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.

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 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.

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.

Disclosed herein is a process and catalyst for producing an ethylbenzene feed from a polyethylbenzene feed, comprising the step of contacting a benzene feed with a polyethylbenzene feed under at least partial liquid phase conditions in the presence of a zeolite beta catalyst having a phosphorus content in the range of 0.01 wt. % to 0.5 wt. % of said catalyst, to provide a product which comprises ethylbenzene.

The catalyst for producing aromatic hydrocarbon is for producing monocyclic aromatic hydrocarbon 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 and contains crystalline aluminosilicate and phosphorus. A molar ratio (P / Al ratio) between phosphorus contained in the crystalline aluminosilicate and aluminum of the crystalline aluminosilicate is from 0.1 to 1.0. The production method of monocyclic aromatic hydrocarbon is a method of bringing oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower into contact with the catalyst for producing monocyclic aromatic hydrocarbon.

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.

An aromatics / naphthalene rich stream obtained by processing heavy gas oil derived from tar sands and cycle oils derived from cracking heavy gas oil may optionally be blended and subjected to a hydrogenation process and a ring opening reaction typically in the presence of a zeolite, alumina, or silica alumina based catalyst which may contain noble metals and or copper or molybdenum to produce paraffinic feedstocks for further chemical processing.

The invention discloses a method for reducing the unit consumption of cumene in the process of producing propylene oxide by a cumene co-oxidation method. In the process of producing propylene oxide by co-oxidation of cumene, heavy components such as cumene are produced by hydrogenolysis of dimethylbenzyl alcohol to prepare cumene. The invention converts the heavy component into cumene for recycling and reuse through two steps of thermal cracking and catalytic hydrogenation, and significantly improves the economy and competitiveness of the cumene co-oxidation method for producing propylene oxide.

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 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 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.

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 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).