Thyssenkrupp Industrial Solutions Ag

Evonik Degussa Gmbh

Thyssen Krupp Ag

Evonik Operations Gmbh

Niels Bredemeyer

Bernd Jaeger

Norbert Ullrich

Wolfgang Wöll

Bärbel Kolbe

Marc Brendel

Maik Bernhard

Willi Hofen

Peter Woltering

Markus Oles

Johannes Kowoll

David Bolz

Frank Funck

Dirk Hoormann

Gregor Polcyn

Ralph Kleinschmidt

Peter Schmöle

Bernd Langanke

Jens Wagner

Reinhold Achatz

Dmitri Donst

Philipp Hofmann

Peter Toros

Peter Porscha

Wolfram Stolp

Manfred Bärz

Christoph Roosen

Christoph Meißner

Jürgen Schemel

Stephan Köberle

Michael Dopfer

Johannes Völkl

Dana Pfenning

Christoph Meissner

Stephan Koberle

Peter Schmoele

Johannes Voelkl

Stephan KÖBERLE

Gregor Damian Polcyn

The invention relates to a plant complex for steel production comprising a blast furnace for producing pig iron, a converter steel mill for producing crude steel and a gas-conducting system for gases that occur when producing the pig iron and/or producing the crude steel. According to the invention, the plant complex additionally has a chemical plant or biotechnological plant, connected to the gas-conducting system, and also energy storage for covering at least part of the electricity demand of the plant complex. Also the subject of the invention is a method for operating the plant complex.

Combined system for producing steel and method for operating the combined system

During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20&#xb0; C. to 50&#xb0; C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60&#xb0; C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20&#xb0; C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load.

Process for the epoxidation of propene

Propene is continuously reacted with hydrogen peroxide in a tube bundle reactor comprising a multitude of parallel reaction tubes in the presence of a titanium silicalite catalyst arranged as a fixed bed in the reaction tubes. A cooling jacket encloses the reaction tubes, which has a feed point for cooling medium near the entry of the reaction tubes, a withdrawal point for cooling medium near the end of the reaction tubes and at least one additional withdrawal point upstream of the withdrawal point near the end of the reaction tubes. Cooling medium is fed to the feed point for cooling medium, a part of the cooling medium is withdrawn at the at least one additional withdrawal point and the remainder exits at the withdrawal point near the end of the reaction tubes.

Process and reactor for the epoxidation of propene

Flow type electrochemical cells are disclosed. The electrochemical cell has an anode half-cell, a cathode half-cell, and permeable separating layer. The half-cells are bounded by side elements. Respective porous electrodes are housed in the half-cells. The permeable separating layer is disposed between the anode half-cell and the cathode half-cell. An electrolyte region connected to an electrolyte feed and an electrolyte outflow region connected to an electrolyte drain are further provided. An electrolyte inflow region and an electrolyte outflow region are disposed on opposite sides of the porous electrodes such that inflowing electrolyte flows through the porous electrode perpendicularly to the permeable separating layer.

Flow-type electrochemical cell

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Waltrop, Germany

Niels Bredemeyer