Chemie Linz Aktiengesellschaft

Metallgesellschaft Aktiengesellschaft

Waagner-Biro Aktiengesellschaft

Vogelbusch Gesellschaft M.b.h.

Omv Aktiengesellschaft

Glanzstoff Austria Gesmbh

M. Kaindl Holzindustrie

Alfred Schmidt

Alfred Garber

Paul Wiesner

Ferdinand Weinrotter

Karlheinz Wegleitner

Josef Herbert Hatzl

Rudolf Sykora

Hans-Martin Stonner

Fritz Wohler

Hans M Stonner

Wilhelm Tschebull

Anton Friedl

Walter Etzenberger

Alfred Windsperger

Lothar Kloimstein

Erwin Niedermayer

Ludwig Berzaczy

Andreas Windsperger

Alan Sinclair

Low-emission drying of wood chips

A biological conversion process is provided for degradation of sulfur-containing pollutants such as H.sub.2 S, CS.sub.2, COS, and also organic surfur compounds such as thio-alcohols, thio-ethers, and thiophenes in waste gas. A packed reactor is provided which has packing material covered with immobilized microorganisms of the family of Thiobacillaceae and which are continuously kept moist, so that metabolic products of the microorganisms are dissolved in the moisture and discharged continuously. A continuous concentration gradient for sulfate ions thereby results in the reactor or in the region of the microorganisms, these sulfate ions being neutralized in a second reactor by supplying lye (soda or potash lye) forming readily-soluble salts. These readily-soluble salts are transformed in a third reactor by addition of milk of lime into crystals (gypsum crystals) which are poorly-soluble in water and with formation of lye for the second reactor capable of being recirculated so that loss of chemicals (lye) is principally minimized. The poorly-soluble crystals from the third reactor can be discarded or utilized. The low sulfate supernatant is then conveyed to the main canal, through a biological clarification plant.

Procedure for microbiologica transformation of sulphur containing

A process for separating oxygenous organic compounds from aqueous media by liquid-liquid extraction with an organic extraction agent. In order to enable the satisfactory and selective separation of the organic compounds without remarkable amounts of extraction agent remaining dissolved in the raffinate and without microorganisms possibly present in the aqueous media being impaired, an extraction agent is used that contains up to 100% by mass of at least one aldehyde including 4 to 20 carbon atoms.

Process for separating oxygenous organic compounds from aqueous media

The aqueous effluent liquors from gasification or de-gasification of coal are extracted with a water-insoluble solvent and the extract is processed to recover the solvent. The aqueous residue is treated to remove NH.sub.3 in a driving-off column. The invention adds the steps of

Processing aqueous effluent liquors from degasification or gasification

Aluminum fluoride with an AlF.sub.3 content of at least 96% by weight relative to the anhydrous product is produced by reacting aluminum hydroxide with aqueous fluosilicic acid, removing the precipitated silica, adding hydrofluoric acid in a quantity of 0.1-1% by weight of HF relative to the so produced AlF.sub.3 containing solution having an AlF.sub.3 content of 20 to 50 percent and atomizing same before the start of crystallization of the aluminum fluoride at temperatures of 110.degree.-350.degree. C. optionally using aluminum fluoride particles as heat transfer agents.

Process for the manufacture of aluminum fluoride

Disclosed is a process and apparatus for purifying and regenerating urea solutions which have been contaminated with biuret and triuret and the like during the use of the urea solutions such as in dewaxing processes. The contaminated urea solution is first contacted with ammonia in gaseous or liquid form and about one to ten percent of the ammonia is absorbed into the contaminated solution. The contaminated solution and absorbed ammonia are reacted in a reactor with heating for a period of time sufficient to complete the reaction of biuret and triuret to produce urea. The purified product solution may then be returned for further use in dewaxing processes. Excess ammonia and CO.sub.2 formed during the reaction process by the decomposition of urea may optionally be separated from the purified solution and from each other with the separated excess ammonia being returned to the absorber for reuse.

Process for the purification of urea solutions containing biuret and the

Pure, concentrated ammonia is recovered from aqueous liquors by stripping off gas water, de-acidifications, scrubbing and withdrawing ammonia from the top of a scrubbing column.

Continuous process for recovering pure, concentrated ammonia

Guanidine carbonate is isolated from dilute aqueous solutions containing guanidine, urea, pyrolysis products of urea, ammonia and carbon dioxide, by evaporation of the solution at a temperature of 80.degree. to 130.degree. C until a guanidine carbonate content of 20g/l and a pyrolysis products content of not more than 28g/l at 80.degree. C or not more than 128.degree. g/l at 30.degree. C is achieved, without exceeding a heating time of 6 hours at the upper temperature limit, separation of the precipitated pyrolysis products, subsequent cooling to not more than 45.degree. C, addition of ammonia to an ammonia content of 15 to 30 % by weight and separation of the precipitated guanidine carbonate.

Recovery of guanidine carbonate from aqueous solutions

Process for obtaining guanidine carbonate from aqueous solutions in which it is present with urea and its pyrolysis products as well as ammonia and carbon dioxide, which comprises heating the aqueous solution to a temperature of at most 80.degree.C at atmospheric pressure, evaporating the resulting solution, which contains an amount of carbon dioxide equal to the guanidine content, until it is saturated with urea, separating the solid precipitate, suspending the mother liquor in liquid ammonia and separating the resulting guanidine carbonate.

Process for the preparation of guanidine carbonate

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Vienna, Austria

Alfred Schmidt