Abstract: In a process for reducing iron-ore-containing particulate material in at least a two-stage process, reducing gas is conducted through at least two reaction zones consecutively arranged in series and formed by a moving particulate material and the particulate material passes through the reaction zones in reverse order to the reducing gas, with the particulate material being heated in the reaction zone arranged first for the particulate material and being reduced in the further reaction zone.

Abstract: In a process for reducing iron-ore-containing particulate material in at least a two-stage process, reducing gas is conducted through at least two reaction zones consecutively arranged in series and formed by a moving particulate material and the particulate material passes through the reaction zones in reverse order to the reducing gas, with the particulate material being heated in the reaction zone arranged first for the particulate material and being reduced in the further reaction zone.

Abstract: In a process for reducing iron-ore-containing particulate material in at least a two-stage process, reducing gas is conducted through at least two reaction zones consecutively arranged in series and formed by a moving particulate material and the particulate material passes through the reaction zones in reverse order to the reducing gas, with the particulate material being heated in the reaction zone arranged first for the particulate material and being reduced in the further reaction zone.

Abstract: In a process for the direct reduction of particulate iron-oxide-containing material by fluidization, a synthesis gas is introduced as a reducing gas into several fluidized bed zones consecutively arranged in series. The reducing gas is conducted from one fluidized bed zone to another fluidized bed zone in counterflow to a flow of particulate iron-oxide containing material through the fluidized bed zones. In order to reduce operating costs and, in particular, the energy demand, various process parameters are varied according to the temperature of the iron-oxide-containing material in the first fluidized bed zone being adjusted to be below 400° C. (and, preferably, below 350° C.), above 580° C. (and preferably about 650° C.), or to a temperature within the range of from 400° C. to 580° C. If the temperature of the iron-oxide-containing material in the first fluidized bed zone is maintained to be below 400° C.

Abstract: In a process for the direct reduction of particulate iron-oxide-containing material by fluidization, a synthesis as is introduced as a reducing gas into several fluidized bed zones consecutively arranged in series for the reducing gas and the reducing as is conducted from one fluidized bed zone to another fluidized bed zone in counterflow to the particulate iron-oxide containing material.

Abstract: A device and method for reducing vibrations of a structure along an axis of vibration propagation, in particular in a helicopter, wherein two vibrating members of masses m1 and m2 are located at the ends of a spring, the spring and/or the masses being so constructed that the resonance characteristics of the assembly may be variably adjusted within a range decisive for the reduction of vibrations of the structure. The phases of the movement of the two masses and of a central point of the spring connected to the structure are measured by accelerometers and the differences of phase angle compared to the base point are maintained at 90° by moving the masses using motors to bring about the necessary change in resonance of the assembly.

Abstract: A process for the direct reduction of particulate iron-oxide-containing material by fluidization. A synthesis gas is introduced as a reducing gas into several fluidized bed zones consecutively arranged in series for the reducing gas. The reducing gas is conducted from one fluidized bed zone to another fluidized bed zone in counterflow to the particulate iron-oxide containing material. In order to reduce operating costs and, in particular, the energy demand, the temperature of the iron-oxide-containing material is adjusted in the first fluidized bed zone to be either below 400° C. (and, preferably, below 350° C.), or above 580° C. (and preferably about 650° C.), or to a temperature ranging from 400° C. to 580° C. If the temperature of the iron-oxide-containing material in the first fluidized bed zone is adjusted to be below 400° C., the temperature range in the following fluidized bed zone between 400° C. and 580° C.

Abstract: In a process for producing sponge iron by direct reduction of iron-oxide-containing material, synthesis gas is mixed with top gas forming in the direct reduction of the iron-oxide-containing material and is utilized as a CO- and H.sub.2 -containing reducing gas for direct reduction and for heating the iron-oxide-containing material to a reduction temperature. To be able to save energy in an economically efficient manner when producing steel, especially in the refining process, direct reduction is carried out as follows: (1) in addition to the reducing gas, a carbon-containing gas, such as natural gas, or a gas having higher hydrocarbons is utilized for reduction; (2) the iron-oxide-containing material for a predetermined period of time exceeding the period necessary for complete reduction is exposed to the reducing gas and to the additionally supplied carbon-containing gas, and (3) a CO/CO.sub.2 ratio ranging between 2 and 5, preferably a ratio in excess of 2.5, is adjusted in the reducing gas.

Abstract: In a process for reducing particulate oxide-containing material using the whirl bed method, the oxide-containing material, by means of reducing gas flowing from bottom to top, is maintained in the whirl layer, thus being reduced. In order to avoid or considerably reduce operational interruptions of the reduction process caused by sticking or fouling, the clear tube speed (superficial velocity) of the reducing gas, exclusively above the whirl layer, is continuously lowered along the total free height of a space above the whirl layer while the formation of further whirl formations is avoided.

Abstract: In a process for the direct reduction of particulate iron-oxide-containing material by the fluidized bed method, reformed gas is mixed with top gas forming in the direct reduction of the iron-oxide-containing material and is fed to a fluidized-bed reduction zone as a reducing gas. To lower the energy demand and utilizing the potential of the reducing gas, both the top gas and the reformed gas are subjected to CO.sub.2 scrubbing and the reducing gas formed by mixing top gas with reformed gas is adjusted to an H.sub.2 content ranging between 45 and 75%, preferably between 50 and 65%, and to a CO content ranging between 10 and 20%.

Abstract: There is described a mill for the production of steel from liquid and solid charging substances. It includes a coking plant, a blast furnace plant, a converter steelworks, and a plant for the direct reduction of iron ore. The converter steelworks is charged with molten pig iron from the blast furnace and with scrap as well as with sponge iron from the direct reduction plant. The reduction gas is composed of converter offgas, top gas and blast furnace gas. In order to avoid coal deposits in the direct reduction plant and to improve the composition of the reduction gas, the coke oven gas component is subjected to fractionation by alternating pressure adsorption so as to increase its portion of hydrogen and to lower its portion of hydrocarbons.

Abstract: When operating mills including a coling plant, a blast furnace arrangement and a converter steelworks, large amounts of partially high-grade so-called cupola gases, such as coke oven gas and converter exhaust gases, form, which cupola gases, so far. In order to render these cupola gases utilizable at a better efficiency, thus reducing the specific energy consumption per ton of crude steel produced, and in order to be less dependent on external scrap, a plant for directly reducing iron ore is additionally adjoined to the mill. The ducts for the exhaust gas from the converters and the coke oven gas ducts from the coking plant are connected to a reformer to produce reducing gas substantially containing CO and H. The reformer is connected with the direct reduction plant via a reducing gas duct.