Uhde Gmbh

Krupp Koppers Gmbh

Degussa Aktiengesellschaft

Krupp Uhde Gmbh

Evonik Degussa Gmbh

Thyssenkrupp Industrial Solutions Ag

Thyssenkrupp Uhde Chlorine Engineers Gmbh

Werner Pohl

Johannes Menzel

Thomas Haas

Guido Stochniol

Willi Hofen

Georg Thiele

Norbert Ullrich

Wolfgang Wöll

Adolf Linke

Rolf Wetzel

Karl Schmid

Hubertus Eickhoff

Claudia Brasse

Thomas Steinmetz

Percy Kampeis

Sami Petteri Pelkonen

Wolfgang Woell

José Berges

Manfred Gross

Gerald Moroff

Christoph Stegemann

Christoph Herwig

Simon Rittmann

Mohammadhadi Jazini

Gerhard Henssen

Bettina Lorantfy

A process for removing silicon compounds from aqueous NaCl brine includes, first, adjusting a weak brine to a pH value of less than 3 with hydrochloric acid. Iron(III) chloride or other trivalent iron ions are added to the acidified weak brine, the obtained weak brine is then continuously fed to a stirred dissolution vessel which contains undissolved salt in addition to brine. Fresh salt is charged batch-wise and intermittently to the dissolution vessel to produce strong brine. The obtained strong brine is fed to a stirred buffer vessel, the pH value in this buffer vessel being maintained at a level ranging from 5 to 8. A strong-brine flow is continuously withdrawn from the buffer vessel and filtered, and the filtrate containing the added iron and silicon is discharged. Also a system for carrying out this process is disclosed.

Removal of silicon from brine

A process for the epoxidation of olefins which includes

Process for the epoxidation of olefins

A process for the removal of CO.sub.2 and sulfur compounds from natural gas and raw synthesis gas wherein N-formylmorpholine and N-acetylmorpholine mixtures are used as the desorbent at temperatures between -20.degree. C. and +40.degree. C. at pressures of 10 to 150 bar in a scrubbing operation. The acid gases are removed from the absorbent by flashing and the regenerated absorbent is recycled to the absorbent.

Process for the removal of CO.sub.2 and sulfur compounds from industrial

In the process for purifying an aqueous MDEA-solution the formate content of the MDEA-solution circulated in a main stream between the absorber and desorber of a hydrogen sulfide wash unit for gas produced by gasification of a carbonaceous material, e.g. coal, is measured. A partial stream of MDEA-solution is withdrawn from the main stream, passed over an ion exchange medium which removes some formate present to form a partially purified partial stream and subsequently the purified partial stream is returned to the main stream. The amount of the withdrawal from the main stream is controlled so that the formate content of the main stream is maintained between 10 and 30 g/l. Only from 0.5 to 0.08% by volume need be withdrawn from the main stream to form the partial stream. The ion exchange medium can be regenerated with a hydroxide-containing solution, which is subsequently fed to an ammonia separator column of a hydrogen sulfide wash apparatus.

Process for purifying an aqueous methyldiethanolamine solution

In the process for gasification of municipal waste plastic waste material pieces of about a 20 mm piece size are compressed and heated at a pressure of from 40 to 80 bar until at a temperature of from 230.degree. to 300.degree. C. to produce an HCl-containing gas and a plastic waste material containing less than 3000 mg of HCl per kg and the HCl-containing gas produced is washed with water to produce a hydrochloric acid solution. The plastic waste material is then heated further until at a temperature of from 400.degree. to 500.degree. C. to form a plastic melt having a viscosity of less than 300 cSt, advantageously less than 50 cSt. This plastic melt is gasified at a pressure of 4 bar with oxygen in a flame reaction to form a crude gas containing a preponderant proportion of CO in relation to CO.sub.2 in a gasification chamber having a central temperature of about 1600.degree. C. The crude gas is withdrawn from the gasification reactor at a temperature of 1300.degree. to 1600.degree. C., quenched with a water spray to cool it until at a temperature of 700.degree. to 900.degree. C. and then further cooled by indirect heat transfer in a heat exchanger producing steam until at a temperature of from 220.degree. to 300.degree. C. The cooled crude gas is dedusted until a dust content of less than 20 mg/Nm.sup.3 of crude gas is reached and the dedusted gas is washed and desulfurized to form the product gas.

Process for working up municipal plastic waste materials by gasification

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Essen, Germany

Werner Pohl