Abstract: An aqueous solution which contains ammonium polysulfide is proportionally added to the sour water, which contains cyanide ions, ammonium ions, and sulfide ions. At least part of the cyanide ions contained in the sour water is converted to thiocyanate ions by the ammonium polysulfide. The solution which contains ammonium polysulfide is prepared from an aqueous solution by oxidation in an electrochemical cell. That aqueous solution may consist entirely or in part of sour water.

Abstract: The starting material is a vanadium-containing residue, which contains at least 5 weight percent carbon on an anhydrous basis. The residue is thermally treated in a furnace a) at temperatures from 400.degree. to 700.degree. C. under an oxidizing atmosphere and an O.sub.2 partial pressure of at least 10.sup.-4 bar, measured within the region which is occupied by the residue, and/or b) at temperatures from 500.degree. to 1300.degree. C. under an O.sub.2 partial pressure not in excess of 10.sup.-2 bar, measured within the region which is occupied by the residue. A solids mixture which contains at least 5 weight percent vanadium oxide is withdrawn from the furnace. A multiple-hearth furnace or a rotary kiln or a fluidized bed reactor containing a stationary or circulating fluidized bed may be used as a furnace for the thermal treatment.

Abstract: The waste materials are gasified in a circulating fluidized bed in a gasification reactor, which is supplied with oxygen-containing gas. A gas-solids mixture is withdrawn from the upper region of the gasification reactor and is fed to a separator. Dust-laden gas and separated solids are separately withdrawn from the separator and the separated solids are recycled at least in part to the lower region of the gasification reactor. Temperatures in the range from 700.degree. to 1000.degree. C. are maintained in the gasification reactor. The dust-laden gas which is withdrawn from the separator has a heating value of about 3000 to 6000 kJ/sm.sup.3 and is fed to a combustion chamber and is combusted therein at temperatures from 1200.degree. to 1900.degree. C. Liquid slag is withdrawn from the combustion chamber.

Abstract: Refractory gold ores are roasted at temperatures from 500.degree. to 650.degree. C. in an oxidizing atmosphere in a fluidized bed, which is supplied with a carbonaceous additional fuel. To effect a substantially complete combustion of the additional fuel to form CO.sub.2 and H.sub.2 O, methanol is added as a carbonaceous fuel.

Abstract: In a process for facilitating non-cutting cold working of ferrous materials by application of a phosphate coating, ferrous materials are dipped into a phosphating solution which is free of elements of group VIB of the periodic table which consists of Cr, Mo and W, of nitrogen compounds and preferably also free of nickel and contains5 to 20 g/l zinc1 to 15 g/l magnesium10 to 26 g/l phosphate calculated as P.sub.2 O.sub.51 to 15 g/l fluoroborate calculated as BF.sub.41 to 7 g/l chlorate calculated as ClO.sub.3and in which the weight ratio of Zn:Mg:BF.sub.4 is adjusted to from 1:0.15:0.15 to 1:1:1.

Abstract: The reactor comprises a plurality of gas-permeable plates, which define reaction stages, which are connected by overflow lines. An annular duct for effecting a gas distribution is provided on at least one plate. The outer wall and the inner wall of the annular duct comprises numerous gas outlet openings. The annular duct is provided with at least one vertical gas-conduction pipe, which extends from the plate and is open at both ends. The top end of the gas-conduction pipe is surrounded by a bell-like cap, which is connected to the annular duct, so that a space through which gases can flow is left between the gas-conducting pipe and the cap.

Abstract: An electrostatic separator is described which includes honeycomb collecting electrodes, which consist of star-shaped elements, wherein each star-shaped element consists of three wall parts (1, 2, 3), which are centrally joined and extend at an angle of 120.degree. to each other, at least one tube section (1', 2', 3', 5', 6') extends along the outer edge of each wall part, the tube sections (2', 5', 6') of any two adjacent star-shaped elements are arranged one over the other and adjacent star-shaped elements are connectted by a connecting rod (4), which extends in the tube sections (1', 2', 3', 5', 6') of at least two adjacent star-shaped elements.

Abstract: In a process of producing monotectic alloys having a relatively large miscibility gap in a liquid state and having in a solidified state a minority phase, which is included in the matrix and has the shape of droplets and has a higher density than the matrix, a molten material which is heated above the segregation temperature is continuously cast at a high casting speed end cooling rats. In order to achieve a sufficiently good disoersion of the minority phase the molten material is cast in a vertical direction.

Abstract: A fluidized bed reactor comprising a housing, and a nozzle grate disposed in the lower portion of the housing and serving to introduce a fluidizing fluid into the reactor. The nozzle grate consists of a plurality of approximately horizontally extending tubes and nozzles provided on such tubes. The tubes are detachably connected to the housing of the reactor and the housing of the reactor has at least one support for each tube, which support supports the tube as it is rotated about its longitudinal axis.

Abstract: The invention describes a device for transporting materials which has at least a first pipe (I) and a second pipe (II), each having a six-cornered, honeycomb-shaped flow cross section, the first pipe (I) having at least two first wall parts (1) which are not arranged adjacent to one another and whose longitudinal edges (1') are arranged at a first distance (a) from the connection point (3) between the first wall part (1) and the adjacent second wall part (2), which connection point (3) is nearest to the longitudinal edge (1'). Plate-shaped brackets (4) are arranged at the sides of the first wall parts (1) remote of the materials to be transported at a second distance (c) from the nearest longitudinal edge (1'). The angle (.alpha.) of inclination between the plane of the bracket (4) and the plane of the first wall part (1) is 60.degree., and the second pipe (II) has at least one corresponding first wall part (1) which is arranged parallel to the second wall part (2) of the first pipe (I).

Abstract: Dried fuel is at least partly combusted, gasified or carbonized in the presence of cooled solid residue in a reactor. Hot solid residue, which is at temperatures in the range from 500.degree. to 1200.degree. C., is withdrawn from the reactor and is mixed with water-containing fuel in the receiving region of a mechanical mixer, without a supply of fluidizing gas. The mixture is transported with further mixing from the receiving region of the mixer through a mixing section of 1 to 10 meters to an outlet. A fuel-containing, substantially water-free mixture at a temperature in the range from above 100.degree. C. to 150.degree. C. is fed from the outlet of the mixer to the reactor. A mixer which comprises two intermeshing shafts, which rotate in the same sense, may be employed in the process.

Abstract: To effect a quasi-isothermal catalytic reaction of SO.sub.2 to SO.sub.3, a plurality of consecutive rows of banks of cooling tubes, are provided in the bed of shaped catalyst bodies in a contact reactor in such a manner that the banks of succeeding rows are staggered from the banks of the preceding rows. The distance between the cooling tubes in the banks is so selected that a penetration of entire catalyst bodies into the banks will virtually be prevented. The banks are so designed that the pressure drop of the gas in the banks is approximately the same as the pressure drop in the layer of catalyst between the bank. The distance between the banks is larger than the width of the banks.

Abstract: A process of producing a phosphate coating on a metal surface of iron or steel by contacting the surface with an aqueous phosphating solution on the basis of magnesium phosphate. The solution contains 0.2 to 4 g/l magnesium, 1 to 20 g/l phosphate (calculated as P.sub.2 O.sub.5) and a peroxide compound as an accelerator. The phosphating solution is free of inorganic substances which are not precipitable with calcium hydroxide in a neutral or alkaline medium. It is preferred to use phosphating solutions which also contain activators, which are precipitable with calcium hydroxide in a neutral or alkaline medium.

Abstract: A process is described in which iron oxide-containing materials are reduced by a treatment with a gas underpressure in series-connected fluidized bed reactors, wherein hydrocarbons are cracked to produce the fresh reducing gas, reducing gas is fed to the first fluidized bed reactor as a fluidizing gas, the gaseous effluent from the first fluidized bed reactor is dedusted and is then fed as a fluidizing gas to at least one further fluidized bed reactor is dedusted and is subsequently treated in a scrubber-cooler to remove substantially all H.sub.2 O and residual dust, purified gas is recycled as recycle gas to the first fluidized bed reactor and the iron oxide-containing materials are preheated and are subsequently fed to the last fluidized bed reactor. The hydrocarbons are cracked by an approximately stoichiometric steam stoichiometric steam reforming. The freshly produced reducing gas is fed to one or more fluidized bed reactors.

Abstract: Fatty acids and/or fatty acid derivatives as well as hydrogen, fresh catalyst and a dispersion which contains used catalyst are supplied to the hydrogenating means, which are operated at temperatures in the range from 100.degree. to 400.degree. C. and under pressures in the range from 20 to 400 bars to produce a product stream, which contains fatty alcohols and used catalyst. A part of the product stream is circulated. A first partial stream Is withdrawn at a controllable rate from the circulating stream and is passed through a separator. A product which is rich in fatty alcohol and a dispersion which contains used catalyst are separately delivered by the separator. The dispersion is recycled to the hydrogenating means. A second partial stream is withdrawn at a controllable rate from the circulating product stream. Used catalyst is separated from the second partial stream and is removed from the process.

Abstract: At least one absorbent is added to the exhaust gas, which is passed at temperatures in the range from about 40.degree. to 500.degree. through a fluidized bed reactor and through dedusting means. Part of the solids separated in the dedusting means is recycled to the fluidized bed reactor. At least part of the recycled solids is blown with an entraining gas upwardly through a tube into the lower portion of the reactor. At least part of the combustion exhaust gas is fed to the reactor as a rising stream from a space which surrounds the tube. Air or combustion exhaust gas may be used, e.g., as an entraining gas.

Abstract: The method of reprocessing cured polysulfide and polymercaptan elastomers includes reacting an 0.5 to 400 percent-by-weight portion of a polysulfide and/or polymercaptan elastomer with at least one liquid di- or polymercapto compound, with a plasticizer and with a filling material and with an binding agent to form a polysulfide sealing material-base component. Then a polysulfide sealing material curing agent is added to the polysulfide sealing material-base component to form the reprocessed cured polysulfide sealing material with a Shore-A-Hardeness>40 and a tensile strength>1 MPa.

Abstract: A combustion exhaust gas which is to be dedusted and denitrated is mixed with NH.sub.3 and at temperatures in the range of about 250.degree. to 600.degree. C. is passed through a fluidized bed. The fluidized bed contains a denitrating catalyst, which contains FeSO.sub.4. The combustion exhaust gas serves as a fluidizing gas in the fluidized bed. Fresh denitrating catalyst is supplied to the fluidized beg and comprises at least 90% by weight FeSO.sub.4, which contains water of crystallization and has particle size in the range from 1 to 150 micrometers. The treated exhaust gas is dedusted in an electrostatic precipitator.

Abstract: Methanol is catalytically produced from a synthesis gas which contains H.sub.2, CO and CO.sub.2 in a synthesis reactor at temperatures from 220.degree. to 300.degree. C. and under a pressure in the range from 20 to 120 bars. A product mixture which contains methyl formate is withdrawn from the synthesis reactor and is cooled to temperatures in the range from 20.degree. to 60.degree. to provide a condensate which contains methanol, water and methylformate. A gas mixture which contains H.sub.2, CO and CO.sub.2 is formed at the same time. A fraction which comprises 10 to 100% by weight methyl formate is separated from the condensate and is admixed with the synthesis gas which is fed to the synthesis reactor.

Abstract: Water-containing solids are dried in a fluidized bed, which is indirectly heated by at least one heat exchanger. Water vapors having a high water vapor content are withdrawn from the fluidized bed and a part of the vapors is passed as a fluidizing fluid through the fluidized bed. The remaining vapors are cooled to form an aqueous condensate. At least part of the aqueous condensate is contacted in a purification zone with a gaseous or vaporous stripping fluid. Purified condensate and contaminated stripping fluid are separately withdrawn from the purification zone. Water vapor is preferably used as a stripping fluid in the purification zone.