Abstract: The present disclosure relates to an aircraft and to a method using this aircraft to inspect equipment in coking plants for detecting sources of error. The aircraft has at least one inspection device for inspecting surfaces of the equipment that are to be inspected, and an airspace, distanced from one of the surfaces to be inspected, and at least one transmitting and receiving device for data communication with at least other aircraft or at least one external analysis device for detecting the sources of error. The method comprises converting the detected phototechnical and optical data, in particular 2D data, into a 3D thermal point cloud by means of a conversion unit of the analysis device.

Abstract: A gas scrubber may include an absorption apparatus configured for receiving a gas and absorbing the gas in an absorption medium, as well as an evaporation apparatus configured for evaporating at least a part of the liquid that is introduced. The absorption apparatus may have an introduction apparatus for the gas, an apparatus for circulating the absorption solution that has reacted with the gas, a discharge apparatus for at least a part of the absorption solution that has reacted with the gas, and a cooling system for the circulating absorption solution. The absorption apparatus and the evaporation apparatus can be connected via a heat exchanger such that heat content of the absorption solution that has reacted with the gas is used at least in part for the evaporation.

Abstract: A method can be used to cool bulk material in a fine material cooler. The method may involve admitting bulk material to be cooled into the fine material cooler through a material inlet, conveying the coarse material with a first mechanical or pneumatic conveying unit, and conveying the fine material with a second conveying unit in a conveying direction through the fine material cooler to a material outlet. The bulk material may have a fine material proportion of 70% to 95% and a coarse material proportion of 5% to 30%. The fine material may have a grain size of 10-5 mm to 4 mm, and the coarse material may have a grain size of 4 mm to 100 mm.

Abstract: Processes and plants for producing cement clinker, in which an oxygen-containing gas having a proportion of 15% by volume or less of nitrogen and a proportion of 50% by volume or more of oxygen is conveyed from a first section of the cooler directly adjoining the top of the furnace into the rotary furnace and is optionally additionally conveyed to the calciner, and where the total gas streams fed in to the combustion processes consist to an extent of more than 50% by volume (preferably more than 85% by volume) of oxygen.

Abstract: The present disclosure relates to a process for feeding firing units of a steam reformer with a second fuel gas and a first flue gas, wherein the first flue gas is generated in an external combustion chamber arranged outside the steam reformer and upstream of the steam reformer by combustion of a first fuel gas with air and, together with the second fuel gas, introduced into the firing units of the steam reformer for firing, wherein the first flue gas has a residual oxygen content sufficient for the firing. The disclosure also relates to a steam reforming plant for performing such a process.

Abstract: A process for producing sulfuric acid and cement clinker may use calcium sulfate that is formed as a solid by-product and separated off in phosphoric acid production in a reaction of raw phosphate with sulfuric acid to form phosphoric acid. The process comprises treating calcium sulfate separated from the phosphoric acid with an acid to obtain a suspension comprising purified calcium sulfate, separating the purified calcium sulfate in solid form from the liquid phase of the suspension, mixing the purified calcium sulfate with admixtures and reducing agents to obtain a raw meal mixture for cement clinker production, burning the raw meal mixture to obtain the cement clinker, with formation of sulfur dioxide as offgas, and subjecting the sulfur dioxide formed to offgas purification and feeding the sulfur dioxide as raw material to sulfuric acid production to produce the sulfuric acid. The sulfuric acid produced may be used as starting material in phosphoric acid production.

Abstract: A process may involve digesting raw phosphate with concentrated sulfuric acid and converting the raw phosphate to calcium sulfate in the form of dihydrate and/or hemihydrate, and phosphoric acid, separating off calcium sulfate as solid from a liquid phase of a suspension that is obtained, treating the calcium sulfate that is separated off or from a stockpile with an acid to give a suspension with purified calcium sulfate and P2O5-containing acid solution, separating off the purified calcium sulfate as solid from a liquid phase of a suspension obtained, using the P2O5-containing liquid phase as a portion of the sulfuric acid required for digesting the raw phosphate or as feedstock for treating phosphogypsum from the stockpile to give a suspension of purified calcium sulfate and P2O5-containing acid solution, which is thereafter processed.

Abstract: The present invention relates to a method for preparing vinyl chloride by catalytic thermal cracking of 1,2-dichloroethane, in which method the heat required for the thermal cracking is supplied via a liquid or condensing heat transfer medium. The present invention also relates to a plant for preparing vinyl chloride by catalytic thermal cracking of 1,2-dichloroethane, in which the heat required for the thermal cracking, as well as for the preceding preheating, evaporation and optionally overheating of the 1,2-dichloroethane, is supplied via a liquid or condensing heat transfer medium, said plant comprising at least one reactor in which the thermal cracking takes place and at least one first heating device by means of which heat is transported to the reaction medium in the reactor by means of the liquid or condensing heat transfer medium.

Abstract: A system suitable for oxidizing ammonia with oxygen in the presence of catalysts is described. The system includes a reactor equipped with at least one supply line for a reactant gas mixture and at least one discharge line for a process gas; a catalyst comprising at least one transition metal oxide that is not an oxide of a platinum metal; and a device for adjusting a molar ratio of oxygen to ammonia of less than or equal to 1.75 mol/mol in the reactant gas mixture by mixing an oxygen-containing gas stream having an O2 content of <20% by volume with a chosen amount of ammonia. The oxygen-containing gas stream is produced by a device for: diluting an air stream with a gas stream comprising less than 20% by volume oxygen; or depleting oxygen from an oxygen-containing gas mixture, preferably from air; or by a combination thereof.

Abstract: Processes and plants for producing cement clinker, wherein no recirculation of preheater exhaust gases occurs and the ratio of solid fed in to exhaust gas in the preheater is set to greater than 1.0 kg of solid to gas.

Abstract: A reactor may have a catalyst bed for the catalytic treatment of a gas stream, with the catalyst bed extending substantially over a cross section of the reactor. Gas to be treated may axially fly through the catalyst bed. A carrier structure for the catalyst bed that is at least partly floatingly mounted in the reactor may include a sieve element and, radially outwardly, carrier elements fixedly joined to the reactor wall below the sieve element. The sieve element provides a resting surface for the catalyst bed. The sieve element terminates, radially outwardly, at a distance from the reactor wall. The carrier structure also includes support elements for the sieve element that are floatingly mounted in the reactor. An improved floating mounting is thus provided where not only the sieve element itself but also further parts of the carrier structure are mounted to prevent stresses due to thermal expansion.

Abstract: A method for calcining and cooling material such as carbonate rocks may be employed in a parallel-flow regenerative shaft kiln that has two shafts, which are operated alternately as a calcining shaft and as a regenerative shaft. Material flows through a preheating zone, a calcining zone, and a cooling zone to a product outlet. At least one gas flow is compressed by a high-pressure fan and introduced into the parallel-flow regenerative shaft kiln. The high-pressure fan is configured as an axial fan or as a radial fan, having an impeller through which flow takes place axially or radially. A parallel-flow regenerative shaft kiln may also be utilized to perform such methods.

Abstract: A cooler for cooling bulk material, such as cement clinker, for example, may include an aeration floor through which cooling gas can flow. The aeration floor may be configured to receive bulk material and to transport the bulk material in a conveying direction. The aeration floor comprises a plurality of conveying beams that are mounted so as to be movable in the conveying direction and counter to the conveying direction. A seal is mounted between two adjacent conveying beams, and the seal has at least two sealing elements mounted so as to be movable relative to one another. The sealing elements each have a sealing profile, which interact with one another such that a sealing gap is formed between them. The sealing gap has a double or multiple U-profile.

Abstract: A plant complex may include a unit that produces CO2-containing gases, a gas conducting system for CO2-containing gases, a gas/liquid separation system, a reformer that is connected to the gas conducting system and where the CO2-containing gas reacts with H2 and/or hydrocarbons to give a CO— and H2-containing synthesis gas mixture. The reformer is connected to a reactor for producing higher alcohols in which the synthesis gas mixture reacts with H2 to give a gas/liquid mixture containing higher alcohols. For separating off the alcohols of the gas/liquid mixture, the gas/liquid separation system is connected to the reactor for producing higher alcohols.

Abstract: A process can be used for recovering 1-methoxy-2-propanol and 2-methoxy-1-propanol from an aqueous effluent stream by liquid-liquid-extraction, followed by extractive distillation, distillation of methoxypropanols from the extraction solvent, and distillative separation of the methoxypropanol isomers. Recovered extraction solvent is recycled to the extraction and extractive distillation. Heat transfer from recovered extraction solvent to the extract fed to the extractive distillation reduces energy demand of the process. A facility for this process contains a countercurrent extraction column, an extractive distillation column, a solvent recovery distillation column, an isomer separation distillation column, and a heat exchanger for transferring heat from recovered extraction solvent to the extract fed to the extractive distillation.

Abstract: An installation for thermal treatment of free-floating raw material, in particular cement raw meal and/or mineral products, may include a riser line through which hot gases can flow. The riser line has at least one fuel inlet for introducing fuel into the riser line. The riser line has at least one raw meal inlet for introducing raw meal into the riser line, which raw meal inlet is arranged upstream of the fuel inlet in a flow direction of gas inside the riser line. Further, a method for thermal treatment of free-floating raw material may involve introducing fuel via a fuel inlet into a riser line for guiding hot gases and introducing raw meal into the riser line. The raw meal is introduced into the riser line upstream of the fuel inlet in the flow direction.

Abstract: A cement production plant may include a preheater for preheating raw meal, a calciner for calcining the preheated raw meal, and a furnace with a furnace burner for firing the raw meal to form cement clinker. The furnace has a combustion gas inlet for admitting a combustion gas with an oxygen content of 30% to 75% into the furnace. The cement production plant may also include a cooler for cooling the cement clinker. The calciner and the furnace each have at least one respective fuel inlet for admitting at least one fuel into the calciner and the furnace. The calciner and the furnace each have at least one respective inert gas inlet for respectively admitting inert gas into the calciner and the furnace.

Abstract: A process for producing cement clinker may involve preheating raw meal in a preheater, calcining the preheated raw meal in a calciner, burning the preheated and calcined raw meal in a furnace to give cement clinker, cooling the cement clinker in a cooler, branching off a portion of the furnace offgases flowing out of the furnace as bypass gas, cooling the bypass gas in a mixing chamber with a cooling gas, and separating out dust present in the bypass gas. The cooling gas is formed at least partly or completely from the bypass gas and/or the calciner offgas and/or the preheater offgas. The cooling gas is introduced into the mixing chamber in a ratio of 2-10:1 relative to the bypass gas.

Abstract: A process for producing cement clinker, may involve preheating raw meal in a preheater, calcining the preheated raw meal in a calciner, and burning the preheated and calcined raw meal in a furnace to give cement clinker. The furnace may be supplied with a combustion gas having an oxygen content, and the temperature within the furnace is ascertained. The process may involve cooling the cement clinker in a cooler. The oxygen supply to the furnace is under closed-loop control as a function of the temperature ascertained within the furnace. The temperature ascertained is compared with a target value and, in the event of any variance of the temperature ascertained from the target value, the oxygen supply to the furnace and/or to the calciner is increased or decreased. The target value is adjusted depending on a particle size distribution and/or a lime standard.

Abstract: A process for catalytic oxidation of ammonia gas by way of an oxygen-containing gas in a presence of a noble metal-containing catalyst may be employed to give nitrogen monoxide. A temperature of an ammonia/air mixed gas may be optimized in respect of nitrogen monoxide selectivity of the reaction before contact with the catalyst. Examination of catalytic NH3 oxidation according to 4NH3+5O2?4NO+6H2O revealed that an optimum mode of operation of an NH3 burner in an HNO3 plant is not to be achieved by maintenance of a constant gauze temperature of the catalyst gauze by automatic setting of the NH3:air ratio. Rather, there is an optimum temperature for each process condition that should be set not by changing the NH3:air ratio but instead by altering the temperature of the NH3/air mixed gas before contact with the catalyst gauzes.