Abstract: The invention relates to a method for largely eliminating chlorine compounds from organic isocyanates or isocyanate mixtures by contacting said isocyanates or isocyanate mixtures with a water-containing inert gas flow or an organic material having a cation-exchanging effect. The inventive method allows the isocyanates to be gently freed from chorine-containing compounds and is particularly suitable for temperature-sensitive isocyanates.

Abstract: 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 1 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 3 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 6. The post-dried reaction gas consisting of chlorine, oxygen and hydrogen chloride is then compressed to 1 to 30 bar by a compressor 7. In the subsequent stage, the compressed reaction gas is passed through a cooled chlorine recuperator 8, wherein the chlorine is very largely liquefied.

Abstract: 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.

Abstract: 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).

Abstract: 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.

Abstract: 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).

Abstract: 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.

Abstract: 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.

Abstract: The invention relates to a process and a device for detoxifying the waste gases from waste incinerating plants, at least one plasma gas flow being admixed to the hot fresh flue gas flow from the waste incinerating plant for the thermal decomposition of the toxic compounds, the fresh flue gas flow is preferably heated up in a recuperation stage with a high-temperature heat exchanger by the plasma-beam-treated flue gas in the counter-flow principle and subsequently at least one plasma gas flow is mixed into the fresh flue gas heated in this fashion. Following this, the gas mixture being at a peak temperature is used for heating up the fresh flue gas flow in the recuperation stage and cooled to a temperature which is still above the waste gas temperature, and it is subsequently finally treated in a waste heat system and a flue gas purification.

Abstract: The present invention refers to a plasmatron as well as to a process for stable operation of plasmatrons with steam as the plasma gas, in the case of which the operational fluctuations which are typical of steam plasmas as well as the increased degree of electrode erosion are to be avoided. In accordance with the present invention, this is achieved on the basis of a limitation of electrode cooling by using hot water as a coolant having a temperature of at least 80.degree. C. If necessary, it is possible to use, on the one hand, hot water cooling and to exclude, on the other hand, a condensation of the steam on the electrodes by admixing a gas which will lower the condensation temperature of the steam.

Abstract: 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.

Abstract: Toxic wastes are destroyed by contact thereof with a steam plasma jet and immediately thereafter with an oxidizing medium followed by washing of the resultant gaseous product with an alkaline medium. An apparatus for carrying out this method is in the form of a tubular assembly adapted to be received on a plasmatron in axial alignment therewith.

Abstract: Polymer waste products are converted into a subdivided form and into a conveyable consistency and supplied to hydrogen plasma jet, preferably with an average mass temperature of at least 1,000.degree. C. and a pressure of 0.05 to 0.5 MPa, so that a mixing of the polymer suspension or granulate with the hydrogen plasma occurs.In this hydrogen plasma, the polymer waste products are decomposed completely and react to form highly endothermic, valuable products, such as acetylene, ethylene, hydrogen, CO, HCN or HCl.