Abstract: A process for the production of methanol from synthesis gas via an equilibrium reaction is conducted in a methanol pre-converter within a certain operational window, said operational window being defined by the area below an approximately linear curve of the partial pressure of carbon monoxide vs. the boiling water temperature for water temperatures between 210 and 270° C. Methanol of different product grades may be obtained by operating in specific areas of the operational window.

Abstract: The deterioration of methanol synthesis catalysts that is caused by iron poisoning of the catalyst is counteracted by using a catalyst containing a maximum of 100 ppmw Fe in the synthesis process. The method is especially useful in a methanol synthesis plant comprising a make-up gas compressor and a synthesis reactor in a methanol loop with a once-through pre-converter installed between the make-up gas compressor and the methanol loop.

Abstract: A process for the production of methanol from synthesis gas via an equilibrium reaction is conducted in a methanol preconverter within a certain operational window, said operational window being defined by the area below an approximately linear curve of the partial pressure of carbon monoxide vs. the boiling water temperature for water temperatures between 210 and 270° C. Methanol of different product grades may be obtained by operating in specific areas of the operational window.

Abstract: A process for the hydrotreatment of a fuel gas stream containing up to 15% olefins comprises the steps of introducing the fuel gas stream into at least one co-current reactor, where the stream is split into two flow fractions, of which one fraction is routed through an olefin treatment section, while the other fraction is routed through another section, subjecting the sections to heat exchange, combining the two flows, thereby equalizing temperatures and compositions, cooling the combined flow over a heat exchanger and reacting the combined flow to equilibrium in an adiabatic hydrotreatment reactor. A second co-current reactor with intercooling arranged in series after the first cocurrent reactor and before the final adiabatic reactor is used if the fuel gas stream contains more than 8% olefins.

Abstract: A process for the hydrotreatment of a fuel gas stream containing up to 15% olefins comprises the steps of introducing the fuel gas stream into at least one co-current reactor, where the stream is split into two flow fractions, of which one fraction is routed through an olefin treatment section, while the other fraction is routed through another section, subjecting the sections to heat exchange, combining the two flows, thereby equalizing temperatures and compositions, cooling the combined flow over a heat exchanger and reacting the combined flow to equilibrium in an adiabatic hydrotreatment reactor. A second co-current reactor with intercooling arranged in series after the first cocurrent reactor and before the final adiabatic reactor is used if the fuel gas stream contains more than 8% olefins.

Abstract: In a process for methanol production from synthesis gas, which comprises the steps of providing a make-up gas containing hydrogen and carbon monoxide, in which the content of carbon dioxide is less than 0.1 mole %, mixing the make-up gas with a hydrogen-rich recycle gas and passing the gas mixture to a methanol synthesis reactor, optionally via a sulfur guard, and subjecting the effluent from the synthesis reactor to a separation step, thereby providing crude methanol and the hydrogen-rich recycle gas, the customary addition of carbon dioxide to the make-up gas is replaced by addition of water in an amount of 0.1 to 5 mole %. This way, a CO2 compressor is saved, and the amount of poisonous sulfur in the make-up gas is markedly reduced.

Abstract: In a process for methanol production from synthesis gas, which comprises the steps of providing a make-up gas containing hydrogen and carbon monoxide, in which the content of carbon dioxide is less than 0.1 mole %, mixing the make-up gas with a hydrogen-rich recycle gas and passing the gas mixture to a methanol synthesis reactor, optionally via a sulfur guard, and subjecting the effluent from the synthesis reactor to a separation step, thereby providing crude methanol and the hydrogen-rich recycle gas, the customary addition of carbon dioxide to the make-up gas is replaced by addition of water in an amount of 0.1 to 5 mole %. This way, a CO2 compressor is saved, and the amount of poisonous sulfur in the make-up gas is markedly reduced.

Abstract: Method and apparatus for separating a liquid reaction product from a gaseous stream in a catalytic reactor by means of a metallic sheet being indirectly cooled by a cooling surface and having a plurality of percolations in form of geometric-shaped protrusions on both sides of the sheet each with an open base, the open base is on the side of the sheet facing a catalyst bed are arranged upwards and on the side facing the cooling surface the open base faces downwards.

Abstract: Method and a reactor for performing exothermic catalytic reactions. The method comprises the steps of providing a feed gas stream comprising reactants for the exothermic catalytic reaction to a fixed bed catalytic reactor comprising one or more catalyst beds each with catalyst particles filled sections with a catalyst volume; providing a feed gas bypass inside the reactor by arranging within at least one of the catalyst beds a number of bypass passageways without catalytic active particles inside the passageways and having a cooling surface area; passing a part of the feed gas stream through the bypass passageways and reminder of the stream through the catalyst particles filled sections; and removing heat from the feed gas stream being passed through the catalyst filled sections by indirect heat transfer to the part of the feed gas stream being passed through the bypass passageways.

Abstract: Improved design of a catalytic method and reactor for the production of methanol at equilibrium conditions, whereby methanol, as it is formed, is separated from the gaseous phase into the liquid phase within the reactor without reducing the catalytic activity of the methanol catalyst. This is achieved by adjusting the boiling point or temperature of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place for the most at the cooling surface arranged evenly distributed within the reactor and if at all within a very limited region of the catalyst bed.

Abstract: Improved design of a catalytic reactor for the production of methanol at equilibrium conditions whereby methanol as it is formed is separated from the gaseous phase into the liquid phase within the reactor, without reducing the catalytic activity of the methanol catalysts This is achieved by adjusting the boiling point of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place at the cooling surface arranged evenly distributed within the reactor and within a very limited region of the catalyst bed.

Abstract: Method and apparatus for separating a liquid reaction product from a gaseous stream in a catalytic reactor by means of a metallic sheet being indirectly cooled by a cooling surface and having a plurality of percolations in form of geometric-shaped protrusions on both sides of the sheet each with an open base, the open base is on the side of the sheet facing a catalyst bed are arranged upwards and on the side facing the cooling surface the open base faces downwards.

Abstract: Method and reactor for performing Fischer-Tropsch (FT) synthesis with controlled steam partial pressure by introducing cool points in the FT reactor, typically in form of cooled solid surfaces. At the surface, the low temperature will force condensation of the water into a liquid film. Thereby, the partial pressure of steam in the gas and reactor will not exceed significantly the vapour partial pressure at the liquid film and water from the gas stream will be removed as it is produced, i.e. steam induced deactivation is avoided. In addition, the decrease of hydrogen and carbon monoxide partial pressures due to dilution by steam will be kept low ensuring a constant high reaction rate.

Abstract: Improved design of a catalytic method and reactor for the production of methanol at equilibrium conditions, whereby methanol, as it is formed, is separated from the gaseous phase into the liquid phase within the reactor without reducing the catalytic activity of the methanol catalyst. This is achieved by adjusting the boiling point or temperature of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place for the most at the cooling surface arranged evenly distributed within the reactor and if at all within a very limited region of the catalyst bed.

Abstract: Method and reactor for performing Fischer-Tropsch (FT) synthesis with controlled steam partial pressure by introducing cool points in the FT reactor, typically in form of cooled solid surfaces. At the surface, the low temperature will force condensation of the water into a liquid film. Thereby, the partial pressure of steam in the gas and reactor will not exceed significantly the vapor partial pressure at the liquid film and water from the gas stream will be removed as it is produced, i.e. steam induced deactivation is avoided. In addition, the decrease of hydrogen and carbon monoxide partial pressures due to dilution by steam will be kept low ensuring a constant high reaction rate.

Abstract: Improved design of a catalytic method and reactor for the production of methanol at equilibrium conditions whereby methanol as it is formed is separated from the gaseous phase into the liquid phase within the reactor without reducing the catalytic activity of the methanol catalyst. This is achieved by adjusting the boiling point or temperature of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place for the most at the cooling surface arranged evenly distributed within the reactor and if at all within a very limited region of the catalyst bed.

Abstract: Improved design of a catalytic reactor for the production of methanol at equilibrium conditions whereby methanol as it is formed is separated from the gaseous phase into the liquid phase within the reactor, without reducing the catalytic activity of the methanol catalysts This is achieved by adjusting the boiling point of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place at the cooling surface arranged evenly distributed within the reactor and within a very limited region of the catalyst bed.

Abstract: Improved design of a catalytic method and reactor for the production of methanol at equilibrium conditions whereby methanol as it is formed is separated from the gaseous phase into the liquid phase within the reactor without reducing the catalytic activity of the methanol catalyst. This is achieved by adjusting the boiling point or temperature of a liquid cooling agent being in indirect contact with the catalyst particles and by providing a specific ratio of catalyst bed volume to cooling surface area. Thereby, condensation of methanol as it is formed in the gaseous phase takes place for the most at the cooling surface arranged evenly distributed within the reactor and if at all within a very limited region of the catalyst bed.

Abstract: Method and reactor for performing Fischer-Tropsch (FT) synthesis with controlled steam partial pressure by introducing cool points in the FT reactor, typically in form of cooled solid surfaces. At the surface, the low temperature will force condensation of the water into a liquid film. Thereby, the partial pressure of steam in the gas and reactor will not exceed significantly the vapour partial pressure at the liquid film and water from the gas stream will be removed as it is produced, i.e. steam induced deactivation is avoided. In addition, the decrease of hydrogen and carbon monoxide partial pressures due to dilution by steam will be kept low ensuring a constant high reaction rate.

Abstract: The invention relates to a method for controlling injection of a reductant into a NOx containing exhaust gas stream from a combustion engine, where combustion of a known fuel takes place and where the NOx is reduced by selective catalytic reduction, SCR, in the presence of a SCR catalyst, comprising establishing signals related to exhaust gas flow, HOx concentration in the exhaust gas stream upstream of the catalyst, exhaust gas temperature upstream of the SCR catalyst, exhaust gas temperature downstream of the SCR catalyst and to input data for catalyst characteristics. From the signals an adjusted amount of the reductant is calculated by using a calculated amount of reductant and a value d(E*T)/dt, where E is the exhaust gas flow, T is the exhaust gas temperature upstream of the catalyst and t is time.