APPARATUS FOR PRODUCING TREATED OIL FOR CRUDE OIL BLENDING, METHOD FOR PRODUCING TREATED OIL FOR CRUDE OIL BLENDING, AND TREATED OIL FOR CRUDE OIL BLENDING
JAPAN ORGANIZATION FOR METALS AND ENERGY SECURITY (Japan)
Inventor
Fukatsu Naoya
Moriyama Taku
Ikeda Kenji
Abstract
Provided is an apparatus for mixing recovered light hydrocarbon, recovered by centrifugation from crude oil sludge, with crude oil and producing a treated oil for crude oil blending, the apparatus for producing treated oil for crude oil blending being characterized by having: a recovered light hydrocarbon storage apparatus for storing the recovered light hydrocarbon in a state heated to or above a temperature that keeps the recovered light hydrocarbon fluid and permits delivery by liquid delivery pump; a first blending apparatus for blending recovered light hydrocarbon and crude oil and obtaining a first blended liquid; a recovered light hydrocarbon supply pipe; a recovered light hydrocarbon discharge apparatus; a first crude oil separation pipe; a first flow rate control apparatus; a second blending apparatus for blending the first blended liquid with crude oil and obtaining a treated oil for crude oil blending; a first blended liquid supply pipe; a first heating apparatus for heating the first blended liquid to a temperature above the precipitation oil of the first blended liquid; a second crude oil separation pipe; and a second flow rate control apparatus. According to the present invention, it is possible to provide a method for treating a recovered light hydrocarbon which is less likely to generate sludge due to the recovered light hydrocarbon in a blended crude oil when blended with crude oil.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 31/10 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
2.
METHOD FOR RECOVERING OIL FRACTION IN CRUDE OIL SLUDGE AND METHOD FOR PRODUCING REGENERATED CRUDE OIL
C10G 31/10 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
B04B 1/20 - Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl
B04B 13/00 - Control arrangements specially designed for centrifugesProgramme control of centrifuges
C02F 11/127 - Treatment of sludgeDevices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
C10G 33/06 - De-watering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
NATIONAL UNIVERSITY CORPORATION SHIZUOKA UNIVERSITY (Japan)
Inventor
Fukuhara Choji
Watanabe Ryo
Miyagi Yuichi
Ohshio Nobuyasu
Abstract
This method for producing an olefin is characterized in that contact of a C5 saturated hydrocarbon and a dehydrogenation catalyst containing at least one metal selected from among transition metals is performed in the presence of hydrogen sulfide to perform a dehydrogenation reaction of the C5 saturated hydrocarbon. According to the present invention, it is possible to provide a method which is for producing an olefin through dehydrogenation of a C5 saturated hydrocarbon and by which the selectivity of diolefins in a product is high.
C07C 5/46 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with sulfur or a sulfur-containing compound as an acceptor
HYDROGENATION TREATMENT CATALYST FOR HYDROCARBON OIL, METHOD FOR PRODUCING HYDROGENATION TREATMENT CATALYST FOR HYDROCARBON OIL, AND HYDROGENATION TREATMENT METHOD FOR HYDROCARBON OIL
The present invention pertains to a hydrogenation treatment catalyst which is for a hydrocarbon oil and in which at least one metal selected from among metals belonging to Group 6 in the periodic table and at least one metal selected from among metals belonging to Group 9 and Group 10 in the periodic table are carried on a zinc and titanium-containing alumina carrier containing zinc and titanium.
B01J 37/02 - Impregnation, coating or precipitation
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
5.
RESIN DISSOLVING METHOD, METHOD FOR PRODUCING DISSOLVED RESIN-CONTAINING LIQUID, METHOD FOR PRODUCING PETROCHEMICAL FEEDSTOCK, METHOD FOR MANUFACTURING PETROLEUM PRODUCT, AND PETROLEUM PRODUCT MANUFACTURING SYSTEM
In this resin dissolving method in which a specific resin is not dissolved but resins other than the specific resin are dissolved from a mixture containing a plurality of types of resins, a solvent, in which the relative energy difference based on the Hansen solubility parameter for the specific resin is greater than 1 and the relative energy difference based on the Hansen solubility parameter for the resins other than the specific resin is at most 1, is selected, and the mixture is brought into contact with the solvent to dissolve the resins other than the specific resin.
C08J 11/08 - Recovery or working-up of waste materials of polymers without chemical reactions using selective solvents for polymer components
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
HYDROPROCESSING CATALYST FOR HEAVY HYDROCARBON OIL, METHOD FOR PRODUCING HYDROPROCESSING CATALYST FOR HEAVY HYDROCARBON OIL, AND METHOD FOR HYDROPROCESSING HEAVY HYDROCARBON OIL
The present invention relates to a hydroprocessing catalyst for a heavy hydrocarbon oil, the hydroprocessing catalyst comprising phosphorus- and zinc-containing alumina that serves as a support and at least one metal selected from group-6 metals on the periodic table and cobalt both supported on the support, in which the phosphorus- and zinc-containing alumina contains phosphorus in an amount of 0.1 to 4% by mass in terms of oxide content relative to the amount of the support and also contains zinc in an amount of 1 to 8% by mass in terms of oxide content relative to the amount of the support, the at least one metal is supported on the support in an amount of 8 to 30% by mass in terms of oxide content relative to the amount of the catalyst, and cobalt is supported on the support in an amount of 2 to 8% by mass in terms of oxide content relative to the amount of the catalyst.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
This naphthene-based solvent is characterized in that: the content therein of a hydrocarbon component having a boiling point of 190-310°C is 90.0 vol% or greater; the content therein of an aromatic hydrocarbon is 1.0 vol% or less; the content therein of a naphthene having two or more rings is 70.0 vol% or greater; the flash point is 70.0°C or greater; and the aniline point is 48.0-75.0°C. The naphthene-based solvent is further characterized in that for a petroleum fraction feedstock thereof: the content therein of a hydrocarbon component having a boiling point of 230-330°C is 90.0 vol% or greater; the content therein of an aromatic hydrocarbon component having 11-18 carbon atoms is 90.0 mass% or greater; the content therein of an aromatic hydrocarbon component having two or more rings is 70.0 mass% or greater; the content therein of a hydrocarbon component having 14-18 carbon atoms is 68.0 mass% or greater; and the content therein of a hydrocarbon component having a boiling point of 250°C or greater is 50.0 vol% or greater. According to the present invention, it is possible to provide a naphthene-based solvent with a low aromatic hydrocarbon content, wherein said naphthene-based solvent has a high flash point and an aniline point that is not excessively low.
Provided is a method for providing a recommended operating condition with which an oil refinery device can be operated more efficiently. A server 20: acquires past operational data for a device, a scheduled operating condition which is an operation condition for the device scheduled by a user, and plant information including at least a usage expiry time of the device; creates a user-specific catalyst deterioration function from the past operational data; calculates, on the basis of the catalyst deterioration function, the plant information, and the schedule operating condition, a recommended operating condition that achieves a catalyst lifetime which is later than the usage expiry time of the device and is earlier than the catalyst lifetime when the device is operated under a scheduled operating condition calculated on the basis of the scheduled operating condition and the catalyst deterioration function; and transmits the recommended operating condition to a user terminal.
G06Q 10/04 - Forecasting or optimisation specially adapted for administrative or management purposes, e.g. linear programming or "cutting stock problem"
A method identifies the molecular structure of each component in a multicomponent mixture. The method includes (1) subjecting the multicomponent mixture to mass spectrometry to identify the formula of a molecule attributed to each obtained peak, and to identify abundance of the molecule; (2) subjecting the multicomponent mixture to collision induced dissociation; (3) performing mass spectrometry on each fragment ion generated via the collision induced dissociation in (2) to identify the core structure forming each fragment ion and abundance thereof; (4) dividing the molecules attributed to each peak in (1) into “classes” based on “a type and number of heteroatoms, and a DBE value”, and on all the molecules belonging to each “class”, estimating the existence state and abundance thereof; and (5) determining the core structure forming each molecule, for which the existence state is estimated in (4), and determining and assigning a side chain and a cross-link thereto.
There is proposed a product yield rate of an FCC device that obtains a product from feedstock oil by fluid catalytic cracking. This device (20) is configured so as to execute: a step (S07) for acquiring user performance information including at least the feedstock oil flow rate, feedstock oil properties, product yield rate balance, and type of catalyst as the actual results of the user's FCC device, and planned operating conditions planned by the user, the planned operating conditions including at least the feedstock oil flow rate and the feedstock oil properties; a step for correcting a yield rate balance calculation function, which calculates the amount of each product produced on the basis of at least the feedstock oil flow rate, the feedstock oil properties, the product yield rate balance, and the type of catalyst, the function being corrected on the basis of a comparison of (a) reference performance information including at least the feedstock oil flow rate, the feedstock oil properties, the product yield rate balance, and the type of catalyst in a bench plant and (b) the user performance information; and a step (S08) for calculating the amount of each product produced as obtained by each of at least one or more types of catalyst using the yield rate balance calculation function corrected on the basis of the planned operating conditions.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
12.
DEVICE FOR SUGGESTING RECOMMENDED CATALYST FOR USE IN FCC DEVICE, METHOD, PROGRAM AND NON-TRANSITORY COMPUTER-READABLE STORAGE MEDIUM
This device for suggesting a recommended catalyst for use in an FCC device is configured to carry out: a step (S02, S10) for acquiring user results information and a planned operating condition; a step (S06) for correcting, on the basis of a comparison between reference results information and the user results information, a yield balance calculation function that calculates production amounts for products on the basis of at least a raw oil flow rate, raw oil characteristics, a product yield balance and a catalyst type; and a step (S13) for communicating to a terminal the catalyst with which the most useful product is obtained, on the basis of weighting coefficients for the usefulness of each product and on the basis of the production amount that is obtained for each product by each of a plurality of catalyst types, said production amount being calculated on the basis of the planned operating condition and a limiting condition for the FCC device from a user.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
13.
DEVICE, METHOD, AND PROGRAM FOR PROPOSING RECOMMENDED CATALYST FOR RF DEVICE, AND NON-TRANSITORY COMPUTER-READABLE RECORDING MEDIUM
A device (20): compares reference performance information with user performance information, corrects a reference operation function, and calculates a user operation function; calculates, for a plurality of types of catalyst, the other of a scheduled number of operation days and a final attainment temperature on the basis of a schedule condition, a constraint condition, a diversion condition, and the user operation function when the RF device of a user is operated under the schedule condition and the diversion condition; and outputs, to a terminal (10), at least one of the types of catalyst with which the other of the calculated scheduled number of operation days and final attainment temperature satisfies the constraint condition, the type of catalyst being outputted as a recommended catalyst.
C10G 35/24 - Controlling or regulating of reforming operations
G06Q 10/04 - Forecasting or optimisation specially adapted for administrative or management purposes, e.g. linear programming or "cutting stock problem"
14.
DEVICE, METHOD, AND PROGRAM FOR PROVIDING OPERATING CONDITION OR PRODUCT COMPOSITION OF RF DEVICE, AND NON-TRANSITORY COMPUTER-READABLE RECORDING MEDIUM
This device is connected to a user terminal via a network and provides an operating condition in the user's RF device. The device: acquires user performance information from the terminal; compares reference performance information with the user performance information; corrects a reference operating function; calculates a user operating function; acquires planned conditions and usage conditions; calculates either the planned number of operation days or the final attainment temperature when the user's RF device is operated under the planned conditions and usage conditions together with a catalyst included in the user performance information, the number or temperature being calculated from the planned conditions, the usage conditions, and the user operating function; and outputs the number or temperature to the terminal.
Provided is a method for providing a recommended operating condition with which an oil refinery device can be operated more efficiently. A server 20: acquires past operational data for a device, a scheduled operating condition which is an operation condition for the device scheduled by a user, and plant information including at least a usage expiry time of the device; creates a user-specific catalyst deterioration function from the past operational data; calculates, on the basis of the catalyst deterioration function, the plant information, and the schedule operating condition, a recommended operating condition that achieves a catalyst lifetime which is later than the usage expiry time of the device and is earlier than the catalyst lifetime when the device is operated under a scheduled operating condition calculated on the basis of the scheduled operating condition and the catalyst deterioration function; and transmits the recommended operating condition to a user terminal.
The objective of the present invention is to provide a method for identifying the molecular structure of each component forming a multicomponent mixture. The method of the present invention comprises: a step 1 of subjecting a multicomponent mixture to mass spectrometry to identify a molecular formula of molecules attributed to each obtained peak, and to identify the abundance of the molecules corresponding to each molecular formula; a step 2 of subjecting the multicomponent mixture to collision-induced dissociation; a step 3 of performing mass spectrometry for each fragment ion generated by means of the collision-induced dissociation in step 2, to identify the configuration and abundance of a core forming each fragment ion; a step 4 of dividing the molecules attributed to each peak in step 1 into a "class" on the basis of the "type and number of heteroatoms, and a DBE value", and, for all the molecules belonging to each "class", estimating a state of existence and the abundance thereof; and a step 5 of determining the structure of the cores forming each molecule of which the state of existence was estimated in step 4, and determining and assigning side chains and cross-links thereto.
G01N 27/62 - Investigating or analysing materials by the use of electric, electrochemical, or magnetic means by investigating the ionisation of gases, e.g. aerosolsInvestigating or analysing materials by the use of electric, electrochemical, or magnetic means by investigating electric discharges, e.g. emission of cathode
19.
SERVER, METHOD, AND PROGRAM FOR SUPPLYING DESULFURIZATION CATALYST-RELATED INFORMATION, AND COMPUTER-READABLE RECORDING MEDIUM RECORDING SAME
Provided are a desulfurization catalyst performance prediction system and a desulfurization catalyst performance prediction program with which the performance of a desulfurization catalyst is predicted with high accuracy, without performing a complicated process such as a plant simulation. A server, which is connected to a user terminal via a network, and which supplies a desulfurization catalyst lifetime of a user plant to a user on the basis of desulfurization catalyst bench plant data and a desulfurization catalyst lifetime function, is equipped with a processor and a storage means that stores computer-readable command. When a computer-readable command is executed by the processor, the server receives user plant-related data and a user desulfurization catalyst performance prediction condition from the user terminal, generates from the desulfurization catalyst lifetime function a user desulfurization catalyst lifetime function tailored to the user plant on the basis of a comparison between the desulfurization catalyst bench plant data and the obtained user plant-related data, calculates a catalyst lifetime for the user's desulfurization catalyst on the basis of the obtained user desulfurization catalyst performance prediction condition and the user desulfurization catalyst lifetime function, and transmits the calculated catalyst lifetime to the user terminal.
Provided are: activated carbon which uses petroleum coke as feedstock and which has a high adsorptive capacity for metal ions such as nickel ions and chromium ions; and a method for producing the same. This method for producing activated carbon is characterized by including: an activation process step of performing an activation process on petroleum coke; and an oxidation treatment step of performing an oxidation treatment on the activated substance of petroleum coke obtained in the activation process step with nitric acid, persulphate, permanganate, hydrogen peroxide, or ozone.
B01J 20/20 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbonSolid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising carbon obtained by carbonising processes
B01J 20/30 - Processes for preparing, regenerating or reactivating
C02F 1/28 - Treatment of water, waste water, or sewage by sorption
21.
THERMALLY CONDUCTIVE FILLER, MIXED THERMALLY CONDUCTIVE FILLER, AND THERMALLY CONDUCTIVE MATERIAL
Provided are a thermally conductive filler comprising an inexpensive carbon material, and a thermally conductive material containing the thermally conductive filler. A thermally conductive filler characterized by being a calcined product of petroleum coke obtained by calcining petroleum coke at 700-2,400°C, the thermally conductive filler having an average particle size of 1-100 μm and a carbon atom content of 88.0-99.9 mass%, the average plane spacing (d002) of the (002) plane by x-ray diffraction being 3.36-3.50 Å; and a thermally conductive material characterized by containing a rubber or resin and the above thermally conductive filler, the thermally conductive material containing 50-450 parts by mass of the above thermally conductive filler per 100 parts by mass of the rubber or resin.
Provided is a resin formulation which, while suppressing an increase in cost, is capable of producing a molded product having a predetermined durability and effectively improving the homogeneity and moldability of the molded product; producing a molded product having a predetermined durability and a sufficiently low linear thermal expansion coefficient, and easily controlling the linear thermal expansion coefficient of the molded product; and producing a molded product having a predetermined durability and a sufficiently high deflection temperature under load. This resin formulation is characterized by containing 20-99 mass% of a resin component and 1-80 mass% of petroleum coke.
A method for recovering an oil fraction in crude oil sludge, characterized in having: a first step (1) for mixing crude oil sludge (A) and crude oil (B), and subsequently heating and stirring the mixture of the crude oil sludge (A) and crude oil (B) to obtain a heated and stirred processed product composed of the crude oil sludge (A) and the crude oil (B); a second step (1) for centrifugally separating the heated and stirred processed product at 40-200°C to thereby separate light liquid from the heavy fraction and obtain a light liquid; and a third step (1) for bringing the temperature of the light liquid to the melting point temperature or greater and mixing the light liquid, which is equal to or greater than the melting point temperature, with crude oil (C) in a crude oil transfer tube, the temperature of the crude oil (C) being equal to or greater than the temperature of the light liquid, alternatively, the temperature of the crude oil (C) being less than that of the light liquid, and the difference between the temperature of the light liquid and the crude oil (C) being within 40°C. The present invention provides a method for recovering an oil fraction in crude oil sludge in which sludge is less likely to be generated even when the oil fraction recovered from the crude oil sludge is mixed with crude oil.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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.
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 49/00 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
C01B 3/54 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids including a catalytic reaction
C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
25.
Hydroprocessing catalyst for heavy hydrocarbon oil, method for manufacturing hydroprocessing catalyst for heavy hydrocarbon oil, and hydroprocessing method for heavy hydrocarbon oil
The hydroprocessing catalyst for a heavy hydrocarbon oil, includes, as a carrier, a phosphorus-silica-containing alumina carrier containing 0.1% by mass to 4% by mass of phosphorus in terms of oxide based on the carrier, and 0.1% by mass to 1.5% by mass of silica based on the carrier, the carrier supporting 8% by mass to 20% by mass of at least one selected from metals in Group 6 of the periodic table in terms of oxide based on the catalyst and 2% by mass to 6% by mass of at least one selected from metals in Groups 8 to 10 of the periodic table in terms of oxide based on the catalyst.
B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
B01J 27/182 - PhosphorusCompounds thereof with silicon
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
B01J 35/10 - Solids characterised by their surface properties or porosity
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
Hydrogenation catalyst for heavy hydrocarbon oil, production method for hydrogenation catalyst for heavy hydrocarbon oil, and hydrogenation method for heavy hydrocarbon oil
The hydrogenation catalyst for heavy hydrocarbon oil, includes: as a carrier, phosphorous-zinc-containing alumina that contains 0.1% by mass to 4% by mass, in terms of oxide based on the carrier, of phosphorous and 1% by mass to 12% by mass, based on the carrier, of zinc oxide particles, and supporting, on the carrier, 8% by mass to 20% by mass, in terms of oxide based on the catalyst, of at least one selected from metals in Group 6 of the periodic table and 2% by mass to 6% by mass, in terms of oxide based on the catalyst, of at least one selected from metals in Groups 8 to 10 of the periodic table, and the average particle diameter of the zinc oxide particles being 2 μm to 12 μm.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C10G 45/04 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used
B01J 35/10 - Solids characterised by their surface properties or porosity
B01J 37/02 - Impregnation, coating or precipitation
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
A hydrodesulfurization catalyst supports one or more metals selected from elements in Group 6 of the Periodic table, one or more metals selected from elements in Group 9 or Group 10 of the same, phosphorus, and an organic acid on a composite oxide support having a specific content of both alumina and HY zeolite having a specific crystallite size. The catalyst includes 10% to 40% by mass of the Group 6 metal, 1% to 15% by mass of the Group 9 or Group 10 metal, and 1.5% to 8% by mass of phosphorus in terms of an oxide based on the catalyst. The catalyst includes 0.8% to 7% by mass of carbon derived from an organic acid and for 1 mole of the Group 9 or Group 10 element metal in terms of an element based on the catalyst, and includes 0.2 to 1.2 moles of the organic acid.
C10G 45/12 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
B01J 29/16 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 31/34 - Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups of chromium, molybdenum or tungsten
B01J 35/10 - Solids characterised by their surface properties or porosity
30.
Method for manufacturing catalytic cracking catalyst for hydrocarbon oil
5 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.
A01N 33/04 - Nitrogen directly attached to aliphatic or cycloaliphatic carbon atoms
A01N 37/44 - Biocides, pest repellants or attractants, or plant growth regulators containing organic compounds containing a carbon atom having three bonds to hetero atoms with at the most two bonds to halogen, e.g. carboxylic acids containing at least one carboxylic group or a thio-analogue, or a derivative thereof, and a nitrogen atom attached to the same carbon skeleton by a single or double bond, this nitrogen atom not being a member of a derivative or of a thio-analogue of a carboxylic group, e.g. amino-carboxylic acids
Provided is a method for simply producing xylene with high yield even though a catalytically cracked gasoline, which has a low aromatic hydrocarbon content ratio and contains an unsaturated hydrocarbon, a sulfur content, a nitrogen content and the like, is used as a starting material for a conversion reaction such as a disproportionation reaction or a transalkylation reaction. A method for producing xylene, which is characterized by comprising: (a) a fractional distillation step for obtaining a distillate fraction having a boiling point range of 145-205°C by fractional distillation by subjecting a fluid catalytically cracked gasoline to distillation; (b) a hydrogenation step for adjusting the sulfur content to 0-6 ppm by mass and the nitrogen content to 0-6 ppm by mass by subjecting the distillate fraction obtained in the fractional distillation step (a) and having a boiling point range of 145-205°C to a hydrodesulfurization/denitrification reaction; and (c) a disproportionation/transalkylation step for subjecting a product oil obtained in the hydrogenation step (b) and containing an aromatic hydrocarbon to a disproportionation reaction or a transalkylation reaction.
C07C 5/27 - Rearrangement of carbon atoms in the hydrocarbon skeleton
C07C 6/12 - Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
Provided is a method for producing xylene with high yield by selecting an adequate starting material oil in cases where xylene is produced by subjecting a starting material oil composed of a petroleum fraction to a disproportionation reaction or a transalkylation reaction. A method for producing xylene by subjecting a starting material oil, which comprises a petroleum fraction as a base material, to a transalkylation reaction or a disproportionation reaction. This method for producing xylene is characterized in that an oil, which contains an alkyl benzene having 7-10 carbon atoms or the like, and wherein the average number of methyl groups directly bonded to each benzene ring of the alkyl benzene or the like is 1.2 to 2.8, is used as the starting material oil.
C07C 6/12 - Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
A start-up method for a hydrocarbon synthesis reaction apparatus, comprising: an initial slurry-loading step in which the slurry is loaded into the reactor at the initial stage of the Fischer-Tropsch synthesis reaction at a lower loading rate than that applied to the reactor in a steady-state operation; and a CO conversion ratio-increasing step in which the liquid level of the slurry in the reactor is raised by adding to the slurry the hydrocarbons synthesized at the early stage of the Fischer-Tropsch synthesis reaction so that the CO conversion ratio is increased in proportion to a rise in the liquid level of the slurry in the reactor.
Provided are: a solid acid catalyst produced from a starting material that can be obtained easily and in large quantities; and a method for producing same. The solid acid catalyst is characterized by a sulfonic acid group being introduced into petroleum coke. In the solid acid catalyst, 1-6 mmol of the sulfonic acid group is preferably contained per gram of solid acid catalyst, oxygen is preferably bonded to 10-30% of the carbon atoms among all the carbon atoms in the solid acid catalyst, and the petroleum coke preferably has a sulfur content in the dry state of 5-12 mass%. Also, the method for producing a solid acid catalyst is characterized by the petroleum coke being processed in sulfuric acid or fuming sulfuric acid at 20-300°C.
C07C 67/08 - Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
C07C 69/24 - Esters of acyclic saturated monocarboxylic acids having the carboxyl group bound to an acyclic carbon atom or to hydrogen having three or more carbon atoms in the acid moiety esterified with monohydroxylic compounds
36.
FINELY PULVERIZED PETROLEUM COKE, FIRED FINELY PULVERIZED PETROLEUM COKE, FILLER FOR RUBBER COMPOSITION, AND RUBBER COMPOSITION
Provided are finely pulverized petroleum coke and fired finely pulverized petroleum coke that can be suitably used as a filler for rubber compositions; also provided are a filler for rubber compositions and a rubber composition that effectively improve durability, particularly when used in tire parts, while suppressing an increase in cost. Finely pulverized petroleum coke having an average particle size (D50) of from more than 0 μm to 50 μm or less, fired finely pulverized petroleum coke having an average particle size (D50) of from more than 0 μm to 50 μm or less that is obtained by firing and pulverizing petroleum coke, filler for rubber compositions obtained by pulverizing petroleum coke, and a rubber composition obtained by combining this finely pulverized petroleum coke or fired finely pulverized petroleum coke.
A production method for activated carbon, the method characterized by having an activation step that is for obtaining activated carbon by means of activating petroleum coke, the petroleum coke including petroleum coke that has a particle size of 100 μm or less. The present invention can provide a production method for activated carbon whereby activated carbon that has a large specific surface area can be produced using petroleum coke as a raw material that undergoes activation processing.
B01J 20/20 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbonSolid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising carbon obtained by carbonising processes
B01J 20/28 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof characterised by their form or physical properties
B01J 20/30 - Processes for preparing, regenerating or reactivating
38.
Catalyst for catalytic cracking of hydrocarbon oil and method for catalytic cracking of hydrocarbon oil
A catalyst for catalytic cracking of a hydrocarbon oil can produce a gasoline fraction having a high octane number in high yield while suppressing an increase in yield of a heavy distillate, and produce LPG having a high propylene content in high yield. The catalyst includes a specific amount of a granulated catalyst A that includes a zeolite having a sodalite cage structure, silicon derived from a silica sol, phosphorus and aluminum derived from mono aluminum phosphate, a clay mineral, and a rare-earth metal, and a specific amount of a granulated catalyst B that includes a pentasil-type zeolite, the ratio of the mass of phosphorus and aluminum derived from mono aluminum phosphate included in the granulated catalyst A to the mass of the pentasil-type zeolite included in the granulated catalyst B being 0.015 to 3000.
B01J 38/12 - Treating with free oxygen-containing gas
B01J 29/70 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups
HYDROPROCESSING CATALYST FOR HEAVY HYDROCARBON OIL, METHOD FOR MANUFACTURING HYDROPROCESSING CATALYST FOR HEAVY HYDROCARBON OIL, AND HYDROPROCESSING METHOD FOR HEAVY HYDROCARBON OIL
In order to provide a hydroprocessing catalyst capable of improving the storage stability of a hydroprocessed heavy hydrocarbon oil without reducing the desulfurization activity and demetalization activity, a method for manufacturing the hydroprocessing catalyst, and a method for hydroprocessing a heavy hydrocarbon oil using the hydroprocessing catalyst, the present invention provides a hydroprocessing catalyst for a heavy hydrocarbon oil characterized in having, as a carrier, a phosphorus/silica-containing alumina containing 0.1-4 mass% of phosphorus based on the carrier and in terms of an oxide and 0.1-1.5 mass% of silica based on the carrier, the carrier carrying 8-20 mass% of at least one metal selected from group 6 metals on the periodic table based on the catalyst and in terms of an oxide and 2-6 mass% of at least one metal selected from group 8-10 metals on the periodic table based on the catalyst and in terms of an oxide.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
40.
HYDROGENATION CATALYST FOR HEAVY HYDROCARBON OIL AND HYDROGENATION METHOD FOR HEAVY HYDROCARBON OIL
The purpose of the present invention is to provide: a hydrogenation catalyst capable of improving the storage stability of hydrogenated heavy hydrocarbon oil without reducing desulfurization activity or demetalization activity; and a method for hydrogenation of heavy hydrocarbon oil by using said hydrogenation catalyst. Provided is a hydrogenation catalyst for heavy hydrocarbon oil, characterized by: at least one type of group 6 metal of the periodic table being held by a zinc-containing alumina carrier containing 1%-15%, by carrier mass, of zinc oxide particles having an average particle diameter of 2-12 µm; by the average pore diameter being 18-35 nm, and the specific surface area being 70-150 m2/g. Also provided is a hydrogenation method for heavy hydrocarbon oil, characterized by catalytic reaction of a heavy hydrocarbon oil in the presence of the hydrogenation catalyst, at a temperature of 300-420°C, at a pressure of 3-20 MPa, at a hydrogen/oil ratio of 400-3,000 m3/m3, and at a liquid space velocity of 0.1-3 h-1.
B01J 35/10 - Solids characterised by their surface properties or porosity
C10G 45/04 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used
41.
HYDROGENATION TREATMENT CATALYST FOR HEAVY HYDROCARBON OIL, AND METHOD FOR HYDROGENATION TREATMENT OF HEAVY HYDROCARBON OIL
The purpose of the present invention is to provide a hydrogenation treatment catalyst capable of improving the storage stability of hydrogenated heavy hydrocarbon oil, and a method for hydrogenation treatment of heavy hydrocarbon oil in which the hydrogenation treatment catalyst is used. The present invention provides a hydrogenation treatment catalyst for heavy hydrocarbon oil, in which a hydrogenation active component is carried on a silica-containing porous alumina carrier containing silica at an amount of 0.1-1.5 mass% based on the carrier, the total pore volume is 0.55-0.75 mL/g, (1) the total volume of pores having a pore diameter of 5-10 nm is 30-45% of the total volume of pores having a pore diameter of 3-30 nm, (2) the total volume of pores having a pore diameter of 10-15 nm is 50-65% of the total volume of pores having a pore diameter of 3-30 nm, (3) the total volume of pores having a pore diameter of 30 nm or above is equal to or less than 3% of the total pore volume, (4) the average pore diameter of pores having a pore diameter of 10-30 nm is 10.5-13 nm, and (5) the total volume of pores having a pore diameter in a range of ± 1 nm from the average pore diameter is equal to or greater than 25% of the total volume of pores having a pore diameter of 3-30 nm.
B01J 35/10 - Solids characterised by their surface properties or porosity
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
42.
HYDROGENATION CATALYST FOR HEAVY HYDROCARBON OIL, PRODUCTION METHOD FOR HYDROGENATION CATALYST FOR HEAVY HYDROCARBON OIL, AND HYDROGENATION METHOD FOR HEAVY HYDROCARBON OIL
The purpose of the present invention is to provide: a hydrogenation catalyst capable of improving the storage stability of hydrogenated heavy hydrocarbon oil without reducing desulfurization activity or demetalization activity; and a method for hydrogenation of heavy hydrocarbon oil by using said hydrogenation catalyst. Provided is a hydrogenation catalyst for heavy hydrocarbon oil characterized by: using as a carrier a phosphorous-zinc containing alumina that contains 0.1%-4% phosphorous, by carrier mass and in terms of oxide content, and 1%-12% zinc oxide particles, by carrier mass; carrying on said carrier 8%-20%, by catalyst mass and in terms of oxide content, at least one type selected from group 6 metal on the periodic table and carrying 2%-6%, by catalyst mass and in terms of oxide content, at least one type selected from group 8-10 metals on the periodic table; and the average particle diameter of the zinc oxide particles being 2-12 µm.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
43.
Start-up method of bubble column slurry bed reactor
A start-up method of a bubble column slurry bed reactor for producing hydrocarbons includes: a first step that fills into a reactor a slurry in which a Fischer-Tropsch synthesis reaction catalyst particles are suspended in a slurry preparation oil with a 5% distillation point of 120 to 270° C., a 95% distillation point of 330 to 650° C., and a sulfur component and an aromatic component of 1 mass ppm or less, and a second step that, in a state where synthesis gas that is primarily hydrogen and carbon monoxide is introduced into the slurry filled into the reactor, raises the temperature of the reactor and starts the Fischer-Tropsch synthesis reaction. As the slurry preparation oil, one containing predetermined components in preset amounts is used. In the first step, the slurry is filled into the reactor in an amount in which airborne droplets do not flow out.
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
44.
Diesel fuel or diesel fuel base stock and production method thereof
Provided is a hydrotreating step (A) containing a hydroisomerization step (A1) that obtains a hydroisomerized oil (a1) by bringing a FT synthesis oil into contact with a hydroisomerization catalyst and/or a hydrocracking step (A2) that obtains a hydrocracked oil (a2) by bringing it into contact with a hydrocracking catalyst, and a fractionation step (B) that transfers at least a portion of the hydrotreated oil (a) composed of the hydroisomerized oil (a1) and/or the hydrocracked oil (a2) to a fractionator and, at the very least, obtains a middle distillate (b1) with a 5% distillation point of 130 to 170° C. and a 95% distillation point of 240 to 300° C., and a heavy oil (b2) that is heavier than the middle distillate (b1).
C10G 67/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
C10L 1/06 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
C10L 10/14 - Use of additives to fuels or fires for particular purposes for improving low temperature properties
C10G 65/14 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
C10G 45/58 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
45.
Hydrocarbon production apparatus and hydrocarbon production process
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.
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/08 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with moving particles
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/24 - Stationary reactors without moving elements inside
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C07C 1/00 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
C07C 1/02 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon
46.
Hydrogenation refining catalyst and method for producing a hydrocarbon oil
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.
C10G 45/64 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
C10G 45/62 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
C10G 45/60 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used
C10G 45/70 - Aromatisation of hydrocarbon oil fractions with catalysts containing platinum group metals or compounds thereof
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
A process for producing a kerosene base fuel according to the present invention comprises removing paraffins having carbon number of 7 or less from a first fraction having an initial boiling point of 95 to 140° C. and a final boiling point of 240 to 280° C. obtained from a hydrotreated oil of a Fischer-Tropsch synthetic oil to obtain a second fraction having a content of paraffins having carbon number of 7 or less of 0.1 to 0.7% by mass.
This catalyst is a hydrogenation desulfurization catalyst that supports one or more metals selected from a group formed from the group 6 elements of the long period periodic table, one or more metals selected from a group formed from the group 9 elements and the group 10 elements of the same, phosphorus, and an organic acid on a composite oxide carrier having a specific content of both alumina and HY zeolite having a specific crystallite size and the like. The catalyst basis in an oxide conversion includes 10 - 40% by mass of the group 6 metal, 1 - 15% by mass of the group 9 and group 10 metals, and 1.5 - 8% by mass phosphorus. The catalyst basis in an element conversion includes 0.8 - 7 percent by mass of carbon derived from an organic acid and for each mole of the group 9 element and group 10 element metals, the same includes 0.2 - 1.2 moles of the organic acid. The average poor diameter at a specific surface area, pore volume, and pore distribution is within a specific range.
B01J 31/34 - Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups of chromium, molybdenum or tungsten
B01J 35/10 - Solids characterised by their surface properties or porosity
B01J 37/02 - Impregnation, coating or precipitation
C10G 45/12 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
This hydrocarbon synthesis apparatus is provided with: a reactor for bringing a syngas which comprises carbon monoxide gas and hydrogen gas as main components into contact with a slurry obtained by suspending a solid catalyst in a liquid hydrocarbon compound, and thus synthesizing liquid hydrocarbon compounds by a Fischer-Tropsch process; a filter which is provided in the reactor and which separates the liquid hydrocarbon compounds from the catalyst; and a pulverized catalyst particles discharging means for discharging pulverized catalyst particles to the outside of the reactor, said pulverized catalyst particles being formed by pulverization of the solid catalyst contained in the slurry.
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
B03B 5/28 - Washing granular, powdered or lumpy materialsWet separating by sink-float separation
B03B 5/64 - Washing granular, powdered or lumpy materialsWet separating by hydraulic classifiers, e.g. of launder, tank, spiral or helical chute concentrator type of the free settling type
In a hydrocarbon production apparatus, a filler layer is provided at an intermediate position in a gas/liquid separation vessel of a second gas/liquid separation unit, a first return line is provided in a gas/liquid separation vessel of a first gas/liquid separation unit, and a second return line is provided in the gas/liquid separation vessel of the second gas/liquid separation unit. In the first gas/liquid separation unit, a light fraction of a light oil, which is introduced from the bottom of the gas/liquid separation vessel, is returned, through the first return line, to a part which is located between a position closer to the top part relative to a return part of the second return line in the gas/liquid separation vessel of the second gas/liquid separation unit and a position located on a line right in front of the cooler in the first gas/liquid separation unit. In the second gas/liquid separation unit, a heavy fraction of the light oil, which is introduced from the bottom of the gas/liquid separation vessel of the second gas/liquid separation unit, is returned to the filler layer through the second return line.
Provided is a method for easily manufacturing a catalytic cracking catalyst for hydrocarbon oil having high cracking activity when used on heavy hydrocarbon oil and allowing production with a high yield ratio of a gasoline fraction with a high octane value. A method for manufacturing a catalytic cracking catalyst for hydrocarbon oil, characterized in that when the solid content is converted, an aqueous slurry is produced containing 20-50 mass% of a zeolite having a sodalite cage structure, 10-30 mass% of silica sol in terms of SiO2 conversion, 0.1-21 mass% of a first aluminum phosphate in terms of Al2O3⋅3P2O5 conversion, and 5-65 mass% of a clay mineral, after which the slurry is aged for 5-200 minutes and then spray-dry processed.
B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
B01J 29/08 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y
B01J 29/16 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
C10G 11/05 - Crystalline alumino-silicates, e.g. molecular sieves
52.
METHOD FOR PRODUCING 5-AMINOLEVULINIC ACID OR SALT THEREOF
Provided is a method for producing 5-aminolevulinic acid or a salt thereof at a high yield using microorganisms that produce 5-aminolevulinic acid. A method for producing 5-aminolevulinic acid or a salt thereof characterized by culturing microorganisms that produce 5-aminolevulinic acid in a medium containing one or more selected from L-arginine, glutamic acid, and salts of these; wherein the content of glutamic acid or salt thereof is 42 mM-100 mM in terms of glutamic acid in the medium.
Provided is a method for producing ethanol with high efficiency even when a fermentation inhibitor is present in a hydrolysate of a cellulosic biomass. A method for producing ethanol, characterized by fermenting a fermentation solution containing a hydrolysate of a cellulosic biomass using yeast belonging to Candida intermedia under such conditions that the rate of supply of air into a fermentation vessel becomes 0.0001 to 100 L/hr/g dry cell weight.
A plant growth accelerator which contains, as an active ingredient, a 5-amino-4-hydroxypentanoic acid represented by general formula (1), a derivative thereof, or a salt of the compound or the derivative. H2NCH2CH(OH)CH2CH2COOR1 (1) (In the formula, R1 represents a hydrogen atom or a hydrocarbon group having 1-10 carbon atoms.)
A01N 37/44 - Biocides, pest repellants or attractants, or plant growth regulators containing organic compounds containing a carbon atom having three bonds to hetero atoms with at the most two bonds to halogen, e.g. carboxylic acids containing at least one carboxylic group or a thio-analogue, or a derivative thereof, and a nitrogen atom attached to the same carbon skeleton by a single or double bond, this nitrogen atom not being a member of a derivative or of a thio-analogue of a carboxylic group, e.g. amino-carboxylic acids
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.
F25J 3/08 - Separating gaseous impurities from gases or gaseous mixtures
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 31/06 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
A hydrocarbon synthesis reaction apparatus according to the present invention is provided with: a reactor for bringing a synthetic gas into contact with a slurry that is produced by suspending a solid catalyst in a liquid hydrocarbon, thereby synthesizing a hydrocarbon through a Fischer-Tropsch synthesis reaction; a cylindrical inner tube which is arranged in the reactor in such a manner that there is a space between the lower end of the inner tube and the bottom of the reactor; and a sparger which is arranged on the inner lower side of the inner tube and can blow the synthetic gas into the inside of the inner tube. When the slurry is introduced into the reactor until the position of the upper end of the inner tube becomes lower than the liquid level of the slurry, a Fischer-Tropsch synthesis reaction zone is formed in a space between an extended part from the upper end of the inner tube and the inner surface of the reactor, wherein the slurry containing bubbles flows into the Fischer-Tropsch synthesis reaction zone from the inside of the inner tube via the upper end of the inner tube.
The present invention provides a method for producing a hydroprocessing catalyst including a supporting step of allowing a catalyst support having a content of a carbonaceous substance containing carbon atoms of 0.5% by mass or less in terms of carbon atoms to support an active metal component containing at least one active metal element selected from metals belonging to Group 6, Group 8, Group 9 and Group 10 in the periodic table, to obtain a catalyst precursor, and a calcining step of calcining the catalyst precursor obtained in the supporting step to obtain the hydroprocessing catalyst.
B01J 29/10 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
B01J 29/16 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
C10G 47/14 - Inorganic carriers the catalyst containing platinum group metals or compounds thereof
C10G 65/14 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
C10G 45/10 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing platinum group metals or compounds thereof
C10G 49/06 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing platinum group metals or compounds thereof
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.
C07C 1/00 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
C07C 1/02 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles
B01J 8/20 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/24 - Stationary reactors without moving elements inside
59.
START UP METHOD FOR HYDROCARBON SYNTHESIS REACTION APPARATUS
This start up method for a hydrocarbon synthesis reaction apparatus is provided with: an initial slurry-filling step in which, during start up, the inside of a reaction vessel is filled with an initial preparation slurry amount which is less than a slurry amount during steady operation; and a CO-conversion-rate increasing step in which hydrocarbons to be synthesized when operation is initiated are added to the slurry to increase the height of the liquid level of the slurry, and the CO conversion rate is increased in accordance with the increase in the height of the liquid level of the slurry.
The hydrocracking catalyst of the present invention is a hydrocracking catalyst comprising a catalyst support comprising a zeolite and 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 hydrocracking catalyst contains a carbonaceous substance comprising a carbon atom, and the content of the carbonaceous substance in the hydrocracking catalyst is 0.05 to 1% by mass in terms of the carbon atom.
C10G 47/18 - Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
C10G 45/60 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used
C10G 45/70 - Aromatisation of hydrocarbon oil fractions with catalysts containing platinum group metals or compounds thereof
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
C10G 45/62 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
C10G 45/64 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
61.
Method for starting up bubble-column-type slurry-bed reactor, start-up solvent, and method for producing hydrocarbon oil
A method for starting up a bubble column slurry bed reactor of the present invention includes, when restarting operation of a bubble column slurry bed reactor for producing hydrocarbons by the Fischer-Tropsch synthesis reaction, feeding a hydroprocessed oil produced in the bubble column slurry bed reactor and hydroprocessed that contains 40% by mass or more of paraffin hydrocarbons having carbon number of 21 or more and that has a peroxide value of 1 ppm or less, to the bubble column slurry bed reactor.
A catalyst for the catalytic cracking of a hydrocarbon oil is provided with which it is possible to produce a gasoline fraction with a high octane number in high yield while inhibiting the yield of heavy fractions from increasing, in particular, it is possible to produce LPG with a high propylene content in high yield. The catalyst for the catalytic cracking of a hydrocarbon oil is characterized by comprising a given amount of catalyst granules (A) which comprise a zeolite having a sodalite cage structure, silicon derived from a silica sol, phosphorus and aluminum that are derived from aluminum primary phosphate, a clay mineral, and a rare-earth metal and a given amount of catalyst granules (B) which contain a pentasil type zeolite, the ratio represented by (mass of the phosphorus and aluminum derived from aluminum primary phosphate that constitute the catalyst granules (A))/(mass of the pentasil type zeolite constituting the catalyst granules (B)) being 0.015-3,000.
A method for estimating a particulate content in a slurry of the present invention is a method for estimating a content of particulates having a predetermined particle size or less in a slurry with solid particles dispersed in hydrocarbons including a wax, the method including, based on a correlation between a visible light transmittance and a content of solid particles having the predetermined particle size or less at a temperature at which hydrocarbons including a wax are liquefied when the solid particles having the predetermined particle size or less are dispersed in the hydrocarbons, estimating a content of particulates having the predetermined particle size or less in the slurry from a visible light transmittance of a supernatant part when the slurry is left to stand at the temperature.
C07C 27/00 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds
G01N 31/10 - Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroupsApparatus specially adapted for such methods using catalysis
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
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.
C10G 49/02 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used
C10G 47/02 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used
B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
65.
Method of suppressing metal contamination of synthesis gas production apparatus
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.
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 49/00 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
C01B 3/54 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids including a catalytic reaction
C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
66.
Activated fischer-tropsch synthesis reaction catalyst and method for producing hydrocarbons
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.
The method for stopping operation of a reactor is provided with a stop step of stopping supply of a synthesis gas containing a carbon monoxide gas and a hydrogen gas into the reactor; a slurry discharge step of discharging slurry from the reactor; a steam supply step of supplying steam higher in temperature than the decomposition temperatures of metal carbonyls into the reactor, thereby discharging gaseous matters inside the reactor; and a carbon monoxide gas detecting step of detecting an amount of carbon monoxide gas contained in the gaseous matters discharged from the reactor. In the steam supply step, supply of the steam is stopped when an amount of the detected carbon monoxide gas continuously declines to be lower than a predetermined reference value.
A catalyst recovery system that includes a concentrated slurry production unit that concentrates a slurry extracted from a reactor main unit and continuously produces a concentrated slurry, a first discharge unit that discharges the concentrated slurry from the concentrated slurry production unit, a solidified slurry production unit that cools the concentrated slurry discharged from the concentrated slurry production unit, thereby solidifying the liquid medium within the concentrated slurry and producing a solidified slurry, and a recovery mechanism that recovers the solidified slurry from the solidified slurry production unit.
Provided is a catalyst packing device disposed at a bubble tower-type slurry bed reactor for FT synthesis. The packing device comprises, disposed adjacent to the reactor, a slurry preparation cell for preparing a slurry S from an FT synthesis catalyst and a slurry preparation oil, a top communicating pipe for guiding slurry from the reactor to the slurry preparation cell and a bottom communicating pipe for guiding slurry from the slurry preparation cell to the reactor, and an equalizing pipe for communication between the inside of the reactor and the inside of the slurry preparation cell. The top communicating pipe is inclined down from the reactor toward the slurry preparation cell and the bottom communicating pipe is inclined up from the reactor toward the slurry preparation cell. Inert gas introduction means for introducing inert gas are disposed at the slurry preparation cell.
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
70.
METHOD FOR STARTUP OF BUBBLE TOWER-TYPE SLURRY BED REACTOR
Provided is a method for the startup of a bubble tower-type slurry bed reactor for producing hydrocarbons by Fischer-Tropsch synthesis. The method comprises a first step for filling in a reactor a slurry obtained by suspending a Fisher-Tropsch synthesis catalyst in an oil for preparing a slurry having a 5% distillation temperature between 120 and 270ºC, a 95% distillation temperature between 330 and 650ºC, and a sulfur content and aromatic content of 1 ppm or less in terms of mass, and a second step for initiating Fischer-Tropsch synthesis by raising the temperature of the reactor, with synthetic gas that is primarily hydrogen and carbon monoxide already being introduced to the slurry filled in the reactor. The oil for slurry preparation is an oil that contains a predetermined amount of specific components. During the first step, the slurry is filled into the reactor in an amount such that none sprays out from the reactor.
This process for manufacturing a diesel fuel base comprises: (A) a hydrogenation step that includes (A1) a hydroisomerization step of bringing an FT synthetic oil into contact with a hydro- isomerization catalyst to obtain a hydroisomerized oil (a1) and/ or (A2) a hydrocracking step of bringing an FT synthetic oil into contact with a hydrocracking catalyst to obtain a hydrocracked oil (a2); and (B) a rectification step of transferring at least a part of a hydrogenated oil (a) consisting of the hydroisomerized oil (a1) and/or the hydrocracked oil (a2) into a rectifying column to obtain, at least, an intermediate fraction (b1) which has a 5% distillation temperature of 130 to 170°C and a 95% distillation temperature of 240 to 300°C and a heavy oil (b2) which is heavier than the intermediate fraction (b1).
C10G 65/14 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
C10G 45/62 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
JAPAN OIL, GAS AND METALS NATIONAL CORPORATION (Japan)
INPEX CORPORATION (Japan)
JX NIPPON OIL & ENERGY CORPORATION (Japan)
JAPAN PETROLEUM EXPLORATION CO., LTD. (Japan)
COSMO OIL CO., LTD. (Japan)
NIPPON STEEL ENGINEERING CO., LTD. (Japan)
Inventor
Tasaka, Kazuhiko
Abstract
A startup method for a fractionator that is supplied with, and fractionally distills, a hydrocracked product obtained in a wax fraction hydrocracking step by hydrocracking a wax fraction contained within a Fischer-Tropsch synthetic oil, the method including a preheating step of preheating the fractionator using a hydrocarbon oil that includes at least a portion of the hydrocracked product and is liquid at a normal temperature and normal pressure.
Provided are: novel yeast capable of producing ethanol with high efficiency within a short time from glucose and xylose in the co-presence of glucose and xylose; and a method for producing ethanol using the yeast. Yeast that is designated Candida intermedia 4-6-4T2 and is deposited under the accession number of FERM BP-11509.
This cleaning device is for filters used in a reaction system provided with: a reaction tank having a filter; a first transport pipe, one end of which is connected to a filter; a recovery tank connected to the other end of the first transport pipe; and a second transport pipe one end of which is connected to the recovery tank. This cleaning device is provided with: a first return pipe, one end of which is connected to the second transport pipe; a first backwash fluid tank and a second backwash fluid tank connected to the first return pipe; a first flow rate adjusting valve that can adjust filtered fluid supplied to the first backwash fluid tank; a second flow rate adjusting valve that can adjust filtered fluid supplied to the second backwash fluid tank; and a switching unit that switches and transports either of the filtered fluids accommodated in the two backwash fluid tanks.
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
This temperature control system collects reaction heat within a reaction apparatus wherein a heat generation reaction occurs, controlling temperature within the reaction apparatus. The temperature control system comprises: a coolant drum wherein vapor and liquid coolants are stored in a vapor-liquid equilibrium state; a heat removal unit which is disposed with the reaction apparatus and which vaporizes some of the liquid coolant which is supplied from the coolant drum with the reaction heat; a return pipe which returns a multiphase fluid of vapor which arises in the heat removal unit and the liquid coolant to the coolant drum; a vapor exhaust pipe which supplies the vapor in the coolant drum externally to the assembly; and a supplement tube which supplies supplemental water to the return pipe at a quantity which is estimated from the quantity of vapor which is discharged externally to the assembly.
Japan Oil, Gas and Metals National Corporation (Japan)
Inpex Corporation (Japan)
JX Nippon Oil & Energy Corporation (Japan)
Japan Petroleum Exploration Co., Ltd. (Japan)
Cosmo Oil Co., Ltd. (Japan)
Nippon Steel Engineering Co., Ltd. (Japan)
Inventor
Tasaka, Kazuhiko
Abstract
In a process for producing hydrocarbons according to the present invention, estimated production rates for a light hydrocarbon oil and a heavy hydrocarbon oil are respectively determined based on a set reaction temperature used when the hydrocarbons are synthesized by a Fischer-Tropsch synthesis reaction, and the discharge flow rates of the light hydrocarbon oil and the heavy hydrocarbon oil from temporary storage buffer tanks (91, 92) during supply to a fractionator (40) are respectively controlled so as to be equal to the respective estimated production rates.
Japan Oil, Gas and Metals National Corporation (Japan)
Inpex Corporation (Japan)
JX Nippon Oil & Energy Corporation (Japan)
Japan Petroleum Exploration Co., Ltd. (Japan)
Cosmo Oil Co., Ltd. (Japan)
Nippon Steel Engineering Co., Ltd. (Japan)
Chiyoda Corporation (Japan)
Inventor
Hodoshima, Shinya
Yagi, Fuyuki
Wakamatsu, Shuhei
Kawazuishi, Kenichi
Abstract
A situation where sulfur compounds originating from a castable are mixed into synthesis gas produced by way of a reforming reaction and the mixed sulfur compounds are separated and collected with carbon dioxide and further fed into a reformer to thereby degrade the reforming catalyst of the reformer by sulfur poisoning is avoided. Purge gas that is steam or steam-containing gas is made to flow into the piping to be used for a synthesis gas production apparatus and dried out to remove the sulfur compounds contained in the castable prior to the start-up of operation of the synthesis gas production apparatus, in order to prevent the sulfur compounds from being released by hot synthesis gas.
F26B 3/06 - Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
B01J 19/02 - Apparatus characterised by being constructed of material selected for its chemically-resistant properties
C01B 3/48 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
JAPAN OIL GAS AND METALS NATIONAL CORPORATION (Japan)
INPEX CORPORATION (Japan)
JX NIPPON OIL & ENERGY CORPORATION (Japan)
JAPAN PETROLEUM EXPLORATION CO., LTD. (Japan)
COSMO OIL CO., LTD. (Japan)
NIPPON STEEL ENGINEERING CO., LTD. (Japan)
CHIYODA CORPORATION (Japan)
Inventor
Hodoshima, Shinya
Yagi, Fuyuki
Wakamatsu, Shuhei
Kawazuishi, Kenichi
Abstract
It is avoided that the sulfur compounds originating from the castable is mixed into produced synthesis gas, the mixed sulfur compounds are separated and collected with carbon dioxide, the collected carbon dioxide is recycled as raw material gas and then the sulfur compounds is directly supplied to the reformer to consequently degrade the reforming catalyst in the reformer by sulfur poisoning. The carbon dioxide separated and collected in the carbon dioxide removal step is introduced into the desulfurization apparatus of the desulfurization step or the sulfur compounds adsorption apparatus before being recycled to the reformer to remove the sulfur compounds.
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
C01B 3/48 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
79.
HYDROCARBON SYNTHESIS REACTION DEVICE, METHOD FOR STARTING UP SAME AND HYDROCARBON SYNTHESIS REACTION SYSTEM
This hydrocarbon synthesis reaction device comprises: a synthetic gas supply passage for supplying a synthetic gas compressed by a first compressor; a reaction vessel for containing a catalyst slurry; a gas-liquid separator for gas-liquid separating unreacted synthetic gas and hydrocarbon derived from the reaction vessel; a first recirculation passage for recirculating the unreacted synthetic gas after the gas-liquid separation compressed by a second compressor to the reaction vessel; and a second recirculation passage for recirculating the rest of the unreacted synthetic gas after the gas-liquid separation to a suction side of the first compressor at the time of start up operation when the introduction amount of the synthetic gas is gradually increased.
This catalyst for the Fischer-Tropsch synthesis reaction comprises: a carrier containing silica and 0.5-14% by mass of zirconium oxide with respect to the mass of the carrier; and 10-40% by mass of cobalt metal and cobalt oxides in terms of tricobalt tetraoxide with respect to the mass of the catalyst, the cobalt metal and cobalt oxides being supported by the carrier. The degree of reduction of the cobalt atoms is 75-93%, and the hydrogen gas adsorption amount per unit mass of the catalyst at 100°C is 0.40-1.0 ml/g.
This method for producing hydrocarbon comprises: a synthesis step for using a bubble column-type slurry bed reactor to synthesize hydrocarbon by a Fischer-Tropsch synthesis reaction, the reactor having a gas phase part at the top and holding a slurry including catalyst particles and liquid hydrocarbon; an extraction step for causing the slurry to flow through a filter disposed on the interior and/or exterior of the reactor to separate out the heavy liquid hydrocarbon, and extracting the heavy liquid hydrocarbon; a backwashing step for causing the liquid hydrocarbon to flow through the filter in a direction inverse to the direction of flow of the slurry and returning the catalyst particles to the reactor; and a cooling and gas-liquid separation step for cooling the hydrocarbon expelled from the gas phase part and separating out and collecting the condensed light liquid hydrocarbon. The liquid hydrocarbon made to flow in the backwashing step includes the light liquid hydrocarbon obtained in the cooling and gas-liquid separation step.
This temperature control system is provided with a lower heat removal part through the interior of which a liquid refrigerant passes and which is disposed on the bottom part of a reaction container for producing an exothermic reaction in the interior, and an upper heat removal part through the interior of which a liquid refrigerant passes and which is disposed above the lower heat removal part in the reaction container. The temperature control system controls the temperature within the reaction container by absorbing the reaction heat in the reaction container. A liquid refrigerant of which the temperature is adjusted by means of a first temperature adjusting unit is supplied to the lower heat removal part, and a liquid refrigerant of which the temperature is adjusted by means of a second temperature adjusting unit that is different from the first temperature adjusting unit is supplied to the upper heat removal part.
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
This regenerated hydrogenation refining catalyst is formed by regenerating a used hydrogenation refining catalyst which contains both a carrier containing an amorphous composite metal oxide having solid acidity, and at least one type of active metal selected from the noble metals of group 8 to group 10 of the periodic table and supported on the aforementioned carrier; relative to the total mass of the catalyst, this regenerated hydrogenation refining catalyst contains 0.05-1 mass% of a carbonaceous material in terms of carbon atoms.
C10G 45/10 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing platinum group metals or compounds thereof
84.
METHOD FOR STARTING UP BUBBLE-COLUMN-TYPE SLURRY-BED REACTOR, START-UP SOLVENT, AND METHOD FOR PRODUCING HYDROCARBON OIL
This method for starting up a bubble-column-type slurry-bed reactor is characterized in that, at the time of re-starting a bubble-column-type slurry-bed reactor for producing hydrocarbons by the Fischer-Tropsch synthesis reaction, a hydrotreated oil that has been produced in the bubble-column-type slurry-bed reactor and hydrotreated is supplied to the bubble-column-type slurry-bed reactor, the hydrotreated oil having a peroxide value of 1 ppm or less and containing 40% by mass or more of paraffin hydrocarbons with carbon numbers of 21 or greater.
This kerosene base material production method is characterized in obtaining, by removing paraffin of seven carbons or less from a first distillate with an initial boiling point of 95 - 140°C and an end point of 240 - 280°C that is obtained from a hydrogenated oil of a Fischer-Tropsch synthetic oil, a second distillate wherein the content of paraffin of seven carbons or less is 0.1 - 0.7 mass%.
The present invention prevents mixing in of metal components in an apparatus (reformer) for manufacturing synthetic gas used in a gas-to-liquid (GTL) synthetic gas manufacturing process. The present invention is a method for controlling mixing in of metal in an apparatus for manufacturing synthetic gas in a GTL process that includes a synthetic gas manufacturing process that manufactures synthetic gas by a reforming reaction for natural gas and gas that includes steam and/or carbon dioxide in the apparatus for manufacturing synthetic gas. The method for controlling mixing in of metal in the apparatus for manufacturing synthetic gas is characterized by the carbon dioxide gas in the synthetic gas manufactured by the synthetic gas manufacturing process being separated and recovered and, when the separated and recovered carbon dioxide gas is recycled into the starting material gas for the reforming reaction in the synthetic gas manufacturing process, the nickel concentration in the recycled carbon dioxide gas is 0.05 ppmv or less.
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
87.
METHOD FOR STOPPING OPERATION OF REACTION CONTAINER
This method for stopping the operation of a reaction container involves a stopping step in which the supply of synthesis gas containing carbon monoxide gas and hydrogen gas into a reaction container is stopped, a slurry discharging step in which a slurry is discharged from the reaction container, a steam supplying step in which steam having a temperature equal to or higher than the decomposition temperature of metal carbonyl is supplied into the reaction container and the gas in the reaction container is discharged, and a carbon monoxide gas detecting step in which the amount of carbon monoxide in the gas discharged from the reaction container is detected. In the steam supplying step, the supply of steam is stopped when the detected amount of carbon monoxide gas continuously drops and becomes equal to or less than a predetermined reference value.
This hydrogenation refining catalyst contains both a carrier containing an amorphous composite metal oxide having solid acidity, and at least one type of active metal selected from the noble metals of group 8 to group 10 of the periodic table and supported on the aforementioned carrier. This hydrogenation refining catalyst contains a carbonaceous material containing carbon atoms, and the amount of the carbonaceous material contained in the hydrogenation refining catalyst is 0.05-1 mass% in terms of carbon atoms.
C10G 45/62 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
89.
HYDROCRACKING CATALYST AND METHOD FOR PRODUCING A HYDROCARBON OIL
This hydrocracking catalyst contains both a carrier containing zeolite and an amorphous composite metal oxide having solid acidity, and at least one type of active metal selected from the noble metals of group 8 to group 10 of the periodic table supported on the aforementioned carrier. This hydrocracking catalyst contains a carbonaceous material containing carbon atoms, and the amount of the carbonaceous material contained in the hydrocracking catalyst is 0.05-1 mass% in terms of carbon atoms.
This regenerated hydrocracking catalyst is formed by regenerating a used hydrocracking catalyst which contains both a carrier containing zeolite and an amorphous composite metal oxide having solid acidity, and at least one type of active metal selected from the noble metals of group 8 to group 10 of the periodic table and supported on the aforementioned carrier; relative to the total mass of the catalyst, this regenerated hydrocracking catalyst contains 0.05-1 mass% of a carbonaceous material in terms of carbon atoms.
This method for producing a hydrocarbon oil uses a Fischer-Tropsch synthesis reaction device provided with a reactor having both a slurry containing catalyst particles and a gas phase portion positioned above said slurry, and obtains a hydrocarbon oil by means of Fischer-Tropsch synthesis reactions. Fischer-Tropsch synthesis reactions are performed after the slurry temperature is adjusted such that the difference T2-T1 is 5-30°C, wherein T1 is the average slurry temperature and T2 is the temperature of the liquid surface contacting the gas phase portion of the slurry.
This method for estimating the content of fine particles in a slurry is a method for estimating the content of fine particles having a particle diameter of a given value or less in a slurry that comprises hydrocarbons comprising wax and solid particles dispersed in the hydrocarbons. The method is characterized in that a correlation between the visible-light transmittances of dispersions obtained by dispersing solid particles having a particle diameter of the given value or less in the hydrocarbons comprising wax, the transmittances being measured at a temperature at which the hydrocarbons are liquid, and the contents of the solid particles having a particle diameter of the given value or less is determined, and the content of fine particles having a particle diameter of the given value or less in the slurry is estimated, on the basis of the correlation, from the visible-light transmittance of the supernatant of the slurry that was allowed to stand still at that temperature.
G01N 15/06 - Investigating concentration of particle suspensions
B01J 8/20 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
A method for producing a hydrogenation catalyst which comprises: a loading step wherein a carrier, which contains a carbonaceous substance containing a carbon atom in an amount of 0.5% by mass or less in terms of carbon atoms, is loaded with an active metal component that contains at least one active metal element selected from among group 6 metals, group 8 metals, group 9 metals and group 10 metals of the periodic table so as to obtain a catalyst precursor; and a firing step wherein the catalyst precursor obtained in the loading step is fired so as to obtain a hydrogenation catalyst.
In the present invention, when an FT off-gas is used as fuel for a tubular reformer in a GTL process, blockage of a heating burner tip by deposition of a heavy hydrocarbon contained in FT off-gas is prevented. The heavy hydrocarbon contained in FT off-gas is removed by being put into contact with absorber oil, introduced into a distillation column, and aerated with a coolant or an absorbent, and the FT off-gas from which the heavy hydrocarbon has been removed is used as fuel for the tubular reformer. With this configuration, prolonged stable operation of the tubular reformer becomes possible and effective use of the FT off-gas as a fuel can be ensured.
This manufacturing device for hydrocarbons is provided with a gas-liquid separation device that cools hydrocarbons in gaseous form extracted from the gaseous phase section of a Fischer-Tropsch synthesis reaction vessel, causes some of the hydrocarbons to liquefy, and separates gas and liquid. Between a line downstream from a final-stage gas-liquid separation unit of the gas-liquid separation device and an upstream line upstream from the final-stage gas-liquid separation unit of the gas-liquid separation device, a light liquid hydrocarbon supply line that supplies light hydrocarbons is provided. This downstream line is a downstream light liquid hydrocarbon line through which flow light hydrocarbons with a cloud point lower than the outlet temperature of a cooling vessel in the final-stage gas-liquid separation unit.
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.
This method for producing a hydrocarbon oil obtains a hydrocarbon oil containing a hydrocarbon having a boiling point of no greater than 360°C by means of continuously supplying and hydrocracking a wax that is to be processed. The method is characterized by alternatingly providing: a period for hydrocracking the wax to be processed with the condition that the cracking rate defined by the belowmentioned formula (1) is X1 (%), satisfying the belowmentioned formula (2); and a period for hydrocracking with the condition that the cracking rate is X2 (%), satisfying the belowmentioned formula (3). Cracking rate (%) = [(amount of hydrocarbon having boiling point exceeding 360°C contained in 1g of wax to be processed) - (amount of hydrocarbon having boiling point exceeding 360°C contained in 1g of hydrocracking product)]×100/(amount of hydrocarbon having boiling point exceeding 360°C contained in 1g of wax to be processed) …(1); 30 ≤ X1 ≤ 90 …(2); and 0.1 ≤ X2/X1 ≤ 0.9 …(3).
This temperature control system recovers reaction heat generated internally by a heat generating reaction in a reactor and controls the temperature in the reactor. The temperature control system is provided with a refrigerant drum that accommodates a liquid refrigerant in a state of gas-liquid equilibrium, a heat removal part disposed in the reactor with the liquid refrigerant supplied by the refrigerant drum flowing therein, a temperature measurement part that measures the temperature in the reactor, and a pressure control part that controls the pressure in the refrigerant drum. The pressure control part controls the temperature of the liquid refrigerant in the refrigerant drum by controlling the pressure in the refrigerant drum on the basis of the deviation of the actual temperature in the reactor measured by the temperature measurement part and a temperature setting value for the inside of the reactor.
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
99.
CATALYST FOR FISCHER-TROPSCH SYNTHESIS, AND PRODUCTION METHOD THEREFOR, AS WELL AS HYDROCARBON PRODUCTION METHOD USING FISCHER-TROPSCH SYNTHESIS CATALYST
The FT synthesis catalyst is characterized: in comprising, in manganese carbonate, 10-25 mass% of silica calculated as oxide and based on the total mass of the catalyst, 6 mass% or less of organic binder based on the total mass of the catalyst, and 0.5-5 mass% of ruthenium calculated as metal and based on the total mass of the catalyst; and in the surface area being 100-210 m2/g and the pore volume being 0.1-0.6 mL/g.
B01J 31/32 - Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups of manganese, technetium or rhenium
The catalyst recovery system is provided with: a concentrated slurry-generating unit that concentrates slurry that is extracted from the main reactor and continuously generates concentrated slurry; a first discharging unit that discharges the concentrated slurry from the concentrated slurry-generating unit; a solidified slurry-generating unit that cools the concentrated slurry discharged from the concentrated slurry-generating unit and solidifies the liquid medium in the concentrated slurry to generate a solidified slurry; and a recovery mechanism that recovers the solidified slurry from the solidified slurry-generating unit.
