VERFAHREN ZUM GEWINNEN VON AMMONIAK AUS EINEM AMMONIAK, KOHLENDIOXYD UND SCHWEFELWASSERSTOFF ENTHALTENDEN ABWASSER
An aqueous effluent is supplied to a stripping column (total stripping column) from which a mixture that is rich in NH3, CO2 and H2S is withdrawn as a head product. In at least one additional stripping column the mixture is separated into a mixture which is rich in NH3 and a mixture which is rich in...
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| creator | HILSEBEIN, WOLFGANG STOENNER, HANS MARTIN UNGAR, GERT |
| description | An aqueous effluent is supplied to a stripping column (total stripping column) from which a mixture that is rich in NH3, CO2 and H2S is withdrawn as a head product. In at least one additional stripping column the mixture is separated into a mixture which is rich in NH3 and a mixture which is rich in the sour gaes CO2 and H2S. The mixture which is rich in NH3 is scrubbed with liquid ammonia. The overhead product from the total stripping column is cooled in a condenser under a pressure of 1 to 7 bars and is thus transformed into a liquid phase to such an extent that the liquid phase contains 70 to 100% of the NH3 which has been supplied to the condenser. The liquid phase is supplied at a temperature of 30 DEG to 90 DEG C. to a second stripping column (NH3 stripping column), which is operated under a pressure of 1 to 4 bars and from which a gas mixture that is rich in NH3 is withdrawn as a head product. The gas mixture is scrubbed with water and ammonia and the NH3 gas which has been scrubbed is condensed. |
| format | Patent |
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In at least one additional stripping column the mixture is separated into a mixture which is rich in NH3 and a mixture which is rich in the sour gaes CO2 and H2S. The mixture which is rich in NH3 is scrubbed with liquid ammonia. The overhead product from the total stripping column is cooled in a condenser under a pressure of 1 to 7 bars and is thus transformed into a liquid phase to such an extent that the liquid phase contains 70 to 100% of the NH3 which has been supplied to the condenser. The liquid phase is supplied at a temperature of 30 DEG to 90 DEG C. to a second stripping column (NH3 stripping column), which is operated under a pressure of 1 to 4 bars and from which a gas mixture that is rich in NH3 is withdrawn as a head product. 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In at least one additional stripping column the mixture is separated into a mixture which is rich in NH3 and a mixture which is rich in the sour gaes CO2 and H2S. The mixture which is rich in NH3 is scrubbed with liquid ammonia. The overhead product from the total stripping column is cooled in a condenser under a pressure of 1 to 7 bars and is thus transformed into a liquid phase to such an extent that the liquid phase contains 70 to 100% of the NH3 which has been supplied to the condenser. The liquid phase is supplied at a temperature of 30 DEG to 90 DEG C. to a second stripping column (NH3 stripping column), which is operated under a pressure of 1 to 4 bars and from which a gas mixture that is rich in NH3 is withdrawn as a head product. The gas mixture is scrubbed with water and ammonia and the NH3 gas which has been scrubbed is condensed.</abstract><edition>4</edition><oa>free_for_read</oa></addata></record> |
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| subjects | AMMONIA CHEMISTRY COMPOUNDS THEREOF CYANOGEN INORGANIC CHEMISTRY METALLURGY |
| title | VERFAHREN ZUM GEWINNEN VON AMMONIAK AUS EINEM AMMONIAK, KOHLENDIOXYD UND SCHWEFELWASSERSTOFF ENTHALTENDEN ABWASSER |
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