Abstract: In a process for producing fatty acid methyl ester (FAME) from fats or oils by transesterification with methanol in the presence of an alkaline catalyst in at least two reaction stages traversed in succession, each consisting of a stirred-tank reactor and a downstream separator, a phase containing FAME and a phase containing glycerol are generated, which are separated in the separator, wherein the phase containing FAME is recirculated into the stirred-tank reactor of the next succeeding reaction stage and the phase containing glycerol is recirculated into the stirred-tank reactor of the first reaction stage, and the crude FAME withdrawn from the separator of the last reaction stage is transferred into a separator and the FAME withdrawn is dried.

Abstract: A method for producing methanol from a synthesis gas containing hydrogen and carbon oxides with a high content of inert components includes passing the synthesis gas through a synthesis reactor so as to catalytically convert a part of the carbon oxides to methanol. The methanol is separated from the obtained mixture from the reactor. The mixture liberated from methanol is separated into a cycle stream and a purge stream. The cycle stream is recirculated so as to form a synthesis circle and combined with a fresh gas stream including hydrogen and carbon oxides before being charged into the synthesis reactor. The purge stream is supplied to a secondary reactor so as to catalytically convert a further part of the hydrogen and carbon oxides to methanol. Further methanol is separated the obtained mixture including synthesis gas, inert components and methanol vapor.

Abstract: For producing synthetic fuels, an educt mixture containing steam and oxygenates, such as methanol and/or dimethyl ether, is converted to olefins on a catalyst in a first process stage, and this olefin mixture then is divided in a separating means into a stream rich in C1-C4 hydrocarbons and a stream rich in C5+ hydrcarbons. The stream rich in C5+ hydrocarbons is divided into a stream rich in C5 and C6 hydrocarbons and a stream rich in C7+ hydrocarbons, wherein the stream rich in C5 and C6 hydrocarbons is at least partly subjected to an etherification with methanol. The ethers thus obtained are admixed to the gasoline product stream.

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: With a method configured to generate process gas that contains hydrogen sulfide and sulfur dioxide for the Claus process, hydrogen-sulfide containing feed gas is burnt with pure oxygen by means of several burners opening out into a combustion chamber wherein the pure oxygen is fed into the combustion chamber through a central tube each, the feed gas through a tube arranged coaxially around the central tube and inert gas as purge gas via an annular duct coaxially surrounding the feed gas tube. A favorable option of the method consists in the use of CO2 re-claimed by desorption of laden methanol as purge gas.

Abstract: A method for volatile compound (VC) mitigation in a syngas production process is provided. This method includes providing a hydrocarbon reforming syngas production plant, this plant includes a reformer system comprising a primary fuel and oxidant stream, where part of this system is at low pressure, a steam inlet stream, and a primary combustion system for providing heat to the reformer system and producing a reformer flue gas stream, and a gaseous vent stream mainly composed of water and containing VC. This method also includes introducing at least a portion of the vent stream into one or more of the following: the primary fuel and oxidant stream; the steam inlet stream; the reformer flue gas stream.

Abstract: A process and a plant for producing C2-C4 olefins, in particular propylene, from an educt mixture containing steam as well as methanol vapor and/or dimethyl ether vapor.

Abstract: In a process for obtaining CO2, desulfurized natural gas or gas which accompanies mineral oil is reformed autothermally with addition of oxygenous gas at a temperature of from 900 to 1200° C. and a pressure of from 40 to 100 bar (a) by partial catalytic oxidation to give a crude synthesis gas, and then converted catalytically to H2 and CO2 at a temperature of from 75 to 110 DEG C. and a pressure of from 50 to 75 bar (a) of CO, CO2 is scrubbed out of the synthesis gas obtained with methanol at a pressure of from 15 to 100 bar (a) and a temperature of from +10 to ?80° C., and the absorbed CO2 is recovered by decompression. A further possible use of the process consists in converting the recovered CO2 to the supercritical state.

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 for producing a product containing C3H6 and C2H4 includes simultaneous conversion of MeOH and EtOH in an adiabatic sequentially operated reactor containing a plurality of reaction stages. Each of the plurality of reaction stages of the reactor is provided with a fixed bed of a form-selective catalyst. A gaseous feed stream including MeOH, DME and H2O is charged to at least a first of the reaction stages of the reactor with a temperature in a range of 300 to 600° C. at a pressure in a range of 0.1 to 20 bar[a]. EtOH is fed into at least, one of the reaction stages of the reactor.

Abstract: Disclosed herein is a process and a plant for recovering ammonia from a mixture including ammonia, acid gas containing H2S and/or CO2 and low-boiling water-soluble organic components. To avoid an enrichment of volatile organic compounds in the acid gas absorber, a partial stream of the liquid phase is withdrawn from an acid gas absorber and processed such that gaseous ammonia with a reduced content of volatile organic components is obtained, which is recirculated into the acid gas absorber.

Abstract: A process for producing biodiesel from fats, oils or split fatty acids containing steryl glycosides, wherein the fats, oils or split fatty acids are reacted with short-chain alkanols in the presence of a catalyst by transesterification or esterification to a fatty acid alkyl ester to obtain a first product stream, includes washing the first product stream with water in a washing device, so as to form a suspension layer on a phase boundary layer between a heavy phase rich in water and the first light phase rich in the fatty acid alkyl ester. The suspension layer is treated by introducing kinetic energy. A second product stream is withdrawn from the first light phase and intensively mixed with water to obtain a third product stream. A mechanical separation is performed on the third product stream to provide a fourth product stream and a fifth product stream. The fifth product stream is withdrawn as a heavy phase that is enriched in the steryl glycosides.

Abstract: For producing methanol from a synthesis gas containing hydrogen and carbon oxides the synthesis gas is passed through a first, water-cooled reactor in which a part of the carbon oxides is catalytically converted to methanol. The resulting mixture containing synthesis gas and methanol vapor is supplied to a second, gas-cooled reactor in which a further part of the carbon oxides is converted to methanol. Subsequently, methanol is separated from the synthesis gas, and synthesis gas is recirculated to the first reactor. The cooling gas flows through the second reactor cocurrent to the mixture withdrawn from the first reactor.

Abstract: For producing methanol from a synthesis gas containing hydrogen and carbon oxides the synthesis gas is passed through a first, preferably water-cooled reactor in which a part of the carbon oxides is catalytically converted to methanol, and the resulting mixture containing synthesis gas and methanol vapor is supplied to a second, preferably gas-cooled reactor in which a further part of the carbon oxides is converted to methanol. The mixture withdrawn from the first reactor is guided through a gas/gas heat exchanger in which the mixture is cooled to a temperature below its dew point. Subsequently, methanol is separated from the gas stream in a methanol separator and withdrawn, while the remaining gas stream is supplied to the second reactor.

Abstract: A process for recovering solid reaction products during partial oxidation of hydrocarbons in a liquid solvent as a reaction medium by multi-stage evaporative crystallization includes determining a final temperature of the multi-stage evaporative crystallization based on a melting point of the solvent. The pressure and temperature of the solvent is reduced in steps via successive crystallization stages until the final temperature is reached. Each of the crystallization stages includes a compressor configured to perform the reducing of the pressure and to withdraw vapors formed. The vapors from the compressor of a lower expansion pressure crystallization stage are introduced into a vapor discharge conduit of a next successive higher expansion pressure crystallization stage upstream of the compressor of the higher expansion pressure crystallization stage.

Abstract: Upon cooling to 15 to 45° C., a process for the treatment of raw product gas generated by pressure gasification of solid fuels comprises the removal of HCN and NH3 in a preliminary stage, of H2S and COS and possibly other sulfur-containing compounds in a first stage and of CO2 in a second stage by physisorption with cold oxygenate, and the pure product gas is supplied to the direct reduction of iron ore as reduction gas and/or as fuel gas. An improvement of the process consists in that recycle gas loaded with CO2 and steam, which is branched off from the circuit of the recycle gas of the direct reduction of iron ore, is admixed to the desulfurized product gas upon removal of the steam contained therein.

Abstract: In the production of methanol from a synthesis gas containing hydrogen and carbon oxides, the synthesis gas is passed through a first, preferably water-cooled reactor, in which a part of the carbon oxides is catalytically converted to methanol. The obtained mixture containing synthesis gas and methanol vapor is supplied to a second, preferably gas-cooled reactor, in which a further part of the carbon oxides is converted to methanol. Subsequently, methanol is separated from the synthesis gas, and the synthesis gas is recirculated to the first reactor. To achieve a maximum methanol yield even with an aged catalyst, a partial stream of the synthesis gas is guided past the first reactor and introduced directly into the second reactor.

Abstract: Method for producing fatty alcohols includes splitting vegetable oils and animal fats under pressure into fatty acids and glycerol in counterflow to steam. The reaction product is physically separated into fatty acids and sweet water containing glycerol. The fatty acids are subjected to a distillation, and the separated fatty acid fraction is mixed together with fatty alcohol at 230 to 270° C. and atmospheric pressure. The wax esters obtained by esterification are hydrogenated to fatty alcohols by adding hydrogen on a fixed-bed catalyst, and the reaction product is separated into fatty alcohols and hydrogen. The wax esters are hydrogenated on a fixed bed of uniformly shaped catalyst bodies produced by extrusion, which consist of the main components copper and copper-chromium oxide and the secondary components zinc, aluminum, iron, silicon and alkaline earth elements, at 180 to 220° C. and 70 to 100 bar(a).

Abstract: From the CO2-containing stream of process gas obtained in a process for the treatment of a CO2-containing stream of process gas, which is obtained in the production of pure synthesis gas from raw gas in the partial oxidation of heavy oils, petroleum coke or wastes, or in the gasification of coal, or when processing natural gas or accompanying natural gas, CO2 is removed physisorptively or chemisorptively, and the solvent loaded with CO2 is expanded to a lower pressure for the desorption of CO2. In order to generate CO2 as pure as possible, the contaminated CO2 is condensed to at least 60 bar[a] or below its critical temperature to at least 70 bar[a], and the impurities contained in the liquid CO2 are removed by stripping with gaseous CO2 guided in counterflow.

Abstract: Method for producing C3H5(OH)3 and at least one of fatty acid methyl ester (FAME) and fatty acid ethyl ester (FAEE) includes mixing vegetable oils and animal fats, at least one of CH3OH and C2H5OH and at least one first catalyst to transesterify a portion of triglycerides and provide a first mixture. The first mixture is separated, with a first light phase being withdrawn and fed into a second mixer where it is mixed with at least one second catalyst to transesterify a further portion of the triglycerides to provide a second mixture. The second mixture is separated, with a second light phase being withdrawn and mixed with soapless C2H5(OH)3 to provide a dispersion which is separated by density difference. A phase containing at least one of raw FAME and raw FAEE is mixed with an aqueous acid, washed with water, with the water being expelled to provide FAME and FAEE product.