5632 results about "Xylene" patented technology

This invention is a chemical oil refining method of generating low carbon alkene and arene. Material oil, regenerated catalytic cracking catalyst and vapor are contact to each other in cracking device. On condition of 500~7000C, pressure 0.15~0.4MPa, weight ratio of catalytic cracking catalyst and material oil is 5~50, weight ratio of vapor and material oil is 0.05~0.6, catalyst and reaction oil gas are separated, the catalyst go back to reaction device after regenerated, then the low carbon alkene and arene are got after separating the reaction oil gas. Propylene, ethane and other low carbon alkene is got from heavy feed stock at maximum limit, yield of propylene exceed 30%, and toluene, xylene and other arene are generated at the same time.

The invention discloses a catalytic conversion method for preparing ethylene, propylene and aromatic hydrocarbon. Hydrocarbon raw material with different cracking performances is contacted with a catalytic cracking catalyst, and cracking reaction is carried out in a fluidized bed reactor under the conditions that the temperature is 550 DEG C to 800 DEG C, the weight hourly space velocity is 0.1-800h<-1>, the reaction pressure is 0.10MPa to 1.0MPa, the weight ratio of the catalytic cracking catalyst and the raw material is 10-150, and the weight ratio of steam and the raw material is 0.15-1.0.Then a spent catalyst and reaction oil gas are separated, the spent catalyst returns to the reactor after regeneration, and the target products comprising low carbon olefin and the aromatic hydrocarbon are obtained by separating the reaction oil gas, wherein, fraction with the temperature to be 160 DEG C to 260 DEG C returns for catalytic cracking as circulating material, and the ethylene and the propylene are further obtained by cracking of ethane, propane, butane, and the steam entered. Low carbon olefin such as ethylene, propylene, and the like, is produced from heavy feedstock to the utmost extent in the method, and the yield of the ethylene and the propylene is over 20% by weight, in addition, the aromatic hydrocarbon such as toluene, xylene, and the like, are produced in an integrated way.

The present invention is directed to a method for preparing renewable and relatively high purity p-xylene from biomass. For example, biomass treated to provide a fermentation feedstock is fermented with a microorganism capable of producing a C₄ alcohol such as isobutanol, then sequentially dehydrating the isobutanol in the presence of a dehydration catalyst to provide a C₄ alkene such as isobutylene, dimerizing the C₄ alkene to a form one or more C₈ alkenes such as 2,4,4-trimethylpentenes or 2,5-dimethylhexene, then dehydrocyclizing the C₈ alkenes in the presence of a dehydrocyclization catalyst to selectively form renewable p-xylene in high overall yield. The p-xylene can then be oxidized to form terephthalic acid or terephthalate esters.

Disclosed is an optimized process and apparatus for more efficiently and economically carrying out the liquid-phase oxidation of an oxidizable compound. Such liquid-phase oxidation is carried out in a bubble column reactor that provides for a highly efficient reaction at relatively low temperatures. When the oxidized compound is para-xylene and the product from the oxidation reaction is crude terephthalic acid (CTA), such CTA product can be purified and separated by more economical techniques than could be employed if the CTA were formed by a conventional high-temperature oxidation process.

A liquid or partially liquid phase process for isomerizing a non-equilibrium mixture of xylenes and ethylbenzene uses a zeolitic catalyst system preferably based on zeolite beta and on pentasil-type zeolite. The invention obtains an improved yield of para-xylene from the mixture relative to prior art processes in a more economical manner. A preferred beta zeolite is a surface-modified zeolite beta resulting from acid washing of a templated native zeolite at conditions insufficient to effect bulk dealumination. A preferred pentasil zeolite is a MTW-type with a silica-to-alumnina ratio between 20 and 45.

Disclosed is an optimized process and apparatus for more efficiently and economically carrying out the liquid-phase oxidation of an oxidizable compound. Such liquid-phase oxidation is carried out in a bubble column reactor that provides for a highly efficient reaction at relatively low temperatures. When the oxidized compound is para-xylene and the product from the oxidation reaction is crude terephthalic acid (CTA), such CTA product can be purified and separated by more economical techniques than could be employed if the CTA were formed by a conventional high-temperature oxidation process.

A fuel additive for middle distillate fuels is a mixture of at least one methyl, ethyl, propyl or butyl ester of a vegetable oil or a C₁₆-C₁₈ fatty acid, at least one alkyl ether of propylene glycol, a surfactant, and an antioxidant. A fuel additive for gasoline is a mixture of ligroin or toluene/xylene, at least one alkyl ether of propylene glycol, a surfactant, and tertiary amyl methyl ether.

This invention is drawn to a process for isomerizing a non-equilibrium mixture of xylenes and ethylbenzene using an oil-dropped catalyst comprising a zeolite, a platinum-group metal and an aluminophosphate binder, resulting in a greater yield of para-xylene at favorable conditions compared to processes of the known art.

Aromatization of alkanes having one to four carbon atoms per molecule to aromatics, such as benzene, toluene and xylenes (BTX), uses a catalyst of a crystalline zeolite on which platinum has been deposited, specifically a platinum-containing ZSM-5. A byproduct of the process is a light gas fraction of methane and ethane. The use of a platinum-containing ZSM-5 catalyst in an alkane aromatization process, such as the Cyclar process, suppresses the formation of methane and increases selectivity to BTX. The high content of ethane relative to methane in the light gas fraction allows this process effluent to be a feedstream for a cracker.

A method and apparatus for preparing purified terephthalic acid and, optionally, isophthalic acid from mixed xylenes. The method of the present invention purifies the oxidation reactor effluent containing a mixture of terephthalic acid and isophthalic acid as well as minor amounts of 4-carboxybenzaldehyde (4-CBA), 3-carboxybenzaldehyde (3-CBA), and toluic acid isomers, to produce purified terephthalic acid and, optionally, purified isophthalic acid in an integrated process.

The present invention relates to agglomerated zeolite adsorbents based on faujasite with an Si/Al ratio such that 1<=Si/Al<=1.15, at least 70% exchanged with barium and optionally with potassium, and on a binder, preferably a zeolitizable binder.They are obtained by agglomerating zeolite powder with a binder, followed by exchange of the zeolite ions for barium ions and activation of the adsorbents thus exchanged.These adsorbents are particularly suitable for the adsorption of the para-xylene contained in aromatic C8 hydrocarbon fractions in the liquid phase, in processes of simulated fluid-bed type.

A coating composition used for coating of a steel material and/or aluminum material comprises a corrosion inhibitor, a base resin and a curing agent. The corrosion inhibitor may be selected from cerium compounds, lanthanum compounds, molybdate salt compounds, gluconic acid derivative salts, porous base materials, triazole compounds, thiazole compounds, tetracyclines, and metal phosphate salt compounds of ascorbic acid. The base resin may include a xylene-formaldehyde-resin-modified amino-containing epoxy resins obtained by reacting an epoxy resin having an epoxy equivalent of from 180 to 2500 with a xylene formaldehyde resin and an amino-containing compound. The curing agent may be a blocked polyisocyanate compound obtained by blocking an isocyanate group of a polyisocyanate compound with a blocking agent.

A thermocured, heat conductive and heat radiating paint for an LED lamp is prepared by the following raw materials by weight: 40-45 parts of polyacrylic resin, 5-8 parts of polyurethane resin, 4-6 parts of polyacrylamide, 6-8 parts of isophorone diamine IPDA, 20-24 parts of xylene, 2-3 parts of silane coupling agent KH550, 1-2 parts of aluminium powder, 8-12 parts of ethyl acetate, 2-4 parts of benzyltrimethylammonium tribromide, 10-12 parts of aluminium nitride, 2-3 parts of beryllia, and 4-5 parts of film forming auxiliary agent. Aluminium nitride powder, the beryllia and the aluminium powder are added, so as that the paint has high heat conduction rate and good heat radiation effect, and can be long-term used under 200 DEG C without change of mechanical property; polyacrylic resin is used, so as that the paint has advantages of excellent fullness, glossiness, hardness, solvent resistance and weatherability, without color change and brightness reversion when high temperature baked; and the paint has advantages of large adhesion stress, not-easy shedding, aging resistance and long usage life.

The invention provides a catalytic conversion method for producing gasoline containing rich aromatic hydrocarbon. The catalytic conversion method comprises the following steps: cutting catalytic cracking light cycle oil to obtain a light fraction and a heavy fraction, performing hydrogenation treatment on the heavy fraction to obtain a hydrogenated heavy fraction, singly and respectively conveying the light fraction and the heavy fraction into different riser reactors of catalytic cracking devices, performing a cracking reaction in the presence of a catalytic cracking catalyst, and separating reaction products to obtain a product containing the gasoline which contains rich aromatic hydrocarbon and the light cycle oil. According to the method, single catalytic cracking devices are used for processing the light fraction and the hydrogenated heavy fraction of the light cycle oil to satisfy harsh conditions necessary for the catalytic cracking reaction of different fractions of the light cycle oil to the maximum, so as to produce catalytic gasoline containing rich benzene, toluene and xylene to the maximum.

The invention relates to a catalytic conversion method for preparing lower olefins and aromatics. Raw oil with different cracking performances enters different reaction zones of a first riser reactor to contact with a catalytic cracking catalyst for cracking reaction to separate a spent catalyst from reaction oil gas, wherein the reaction oil gas is separated to obtain a product containing lower olefins, gasoline, distillates with distillation range of 180-250 DEG C and catalytic wax oil, wherein the gasoline is extracted by light aromatics to obtain light aromatics and gasoline raffinate; the raw materials are cracked to be sent into a second riser reactor to contract with a hot regenerated catalyst for catalytic conversion; and the spent catalysts of the two riser reactors are burned and regenerated in the same one regenerator and then returns to the two riser reactors. The method uses heavy raw materials to furthest produce the lower olefins, such as propylene, ethylene, and the like, particularly the propylene, the production rate can exceed 40 wt%, and at the same time the method can coproduce the aromatics, such as toluene, xylene, and the like.

The invention relates to a method for preparing aromatic hydrocarbon and cyclopentenone from biomass derivative gamma-valerolactone by catalytic conversion, which comprises the following steps: (1) using biomass derivative gamma-valerolactone as a raw material, which is prepared by carrying out hydrogenation reaction on levulinic acid; (2) introducing one or more transition metals into a zeolite molecular sieve, and preparing a reaction catalyst at the reaction temperature of 350-550 DEG C by using a fixed bed or fluid bed as a reactor; (3) in an inert or reducing atmosphere, carrying out contact reaction on the raw material gamma-valerolactone and catalyst under the reaction pressure of 0-10 MPa; and (4) after the pyrolysis gas is condensed, collecting the liquid product in the condensation receiver, thereby obtaining the aromatic hydrocarbon product (of benzene, toluene and xylene) and the cyclopentenone product. By using the renewable biomass derivative gamma-valerolactone as the raw material, the method has the advantage of milder reaction conditions, and the catalyst is simple to prepare and easy to recover and reuse.

This invention relates to a process for the aromatization of C₆ to C₁₂ alkanes, such as hexane, heptane and octane, to aromatics, such as benzene, ethyl benzene, toluene and xylenes, with a germanium-containing zeolite catalyst. The catalyst is a non-acidic aluminum-silicon-germanium zeolite on which a noble metal, such as platinum, has been deposited. The zeolite structure may be of MFI, BEA, MOR, LTL or MTT. The zeolite is made non-acidic by being base-exchanged with an alkali metal or alkaline earth metal, such as cesium, potassium, sodium, rubidium, barium, calcium, magnesium and mixtures thereof, to reduce acidity. The catalyst is sulfur tolerant and may be pretreated with a sulfur compound, i.e., sulfided. The hydrocarbon feed may contain sulfur up to 1000 ppm. The present invention could be applicable to a feedstream which is predominantly paraffinic and/or low in naphthenes. Lowering the hydrogen to hydrocarbon ratio increases conversion and aromatics selectivity.

The air lift externally circulation bubble tower oxidation apparatus includes cylinder bubble tower with top expanded section, outer circulating pipe, gas distributor, reflux liquid distributor and condensator. The outer circulating pipe has its upper end and lower end communicated with the upper part and the lower part of the bubble tower reaction section separately and is used to lead slurry from the upper part of the tower to the lower part via air lift effect so as to form the fluid circulation in the whole tower and complete the liquid phase catalytic oxidation of xylene. The bubble tower has relatively high height/diameter ratio and thus reinforced gas-liquid mass transfer and the air lift outer circulation pipe improves the temperature distribution and concentraion distribution inside the tower. The tower has no moving part, simple structure and low cost and is suitable for oxidizing xylene to prepare terephthalic acid via different technological processes.

An agglomerated zeolite adsorbent which comprises 95-99.5 mass % of X zeolite and 0.5-5.0 mass % of binder, wherein the exchangeable cationic sites of said X zeolite are occupied by Group IIA metal and/or K, the total pore volume of said adsorbent is no less than 0.26 mL/g as measured by mercury porosimetry, the volume of pores with pore diameters from 100 to 500 nm is at least 60% based on the total pore volume. During shaping, a pore-forming agent is added to this adsorbent, and then the adsorbent is alkali treated for in-situ crystallization, followed by ion exchange. Said adsorbent has high adsorption capacity, fast mass transfer rate and good mechanical strength. Said adsorbent is suitable for liquid phase adsorptive separation of para-xylene from C₈ aromatic hydrocarbons and is also suitable for adsorptive separation of other alkyl aromatic hydrocarbons isomers.