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WO2024245592A1 - Moulage de catalyseur pour l'activation de peroxyde d'hydrogène - Google Patents

Moulage de catalyseur pour l'activation de peroxyde d'hydrogène Download PDF

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Publication number
WO2024245592A1
WO2024245592A1 PCT/EP2024/052763 EP2024052763W WO2024245592A1 WO 2024245592 A1 WO2024245592 A1 WO 2024245592A1 EP 2024052763 W EP2024052763 W EP 2024052763W WO 2024245592 A1 WO2024245592 A1 WO 2024245592A1
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Prior art keywords
catalyst
molding
weight
mmol
range
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Inventor
Andrei-Nicolae PARVULESCU
Natalia Trukhan
Trees Maria DE BAERDEMAEKER
Joaquim Henrique Teles
Jaroslaw Michael MORMUL
Christophe Coperet
Lukas LAETSCH
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BASF SE
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BASF SE
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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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/89—Silicates, aluminosilicates or borosilicates of titanium, zirconium or hafnium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • 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
    • 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
    • B01J35/34—Mechanical properties
    • B01J35/37—Crush or impact strength
    • 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
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • 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
    • B01J35/63—Pore volume
    • B01J35/635—0.5-1.0 ml/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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/03—Precipitation; Co-precipitation
    • B01J37/031—Precipitation
    • B01J37/033—Using Hydrolysis
    • 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
    • B01J37/03—Precipitation; Co-precipitation
    • B01J37/036—Precipitation; Co-precipitation to form a gel or a cogel
    • 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
    • B01J37/08—Heat treatment
    • B01J37/10—Heat treatment in the presence of water, e.g. steam
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
    • C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
    • C01B39/06—Preparation of isomorphous zeolites characterised by measures to replace the aluminium or silicon atoms in the lattice framework by atoms of other elements, i.e. by direct or secondary synthesis
    • C01B39/08—Preparation of isomorphous zeolites characterised by measures to replace the aluminium or silicon atoms in the lattice framework by atoms of other elements, i.e. by direct or secondary synthesis the aluminium atoms being wholly replaced
    • C01B39/085—Group IVB- metallosilicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/36—Steaming
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • 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
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • 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
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B01J2235/05—Nuclear magnetic resonance [NMR]
    • 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
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B01J2235/15—X-ray diffraction
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/12—Surface area
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/14—Pore volume
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/90—Other properties not specified above

Definitions

  • the present invention relates to a catalyst molding for hydrogen peroxide activation, wherein the catalyst molding comprises a catalyst, wherein the catalyst comprises Ti, Si, and O, and wherein the catalyst displays a water adsorption (W), a concentration (C) of bridging p 2 q 2 - peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, and a specific activation factor (A), wherein the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 n 2 -peroxo species per Ti in the H2O2-activated catalyst.
  • W water adsorption
  • C concentration
  • A specific activation factor
  • the present invention relates to a method for the preparation of a catalyst molding, as well as to a catalyst molding obtainable or obtained by said process. Yet further, the present invention relates to a process for the activation of hydrogen peroxide, and use of the inventive catalyst molding in a reaction involving one or more of C-0 bond formation, C-C bond formation and C-C bond conversion.
  • Oxidation reactions such as ammoximation, hydroxylation, and epoxidation reactions are typically carried out in the presence of specific catalysts.
  • zeolitic materials comprising Si and a further tetravalent element are known to be efficient catalysts, wherein these zeolitic materials are often employed in the form of moldings which, in addition to the catalytically active zeolitic material, comprise a suitable binder.
  • epoxidation catalysts are employed on a large scale for the epoxidation of olefins with hydrogen peroxide (H2O2), leaving only water as a byproduct.
  • titanosilicates having an MFI framework structure containing 1-2 wt.- % Ti in which the silicon atoms were substituted for titanium atoms have proven to be efficient catalysts.
  • US 4410501 relates to the preparation of a porous crystalline synthetic material comprising silicon and titanium oxides.
  • WO 2020/074586 A1 relates to a molding comprising a zeolitic material having the framework type MFI.
  • US 9,302,257 B2 relates to a process for the preparation of a titanium zeolite catalyst, whereas WO 2021/123227 A1 relates to the continuous synthesis of a titanosilicate zeolitic material such as TS-1 .
  • WO 2020/174586 A1 relates to a molding comprising a zeolitic material having the MFI-type framework structure.
  • Titanium silicalite-1 (TS-1 ), as a specific titanosilicate, was the subject of a study on the efficient epoxidation over its dinuclear sites in C. P. Gordon et aL, Nature 2020, 586, 708-713. Generally, it was assumed that the catalytic properties of TS-1 are attributed to the presence of isolated Ti(IV) sites within the zeolite framework. However, as has been found by C. P. Gordon et al.
  • WO 2023/094691 A1 specifically relates to catalysts for hydrogen peroxide activation.
  • improved catalyst moldings comprising a catalyst, wherein the catalyst comprised in the catalyst molding displays a unique activation factor.
  • the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per metal in the H2O2-activated catalyst, as determined by quantitative 17 O NMR spectroscopy, of the catalyst which is comprised in the inventive catalyst molding provides a unique activation factor which is not only correlated to its catalytic activity, but furthermore clearly distinguishes the inventive catalyst moldings from those of the art.
  • a catalyst molding can be provided having unique physical and chemical properties, and that said catalyst molding allows for an improved catalytic activity, in particular in the activation of hydrogen peroxide for oxidation, and in particular for epoxidation reactions such as the conversion of propylene and hydrogen peroxide to propylene oxide.
  • the present invention relates to a catalyst molding for hydrogen peroxide activation, wherein the catalyst molding comprises a catalyst for hydrogen peroxide activation, said catalyst comprising Ti, Si, and O, wherein the catalyst comprised in the catalyst molding displays a water adsorption (W), preferably determined according to Reference Example 1 .1 , a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, and an activation factor (A) according to formula I, wherein the activation factor is in the range of from 10 to 75 mmol/mol; wherein in accordance with formula I, the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst:
  • W water adsorption
  • C concentration
  • A activation factor
  • the catalyst molding further comprises one or more oxidic binders, wherein the one or more oxidic binders are more preferably selected from the group consisting of inorganic binders, wherein the one or more oxidic binders more preferably comprise one or more sources of a metal oxide and/or of a metalloid oxide, more preferably one or more sources of a metal oxide and/or of a metalloid oxide selected from the group consisting of silica, alumina, titania, zirconia, lanthana, magnesia, and mixtures and/or mixed oxides of two or more thereof, more preferably from the group consisting of silica, alumina, titania, zirconia, magnesia, silica- alumina mixed oxides, silica-titania mixed oxides, silica-zirconia mixed oxides, silica-lanthana mixed oxides, silica-zirconia-lanthana mixed oxides, alumina-titania mixed oxide
  • the catalyst molding further comprises one or more oxidic binders
  • the catalyst molding comprises the one or more oxidic binders, calculated as the oxide, in an amount in the range of from 1 to 90 wt.-%, more preferably of from 5 to 70 weight-%, more preferably of from 10 to 50 weight-%, more preferably of from 15 to 30 weight-%, more preferably of from 16 to 28 weight-%, more preferably of from 16 to 26 weight-%, more preferably of from 20 to 25 weight-%.
  • the catalyst molding further comprises one or more oxidic binders
  • binder and in particular “oxidic binder” refers to materials which are not catalytically active in the epoxidation of olefins with hydrogen peroxide, i.e. which in any case do not display an activation factor falling within any of the ranges defined in the present patent application.
  • the catalyst molding exhibits a water adsorption in the range of from 1 to 15 wt.-%, more preferably of from 2 to 14 wt.-%, more preferably of from 2.5 to 11 wt.-%, more preferably of from 3 to 10 wt.-%, more preferably of from 4 to 9 wt.-%, more preferably of from 4.4 to 9 wt.-%, more preferably of from 4.4 to 8 wt.-%, more preferably of from 5 to 8 wt.-%, wherein the water adsorption is preferably determined when exposing the catalyst molding to a relative humidity of 85 %, wherein the water adsorption is more preferably determined according to Reference Example 1.1.
  • the catalyst molding exhibits a water adsorption in the range of from 3 to 6.5 wt.-%, preferably of form 3.5 to 6 wt.-%, more preferably of from 4.4 to 5.5 wt.-%.
  • the catalyst molding displays a water adsorption (W), preferably determined according to Reference Example 1.1 , a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding, as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, and an activation factor (A) according to formula I, wherein the activation factor is in the range of from 10 to 75 mmol/mol; wherein in accordance with formula I, the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding:
  • W water adsorption
  • C concentration
  • A activation factor
  • the catalyst molding displays an activation factor in the range of from 10 to 75 mmol/mol
  • a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding in the range of from 100 to 1 ,000 mmol/mol, more preferably from 200 to 900 mmol/mol, more preferably from 300 to 800 mmol/mol, more preferably from 350 to 700 mmol/mol, more preferably from 400 to 600 mmol/mol, more preferably from 420 to 550 mmol/mol.
  • the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst molding into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 2 min to 480 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 10 to 30 min after having brought the catalyst molding into contact with H2 17
  • the activation factor of the catalyst molding is in the range of from 12 to 70 mmol/mol, more preferably from 14 to 65 mmol/mol, more preferably from 16 to 60 mmol/mol, more preferably from 17 to 55 mmol/mol, more preferably from 18 to 50 mmol/mol, more preferably from 19 to 44 mmol/mol, more preferably from 20 to 39 mmol/mol, more preferably from 21 to 34 mmol/mol, more preferably from 22 to 29 mmol/mol, and more preferably from 23 to 26 mmol/mol.
  • the catalyst molding displays a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding in the range of from 100 to 1 ,000 mmol/mol, wherein the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2C>2-activated catalyst molding as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst molding into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • the catalyst molding displays a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1.2, in the range of from 200 to 900 mmol/mol, preferably from 300 to 800 mmol/mol, more preferably from 380 to 750 mmol/mol, more preferably from 420 to 700 mmol/mol, more preferably from 450 to 650 mmol/mol.
  • T is in the range of from 75 to 165 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 85 min to 155 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst molding into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst molding into contact with H2 17 C>2, wherein more preferably ? is 120 min after having brought the catalyst molding into contact with H2 17 C>2.
  • the activation factor of the catalyst molding is in the range of from 12 to 70 mmol/mol, more preferably from 14 to 65 mmol/mol, more preferably from 16 to 60 mmol/mol, more preferably from 18 to 55 mmol/mol, more preferably from 19 to 50 mmol/mol, more preferably from 20 to 45 mmol/mol, more preferably from 21 to 40 mmol/mol, more preferably from 22 to 37 mmol/mol, more preferably from 23 to 35 mmol/mol, and more preferably from 24 to 34 mmol/mol.
  • the catalyst molding exhibits a BET specific surface area in the range of from 50 to 700 m 2 /g, more preferably of from 100 to 500 m 2 /g, more preferably of from 150 to 475 m 2 /g, more preferably of from 200 to 450 m 2 /g, more preferably of from 250 to 425 m 2 /g, more preferably of from 300 to 400 m 2 /g, more preferably of from 320 to 400 m 2 /g, wherein the BET specific surface area is preferably determined according to Reference Example 1 .5.
  • the catalyst molding exhibits a total pore volume in the range of from 0.2 to 1 .5 g/ml, more preferably in the range of from 0.4 to 1 .4 g/ml, more preferably in the range of from 0.4 to 1 .3 g/ml, more preferably in the range of from 0.5 to 1 .1 ml/g, more preferably in the range of from 0.7 to 1 .0 ml/g, wherein the total pore volume is preferably determined according to Reference Example 1.11.
  • the catalyst molding exhibits an average crush strength in the range of from 3 to 30 N, more preferably in the range of from 4 to 25 N, more preferably in the range of from 5 to 20 N, more preferably in the range of from 5 to 15 N, wherein the average crush strength is preferably determined according to Reference Example 1.8.
  • the catalyst molding has a sodium content, calculated as Na2O, in the range of from 0 to 0.5 weight-%, more preferably of from 0 to 0.2 weight-%, more preferably of from 0 to 0.15 weight-%, more preferably of from 0 to 0.14 weight-%, more preferably in the range of from 0 to 0.1 weight-%, more preferably of less than 0.1 weight-%, more preferably of from 0 to 0.08 weight-%, based on the weight of the catalyst molding.
  • the catalyst molding exhibits an acid site density in the range of from 1 to 1000 pmol/g, preferably in the range of from 5 to 500 pmol/g, more preferably in the range of from 10 to 100 pmol/g, at a temperature below 250 °C, determined according to Reference Example 1 .9.
  • the catalyst molding exhibits a propylene oxide activity of at least 2.0 weight- %, preferably in the range of from 3.0 to 15.0 weight-%, more preferably in the range of from 3.5 to 10.0 weight-%, more preferably in the range of from 4.0 to 7.5 weight-%, more preferably in the range of from 4.5 to 6.5 weight-%, more preferably in the range of from 5.5 to 6.3 weight-%, preferably determined as described in Reference Example 1.6.
  • the catalyst molding is in the form of a strand, more preferably having a cross-sectional profile, wherein the cross-sectional profile more preferably is hexagonal, rectangular, quadratic, triangular, oval, or circular, more preferably circular, wherein the cross-sectional profile more preferably has a diameter in the range of from 0.1 to 10 mm, more preferably in the range of from 0.2 to 7 mm, more preferably in the range of from 0.5 to 5 mm, more preferably in the range of from 1.0 to 3.0 mm, more preferably in the range of from 1.5 to 2.0 mm.
  • the catalyst molding is an extrudate.
  • the catalyst comprised in the catalyst molding displays a water adsorption in the range of from 1 to 10 wt.-%, preferably from 1 .5 to 9.5 wt.-%, more preferably from 2 to 9 wt.-%, more preferably from 2.5 to 8.5 wt.-%, more preferably from 3 to 8 wt.-%, more preferably from 3.2 to 7.9 wt.-%, more preferably from 3.5 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • the catalyst comprised in the catalyst molding displays a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst in the range of from 150 to 1 ,000 mmol/mol, preferably from 100 to 800 mmol/mol, more preferably from 150 to 750 mmol/mol, more preferably from 200 to 700 mmol/mol, more preferably from 250 to 650 mmol/mol, more preferably from 300 to 600 mmol/mol, more preferably from 350 to 550 mmol/mol, and more preferably from 400 to 500 mmol/mol.
  • the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2C>2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst, which is comprised in the catalyst molding, into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 2 min to 480 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 10 to 30 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 12 to 20 min after having brought the catalyst into contact with H2 17 C>2, and more
  • the activation factor of the catalyst comprised in the catalyst molding is in the range of from 11 to 65 mmol/mol, preferably from 13 to 55 mmol/mol, more preferably from 15 to 50 mmol/mol, more preferably from 18 to 45 mmol/mol, more preferably from 20 to 40 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 37 mmol/mol, more preferably from 23 to 35 mmol/mol, more preferably from 24 to 32 mmol/mol, and more preferably from 25 to 30 mmol/mol.
  • the catalyst comprised in the catalyst molding displays a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst in the range of from 125 to 750 mmol/mol, wherein the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2C>2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • the catalyst comprised in the catalyst molding displays a water adsorption in the range of from 1 to 7.9 wt.-%, more preferably from 3 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • the catalyst comprised in the catalyst molding displays a water adsorption in the range of from 3 to 6.5 wt.-%, more preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • the catalyst comprised in the catalyst molding displays a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, more preferably determined according to Reference Example 1 .3, in the range of from 200 to 725 mmol/mol, preferably from 250 to 700 mmol/mol, more preferably from 300 to 680 mmol/mol, more preferably from 350 to 660 mmol/mol, more preferably from 400 to 640 mmol/mol, more preferably from 450 to 620 mmol/mol, and more preferably from 500 to 600 mmol/mol.
  • T is in the range of from 75 to 165 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 85 min to 155 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst into contact with H2 17 C>2, wherein more preferably T is 120 min after having brought the catalyst into contact with H2 17 C>2.
  • the activation factor of the catalyst comprised in the catalyst molding is in the range of from 11 to 70 mmol/mol, preferably from 12 to 62 mmol/mol, more preferably in the range of from 13 to 60 mmol/mol, more preferably from 14 to 59 mmol/mol, more preferably from 16 to 54 mmol/mol, more preferably from 18 to 49 mmol/mol, more preferably from 20 to 44 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 34 mmol/mol, more preferably from 23 to 31 mmol/mol, and more preferably from 24 to 28 mmol/mol.
  • the catalyst comprised in the catalyst molding of the present invention displays a XANES spectrum having a ratio of the intensity of the signal at 4987 eV to the intensity of the signal at 4992 eV in the range of from 0.95 : 1 to 1 .07 : 1 , more preferably of from 0.97 : 1 to 1 .07 : 1 , more preferably in the range of from 0.99 : 1 to 1 .07 : 1 , more preferably in the range of from 1.01 : 1 to 1.07 : 1 , more preferably in the range of from 1.03 : 1 to 1.07 : 1 , and more preferably in the range of from 1 .05 : 1 to 1 .07 : 1 , wherein the XANES spectrum is more preferably determined according Reference Example 1.2.
  • the catalyst comprised in the catalyst molding of the present invention has a BET specific surface area in the range of from 350 to 475 m 2 /g, more preferably from 370 to 460 m 2 /g, more preferably from 390 to 445 m 2 /g, wherein the BET specific surface area is preferably determined according to Reference Example 1.5.
  • the catalyst comprised in the catalyst molding of the present invention comprises from 0.2 to 5 weight-%, preferably in the range of from 0.5 to 4 weight-%, more preferably in the range of from 0.7 to 3 weight-%, more preferably of from 0.7 to 2.5 weight-%, more preferably from 0.8 to 2.0 weight-%, more preferably from 1 .0 to 1 .9 weight-%, more preferably from 1 .0 to 1 .8 weight-%, more preferably from 1 .1 to 1 .3 weight-%, of Ti, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of B, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention comprises from 0 to 0.1 weight-%, preferably from 0 to 0.08 weight-%, of Na, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ge, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention comprises from 0 to 1 weight-%, preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.2 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.009 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of C, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention comprises a content of one or more of Fe, Co, Ni, and Cu, calculated as Fe2Os, CO2O3, NiO, and CuO, respectively, in the range of from 0 to 0.1 weight-%, more preferably in the range of from 0 to 0.07 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.02 weight-%, based on the weight of the catalyst which is comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention comprises a content of one or more of Fe, Co, Ni, and Cu, calculated as the element, respectively, in the range of from 0 to 0.1 weight-%, more preferably in the range of from 0 to 0.07 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.02 weight-%, based on the weight of the catalyst which is comprised in the catalyst molding.
  • the catalyst comprised in the catalyst molding of the present invention exhibits a propylene oxide activity of at least 2.0 weight-%, preferably in the range of from 3.0 to 15.0 weight-%, more preferably in the range of from 5.0 to 14.0 weight-%, more preferably in the range of from 9.0 to 13.0 weight-%, preferably determined as described in Reference Example 1.6.
  • the catalyst can further comprise one or more metals selected from the group consisting of K, Zn, Cd, Sn, La, and Ba, including mixtures of two or more thereof, preferably from the group consisting of Zn, Cd, Sn, La, and Ba, including mixtures of two or more thereof.
  • the catalyst which is comprised in the catalyst molding, consists of Ti, Si, and O, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.
  • the catalyst which is comprised in the catalyst molding, consists of Ti, Si, O, and H, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.
  • the catalyst which is comprised in the catalyst molding, comprises, more preferably consists of, a zeolitic material having a framework structure comprising Si, Ti, and O.
  • the catalyst which is comprised in the catalyst molding, comprises a zeolitic material having a framework structure comprising Si, Ti, and O
  • the zeolitic material having an Si : Ti molar ratio in the range of from 1 to 250, more preferably in the range of from 10 to 150, more preferably in the range of from 20 to 95, more preferably in the range of from 30 to 75, more preferably in the range of from 35 to 70, more preferably in the range of from 40 to 65, more preferably in the range of from 45 to 60, more preferably in the range of from 50 to 55.
  • the catalyst which is comprised in the catalyst molding, comprises a zeolitic material having a framework structure comprising Si, Ti, and O
  • the zeolitic material has a framework structure type selected from the group consisting of MFI, MEL, MWW, ITH, IWR, IMF, SVY, FER, SVR, and intergrowth structures of two or more thereof, more preferably selected from the group consisting of MFI, MEL, MWW, ITH, and IWR, and intergrowth structures of two or more thereof, more preferably selected from the group consisting of MFI, MEL, and intergrowth structures thereof, wherein the zeolitic material more preferably has an MFI-type framework structure.
  • the zeolitic material is a TS-1 zeolite.
  • the zeolitic material can optionally further comprise one or more metals selected from the group consisting of K, Zn, Cd, Sn, La, and Ba, including mixtures of two or more thereof, preferably from the group consisting of Zn, Cd, Sn, La, and Ba, including mixtures of two or more thereof, wherein the one or more metals are more preferably contained in the pores of the zeolitic material.
  • the zeolitic material consists of Ti, Si, and O, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.
  • the zeolitic material consists of Ti, Si, O, and H, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.
  • the zeolitic material has a crystallinity in the range of from 50 to 110 weight-%, preferably from 50 to 100 weight-%, more preferably from 75 to 100 weight-%, more preferably from 80 to 100 weight-%, and more preferably from 90 to 100 weight-%, wherein the crystallinity is preferably determined as described in Reference Example 1 .4.
  • the present invention also relates to a method for preparing a catalyst molding, preferably for preparing a catalyst molding according to any one of the embodiments disclosed herein, the method comprising
  • step (b) mixing the catalyst provided in step (a) with one or more binders;
  • step (c) optionally kneading of the mixture obtained in step (b);
  • step (d) molding of the mixture obtained in step (b) or (c) to obtain a precursor of the catalyst molding
  • step (g) calcining of the one or more catalyst moldings obtained in step (d), (e) or (f).
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts comprising Ti, Si, and O, and displaying a water adsorption (W), preferably determined according to Reference Example 1.1 , and a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably according to Reference Example 1.3; wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 10 to 75 mmol/mol, wherein the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2- activated catalyst:
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts comprising Ti, Si, and O
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a water adsorption in the range of from 1 to 10 wt.-%, preferably from 1 .5 to 9.5 wt.-%, more preferably from 2 to 9 wt.-%, more preferably from 2.5 to 8.5 wt.-%, more preferably from 3 to 8 wt.-%, more preferably from 3.2 to 7.9 wt.-%, more preferably from 3.5 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, more preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst in the range of from 150 to 1 ,000 mmol/mol, preferably from 100 to 800 mmol/mol, more preferably from 150 to 750 mmol/mol, more preferably from 200 to 700 mmol/mol, more preferably from 250 to 650 mmol/mol, more preferably from 300 to 600 mmol/mol, more preferably from 350 to 550 mmol/mol, and more preferably from 400 to 500 mmol/mol.
  • the catalyst is selected by calculating an activation factor (A) for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 11 to 65 mmol/mol, preferably from 13 to 55 mmol/mol, more preferably from 15 to 50 mmol/mol, more preferably from 18 to 45 mmol/mol, more preferably from 20 to 40 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 37 mmol/mol, more preferably from 23 to 35 mmol/mol, more preferably from 24 to 32 mmol/mol, and more preferably from 25 to 30 mmol/mol.
  • A activation factor
  • the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 2 min to 480 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 10 to 30 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 12 to 20 min, and more preferably from 14 to 16 min after having brought the catalyst into contact with H2 17 C>2, wherein more
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy in the range of from 125 to 750 mmol/mol, wherein the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a water adsorption in the range of from 1 to 7.9 wt.-%, more preferably from 3 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, more preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, more preferably determined according to Reference Example 1 .3, in the range of from 200 to 725 mmol/mol, preferably from 250 to 700 mmol/mol, more preferably from 300 to 680 mmol/mol, more preferably from 350 to 660 mmol/mol, more preferably from 400 to 640 mmol/mol, more preferably from 450 to 620 mmol/mol, and more preferably from 500 to 600 mmol/mol.
  • C concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy
  • T is in the range of from 75 to 165 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 85 min to 155 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst into contact with H2 17 C>2, wherein more preferably T is 120 min after having brought the catalyst into contact with H2 17 C>2.
  • the activation factor (A) is in the range of from 11 to 70 mmol/mol, preferably from 12 to 62 mmol/mol, more preferably in the range of from 13 to 60 mmol/mol, more preferably from 14 to 59 mmol/mol, more preferably from 16 to 54 mmol/mol, more preferably from 18 to 49 mmol/mol, more preferably from 20 to 44 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 34 mmol/mol, more preferably from 23 to 31 mmol/mol, and more preferably from 24 to 28 mmol/mol.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts comprising from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of B, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts comprising from 0 to 0.1 weight-%, preferably from 0 to 0.08 weight-%, of Na, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts comprising from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ge, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts comprising from 0 to 1 weight-%, more preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.2 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.009 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of C, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst among catalysts exhibiting a propylene oxide activity of at least 2.0 weight-%, more preferably in the range of from 3.0 to 15.0 weight-%, more preferably in the range of from 5.0 to 14.0 weight-%, more preferably in the range of from 9.0 to 13.0 weight-%, more preferably determined as described in Reference Example 1 .6.
  • the one or more binders in (b) are selected from the group consisting of inorganic binders, wherein the one or more binders more preferably comprise one or more sources of a metal oxide and/or of a metalloid oxide, more preferably one or more sources of a metal oxide and/or of a metalloid oxide selected from the group consisting of silica, alumina, titania, zirconia, lanthana, magnesia, and mixtures and/or mixed oxides of two or more thereof, more preferably from the group consisting of silica, alumina, titania, zirconia, magnesia, silica-alumina mixed oxides, silica-titania mixed oxides, silica-zirconia mixed oxides, silica-lanthana mixed oxides, silica-zirconia-lanthana mixed oxides, alumina-titania mixed oxides, alumina-zirconia mixed oxides, alumina-lanthana mixed oxide
  • step (b) further comprises mixing the zeolitic material and the one or more binders with a solvent system, wherein the solvent system comprises one or more solvents, wherein more preferably the solvent system comprises one or more hydrophilic solvents, the hydrophilic solvents preferably being selected from the group consisting of polar solvents, more preferably from the group consisting of polar protic solvents, wherein more preferably the solvent system comprises one or more polar protic solvents selected from the group consisting of water, alcohols, carboxylic acids, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C5 alcohols, C1-C5 carboxylic acids, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C4 alcohols, C1-C4 carboxylic acids, and mixtures of two or more thereof, more preferably from the group consisting of water, C1- C3 alcohols, C1-C3 carboxylic acids, and mixtures of two or more thereof, wherein
  • step (b) further comprises mixing the zeolitic material and the one or more binders with one or more agents, preferably one or more pore forming agents and/or lubricants and/or plasticizers, wherein the one or more agents comprise, preferably consist of, one or more of water, alcohols, organic polymers, carbohydrates, graphite, plant additives, and mixtures of two or more thereof, preferably one or more of water, alcohols, organic polymers, polysaccharides, carbohydrates, graphite, plant additives, and mixtures of two or more thereof, more preferably one or more of water, polymeric vinyl compounds, celluloses, cellulose derivatives, polymannoses, polymannose derivatives, starches, polyalkylene oxides, polystyrenes, polyacrylates, polymethacrylates, polyolefins, polyamides, polyesters, and mixtures of two or more thereof, more preferably one or more of water, polymeric vinyl compounds, polyalkylene oxides, polyacrylates, polyolefin
  • the method further comprises after (d) and prior to (e) drying the precursor of the catalyst molding obtained from (d), obtaining a dried precursor of the catalyst molding, wherein the method preferably further comprises calcining the dried precursor of the catalyst molding, wherein calcining is preferably performed at a temperature ranging from 350 to 850°C, more preferably from 400 to 700°C, more preferably from 450 to 650°C, and more preferably from 475 to 600°C.
  • the water treatment according to (e) is performed with a water containing solvent system and/or with an aqueous solution, wherein more preferably the hydrothermal treatment is performed with deionized water.
  • the water treatment according to (e) comprises a temperature of the mixture in the range of from 130 to 160 °C, preferably in the range of from 140 to 150 °C.
  • the water treatment according to (e) is carried out under autogenous pressure, preferably in an autoclave.
  • the water treatment according to (e) is carried out for 6 to 15 h, preferably for 7 to 10 h.
  • the weight ratio of the precursor of the catalyst molding obtained from (d) relative to the water is in the range of from 1 :25 to 1 :10, preferably in the range of from 1 :21 to 1 :14.
  • the water-treated precursor of the molding is separated from the mixture obtained from (d), wherein separating preferably comprises subjecting the mixture obtained from (d) to filtration or centrifugation, wherein more preferably, separating further comprises washing the water-treated precursor of the molding at least once with a liquid solvent system, wherein the liquid solvent system preferably comprises one or more of water, an alcohol, and a mixture of two or more thereof, wherein the water-treated precursor of the molding is more preferably washed with water.
  • the calcining according to (g) of the dried molding obtained in step (f) is performed at a temperature ranging from 350 to 850°C, more preferably from 400 to 700°C, more preferably from 450 to 650°C, and more preferably from 475 to 600°C.
  • the present invention also relates to a catalyst molding comprising a catalyst for hydrogen peroxide activation according to any one of the particular and preferred embodiments of the present invention, wherein the catalyst molding is preferably obtainable or obtained by a method according to any one of the particular and preferred embodiments of the present invention.
  • the present invention also relates to a process for the activation of hydrogen peroxide comprising:
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, and displaying a water adsorption (W), preferably determined according to Reference Example 1.1 , and a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably according to Reference Example 1.3; wherein the catalyst, which is comprised in the catalyst molding, is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 10 to 75 mmol/mol, wherein the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst:
  • providing the catalyst molding in (1) comprises selecting the catalyst among catalysts comprising Ti, Si, and O, wherein the catalyst, which is comprised in the catalyst molding, is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 1 to 10 wt.-%, more preferably from 1 .5 to 9.5 wt.-%, more preferably from 2 to 9 wt.-%, more preferably from 2.5 to 8.5 wt.-%, more preferably from 3 to 8 wt.-%, more preferably from 3.2 to 7.9 wt.-%, more preferably from 3.5 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%, and more preferably from 5 to 6 wt.-%.
  • providing the catalyst molding in (1 ) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, more preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst in the range of from 150 to 1 ,000 mmol/mol, preferably from 100 to 800 mmol/mol, more preferably from 150 to 750 mmol/mol, more preferably from 200 to 700 mmol/mol, more preferably from 250 to 650 mmol/mol, more preferably from 300 to 600 mmol/mol, more preferably from 350 to 550 mmol/mol, and more preferably from 400 to 500 mmol/mol.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts, it is preferred that the catalyst is selected by calculating an activation factor (A) for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 11 to 65 mmol/mol, preferably from 13 to 55 mmol/mol, more preferably from 15 to 50 mmol/mol, more preferably from 18 to 45 mmol/mol, more preferably from 20 to 40 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 37 mmol/mol, more preferably from 23 to 35 mmol/mol, more preferably from 24 to 32 mmol/mol, and more preferably from 25 to 30 mmol/mol.
  • the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 2 min to 480 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy in the range of from 125 to 750 mmol/mol, wherein the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts
  • providing the catalyst molding in (1) comprises selecting the catalyst among catalysts displaying a water adsorption in the range of from 1 to 7.9 wt.-%, more preferably from 3 to 7.5 wt.- %, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • providing the catalyst molding in (1 ) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, more preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts
  • providing the catalyst molding in (1) comprises selecting the catalyst among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, in the range of from 200 to 725 mmol/mol, preferably from 250 to 700 mmol/mol, more preferably from 300 to 680 mmol/mol, more preferably from 350 to 660 mmol/mol, more preferably from 400 to 640 mmol/mol, more preferably from 450 to 620 mmol/mol, and more preferably from 500 to 600 mmol/mol.
  • T is in the range of from 75 to 165 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 85 min to 155 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst into contact with H2 17 C>2, and more preferably from 119
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, wherein the catalyst is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts, it is preferred that the activation factor (A) is in the range of from 11 to 70 mmol/mol, preferably from 12 to 62 mmol/mol, more preferably in the range of from 13 to 60 mmol/mol, more preferably from 14 to 59 mmol/mol, more preferably from 16 to 54 mmol/mol, more preferably from 18 to 49 mmol/mol, more preferably from 20 to 44 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 34 mmol/mol, more preferably from 23 to 31 mmol/mol, and more preferably from 24 to 28 mmol/mol.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of B, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 0.1 weight-%, more preferably from 0 to 0.08 weight-%, of Na, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ge, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.2 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.009 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of C, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising a content of one or more of Fe, Co, Ni, and Cu, calculated as Fe20s, CO2O3, NiO, and CuO, respectively, in the range of from 0 to 0.1 weight-%, more preferably in the range of from 0 to 0.07 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.02 weight-%, based on the weight of the catalyst which is comprised in the catalyst molding.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising a content of one or more of Fe, Co, Ni, and Cu, calculated as the element, respectively, in the range of from 0 to 0.1 weight-%, more preferably in the range of from 0 to 0.07 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.02 weight-%, based on the weight of the catalyst which is comprised in the catalyst molding.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts exhibiting a propylene oxide activity of at least 2.0 weight-%, more preferably in the range of from 3.0 to 15.0 weight-%, more preferably in the range of from 5.0 to 14.0 weight-%, more preferably in the range of from 9.0 to 13.0 weight-%, preferably determined as described in Reference Example 1.6.
  • hydrogen peroxide is comprised in a liquid feed stream which is fed into the reactor, wherein the liquid feed stream further comprises one or more unsaturated organic compounds, more preferably with one or more olefins, more preferably with one or more C2-C5 alkenes, more preferably with one or more C2-C4 alkenes, more preferably with one or more C2 or C3 alkenes, more preferably propylene.
  • unsaturated organic compounds more preferably with one or more olefins, more preferably with one or more C2-C5 alkenes, more preferably with one or more C2-C4 alkenes, more preferably with one or more C2 or C3 alkenes, more preferably propylene.
  • the liquid feed stream further comprises a solvent system, wherein the solvent system comprises one or more solvents, wherein more preferably the solvent system comprises one or more hydrophilic solvents, the hydrophilic solvents more preferably being selected from the group consisting of polar solvents, more preferably from the group consisting of polar protic solvents, wherein more preferably the solvent system comprises one or more polar protic solvents selected from the group consisting of water, alcohols, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C5 alcohols, Ci to C5 ethers, Ci to C5 nitriles, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C4 alcohols, Ci to C5 ethers, Ci to C4 nitriles, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C4 alcohols, Ci to C5 ethers, Ci to C4 nitriles, and mixtures of two or more
  • the liquid feed stream further comprises a potassium-containing compound, preferably a potassium salt, more preferably one or more of dipotassium hydrogen phosphate and a potassium salt of etidronic acid.
  • a potassium-containing compound preferably a potassium salt, more preferably one or more of dipotassium hydrogen phosphate and a potassium salt of etidronic acid.
  • the liquid feed stream comprises hydrogen peroxide at a concentration in the range of from 1 to 75 weight-%, more preferably from 3 to 50 weight-%, 5 to 30 weight-%, more preferably from 7 to 25 weight-%, more preferably from 8 to 20 weight-%, more preferably from 9 to 15 weight-%, more preferably from 10 to 12 weight-%, based on the total weight of the liquid feed stream.
  • the liquid feed stream fed into the reactor in (2) has a temperature in the range of from 0 to 60 °C, more preferably from 25 to 50 0 C.
  • the liquid feed stream fed into the reactor in (2) is at a pressure in the range of from 5 to 100 bar, more preferably from 10 to 50 bar, more preferably from 15 to 25 bar. Furthermore, and independently thereof, it is preferred that contacting in (2) is conducted at a temperature in the range of from 10 to 100 °C, more preferably from 25 to 80 °C, more preferably from 30 to 75 °C, more preferably from 32 to 65 °C.
  • contacting in (2) is conducted at a pressure in the range of from 5 to 100 bar, more preferably from 10 to 50 bar, more preferably from 14 to 32 bar, more preferably from 15 to 25 bar, wherein the pressure is defined as the pressure at the exit of the reactor.
  • the catalyst molding loading in the reactor in (1 ) is in the range of from 0.05 to 5 IT 1 , preferably from 0.1 to 3 IT 1 , more preferably from 0.2 to 1 IT 1 , more preferably from 0.200 to 0.5 IT 1 , more preferably from 0.210 to 0.25 IT 1 , more preferably from 0.215 to 0.240 IT 1 , more preferably from 0.220 to 0.235 IT 1 , more preferably from 0.225 to 0.230 IT 1 , wherein the catalyst molding loading is defined as the ratio of the mass flow rate in kg/h of hydrogen peroxide contained in the liquid feed stream divided by the amount in kg of the catalyst molding comprised in the reactor in (1 ).
  • the process further comprises (3) removing an effluent stream from the reactor, the effluent stream comprising an oxidized organic compound, and preferably comprising an epoxidized organic compound, more preferably an alkylene oxide, more preferably an alkylene oxide selected from C2-C5 alkylene oxides, more preferably from C2-C4 alkylene oxides, more preferably from C2 or C3 alkylene oxides, more preferably from C3 alkylene oxides, wherein more preferably the effluent stream comprises propylene oxide.
  • the present invention also relates to the use of the catalyst molding according to any one of the particular and preferred embodiments of the present invention as a catalyst and/or catalyst component in a reaction involving one or more of C-0 bond formation, C-C bond formation and C-C bond conversion, and preferably as a catalyst and/or catalyst component in an isomerization reaction, in an ammoximation reaction, in an amination reaction, in a hydrocracking reaction, in an alkylation reaction, in an acylation reaction, in a reaction for the conversion of alkanes to olefins, or in a reaction for the conversion of one or more oxygenates to olefins and/or aromatics, in a reaction for the synthesis of hydrogen peroxide, in an aldol condensation reaction, in a reaction for the isomerization of epoxides, in a transesterification reaction, in a hydroxylation reaction, in a Baeyer-Villiger-type oxidation reaction, in a Dakin-type reaction,
  • the olefin is a C2-C10 alkene, more preferably a C2-C5 alkene, more preferably a C2-C4 alkene, more preferably ethylene or propylene, more preferably propylene.
  • the organic solvent is an organic epoxidation solvent, wherein more preferably the organic solvent is selected from the group consisting of Ci to C5 mono alcohol, Ci to C5 ether, Ci to C5 nitrile, and mixtures of two or more thereof, more preferably from the group consisting of tert-butanol, methanol, acetonitrile, methyl tert-bu- tyl ether (MTBE), and mixtures of two or more thereof.
  • the organic solvent is selected from the group consisting of Ci to C5 mono alcohol, Ci to C5 ether, Ci to C5 nitrile, and mixtures of two or more thereof, more preferably from the group consisting of tert-butanol, methanol, acetonitrile, methyl tert-bu- tyl ether (MTBE), and mixtures of two or more thereof.
  • the reaction mixture obtained in (A) comprises the additive, wherein the additive is more preferably selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, ammonium salt of an organic acid and mixtures of two or more thereof; wherein the additive more preferably comprises a potassium-containing compound, preferably a potassium salt, more preferably one or more of dipotassium hydrogen phosphate and a potassium salt of etidronic acid.
  • the additive is provided in (A) as an aqueous solution, wherein the aqueous solution may further comprise the hydrogen peroxide.
  • a catalyst molding for hydrogen peroxide activation wherein the catalyst molding comprises a catalyst for hydrogen peroxide activation, said catalyst comprising Ti, Si, and O, wherein the catalyst comprised in the catalyst molding displays a water adsorption (W), preferably determined according to Reference Example 1 .1 , a concentration (C) of bridging p 2 n 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, and an activation factor (A) according to formula I, wherein the activation factor is in the range of from 10 to 75 mmol/mol; wherein in accordance with formula I, the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2
  • the catalyst molding further comprises one or more oxidic binders, wherein the one or more oxidic binders are preferably selected from the group consisting of inorganic binders, wherein the one or more binders more preferably comprise one or more sources of a metal oxide and/or of a metalloid oxide, more preferably one or more sources of a metal oxide and/or of a metalloid oxide selected from the group consisting of silica, alumina, titania, zirconia, lanthana, magnesia, and mixtures and/or mixed oxides of two or more thereof, more preferably from the group consisting of silica, alumina, titania, zirconia, magnesia, silica-alumina mixed oxides, sil- ica-titania mixed oxides, silica-zirconia mixed oxides, silica-lanthana mixed oxides, silica- zirconia-lanthana mixed
  • A W x C (I).
  • the catalyst molding of embodiment 7 or 8, wherein the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst molding into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst molding into contact with H2 17 C>2, preferably from 2 min to 480 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 10 to 30 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 12 to 20 min after having brought the catalyst molding into contact with H2 17 C>2, and more
  • the catalyst molding of embodiment 7, displaying a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst molding in the range of from 100 to 1 ,000 mmol/mol, wherein the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2- activated catalyst molding as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst molding into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • the catalyst molding of embodiment 11 displaying a concentration of bridging p 2 q 2 - peroxo species per Ti in the H2O2-activated catalyst molding as determined by quantitative 1 7 O NMR spectroscopy, preferably determined according to Reference Example 1 .2, in the range of from 200 to 900 mmol/mol, preferably from 300 to 800 mmol/mol, more preferably from 380 to 750 mmol/mol, more preferably from 420 to 700 mmol/mol, more preferably from 450 to 650 mmol/mol.
  • T is in the range of from 75 to 165 min after having brought the catalyst molding into contact with H2 17 C>2, preferably from 85 min to 155 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst molding into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst molding into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst molding into contact with H2 17 C>2, wherein more preferably T is 120 min after having brought the catalyst molding into contact with H2 17 C>2.
  • a sodium content calculated as Na2O
  • the catalyst molding of embodiment 28, wherein the catalyst comprised in the catalyst molding displays a water adsorption in the range of from 1 to 7.9 wt.-%, preferably from 3 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • the catalyst molding of embodiment 29, wherein the catalyst comprised in the catalyst molding displays a water adsorption in the range of from 3 to 6.5 wt.-%, preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • the catalyst molding of embodiment 28 to 30, wherein the catalyst comprised in the catalyst molding displays a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2- activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, in the range of from 200 to 725 mmol/mol, preferably from 250 to 700 mmol/mol, more preferably from 300 to 680 mmol/mol, more preferably from 350 to 660 mmol/mol, more preferably from 400 to 640 mmol/mol, more preferably from 450 to 620 mmol/mol, and more preferably from 500 to 600 mmol/mol.
  • T is in the range of from 75 to 165 min after having brought the catalyst into contact with H2 17 C>2, preferably from 85 min to 155 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst into contact with H2 17 C>2, wherein more preferably T is 120 min after having brought the catalyst into contact with H2 17 C>2.
  • the catalyst molding of any one of embodiments 1 to 35, wherein the catalyst comprised in the catalyst molding comprises from 0.2 to 5 weight-%, preferably in the range of from 0.5 to 4 weight-%, more preferably in the range of from 0.7 to 3 weight-%, more preferably of from 0.7 to 2.5 weight-%, preferably from 0.8 to 2.0 weight-%, more preferably from 1 .0 to 1 .9 weight-%, more preferably from 1 .0 to 1 .8 weight-%, more preferably from 1 .1 to 1 .3 weight-%, of Ti, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst molding of any one of embodiments 1 to 36, wherein the catalyst comprised in the catalyst molding comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of B, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst molding of any one of embodiments 1 to 38, wherein the catalyst comprised in the catalyst molding comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ge, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst molding of any one of embodiments 1 to 39, wherein the catalyst comprised in the catalyst molding comprises from 0 to 1 weight-%, preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.2 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.009 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of C, calculated as the element and based on the total weight of the catalyst comprised in the catalyst molding.
  • the catalyst molding of any one of embodiments 1 to 47, wherein the catalyst comprised in the catalyst molding comprises, preferably consists of, a zeolitic material having a framework structure comprising Si, Ti, and O.
  • the catalyst molding of embodiment 48, wherein the zeolitic material has an Si : Ti molar ratio in the range of from 1 to 250, preferably in the range of from 10 to 150, more preferably in the range of from 20 to 95, more preferably in the range of from 30 to 75, more preferably in the range of from 35 to 70, more preferably in the range of from 40 to 65, more preferably in the range of from 45 to 60, more preferably in the range of from 50 to 55.
  • the zeolitic material has a framework structure type selected from the group consisting of MFI, MEL, MWW, ITH, IWR, IMF, SVY, FER, SVR, and intergrowth structures of two or more thereof, preferably selected from the group consisting of MFI, MEL, MWW, ITH, and IWR, and intergrowth structures of two or more thereof, more preferably selected from the group consisting of MFI, MEL, and intergrowth structures thereof, wherein the zeolitic material more preferably has an MFI-type framework structure.
  • the zeolitic material further comprises one or more metals selected from the group consisting of K, Zn, Cd, Sn, La, and Ba, including mixtures of two or more thereof, preferably from the group consisting of Zn, Cd, Sn, La, and Ba, including mixtures of two or more thereof, wherein the one or more metals are preferably contained in the pores of the zeolitic material.
  • a method for preparing a catalyst molding preferably for preparing a catalyst molding according to any one of embodiments 1 to 55, comprising
  • step (b) mixing the catalyst provided in step (a) with one or more binders;
  • step (c) optionally kneading of the mixture obtained in step (b);
  • step (d) molding of the mixture obtained in step (b) or (c) to obtain a precursor of the catalyst molding
  • step (g) calcining of the one or more catalyst moldings obtained in step (d), (e) or (f).
  • the method of embodiment 56 or 57, wherein providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 1 to 10 wt.-%, more preferably from 1 .5 to 9.5 wt.- %, more preferably from 2 to 9 wt.-%, more preferably from 2.5 to 8.5 wt.-%, more preferably from 3 to 8 wt.-%, more preferably from 3.2 to 7.9 wt.-%, more preferably from 3.5 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-acti- vated catalyst in the range of from 150 to 1 ,000 mmol/mol, more preferably from 100 to 800 mmol/mol, more preferably from 150 to 750 mmol/mol, more preferably from 200 to 700 mmol/mol, more preferably from 250 to 650 mmol/mol, more preferably from 300 to 600 mmol/mol, more preferably from 350 to 550 mmol/mol, and more preferably from 400 to 500 mmol/mol.
  • any one of embodiments 56 to 60, wherein the catalyst, which is comprised in the catalyst molding, is selected by calculating an activation factor (A) for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 11 to 65 mmol/mol, more preferably from 13 to 55 mmol/mol, more preferably from 15 to 50 mmol/mol, more preferably from 18 to 45 mmol/mol, more preferably from 20 to 40 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 37 mmol/mol, more preferably from 23 to 35 mmol/mol, more preferably from 24 to 32 mmol/mol, and more preferably from 25 to 30 mmol/mol.
  • A activation factor
  • the concentration (C) of bridging p 2 n 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst, which is comprised in the catalyst molding, into contact with H2 17 C>2, more preferably from 2 min to 480 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 10 to 30 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 12 to 20 min after having brought the catalyst into contact with H2
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy in the range of from 125 to 750 mmol/mol, wherein the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 1 to 7.9 wt.-%, preferably from 3 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • the method of embodiment 64, wherein providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, in the range of from 200 to 725 mmol/mol, preferably from 250 to 700 mmol/mol, more preferably from 300 to 680 mmol/mol, more preferably from 350 to 660 mmol/mol, more preferably from 400 to 640 mmol/mol, more preferably from 450 to 620 mmol/mol, and more preferably from 500 to 600 mmol/mol.
  • C concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy
  • T is in the range of from 75 to 165 min after having brought the catalyst into contact with H2 17 C>2, preferably from 85 min to 155 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst into contact with H2 17 C>2, wherein more preferably T is 120 min after having brought the catalyst into contact with H2 17 C>2.
  • activation factor (A) is in the range of from 11 to 70 mmol/mol, preferably from 12 to 62 mmol/mol, more preferably in the range of from 13 to 60 mmol/mol, more preferably from 14 to 59 mmol/mol, more preferably from 16 to 54 mmol/mol, more preferably from 18 to 49 mmol/mol, more preferably from 20 to 44 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 34 mmol/mol, more preferably from 23 to 31 mmol/mol, and more preferably from 24 to 28 mmol/mol.
  • any one of embodiments 56 to 68, wherein providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of B, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0.1 weight-%, preferably from 0 to 0.08 weight-%, of Na, calculated as the element and based on the total weight of the catalyst.
  • any one of embodiments 56 to 70, wherein providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ge, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.2 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.009 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of C, calculated as the element and based on the total weight of the catalyst.
  • providing the catalyst in (a) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts exhibiting a propylene oxide activity of at least 2.0 weight-%, preferably in the range of from 3.0 to 15.0 weight-%, more preferably in the range of from 5.0 to 14.0 weight-%, more preferably in the range of from 9.0 to 13.0 weight-%, preferably determined as described in Reference Example 1.6.
  • the one or more binders in (b) are selected from the group consisting of inorganic binders, wherein the one or more binders preferably comprise one or more sources of a metal oxide and/or of a metalloid oxide, more preferably one or more sources of a metal oxide and/or of a metalloid oxide selected from the group consisting of silica, alumina, titania, zirconia, lanthana, magnesia, and mixtures and/or mixed oxides of two or more thereof, more preferably from the group consisting of silica, alumina, titania, zirconia, magnesia, silica-alumina mixed oxides, silica-titania mixed oxides, silica-zirconia mixed oxides, silica-lanthana mixed oxides, silica-zirconia- lanthana mixed oxides, alumina-titania mixed oxides, alumina-zirconia mixed oxide
  • step (b) further comprises mixing the zeolitic material and the one or more binders with a solvent system, wherein the solvent system comprises one or more solvents, wherein preferably the solvent system comprises one or more hydrophilic solvents, the hydrophilic solvents preferably being selected from the group consisting of polar solvents, more preferably from the group consisting of polar protic solvents, wherein more preferably the solvent system comprises one or more polar protic solvents selected from the group consisting of water, alcohols, carboxylic acids, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C5 alcohols, C1-C5 carboxylic acids, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C4 alcohols, C1-C4 carboxylic acids, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C3 alcohols, C1-C3 carboxylic
  • step (b) further comprises mixing the zeolitic material and the one or more binders with one or more agents, preferably with one or more pore forming agents and/or lubricants and/or plasticizers, wherein the one or more agents comprise, preferably consist of, one or more of water, alcohols, organic polymers, carbohydrates, graphite, plant additives, and mixtures of two or more thereof, preferably one or more of water, alcohols, organic polymers, polysaccharides, carbohydrates, graphite, plant additives, and mixtures of two or more thereof, more preferably one or more of water, polymeric vinyl compounds, celluloses, cellulose derivatives, polymannoses, polymannose derivatives, starches, polyalkylene oxides, polystyrenes, polyacrylates, polymethacrylates, polyolefins, polyamides, polyesters, and mixtures of two or more thereof, more preferably one or more of water, polymeric vinyl compounds, polyalkylene oxide
  • any one of embodiments 56 to 76 further comprising after (d) and prior to (e) drying the precursor of the catalyst molding obtained from (d), obtaining a dried precursor of the catalyst molding, wherein the method preferably further comprises calcining the dried precursor of the catalyst molding, wherein calcining is preferably performed at a temperature ranging from 350 to 850°C, more preferably from 400 to 700°C, more preferably from 450 to 650°C, and more preferably from 475 to 600°C.
  • any one of embodiments 56 to 82 wherein after (d) and prior to (e), preferably after the drying as defined in claim 77, more preferably after the calcining as defined in claim 77, the water-treated precursor of the molding is separated from the mixture obtained from (d), wherein separating preferably comprises subjecting the mixture obtained from (d) to filtration or centrifugation, wherein more preferably, separating further comprises washing the water-treated precursor of the molding at least once with a liquid solvent system, wherein the liquid solvent system preferably comprises one or more of water, an alcohol, and a mixture of two or more thereof, wherein the water-treated precursor of the molding is more preferably washed with water.
  • step (e) The method of any one of embodiments 56 to 83, wherein the calcining according to (g) of the dried catalyst molding obtained in step (e) is performed at a temperature ranging from 350 to 850°C, preferably from 400 to 700°C, more preferably from 450 to 650°C, and more preferably from 475 to 600°C.
  • a catalyst molding obtainable or obtained by a method according to any one of embodiments 56 to 84.
  • a process for the activation of hydrogen peroxide comprising:
  • the process of embodiment 86, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising Ti, Si, and O, and displaying a water adsorption (W), preferably determined according to Reference Example 1.1 , and a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably according to Reference Example 1 .3; wherein the catalyst, which is comprised in the catalyst molding, is selected by calculating an activation factor (A) in accordance with formula I for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 10 to 75 mmol/mol, wherein the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst:
  • A W x C (I). 88.
  • the process of embodiment 87, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 1 to 10 wt.-%, preferably from 1 .5 to 9.5 wt.-%, more preferably from 2 to 9 wt.-%, more preferably from 2.5 to 8.5 wt.-%, more preferably from 3 to 8 wt.-%, more preferably from 3.2 to 7.9 wt.-%, more preferably from 3.5 to 7.5 wt.-%, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%, and more preferably from 5 to 6 wt.-%.
  • the process of embodiment 88, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst in the range of from 150 to 1 ,000 mmol/mol, preferably from 100 to 800 mmol/mol, more preferably from 150 to 750 mmol/mol, more preferably from 200 to 700 mmol/mol, more preferably from 250 to 650 mmol/mol, more preferably from 300 to 600 mmol/mol, more preferably from 350 to 550 mmol/mol, and more preferably from 400 to
  • any one of embodiments 87 to 90, wherein the catalyst, which is comprised in the catalyst molding, is selected by calculating an activation factor (A) for each of the catalysts, and selecting a catalyst displaying an activation factor in the range of from 11 to 65 mmol/mol, preferably from 13 to 55 mmol/mol, more preferably from 15 to 50 mmol/mol, more preferably from 18 to 45 mmol/mol, more preferably from 20 to 40 mmol/mol, more preferably from 21 to 39 mmol/mol, more preferably from 22 to 37 mmol/mol, more preferably from 23 to 35 mmol/mol, more preferably from 24 to 32 mmol/mol, and more preferably from 25 to 30 mmol/mol.
  • A activation factor
  • the concentration (C) of bridging p 2 n 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 1 7 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst, which is comprised in the catalyst molding, into contact with H2 17 C>2, wherein T is in the range of from 1 to 720 min after having brought the catalyst into contact with H2 17 C>2, preferably from 2 min to 480 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 4 to 240 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 6 to 120 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 8 to 60 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 10 to 30 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 12 to 20 min after having brought the catalyst into
  • providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy in the range of from 125 to 750 mmol/mol, wherein the concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy is the concentration which is determined at a time point T after having brought the catalyst into contact with H2 17 C>2, wherein T is in the range of from 65 to 175 min.
  • the process of embodiment 93, wherein providing the catalyst molding in (1 ) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 1 to 7.9 wt.-%, preferably from 3 to 7.5 wt.- %, more preferably from 4 to 7 wt.-%, more preferably from 4.5 to 6.5 wt.-%.
  • the process of embodiment 94, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a water adsorption in the range of from 3 to 6.5 wt.-%, preferably from 3.2 to 4.5 wt.-%, more preferably from 3.4 to 4.1 wt.-%.
  • the process of embodiment 93 to 95, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts displaying a concentration (C) of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy, preferably determined according to Reference Example 1 .3, in the range of from 200 to 725 mmol/mol, preferably from 250 to 700 mmol/mol, more preferably from 300 to 680 mmol/mol, more preferably from 350 to 660 mmol/mol, more preferably from 400 to 640 mmol/mol, more preferably from 450 to 620 mmol/mol, and more preferably from 500 to 600 mmol/mol.
  • C concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst as determined by quantitative 17 O NMR spectroscopy
  • T is in the range of from 75 to 165 min after having brought the catalyst into contact with H2 17 C>2, preferably from 85 min to 155 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 95 to 145 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 105 to 135 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 112 to 128 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 116 to 124 min after having brought the catalyst into contact with H2 17 C>2, more preferably from 118 to 122 min after having brought the catalyst into contact with H2 17 C>2, and more preferably from 119 to 121 min after having brought the catalyst into contact with H2 17 C>2, wherein more preferably T is 120 min after having brought the catalyst into contact with H2 17 C>2.
  • the activation factor (A) is in the range of from 11 to 70 mmol/mol, preferably from 12 to 62 mmol/mol, more preferably in the range of from 13 to 60 mmol/mol, more preferably from 14 to 59 mmol/mol, more preferably from 16 to 54 mmol/mol, more preferably
  • any one of embodiments 86 to 98, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of B, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • the process of any one of embodiments 86 to 100, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ge, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • any one of embodiments 86 to 101 , wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising from 0 to 1 weight-%, preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.2 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.009 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of C, calculated as the element and based on the total weight of the catalyst, which is comprised in the catalyst molding.
  • any one of embodiments 86 to 102, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising a content of one or more of Fe, Co, Ni, and Cu, calculated as Fe20s, CO2O3, NiO, and CuO, respectively, in the range of from 0 to 0.1 weight-%, preferably in the range of from 0 to 0.07 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.02 weight-%, based on the weight of the catalyst which is comprised in the catalyst molding.
  • any one of embodiments 86 to 102, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts comprising a content of one or more of Fe, Co, Ni, and Cu, calculated as the element, respectively, in the range of from 0 to 0.1 weight-%, preferably in the range of from 0 to 0.07 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.02 weight-%, based on the weight of the catalyst which is comprised in the catalyst molding.
  • any one of embodiments 86 to 104, wherein providing the catalyst molding in (1) comprises selecting the catalyst, which is comprised in the catalyst molding, among catalysts exhibiting a propylene oxide activity of at least 2.0 weight-%, preferably in the range of from 3.0 to 15.0 weight-%, more preferably in the range of from 5.0 to 14.0 weight-%, more preferably in the range of from 9.0 to 13.0 weight-%, preferably determined as described in Reference Example 1 .6.
  • the liquid feed stream further comprises a solvent system, wherein the solvent system comprises one or more solvents, wherein preferably the solvent system comprises one or more hydrophilic solvents, the hydrophilic solvents preferably being selected from the group consisting of polar solvents, more preferably from the group consisting of polar protic solvents, wherein more preferably the solvent system comprises one or more polar protic solvents selected from the group consisting of water, alcohols, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C5 alcohols, Ci to C5 ethers, Ci to C5 nitriles, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C4 alcohols, Ci to C5 ethers, Ci to C4 nitriles, and mixtures of two or more thereof, more preferably from the group consisting of water, C1-C4 alcohols, Ci to C5 ethers, Ci to C4 nitriles, and mixtures of two or more thereof,
  • liquid feed stream comprises hydrogen peroxide at a concentration in the range of from 1 to 75 weight-%, preferably from 3 to 50 weight-%, 5 to 30 weight-%, more preferably from 7 to 25 weight-%, more preferably from 8 to 20 weight-%, more preferably from 9 to 15 weight-%, more preferably from 10 to 12 weight-%, based on the total weight of the liquid feed stream.
  • the catalyst molding loading in the reactor in (1 ) is in the range of from 0.05 to 5 IT 1 , preferably from 0.1 to 3 IT 1 , more preferably from 0.2 to 1 IT 1 , more preferably from 0.200 to 0.5 IT 1 , more preferably from 0.210 to 0.25 IT 1 , more preferably from 0.215 to 0.240 IT 1 , more preferably from 0.220 to 0.235 IT 1 , more preferably from 0.225 to 0.230 IT 1 , wherein the catalyst molding loading is defined as the ratio of the mass flow rate in kg/h of hydrogen peroxide contained in the liquid feed stream divided by the amount in kg of the catalyst molding comprised in the reactor in (1 ).
  • catalyst molding according to any one of embodiments 1 to 55 and 85 as a catalyst and/or catalyst component in a reaction involving one or more of C-0 bond formation, C-C bond formation and C-C bond conversion, and preferably as a catalyst and/or catalyst component in an isomerization reaction, in an ammoximation reaction, in an amination reaction, in a hydrocracking reaction, in an alkylation reaction, in an acylation reaction, in a reaction for the conversion of alkanes to olefins, or in a reaction for the conversion of one or more oxygenates to olefins and/or aromatics, in a reaction for the synthesis of hydrogen peroxide, in an aldol condensation reaction, in a reaction for the isomerization of epoxides, in a transesterification reaction, in a hydroxylation reaction, in a Baeyer-Vil- liger-type oxidation reaction, in a Dakin-type reaction, or in an epoxidation reaction, in
  • the olefin is a C2-C10 alkene, preferably a C2-C5 alkene, more preferably a C2-C4 alkene, more preferably ethylene or propylene, more preferably propylene; and/or, preferably and, wherein the organic solvent is an organic epoxidation solvent, wherein preferably the organic solvent is selected from the group consisting of Ci to C5 mono alcohol, Ci to C5 ether, Ci to C5 nitrile, and mixtures of two or more thereof, more preferably from the group consisting of tert-butanol, methanol, acetonitrile, methyl tert-butyl ether (MTBE), and mixtures of two or more thereof; and/or, preferably and, wherein the reaction mixture obtained in (A) preferably comprises the additive, wherein the additive is more
  • the present invention is further illustrated by the following examples, comparative examples and reference examples.
  • Water uptake by the sample was measured as the increase in weight over that of the dry sample.
  • an adsorption curve was measured by increasing the relative humidity (RH) to which the sample was exposed and measuring the water uptake by the sample at equilibrium.
  • the RH was increased with a step of 10 % from 5 to 85 % and at each step the system controlled the RH and monitored the sample weight until reaching the equilibrium conditions and recording the weight uptake.
  • the total adsorbed water amount by the sample was taken after the sample was exposed to 85 % RH and expressed as weight percent relative to the weight of the dried sample.
  • the RH was decreased from 85 % to 5 % with a step of 10 % and the change in the weight of the sample (water uptake) was monitored and recorded.
  • Ti K edge XANES X-ray absorption near edge structure spectra were recorded at the European Synchrotron Radiation Facility (Grenoble, France). The X-ray beam was monochroma- tized using a liquid nitrogen cooled Si(111) monochromator. A calibration of the energy was performed using Ti reference foil (Ti K-edge position at 4966 eV). The XAS K-edge measurements were carried out with a fluorescent scheme of detection using a silicon drift diode with associated digital electronics. All samples were measured as pressed pellets. Ti K edge XANES is highly sensitive to the local coordination sphere of Ti. Characteristic features can be observed both in the pre-edge and whiteline regions, respectively.
  • anatase showed pre-edge features at 4969 eV, 4971 eV, 4972 eV and 4974 eV, respectively and a sharp first whiteline feature at 4987 eV.
  • Rutile showed pre-edge features at 4969 eV, 4971 eV and 4974 eV, respectively, a moderate first whiteline feature at 4987 eV and a more pronounced feature at 4992 eV.
  • titanosilicalite where all titanium is incorporated into the framework and in tetrahedral geometry, only one distinct feature at 4970 eV was observed in the pre-edge region and none in the whiteline region.
  • Reference Example 1.3 Determination of the concentration of bridging p 2 q 2 -peroxo species in an HzOz-activated catalyst via 17 O NMR spectroscopy
  • a TS-1 sample with 17 O-labelled H2O2 was prepared by impregnating 25 mg of a TS-1 zeolite with one molar equivalent (with respect to Ti) of a 1 .6 M aqueous solution of 17 O-labelled H2O2. The samples were left to equilibrate for 15 min or 2 h before spectroscopic measurements.
  • a sample was prepared by impregnating 25 mg of a molding comprising a TS-1 zeolite with one molar equivalent (with respect to Ti) of a 1.1 M aqueous solution of 17 O-labelled H2O2. The samples were left to equilibrate for 15 min or 2 h before spectroscopic measurements.
  • the initial guess for each component was based on the previously DFT calculated NMR parameters in C. P. Gordon et aL, Nature 2020, 586, 708-713, and the lineshape parameters of each species was optimized to converge to a best fit that provides the ratio of each species. Based on said DFT calculations the observed 17 O NMR signals were assigned. The respective concentrations were obtained by multiplication of these ratios with the initial concentration (1.6 M or 1 .1 M, respectively) of the aqueous stock solution of H2 17 C>2 that was used for the wet impregnation.
  • the concentration of bridging p 2 q 2 -peroxo species in a H2 17 C>2-activated sample was calculated based on the value for the rel. bridging p 2 q 2 -peroxo concentration according to the following calculation:
  • Reference Example 1.4 X-ray powder diffraction and determination of the crystallinity
  • X-ray diffraction data are collected on a CuKa Bragg-Brentano Bruker D8 Advance Series II diffractometer.
  • the samples were ground using an IKA Tube Mill with 10000 U/min and then pressed into a standard flat sample holder provided by Bruker AXS GmbH for Bragg-Brentano geometry data collection.
  • the flat surface was achieved using a glass plate to compress and flatten the sample powder.
  • the angular range is 5°-50° (20) with a step width of 0.02° (20).
  • Acquisition time is optimised to ensure that the highest intensity signal has at least 200‘000 counts.
  • the divergence slit is set to 0.3° opening angle.
  • the total crystallinity is determined using a Rietveld based method as described by I. C.
  • the amorphous content is modelled by collecting scattering data on an amorphous silica compound, obtained by drying colloidal silica (Ludox® AS40, dried at 120°C).
  • an amorphous silica compound obtained by drying colloidal silica (Ludox® AS40, dried at 120°C).
  • the intensities are fit to the pure material.
  • the crystallite size (LVol IB) of 0.6 ensures a good fit to the broad diffraction signals of amorphous material.
  • the BET specific surface area and the micropore volume were determined via nitrogen physisorption at 77 K according to the method disclosed in DIN ISO 9277 from 2014.
  • the catalysts in particular catalyst powders
  • aqueous hydrogen peroxide solution (30 weight-%) to yield propylene oxide.
  • 0.5 g of a catalyst sample were introduced together with 45 ml of methanol in a glass autoclave, which was cooled to -25 °C.
  • 20 ml of liquid propylene was pressed into the glass autoclave and the glass autoclave was heated to 0 °C.
  • 18 g of an aqueous hydrogen peroxide solution (30 weight-% in water) were introduced into the glass autoclave.
  • the propylene oxide content of the liquid phase was the result of the PO test, i.e. the propylene oxide activity of the catalyst.
  • the moldings were tested in a steel autoclave by reaction of propylene with an aqueous hydrogen peroxide solution (30 weight-%) to yield propylene oxide.
  • 0.625 g of the molding were introduced together with 79.2 g of methanol in a steel autoclave.
  • 23 ml of liquid propylene was pressed into the steel autoclave and the steel autoclave was heated to 40 °C.
  • 22.1 g of an aqueous hydrogen peroxide solution (30 weight-% in water) were introduced into the steel autoclave followed by a further 9 g of methanol.
  • the pressure was gently released, and the liquid phase was analyzed by gas chromatography with respect to its propylene oxide content.
  • the k80-test was designed as a semi-quantitative experiment to assess the rate of decomposition of H2O2 by TS-1 and similar titanium containing zeolites. It allows to quantitatively determine the effect of different catalyst treatments on the decomposition of H2O2.
  • the probes were analysed for H2O2 content by using a standard cerimetric titration. It was advisable to analyse the probes as soon as possible after they are collected. In order to ensure a good precision, the amount of titrating solution used should be at least 5 ml. If necessary, a larger amount of probe had to be weighed in.
  • the natural logarithm of the H2O2 concentration was plotted against time. Using least squares methods, the slope is extracted. This slope was the pseudo-first order decay rate of H2O2 in the presence of the catalyst (in h’ 1 ) and was called the k80 value.
  • the crush strength as referred to in the context of the present invention is to be understood as having been determined via a crush strength test machine Z2.5/TS1S, supplier Zwick GmbH & Co., D-89079 Ulm, Germany.
  • a crush strength test machine Z2.5/TS1S supplier Zwick GmbH & Co., D-89079 Ulm, Germany.
  • Register 1 Carbon I Technology- shandbuch fur die Material-Prufmaschine Z2.5/TS1S
  • the machine was equipped with a fixed horizontal table on which the strand was positioned, with the longitudinal axis of the strand parallel to the horizontal table.
  • the apparatus was operated with a preliminary force of 0.5 N , a shear rate under preliminary force of 10 mm/min and a subsequent testing rate of 1.6 mm/min.
  • the vertically movable plunger was connected to a load cell for force pickup and, during the measurement, moved toward the fixed turntable on which the molding (strand) to be investigated is positioned, thus actuating the strand against the table.
  • the plunger was applied to the strands with the short edge of the plunger perpendicularly to the longitudinal axis of the strands. With said machine, a given strand as described below was subjected to an increasing force via the plunger until a break occurs. The force for breaking was referred to as the crushing strength of the strand.
  • Controlling the experiment was carried out by means of a computer which registered and evaluated the results of the measurements.
  • the values obtained were the mean value of the measurements for 25 strands in each case.
  • the obtained mean values are also referred to herein as average crush strength.
  • the temperature-programmed desorption of ammonia was conducted in an automated chemisorption analysis unit (Micromeritics AutoChem II 2920) having a thermal conductivity detector. Continuous analysis of the desorbed species was accomplished using an online mass spectrometer (OmniStar QMG200 from Pfeiffer Vacuum). The sample (0.1 g) was introduced into a quartz tube and analysed using the program described below. The temperature was measured by means of a Ni/Cr/Ni thermocouple immediately above the sample in the quartz tube. For the analyses, He of purity 5.0 was used. Before any measurement, a blank sample was analysed for calibration.
  • Preparation Commencement of recording; one measurement per second. Wait for 10 minutes at 25 °C and a He flow rate of 30 cm 3 /min (room temperature (about 25 °C) and 1 atm); heat up to 600 °C at a heating rate of 20 K/min; hold for 10 minutes. Cool down under a He flow (30 cm 3 /min) to 100 °C at a cooling rate of 20 K/min (furnace ramp temperature); Cool down under a He flow (30 cm 3 /min) to 100 °C at a cooling rate of 3 K/min (sample ramp temperature).
  • NH3-TPD Commencement of recording; one measurement per second. Heat up under a He flow (flow rate: 30 cm 3 /min) to 600 °C at a heating rate of 10 K/min; hold for 30 minutes.
  • the activation factor (A) was calculated based thereon according to formula I, wherein in accordance with formula I, the activation factor is the multiplication product of the water adsorption and the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated zeolitic material:
  • the total pore volume was determined via intrusion mercury porosimetry according to DIN 66133 from 1993.
  • Example 1 Preparation of a TS-1 catalyst in accordance with the present invention
  • tetraethylorthosilicate TEOS
  • TEOTi tetraethylorthotitanate
  • a solution of 300 g de-ionized water and 220 g aqueous tetrapropylammonium hydroxide (TPAOH; 40 weight-% in water) was added under stirring (200 rpm).
  • TPAOH aqueous tetrapropylammonium hydroxide
  • the resulting mixture had a pH of 13.81 , determined with a pH sensitive glass electrode.
  • the mixture was hydrolyzed at room temperature for 60 min during which the temperature rose to 60 °C.
  • the mixture had a pH of 12.91 , determined with a pH sensitive glass electrode, then.
  • the ethanol was distilled off until the sump reached a temperature of 95 °C. 546 g of distillate was obtained from distillation.
  • the synthesis gel was then cooled to 40 °C under stirring and 546 g de-ionized water added thereto.
  • the resulting mixture had a pH of 11 .91 , determined with a pH sensitive glass electrode.
  • the synthesis gel was then transferred into an autoclave.
  • the synthesis gel was heated under stirring in the autoclave to a temperature of 175 °C and stirred at said temperature for 16 h under autogenous pressure.
  • the pressure was in the range of from 8.4 to 11 .9 bar(abs).
  • the resulting suspension was then worked-up. To this effect, the resulting suspension was diluted with de-ionized water, wherein the weight ratio of the suspension to de-ionized water was 1 :1.
  • about 150 g nitric acid (10 weight-% in water) were added and the resulting mixture had a pH of 7.53.
  • the obtained solids were filtered off and washed three times with de-ionized water (each time 1000 ml de-ionized water were used).
  • the solids were dried in an oven in air at 120 °C for 4 h and then calcined in air at 490 °C for 5 h, wherein the heating rate for calcining was 2 °C
  • the resulting product had a Si content of 44 weight-%, a Ti content of 0.52 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the resulting product was 443 m 2 /g determined according to Reference Example 1.5, and the water adsorption 7.5 wt.-% determined according to Reference Example 1.1.
  • the crystallinity was 96 % and no anatase was detectable by X-ray diffraction, as determined according to Reference Example 1.4.
  • TEOS tetraethylorthosilicate
  • TEOTi 7.5 g tetraethylorthotitanate
  • TPAOH aqueous tetrapropylammonium hydroxide
  • the mixture was hydrolyzed at room temperature for 60 min during which the temperature rose to 60 °C.
  • the mixture had a pH of 12.71 , determined with a pH sensitive glass electrode, then.
  • the ethanol was distilled off until the sump reached a temperature of 95 °C. 548 g of distillate was obtained from distillation.
  • the synthesis gel was then cooled to 40 °C under stirring and 548 g de-ionized water added thereto.
  • the resulting mixture had a pH of 12.01 , determined with a pH sensitive glass electrode.
  • the synthesis gel was then transferred into an autoclave.
  • the synthesis gel was heated under stirring in the autoclave to a temperature of 175 °C and stirred at said temperature for 16 h under autogenous pressure.
  • the pressure was in the range of from 8.2 to 11.4 bar(abs).
  • the resulting suspension was then worked-up. To this effect, the resulting suspension was diluted with de-ionized water, wherein the weight ratio of the suspension to de-ionized water was 1 :1.
  • about 155 g nitric acid (10 weight-% in water) were added and the resulting mixture had a pH of 7.28, determined with a pH sensitive glass electrode.
  • the obtained solids were filtered off and washed three times with de-ionized water (each time 1000 ml de-ionized water were used). Subsequently, the solids were dried in an oven in air at 120 °C for 4 h and then calcined in air at 490 °C for 5 h, wherein the heating rate for calcining was 2 °C/min.
  • the resulting product had a Si content of 43 weight-%, a Ti content of 1.0 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the resulting product was 450 m 2 /g determined according to Reference Example 1.5, and the water adsorption 8.45 wt.-% determined according to Reference Example 1.1.
  • the crystallinity was 100 % and no anatase was detectable by X-ray diffraction, determined according to Reference Example 1.3.
  • the results for the PO test and for the K80- test, determined according to Reference Examples 1.6 and 1.7, respectively, are shown in tables 4 and 5, respectively.
  • Example 3 Preparation of a TS-1 catalyst in accordance with the present invention
  • TEOS tetraethylorthosilicate
  • TEOTi 11.25 g tetraethylorthotitanate
  • TPAOH aqueous tetrapropylammonium hydroxide
  • the synthesis gel was then cooled to 40 °C under stirring and 546 g de-ionized water added thereto.
  • the resulting mixture had a pH of 11 .86, determined with a pH sensitive glass electrode.
  • the synthesis gel was then transferred into an autoclave.
  • the synthesis gel was heated under stirring in the autoclave to a temperature of 175 °C and stirred at said temperature for 16 h under autogenous pressure.
  • the pressure was in the range of from 8.4 to 11 .9 bar(abs).
  • the resulting suspension was then worked-up. To this effect, the resulting suspension was diluted with de-ionized water, wherein the weight ratio of the suspension to de-ionized water was 1 :1.
  • about 150 g nitric acid (10 weight-% in water) were added and the resulting mixture had a pH of 7.31 , determined with a pH sensitive glass electrode.
  • the obtained solids were filtered off and washed three times with de-ionized water (each time 1000 ml de-ionized water were used). Subsequently, the solids were dried in an oven in air at 120 °C for 4 h and then calcined in air at 490 °C for 5 h, wherein the heating rate for calcining was 2 °C/min.
  • the resulting product had a Si content of 42 weight-%, a Ti content of 1.5 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the resulting product was 449 m 2 /g determined according to Reference Examples 1.5, and the water adsorption 9.6 wt.-% determined according to Reference Examples 1.1.
  • the crystallinity was
  • the results for the PO test and for the K80- test, determined according to Reference Examples 1.6 and 1.7, respectively, are shown in tables 4 and 5, respectively.
  • Example 4 Preparation of a TS-1 catalyst in accordance with the present invention
  • TEOS tetraethylorthosilicate
  • TEOTi 15 g tetraethylorthotitanate
  • TPAOH aqueous tetrapropylammonium hydroxide
  • the mixture was hydrolyzed at room temperature for 60 min during which the temperature rose to 60 °C.
  • the mixture had a pH of 12.71 , determined with a pH sensitive glass electrode, then.
  • the ethanol was distilled off until the sump reached a temperature of 95 °C. 558 g of distillate was obtained from distillation.
  • the synthesis gel was then cooled to 40 °C under stirring and 558 g de-ionized water added thereto.
  • the resulting mixture had a pH of 11 .95, determined with a pH sensitive glass electrode.
  • the synthesis gel was then transferred into an autoclave.
  • the synthesis gel was heated under stirring in the autoclave to a temperature of 175 °C and stirred at said temperature for 16 h under autogenous pressure.
  • the pressure was in the range of from 8.4 to 11 .4 bar(abs).
  • the resulting suspension was then worked-up. To this effect, the resulting suspension was diluted with de-ionized water, wherein the weight ratio of the suspension to de-ionized water was 1 :1.
  • about 152 g nitric acid (10 weight- % in water) were added and the resulting mixture had a pH of 7.21 , determined with a pH sensitive glass electrode.
  • the obtained solids were filtered off and washed three times with de-ionized water (each time 1000 ml de-ionized water were used). Subsequently, the solids were dried in an oven in air at 120 °C for 4 h and then calcined in air at 490 °C for 5 h, wherein the heating rate for calcining was 2 °C/min.
  • the resulting TS-1 material had a Si content of 43 weight-%, a Ti content of 2 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the resulting TS-1 material was 447 m 2 /g determined according to Reference Examples 1.5.
  • the crystallinity was 92 %, and about 0.5 % of anatase were detectable by X-ray diffraction, as determined according to Reference Examples 1.4.
  • the resulting TS-1 product had a Si content of 44 weight-%, a Ti content of 1 .9 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the resulting TS-1 product was 446 m 2 /g determined according to Reference Examples 1.5, and the water adsorption 7.25 wt.-% determined according to Reference Examples 1.1.
  • the crystallinity was 93 %, and about 0.7 % of anatase were detectable by X-ray diffraction, as determined according to Reference Examples 1.4.
  • the results for the PO test and for the K80- test determined according to Reference Examples 1 .6 and 1 .7, respectively, are shown in tables 4 and 5, respectively.
  • Example 5 Preparation of a TS-1 catalyst in accordance with the present invention
  • a TS-1 zeolite was prepared in accordance with Example 1 of WO 2011/064191 A1 with the exception that 10 weight- % of tetraethyl orthosilicate were used as binder based on 100 weight-% of the TS-1 material.
  • the resulting solid material was heated in air within 60 min to a temperature of 110 °C and dried at said temperature for 4 h. Then, the resulting solid material was heated in air within 190 min to a temperature of 520 °C and calcined at said temperature for 16 h.
  • TS-1 material had a Si content of 45 weight-%, a Ti content of 1 .7 weight-% and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area was 450 m 2 /g determined according to Reference Example 1 .5.
  • aqueous nitric acid (10 weight-% HNO3 in water) were provided in a glass beaker. Under stirring, 250 g of the TS-1 material were added thereto. The resulting suspension - while being stirred at 250 rpm - was refluxed at 100 °C for 1 hour. For work-up, the resulting solids were separated via centrifugation. The resulting solid material was heated in air within 60 min to a temperature of 120 °C and dried at said temperature for 4 h. Then, the resulting solid material was heated in air within 190 min to a temperature of 500 °C and calcined at said temperature for 5 h.
  • the thus obtained TS-1 material had a Si content of 45 weight-%, a Ti content of 1 .8 weight-% and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area was 453 m 2 /g determined according to Reference Example 1.5, and the water adsorption 7.0 wt.-% determined according to Reference Example 1.1.
  • the crystallinity was 97 %, and about 1 % of anatase were detectable by X-ray diffraction, as determined according to Reference Example 1 .4.
  • the results for the PO test and for the K80-test, determined according to Reference Examples 1 .6 and 1 .7, respectively, are shown in tables 4 and 5, respectively.
  • Example 6 Preparation of a catalyst in accordance with the present invention
  • a TS-1 material was synthesized having an Si content of 44 weight-%, a Ti content of 1 .2 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the TS-1 material was 429 m 2 /g determined according to Reference Example 1.5, the micropore volume was 0.07 ml/g, the total pore volume was 0.37 ml/g determined according to Reference Example 1.11 , and the water adsorption 3.4 wt.-% determined according to Reference Example 1.1.
  • the crystallinity was 100 % as determined by X-ray diffraction determined according to Reference Example 1.4.
  • the results for the PO test and for the K80- test, determined according to Reference Examples 1.6 and 1.7, respectively, are shown in tables 4 and 5, respectively.
  • Example 7 Preparation of a catalyst in accordance with the present invention
  • a TS-1 material was synthesized having an Si content of 46 weight-%, a Ti content of 1 .2 weight-%, and a total organic carbon content (TOC) of less than 0.1 weight-%.
  • the BET specific surface area of the resulting TS-1 material was 392 m 2 /g determined according to Reference Example 1.5, the micropore volume was 0.06 ml/g, the total pore volume was 0.39 ml/g determined according to Reference Example 1.11 , and the water adsorption 4.4 wt.-% determined according to Reference Example 1.1.
  • the crystallinity was 89 %, and about 0.9 % of anatase were detectable by X-ray diffraction determined according to Reference Example 1.4.
  • the results for the PO test and for the K80- test, determined according to Reference Examples 1.6 and 1.7, respectively, are shown in tables 4 and 5, respectively.
  • TEOS tetraethylorthosilicate
  • TEOTi tetraethylorthotitanate
  • TPAOH aqueous tetrapropylammonium hydroxide
  • the synthesis gel was then cooled to 40 °C under stirring and 450 g de-ionized water added thereto.
  • the resulting mixture had a pH of 12.1 , determined with a pH sensitive glass electrode.
  • the synthesis gel was then transferred into an autoclave.
  • the synthesis gel was heated under stirring in the autoclave to a temperature of 175 °C and stirred at said temperature for 16 h under autogenous pressure.
  • the resulting suspension was then worked-up. To this effect, the resulting suspension was diluted with de-ionized water, wherein the weight ratio of the suspension to de-ionized water was 1 :1.
  • 178.6 g nitric acid (10 weight-% in water) were added.
  • the pH was adjusted to 7 with about 3 ml of NH4OH solution (25 weight-% NH4OH in water).
  • the obtained solids were filtered off and washed three times with de-ionized water (each time 1000 ml de-ionized water were used). Subsequently, the solids were dried in an oven in air at 120 °C for 4 h and then calcined in air at 490 °C for 5 h, wherein the heating rate for calcining was 2 0 C/min.
  • the resulting TS-1 material had a Si content of 43 weight-%, a Ti content of 2.8 weight-%, and a total organic carbon content of 0.6 weight-%.
  • the BET specific surface area of the resulting TS- 1 material was 434 m 2 /g determined according to Reference Example 1.5.
  • the crystallinity was 81 %, and about 0.7 % of anatase were detectable by X-ray diffraction determined according to Reference Example 1 .4.
  • the results for the PO test and for the K80-test, determined according to Reference Examples 1 .6 and 1 .7, respectively, are shown in tables 4 and 5, respectively.
  • TEOS tetraethylorthosilicate
  • TEOTi 15 g tetraethylorthotitanate
  • TPAOH aqueous tetrapropylammonium hydroxide
  • the mixture was hydrolyzed at room temperature for 60 min during which the temperature rose to 60 °C.
  • the mixture had a pH of 12.6, determined with a pH sensitive glass electrode, then.
  • the ethanol was distilled off until the sump reached a temperature of 95 0 C. 540 g of distillate was obtained from distillation.
  • the synthesis gel was then cooled to 40 °C under stirring and 542 g de-ionized water added thereto.
  • the resulting mixture had a pH of 11 .9, determined with a pH sensitive glass electrode.
  • the synthesis gel was then transferred into an autoclave.
  • the synthesis gel was heated under stirring in the autoclave to a temperature of 175 °C and stirred at said temperature for 16 h under autogenous pressure.
  • the pressure was in the range of from 8.4 to 10.9 bar(abs).
  • the resulting suspension was then worked-up. To this effect, the resulting suspension was diluted with de-ionized water, wherein the weight ratio of the suspension to de-ionized water was 1 :1.
  • about 164 g nitric acid (10 weight-% in water) were added and the resulting mixture had a pH of 7.35.
  • the obtained solids were filtered off and washed four times with de-ionized water (each time 1000 ml de-ionized water were used).
  • TS-1 material had a Si content of 43 weight-%, a Ti content of 2 weight-% and a total organic carbon content of less than 0.1 weight-%.
  • the BET specific surface area was 462 m 2 /g determined according to Reference Example 1 .5, and the water adsorption 11 .5 wt.-% determined according to Reference Example 1.1.
  • the crystallinity was 88 % as determined by X-ray diffraction determined according to Reference Example 1.4.
  • the results for the PO test and for the K80- test, determined according to Reference Examples 1.6 and 1.7, respectively, are shown in tables 4 and 5, respectively.
  • Example 10 Preparing a catalyst in accordance with the present invention (TS-1)
  • a titanium silicalite-1 (TS-1 ) powder was prepared according to the following recipe: 500 g TEOS (tetraethyl orthosilicate) and 15 g TEOTi (tetraethyl orthotitanate) were loaded into a four- neck flask at room temperature and stirring (200 rpm) was started. Then, 220 g of an aqueous solution comprising 40 weight-% TPAOH (tetrapropylammonium hydroxide) and 300 g of deionized water were added. The pH of the resulting solution was 14.21 , determined with a pH sensitive glass electrode. Stirring was continued for 60 min, whereby the temperature of the mixture rose to 60 °C.
  • TEOS tetraethyl orthosilicate
  • TEOTi tetraethyl orthotitanate
  • Ethanol released by hydrolysis was separated by distillation at a bottoms temperature of 95 °C, obtaining about 540 g ethanol and a gel.
  • the pH of the gel was 12.34, determined with a pH sensitive glass electrode.
  • the gel was cooled down to 40 °C under stirring and 540 g of deionized water were added.
  • the pH of the obtained mixture was 12.01 , determined with a pH sensitive glass electrode. Crystallization was performed in an autoclave under stirring at 175 °C within 16 h and 20 min at autogenous pressure.
  • the obtained suspension was worked-up as follows.
  • the suspension was diluted 1 :1 with deionized water under stirring (200 rpm, Teflon anchor stirrer) and precipitated with 10% HNO3 (approx. 130 g) at pH 7.31 , determined with a pH sensitive glass electrode, and filtered off through a porcelain suction filter (blue belt filter).
  • the filter cake was washed 3 times with 1000 ml deionized water, dried in an oven for 4 h at 120 °C and calcined for 5 h at 490 °C (heating rate 2 °C/min) in air.
  • the yield was 148 g.
  • the resulting powder had a total organic carbon content (TOC) of 0.02 g/100 g, determined according to DIN EN 1484, a potassium content of less than 0.01 g/100 g, a sodium content of 0.01 g /100 g, a Si content of 43 g/100 g, and a Ti content of 1 .9 g/100 g.
  • TOC total organic carbon content
  • the yield was 121 g.
  • the resulting powder had a Ti content of 1 .8 g/100 g, a water adsorption of 6.3 weight-% determined according to Reference Example 1.1 , and showed a BET specific surface area of 443 m 2 /g determined as described in Reference Example 1.5.
  • Example 11 Preparing a catalyst molding in accordance with the present invention
  • the kneaded mass was subjected to shaping.
  • the kneaded mass was extruded at a pressure of 150 bar(abs) to give strands with a circular cross-section having a diameter of 1 .9 mm.
  • the strands were then dried in an oven for 4 h at 120 °C and then calcined in air for 5 h at 490 °C (heating rate: 2 °C/min).
  • the yield was 124 g.
  • the obtained material had a water adsorption of 6.7 weight-% determined according to Reference Example 1 .1 , a bulk density of 332 g/l, a total pore volume of 0.957 ml/g determined as described in Reference Example 1 .11 .
  • the sample had a crystallinity of 58 % and essentially consisted of TS-1 (0.7 weight-% crystalline anatase and 99.3 weight-% of crystalline TS-1 ).
  • the resulting material had a Ti content of 1 .4 g/100 g, a water adsorption of 4.5 weight-% determined according to Reference Example 1.1 , and a bulk density of 332 g/l. Furthermore, the re- suiting material dislayed a K-80 test value of 0.06 h- 1 as determined according to Reference Example 4 As determined by X-ray diffraction analysis according to Reference Example 1 .4, the sample had a crystallinity of 51 %.
  • Example 12 Preparing a catalyst molding according to the invention
  • the kneaded mass was subjected to shaping.
  • the kneaded mass was extruded at a pressure of 150 bar(abs) to give strands with a circular cross-section having a diameter of 1 .9 mm.
  • the strands were then dried in an oven for 4 h at 120 °C and then calcined in air for 5 h at 490 °C (heating rate: 2 °C/min).
  • the resulting material had a Ti content of 0.9 g/100 g, a water adsorption of 5.3 weight-% determined according to Reference Example 1.1.
  • the concentration of bridging p 2 q 2 -peroxo species per Ti in the H2O2-activated catalyst (“mmol p-peroxo species/mol Ti”) was determined for the examples and comparative examples according to the method described in Reference Example 1.3, wherein the concentration was determined 15 min and 2 h after having activated the respective samples with hydrogen peroxide. Based thereon, the activation factor was calculated according to Reference Example 1.10. Table 1
  • the catalysts of the examples in accordance with the present invention show far lower decomposition rates of H2O2 as determined according to the K-80 test than the catalysts according to the comparative examples.
  • the catalysts according to Comparative Examples 8 and 9 show decomposition rates of H2O2 of 0.936 and 0.56, respectively.
  • the catalysts of the present invention show at most a decomposition rate of H2O2 of 0.41 for the catalyst according to Example 3. The lowest decomposition rate of H2O2 is shown by the catalyst according to Example 1 where said rate was 0.12.
  • the catalysts according to the present invention show at least a good if not an excellent performance in the PO test, as can be seen from the results shown in tables 4 and 5.
  • the catalysts according to Examples 4-7 show a better performance in the PO test than the catalysts according to Comparative Examples 8 and 9.
  • Figure 1 shows a p 2 n 2 -peroxo species bridging two Ti atoms.

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Abstract

La présente invention concerne un moulage de catalyseur pour l'activation de peroxyde d'hydrogène, le moulage de catalyseur comprenant un catalyseur de titanosilicate pour l'activation de peroxyde d'hydrogène, ledit catalyseur comprenant Ti, Si et O, le catalyseur compris dans le moulage de catalyseur présentant une adsorption d'eau (W), une concentration (C) de pontage µ2η2-espèce peroxo par Ti dans le catalyseur activé par H2O2 tel que déterminée par spectroscopie RMN 17O quantitative, et un facteur d'activation spécifique (A) selon la formule (I), conformément à la formule (I), le facteur d'activation étant le produit de multiplication de l'adsorption d'eau et de la concentration de pontage µ2η2-espèce peroxo par Ti dans le catalyseur activé par H2O2 : A = W x C (I). La présente invention concerne en outre un procédé de préparation d'un moulage de catalyseur et un moulage de catalyseur pouvant être obtenu ou obtenu par ledit procédé. En outre, la présente invention concerne un procédé d'activation de peroxyde d'hydrogène, et l'utilisation du moulage de catalyseur de l'invention dans une réaction impliquant la formation de liaison C-O, et/ou la formation de liaison C-C et/ou la conversion de liaison C-C.
PCT/EP2024/052763 2023-05-31 2024-02-05 Moulage de catalyseur pour l'activation de peroxyde d'hydrogène Pending WO2024245592A1 (fr)

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Citations (6)

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Publication number Priority date Publication date Assignee Title
US4410501A (en) 1979-12-21 1983-10-18 Snamprogetti S.P.A. Preparation of porous crystalline synthetic material comprised of silicon and titanium oxides
WO2011064191A1 (fr) 2009-11-27 2011-06-03 Basf Se Procédé pour la préparation d'un catalyseur à titane-zéolite
WO2020074586A1 (fr) 2018-10-09 2020-04-16 Basf Se Moulage comprenant un matériau zéolithique ayant un type de structure mfi
WO2020174586A1 (fr) 2019-02-26 2020-09-03 株式会社ソニー・インタラクティブエンタテインメント Dispositif de traitement d'informations, procédé de traitement d'informations et programme
WO2021123227A1 (fr) 2019-12-19 2021-06-24 Basf Se Synthèse continue de matériau zéolithique de titanosilicate, ledit matériau zéolithique, moulage préparé à partir de celui-ci, ainsi que leur utilisation
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Publication number Priority date Publication date Assignee Title
US4410501A (en) 1979-12-21 1983-10-18 Snamprogetti S.P.A. Preparation of porous crystalline synthetic material comprised of silicon and titanium oxides
WO2011064191A1 (fr) 2009-11-27 2011-06-03 Basf Se Procédé pour la préparation d'un catalyseur à titane-zéolite
US9302257B2 (en) 2009-11-27 2016-04-05 Basf Se Process for the preparation of a titanium zeolite catalyst
WO2020074586A1 (fr) 2018-10-09 2020-04-16 Basf Se Moulage comprenant un matériau zéolithique ayant un type de structure mfi
WO2020174586A1 (fr) 2019-02-26 2020-09-03 株式会社ソニー・インタラクティブエンタテインメント Dispositif de traitement d'informations, procédé de traitement d'informations et programme
WO2021123227A1 (fr) 2019-12-19 2021-06-24 Basf Se Synthèse continue de matériau zéolithique de titanosilicate, ledit matériau zéolithique, moulage préparé à partir de celui-ci, ainsi que leur utilisation
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D. MASSIOT ET AL., MAGNETIC RESONANCE IN CHEMISTRY, vol. 40, 2002, pages 70 - 76
LAMBERTI C.BORDIGA S.ZECCHINA A.CARATI A.FITCH A.N.ARTIOLI G.PETRINI G.SALVALAGGIO M.MARRA G.L.: "Structural Characterization of Ti-Silicalite-1: A Synchrotron Radiation X-Ray Powder Diffraction Study", J. CATAL., vol. 183, 1999, pages 222 - 231, XP004443172, DOI: 10.1006/jcat.1999.2403
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