Abstract: The present invention relates to a revamp method for increasing the front-end capacity of a plant comprising a reforming section, wherein a feed is reformed in at least one reforming step to a reformed stream comprising CH4, CO, CO2, H2 and H2O a shift section wherein the reformed stream is shifted in a shift reaction in at least a high temperature shift step, said method comprising the steps of In the High temperature shift step exchanging an original Fe-based catalyst with a non-Fe-based catalyst Increasing the feed flow to the reforming section, and The HTS step is carried out at a reduced steam/dry-gas ratio (S/DG) compared to an original S/DG in the original HTS step with the original Fe-based catalyst.

Abstract: In a process for the production of ammonia synthesis gas from a hydrocarbon-containing feedstock, comprising steam reforming of the feedstock and treatment of the synthesis gas obtained, the shift of the synthesis gas comprises two shift steps, both including stable catalysts, whereby the formation of hazardous by-products is avoided or at least reduced to an acceptable low level. The two shift steps can both be HTS, or they can be one HTS and one LTS or one HTS and one MTS. The catalyst used in the HTS and the LTS steps is based on zinc oxide and zinc aluminum spinel, and the catalyst used in the MTS and the LTS steps can be based on copper.

Abstract: The present invention relates to a revamp method for increasing the front-end capacity of a plant comprising a reforming section, wherein a feed is reformed in at least one reforming step to a reformed stream comprising CH4, CO, CO2, H2 and H2O a shift section wherein the reformed stream is shifted in a shift reaction in at least a high temperature shift step, said method comprising the steps of In the High temperature shift step exchanging an original Fe-based catalyst with a non-Fe-based catalyst Increasing the feed flow to the reforming section, and The HTS step is carried out at a reduced steam/dry-gas ratio (S/DG) compared to an original S/DG in the original HTS step with the original Fe-based catalyst.

Abstract: In a process for the production of ammonia synthesis gas from a hydrocarbon-containing feedstock, comprising steam reforming of the feedstock and treatment of the synthesis gas obtained, the shift of the synthesis gas comprises two shift steps, both including stable catalysts, whereby the formation of hazardous by-products is avoided or at least reduced to an acceptable low level. The two shift steps can both be HTS, or they can be one HTS and one LTS or one HTS and one MTS. The catalyst used in the HTS and the LTS steps is based on zinc oxide and zinc aluminum spinel, and the catalyst used in the MTS and the LTS steps can be based on copper.

Abstract: A device and a process for producing high purity CO by electrolysis of CO2 in a Solid Oxide Electrolysis Cell stack and a gas separation unit, also the gas separation unit may be a Solid Oxide Electrolysis Cell stack.

Abstract: Process for operating a high temperature fuel cell stack by the steps of: connecting the fuel cell stack in parallel to a power supply unit at a predefined temperature and/or voltage of the fuel cell stack, applying a voltage from the power supply unit of between 700 to 1500 mV per fuel cell across the fuel cell stack irrespective of the electro-motive force of the fuel cell stack, heating up the fuel cell stack from the predefined temperature to operation temperature while maintaining the voltage per fuel cell the power supply unit, maintaining the fuel cell stack at or above a predetermined operation temperature and/or above a predetermined voltage until the fuel cell stack is to be put into operation, supplying fuel to the fuel cell stack, and disconnecting the power supply unit followed by connecting a power-requiring load to the fuel cell stack.

Abstract: A device and a process for producing high purity CO by electrolysis of CO2 in a Solid Oxide Electrolysis Cell stack and a gas separation unit, also the gas separation unit may be a Solid Oxide Electrolysis Cell stack.

Abstract: A method for desulphurization of a liquid fossil fuel to be used in connection with a fuel cell is performed in a system comprising an evaporator unit (1), wherein the liquid fuel is first evaporated, a fixed bed reactor (2) in the form of a gas-phase hydro-desulphurizer, where the fuel is treated with hydrogen at atmospheric pressure over a highly active hydro-cracking (HAHT) catalyst, whereby sulphur species are converted to H2S, an adsorber (3), where the produced hydrogen sulphide can be adsorbed on a catalytic bed, and a fuel reformer (4), in which the fuel product is converted to syngas to be fed to an SOFC system (6). The evaporator unit (1) comprises a liquid spraying device, preferably in the form of a piezoelectric spray nozzle.

Abstract: A process for the preparation of hydrocarbon products and for the generation of power that includes the steps of (a) providing a synthesis gas having a hydrogen to carbon monoxide ratio of between 0.1 and 1; (b) contacting the synthesis gas with one or more catalysts which together catalyse a reaction of hydrogen and carbon monoxide to oxygenates comprising methanol and dimethyl ether with a dimethyl ether to methanol ratio of higher than 2 and a carbon dioxide content of above 20 mole %; (c) contacting the carbon dioxide containing oxygenate mixture at an inlet temperature of between 240° and 4000° C. with a catalyst being active in the conversion of oxygenate to higher hydrocarbons and a tail gas being rich in carbon dioxide; (d) combusting the carbon dioxide rich tail gas in a gas turbine combustion chamber to flue gas; and (e) expanding the flue gas stream through a gas turbine for the generation of power.

Abstract: Process for operating a high temperature fuel cell stack, the process comprising the following steps: b) connecting the fuel cell stack in parallel to a power supply unit at a predefined temperature and/or voltage of the fuel cell stack, h) applying a voltage from the power supply unit of between 700 to 1500 mV per fuel cell across the fuel cell stack irrespective of the electro-motive force of the fuel cell stack, i) heating up the fuel cell stack from the predefined temperature to operation temperature while maintaining the voltage per fuel cell the power supply unit, j) maintaining the fuel cell stack at or above a predetermined operation temperature and/or above a predetermined voltage until the fuel cell stack is to be put into operation, k) supplying fuel to the fuel cell stack, l) disconnecting the power supply unit followed by m) connecting a power-requiring load to the fuel cell stack.

Abstract: A process for the preparation of hydrocarbon products and for the generation of power comprising the steps of (a) providing a synthesis gas having a hydrogen to carbon monoxide ratio of between 0.1 and 1; (b) contacting the synthesis gas with one or more catalysts which together catalyse a reaction of hydrogen and carbon monoxide to oxygenates comprising methanol and dimethyl ether with a dimethyl ether to methanol ratio of higher than 2 and a carbon dioxide content of above 20 mole %; (c) contacting the carbon dioxide containing oxygenate mixture at an inlet temperature of between 240 and 4000 C with a catalyst being active in the conversion of oxygenate to higher hydrocarbons and a tail gas being rich in carbon dioxide; (d) combusting the carbon dioxide rich tail gas, optionally admixed with fresh carbon monoxide rich synthesis gas in a gas turbine combustion chamber to flue gas; and (e) expanding the flue gas stream through a gas turbine for the generation of power.

Abstract: Process for the preparation of dimethyl ether product by catalytic conversion of synthesis gas to dimethyl ether comprising the steps of contacting a stream of synthesis gas comprising carbon dioxide in a dimethyl ether synthesis step in one or more reactors and with one or more catalysts being active in formation of methanol and dehydration of methanol to dimethyl ether, to form a product mixture comprising the dimethyl ether and carbon dioxide, washing the product mixture in a scrubbing zone with a liquid solvent being rich in dialkyl ether of a polyalkylene glycol and thereby dissolving carbon dioxide and dimethyl ether in the liquid solvent, treating the liquid solvent being withdrawn from the scrubbing zone sequentially in separation zone to effect desorption of the dissolved carbon dioxide and to recover a substantially pure dimethyl ether product and the liquid solvent in its substantially lean form and recycling the lean liquid solvent to the scrubbing zone.

Abstract: Process for the preparation of dimethyl ether by catalytic conversion of synthesis gas to dimethyl ether comprising contacting a stream of synthesis gas comprising carbon dioxide with one or more catalysts active in the formation of methanol and the dehydration of methanol to dimethyl ether, to form a product mixture comprising the components dimethyl ether, carbon dioxide and unconverted synthesis gas, washing the product mixture comprising carbon dioxide and unconverted synthesis gas in a first scrubbing zone with a first solvent rich in dimethyl ether and subsequently washing the effluent from the first scrubbing zone in a second scrubbing zone with a second solvent rich in methanol to form a vapour stream comprising unconverted synthesis gas stream with reduced content of carbon dioxide, transferring the vapour stream comprising unconverted synthesis gas stream with reduced carbon dioxide content for further processing to dimethyl ether.

Abstract: Process and system for the production of synthesis gas from a hydrocarbon feed stock comprising the steps of endothermic and/or adiabatic catalytic steam reforming and autothermal steam reforming in series, wherein the steam reforming is carried out in one or more endothermic stages in series or in one or more adiabatic steam reforming stages in series with intermediate heating of feed stock gas leaving the adiabatic reforming stages and wherein carbon monoxide containing gas characterised by having a molar ratio of hydrogen to carbon of less than 4.5 is added prior to at least one of the endothermic or adiabatic steam reforming stages and/or prior to the autothermal steam reforming step.

Abstract: Process for the preparation of dimethyl ether product by catalytic conversion of synthesis gas to dimethyl ether comprising the steps of contacting a stream of synthesis gas comprising carbon dioxide in a dimethyl ether synthesis step in one or more reactors and with one or more catalysts being active in formation of methanol and dehydration of methanol to dimethyl ether, to form a product mixture comprising the dimethyl ether and carbon dioxide, washing the product mixture in a scrubbing zone with a liquid solvent being rich in dialkyl ether of a polyalkylene glycol and thereby dissolving carbon dioxide and dimethyl ether in the liquid solvent, treating the liquid solvent being withdrawn from the scrubbing zone sequentially in separation zone to effect desorption of the dissolved carbon dioxide and to recover a substantially pure dimethyl ether product and the liquid solvent in its substantially lean form and recycling the lean liquid solvent to the scrubbing zone.

Abstract: Process and apparatus for the preparation of synthesis gas by catalytic steam and/or CO2 reforming of a hydrocarbon feedstock comprising the following steps: (a) heating the reaction mixture of hydrocarbon and steam and/or CO2 in a heated steam reforming unit integrated with the flue gas containing waste heat section from the fired tubular reformer in which reforming of the reaction mixture takes place by contact with a solid reforming catalyst (b) feeding the partially steam reformed mixture to the fired tubular reformer and further reforming the mixture to the desired composition and temperature, wherein the heated steam reforming unit comprises a piping system containing reaction sections with solid reforming catalyst comprising catalyst pellets and/or catalysed structured elements, the piping system being part of the process gas piping system integrated with the flue gas-containing waste heat section.

Abstract: Process for cooling an exothermic reaction zone by introducing a stream of water and a hydrocarbon-containing stream into a plurality of humidifying tubes extending through a catalytic exothermic reaction zone of a catalytic fixed bed with solid catalyst, introducing a process stream into the reaction zone for one or more catalytic exothermic reactions, passing the stream of water in a falling film along the inner circumference of the humidifying tubes, humidifying the hydrocarbon-containing stream with water in the humidifying tubes in indirect heat exchange with the exothermic reaction zone, withdrawing cooled reaction product of the exothermic reaction from the reaction zone, withdrawing the heated humidified, hydrocarbon-containing stream from the humidifying tubes, and transferring the heated humidified, hydrocarbon-containing process stream for further processing.

Abstract: Process and reaction unit for isothermal shift conversion of a carbon monoxide containing feed gas, the process comprising the steps of introducing the feed gas in a reaction unit into reactor tubes with a fixed bed of a shift conversion catalyst in a reaction zone; contacting the feed gas with the catalyst at conditions being effective in carbon monoxide shift conversion reaction with steam reactant to hydrogen and cooling the reaction by indirect heat exchange with a cooling agent by passing the cooling agent in a falling film along shell side of the reactor tubes and removing heated cooling agent from the falling film; passing hydrogen when it is formed by the shift conversion reaction through a hydrogen selective membrane to a permeate zone; withdrawing hydrogen from the permeate zone and carbon monoxide depleted feed gas from the reaction zone.

Abstract: Process and system for the production of synthesis gas from a hydrocarbon feed stock comprising the steps of endothermic and/or adiabatic catalytic steam reforming and autothermal steam reforming in series, wherein the steam reforming is carried out in one or more endothermic stages in series or in one or more adiabatic steam reforming stages in series with intermediate heating of feed stock gas leaving the adiabatic reforming stages and wherein carbon monoxide containing gas characterised by having a molar ratio of hydrogen to carbon of less than 4.5 is added prior to at least one of the endothermic or adiabatic steam reforming stages and/or prior to the autothermal steam reforming step.

Abstract: A process and reaction unit for isothermal shift conversion of a carbon monoxide containing feed gas. The process comprises the steps of introducing the feed gas in a reaction unit into reactor tubes with a fixed bed of a shift conversion catalyst in a reaction zone, contacting the feed gas with the catalyst at conditions being effective in carbon monoxide shift conversion reaction with steam reactant to hydrogen and cooling the reaction by indirect heat exchange with a cooling agent by passing the cooling agent in a falling film along shell side of the reactor tubes and removing heated cooling agent from the falling film, passing hydrogen when it is formed by the shift conversion reaction through a hydrogen selective membrane to a permeate zone, and withdrawing hydrogen from the permeate zone and carbon monoxide depleted feed gas from the reaction zone.