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: 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 plant for the production of pig iron and/or sponge iron, comprising at least one fluidized bed reactor adapted to receive fine ore, a reducing-gas feed duct leading to said fluidized bed reactor, an off gas discharge duct departing from the fluidized bed reactor and a discharge means, preferably a briquetting means, provided for the reduction product formed in the fluidized bed reactor, the off gas discharge duct of the fluidized bed reactor runs into a purification means, such as a scrubber, subsequently into a heating means and finally into the reducing gas feed duct of the fluidized bed reactor. To produce a product having a high quality standard at a minimum energy input, the heating means is constructed such that it comprises two stages including a heat exchanger as the heating means for the reducing gas and, connected serially therewith, a partial combustion means for the reducing gas with an oxygen feeding means.

Abstract: In a process for the production of molten pig iron or molten steel pre-products and sponge iron from charging materials consisting of iron ore and, if desired, fluxes, direct reduction of the charging materials to sponge iron is carried out in a fixed-bed reduction zone, the sponge iron is melted in a meltdown gasifying zone under supply of carbon carriers as well as an oxygen-containing gas and a CO- and H.sub.2 -containing reducing gas is produced which is fed to the reduction zone, is reacted there and is drawn off as an export gas, and the drawn-off export gas is subjected to CO.sub.2 elimination and for the production of sponge iron is along with part of the reducing gas formed in the meltdown gasifying zone as an at least largely CO.sub.2 free reducing gas conveyed to a further reduction zone for the direct reduction of iron ore.

Abstract: A plant for the production of pig iron and/or sponge iron includes a direct-reduction shaft furnace for lumpy iron ore, a melter gasifier, a feed duct for a reducing gas connecting the melter gasifier with the shaft furnace, a conveying duct for the reduction product formed in the shaft furnace connecting the shaft furnace with the melter gasifier, a top-gas discharge duct departing from the shaft furnace, feed ducts for oxygen-containing gases and carbon carriers running into the melter gasifier and a tap for pig iron and slag provided at the melting vessel.

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: A method of and apparatus for charging fine-grained ore into a reactor pressure vessel through which process gas flows. The heated ore at first is introduced into a conveying pressure vessel, is pressurized within the same by compressed gas and subsequently is conveyed into the reactor pressure vessel through a conveying duct by aid of the compressed gas. In order to ensure favorable utilization of the reactor pressure vessel under uniform stress and to safeguard troublefree progression of reduction while directly charging the ore, a portion of the ore is introduced into at least one further conveying pressure vessel and is pressurized within the same also by compressed gas. Charging of the ore into the reactor pressure vessel is effected continuously by alternately feeding once from the one conveying pressure vessel and subsequently from the other conveying pressure vessel.

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: 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.

Abstract: There is disclosed a process for the direct reduction of iron-oxide-containing materials by a gasification gas produced in a gasifier by reacting carbon with oxygen and, if desired, with steam, upon the addition of sulfur acceptors in a fluidized bed. The gasification gas is supplied to a direct reduction shaft furnace after separation of solid particles carried therewith. At least part of the top gas withdrawn from the direct reduction shaft furnace is compressed after dust scrubbing and is recycled to the gasifier. The sulfur acceptors are supplied as fine particles separated from the coal in cocurrent with, and/or counterflow to, the fluidized-bed forming gases. The top gas from the reduction shaft furnace, which has a concentration of from 15 to 30% CO.sub.2 and a temperature of from 80.degree. to 800.degree. C., is recycled laterally through the wall of the gasifier into the region of the fluidized bed, which is maintained at a temperature of at least 1,150.degree. C.

Abstract: A method for the direct reduction of particulate iron-oxide-containing material. The method is carried out in a shaft furnace, wherein reformed gas from a reformer is fed as reducing gas to a reducing zone of the shaft furnace, the directly reduced ferrous particles are discharged from the shaft furnace and the top gas forming during reduction is extracted from the upper section of the shaft furnace. A hydrocarbon-containing gas is injected into the shaft furnace. Natural gas is separated into a first fraction enriched with low hydrocarbons and a second fraction enriched with higher hydrocarbons. The first fraction is conducted through the reformer and the second fraction is fed into the shaft furnace.

Abstract: A process and a plant for the direct reduction of iron oxide particles in a shaft furnace and for smelting the obtained iron sponge particles in a meltdown gasifier. A coal fluidized bed is formed in the meltdown gasifier by supplying coal and oxygen-containing gas, in which the heat necessary to smelt the iron sponge particles as well as the reducing gas to be injected into the shaft furnace are produced. The top gas remaining after the reduction is drawn off the upper part of the shaft furnace and the dusty solid particles, which are discharged together with the reducing gas and/or with the top gas, are washed out by scrubbers. The suspension of the washed out solid particles is thickened and separated into a clear overflow and a concentrated coal slurry. The coal slurry is recycled into the meltdown gasifier, is pressure-gasified with oxygen and is burnt by burners arranged in the upper part of the meltdown gasifier and directed towards the coal fluidized bed.