Haldor Topsoe A/s

Haldor Topse A/s

Topsoe A/s

Christian Henrik Speth

Per Juul Dahl

Niels Christian Schjødt

Annette E Krøll Jensen

Marcus Symreng

Thomas Rostrup-Nielsen

Tommy Lykke Wind

Pat A Han

Anders Helbo Hansen

Emil Andreas Tjärnehov

Niels Ulrik Andersen

Uffe Bach Thomsen

Lari Bjerg Knudsen

Annette E Kroll Jensen

Anne Krog Jensen

Peter Bruun Jensen

Niels Christian SCHJØDT

Niels Christian Schjodt

Parallel co-production process for the production of methanol and urea product from a hydrocarbon containing feedstock by means of autothermal reforming, intermediary methanol and ammonia formation and conversion of the ammonia to urea product and catalytic oxidation of the methanol to formaldehyde.

Process for the production of urea formaldehyde concentrate

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

The present invention relates to a revamp method for increasing the front-end capacity of a plant comprising

Low steam/carbon revamp of a plant comprising a steam reforming section and a water-gas shift section

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.

Method and catalysts for the production of ammonia synthesis gas

A method and an apparatus for protection of a combustion unit of a chemical process against over firing, the burner(s) of the combustion unit are limited by a fuel and duty limiter which limits the duty based on process feeds, combustion gas and fuel flows.

Over firing protection of combustion unit

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

A method and reactor for performing exothermic reactions with parallel operated catalyst modules arranged in stacked order within a pressure shell and adapted to axial flow of process gas through one or more catalyst layers and at least one catalyst layer cooled by an intrabed heat exchanger.

Method and reactor for performing exothermic reactions

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

In a cooled axial/radial flow converter, in which process gas passes from an outer annulus via a catalyst bed to an inner center tube, the catalyst bed is divided into identical modules stacked on top of each other. The process gas reaches the catalyst through openings facing the outer annulus, passes axially down the catalyst bed of each module, leaves the module through collectors in the bottom thereof, and flows to the center tube. The catalyst bed is cooled by cooling panels, in which the process gas is pre-heated to the reaction temperature, while at the same time the heat of reaction is partly removed from the catalyst bed. The converter is especially suitable as ammonia converter.

Axial-radial flow converter

In an ammonia or hydrogen plant comprising a desulfurisation section, a reforming section and a shift section, where the shift section comprises a low temperature shift converter and a medium temperature shift converter, a vent line is arranged downstream from the low temperature shift converter and the medium temperature shift converter in order to allow the shift converters to be re-heated with process gas at a low pressure (typically 3-7 bar). This way condensation of water vapour in the process gas is avoided. By applying this vent line it becomes possible to save significant time, more specifically 8-24 hours, for restarting the production after temporary shut-down thereof, because a heat-up of the LTS/MTS converter in circulating nitrogen is avoided.

Vent line for use in ammonia and hydrogen plants

Process for the preparation of ammonia comprising steps of

Process for the preparation of ammonia

Process for the integrated preparation of ammonia and urea

The invention relates to ammonia synthesis loops containing gases, which do not react and would accumulate if they were not purged out. By the present invention ammonia in a purge gas is recovered by an absorption agent operating at the full synthesis loop pressure. The absorption agent is chosen in such a way that the ammonia can be removed again by passing a gas comprising hydrogen and nitrogen through it at the same elevated pressure as the loop pressure. This enables the adsorption agent to be regenerated by fresh synthesis gas coming from the synthesis gas compressor just before this gas enters the synthesis loop. Thereby, the regeneration requires an absolute minimum of energy consumption and equipment.

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Lynge, Denmark

Christian Henrik Speth