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WO2025219326A1 - Méthode de production d'ammoniac bleu - Google Patents

Méthode de production d'ammoniac bleu

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Publication number
WO2025219326A1
WO2025219326A1 PCT/EP2025/060229 EP2025060229W WO2025219326A1 WO 2025219326 A1 WO2025219326 A1 WO 2025219326A1 EP 2025060229 W EP2025060229 W EP 2025060229W WO 2025219326 A1 WO2025219326 A1 WO 2025219326A1
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WIPO (PCT)
Prior art keywords
stream
process gas
feed
gas stream
steam
Prior art date
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Pending
Application number
PCT/EP2025/060229
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English (en)
Inventor
Sagar AHUJA
Annette E. Krøll JENSEN
Per Juul DAHL
Ilayaraja KARUPPASAMY
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Topsoe AS
Original Assignee
Haldor Topsoe AS
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Publication of WO2025219326A1 publication Critical patent/WO2025219326A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
    • C—CHEMISTRY; METALLURGY
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • C01B2203/0894—Generation of steam
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/84—Energy production

Definitions

  • the present invention relates to an ammonia plant and process for production of ammonia.
  • a syngas purification section comprises a PSA unit and a cryogenic CO2 removal unit. Heat from the shift section is used to generate electrical power in an alternator.
  • Blue ammonia is a fossil fuel-based product produced with minimum emission of CO2 to the atmosphere. It is seen as a transition product between conventional fossil fuel-based ammonia and green ammonia produced from green or renewable power, water and air.
  • the CO2 resulting from a blue ammonia production shall be stored permanently or converted into other chemicals.
  • the main steps for producing blue ammonia are essentially the same as for producing conventional fossil fuel-based ammonia, the difference being that more of the carbon stemming from the carbon fuel is captured, providing a possibility for further processing.
  • Blue ammonia does not release any carbon dioxide when used as fertilizer or burned .
  • An ammonia plant comprising : a hydrocarbon feed; a burner steam feed; a first process steam feed; a second process steam feed; an oxygen feed; a nitrogen feed; a high pressure boiler feed water; a low pressure boiler feed water; a feed pre-heater being arranged to pre-heat the hydrocarbon feed and to generate a pre-heated hydrocarbon feed a feed purification section, being arranged to hydrogenate and remove sulfur compounds from the preheated hydrocarbon feed, and to generate a purified hydrocarbon feed; a prereformer feed preheater arranged to heat a combined stream comprising purified hydrocarbon feed and process steam feed and to generate a heated combined stream; a prereforming section arranged to pre-reform the heated combined stream from the prereformer feed preheater and to generate a first process gas stream; a process gas pre-heater arranged to heat said first process gas stream and to generate a heated first process gas stream; an autothermal reforming ATR section arranged to receive at least
  • a process for generating ammonia in the ammonia plant described herein is also provided.
  • the new optimized layout is a layout utilizing low temperature calories downstream the low temperature (LT) shift converter and downstream a high pressure (HP) boiler feed water (BFW) preheater for low pressure (LP) steam generation and demineralized water (DMW) preheating.
  • the generated LP steam is superheated in the process in a steam superheater heat exchanger and is subsequently used as injection steam in a turbine alternator for additional power generation.
  • Fig. 1 shows a layout of an ammonia plant according to the invention.
  • An ammonia plant (A) is provided.
  • the feeds inputted to the plant comprise: a hydrocarbon feed (typically natural gas or biogas) a burner steam feed; a first process steam feed; a second process steam feed; an oxygen feed; a nitrogen feed; a high pressure boiler feed water; and a low pressure boiler feed water.
  • a hydrocarbon feed typically natural gas or biogas
  • a feed pre-heater is arranged to pre-heat the hydrocarbon feed and to generate a pre-heated hydrocarbon feed.
  • Typical temperatures of the preheated hydrocarbon feed are between 350 and 400°C.
  • Preheating of the hydrocarbon feed may take place in a heater coil within a fired heater.
  • the feed pre-heater may be an electrical heater or a steam preheater.
  • a feed purification section is arranged to hydrogenate and remove sulfur compounds from the preheated hydrocarbon feed, and to generate a purified hydrocarbon feed.
  • the feed purification section suitably comprises a hydrogenation unit upstream a sulfur removal unit. Hydrogenation removes any unsaturated components of the hydrocarbon feed. Both unsaturated components of the hydrocarbon feed and sulfur components may contaminate downstream catalysts in the ammonia plant.
  • the purified hydrocarbon feed is combined with process steam feed and then heated again in a prereformer feed preheater to generate a heated combined stream.
  • Typical temperatures of the heated combined stream are between 400 and 550°C.
  • the prereformer feed preheater may comprise a heater coil within a fired heater. Alternatively, the prereformer feed preheater may be an electrical heater.
  • the heated combined stream is fed to prereforming section, which is arranged to pre-reform the heated combined stream and to generate a first process gas stream.
  • Pre-reforming is the process by which methane and heavier hydrocarbons are steam reformed and the products of the heavier hydrocarbon reforming are methanated. Typically, a nickel-containing catalyst is used. Pre-reforming sections suitable for this process are known to the person skilled in the art.
  • First process gas stream is then fed to a process gas pre-heater which is arranged to heat this first process gas stream and to generate a heated first process gas stream.
  • Typical temperatures of the heated first process gas stream are between 350 and 650 °C.
  • the plant comprises an autothermal reforming ATR section arranged to receive at least a portion of the heated first process gas stream, optionally an offgas recycle stream from downstream recycled back to the ATR, the oxygen feed and the burner steam feed and to generate a second process gas stream.
  • Autothermal reforming sections, catalysts and conditions are known to the person skilled in the art.
  • the ammonia plant comprises a steam drum.
  • the steam drum is arranged to receive high pressure boiler feed water and supply a first boiler water stream.
  • a first waste heat boiler is arranged to heat exchange at least a portion of the second process gas stream with the first boiler water stream from the steam drum and generate a cooled second process gas stream and a first steam stream.
  • a high temperature (HT) shift section is arranged to receive the cooled second process gas stream from the first waste heat boiler, as well as the second process steam feed, and generate a third process gas stream.
  • Shift means Water-gas shift reaction (WGSR) or Shift reaction, the reaction of carbon monoxide and water vapor to form carbon dioxide and hydrogen:
  • the WGSR is an important industrial reaction that is used in the manufacture of ammonia, hydrocarbons, methanol, and hydrogen. It is also often used in conjunction with steam reforming of methane and other hydrocarbons. In the Fischer-Tropsch process, the WGSR is one of the most important reactions used to balance the H2/CO ratio.
  • the water gas shift reaction is a moderately exothermic reversible reaction. Therefore, with increasing temperature the reaction rate increases but the carbon dioxide production becomes less favourable. Due to its exothermic nature, high carbon monoxide percentage is thermodynamically favoured at low temperatures. Despite the thermodynamic favourability at low temperatures, the reaction is faster at high temperatures.
  • a second shift section is arranged to receive the third process gas stream and generate a fourth process gas stream.
  • the second shift section may be a low temperature (LT) or a medium temperature (MT) shift section, and is preferably a low temperature shift section.
  • LT shift typically takes place at temperatures between process gas Tdew+ 15°C and 250°C
  • MT shift typically takes place between 190 - 330°C.
  • CO is shifted to a minimum to maximize H2 production and to increase process carbon capture.
  • a low pressure waste heat boiler is arranged to receive the low pressure boiler feed water, and heat exchange at least a portion of the low pressure boiler feed water with the fourth process gas stream from said second shift section; and to generate a low pressure steam stream and a cooled fourth process gas stream.
  • a low pressure steam superheater is arranged to heat exchange at least a first portion of the low pressure steam stream from the low pressure waste heat boiler with the third process gas stream from the high temperature (HT) shift section, so as to generate a low pressure superheated steam stream and a cooled third process gas stream.
  • HT high temperature
  • a syngas purification section comprises, in order: a separator section, a pressure swing absorption unit and a cryogenic CO2 removal unit.
  • the separator section is arranged to receive said cooled fourth process gas stream and generate a dried fourth process gas stream and a process condensate stream.
  • the PSA unit is arranged to receive the dried fourth process gas stream and to generate a hydrogen product stream and a tail gas stream.
  • the cryogenic CO2 removal unit is arranged to receive said tail gas stream from the PSA unit and to generate a CCh-rich stream, a carbon-containing ATR. recycle stream and an offgas fuel stream and optionally an additional hydrogen product stream.
  • the syngas purification section is arranged to mix at least a first portion of the hydrogen product stream from the PSA unit with the nitrogen feed and generate a syngas stream.
  • the ammonia synthesis loop is arranged to receive at least a first portion of the hydrogen product stream from the PSA unit, and said nitrogen feed (preferably in admixture, in the form of a syngas stream), and a portion of the boiler feed water, and to generate a first ammonia- rich stream and a second steam stream.
  • the ammonia synthesis loop comprises an ammonia reactor, a compressor section (both a makeup and a recycle syngas compressor), an ammonia separator, at least one waste heat boiler, and optionally a steam superheater.
  • the waste heat boiler and optional steam superheater are arranged downstream the ammonia reactor, wherein said portion of the boiler feed water is arranged to be heat exchanged in said at least one waste heat boiler with the effluent from the ammonia reactor, and optionally said steam superheater, so as to generate said second steam stream.
  • the ammonia plant does not comprise a fired steam superheater.
  • the ammonia plant comprises a fired heater and a fuel stream for said fired heater. At least one - and preferably all - of said feed pre-heater, prereformer feed preheater and syngas pre-heater comprise a heater coil within said fired heater.
  • Various streams in the plant can be used as (part of) the fuel for the fired heater.
  • offgas from the purification unit and hydrogen rich fuel stream(s) and optionally, a portion of the syngas stream comprising hydrogen and nitrogen are arranged to be fed as fuel(s) to the fired heater.
  • a second portion of the hydrogen product stream from the PSA unit is arranged to be fed as fuel to the fired heater.
  • at least a portion of the offgas fuel stream from the cryogenic CO2 removal unit may be arranged to be fed as fuel to the fired heater, optionally in combination with a portion of the syngas stream.
  • the ammonia synthesis loop suitably comprises an ammonia reactor, a compressor section, an ammonia separator, at least one waste heat boiler and optionally a steam superheater, said at least one waste heat boiler and optional steam superheater being arranged downstream the ammonia reactor, wherein said portion of the boiler feed water is arranged to be heat exchanged in said at least one waste heat boiler with the effluent from the ammonia reactor, and optionally said steam superheater, so as to generate said second steam stream.
  • a high pressure steam stream is also arranged to be provided to the alternator.
  • the autothermal reforming ATR section may also be arranged to receive at least a portion of the carbon-containing ATR recycle stream at the inlet of said ATR section, suitably in admixture with the heated first process gas stream.
  • the ammonia plant may further comprise a demineralised water (DMW) preheater and a process gas cooler arranged to further cool the cooled fourth process gas stream upstream the separator section.
  • DMW demineralised water
  • the cryogenic CO2 removal unit comprises a cryogenic CO2 fractionation system, followed by at least one overhead (OHVD) PSA unit, and optionally a membrane separation unit arranged downstream the overhead (OHVD) PSA unit.
  • a process for generating ammonia in the ammonia plant (A) described herein, said process comprising the steps of: providing the plant as defined herein, pre-heating the hydrocarbon feed in the feed pre-heater and generating a pre-heated hydrocarbon feed; hydrogenating and removing sulfur compounds from the preheated hydrocarbon feed in the feed purification section, and generating a purified hydrocarbon feed; heating a combined stream comprising purified hydrocarbon feed and process steam feed in the prereformer feed preheater and generating a heated combined stream; pre-reforming the heated combined stream from the prereformer feed preheater in the prereforming section and generating a first process gas stream; heating the first process gas stream in the process gas pre-heater and generating a heated first process gas stream feeding at least a portion of the heated first process gas stream, said oxygen feed and said burner steam feed to the autothermal reforming ATR section and generating a second process gas stream; feeding at least a portion of the high pressure boiler feed water to the
  • recycle stream and an offgas fuel stream feeding a first portion of the hydrogen product stream from the PSA unit, said nitrogen feed, and a portion of the boiler feed water, to the ammonia synthesis loop and generating a first ammonia-rich stream and a second steam stream.
  • the syngas stream generated from the first portion of the hydrogen product stream and said nitrogen feed typically comprises hydrogen and nitrogen in a ratio of ca. 3: 1.
  • FIG. 1 shows a layout of an ammonia plant according to the invention, with the following features: hydrocarbon feed (1) burner steam feed (2') a first process steam feed (2) a second process steam feed (7) oxygen feed (3) nitrogen feed (4) high pressure boiler feed water (8, 8A, 8B) low pressure boiler feed water (5) saturated high pressure steam stream(s) (111, 111A, 111B) feed pre-heater (91) pre-heated hydrocarbon feed (1') feed purification section (80) purified hydrocarbon feed (1") prereformer feed preheater (92) combined stream (81) comprising purified hydrocarbon feed (1") and process steam feed (2) heated combined stream (81') hydrogenation unit (82) sulfur removal unit (83) prereforming section (20) first process gas stream (21) process gas pre-heater (93) heated first process gas stream (21') autothermal reforming ATR.
  • hydrocarbon feed (1) burner steam feed (2') a first process steam feed (2) a second process steam feed (7) oxygen feed (3) nitrogen feed (4) high pressure boiler feed water (8, 8A,
  • second process gas stream (31) steam drum (110) first boiler water stream (112) first waste heat boiler (40) steam superheater (75) cooled second process gas stream (31') first steam stream (41) high temperature (HT) shift section (50) third process gas stream (51)
  • CC -rich stream (151) process condensate (102) carbon-containing ATR. recycle stream (152) offgas fuel stream (153), a separator section (130) pressure swing absorption (PSA) unit (140) cryogenic CO2 removal unit (150) dried fourth process gas stream (131) hydrogen rich fuel stream (103) hydrogen product stream (104) tail gas stream (141) low pressure steam stream (311, 311A, 311B) ammonia synthesis loop (200) first ammonia-rich stream (201) fired steam superheater (120) superheated steam stream (s) (121A, 121B) ammonia reactor (240), compressor section (220) ammonia separator (230) waste heat boiler (251) effluent (241) from the ammonia reactor (240),
  • Example 1 LP steam flow of 75691 kg/h is generated in LP steam waste heat boiler (310) with the conditions 4 bar g and 152°C, the LP steam is following superheated in LP steam superheater 70 located between the HT and LT shift converters. With higher LP steam conditions (compared to example 2) more calories are wasted in the process gas cooler (air cooler located upstream of unit 100) ⁇ 77.55 Gcal/h. Stream 61' is sent to unit 100 (130+ 140+150). In the table below stream conditions for streams 51, 61 and 61' are given. Table for example 1 :
  • Example 2 LP steam flow of 107857 kg/h is generated in LP steam waste heat boiler (310) with the conditions 1.9 bar g and 132°C and part of the saturated LP steam is used in various preheaters. The rest of the LP steam is following superheated in LP steam superheater 70 with MP steam from the header. With lower LP steam conditions (compared to example 1) less calories are wasted in the process gas cooler (air cooler located upstream of unit 100) ⁇ 13.63 Gcal/h. Stream 61' is sent to unit 100 (130+ 140+ 150). In the table below stream conditions for streams 61 and 61' are given. Table for example 2 :

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne une usine d'ammoniac et un procédé de production d'ammoniac. Une section de purification de gaz de synthèse comprend une unité d'adsorption à pression modulée (APM) et une unité d'élimination de CO₂ cryogénique. La chaleur provenant d'une section de décalage est utilisée pour générer de l'énergie électrique dans un alternateur.
PCT/EP2025/060229 2024-04-17 2025-04-14 Méthode de production d'ammoniac bleu Pending WO2025219326A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
IN202411030810 2024-04-17
IN202411030810 2024-04-17
EP24193562.6 2024-08-08
EP24193562 2024-08-08

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018149641A1 (fr) 2017-02-15 2018-08-23 Casale Sa Procédé de synthèse d'ammoniac avec de faibles émissions de co2 dans l'atmosphère
WO2023049570A1 (fr) * 2021-09-24 2023-03-30 Exxonmobil Chemical Patents Inc. Production de gaz combustible riche en hydrogène avec réduction des émissions de co2
WO2023084084A1 (fr) * 2021-11-15 2023-05-19 Topsoe A/S Procédé et usine de production d'hydrogène bleu
US20230174377A1 (en) * 2020-06-30 2023-06-08 Johnson Matthey Public Limited Company Process for the production of hydrogen
WO2024056870A1 (fr) * 2022-09-16 2024-03-21 Topsoe A/S Reformage atr

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018149641A1 (fr) 2017-02-15 2018-08-23 Casale Sa Procédé de synthèse d'ammoniac avec de faibles émissions de co2 dans l'atmosphère
US20230174377A1 (en) * 2020-06-30 2023-06-08 Johnson Matthey Public Limited Company Process for the production of hydrogen
WO2023049570A1 (fr) * 2021-09-24 2023-03-30 Exxonmobil Chemical Patents Inc. Production de gaz combustible riche en hydrogène avec réduction des émissions de co2
WO2023084084A1 (fr) * 2021-11-15 2023-05-19 Topsoe A/S Procédé et usine de production d'hydrogène bleu
WO2024056870A1 (fr) * 2022-09-16 2024-03-21 Topsoe A/S Reformage atr

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