Abstract: Method for fast pyrolysis of lignocellulose including: mechanically comminuting the lignocellulose to lignocellulose particles; at least one of completely drying and preheating the lignocellulose particles; mixing the lignocellulose particles with heat transfer particles so as to provide a mixture; heating the heat transfer particles, prior to the mixing, to a temperature between 500° C. and 650° C.; and heating, in a pyrolysis reactor with oxygen excluded, the lignocellulose particles using the heat transfer particles so as to establish a temperature between 400° C. and 600° C. for 1 to 50 seconds and so as to react the lignocellulose particles so as to provide pyrolysis coke, pyrolysis condensate, and pyrolysis gas.

Abstract: A method is provided for producing and preparing fast pyrolysis products from a biomass for entrained-flow pressure gasification that includes: heating of the biomass under exclusion of oxygen in a pyrolysis reactor, a temperature of between 400 to 600° C. being established for one to 50 seconds, such that the biomass reacts to form porous pyrolysis coke, pyrolysis condensate and pyrolysis gas; and drawing off the pyrolysis gas; condensing vaporous constituents of the pyrolysis condensate in a plurality of condensation stages so as to: condense, in a first condensation stage, at temperatures above the dew point of water, a low-temperature carbonization tar from the vaporous constituents; and condense and separate at temperatures between 0° C. and the dew point of water, in at least one subsequent condensation stage, an aqueous solution of oxygen containing organic compounds.

Abstract: Method for fast pyrolysis of lignocellulose including: mechanically comminuting the lignocellulose to lignocellulose particles; at least one of completely drying and preheating the lignocellulose particles; mixing the lignocellulose particles with heat transfer particles so as to provide a mixture; heating the heat transfer particles, prior to the mixing, to a temperature between 500° C. and 650° C.; and heating, in a pyrolysis reactor with oxygen excluded, the lignocellulose particles using the heat transfer particles so as to establish a temperature between 400° C. and 600° C. for 1 to 50 seconds and so as to react the lignocellulose particles so as to provide pyrolysis coke, pyrolysis condensate, and pyrolysis gas.

Abstract: A method is provided for producing and preparing fast pyrolysis products from a biomass for entrained-flow pressure gasification that includes: heating of the biomass under exclusion of oxygen in a pyrolysis reactor, a temperature of between 400 to 600° C. being established for one to 50 seconds, such that the biomass reacts to form porous pyrolysis coke, pyrolysis condensate and pyrolysis gas; and drawing off the pyrolysis gas; condensing vaporous constituents of the pyrolysis condensate in a plurality of condensation stages so as to: condense, in a first condensation stage, at temperatures above the dew point of water, a low-temperature carbonization tar from the vaporous constituents; and condense and separate at temperatures between 0° C. and the dew point of water, in at least one subsequent condensation stage, an aqueous solution of oxygen-containing organic compounds.

Abstract: A process and an apparatus in a column arrangement for improving the separation of noble gases, particularly krypton, from a gas mixture containing such noble gases using an organic solvent as an absorption agent, utilizing a boiling point spacing of the charged absorption agent of less than or equal to 1.5.degree. C. below the boiling point of the pure absorption agent. The resulting pure absorption agent which is to be recycled, after heating it to a temperature corresponding to the boiling point at the associated operating pressure or up to 10.degree. higher is initially used as a heat exchange medium to regulate the evaporation rate of the charged absorption agent during the desorption of N.sub.2 and O.sub.2. The pure absorption agent is then used as a heat exchange medium to heat the cold absorption agent charged with Kr, N.sub.2 and O.sub.2 before the pure absorption agent is brought in contact with the gas mixture of N.sub.2, O.sub.2 and Kr entering the column.

Abstract: Process for the batch purification of uranium recovered in a reprocessing process, after a first separation of impurities, in which for each batch an aqueous, nitric acid uranyl-nitrate solution (UNH original solution), which still contains residual amounts of impurities, is cooled to crystallize out purified UO.sub.2 (NO.sub.3).sub.2 .multidot.6H.sub.2 O (UNH) from the solution and the resulting crystals are separated out of their mother liquor and washed. The original solution is adjusted to a specified uranium concentration and the adjusted solution is cooled to below 0.degree. C. to bring about the crystallization. The duration between starting and ending the crystallization is held between 0.1 and 10 hours. The amount of the UNH crystals which is crystallized out corresponds to at least about 80 weight % of the uranium content introduced. The ratio of the volume of the crystals formed to the volume of the remaining mother liquor is not larger than 0.5.

Abstract: A process for desorbing fission iodine from a solution in a dissolver containing nitric acid and nuclear fuel. At least part of the solution is distilled by boiling creating an iodine-containing vapor, and the condensate vapor is conducted in an ascending condenser in countercurrent with its condensate. The resulting condensate is the returned to the dissolver. The desorption of the iodine in the condenser is effected by means of a gas.

Abstract: Process for separating the noble fission gases xenon and krypton from a prepurified waste gas from a nuclear plant. The prepurified waste gas is brought into contact with liquid Cl.sub.2 CF.sub.2 as an absorption agent in a first column at an operating pressure which is less than or equal to normal pressure, whereby Xe, Kr, N.sub.2 O, CO.sub.2, O.sub.2 and N.sub.2 are absorbed by the agent. Subsequently, the liquid absorption agent containing the absorbed gases is heated to substantially the boiling temperature of Cl.sub.2 CF.sub.2 at the operating pressure for vaporizing part of the liquid absorption agent and desorbing the absorbed Kr, N.sub.2 and O.sub.2 to thereby separate the Kr and Xe from one another. The desorbed Kr, N.sub.2 and O.sub.2 gases are separated from the vaporized absorption agent. The liquid absorption agent which has not been vaporized is treated to recover Xe, N.sub.2 O and CO.sub.2. Waste gas containing Kr, N.sub.2 and O.sub.