2106 results about "Ethylbenzene" patented technology

An organic electroluminescence device includes: a cathode; an anode; and a single-layered or multilayered organic thin-film layer provided between the cathode and the anode. The organic thin-film layer includes at least one emitting layer. The at least one emitting layer contains at least one phosphorescent material and a host material represented by the following formula (1).In the formula, Ar1, Ar2, Ar3, B1, B2, B3 and B4 each represent a substituted or unsubstituted benzene ring or a substituted or unsubstituted condensed aromatic hydrocarbon ring selected from a naphthalene ring, a chrysene ring, a fluoranthene ring, a phenanthrene ring, a benzophenanthrene ring, a dibenzophenanthrene ring, a triphenylene ring, a benzo[a]triphenylene ring, a benzochrysene ring, a benzo[b]fluoranthene ring and a picene ring. p is 0 or 1.

The present invention provides a process for producing a monoalkylated aromatic compound, particularly ethylbenzene or cumene, in which a polyalkylated aromatic compound is contacted with an alkylatable aromatic compound in the liquid phase and in the presence of a transalkylation catalyst comprising TEA-mordenite having an average crystal size of less than 0.5 micron.

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.

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.

Apparatus and process are disclosed for the distillation separation of styrene monomer from ethylbenzene utilizing a split feed to two distillation columns in conjunction with cascade reboiling utilizing thermal energy from the overhead of one column to supply heat to the second.

An ethylbenzene production system comprises a reactor vessel, a vapor phase ethylene feed stream, a benzene feed stream entering the reactor vessel, and a product stream containing ethylbenzene exiting the reactor vessel. The reactor vessel has an ethylation section and a benzene stripping section, whereby fluid communication via integrated vapor and liquid traffic is maintained between the ethylation section and stripping section. The vapor phase ethylene feed stream contains 3 to 50 mol % ethylene and at least 20 mol % methane entering the reactor vessel.

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.

A process for making ethylbenzene and / or styrene by reacting toluene with methane in one or more microreactors is disclosed. In one embodiment a method of revamping an existing styrene production facility by adding one or more microreactors capable of reacting toluene with methane to produce a product stream comprising ethylbenzene and / or styrene is disclosed.

Catalysts for converting polyalkylaiomatics to monoalkylaromatics, particularly cumene and ethyl benzene are disclosed which comprise modified Y-85 or LZ-210 zeolites. For cumene and ethylbenzene production, a disclosed catalyst, made of 80 wt % zeolite and 20 wt % alumina binder on a volatile-flee basis, has one or more of the following physical characteristics: (1) an absolute intensity of the modified Y zeolite as measured by X-ray diffraction (XRD) of preferably at least 50 and (2) a framework aluminum of the modified Y zeolite of preferably at least 50% of the aluminum of the modified Y zeolite.

Ethylbenzene is produced by alkylation over monoclinic silicalite catalysts having a weak acid site concentration of less than 50 micromoles per gram. A feedstock containing benzene and ethylene is applied to an alkylation reaction zone having at least one catalyst bed containing a monoclinic silicalite catalyst having a weak acid site concentration of less than 50 micromoles per gram. The alkylation reaction zone is operated at temperature and pressure conditions in which the benzene is in a gaseous phase to cause gas-phase alkylation of the aromatic substrate in the presence of the silicalite catalysts to produce an alkylation product. The alkylation product is then withdrawn from the reaction zone for separation and recovery.

A titanium-containing silicon oxide catalyst satisfying all of the following conditions (1) to (4):(1): an average pore size of 10 Å or more,(2): a pore size of 90% or more of the total pore volume of 5 to 200 Å,(3): a specific pore volume of 0.2 cm3 / g or more, and(4): a quarternary ammonium ion represented by the following general formula (I) is used as a template and then said template is removed by solvent extraction operation;wherein, R1 represents a linear or branched hydrocarbon chain having 2 to 36 carbon atoms, and R2 to R4 represent an alkyl group having 1 to 6 carbon atoms, a method for producing said catalyst, and a method for producing propylene oxide by reacting propylene with a hydroperoxide, except for ethylbenzene hydroperoxide, in the presence of said catalyst.

The invention is for a process for producing propylene and hexene (along with ethylene, pentenes, product butenes, heptenes and octenes) by metathesis from butenes (iso-, 1- and cis and trans 2-) and pentenes and then aromatizing the hexenes (along with higher olefins, such as heptenes and octenes) to benzene (along with toluene, xylenes, ethylbenzene and styrene). Since the desired products of the metathesis reaction are propylene and hexene, the feed to the metathesis reaction has a molar ratio for 1-butene:2-butene which favors production of propylene and 3-hexene with the concentration of hexenes and higher olefins in the metathesis product being up to 30 mole %. An isomerization reactor may be used to obtain the desired molar ratio of 1-butene:2-butene for the feed composition into the metathesis reactor. After the metathesis reaction, of hexene and higher olefins are separated for aromatization to benzene and other aromatics.

A process for the regeneration of materials used in the guard beds preceding the reactors used in an olefin conversion process which converts olefinic refinery streams to higher boiling hydrocarbon products by polymerization (oligomerization) or alkylation of aromatics including benzene. Products of the process may include olefin oligomers and alkylaromatics in the gasoline boiling range as well as alkylaromatic petrochemicals such as cumene and ethylbenzene. The process is integrated with the olefin conversion process to ensure continuous operation of the olefin conversion without sending the feedstock containing the contaminant(s) to the reactor. The process uses reaction products from the olefin conversion process to regenerate the guard bed material and so is economically attractive since it does not require the use of separate purge, regeneration feed and separation systems. A plurality of guard beds is used, each containing a material which removes catalyst poisons. The guard beds are operated on a swing system in which one or more beds is kept on stream to remove the contaminant(s) while one or more of the remaining beds is being purged or regenerated. In this way, continuity of operation is assured. The regeneration medium is a product stream from the olefin conversion process.

Adsorbents and methods for the adsorptive separation of para-xylene from a mixture containing at least one other C8 aromatic hydrocarbon (e.g., a mixture of ortho-xylene, meta-xylene, para-xylene, and ethylbenzene) are described. Suitable binderless adsorbents (e.g., formulated with the substantial absence of an amorphous material that normally reduces selective pore volume), particularly those with a water content from about 3% to about 5.5% by weight, improve capacity and / or mass transfer. These properties are especially advantageous for improving productivity in low temperature, low cycle time adsorptive separation operations in a simulated moving bed mode.

A process for producing an ethylbenzene product having a purity of at least 99.50 percent based on the weight of ethylbenzene present in the product by the ethylation of the benzene present in non-extracted feed, e.g., non-extracted hydrocarbon composition. The non-extracted feed is substantially free of both C4− hydrocarbons and the C7+ aromatic hydrocarbons and contains benzene and benzene coboilers. The process is carried out in the liquid phase, in the presence of an acid-active catalyst containing MCM-22 family molecular sieve, and under specified conditions.

The invention discloses a catalytic thermal cracking method for lignin. The method comprises the following steps: preheating a molecular sieve catalyst to 200-300 DEG C, gradually adding lignin into the molecular sieve catalyst to carry out catalytic cracking reaction under the temperature of 500-800 DEG C and in the protective atmosphere of inert gas, separating the catalytic thermal cracking product of lignin after the reaction to obtain liquid, gas and solid products. By GC / MS analysis, the main components of the liquid product comprise benzene, toluene, ethylbenzene, naphthalene and other aromatic compounds, which account for 70%-80% of the total mass of the liquid products. The gas product is measured by GC, in which the volume of methane and carbon monoxide accounts for over 90% of that of the total gas. The main component of the solid product is carbon the mass fraction of which is between 75% and 85%. The products can be used for preparing fuel or aromatic chemicals.

A process for producing para-xylene from a hydrocarbon feed is described in which an adsorption column operating as a simulated moving bed with at least five zones delivers an extract, a 2-raffinate and an intermediate raffinate.The extract is distilled and the distillate is optionally re-crystallized to recover para-xylene with a purity of at least 99.7%. The 2-raffinate is distilled then isomerized in a reactor preferably operating in the liquid phase and at a low temperature. The intermediate raffinate with an enriched ethylbenzene content is distilled then isomerized in the vapour phase.

The invention belongs to the technical field of catalysis and relates to a method for preparing a monatomic cobalt catalyst by roasting silicon dioxide pellets and immobilizing metalloporphyrin. The method is realized by adopting the following technical scheme: namely stirring and dispersing nano silicon dioxide particles, dropwise adding 3-aminopropyl triethoxy silane, so as to obtain amino modified SiO2 pellets, then linking monocarboxyl metalloporphyrin (CoTPCPP) onto an amino modified SiO2 carrier through organic complexing, carbonizing porphyrin through high-temperature calcination in an inert atmosphere, and loading highly dispersed cobalt atoms onto the amino modified SiO2 pellets, thus an amino modified silicon dioxide pellet loaded monatomic cobalt catalyst is obtained. The monatomic dispersion catalyst has high catalytic activity and stability on a molecular oxygen selective ethylbenzene catalytic oxidation reaction in absence of solvent; meanwhile, a preparation method is simple, and product quality can be easily controlled, so that the monatomic dispersion catalyst is applicable to the fields of alkane selective oxidation reactions and synthesis of medical intermediates.

Adsorbents and methods for the adsorptive separation of para-xylene from a mixture containing at least one other C8 aromatic hydrocarbon (e.g., a mixture of ortho-xylene, meta-xylene, para-xylene, and ethylbenzene) are described. Suitable binderless adsorbents (e.g., formulated with the substantial absence of an amorphous material that normally reduces selective pore volume), particularly those with a water content from about 3% to about 5.5% by weight, improve capacity and / or mass transfer. These properties are especially advantageous for improving productivity in low temperature, low cycle time adsorptive separation operations in a simulated moving bed mode.

The process of preparing catalyst for C8 arene isomerization includes forming the mixture of EUO type molecular sieve and adhesive to obtain carrier, introducing VIII metal, drying, roasting and reducing with reductant gas. The catalyst contains EUO type molecular sieve in 5-90 wt%, adhesive 10-90 wt%, and VIII metal 0.1-5.0 wt%. The EUO type molecular sieve is prepared through mixing compound containing element X, compound containing element T, alkali metal compound and water, hydrothermal crystallization reaction in the presence of template agent precursor compounded with coarse dibromoalkane and monamine, collecting the solid and drying, where X is Si and Ge, T is Al, Fe, Ga or B, and the coarse dibromoalkane is mixture of dibromoalkane in the content of 80-95 wt%, Monobromoalkane and paraffin hydrocarbon diol. The catalyst has high ethyl benzene converting rate and low arene losing rate.

A catalyst for dehydrogenating ethylbenzene in the condition of low water ratio is prepared through adding at least two compounds of light RE elements other than Ce, and at least one oxide of metal chosen from Ca, Mg, Ba, B, Sn, Pb, Cu, Zn, Ti, Zr, V and Mo to the Fe-K-Ce-W system. It has high stability and activity.

The use of two transalkylation catalysts to react aromatic compounds of carbon number nine (and heavier carbon numbers) with benzene to form carbon number eight aromatics is disclosed. The two catalyst system preserves ethyl-group species on the heavier aromatics that would otherwise de-ethylate over most gas-phase transalkylation catalysts to form undesired ethane gas with benzene or toluene. Thus, by using a transalkylation step to save ethylbenzene, a greater yield of para-xylene or other carbon number eight aromatics may be achieved within an integrated complex. An apparatus and process for the two transalkylation catalyst system is disclosed with a liquid-phase unit and a gas-phase unit.

A process for isomerizing xylenes while retaining ethylbenzene in a C8-aromatics stream in liquid phase uses a gallium-substituted pentasil zeolite in the absence of hydrogen.

A method for producing propylene oxide by reacting propylene with ethylbenzene hydroperoxide, wherein the reaction is conducted in the presence of a catalyst comprising a titanium-containing silicon oxide and satisfying all of the following conditions (1) to (6):(1) there is at least one peak showing a interplanar spacing (d) larger than 18 Å in X-ray diffraction;(2) an average pore size is 10 Å or more;(3) a pore size of 90% or more of the total pore volume is 5 to 200 Å;(4) a specific pore volume is 0.2 cm3 / g or more;(5) a quaternary ammonium ion represented by the following general formula (I) is used as a template and then said template is removed by calcination operation:wherein R1 represents a linear or branched hydrocarbon chain having 2 to 36 carbon atoms, and R2 to R4 represent an alkyl group having 1 to 6 carbon atoms; and(6) The catalyst has been subjected to silylation treatment.

The invention discloses a method for preparing ethylbenzene by reaction of dilute ethylene and benzene, which uses the dilute ethylene in dry gas of oil refinery as raw material, water washing and selective removal of propylene are conducted for the dry gas before the dry gas enters an alkylation reactor in sections, alkylation reaction of the dilute ethylene in dry gas and the benzene proceeds under the circumstances that zeolite catalyst exists, the dry gas and / or low-temperature gas-phase benzene are utilized for taking heat during the alkylation reaction, and the reaction temperature rising is reduced; after the vapor-liquid separation of the alkylation reaction product, tail gas is discharged from the device through low-temperature absorption, and cycle benzene, ethylbenzene, propyl benzene, diethylbenzene and heavy component are sequentially separated from the liquid product through a separation system; the diethylbenzene and the benzene are mixed and enter an anti-alkylation reactor and anti-alkylation reaction proceeds on molecular sieve catalyst for further converting to the ethylbenzene. The invention effectively reduces the benzene consumption and the energy consumption during the course of preparing ethylbenzene by dilute ethylene, the ethylene conversion rate is more than or equal to 99%, the total selectivity of generating ethylbenzene is more than or equal to 99%, the recovery rate of benzene carried by the tail gas is more than or equal to 99.5%, and the xylene content in the ethylbenzene is less than 800 ppm.

The invention discloses a predisposing technological flow path of ethylbenzene through catalyzing dried gas, which comprises the following steps: adsorbing propylene; desorbing ethylene; desorbing propylene; adding raw material to strip propylene; washing most of MEDA; entering standard dried gas in the delivery tank; entering into propylene adsorbing tower; draining purified dried gas from top of propylene adsorbing tower; making one path as cool material in the ethylene stripping tower and one path to exchange heat with base material of propylene stripping tower under 10-300 deg.c in the ethylene stripping tower; desorbing ethylene component; draining ethylene gas; returning in the dried gas delivery tank; circulating between ethylene stripping tower and propylene stripping tower; desorbing propylene component from adsorbant with 150ppm-0.7% dried propylene in the stripped propylene.

A process for producing para-xylene from a hydrocarbon feed is described in which an adsorption column operating as a simulated moving bed with at least five zones delivers an extract, a 2-raffinate and an intermediate raffinate.The extract is distilled and the distillate is optionally re-crystallized to recover para-xylene with a purity of at least 99.7%. The 2-raffmate is distilled then isomerized in a reactor preferably operating in the liquid phase and at a low temperature. The intermediate raffinate with an enriched ethylbenzene content is distilled then isomerized in the vapour phase.

The invention aims to provide a catalyst for preparing phenylethane from dilute ethylene and benzene alkylation and a method for preparing the same. The catalyst is characterized in that the crystal is formed by a small crystal grain ZSM-5 molecular screen with the crystal grain size of between 0.15 and 0.8 mircometer and a bonding agent of aluminum oxide and silicon dioxide, and then prepared by steps of vapor / ammonia vapor treatment and acid treatment, wherein the relative mass ratio of the ZSM-5 molecular screen to the bonding agent of the aluminum oxide and the silicon dioxide is (5-9):(1-5). When the catalyst is used for preparing the phenylethane from the dilute ethylene and the benzene alkylation in dry gas, because the crystal grain size of the used molecular screen is small, the number of acidic sites and the acidic utilization ratio of the catalyst are high, and simultaneously the pore canal of the molecular screen is short, which is favorable for dispersion of reactants and products, so that the catalyst has the characteristics of high activity, low reaction temperature, high selectivity of target products, low content of xylene impurity in the product and good satiability.