31results about "Hydrocarbon by polyarylsubstituted aliphatic compound split-off" patented technology

A catalyst and process is disclosed to selectively upgrade a paraffinic feedstock to obtain an isoparaffin-rich product for blending into gasoline. The catalyst comprises a support of a sulfated oxide or hydroxide of a Group IVB (IUPAC 4) metal, a first component comprising at least one Group III A (IUPAC 13) component, and at least one platinum-group metal component which is preferably platinum.

A catalyst and process is disclosed to selectively upgrade a paraffinic feedstock to obtain an isoparaffin-rich product for blending into gasoline. The catalyst comprises a support of a tungstated oxide or hydroxide of a Group IVB (IUPAC 4) metal, a first component of at least one lanthanide element, yttrium or mixtures thereof, which is preferably ytterbium or holmium, and at least one platinum-group metal component which is preferably platinum.

Hydrocarbon or oxygenate conversion process in which a feedstock is contacted with a non zeolitic molecular sieve which has been treated to remove most, if not all, of the halogen contained in the catalyst. The halogen may be removed by one of several methods. One method includes heating the catalyst in a low moisture environment, followed by contacting the heated catalyst with air and / or steam. Another method includes steam-treating the catalyst at a temperature from 400° C. to 1000° C. The hydrocarbon or oxygenate conversion processes include the conversion of oxygenates to olefins, the conversion of oxygenates and ammonia to alkylamines, the conversion of oxygenates and aromatic compounds to alkylated aromatic compounds, cracking and dewaxing.

A catalyst, and a process for using the catalyst, that effectively converts and transalkylates indane and C10 and heavier polycyclic aromatics into C8 aromatics is herein disclosed. The catalyst comprises a solid-acid support such as mordenite plus a metal component such as rhenium. The catalyst provides excellent conversion of such heavy aromatic species as naphthalene, which is also observed by a decrease in the ending-boiling-point of a hydrocarbon stream passed over the catalyst. The same catalyst is also effective for transalkylation of lighter aromatics, thus yielding a valuable xylenes product stream out of the process.

A process for the combined production of para-xylene and benzene comprises:separating a first feed, by adsorption in a simulated moving bed SMB, to produce an extract E rich in para-xylene and at least one raffinate R which is depleted in para-xylene;converting a secondary feed of toluene by selective disproportionation to produce benzene and xylenes;a) at the start of the cycle, producing a supplemental quantity of para-xylene in a crystallization unit supplied with the xylenes from the disproportionation;b) at the end of the cycle, when the adsorbant has aged:dividing the distilled extract E into a first fraction Ea and a complementary second fraction Eb;replacing the feed to the initial crystallization by the stream Ea;and recycling the xylenes from the disproportionation to the SMB.The invention enables para-xylene and benzene production to be maintained despite ageing of the SMB absorbent.

A method of producing monocyclic aromatic hydrocarbons includes bringing a feedstock oil having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower, into contact with a catalyst for monocyclic aromatic hydrocarbon production containing a crystalline aluminosilicate, in which a content ratio of monocyclic naphthenobenzenes in the feedstock oil is adjusted to 10 mass % to 90 mass %, by mixing a hydrocarbon oil A having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower with a hydrocarbon oil B containing more monocyclic naphthenobenzenes than the hydrocarbon oil A.

A process for the selective ring opening of ring-containing hydrocarbons in a feed stream having at least 10% ring-containing hydrocarbons includes contacting the feed stream with a ring opening catalyst containing a metal or a mixture of metals active for the selective ring opening of the ring-containing hydrocarbons on a support material, wherein the support material is a non-crystalline, porous inorganic oxide or mixture of inorganic oxides having at least 97 volume percent interconnected mesopores based on micropores and mesopores, and wherein the ring-containing hydrocarbons have at least one C6 ring and at least one substituent selected from the group consisting of fused 5- or 6-membered rings, alkyl, cycloalkyl and aryl groups.

The catalyst for producing monocyclic aromatic hydrocarbons is for producing monocyclic aromatic hydrocarbons having 6 to 8 carbon number from oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower. The catalyst includes crystalline aluminosilicate, phosphorus, and a binder, and the amount of phosphorus is 0.1 to 10 mass % based on the total mass of the catalyst.

A pyrolysis tube for use with a material deposition system includes a plurality of channels. The channels may be defined by internal elements of the pyrolysis tube, or by internal elements that form an insert for a conventionally configured pyrolysis tube. One or more of the channels may extend straight through the pyrolysis tube, providing a direct line of sight through the pyrolysis tube. Material deposition systems that include such an insert or pyrolysis tube are also disclosed, as are methods for efficiently pyrolyzing precursor materials at temperatures that are reduced relative to conventional pyrolysis temperatures and / or at rates that are increased relative to conventional pyrolysis rates.

The invention relates to a method for preparing a loaded solid super acidic catalyst directly by a microwave method, and belongs to a method for preparing a super acidic catalyst. The method comprises the following steps of: (1) mixing and stirring NaHCO3 and a carbon nano tube in a weight ratio of 1:500 fully, and roasting in a microwave reactor to obtain a Na-loaded catalyst carrier; (2) heating the Na-loaded catalyst carrier by microwave radiation, adding a mixed solution of antimony pentachloride (SbCl5) and trimethylsilyl trifluoromethanesulfonate (F3CSO3Si(CH3)3) dropwise, stirring and immersing to obtain a suspension mixed solution; (3) filtering the suspension mixed solution to obtain a solid precursor and a mixed solution; (4) putting the solid precursor into the microwave reactor, heating by the microwave radiation, and roasting to obtain a solid super acidic catalyst prototype; and (5) performing operation for 1 to 5 times by taking the solid super acidic catalyst prototype as a raw material according to the steps (2), (3) and (4) to obtain the solid-loaded super acidic catalyst. The method has the advantages that: the loaded solid super acidic catalyst prepared by the microwave method is high in catalytic hydrocracking activity and selectivity.

A method of producing monocyclic aromatic hydrocarbons includes bringing a light feedstock oil having a 10 vol % distillation temperature of 140° C. to 205° C. and a 90 vol % distillation temperature of 300° C. or lower, which has been prepared from a feedstock oil having a 10 vol % distillation temperature of 140° C. or higher and a 90 vol % distillation temperature of 380° C. or lower, into contact with a catalyst for monocyclic aromatic hydrocarbon production containing a crystalline aluminosilicate, in which a content ratio of monocyclic naphthenobenzenes in the light feedstock oil is adjusted by distillation of the feedstock oil such that the content ratio of monocyclic naphthenobenzenes in the light feedstock oil is higher than a content ratio of monocyclic naphthenobenzenes in the feedstock oil.

According to one or more embodiments presently disclosed, a method of catalytically converting polystyrene may include contacting polystyrene with a catalyst to form a product comprising ethylbenzene. The catalyst may include oxidized iron, oxidized cobalt, and oxidized copper. The catalyst may further include a mesoporous support material with pores having an average pore diameter of from 2 nm to 50 nm.

The invention discloses a method for reducing unit consumption of a cumene in epoxypropane production process using a cumene co-oxidation method. In a process for producing epoxypropane by a cumene co-oxidation method, heavy components such as diisopropylbenzene and the like are byproduced when cumene is prepared by hydrogenolysis of dimethyl benzyl alcohol. According to the invention, a heavy component is converted into cumene through two steps of thermal cracking and catalytic hydrogenation to be recycled, so that the economical efficiency and competitiveness of a process for producing epoxypropane through a cumene co-oxidation method are remarkably improved.

A process for recovering cumene, characterized by subjecting 2,3-dimethyl-2,3-diphenylbutane produced in a process in which cumene is used, to hydrogenolysis in the presence of a catalyst thereby to convert it into cumene, and recovering the cumene.

The catalyst for producing monocyclic aromatic hydrocarbons is for producing monocyclic aromatic hydrocarbons having 6 to 8 carbon number from oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower. The catalyst contains crystalline aluminosilicate and a rare earth element, in which the amount of the rare earth element expressed in terms of the element is 0.1 to 10 mass % based on the crystalline aluminosilicate. In the production method of monocyclic aromatic hydrocarbons, oil feed stock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower is brought into contact with the catalyst for producing monocyclic aromatic hydrocarbons.

A catalyst for producing monocyclic aromatic hydrocarbons, used for producing monocyclic aromatic hydrocarbons of 6 to 8 carbon number from a feedstock oil having a 10 volume % distillation temperature of at least 140° C. and an end point temperature of not more than 400° C., wherein the catalyst contains a crystalline aluminosilicate, gallium and / or zinc, and phosphorus, the molar ratio between silicon and aluminum (Si / Al ratio) in the crystalline aluminosilicate is not more than 100, the molar ratio between the phosphorus supported on the crystalline aluminosilicate and the aluminum of the crystalline aluminosilicate (P / Al ratio) is not less than 0.01 and not more than 1.0, and the amount of gallium and / or zinc is not more than 1.2% by mass based on the mass of the crystalline aluminosilicate.

The invention provides a system for recovering effective components in styrene byproduct tar. The system for recovering the effective components in the styrene byproduct tar comprises a rectifying tower, a tower top condenser, a recovery tank and a tower kettle pump; the tower top condenser is communicated with the top of the rectifying tower through a conveying pipe; the recovery tank is communicated with the output end of the tower top condenser through a connecting pipe, and one side of the recovery tank is communicated with the input end of a recovery pump through a conveying pipe; the input end of the tower kettle pump is communicated with the bottom end of the rectifying tower through a connecting pipe. The system for recovering the effective components in styrene byproduct tar has amethod for preparing monomer styrene through catalytic cracking of tar negative pressure rectification coupled tower kettle circulating tar. 90% or more of effective components (styrene and polystyrene) in the styrene by-product tar can be separated, and the material loss of the styrene component in the by-product can be reduced.

A method for producing a norbornene derivative wherein,in the presence of palladium and at least one selected from phosphorus compounds represented by the following General Formulae (1) and (2):[in Formula (1), R1, R2, R3 and R4 each independently represent a hydrogen atom or the like, and R5 and R6 each independently represent a branched chain saturated hydrocarbon group having 3 to 10 carbon atoms or the like], and[in Formula (2), R7 represents a branched chain saturated hydrocarbon group having 3 to 10 carbon atoms],a norbornadiene derivative represented by the following General Formula (3):[in Formula (3), R8, R9, R10, R11 and R12 each independently represent a hydrogen atom or the like, l represents an integer of 0 or 1, m represents an integer of 0 or 1, and n represents an integer of 0 or 1], and a bromine compound represented by the following General Formula (4):[Chemical Formula 4]Br—Z—R13  (4)[in Formula (4), Z represents a phenylene group or the like, and R13 represents a hydrogen atom or the like] are reacted with each other, to thereby obtain a norbornene derivative represented by the following General Formula (5):[in Formula (5), R14, R15, R16, R17 and R18 each independently represent a hydrogen atom or the like, Z represents a phenylene group or the like, R19 represents a hydrogen atom or the like, l represents an integer of 0 or 1, m represents an integer of 0 or 1, and n represents an integer of 0 or 1], the norbornene derivative having a configuration of a substituent represented by Z in General Formula (5) that is an exo configuration.

In the production method of monocyclic aromatic hydrocarbons, oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower is brought into contact with a catalyst for producing monocyclic aromatic hydrocarbons that includes a mixture containing a first catalyst which contains crystalline aluminosilicate containing gallium and / or zinc and phosphorus and a second catalyst which contains crystalline aluminosilicate containing phosphorus.

A catalyst for producing monocyclic aromatic hydrocarbons of 6 to 8 carbon number from a feedstock oil having a 10 volume % distillation temperature of at least 140° C. and an end point temperature of not more than 400° C., or a feedstock oil having a 10 volume % distillation temperature of at least 140° C. and a 90 volume % distillation temperature of not more than 360° C., wherein the catalyst contains a crystalline aluminosilicate, gallium and / or zinc, and phosphorus, and the amount of phosphorus supported on the crystalline aluminosilicate is within a range from 0.1 to 1.9% by mass based on the mass of the crystalline aluminosilicate; and a method for producing monocyclic aromatic hydrocarbons, the method involving bringing a feedstock oil having a 10 volume % distillation temperature of at least 140° C. and an end point temperature of not more than 400° C., or a feedstock oil having a 10 volume % distillation temperature of at least 140° C. and a 90 volume % distillation temperature of not more than 360° C., into contact with the above-mentioned catalyst for producing monocyclic aromatic hydrocarbons.

A pyrolysis tube for use with a material deposition system includes a plurality of channels. The channels may be defined by internal elements of the pyrolysis tube, or by internal elements that form an insert for a conventionally configured pyrolysis tube. One or more of the channels may extend straight through the pyrolysis tube, providing a direct line of sight through the pyrolysis tube. Material deposition systems that include such an insert or pyrolysis tube are also disclosed, as are methods for efficiently pyrolyzing precursor materials at temperatures that are reduced relative to conventional pyrolysis temperatures and / or at rates that are increased relative to conventional pyrolysis rates.

The present invention relates to a method for decomposing phenolic by-products and, more specifically, provides a method for decomposing phenolic by-products, the method comprising the steps: supplying a phenolic by-product stream to a decomposing device to thermally decompose the stream (S10); recovering active ingredients from an upper discharge stream of the decomposing device and discharging high-boiling point materials from a lower discharge stream (S20); supplying a portion of the lower discharge stream of the decomposing device through a reboiler to the decomposing device, and discharging the remainder of the stream (S30); and supplying a side discharge stream of the decomposing device to the reboiler (S40).