WO2011069933A2 - Procédé de régénération d'un catalyseur d'hydrogénation supporté à teneur en ruthénium - Google Patents

Procédé de régénération d'un catalyseur d'hydrogénation supporté à teneur en ruthénium Download PDF

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WO2011069933A2
WO2011069933A2 PCT/EP2010/068911 EP2010068911W WO2011069933A2 WO 2011069933 A2 WO2011069933 A2 WO 2011069933A2 EP 2010068911 W EP2010068911 W EP 2010068911W WO 2011069933 A2 WO2011069933 A2 WO 2011069933A2
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catalyst
hydrogenation
ruthenium
range
carried out
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WO2011069933A3 (fr
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Daniela Mirk
Christoph Schappert
Uwe Stabel
Eberhardt Gaffron
Roman Prochazka
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Basf Se
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Priority to EP10787119A priority Critical patent/EP2509712A2/fr
Priority to CN2010800560855A priority patent/CN102652037A/zh
Publication of WO2011069933A2 publication Critical patent/WO2011069933A2/fr
Publication of WO2011069933A3 publication Critical patent/WO2011069933A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/90—Regeneration or reactivation
    • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/06—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using steam
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/10—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/396—Distribution of the active metal ingredient
    • B01J35/397—Egg shell like
    • 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
    • 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
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • 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
    • B01J35/64—Pore diameter
    • B01J35/651—50-500 nm
    • 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
    • B01J35/64—Pore diameter
    • B01J35/653—500-1000 nm
    • 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
    • B01J35/64—Pore diameter
    • B01J35/657—Pore diameter larger than 1000 nm
    • 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
    • B01J35/66—Pore distribution
    • B01J35/69—Pore distribution bimodal
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
    • C07C2521/04—Alumina
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • C07C2521/08—Silica
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/46—Ruthenium, rhodium, osmium or iridium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2601/00—Systems containing only non-condensed rings
    • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
    • C07C2601/14—The ring being saturated
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates to a process for the regeneration of a ruthenium-containing supported hydrogenation catalyst.
  • a decrease in the catalytic activity is caused by various physical and chemical effects on the catalyst, for example by blocking the catalytically active centers or by loss of catalytically active centers by thermal, mechanical or chemical processes.
  • catalyst deactivation or, in general, aging can be caused by sintering of the catalytically active centers, by loss of (precious) metal, by deposits or by poisoning of the active sites.
  • the mechanisms of aging / deactivation are manifold.
  • JP 2008 238043 A relates to the regeneration of a reforming catalyst by means of steam at temperatures> 400 ° C.
  • WO 08/015103 A2 and WO 08/015170 A2 relate to processes for the regeneration of a suitable for hydrogenation Ru catalyst, comprising purging the catalyst with inert gas in a regeneration step until reaching the original activity or a part of original activity.
  • the underlying object of the present invention was to provide a process for regenerating a ruthenium-containing hydrogenation catalyst, especially a ruthenium catalyst used in the hydrogenation of benzene. This should be easy to implement in terms of apparatus and inexpensive to carry out. In particular, this should allow a multiple and complete regeneration of the catalyst can be achieved.
  • the BET surface area (DIN ISO 9277) of the hydrogenation catalyst (fresh, before it is used for hydrogenation) is preferably in the range from 100 to 250 m 2 / g, in particular in the range from 120 to 230 m 2 / g.
  • the process according to the invention is particularly suitable for the regeneration of Ru catalysts described in patent applications EP 814 098 A2, WO 00/63142 A1 (EP 1 169 285 A1), WO 06/136541 A2 (DE 102 005 029 200 A) and WO 02/100537 A2 (all BASF AG) are described and used in the methods disclosed therein. These catalysts and methods are listed below.
  • catalyst variant I The catalysts described below will be referred to in the present application as "catalyst variant I”.
  • all metals of subgroup VIII of the Periodic Table can be used as the active metal.
  • the active metals used are preferably platinum, rhodium, palladium, Cobalt, nickel or ruthenium or a mixture of two or more thereof used, in particular ruthenium is used as the active metal.
  • Macropores and “mesopores” are used in the context of the present invention as described in Pure & Appl. Chem., Vol. 46, p. 79 (1976), namely as pores whose diameter is above 50 nm (macropores) or whose diameter is between 2 nm and 50 nm (mesopores).
  • macropores are also corresponding to US Pat The above literature defines and describes pores with a diameter of ⁇ 2 nm.
  • the content of the active metal is generally about 0.01 to about 30% by weight, preferably about 0.01 to about 5% by weight, and more preferably about 0.1 to about 5% by weight, based on the total weight the catalyst used.
  • the total metal surface area on catalyst variant I is preferably about 0.01 to about 10 m 2 / g, more preferably about 0.05 to about 5 m 2 / g, and especially about 0.05 to about 3 m 2 / g of the catalyst ,
  • the metal surface is prepared by the methods described by J. Lemaitre et al. in "Characterization of Heterogeneous Catalysts", ed. Francis Delanney, Marcel Dekker, New York 1984, pp. 310-324.
  • the ratio of the surfaces of the active metal (s) and the catalyst carrier is preferably less than about 0.05, the lower limit being about 0.0005.
  • Catalyst variant I comprises a carrier material which is macroporous and has an average pore diameter of at least about 50 nm, preferably at least about 100 nm, in particular at least about 500 nm, and whose BET surface area is at most about 30 m 2 / g, preferably at most about 15 m 2 / g, more preferably at most about 10 m 2 / g, in particular at most about 5 m 2 / g and more preferably at most about 3 m 2 / g.
  • the average pore diameter of the support is preferably about 100 nm to about 200 ⁇ m, more preferably about 500 nm to about 50 ⁇ m.
  • the BET surface area of the support is preferably about 0.2 to about 15 m 2 / g, more preferably about 0.5 to about 10 m 2 / g, more preferably about 0.5 to about 5 m 2 / g, and more preferably about 0.5 to about 3 m 2 / g.
  • the surface of the support is determined by the BET method by N 2 adsorption, in particular according to DIN ISO 9277.
  • the determination of the average pore diameter and the pore size distribution is carried out by Hg porosimetry, in particular according to DIN 66133.
  • the pore size distribution of the carrier can be approximately bimodal, with the pore diameter distribution with maxima at about 600 nm and about 20 ⁇ m in the bimodal distribution being a specific embodiment.
  • the pore volume of this preferred carrier is preferably about 0.53 ml / g.
  • Useful macroporous support materials include, for example, macroporous activated carbon, silicon carbide, alumina, silica, titania, zirconia, magnesia, zinc oxide, or mixtures of two or more thereof, with alumina and zirconia preferably being used.
  • catalyst variant II The catalysts described below will be referred to in the present application as "catalyst variant II". From this variant II different subvariants exist.
  • This catalyst corresponds to that described above under EP 0 814 098 A2.
  • the usable carrier materials are those which are macroporous and have an average pore diameter of at least 0.1 ⁇ m, preferably at least 0.5 ⁇ m, and a surface area of at most 15 m 2 / g, preferably at most 10 m 2 / g, particularly preferably at most 5 m 2 / g, in particular at most 3 m 2 / g.
  • the average pore diameter of the carrier used there is preferably in the range from 0.1 to 200 ⁇ m, in particular from 0.5 to 50 ⁇ m.
  • the surface of the support is preferably 0.2 to 15 m 2 / g, particularly preferably 0.5 to 10 m 2 / g, in particular 0.5 to 5 m 2 / g, especially 0.5 to 3 m 2 / g of carrier.
  • This catalyst also has respect to the pore diameter distribution the already described above bimodality with the analog distributions and the corresponding preferred pore volume.
  • Sub-variant 2 contains one or more metals of subgroup VIII of the Periodic Table as active component (s) on a support as defined herein. Ruthenium is preferably used as the active component.
  • the total metal surface area on the catalyst is preferably 0.01 to 10 m 2 / g, particularly preferably 0.05 to 5 m 2 / g and more preferably 0.05 to 3 m 2 / g of the catalyst.
  • the metal surface was measured by the chemisorption method as described in J. Lemaitre et al., "Characterization of Heterogenous Catalysts", Ed. Francis Delanney, Marcel Dekker, New York (1984), pp. 310-324.
  • the ratio of the surfaces of the at least one active metal and the catalyst support is less than about 0.3, preferably less than about 0.1, and more preferably about 0.05 or less, the lower limit being about 0.0005.
  • the carrier materials used in sub-variant 2 have macropores and mesopores.
  • the useful supports have a pore distribution corresponding to about 5 to about 50%, preferably about 10 to about 45%, more preferably about 10 to about 30% and most preferably about 15 to about 25% of the pore volume of macropores having pore diameters in the Range from about 50 nm to about 10,000 nm and about 50 to about 95%, preferably about 55 to about 90%, more preferably about 70 to about 90%, and especially about 75 to about 85% of the pore volume of mesopores with a pore diameter be formed from about 2 to about 50 nm, each adding up the sum of the proportions of the pore volumes to 100%.
  • the total pore volume of the carriers used is about 0.05 to 1.5 cm 3 / g, preferably 0.1 to 1.2 cm 3 / g and especially about 0.3 to 1.0 cm 3 / g.
  • the average pore diameter of the carriers used in the invention is about 5 to 20 nm, preferably about 8 to about 15 nm and more preferably about 9 to about 12 nm.
  • the surface area of the support is about 50 to about 500 m 2 / g, more preferably about 200 to about 350 m 2 / g, and most preferably about 250 to about 300 m 2 / g of the support.
  • the surface of the support is determined by the BET method by IS adsorption, in particular according to DIN ISO 9277.
  • the determination of the average pore diameter and the size distribution is carried out by Hg porosimetry, in particular according to DIN 66133.
  • all support materials known in catalyst preparation i. which have the above-defined pore size distribution can be used, are preferably activated carbon, silicon carbide, alumina, silica, titania, zirconia, magnesia, zinc oxide or mixtures thereof, more preferably alumina and zirconia used.
  • catalysts described below will be referred to in the present application as "catalyst variant III" or "coated catalyst”.
  • the subject matter is a coated catalyst containing as active metal ruthenium alone or together with at least one further metal of subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS notation), applied to a support containing silicon dioxide as support material.
  • This coated catalyst 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 on 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 ⁇ .
  • the above data are obtained by SEM (electron probe microanalysis) - EDXS (energy dispersive X-ray spectroscopy) and represent averaged values. Further information regarding the above measurement methods and techniques is available, for example, "Spectroscopy in Catalysis "by JW Niemantsverdriet, VCH, 1995.
  • the shell catalyst 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 near 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.
  • This catalyst variant III has - in spite of the small amount of active metal - a very high activity in the hydrogenation of organic compounds containing hydrogenatable groups, in particular in the hydrogenation of carbocyclic aromatic groups, with very good selectivities on. In particular, the activity of catalyst variant III does not decrease over a long hydrogenation period. Very particular preference is given to a coated catalyst 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 to 200 ⁇ m.
  • the coated catalyst is distinguished by the fact that in the (FEG) -TEM (Field Emission Gun Transmission Electron Microscopy) with EDXS only in the outermost 200 ⁇ m, preferably 100 ⁇ m, very particularly preferably 50 ⁇ m ( Penetration depth) of active metal particles can be detected. Particles smaller than 1 nm can not be detected.
  • FEG Fluorescence Emission Gun Transmission Electron Microscopy
  • ruthenium can be used alone or together with at least one other metal of subgroups IB, VIIB or VIII of the Periodic Table of the Elements (CAS notation).
  • 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 used alone as the active metal or together with platinum or iridium in the shell catalyst; very particular preference is given to using ruthenium alone as active metal.
  • the coated catalyst exhibits the above-mentioned very high activity at 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 shell catalyst is preferably from 0.1 to 0.5% by weight, more preferably from 0.25 to 0.35% by weight.
  • Penetration depth of the active metal in the carrier material is dependent on the loading of the catalyst variant III with active metal.
  • a substantial amount of active metal present which impairs the activity of the hydrogenation catalyst, in particular the activity over a long hydrogenation period, especially in rapid reactions, where hydrogen deficiency can occur inside the catalyst (core).
  • the shell catalyst there are in the shell catalyst at least 60 wt .-% of the active metal, based on the total amount of the active metal, in the shell of the catalyst to a penetration depth of 200 ⁇ before.
  • At least 80% by weight of the active metal, based on the total amount of the active metal, in the shell of the catalyst up to a penetration depth of 200 ⁇ m, are preferably present in the shell catalyst.
  • Very particular preference is given to a coated catalyst 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 to 200 ⁇ m.
  • active metal is present only in the outermost shell, for example in a zone up to a penetration depth of 100 to 200 ⁇ m.
  • 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
  • To determine the penetration depth of the active metal particles a plurality of catalyst particles (eg 3, 4 or 5) transverse to the strand axis (when the catalyst is in the form of strands) ground.
  • the profiles of the active metal / Si concentration ratios are then recorded by means of line scans. On each measuring line, for example, 15 to 20 measuring points are measured at equal intervals; the spot size is about 10 ⁇ x 10 ⁇ .
  • 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 ⁇ x 2000 ⁇ and with an information depth of about 2 ⁇ .
  • 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 outer shell of the catalyst Under the surface of the shell catalyst is the outer shell of the catalyst to a penetration depth of about 2 ⁇ to understand. This penetration depth corresponds to the information depth in the above-mentioned surface analysis.
  • a shell catalyst in which the amount of the active metal, based on the weight ratio of active metal to Si (w / w%), at the surface of the shell catalyst is 4 to 6%, at a penetration depth of 50 ⁇ 1, 5 to 3% and in the range of 50 to 150 ⁇ 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 shell catalyst.
  • the content of alkaline earth metal ion (s) (M 2+ ) in the catalyst is preferably from 0.01 to 1% by weight. %, in particular 0.05 to 0.5 wt .-%, especially 0.1 to 0.25 wt .-%, each based on the weight of the silica support material.
  • catalyst variant III An essential component of catalyst variant III is the carrier material based on silicon dioxide, generally amorphous silicon dioxide.
  • the term " ⁇ -morph" in this context means that the proportion of crystalline silicon dioxide phases is less than 10% by weight of the carrier material.
  • the support materials used for the preparation of the catalysts may have superstructures, which are formed by regular arrangement of pores in the carrier material.
  • Suitable carrier 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 carrier material also being another oxidic material can, for example MgO, CaO, T1O2, ZrÜ2, Fe2Ü3 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 both natural and artificial.
  • suitable amorphous support materials based on silica are silica gels, kieselguhr, fumed silicas and precipitated silicas.
  • the catalysts comprise silica gels as support materials.
  • the carrier material may have different shapes. If the process in which the shell catalysts are used is designed as a suspension process, the support material in the form of a finely divided powder will usually be used to prepare the catalysts.
  • the powder preferably has particle sizes in the range from 1 to 200 ⁇ m, in particular from 1 to 100 ⁇ m.
  • moldings of the carrier material for example by extrusion, Extruders or tableting are available and, for example, the shape of spheres, tablets, cylinders, strands, rings or hollow cylinders, stars and the like may have. 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 frequently 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 catalysts described below will be referred to in the present application as "catalyst variant IV".
  • the ruthenium catalyst according to this catalyst variant IV is obtainable by: i) one or more treatment of a support material based on amorphous silicon dioxide with a halogen-free aqueous solution of a low molecular weight ruthenium compound and subsequent drying of the treated support material at a temperature below 200 ° C., especially ⁇ 150 ° C,
  • step ii) is carried out immediately after step i).
  • the support based on amorphous silicon dioxide preferably has a BET surface area (DIN ISO 9277) in the range from 50 to 700 m 2 / g.
  • the ruthenium catalyst contains ruthenium in an amount of 0.2 to 10 wt .-%, particularly 0.2 to 7 wt .-%, more preferably 0.4 to 5 wt .-%, each based on the weight of carrier.
  • the ruthenium compound used in step i) is selected from ruthenium (III) nitrosyl nitrate, ruthenium (III) acetate, sodium and potassium ruthenate (IV).
  • the solid obtained from i) used for reduction in ii) preferably has a water content of less than 5% by weight, especially less than 2% by weight, in each case based on the total weight of the solid.
  • the drying in step i) takes place while moving the treated support material.
  • the ruthenium catalyst comprising less than 0.05% by weight of halogen, especially less than 0.01% by weight of halogen, in each case based on the total weight of the catalyst, and consisting of:
  • the hydrogenation catalyst especially one of the catalysts described above (catalyst variants I, II, III and IV and mentioned sub-variants) of the process according to the invention is preferably used for the ring hydrogenation of an aromatic organic compound.
  • the hydrogenation catalyst is used for the hydrogenation of benzene to cyclohexane.
  • a conversion of educt eg benzene
  • a conversion of educt of generally> 98%, preferably> 99%, particularly preferably> 99.5%, very particularly preferably> 99.9%, in particular> 99.99% and specifically> 99.995%.
  • Another object of the present application is therefore an integrated process for the hydrogenation of benzene to cyclohexane in the presence of a Ru-containing supported catalyst, which in addition to the hydrogenation step comprises the regeneration steps according to the invention.
  • the hydrogenation step can be carried out in the liquid phase or in the gas phase.
  • the hydrogenation step is preferably carried out in the liquid phase.
  • the hydrogenation step can be carried out in the absence of a solvent or diluent or in the presence of a solvent or diluent, ie it is not necessary to carry out the hydrogenation in solution.
  • a solvent or diluent any suitable solvent or diluent may be used.
  • Suitable solvents or diluents are in principle those which are able to dissolve the organic compound to be hydrogenated as completely as possible or completely mix with it and which are inert under the hydrogenation conditions, ie are not 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 acid 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,
  • the amount of solvent or diluent used is not particularly limited and can be freely selected as needed, but those amounts are preferred which lead to a 3 to 70 wt .-% solution of the organic compound intended for hydrogenation.
  • 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 step. Suitable hydrogenation temperatures are mentioned below.
  • the product formed during the hydrogenation ie cyclohexane
  • the solvent is particularly preferably used as the solvent, optionally in addition to other solvents or diluents.
  • a part of the cyclohexane formed in the process can be admixed with the benzene still to be hydrogenated.
  • Based on the weight of the hydrogenation benzene is preferably 1 to 30 times, more preferably 5 to 20 times, in particular 5 to 10 times the amount of the product cyclohexane as a solvent or diluent admixed.
  • the actual hydrogenation is usually carried out in such a way that the organic compound as a liquid phase or gas phase, preferably as a liquid phase, brought into contact with the catalyst in the presence of hydrogen.
  • the liquid phase can be passed through a catalyst suspension (suspension mode) or a fixed catalyst bed (fixed bed mode).
  • the hydrogenation can be configured both continuously and discontinuously, wherein the continuous process procedure is preferred.
  • the process is carried out in trickle reactors or in flooded mode after the fixed bed driving way through.
  • the hydrogen can be passed both in cocurrent with the solution of the educt to be hydrogenated and in countercurrent over the catalyst.
  • Suitable apparatuses for carrying out a hydrogenation on the catalyst fluidized bed and on the fixed catalyst bed are known from the prior art, for example from Ullmanns Enzyklopadie der Technischen Chemie, 4th Edition, Volume 13, p. 135 ff., And from PN Rylander, "Hydrogenation and Dehydrogenation” in Ullmann's Encyclopaedia of Industrial Chemistry, 5th ed. on CD-ROM.
  • the hydrogenation can be carried out both at normal hydrogen pressure and at elevated hydrogen pressure, e.g. be carried out at a hydrogen absolute pressure of at least 1, 1 bar, preferably at least 2 bar.
  • the hydrogen absolute pressure will not exceed a value of 325 bar and preferably 300 bar.
  • the hydrogen absolute pressure is in the range from 1.1 to 300 bar, very particularly preferably in the range from 5 to 40 bar.
  • the hydrogenation of benzene occurs e.g. 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 hydrogenation step are generally at least 30 ° C and often will not exceed 250 ° C.
  • the hydrogenation step is preferably carried out at temperatures in the range from 50 to 200.degree.
  • the hydrogenation of benzene is carried out at temperatures in the range of 75 to 170 ° C, in particular 80 to 160 ° C.
  • Suitable reaction gases besides hydrogen are also hydrogen-containing gases which do not contain catalyst poisons such as carbon monoxide or sulfur-containing gases such as H 2 S or COS, e.g. Mixtures of hydrogen with inert gases such as nitrogen or reformer waste gases, which usually contain volatile hydrocarbons. Preference is given to using pure hydrogen (purity> 99.9% by volume, especially> 99.95% by volume, in particular> 99.99% by volume).
  • the aromatics hydrogenation comprising the regeneration steps according to the invention is generally carried out at a temperature of 75 to 170 ° C, preferably 80 to 160 ° C.
  • the pressure is generally ⁇ 50 bar, preferably 10 to 45 bar, more preferably 15 to 40 bar, most preferably 18 to 38 bar.
  • benzene is hydrogenated at an absolute pressure of about 20 bar to cyclohexane.
  • the benzene used in the hydrogenation step 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 especially ⁇ 0.1 mg / kg.
  • a sulfur content of ⁇ 0.1 mg / kg means that no sulfur is detected in benzene using the method of measurement given below.
  • Measuring method Determination according to Wickbold (DIN EN 41), followed by ion chromatography.
  • the hydrogenation may generally be carried out in the suspension or fixed bed mode, preference being given to carrying out in the fixed bed mode.
  • the hydrogenation process is particularly preferably carried out with liquid circulation, wherein the hydrogenation heat can be removed and used 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 can be passed in the straight pass, through a downstream reactor following the hydrogenation in the gas phase or in the liquid phase.
  • the reactor can be operated in liquid-phase hydrogenation in trickle-run mode or operated flooded.
  • the reactor is filled with the catalyst according to the invention or with another catalyst known to the person skilled in the art.
  • the hydrogen used in the hydrogenation step preferably contains no harmful catalyst poisons, such as CO.
  • catalyst poisons such as CO.
  • reformer gases can be used.
  • pure hydrogen is used as the hydrogenation gas.
  • such a deactivated ruthenium catalyst can be returned to the state of the original activity by treatment with steam and subsequent drying.
  • the activity is particularly up > 90%, preferably> 95%, more preferably> 98%, in particular> 99%, most preferably> 99.5% of the original value (ie the activity of the fresh catalyst before the hydrogenation step, ie prior to its use in the hydrogenation)
  • the treatment with steam is preferably carried out at a temperature in the range of 100 to 200 ° C, especially 105 to 150 ° C, most preferably 1 10 to 130 ° C.
  • the treatment with steam is preferably carried out at an absolute pressure in the range of 0.5 to 10 bar, especially 0.8 to 8 bar, especially 0.9 to 4 bar.
  • the treatment with steam is preferably carried out over a period in the range of 10 to 200 hours, especially 20 to 150 hours, especially 50 to 100 hours.
  • the treatment with steam is preferably carried out continuously with a flow of 100 to 400 kg (steam), especially 150 to 350 kg, more particularly 200 to 300 kg, per square meter (catalyst cross-sectional area of the catalyst bed) and per hour [kg / (m 2 h )] carried out.
  • the drying is preferably carried out directly after the treatment with steam.
  • the drying is preferably carried out at a temperature in the range from 10 to 350.degree. C., especially from 50 to 250.degree. C., very particularly from 70 to 180.degree. C., more particularly from 80 to 130.degree.
  • the drying is preferably carried out at an absolute pressure in the range from 0.5 to 5 bar, especially 0.8 to 2 bar, very particularly 0.9 to 1, 5 bar.
  • the drying is preferably carried out over a period in the range of 10 to 50 hours, especially 10 to 20 hours.
  • the drying is preferably carried out by rinsing with a gas or gas mixture.
  • the calculated drying time of the catalyst bed of a large-scale cyclohexane production plant with an assumed moisture content of 2 or 5 wt .-% is approximately 18 or 30 hours.
  • Rinsing can be carried out in the method according to the invention both in the down-flow direction and in the up-flow direction.
  • "Rinse" means that the catalyst is contacted with the gas or gas mixture.
  • the gas or gas mixture is passed over the catalyst by means of suitable design measures known to the person skilled in the art.
  • the gas is selected from nitrogen, oxygen, carbon dioxide, helium, argon, neon, and mixtures thereof. Most preferred is air.
  • the regeneration process according to the invention is carried out without removal of the catalyst in the same reactor in which the hydrogenation has taken place.
  • the drying of the catalyst in particular by purging with a gas or gas mixture, carried out at temperatures and pressures in the reactor which are similar or similar to the hydrogenation, resulting in a very short interruption of the reaction process.
  • a further subject of the present invention is an integrated process for hydrogenating benzene in the presence of a ruthenium catalyst comprising the catalyst regeneration steps according to the invention with the following steps:
  • a Ru / Al 2 O 3 catalyst containing 0.5% by weight of ruthenium was prepared analogously as described in EP 814 098 A2 (BASF AG), page 14, lines 20 to 29.
  • Example 4 After its complete deactivation in the hydrogenation of benzene, the catalyst prepared according to Example 1 was removed. For this purpose, the reactor was first emptied and purged still about 1 10 ° C warm catalyst bed with 2.5 t / h steam. After the steam was free of organic carbon, the bed, which was initially about 110 ° C. warm, was first flushed with nitrogen and then with air, whereby the bed was cooled.
  • Example 4
  • a continuous system with a 90 ml tube reactor was charged with 2 samples of the used catalyst (90 ml each, 75 g of a sample from the lower quarter of the hydrogenation reactor of a cyclohexane unit, 72 g of a sample from the upper fourth of the hydrogenation reactor of a cyclohexane unit).
  • a continuous system with a 90 ml tube reactor was equipped with a Samples of the recovered catalyst (90 ml, 62 g of a recovery sample) are charged.
  • the reactor was operated in trickle mode with circulation. There were 60.6 ml / h of benzene and 58 Nl / h of hydrogen at 75 ° C inlet and 125 ° C outlet temperature, a pressure of 30 bar and 1, 5 kg / h circulation passed through the reactor.
  • the gas chromatographic analysis of the reaction output showed that the benzene had been converted to> 99.5%.

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  • Engineering & Computer Science (AREA)
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Abstract

L'invention concerne un procédé de régénération d'un catalyseur d'hydrogénation supporté à teneur en ruthénium, le catalyseur étant traité à la vapeur d'eau, puis séché. L'invention concerne un procédé intégré d'hydrogénation de benzène en cyclohexane en présence d'un catalyseur supporté à teneur en ruthénium, comprenant en plus de l'étape d'hydrogénation les étapes de régénération du catalyseur.
PCT/EP2010/068911 2009-12-11 2010-12-06 Procédé de régénération d'un catalyseur d'hydrogénation supporté à teneur en ruthénium WO2011069933A2 (fr)

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CN2010800560855A CN102652037A (zh) 2009-12-11 2010-12-06 再生含钌的负载型氢化催化剂的方法

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8933262B2 (en) 2011-05-24 2015-01-13 Basf Se Process for preparing polyisocyanates from biomass
CN109382095A (zh) * 2018-11-13 2019-02-26 江西理工大学 乙苯加氢制备乙基环己烷的催化剂及制备方法、应用

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* Cited by examiner, † Cited by third party
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WO2013103394A1 (fr) 2012-01-06 2013-07-11 Celanese International Corporation Procédés de fabrication de catalyseurs avec des précurseurs d'halogénure métallisé
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US20130178663A1 (en) 2012-01-06 2013-07-11 Celanese International Corporation Cobalt-containing hydrogenation catalysts and processes for making same
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MX2014008252A (es) 2012-01-06 2014-08-08 Celanese Int Corp Catalizadores de hidrogenacion.
WO2013103393A1 (fr) 2012-01-06 2013-07-11 Celanese International Corporation Procédés de fabrication de catalyseurs comprenant un support modifié comprenant un métal précieux et des métaux actifs
WO2013103392A1 (fr) 2012-01-06 2013-07-11 Celanese International Corporation Catalyseur d'hydrogénation et procédé de production d'éthanol à l'aide dudit catalyseur
US11918989B2 (en) * 2020-12-18 2024-03-05 Evonik Operations Gmbh Process for regeneration of hydrogenation catalysts
EP4015079A1 (fr) * 2020-12-18 2022-06-22 Evonik Operations GmbH Procédé de régénération des catalyseurs d'hydrogène
CN114522707B (zh) * 2022-02-22 2023-07-21 中南大学 一种碱土金属碳酸盐负载纳米钌复合材料及其制备方法和应用

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2757128A (en) 1951-04-27 1956-07-31 Exxon Research Engineering Co Low pressure hydrogenation and hydrogen regeneration of the catalyst
US3245919A (en) 1961-05-22 1966-04-12 Sinclair Refining Co Boehmite base precursor
US3851004A (en) 1973-09-27 1974-11-26 Union Carbide Corp Hydrocarbon alkylation process using catalyst regeneration
EP0243894A2 (fr) 1986-05-02 1987-11-04 W.R. Grace & Co.-Conn. Catalyseurs d'hydrotraitement et support ayant une structure de pores doublement dispersée
WO1993004774A1 (fr) 1991-08-29 1993-03-18 Basf Aktiengesellschaft Catalyseur a support, a teneur en argent, et procede de decomposition catalytique de monoxyde de diazote
DE19634880A1 (de) 1996-04-02 1997-10-09 Intevep Sa Prozeß zum Regenerieren eines Katalysators
EP0814098A2 (fr) 1996-06-19 1997-12-29 Basf Aktiengesellschaft Procédé de conversion d'un composé organique en présence d'un catalyseur supporté en ruthénium
WO2000063142A1 (fr) 1999-04-15 2000-10-26 Basf Aktiengesellschaft Procede d'hydrogenation d'aromates non substitues ou substitues par alkyle a l'aide d'un catalyseur macroporeux
WO2002100537A2 (fr) 2001-06-11 2002-12-19 Basf Aktiengesellschaft Catalyseurs ruthenium
DE102005029200A1 (de) 2005-06-22 2006-12-28 Basf Ag Katalysator und Verfahren zur Hydrierung von hydrierbare Gruppen enthaltenden organischen Verbindungen
WO2008015170A2 (fr) 2006-07-31 2008-02-07 Basf Se Procédé de régénération de catalyseurs de ruthénium utilisés pour l'hydrogénation de benzène
WO2008015103A2 (fr) 2006-07-31 2008-02-07 Basf Se Procédé de régénération de catalyseurs de ruthénium utilisés pour l'hydrogénation
JP2008238043A (ja) 2007-03-27 2008-10-09 Nippon Oil Corp 改質触媒の再生方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3753926A (en) * 1971-03-08 1973-08-21 Universal Oil Prod Co Regeneration of a coke deactivated catalyst comprising a combination of platinum rhenium and halogen with a porous carrier material
CA1023333A (fr) * 1972-11-13 1977-12-27 Shell Canada Limited Procede de regeneration d'un catalyseur de reforming desactive
US4431750A (en) * 1982-05-19 1984-02-14 Phillips Petroleum Company Platinum group metal catalyst on the surface of a support and a process for preparing same
US5495055A (en) * 1994-08-12 1996-02-27 Arco Chemical Technology, L.P. Acetone hydrogenation using a supported ruthenium catalyst
US7230035B2 (en) * 2002-12-30 2007-06-12 Conocophillips Company Catalysts for the conversion of methane to synthesis gas
DE10361157A1 (de) * 2003-12-22 2005-07-21 Basf Ag Ruthenium-Heterogenkatalysator und Verfahren zur Herstellung eines Bisglycidylethers der Formel I

Patent Citations (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2757128A (en) 1951-04-27 1956-07-31 Exxon Research Engineering Co Low pressure hydrogenation and hydrogen regeneration of the catalyst
US3245919A (en) 1961-05-22 1966-04-12 Sinclair Refining Co Boehmite base precursor
US3851004A (en) 1973-09-27 1974-11-26 Union Carbide Corp Hydrocarbon alkylation process using catalyst regeneration
EP0243894A2 (fr) 1986-05-02 1987-11-04 W.R. Grace & Co.-Conn. Catalyseurs d'hydrotraitement et support ayant une structure de pores doublement dispersée
WO1993004774A1 (fr) 1991-08-29 1993-03-18 Basf Aktiengesellschaft Catalyseur a support, a teneur en argent, et procede de decomposition catalytique de monoxyde de diazote
DE19634880A1 (de) 1996-04-02 1997-10-09 Intevep Sa Prozeß zum Regenerieren eines Katalysators
EP0814098A2 (fr) 1996-06-19 1997-12-29 Basf Aktiengesellschaft Procédé de conversion d'un composé organique en présence d'un catalyseur supporté en ruthénium
WO2000063142A1 (fr) 1999-04-15 2000-10-26 Basf Aktiengesellschaft Procede d'hydrogenation d'aromates non substitues ou substitues par alkyle a l'aide d'un catalyseur macroporeux
EP1169285A1 (fr) 1999-04-15 2002-01-09 Basf Aktiengesellschaft Procede d'hydrogenation d'aromates non substitues ou substitues par alkyle a l'aide d'un catalyseur macroporeux
WO2002100537A2 (fr) 2001-06-11 2002-12-19 Basf Aktiengesellschaft Catalyseurs ruthenium
DE102005029200A1 (de) 2005-06-22 2006-12-28 Basf Ag Katalysator und Verfahren zur Hydrierung von hydrierbare Gruppen enthaltenden organischen Verbindungen
WO2006136541A2 (fr) 2005-06-22 2006-12-28 Basf Aktiengesellschaft Catalyseur et procede d'hydrogenation de composes organiques contenant des groupes hydrogenables
WO2008015170A2 (fr) 2006-07-31 2008-02-07 Basf Se Procédé de régénération de catalyseurs de ruthénium utilisés pour l'hydrogénation de benzène
WO2008015103A2 (fr) 2006-07-31 2008-02-07 Basf Se Procédé de régénération de catalyseurs de ruthénium utilisés pour l'hydrogénation
JP2008238043A (ja) 2007-03-27 2008-10-09 Nippon Oil Corp 改質触媒の再生方法

Non-Patent Citations (10)

* Cited by examiner, † Cited by third party
Title
"Ullmann's Encyclopedia of Industrial Chemistry", vol. AI, 1985, VCH, pages: 588 - 590
"Ullmanns Enzyklopädie der Technischen Chemie", vol. 13, pages: 135
J. LEMAITRE; FRANCIS DELANNEY ET AL.: "Characterization of Heterogeneous Catalysts", 1984, MARCEL DEKKER, pages: 310 - 324
O.W. FLÖRKE; SILICA: "Ullmann's Encyclopedia of Industrial Chemistry"
OBERLANDER, R. K.: "Aluminas for Catalysts, in Applied Industrial Catalysis", vol. 3, 1984, D. E. LEACH, ACADEMIC PRESS
P. N. RYLANDER: "Ullmann's Encyclopedia of Industrial Chemistry", article "Hydrogenation and Dehydrogenation"
PURE & APPL. CHEM., vol. 46, 1976, pages 79
R. J. FARRAUTO; C. H. BARTHOLOMEW: "Fundamentals of Industrial Catalytic Processes", vol. 16, 1997, pages: 17,57 - 62,88-91
VON J. LEMAITRE ET AL.: "Characterization of Heterogeneous Catalysts", 1984, MARCEL DEKKER, pages: 310 - 324
VON J.W. NIEMANTSVERDRIET: "Spectroscopy in Catalysis", 1995, VCH

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8933262B2 (en) 2011-05-24 2015-01-13 Basf Se Process for preparing polyisocyanates from biomass
CN109382095A (zh) * 2018-11-13 2019-02-26 江西理工大学 乙苯加氢制备乙基环己烷的催化剂及制备方法、应用

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