A method of producing a fuel additive includes producing a first product stream comprising butadiene by passing a feed stream comprising C4 hydrocarbons through a steam cracker; transforming greater than or equal to 90 weight % of the butadiene in the first product stream into a second product stream by passing the first product stream through a first hydrogenation unit, wherein the second product stream comprises 1-butene, 2-butene, n-butane, isobutylene, isobutane, or a combination thereof; and converting the second product stream into the fuel additive by passing the second product stream through a fuel additive synthesis unit with an acid catalyst.

Disclosed are a ferrite catalyst and preparation methods thereof. The catalyst is provided with a formula below, wherein A is Mg atom, Zn atom or a mixture of both atoms at any ratio; D is one or more atoms selected from the group consisting of Ni, Co, W, Mn, Ca, Mo or V atom; Z is a catalyst carrier, which is one or more selected from the group consisting of calcium phosphate, calcium dihydrogen phosphate, aluminum phosphate, aluminum dihydrogen phosphate, ferric phosphate, magnesium phosphate, zinc phosphate, Mg—Al hydrotalcite, calcium carbonate, magnesium carbonate; a=0.01-0.6; b=0-0.30; c is a number balancing each valence; x, y represent the amounts of principal catalyst and carrier Z respectively, wherein the weight ratio y/x=0.5:1-7:1.
x(FeA.sub.aD.sub.bO.sub.c)/yZ

An apparatus and method for producing hydrocarbons including aromatic hydrocarbons and lower olefins including propylene from CH.sub.4 and CO.sub.2 through CO and H.sub.2 with high activity and high selectivity. The apparatus is provided with: a synthetic gas production unit to which a gas containing CH.sub.4 and CO.sub.2 is supplied from a first supply unit, and which generates a synthetic gas containing CO and H.sub.2 while heating a first catalyst structure; a production unit to which the synthetic gas is supplied and which generates hydrocarbons including aromatic hydrocarbons having 6-10 carbon atoms and lower olefins including propylene while heating a second catalyst structure; and a detection unit which detects propylene and the aromatic hydrocarbons discharged from the production unit, in which the first catalyst structure includes first supports having a porous structure and a first metal fine particle in the first supports, the first supports have a first channels, the first metal fine particle is present in the first channels, the second catalyst structure includes second supports having a porous structure and a second metal fine particle in the second supports, the second supports have a second channels, and a portion of the second channels have an average inner diameter of 0.95 nm or less.

Nickel and copper catalyst, and an alumina support: nickel distributed both in the core of and on a crust at the periphery of the support, crust thickness being 2% to 15% of catalyst diameter; nickel density ratio between the crust and the core greater than 3; crust contains more than 25% by weight of nickel element relative to total weight of nickel in the catalyst; mole ratio between nickel and copper is 0.5 to 5, at least one portion of nickel and copper is a nickel-copper alloy; nickel content in the nickel-copper alloy is 0.5% to 15% by weight of nickel element relative to total weight of the catalyst; size of the nickel particles in the catalyst is less than 7 nm.

An object of the present invention is to suppress performance deterioration of a molybdenum composite oxide-based catalyst at the time of performing gas-phase catalytic partial oxidation with molecular oxygen by using a tubular reactor. The present invention relates to a catalytic oxidation method using a tubular reactor in which a Mo compound layer containing a Mo compound and a composite oxide catalyst layer containing a Mo composite oxide catalyst are arranged in this order from a reaction raw material supply port side and under a flow of a mixed gas containing 75 vol % of air and 25 vol % of water vapor at 440° C., a Mo sublimation amount of the Mo compound is larger than a Mo sublimation amount of the Mo composite oxide catalyst under the same conditions.

The present disclosure relates to a reactor and a method of operation for an exothermal process being catalyzed by a catalytically active material receiving a reactant gas and providing a product gas, in which said exothermal process has a heat development having a potential for thermally degrading said catalytically active material, and which exothermal process operates at a temperature at which the reactants and at least 80% or all of the products are present as gases, said method comprising the steps of a) directing the reactant gas to a first zone of a material catalytically active in the exothermal process producing an first product gas, and b) directing the first product gas to a second zone of a material catalytically active in the exothermal process producing a product gas, with the option of fully or partially by-passing either said first zone or said second zone, while directing a non-condensing gas stream having a temperature at least 50° C. lower than the product gas to said by-passed zone, wherein the choice of by-passing said zone is made based on the time of operation or a process parameter reflecting the catalytic activity of the zone of catalytically active material which is not by-passed with the associated benefit of reducing the extent of thermal deactivation of the catalytically active material, and thus increasing the overall lifetime of the catalytically active material.

The present disclosure provides a premixer for at least two gases, comprising: a tubular body having a closed end and an opposite, open end; a first flow passage for receiving a first gas, the first flow passage axially extending through the closed end into the tubular body in a sealable manner; a conical tube arranged in the tubular body, wherein a small end of the conical tube communicates with the first flow passage, and a large end of the conical tube extends toward the open end with an edge thereof being fixed to an inner wall of the tubular body, thereby defining a sealed distribution chamber between the tubular body and the conical tube; and a second flow passage arranged on a side portion of the tubular body for receiving a second gas, wherein the second flow passage communicates with the distribution chamber, so that the second gas can be introduced into said conical tube via the distribution chamber in a substantially radial manner. The present disclosure further relates to a radially fixed bed reactor comprising the premixer, a reaction system of oxidative dehydrogenation of butene comprising the racially fixed bed reactor, and a corresponding process.

Systems, processes, and catalysts are disclosed for obtaining fuels and fuel blends containing selected ratios of open-chain and closed-chain fuel-range hydrocarbons suitable for production of alternate fuels including gasolines, jet fuels, and diesel fuels. Fuel-range hydrocarbons may be derived from ethylene-containing feedstocks and ethanol-containing feedstocks.

A fuel synthesis catalyst of an embodiment for hydrogenating a gas includes at least one selected from the group consisting of; carbon dioxide and carbon monoxide, the catalyst comprising, an oxide base material containing at least one oxide selected from the group consisting of; Al.sub.2O.sub.3, MgO, TiO.sub.2, and SiO.sub.2, first metal particles containing at least one metal selected from the group consisting of; Ni, Co, Fe, and Cu and brought into contact with the oxide base material, and a porous oxide layer containing at least one selected from the group consisting of; CeO.sub.2, ZrO.sub.2, TiO.sub.2, and SiO.sub.2 and having an interface with each of the first metal particles and the oxide base material.

A method for producing a conjugated diolefin is configured as follows. A monoolefin having four or more carbon atoms is fed from a plurality of monoolefin feed nozzles. In addition, at least 50% or more of a total amount of an oxygen-containing gas is fed from an oxygen-containing gas feed nozzle located at a bottom of a fluidized bed reactor. Furthermore, the plurality of monoolefin feed nozzles at n places located at heights a1, a2, . . . , and an from the oxygen-containing gas feed nozzle, respectively, feed the monoolefin having four or more carbon atoms at ratios of b1, b2, . . . , bn (b1+b2+ . . . +bn=1), respectively. Furthermore, a weighted mean value represented by the following formula is 100 mm or greater:
weighted mean value=a1*b1+a2*b2+ . . . +an*bn.