WO2006136541A2 - Ru-katalysator und verfahren zur hydrierung von hydrierbare gruppen enthaltenden organischen verbindungen - Google Patents
Ru-katalysator und verfahren zur hydrierung von hydrierbare gruppen enthaltenden organischen verbindungen Download PDFInfo
- Publication number
- WO2006136541A2 WO2006136541A2 PCT/EP2006/063323 EP2006063323W WO2006136541A2 WO 2006136541 A2 WO2006136541 A2 WO 2006136541A2 EP 2006063323 W EP2006063323 W EP 2006063323W WO 2006136541 A2 WO2006136541 A2 WO 2006136541A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- hydrogenation
- substituted
- ruthenium
- alkyl
- Prior art date
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 278
- 238000000034 method Methods 0.000 title claims abstract description 89
- 150000002894 organic compounds Chemical class 0.000 title claims abstract description 23
- 229910052751 metal Inorganic materials 0.000 claims abstract description 106
- 239000002184 metal Substances 0.000 claims abstract description 106
- 229910052707 ruthenium Inorganic materials 0.000 claims abstract description 96
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims abstract description 55
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 23
- 239000012876 carrier material Substances 0.000 claims abstract description 21
- 125000001931 aliphatic group Chemical group 0.000 claims abstract description 16
- 125000002837 carbocyclic group Chemical group 0.000 claims abstract description 16
- 235000012239 silicon dioxide Nutrition 0.000 claims abstract description 15
- 150000001298 alcohols Chemical class 0.000 claims abstract description 12
- 150000001299 aldehydes Chemical class 0.000 claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 174
- 238000005984 hydrogenation reaction Methods 0.000 claims description 165
- -1 amino, hydroxy Chemical group 0.000 claims description 61
- 229910052739 hydrogen Inorganic materials 0.000 claims description 43
- 239000000463 material Substances 0.000 claims description 42
- 238000005470 impregnation Methods 0.000 claims description 37
- 230000008569 process Effects 0.000 claims description 35
- 125000003118 aryl group Chemical group 0.000 claims description 31
- 125000004432 carbon atom Chemical group C* 0.000 claims description 31
- 239000000203 mixture Substances 0.000 claims description 27
- OJLCQGGSMYKWEK-UHFFFAOYSA-K ruthenium(3+);triacetate Chemical compound [Ru+3].CC([O-])=O.CC([O-])=O.CC([O-])=O OJLCQGGSMYKWEK-UHFFFAOYSA-K 0.000 claims description 26
- HBGGXOJOCNVPFY-UHFFFAOYSA-N diisononyl phthalate Chemical compound CC(C)CCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCC(C)C HBGGXOJOCNVPFY-UHFFFAOYSA-N 0.000 claims description 22
- 150000002739 metals Chemical class 0.000 claims description 21
- 230000000737 periodic effect Effects 0.000 claims description 21
- 238000001035 drying Methods 0.000 claims description 20
- 230000035515 penetration Effects 0.000 claims description 20
- 150000003839 salts Chemical class 0.000 claims description 20
- 229910052717 sulfur Inorganic materials 0.000 claims description 20
- 125000000217 alkyl group Chemical group 0.000 claims description 19
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 17
- 239000011593 sulfur Substances 0.000 claims description 17
- 230000009467 reduction Effects 0.000 claims description 15
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 13
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 claims description 13
- NIQCNGHVCWTJSM-UHFFFAOYSA-N Dimethyl phthalate Chemical compound COC(=O)C1=CC=CC=C1C(=O)OC NIQCNGHVCWTJSM-UHFFFAOYSA-N 0.000 claims description 12
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 12
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 12
- 125000000392 cycloalkenyl group Chemical group 0.000 claims description 12
- 125000001072 heteroaryl group Chemical group 0.000 claims description 12
- 229910052799 carbon Inorganic materials 0.000 claims description 11
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 11
- 125000003545 alkoxy group Chemical group 0.000 claims description 10
- 229910052736 halogen Inorganic materials 0.000 claims description 10
- 150000002367 halogens Chemical class 0.000 claims description 10
- 125000005346 substituted cycloalkyl group Chemical group 0.000 claims description 10
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 claims description 9
- 229910001420 alkaline earth metal ion Inorganic materials 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 125000000547 substituted alkyl group Chemical group 0.000 claims description 9
- 125000003107 substituted aryl group Chemical group 0.000 claims description 9
- 125000003342 alkenyl group Chemical group 0.000 claims description 8
- 125000005842 heteroatom Chemical group 0.000 claims description 8
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims description 8
- 125000004104 aryloxy group Chemical group 0.000 claims description 7
- 238000004453 electron probe microanalysis Methods 0.000 claims description 7
- IGFHQQFPSIBGKE-UHFFFAOYSA-N 4-nonylphenol Chemical compound CCCCCCCCCC1=CC=C(O)C=C1 IGFHQQFPSIBGKE-UHFFFAOYSA-N 0.000 claims description 6
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims description 6
- 125000000304 alkynyl group Chemical group 0.000 claims description 6
- PXKLMJQFEQBVLD-UHFFFAOYSA-N bisphenol F Chemical compound C1=CC(O)=CC=C1CC1=CC=C(O)C=C1 PXKLMJQFEQBVLD-UHFFFAOYSA-N 0.000 claims description 6
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 6
- BJQHLKABXJIVAM-UHFFFAOYSA-N bis(2-ethylhexyl) phthalate Chemical compound CCCCC(CC)COC(=O)C1=CC=CC=C1C(=O)OCC(CC)CCCC BJQHLKABXJIVAM-UHFFFAOYSA-N 0.000 claims description 5
- FBSAITBEAPNWJG-UHFFFAOYSA-N dimethyl phthalate Natural products CC(=O)OC1=CC=CC=C1OC(C)=O FBSAITBEAPNWJG-UHFFFAOYSA-N 0.000 claims description 5
- 229960001826 dimethylphthalate Drugs 0.000 claims description 5
- 125000004404 heteroalkyl group Chemical group 0.000 claims description 5
- 238000004255 ion exchange chromatography Methods 0.000 claims description 5
- 125000001424 substituent group Chemical group 0.000 claims description 5
- 125000005017 substituted alkenyl group Chemical group 0.000 claims description 5
- 125000004426 substituted alkynyl group Chemical group 0.000 claims description 5
- 125000000446 sulfanediyl group Chemical group *S* 0.000 claims description 5
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 claims description 4
- 125000003368 amide group Chemical group 0.000 claims description 4
- 150000001448 anilines Chemical class 0.000 claims description 4
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 claims description 4
- 150000002016 disaccharides Chemical class 0.000 claims description 4
- 150000002772 monosaccharides Chemical class 0.000 claims description 4
- 150000002989 phenols Chemical class 0.000 claims description 4
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 4
- GEYOCULIXLDCMW-UHFFFAOYSA-N 1,2-phenylenediamine Chemical compound NC1=CC=CC=C1N GEYOCULIXLDCMW-UHFFFAOYSA-N 0.000 claims description 3
- KMKJEJNILQYGCU-UHFFFAOYSA-N 3-[(5-amino-2-methylphenyl)methyl]-4-methylaniline Chemical compound CC1=CC=C(N)C=C1CC1=CC(N)=CC=C1C KMKJEJNILQYGCU-UHFFFAOYSA-N 0.000 claims description 3
- YBRVSVVVWCFQMG-UHFFFAOYSA-N 4,4'-diaminodiphenylmethane Chemical compound C1=CC(N)=CC=C1CC1=CC=C(N)C=C1 YBRVSVVVWCFQMG-UHFFFAOYSA-N 0.000 claims description 3
- QHPQWRBYOIRBIT-UHFFFAOYSA-N 4-tert-butylphenol Chemical compound CC(C)(C)C1=CC=C(O)C=C1 QHPQWRBYOIRBIT-UHFFFAOYSA-N 0.000 claims description 3
- MQIUGAXCHLFZKX-UHFFFAOYSA-N Di-n-octyl phthalate Natural products CCCCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCCC MQIUGAXCHLFZKX-UHFFFAOYSA-N 0.000 claims description 3
- 150000004996 alkyl benzenes Chemical class 0.000 claims description 3
- 125000001797 benzyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])* 0.000 claims description 3
- 239000004305 biphenyl Substances 0.000 claims description 3
- 235000010290 biphenyl Nutrition 0.000 claims description 3
- 125000006267 biphenyl group Chemical group 0.000 claims description 3
- MTYUOIVEVPTXFX-UHFFFAOYSA-N bis(2-propylheptyl) benzene-1,2-dicarboxylate Chemical compound CCCCCC(CCC)COC(=O)C1=CC=CC=C1C(=O)OCC(CCC)CCCCC MTYUOIVEVPTXFX-UHFFFAOYSA-N 0.000 claims description 3
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 claims description 3
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 claims description 3
- 150000004820 halides Chemical class 0.000 claims description 3
- 125000001624 naphthyl group Chemical group 0.000 claims description 3
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N phenylbenzene Natural products C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 claims description 3
- 125000004076 pyridyl group Chemical group 0.000 claims description 3
- 230000007704 transition Effects 0.000 claims description 3
- QWUWMCYKGHVNAV-UHFFFAOYSA-N 1,2-dihydrostilbene Chemical group C=1C=CC=CC=1CCC1=CC=CC=C1 QWUWMCYKGHVNAV-UHFFFAOYSA-N 0.000 claims description 2
- 239000004803 Di-2ethylhexylphthalate Substances 0.000 claims description 2
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical class OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 claims description 2
- FVZVCSNXTFCBQU-UHFFFAOYSA-N phosphanyl Chemical group [PH2] FVZVCSNXTFCBQU-UHFFFAOYSA-N 0.000 claims description 2
- 150000005846 sugar alcohols Chemical class 0.000 claims description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims 2
- 239000000243 solution Substances 0.000 description 66
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 40
- 239000001257 hydrogen Substances 0.000 description 40
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 30
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 29
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
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- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 8
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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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
- B01J23/462—Ruthenium
-
- 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
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/08—Silica
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/656—Manganese, technetium or rhenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0205—Impregnation in several steps
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B35/00—Reactions without formation or introduction of functional groups containing hetero atoms, involving a change in the type of bonding between two carbon atoms already directly linked
-
- 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
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
- B01J35/615—100-500 m2/g
Definitions
- the present invention relates to a shell catalyst containing as active metal ruthenium alone or together with at least one further metal of the subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS version), applied to a support containing silicon dioxide as support material
- a process for the preparation of this coated catalyst a process for the hydrogenation of an organic compound containing hydrogenatable groups, preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic groups or for the hydrogenation of aldehydes to the corresponding alcohols, using the inventive coated catalyst and the use of the coated catalyst according to the invention for the hydrogenation of an organic compound containing hydrogenatable groups, preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic table en groups or for the hydrogenation of aldehydes to the corresponding alcohols.
- Cycloaliphatic alcohols in particular alkylcyclohexanols, are important intermediates for the preparation of various fragrances, pharmaceuticals and other organic fine chemicals.
- the hydrogenation products of benzene polycarboxylic acids or derivatives thereof to the corresponding cyclohexane polycarboxylic acids or derivatives thereof are used, for example, as plasticizers for plastics. Hydrogenation of benzene to cyclohexane is also of technical interest.
- Cycloaliphatic amines in particular optionally substituted cyclohexylamines and dicyclohexylamines, are used for the production of anti-theft agents for rubbers and plastics, as corrosion inhibitors and as precursors for crop protection agents and textile auxiliaries.
- Cycloaliphatic diamines are also used in the production of polyamide and polyurethane resins and continue to be used as hardeners for epoxy resins.
- the nuclear hydrogenation of aromatics has long been known and can be catalyzed by many metals, e.g. By supported catalysts containing nickel, cobalt or noble metals as active metals.
- ruthenium which contain aluminum oxide or silicon dioxides as support materials.
- DE-A 101 282 05 and DE-A 101 282 42 relate to ruthenium catalysts which are obtained by treating the support material one or more times on the basis of amorphous silicon dioxide with a halogen-free aqueous solution of a low-molecular-weight ruthenium compound and then drying the treated one Support material at a temperature below 200 ° C, followed by reduction of the resulting solid with hydrogen at a temperature in the range of 100 to 350 ° C, wherein the reduction takes place immediately after the treatment of the support material with an aqueous solution of a low molecular weight ruthenium compound , are available.
- these catalysts can be used for the hydrogenation of aromatic compounds to give the corresponding cycloaliphatic compounds.
- the catalysts disclosed in DE-A 101 282 05 and DE-A 101 282 42 have a ruthenium content of at least 0.1% by weight to 10% by weight.
- the ruthenium catalysts are prepared by impregnating silicon dioxide-containing support material with ruthenium (III) nitrosyl nitrate and have a ruthenium content of 5% by weight and 1% by weight, respectively.
- a disadvantage of the catalysts disclosed in DE-A 101 282 05 and DE-A 101 282 42 is the occurrence of side reactions in the hydrogenation of benzene to cyclohexane.
- cyclohexene can be formed because of hydrogen deficiency in the hydrogenation of benzene, and on the other hand because cyclohexane is dehydrogenated by the active metal ruthenium to give cyclohexene. It is believed that in catalysts containing ruthenium homogeneously distributed throughout the catalyst to weakly depleted in the core of the catalyst, due to the presence of ruthenium in the core of the catalyst and localized hydrogen limitation at the core of the catalyst Formation of cyclohexene is promoted, resulting in a decrease in activity during the hydrogenation of benzene to cyclohexane.
- Such a decrease in activity can be observed in the catalysts produced in DE-A 101 282 05 and DE-A 101 282 42 by impregnation of silica support material with a solution of ruthenium (III) nitrosyl nitrate.
- catalysts which, over a prolonged period, have a higher activity in the hydrogenation of organic compounds containing hydrogenatable groups, in particular in the hydrogenation of aromatic groups to the corresponding cycloaliphatic groups, than those described in DE-A 101 282 05 and US Pat DE-A 101 282 42 disclosed catalysts is therefore desirable.
- Suitable catalysts for achieving this object are coated catalysts, i. Catalysts which have a significantly higher concentration of active metal on the catalyst surface than in the catalyst core.
- Shell catalysts are known in the art and can be obtained by various methods.
- inorganic carrier materials can be impregnated with a metal salt solution of the catalytically active metal, followed by a drying and reduction step.
- a metal salt solution of the catalytically active metal such as. B. on the catalysts according to DE-A 101 282 05 and DE-A 101 282 42 recognizable is bar.
- shell catalysts can be prepared by chemical vapor deposition (CVD) processes.
- CVD chemical vapor deposition
- the carrier material is prepared with decomposable precursors vaporizable by the CVD method with subsequent fixation of the metals by simultaneous or subsequent thermal or chemical reduction.
- Allyl cyclopentadienylpalladium and trimethylphosphinic methylgold are used in particular as precursors.
- the process control of the CVD process is complicated because the vaporized metal precursor must be guided onto the catalyst carrier with the aid of a carrier gas.
- special Metallpreavesor are required because not all metal precursors show a suitable evaporation behavior.
- US 2004/0192792 A1 relates to shell catalysts wherein more than 60% by weight of the catalytically active metal is in an outer region of the catalyst, wherein this outer region has a thickness of not more than 200 ⁇ m.
- These catalysts are suitable for the production of synthesis gas from hydrocarbons (eg natural gas).
- hydrocarbons eg natural gas
- ruthenium as active metal is not mentioned in US 2004/0192792 A1.
- aluminum oxide supports are used.
- the hydrogenation of aromatics is likewise not mentioned in US 2004/0192792 A1.
- EP-A-0 094 684 relates to coated catalysts containing platinum or other noble metals substantially on the surface. These shell catalysts are prepared by impregnating a carrier with hexammonium platinum tetrasulfide. According to EP-A 0 094 684, SnO / ZnAl 2 O 4 supports are preferably used as supports. Silicon dioxide as a carrier material is not mentioned. These catalysts can be used according to EP-A 0 904 684 in numerous processes, including hydrogenation processes. The use of these catalysts in the dehydrogenation of alkanes is preferred.
- EP-A 1 420 012 discloses a process for the preparation of aliphatic isocyanates from aromatic isocyanates.
- the catalysts used are special catalysts which have ruthenium as active metal and have a meso / macroporous support material with a BET surface area in the range from> 30 m 2 / g to ⁇ 70 m 2 / g.
- catalysts based on alumina support materials are used, which are impregnated with ruthenium (III) nitrate solutions.
- shell catalysts are frequently obtained, they are distinguished by the presence of substantial amounts of active metal particles in the core.
- this presence of substantial amounts of active metal particles in the core adversely affects the activity of the catalyst in hydrogenation processes, particularly the long-term use activity as well as by-product formation in hydrogenation processes.
- the presence of substantial amounts of active metal particles in the core is disadvantageous in particular if the active metal particles in the core do not have sufficient hydrogen available, which may be the case, in particular in the case of rapid reactions in which hydrogen replenishment is limited.
- the object of the present application is therefore to provide catalysts which have a very high activity in hydrogenation processes even in long-term use, the amount of active metal being as low as possible, since precious metals are used as the active metal, which are expensive. Despite high activity and low amount of active metal byproduct formation should be low.
- the solution of this object is based on a coated catalyst containing ruthenium as an active metal alone or together with at least one further metal of the subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS version), applied to a support containing silicon dioxide as support material.
- the coated catalyst of the invention is then characterized in that the amount of the active metal ⁇ 1 wt .-%, preferably 0.1 to 0.5 wt .-%, particularly preferably 0.25 to 0.35 wt .-%, based to the total weight of the catalyst, and at least 60 wt .-%, particularly preferably 80 wt .-% of the active metal, based on the total amount of the active metal, present in the shell of the catalyst to a penetration depth of 200 microns.
- the abovementioned data are determined by means of scanning electron microscopy (EPMA) (electron probe microanalysis) - EDXS (energy dispersive X-ray spectroscopy) and represent averaged values. Further information relating to the abovementioned measuring methods and techniques is available on Example "Spectroscopy in Catalysis" by JW Niemantsverdriet, VCH, 1995.
- the coated catalyst according to the invention is characterized in that the predominant amount of the active metal in the shell is present up to a penetration depth of 200 ⁇ m, ie close to the surface of the shell catalyst. In contrast, there is no or only a very small amount of the active metal in the interior (core) of the catalyst. Surprisingly, it has been found that the catalyst according to the invention - despite the small amount of active metal - a very high activity in the hydrogenation of organic compounds containing hydrogenatable groups, especially in the hydrogenation of carbocyclic aromatic groups, with very good selectivities having. In particular, the activity of the catalyst according to the invention does not decrease over a long hydrogenation period.
- a coated catalyst according to the invention in which no active metal can be detected in the interior of the catalyst, ie active metal is present only in the outermost shell, for example in a zone up to a penetration depth of 100-200 ⁇ m.
- the shell catalyst according to the invention is distinguished in another particularly preferred embodiment in that in (FEG) -TEM (Field Emission Gun - Transmission Electron Microscopy) with EDXS only in the outermost 200 .mu.m, preferably 100 .mu.m, most preferably 50 .mu.m (penetration depth ) Active metal particles can be detected. Particles smaller than 1 nm can not be detected.
- ruthenium can be used alone or together with at least one further metal of subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS version).
- Other active metals suitable besides ruthenium are e.g. Platinum, rhodium, palladium, iridium, cobalt or nickel or a mixture of two or more thereof.
- the usable metals of subgroups IB and / or VIIB of the Periodic Table of the Elements are e.g. Copper and / or Rhenium suitable.
- Ruthenium is preferably used alone as an active metal or together with platinum or iridium in the shell catalysts of the invention; very particular preference is given to using ruthenium alone as active metal.
- the coated catalyst according to the invention exhibits the above-mentioned very high activity with a low loading of active metal, which is ⁇ 1 wt .-%, based on the total weight of the catalyst.
- the amount of active metal in the coated catalyst according to the invention is preferably from 0.1 to 0.5% by weight, more preferably from 0.25 to 0.35% by weight. It has been found that the penetration depth of the active metal into the carrier material is dependent on the loading of the catalyst with active metal.
- a loading of the catalyst with 1 wt .-% or more, e.g. at a loading of 1, 5 wt .-% is in the interior of the catalyst, i.
- the coated catalyst according to the invention at least 60% by weight of the active metal, based on the total amount of the active metal, is present in the shell of the catalyst up to a penetration depth of 200 ⁇ m.
- a shell catalyst according to the invention in which no active metal can be detected in the interior of the catalyst, ie active metal lies only in the outermost shell, for example in a zone up to a penetration depth of 100-200 ⁇ m, in front.
- the abovementioned data are determined by means of scanning electron microscopy (EPMA) (electron probe microanalysis) - EDXS (energy dispersive X-ray spectroscopy) and represent averaged values.
- EPMA scanning electron microscopy
- EDXS energy dispersive X-ray spectroscopy
- the amount of the active metal, based on the concentration ratio of active metal to Si, on the surface of the coated catalyst is 2 to 25%, preferably 4 to 10%, particularly preferably 4 to 6%, determined by means of SEM EPMA-EDXS ,
- the surface analysis is carried out by means of area analyzes of areas of 800 ⁇ m x 2000 ⁇ m and with an information depth of about 2 ⁇ m.
- the elemental composition is determined in% by weight (normalized to 100%).
- the mean concentration ratio (active metal / Si) is averaged over 10 measuring ranges.
- the surface of the coated catalyst is understood to mean the outer shell of the catalyst up to a penetration depth of approximately 2 ⁇ m. This penetration depth corresponds to the information depth in the above-mentioned surface analysis.
- a shell catalyst in which the amount of active metal, based on the weight ratio of active metal to Si (wt / wt.%), At the surface of the shell catalyst is 4 to 6%, in a penetration depth of 50 1.5 to 3% and in the range of 50 to 150 microns penetration 0.5 to 2%, determined by means of SEM EPMA (EDXS), is.
- the stated values represent averaged values.
- the size of the active metal particles preferably decreases with increasing penetration, as determined by (FEG) TEM analysis.
- the active metal is preferably partially or completely crystalline in the coated catalyst according to the invention.
- very finely crystalline active metal can be detected in the shell of the shell-type catalyst according to the invention by means of SAD (Selected Area Diffraction) or XRD (X-Ray Diffraction).
- the content of alkaline earth metal ion (s) (M 2+ ) in the catalyst is preferably from 0.01 to 1% by weight, in particular from 0.05 to 0.5% by weight, very particularly preferably from 0.1 to 0.25% by weight .-%, each based on the weight of the silica support material.
- An essential component of the catalysts according to the invention is the support material based on silicon dioxide, generally amorphous silicon dioxide.
- amorphous in this context means that the proportion of crystalline silicon dioxide phases makes up less than 10% by weight of the carrier material.
- the support materials used to prepare the catalysts may have superstructures that are formed by regular arrangement of pores in the Suma- material.
- Suitable support materials are in principle amorphous silicon dioxide types which consist of at least 90% by weight of silicon dioxide, the remaining 10% by weight, preferably not more than 5% by weight, of the support material also being one may be other oxidic material, for example MgO, CaO, TiO 2 , ZrO 2 , Fe 2 O 3 and / or alkali metal oxide.
- the support material is halogen-free, in particular chlorine-free, d. H.
- the content of halogen in the carrier material is less than 500 ppm by weight, e.g. in the range of 0 to 400 ppm by weight.
- Suitable amorphous silica-based support materials are known to those skilled in the art and are commercially available (see, for example, O.W. Flörke, "Silica” in Ullmann's Encyclopaedia of Industrial Chemistry 6th Edition on CD-ROM). They may have been either of natural origin or artificially produced. Examples of suitable amorphous support materials based on silica are silica gels, kieselguhr, fumed silicas and precipitated silicas. In a preferred embodiment of the invention, the catalysts comprise silica gels as support materials.
- the carrier material may have different shapes. If the process in which the coated catalysts according to the invention are used is designed as a suspension process, Production of the catalysts according to the invention usually use the carrier material in the form of a finely divided powder.
- the powder preferably has particle sizes in the range from 1 to 200 ⁇ m, in particular from 1 to 100 ⁇ m.
- shaped bodies from the support material which are obtainable, for example, by extrusion, extrusion or tableting and which, for example, take the form of spheres, tablets, cylinders, strands, rings or hollow cylinders, stars and the like.
- the dimensions of these moldings usually range from 0.5 mm to 25 mm.
- catalyst strands with strand diameters of 1, 0 to 5 mm and strand lengths of 2 to 25 mm are used. With smaller strands, generally, higher activities can be achieved; However, these often do not show sufficient mechanical stability in the hydrogenation process. Therefore, very particularly preferably strands with strand diameters in the range of 1, 5 to 3 mm are used.
- the preparation of the coated catalysts according to the invention is preferably carried out by first comprising the support material with a solution of ruthenium (III) acetate alone or together with a solution of at least one further salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS version) one or more soaks, the resulting solid is dried and then reduced, the solution of at least one further salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements in one or more common impregnation steps together with the solution of ruthenium (III) acetate or in one or more impregnation steps separately from the solution of ruthenium (III) acetate can be applied.
- the individual process steps are described in more detail below.
- a further subject of the present application is thus a process for preparing the shell catalyst according to the invention comprising the steps: a) one or more impregnation of the support material comprising silicon dioxide with a solution of ruthenium (III) acetate alone or together with a solution of at least one further salt of metals of transition groups IB, VIIB or VIII of the Periodic Table of the Elements (CAS version); b) subsequent drying; c) subsequent reduction; wherein the solution of the at least one further salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements in one or more impregnation steps together with the solution of ruthenium (III) acetate or in one or more impregnation steps separated from the solution of Ruthenium (III) acetate can be applied.
- Step a) one or more impregnation of the support material comprising silicon dioxide with a solution of ruthenium (III) acetate alone or together with a solution of at least one further salt of metals of
- step a) a single or multiple impregnation of the support material comprising silicon dioxide with a solution of ruthenium (III) acetate alone or together with at least one further dissolved salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS) Version). Since the amount of active metal in the coated catalyst according to the invention is very low, in a preferred embodiment, a simple impregnation takes place. Ruthenium (III) acetate or the salts of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements are active metal precursors.
- shell catalyst when ruthenium (III) acetate is used as precursor, shell catalyst Among other things, these are distinguished by the fact that the essential part of the active metal, preferably ruthenium alone, is in the shell catalyst up to a penetration depth of 200 ⁇ m. The interior of the shell catalyst has no or only little active metal.
- ruthenium (III) nitrosyl nitrate is used as a precursor, as disclosed in the examples in DE-A 101 28 205 and DE-A 101 28 242, a ruthenium catalyst is obtained which homogeneously distributes ruthenium over the catalyst to slightly depleted in the interior of the catalyst.
- Suitable solvents for providing the solution of ruthenium (III) acetate or the solution of at least one further salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements are water or else mixtures of water or solvent with up to 50 vol % of one or more organic solvents which are miscible with water or solvents, for example mixtures with C 1 -C 4 -alkanols, such as methanol, ethanol, n-propanol or isopropanol.
- Aqueous acetic or glacial acetic acid may also be used. All mixtures should be chosen so that there is a solution or phase.
- Preferred solvents are acetic acid, water or mixtures thereof.
- ruthenium (III) acetate is usually present dissolved in acetic acid or glacial acetic acid.
- ruthenium (III) acetate can also be used as a solid after dissolution.
- the catalyst according to the invention can also be prepared without the use of water.
- the solution of the at least one further salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements can be separated in one or more impregnation steps together with the solution of ruthenium (III) acetate or in one or more impregnation steps from the solution of ruthenium (US Pat. III) acetate.
- the impregnation can be carried out with a solution comprising ruthenium (III) acetate and at least one further salt of metals of subgroups IB, VIIB or VIII of the Periodic Table of the Elements.
- the impregnation with this solution can be done one or more times.
- Suitable salts of further metals of subgroups IB, VIIB or VIII of the periodic table of the elements which can be used in the impregnation step are e.g. Nitrates, acetonates and acetates, with acetates being preferred.
- the impregnation of the carrier material can take place in different ways and depends in a known manner on the shape of the carrier material. For example, one can spray or rinse the carrier material with the precursor solution or suspend the carrier material in the precursor solution. For example, it is possible to suspend the support material in an aqueous solution of the active metal precursor and to filter off the aqueous supernatant after a certain time.
- the active metal content of the catalyst can then be controlled in a simple manner via the amount of liquid taken up and the active metal concentration of the solution.
- the impregnation of the carrier material can also be carried out, for example, by treating the carrier with a defined amount of the solution of the active metal precursor, which corresponds to the maximum amount of liquid that can absorb the carrier material.
- Suitable apparatuses for this purpose are the apparatus commonly used for mixing liquids with solids (see Vauck / Müller, Basic Operations of Chemical Process Engineering, 10th Edition, German Publishing for Basic Industry, 1994, p. 405 et seq.), For example tumble dryers, trough drums , Drum mixer, paddle mixer and the like. Monolithic carriers are usually rinsed with the aqueous solutions of the active metal precursor.
- the solutions used for impregnating are preferably low in halogen, in particular low in chlorine, ie they contain no or less than 500 ppm by weight, in particular less than 100 ppm by weight of halogen, for example 0 to ⁇ 80 ppm by weight of halogen, based on the total weight of the solution.
- concentration of the active metal precursor in the solutions naturally depends on the amount of active metal precursor to be applied and the absorption capacity of the carrier material for the solution and is ⁇ 20% by weight, preferably 0.01 to 6% by weight, particularly preferably 0.1 to 1.1 wt .-%, based on the total mass of the solution used.
- the drying can be carried out according to the customary methods of drying solids while observing the upper temperature limits mentioned below.
- the observance of the upper limit of the drying temperatures is for the quality, i. the activity of the catalyst important. Exceeding the drying temperatures given below results in a significant loss of activity. Calcination of the support at higher temperatures, e.g. Above 300 ° C or even 400 ° C, as proposed in the prior art, is not only superfluous but also adversely affects the activity of the catalyst.
- the drying is preferably carried out at elevated temperature, preferably at ⁇ 180 ° C, especially at ⁇ 160 ° C, and at least 40 ° C, especially at least 70 ° C, especially at least 100 ° C, especially in Range from 110 ° C to 150 ° C.
- the drying of the solid impregnated with the active metal precursor is usually carried out under normal pressure, whereby a reduced pressure can also be used to promote drying.
- a gas stream will be passed over or through the material to be dried, e.g. Air or nitrogen.
- the drying time naturally depends on the desired degree of drying and the drying temperature and is preferably in the range of 1 h to 30 h, preferably in the range of 2 to 10 h.
- the drying of the treated support material is preferably carried out to such an extent that the content of water or of volatile solvent constituents prior to the subsequent reduction is less than 5% by weight, in particular not more than 2% by weight, based on the total weight of the solid.
- the stated proportions by weight in this case relate to the weight loss of the solid, determined at a temperature of 16O ° C., a pressure of 1 bar and a duration of 10 minutes. In this way, the activity of the catalysts used according to the invention can be further increased , Step c)
- the conversion of the solid obtained after drying into its catalytically active form is carried out by reducing the solid at temperatures in the range of generally from 150 ° C. to 450 ° C., preferably from 250 ° C. to 350 ° C., in a manner known per se.
- the carrier material is brought into contact with hydrogen or a mixture of hydrogen and an inert gas at the above-mentioned temperatures.
- the hydrogen absolute pressure is of subordinate importance for the result of the reduction and can be in the range of 0, for example. 2 bar to 1, 5 bar can be varied.
- the hydrogenation of the catalyst material takes place at normal hydrogen pressure in the hydrogen stream.
- the reduction is carried out by moving the solid, for example by reducing the solid in a rotary kiln or a rotary kiln. In this way, the activity of the catalysts according to the invention can be further increased.
- the hydrogen used is preferably free of catalyst poisons, such as CO- and S-containing compounds, eg H 2 S, COS and others.
- the reduction can also be carried out by means of organic reducing reagents such as hydrazine, formaldehyde, formates or acetates.
- the catalyst can be passivated in a known manner to improve the handling, for example by briefly mixing the catalyst with an oxygen-containing gas, for example air, but preferably with an inert gas mixture containing 1 to 10% by volume of oxygen , treated.
- an oxygen-containing gas for example air
- an inert gas mixture containing 1 to 10% by volume of oxygen
- CO 2 or CO 2 / O 2 mixtures can also be used here.
- the active catalyst may also be added under an inert organic solvent, e.g. Ethylene glycol, be kept.
- an inert organic solvent e.g. Ethylene glycol
- the active metal catalyst precursor e.g. as prepared above or prepared as described in WO-A2-02 / 100538 (BASF AG)
- the active metal catalyst precursor are impregnated with a solution of one or more alkaline earth metal (II) salts.
- Preferred alkaline earth metal (II) salts are corresponding nitrates, in particular magnesium nitrate and calcium nitrate.
- the preferred solvent for the alkaline earth metal (II) salts in this impregnation step is water.
- the concentration of the alkaline earth metal (II) salt in the solvent is, for example, 0.01 to 1 mol / liter.
- the active metal / SiO 2 catalyst incorporated in a pipe is contacted with a stream of an aqueous solution of the alkaline earth metal salt.
- the catalyst to be impregnated can also be treated with a supernatant solution of the alkaline earth metal salt.
- Such saturation of the active metal / SiO 2 catalyst, in particular its surface, preferably takes place with the alkaline earth metal ion (s).
- the catalyst according to the invention can be dried after the impregnation.
- the drying can be done e.g. in an oven at ⁇ 200 ° C, e.g. at 50 to 190 ° C, more preferably at ⁇ 140 ° C, z. B. at 60 to 130 ° C, are performed.
- This impregnation process can be carried out ex situ or in situ: Ex situ means prior to incorporation of the catalyst into the reactor, in situ means in the reactor (after catalyst installation).
- impregnation of the catalyst with alkaline earth metal ions can also be carried out in situ by dissolving the solution of the aromatic substrate (educt) to be hydrogenated with alkaline earth metal ions, e.g. in the form of dissolved alkaline earth metal salts.
- alkaline earth metal ions e.g. in the form of dissolved alkaline earth metal salts.
- the appropriate amount of salt is first dissolved in water and then added to the dissolved in an organic solvent substrate.
- the catalyst according to the invention is used in combination with an alkaline earth metal ion-containing solution of the substrate to be hydrogenated.
- the content of the solution of the substrate to be hydrogenated in alkaline earth metal ions is generally from 1 to 100 ppm by weight, in particular from 2 to 10 ppm by weight.
- the active metal is present in the catalysts according to the invention as metallic active metal.
- the halide content, in particular chloride content, of the inventive shell catalysts is also less than 0.05 wt .-% (0 to ⁇ 500 ppm by weight, eg Range of 0-400 ppm by weight), based on the total weight of the catalyst.
- the chloride content is e.g. determined by ion chromatography with the method described below.
- the percentage ratio of the Q 2 and Q 3 structures Q 2 / Q 3 determined by means of 29 Si solid-state NMR is less than 25, preferably less than 20, particularly preferably less than 15, eg is in the range of 0 to 14 or 0.1 to 13. This also means that the degree of condensation of the silica in the carrier used is particularly high.
- the support material preferably contains not more than 1% by weight and in particular not more than 0.5% by weight and in particular ⁇ 500 ppm by weight of aluminum oxide, calculated as Al 2 O 3 .
- the concentration of Al (III) and Fe (II and / or III) in total is preferably less than 300 ppm, particularly preferably less than 200 ppm, and is for example in the range from 0 to 180 ppm.
- the proportion of alkali metal oxide preferably results from the preparation of the carrier material and may be up to 2 wt .-%. Often it is less than 1 wt .-%. Also suitable are alkali metal oxide-free carrier (0 to ⁇ 0.1 wt .-%).
- the proportion of MgO, CaO, TiO 2 or ZrO 2 can be up to 10 wt .-% of the support material and is preferably not more than 5 wt .-%.
- carrier materials which contain no detectable amounts of these metal oxides (O to ⁇ 0.1% by weight) are also suitable.
- Another object of the present application is a shell catalyst produced by the method according to the invention. It has surprisingly been found that in the preparation of coated catalysts containing ruthenium alone or together with at least one further metal as active metal, the sub-groups IB, VIIB or VIII of the Periodic Table of the Elements (CAS version), deposited on a support containing silicon dioxide as the support material, a distribution of the active metal can be achieved, wherein the essential part of the active metal in the catalyst is present to a penetration depth of 200 microns and the interior of the catalyst has little or no active metal, if used as precursor in the impregnation step ruthenium (III) acetate is used.
- the shell catalyst according to the invention preferably contains ruthenium alone as the active metal. Preferred embodiments of catalysts which can be prepared by the process according to the invention are mentioned above.
- the coated catalyst according to the invention is preferably used as the hydrogenation catalyst. It is particularly suitable for the hydrogenation of organic compounds containing hydrogenatable groups.
- the hydrogenatable groups can be groups having the following structural units: C-C double bonds, C-C triple bonds, aromatic groups, C-N double bonds, C-N triple bonds, C-O double bonds, N-O double bonds, C-C double bonds fertilize, NO 2 groups, wherein the groups may also be contained in polymers or cyclic structures, for example in unsaturated heterocycles.
- the hydrogenatable groups may each be present individually or multiply in the organic compounds. men. It is also possible that the organic compounds are two or more
- the shell catalysts according to the invention are preferably used for hydrogenating a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group or for hydrogenating aldehydes to the corresponding alcohols, very particularly preferably for hydrogenating a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group.
- Particular preference is given to complete hydrogenation of the aromatic group, with complete hydrogenation giving a conversion of the compound to be hydrogenated of generally> 98%, preferably> 99%, more preferably> 99.5%, very particularly preferably> 99.9 %, in particular> 99.99% and especially> 99.995%.
- the coated catalyst according to the invention for the hydrogenation of benzene to cyclohexane thus the typical cyclohexane specifications that require a benzene residual content of ⁇ 100 ppm (equivalent to a benzene conversion of> 99.99%), complied.
- the benzene conversion in a hydrogenation of benzene with the shell catalyst of the invention > 99.995%.
- the typical specifications which require a residual content of the aromatic dicarboxylic acid ester, in particular phthalic acid ester residual content, of ⁇ 100 ppm are likewise required Turnover of> 99.99%).
- the conversion in a hydrogenation of aromatic dicarboxylic esters, in particular phthalic acid esters, with the coated catalyst according to the invention is preferably> 99.995%.
- a further subject of the present application is therefore a process for the hydrogenation of an organic compound containing hydrogenatable groups, preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group or for the hydrogenation of aldehydes to the corresponding alcohols, very particularly preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group, wherein the shell catalyst according to the invention is used.
- the carbocyclic aromatic group is preferably part of an aromatic hydrocarbon which has the following general formula: (A) - (B) n
- A is independently aryl or heteroaryl, A is preferably selected from among phenyl, diphenyl, benzyl, dibenzyl, naphthyl, anthracene, pyridyl and quinoline, A is particularly preferably phenyl; n is a number from 0 to 5, preferably 0 to 4, particularly preferably 0 to 3, in particular in the case when A is a 6-membered aryl or heteroaryl ring; in the case where A is a 5-membered aryl or heteroaryl ring, n is preferably 0 to 4; irrespective of the ring size n is more preferably 0 to 3, very particularly preferably 0 to 2 and in particular 0 to 1;
- the other carbon atoms or heteroatoms of A carrying no substituents B carry hydrogen atoms or, if appropriate, none
- B is independently selected from the group consisting of alkyl, alkenyl, alkynyl, substituted alkyl, substituted alkenyl, substituted alkynyl, heteroalkyl, substituted heteroalkyl, heteroalkenyl, substituted heteroalkenyl, heteroalkynyl, substituted heteroalkynyl, cycloalkyl, Cycloalkenyl, substituted cycloalkyl, substituted cycloalkenyl, COOR, wherein R is H, alkyl, substituted alkyl, cycloalkyl, substituted cycloalkyl, aryl or substituted aryl, halogen, hydroxy, alkoxy, aryloxy, carbonyl, amino, amido, thio and phosphino; preferably B is independent selected from Ci -6 alkyl, Ci -6 alkenyl, Ci -6 alkynyl,
- alkyl according to the present application is to be understood as meaning branched or linear, saturated acyclic hydrocarbon radicals.
- suitable alkyl radicals are methyl, ethyl, n-propyl, i-propyl, n-butyl, t-butyl, i-butyl, etc.
- R is H or branched or linear alkyl, preferably H or Preferred alkyl groups are C 4- i 0 alkyl groups,
- C 8- i 0 -alkyl groups are particularly preferably C 8- i 0 -alkyl groups. These may be branched or unbranched and are preferably branched.
- the alkyl groups having more than three carbon atoms may be mixtures of isomers of different alkyl groups having the same carbon number.
- One example is a C 9 -alkyl group, which may be an isononyl group, ie an isomer mixture of various C 9 -alkyl groups.
- Such isomer mixtures are obtained starting from the alcohols corresponding to the alkyl groups, which are obtained as isomer mixtures on the basis of their preparation process known to the person skilled in the art.
- Alkenyl according to the present application is to be understood as meaning branched or unbranched acyclic hydrocarbon radicals which have at least one carbon-carbon double bond. Suitable alkenyl radicals are, for example, 2-propenyl, vinyl, etc.
- the alkenyl radicals preferably have 2 to 50 carbon atoms, particularly preferably 2 to 20 carbon atoms, very particularly preferably 2 to 6 carbon atoms and in particular 2 to 3 carbon atoms.
- the term alkenyl is to be understood as meaning those radicals which have either an cis or a trans orientation (alternatively E or Z orientation).
- Alkynyl according to the present application is to be understood as meaning branched or unbranched acyclic hydrocarbon radicals which have at least one carbon-carbon triple bond.
- the alkynyl radicals preferably have 2 to 50 carbon atoms, particularly preferably 2 to 20 carbon atoms, very particularly preferably 1 to 6 carbon atoms and in particular 2 to 3 carbon atoms.
- Substituted alkyl, substituted alkenyl and substituted alkynyl are alkyl-alkenyl and alkynyl radicals in which one or more hydrogen atoms bound to one carbon atom of these radicals are replaced by another group.
- Examples of such other groups are heteroatoms, halogen, aryl, substituted aryl, cycloalkyl, cycloalkenyl, substituted cycloalkyl, substituted cycloalkenyl and combinations thereof.
- suitable substituted alkyl radicals are benzyl, trifluoromethyl and the like. a.
- heteroalkyl, heteroalkenyl and heteroalkynyl are meant alkyl-alkenyl and alkynyl radicals wherein one or more of the carbon atoms in the carbon chain are replaced by a heteroatom selected from N, O and S.
- the bond between the heteroatom and another carbon atom may be saturated or optionally unsaturated.
- Cycloalkyl according to the present application is to be understood as meaning saturated cyclic nonaromatic hydrocarbon radicals which are composed of a single ring or several condensed rings.
- Suitable cycloalkyl radicals are, for example, cyclopentyl, cyclohexyl, cyclooctanyl, bicyclooctyl, etc.
- the cycloalkyl radicals have between 3 and 50 carbon atoms, particularly preferably between 3 and 20 carbon atoms, very particularly preferably between 3 and 8 carbon atoms and in particular between 3 and 6 carbon atoms.
- cycloalkenyl By cycloalkenyl, according to the present application, partially unsaturated, cyclic non-aromatic hydrocarbon radicals are to be understood which have a single or multiple condensed rings. Suitable cycloalkenyl radicals are, for example, cyclopentenyl, cyclohexenyl, cyclooctenyl etc.
- the cycloalkenyl radicals preferably have 3 to 50 carbon atoms, particularly preferably 3 to 20 carbon atoms, very particularly preferably 3 to 8 carbon atoms and in particular 3 to 6 carbon atoms ,
- Substituted cycloalkyl and substituted cycloalkenyl radicals are cycloalkyl and cycloalkenyl radicals in which one or more hydrogen atoms of any carbon atom of the carbon ring are replaced by another group.
- Such other groups are, for example, halogen, alkyl, alkenyl, alkynyl, substituted alkyl, substituted alkenyl, substituted alkynyl, aryl, substituted aryl, cycloalkyl, cycloalkenyl, substituted cycloalkyl, substituted cycloalkenyl, an aliphatic heterocyclic radical, a substituted one aliphatic heterocyclic radical, heteroaryl, substituted heteroaryl, alkoxy, aryloxy, boryl, phosphino, amino, SiIyI, thio, seleno and combinations thereof.
- substituted cycloalkyl and cycloalkenyl radicals are 4-dimethylaminocyclohexyl, 4,5-dibromocyclohept-4-enyl and the like. a ..
- aryl is to be understood as meaning aromatic radicals which have a single aromatic ring or a plurality of aromatic rings which are condensed, linked via a covalent bond or are bonded by a suitable unit, eg. Example, a methylene or ethylene unit are linked.
- suitable units may also be carbonyl units, as in benzophenone, or oxygen units, such as in diphenyl ether, or nitrogen units, such as in diphenylamine.
- the aromatic ring or the aromatic rings are, for example, phenyl, naphthyl, diphenyl, diphenyl ether, diphenylamine and benzophenone.
- the aryl radicals preferably have 6 to 50 carbon atoms, particularly preferably 6 to 20 carbon atoms, very particularly preferably 6 to 8 carbon atoms.
- Substituted aryl radicals are aryl radicals wherein one or more hydrogen atoms attached to carbon atoms of the aryl radical are replaced by one or more other groups.
- Other suitable groups include alkyl, alkenyl, alkynyl, substituted alkyl, substituted alkenyl, substituted alkynyl, cycloalkyl, cycloalkenyl, substituted cycloalkyl, substituted cycloalkenyl, heterocyclo, substituted heterocyclo, halo, halo-substituted alkyl (eg CF.
- Heteroaryl radicals are to be understood as those aryl radicals in which one or more of the carbon atoms of the aromatic ring of the aryl radical has been replaced by a heteroatom selected from N, O and S.
- Substituted heteroaryl radicals are to be understood as meaning those substituted aryl radicals in which one or more of the carbon atoms of the aromatic ring of the substituted aryl radical has been replaced by a heteroatom selected from N, O and S.
- Heterocyclo means a saturated, partially unsaturated or unsaturated cyclic radical in which one or more carbon atoms of the radical are represented by a heteroatom, e.g.
- Substituted heterocyclo radicals are piperazinyl, morpholinyl, tetrahydropyranyl, tetrahydrofuranyl, piperidinyl, pyrrolidinyl, oxazolinyl, pyridyl, and the like are substituted by the term "heterocyclo".
- Substituted heterocyclo radicals are those heterocyclo radicals in which one or more hydrogen atoms which are bonded to one of the ring atoms are replaced by another group.
- Other suitable groups include halogen, alkyl, substituted alkyl, aryl, substituted aryl, heteroaryl, substituted heteroaryl, alkoxy, aryloxy, boryl, phosphino, amino, SiIyI, thio, seleno and combinations thereof.
- Alkoxy radicals are radicals of the general formula -OZ 1 , where Z 1 is selected from alkyl, substituted alkyl, cycloalkyl, substituted cycloalkyl,
- Suitable alkoxy radicals are, for example, methoxy, ethoxy, benzyloxy, t-butoxy, etc.
- aryloxy means those radicals of the general formula -OZ 1 in which Z 1 is selected from aryl, substituted aryl, heteroaryl, substituted heteroaryl and combinations thereof.
- Suitable aryloxy radicals are phenoxy, substituted phenoxy, 2-pyridinoxy, 8-quinolinoxy and others.
- A is phenyl
- n is 0 to 3
- the hydrogenation process according to the invention is preferably carried out in such a way that the phenyl group is completely hydrogenated to the corresponding cyclohexyl group.
- the aromatic hydrocarbon is selected from the group consisting of benzene and alkyl-substituted benzenes such as toluene, ethylbenzene, XyIoI (o-, m-, p- or isomer mixture) and mesitylol (1,2,4 or 1 , 3,5 or isomer mixture).
- benzene is thus preferably hydrogenated to cyclohexane and the alkyl-substituted benzenes such as toluene, ethylbenzene, xylene and mesitylol to alkyl-substituted cyclohexanes such as methylcyclohexane, ethylcyclohexane, dimethylcyclohexane and trimethylcyclohexane. It is also possible to hydrogenate any mixtures of the aforementioned aromatic hydrocarbons to mixtures of the corresponding cyclohexanes.
- any mixtures containing two or three compounds selected from benzene, toluene and xylene can be hydrogenated to mixtures containing two or three compounds selected from cyclohexane, methylcyclohexyl and dimethylcyclohexane.
- the aromatic hydrocarbon is selected from the group consisting of phenol, alkyl-substituted phenols such as 4-tert-butylphenol and 4-nonylphenol, bis (p-hydroxyphenyl) methane and bis (p-hydroxyphenyl) dimethylmethane.
- phenol to cyclohexanol preference is given to phenol to cyclohexanol, the alkyl-substituted phenols, such as 4-tert-butylphenol and 4-nonylphenol, to alkyl-substituted cyclohexanols, such as 4-tert-butylcyclohexanol and 4-nonylcyclohexanol, bis (p-hydroxyphenyl) methane to bis (p-hydroxycyclohexyl) methane and bis (p-hydroxyphenyl) dimethylmethane hydrogenated to bis (p-hydroxycyclohexyl) dimethylmethane.
- the alkyl-substituted phenols such as 4-tert-butylphenol and 4-nonylphenol
- alkyl-substituted cyclohexanols such as 4-tert-butylcyclohexanol and 4-nonylcyclohexanol
- the aromatic hydrocarbon is selected from the group consisting of aniline, alkyl-substituted aniline, N, N-dialkylaniline, diaminobenzene, bis (p-aminophenyl) methane and bis (p-aminotolyl) methane.
- aniline to cyclohexylamine alkyl-substituted aniline to alkyl-substituted cyclohexylamine, N, N-dialkylaniline to N, N-dialkylcyclohexylamine, diaminobenzene to diaminocyclohexane, bis (p-aminophenyl) methane to bis (p-aminocyclohexyl) methane and Bis (p-aminotolyl) methane hydrogenated to bis (p-amino-methylcyclohexyl) methane.
- the aromatic hydrocarbon is selected from the group consisting of aromatic carboxylic acids such as phthalic acid and aromatic carboxylic acid esters such as C 1-12 -alkyl esters of phthalic acid, where the C 1-12 -alkyl radicals may be linear or branched, for example, dimethyl phthalate, di-2-propylheptyl phthalate, di-2-ethylhexyl phthalate, dioctyl phthalate, diisononyl phthalate.
- aromatic carboxylic acids such as phthalic acid are therefore preferably cycloaliphatic carboxylic acids such as tetrahydrophthalic acid and aromatic carboxylic esters such as C 12 -alkyl esters of phthalic acid, aliphatic carboxylic acid esters such as C 12 -alkyl esters of tetrahydrophthalic acid, for example dimethyl phthalate to dimethylcyclohexyl-dicarboxylate, Di-2-propylheptyl phthalate to di-2-propylheptylcyclohexandicarboxylat, di-2-ethylhexylphthalat to di-2-ethylhexylcyclohexandicarboxylat, dioctyl phthalate to Dioctylcyclohexandicarboxylat and diisononyl phthalate to diisononyl-cyclohexanedicarboxylate, hydrogenated
- the present application relates to a process for the hydrogenation of aldehydes to the corresponding alcohols.
- Preferred aldehydes are mono- and disaccharides such as glucose, lactose and xylose.
- the mono- and disaccharides are hydrogenated to the corresponding sugar alcohols, e.g. Glucose is hydrogenated to sorbitol, lactose to lactitol and xylose to xylitol.
- Suitable mono- and disaccharides and suitable hydrogenation conditions are e.g. in DE-A 101 28 205, wherein, instead of the catalyst disclosed in DE-A 101 28 205, the shell catalyst according to the present invention is used.
- the hydrogenation process according to the invention is a selective process for the hydrogenation of organic compounds which contain hydrogenatable groups, preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group, with which high yields and space-time yields, [amount of product / ( Catalyst volume • time)] (kg / (l cat . • h)), [product amount / (reactor volume • time)] (kg / (l reactor • h)), based on the catalyst used can be used and in which the catalysts used without workup can be used repeatedly for hydrogenations. In particular, long catalyst life times are achieved in the hydrogenation process according to the invention.
- the hydrogenation process according to the invention can be carried out in the liquid phase or in the gas phase.
- the hydrogenation process according to the invention is preferably carried out in the liquid phase.
- the hydrogenation process of the invention may be carried out in the absence of a solvent or diluent or the presence of a solvent or diluent, i. it is not necessary to carry out the hydrogenation in solution.
- Suitable solvent or diluent are, in principle, those which are capable of dissolving or completely mixing with the organic compound to be hydrogenated and which are inert under the hydrogenation conditions, ie. not be hydrogenated.
- Suitable solvents are cyclic and acyclic ethers, e.g. Tetrahydrofuran, dioxane, methyl tert-butyl ether, dimethoxyethane, dimethoxypropane, dimethyldiethylene glycol, aliphatic alcohols such as methanol, ethanol, n- or isopropanol, n-, 2-, iso- or tert-butanol, carboxylic esters such as methyl acetate, ethyl acetate, propyl acetate or butyl acetate, and aliphatic ether alcohols such as methoxypropanol and cycloaliphatic compounds such as cyclohexane, methylcyclohexane and dimethylcyclohexane.
- aliphatic alcohols such as methanol, ethanol, n- or isopropanol, n-, 2-, iso- or tert-butanol, carb
- the amount of solvent or diluent used is not particularly limited and can be freely selected as required, but those amounts are preferred which are to a 3 to 70 wt .-% solution of the intended for hydrogenation organic compound to lead.
- the use of a diluent is advantageous in order to avoid excessive heat of reaction in the hydrogenation process. Excessive heat of reaction can lead to deactivation of the catalyst and is therefore undesirable. Therefore, careful temperature control is useful in the hydrogenation process of the present invention. Suitable hydrogenation temperatures are mentioned below.
- the product formed during the hydrogenation that is to say preferably the respective cycloaliphatic (s)
- solvent if appropriate in addition to other solvents or diluents.
- a part of the product formed in the process can be admixed with the aromatic still to be hydrogenated.
- cyclohexane is thus used as solvent in a particularly preferred embodiment.
- the corresponding cyclohexanedicarboxylic acid dialkyl esters are preferably used as solvent.
- the present invention relates to a hydrogenation of the type in question, wherein benzene is hydrogenated in the presence of the catalyst according to the invention to cyclohexane.
- the actual hydrogenation is usually carried out analogously to the known hydrogenation processes for the hydrogenation of organic compounds which have hydrogenatable groups, preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group, as described in the aforementioned prior art ,
- the organic compound is brought into contact with the catalyst in the presence of hydrogen as the liquid phase or gas phase, preferably as the liquid phase.
- the liquid phase can be passed through a fluid catalytic bed (fluid bed mode) or a fixed catalyst bed (fixed bed mode).
- the hydrogenation can be configured both continuously and discontinuously, wherein continuous operation of the process is preferred.
- the process according to the invention is carried out in trickle-bed reactors or in flooded mode according to the fixed-bed procedure.
- the hydrogen can be passed both in cocurrent with the solution of the reactant to be hydrogenated and in countercurrent through the catalyst.
- Suitable apparatuses for carrying out hydrogenation after the hydrogenation on the catalyst fluidized bed and on the fixed catalyst bed are known from the prior art, e.g. from Ullmanns Enzyklopadie der Technischen Chemie, 4th Edition, Vol. 13, p. 135 ff., and P.N. Rylander, "Hydrogenation and Dehydrogenation” in Ullmann's Encyclopedia of Industrial Chemistry, 5th ed. on CD-ROM.
- the hydrogenation according to the invention can be carried out both at normal hydrogen pressure and at elevated hydrogen pressure, for example at a hydrogen absolute pressure of at least 1, 1 bar, preferably at least 2 bar. In general the hydrogen absolute pressure will not exceed a value of 325 bar and preferably 300 bar.
- the hydrogen absolute pressure is particularly preferably in the range from 1.1 to 300 bar, very particularly preferably in the range from 5 to 40 bar.
- the hydrogenation of benzene takes place, for example, at a hydrogen pressure of generally ⁇ 50 bar, preferably 10 bar to 45 bar, particularly preferably 15 to 40 bar.
- the reaction temperatures in the process according to the invention generally amount to at least 30 ° C. and frequently will not exceed 250 ° C.
- the hydrogenation process is preferably carried out at temperatures in the range from 50 to 200.degree. C., particularly preferably from 70 to 18.degree. C., and very particularly preferably in the range from 80 to 16.degree.
- the hydrogenation of benzene occurs e.g. at temperatures in the range of generally from 75 ° C to 170 ° C, preferably from 80 ° C to 160 ° C.
- Hydrogen-containing gases which contain no catalyst poisons such as carbon monoxide or sulfur-containing gases such as H 2 S or COS, for example mixtures of hydrogen with inert gases such as nitrogen or reformer exhaust gases, which usually still emit volatile hydrocarbons, are also suitable as reaction gases - hold. Preference is given to using pure hydrogen (purity ⁇ 99.9% by volume, especially ⁇ 99.95% by volume, in particular ⁇ 99.99% by volume).
- the educt to be hydrogenated is usually used in an amount of 0.05 to 3 kg / (l (catalyst) » h), in particular 0.15 to 2 kg / (l (catalyst) » h) , lead over the catalyst.
- the catalysts used in this process can be regenerated with decreasing activity according to the usual for noble metal catalysts such as ruthenium catalysts, the skilled person known methods.
- noble metal catalysts such as ruthenium catalysts
- a solvent for. As water, rinse.
- the hydrogenated group-containing organic compounds (preferred compounds used in the hydrogenation process of the present invention are above in a preferred embodiment of the method according to the invention have a sulfur content of generally ⁇ 2 mg / kg, preferably ⁇ 1 mg / kg, more preferably ⁇ 0.5 mg / kg, most preferably ⁇ 0.2 mg / kg , and in particular ⁇ 0.1 mg / kg.
- the method for determining the sulfur content is mentioned below.
- a sulfur content of ⁇ 0.1 mg / kg means that no sulfur is detected in the feedstock, such as benzene, using the measuring method given below.
- the hydrogenation process according to the invention is preferably characterized in the case of the preferred hydrogenation of carbocyclic aromatic groups to the corresponding carbocyclic aliphatic groups by the complete hydrogenation of the aromatic nuclei of the organic compounds with carbocyclic aromatic groups, the degree of hydrogenation generally being> 98%, preferably at> 99%, particularly preferably> 99.5%, very particularly preferably> 99.9%, in particular> 99.99% and especially> 99.995%.
- the degree of hydrogenation is determined by gas chromatography.
- the degree of hydrogenation is determined by means of UV / VIS spectrometry.
- a particularly preferred embodiment of the hydrogenation process according to the invention relates to the hydrogenation of benzene to cyclohexane.
- the hydrogenation process according to the invention is therefore described in more detail below using the example of benzene hydrogenation.
- the hydrogenation of benzene is generally in the liquid phase. It can be carried out continuously or discontinuously, continuous operation being preferred.
- the benzene hydrogenation according to the invention is generally carried out at a temperature of 75 ° C to 170 ° C, preferably 80 ° C to 160 ° C.
- the pressure is generally ⁇ 50 bar, preferably from 10 to 45 bar, particularly preferably from 15 to 40 bar, very particularly preferably from 18 to 38 bar.
- the benzene used in the hydrogenation process according to the invention has a sulfur content of generally ⁇ 2 mg / kg, preferably ⁇ 1 mg / kg, more preferably ⁇ 0.5 mg / kg, most preferably ⁇ 0 , 2 mg / kg, and in particular ⁇ 0.1 mg / kg.
- the Method for determination of sulfur content is mentioned below.
- a sulfur content of ⁇ 0.1 mg / kg means that no sulfur is detected in benzene using the method of measurement given below.
- the hydrogenation can generally be carried out in the fluid bed or fixed bed mode, preference being given to carrying out in the fixed bed mode.
- the hydrogenation process according to the invention is particularly preferably carried out with liquid circulation, wherein the heat of hydrogenation can be removed and utilized via a heat exchanger.
- the feed / circulation ratio is generally from 1: 5 to 1:40, preferably from 1:10 to 1:30.
- the hydrogenation effluent can be passed in the gas phase or in the liquid phase in a straight pass, following the hydrogenation process according to the invention, through a downstream reactor.
- the reactor can be operated with liquid phase hydrogenation in trickle mode or flooded.
- the reactor is filled with the catalyst according to the invention or with another catalyst known to the person skilled in the art.
- Hydrogenated products which contain no or very low residual contents of the starting products to be hydrogenated can thus be obtained with the aid of the process according to the invention.
- a further subject of the present application is the use of the coated catalyst according to the invention in a process for the hydrogenation of an organic compound containing hydrogenatable groups, preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group or for the hydrogenation of aldehydes to the corresponding alcohols, more preferably for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group.
- Suitable catalysts, process conditions and compounds to be hydrogenated are mentioned above. The following examples further illustrate the invention.
- catalyst B is carried out according to the general preparation example (Example 29) in DE-A 101 28 242:
- Impregnation of ruthenium (III) nitrosyl nitrate onto SiO 2 the amount of ruthenium was chosen such that there is a similar amount of ruthenium per reactor volume as in catalyst A, ie 0.7% by weight of Ru).
- Catalyst B has a weak ruthenium gradient: inside, the ruthenium concentration is about 50% of the ruthenium concentration in the shell (determined by SEM, EDXS, across the cross-section of the catalyst strand).
- Ru compound ruthenium (III) acetate dissolved in acetic acid (from Umicore, 5.22% by weight Ru product number 68 1875 2605 order number 240299)
- ruthenium (III) acetate solution is made up to 83 ml with demineralized water and distributed over 100 g of the D11-10 support, dried at 120-130 ° C (agitated), reduced at 300 ° C for 2 h (50 Nl / h H 2 - IO NI / h N 2 ); and passivated at room temperature (6 vol% air in N 2 ).
- Catalyst D contains 0.35 wt% Ru
- Catalyst E has 0.34 wt% Ru.
- Catalyst F is prepared similarly to Catalyst D and E, but on 1.5 mm strands (Carrier No. 84084, the water uptake of this batch is 9.5 ml / 10 g, BET 167 m 2 / g). It is again soaked in 95-98 wt.% Water absorption).
- the finished catalyst F contains 0.36% by weight of Ru.
- the reduction is carried out in hydrogen (about 75% H 2 in N 2 , where N 2 is used as purge stream; 1.5 NnrrVh H 2 - 0.5 Nm 3 / h N 2 ) moving bed at 300 ° C and a residence time of 90 minutes (1-2 h).
- the passivation takes place in diluted air (air in N 2 ).
- the air addition is regulated so that the temperature of the catalyst remains below 30-35 ° C.
- the finished catalyst G contains 0.31-0.32 wt .-% Ru.
- SiO 2 carrier 50 g Davicat Grade 57 (Davison-Grace, Grit, Lott 2169, WA 1, 01 ml / g, BET 340 m 2 / g);
- Ru solution 3.36 g of ruthenium (III) acetate (from Umicore, 5.22% by weight of Ru, product number 68 1875 2605, order No. 240299)
- the Ru solution is made up to 50 ml with DI water. This solution is distributed over the support and dried in an oven at 120 ° C, at 300 ° C for 2 h reduced (50 Nl / h H 2 - IO Nl / h N 2 ); and passivated at room temperature 6 vol.% Air in N 2 .
- the catalyst contains 0.33 wt% Ru.
- the support used is the BASF SiO 2 support D11-10 (3 mm stripping):
- D11-10 is a commercial product of BASF and can be purchased.
- the porosity of the shaped article 0.95 ml / g (water absorption determination, BASF -
- CAK / Q Method 1021 consists of saturating the carrier with water - supernatants
- the shaking density of the shaped body is: 467 g / l (to diameter of the shaped body of 6 mm) (BASF-CAK / Q method 1001).
- the manufacturing method is described above.
- Method description 0.03 to 0.05 grams of the sample is mixed in a Alsint crucible with 5 g of sodium peroxide and slowly heated on a hotplate. Subsequently, the substance-flux mixture is first melted over an open flame and then heated to red-hot over a fan flame. The digestion is finished as soon as a clear melt is reached.
- the cooled melt cake is dissolved in 80 ml of water, the solution is heated to boiling (destruction of H 2 O 2 ) and then - after cooling - mixed with 50 ml of 21 wt.% Hydrochloric acid.
- Ru dispersity 90-95% (after CO sorption, assumed stoichiometric factor: 1)
- Sample preparation Reduction of the sample for 30 min at 200 ° C with hydrogen and then rinsed for 30 min with helium at 200 ° C - Measurement of the metal surface with pulses from the gas to be adsorbed in the inert gas stream (CO) to saturation Chemisorption at 35 ° C. Saturation is achieved until CO is no longer adsorbed, ie the areas of 3 to 4 successive peaks ( Detector signal) are constant and similar to the peak of an unadsorbed pulse Pulse volume is determined to 1%, pressure and temperature of the gas must be checked). (Method: See DIN 66136)
- the reduced catalyst G contains at least partially crystalline ruthenium in the outermost zone (strand surface).
- ruthenium comes in single particles before 1-10 nm (> 5 nm in places): usually 1-5 nm. The size of the particles decreases from outside to inside.
- Ruthenium particles are spotted down to a depth of 30-50 microns below the strand surface. Ruthenium is at least partially crystalline in this shell (SAD: selected area diffraction). The main part of the ruthenium is thus in this shell (> 90% within the first 50 microns).
- 2-L pressure vessel inner diameter 90 mm, vessel height: 200 mm, material 1.4580 or 2.4610 with 4-blade beam agitation stirrer, power surge and an internal riser for sampling or for filling and emptying the pressure vessel is the respective amount used (volume or mass) of the catalyst in a "catalyst basket" (material 2.4610) filled.
- the pressure vessel is closed for pressure testing and treated with 50 bar of nitrogen. Afterwards, the pressure vessel is evacuated with a vacuum pump, separated from the vacuum pump, and the starting material or the feed solution is sucked into the vessel via the riser. To remove residual amounts of oxygen at room temperature, the container is successively charged twice with 10-15 bar nitrogen and twice with 10-15 bar hydrogen and relaxed. The stirrer is switched on, a stirring speed of 1000 rpm is set and the reaction solution is heated to the reaction temperature. The set temperature is reached after 15 minutes at the latest. Hydrogen is pressed up to the respective target pressure within 5 minutes. The hydrogen consumption is determined by means of a book station and the pressure is kept constant at the respective target pressure. Sampling (for flushing the riser) and samples of the reaction mixture are taken at regular intervals via the riser to monitor the progress of the reaction.
- the heater is switched off, the pressure vessel is cooled to 25 ° C, the pressure is slowly relieved and the reaction mixture is discharged via the riser with a slight overpressure.
- the hydrogen used had a purity of at least 99.9-99.99 vol.% (Based on dry gas). Secondary components are carbon monoxide (10 ppm maximum), nitrogen (100 ppm maximum), argon (100 ppm maximum) and water (400 ppm maximum).
- the procedure is carried out according to the general experimental description (GCI), but the catalyst used remains in the catalyst basket after the end of the experiment. After evacuation of the pressure vessel with the vacuum pump, the vessel is disconnected from the vacuum pump and new feedstock or feed solution is drawn into the vessel via the riser.
- GCI general experimental description
- Benzene (BASF) with a purity of> 99.90% by weight and a total sulfur content of ⁇ 0.2 mg / kg is used (the sulfur determination method is given below).
- the cyclohexane (BASF) used has a purity of > 99.95 wt.% And a total sulfur content of ⁇ 0.2 mg / kg (the sulfur determination method is given below).
- the experiments are carried out in such a way that the same amount of ruthenium is used in the experiments.
- 750 ml of a 5% by weight solution of benzene in cyclohexane serve as the starting material.
- Catalysts used 20.6 g of catalyst E (according to the invention) (0.34% Ru / SiO 2 D11-10 support, 3 mm)
- catalyst F (according to the invention) (0.36% Ru / SiO 2 D11-10 support, 1.5 mm)
- the respective contacts are repeatedly used in four consecutive attempts. Sampling takes place after reaction times of 20, 40, 60 90, 120 180 and 240 minutes.
- the feedstock used is 750 ml of a 5% strength by weight solution of benzene in cyclohexane.
- Catalysts used 6.9 g of catalyst E (0.34% Ru / SiO 2 D11-10 support, 3 mm)
- the respective contacts are used repeatedly in four consecutive experiments. Sampling takes place after reaction times of 20, 40, 60, 90 and 120 minutes.
- Catalyst F is the more active of the two contacts in direct comparison with catalyst E with approximately the same ruthenium content due to the smaller particle diameter and a concomitant higher accessibility of the catalytically active centers (larger external surface area).
- Catalyst B (0.70% Ru / SiO 2 D11-10 support) at 20 and 32 bar at 100 ° C;
- Catalyst G (0.32% Ru / SiO 2 D11-10 support) at 20 and 32 bar at 100 ° C.
- Catalyst G (catalyst according to the invention) (0.32% Ru / SiO 2 supported on D11-10, 3 mm): 9.0 g (about 22 ml).
- the contact is used repeatedly in five consecutive attempts. Sampling takes place after reaction times of 10, 20, 30, 40, 60, 90, 120 and 180 minutes.
- Catalyst G (according to the invention) (0.32% Ru / SiO 2 on D11-10 support, 3 mm) amount of catalyst used: 9.0 g (about 22 ml) analytics: GC analysis in GC area% (the implementation is given below)
- the contact is used repeatedly for five consecutive attempts. Sampling takes place after reaction times of 10, 20, 30, 40, 60, 90, 120 and 180 minutes.
- the contact is used repeatedly for five consecutive attempts. Trial takes place after reaction time of 10, 20, 30, 40, 60, 90, 120 and 180 minutes.
- the contact is used repeatedly for five consecutive attempts. Sampling takes place after reaction times of 10, 20, 30, 40, 60, 90, 120 and 180 minutes.
- Catalyst G (according to the invention) (0.32% Ru D11-10, 3 mm) at 20 bar and 100 ° C. (hydrogenation example 8, about 29 mg of ruthenium)
- Catalyst G (according to the invention) (0.32% Ru D11-10, 3 mm) at 32 bar and 100 ° C. (hydrogenation example 9, about 29 mg of ruthenium)
- catalyst B (comparison) (0.70% Ru D11-10, 3 mm): catalyst B (0.70% Ru D11-10, 3 mm) at 32 bar and 100 ° C. (hydrogenation example 12, approx 31 mg ruthenium)
- Catalyst B (0.70% Ru D11-10, 3 mm) at 32 bar and 100 ° C. (hydrogenation example 13, about 31 mg of ruthenium)
- the filler used is 750 ml of a 5% strength by weight solution of benzene in cyclohexane.
- Catalyst B (comparative) (0.70% Ru / SiO 2 D11)
- the contact is used repeatedly for five consecutive attempts. Sampling takes place after reaction times of 10, 20, 30, 40, 60, 90, 120, 180 and 240 minutes.
- Catalyst B (comparison) (0.70% Ru / SiO 2 D11-10 support, 3 mm) amount of catalyst used: 4.4 g analytics: GC analysis in GC area% (the procedure is given below)
- the contact is used repeatedly for five consecutive attempts. Sampling takes place after reaction times of 10, 20, 30, 40, 60, 90, 120, and 180 minutes.
- the results of the four hydrogenation examples (8, 9, 12 and 13) show that, when using the approximately equal ruthenium content, the catalyst G (inventive) measure) (0.32% Ru D11-10, 3 mm) with shell structure compared to Catalyst B (comparative) (0.70% Ru D11-10, 3 mm) is the more active contact. This applies both at a hydrogen pressure of 20 bar (comparison of hydrogenation examples 8 and 12 and at a hydrogen pressure of 32 bar (comparison of hydrogenation examples 9 and 13).
- the experiment is carried out in a continuously operated jacketed reactor (0 12 mm, length: 1050 mm) with three evenly distributed to the reactor length ⁇ lsammlungniken, which is operated with volume-controlled liquid circulation (HPLC pump) in a continuous trickle mode.
- the test facility is also equipped with a separator for separation of gas and liquid phase with standstill, exhaust gas control, external heat exchanger and sampling.
- the metering of the hydrogen is controlled by pressure (in bar), the measurement of the excess hydrogen is volume-controlled (in NL / h), and the dosage of the benzene feedstock is controlled by an HPLC pump.
- the product discharge is controlled by a valve.
- the temperature is measured at the beginning (inlet) and at the end (outlet) of the reactor or the catalyst bed with a thermocouple
- the procedure is carried out according to regulation "AVB”, but the following parameters are changed:
- the starting material used is a solution of 37.6 g of phenol (Riedel de Haen, article number 3350017) and 712.4 g of cyclohexanol (Riedel de Haen, article number 24217). ,
- Catalyst B (comparison) (0.70% Ru / SiO 2 D11-10 support, 3 mm)
- Carrier gas helium
- the shell catalyst G (according to the invention) is the most active of the three ruthenium catalysts tested under the selected reaction conditions.
- catalyst G used amount of catalyst: 13.7 g of catalyst G (0.32% Ru / SiO 2 D11-10 support, 3 mm)
- the determination of the residual content of DINP is carried out by quantitative UV / VIS determination (method description below), the content of by-products is determined by gas chromatography (method description see below). Sampling takes place after reaction times of 3, 6, 9, 12, 15, 18 and 24 hours.
- the residual content of DINP is ⁇ 100 ppm by weight
- the combustion condensate is collected in an alkaline receiver (40 mmol KOH).
- the sulfur is determined as sulfate by ion chromatography.
- Ion Chromatography System e.g. modular system, company Metrohm
- Acetone Merck Suprasolv Article number 1.0012.1000 Determination limit for sulfur on the sample calculated: 0.1 mg / kg.
- the method is based on the presence of a UV chromophore (aromatic ring) in the analyte.
- sample solutions can be measured directly without preparation.
- Samples with a concentration of> 2000 ppm are diluted with methanol sufficiently far for the UV measurement that the absorption at the evaluation wavelength is 275 nm ⁇ 1.2.
- the content of DINP is then calculated to the original concentration.
- Cuvette material quartz layer thickness: 2 mm
- the evaluation takes place at a wavelength of 275 nm.
- E 275 UV / VIS absorbance of the sample at the wavelength 275 nm.
- the reproducibility of the measurement was checked by repeating the calibration solution three times, the maximum absolute error of the palatinol determination being 26 ppm (calculated to the initial weight) or 20 ppm (calculated as the mean value), corresponding to 1.26 % and 0.97% rel. Error.
- This gas chromatographic method is suitable for determining the impurities in monomer plasticizers in the concentration range from about 0.05% to about 5%.
- Equipment Gas Chromatograph: Hewlett Packard HP 5890 Series II Control and Evaluation Software: Chromeleon 6.4 SP2 Column: Capillary Column DB 1
- Dimethyl phthalate from BASF, Palatinol M is used as the internal standard.
- Carrier gas helium
- the main component is excluded from the integration.
- the impurities are calculated with the correction factor 1 compared to the internal standard. Calculation:
- m (ver.) mass of the impurity to be determined
- a (ver.) peak area of the impurity to be determined
- ⁇ c (ver.) Sum of impurities in g / 100g (%)
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Abstract
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Priority Applications (6)
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KR1020087001732A KR101354236B1 (ko) | 2005-06-22 | 2006-06-20 | 수소화가능한 기를 포함하는 유기 화합물의 수소화용 촉매및 방법 |
US11/993,777 US8207327B2 (en) | 2005-06-22 | 2006-06-20 | Catalyst and process for hydrogenating organic compounds comprising hydrogenatable groups |
CA2612435A CA2612435C (en) | 2005-06-22 | 2006-06-20 | Catalyst and method for hydrogenating organic compounds containing hydrogenable groups |
JP2008517476A JP2008543550A (ja) | 2005-06-22 | 2006-06-20 | 水素化可能な基を含む有機化合物の水素化用触媒及び水素化方法 |
CN2006800305342A CN101242895B (zh) | 2005-06-22 | 2006-06-20 | 用于氢化含有能被氢化的基团的有机化合物的催化剂和方法 |
EP06777365A EP1899051A2 (de) | 2005-06-22 | 2006-06-20 | Katalysator und verfahren zur hydrierung von hydrierbare gruppen enthaltenden organischen verbindungen |
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DE102005029200.3 | 2005-06-22 | ||
DE102005029200A DE102005029200A1 (de) | 2005-06-22 | 2005-06-22 | Katalysator und Verfahren zur Hydrierung von hydrierbare Gruppen enthaltenden organischen Verbindungen |
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US (1) | US8207327B2 (de) |
EP (1) | EP1899051A2 (de) |
JP (1) | JP2008543550A (de) |
KR (1) | KR101354236B1 (de) |
CN (1) | CN101242895B (de) |
CA (1) | CA2612435C (de) |
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WO (1) | WO2006136541A2 (de) |
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-
2005
- 2005-06-22 DE DE102005029200A patent/DE102005029200A1/de not_active Withdrawn
-
2006
- 2006-06-20 US US11/993,777 patent/US8207327B2/en not_active Expired - Fee Related
- 2006-06-20 CN CN2006800305342A patent/CN101242895B/zh not_active Expired - Fee Related
- 2006-06-20 KR KR1020087001732A patent/KR101354236B1/ko not_active IP Right Cessation
- 2006-06-20 CA CA2612435A patent/CA2612435C/en not_active Expired - Fee Related
- 2006-06-20 WO PCT/EP2006/063323 patent/WO2006136541A2/de active Application Filing
- 2006-06-20 JP JP2008517476A patent/JP2008543550A/ja active Pending
- 2006-06-20 EP EP06777365A patent/EP1899051A2/de not_active Withdrawn
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Cited By (17)
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US8598392B2 (en) | 2008-12-17 | 2013-12-03 | Basf Se | Continuous method for producing substituted cyclohexylmethanols |
WO2010079035A3 (de) * | 2008-12-17 | 2010-09-10 | Basf Se | Kontinuierliches verfahren zur herstellung von substituierten cyclohexylmethanolen |
WO2010079035A2 (de) * | 2008-12-17 | 2010-07-15 | Basf Se | Kontinuierliches verfahren zur herstellung von substituierten cyclohexylmethanolen |
WO2011069933A2 (de) | 2009-12-11 | 2011-06-16 | Basf Se | Verfahren zur regenerierung eines ruthenium-haltigen geträgerten hydrierkatalysators |
WO2011082991A2 (de) | 2009-12-15 | 2011-07-14 | Basf Se | Katalysator und verfahren zur hydrierung von aromaten |
US9084983B2 (en) | 2009-12-15 | 2015-07-21 | Basf Se | Catalyst and process for hydrogenating aromatics |
EP2722323A2 (de) | 2010-03-24 | 2014-04-23 | Basf Se | Verfahren zur Herstellung von 2-Methyl-4-phenyl-2-pentanol |
US8450534B2 (en) | 2010-03-24 | 2013-05-28 | Basf Se | Process for preparing 4-cyclohexyl-2-methyl-2-butanol |
US9040592B2 (en) | 2010-03-24 | 2015-05-26 | Basf Se | Process for preparing 4-cyclohexyl-2-methyl-2-butanol |
WO2011117360A2 (de) | 2010-03-24 | 2011-09-29 | Basf Se | Verfahren zur herstellung von 4-cyclohexyl-2-methyl-2-butanol |
WO2013037737A1 (de) | 2011-09-16 | 2013-03-21 | Basf Se | Verfahren zur herstellung von 4-cyclohexyl-2-methyl-2-butanol |
US9056812B2 (en) | 2011-09-16 | 2015-06-16 | Basf Se | Process for preparing 4-cyclohexyl-2-methyl-2-butanol |
US9416079B2 (en) | 2011-09-16 | 2016-08-16 | Basf Se | Process for preparing 4-cyclohexyl-2-methyl-2-butanol |
US9340754B2 (en) | 2012-11-27 | 2016-05-17 | Basf Se | Process for the preparation of cyclohexyl-substituted tertiary alkanols |
US9717664B2 (en) | 2012-11-27 | 2017-08-01 | Basf Se | Composition that includes cyclohexyl-substituted tertiary alkanols |
EP4015079A1 (de) * | 2020-12-18 | 2022-06-22 | Evonik Operations GmbH | Verfahren zur regenerierung von hydrierkatalysatoren |
US11701649B2 (en) | 2020-12-18 | 2023-07-18 | Evonik Operations Gmbh | Process for regeneration of hydrogenation catalysts |
Also Published As
Publication number | Publication date |
---|---|
CA2612435A1 (en) | 2006-12-28 |
EP1899051A2 (de) | 2008-03-19 |
DE102005029200A1 (de) | 2006-12-28 |
KR20080027871A (ko) | 2008-03-28 |
CN101242895B (zh) | 2012-01-11 |
US20100152436A1 (en) | 2010-06-17 |
CN101242895A (zh) | 2008-08-13 |
CA2612435C (en) | 2015-02-24 |
JP2008543550A (ja) | 2008-12-04 |
US8207327B2 (en) | 2012-06-26 |
KR101354236B1 (ko) | 2014-01-22 |
WO2006136541A3 (de) | 2007-04-12 |
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