Haldor Topsoe A/s

Haldor Topse A/s

Topsoe A/s

Per Juul Dahl

Christian Henrik Speth

Niels Christian Schjødt

Peter Mølgaard Mortensen

Max Thorhauge

Annette E Krøll Jensen

Emil Andreas Tjärnehov

Marcus Symreng

Niels Christian Schjodt

Kim Aasberg-Petersen

Thomas Sandahl Christensen

Martin Østberg

Robert Klein

Henrik Otto Stahl

Kasper Emil Larsen

Hassan Modarresi

Christophe Duwig

Søren Grønborg Eskesen

Esben Lauge Sørensen

Tommy Lykke Wind

Stefan Andersen

Marcus Almqvist

Annette E Kroll Jensen

Janni Østergaard

Johannes Quintero

Tais Bjerg Claridge

Niels Christian SCHJØDT

Janni Ostergaard

A process for producing synthesis gas, the process comprising the steps of a) reforming a hydrocarbon feed in a reforming section thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O and impurities comprising ammonia; b) shifting the synthesis gas in a shift section comprising one or more shift steps in series to a shifted synthesis gas; c) separating from the shifted synthesis gas a process condensate originating from cooling and optionally washing of the shifted synthesis gas; d) passing a part of the process condensate to a condensate steam stripper, wherein dissolved shift byproducts comprising ammonia, methanol and amines formed during shifting the synthesis gas are stripped out of the process condensate using steam resulting in a stripper steam stream, e) adding the stripper steam stream from the process condensate steam stripper to the hydrocarbon feed and/or to the synthesis gas downstream the reforming section, up-stream the last shift step, wherein the remaining part of the process condensate is purged.

Process for the production of synthesis gas

An offshore installation or offshore vessel is provided which comprises a reactor system for carrying out steam reforming of a feed gas comprising hydrocarbons.

Offshore reforming installation or vessel

Process for the production of a product gas containing nitrogen and hydrogen from ammonia comprising the steps of non-catalytic partial oxidation of ammonia with an oxygen containing gas to a process gas containing nitrogen, water, amounts of nitrogen oxides and residual amounts of ammonia; cracking of at least a part of the residual amounts of ammonia to hydrogen and nitrogen in the process gas by contact with a nickel containing catalyst and simultaneously reducing the amounts of nitrogen oxides to nitrogen and water by reaction with a part of the hydrogen formed during cracking of the process gas by contact of the process gas with the nickel containing catalyst; and withdrawing the hydrogen and nitrogen containing product gas.

Autothermal ammonia cracking process

A method for producing methanol comprises the steps of passing a feed stream of methanol synthesis pas through a main methanol reactor containing a methanol synthesis catalyst, to form a mixed gas containing methanol, cooling the mixed gas containing methanol, separating methanol from the mixed pas and heating the mixed gas. The stream of heated mixed gas is passed through an additional methanol reactor containing a methanol synthesis catalyst, and the effluent from the additional methanol reactor is mixed with the feed stream of methanol synthesis gas and passed through the main methanol reactor.

Method for producing methanol in a reactor with bypass

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&#xb0; C. Methanol of different product grades may be obtained by operating in specific areas of the operational window.

Process and a plant for the production of methanol

The invention relates to a chemical reactor and reformer tubes for reforming a first feed stream comprising a hydrocarbon gas and steam. The chemical reactor comprises a shell with a heat source and one or more reformer tubes. The reformer tube is arranged to house catalyst material and is arranged to being heated by the heat source. The reformer tube comprises a first inlet for feeding said first feed stream into a first reforming reaction zone of the reformer tube, and a feed conduct arranged to allow a second feed stream into a second reforming reaction zone of the reformer tube. The second reforming reaction zone is positioned downstream of the first reforming reaction zone. The feed conduct is configured so that the second feed stream is only in contact with catalyst material in the second reforming reaction zone. The invention also relates to a process of producing CO rich synthesis gas at low S/C conditions.

CO rich synthesis gas production

In a cooled axial flow converter, in which process gas passes from an outer annulus via a catalyst bed, wherein the process gas is converted to a product, to an inner centre tube, the catalyst bed comprises at least one module comprising at least one catalyst layer. Feed means are arranged to provide a flow of process gas from the outer annulus to an inlet part of one or more modules, and collector means are arranged to provide a flow of product stream of converted process gas, which has passed axially down the catalyst bed of one or more of the modules to the centre tube. At least one of the one or more modules comprises one or more cooling plates arranged to be cooled by a cooling fluid.

Cooled axial flow converter

A process for producing an ammonia synthesis gas, said process comprising the steps of: &#x2014;Reforming a hydrocarbon feed in a reforming step thereby obtaining a synthesis gas comprising CH, CO, CO, Hand HO, &#x2014;Shifting the synthesis gas in one in or more shift steps in series, &#x2014;Optionally wash the synthesis gas leaving the shift section with water, &#x2014;Sending the process condensate originating from cooling and washing the synthesis gas leaving the shift section to a process condensate stripper wherein the dissolved shift byproducts and dissolved gases are stripped out of the process condensate using steam resulting in a steam stream containing more than 99% of the dissolved methanol in process condensate. &#x2014;Adding all or part of said steam stream from the process condensate stripper to the synthesis gas downstream the reforming step, prior to the last shift step, wherein &#x2014;The steam/carbon ratio in the reforming step and the shift step is less than 2.6.

Ammonia process using advanced shift process

In an adiabatic axial flow converter, in which process gas passes from an outer annulus via a catalyst bed, wherein the process gas is converted to a product, to an inner centre tube, the catalyst bed comprises at least one module comprising one or more catalyst layers. Feed means are arranged to provide a flow of process gas from the outer annulus to an inlet part of one or more modules, and collector means are arranged to provide a flow of product stream of converted process gas which passes axially through the catalyst bed of one or more of the modules to the centre tube.

Adiabatic axial flow converter

A process for producing urea with controlled excess of COand/or NH. The process includes the steps of: reforming the hydrocarbon feed gas, thereby obtaining a synthesis gas comprising CH, CO, CO, Hand HO, shifting the synthesis gas, removing COfrom the synthesis gas, removing residual HO and/or COfrom the synthesis gas, removing CH, CO, Ar and/or He, and adding stoichiometric nitrogen to produce NHto the synthesis gas, synthesizing NHto obtain a NHproduct, and adding at least part of the product COand at least part of the NHproduct to a urea synthesis step to make a urea product. The amount of excess COand/or NHis controlled by adjusting the steam/carbon in the reforming step and/or the HO addition upstream the shift step and/or adjusting the inlet temperature to at least one or more shift steps.

Urea process with controlled excess of COand/or NH

A process for producing an ammonia synthesis gas, said process including the steps of: reforming a hydrocarbon feed in a reforming step thereby obtaining a synthesis gas comprising CH, CO, CO, Hand HO; and shifting said synthesis gas in a high temperature shift step over a promoted zinc-aluminum oxide based high temperature shift catalyst, wherein the steam/carbon ratio in the reforming step is less than 2.6.

ATR based ammonia process and plant

A heat exchanger has a pass baffle which is formed as an enclosure with two openings, one opening for connection to a shell-side fluid opening and one opening for passing heat exchanger tubes.

True countercurrent heat exchanger with sealing arrangement

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 COcompressor is saved, and the amount of poisonous sulfur in the make-up gas is markedly reduced.

Method for methanol synthesis

In a process for co-production of ammonia and methanol, the outlet stream from the reformer is split into two parts, one of which is subjected to shift, carbon dioxide removal, methanation, compression and ammonia synthesis, while the other part is compressed and fed to a once-through methanol synthesis section. Methanol is withdrawn from the methanol synthesis section, and the remaining effluent from said section is divided into two streams comprising hydrogen, of which one is fed to the shift section, while the other is recycled to the desulfurization unit. This way a favourable co-production method is obtained because recycle hydrogen for the desulfurization is provided, and furthermore a compression step is avoided.

Process for co-production of ammonia and methanol

The present invention relates to a process for heating an ATR or POX comprising the steps of heating a process stream by at least one heating means, admitting the heated process stream to an ATR or POX reactor through a main burner, and heating the ATR or POX reactor to or above autoignition temperature of the process stream via the heated process stream.

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Vedbæk, Denmark

Per Juul Dahl