Metallgesellschaft Aktiengesellschaft

Lurgi Gmbh

Rohm Gmbh Chemische Fabrik

Air Liquide Global E&c Solutions Germany Gmbh

Mg Technologies Ag

Deggendorfer Werft Und Eisenbau Gmbh

Lurgi Ag

Henning Buchold

Martin Rothaemel

Hans-Martin Stonner

Ulrich Wagner

Jürgen Eberhardt

Hans-Jörg Wölk

Rudolf Boensch

Walter Laber

Helmut Klein

Eberhard Julius Schlichting

Holger Dropsch

Otto-Ludwig Garkisch

Helmut Saft

Walter Boll

Friedrich-Wilhelm Moller

Harald Koempel

Sven Pohl

Friedrich Gutlhuber

Thomas Renner

Peter Mitschke

Harald Kömpel

Friedrich Guetlhuber

Andreas Ochs

Friedrich-Wilhelm Moeller

Uwe Finck

Andreas Glasmacher

Fritz-J Urgen G Artner

Gert Mallok

Hans-Martin St Onner

Gerd Mallok

Fritz-Jurgen Gartner

Joerg Schroeppel

Uwe Fincke

In producing C-Colefins, in particular propylene, from an educt mixture containing steam and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted in a reactor on a catalyst to a reaction mixture comprising low-molecular olefins and gasoline hydrocarbons, which in a first separating device is separated into a mixture rich in Colefins, a mixture rich in Cgasoline hydrocarbons, and an aqueous phase. To increase the yield of propylene the mixture rich in Cgasoline hydrocarbons is supplied to a second separating device, in which the aromatics contained in the mixture are separated. The residual stream largely free from aromatics is at least partly recirculated to the reactor.

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A process and a plant for producing C-Colefins, in particular propylene, from an educt mixture containing steam as well as methanol vapor and/or dimethyl ether vapor. The educt mixture is reacted in at least one first reactor on a granular, form-selective zeolite catalyst to obtain a reaction mixture including low-molecular olefins and gasoline hydrocarbons, which in a first separating device is separated into a mixture rich in C-Colefins, a mixture rich in Cgasoline hydrocarbons, and an aqueous phase, wherein the mixture rich in gasoline hydrocarbons is mixed with an inert medium, the mixture thus obtained is reacted in at least one second reactor on a granular zeolite catalyst to obtain a product mixture including C-Colefins, and this product mixture is recirculated to the first separating device, and wherein the mixture rich in Cgasoline hydrocarbons is separated in a second separating device into a product stream containing C-Chydrocarbons and a product stream containing Chydrocarbons, before being supplied to the second reactor, and only the product stream containing Chydrocarbons is supplied to the second reactor, whereas the product stream containing C-Chydrocarbons together with the educt mixture is supplied to the at least one first reactor.

Process and plant for producing C2-C4 olefins from methanol and/or dimethyl ether with increased yield

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&#xb0; 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.

In a process for producing synthetic fuels from an educt mixture containing hydrogen and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted on a catalyst in a first process stage to obtain a hydrocarbon product containing olefins with preferably 2 to 8 carbon atoms. In a second process stage the hydrocarbon product is oligomerized to long-chain olefins, from which gasoline and Diesel products are obtained. The hydrocarbon product obtained in the first process stage is separated into a liquid phase and a gaseous phase. The gaseous phase is supplied to the second process stage. The liquid phase is separated into a mixture rich in Chydrocarbons and a mixture containing Chydrocarbons and aromatics. The mixture rich in Chydrocarbons is supplied to the second process stage. The mixture containing Chydrocarbons &#x2212;+ and aromatics can be admixed to the gasoline product for quality improvement.

Process and plant for producing synthetic fuels

Method for producing CH(OH)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 CHOH and CHOH 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 CH(OH)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.

Method for producing fatty acid methyl esters or fatty acid ethyl esters

The invention relates to a method for the production of monomer organic carbonates from a mixture of organic carbonates and carbamates which are obtained by reacting urea, substituted urea, a salt or ester of carbamide acid or one of the N-substituted derivatives thereof with a polyalkylene glycol, polyester-polyol or a polyether-polyol of general formula (I), wherein R represents a linear or branched alkylene group having 2-12 carbon atoms and n represents a number between 2 and 20, or with a completely or partially hydrolysed polyvinyl alcohol of general formula (II), wherein R' represents an alkyl group, an aryl group or an acyl group having 1-12 carbon atoms, p and q represent a number between 120, or with mixtures of said compounds in the presence of a catalyst facilitating the separation of ammonia and the ammonia becomes free or the amine is removed from the reaction mixture by means of a strip gas, whereby said mixture is reacted with an alcohol or a phenol whereby monomer carbonates are formed and polymer polyalcohols of formulae (I) or (II) are reformed. 

Method for the production of organic carbonates

The invention relates to a method for the production of monomer organic carbonates, wherein urea, substituted urea, a salt or an ester of carbamide acid or one of the N-substituted derivatives thereof is reacted in a first step in a polyalkylene glycol, a polyester-polyol or a polyether-polyol of general formula (I), wherein R represents a linear or branched alkylene group having 2-12 carbon atoms and n is a number between (2) and (20), or in a completely or partially hydrolysed polyvinyl alcohol of general formula (II) wherein R' represents an alkyl group, an aryl group or an acyl group having 1-12 carbon atoms, p and q are numbers between 1 and 20, or in mixtures of said compounds in the presence of a catalyst facilitating the separation of ammonia in order to form a mixture containing carbonates and carbamates, the ammonia becomes free or the amine is removed form the reaction mixture by means of a strip gas. In a second reaction step (transesterification), the mixture containing the carbonates and carbamates is reacted with a monomer alcohol or a phenol whereby monomer carbonates are formed and polymer polyalcohols of formulae (I) or (II) are reformed.HO&#x2014;ROH&#x2003;&#x2003;(I)

In the presence of a catalyst, at least one isoparaffin having 4 to 6 C atoms per molecule is reacted with at least one olefin having 2 to 6 C atoms per molecule in a liquid phase to obtain a product containing alkylate, a suspension containing isoparaffin and a granular zeolite catalyst being supplied to the upper region of a reaction column. Below the point where the catalyst-containing suspension is supplied, an isoparaffin-olefin mixture is introduced into the reaction column, the temperatures in the reaction column being maintained in the range from 50 to 120&#xb0; C. From the bottom region of the reaction column a product mixture containing alkylate is withdrawn, and in a separation by distillation alkylate product is recovered therefrom. Preferably, isoparaffin and catalyst are recovered from the separation by distillation and at least partly recirculated to the upper region of the reaction column.

Method for the catalytically reacting of isoparaffins with olefins to form alkylates

A liquid starting mixture contains at least one fatty acid having 6 to 30 carbon atoms per molecule and per mole of fatty acid comprises 1.0 to 1.5 moles of fatty alcohol having 6 to 30 carbon atoms. An intermediate product which contains at least 50% by weight is prepared from the liquid starting product, which is passed at temperatures from about 120 to 320.degree. C. through a stirring zone and is sprayed and water vapor is removed. The intermediate product is hydrogenated to produce a raw product, which contains at least 75% by weight fatty alcohol. A partial stream which contains fatty alcohol is removed from the raw product and is added to the liquid starting mixture. The intermediate product which contains at least 50% by weight wax ester can be prepared without use of a solids containing catalyst.

Process for preparing wax esters and hydrogenation of wax esters to

A process is disclosed for enzymatically degumming vegetable oil where the vegetable oil to be degummed is adjusted to a pH from 3 to 6 and is mixed with an aqueous enzyme solution, which contains one of the enzymes phospholipase A1, A2 or B. In a degumming reactor the enzymes are permitted to act on the oil at temperatures from 20.degree. to 90.degree. C. with stirring. Before or after a separation of the degummed oil a separation promoter or a solubilizer is added at temperatures from 20.degree. to 90.degree. C. to the liquid which has been withdrawn from the degumming reactor. A substantially sludgefree solution, which contains used enymes, is thus recovered and is recycled at least in part to a location preceding the degumming rector. The content of recycled used enzymes in the total amount of the enzymes dispersed in the oil is at least 10%.

Process for enzymatically degumming vegetable oil

The wax ester is prepared from a liquid mixture which contains at least one fatty acid and at least one fatty alcohol. The fatty acid and the fatty alcohol contain 6 to 30 carbon atoms per molecule. The mixture is agitated at temperatures in the range from about 105.degree.to 300.degree. C. and is sprayed into a spraying zone. An atmosphere which contains water vapor is formed in the spraying zone and is removed at least in part. The mixture of fatty acid and fatty alcohol may be agitated in at least one stirred vessel preceding the spraying zone. A catalyst is preferably not added.

Process of preparing wax ester

Fatty acids and/or fatty acid derivatives as well as hydrogen, fresh catalyst and a dispersion which contains used catalyst are supplied to the hydrogenating means, which are operated at temperatures in the range from 100.degree. to 400.degree. C. and under pressures in the range from 20 to 400 bars to produce a product stream, which contains fatty alcohols and used catalyst. A part of the product stream is circulated. A first partial stream Is withdrawn at a controllable rate from the circulating stream and is passed through a separator. A product which is rich in fatty alcohol and a dispersion which contains used catalyst are separately delivered by the separator. The dispersion is recycled to the hydrogenating means. A second partial stream is withdrawn at a controllable rate from the circulating product stream. Used catalyst is separated from the second partial stream and is removed from the process. The rate at which used catalyst is fed to the hydrogenating means can be increased in that the rate of the second partial stream is decreased.

Process of controlling the rate at which used catalyst is recycled to

A process for producing styrene by the dehydrogenation of ethyl benzene whereby the ethyl benzene in a mixture with steam is introduced into a tubular reactor, the tubes of which are heated by molten salts. The structural parameters of this process are the tube diameter which should be 20 to 35 millimeters, the temperature of the molten salts which should be 580.degree. to 660.degree. C. and at most 20.degree. C. higher than the reaction temperature at the catalyst and the weight ratio of steam to ethyl benzene of the feed stock which should be 0.5 to 1. The process saves energy and increases efficiency by reducing the steam consumption.

Process for producing styrene

The invention relates to a process of converting ethylbenzene to styrene by catalytic dehydrogenation at temperatures of about 600.degree. C. in the presence of water vapor in a tubular reactor. The heat required for the dehydrogenation is fed to the tubular reactor with a molten salt bath. The dehydrogenation is effected isothermally and in a single stage under atmospheric pressure or preferable under a subatmospheric pressure with a water vapor-ethylbenzene ratio of 1.2 to 1.5 kg of water vapor per kg of ethylbenzene. The temperature of the ethylbenzene-water-vapor mixture entering the tubular reactor is maintained 50.degree. to 100.degree. C. below the temperature of the molten salt bath.

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Hanau, Germany

Henning Buchold