Abstract: Plant growth accelerator comprising, as an active ingredient, 5-amino-4-hydroxypentanoic acid of formula (1) H2NCH2CH(OH)CH2CH2COOR1??(1) wherein R1 represents a hydrogen atom or a hydrocarbon group having 1 to 10 carbon atoms, a derivative thereof or a salt thereof.

Abstract: In the hydrocarbon-producing apparatus, a vapor-liquid separation tank of a second vapor-liquid separation unit is provided with a filling material layer. A vapor-liquid separation tank of the first vapor-liquid separation unit has a first return line. The vapor-liquid separation tank of the second vapor-liquid separation unit has a second return line. A light component of light oil discharged from a bottom of the vapor-liquid separation tank is returned to a portion between a top side above a return-location from the second return line within the vapor-liquid separation tank of the second vapor-liquid separation unit, and a line directly connected with a cooler installed on the first vapor-liquid separation unit through the first return line. A heavy component of light oil discharged from a bottom of the vapor-liquid separation tank of the second vapor-liquid separation unit is returned to the filling material layer through the second return line.

Abstract: The hydrocarbon synthesis reaction apparatus according to the present invention includes a reaction vessel that brings a synthesis gas having carbon monoxide gas and hydrogen gas as main components into contact with a slurry having a solid catalyst suspended in a liquid hydrocarbon compound to synthesize a liquid hydrocarbon compound using a Fischer-Tropsch reaction; a filter that is provided within the reaction vessel and is configured to separate the liquid hydrocarbon compound from the catalyst; and a powdered catalyst particles-discharging device configured to discharge powdered catalyst particles in the solid catalyst in the slurry to the outside of the reaction vessel.

Abstract: There are provided a catalyst composition for producing hydrocarbons and a method for producing hydrocarbons which exhibit a high CO conversion rate, generates minimal amount of gaseous components, and is also capable of efficiently obtaining, from a syngas, a gasoline fraction which is selective for and rich in the components having a high octane number, such as aromatic, naphthenic, olefinic and branched paraffinic hydrocarbons, by using a Fischer-Tropsch synthesis catalyst that contains at least one type of metal exhibiting activity in Fischer-Tropsch reaction and manganese carbonate and a zeolite serving as a solid acid.

Abstract: Provided are: a novel yeast having an ability to efficiently produce ethanol from glucose and xylose in a short time in the coexistence of the glucose and the xylose; and a method for producing ethanol using the novel yeast. A yeast, which was designated as Candida intermedia 4-6-4T2 and was deposited as FERN BP-11509.

Abstract: Hydrocarbon oil obtained by Fischer-Tropsch (FT) synthesis reaction using a catalyst within a slurry bed reactor is fractionated into a distilled oil and a column bottom oil in a rectifying column, part of the column bottom oil is flowed into a first transfer line that connects a column bottom of the rectifying column to a hydrocracker, at least part of the column bottom oil is flowed into a second transfer line branched from the first transfer line and connected to the first transfer line downstream of the branching point, the amount of the catalyst fine powder to be captured is monitored while the catalyst fine powder in the column bottom oil that flows in the second transfer line are captured by a detachable filter provided in the second transfer line, and the column bottom oil is hydrocracked within the hydrocracker.

Abstract: A support for hydrocracking catalyst of hydrocarbon oil, which comprises a modified zeolite obtained by incorporating titanium into a faujasite-type zeolite, wherein the modified zeolite satisfies conditions (a) to (e) as described, and to a hydrocracking catalyst employing the support and a method for hydrocracking of hydrocarbon oil containing aromatics using the catalyst.

Abstract: There is provided a method for recovering hydrocarbon compounds from a gaseous by-products generated in the Fisher-Tropsch synthesis reaction, the method comprising a pressurizing step in which the gaseous by-products are pressurized, a cooling step in which the pressurized gaseous by-products are pressurized to liquefy hydrocarbon compounds in the gaseous by-products, and a separating step in which the hydrocarbon compounds liquefied in the cooling step are separated from the remaining gaseous by-products.

Abstract: A catalyst filling apparatus is for a bubble column slurry bed reactor for the FT synthesis reaction. The apparatus includes: a slurry preparation tank installed adjacent to the reactor and configured to prepare a slurry S from a FT synthesis reaction catalyst and a slurry preparation oil; an upper part communication line configured to direct the slurry from the reactor to the slurry preparation tank; a lower part communication line configured to direct the slurry in the slurry preparation tank to the reactor; and a pressure equalizing line configured to communicate the reactor with the slurry preparation tank. The upper part communication line is downwardly inclined from the reactor toward the slurry preparation tank, and the lower part communication line is upwardly inclined from the reactor toward the slurry preparation tank. An inert gas introduction device is provided on the slurry preparation tank.

Abstract: Hydrocarbon oil obtained by Fischer-Tropsch (FT) synthesis reaction using a catalyst within a slurry bed reactor is fractionated into a distilled oil and a column bottom oil in a rectifying column, part of the column bottom oil is flowed into a first transfer line that connects a column bottom of the rectifying column to a hydrocracker, at least part of the column bottom oil is flowed into a second transfer line branched from the first transfer line and connected to the first transfer line downstream of the branching point, the amount of the catalyst fine powder to be captured is monitored while the catalyst fine powder in the column bottom oil that flows in the second transfer line are captured by a detachable filter provided in the second transfer line, and the column bottom oil is hydrocracked within the hydrocracker.

Abstract: The present invention provides a method for producing a hydrocarbon oil, including performing a hydrocracking by continuously feeding, to a hydrocracking reactor containing a hydrocracking catalyst, a wax to be processed including: a raw wax containing 70% by mass or more of straight-chain hydrocarbons with a boiling point of higher than 360° C; and an uncracked wax containing 70% by mass or more of straight-chain hydrocarbons with a boiling point of higher than 360° C, which uncracked wax is separated from a hydrocracking product discharged from the reactor, to thereby yield a hydrocarbon oil including hydrocarbons with a boiling point of 360° C or lower.

Abstract: The hydrotreating catalyst of the present invention is a hydrotreating catalyst including a catalyst support including an amorphous composite metal oxide having solid acidity, and at least one active metal supported by the catalyst support and selected from noble metals of Group 8 to Group 10 in the periodic table, wherein the hydrotreating catalyst contains a carbonaceous substance including a carbon atom, and the content of the carbonaceous substance in the hydrotreating catalyst is 0.05 to 1% by mass in terms of the carbon atom.

Abstract: A Fischer-Tropsch synthesis reaction catalyst includes a catalyst support containing a silica and zirconium oxide in an amount of 0.5 to 14% by mass based on the mass of the catalyst support, and cobalt metal and a cobalt oxide supported on the catalyst support in an amount equivalent to 10 to 40% by mass of tricobalt tetroxide based on the mass of the catalyst, wherein the degree of reduction of the cobalt atoms is within a range from 75 to 93%, and the amount of hydrogen gas adsorption per unit mass of the catalyst at 100° C. is within a range from 0.40 to 1.0 ml/g.

Abstract: A liquid-fuel synthesizing method includes a synthesizing step of synthesizing liquid fuels by making a synthesis gas including a carbon monoxide gas and a hydrogen gas as the main components and a slurry having solid catalyst particles suspended in a liquid react with each other in a reactor, and a synthesis gas supply step of supplying the synthesis gas to the reactor from a plurality of supply devices provided in the reactor so as to have different heights.

Abstract: A synthesis gas production apparatus (reformer) to be used for a synthesis gas production step in a GTL (gas-to-liquid) process is prevented from being contaminated by metal components. A method of suppressing metal contamination of a synthesis gas production apparatus operating for a GTL process that includes a synthesis gas production step of producing synthesis gas by causing natural gas and gas containing steam and/or carbon dioxide to react with each other for reforming in a synthesis gas production apparatus in which, at the time of separating and collecting a carbon dioxide contained in the synthesis gas produced in the synthesis gas production step and recycling the separated and collected carbon dioxide as source gas for the reforming reaction in the synthesis gas production step, a nickel concentration in the recycled carbon dioxide is not higher than 0.05 ppmv.

Abstract: The temperature control system is provided with a lower heat removing unit which is disposed at the bottom of a reactor inside which an exothermic reaction takes place and through which a liquid coolant is flowed, and an upper heat removing unit which is disposed in the reactor further above from the lower heat removing unit and through which the liquid coolant is flowed, recovering reaction heat inside the reactor and controlling a temperature inside the reactor. The lower heat removing unit is supplied with the liquid coolant which is adjusted for temperature by a first temperature adjustment unit, and the upper heat removing unit is supplied with the liquid coolant which is adjusted for temperature by a second temperature adjustment unit different from the first temperature adjustment unit.

Abstract: The hydrocarbon synthesis reaction apparatus is provided with a synthesis gas supply line in which a synthesis gas is compressed and supplied by a first compressor, a reactor configured to accommodate a catalyst slurry, a gas-liquid separator configured to separate an unreacted synthesis gas and hydrocarbons discharged from the reactor into a gas and a liquid, a first recycle line in which the unreacted synthesis gas after separation into a gas and a liquid is compressed and recycled into the reactor by a second compressor, and a second recycle line configured to recycle a residual unreacted synthesis gas after separation into a gas and a liquid into the inlet side of the first compressor at the time of start-up operation when the synthesis gas is gradually increased in the amount to be introduced.

Abstract: The hydrocarbon production apparatus is provided with a gas-liquid separator for cooling gaseous state hydrocarbons drawn out from a gas phase portion of a reactor for the Fischer-Tropsch synthesis reaction and liquefying a portion of the hydrocarbons. A light liquid hydrocarbon supply line for supplying light hydrocarbons is disposed between a downstream side line which is downstream from the last stage of a gas-liquid separating unit of the gas-liquid separator, and an upstream side line which is upstream from the last stage of the gas-liquid separating unit of the gas-liquid separator, wherein the downstream side line is a liquid hydrocarbon line on the downstream side through which the light hydrocarbons having cloud points lower than the temperature at an outlet of a cooler in the last stage of the gas-liquid separating unit are flowed.

Abstract: A method for producing a catalyst for catalytic cracking of a hydrocarbon oil easily produces a catalyst for catalytic cracking of a hydrocarbon oil that exhibits high cracking activity with respect to a heavy hydrocarbon oil, and can produce a gasoline fraction having a high octane number in high yield. The method includes preparing an aqueous slurry that includes 20 to 50 mass % of a zeolite having a sodalite cage structure, 10 to 30 mass % (on a SiO2 basis) of a silica sol, 0.1 to 21 mass % (on an Al2O3.P2O5 basis) of mono aluminum phosphate, and 5 to 65 mass % of a clay mineral on a solid basis, aging the aqueous slurry for 5 to 200 minutes, and spray-drying the aqueous slurry.

Abstract: A hydrogenation treatment catalyst is provided for heavy hydrocarbon oil, in which a hydrogenation-active component is supported on a silica-containing porous alumina carrier containing 0.1% to 1.5% by mass of silica based on the carrier. The total pore volume is 0.55 to 0.75 mL/g. Of the total volume of pores having a pore diameter of 3 to 30 nm (1) 30% to 45% have a pore diameter of 5 to 10 nm, (2) 50% to 65% have a pore diameter of 10 to 15 nm, and (3) the total volume of pores having a pore diameter in a range of ±1 nm from the average pore diameter is 25% or more. The total volume of pores having a pore diameter of 30 nm or more is 3% or less. The average pore diameter of pores having a pore diameter of 10 to 30 nm is 10.5 to 13 nm.