Abstract: Disclosed are an apparatus and method for continuously producing carbon nanotubes. More specifically, disclosed are an apparatus for continuously producing carbon nanotubes including i) a reactor to synthesize carbon nanotubes, ii) a separator to separate a mixed gas from the carbon nanotubes transferred from the reactor, iii) a filter to remove all or part of one or more component gases from the separated mixed gas, and iv) a recirculation pipe to recirculate the filtered mixed gas to the reactor for carbon nanotubes. Advantageously, the apparatus and method for continuously producing carbon nanotubes enable rapid processing, exhibit superior productivity and excellent conversion rate of a carbon source, significantly reduce production costs, reduce energy consumption due to decrease in reactor size relative to capacity, and generate little or no waste gas and are thus environmentally friendly.

Abstract: The present invention relates to a continuous manufacturing apparatus for a carbon nanotube having gas separation units and a continuous manufacturing method for a carbon nanotube using the same, and more specifically, to a continuous manufacturing apparatus for a carbon nanotube having gas separation units and a continuous manufacturing method for a carbon nanotube using the same, in which the apparatus includes i) a reactor for synthesizing the carbon nanotube; ii) a separator for separating a mixed gas and the carbon nanotube transferred from the reactor; iii) a gas separation unit including more than one polymer membrane for removing in part or in whole of more than one component gas from the mixed gas separated; and iv) a recirculation pipe for recirculating the mixed gas without in part or in whole of the component gas to the reactor of carbon nanotube.

Abstract: The present invention provides a catalyst for use in gas-phase contact oxidation of hydrocarbon with an improved yield and selectivity, a preparation method thereof, and a method of a gas-phase oxidation of the hydrocarbon using the same. The catalyst comprises a composite metal oxide of Mo, V, Te and Nb; and a palladium or palladium oxide attached to the composite metal oxide, wherein an atomic molar ratio of the palladium attached to the composite metal oxide to the molybdenum contained in the composite metal oxide ranges from 0.00001:1 to 0.02:1.

Abstract: The present invention provides a catalyst for use in gas-phase contact oxidation of hydrocarbon with an improved yield and selectivity, a preparation method thereof, and a method of a gas-phase oxidation of the hydrocarbon using the same. The catalyst comprises a composite metal oxide of Mo, V, Te and Nb; and a tungsten or tungsten oxide attached to the composite metal oxide, wherein an atomic molar ratio of the tungsten attached to the composite metal oxide to the molybdenum contained in the composite metal oxide ranges from 0.00001:1 to 0.02:1.

Abstract: The present invention relates to a thermal-cracking method of hydrocarbon using a hydrocarbon thermal-cracking apparatus including a tube type furnace having a radiation part for thermally cracking hydrocarbon feedstocks supplied together with steam and a convection part. A hydrocarbon thermal-cracking catalyst is packed in some or entire area of the tube placed in the radiation part of the tube type furnace, wherein the hydrocarbon thermal-cracking catalyst includes an oxide catalyst represented by CrZrjAkOx (wherein, 0.5?j?120 and 0?k?50, A is a transition metal, and x is a number corresponding to the atomic values of Cr, Zr, and A and the numbers of j and k). Therefore, it is possible to improve yield and selectivity of olefin, reduce fuel consumption due to an excellent heat transfer efficiency and extend decoking interval by reduced production of coke deposited to an inside wall of a tube, in steam cracking of hydrocarbon for producing olefin.

Abstract: The present invention relates to a thermal-cracking method of hydrocarbon using a hydrocarbon thermal-cracking apparatus including a tube type furnace having a radiation part for thermally cracking hydrocarbon feedstocks supplied together with steam and a convection part. A hydrocarbon thermal-cracking catalyst is packed in some or entire area of the tube placed in the radiation part of the tube type furnace, wherein the hydrocarbon thermal-cracking catalyst includes an oxide catalyst represented by CrZrjAkOx (wherein, 0.5?j?120 and 0?k?50, A is a transition metal, and x is a number corresponding to the atomic values of Cr, Zr, and A and the numbers of j and k). Therefore, it is possible to improve yield and selectivity of olefin, reduce fuel consumption due to an excellent heat transfer efficiency and extend decoking interval by reduced production of coke deposited to an inside wall of a tube, in steam cracking of hydrocarbon for producing olefin.

Abstract: Enhanced lace tightening system including a plurality of apertures extending through the main body of a shoelace and smoothly finished end caps allowing unimpeded passage therethrough. A process includes a finishing step whereby end caps are generated without frayed edges to facilitate passage of the same through apertures to position appropriate aspects of the laces rapidly in a position from whence little tension loss occurs when properly disposed. Products by the process incorporate silicone, metallic elements, and related enhancements providing specifically improved shoelaces for any number of applications for a stated goal of drawing and fixing together two opposite edges.

Abstract: The present invention relates to a novel oxide catalyst, more specifically, a novel modified magnesium oxide catalyst which is highly active and selective for ortho-alkylation of phenol.The catalysts for phenol alkylation of the invention are represented as Mg.sub.a Mn.sub.b L.sub.c T.sub.d Q.sub.e O.sub.x .wherein:L is vanadium or chromium;T is alkali metal, alkali earth metal, lead, bisumth, cobalt, aluminum, silicon., gallium, germanium or molybdenum;Q is antimony, cesium or iron;b/a=0 to 0.35(atomic molar ratio);c/a=0.01 to 0.35(atomic molar ratio);d/a=0 to 0.35(atomic molar ratio);e/c=0.1 to 10(atomic molar ratio); and,x is determined by oxidation state of each component.