Abstract: Disclosed is a method for producing precursors for L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 2-[18F]fluoro-L-tyrosine and the ?-methylated derivatives thereof, the precursor, and to a method for producing L-3,4-dihydroxy-6[18F]fluorophenylalanine and 2-[18F]fluoro-L-tyrosine and the ?-methylated derivatives thereof from the precursor. A compound of formula (3) is provided which enables automated synthesis of L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 2-[18F]fluoro-L-tyrosine. The enantiomeric purity of the product is ?98%.

Abstract: Disclosed is a method for producing precursors for 2-[18F]fluorophenylalanine and 6-[18F]fluoro-L-meta-tyrosine and the ?-methylated derivatives thereof, to the precursor, and to a method for producing 2-[18F]fluorophenylalanine and 6-[18F]fluoro-L-meta-tyrosine and the ?-methylated derivatives thereof from particular precursor. A compound of formula (3) is provided which enables an automated synthesis of L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 6-[18F]fluoro-L-meta-tyrosine. The enantiomeric purity of the product is ?98%.

Abstract: Disclosed is a method for producing precursors for L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 2-[18F]fluoro-L-tyrosine and the ?-methylated derivatives thereof, the precursor, and to a method for producing L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 2-[18F]fluoro-L-tyrosine and the ?-methylated derivatives thereof from the precursor. A compound of formula (3) is provided which enables automated synthesis of L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 2-[18F]fluoro-L-tyrosine. The enantiomeric purity of the product is ?98%.

Abstract: Disclosed is a method for producing precursors for 2-[18F]fluorophenylalanine and 6-[18F]fluoro-L-meta-tyrosine and the ?-methylated derivatives thereof, to the precursor, and to a method for producing 2-[18F]fluorophenylalanine and 6-[18F]fluoro-L-meta-tyrosine and the ?-methylated derivatives thereof from particular precursor. A compound of formula (3) is provided which enables an automated synthesis of L-3,4-dihydroxy-6-[18F]fluorophenylalanine and 6-[18F]fluoro-L-meta-tyrosine. The enantiomeric purity of the product is ?98%.

Abstract: Furanosides or pyranosides can be reacted with pyruvate and converted into sialic acids in good yields by an enzymatic synthesis, using a suitable aldolase, where the concentration of aldolase, per 50 mM of pyruvate, is 1 to 2,500 U*/ml. For example, 3-fluoroneuraminic acid and other 3,3-didesoxy-3-fluorononulopyranosonic acid derivatives can be prepared in this manner. The F-atom in the resulting sialic acid (which can be 19F or 19F and 18F) provides a label which makes possible studies of mammalian physiology and diagnosis of mammalian diseases.

Abstract: In UASB-type biogas reactors, the biogas is separated from the rising waste water stream by collection hoods arranged in staggered fashion, in which a zero pressure level is maintained, at which the gas transition takes place. In cross-section shapes of existing collection hoods, the zero pressure surface is sharply reduced when the water level is high, and the conversion to gas is correspondingly sharply reduced. Therefore, in accordance with the invention, a rectangular section shape is employed in which the zero pressure surface remains unchanged. The topside of the collection hoods can be formed as a smooth sliding surface in the shape of a roof for the anaerobic sludge sediment.

Abstract: A process for decaffeinating raw coffee by selective extraction of the caffeine by means of a solvent that is liquid under normal conditions. Raw coffee beans are extracted for between one and several hours by means of a liquid solvent that is comprised of water and that has been saturated with carbon dioxide or other suitable gas or gas mixture at a temperature of between about 20.degree. C. and 110.degree. C. and a pressure of between about 30 bar and 300 bar to provide a charged liquid solvent. The pressure is reduced abruptly or within a few minutes to a pressure between about 1 bar and 10 bar to expand the raw coffee beans. The expanded raw coffee beans are rinsed in the liquid solvent for a period of between a few minutes and two hours.

Abstract: A method of thermal disposal of sewage sludge. The sludge is dried and incinerated. The flue gases from the incineration are washed. The flue gas dust resulting from the incineration and the sludge resulting from washing of the flue gases are treated together with high temperature combustion which includes melting of solids.

Abstract: The process for recovering vegetable oleaginous substances from oil-containing natural substances comprises a series of continuous combined pressing and extraction steps to increase and simultaneously to guarantee a high quality product for different kinds of natural substance starting materials. This is accomplished by subjecting the natural substances, conditioned and comminuted if necessary, after mixing with a solvent phase containing some oil to an intensive processing, mixing and extraction in the shear field of at least one rotor-stator unit and subsequently feeding the resulting liquid phase, through a filter if necessary, to a distillation column. The solid phase is extracted in successive stages until a residual oil content of 1% is reached and the solvent is fed back to a solid phase in a counterflow. The process as defined in my invention is universally applicable to all fat and oil-containing natural substances using suitable fluid extraction means.

Abstract: Phosphates which are dissolved or contained in suspension are substantially completely removed from a low-solids waste water which has been clarified. Precipitating and flocculating agents for transforming the dissolved phosphated to an undissolved form are added to the low-solids wate water and precipitation products and suspended matter are removed by microsieving through mesh openings in the range of about 10 to 150 .mu.m. Microsieving is preferably effected in two stages including a preliminary sieving through mesh openings from 60 to 150 .mu.m and a fine sieving through mesh openings from 10 to 80 .mu.m.

Abstract: A process for the extraction of vanillin by means of the extraction from a vanillin-containing, water-containing, liquid mixture of substances with carbon dioxide at a temperature of 0.degree. to 110.degree. C. as well as a pressure of 30 to 400 bar and a subsequent separation of vanillin is described. It is contemplated that with this process the vanillin-containing carbon dioxide is passed through an aqueous hydrogen sulfite- or sulfite-solution at the extraction temperature and the extraction pressure, that this solution is subsequently acidified with sulfuric acid to a pH value of 2 to 4, and that the vanillin-free carbon dioxide is fed back into the extraction stage.

Abstract: Process for separating solid substances from liquid mixtures of substances, wherein the liquid substances contained in the mixture are separated from the solid substances by countercurrent extraction with a solvent which, during the extraction process, is in a liquid or supercritical state and which, under standard conditions, is gaseous. The solvent is fed to a cylindrical extraction chamber at the lowest point of the extraction chamber. The solvent leaves the nozzles with a Reynold's number of 40,000 and flows upward in the extraction chamber with a Reynold's number of 2,700 to 8,000.

Abstract: Apparatus for separating solid substances from liquid mixtures of substances, wherein the liquid substances contained in the mixture are separated from the solid substances by countercurrent extraction with a solvent which, during the extraction process, is in a liquid or supercritical state and which, under standard conditions, is gaseous. The solvent is fed to a cylindrical extraction chamber at the lowest point of the extraction chamber. The solvent leaves the nozzles with a Reynold's number of 40,000 and flows upward in the extraction chamber with a Reynold's number of 2,700 to 8,000.

Abstract: A process is disclosed for the working up of salvage oil, in which the salvage oil is subjected to an extraction under supercritical conditions. The halogen compounds contained in the produced extract are removed by catalytic hydrogenation. The extraction residue is eliminated by deposition or thermal treatment (gasification). In the case of a thermal treatment of the extraction residue, other residues can be simultaneously converted, so that the process is performed without yield of environmentally burdensome residues or by-products. Ethane in particular and/or propane is employed as solvent for the supercritical extraction.

Abstract: A process for producing hydrocarbons from biological sludge, wherein the sludge is treated at a temperature of from 300.degree. to 600.degree. C. and at a pressure of from 100 to 500 bar to cause cracking of the organic compounds present in the sludge, the sludge is simultaneously or immediately thereafter hydrogenated with hydrogen under the same pressure and temperature conditions in the presence of a catalyst, and thereafter the resulting gas phase is separated into its components by stepwise reduction of pressure and/or temperature; thereby disposing of the biological sludge without environmental damage and with the simultaneous recovery of hydrocarbons.

Abstract: A process for the production of liquid hydrocarbons from old tires, cable wastes, polyethylene wastes and/or polypropylene wastes, by which the waste products, in pulverized form, are treated at a temperature of 150.degree. to 500.degree. C. and a pressure 20 to 300 bar with a solvent which is liquid at 1 bar and 20.degree. C. to form a solvent phase charged with liquid hydrocarbons and a residue phase. The charged solvent phase is separated from the residue, and the separated charged solvent phase is resolved into its components by lowering of pressure and/or temperature, and by distillation.

Abstract: A process is proposed for the isolation and purification of antibiotics wherein an antibiotic containing solution is extracted with an extraction agent at a temperature of from 0.degree. to 40.degree. C. and at a pressure which lies between the critical pressure and the ten-fold value of the critical pressure of the extraction agent, with the weight ratio of antibiotic containing solution to the extraction agent being 1:5 to 1:20, wherein the antibiotics are precipitated from the antibiotic containing extraction agent by reducing its density and wherein the extraction agent is recirculated. An entrainer may be added to the extraction agent. The reduction in density of the antibiotic containing extraction agent may be effected by expansion to a pressure of from 30 to 70 bar.

Abstract: A process for the recovery of lecithin from mucilaginous substances obtained in the production of vegetable fats and oils by extraction with a solvent which is gaseous under normal conditions. The mucilaginous substances are extracted at a pressure from 2.times.p.sub.k to 500 bar and at a temperature from 0.degree. C. to <T.sub.k for a period from 15 to 60 minutes to form a charged compressed solvent phase containing extracted substances and an extraction residue containing insoluble lecithin. Then, the charged, compressed solvent phase is separated from the insoluble lecithin. Thereafter the extracted substances are separated from the charged, compressed solvent phase and the gaseous solvent is returned to the extraction stage. The lecithin is removed from the extraction stage and is obtained in solid form by evaporating the solvent.

Abstract: A process for recovering petroleum from deposits which have already been worked by primary extraction or are not suited for primary extraction. A gas in its supercritical state is introduced into the deposit. The supercritical gas charges itself with the petroleum while flowing through the deposit. The charged supercritical gas leaves the deposit and the petroleum is separated in a plurality of fractions from the charged supercritical gas.

Abstract: A method for processing a used oil which comprises about 70 percent by weight spindle and neutral oils, about 5 percent by weight lower and higher boiling point oils, about 10 percent by weight useful additives and oxidation products, about 10 percent by weight water, about 5 percent by weight difficultly volatile and nonvolatile hydrocarbons, and solid impurities, comprising: (a) dewatering the used oil; (b) contacting the dewatered used oil with a gas in a supercritical state, at a temperature above the critical temperature and at a pressure from its critical pressure up to about 350 bar to form (1) a gaseous extraction phase containing the spindle and neutral oils and the additives, the spindle and neutral oils and substantially all the additives being extracted into the gaseous extraction phase during the contact with the supercritical gas and (2) an extraction residue; (c) separating the gaseous extraction phase from the extraction residue; and (d) separating the extracted spindle and neutral oils and th