Abstract: A process for producing methyl tert-butyl ether (MTBE) comprising introducing a butane feed stream (n-butane, i-butane) and hydrogen to a hydrogenolysis reactor comprising a hydrogenolysis catalyst to produce a hydrogenolysis product stream comprising hydrogen, methane, ethane, propane, i-butane, and optionally n-butane; separating the hydrogenolysis product stream into a first hydrogen-containing stream, an optional methane stream, a C2 to C3 gas stream (ethane, propane), and a butane stream (i-butane, optionally n-butane); feeding the butane stream to a dehydrogenation reactor to produce a dehydrogenation product stream, wherein the dehydrogenation reactor comprises a dehydrogenation catalyst, and wherein the dehydrogenation product stream comprises hydrogen, i-butane, and isobutylene; and feeding the dehydrogenation product stream and methanol to an etherification unit to produce an unreacted methanol stream, an unreacted isobutylene stream, and an MTBE stream.

Abstract: A steam-assisted catalytic cracking process for a hydrocarbon feed is provided. The process includes: introducing the hydrocarbon feed, a fluid catalytic cracking (FCC) catalyst, and steam to a FCC reactor with a mass ratio of steam to hydrocarbon feed between 0.05 and 1.0; cracking the hydrocarbon feed in the presence of the FCC catalyst and steam to produce a cracked hydrocarbon feed and spent FCC catalyst, the spent FCC catalyst comprising coke deposits and hydrocarbon deposits; stripping the hydrocarbon deposits from the spent FCC catalyst with steam in a stripper to obtain a hydrocarbon-stripped spent FCC catalyst; regenerating the hydrocarbon-stripped spent FCC catalyst in a regenerator by subjecting the stripped spent FCC catalyst to heat in the presence of oxygen to combust the coke deposits on the stripped spent FCC catalyst and produce a regenerated FCC catalyst; recycling the regenerated FCC catalyst.

Abstract: The present application provides systems and methods for producing isononanol and gasoline and diesel blending components. In at least one embodiment of the present systems and methods, a hydrocarbon feed is cracked in a steam cracker to form a first ethylene stream, a first propylene stream, and a C4 stream comprising isobutene and butadiene. The C4 stream is reacted with a methanol stream in a methyl tertiary butyl ether (MTBE) unit to form MTBE and a butadiene-rich C4 stream. The butadiene-rich C4 stream is selectively hydrogenated in a butadiene unit to form a butene-rich C4 stream. The butene-rich C4 stream undergoes a series of reactions in an isononanol unit to produce isononanol and an olefin-rich stream. The olefin-rich stream is then separate, in a separation unit, a C8, C12, and C16 fuel oil streams.

Abstract: A process for preparing a hydrocarbon fluid includes a step of oligomerising an initial hydrocarbon composition which contains, in relation to the total weight of said initial hydrocarbon composition, at least 2% by weight of 3-methyl-but-1-ene, at least 5% by weight of 2-methyl-but-2-ene and at least 5% by weight of 2-methyl-but-1-ene.

Abstract: Disclosed is a process for the regeneration of an adsorber. For the regeneration a liquid stream (S2) is applied which is obtained by hydrogenation of a stream (S1) comprising at least one alkane and least one olefin. The stream (S2) comprises one alkane and a reduced amount of at least one olefin compared to the amount in the stream (S1). Then the stream (S2) is converted from the liquid into the gaseous phase and the adsorber is regenerated by contact with the gaseous stream (S2).

Abstract: Disclosed is a process for the regeneration of an adsorber (A1). The adsorber (A1) is regenerated by contact with a gaseous stream (S2) and the outflow of the adsorber (A1) comprising condensate of stream (S2) and organic composition (OC1) collected in a device. After regeneration of the adsorber (A1) the stream (S2) in the adsorber (A1) is replaced completely or at least partially by the content of the device. Then the adsorber (A1) is fed with organic composition comprising at least one olefin, at least one alkane and at least one compound containing oxygen and/or sulfur.

Abstract: Disclosed is a process for the purification of an organic composition (OC1) by adsorption using an assembly containing at least two adsorbers. The organic composition (OC1) comprising at least one alkane, at least one olefin and at least one compound containing oxygen and/or sulphur is fed into a first adsorber (A1) of the assembly in order to obtain an organic composition (OC2) comprising at least one alkane, at least one olefin and a reduced amount of at least one compound containing oxygen and/or sulphur compared to the respective amount in organic composition (OC1). Hydrogenation of the organic composition (OC2) provides a stream (S2) comprising at least one alkane and a reduced amount of at least one olefin compared to the respective amount in organic composition (OC2) obtained after feeding into the first adsorber (A1). A second adsorber (A2) of the assembly is regenerated by contact with stream (S2).

Abstract: Use of a catalyst composition comprising A) a first component containing oxidic compounds comprising aluminum and silicon with a molar ratio of silicon to aluminum of more than 1) B) a second component containing an oxidic compound of silicon wherein the ratio of the number of acidic sites of component A, determined by temperature programmed desorption with ammonia as a base, to the number of acidic sites of component B, determined under the same conditions, is at least 3: in a process for the catalytic depolymerization of plastics waste.

Abstract: Processes for co-production of methyl tertiary-butyl ether (MTBE) and alkylate is disclosed. The process includes comprising passing a hydrocarbon feed stream comprising C4 hydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising C4 olefins. The dehydrogenation effluent is passed to a MTBE unit to provide a mixed stream comprising C4 olefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylation product stream comprising an alkylate.

Abstract: The present invention relates to a process for etherification of mixed olefinic light naphtha boiling in the range of C5-90° C. cut with simultaneous minimization of unreacted methanol concentration in the product. The etherification of mixed olefinic light naphtha produces the high octane blending component which can be blended directly in the gasoline pool without any recovery of the feed oxygenates like methanol, ethanol etc. which conventionally uses energy intensive separation processes.

Abstract: A process for the production of oligomerized olefins comprising the following steps: purification of an organic composition (OC1) in at least one adsorber to obtain an organic composition (OC2); oligomerization of organic composition (OC2) in the presence of a catalyst to obtain an organic composition (OC3); distillation of organic composition (OC3) in a distillation column (D1) to obtain an organic composition (OC4) from the upper part of (D1) and an organic composition (OC5) from the lower part of (D1); hydrogenation of organic composition (OC4) to obtain an organic composition (OC11) and regeneration of an adsorber (A1) employing organic composition (OC11) as regeneration media.

Abstract: The present invention provides a method for directly preparing glycol dimethyl ether and co-producing ethylene glycol from ethylene glycol monomethyl ether. More specifically, the method comprises passing a feedstock containing a raw material of ethylene glycol monomethyl ether and a carrier gas through a reactor loaded with a solid acid catalyst to produce glycol dimethyl ether and ethylene glycol, at a reaction temperature range from 40° C. to 150° C. and a reaction pressure range from 0.1 MPa to 15.0 MPa; wherein a carrier gas is an optional inactive gas; and the feedstock contains water whose volume concentration in the feedstock is in a range from 0% to 95%; and the weight hourly space velocity of the raw material of ethylene glycol monomethyl ether is in a range from 0.05 h?1 to 5.

Abstract: The invention provides a process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation, comprising: a high-efficiency atomizing nozzle sprays the preheated crude oil into an upper portion of the downflow modification reaction tube, the produced oil mist is mixed with a high temperature heat carrier flowing downward from a first return controller for pyrolysis in milliseconds and then the pyrolysis products are subject to a gas-solid separation; the coked heat carrier obtained by the separation enters into a modification regeneration reactor to conduct a regeneration reaction, the obtained high temperature heat carrier returns to a top of the downflow reaction tube to participate in circulation, the regeneration gas is subject to heat exchange and then output; the high temperature oil and gas produced by the pyrolysis reaction directly flow into the millisecond cracking reactor and conduct a cracking

Abstract: This invention pertains to a method for purifying an olefinic feedstock that comprises olefins with 4 carbon atoms and impurities including isobutanal, ethanol, and acetone, where said method comprises a pretreatment that comprises a step for eliminating acetone and optionally a step for eliminating the water that is present in said olefinic feedstock, and a step for simultaneously eliminating isobutanal and ethanol by running the feedstock obtained from the pretreatment over at least one fixed bed having at least one adsorbent that comprises at least one porous refractory oxide-based material, optionally impregnated with one or more alkaline or alkaline-earth cations; where said step for simultaneously eliminating isobutanal and ethanol operates at a temperature of between 0 and 200° C., at a pressure of 0.1 to 10 MPa, and with an hourly volumetric flow rate (VVH) of the feedstock on the fixed bed of between 0.1 and 10 h?1.

Abstract: A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a propane diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) allowing propane to build-up to an amount sufficient to operate as a diluent and (6) recovering product diisopropyl alcohol.

Abstract: A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a C4 diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) purging a portion to prevent propane build-up and (6) recovering product diisopropyl alcohol.

Abstract: A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a C4 diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) purging a portion to prevent propane build-up and (6) recovering product diisopropyl alcohol.

Abstract: The present disclosure relates to processes for the removal of paraffins. The processes generally include providing a C4 containing stream including isobutylene, 1-butene, 2-butene, n-butane and isobutane, introducing the C4 containing stream into a paraffin removal process to form an olefin rich stream, wherein the paraffin removal process is selected from extractive distillation utilizing a solvent including an organonitrile, passing the C4 containing stream over a semi-permeable membrane and combinations thereof; and recovering the olefin rich stream from the paraffin removal process, wherein the olefin rich stream includes less than 5 wt. % paraffins.

Abstract: Processes and systems for producing olefins, including: dehydrogenating a first n-alkane to produce a first effluent; and dehydrogenating at least one of a first isoalkane or a second n-alkane to produce a second effluent. The first and second effluents may be compressed and fed to a common separation train to separate the effluents into two or more fractions. In some embodiments, each of the first and second dehydrogenation reaction zones may include two reactors, one reactor in each of the reaction zones operating in a dehydrogenation cycle, one operating in a regeneration cycle, and one operating in a purge or evacuation/reduction cycle. Operation of the reactors in the dehydrogenation cycle is staggered, such that the purge cycle, regeneration cycle, or evacuation/reduction cycle of the reactors may not overlap.

Abstract: An integrated process for making propene oxide and an alkyl tert-butyl ether comprises dehydrogenating a feed stream comprising iso-butane to provide a stream comprising iso-butene and hydrogen and separating this stream into a stream consisting essentially of hydrogen and a stream comprising iso-butene; reacting a part or all of the stream comprising iso-butene with an alkanol in the presence of a solid acid catalyst to provide an alkyl tert-butyl ether; reacting a part or all of the stream consisting essentially of hydrogen with oxygen, providing a stream comprising hydrogen peroxide; and reacting a part or all of the stream comprising hydrogen peroxide with propene in the presence of an epoxidation catalyst to provide propene oxide.

Abstract: An integrated process for making propene oxide and an alkyl tert-butyl ether comprises dehydrogenating a feed stream comprising propane and iso-butane to provide a stream comprising propene, iso-butene and hydrogen; separating this stream into a stream consisting essentially of hydrogen and a stream comprising propene and iso-butene; separating the stream comprising propene and iso-butene into a stream comprising propene and a stream comprising iso-butene; reacting a part or all of the stream comprising iso-butene with an alkanol in the presence of a solid acid catalyst to provide an alkyl tert-butyl ether; and reacting a part or all of the stream comprising propene with hydrogen peroxide in the presence of an epoxidation catalyst to provide propene oxide.

Abstract: A diesel fuel based on ethanol is described, which comprises about 60 to about 90% (v/v) ethanol, up to about 20% (v/v) of a linear dialkyl ether with a chain length of about 10 to about 40 as well as mixtures thereof, and 0 to about 30% (v/v) combustion accelerator.

Abstract: The present invention provides, among other things, new processes for separating and purifying C4 fractions from a crude C4 stream. Compared to prior methods, the processes of the present invention simplify the C4 separation processes, afford more possible configurations for separation and purification, and are more cost effective. The processes and systems provided herein can be used as part of a cost-effective and efficient method for synthesizing methyl tertiary-butyl ether.

Abstract: The invention relates to a membrane having a pore-free separating layer including a polymer mixture for separating simple alcohols and water from their mixtures with other organic fluids by means of pervaporation or vapor permeation. In accordance with the invention, the polymer mixture is composed of at least two polymer components which are taken from the group of polymer components which includes of the following polymer components: Polyvinyl alcohol, other polymers such as poly N—N-dimethylaminoethyl methacrylate (poly DMAEMA), a copolymer of DMAEMA and N-vinyl pyrrolidone (NVP) or of DMAEMA and N-vinyl caprolactam (NVCL), a terpolymer of DMAE, NVP and NVCL or of vinyl acetate ethylene vinyl chloride or from vinyl chloride ethylene acrylic ester or from vinyl acetate vinyl chloride acrylic ester. The invention further relates to the use and to a method for manufacturing a membrane in accordance with the invention.

Abstract: Disclosed is a method of preparing isobutene in which high-purity isobutene is separated (prepared) from a C4 mixture by cracking glycol ether prepared from a C4 mixture (in particular, C4 raffinate-1) containing isobutene and a glycol. The method includes cracking glycol ether into isobutene and glycol at a temperature between 50° C. and 300° C. in the presence of a strongly acidic catalyst. The glycol ether may be prepared by reaction between a C4 mixture containing isobutene and glycol in the presence of an acid catalyst.

Abstract: Processes for providing an isobutane recycle stream to be recycled to a dehydrogenation zone. In some embodiments a dividing wall column is used to separate a hydrogenation effluent. The hydrogenation effluent may include olefins, or it may be fully saturated. A hydrogenation zone may include a nickel based catalyst and may fully saturate dienes and olefins, or only hydrogenate dienes.

Abstract: A method and apparatus for processing hydrocarbons are described. The method includes fractionating a hydrocarbon stream to form at least two fractions. The first fraction is reformed to form a reformate stream, and the reformate stream is introduced into an aromatics processing zone to produce aromatic products. At least a portion of the second fraction is cracked in a fluid catalytic cracking unit. A selectively hydrogenated light naphtha stream is formed by separating the cracked hydrocarbon stream into at least two streams and selectively hydrogenating the light naphtha stream, or selectively hydrogenating the cracked hydrocarbon stream and separating the hydrogenated cracked hydrocarbon stream into at least two streams. Aromatics are extracted from the selectively hydrogenated light naphtha stream forming an extract stream and a raffinate stream. The extract stream is hydrotreated, sent to the aromatics processing zone to produce additional aromatic products.

Abstract: In this invention, a portion of the products from a pyrolysis reactor are reacted in a process to form one or more chemical intermediates.

Abstract: A method for producing synthesis gas, including: 1) pre-processing a biomass raw material; 2) pyrolyzing the biomass raw material to yield a pyrolysis gas and a carbon powder; 3) separating the pyrolysis gas from the carbon powder and a solid heat carrier; 4) separating the carbon powder away from the solid heat carrier via a solid-solid separator; 5) conveying the generated pyrolysis gas to a condensate tank for spray condensation, condensing a condensable part in the pyrolysis gas to generate biological fuel oil, pressurizing the generated biological fuel oil by a high pressure oil pump and feeding to a gasification furnace to be gasified; and 6) feeding one part of non-condensable pyrolysis gas to a combustion bed to combust with air, and conveying the other part of the non-condensable pyrolysis gas to the pyrolysis bed as a fluidizing medium.

Abstract: A process for the oligomerization of olefins includes treating, e.g., water washing, an olefin-containing hydrocarbon stream to lower the concentration of an organic nitrogen-containing Lewis base contained therein until the treated hydrocarbon stream is substantially free of the Lewis base; and subsequently contacting the treated hydrocarbon stream with a molecular sieve catalyst to produce a product including at least one oligomer.

Abstract: A process for the production of dialkyl ether, the process including: feeding a stream comprising an alkyl alcohol to a distillation column reactor system; concurrently in the distillation column reactor system: i) contacting the alkyl alcohol with a catalytic distillation structure in a distillation reaction zone thereby catalytically reacting at least a portion of the alkyl alcohol to form a corresponding dialkyl ether and water; and ii) fractionating the resulting dialkyl ether from the water; operating the distillation column reactor system to obtain substantially complete conversion of the alkyl alcohol to form the corresponding dialkyl ether and water; recovering the dialkyl ether from the distillation column reactor as an overheads fraction; recovering the water from the distillation column reactor as a bottoms fraction.

Abstract: A process for the production of C4 olefins, which may include: contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes; contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and C5 olefins; and fractionating the first metathesis product to for an ethylene fraction, a propylene fraction, a butene fraction, and a C5 fraction.

Abstract: A process for glycerol etherification, including a recycle of glycerol and/or mono-ether, to produce glycerol alkyl ethers with low amount of mono-ether by reacting glycerol and olefinic hydrocarbon, and/or the corresponding aldehydes, ketones and alcohols, having 2 to 10 carbon atoms in the presence of homogeneous acid catalyst with hindered formation of olefin oligomers comprising of two essential steps: reaction step (1) neutralization and salt removal step (2).

Abstract: The present invention relates to a process for the production of 1,3-butadiene which comprises the following phases: a) extracting, by means of extractive distillation, in an extraction section, an end-product containing 1,3-butadiene and a raffinate product, starting from mixtures of saturated and unsaturated compounds having from 2 to 10 carbon atoms in the chain; b) sending the raffinate product to a dehydrogenation section; c) dehydrogenating the raffinate product in the dehydrogenation section in the presence of a dehydrogenation catalyst and an inert product so as to form a reaction effluent containing 1,3-butadiene; d) recirculating the reaction effluent containing 1,3-butadiene directly to the extraction section after separating the incondensable compounds.

Abstract: A method of producing a solid glycerol derived material includes the steps of combining glycerol with a metal oxide, the glycerol having a water content of between about 5 and 50%, and the rate of combination of the glycerol and the metal oxide and the amount of the metal oxide being selected so that at least part of the water present in the glycerol reacts with the metal oxide in an exothermic reaction and at least part is driven off by heat produced in the exothermic reaction to produce the solid glycerol derived material.

Abstract: Disclosed herein is a process for preparing a salt of a sulfurized alkyl-substituted hydroxyaromatic composition having a reduced content of unsulfurized alkyl-substituted hydroxyaromatic compound and its unsulfurized metal salt.

Abstract: Disclosed is a method of preparing a glycol mono-tertiary-butyl ether compound using a C4 hydrocarbon mixture containing isobutene and a glycol compound as reactants, in which a glycol di-tertiary-butyl ether compound as a byproduct is decomposed into isobutene and a glycol compound and the obtained isobutene and glycol compound are recycled as reactants, whereby product yield per unit raw material may be maximized.

Abstract: An enhanced method of producing ethers from iso-olefins and alcohols comprises at least one stage of separation of the excess alcohol by an ionic liquid. The ether-hydrocarbon-alcohol effluent treated in said separation stage by the ionic liquid comes from the reaction section and/or from a fractionating column. The separated and condensed alcohol is recycled in the process.

Abstract: A catalytic reaction-rectification integrated process and a catalytic reaction-rectification integrated column, and the specialized device of such process is provided. The reactants are preheated and mixed with catalysts, and then fed into a jet agitation reaction section located in the middle of the catalytic reaction-rectification integrated column from a feeding inlet. The jet agitation reaction section is a kettle-like reactor located in the middle of the catalytic reaction-rectification integrated column. After pressurized by a centrifugal pump, the reactant materials are admitted into a subsonic or transonic agitator located within the reaction section. The reactant materials are ejected into the jet agitation reaction section at high speed, to efficiently mix the solid and liquid phases in the reaction section and to reinforce heat and mass transfer efficiency during the reaction. The liquid reaction mixture is separated and purified directly in the catalytic reaction-rectification integrated column.

Abstract: The invention relates to processes for the etherification of olefins with alcohols. According to one aspect, a heterogeneous etherification catalyst is used under conditions that permit limiting the contact time between the desired product and the catalyst, thereby mitigation reverse reactions. According to a second aspect, a recycling process is used that significantly increases the yield of desired product.

Abstract: The present invention relates to a catalytic process for making isooctenes using a reactant comprising isobutanol and water. The isooctenes so produced are useful for the production of fuel additives.

Abstract: A method of crystallizing a crystalline molecular sieve having a pore size in the range of from about 2 to about 19 ?, said method comprising the steps of (a) providing a mixture comprising at least one source of ions of tetravalent element (Y), at least one hydroxide source (OH?), and water, said mixture having a solid-content in the range of from about 15 wt. % to about 50 wt. %; and (b) treating said mixture to form the desired crystalline molecular sieve with stirring at crystallization conditions sufficient to obtain a weight hourly throughput from about 0.005 to about 1 hr?1, wherein said crystallization conditions comprise a temperature in the range of from about 200° C. to about 500° C. and a crystallization time less than 100 hr.

Abstract: The present invention relates to a process for the production of fuel additives in which in a first step isobutanol is subjected to a simultaneous dehydration and skeletal isomerisation to make substantially corresponding olefins, having the same number of carbons and consisting essentially of a mixture of n-butenes and iso-butene and in a second step the butene mixture is subjected to etherification, said process comprising: a) introducing in at least one reactor a stream (A) comprising at least 40 wt % isobutanol, optionally an inert component, b) contacting said stream with at least one catalyst in said reactor(s) at conditions effective to simultaneously dehydrate and skeletal isomerise at least a portion of the isobutanol to make a mixture of n-butenes and iso-butene, c) removing the inert component if any, recovering from said reactor(s) a stream (B) comprising a mixture of n-butenes and iso-butene, d) sending the stream (B) to at least one etherification reactor and contacting stream (B) with at lea

Abstract: A process for the production of dimethyl ether from a methanol reactor effluent is disclosed. The process may include: contacting an aqueous extractant comprising water and an effluent from a methanol synthesis reactor comprising methanol and one or more of methane, water, carbon monoxide, carbon dioxide, hydrogen, and nitrogen. At least a portion of the methanol partitions into the aqueous extractant; recovering an extract fraction comprising the aqueous extractant and methanol. The extract fraction is fed to a catalytic distillation reactor system for concurrently: contacting the methanol with catalyst in a reaction zone thereby catalytically reacting at least a portion of the methanol to form dimethyl ether and water; and fractionating the resulting dimethyl ether and the water to recover a first overheads fraction comprising dimethyl ether and a first bottoms fraction comprising water.

Abstract: The invention is a process for preparing lower olefins comprising: a) steam cracking a paraffinic feedstock to obtain a cracker effluent comprising olefins and saturated and unsaturated C4 hydrocarbons; b) contacting an oxygenate feedstock with a molecular sieve-comprising catalyst, at a temperature in the range of from 350 to 1000° C. to obtain an oxygenate conversion effluent comprising olefins and saturated and unsaturated C4 hydrocarbons; c) subjecting the cracker effluent and the oxygenate conversion effluent to one or more separation steps such that an olefin product stream comprising ethylene and/or propylene, and a stream comprising saturated and unsaturated C4 hydrocarbons are obtained; and d) subjecting part of the stream comprising C4 hydrocarbons from both the cracker effluent and the oxygenate conversion effluent to extractive distillation to obtain a stream enriched in unsaturated C4 hydrocarbons and a stream enriched in saturated C4 hydrocarbons.

Abstract: This disclosure provides a molecular sieve composition having a first and second crystalline molecular sieve, made by the method comprising: (a) providing a reaction mixture comprising at least one source of ions of tetravalent element Y, at least one source of alkali metal hydroxide, water, optionally at least one seed crystal, and optionally at least one source of ions of trivalent element X, the reaction mixture having the following molar composition: Y:X2=2 to infinity, preferably from about 2 to about 1000, OH?:Y=0.001 to 2, preferably from 0.1 to 1, M+:Y=0.001 to 2, preferably from 0.

Abstract: Embodiments of methods for producing ethyl tert-butyl ether (ETBE) are provided herein. A method for producing ETBE comprises the steps of contacting a C4 olefin-rich stream that contains isobutene with a first catalyst in the presence of ethanol at etherification conditions effective to form a reaction effluent comprising ETBE and residual ethanol. The reaction effluent is combined with a C5 paraffin-rich stream that contains isopentane to form a combined stream. The combined stream is fractionated at distillation conditions effective to produce an ETBE-rich product stream. Fractionating the combined stream comprises forming a light boiling azeotrope of ethanol with isopentane to remove at least a portion of the residual ethanol from the combined stream.

Abstract: A composition that includes one or more compounds represented by the formula R1(X)R2 wherein R1 is an alkyl group having from 4 to 40 carbon atoms, R2 is an aliphatic group having from 4 to 20 carbon atoms, an aromatic group having from 6 to 20 carbon atoms, or a cycloaliphatic group having from 5 to 20 carbon atoms, and X is a heteroatom. The composition has a viscosity (Kv100) from 2 to 30 at 100° C., a viscosity index (VI) from 100 to 200, and a Noack volatility of no greater than 20 percent. The disclosure also relates to a process for producing the composition, a lubricating oil base stock and lubricating oil containing the composition, and a method for improving one or more of solubility and dispersancy of polar additives in a lubricating oil by using as the lubricating oil a formulated oil containing the composition.

Abstract: We provide a method for operating a navigation system for a motor vehicle in a road network, and to a navigation system. To this end, first a zone of the road network is provided with an emissions class-dependent drive-through restriction, wherein the motor vehicle is associated with at least one emissions class. First, information about the geographical location of the zone and about the emissions class at least required there is stored in the navigation system. Then, information about the at least one emissions class of the motor vehicle is entered into the navigation system. Thereafter, the information entered is considered in the destination guidance process, wherein destination guidance into or through the zone is avoided if the at least one emissions class of the motor vehicle is affected by emissions class-dependent drive-through restrictions in the zone.

Abstract: The invention relates to a process for preparing ETBE from technical mixtures which comprise at least 1-butene, isobutene, n-butane and 2-butenes, by reacting the isobutene present, distillatively removing a fraction comprising 1-butene and isobutene and again reacting the isobutene present therein to give ETBE.