Bayer Aktiengesellschaft

Metallgesellschaft Aktiengesellschaft

Hch. Bertrams Aktiengesellschaft

Hans Guth

Hermann Wieschen

Hans-Joachim Kaiser

Klaus Kleine-Weischede

Karl-Heinz Dorr

Hans L Kuhnlein

Hermann Rohe

Edgar Muschelknautz

Hugo Grimm

Rudolf Gerken

Marko Zlokarnik

Bernhard Spreckelmeyer

Wolfgang Richter

Werner Ludovici

Armin Burkholz

Alex Burger

Theo Mann

Siegfried Bielz

Gerhard Jonas

Werner Schabacher

Werner Bruch

Christoph Mucke

Willi Potes

Rudolf Beuchelt

Herman Wieschen

Dan Constantinescu

Helmut Kuhn

Hubert Vollmer

Peter Reher

A process and apparatus for the continuous introduction of air or oxygen-containing gases into an effluent containing activated sludge, the oxygen-containing gas largely being consumed by the effluent containing activated sludge in a single absorption stage, comprising introducing through a plurality of gas inlets an oxygen-containing gas into an effluent containing activated sludge which is in a basin under its own hydrostatic pressure of at least about 0.9 bar, the gas pressure of the gas introduced being about 0.01 to 0.5 bar above the hydrostatic pressure prevailing at the gas inlet, each gas inlet having a gas-swept cross-sectional area of at least about 0.01 m.sup.2 which is loaded by at least about 100 effective cubic meters of gas per square meter of cross-sectional area per hour, and the individual gas inlets being separated by a distance of at least about 0.5 meter, as measured from the middle point of a gas inlet. The gas inlets may be nozzles, ejectors or apertured plates preferably spaced equidistantly from one another and each may be supplied with propulsion liquid comprising effluent containing activated sludge. Preferred ranges from the various parameters depend upon whether the gas introduced contains more or less than 50% by volume of oxygen. Special gas injectors are also provided.

Single stage process for continuous introduction of oxygen-containing

Spent sulphuric acid, either alongside or mixed with contaminated metal salts such as iron sulphate heptahydrate, is regenerated to fresh acid by countercurrent contact with gases from cleavage of the sulphate salts, such gases containing SO.sub.3 which effects build up of the acid concentration. The built up acid is evaporated in another stage to obtain pure acid. The metal sulphate solids are subjected to high temperature cleavage, generating SO.sub.3 which effects the previous concentration. Cleavage also produces some SO.sub.2 which is converted to SO.sub.3 by wet catalysis.

Working up spent sulphuric acid simultaneously with sulphate salts

In the production of activated carbon by passing a preheated gaseous activation medium through a zone containing a bed of carbon-containing material while indirectly heating to maintain a temperature of about 500.degree. to 1100.degree. C., supplying carbon-containing material to the bed, and removing activated carbon from the bed, the improvement which comprises introducing the activation medium and the carbon-containing material co-current near the bottom of the zone at a rate such that gaseous products are formed in a quantity sufficient to maintain in the zone a lower static layer and an upper fluidized layer in particular proportions, the rate of supply of the carbon-containing material and withdrawal of activated carbon being related so as to convert about 30 to 55% by weight of the carbon-containing material to gaseous products. The average residence of the carbon-containing material is from about 0.2 to 6, preferably 1 to 4, hours. A suitable apparatus for carrying out the process is described.

Production of activated carbon in a reactor having a lower static layer

In an apparatus for the gasification of a biomass in an aqueous medium in the presence of organic substances degradable by the biomass, comprising a gasification tank, and a clearing chamber for the gasified water-containing biomass provided concentrically around the gasification tank, the gasification tank communicating with the clearing chamber through an inlet in the latter, the improvement wherein A. the gasification tank is from about 10 to 32 meters high, has a height/diameter ratio between approximately 40 and 0.2, is provided adjacent its floor with gas inlet points, and is connected via inlet pipes to at least one gas removal and flocculation cyclone; B. the same liquid level in all the clearing chambers is maintained by means of an overflow channel at about 0.1 to 2 meters below the liquid level of the gasification tank; and C. a sludge removal pipe connects each clearing chamber with a collector pipe. Advantageously the clearing chamber is funnel shaped.

Apparatus for aerobic treatment of activated sludge

This invention relates to an arrangement for separating for films, droplets and sprays from pipe-borne gas flows wherein a pipe is provided with a cross-sectional constriction adapted to accelerate the gas flow in the pipe and annular stripping slot having an annular baffle surface and communicating with a collecting trap, the annular baffle surface being adapted to receive the liquid-containing gas flow and to cause the flow to pass into the collecting trap.

Separator, especially for chimneys

In the removal of water from a gas by contact with sulfuric acid, the improvement which comprises supplying the sulfuric acid in finely divided form having a surface of about 10.sup.4 to 10.sup.7 m.sup.2 /h at a concentration of about 95 to 99% and a temperature of about 35.degree. to 80.degree. C and with a contact time of about 0.2 to 2 seconds, whereby the residual moisture content of the gas is reduced to about 30 to 250 mg of H.sub.2 O/Nm.sup.3. Preferably the sulfuric acid is sprayed through a constriction into a vessel through which the gas is passed. The large sulfuric acid surface area permits high levels of dehydration to be achieved with far less sulfuric acid than heretofore believed possible and with small vessels and minimal contact times. Contact may be effected serially in several stages with the spent acids combined, brought up to initial concentration and recirculated.

Process for dehydrating gas with sulfuric acid

In the processing of a corrosive liquid mixture, such as 50 to 80% aqueous sulfuric acid, by its passage over one surface of a wall of inert heat resistant material, and heating the other surface of said wall, thereby to evaporate from said corrosive liquid mixture the more volatile component thereof, the improvement which comprises heating said wall by contact with an inert liquid material, and heating said inert liquid material indirectly through heat exchange with a normally solid molten material. Desirably the wall of inert material is a pipe surrounded by a molten metal in a first annular jacket and a molten salt in a second annular jacket.

Concentration and separation of corrosive liquid mixtures

In the production of hydrofluoric acid and calcium sulfate by subjecting sulfuric acid and fluorspar to a partial preliminary reaction in a preliminary reaction zone and the reaction is completed in an after-reaction zone at a temperature from about 100.degree. to 500.degree. C, the improvement which comprises effecting the preliminary reaction by circulating preliminary reaction product through said preliminary reaction zone, adding to the circulating preliminary reaction product at spaced locations in the preliminary reaction zone sulfuric acid preheated to a temperature of about 80.degree. to 200.degree. C and fluorspar preheated to a temperature of about 400.degree. to 800.degree. C, removing from said preliminary reaction zone gaseous hydrofluoric acid and a substantially dry mixture of calcium sulfate, unreacted sulfuric acid and fluorspar, and passing said dry mixture of calcium sulfate, unreacted sulfuric acid and fluorspar to said after-reaction zone. Only some of the necessary sulfuric acid may be supplied to the preliminary reaction zone and the balance supplied to the after-reaction zone. Heating of the preliminary reaction zone can be external or materials can be added which will react exothermically, e.g. SO.sub.3 to react with water in the system, CaO to react with sulfuric acid. A suitable apparatus is provided, comprising two parallel troughs connected at their ends by overflows and with oppositely rotating screws to circulate the contents. Means are provided for introducing reactants at spaced locations and for removing a mixture of product plus unreacted starting materials.

Production of hydrogen fluoride and calcium sulfate

Sulfur dioxide is formed by the combustion of elemental sulfur in two distinct stages wherein oxygen-containing gas in a quantity which is initially less than that stoichiometrically required for total combustion of the sulfur to sulfur dioxide and the sulfur-dioxide gases and residual elemental sulfur are thereupon passed through a heat exchanger and subjected to an afterburning with additional quantities of oxygen-containing gas. 70% to 95% of the total oxygen required for combustion of sulfur is supplied in the initial or combustion stage and the remainder (i.e. 30 to 5%) is supplied in the afterburning stage.

Sulfur-producing process and system for producing sulfur dioxide

Separation of corrosive liquid mixtures

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Berg. Neukirchen, undefined

Hans Guth