Method for producing blue ammonia

Abstract

The present disclosure provides an ammonia production plant in which a heat exchanger for steam generation (HP and / or MP steam) and / or steam overheating (utilizing process stream) is arranged downstream of the ATR section and between a high temperature (HT) shift section and a subsequent second shift section. In this manner, since partial steam superheating is performed in the process cooling roll set, less steam is generated at the front end and less steam superheating is required in the combustion type steam superheater.

Description

Methods for producing blue ammonia Technical Field

[0001] This invention relates to an ammonia production apparatus and a method for producing ammonia, wherein a heat exchanger for steam generation and / or steam superheating is arranged downstream of the ATR section, between the high-temperature (HT) converter section and the second converter section (low-temperature (LT) or alternatively, the medium-temperature (MT) converter section), and downstream of the ammonia converter in the ammonia synthesis loop. The method and system of this invention can be used in any ammonia production apparatus. Background Technology

[0002] Blue ammonia is a fossil fuel-based product that emits minimal CO2 into the atmosphere during its production. It is considered a transitional product between traditional fossil fuel-based ammonia and green ammonia produced from green or renewable electricity, water, and air. The CO2 produced during blue ammonia production should be permanently stored or converted into other chemicals. The main steps in producing blue ammonia are essentially the same as those in producing traditional fossil fuel-based ammonia, the difference being the capture of more carbon from carbon-based fuels, thus providing possibilities for further processing.

[0003] The key here is that blue ammonia releases no carbon dioxide when used as fertilizer or burned. Currently available technologies capture almost all of the CO2 produced during the conversion process, making this fuel one of the first carbon-free fuel options for large-scale use. Blue ammonia is considered an environmentally friendly product that can be used indefinitely until sufficient renewable or green electricity is available for its production.

[0004] Utility prices vary depending on the location of the equipment / site. The optimal and most attractive blue ammonia layout, given a specific utility price, also varies accordingly. It may also be desirable to avoid or reduce the need for combustion-type steam superheaters.

[0005] The known techniques in this field are described in WO2018 / 149641, PCT / EP2022 / 059091 and PCT / EP2023 / 061637. Summary of the Invention

[0006] An ammonia production apparatus is provided, the apparatus comprising: - a hydrocarbon feed; - a burner steam feed; - a process steam feed; - an oxygen feed; - a nitrogen feed; - boiler feedwater; - a feed preheater arranged for preheating the hydrocarbon feed to produce a preheated hydrocarbon feed; - a feed purification section arranged for hydrogenating the preheated hydrocarbon feed and removing sulfur-containing compounds therein to produce a purified hydrocarbon feed; - a pre-reforming feed preheater arranged for heating a mixed stream comprising the purified hydrocarbon feed and the process steam feed to produce a heated mixed stream; - a pre-reforming section arranged for pre-reforming the heated mixed stream from the pre-reforming feed preheater to produce a first process gas flow; - a process gas preheater arranged for heating the first process gas flow to produce a heated first process gas flow; The self-heating reforming (ATR) section is arranged to receive at least a portion of the heated first process gas stream, the oxygen feed, and the burner steam feed, and to generate a second process gas stream; - a steam drum is arranged to receive boiler feedwater and provide a first boiler water stream and a second boiler water stream; - a first waste heat boiler (WHB) is arranged to exchange heat between at least a portion of the second process gas stream and the first boiler water stream from the steam drum, and to generate a cooled second process gas stream and a first steam stream; - a high-temperature (HT) conversion section is arranged to receive the cooled second process gas stream from the first waste heat boiler and to generate a third process gas stream; A second waste heat boiler is arranged to exchange heat between at least a portion of the third process gas stream and a second boiler water stream from the steam drum, producing a cooled third process gas stream and a second steam stream; and / or a steam superheater is arranged to exchange heat between at least a portion of the third process gas stream and a steam stream from the steam drum, producing a cooled third process gas stream and a superheated steam stream; provided that, when the ammonia production plant includes a second waste heat boiler and a steam superheater, the third process gas stream is arranged to be fed into the steam superheater and cooled into a third process gas stream, and then the third process gas stream is arranged to be fed into the second waste heat boiler and cooled into a further cooled third process gas stream; - a second conversion section is arranged to receive the cooled third process gas stream and produce a fourth process gas stream; - a second conversion section is arranged to receive the third process gas stream and produce a fourth process gas stream; - a syngas purification section is arranged to receive the fourth process gas stream and the nitrogen feed, and produce a syngas stream comprising hydrogen and nitrogen (e.g., in a ratio of 3:1), a CO2-rich stream, process condensate, and at least one tail gas stream; The ammonia synthesis circuit is arranged to receive the synthesis gas stream and generate the first ammonia-rich stream.

[0007] A method for generating ammonia in the ammonia-generating equipment described herein is also provided.

[0008] Further details of the apparatus and method are specified in the following detailed description, drawings and claims. Attached Figure Description

[0009] Figure 1 shows the layout of an ammonia production device according to the present invention.

[0010] Figure 2 shows an alternative layout of the ammonia production equipment according to the present invention.

[0011] Figure 3 shows the layout of the syngas purification section and ammonia circuit, which can be used in the ammonia production equipment shown in Figures 1 and 2.

[0012] Figure 4 shows the layout of an ammonia production equipment based on a combination of the layouts in Figures 1 and 2.

[0013] Figure 5 shows when different steam generation systems become attractive relative to natural gas and electricity prices.

[0014] Figure 6 shows the layout of an ammonia production unit, an improvement on the layout in Figure 4, designed for maximum HP steam generation.

[0015] Figures 7, 8, and 9 show various layouts of the ammonia production apparatus according to the present invention. Figure 7 is a layout for achieving reduced HP steam generation.

[0016] Figure 8 shows the layout for achieving reduced front-end HP steam generation and loop MP steam generation.

[0017] Figure 9 shows the layout for generating superheated MP steam in the front end and loop. A combustion-type steam superheater is not required.

[0018]

[0019] Unless otherwise stated, any given percentage of gas content is by volume. The terms “syngas” and “synthesis gas” are used interchangeably herein.

[0020] An ammonia production apparatus (A) is provided. The feeds into the apparatus include: - hydrocarbon feed (typically natural gas or biogas); - burner steam feed; - process steam feed; - oxygen feed; - nitrogen feed; and - boiler feedwater.

[0021] A feed preheater is arranged to preheat the hydrocarbon feed and produce preheated hydrocarbon feed. The typical temperature of the preheated hydrocarbon feed is between 350 and 400°C. Preheating of the hydrocarbon feed can be carried out in heating coils within a combustion heater. Alternatively, the feed preheater can be an electric heater.

[0022] On one hand, the feed preheater can be arranged to preheat the hydrocarbon feed by exchanging heat with at least a portion of the second steam stream. Advantageously, this will also allow for a reduction in the size of the gas-fired process heater. To achieve the preheating temperature required for the process stream, the steam temperature will need to be sufficiently high for preheating. If superheated HP steam is produced, the temperature of the superheated HP steam is typically 510°C, and for superheated MP steam, it is typically 380°C. This sets a limitation on preheating the process stream with steam.

[0023] A feed purification section is arranged to hydrogenate the preheated hydrocarbon feed and remove sulfur-containing compounds, producing purified hydrocarbon feed. The feed purification section suitably includes a hydrogenation unit located upstream of the sulfur removal unit. Hydrogenation removes any unsaturated components from the hydrocarbon feed. Both unsaturated and sulfur-containing components in the hydrocarbon feed can contaminate the downstream catalyst in the ammonia production unit.

[0024] The purified hydrocarbon feed is mixed with the process steam feed and then reheated in a pre-reformer feed preheater to produce a heated mixed stream. The typical temperature of the heated mixed stream is between 400 and 550°C. The pre-reformer feed preheater may include heating coils within a combustion heater, similar to the feed preheater described above.

[0025] The heated mixture is fed into a pre-reforming section, which is configured to pre-reform the heated mixture and generate a first process gas stream. Pre-reforming is a process in which methane and heavier hydrocarbons are steam-reformed, and the reforming product of the heavier hydrocarbons is methanated. Nickel-containing catalysts are typically used. Pre-reforming sections suitable for this process are known to those skilled in the art.

[0026] The first process gas stream is then fed into a process gas preheater, which is configured to heat the first process gas stream and generate a heated first process gas stream. The typical temperature of the heated first process gas stream is between 350 and 650°C.

[0027] The apparatus includes an autothermal reforming (ATR) section, which is arranged to receive at least a portion of a heated first process gas stream, oxygen feed, and burner steam feed, and to generate a second process gas stream. The autothermal reforming section, catalyst, and conditions are known to those skilled in the art.

[0028] The ammonia production equipment includes a steam drum. The steam drum is arranged to receive boiler feedwater and provide a first boiler water flow and a second boiler water flow. In one aspect, the steam drum is arranged to receive at least a first steam flow from a first waste heat boiler, and optionally a second steam flow from a second heat exchanger (if it is a waste heat boiler). The steam drum may also receive steam from heat exchangers in the ammonia circuit.

[0029] Suitably, the second boiler water flow is in the form of a water flow, and the steam drum is also arranged to receive at least a first steam flow from the first waste heat boiler and a second steam flow from the second heat exchanger. The ammonia production unit further includes a combustion-type steam superheater, which is arranged to receive and superheat the saturated steam flow from the steam drum to provide a superheated steam flow. The combustion-type superheater has a fuel flow. The fuel used for the combustion-type heater and the combustion-type steam superheater is suitably a combination of exhaust gas from the equipment and natural gas. Steam superheating in the combustion-type steam superheater also takes place in the heating coils.

[0030] Steam production (superheated HP steam and / or superheated MP steam in the front-end and synthesis loop) can be minimized or maximized based on actual utility prices and the most attractive approach in a given situation. Medium-pressure steam production in the front-end and loop, as well as steam superheating after the first shift reactor in the process cooling chain, is attractive for high natural gas prices and / or low electricity prices. Maximum steam production is attractive for low natural gas prices and / or high electricity prices. By replacing the waste heat boiler downstream of the first shift reactor with a steam superheater, less steam is produced at the front-end, and less steam superheating is required in the gas-fired steam heater due to partial steam superheating in the process cooling rollers. The size of the combustion steam superheater load is thus reduced, and in cases where MP steam is produced in the front-end and loop, the combustion steam superheater can even be avoided. Furthermore, layouts with high front-end pressures are found to be attractive in blue ammonia processes across a wide range of utility price ranges.

[0031] A first waste heat boiler is arranged to exchange heat between at least a portion of the second process gas stream and a first boiler water stream from a steam drum, thereby generating a cooled second process gas stream and a first steam stream. The first steam stream is then returned to the steam drum.

[0032] The high-temperature (HT) shift section is configured to receive the cooled second process gas stream from the first waste heat boiler and generate the third process gas stream. The desired syngas composition can be achieved through this shift section. Shift refers to the water-gas shift reaction (WGSR) or shift reaction, where carbon monoxide and water vapor react to form carbon dioxide and hydrogen.

[0033] WGSR is an important industrial reaction used to produce ammonia, hydrocarbons, methanol, and hydrogen. It is also frequently used in conjunction with steam reforming of methane and other hydrocarbons. In Fischer-Tropsch synthesis, WGSR is one of the most important reactions for balancing the H2 / CO ratio. The water-gas shift reaction is a moderately exothermic and reversible reaction. Therefore, the reaction rate increases with increasing temperature, but carbon dioxide production becomes unfavorable. Due to its exothermic nature, a low carbon monoxide percentage is thermodynamically favorable at lower temperatures. Despite the thermodynamic advantage at lower temperatures, the reaction is faster at higher temperatures.

[0034] The second waste heat boiler is located downstream of the HT converter section and is arranged to exchange heat between at least a portion of the third process gas stream and the second boiler water stream from the steam drum. This produces a cooled third process gas stream and a second steam stream. The second steam stream is then returned to the steam drum.

[0035] Alternatively, a steam superheater is arranged to exchange heat between at least a portion of the third process gas stream and the steam stream from the steam drum, thereby producing a cooled third process gas stream and a superheated steam stream. In the case where steam generation and superheating occur downstream of the HT converter section, the steam superheater is located upstream of the second waste heat boiler. In other words, when the ammonia production plant includes a second waste heat boiler and a steam superheater, the third process gas stream is arranged to be fed into the steam superheater and cooled into a third process gas stream, which is then arranged to be fed into the second waste heat boiler and cooled into a further cooled third process gas stream.

[0036] Subsequently, a second conversion stage is arranged to receive the third process gas stream and generate the fourth process gas stream. The second conversion stage can be a low-temperature (LT) or medium-temperature (MT) conversion stage, and is preferably a low-temperature conversion stage. LT conversion typically takes place at a temperature between process gas Tdew + 15°C and 250°C, while MT conversion typically takes place between 190 and 330°C. At this temperature, CO is converted to a minimum to maximize H2 production and increase process carbon capture.

[0037] The syngas purification section is arranged to receive the fourth process gas stream and nitrogen feed, and to produce a syngas stream comprising hydrogen and nitrogen (e.g., in a 3:1 ratio), as well as: a CO2-rich stream, process condensate, and one or more tail gas streams. Suitably, the syngas purification section produces a syngas stream, a CO2-rich stream, process condensate, and one or more tail gas streams.

[0038] In one aspect, the syngas purification section includes a separator, a CO2 removal unit, and a hydrogen purification unit. The syngas purification section may include a separator, a hydrogen purification unit, and a CO2 removal unit in this order. The separator is typically arranged to receive the fourth process gas stream and produce a dry fourth process gas stream and process condensate. In a first aspect, the CO2 removal unit is arranged to receive the dry fourth process gas stream and produce a CO2-rich stream and a CO2-lean fourth process gas stream. The hydrogen purification unit is arranged to receive the CO2-lean fourth process gas stream and produce a syngas stream comprising hydrogen and nitrogen (e.g., in a 3:1 ratio) and a tail gas stream. In a further aspect, the hydrogen purification unit is arranged to receive the dry fourth syngas (or process gas) stream and produce a hydrogen product stream, one or more hydrogen-rich fuel streams, and a CO2-rich tail gas stream. The CO2 removal section is arranged to receive the CO2-rich tail gas stream and produce a CO2 product stream and a tail gas stream, which is further fed to one or more PSA units to produce a hydrogen-rich fuel stream and a carbon-rich stream. The latter is then recycled to the ATR.

[0039] In the alternative, the syngas purification section includes, in sequence, a separator, a hydrogen purification unit, and a CO2 removal unit. This arrangement ensures that the fourth process gas stream first passes through the separator, then through the hydrogen purification unit, and subsequently through the CO2 removal unit.

[0040] In a further aspect, as shown in Figure 4, a hydrogen purification unit arranged downstream of the CO2 removal section is configured to generate a tail gas flow, and at least a first portion of the tail gas flow is configured to be compressed in a compressor and combined with a first process gas flow upstream of the ATR section.

[0041] Alternatively, at least a second portion of the exhaust gas may be arranged as fuel supplied to a combustion heater, optionally combined with a portion of the synthesis gas.

[0042] The ammonia synthesis loop is arranged to receive the synthesis gas stream and generate a first ammonia-rich stream. In a standard layout, the ammonia synthesis loop includes an ammonia reactor, a recirculation compressor, an ammonia separator, and at least one heat exchanger arranged downstream of the ammonia separator. Suitably, a third boiler water stream is arranged to exchange heat in said at least one heat exchanger.

[0043] In one aspect, the ammonia production equipment includes a combustion heater and a fuel stream for the combustion heater. At least one (and preferably all) of the feed preheater, the pre-reformer feed preheater, and the syngas preheater includes heating coils within the combustion heater. Advantageously, a portion of the syngas stream, comprising hydrogen and nitrogen, is arranged to be supplied as fuel to the combustion heater.

[0044] A method for producing ammonia in the ammonia production apparatus (A) described herein is also provided, the method comprising the steps of: - providing the apparatus as described herein; - preheating a hydrocarbon feed in a feed preheater to produce a preheated hydrocarbon feed; - hydrogenating the preheated hydrocarbon feed in a feed purification section to remove sulfur-containing compounds therein to produce a purified hydrocarbon feed; - heating a mixed stream comprising the purified hydrocarbon feed and process steam feed in a pre-reformer feed preheater to produce a heated mixed stream; - pre-reforming the heated mixed stream from the pre-reformer feed preheater in a pre-reformer section to produce a first process gas stream; - heating the first process gas stream in a syngas preheater to produce a heated first process gas stream; - supplying at least a portion of the heated first process gas stream, the oxygen feed, and the burner steam feed into an autothermal reforming (ATR) section to produce a second process gas stream; - supplying boiler feedwater into a steam drum to provide a first boiler water stream and a second boiler water stream; - In a first waste heat boiler (WHB), at least a portion of the second process gas stream is heat-exchanged with a first boiler water stream from the steam drum, generating a cooled second process gas stream and a first steam stream; - The cooled second process gas stream from the first waste heat boiler is supplied to a high-temperature (HT) converter section to generate a third process gas stream; - In a second waste heat boiler, at least a portion of the third process gas stream is heat-exchanged with a second boiler water stream from the steam drum, generating a cooled third process gas stream and a second steam stream; and / or In a steam superheater, at least a portion of the third process gas stream is heat-exchanged with a steam stream from the steam drum, generating a cooled third process gas stream and a superheated steam stream; provided that, when the ammonia production plant includes a second waste heat boiler and a steam superheater, the third process gas stream is supplied to the steam superheater and cooled into a third process gas stream, and then supplied to the second waste heat boiler and cooled into a further cooled third process gas stream; - The cooled third process gas stream is supplied to a second converter section to generate a fourth process gas stream; The fourth process gas stream and the nitrogen feed are supplied to the syngas purification section to generate a syngas stream comprising hydrogen and nitrogen (e.g., in a ratio of 3:1), and at least one of the following: - a CO2-rich stream, process condensate, and one or more tail gas streams; - the syngas stream is supplied to the ammonia synthesis loop to generate a first ammonia-rich stream. Detailed Implementation

[0045] Detailed Implementation Plan

[0046] Figure 1 shows the layout of an ammonia production apparatus according to the present invention, having the following features: - Hydrocarbon feed (1) - Burner steam feed (2') - Process steam feed (2) - Oxygen feed (3) - Nitrogen feed (4) - Boiler feedwater (8) - Feed preheater (91) - Preheated hydrocarbon feed (1') - Feed purification section (80) - Purified hydrocarbon feed (1'') - Pre-reformer feed preheater (92) - Mixed stream (81) including purified hydrocarbon feed (1'') and process steam feed (2) - Heated mixed stream (81') - Hydrogenation unit (82) - Sulfur removal unit (83) - Pre-reformation section (20) - First process gas stream (21) - Syngas preheater (93) - Heated first process gas stream (21') - Autothermal reforming (ATR) section (30) - Second process gas stream (31) - Steam drum (110) - First boiler water flow (112) - Second boiler water flow (113) - First waste heat boiler (40) - Cooled second process gas flow (31') - First steam flow (41) - High temperature (HT) shift section (50) - Third process gas flow (51) - Waste heat boiler (70) - Cooled third process gas flow (51') - Second steam flow (71) - Second (e.g., low temperature (LT)) shift section (60) - Fourth process gas flow (61) - Combustion heater (90) - Fuel flow for combustion heater and combustion SSH (9) - Syngas purification section (100) - Syngas flow including hydrogen and nitrogen (104) - CO2-rich flow (101) - Process condensate (102) - Tail gas flow (151) (one or more) - Ammonia synthesis loop (200) - First ammonia-rich flow (201) - Combustion-type steam superheater (120) - saturated steam flow (111) - superheated steam flow (121) In Figure 2, the corresponding elements have the same reference numerals as in Figure 1. Other reference numerals are: - steam superheater (75) - superheated steam flow (115') - steam flow (115) Figure 3 shows the layout of the syngas purification section and ammonia circuit, which can be used in the ammonia production equipment shown in Figures 1 and 2. Other reference numerals are: - Separator (130) - Dried fourth process gas stream (131) - Process condensate (102) - CO2 removal unit (140) - CO2-rich stream (101) - CO2-lean fourth process gas stream (141) - Hydrogen purification unit (150) - Tail gas stream (151) - Ammonia reactor (240) - Recirculation compressor (220) - Ammonia separator (230) - Heat exchanger (250) - Synthesis gas stream (231, 221, 241) Figure 4 shows the layout of an ammonia production plant based on the combined layout of Figures 1 and 2.Other reference numerals are: - exhaust gas flow (151) - first part of exhaust gas flow (151) (151A) - exhaust gas recirculation compressor (160) - second part of exhaust gas flow (151) (151B) - compressed exhaust gas (161) Figure 6 shows an ammonia production plant layout improved from the layout of Figure 4. Other reference numerals are: - third boiler water flow (114) - third steam flow (114') Figure 7 shows an ammonia production plant layout similar to Figure 6, except that a portion of the superheated steam flow (115') from the steam superheater (75) passes through a combustion superheater (120) to provide a further superheated steam flow (121).

[0047] Figure 8 shows the layout of the ammonia production unit, similar to Figure 7, wherein the ammonia loop includes a loop waste heat boiler (250); a loop steam drum (260), which is arranged to provide a superheated medium-pressure steam flow (261) by exchanging heat between water flow and one or more (e.g., two) heat exchangers (251) in the ammonia loop. The last heat exchanger it passes through in the loop is a steam superheater (252).

[0048] Figure 9 shows a similar layout to Figure 8, where the superheated steam flow (115') from the steam superheater (75) does not pass through a further steam superheater (120). A combustion-type steam superheater (120) is not required because the steam has already been fully superheated in the steam superheater (75).

[0049] Example

[0050] Figure 5 shows when different steam generation systems become attractive, based on values ​​such as those in Table 1 below, and when natural gas or electricity prices change: Table 1:

[0051] Example 1

[0052] Table 2 shows the advantages of the proposed layout in terms of consumption value, CAPEX, specific carbon emissions, and carbon capture or recycling.

[0053] Traditional ammonia production typically involves maximum power steam generation and steam superheating for use in process steam and steam turbines.

[0054] Steam generation (HP steam and / or MP steam generation in the front end and synthesis loop) can be optimized, i.e., minimized or maximized based on actual utility prices and the most attractive practice under given conditions. Overall steam / electricity balance is approximated by inputting electricity.

[0055] To meet the 90% carbon capture requirement, a front-end was added to generate a supplemental excess H2 stream for use as fuel in the combustion heater / process furnace (combustion process preheater + combustion steam superheater). Table 2 shows the required front-end additions for various steam generation configurations.

[0056] This invention provides the layout of the last three columns on the right in Table 2, showing the results for an ammonia production unit with 3000MTPD blue ammonia and 90% carbon capture, from reduced HP generation to reduced MP steam generation in the front end and loop, by increasingly utilizing process heat to superheat the steam, thereby reducing steam production. Advantageously, in the latter case, a combustion-type steam superheater can be avoided. In contrast, all steam superheating is carried out in the process cooling roller assembly. The results show reductions in consumption, specific CO2 emissions, and CAPEX compared to the maximum HP steam generation in conventional ammonia production.

[0057] As can be seen from Table 2, if low-cost renewable electricity is available, MP steam generation in both the front end and the loop will be the most attractive layout. This scenario represents the minimum steam generation case, which has the lowest NG (feed + fuel) consumption of all cases, and as shown in Figure 5 above, at a natural gas price of approximately 7... It has advantages at / MMBTU and above. Furthermore, it has the lowest CAPEX value. Electricity input demand increases as steam production decreases, and is highest in this case. This means, as shown in Figure 5, at approximately 75 At low electricity prices below / MWh, MP steam generation in the front end and loop becomes attractive.

[0058] In the first three scenarios, flash vapor recirculation is included in the CO2 removal section to maximize CO2 capture in the process. For the last scenario (MP vapor generation in the front end and loop), when flash vapor recirculation is included in the CO2 removal section, 93% carbon capture can be achieved without generating supplemental hydrogen fuel. To achieve 90% carbon capture, the flash vapor from the CO2 removal section is therefore used as fuel for the combustion heater. This means that in this case, up to 93% carbon capture can be achieved without adding a front end for generating supplemental hydrogen fuel.

[0059]

[0060] The present invention has been described with reference to several aspects and accompanying drawings. However, those skilled in the art will be able to select and combine various aspects within the scope of the invention as defined by the appended claims. All documents referenced herein are incorporated by reference.

Claims

1. An ammonia production device (A), said device (A) comprising: - Hydrocarbon feed (1); - Burner steam feed (2'); - Process steam feed (2); - Oxygen feed (3); - Nitrogen feed (4); - Boiler feedwater (8); - Feed preheater (91), arranged to preheat hydrocarbon feed (1) and produce preheated hydrocarbon feed (1'); - Feed purification section (80), arranged to hydrogenate the preheated hydrocarbon feed (1') and remove sulfur-containing compounds therein, and produce purified hydrocarbon feed (1''); - Pre-reforming feed preheater (92), arranged to heat the mixed stream (81) including purified hydrocarbon feed (1'') and process steam feed (2), and produce heated mixed stream (81'); - Pre-reforming section (20), arranged to pre-reform the heated mixed stream (81') from the pre-reforming feed preheater (92), and produce first process gas flow (21); A process gas preheater (93) is arranged to heat the first process gas stream (21) and generate a heated first process gas stream (21'); - an autothermal reforming ATR section (30) is arranged to receive at least a portion of the heated first process gas stream (21'), the oxygen feed (3), and the burner steam feed (2') and generate a second process gas stream (31); - a steam drum (110) is arranged to receive boiler feedwater (8) and provide a first boiler water stream (112) and a second boiler water stream (113); - a first waste heat boiler (40) is arranged to exchange heat between at least a portion of the second process gas stream (31) and the first boiler water stream (112) from the steam drum (110) to generate a cooled second process gas stream (31') and a first steam stream (41); The high-temperature (HT) conversion section (50) is arranged to receive the cooled second process gas flow (31') from the first waste heat boiler (40) and generate the third process gas flow (51); - A second waste heat boiler (70) is arranged to exchange heat between at least a portion of the third process gas stream (51) and a second boiler water stream (113) from the steam drum (110), and to generate a cooled third process gas stream (51') and a second steam stream (71); and / or a steam superheater (75) is arranged to exchange heat between at least a portion of the third process gas stream (51) and a steam stream (115) from the steam drum (110), to generate a cooled third process gas stream (51') and a superheated steam stream (115'); provided that, when the ammonia production plant includes the second waste heat boiler (70) and the steam superheater (75), the third process gas stream (51) is arranged to be fed into the steam superheater (75) and cooled into the third process gas stream (51'), and then the third process gas stream is arranged to be fed into the second waste heat boiler (70) and cooled into a further cooled third process gas stream (51''); - A second conversion section (60) is arranged to receive a cooled third process gas stream (51', 51'') and generate a fourth process gas stream (61); a syngas purification section (100) is arranged to receive the fourth process gas stream (61) and the nitrogen feed (4) and generate a syngas stream (104) comprising hydrogen and nitrogen, a CO2-rich stream (101), process condensate (102) and at least one tail gas stream (151); and an ammonia synthesis loop (200) is arranged to receive the syngas stream (104) and generate a first ammonia-rich stream (201).

2. The ammonia production apparatus according to claim 1, wherein the steam drum (110) is arranged to receive at least a first steam flow (41) from the first waste heat boiler (40) and optionally a second steam flow (71) from the second heat exchanger (70).

3. The ammonia production equipment according to any one of the preceding claims, wherein the second conversion section is a low-temperature (LT) or medium-temperature (MT) conversion section, preferably a low-temperature conversion section.

4. The ammonia production apparatus according to any one of the preceding claims, wherein the steam drum (110) is further arranged to receive at least a first steam flow (41) from the first waste heat boiler (40), a second steam flow (71) from the second heat exchanger (70), and, optionally, a third steam flow (114') from the loop heat exchanger (251), the ammonia production apparatus further comprising a combustion-type steam superheater (120) arranged to receive and superheat the saturated steam flow (111) from the steam drum (110) to provide a superheated steam flow (121).

5. The ammonia production equipment according to any one of the preceding claims, wherein the ammonia production equipment does not include a combustion-type steam superheater (120).

6. The ammonia production equipment according to any one of the preceding claims, comprising a combustion heater (90) and a fuel flow (9) for the combustion heater, wherein at least one of the feed preheater (91), the pre-reformer feed preheater (92) and the syngas preheater (93), and preferably all of them, comprises a heating coil within the combustion heater (90).

7. The ammonia production apparatus according to claim 6, wherein a portion of the synthesis gas stream (104) of hydrogen and nitrogen is arranged as fuel to be supplied to a combustion heater (90) and / or a combustion superheater (120).

8. The ammonia production equipment according to any one of the preceding claims, wherein the syngas purification section (100) includes a separator (130), a CO2 removal unit (140), and a hydrogen purification unit (150).

9. The ammonia production apparatus according to claim 8, wherein a separator (130) is arranged to receive the fourth process gas stream (61) and produce a dry fourth process gas stream (131) and process condensate (102), wherein a CO2 removal unit (140) is arranged to receive the dry fourth process gas stream (131) and produce a CO2-rich stream (101) and a CO2-lean fourth process gas stream (141), and wherein a hydrogen purification unit (150) is arranged to receive the CO2-lean fourth process gas stream (141) and produce a synthesis gas stream (104) comprising hydrogen and nitrogen (suitably in a ratio of 3:1) and a tail gas stream (151).

10. The ammonia production equipment according to claim 8, wherein the syngas purification section (100) comprises, in sequence: Separator (130), hydrogen purification unit (150) and CO2 removal unit (140).

11. The ammonia production apparatus according to any one of claims 8-10, wherein at least a first portion (151A) of the tail gas stream (151) is arranged to be compressed in the compressor (160) and mixed with the first process gas stream (21) upstream of the ATR section (30).

12. The ammonia production apparatus according to claim 11, wherein at least a second portion (151B) of the tail gas stream (151) is arranged as fuel to be supplied to a combustion heater, optionally combined with a portion (104A) of the synthesis gas stream (104).

13. The ammonia production apparatus according to any one of the preceding claims, wherein the ammonia synthesis loop (200) comprises an ammonia reactor (240), a recirculation compressor (220), an ammonia separator (230), and at least one heat exchanger (250, 251) arranged downstream of the ammonia reactor (240), wherein a third boiler water flow (114) is arranged to exchange heat in the at least one heat exchanger (251), the heat exchanger comprising a waste heat boiler and optionally a steam superheater.

14. The ammonia production apparatus according to any one of the preceding claims, wherein a feed preheater (91) is arranged to preheat the hydrocarbon feed (1) by exchanging heat with at least a portion of the second steam stream (71) or the superheated steam stream (121, 115').

15. A method for generating ammonia in an ammonia generating apparatus (A) according to any one of the preceding claims, the method comprising the following steps: - Provides an apparatus according to any one of the preceding claims, - preheating a hydrocarbon feed (1) in a feed preheater (91) to produce a preheated hydrocarbon feed (1'); - hydrogenating the preheated hydrocarbon feed (1') in a feed purification section (80) to remove sulfur-containing compounds therein, producing a purified hydrocarbon feed (1''); - heating a mixed stream (81) comprising the purified hydrocarbon feed (1'') and process steam feed (2) in a pre-reforming feeder (92) to produce a heated mixed stream (81'); - pre-reforming the heated mixed stream (81') from the pre-reforming feeder (92) in a pre-reforming section (20) to produce a first process gas stream (21); - heating the first process gas stream (21) in a syngas preheater (93) to produce a heated first process gas stream (21'); - At least a portion of the heated first process gas stream (21'), the oxygen feed (3), and the burner steam feed (2') are fed into the autothermal reforming ATR section (30) to generate a second process gas stream (31); - Boiler feedwater (8) is supplied to the steam drum (110) to provide a first boiler water stream (112) and a second boiler water stream (113); - At least a portion of the second process gas stream (31) is exchanged with the first boiler water stream (112) from the steam drum (110) in the first waste heat boiler (40) to generate a cooled second process gas stream (31') and a first steam stream (41); - The cooled second process gas stream (31') from the first waste heat boiler (40) is fed into the high-temperature (HT) conversion section (50) to generate a third process gas stream (51); In the second waste heat boiler (70), at least a portion of the third process gas stream (51) is heat-exchanged with a second boiler water stream (113) from the steam drum (110) to produce a cooled third process gas stream (51') and a second steam stream (71); and / or in the steam superheater (75), at least a portion of the third process gas stream (51) is heat-exchanged with a steam stream (115) from the steam drum (110) to produce a cooled third process gas stream (51') and a superheated steam stream (115'); provided that, when the ammonia production plant includes the second waste heat boiler (70) and the steam superheater (75), the third process gas stream (51) is supplied to the steam superheater (75) and cooled to the third process gas stream (51'), and then supplied to the second waste heat boiler (70) and cooled to a further cooled third process gas stream (51''); A cooled third process gas stream (51', 51'') is supplied to a second conversion section (60) to generate a fourth process gas stream (61); - The fourth process gas stream (61) and the nitrogen feed (4) are supplied to a syngas purification section (100) to generate a syngas stream (104) comprising hydrogen and nitrogen (e.g., in a ratio of 3:1), a CO2-rich stream (101), process condensate (102), and at least one tail gas stream (151);- The synthesis gas stream (104) is supplied to the ammonia synthesis circuit (200) to generate the first ammonia-rich stream (201).

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