Krupp Koppers Gmbh

Peter Diemer

Norbert Deuser

Hans J Wohner

Rainer Dittmer

Gunter Adomat

John Rizzon

Werner Brake

Wilfried Pappmann

A process for the simultaneous production of methanol synthesis gas and ammonia synthesis gas proceeds from the crude gas of a coal gasification, which initially is subjected to a H.sub.2 S-washing at low temperatures. Then follows a splitting of the desulfurized gas into two partial streams, of which one partial stream is led directly into the CO.sub.2 -washing which serves for production of the methanol-synthesis gas. Another partial stream is in contrast initially subjected to a conversion. From the converted gas then a partial stream is branched off which is provided for the production of ammonia-synthesis gas, whereas the remainder of the converted gas is led into the CO.sub.2 -washing serving for the production of the methanol-synthesis gas. The partial straem serving for the production of the ammonia-synthesis gas is treated to a separate CO.sub.2 -washing, in which simultaneously the so-called purge gas from the ammonia-synthesis is led in. The H.sub.2 S-washing and the CO.sub.2 -washings are conneced with each other by a common washing agent circulation.

Process for the simultaneous production of methanol synthesis gas and

In a method of subsequent treatment of sulfur gas from waste pyrolysis, the sulfur gas is cooled after hot dust removal in many stages to an end temperature between 0.degree. and 5.degree. C., wherein the components [condensate] separated from the gas are subdivided into a heavy tar, an oil and a water phase. The obtained heavy tar is supplied back to the pyrolysis reactor, whereas the oil phase is again used partially or completely for gas treatment, and the separated water is discharged from the process. The end product of the method is a stable gas which can be used for heating.

Method of subsequent treatment of sulfur gas from waste pyrolysis

In a multi-stage washing process for the removal of ammonia from coking oven gas, a portion of waste water, produced during the separation of ammonia from ammonia-containing water in an ammonia still, is supplied to an ammonia water at the final stage of washing, at which ammonia is washed out from gas with ammonia-free water.

Multi-stage method for washing-out ammonia from gas, particularly coking

In a method of removing heavy tar produced in a coke oven during the cooling of a coke-oven gas from the coke-oven gas, the heavy tar pieces are crushed in a pulverizer to obtain particles of the size of less than 1 mm. The heavy tar particles are then rarefied by the addition to them of a mixture of tar and water. The resulting mixture is maintained under the temperature of 55.degree.-75.degree. C. and then transported to a charge coal which is then charged into the coke-oven.

Method and device for removal of heavy tar from a coke-oven gas during

A process and system are disclosed for the bridging of operational standstills of an ammonia washer of a plant operating according to the semi-direct technique for the removal of ammonia from coking oven gas. During the operational standstills of the ammonia washer, the ammonia is washed out from the coking oven gas in a secondary cooler constituting three parts, an upper part (Wash Stage I) provided with stripped water from an ammonia still, a middle part (wash stage II) provided with gas water, and a lower part (wash stage III) provided with circulation water. All of the waters provided for the secondary cooler are collected in its sump, and after a separation of the circulation water necessary for the Wash Stage III, it is split into two partial streams, one serving for the recovery of stripped water for Wash Stage I and which is led into an ammonia still provided only with water vapor and the other partial stream is led into an ammonia still provided with water vapor and alkali. Also disclosed is a system containing a secondary cooler defining three vertically disposed sections of metal mesh beds.

Bridging operational shut-downs of the ammonia washer of a plant

A process is disclosed for the elimination of waste water falling out with the desulfurization of coking oven gas by means of an organic oxygen carrier--containing washing solution with simultaneous recovery of elemental sulfur. The waste water is decomposed in a combustion chamber in a reducing atmosphere at temperatures between about 1000.degree. and 1100.degree. C. under such conditions that the mole ratio of H.sub.2 S:SO.sub.2 in the exhaust gas of the combustion chamber amounts to at least 2:1. Sulfur falling out is separated and the sensible heat of the exhaust gas is utilized for steam generation. The cooled and desulfurized exhaust gas is added to the coking oven gas before the pre-cooling. Sulfur falling out from the washing solution in the oxidizer is separated out and lead into the combustion chamber together with the part of the washing solution discharged as waste water from the washing solution circulation. Preferred embodiments include that the sulfur loading of the waste water can amount to up to about 370 kg sulfur per m.sup.3 waste water; having the cooling of sulfur--containing exhaust gas leaving the combustion chamber follow in a waste heat boiler and a sulfur condenser heated by pre-heated boiler feed water, from which condenser sulfur is discharged in liquid state.

Process for the elimination of waste water produced upon the

Crude gas obtained through partial oxidation of carbon-containing material is subjected to catalytic conversion in an apparatus containing a moistening-demoistering system connected by means of a combined water circulation. To reduce the required amount of steam and process heating, a partial stream of water coming from the moistener is branched off, heated by indirect heat exchange with converted, hot synthesis gas, and then united with the partial stream of water coming from the demoistener for re-delivery to the moistener.

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Essen, Germany

Peter Diemer