3 g olefin/g catalyst/hour.
Table 1 Ex. No. Catalyst Conversion, Comp. A (a) Parent, powder 97.0 Comp. B (a) Parent, extrudate 80.3.
Comp. C (b) Collidine-Treated, g l extrudate .
Example 1, powder 91.3 Example 2, powder 84.9 R'O 96/24567 PCT/EP96I00395 Examples 6 to 13 and Comparative Examples D to H .
In these Examples, the catalysts of Examples 1 and 2 and of Comparison Examples B and C were used in butene dimerization and the degree of branching of the resulting octenes was compared. The feed and conditions used were as described above with reference to Examples 4 and 5 above, but feed rates and hence space velocities were varied to give different conversion rates. The results are summarized in Table 2 below.
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l0 tn In tf1C ri M M If7C M M M N
.~
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n O
U o m ~ 0 00 ~ ~ ~n N n r av o\
H Lf7 C M N O N N M N M N ~-1.-i to o\o N N M CO G1 C W N O O .-IG1 tl~CO
U O N G1 C M t!1(~ (~ U r1 tn O t~
N n (17 In C C' N M M C' C M M V' N
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f0 U ~ M N C C M l~ N ri ~-1O N V' .~..
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f0 O G1 N I~ V7 Ur C Lf1(~ b Vr N M
S-1 C M C C l~ L11lf~C C tf7tf1lf1V~
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w-i C M C lf1CO V~ tf1C' ~T lf1If7If1V' a o ..
.~, U7 c0 V~ N H tf7OW f) M C t~ ri tn O
~
~..1 0\0 C C O l~ M M GW i M N .-1',-1tn I~ N 01 G1 f~ n I~ G1 G~ (~ 00 G1 G1 Oa ~
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SUBSTITUTE SHEET (RULE 26~
Claims (18)
1. A particulate molecular sieve, each particle of the molecular sieve comprising a core having deposited thereon a surface layer, the core comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, and the surface layer comprising a zeolite containing silicon and at least one element selected from aluminium, gallium and iron, the zeolite of the surface layer being of the same crystalline structure as the core and having a higher silicon: selected element ratio than that of the core.
2. A process for the oligomerization of an olefin, which comprises contacting under oligomerization conditions a feed comprising at least one olefin with an olefin oligomerization catalyst comprising the particulate molecular sieve of claim 1.
3. A process as claimed in claim 2, wherein the silicon:selected element ratio of the core is at most 120:1.
4. A process as claimed in claim 3, wherein the silicon:selected element ratio of the core is in the range 60:1 to 100:1.
5 . A process as claimed in claim 2, 3 or 4, wherein the silicon:selected element ratio in the surface layer is at least 150:1.
6. A process as claimed in claim 5, wherein the silicon:selected element ratio in the surface layer is in the range 300:1 to 1500:1.
7. A process as claimed in any one of claims 2 to 6, wherein the molecular sieve has a Refined Constraint Index, CI°, of at least 2.
8. A process as claimed in claim 7, wherein the molecular sieve has a Refined Constraint Index, CI°, of at least 10.
9. A process as claimed in any one of claims 2 to 8, wherein the molecular sieve is ZSM-22.
10. A process as claimed in any one of claims 2 to 9, wherein the selected element is aluminium.
11. A process as claimed in any one of claims 2 to 10, wherein the proportion by weight of the crystallite represented by the surface layer is within the range of from 2% to 20%.
12. A process as claimed in any one of claims 2 to 11, wherein the crystallite size is at most 5 µm.
13. A process as claimed in claim 12, wherein the crystallite size is in the range of from 0.1 to 1.0 µm.
14. A process as claimed in any one of claims 2 to 13, wherein the olefin contains from 2 to 12 carbon atoms.
15. A process as claimed in claim 14, wherein the olefin contains from 2 to 6 carbon atoms.
16. A process as claimed in any one of claims 2 to 14, carried out at a temperature within the range of from 160°C to 300°C.
17. The use of the particulate molecular sieve of any one of claims 1 to 14 as an olefin oligomerization catalyst to reduce the degree of branching of the oligomer product.
18. A process for the manufacture of a particulate molecular sieve, which comprises heating an aqueous synthesis mixture comprising a source of silicon, a source of an element selected from aluminium, gallium and iron, a source of monovalent inorganic cations, and, if desired, an organic structure directing agent, the synthesis mixture having dispersed therein crystals of a molecular sieve containing silicon and an element selected from aluminium, gallium, and iron, the molar ratio of silicon to selected element in the crystals being lower than the molar ratio of silicon to selected element in their respective sources in the synthesis mixture, to cause crystallization of a molecular sieve layer from the synthesis mixture onto the surfaces of the crystals.
Applications Claiming Priority (3)
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GB9502342.0 | 1995-02-07 | ||
GBGB9502342.0A GB9502342D0 (en) | 1995-02-07 | 1995-02-07 | Hydrocarbon treatment and catalyst therefor |
PCT/EP1996/000395 WO1996024567A1 (en) | 1995-02-07 | 1996-01-29 | Hydrocarbon treatment and catalyst therefor |
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CA2211043A1 CA2211043A1 (en) | 1996-08-15 |
CA2211043C true CA2211043C (en) | 2001-03-20 |
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US (2) | US6013851A (en) |
EP (1) | EP0808298B1 (en) |
JP (1) | JP3937241B2 (en) |
KR (1) | KR100360734B1 (en) |
CN (2) | CN1072187C (en) |
AT (1) | ATE171155T1 (en) |
AU (1) | AU697790B2 (en) |
CA (1) | CA2211043C (en) |
DE (1) | DE69600667T2 (en) |
ES (1) | ES2122782T3 (en) |
GB (1) | GB9502342D0 (en) |
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ZA (1) | ZA96891B (en) |
Families Citing this family (61)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6504074B2 (en) | 1997-12-03 | 2003-01-07 | Exxonmobil Chemical Patents Inc. | Toluene disproportionation using coated zeolite catalyst |
US6177381B1 (en) | 1998-11-03 | 2001-01-23 | Uop Llc | Layered catalyst composition and processes for preparing and using the composition |
EP1276829A2 (en) | 2000-04-03 | 2003-01-22 | Chevron U.S.A. Inc. | Improved conversion of syngas to distillate fuels |
GB0010433D0 (en) * | 2000-04-28 | 2000-06-14 | Exxon Chemical Patents Inc | Alkene oligomerization process |
US7112711B2 (en) | 2000-04-28 | 2006-09-26 | Exxonmobil Chemical Patents Inc. | Alkene oligomerization process |
US6521198B2 (en) * | 2000-05-17 | 2003-02-18 | The Regents Of The University Of California | Metal surfaces coated with molecular sieve for corrosion resistance |
US6515033B2 (en) | 2001-05-11 | 2003-02-04 | Chevron U.S.A. Inc. | Methods for optimizing fischer-tropsch synthesis hydrocarbons in the distillate fuel range |
AU2003222120A1 (en) * | 2002-03-29 | 2003-10-13 | Exxonmobil Chemical Patents Inc. | Oxon process |
AU2003220593A1 (en) * | 2002-03-29 | 2003-10-13 | Exxonmobil Chemical Patents Inc. | Improved cobalt flash process |
EP1494983A1 (en) * | 2002-03-29 | 2005-01-12 | ExxonMobil Chemical Patents, Inc. a Corporation of the State of Delaware | Oligomerization of olefins |
DE60332819D1 (en) * | 2002-03-29 | 2010-07-15 | Exxonmobil Chem Patents Inc | PROCESS FOR OLEFIN OLIGOMERIZATION |
FR2843049B1 (en) * | 2002-08-01 | 2005-03-25 | Inst Francais Du Petrole | NON-HOMOGENEOUS ADSORBENT AND ITS USE IN DIFFUSIONS SEPARATION PROCESSES |
CN1894183B (en) | 2003-12-18 | 2010-09-08 | 埃克森美孚化学专利公司 | Improvements in or relating to hydrogenation |
US7405329B2 (en) | 2003-12-18 | 2008-07-29 | Exxonmobil Chemical Patents Inc. | Hydroformylation |
US20070255081A1 (en) * | 2003-12-18 | 2007-11-01 | Exxonmobil Chemical Company | Catalysed Reactions |
US7320782B1 (en) * | 2004-06-14 | 2008-01-22 | Uop Llc | Process for preparing a layered molecular sieve composition |
US7442365B1 (en) | 2004-06-14 | 2008-10-28 | Uop Llc | Process for preparing molecular sieve beads |
ES2439691T3 (en) * | 2004-07-16 | 2014-01-24 | Uop Llc | Procedure to synthesize molecular sieves |
GB0512377D0 (en) | 2005-06-17 | 2005-07-27 | Exxonmobil Chem Patents Inc | Oligomerisation of olefins with zeolite catalyst |
US9108181B2 (en) | 2007-06-20 | 2015-08-18 | Basf Corporation | Structurally enhanced cracking catalysts |
US8278235B2 (en) * | 2007-06-20 | 2012-10-02 | Basf Corporation | Structurally enhanced cracking catalysts |
EP2067528A1 (en) | 2007-11-29 | 2009-06-10 | Uop Llc | Process for preparing a layered molecular sieve composition |
JP2011505490A (en) | 2007-12-03 | 2011-02-24 | ジーヴォ,インコーポレイテッド | Renewable composition |
US8193402B2 (en) | 2007-12-03 | 2012-06-05 | Gevo, Inc. | Renewable compositions |
CN101314135B (en) * | 2008-06-27 | 2011-05-11 | 吉林大学 | Method for preparing double-catalysis center molecular sieve nucleocapsid material with hydrothermal/solvent-thermal system |
US8476350B2 (en) * | 2008-12-24 | 2013-07-02 | Exxonmobil Research And Engineering Company | Triglyceride plasticizer and process of making |
WO2011072992A1 (en) | 2009-12-15 | 2011-06-23 | Exxonmobil Chemical Patents Inc. | Temperature control of an oligomerisation process and reactor |
US8771815B2 (en) | 2009-12-17 | 2014-07-08 | Exxonmobil Research And Engineering Company | Process for making triglyceride plasticizer |
CA2786607A1 (en) | 2010-01-08 | 2011-07-14 | Gevo, Inc. | Integrated methods of preparing renewable chemicals |
EP2566830B1 (en) | 2010-05-07 | 2017-03-22 | GEVO, Inc. | Renewable jet fuel blendstock from isobutanol |
WO2012033562A1 (en) | 2010-09-07 | 2012-03-15 | Exxonmobil Chemical Patents Inc. | Extrudates including zeolite catalysts and their use in oligomerization processes |
WO2012145495A2 (en) | 2011-04-19 | 2012-10-26 | Gevo, Inc. | Variations on prins-like chemistry to produce 2,5-dimethylhexadiene from isobutanol |
WO2013013885A2 (en) | 2011-07-25 | 2013-01-31 | Exxonmobil Chemical Patents Inc. | Integrated nitrile poison adsorption and desorption system |
US9550705B2 (en) | 2011-07-25 | 2017-01-24 | Exxonmobill Chemical Patents Inc. | Olefin oligomerization process |
US9428427B2 (en) | 2011-07-25 | 2016-08-30 | Exxonmobil Chemical Patents Inc. | Process for nitrile removal from hydrocarbon feeds |
WO2013013887A2 (en) | 2011-07-25 | 2013-01-31 | Exxonmobil Chemical Patents Inc. | Olefin oligomerization process |
WO2013013888A2 (en) | 2011-07-25 | 2013-01-31 | Exxonmobil Chemical Patents Inc. | Olefin oligomerization process |
KR20130017165A (en) * | 2011-08-10 | 2013-02-20 | 서강대학교산학협력단 | Zeolite core/silica zeolite shell composites, method of prefaring the same and catalystic use the same |
PL2797854T3 (en) | 2011-12-30 | 2017-10-31 | K S Kali Gmbh | Composition of a magnesium sulphate urea compound |
AU2013207783B2 (en) | 2012-01-13 | 2017-07-13 | Lummus Technology Llc | Process for providing C2 hydrocarbons via oxidative coupling of methane and for separating hydrocarbon compounds |
US9969660B2 (en) | 2012-07-09 | 2018-05-15 | Siluria Technologies, Inc. | Natural gas processing and systems |
US9598328B2 (en) | 2012-12-07 | 2017-03-21 | Siluria Technologies, Inc. | Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products |
DE102012025141A1 (en) | 2012-12-21 | 2014-06-26 | K+S Aktiengesellschaft | Composition of a magnesium-urea compound |
WO2015081122A2 (en) | 2013-11-27 | 2015-06-04 | Siluria Technologies, Inc. | Reactors and systems for oxidative coupling of methane |
CA2935937A1 (en) | 2014-01-08 | 2015-07-16 | Siluria Technologies, Inc. | Ethylene-to-liquids systems and methods |
US10377682B2 (en) | 2014-01-09 | 2019-08-13 | Siluria Technologies, Inc. | Reactors and systems for oxidative coupling of methane |
CA2935946C (en) | 2014-01-09 | 2022-05-03 | Siluria Technologies, Inc. | Oxidative coupling of methane implementations for olefin production |
US9334204B1 (en) | 2015-03-17 | 2016-05-10 | Siluria Technologies, Inc. | Efficient oxidative coupling of methane processes and systems |
US10793490B2 (en) | 2015-03-17 | 2020-10-06 | Lummus Technology Llc | Oxidative coupling of methane methods and systems |
CN107406340A (en) | 2015-03-20 | 2017-11-28 | 埃克森美孚化学专利公司 | The hydrocarbon charging of olefin-containing is converted into oligomerization product or the method for hydrogenating oligomerization product |
US20160289143A1 (en) | 2015-04-01 | 2016-10-06 | Siluria Technologies, Inc. | Advanced oxidative coupling of methane |
US20160312134A1 (en) * | 2015-04-24 | 2016-10-27 | Uop Llc | Process for the production of jet-range hydrocarbons |
US9328297B1 (en) | 2015-06-16 | 2016-05-03 | Siluria Technologies, Inc. | Ethylene-to-liquids systems and methods |
EP3786138A1 (en) | 2015-10-16 | 2021-03-03 | Lummus Technology LLC | Oxidative coupling of methane |
WO2017180910A1 (en) | 2016-04-13 | 2017-10-19 | Siluria Technologies, Inc. | Oxidative coupling of methane for olefin production |
WO2018118105A1 (en) | 2016-12-19 | 2018-06-28 | Siluria Technologies, Inc. | Methods and systems for performing chemical separations |
DE102017104877A1 (en) | 2017-03-08 | 2018-09-13 | K+S Aktiengesellschaft | Magnesium sulfate granules based on synthetic magnesium sulfate |
DE102017104876A1 (en) | 2017-03-08 | 2018-09-13 | K+S Aktiengesellschaft | Use of magnesium sulfate granules |
JP2020521811A (en) | 2017-05-23 | 2020-07-27 | ラマス テクノロジー リミテッド ライアビリティ カンパニー | Integration of methane oxidation coupling process |
WO2019010498A1 (en) | 2017-07-07 | 2019-01-10 | Siluria Technologies, Inc. | Systems and methods for the oxidative coupling of methane |
CN109908944B (en) * | 2019-04-12 | 2020-09-15 | 西南化工研究设计院有限公司 | Catalyst for preparing nonene and dodecene by oligomerization of propylene and preparation method thereof |
Family Cites Families (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4203869A (en) * | 1976-09-24 | 1980-05-20 | Mobil Oil Corporation | ZSM-5 Containing aluminum-free shells on its surface |
US4394362A (en) * | 1981-04-28 | 1983-07-19 | Chevron Research Company | Crystalline silicate particle having an aluminum-containing outer shell |
EP0118632A1 (en) * | 1983-03-14 | 1984-09-19 | Mobil Oil Corporation | Crystalline materials and process for their manufacture |
US4975401A (en) | 1983-05-02 | 1990-12-04 | Mobil Oil Corporation | ZSM-5/ZSM-12 catalyst mixture for cracking alkylbenzenes |
US4575416A (en) | 1984-07-16 | 1986-03-11 | Mobil Oil Corporation | Hydrodewaxing with mixed zeolite catalysts |
FR2600557B1 (en) * | 1986-06-24 | 1993-03-19 | Elf France | BINARY ZEOLITIC SYSTEMS, THEIR SYNTHESIS AND THEIR USE |
AU613954B2 (en) | 1987-10-07 | 1991-08-15 | Mobil Oil Corporation | Olefin oligomerization |
US4788374A (en) * | 1987-12-23 | 1988-11-29 | Mobil Oil Corporation | Zeolite catalysis |
DE3914817C2 (en) | 1989-05-05 | 1995-09-07 | Huels Chemische Werke Ag | Process for oligomerizing olefins |
GB9114390D0 (en) | 1991-07-03 | 1991-08-21 | Shell Int Research | Hydrocarbon conversion process and catalyst composition |
JP2800499B2 (en) * | 1991-09-18 | 1998-09-21 | 日産自動車株式会社 | Hydrocarbon adsorbent |
US5250484A (en) | 1991-11-26 | 1993-10-05 | Mobil Oil Corporation | Surface modified porous acidic crystalline catalyst |
DE69318553T2 (en) | 1992-06-05 | 1998-12-10 | Exxon Chemical Patents Inc | ZSM 22 ZEOLITH |
US5284989A (en) | 1992-11-04 | 1994-02-08 | Mobil Oil Corporation | Olefin oligomerization with surface modified zeolite catalyst |
BR9406483A (en) * | 1993-04-23 | 1996-01-09 | Exxon Chemical Patents Inc | Layer and processes for preparing it to separate a fluid mixture and to catalyze a chemical reaction |
CN1066426C (en) * | 1994-02-22 | 2001-05-30 | 埃克森化学专利公司 | Oligomerization and catalyst therefor |
DE19619138C2 (en) * | 1996-05-11 | 2002-04-18 | Degussa | Process for the production of vinylated organic silicon compounds |
-
1995
- 1995-02-07 GB GBGB9502342.0A patent/GB9502342D0/en active Pending
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1996
- 1996-01-29 KR KR1019970705388A patent/KR100360734B1/en not_active IP Right Cessation
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- 1996-01-29 WO PCT/EP1996/000395 patent/WO1996024567A1/en active IP Right Grant
- 1996-01-29 CA CA002211043A patent/CA2211043C/en not_active Expired - Fee Related
- 1996-01-29 AT AT96901339T patent/ATE171155T1/en not_active IP Right Cessation
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- 1996-01-29 CN CN96191820A patent/CN1072187C/en not_active Expired - Fee Related
- 1996-01-29 JP JP52394896A patent/JP3937241B2/en not_active Expired - Fee Related
- 1996-01-29 US US08/875,749 patent/US6013851A/en not_active Expired - Lifetime
- 1996-01-29 AU AU45395/96A patent/AU697790B2/en not_active Ceased
- 1996-01-29 EP EP96901339A patent/EP0808298B1/en not_active Expired - Lifetime
- 1996-02-05 ZA ZA96891A patent/ZA96891B/en unknown
-
1999
- 1999-11-08 US US09/436,485 patent/US6300536B1/en not_active Expired - Fee Related
- 1999-11-30 CN CN99124400A patent/CN1277951A/en active Pending
Also Published As
Publication number | Publication date |
---|---|
EP0808298B1 (en) | 1998-09-16 |
CN1173858A (en) | 1998-02-18 |
DE69600667T2 (en) | 1999-04-08 |
US6013851A (en) | 2000-01-11 |
ES2122782T3 (en) | 1998-12-16 |
EP0808298A1 (en) | 1997-11-26 |
KR19980701991A (en) | 1998-06-25 |
ATE171155T1 (en) | 1998-10-15 |
GB9502342D0 (en) | 1995-03-29 |
JP3937241B2 (en) | 2007-06-27 |
AU697790B2 (en) | 1998-10-15 |
US6300536B1 (en) | 2001-10-09 |
CN1277951A (en) | 2000-12-27 |
ZA96891B (en) | 1996-07-16 |
JPH10513459A (en) | 1998-12-22 |
CA2211043A1 (en) | 1996-08-15 |
DE69600667D1 (en) | 1998-10-22 |
WO1996024567A1 (en) | 1996-08-15 |
AU4539596A (en) | 1996-08-27 |
KR100360734B1 (en) | 2003-02-07 |
CN1072187C (en) | 2001-10-03 |
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