Abstract: A process can be used to treat a synthesis gas stream comprising steam reforming firstly in a primary reformer and subsequently in a secondary reformer. Crude synthesis gas exiting the secondary reformer may be cooled in a steam generator and then further cooled in a steam superheater. The crude synthesis gas stream after exiting the secondary reformer may be split into at least two gas substreams, of which only a first gas substream is fed to the steam generator. A second gas substream may be supplied to the steam superheater, bypassing the steam generator. Only the first gas substream, after flowing through the steam generator, may be subjected to a CO conversion reaction in a first CO conversion reactor before the first gas substream is supplied to the steam superheater.

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 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: Processes for separating carbon dioxide from CO2-containing gases and an apparatus for providing carbon dioxide for the synthesis of urea.

Abstract: The invention relates to a loading device having N loading heads offset by N/360°, wherein N is the number 3 or an integer multiple thereof, wherein each of the N loading heads has a connecting device for a hose arranged at the upper end, through which hose the catalyst material can be delivered from above, wherein each of the N loading heads has a deflecting cone with the tip pointing upwards beneath the connecting device and joined to the connecting device, a vertical holder is mounted on the underside of said deflecting cone, at least two circular deflector funnel elements are mounted on the vertical holder by means of horizontal braces, the deflector funnel elements open more narrowly at the top than at the bottom, gaps are provided between the deflector funnel elements and the lower deflector funnel elements have a larger diameter than the deflector funnel elements above them.

Abstract: “The invention relates to a loading device having N loading heads offset by N/360° , wherein N is the number 3 or an integer multiple thereof, wherein each of the N loading heads has a connecting device for a hose arranged at the upper end, through which hose the catalyst material can be delivered from above, wherein each of the N loading heads has a deflecting cone with the tip pointing upwards beneath the connecting device and joined to the connecting device, a vertical holder is mounted on the underside of said deflecting cone, at least two circular deflector funnel elements are mounted on the vertical holder by means of horizontal braces, the deflector funnel elements open more narrowly at the top than at the bottom, gaps are provided between the deflector funnel elements and the lower deflector funnel elements have a larger diameter than the deflector funnel elements above them.

Abstract: A method of starting up an autothermal reactor for the production of synthesis gas by reforming of hydrocarbon-containing feed gases in a reaction chamber in which oxidation reactions and reforming reactions are carried out, by feeding a hydrocarbon containing feed gas, steam and an oxidant.

Abstract: A method of starting up an autothermal reactor for the production of synthesis gas by reforming of hydrocarbon-containing feed gases in a reaction chamber in which oxidation reactions and reforming reactions are carried out, by feeding a hydrocarbon containing feed gas, steam and an oxidant.

Abstract: A measurement device for regulating the filling level of a liquid-gas mixture via a inlet valve in a container, having at least one vertical liquid standpipe fixed to a outer wall of the container and fluidically connected to the interior of the container via horizontal tube-shaped hydraulic devices. A first lower hydraulic device is disposed near the container base so the standpipe level changes with the container. A second hydraulic device is provided above the desired filling level so that the standpipe level changes when a selectable desired filling level value is exceeded. The device has a display and regulator that is in controlled connection to the liquid inlet valve. The liquid standpipe has a third tube-shaped hydraulic device that protrudes horizontally into the container and is arranged in the container at or below the desired filling level. The first lower hydraulic device is configured as a return.

Abstract: Combined removal of both ammonia from an ammonia-containing waste gas and nitrogen oxides from a nitrogen oxide-containing waste gas in a combined ammonia/urea synthesis plant is accomplished by mixing the gases and employing one or both of selective non-catalytic reduction at a temperature of 850° C. to 1100° C. or selective catalytic reduction at a temperature of 150° C. to 550° C., in which the ammonia and the nitrogen oxides react with one another to give nitrogen and water, the ammonia-containing waste gas derived from a low-pressure and/or atmospheric absorber of the urea synthesis plant, and the nitrogen oxide-containing waste gas derived from a flue gas duct of a primary reformer of the ammonia synthesis plant, both the ammonia and the nitrogen oxides of the mixed waste gas flows being depleted simultaneously during the same process step.

Abstract: Combined removal of both ammonia from an ammonia-containing waste gas and nitrogen oxides from a nitrogen oxide-containing waste gas in a combined ammonia/urea synthesis plant is accomplished by mixing the gases and employing one or both of selective non-catalytic reduction at a temperature of 850° C. to 1100° C. or selective catalytic reduction at a temperature of 150° C. to 550° C., in which the ammonia and the nitrogen oxides react with one another to give nitrogen and water, the ammonia-containing waste gas derived from a low-pressure and/or atmospheric absorber of the urea synthesis plant, and the nitrogen oxide-containing waste gas derived from a flue gas duct of a primary reformer of the ammonia synthesis plant, both the ammonia and the nitrogen oxides of the mixed waste gas flows being depleted simultaneously during the same process step.

Abstract: A process for utilizing synthesis gas heat for the generation of supercritical steam in a low energy ammonia or methanol plant is disclosed. The process involves a reforming or partial oxidation stage, at least one supercritical steam generator having a shell side and a tube side, at least one superheater, at least one back pressure turbine, at least one extraction and condensing turbine, and at least one boiler feedwater pump. The synthesized synthesis gas is sent to the shell side of the supercritical steam generator, and the supercritical steam generator is fed with pressurized feedwater. The feedwater flow is adjusted to maintain the steam temperature at the exit of the supercritical steam generator in the range of 375-500° C. The supercritical steam is generated in the supercritical steam generator at a pressure of 225-450 bar, the supercritical steam is further heated in a superheater to a temperature of 500-750° C.

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: 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 method for the production of nitric acid having a concentration of between 50 and 76%, from ammonia and gas containing oxygen, under pressure, according to a single pressure method or dual pressure method. The expansion of the residual gas takes place in at least two stages in a work efficient manner. At least one device for heating the previously expanded gas to a temperature of more than 450° is disposed between every other expansion stage, using waste heat from the production process of nitric acid.

Abstract: The invention relates to a method for the production of nitric acid having a concentration of between 50 and 76%, from ammonia and gas containing oxygen, under pressure, according to a single pressure method or dual pressure method. The expansion of the residual gas takes place in at least two stages in a work efficient manner. At least one device for heating the previously expanded gas to a temperature of more than 450° is disposed between every other expansion stage, using waste heat from the production process of nitric acid.