Following today's demand and competitiveness in e.g. ammonia production, significant efforts have been put into developing optimized production for ammonia plants, with the objective to improve overall energy efficiency and reduce capital cost. The need for more cost-efficient production solutions has spurred the development of technology and catalysts for large-scale ammonia production units, in order to benefit from economy of scale. Production plants such as H2and ammonia plants have a long lifetime which means that the development within the field has led to new and better solutions for new plants before an old plant is “run out”. However by revamping existing plants it is possible to optimize older plants to achieve positive effects on field, economy and environmental parameters.

Targeted revamps of existing plants is thus an important but not trivial option as solutions viable in new plants may not necessarily be the best option in relation to revamps of existing plants as well as solutions which may not be the best option in a new plant still may provide a significant improvement during a revamp.

According to the present invention is provided a method for increasing the front-end capacity of a plant comprisinga reforming section, wherein a feed is reformed in at least one reforming step to a reformed stream comprising CH4, CO, CO2, H2and H2Oa shift section wherein the reformed stream is shifted in at least a high temperature shift (HTS) step (CO+H2O↔CO2+H2+heat),
said method comprising the steps ofIn the HTS step exchanging an original Fe-based catalyst with a non-Fe-based catalystIncreasing the feed flow to the reforming section, andThe HTS step is carried out at a reduced steam/dry-gas (S/DG) ratio compared to an original S/DG in the original HTS step with the original Fe-based catalyst.

I.e. by the present method it is possible to increase the capacity of an existing front-end, and thereby of an existing production plant and process by a highly efficient revamp solution.

By reducing the relative steam amount in the feed, it is possible that the mass flow through the plant is reduced allowing a larger natural gas throughput and thus increased capacity of the plant.

Even when the firing profile in the reformer section e.g. in the primary reformer is kept constant it is possible to increase production capacity up to e.g. 3-5% by the present method for revamping a plant when used in an existing ammonia plant.

The present method may be especially beneficial when applied on an existing H2plant, NH3plant or in a plant producing synthesis gas for H2or NH3production.

Depending on the type of plant, location, feeds available on site etc., the feed may be natural gas (e.g. comprising mainly CH4including possibly small amounts of higher hydrocarbons, nitrogen, CO2and other traces), naphtha, rich gases, LPG etc. or combinations hereof.

In known standard plants of the type mentioned above the standard original catalyst is a Fe-based catalyst comprising oxides of Fe, Cr (0-20% wt/wt) and/or Cu (0-10% wt/wt).

The above mentioned Fe-based catalysts are typically containing iron oxide as the main component; i.e. the iron oxide content on a weight basis exceeds 50%. This is valid both for the catalyst in its oxidized and reduced (activated) form.

The non-Fe-based catalysts may either be completely free of iron (other than trace levels) or may contain limited amounts of Fe (up to 10% iron oxide on a weight basis).

Fe-based catalysts suffer from an inherent weakness, namely their propensity to form iron carbides or even elemental iron under conditions of low S/DG ratios. This is exemplified by the following reaction:
5Fe3O4+32CO↔3Fe5C2+26CO2(1)

Formation of iron carbide and/or elemental iron will weaken the catalyst pellets and may result in catalyst disintegration and pressure drop increase.

Furthermore, iron carbide will catalyze Fischer-Tropsch by-product formation
nCO+(n+m/2)H2↔CnHm+nH2O  (2)

The Fischer-Tropsch reactions consume hydrogen, whereby the efficiency of the shift section is reduced.

Thus, the standard use of iron based HT shift catalyst requires a steam/carbon (S/C) ratio of around 2.6 or above to avoid iron carbide formation.

The applicant has shown that using a non-Fe-based catalyst such as a promoted zinc-aluminum oxide based catalyst, for example the Topsøse SK-501 FIex™ HT shift catalyst, which enables operation of the reforming section and HT shift section at a S/C ratio down to 0.3 is a highly advantageous substitute for the standard original Fe based catalyst. The new non-Fe-based HTS catalyst is not limited by S/C and/or S/DG requirements which results in high operational flexibility and a benefit of capacity revamping with a non-Fe-based catalyst e.g. promoted zinc-aluminum oxide based catalyst such as SK-501 FIex™ is seen which was not possible with the previous conventional HTS catalysts.

In advantageous embodiments of the method the non-Fe-based catalyst is a zinc-aluminum oxide based catalyst which in its active form comprises a mixture of zinc aluminum spinel and zinc oxide in combination with an alkali metal selected from the group consisting of Na, K, Rb, Cs and mixtures thereof, and optionally in combination with Cu. The catalyst may have a Zn/AI molar ratio in the range 0.5 to 1.0, a content of alkali metal in the range 0.4 to 8.0 wt % and a copper content in the range 0-10% based on the weight of oxidized catalyst.

The shift section may comprise one or more HT shift steps together with one or more medium temperature (MT) shift steps and/or one or more low temperature (LT) shift steps.

The temperature in the HT shift step may e.g. be in the range 300-600° C., such as 360-470° C. For example, the high temperature shift inlet temperature may be 300-400° C., such as 350-380° C.

This lowered requirement to the S/C and/or S/DG ratio enables an increased feed flow into the reforming section resulting in increased production rates.

In preferred embodiments the HTS step may be carried out at a reduced S/DG ratio of 0.1-0.9 such as 0.2-0.5 or 0.25-0.45 or 0.3-0.44.

The requirement of a minimum S/DG ratio in the HTS reactor represents a significant impediment for many producers wanting to remain competitive in the current market.

Removing or minimizing the S/DG limitation according to the present invention allows producers to achieve better profitability through increased production capacity, which is essential in today's economy of rising costs and rapid market fluctuations.

The S/DG ratio is defined as the ratio of steam and the dry process gas on molar basis inlet the HTS reactor.

The S/C ratio is defined as the ratio of all steam added to the reforming section up-stream the HT shift section and the hydrocarbons in the feedgas to the reforming section on molar basis.

In various embodiments the S/DG ratio is reduced with 5-25%, such as 10-20%, e.g. with 12-17% with respect to the original S/DG ratio.

Original S/DG, original HTS step, original Fe-based catalyst, original steam addition refers to the S/DG, HTS step, catalyst, steam addition prior to revamp. I.e. Original is used for terms pre-revamp.

Preferably the feed flow is increased with at least 2% preferably as at least 5%. For example the feed flow is increased 2-25%, such as 4-20%.

When the feed flow is increased and the steam addition is kept constant or only raised less than the feed flow the S/DG ratio is lowered compared to the original process.

However, it is possible that the steam addition up-stream the HTS step is reduced compared to the original steam addition by 0.1-50%, such as 0.5%-15%, such as 1-10%.

By reducing the steam amount in the feed the mass-flow through the plant is reduced allowing a larger natural gas throughput and thus increased capacity of the plant. The firing profile in the primary reformer may be kept constant to maintain design conditions for the primary reformer and/or other parts of the reforming section.

The pressure drop dP is generally increased compared to the original dP when the capacity of the plant is increased. The increased pressure drop dP which may be induced by the present method (due to increased plant load when increasing the capacity up to e.g. 3-5%) can be at least partly compensated if desired by using low pressure drop catalyst (e.g. in the reforming section and in additional shift step(-s)). Further pressure drop reduction is possible by replacing most of the aluminum support balls with a catalyst support grid in the bottom of the HTS reactor. The support grid consists of a modified outlet collector, outlet brackets, outlet connector rods, skirt section and a mesh grid section, all of which float in the bottom of the vessel.

The reforming section may comprise a primary reformer possibly in combination with a pre-reformer and/or additional reformer types in parallel and/or series.

The shift section may further comprise one or more Medium and/or Low temperature shift steps.

The reforming section is optionally revamped to include one or more reformer types, adiabatic, gas/flue gas convective, gas/gas convective, radiant, autothermal. Furthermore, the present revamp of an existing process and plant may be combined with one or more additional revamps up- and/or downstream the reforming section.

