In order to specify a catalytic converter, especially SCR catalytic converter, with maximum catalytic activity, this catalytic converter has at least one catalytically active component and additionally at least one porous inorganic filler component having meso- or macroporosity. The organic porous filler component has a proportion of about 5 to 50% by weight. More particularly, a diatomaceous earth or a pillared clay material is used as the porous inorganic filler component.

The present invention relates to a method for the preparation of a molecular sieve of the CHA-type as well as catalytic applications thereof.

A method for preparing C.sub.2 to C.sub.5 paraffins includes introducing a feed stream including hydrogen gas and a carbon-containing gas selected from carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor. Converting the feed stream into a product stream including C.sub.2 to C.sub.5 paraffins in the presence of a hybrid catalyst. The hybrid catalyst includes a microporous catalyst component; and a metal oxide catalyst component selected from (A) a bulk material consisting of gallium oxide, (B) gallium oxide present on a titanium dioxide support material, and (C) a mixture of gallium oxide and at least one promoter present on a support material selected from Group 4 of the IUPAC periodic table of elements.

A process for dehydrating methanol to dimethyl ether product in the presence of a catalyst and a promoter, wherein the catalyst is at least one aluminosilicate zeolite, and the promoter is selected from one or more compounds of Formula I: (I) wherein each of X and any or all of the Y's may independently be selected from hydrogen, halide, a substituted or unsubstituted hydrocarbyl substituent, or a compound of the formula —CHO, —CO.sub.2R, —COR, or —OR, where R is hydrogen or a substituted or unsubstituted hydrocarbyl substituent, and wherein the molar ratio of promoter to methanol is maintained at less than 1.

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Processes are provided for the removal of hydrogen from a mixture. The process can be performed by contacting a mixture comprising hydrogen, oxygen, and one or more organic compounds with a synthetic zeolite to produce water or steam. The synthetic zeolite can include Si and Al and has a SiO.sub.2:Al.sub.2O.sub.3 molar ratio of greater than 4:1, an 8-membered ring zeolite having a framework type of AEI, AFT, AFX, CHA, CDO, DDR, EDI, ERI, IHW, ITE, ITW, KFI, MER, MTF, MWF, LEV, LTA, PAU, PWN, RHO, SFW or UFI, a degree of crystallinity of at least 80% as measured by ASTM D535-197, and at least 0.01 wt % of at least one catalytic metal, based on a weight of the synthetic zeolite, where the at least one catalytic metal can include Ru, Rh, Pd, Ag, Os, Ir, Pt, Au, Mo, W, Re, Co, Ni, Zn, Cr, Mn, Ce, Ga, alloys thereof, or mixtures thereof. At least 95% of the catalytic metal can be disposed within a plurality of pores of the synthetic zeolite.

The invention provides a method of synthesizing a zeolite having the CHA crystalline framework, the method including forming a reaction mixture comprising an alumina source comprising a zeolite having an FAU crystalline framework, a silica source, and an organic structure directing agent, the reaction mixture—having a combined molar ratio of M/Si+R/Si higher than the molar ratio OH/Si, wherein M is moles of alkali metal and R is moles of organic structure directing agent; and crystallizing the reaction mixture to form a product zeolite having the CHA crystalline framework, wherein the product zeolite has a mesopore surface area (MSA) of less than about 25 m.sup.2/g. The invention also includes catalyst articles made using the product zeolite, exhaust gas treatment systems including the catalyst articles, and methods of treating exhaust gas using the catalyst articles.

A cluster-supporting catalyst including porous carrier particles having acid sites, and catalyst metal clusters supported within the pores of the porous carrier particles. In the cluster-supporting catalyst including porous carrier particles having acid sites, and catalyst metal clusters supported within the pores of the porous carrier particles, the catalyst metal may be rhodium, the catalyst metal may be palladium, the catalyst metal may be platinum, or the catalyst metal may be copper.

A cluster-supporting catalyst including porous carrier particles having acid sites, and catalyst metal clusters supported within the pores of the porous carrier particles. The catalyst metal clusters are obtained by supporting catalyst metal clusters having a positive charge, which is formed in a dispersion liquid containing a dispersion medium and the porous carrier particles dispersed in the dispersion medium, on the acid sites within the pores of the porous carrier particles through an electrostatic interaction.

An exhaust gas purification catalyst device includes a honeycomb base material and an inlet-side coat layer, wherein: the honeycomb base material includes a plurality of cells partitioned by porous partition walls, the plurality of cells including inlet-side cells and outlet-side cells and being configured such that exhaust gas that has flowed into the inlet-side cells passes through the partition walls and is exhausted from the outlet-side cells; and the inlet-side coat layer is present on the surface sides of the partition walls of the inlet-side cells, with the proportion of 4-9 μm through-pores in the through-pore diameter distribution of the partition walls being at least 80 vol %, and the peak pore diameter measured using a mercury porosimeter being at least 3.0 μm greater than the peak through-pore diameter measured using a perm porometer.

An AFI-CHA hybrid crystal molecular sieve and an NH.sub.3—SCR catalyst using the AFI-CHA hybrid crystal molecular sieve as a carrier, and preparation methods thereof are disclosed. The AFI-CHA hybrid crystal molecular sieve includes an AFI-type SAPO-5 molecular sieve and a CHA-type SAPO-34 molecular sieve, with hybrid crystal grains of AFI and CHA. The hybrid crystal molecular sieve is synthesized by a hydrothermal synthesis method and can be obtained by changing the structure directing agent, the heating rate and the calcinating temperature in the preparation process. Further, copper is loaded on the basis of the hybrid crystal molecular sieve to prepare copper-based NH.sub.3—SCR catalyst and corresponding monolithic catalyst. The catalytic activity and hydrothermal stability of the catalyst are significantly improved by the hybrid crystal molecular sieve.