Bayer Aktiengesellschaft

Rheinbraun Aktiengesellschaft

Maschinen- Und Anlagenbau Grimma Gmbh (mag)

Maschinen-und Anlagenbau Grimma Gmbh

Lanxess Deutschland Gmbh

Hans-Ulrich Dummersdorf

Helmut Waldmann

Fritz Gestermann

Kaspar Hallenberger

Franz-Rudolf Minz

Dieter Grenner

Hans-Martin Weber

Helmut Harle

J&uuml;rgen Schneider

Gerhard Moormann

Helmut Waldman

Carsten Winter, Deceased

Oliver Pfohl

Renate Winter, Heir

Helmut Kreusing

Franz-Josef Menge

Manfred Erken

Gunther Herbst

Walter Winter, Heir

Dietrich Hebecker

Dirk Von Lengerken

Heinz Dummersdorf

Hans-Joachim Muller

Helmut H&auml;rle

Alexander Przyklenk

Siegfried Janzen

In the process for working up the reaction gas consisting of chlorine, hydrogen chloride, oxygen and water vapour produced in a chlorine reactor, the reaction gas leaving the reactor is first cooled until the water of reaction and hydrogen chloride condense in the form of concentrated hydrochloric acid. The concentrated hydrochloric acid is then separated from the reaction gas in a phase separation column and discharged. The remaining reaction gas, from which the substantial proportion of the water and a proportion of the hydrogen chloride has been removed, is then post-dried in a drying tower The post-dried reaction gas consisting of chlorine, oxygen and hydrogen chloride is then compressed to 1 to 30 bar by a compressor In the subsequent stage, the compressed reaction gas is passed through a cooled chlorine recuperator wherein the chlorine is very largely liquefied. Finally, the components of the reaction gas which could not be condensed in the chlorine recuperator are at least partially returned to the reactor

Process for working up reaction gases during the oxidation HCI to chlorine

The present invention is directed to a process for simultaneously obtaining pure carbon monoxide and pure hydrogen in a steam reformer plant for hydrogen or ammonia generation, having a primary reformer, a secondary reformer and downstream thereof, a CO conversion stage. A part gas stream of the synthesis gas stream, which is discharged from the secondary reformer having a CO content of between 2 and 20 mol. % and is at a temperature of from 200 to 500.degree. C. and a pressure between 15 and 50 bar, is removed between the secondary reformer and the CO conversion stage. The part gas stream is then is cooled to a temperature below 100.degree. C., thereby condensing out the major part of the steam contained in the gas stream. The remaining raw synthesis gas stream is then guided by way of a multistage gas separation plant in which the gas components H.sub.2, residual steam, CH.sub.4, CO.sub.2 and optionally N.sub.2 are separated, either individually or together, from the CO. The separated gas components are then compressed to a pressure which exceeds the pressure in the CO conversion stage and are recombined to form a mixed gas stream. The mixed gas stream is then guided into the CO conversion stage of the steam reformer after being heated to a temperature of from 200 to 500.degree. C. The remaining pure CO fraction is removed in separate manner and may optionally, be supplied for further processing.

Process for obtaining carbon monoxide and hydrogen

In the method for the chemical reaction of gaseous educts, the educts are brought to reaction in a phase contact apparatus 1 in the presence of a catalytically active corrosive liquid. This corrosive liquid is delivered hydropneumatically in an intermittent cycle in the circuit from a sump vessel 4 connected to the lower end of the phase contact apparatus 1 to a supply vessel 9, connected to the upper end of the phase contact apparatus (delivery cycle), from which the corrosive liquid drains through the phase contact apparatus 1 and a connecting line 11 connected at its lower end and then collects in the sump vessel 4 (drainage cycle).

Method and device for delivering hot, aggressive media

In mass transfer columns, particularly in distillation and extraction columns, fluidised bed bodies are frequently used to improve mass transfer. A substantial improvement in the mass transfer rate may be achieved if asymmetrically shaped fluidised bed bodies are used, which are characterised in that their geometric center does not coincide with the center of mass, whereby the geometric center is defined as the point of intersection of the body diagonals of the smallest possible right parallelepiped completely enveloping the fluidised bed body. Typical examples of such shapes are bird's egg-shaped or drop-shaped bodies. Apart from the improvement in mass transfer, a reduction in the specific pressure drop may also be achieved with such fluidised bed bodies.

Process for mass transfer using fluidized bed bodies

In the method for the chemical reaction of gaseous educts the educts are brought to reaction in a phase contact apparatus 1 in the presence of a catalytically active corrosive liquid. This corrosive liquid is delivered hydropneumatically in an intermittent cycle in the circuit from a sump vessel 4 connected to the lower end of the phase contact apparatus 1 to a supply vessel 9, connected to the upper end of the phase contact apparatus (delivery cycle), from which the corrosive liquid drains through the phase contact apparatus 1 and a connecting line 11 connected at its lower end and then collects in the sump vessel 4 (drainage cycle).

In the process, the wet sewage sludge originating from a preceding mechanical dewatering is mixed with brown coal, brown coal coke or their mixtures in a weight ratio of sewage sludge to brown coal or its mixtures with brown coal coke of 1:3 to 3:1 and subsequently compacted wet at moderate compaction pressures above 50 bar to dimensionally stable mouldings. The briquetted mouldings can then be fed to a power station boiler as an auxiliary fuel to a thermal utilization or utilized chemically in a pyrolysis or gasification process for the production of fuel gas or synthesis gas.

Process for the utilization of sewage sludges

A pump for delivering hot, corrosive material having a shaft seal comprising a seal gap through which hot gases flow, and wherein the sealing gases also flow around the pump bearings for the purpose of cooling the bearings.

Pump for delivering hot, corrosive media

Process and a device for detoxifying the waste gases from waste

Plasmatron with steam as the plasma gas and process for stable operation

The plastic waste is reacted in a plasma reactor 3 under reducing conditions in a plasma containing substoichiometric oxygen at temperatures above 1200.degree. C. to form a plasma pyrolysis gas consisting of low molecular weight carbon fragments which is then cooled to temperatures below 1500.degree. C. The cooled plasma pyrolysis gas is then delivered in compressed form as a fuel of high calorific value and high temperature to a gas turbine 10 for generating power. The waste heat of this gas turbine is used to generate steam which is fed into a steam turbine 12 for generating more power. The process is suitable for plastic waste of any composition and leads to complete conversion into a gas of high calorific value so that a high exergetic efficiency level is achieved.

Process for converting plastic waste into power

Growing community of inventors

Burscheid, Germany

Hans-Ulrich Dummersdorf