Disclosed is a cyclopropanation process comprising the step of reacting an alkene compound having at least one carbon-carbon double bond with at least one dihaloalkane. The reaction is carried out in the presence of (i) particulate metal Zn, (ii) catalytically effective amount of particulate metal Cu or a salt thereof, (iii) at least one haloalkylsilane, and (iv) at least one solvent.

Synthesis of aromatic hydrocarbons from synthesis gas in a fixed bed or a moving bed reactor loaded with a composite catalyst comprising Catalyst Component A and Catalyst Component B mixed via a mechanical mixing mode, wherein the active ingredient of the Catalyst Component A is active metal oxides; and the Catalyst Component B is one or both of ZSM-5 zeolite and metal modified ZSM-5; the pressure of the synthesis gas is 0.1-6 MPa; the reaction temperature is 300-600 C.; and the space velocity is 500-8000 h.sup.1. The reaction process has a high product yield and selectivity, with the selectivity of aromatics reaching 50-85%, while the selectivity of the methane byproduct is less than 15%.

The present invention discloses a process for preparing perhydrofluorene or alkyl-substituted perhydrofluorene, comprising the steps of: (1) reacting a phenolic compound or an aromatic hydrocarbon compound or an aromatic ketone compound or an aromatic ether compound with a benzyl compound to carry out an alkylation reaction in the presence of a first catalyst, thereby to produce substituted or unsubstituted diphenyl methane, wherein the first catalyst is an acidic catalyst; and (2) reacting the substituted or unsubstituted diphenyl methane with hydrogen gas to carry out an hydrogenation reaction or a hydrodeoxygenation reaction, thereby to produce perhydrofluorene or alkyl-substituted perhydrofluorene, wherein the second catalyst is a physical mixture of a metal catalyst and an acidic catalyst or a metal catalyst loaded on an acidic catalyst.

A process includes reacting a feed stream containing ethanol and optionally acetaldehyde in a dehydration reactor in the presence of a dehydration catalyst system having a Group 4 or Group 5 metal oxide and a support. The process includes obtaining a product stream containing butadiene from the dehydration reactor. Another process includes reacting a feed stream containing ethanol and optionally acetaldehyde in a dehydration reactor in the presence of a dehydration catalyst system containing a tungsten oxide supported on a zeolite or a tantalum oxide supported on a zeolite. The process includes obtaining a product stream containing butadiene from the dehydration reactor.

Catalyst compositions including a zeolite having a molar ratio of silicon to aluminum of about 10.0 to about 300.0; a Group 10-12 element and combinations thereof; a Group 15 element and combinations thereof; and optionally, a binder, wherein the catalyst composition has a molar ratio of Group 15 element to Group 10-12 element of about 0.01 to about 10.0 are disclosed. Methods of converting organic compounds to aromatics using such catalyst compositions are also disclosed.

The present invention discloses a composite catalyst for the photocatalytic isomerization of norbornadiene to prepare quadricyclane, comprising: a solid photocatalyst, selected from the group consisting of TiO.sub.2, Ti-MCM-41, Ti-SBA-15, ZnO, WO.sub.3, Ta.sub.2O.sub.5 or SrTiO.sub.3; and an organic photo-sensitizer loaded on the surface or in the channel of said solid photocatalyst, selected from benzophenone, acetophenone, Michler's Ketone, tetraethyl Michler's Ketone, and diethyl Michler's Ketone, where the organic photo-sensitizer is present in the solid photocatalyst in an amount of 0.5% to 20% by weight. The catalyst of the invention can catalyze a target reaction under the condition that no solvent is used, and the yield of the target product quadricyclane is higher. Furthermore, the catalyst of the invention has a stable activity, and it can be recycled. The invention further discloses a process for preparing the composite catalyst.

A process for preparing C2 and C3 olefins comprises contacting a feedstream including hydrogen, carbon monoxide, and a bifunctional catalyst in a reaction under certain specified conditions. The catalyst includes as components (1) chromium oxide and zinc oxide mixed metal oxides, and (2) a SAPO-34 molecular sieve. The resulting product of the reaction is relatively high in the target lower olefins and relatively low in less desirable products, including C2 and C3 paraffins, C4+ hydrocarbons, oxygenates, and methane, thereby reducing or eliminating the need for certain previously common and costly separations. The bifunctional catalyst as used in the inventive process also offers improvements in catalyst life in comparison with some methanol-to-olefins catalysts. The process may be carried out as a single unit operation.

A catalyst composition includes a zeolite, a binder, and a Group 12 transition metal selected from the group consisting of Zn, Cd, or a combination thereof, the zeolite having a silicon to aluminum ratio of at least about 10, the catalyst composition comprising about 50 wt % or less of the binder based on a total weight of the catalyst composition, the catalyst composition having a micropore surface area of at least about 340 m.sup.2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of (a) a mesoporosity of greater than about 20 m.sup.2/g; (b) a diffusivity for 2,2-dimethylbutane of greater than about 110.sup.2 sec.sup.1 when measured at a temperature of about 120 C. and a 2,2-dimethylbutane pressure of about 60 torr (about 8 kPa).

An alkylation catalyst having a zeolite catalyst component and a binder component providing mechanical support for the zeolite catalyst component is disclosed. The binder component is an ion-modified binder that can include metal ions selected from the group consisting of Co, Mn, Ti, Zr, V, Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinations thereof. The metal ions reduce the number of acid sites on the zeolite catalyst component. The metal ions can range from 0.1 to 50 wt % based on the total weight of the ion-modified binder. Optionally, the ion-modified binder is present in amounts ranging from 1 to 80 wt % based on the total weight of the catalyst.

A catalyst composition comprising a zeolite, an alumina binder, and a Group 12 transition metal selected from Zn and/or Cd, the zeolite having a Si/Al ratio of at least about 10 and a micropore surface area of at least about 340 m.sup.2/g, the catalyst composition comprising about 50 wt % or less of the binder, based on a total weight of the catalyst composition, and having a micropore surface area of at least about 290 m.sup.2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: a mesoporosity of about 20 m.sup.2/g to about 120 m.sup.2/g; a diffusivity for 2,2-dimethylbutane of greater than about 110.sup.2 sec.sup.1 when measured at a temperature of about 120 C. and a 2,2-dimethylbutane pressure of about 60 torr (8 kPa); and a combined micropore surface area and mesoporosity of at least about 380 m.sup.2/g.