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: 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 order to attain as low a final temperature as possible after as short a period of time as possible in a method of cooling hot briquetted sponge iron (3) under optimum utilization of the cooling medium, the hot briquetted sponge iron (3), in a first cooling step (11), is passed exclusively by a gaseous cooling medium while being gently cooled and subsequently, in a second cooling step (14), is sprayed with a liquid cooling medium, thus being intensively cooled to the final temperature desired.

Abstract: An apparatus for treating fine ore in which fine ore is dried by aid of a hot drying gas flowing around the ore particles. After having flown around the ore particles, the drying gas is purified while releasing entrained dust ore particles. The dust ore particles are collected and admixed to the dried fine ore. In order to avoid process disturbances in the further processing of fine ore due to excessive portions of dust ore particles present without the fine ore, drying is effected in the whirl-bed method under simultaneous wind-screening of the fine ore. The drying gas is passed through the fine ore under formation of a whirl bed and the speed of the drying gas is fixed at a rate at which entraining of dust ore particles having dimensions below a predetermined dimension is effected. The dust ore particles entrained in the drying gas are separated, collected and admixed to the dried fine ore in dosed amounts. The apparatus includes a fine ore whirl-bed drying means including a drying-gas feeding means.

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: A direct reduction process is disclosed for iron oxide-containing materials. Synthesis gas is mixed with top gas produced during direct reduction of the iron oxide-containing materials and is used as reduction gas for directly reducing and heating the iron oxide-containing materials up to reduction temperature. In order to set the H.sub.2 S content at a predetermined value by a relatively simple technique and with a relatively simple equipment, at least part of the sulphur contained in the iron oxide-containing materials as H.sub.2 S produced during heating or direct reduction is added to the reduction gas together with the top gas.

Abstract: A direct reduction process is disclosed for iron-oxide-containing materials. Synthesis gas is mixed with top gas produced during direct reduction of the iron-oxide-containing materials and is used as reduction gas for directly reducing iron-oxide-containing materials. In order to avoid or reduce metal dusting caused by an increased CO content of the reduction gas with a simple technique and equipment, the CO/CO.sub.2 ratio of the reduction gas is set at a predetermined value from 1 to 3.

Abstract: In a process for the direct reduction of iron-oxide containing material, synthesis gas is mixed with top gas formed in the direct reduction of the iron-oxide containing material and is used as a reducing gas for direct reduction. In order to avoid metal dusting despite an elevated CO-content of the reducing gas, or to reduce metal dusting, in a procedurally simple and cost-saving manner while minimizing the energy demand, an H.sub.2 O content of between 1 and 2%, preferably amounting to about 1.5%, is achieved in the reducing gas by subjecting a partial volume of the top gas to CO.sub.2 scrubbing prior to being used as a reducing gas, wherein the top gas subjected to CO.sub.2 scrubbing is mixed with the synthesis gas, is brought to a predetermined temperature by direct water irrigation while being saturated with H.sub.2 O, after direct water irrigation is heated to a temperature above the saturation temperature by admixing CO.sub.2 -unscrubbed top gas, and subsequently is used as a reducing gas.

Abstract: With a process for the direct reduction of particulate iron-containing material by fluidization, reformed gas, at least partially freed from CO.sub.2, is supplied to a fluidized-bed reduction zone as a reducing gas and is carried off from the same as a top gas and at least a portion of the top gas together with reformed gas is utilized for direction reduction. To economize on parts of the plant that are impinged on by reducing gas and in order to achieve savings in terms of heating costs, CH.sub.4 and N.sub.2 are, in addition to CO.sub.2, at least partially removed by adsorption, from 50 to 100% of the reformed as and 0 to 100% of the top gas, and the tail gas removed from the reformed gas and/or the top gas by adsorption is utilized as a heating gas.

Abstract: In a process for treating fine ore, the fine ore is dried by aid of a hot drying gas flowing around the ore particles of the fine ore, the drying gas, after having flown around the ore particles, is purified while releasing entrained dust ore particles and the dust ore particles are collected and admixed to the dried fine ore. In order to avoid process disturbances in the further processing of fine ore due to excessive portions of dust ore particles present within the fine ore,drying is effected in the whirl-bed, i.e., fluidized-bed method under simultaneous wind-screening of the fine ore, whereinthe drying gas is passed through the fine ore under formation of a whirl bed andthe speed of the drying gas is fixed at a rate at which entraining of dust ore particles having dimensions below a predetermined dimension is effected, andthat the dust ore particles entrained by the drying gas are separated, collected and admixed to the dried fine ore in dosed amounts.