Abstract: A synthesis device may include a pressure vessel with an inlet and an outlet for fluid, a catalyst bed that is disposed within the pressure vessel, a plate heat exchanger that is disposed in a flow path of fluid between the inlet of the pressure vessel and the catalyst bed such that fluid flowing into the catalyst bed is heated by fluid flowing out of the catalyst bed. The plate heat exchanger may be disposed outside a reactor volume occupied by the catalyst bed in the pressure vessel. The catalyst bed may be one of a plurality of catalyst beds disposed axially over one another in the pressure vessel.

Abstract: A cooler for cooling bulk material such as cement clinker may include a stationary aeration grate that is for receiving the bulk material is passably by a flow of cooling gas, a conveyor unit having conveyor planks that are disposed above the aeration grate and that for transporting the bulk material are movable in a reciprocating manner in a conveying direction and counter to the conveying direction, a seal assembly that prevents grate riddlings and is attached to the stationary aeration grate, and a drive element that drives the conveyor planks and extends through the stationary aeration grate. The seal assembly may lie against the drive element, and spacing between the seal assembly and the drive element may be adjustable. Further, a method for preventing grate riddlings in a cooler may involve in the event of wear decreasing the spacing between the seal assembly and the drive element.

Abstract: A method for closed-loop control of a chemical process may involve acquiring process data with sensors, transferring the process data to a control system via a fieldbus, transferring a subset of the process data to a computer system that includes a simulation program for stationary and dynamic process simulation of the chemical process, a closed-loop control program for implementing a closed-loop controller, and a memory for storing simulated state variables, cyclically repeatedly calculating and storing the simulated state variables of the chemical process by the simulation program from the subset of the process data, transferring a setpoint value of a control variable of the chemical process to the closed-loop control program, reading a subset of the simulated state variables for input into the closed-loop control program, ascertaining a manipulated variable to achieve the setpoint value by the closed-loop control program, and transferring the calculated manipulated variable to the control system.

Abstract: A bearing for a crusher, in particular for a gyratory crusher or cone crusher, may include a housing, an eccentric bush that is mounted in the housing such that the eccentric bush can be rotated about an axle, a bushing that is disposed between the housing and the eccentric bush, and a lubricant line for supplying the bushing with lubricant that extends into the eccentric bush. The lubricant line may extend along an axial direction within a wall of the eccentric bush. An outer side of the eccentric bush may have an outlet opening for the lubricant line, with the outlet opening being directed onto the bushing.

Abstract: An apparatus for producing ammonia or hydrogen may include a) a gas stream feed conduit having a connecting conduit to a steam reformer with a waste heat section; b) a heat exchanger downstream of the gas stream feed conduit; c) a gas stream preheater downstream of the heat exchanger; d) a recirculation conduit which is located downstream of the gas stream preheater and leads to the gas stream feed conduit or, upstream of the heat exchanger, to the connecting conduit; and e) the steam reformer with the waste heat section, where the waste heat section may be in thermal contact with the gas stream preheater and the flow of the gas stream which has been heated in the gas stream preheater through the recirculation conduit can be regulated. A process for producing ammonia or hydrogen may employ such an apparatus.

Abstract: A process may be utilized to coat urea-containing granules with organic polymers. The process may involve compressing gaseous carbon dioxide and condensing the carbon dioxide to obtain liquid carbon dioxide, increasing the pressure and/or the temperature above the critical point of carbon dioxide and obtaining supercritical carbon dioxide, dissolving an organic polymer in the supercritical carbon dioxide to obtain a polymer-containing solution, and mixing the polymer-containing solution with urea-containing granules and lowering the temperature and/or the pressure below the critical point of carbon dioxide and obtaining coated urea-containing granules and gaseous carbon dioxide. In some cases the organic polymer may include biodegradable polymers, and the polymer-containing solution may contain between 20 to 70% by weight biodegradable polymers.

Abstract: Systems and methods for the synthesis of ammonia includes a reformer; a carbon monoxide converter; a carbon dioxide scrubber unit with recovery; a methanation unit; and an ammonia synthesis unit; wherein the carbon dioxide scrubber unit with recovery is connected to at least one fired auxiliary steam boiler.

Abstract: A system for continuously loading utility vehicles with material may include a multiple chute that is switchable into different states to load different utility vehicles successively with material, at least two utility vehicles arranged in a front row and at least one utility vehicle in at least one subsequent row, wherein at least one utility vehicle in the front row is followed, counter to its direction of travel, by the utility vehicle unfilled in the subsequent row, a drive-through control system with each utility vehicle being assigned a drive-through control element, a presence sensor system with each utility vehicle being assigned a presence sensor, a material filling level-sensing system, wherein each utility vehicle in the front row is assigned a material filling level-sensing sensor, and a computer system for controlling the state of the multiple chute based on data from the presence sensor system and the material filling level-sensing system.

Abstract: The present invention concerns a process for the treatment of a feed comprising biomass, said process comprising at least the following steps: a) a step for drying said feed at a temperature in the range 20° C. to 180° C. for a period in the range 5 to 180 minutes, b) a step for torrefaction of the dried feed obtained from step a) in order to produce at least one solid torrefied biomass effluent, and c) a step for co-grinding the solid torrefied biomass effluent obtained from step b) in the presence of a second biomass feed in order to obtain a powder.

Abstract: A reformer for steam reforming a hydrocarbon-containing mixture, including a combustion chamber, a burner arranged within the combustion chamber, a first reactor tube which is arranged at least in sections within the combustion chamber, a catalyst arranged inside the first reactor tube, and an electrically heatable heating element is arranged inside the first reactor tube.

Abstract: A process for performing the water gas shift reaction wherein raw synthesis gas is reacted in the presence of steam and at least one water gas shift catalyst to convert carbon monoxide into carbon dioxide and to form hydrogen. The raw synthesis gas is initially passed through at least one unit for high-temperature CO conversion and subsequently, downstream thereof, passed through at least one unit for low-temperature CO conversion. After passing through the at least one unit for high-temperature CO conversion the synthesis gas stream is divided into at least two substreams. The first substream is passed through a first unit for low-temperature CO conversion and the second substream is passed through a second unit for low-temperature CO conversion, wherein both units for low-temperature CO conversion are arranged in parallel relative to one another.

Abstract: A process for preparing ammonia or ammonia and urea in a facility may involve compressing a crude synthesis gas stream that includes hydrogen, nitrogen, and carbon dioxide, washing a substream of the crude synthesis gas with ammonia to form a purified synthesis gas stream depleted of carbon dioxide and a condensate, synthesizing ammonia from the purified synthesis gas stream, and synthesizing urea from the condensate to form an aqueous urea composition. In the preparation of ammonia and urea, the crude synthesis gas stream may be, after being compressed, divided into a first synthesis gas substream and a second synthesis gas substream. In some instances, only the first synthesis gas substream is scrubbed with liquid ammonia.

Abstract: A plant complex for producing steel, having a blast furnace for producing pig iron; a converter steel works for producing crude steel; a gas pipeline system for gases that occur in the production of pig iron and/or the production of crude steel; a chemical plant and/or a biotechnology plant which are/is connected to the gas pipeline system, wherein the plant complex additionally includes a biogas plant which is connected to the gas pipeline system.

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 method for producing synthesis gas may involve introducing a hydrocarbon-containing coke-oven gas and a carbon dioxide-containing converter gas into a first reaction zone where hydrogen present in the hydrocarbon-containing coke-oven gas reacts at least partly with carbon dioxide to form water, which reacts thermally with hydrocarbon to form synthesis gas containing carbon monoxide and hydrogen. The method may further involve introducing an oxygen-containing gas in a second reaction zone, and using the oxygen-containing gas and some hydrogen from the first reaction zone to produce thermal energy. Still further, the method may involve supplying the thermal energy produced in the second reaction zone to the first reaction zone.

Abstract: A tray for a mass-transfer column permits contact between a liquid phase and a gas phase. The tray may comprise a tray feed via which the tray is charged with the liquid phase, a tray drain via which the liquid phase drains from the tray, and first guide means for guiding the liquid phase where the first guide means forms a first course path along which the liquid phase flows from the tray feed to the tray drain, enabling contact with the gas phase. A second guide means may form a second course path overlapping with the first course path, which leads from an inlet to an outlet. The first guide means may have at least two partial concentric paths. Temperature-control fluid may flow along the second course path in at least one of the at least two partial paths opposite the flow direction of the liquid phase.

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.

Abstract: A device for waste gas scrubbing in a urea plant may be configured such that a waste gas passes along a transportation direction in the duct. The duct may include a first region for removing urea dust particles from the waste gas and a second region for removing chemical compounds from the waste gas, which can be integrated by an acid-base reaction into an aqueous liquid phase. A cross-sectional area of the duct extending perpendicular to the transportation direction in the second region may be greater than a cross-sectional area extending perpendicular to the transportation direction in the first region. Further, the device may be configured such that the duct extends horizontally at least in sections and/or the transportation direction of the waste gas through the duct extends horizontally in an installed state.

Abstract: A plant complex for pig iron production may include a furnace and a furnace gas conduit system for a furnace gas quantity stream that comprises nitrogen, carbon monoxide, and carbon dioxide. The plant complex may also include a hydrogen source, an H2 gas conduit system for a hydrogen-containing gas quantity stream emitted from the hydrogen source, a mixing apparatus for establishing a mixed gas formed from the furnace gas stream and the hydrogen-containing gas quantity stream. The mixing apparatus may be connected to the furnace gas conduit system and to the H2 gas conduit system. The mixed gas established may have a stoichiometric mixing quotient formed from a dividend with a difference value between molar amounts of hydrogen as minuend and carbon dioxide as subtrahend and of a divisor with a sum value of molar amounts of carbon monoxide and carbon dioxide. The plant complex may also include a mixed gas conduit system and a chemical plant connected to the mixed gas conduit system.

Abstract: A method of reducing NOx in tail gas obtained during startup of a plant for preparing nitric acid may involve heating the tail gas from a starting temperature T0, through a threshold temperature TG, to an operating temperature TB at which steady-state operation of the plant can occur (T0<TG<TB). NOx-containing tail gas may be passed through a storage medium and at least partially stored while the temperature of the tail gas is lower than the threshold temperature TG. The NOx may be released, preferably when the temperature of the tail gas has attained the threshold temperature TG. The NOx may be combined with a reducing agent in the presence of an SCR catalyst after the temperature of the tail gas has exceeded the threshold temperature TG, but not before, resulting in catalytic reduction of at least a portion of the NOx.