Methods for synthesizing a mesoporous nano-sized ultra-stable Y zeolite include combining a microporous Y zeolite having a SiO.sub.2/Al2O.sub.3 molar ratio of less than 5.2 with water to form a microporous Y zeolite slurry and heating the microporous Y zeolite slurry to 30? C. to 100? C. to form a heated microporous Y zeolite slurry. Further the method includes adding a 0.1M to 2.0M ammonium hexafluorosilicate solution and a 0.1M to 2.0M ammonium hydroxide solution in a drop-wise manner, either sequentially or simultaneously, to the heated microporous Y zeolite slurry to form a treated zeolite solution and holding the treated zeolite solution at 50? C. to 100? C. Finally the method includes filtering and washing the dealuminated solution with water to form an ultra-stable Y zeolite precursor, drying the ultra-stable Y zeolite precursor, and calcining the dried zeolite precursor to form the nano-sized ultra-stable Y zeolite.

A method for making a supported tantalum oxide catalyst precursor or catalyst with controlled Ta distribution and the resulting supported Ta catalyst. In an embodiment, the method comprises selecting a Ta-precursor with appropriate reactivity with the surface hydroxyls of the solid oxide support material to give a desired Ta distribution in the catalyst precursor or catalyst. In an embodiment the method comprises controlling the number of surface hydroxyls available on the support material to react with the Ta-precursor by thermal methods, such as calcination, to achieve the desired Ta distribution.

The present invention relates to a composition based on Al and Ce in the form of oxides (composition C1); or based on Al, Ce and La in the form of oxides (composition C2), with the following proportions: the proportion of CeO.sub.2 is between 3.0 wt % and 35.0 wt %; the proportion of La.sub.2O.sub.3 (for composition C.sub.2 only) is between 0.1 wt % and 6.0 wt %; the remainder as Al.sub.2O.sub.3; exhibiting the following porosity profile: a pore volume in the range of pores with a size of between 5 nm and 100 nm which is between 0.35 and 1.00 mL/g; anda pore volume in the range of pores with a size of between 100 nm and 1000 nm which is less than or equal to 0.15 mL/g, these pore volumes being determined by means of the mercury porosimetry technique; and the following properties: a mean size of the crystallites after calcination in air at 1100? C. for 5 hours (denoted D1100? C.-5 h) which is lower than 45.0 nm, preferably lower than 40.0 nm; a mean size of the crystallites after calcination in air at 900? C. for 2 hours (denoted D900? C.-2 h) which is lower than 25.0 nm, preferably lower than 20.0 nm, even more preferably lower than 15.0 nm; andan increase ?D of the mean size of the crystallites lower than 30.0 nm, preferably lower than 25.0 nm, ?D being calculated with the following formula: ?D=D.sub.1100?C-2h-D.sub.900C-5h; the mean size of the crystallites being obtained by XRD from the diffraction peak [111] of the cubic phase corresponding to cerium oxide, generally present at 2? between 28.0 and 30.0.

A photocatalytic functional film has a structure of a substrate, a barrier layer and a photocatalytic layer stacked one on another. The barrier layer is an amorphous TiO.sub.2 film, the photocatalyst layer comprises an amorphous TiO.sub.2 film, and particles of visible light responsive photocatalytic material formed on the surface of the amorphous TiO.sub.2 film. A method for producing a photocatalytic functional film includes: adding an alcohol solvent and an acid to a titanium precursor to obtain a TiO.sub.2 amorphous sol by dehydration and de-alcoholization reaction; applying and drying the TiO.sub.2 amorphous sol on a substrate to form a barrier layer; and applying and drying a composition formed by mixing particles of visible light responsive photocatalyst material with the TiO.sub.2 amorphous sol on the barrier layer, to form a photocatalyst layer.

A process for the co-production of acetic acid and dimethyl ether by contacting methyl acetate and methanol in the presence of catalysts comprising crystalline zeolites having a FER framework type which crystallites have a dimension in the c-axis of about 500 nm or less and a ratio of the c-axis:b-axis dimension of 5:1 or greater and a method for preparation of the zeolites utilizing piperazines.

Carbonylation process for producing methyl acetate, by contacting dimethyl ether and carbon monoxide under carbonylation conditions in the presence of a catalyst having a zeolite of micropore volume of 0.01 ml/g. The zeolite is an as-synthesized organic structure directing agent-containing zeolite and contains at least one channel which is defined by an 8-member ring.

The manufacturing method includes a step of mixing a coarse particle zeolite, a fine particle zeolite, and a raw material of an inorganic bonding material to prepare a zeolite raw material; a step of forming the prepared zeolite raw material into a honeycomb shape to prepare a honeycomb formed body; and a step of firing the prepared honeycomb formed body to prepare the honeycomb structure. In the step of preparing the zeolite raw material, as the coarse particle zeolite, a chabazite type zeolite having a specific average particle diameter, the fine particle zeolite having a specific average particle diameter, the raw material of the inorganic bonding material which includes at least basic aluminum lactate is used.

Methods are provided for forming supported catalyst compositions and/or corresponding intermediate catalyst products. The catalyst compositions have improved activity for hydroprocessing of distillate boiling range feeds under hydroprocessing conditions where the hydrogen partial pressure in the hydroprocessing environment is reduced or minimized. The catalyst compositions can correspond to supported CoMo catalysts. The improved activity for hydroprocessing under lower pressure conditions is unexpectedly achieved by using a plurality of treatments with organic compounds during the catalyst formation process.

A method of catalytic hydrogenation and reduction in which a reactive substrate and a hydrogen source are brought into contact in the presence of a platinum-group metal-supported catalyst to run the reactive substrate through catalytic hydrogenation and reduction; the ion exchanger is made of a continuous skeleton phase and a continuous hole phase; the thickness of the continuous skeleton is in the range of 1-100 ?m; the average diameter of the continuous holes is in the range of 1-1000 ?m; the total pore volume is in the range of 0.5-50 mL/g; the ion exchange capacity per unit weight in a dry state is in the range of 1-9 mg eq/g; and the ion exchanger is a non-particulate, weakly basic, organic porous ion exchanger where an ion exchange group is distributed in the ion exchanger.

[Problem] To provide a catalyst for hydrotreating a heavy hydrocarbon oil, the catalyst exhibiting excellent demetallization performance, desulfurization performance, and deasphaltene performance and having high strength. [Solution] A hydrotreating catalyst, which is a catalyst for hydrotreating a heavy hydrocarbon oil, the catalyst including an alumina-phosphorus oxide carrier, and a hydrogenation-active metal component supported on the carrier, in which the content of phosphorus in the carrier is 0.4 to 2.0 mass % in terms of P.sub.2O.sub.5, the carrier has a local maximum value of the differential pore volume distribution in a pore diameter range of 18 to 22 nm measured by mercury intrusion porosimetry, in the carrier, the ratio (?PV/PV.sub.T) of a volume (?PV) of pores having a pore diameter in a range deviating from a range of a pore diameter at the local maximum value?2 nm to the total pore volume (PV.sub.T) measured by mercury intrusion porosimetry is 0.50 or less, and the crystalline form of a portion of alumina in the alumina-phosphorus oxide carrier is ?-alumina.