A xenon adsorbent capable of efficiently adsorbing xenon, even at a low concentration, from a mixture gas is Provided. A xenon adsorbent comprising a zeolite having a pore size in the range of 3.5 to 5 Å and a silica alumina molar ratio in the range of 10 to 30.

A xenon adsorbent capable of efficiently adsorbing xenon, even at a low concentration, from a mixture gas is Provided. A xenon adsorbent comprising a zeolite having a pore size in the range of 3.5 to 5 Å and a silica alumina molar ratio in the range of 10 to 30.

A process for dehydrating methanol to dimethyl ether product in the presence of an aluminosilicate zeolite catalyst and a promoter selected from (i) aldehyde of formula R.sup.1CHO (Formula I) in which R.sup.1 is hydrogen, a C.sub.1-C.sub.11 alkyl group or a C.sub.3-C.sub.11 alkyl group in which 3 or more carbon atoms are joined to form a ring; or (ii) acetal derivative of an aldehyde of Formula I; and the molar ratio of promoter to methanol is maintained at 0.1 or less.

The present invention relates to a process for preparing a zeolitic material having a framework type FER and having a framework structure comprising silicon, aluminum, and oxygen, said process comprising (i) preparing an aqueous synthesis mixture comprising water; a zeolitic material having a framework type other than FER and having a framework structure comprising silicon, aluminum, and oxygen; a source of silicon other than the zeolitic material having a framework type other than FER; an organic structure directing agent comprising piperidine; a source of an alkali metal; and a source of a base; (ii) subjecting the aqueous synthesis mixture prepared according to (i) to hydrothermal synthesis conditions comprising heating the synthesis mixture to a temperature in the range of from 140 to 190° C. and keeping the synthesis mixture at a temperature in this range under autogenous pressure, obtaining a mother liquor comprising a solid material which comprises the zeolitic material having a framework type FER.

The present invention relates to a catalyst comprising a carrier substrate of the length L extending between substrate ends a and b and two washcoat zones A and B, wherein washcoat zone A comprises a zeolite having a smallest lower channel width of at least 0.4 nm and extends starting from substrate end a over a part of the length L, and washcoat zone B comprises the same components as washcoat A and palladium and extends from substrate end b over a part of the length L, wherein L=L.sub.A+L.sub.B, wherein L.sub.A is the length of washcoat zone A and L.sub.B is the length of substrate length B.

The present invention discloses a catalyst for preparing pyridine base from syngas. The catalyst includes a carrier, an active component, a first auxiliary and a second auxiliary. The carrier is molecular sieves. The active component is Rh. The first auxiliary is one or more of Mn, Fe, Na and La. The second auxiliary is one or more of Zn, Co, Cr, Bi and Cu. The active component Rh is 0.5-3% of a mass of the carrier. The first auxiliary is 0.05-5% of the mass of the carrier. The second auxiliary is 0.5-15% of the mass of the carrier. The present invention further discloses application of the catalyst to preparation of pyridine base by catalyzing syngas, where the syngas and an ammonia donor are used as reaction raw materials for reaction to generate pyridine base products. The catalyst of the present invention can couple a cyclization reaction of generating acetaldehyde through hydrogenation of carbon monoxide with a condensation reaction of aldehyde and ammonia to convert the syngas into the pyridine base through one-step catalysis, with a carbon monoxide conversion rate of 8-20% and a pyridine base selectivity of 10-18%.

A process for dehydrating methanol to dimethyl ether using a Brønsted acid catalyst which is a 1-dimensional or a 3-dimensional aluminosilicate zeolite or a heteropolyacid, and a promoter of Formula I C.sub.nH.sub.(2n+1)CO.sub.2CH.sub.3 wherein n=1 to 11 or Formula II C.sub.mH.sub.2m(CO.sub.2CH.sub.3).sub.2 wherein m=2 to 7 and the molar ratio of promoter to methanol is maintained at less than 1.

A process for dehydrating methanol to dimethyl ether product in the presence of a solid Brønsted acid catalyst which is an aluminosilicate zeolite or a heteropolyacid and a promoter which is (i) a ketone of formula R.sup.1COR.sup.2 (Formula I) in which R.sup.1 and R.sup.2 are identical or different and are each a C.sub.1-C.sub.11 alkyl group and furthermore R.sup.1 and R.sup.2 together with the carbonyl carbon atom to which they are bonded may form a cyclic ketone; or (ii) a ketal derivative of a ketone of Formula I; and the molar ratio of promoter to methanol is maintained at 0.5 or less.

A process for dehydrating methanol to dimethyl ether product in the presence of a solid Brønsted acid catalyst which is an aluminosilicate zeolite or a heteropolyacid and a promoter which is (i) a ketone of formula R.sup.1COR.sup.2 (Formula I) in which R.sup.1 and R.sup.2 are identical or different and are each a C.sub.1-C.sub.11 alkyl group and furthermore R.sup.1 and R.sup.2 together with the carbonyl carbon atom to which they are bonded may form a cyclic ketone; or (ii) a ketal derivative of a ketone of Formula I; and the molar ratio of promoter to methanol is maintained at 0.5 or less.

Process for preparing a catalyst composition containing a modified crystalline aluminosilicate and a binder, wherein the catalyst composition comprises from 5 to 95% by weight of crystalline aluminosilicate as based on the total weight of the catalyst composition, the process being remarkable in that it comprises a step of steaming said crystalline aluminosilicate: at a temperature ranging from 100° C. to 380° C.; under a gas phase atmosphere containing from 5 wt % to 100 wt % of steam; at a pressure ranging from 2 to 200 bars; at a partial pressure of H.sub.2O ranging from 2 to 200 bars; and said steaming being performed during at least 30 min and up to 144 h;
and in that the process also comprises a step of shaping, or of extruding, the crystalline aluminosilicate with a binder, wherein the binder is selected to comprise at least 85 wt % of silica as based on the total weight of the binder, and less than 1000 ppm by weight as based on the total weight of the binder of aluminium, gallium, boron, iron and/or chromium.