Systems and methods of dehydrogenating a hydrocarbon in a fixed bed dehydrogenation unit. A method for dehydrogenating a hydrocarbon is applied to a fixed bed reactor. The hydrocarbon flows to a fixed bed reactor to be dehydrogenated in presence of a catalyst in the fixed bed reactor. The catalyst in the fixed bed reactor is then regenerated. The period for dehydrogenation, the period for catalyst regeneration and the period for total slack time are controlled such that total slack time is less than both half of the period for dehydrogenation and half of the period for regeneration. One of the advantages of the process comes from optimization of the slack time, thereby increasing the catalyst utilization rate and number of reactors concurrently online.

An antireflection film 3 provided on an optical substrate 2 of an optical member 1 has a reflectivity adjusting film 4 including a first layer 10, a second layer 11 having a refractive index higher than a refractive index of the first layer 10, a third layer 12 having a refractive index lower than a refractive index of the second layer 11, and a photocatalyst film 5 including one or more photocatalytically active layers 14 containing titanium dioxide, in which a thickness of the reflectivity adjusting film measured from a surface 4a is equal to or greater than 20 nm and less than 150 nm, the photocatalyst film 5 is provided between the reflectivity adjusting film 4 and the optical substrate 2, an interface 5a between the photocatalyst film 5 and the reflectivity adjusting film is disposed at position spaced apart from the surface 4a by a distance equal to or shorter than 150 nm, and a total thickness of the photocatalytically active layers 14 is equal to or greater than 350 nm and equal to or smaller than 1,000 nm.

A self-cleaning window blind includes a thin layer of photocatalytic material on at least one surface of the slats. The window blind includes an ultraviolet light source which directs ultraviolet light onto the photocatalytic material. Consequently, the window blind is not dependent on available sunlight. The ultraviolet light source is located in either the headrail or the bottom rail of the window blinds. Upon exposure to ultraviolet light, organic material on the slats which may include dust, grease, or microorganisms, is converted to carbon dioxide and water. One or both of the horizontal edges of the slats may include a lip which collects water formed by the photocatalytic reaction. In some embodiments, the slats are slightly convex. This shape may inhibit water from collecting in droplets on the slat and help direct the water towards the lip. Consequently, water spots are not created on the slats.

A self-cleaning window blind includes a thin layer of photocatalytic material on at least one surface of the slats. The window blind includes an ultraviolet light source which directs ultraviolet light onto the photocatalytic material. Consequently, the window blind is not dependent on available sunlight. The ultraviolet light source is located in either the headrail or the bottom rail of the window blinds. Upon exposure to ultraviolet light, organic material on the slats which may include dust, grease, or microorganisms, is converted to carbon dioxide and water. One or both of the horizontal edges of the slats may include a lip which collects water formed by the photocatalytic reaction. In some embodiments, the slats are slightly convex. This shape may inhibit water from collecting in droplets on the slat and help direct the water towards the lip. Consequently, water spots are not created on the slats.

A process for preparing a catalyst comprises coating substantial internal surfaces of porous inorganic powders with titanium oxide to form titanium oxide-coated inorganic powders. After the coating, an extrudate comprising the titanium oxide-coated inorganic powders is formed and calcined to form a catalyst support. Then, the catalyst support is impregnated with a solution containing one or more salts of metal selected from the group consisting of molybdenum, cobalt, and nickel.

Disclosed is a manufacturing method of 1,2-dichlorohexafluorocyclopentene. The first reaction uses dicyclopentadiene as a starting material and nitrogen gas or another inert gas as a diluting agent in a gas-phase thermal cracking reaction to obtain cyclopentadiene. The second reaction uses cyclopentadiene as a starting material in a liquid phase chlorination reaction with chlorine gas to obtain 1,2,3,4-tetrachlorocyclopentane. The third reaction uses 1,2,3,4-tetrachlorocyclopentane as a starting material in a gas-phase chlorination and fluorination reaction with hydrogen fluoride and chlorine gas in the presence of a chromium-based catalyst to obtain 1,2-dichlorohexafluorocyclopentene. The method uses easily acquired starting material and a stable fluorination catalyst, provides a high yield for a target product, and is applicable for large-scale continuous gas-phase production of 1,2-dichlorohexafluorocyclopentene.

Disclosed is a manufacturing method of 1,2-dichlorohexafluorocyclopentene. The first reaction uses dicyclopentadiene as a starting material and nitrogen gas or another inert gas as a diluting agent in a gas-phase thermal cracking reaction to obtain cyclopentadiene. The second reaction uses cyclopentadiene as a starting material in a liquid phase chlorination reaction with chlorine gas to obtain 1,2,3,4-tetrachlorocyclopentane. The third reaction uses 1,2,3,4-tetrachlorocyclopentane as a starting material in a gas-phase chlorination and fluorination reaction with hydrogen fluoride and chlorine gas in the presence of a chromium-based catalyst to obtain 1,2-dichlorohexafluorocyclopentene. The method uses easily acquired starting material and a stable fluorination catalyst, provides a high yield for a target product, and is applicable for large-scale continuous gas-phase production of 1,2-dichlorohexafluorocyclopentene.

A process for preparing C.sub.2 to C.sub.3 olefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350 C. to 450 C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of C.sub.2 to C.sub.3 olefins greater than 15 kg C.sub.2 to C.sub.3 olefins/kg catalyst.

A process for preparing C.sub.2 to C.sub.3 olefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350 C. to 450 C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of C.sub.2 to C.sub.3 olefins greater than 15 kg C.sub.2 to C.sub.3 olefins/kg catalyst.

The present invention discloses catalyst and method for producing light olefins directly from synthesis gas by a one-step process, and particularly relates to method and catalyst for directly converting synthesis gas into light olefins by a one-step process. The provided catalysts are composite materials formed of multicomponent metal oxide composites and inorganic solid acids with hierarchical pore structures. The inorganic solid acids have a hierarchical pore structure having micropores, mesopores and macropores. The metal composites can be mixed with or dispersed on surfaces or in pore channels of the inorganic solid acid and can catalyze the synthesis gas conversion to a C.sub.2-C.sub.4 light hydrocarbon product containing two to four carbon atoms. The single pass conversion of CO is 10%-60%. The selectivity of light hydrocarbon in all hydrocarbon products can be up to 60%-95%, wherein the selectivity of light olefins (C.sub.2.sup.C.sub.4.sup.) is 50%-85%.