Water extraction using a direct reduction plant

Abstract

The invention relates to a method for water production, wherein an oxide ore is reduced by reacting a hydrogen-containing gas, and the water produced is separated and treated. The invention also includes a device for carrying out the method, as well as a system and a use of the device or system for water production.

Description

In the steel industry, the majority of the CO2 emissionen are produced during the reduction of the iron ores, in particular via the blast furnace route. In order to reduce these CO2 emissionen, the prior art uses direct reduction of iron ore, in which hydrogen-rich (reformed) natural gas, i.e. essentially CO and H2, is used as reducing agent for the reduction.In the direct reduction of the iron ore, which, as can take place, for example, in the Midrex process, in a shaft furnace, not all the added reducing agent is reacted. Rather, the exhaust gas stream of the reduction reactor still contains unused reactive components (essentially H2and CO). The exhaust gas stream is post-treated in the prior art in order to be able to feed these reactive components back to the direct reduction process and, for example, to combine them with "fresh" natural gas before it is introduced into the reformer.Even if the CO2 emissionen can already be lowered by using direct reduction methods in comparison with the blast furnace route, CO2 wie to be produced due to the use of natural gas-via the CO. The prior art therefore discusses the use of hydrogen (H2) as reducing agent in order to make the direct reduction process even more environmentally compatible.The object of the present invention is the further improvement of the known direct reduction processes, in particular with regard to better environmental compatibility.The object underlying the present invention is achieved by a method having the features of claim 1, a device having the features of claim 15, a system having the features of claim 19, and the use of the device having the features of claim 20. Advantageous embodiments are described in the dependent claims.More specifically, the invention relates to a method for supplying water, in particular by means of a direct reduction device for iron ore. The method comprises the following steps: a) introducing a hydrogen-containing gas and an oxidic ore into at least one reduction reactor; b) reducing the oxidic ore present in the reduction reactor with reaction of the hydrogen-containing gas; c) separating at least part of the water from the offgas stream of the at least one reduction reactor; and d) preparing the separated water for at least one specific use.The invention is based on the finding that the water which is formed during the direct reduction and is present in the exhaust gas stream and is present in the form of water vapor on account of the temperature constitutes a valuable raw material and can be used further as industrial and / or drinking water instead of the disposal customary hitherto. The environmental compatibility of the direct reduction process is thereby significantly increased. The method according to the invention can thus also be referred to as a method for supplying industrial and / or drinking water.In the process according to the invention, oxidic ore is reduced by means of a hydrogen-containing gas in a reduction reactor suitable for this purpose. In this case, the oxygen contained in the oxidic ore is reacted with the hydrogen of the hydrogen-containing gas to form at least partially reduced metal and water. The hydrogen-containing gas may have been heated before introduction into the reduction reactor, for example in a reformer, via an electric heater, via a heat exchanger and / or via conversion into a plasma. During the preheating of the hydrogen-containing gas, the latter can be heated to a temperature which lies 100° C. or 150° C. above the operating temperature ranges of the reduction reactor set out further below. Preferably, the energy for such preheating is from a regenerative energy source. For example, the electric heating can be operated by means of regeneratively generated current (e.g. from photovoltaics). The energy for preheating can also be provided from the thermal energy of the water / water vapor formed during the reduction of the oxidic ore.The hydrogen-containing gas may be any gas suitable for the direct reduction of oxidic ore. The hydrogen-containing gas may also be a gas mixture. The hydrogen-containing gas can in particular be selected from the group consisting of H2, CH4, NH3, C2H6, C3H8, a pentane or mixtures thereof. The hydrogen-containing gas mixture may be a synthesis gas. The hydrogen-containing gas mixture can preferably be synthesis gas produced from natural gas and optionally enriched with hydrogen. In particular, the hydrogen-containing gas mixture may comprise at least two or all of the following constituents: CO, CO2, H2, H2O and CH4.The hydrogen-containing gas can have a distribution with respect to the components total hydrogen content, carbon monoxide content, water vapor content and carbon dioxide content in which the ratio of these components ((H2+CO) / (H2O+CO2)) is ≥10. Preferably, this ratio is in a range of ≥15 and ≤100, more preferably in a range of ≥20 and ≤100.The hydrogen-containing gas and / or the hydrogen-containing gas mixture can be derived at least partially, preferably completely, from regenerative sources. Preferably, the hydrogen may have been generated via electrolysis of water by means of a regenerative energy source, such as photovoltaics. The hydrogen-containing gas and / or the hydrogen-containing gas source may have been produced from biomass. Such hydrogen may also be referred to as "green hydrogen".The hydrogen-containing gas introduced into the reduction reactor may have a proportion of at least 20% by volume, preferably 40% by volume to 99.5% by volume, of molecular hydrogen (H2). Unless otherwise indicated in this application, percentages for gaseous and liquid materials are by volume (% by volume), while percentages for solids are by weight (% by weight).The oxidic ore can be any iron-containing source suitable for reduction. The oxidic ore is preferably an iron ore, for example an iron ore comprising oxidized iron (Fe), such as magnetite (Fe3O4) or hematite (Fe2O3). In particular, the iron ore can be an iron ore which is present in a form selected from the group consisting of pellet, lump ore ("dump ore"), fine ore, ore concentrates, ultra-fine ore, powder containing iron oxide and mixtures thereof. Pellets may be substantially spherical iron ore having a diameter of ≥4 and ≤20 mm or ≥8 and ≤18 mm. Pellets may have an Fe content of ≥55% by weight and ≤72% by weight or ≥67% by weight and ≤71% by weight. Fine ore may be iron ore particles having a diameter of ≥0.001 mm and ≤4.0 mm or ≥0.1 mm and ≤2.0 mm. Feierz may have an Fe content of ≥55 wt % and ≤72 wt % or ≥67 wt % and ≤71 wt %. The iron ore can in particular also be waste, fines and / or iron ore dust, which can be present in the form of fine ore, in particular in microgranular form as an iron ore fraction.The reduction mentioned in step b) can be, in particular, a direct reduction (DR) or a melting reduction (SR). Direct reduction is preferred and includes any process in which metallic iron is produced by reduction of iron ore or other iron oxides, bypassing the liquid melting phase and below the melting temperature of the materials involved, using solid, liquid or gaseous reducing agents.The degree of metallisation of the iron ore can be stated as the weight ratio of metallic iron to total iron. The total iron here includes the metallic iron as well as iron which is connected to other elements such as oxygen. The metallic iron includes chemically unbound iron, as well as cementite (Fe3C).Before the reduction of the iron ore in step b) of the method according to the invention, the latter can have a degree of metallization of at least 0% and / or at most 5%.After the reduction of the iron ore in step b) of the method according to the invention, the latter can have a degree of metallization of at least 60%. After the reduction of the iron ore in step b), the degree of metallization can be in a range of ≥60% and ≤99%, ≥65% and ≤85%, ≥74% and ≤76%, or ≥91% and ≤97%.The reduction reactor may be any reactor suitable for the reduction of iron ore. The reduction reactor is preferably a shaft furnace or a fluidized bed reactor (fluidized bed reactor), in particular a circulating fluidized bed (CFB) reactor or a bubbling fluidized bed (FB) reactor.The reduction reactor can be the reduction reactor of a reduction device, in particular a reduction device for reducing iron ore, which has further components. In particular, the reduction reactor can be a reduction reactor of a direct reduction device or a melt reduction device (melting reactor). The reduction device, in particular the direct reduction device, can have a single or a plurality of reduction reactors. Preferably, the reduction device may comprise ≥2 or ≥4 reduction reactors arranged sequentially. This is understood to mean that the iron ore to be reduced passes through the reduction reactors in succession in the course of the reduction. The reduction device can have as further components, which will be discussed in more detail in the further course of the description: at least one gas reformer, at least one gas scrubber (scrubber), at least one compressor and / or at least one heat exchanger.The gas reformer can be a steam reformer and / or comprise a nickel catalyst. It can be fluidly connected to an inlet of the at least one reduction reactor. The gas scrubbing device can be fluidically connected to an outlet of the at least one reduction reactor. This can preferably be the first outlet for the exhaust gas stream of the reduction reactor, in particular the outlet for the top gas ("top gas") or the outlet for the cooling gas of the reduction reactor. The compressor can be fluidically connected to the gas scrubbing device, in particular to the gas scrubbing device which is fluidically connected to the first outlet for the top gas or to the second outlet for the exhaust gas stream for the cooling gas, along the flow direction of the exhaust gas stream.The direct reduction device may be configured to perform at least one specific direct reduction method. The direct reduction method here can be selected from the group consisting of: the Midrex method, the Midrex-H2 method, the HyL-Energy method, the H2-HyL-Energy method, the HyRex method, the Hyfor method, the Circular method, the Finmet method, the iron carbide method, the Finex method and the Corex method. The direct reduction process can be a multistage, in particular a two- or four-stage, reduction process. A multistage reduction process is understood to mean that the iron ore to be reduced passes through different reduction reactors in succession in the course of the reduction.The reduction reactor can be operated at an operating pressure in the range of ≥2 bar and ≤13 bar. Preferably, the reduction reactor can be operated at an operating pressure in the range of ≥3 bar and ≤8 bar, ≥5 bar and ≤8 bar, or ≥2 bar and ≤4 bar. Preferably, the reduction reactor can be operated at an operating pressure of about 3 bar. An increased operating pressure has the advantage that the yield of water produced is increased.The reduction reactor can be operated with an operating temperature for the reduction in the range of ≥400 °C and ≤1000 °C. Preferably, the reduction reactor can be operated with an operating temperature in the range of ≥50° C. and ≤700 ° C. or ≥50° C. and ≤60° C.The direct reduction device can be configured to provide DRI (direct reduced iron), HBI (hot cooled iron), CBI (cold cooled iron) or LRI (low reduced iron), wherein DRI and HBI are particularly preferred.The separation of the water from the exhaust gas stream according to step c) of the method according to the invention can be carried out in any suitable manner. Preferably, the separation of the water also comprises a collection / collection of the separated water. The separated and / or collected water can then be processed directly and / or subsequently in time in step d) of the method.The portion of the water separated from the exhaust gas stream may preferably be so large that the exhaust gas stream after the water separation has a residual water content, in particular a residual water vapor content, of ≤7 vol. %, ≤5 vol. % or preferably ≤3 vol. %. Particularly preferably, after the water separation, the residual water content, in particular the residual water vapor content, in the exhaust gas stream is in a range of >1 vol % and <5 vol % or preferably >1.5 vol % and<3 vol %. As described above, the exhaust gas stream can be the furnace gas discharged from the reduction reactor and / or the cooling gas, wherein the furnace gas is preferred.The water separation after step c) of the method according to the invention can be effected by any suitable means or any suitable separation device. In particular, the water separation can be effected via drop separation (also called aerosol separation), i.e. the water separation is effected using a drop separator. Further preferably, the droplet separator can be combined with a heat exchanger for cooling the exhaust gas stream and / or be in thermal contact therewith. The droplet separator can be a lamella separator. The droplet separator can likewise be a vertically or horizontally inflowed droplet separator, in particular a vertically or horizontally inflowed lamella separator. Most preferably, the droplet separator can be a rotary separator. It could be advantageously observed in rotary separators that their use resulted in a lower pressure drop and furthermore reduced maintenance intervals (in particular because of clogging of the separator) resulted.Alternatively or additionally, the water can be separated from the exhaust gas stream via a thermal separation. In the case of thermal water separation, the exhaust gas stream can be cooled until the condensation of the water vapor contained therein, for example and preferably using a heat exchanger.Alternatively or additionally, the water can take place via a pressure change, in particular a pressure increase (compression) or pressure reduction (relaxation) of the exhaust gas stream. Preferably, the exhaust gas stream is compressed, for example by means of a compressor. Preferably, the device for changing the pressure of the exhaust gas stream, for example a compressor, can be combined with a heat exchanger and / or be in thermal contact therewith.Alternatively or additionally, the water can be separated from the exhaust gas stream by gas separation, in particular by means of the membrane method. In this case, the gases can be separated on account of their size and / or their affinity for the membrane.Alternatively or additionally, the water can be separated from the exhaust gas stream via adsorption and subsequent desorption on solids, in particular by means of a zeolite. Zeolites have the property of adsorbing water vapor, binding it into their porous structure and thereby releasing heat. In a second step, the adsorbed water can be desorbed from the zeolite by supplying heat and thereafter liquefied. Preferably, the solid adsorption and / or the solid desorption can be combined with a heat exchanger. As a result, the thermal energy emitted during the adsorption can be advantageously utilized, preferably for the desorption step.Particularly preferably, at least two of the aforementioned water separation methods can be combined with one another. Particularly preferably, drop deposition can be combined with thermal water deposition or drop deposition with compression. Such a combination of different water separation methods advantageously leads to an increased yield of separated water.The heat exchanger can be in particular a shell-and-tube heat exchanger or a plate heat exchanger. When tube bundle heat exchangers were used, a reduced pressure loss was found to be advantageous, among other things. Plate heat exchangers have an advantageously smaller overall size. In an advantageous configuration of the shell-and-tube heat exchanger, the exhaust gas stream is guided within the shell-and-tube bundles, while the heat transfer fluid is guided outside the shell-and-tube bundles. In another advantageous configuration of the shell-and-tube heat exchanger, the exhaust gas stream is guided outside the shell-and-tube bundles, while the heat transfer fluid is guided inside the shell-and-tube bundles.In water separation methods in which thermal energy is released or can be absorbed, at least one heat exchanger is most preferably used in order to supply the thermal energy extracted from the exhaust gas stream and / or the water and / or the water vapor to a further process. Particularly preferably, the aforementioned thermal energy can be used for the above-described preheating of the hydrogen-containing gas according to the invention before it is introduced into the reduction reactor. Additionally or alternatively, the thermal energy can also be used for the operation of the reformer and / or for preheating the iron ore. The heat exchanger can be in fluid communication with the reformer of the reduction device, a heating device of the reduction device for the hydrogen-containing gas and / or a heating device of the reduction device for the iron ore via a heat transfer fluid.Preferably, the water separation takes place after a gas scrubbing of the exhaust gas stream. For this purpose, the reduction device according to the invention can have a gas scrubbing device. In the gas scrubbing device, the exhaust gas stream is brought into contact with a liquid stream, in particular with water or preferably lime milk, in order to absorb constituents of the exhaust gas stream in the liquid. The gas scrubbing device is particularly preferably designed as a spray scrubber or vortex scrubber, in particular as a spray scrubber in countercurrent.Further preferably, this gas scrubbing device can have at least one heat exchanger. Likewise preferably, after the gas scrubbing, the water is separated off by means of a droplet separator described above. More preferably, the water thus separated has suspended solids of more than 800 ppmw. The water separated may have suspended solids in the range ≥ 800 ppmw and ≤ 2500 ppmw, or ≥ 1200 ppmw and ≤ 2000 ppmw.According to the invention, the separated and / or the collected water is processed in step d) of the method according to the invention for at least one specific use. Preferably, the water can be processed to provide service water and / or drinking water. The term "treatment for a specific use" can be understood to mean that the water is not disposed of-for example via the waste water-after separation from the waste gas stream. Likewise, the term "treatment for a specific use" can be understood to mean that the treated water can be used directly and / or without a further treatment.The term "service water" is understood to mean water that can be used in at least one specific application. This application is preferably a technical, agricultural and / or domestic application. "service water" cannot be suitable for human consumption. The term "drinking water" is understood to mean water which is suitable for human consumption and / or meets the legal requirements applicable thereto.The service water is particularly preferably partially demineralized or demineralized water, deionized water, water as a heat fluid having a temperature > 30° C., preferably ≥ 50° C., sanitary water, cooling water, in particular for industrial and / or energy plants, water for steam generation, in particular high-pressure steam generation, water for concrete production, sterilized water and / or water for electrolysis for the purpose of hydrogen production.The term "treatment" or "water treatment" can be understood to mean the targeted change in the water quality and / or water composition. Any suitable water treatment device can be used here. In particular, this can be understood to mean the targeted change in the water quality and / or water composition for at least one specific use of the water. The treatment of the water can relate to the removal of substances from the water and / or the addition of substances into the water and / or the setting of parameters of the water, for example the pH, the concentration of specific ions and / or the conductivity.The substances to be removed can be solids and / or metals or dissolved metal salts thereof. The metals are preferably transition metals, preferably iron, manganese, cadmium, chromium, nickel, mercury and / or zinc. Alternatively or additionally, the metals can be heavy metals, preferably lead, and / or alkaline earth metals, preferably calcium and / or magnesium. Alternatively or additionally, they can be chlorine-containing and / or sulfur-containing and / or phosphorus-containing and / or nitrogen-containing substances, in particular nitrites, nitrates, ammonia or ammonium, preferably chlorides and / or sulfates and / or phosphates. Alternatively or additionally, they can be biological substances, preferably microorganisms, such as bacteria and / or viruses and / or bacterial toxins. Alternatively or additionally, they can be organic carbons.The substances to be added can be chlorine or chloride ions, and / or ozone and / or H + or OH -.After treatment at 20° C., the water can have an electrical conductivity in the range of ≥0.005 and ≤0.05 S / m. The water may have an electrical conductivity of ≤1.1 μS / cm or 0.2 μS / cm at 20° C. The water may have an electrical conductivity of ≤3000 μS / cm, ≤280 μS / cm, ≤2500 μS / cm, ≤2000 μS / cm, ≤1300 μS / cm, or ≤0.1 μS / cm at 25° C.The water after treatment may have a TOC (sum of total organic carbon in mg / l) of ≤ 27, ≤ 20, ≤ 10, ≤ 7, ≤ 5, ≤ 3, ≤ 1 or ≤ 0.1.After treatment, the water can have a pH of ≤10. Preferably, the water after treatment can have a pH of ≤9.5, ≤9.0, ≤8.5, ≤8.5 or ≤8.5. Likewise preferably, the pH of the water after treatment can be in a range of ≥6.0 and ≤9.5, ≥6.5 and ≤9.5, ≥6.5 and ≤8.5, ≥7.0 and ≤8.5, ≥7.5 and ≤8.5, or ≥6.0 and ≤8.0. The pH of the water after treatment may furthermore be in a range of ≥7.1 and ≤7.5 or 7.3.After treatment, the water can have an iron content of ≤5.0 mg / l, ≤3.0 mg / l, ≤1.8 mg / l, ≤1.5 mg / l or ≤0.2 mg / l. Alternatively or additionally, the water after treatment can have a sulfate content of ≤250 mg / l or ≤200 mg / l. Alternatively or additionally, the water after treatment may have a zinc content of ≤2.0 mg / l or ≤1.0 mg / l. Alternatively or additionally, the water after treatment can have a chlorine or chloride content of ≤250 mg / l or ≤200 mg / l.Alternatively or additionally, the water after treatment may have a nitrite nitrogen content of ≤50 mg / l, ≤5.0 mg / l or ≤0.5 mg / l.Alternatively or additionally, the water after treatment may have a TOC of ≤ 10.0 mg / l, ≤ 7 mg / l or ≤ 5 mg / l.Alternatively or additionally, the water after treatment may have a phosphorus content of ≤2.0 mg / l or ≤0.10 mg / l.Alternatively or additionally, the water after treatment may have a lead content of ≤0.5 mg / l, ≤0.01 mg / l or ≤0.005 mg / l.Alternatively or additionally, the water after treatment may have a nickel content of ≤0.5 mg / l or ≤0.02 mg / l.Alternatively or additionally, the water after treatment may have a copper content of ≤2.0 mg / l or ≤0.5 mg / l.Alternatively or additionally, the water after treatment may have a chromium content of ≤0.5 mg / l, ≤0.025 mg / l or ≤0.005 mg / l.Alternatively or additionally, the water after treatment may have a cyanide content of ≤0.4 mg / l or ≤0.05 mg / l.Alternatively or additionally, the water after treatment can have a value ≤0.62 in the fish egg test (measured according to DIN EN ISO 15088).Alternatively or additionally, the water after treatment may have an ammonium content of ≤0.5 mg / l, ≤0.2 mg / l or ≤0.1 mg / l.Alternatively or additionally, the water after treatment can have an ammonia content of ≤2 mg / l.Alternatively or additionally, the water after treatment can have a content of filterable substances of ≤30 mg / l or ≤20 mg / l.Alternatively or additionally, the water after treatment can have a BOD 5( biochemical oxygen requirement; measured preferably according to DIN EN 1899-1 and 1899-2 or by means of the saproma method)≤0.4 mg / l.Alternatively or additionally, the water after treatment may have a mercury content of ≤0.001 mg / l.Alternatively or additionally, the water after treatment can have a selenium content of ≤0.01 mg / l.Alternatively or additionally, the water after treatment can have a nitrate nitrogen content of ≤50 mg / l.Alternatively or additionally, the water after treatment may have a sodium content of ≤1200 mg / l, ≤700 mg / l or ≤200 mg / l.Alternatively or additionally, the water after treatment may have a manganese content of ≤0.005 mg / l.Alternatively or additionally, the water after treatment may have an arsenic content of ≤0.01 mg / l or 0.004 mg / l.Alternatively or additionally, the water after treatment may have a uranium content of ≤0.01 mg / l.A large number of water treatment processes which can be used for step d) of the process according to the invention are known to the skilled worker. Any suitable water treatment device can be used for the water treatment.The water treatment can preferably take place via sedimentation, in particular by means of a settling basin and / or by means of a centrifuge. The water treatment can alternatively or additionally be effected via flocculation, in particular using sodium hydroxide solution or particularly preferably lime milk as flocculant. If these two water treatment methods are combined with one another, then preferably first flocculation and then sedimentation can be carried out. During flocculation, the desired pH of the water can be adjusted.Alternatively or additionally, the water treatment can be effected by precipitation. Dissolved substances are converted into undissolved substances and these can preferably subsequently be removed from the water via flocculation and / or sedimentation.Alternatively or additionally, the water treatment can be effected by flotation, i.e. by blowing in a gas, in particular air.Alternatively or additionally, the water treatment can be effected by filtration. Particularly preferably, a sand filter, a gravel filter or an activated carbon filter can be used as filter.Alternatively or additionally, the water treatment can be effected by sieving, in particular by means of a microscreen.Alternatively or additionally, the water treatment can be effected by oxidation, in particular using a ventilation system for blowing in air and / or oxygen and a gravel filter. This method can serve in particular for the removal of dissolved iron ions and / or manganese ions.Alternatively or additionally, the water treatment can be effected by disinfection. Chlorine, chlorine dioxide and / or ozone can preferably be added to the water. Alternatively or additionally, irradiation with electromagnetic waves, in particular in the UV range, can be carried out for disinfection.Alternatively or additionally, the water treatment can be carried out via reverse osmosis and using a reverse osmosis unit with osmosis membrane.After the water treatment in step d) of the method according to the invention, in a further step e) the treated water can be supplied to at least one dispensing point. Particularly preferably, the supply can be effected to a plurality of different dispensing points. A dispensing point can preferably be a water consumer. A delivery point can also be referred to as a transfer point. The dispensing point is at least characterized in that it is located at a position different from the position at which the treatment of the water takes place, for example the water treatment device of the water extraction device according to the invention.A feed line can be understood in particular to mean the directed transport of the water to the discharge point. Furthermore, a feed line can be understood to mean the active transport of the water to the discharge point, for example using a pump. A feed line can furthermore be understood to mean that the water is transported on the transport path to the discharge point in a closed system and / or does not come into contact with the environment. Preferably, the water reaches the dispensing point with the substantially identical composition that it has after the treatment in step d) of the method according to the invention. The supply line to the dispensing point can preferably be effected by means of pipelines, hoses, pumps and / or vehicles.Before the treated water is supplied to the dispensing point, the water can be stored and / or portioned in a water reservoir. The water reservoir can be any suitable container which can furthermore be designed to be closed off from the environment or not closed off. Preferably, the water reservoir may be an artificial or a natural water reservoir. The water reservoir can be located above ground or underground. Water reservoirs arranged above ground, in particular when they are designed as high tanks, have the advantage that the water can be supplied to the discharge point using gravity.Particularly preferred water accumulators, in particular artificial water accumulators, are water tanks, water accumulator basins, high tanks, water towers or cisterns. The water reservoir can further preferably be thermally insulated. This is advantageous in particular when the water is to be used as heated heat fluid or for steam generation.The dispensing point and / or the water consumer can be part of the water extraction device according to the invention or not part of the water extraction device according to the invention. For example, the consumer can be designed as the previously described gas scrubbing device.The treated water can be supplied to the dispensing point over a distance of at least 50 m. The supply can preferably be effected over a distance of ≥500 m, ≥1 km, ≥5 km, ≥10 km, ≥500 m and ≤100 km, or ≥500 m and ≤200 km.This has the advantage that water consumers which are arranged in the spatial vicinity of the water extraction device according to the invention can be supplied with water in an economical and environmentally friendly manner.The water consumer is an industrial consumer, in particular a consumer from the textile industry or the paper industry. The water consumer may be an agricultural consumer or a livestock consumer. Both industrial and agricultural and livestock consumers have a high water requirement. The invention provides these water-intensive economic branches with the valuable raw material water. In particular, this may be advantageous in arid regions or regions with water shortage.Furthermore, the consumer can be a cooling system, in particular the cooling system of a steel processing plant. The cooling system can be an open or a closed water cooling system and can be designed in particular as a laminar cooling section.Alternatively or additionally, the water consumer can be a descaling device, in particular the descaling device of a steel processing plant.Alternatively or additionally, the water consumer can be a slag granulation device, in particular a slag granulation device of a steel processing plant.Alternatively or additionally, the transfer point and / or the water consumer can be a steam reformer, in particular a steam reformer of a steel processing plant.Alternatively or additionally, the water consumer can be an electrolysis device, in particular an electrolysis device for electrolysis of the supplied water using regenerative energy and / or an electrolysis device of a steel processing plant.Alternatively or additionally, the transfer point and / or the water consumer can be a fluid heating system, in particular a fluid heating system of a steel processing plant or a district heating network. The fluid heating system can preferably have at least one heat exchanger. The heat energy stored in the supplied water can be removed by the heat exchanger and used further for heating purposes.Alternatively or additionally, the transfer point and / or the water consumer can be a water reservoir, in particular a drinking water reservoir or the water reservoir of a steel processing plant. The water reservoir can preferably have at least one pump. The pump can lead in and / or lead off the water.Alternatively or additionally, the transfer point and / or the water consumer can be a clarifier, a water mill and / or a pressure-increasing system of a water network, in particular of a drinking water network.Alternatively or additionally, the transfer point and / or the water consumer may be a mining or textile manufacturing company. Companies of this type are distinguished by an increased water requirement, for example in the processing of metallic ores or in the dyeing of textiles.The invention further relates to a device for providing water, comprising at least one reduction reactor for reducing an oxidic ore, in particular an iron ore, with reaction of a hydrogen-containing gas, wherein the reduction reactor comprises a first outlet for an exhaust gas stream. The apparatus according to the invention furthermore has a first separation device for separating at least part of the water from the exhaust gas stream (which can also be referred to as a water separation device), wherein the first separation device is in fluid communication with the first outlet. Furthermore, the apparatus according to the invention has at least one first water treatment device for treating the water separated by means of the separation device, wherein the first water treatment device is in fluid communication with the first separation device. The device according to the invention can also be referred to as a water extraction device.If the suitability of a device, a system or a device is described in this application, it is therefore preferably also included that the device or device is configured for the stated purpose. In other words, the device according to the invention can be not only suitable, but also configured to provide water according to the method according to the invention described above, or to carry out the method described above. For example, the reduction reactor can be configured for reducing an iron ore, with reaction of a hydrogen-containing gas. For example, the separation device can likewise be configured to separate at least part of the water from the exhaust gas stream. For example, the water treatment device can likewise be configured for treatment of the water separated by means of the separation device, in particular with regard to the previously described composition of the treated water.A fluid connection can be understood to mean that a fluid, in particular the exhaust gas flow, is conducted between the two mentioned devices and / or has a transport direction between the two mentioned devices and in particular from the second to the first mentioned device. The fluid connection can be indirect or direct. In the case of an indirect fluid connection, at least one further device which is fluidically connected to the two said devices is arranged between the two said devices. For example, when the first separation device is in fluid communication with the first outlet, the exhaust gas stream is directed from the first outlet to the first separation device and / or the exhaust gas stream has a transport direction from the first outlet to the first separation device.Furthermore, the devices described with reference to the method, such as for example reduction reactor, separation device or water treatment device, also apply to the device described below that described below and / or the use described below.The reduction reactor can be at least one direct reduction reactor or a direct reduction device, or at least one melt reduction reactor or a melt reduction device. In particular, the reduction reactor can be at least one shaft furnace and / or at least one fluidized bed reactor. The direct reduction device can be, in particular, a direct reduction device which is configured to carry out the Midrex method, the Circuit method or the Hyfor method.The reduction reactor may have a filling opening for filling the reduction reactor with the iron ore. The filling opening can be arranged at the top of the reduction reactor, for example in the upper eighth of the reduction reactor. A transport device for supplying the oxidic ore can be arranged upstream of the filling opening. The transport device can be configured in particular to transport iron ore in solid form, in particular as piece goods. An exemplary and preferred transport device may be a conveyor belt.The reduction reactor can furthermore have a removal opening for the reduced iron ore, in particular liquid reduced iron ore or pig iron. The removal opening can be arranged at the base of the reduction reactor, for example at the lower eighth and / or at the lowest point of the reduction reactor.The reduction reactor may further comprise a first inlet for the hydrogen-containing gas. The first inlet may be located in the middle third of the reduction reactor. The first outlet for the offgas stream of the hydrogen-containing gas can be arranged in the upper third, in the upper quarter or in the upper fifth of the reduction reactor.The reduction reactor can have a second inlet for a cooling gas, in particular a hydrogen-containing cooling gas, such as natural gas, for example. The second inlet can be arranged in the lower third, in the lower quarter or in the lower fifth of the reduction reactor. The reduction reactor may have a second outlet for the exhaust stream. This second outlet can be arranged in the lower half or in the lower third of the reduction reactor. In particular, the second outlet can be arranged above the second inlet. Preferably, this further outlet can be an outlet for the aforementioned cooling gas which is blown into the reduction reactor during the reduction reaction.The second outlet and the second inlet can be part of a cooling circuit, wherein the second outlet and the second inlet can be fluidically connected. The cooling circuit of the device according to the invention can have further elements which are described below.The second outlet can be in fluid communication with the first and / or preferably a second separation device for separating at least part of the water from the exhaust gas stream. The second separation device can thus be referred to as part of the cooling circuit. The second separation device may be disposed between the second outlet and the second inlet. The second separation device can be in fluid communication with the first and / or preferably a second water treatment device. The second water treatment device may be disposed between the second separation device and the second inlet.A compressor can be arranged between the second separation device and the second inlet, in particular between the second water treatment device and the second inlet. The compressor may be in fluid communication with the second separation device or the second water treatment device and the second inlet. The compressor can thus be referred to as part of the cooling circuit.The second separation device, as well as a compressor in fluid communication therewith, can each be in thermal contact with a heat exchanger. As a result, the thermal energy of the cooling gas exiting from the reduction reactor can advantageously also be used further, or the cooling gas can be cooled.The first and / or second separation device can be, as described above, a droplet separator, in particular a lamella separator or preferably a rotary separator. As also described above, the separators of the invention may be in thermal contact with a heat exchanger.The first and / or second separation device can be configured to reduce the residual water content in the exhaust gas stream to ≤7 vol %. As stated above, the first and / or second separation device can also be configured to reduce the residual water content in the exhaust gas stream to ≤5 vol % or preferably ≤3 vol %. The first and / or second separation device can likewise be configured to reduce the residual water content in the exhaust gas stream to a range of >1 vol % and <5 vol % or preferably >1.5 vol % and<3 vol %.The apparatus according to the invention can have at least one first gas scrubbing device which is in fluid communication with the first outlet. The first gas scrubbing device can be configured to clean the exhaust gas stream led out of the reduction reactor. The apparatus according to the invention can furthermore have a second gas scrubbing device which is in fluid communication with the second outlet and which can be configured to clean up the exhaust gas stream of the cooling gas.Preferably, the first gas scrubbing device is arranged between the first outlet and the first separation device. In this case, the first gas scrubber is in fluid communication with the first outlet and the first separation device. Likewise preferably, the second gas scrubbing device is arranged between the second outlet and the second separation devices. In this case, the second gas scrubber is in fluid communication with the second outlet and the second separation device.The device according to the invention for providing water can furthermore have a reformer. In the reformer, longer-chain hydrogen-containing gas, for example natural gas and / or methane, can be split into hydrogen under the action of heat. Air can also be supplied to the reformer. Additionally or alternatively, hydrogen-containing gas can be supplied to the reformer from the first separation device and / or the second separation device. The first inlet of the reduction reactor may be fluidly connected to an outlet of the reformer.Particularly preferably, the device according to the invention cannot have a reformer. This is the case in particular when hydrogen is used as the hydrogen-containing gas. In this case, the cooling circuit, or the second inlet, the second outlet and the possible devices for the cooling gas lying therebetween, can likewise be dispensed with.The device according to the invention can furthermore have a heating device, for example an electric heater. The first inlet of the reduction reactor may be fluidly connected to an outlet of the heater. The heating device can be arranged between the reformer and the first inlet. The heating device can likewise be part of the reformer and have a gas burner which is fired with a part of the exhaust gas stream emerging from the first separation device.The water treatment device of the apparatus according to the invention can be a precipitation device, a flocculation device, a sedimentation device, a flotation device, a filtration device, an oxidation device, a disinfection device and / or a reverse osmosis device. The water treatment device can be configured to modify the water quality or water composition in a targeted manner. The water treatment device can be configured, for example, to remove certain substances, such as ions, from the water and / or add them thereto. In particular, the water treatment device can be configured to treat the water for a specific use. In particular, the water treatment device can be configured to provide service water and / or drinking water. In order to avoid repetitions, reference is made to the statements regarding the method according to the invention.The apparatus according to the invention can furthermore have at least one feed device for feeding the treated water to at least one discharge point. The supply devices can have at least one, preferably at least two or three, or all elements selected from the group consisting of pipelines, water reservoirs, hoses, valves and / or pumps. The supply devices can be in particular in fluid communication with a previously mentioned dispensing point and / or consumer. The pump can be designed to distribute the water to at least two dispensing points and / or consumers. The pump can likewise be a component of a distribution device which is designed to distribute the water to at least two dispensing points and / or consumers. For this purpose, the distribution device can have one or more valves, and a corresponding number of outgoing fluid connections, which are in fluid communication with at least one water consumer in each case. This makes it possible to ensure the supply of water consumers in any combination.The supply device can be designed to bridge a supply path of the water of at least 50 m. The supply device can be designed to bridge a supply path of the water of ≥500 m, ≥1 km, ≥5 km, ≥10 km, ≥500 m and ≤100 km, or ≥500 m and ≤200 km.According to the invention, a system consisting of the device according to the invention is thus also provided, which is fluidically connected to at least one water consumer via at least one feed device. Exemplary and preferred water consumers are specified above with regard to the method according to the invention.The invention thus also relates to the use of the device according to the invention or of the system according to the invention for supplying water.Further advantages, details and features of the invention are evident below from the explained exemplary embodiments. In this context, the following show in detail: FIG. 1 : a first embodiment of the device according to the invention as a component of a steel processing plant which is set up for the direct reduction of iron ore in the Midrex method. FIG. 2 : shows a second embodiment of the device according to the invention as a component of a steel processing plant which is set up for the direct reduction of iron ore in the Midrex method. Only the relevant section showing the differences compared to the first embodiment is shown. In particular, the device has a plurality of water consumers which are part of the steel processing installation. FIG. 3 : a third embodiment of the device according to the invention as a component of a steel processing plant which is set up for the direct reduction of iron ore in the Midrex method. Only the relevant section showing the differences compared to the first or second embodiment is shown. In particular, the device has a water consumer which is not a component of the steel processing installation. FIG. 4 : a fourth embodiment of the device according to the invention as a component of a steel processing plant which is set up for the direct reduction of iron ore in the Midrex method. Only the relevant section showing the differences compared to the first to third embodiments is shown. In particular, the device has both a water consumer which is a component of the steel processing installation and a further consumer which is not a component of the steel processing installation.In the description which follows, the same reference numerals designate the same components or the same features, so that a description with respect to a component carried out with respect to a figure also applies to the other figures, so that a repetitive description is avoided. Furthermore, individual features which have been described in connection with an embodiment can also be used separately in other embodiments.FIG. 1 shows a first embodiment of the device according to the invention for supplying water, wherein this is used as a component of a steel processing plant 170, 171 which is set up for the direct reduction of iron ore in the Middlex method.The device comprises a reduction reactor 10, which is a component of a direct reduction device and which is designed as a shaft furnace 11. Within the reduction reactor 10, the direct reduction of an iron ore supplied in pellet form takes place with reaction with a hydrogen-containing gas. The iron ore supplied to the reduction reactor 10 has a degree of metallization in the range of ≥ 0% and ≤ 5%.The iron ore is supplied via the filling opening 15 to the reduction reactor 10, which is arranged in the upper eighth of the reduction reactor 10. A transport device, not shown, in the form of a conveyor belt is arranged upstream of the filling opening 15, by means of which transport device the iron ore is fed from a bunker to the filling opening 15. The directly reduced iron ore or pig iron with a degree of metallization in the range of ≥60 and ≤99% leaves the reduction reactor 10 via the removal opening 16, which is arranged in the lower eighth of the reduction reactor 10.The reduction reactor 10 furthermore has a first outlet 13 for the exhaust gas stream which is formed during the direct reduction of the iron ore with the hydrogen-containing gas. The first outlet 13 is arranged in the upper fifth of the reduction reactor 10 and can also be referred to as a "top gas" or top gas outlet.The apparatus further includes a first separation device 20 in fluid communication with the first outlet 13 via a fluid connection for the exhaust gas flow 40, 41. Accordingly, the exhaust gas stream flows from the first outlet 13 to the first separation device 20.The first separation device 20 is furthermore in thermal contact with a heat exchanger 110 which is designed as a shell-and-tube heat exchanger 111. The transfer of the thermal energy from the exhaust gas stream to the heat transfer medium of the heat exchanger 110 promotes the separation of the water from the exhaust gas stream. Furthermore, the thermal energy removed can advantageously be used elsewhere, for example for preheating the hydrogen-containing gas and / or for preheating the iron ore fed to the reduction reactor 10.The exhaust gas stream treated in the first separation device 20 then flows via the fluid connection 40, 45 to at least one compressor 120, which is likewise in thermal contact with a heat exchanger 110. The exhaust gas stream compressed by means of the compressor 120 is then fed to a reformer 130, which is designed as a steam reformer, methane gas being added to the exhaust gas stream via the fresh gas feed 140, 141. The methane gas mixed in is methane gas from a regenerative source, for example biomethane gas. A portion of the exhaust gas stream discharged from the first separation device 20 is furthermore supplied to the reformer 130, this exhaust gas stream being branched off upstream of the compressor 120. Both biomethane gas and air are added to this partial exhaust gas stream via the fresh gas feed 140, 141, 143. The gas mixture thus generated is burned in the reformer 130 by means of a gas burner and serves to provide the thermal energy required for the reforming process.The gas mixture exiting from the reformer 130 via the outlet 131 flows via the fluid connection 40, 46 to the first inlet of the reduction reactor for hydrogen-containing gas 17. The first inlet of the reduction reactor 17 is arranged in the middle third of the reduction reactor 10.Thus there is a circulation of the exhaust gas flow which leads from the first outlet 13 to the first inlet 17 of the reduction reactor. Within the cycle, the exhaust gas stream is freed of a major part of the water vapor contained therein and enriched with fresh gas in order thereafter to be provided again as hydrogen-containing gas for use in the reduction reactor 10.Also shown is a gas scrubbing device 100, which can also be referred to as a "scrubber" or "top gas scrubber". The gas scrubbing device is designed as a spray scrubber in countercurrent and is arranged in the exhaust gas flow circuit between the first outlet of the reduction reactor 13 and the first separation device 20, i.e. is fluidically connected in each case to the outlet 13 and to the separation device 20. In the gas scrubber 100, the exhaust gas stream is contacted with lime milk to receive components of the exhaust gas stream therein.The hydrogen-containing gas which is introduced into the reduction reactor 10 via the first inlet 17 is a synthesis gas mixture which, with respect to the components total hydrogen content, carbon monoxide content, steam content and carbon dioxide content, has a distribution in which the ratio of these components ((H 2+ CO) / (H 2 O+CO 2)) ≥10.The device according to the invention of the first embodiment further comprises a cooling circuit. By means of hydrogen-containing gas (cooling gas) injected into the reduction reactor 10, the temperature of the direct reduction device is controlled, i.e. lowered. The cooling gas is likewise converted here and leaves the reduction reactor 10 as an exhaust gas stream via the second outlet 14. Via the fluid connection 40, 43, this exhaust gas stream then flows to a second separation device 25, which is likewise configured to separate at least part of the water from this exhaust gas stream. The second separation device 25 is also designed as a rotary separator 26. The water separated from the exhaust gas stream by means of the second separation device 25 can be supplied via a fluid connection, not shown, to the first water treatment device 30 described below and / or to a second water treatment device.The exhaust gas stream leaving the second separation device 25 flows via a fluid connection to the compressor 121 and is compressed here. The compressed exhaust gas stream leaving the compressor 121 is then conducted via the fluid connection 40, 44 to the second inlet of the reduction reactor 18 and at this point injected as cooling gas into the reduction reactor 10. In this case, biomethane gas is added beforehand to the exhaust gas stream via the fresh gas feed 140, 141.The water separated off via the first separation device 20 has a temperature of > 30° C. and suspended solids with a concentration of ≥ 800 ppmw. It is supplied to the first water treatment device 30 via the fluid connection 40, 42.The first water treatment device 30 is configured to provide service water. In particular, the first water treatment device 30 is configured to change the water composition in a targeted manner for at least one specific use of the water, namely as water for use in a laminar cooling section 61.In particular, the first water treatment device 30 is configured to provide water having a pH value in the range of ≥7.5 and ≤8.5 at 20° C. Furthermore, the first water treatment device 30 is configured to provide water having an electrical conductivity (at 20° C.) of ≤ 2500 uS / cm. Furthermore, the first water treatment device 30 is configured to provide water which has an iron content of ≤1.5 mg / l, which has a chloride content (Cl -) of ≤200 mg / l and which has an ammonium content (NH 3+ NH 4) of ≤0.1 mg / l.The adjustment of the water composition by means of the first water treatment device 30 is effected inter alia via precipitation, followed by flocculation, which is effected with milk of lime as flocculant. During flocculation, the desired pH of the water is also adjusted.The device according to the invention further comprises a supply device 50, via which the water treated via the first water treatment device 30 is supplied to a water consumer 60 in the form of a laminar cooling section 61, which is located within the steel processing plant 170 or is a component thereof. The supply device has a water reservoir 150, which is in fluid contact with the first water treatment device 30 via the fluid connection 40, 47. This fluid connection is designed as a pipeline 48. The water reservoir 150 serves for intermediate storage of the separated water and can have a further inlet (not shown) for suitable service water. This ensures that the laminar cooling section 61 can be supplied with sufficient service water / cooling water at any time.The laminar cooling section 61 is in fluid communication with the water reservoir 150 via the fluid connection 40, 47, 48, i.e. likewise via a pipeline. Furthermore, a pump 160 is part of this fluid connection, which ensures that the water reaches from the water reservoir 150 to the water consumer 60, or the laminar cooling section 61.FIG. 2 shows a second embodiment of the device according to the invention for supplying water, wherein only the differences compared to the first embodiment from the fluid connection 40, 42 from the first separation device 20, 21 to the first water treatment device 30 are shown. The other components of the direct reduction device of the steel mill 170, 171 are identical to those of the first embodiment.Again, the first water treatment device 30 can be seen, which is configured to provide service water, as is described for the first embodiment of the invention. Likewise, the processed service water is first conducted to a water reservoir 150 via the fluid connection 40, 47, which is designed as a pipeline 48. The water reservoir 150 may also have a further feed (not shown) for suitable service water.The water reservoir 150 is again connected via a supply device 50 to water consumption 61, which is a plurality in this case. In particular, the water reservoir 150 is connected via a pipeline 48 to a distribution device 161, which has a pump. Proceeding from this distributor device, further fluid connections, which are designed as a pipeline 48, run to various water consumers 60 of the steel processing installation 170. The laminar cooling section 61 also present in the first embodiment is shown on the one hand. A descaling device 62 is shown as a further water consumer, and any desired third water consumer 60 of the steel processing plant 170.FIG. 3 shows a third embodiment of the device according to the invention for supplying water, wherein only the differences compared to the first or second embodiment from the fluid connection 40, 42 from the first separation device 20, 21 to the first water treatment device 30 are shown. The other components of the direct reduction device of the steel mill 170, 171 are identical to those of the previous embodiments.The first water treatment device 30 can be seen again, which, in contrast to the first or second embodiment, is configured to provide drinking water.In particular, the first water treatment device 30 is configured to provide water having a pH value in the range of ≥6.5 and ≤9.5 at 20° C. Furthermore, the first water treatment device 30 is configured to provide water having an electrical conductivity (at 25° C.) of ≤280 uS / cm or ≤2790 uS / cm. Furthermore, the first water treatment device 30 is configured to provide water having, among other things, an iron content of ≤0.2 mg / l, a chloride content (Cl -) of ≤250 mg / l, a lead content of ≤0.01 mg / l or ≤0.005 mg / l, a nickel content of ≤0.02 mg / l, a mercury content of ≤0.001 mg / l, a nitrate nitrogen content of ≤50 mg / l, a nitrite nitrogen content of ≤0.5 mg / l, an arsenic content of ≤0.01 mg / l or 0.004 mg / l and a copper content of ≤2.0 mg / l.It can also be seen that the first water treatment device 30 is also fluidically connected to a water consumer 60 via a feed device 50. The supply device 50 likewise has fluid connections 40, 47 in the form of pipelines 48, and a pump 160. It can also be seen that the fluid connection 49, which connects to the pump 160, is designed as a pipeline which is fluidically connected to a water consumer 60 located outside the steel processing installation 170. In particular, the supply line device 50 is designed to bridge a supply line section up to the water consumer 60, which is at least ≥1 km. In other words, the water consumer 60 is located at a distance of approximately at least 1 km from the first water treatment device 30.In the case of the third embodiment, the water consumer 60 is a water station or a pressure increase system 64 of a drinking water network.FIG. 4 shows a fourth embodiment of the device according to the invention for supplying water, wherein only the differences compared to the first to third embodiments from the fluid connection 40, 42 from the first separation device 20, 21 to the first water treatment device 30 are shown. The other components of the direct reduction device of the steel mill 170, 171 are identical to those of the previous embodiments.It is again possible to see the first water treatment device 30, which, in contrast to the first or second embodiment, is configured to provide service water, in particular water for electrolysis for the purpose of hydrogen production. In other words, the water is partially demineralized, preferably demineralized water or deionized water.For this purpose, the first water treatment device 30 can have, inter alia, a reverse osmosis unit, and mixed-bed ion exchange cylinders or a continuous electrodeionization (CEDI) unit.It can be seen again that the first water treatment device 30 is likewise fluidically connected to a water consumer 60 via a feed device 50. The supply device 50 likewise has fluid connections 40, 47 in the form of pipelines 48, and a distribution device 161 having a pump.From the distribution device, two fluid connections 40, 47 can be seen, which are each designed as pipelines 48 and are in fluid communication with water consumers 60. Both of these water consumers are electrolysis devices 65, wherein the first electrolysis device 65 is part of the steel processing plant 170, while the second electrolysis device 65 is not part of the steel processing plant 170 but is arranged at a distance of at least approximately 1 km from it.In a fifth to seventh and not illustrated embodiment of the invention, the embodiments illustrated in FIGS. 2 to 4 are each part of a steel processing installation 170 which is set up for the direct reduction in the circular method.The Circular method is known to the person skilled in the art and the main differences from the Middlex method are discussed below.In embodiments 5 to 7, exclusively H2, in particular green hydrogen, is used as the hydrogen-containing gas for the circulating method. This advantageously lowers the CO2 em.Furthermore, in embodiments 5 to 7, the iron ore is introduced into the reduction device in the form of fine ore or ultra-fine ore and is reduced at an elevated operating pressure-in comparison to the Midrex process. This has the advantage that a higher amount of water is produced in the exhaust gas stream, which can be separated out. The fresh gas used is likewise exclusively H2, in particular green hydrogen.The direct reduction apparatus of the circulating method employed in Embodiments 5 to 7 is composed of two reduction reactors 10 which are arranged sequentially and which are passed through one after another by the iron ore to be reduced. These two reduction reactors are fluidized bed reactors, in particular a circulating fluidized bed (CFB) reactor followed by a blowing fluidized bed (FB) reactor. In the CFB, the iron ore is reduced in about 20-30 minutes to a degree of reduction of 65%-80%. The final reduction with a degree of reduction of 93%-95% takes place in the FB.In embodiments 5 to 7, the use of H2 means that, among other things, a reformer 130, as well as the cooling circuit for the shaft furnace described above for the Midrex method, are no longer required.List of reference characters10 Reduction reactor 11 Shaft furnace 13 First outlet for exhaust gas flow of the reduction reactor 14 Second outlet for exhaust gas flow of the reduction reactor, in particular for cooling gas 15 Filling opening for filling with iron ore 16 Removal opening for reduced iron ore 17 First inlet of the reduction reactor for hydrogen-containing gas 18 Second inlet of the reduction reactor for cooling gas 20 First separation device, in particular droplet separator 21 Rotary separator 25 Second separation device 26 Rotary separator 30 First water treatment device 40 Fluid connection 41 Fluid connection from first outlet to first separation device; Fluid connection for gaseous fluid, in particular exhaust gas flow 42 Fluid connection from first separation device to first water treatment device; Fluid connection for a liquid fluid, in particular separated and treated water 43 Fluid connection of the cooling circuit, in particular from second outlet to second separation device; Fluid connection for gaseous fluid, in particular cooling gas 44 Fluid connection of the cooling circuit, in particular from compressor to second inlet of the reduction reactor; Fluid connection for gaseous fluid, in particular cooling gas 45 Fluid connection for gaseous fluid, in particular exhaust gas stream 46 Fluid connection for gaseous fluid, in particular hydrogen-containing gas 47 Fluid connection for a liquid fluid, in particular separated and processed water 48 Pipe line 49 Pipe line to a discharge point / water consumer 50 Feed device 60 Discharge point, water consumer 61 Cooling system, in particular laminar cooling section 62 Descaling device 63 Further water consumer as a component of the steel processing system 64 Water unit or pressure increasing system of a drinking water network 65 Electrolysis device 100 Gas scrubbing device, in particular as spray scrubber in countercurrent 110 Heat exchanger 111 Shell-and-tube heat exchanger 120 Compressor 121 Compressor 130 Reformer, In particular, steam reformer 131 outlet of reformer 140 fresh gas supply 141 methane gas supply 142 oxygen supply 143 air supply 150 water storage 160 pump 161 distribution device having a pump 170 steel processing plant 171 steel processing plant configured for the direct reduction in the Middlex method

Claims

Method for providing water, comprising the steps: a) introducing a hydrogen-containing gas and an oxidic ore, in particular an iron ore, into at least one reduction reactor (10), b) reducing the oxidic ore with reaction of the hydrogen-containing gas, c) separating at least part of the water from the exhaust gas stream of the at least one reduction reactor, and d) preparing the separated water for at least one specific use.The method according to claim 1, wherein the reduction reactor is a shaft furnace (11) or a fluidized bed reactor.The method of any preceding claim, wherein the oxidic ore is an iron ore and is in a form selected from the group consisting of pellet, lump ore, fine ore, iron oxide-containing powder and mixtures thereof.Method according to one of the preceding claims, wherein after the water separation the residual water content in the exhaust gas stream is ≤ 7 vol.%.The method according to any of the preceding claims, wherein the water separation comprises a droplet separation and / or a thermal water separation and / or a cooling of the exhaust gas flow using a heat exchanger.The method according to any of the preceding claims, wherein the water has a pH ≤ 10, or ≥ 6.5 and ≤ 8.5 by the treatment after step d).The method according to any of the preceding claims, wherein the water has an iron content of ≤ 1.8 mg / l and / or a zinc content of ≤ 2.0 mg / l or ≤ 1.0 mg / l as well as optionally a sulfate content of ≤ 200 mg / l as a result of the treatment according to step d).Method according to any of the preceding claims, wherein the water has a BOD 5 ≤ 4 mg / l, a filterable material content of ≤ 30 mg / l and / or a value of ≤ 0.62 in the fish egg test by the treatment according to step d).The method according to any of the preceding claims, wherein the specific use is the provision of industrial and / or drinking water.The method according to any one of the preceding claims, wherein the treatment of the water is effected via at least one water treatment method selected from the group consisting of: precipitation, flocculation, sedimentation, flotation, filtration, oxidation, disinfection and reverse osmosis.Method according to one of the preceding claims, wherein after step d) the method comprises the additional step: e) supplying the treated water to at least one dispensing point (60), in particular a water consumer, wherein the water has optionally been previously stored in a water storage device (150).Method according to one of the preceding claims, wherein the supply is effected over a distance of at least 50 m.Method according to one of the preceding claims 11 or 12, wherein the dispensing point (60) and / or the water consumer is a cooling system (61), a laminar cooling section, a descaling device (62), a slag granulation device, an electrolysis device (65), a fluid heating system, a water reservoir, a clarifier, a water mill and / or a pressure increasing device (64).Method according to one of the preceding claims 11 to 13, wherein the dispensing point (60) and / or the consumer is part of a steel processing installation (170).Device for supplying water, comprising: - at least one reduction reactor (10) for reducing an oxidic ore, in particular an iron ore, by reacting a hydrogen-containing gas, wherein the reduction reactor has a first outlet (13) for an exhaust gas stream, - at least one first separation device (20) for separating at least part of the water from the exhaust gas stream, wherein the separation device (20) is in fluid communication with the first outlet (13), - at least one first water treatment device (30) for treating the water separated by means of the first separation device, wherein the first water treatment device (30) is in fluid communication with the first separation device (20).The apparatus of claim 15, wherein the apparatus is configured to perform the method of any one of claims 1 to 14.The device according to any one of claims 15 or 16, wherein the device comprises at least one supply device (50) which is in fluid communication with at least one water consumer (60), and wherein the at least one water consumer (60) is selected from the group consisting of a cooling system (61), in particular a laminar cooling section, a descaling device (62), a slag granulation device, an electrolysis device (65), a fluid heating system, a water reservoir, a clarifier, a water mill and / or a pressure increasing device (61).The apparatus of claim 17, wherein the water consumer (60) is part of a steel processing plant (170).System comprising an apparatus according to one of Claims 15 to 16, at least one feed device (50), and at least one water consumer (60), wherein the apparatus is fluidically connected to the at least one water consumer (60) via the at least one feed device (50).Use of a device according to any one of claims 15 to 18 or the system according to claim 19 for supplying water.

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