Abstract: A process the dehydration of methanol to dimethyl ether in the presence of a solid Brønsted acid catalyst selected from aluminosilicate zeolites which have a maximum free sphere diameter of greater than 3.67 Angstroms and heteropolyacids and a promoter selected from methyl formate, dimethyl oxalate and dimethyl malonate and the molar ratio of promoter to methanol is maintained at less than 1.

Abstract: A process for dehydrating C2+ alcohols to ether products in the presence of a catalyst and promoter, wherein the catalyst is at least one aluminosilicate zeolite catalyst which is a medium pore zeolite having a 3-dimensional framework structure, and the promoter is one or more organic carbonyl compounds or derivatives thereof, and wherein and the molar ratio of promoter to C2+ alcohols is maintained at less than 1.

Abstract: A method for producing methanol is disclosed. The method includes supplying a high oxygen content oxidant to combust hydrocarbons, in particular methane, and then using the resulting hot gases to heat natural gas so as to convert the natural gas to synthesis gas. The synthesis gas is used to produce methanol in a methanol synthesis reactor. At least some of the carbon dioxide from the hot gases is fed to the methanol synthesis reactor to make methanol.

Abstract: A method of modifying a chemical interaction between a functional group of an immobilized amine in a solid sorbent composition and a compound that chemically interacts with the functional group to reduce the heat required to desorb the compound from the solid sorbent. A method of inhibiting degradation of an immobilized amine in an immobilized amine solid sorbent. Compositions and methods of use of a low-cost regenerable immobilized amine solid sorbent resistant to degradation.

Abstract: A method of producing one or more glycerol ethers, the method comprising contacting glycerol and tertiary butanol (TBA) in the presence of an acidic catalyst to produce one or more glycerol ethers selected from mono-tert butyl glycerol ethers, di-tert butyl glycerol ethers, tri-tert butyl glycerol ethers, or a combination thereof; separating water and a stream comprising isobutylene, unreacted TBA, or a combination thereof from the one or more glycerol ethers; and recycling at least a portion of the stream comprising isobutylene, unreacted TBA, or a combination thereof to the contacting. Also disclosed is a process of co-producing isooctene, wherein the process involves contacting glycerol and tertiary butanol in the presence of a dehydrating catalyst and dimerizing/oligomerizing the dehydrated products in the presence of an oligomerizing catalyst to form isooctene, a precursor of isooctane and isomers thereof.

Abstract: A process is proposed for production of dimethyl ether (DME) from synthesis gas (SG), in which at least one feed stream formed from synthesis gas (SG) is subjected to at least one synthesis step, in which components present in the feed stream are at least in part converted to dimethyl ether (DME), wherein at least one crude product stream is obtained which contains at least dimethyl ether (DME) and the unreacted components of the feed stream. The feed stream contains at least hydrogen, carbon monoxide and carbon dioxide, and has a stoichiometric number of 2.0 to 5.0. The feed stream further contains 4 to 20 mol percent carbon dioxide, and the ratio of carbon dioxide to carbon monoxide in the feed stream is in a range from 0.5 to 4. The at least one synthesis step is carried out under isothermal conditions. A system for production of dimethyl ether (DME) from synthesis gas (SG) is likewise subject matter of the present invention.

Abstract: The invention provides a process for the production of purified dimethylether (DME). Methanol is dehydrated to provide a first DME-containing product. The first DME-containing product is purified in a two-stage process. The invention also provides an apparatus arranged to carry out said process.

Abstract: The invention relates to a self-igniting internal combustion engine (10) with ether fumigation of the combustion air for vehicles, wherein to provide for ether fumigation, a feed means (1, 2, 3) is provided for an alkanol fuel in the flow direction, an exhaust gas heat exchanger (4) is provided for cooling a portion of the exhaust gas arising from the firing of the internal combustion engine (10) and for vaporizing the alkanol fuel fed while at the same time absorbing the thermal energy to be dissipated during cooling of the exhaust gas, and a catalyst (5) is provided for dehydrating the evaporated alkanol fuel to form ether, and wherein the feed means (1, 2, 3), the exhaust gas heat exchanger (4) and the catalyst (5) are connected to the combustion chamber of the internal combustion engine (10) and adapted in such a way that a portion of the fuel required to fire the internal combustion engine (10) can be fed to the combustion chamber of the internal combustion engine (10) by way of the ether fumigation of t

Abstract: In the production of purified methanol and/or dimethyl ether from crude methanol, the crude methanol is processed in at least one prepurification stage, a first partial stream of the prepurified methanol is supplied to a final methanol purification and a second partial stream of the prepurified methanol is supplied to a reactor and at least partly converted to dimethyl ether. The dimethyl ether recovered is purified in at least one purification stage, wherein non-reacted methanol is withdrawn from the dimethyl ether purification stage and at least partly supplied to the final methanol purification. In this way, both purified methanol and dimethyl ether can be produced in parallel, wherein the quantities of both products obtained are flexibly adjustable.

Abstract: A carboxylic acid e.g. acetic acid, is recovered from an aqueous feed stream containing the corresponding ester, an alcohol and a small amount of water by catalytically dehydrating the alcohol to the corresponding ether and water, and reacting the water with the ester to generate a liquid carboxylic acid rich product stream. The acid is recovered by distillation. In a second embodiment, additional alcohol and/or water are co-fed with the feed or fed directly to a catalytic distillation column, resulting in a liquid bottom product stream of substantially pure acetic acid and a top distillate stream of substantially pure ether.

Abstract: The present invention relates to the process of production of olefins by means of the dehydration of light alcohols using ionic liquids as an acidic medium. Furthermore, the present invention relates to the use of such olefins, for example, for the production of polymers and ethylene glycol.

Abstract: This invention describes a method for co-producing isobutene and ethyl tert-butyl ether from tert-butanol mixture in a catalytic distillation column, wherein catalyzing the tert-butanol mixture with the ethanol undergoes dehydration and etherification. The tert-butanol mixture contains absolute ethanol or aqueous ethanol as the antifreeze agent. The isobutene and the ethyl tert-butyl ether withdrawn from the column top are further separated, thus high purity isobutene and ethyl tert-butyl ether for fuel-additive are obtained.

Abstract: The invention relates to a method for processing coke oven gas, said coke oven gas containing hydrogen, wherein the coke oven gas is at least partially integrated into a method for producing dimethyl ether in conjunction with a gas containing carbon monoxide and/or carbon dioxide, whereby a DME-containing product gas is formed. At the outset of the method for the formation of dimethyl ether, a ratio of hydrogen to carbon monoxide, weighted with the carbon dioxide concentration (formula (I)), of 0.9 to 1.1 is set, wherein the DME-containing product gas is integrated into a method for converting dimethyl ether to olefins, whereby an olefin-containing product gas is formed, and wherein olefins, in particular ethylene and/or propylene, is/are separated from the olefin-containing product gas by means of separating methods.

Abstract: The invention provides for \ a method of forming methanol by combining a mixture of methane, water and carbon dioxide under reaction conditions sufficient to form a mixture of hydrogen and carbon monoxide. Hydrogen and carbon monoxide are reacted under conditions sufficient to form methanol. The molar ratio of hydrogen to carbon monoxide is at least two moles of hydrogen to one mole of carbon monoxide and the overall molar ratio between methane, water and carbon dioxide is about 3:2:1. Methane, carbon dioxide and water are bi-reformed over a catalyst. The catalyst includes a single metal, a metal oxide, a mixed catalyst of a metal and a metal oxide or a mixed catalyst of at least two metal oxides.

Abstract: Methods of cultivating autotrophic microorganisms, particularly microalgae or diatoms, in a bioreactor by entraining a culture of the microorganisms in a tenuous, gelated, thixotrophic carrier medium having nutrients therefor and moving the medium along a passage at a sufficiently slow speed to enable laminar flow which in cross section is closed and which has transparent walls through which the culture is irradiated to enable photosynthesis. The method includes effecting convective turnover of the culture and medium as they flow along the passage by differentially heating the medium laterally relative to the flow direction so as to produce a generally helical flow of the culture and medium. Also described are processing methods, both physical and chemical, performed underground e.g.

Abstract: Disclosed are methods for producing dimethyl ether (DME) from methanol and for producing DME directly from syngas, such as syngas from biomass. Also disclosed are apparatus for DME production. The disclosed processes generally function at higher temperatures with lower contact times and at lower pressures than conventional processes so as to produce higher DME yields than do conventional processes. Certain embodiments of the processes are carried out in reactors providing greater surface to volume ratios than the presently used DME reactors. Certain embodiments of the processes are carried out in systems comprising multiple microchannel reactors.

Abstract: A cooled reactor for the production of dimethyl ether by catalytic dehydration of methanol in the gas phase, the reactor having an adiabatic catalyst bed as starting zone, a moderator zone cooled by direct or indirect heat exchange, and optionally an adiabatic catalyst bed as conditioning zone. The conversion of methanol to dimethyl ether is increased and the formation of undesired by-products is decreased.

Abstract: A dialkyl or diaryl ether is produced by reacting carbon dioxide with a metal alcoholate having the formula, M(RO)x, where “M” is a Group 1, Group 2, or Group 3 metal; “x” is the valence of the metal M; “R” is a C1 to C6 lower alkyl or aryl, wherein the reaction produces a dialkyl or diaryl ether having a formula, R—O—R, and a metal carbonate having a formula M2CO3 where M is a Group 1 metal, MCO3 where M is a Group 2 metal, and M2(CO3)3 where M is a Group 3 metal. The metal carbonate may be removed by conventional means, such as filtration. The dialkyl or diaryl ether may be recovered and used as a fuel, fuel additive, propellant, or building block for other fuels or petrochemicals. In some cases the metal alcoholate is in an alcohol solution and the alcohol and metal carbonate are recycled to regenerate the metal alcoholate. A specific example of dimethyl ether production is disclosed.

Abstract: Disclosed herein is a process for monetization of natural gas by producing fuel grade dimethyl ether (DME). The process includes three reactive stages with the first reactive stage being the conversion of natural gas into syngas, the second reactive stage being the conversion of syngas into crude methanol and the third reactive stage being the production of fuel grade dimethyl ether. The management and optimization of the water and steam circuits is important to maintain net overall system efficiency and mitigation of any liquid effluents.

Abstract: A system or method for producing gasoline or dimethyl ether from natural gas via methanol includes: steam-reforming natural gas to generate reformed gas; synthesizing methanol from the reformed gas; synthesizing gasoline or dimethyl ether from the methanol; and at least one is selected from the group consisting of: pre-reforming natural gas prior to the steam-reforming; recovering carbon dioxide from flue gas generated in the steam-reforming; and preheating combustion air to be supplied to the steam-reforming by using synthesis heat generated in the synthesis of gasoline or dimethyl ether. In addition, an overall energy balance of the system is constructed by using heat recovery from flue gas generated in the steam-reforming, heat recovery from the reformed gas, synthesis heat generated in the synthesis of methanol, synthesis heat generated in the synthesis of gasoline or DME, and heat recovered in the pre-reforming, carbon dioxide recovering, or air preheating, respectively if selected.

Abstract: A process produces dimethyl ether (DME) from methanol (MeOH). The process includes charging a feed mixture consisting of raw MeOH and a process-internally obtained return flow substantially consisting of unconverted MeOH and reaction water to an MeOH column. The feed mixture is evaporated in the MeOH column to form a first distillate substantially consisting of vaporous MeOH. The first distillate is supplied to a reactor and the MeOH is converted to DME by splitting off water in the reactor so as to form a reaction mixture. The reaction mixture is withdrawn from the reactor, charged to a mixture column and separated into a bottom product substantially consisting of water and a second distillate substantially consisting of DME and MeOH. The second distillate is separated in a DME column into a third distillate substantially consisting of DME, a bottom product consisting essentially of water-poor MeOH, and uncondensable gases discharged overhead.

Abstract: A process is disclosed for producing of diethyl ether by dehydrating ethanol in the presence of an inventive catalyst. A preferred catalyst achieves high conversions of ethanol and high selectivites to diethyl ether. The diethyl ether may be used as a solvent, fuel additive, or fuel.

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 is a method for making dimethyl ether by reactive distillation. The method provides a reactive distillation tower with a top, a bottom, and rectification, reaction and stripping zones defined therein. The top of the reactive distillation tower is retained at 25° C. to 40° C. while the bottom of the reactive distillation tower is retained at 84.6° C. to 170° C. Each of the rectification, reaction and stripping zones includes several sieving trays. The reaction zone of the reactive distillation tower is filled with catalyst. The pressure in the reactive distillation tower is lower than 8.0 bars. Methanol is introduced into the reactive distillation tower so that the methanol travels from the reaction zone toward the bottom for contact with the catalyst to provide a top stream and a bottom stream. The top stream includes dimethyl ether. The bottom stream includes water and a remaining portion of the methanol. Finally, the dimethyl ether is collected in the top of the reactive distillation tower.

Abstract: The present invention discloses a system for converting methanol or synthesis gas to liquid hydrocarbons with comparable energy content to gasoline within a mixed bed single reactor or double reactor systems. Varying catalyst composition and temperature profiles allow for significant tailoring of reaction conditions to the specific feedstocks or the desired products.

Abstract: A process for producing of diethyl ether by hydrogenating acetic acid in the presence of a catalyst comprising a first metal on an acidic support, preferably a zeolite support. A preferred catalyst comprises platinum and tin on an acidic support. Selectivities to diethyl ether of at least 60% may be achieved.

Abstract: A method for producing methanol from a methane source such as methane from natural (shale) gas by first reacting one equivalent of methane with oxygen from the air to result in complete combustion to produce carbon dioxide and water in a molar ratio of 1:2; then conducting a bi-reforming process with a mixture of methane: carbon dioxide:water having a ratio of 3:1:2 to produce metgas, a mixture of hydrogen and carbon monoxide having a molar ratio of 2:1 to 2.1:1; and finally converting metgas exclusively to methanol. The thus produced methanol can be dehydrated to form dimethyl ether, with water produced being recycled back to the bi-reforming process, if necessary.

Abstract: A dual-bed catalytic distillation tower has a catalytic column having an upper catalytic bed filled with low temperature dehydration catalysts and a lower catalytic bed filled with high temperature dehydration catalysts. When using the dual-bed catalytic distillation tower, the feeding may be fed to the tower at the top of the upper catalytic bed, between the upper and lower catalytic beds, or at the bottom of the lower catalytic bed for dehydration to obtain DME. The dual-bed catalytic distillation tower has the advantage of flexible set-up depending on various feedings such as anhydrous or crude methanol and on different grades of DME to be obtained.

Abstract: A dual-bed catalytic distillation tower has a catalytic column having an upper catalytic bed filled with low temperature dehydration catalysts and a lower catalytic bed filled with high temperature dehydration catalysts. When using the dual-bed catalytic distillation tower, the feed may be fed to the tower at the top of the upper catalytic bed, between the upper and lower catalytic beds, or at the bottom of the lower catalytic bed for dehydration to obtain DME. The dual-bed catalytic distillation tower has the advantage of flexible set up depending on various feeds, such as anhydrous or crude methanol and on different grades of DME to be obtained.

Abstract: Disclosed is a process for producing dimethyl ether from methanol, which is characterized in that the absorbing liquid used in said absorbing column is the bottom liquid of DME-fractionating column and/or bottom waste water of the methanol-recovering column. Said process can significantly reduce energy consumption of the apparatus.

Abstract: A solid material is subjected to surface treatment by chemically bonding onto a surface of the solid material a stabilized monofunctional silanol represented by R1R2R3SiOH. R1, R2 and R3 may be the same or different, and each represent a substituent group independently selected from a substituted or unsubstituted, monovalent hydrocarbon group having from 1 to 40 carbon atoms or a substituted or unsubstituted, monovalent heterocyclic group having from 1 to 100 carbon atoms. The monofunctional silanol has a dehydrative self-condensation rate lower than triethylsilanol.

Abstract: A catalyst and process for synthesis of dimethyl ether from synthesis gas are disclosed. The catalyst and process allow dimethyl ether synthesis at low pressures (below 20 bars) at a conversion rate close to the expected equilibrium rate. The catalyst is a combination of a methanol synthesis catalyst and a methanol dehydration catalyst, wherein the dehydration catalyst is a mixture of dehydration agents which allow optimum production of dimethyl ether.

Abstract: Catalysts and methods for their manufacture and use for the synthesis of dimethyl ether from syngas are disclosed. The catalysts comprise ZnO, CuO, ZrO2, alumina and one or more of boron oxide, tantalum oxide, phosphorus oxide and niobium oxide. The catalysts may also comprise ceria. The catalysts described herein are able to synthesize dimethyl ether directly from synthesis gas, including synthesis gas that is rich in carbon monoxide.

Abstract: A catalytic process is taught for non-oxidative alkylation of organic compounds, comprising alcohols, alkanes, glycols, ethers, aldehydes, ketones, carboxylic acids, esters, amines, thiols or phosphines, by alkyl groups produced from alcohols or glycols, forming products comprising ethers and other higher molecular weight alkylated compounds. The process is conducted at a reflux temperature below 200° C. in the presence of an acid, alkali or neutral salt dehydrating agent comprising sulfuric acid, phosphoric acid or their salts, lime or anhydrous calcium sulfate in the absence of zero valent metals and air. Specifically, this catalytic process converts ethanol to ethyl butyl ethers, ethyl hexyl ethers and dibutyl ethers or oxygenated gasoline as well as amines comprising n-butyl amine plus butanol to dibutyl amine and butyl hexyl amines at ambient pressure.

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: A method and an apparatus for producing gasoline and hydrogen from methanol are disclosed. First, methanol is supplied to a first catalyst layer located in a reaction tube arranged in a reactor via a first methanol supply path to synthesize gasoline from the methanol. At the same time, methanol is supplied to a second catalyst layer located on the outer periphery of the reaction tube provided within the reactor from a second supply path, which serves as a methanol supply path, to generate hydrogen from the methanol. Heat generated in the first catalyst layer is conducted to the second catalyst layer through the reaction tube to heat the second catalyst layer to a predetermined temperature.

Abstract: The present invention further contemplates a process for making a dialkyl ether composition comprising two or more ethers of the formula R1—O—R2. The present invention further contemplates a process for making a dialkyl ether composition starting from a first reaction product comprising 1-butanol. The invention further contemplates a dialkyl ether composition comprising two or more ethers of the formula R1—O—R2, where each R1 and R2 can independently be any carbon chain length, saturated or unsaturated; branched or straight-chain, of between C2 and C10; specifically between C4 and C10; more specifically between C4 and C6; more specifically C6; more specifically 04.

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: Provided is a process for the production of dimethyl ether. The process improves the effectiveness of the production of dimethyl ether. Especially, the process can be combined with processes for the production of methanol.

Abstract: Process for the preparation of dimethyl ether comprising the steps of: a) providing a methanol containing feed stock; b) introducing the feed stock into a reaction zone within a gas cooled dimethyl ether reactor and passing the feed stock through the reaction zone; c) introducing a cooling gas stream into a cooling space within the gas cooled dimethyl ether reactor; d) reacting the feed stock in the reaction zone in presence of a catalyst being active in the dehydration of methanol to dimethyl ether to obtain a reactor effluent comprising dimethyl ether.

Abstract: The present invention provides a fluidized catalytic process for production of dimethyl ether from methanol, wherein said process is carried out in a reactor in which the catalyst is in a fluidized state. Said process comprises the following steps of (1) feeding the methanol feedstock via two or more locations selected from the bottom, lower part, middle part and upper part of the reactor, contacting with the catalyst for preparation of dimethyl ether by methanol dehydration, carrying out the reaction of preparing dimethyl ether by methanol dehydration to obtain the reaction stream, separating said reaction stream to obtain a coked catalyst and a crude product primarily containing the target product, i.e. dimethyl ether; (2) totally or partially feeding the coked catalyst obtained in step (1) into a regenerator in a continuous or batch manner for regeneration via coke-burning, the regenerated catalyst being directly recycled to step (1) after being totally or partially cooled.

Abstract: Disclosed is a method for making dimethyl ether by reactive distillation. The method provides a reactive distillation tower with a top, a bottom, and rectification, reaction and stripping zones defined therein. The top of the reactive distillation tower is retained at 25° C. to 40° C. while the bottom of the reactive distillation tower is retained at 84.6° C. to 170° C. Each of the rectification, reaction and stripping zones includes several sieving trays. The reaction zone of the reactive distillation tower is filled with catalyst. The pressure in the reactive distillation tower is lower than 8.0 bars. Methanol is introduced into the reactive distillation tower so that the methanol travels from the reaction zone toward the bottom for contact with the catalyst to provide a top stream and a bottom stream. The top stream includes dimethyl ether. The bottom stream includes water and a remaining portion of the methanol. Finally, the dimethyl ether is collected in the top of the reactive distillation tower.

Abstract: A method of producing dimethyl ether by catalytic dehydration of crude methanol as feedstock in the gas phase includes providing the crude methanol from methanol synthesis, where the crude methanol having a total content of carbonyl compounds of not more than 100 wt-ppm, calculated, as mass equivalents of acetone. The crude methanol is evaporated, and the reaction temperature and reaction pressure are adjusted. A reactor filled with dehydration catalyst is charged with the evaporated crude methanol with a defined space velocity. A gaseous product mixture comprising dimethyl ether, non-reacted methanol and water is discharged. Cooling, partial condensation and separation of the gaseous product mixture are carried out so as to provide gaseous dimethyl ether, liquid water and methanol as products, and the methanol is recirculated.

Abstract: The present disclosure relates to methods for converting biomass-derived hydrocarbon streams into products suitable for use as fuel additives. These methods involve the acidic condensation of hydrocarbon monofunctional alcohols comprising five or six carbon atoms to form ether condensation products containing at least ten carbon atoms. The oxygenated condensation products can be separated from un-reacted alcohols and gasoline range hydrocarbons to provide an oxygenated fuel additive that may be mixed with a diesel or kerosene-type liquid hydrocarbon fuel to provide an improved fuel that may have an increased cetane number, decreased emissions of environmental pollutants during combustion, or both.

Abstract: A method of reacting compounds can include directing a liquid into a helical constrained flow (37) having an inner circumferential flow surface and an outer circumferential flow surface. The helical constrained flow (37) can be formed around an axial interior volume (38). At least a portion of the helical constrained flow can be exposed to a sparging portion (35) to allow a fluid to be sparged into the liquid along the helical constrained flow (37). The fluid reactant can be sparged through the helical constrained flow so as to form a fluid product.

Abstract: A dual-bed catalytic distillation tower has a catalytic column from the top down having an upper catalytic bed filled with low temperature dehydration catalysts and a lower catalytic bed filled with high temperature dehydration catalysts. When using the dual-bed catalytic distillation tower, the feeding may be fed to the tower from the top of the upper catalytic bed, between the upper and lower catalytic beds or the bottom of the lower catalytic bed for dehydration to obtain DME. The dual-bed catalytic distillation tower has the advantage of flexible set up depending on various feedings such as anhydrous or crude methanol and on different grade of DME to be obtained.

Abstract: A process produces dimethyl ether (DME) from methanol (MeOH). The process includes charging a feed mixture consisting of raw MeOH and a process-internally obtained return flow substantially consisting of unconverted MeOH and reaction water to an MeOH column. The feed mixture is evaporated in the MeOH column to form a first distillate substantially consisting of vaporous MeOH. The first distillate is supplied to a reactor and the MeOH is converted to DME by splitting off water in the reactor so as to form a reaction mixture. The reaction mixture is withdrawn from the reactor, charged to a mixture column and separated into a bottom product substantially consisting of water and a second distillate substantially consisting of DME and MeOH. The second distillate is separated in a DME column into a third distillate substantially consisting of DME, a bottom product consisting essentially of water-poor MeOH, and uncondensable gases discharged overhead.

Abstract: The present inventions are (A) a solvent comprising at least one cycloalkyl alkyl ether (1) represented by the general formula: R1—O—R2 (wherein R1 is cyclopentyl or the like; and R2 is C1-10 alkyl or the like); (B) a method of preparations the ethers (1) characterized by reacting an alicyclic olefin with an alcohol in the presence of an acid ion-exchange resin having a water content of 5 wt % or less. The solvent is useful as cleaning solvent for electronic components, precision machinery components or the like, reaction solvent using various chemical reactions, extraction solvent for extracting objective organic substances, solvent or remover for electronic and electrical materials, and so on. The process enables industrially advantageous production of the objective cycloalkyl alkyl ethers (1).

Abstract: The invention relates to a chemical reactor with a nanometric superstructure, comprising at least one member wherein at least one reaction chamber is arranged, and said reaction chamber being filled at least partially with a high specific surface area material having a specific surface area greater than 5 m2/g, and characterised in that said high specific surface area material is selected from nanotubes or nanofibres. These nanotubes or nanofibres are preferably selected in the group consisting of carbon nanofibres or nanotubes, ?-SiC nanofibres or nanotubes, TiO2 nanofibres or nanotubes. They may be deposited on an intermediate structure selected in the group consisting of glass fibres, carbon fibres, SiC foams, carbon foams, alveolar ?-SiC foams, said intermediate structure filling the reaction chamber of said reactor at least partially.

Abstract: A process for producing of diethyl ether by hydrogenating acetic acid in the presence of a catalyst comprising a first metal on an acidic support, preferably a zeolite support. A preferred catalyst comprises platinum and tin on an acidic support. Selectivities to diethyl ether of at least 80% may be achieved.