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 process for producing prills, in particular fertilizer prills, coated with at least one biologically degradable polymer layer, in particular a PLA layer, may involve applying a degradable polymer layer to a carrier material of the respective prill in a drum coating step, in particular in a drum coater at relative negative pressure, and then coating the prills with a second degradable polymer layer on top of the first degradable polymer layer in a fluidized bed coating step, in particular in a fluidized bed coater at a relative positive pressure. Coating the prills with the second degradable polymer layer may involve introducing the prills into a fluidized bed coater after the drum coating step, and the fluidized bed coating step may be performed spatially adjacent alongside the drum coating step.

Abstract: A process and a device for the production of ammonia at different pressure levels may involve removing gases that are inert (inert gases) or harmful with regard to ammonia synthesis from the process in a process step before the ammonia synthesis so that enrichment of these is decreased or suppressed. For example, with respect to a gas mixture that includes hydrogen, nitrogen, water, methane, carbon monoxide, and carbon dioxide, at least part of the water, at least part of the methane, at least part of the carbon monoxide, and at least part of the carbon dioxide may be removed from the gas mixture before the synthesis of the ammonia occurs.

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 reactor for catalytic conversion of gas mixtures may include a catalyst bed. An upper side of the catalyst bed may include a gas lock that is movable in a vertical direction. The gas lock may be lowered when the catalyst bed contracts. In some examples, the gas lock prevents a gas mixture from flowing out of the catalyst bed via the upper side of the catalyst bed.

Abstract: By means of a method and a system for heating and partial oxidation of not separately pre-heated, pre-reformed steam/natural gas mixture for an NH3 synthesis gas, whereby energy is supplied to the gas stream (raw synthesis gas), in the direction of flow, after a primary reformer, a solution is to be created, with which soot formation is to be prevented as much as possible, whereby the possibility of the addition of variable amounts, for example of N2 and O2 or mixtures thereof, is also supposed to be possible. This is achieved, according to the method, in that the energy is supplied directly after the primary reformer, by way of at least one pore burner positioned in the gas discharge line of the primary reformer.

Abstract: The invention relates to a gas burner for burning fuel gases with oxygen, said gas burner comprising a primary gas nozzle (6) and secondary gas nozzles (5) which are connected to a common central feed line (3). In this case, the non-horizontal openings (8), directed obliquely downwards, of the primary gas nozzle are oriented in such a way that the gas jet of said primary gas nozzle is directed towards a point of a centre line (10) between two respective secondary gas nozzles, and the centre line is defined as an imaginary line which runs parallel to the rotation axis of the primary gas nozzle and centrally between two adjacent secondary gas nozzles.

Abstract: A synthesis furnace has a furnace chamber surrounded by a circumferential furnace wall, in which burners are disposed essentially in one plane, with burner exit direction directed downward, and reaction tubes are disposed essentially vertically and parallel to one another. The reaction tubes are heated externally by the ignited burners. To improve the heat distribution and the entire heat transfer in as simple a manner as possible, in terms of design and control technology, at least the outer burners disposed in the vicinity of the furnace wall have a burner exit direction that runs at an incline away from the center of the furnace in relation to the vertical.

Abstract: By means of a method and a system for heating and partial oxidation of not separately pre-heated, pre-reformed steam/natural gas mixture for an NH3 synthesis gas, whereby energy is supplied to the gas stream (raw synthesis gas), in the direction of flow, after a primary reformer, a solution is to be created, with which soot formation is to be prevented as much as possible, whereby the possibility of the addition of variable amounts, for example of N2 and O2 or mixtures thereof, is also supposed to be possible. This is achieved, according to the method, in that the energy is supplied directly after the primary reformer, by way of at least one pore burner positioned in the gas discharge line of the primary reformer.

Abstract: With a synthesis furnace having a furnace chamber surrounded by a circumferential furnace wall, in which a plurality of burners disposed essentially in one plane, with burner exit direction directed downward, and a plurality of reaction tubes disposed essentially vertically and parallel to one another are disposed, whereby the reaction tubes are heated from the outside, by means of the firing burners, the heat distribution and the entire heat transfer are supposed to be improved in as simple a manner as possible, in terms of design and control technology. This is achieved in that at least the outer burners (5) disposed in the region of the furnace wall (2) have a burner exit direction (R) that is inclined relative to the vertical, leading away from the center of the furnace.