WO2024008270A1 - Procédé de craquage d'ammoniac et agencement de craquage pour le craquage de l'ammoniac - Google Patents

Procédé de craquage d'ammoniac et agencement de craquage pour le craquage de l'ammoniac Download PDF

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Publication number
WO2024008270A1
WO2024008270A1 PCT/EP2022/068439 EP2022068439W WO2024008270A1 WO 2024008270 A1 WO2024008270 A1 WO 2024008270A1 EP 2022068439 W EP2022068439 W EP 2022068439W WO 2024008270 A1 WO2024008270 A1 WO 2024008270A1
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WIPO (PCT)
Prior art keywords
cracking
ammonia
vessel
burner
space
Prior art date
Application number
PCT/EP2022/068439
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English (en)
Inventor
Aage Ingebrigt JØSANG
Odd Ivar LINDLØV
Lars Grønnæss
Original Assignee
Wärtsilä Gas Solutions Norway AS
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Priority to PCT/EP2022/068439 priority Critical patent/WO2024008270A1/fr
Publication of WO2024008270A1 publication Critical patent/WO2024008270A1/fr

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Classifications

    • 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
    • C01B3/04—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of inorganic compounds, e.g. ammonia
    • C01B3/047—Decomposition of ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00157—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical

Definitions

  • the present invention relates to a method of cracking ammonia and a cracking arrangement of cracking ammonia.
  • ammonia is considered to be a promising candidate for carbon free fuel and/or a hydrogen carrier.
  • Excess energy in one location can be used to produce NH 3 , that can be transported to locations where energy is needed.
  • the energy in the NH 3 can be utilised by direct combustion or cracked into H 2 .
  • At high temperature, and in the presence of a suitable catalyst, ammonia is cracked into its constituent elements. Cracking of ammonia is a slightly endothermic process requiring 23 kJ/mol (5.5 kcal/mol) of ammonia and yields hydrogen and nitrogen gas.
  • NH 3 as hydrogen carrier and the hydrogen contained in the NH 3 it is referred to US 6936363.
  • the document discloses a process for producing a hydrogen and nitrogen mixture from gaseous ammonia and utilizing the mixture in an alkaline fuel cell.
  • Ammonia is fed into an ammonia cracker.
  • Off gas from the fuel cell is fed to a heating unit of the ammonia cracker.
  • the heating unit is either a lean gas combustor or a catalytic burner.
  • An object of the invention is to provide method of and cracking arrangement for cracking ammonia in which the improvement is its simple construction and effective operation.
  • a method of cracking ammonia comprises feeding a first portion of ammonia into a burner arranged to a cracking vessel; feeding gas containing oxygen into the burner; combusting the first portion of ammonia forming a combustion zone in the cracking vessel producing heat; feeding a second portion of ammonia into a cracking zone of the cracking vessel outside the combustion zone, and cracking the second portion of ammonia by utilizing the heat produced by the combustion of the first portion of ammonia and producing product gas comprising hydrogen and nitrogen from the second portion of ammonia.
  • the first portion of the ammonia is consuming the fed oxygen forming a non-oxidizing zone outside the combustion zone in the cracking vessel.
  • second portion of ammonia is cracked in a presence of an ammonia cracking catalyst.
  • the first portion of the ammonia is consuming the fed oxygen forming annon-oxidizing zone outside the combustion zone in the cracking vessel and the second portion of ammonia is cracked in a presence of an ammonia cracking catalyst.
  • second portion of ammonia is cracked using non-catalytic reactions.
  • the combustion zone the first portion of the ammonia is consuming the fed oxygen forming and non-oxidizing zone is formed outside the combustion zone in the cracking vessel and that second portion of ammonia is cracked using non-catalytic reactions.
  • the first portion of ammonia and the gas containing oxygen are fed as a gas mixture into the burner.
  • ammonia is preheated by transferring heat from the product gas to the gas mixture before feeding to the burner.
  • ammonia is evaporated by transferring heat from the product gas to the gas mixture before feeding to the burner.
  • the vessel has a cylindrical inner reaction space, having a diameter and a length, the length being greater than the diameter, wherein the first portion of ammonia and the gas containing oxygen are fed to a first end of the reaction space of the vessel in its longitudinal direction and the product gas is removed from a second end of reaction space of the cracking vessel.
  • the second portion of the ammonia is heated to a predetermined temperature by the heat provided by combustion of the first portion of the ammonia, and the heated second portion of the ammonia is fed in non-oxidizing conditions to the cracking catalyst.
  • the combustion zone is formed to a centre axis of the cracking vessel and at least part of the second portion of the ammonia is fed around the combustion zone from the first end of the space in the vessel.
  • At least part of the second portion of the ammonia is fed into the vessel near its side wall between a first end and a second end of space in the vessel.
  • gas containing oxygen is a mixture of NH3 and gas containing oxygen.
  • gas containing oxygen is air.
  • gas containing oxygen is pure 02.
  • the ammonia cracking catalyst is for example Nickel based catalyst, Ruthenium based catalyst, Lithium amide or Sodium amide-based catalyst.
  • the combustion zone temperature is maintained at about 800 - 1800°C.
  • temperature in the cracking zone is maintained at 350 - 800°C by combusting the first portion of ammonia in a combustion zone of the vessel.
  • amount of oxygen present in the combustion zone is controlled such that all of the oxygen is reacted with the ammonia.
  • gas containing oxygen is a mixture of NH 3 and air and air-fuel ratio in the combustion zone is rich.
  • product gas is fed from the reaction space to an oxidizer part where the product gas is oxidized by feeding oxygen containing gas into a stream of the product gas.
  • a cracking arrangement for cracking ammonia comprises a cracking vessel and a burner arranged to the cracking vessel, the burner comprising a first inlet for feeding ammonia into the burner, and a second inlet for feeding gas containing oxygen into the burner, and an outlet for product gas in the cracking vessel, characterized in that the cracking vessel is a cylindrical vessel where the burner is arranged at the first end of the vessel arranged to a centre axis of the vessel, and the outlet is arranged to the second end of the space of the vessel, the cracking vessel further comprising a third inlet for feeding ammonia into cracking vessel arranged near to a side wall and/or near to the first end of the space in the vessel.
  • the cracking vessel comprises an open space inside, that space comprising a combustion zone adjacent to the burner at the first end of the vessel and a cracking zone at the second end of the space in the vessel and around the burner.
  • the vessel is provided with an ammonia cracking catalytic converter in the cracking zone at the second end of the space in the vessel.
  • catalytic converter comprises at least one of a catalyst bed of loose material, a catalyst support coated with catalyst material or catalyst coat on inner surface of the vessel.
  • the third inlet comprises several inlets into the inner reaction space of the vessel arranged to an end wall at the first end of the space in the vessel around the burner.
  • the third inlet comprises several inlets arranged near a side wall of the vessel at a distance from the end wall at the first end of the space in the vessel.
  • the vessel comprises an oxidizer part, arranged downstream of the cracking zone, and the oxidizer part is provided with at least one inlet for oxygen containing gas.
  • the invention provides several advantageous effects. Since the basic concept is to mix both NH 3 to be cracked and combustion gases in a single vessel heat is directly mixed into the NH 3 to be cracked. The NH 3 to be cracked is heated by an internal combustion inside the vessel. Effective heat transfer between combustion gases and NH 3 is accomplished because heat is transferred by mixing, convective heat transfer and radiation.
  • Figure 1 illustrates a cracking arrangement according to an embodiment of the invention
  • Figure 2 illustrates a cracking arrangement according to another embodiment of the invention
  • FIG. 3 illustrates a cracking arrangement according to still another embodiment of the invention
  • Figure 4 illustrates a cracking arrangement according to still another embodiment of the invention.
  • Figure 5 illustrates a cracking arrangement according to still another embodiment of the invention.
  • Figure 1 depicts schematically a cracking arrangement 10 for cracking ammonia according to an embodiment of the invention.
  • the arrangement comprises a cracking vessel 12.
  • the cracking vessel 12 is advantageously rotation- ally symmetrical, such as cylindrical, vessel having a longitudinal centre axis 16.
  • the burner 14 arranged at the first end 12.1 of the rection space 100 of the vessel 12 for combustion of fuel.
  • the cracking vessel 12 is provided with an outlet 18 for product gas in the second end 12.2 of the reaction space 100 of the vessel 12, opposite to the burner 14.
  • the outlet 18 is not necessarily arranged to the centre axis 16 even if that is shown in the figure.
  • the burner 14 is, however, arranged to the centre axis 16 of the vessel such that its flame is directed coaxially to the centre axis 16 inside the vessel 12.
  • the burner 14 comprises a first inlet 20 which is connected to a source of ammonia 22 for feeding ammonia as fuel into the burner 14, and a second inlet 24, which is connected to a source of gas containing oxygen 26 for feeding gas containing oxygen into the burner 14.
  • the first inlet 20 and the second inlet 24 function as introduction of gases needed for production of heat for cracking ammonia in the vessel 12.
  • the cracking vessel 12 further comprising a number of third inlets 28 for feeding ammonia into cracking vessel 12 arranged to a side wall 30 and/or to an end wall 32 at the first end 12.1 of the space 100 in the vessel.
  • the third inlets 28 function as introduction of ammonia into the cracking vessel 12 for cracking the ammonia by means of the heat produced by combustion of gases with the burner 14.
  • the reaction space 100 inside the cracking vessel 12 is an open space 100, in which a combustion zone 101 adjacent to the burner 14 is formed when the burner 14 is in operation and a cracking zone 102 in the portion of the space 100 at the second end 12.2 of the space 100 of the vessel 12.
  • the combustion zone 101 can be considered to be a flame area where oxidation of fuel takes place in a presence of oxygen.
  • the diameter of the space of the vessel at its first end 12.1 is greater than effective diameter of the flame, that is the combustion zone 101 , and therefore an annular portion around the combustion zone 101 is part of the cracking zone 102. Since the vessel is intended to operate at considerably high temperatures, its walls are preferably provided with a heat insulation and/or with a cooling system, like a fluid jacket.
  • the vessel 12 comprises several third inlets 28 arranged to an end wall 32 at the first end of the space 100 of the vessel evenly around the burner 14. These inlets 28 at the end wall 32 are arranged to feed ammonia into the annular cracking zone 102 around the burner.
  • the third inlets 28 are positioned such that ammonia which is introduced via the third inlets 28 is heated by the combustion in the burner in the space 100.
  • the cracking zone 102 outside the combustion zone 101 is practically non-oxidizing zone.
  • the space 100 is empty.
  • the cracking reaction is non-catalytic thermal cracking, therefore the cracking zone 102 in the embodiment of figure 1 can be called non- catalytic cracking zone 102.
  • an inner wall bordering the space 100 may be provided with a catalyst coat on its surface wherein the catalyst will promote cracking reactions in the vessel 12.
  • Method of cracking ammonia is practised in the cracking vessel according to figure 1 in a following manner.
  • Ammonia is fed from the source of ammonia 22 into the burner 14 and additionally gas containing oxygen is fed also to the burner 14.
  • the first portion of ammonia is combusted in the burner 14 wherein heat is produced into the vessel 12 and the combustion zone 101 is formed in the cracking vessel 12.
  • the first portion of ammonia is fed via the first inlet 20 and the gas containing oxygen is fed via the second inlet 24 into the burner 14.
  • the gas containing oxygen fed through the first inlet 20 may be air or other gas containing oxygen, or even pure O 2 .
  • combustion of ammonia is exothermic reaction producing heat and consuming oxygen in the vessel. Therefore, combustion of the first portion ammonia forms outside the combustion zone in the vessel is substantially oxygen free, that is the non-oxidizing zone 102.
  • Second portion of ammonia is fed via the third inlets 28 into the cracking zone 102 of the cracking vessel 12 outside the combustion zone 101 , wherein the second portion of ammonia is cracked thermally by utilizing the heat produced by the combustion of the first portion of ammonia.
  • the second portion of ammonia may originate from different source of ammonia than the first portion of ammonia. This is technically applicable also the embodiments shown in the figure 1 to 4.
  • the produced product gas produced from the second portion of ammonia comprises hydrogen and nitrogen.
  • the space in vessel is empty and cracking is non-catalytic reaction.
  • the second portion of the ammonia is heated to a predetermined temperature at which the cracking of ammonia takes place without any catalyst.
  • the heat is provided by combustion of the first portion of the ammonia, and the heated second portion of the ammonia is cracked in non-oxidizing conditions in the empty cracking zone 102. Effective heat transfer between combustion gases and ammonia in the cracking zone is provided because heat is transferred by mixing, convective heat transfer, and radiation.
  • the gas containing oxygen is air and the air-fuel ratio in the combustion zone is rich. This way it is ensured that all oxygen present in the combustion zone 101 is consumed. This also means that a part of the first portion of the ammonia fed into the burner may remain as ammonia. Even if the burner may generate ammonia slip the remaining ammonia will be cracked into hydrogen and nitrogen in the cracking zone 102.
  • Figure 2 discloses a cracking arrangement 10 for cracking ammonia according to another embodiment of the invention. Practically this is otherwise similar to that shown in the figure 1 except that the first and the second inlets are combined as one common gas inlet 24’ so that the gas containing oxygen that is fed to the burner 14 is a mixture of NH 3 and gas containing oxygen.
  • the source of gas containing oxygen 26 and the source of ammonia 22 are both connected with the common gas inlet 24’. This makes possible to control the operation of the burner more easily and preheat both of the gases as a mixture in more straight forward manner.
  • Figure 3 discloses a cracking arrangement 10 for cracking ammonia according to another embodiment of the invention. Practically this is otherwise similar to that shown in the figure 1 except that the first and the second inlets are combined as one common gas inlet 24’, as is shown in the figure 2 and that the cracking zone 102 comprises an ammonia catalytic converter 103 in the zone.
  • the common second outlet 24’ results in that the gas containing oxygen that is fed to the burner 14 is a mixture of NH 3 and gas containing oxygen.
  • the source of gas containing oxygen 26 and the source of ammonia 22 are both connected with the common gas inlet 24’. This makes possible to control the operation of the burner more easily and preheat both of the gases as a mixture in more straight forward manner.
  • the catalytic converter 103 is arranged at the second end of the space in the vessel, at outlet side of the vessel 12 from the third inlets 28 arranged to a side wall 30 of the vessel 12. This way the second portion of ammonia is cracked in a presence of an ammonia cracking catalyst.
  • the catalytic converter 103 is shown as a support grid with catalyst material arranged on its surface.
  • the catalytic converter may be arranged also in different manner, for example to comprise alternatively a bed of loose material with catalyst on its surface as is shown in the figure 4.
  • suitable catalyst materials are: Nickel based, Ruthenium based, Lithium amide or Sodium amide catalyst.
  • Each of the catalyst are effective at temperature 350 - 800°C. However, conversion efficiency and expected lifetime are different.
  • the second portion of the ammonia is heated to a predetermined temperature at which the cracking of ammonia takes place without any catalyst.
  • the heat is provided by combustion of the first portion of the ammonia, and the heated second portion of the ammonia is fed in non-oxidizing conditions to the cracking catalyst.
  • FIG. 4 depicts schematically a cracking arrangement 10 for cracking ammonia according to still another embodiment of the invention.
  • the arrangement comprises a cracking vessel 12 which is advantageously rotationally symmetrical vessel, such as cylindrical, having a longitudinal centre axis 16.
  • the vessel 12 is at upright position such that the centre axis 12 is arranged substantially in vertical position. This way the flame and heat distribution in the vessel are formed advantageously symmetrical in respect to the centre axis 16.
  • the burner 14 is arranged at the lower end 12.1 of the vessel 12 for combustion of fuel.
  • the cracking vessel 12 is provided with an outlet 18 for product gas in the upper end 12.2 of the vessel 12, opposite to the burner 14.
  • the burner 14 is arranged to the centre axis 16 of the vessel such that its flame is directed upwards coaxially to the centre axis 16 inside the vessel 12.
  • the burner 14 comprises a combined second inlet 24’, which is connected to a surrounding air 26, a source of ammonia 22 and a source of pressurized oxygen 26’, for feeding a mixture of oxygen enriched air and ammonia into the burner 14.
  • the source of oxygen is not a necessary feature of the invention and when it is not present the gas mixture fed into the burner substantially consist of air and ammonia.
  • the combined second inlet 24’ functions as introduction of gases needed for production of heat for cracking ammonia in the vessel 12.
  • the cracking vessel 12 further comprising a number of third inlets 28 for feeding ammonia into cracking vessel 12 arranged to or near to a side wall 30 and/or to an end wall 32 at the first end 12.1 of the space 100 in the vessel.
  • the third inlets 28 function as introduction of ammonia into the cracking vessel 12 for cracking the ammonia by means of the heat produced by combustion of gases with the burner 14.
  • the cracking vessel 12 comprises an open space 100 inside, in which a combustion zone 101 adjacent to the burner 14 is formed when the burner 14 is in operation and a cracking zone 102 in the portion of the space 100 at the second end 12.2 of the space in the vessel 12.
  • the diameter of the space 100 in the vessel at its first end 12.1 is greater than effective diameter of the flame, that is the combustion zone 101 and therefore an annular portion of around the combustion zone 101 is part of the cracking zone 102.
  • the vessel 12 comprises third inlets 28 arranged to an end wall 32 at the first end of the space 100 of the vessel evenly around the burner 14. Like in other embodiments of the invention, these inlets 28 at the end wall 32 are arranged to feed ammonia into the annular cracking zone 102 formed around the burner.
  • third inlets 28 arranged to a side wall 30 of the vessel at a distance from the end wall 32 at the first end 12.1 of the space 100 in the vessel 12. The third inlets 28 are positioned such that ammonia which is introduced via the third inlets 28 is heated by the combustion in the burner and is in non-oxidizing zone in the space 100.
  • the third inlets at side wall are connected to feed channels 27 which are arranged in direct heat transfer communication with the annular cracking zone 102, which preheats the ammonia due to heat transfer from the gas and/or flame in the space 100.
  • the feed channels 27 running inside the vessel are an optional feature.
  • the feed channels 27 may run also outside the vessel 12, as is depicted in figures 1-3, If the preheating is not required in terms of process design.
  • the feed channels may be practically realized for example by providing an annular slot channel inside the vessel 12 between the wall of the vessel and a sleeve or a shield 29 inside the vessel 12 as is illustrated by dashed line.
  • the cracking zone 102 outside the combustion zone 101 is practically non-oxidizing zone.
  • the space 100 is empty at the combustion zone 101 and at the upper part of the vessel 12, while in the embodiment shown in the figure 3 is provided with a catalytic converter 103 in the upper part of the space 100.
  • the upper part of the space 100 is provided with a catalytic converter 103.
  • both options - using a catalyst of refrain from using a catalyst - may be used depending on the required design, but using catalyst is preferred because that way cracking of ammonia is practised at lower temperature, which result in decreased heat losses and consumption of ammonia as fuel, which reduces yield of H 2 from the available ammonia.
  • Cracking reaction in the embodiment shown in the figure 4 is catalytic thermal cracking, therefore the cracking zone 102 in the embodiment of figure 1 can be called catalytic cracking zone 102.
  • feed line 25 provided in the arrangement 10, which feed line 25 is connected to the burner 14, more precisely to the combined second inlet 24’ at the second end of the feed line 25.
  • the source of ammonia is in this example configured to store the ammonia in liquid phase.
  • the feed line 25 is provided with a pump 23 for raising the pressure of the ammonia to suitable pressure.
  • the cracking arrangement according to figure 4 comprises further a heat recovery device 36, such as a heat exchanger, which is connected to the feed line 25 and to an outlet line 38, evaporating the ammonia with heat contained in the product gas.
  • the vessel outlet 18 is connected by the outlet line 38 to the heat recovery device 36 such that product gas is arranged to cool in the heat recovery device 36 and the ammonia is arranged to evaporate in the heat recovery device 36.
  • the heat recovery device 36 functions as an after cooler of the process gas and evaporator of the ammonia. This way, the ammonia is evaporated and preheated by transferring heat from the product gas to the gas mixture before feeding to the burner.
  • branch feed line 21 which is connected to the feed line 25 at downstream position to the heat recovery device 36, such that evaporated ammonia is arranged to flow through the branch feed line 21 to the third inlets 28 of the vessel 12.
  • downstream refers to the flow direction from the source of ammonia 22 to the vessel 12.
  • the arrangement further comprises an air feed line 40 which is configured to feed air in the ammonia into the gas mixture feed line 25.
  • the air feed line is provided with a compressor 42 for suitable pressurizing of the air, alternatively the air feed line 40 may be connected to a source of pressurized air.
  • the air feed line is connected to the gas mixture feed line 25 at location downstream to the heat recovery device 36 and also downstream to the branch feed line 21 delivering ammonia to the third inlets 28 of the vessel 12.
  • the air feed line 40 is connected with a source of oxygen 26’, from which pure oxygen can be fed into the air so that the gas containing oxygen fed into the burner 14 is a mixture of ammonia, air and pure oxygen.
  • Method of cracking ammonia is practised in the cracking vessel according to figure 4 in a following manner.
  • Ammonia is fed from the source of ammonia 22 into the gas mixture feed line 25 by suction of the pump 23.
  • the pump 23 raises the pressure of the ammonia to a desired level and feeds the ammonia (in liquid phase) to the heat recovery device 36.
  • Ammonia is evaporated in the heat recovery device 36 by transferring heat from the product gas. A portion of the evaporated ammonia is passed via the branch feed line 21 to the third inlets 28 of the vessel 12.
  • Air optionally enriched by oxygen
  • Mixture of ammonia and air is fed to the burner 14 via the gas mixture feed line 25. This way the first portion of ammonia is combusted in the burner 14 wherein heat is produced into the vessel 12 and the combustion zone 101 is formed in the cracking vessel 12.
  • Figure 5 discloses a cracking arrangement 10 for cracking ammonia according to another embodiment of the invention.
  • the invention relates to a practical application where the product gas is not intended to be produced for use but merely it is gas transformed into environmentally less harmful composition.
  • Practically the cracking arrangement 10 differs from that shown in the figure 1 as follows.
  • the first and the second inlets are combined as one common gas inlet 24’ so that the gas containing oxygen that is fed to the burner 14 is a mixture of NH 3 and gas containing oxygen.
  • the source of gas containing oxygen 26 and the source of ammonia 22 are both connected with the common gas inlet 24’ of the burner 14.
  • the cracking vessel 12 is provided with an oxidizer part 104 after the cracking zone 120 in the flow direction of the gas when in use. Furthermore, the vessel 12 has at least part of its walls cooled. It is also distinctive to the embodiment of the figure 5 that the gas mixture feed line 25 is connected to the first source of ammonia 22, which corresponds to the source of ammonia in the embodiments of the figure 1 to 4 such that the first portion of ammonia is fed to the burner 14.
  • the second portion of ammonia originates from a second source of ammonia 22’ which may be different from that from which the first portion of ammonia fed to the burner 14.
  • the combustion gas used in the burner 14 may have different composition compared to the ammonia containing gas cracked in cracking zone 102 of the vessel.
  • the second source of ammonia 22’ may be ammonia fuel line in connection with a gas consumer, such as an internal combustion engine, during inerting procedure of the fuel line with nitrogen.
  • the vessel 12 comprises a fluid jacket 44 which is arranged for cooling the vessel by circulating a cooling fluid, such as water therein.
  • the fluid jacket 44 is provided with a fluid inlet 46 and a fluid outlet 48.
  • the cracking zone 102 is provided with an outlet 18’ which forms a constriction to the cross-sectional area of the cracking zone 102.
  • the constriction is preferable conical at both sides of the constriction smoothly separating the cracking zone and the oxidizer part 104.
  • the oxidizer part 104 is provided with one or more oxidizer inlets 50 connected to the source of gas containing oxygen 26 via flow channels 52.
  • the flow channels open into an annular slot 54 which is arranged radially outside to the sleeve 29.
  • the annular slot 54 is formed between an inner wall of the vessel 12 and a second sleeve 56.
  • the second sleeve 56 extends from the end wall 32 to the outlet 18’ such that the slot 54 has substantially constant radial width.
  • the slot and the second sleeve 56 which extend axially farther than the sleeve 29 from the end wall 32 which is arranged in direct heat transfer communication with the cracking zone 102 preheating the gas, due to heat transfer from the gas and/or flame in the space 100.
  • the flow channels 52 are preferably arranged not to be in direct heat transfer connection with the fluid jacket 44, or cooled wall of the vessel 12.
  • the source of gas containing oxygen 26 is connected to the flow channel 52. As is shown in the figure the source of gas containing oxygen 26 which is connected to the flow channel 52 may be different from the source of gas containing oxygen connected to the burner 14 for improving controllability of the burner 14.
  • the oxidizer inlet 50 opens into a space in the oxidizer part 104 at proximity to the outlet 18’ of the cracking zone.
  • the burner 14 combusts the ammonia and provides heat for cracking, and ammonia is cracked in the cracking zone 102 as is described in the other embodiments.
  • the product gas from the cracking zone 102 is fed into the oxidizer part 104 is auto ignited in the presence of oxygen due to the gas temperature being higher than its autoignition temperature.
  • Ammonia 22 and combustion air 26 is premixed and swirled in the burner inlet 14, ignited and making a rich i.e. excess fuel flame 101. This flame will provide heat for ammonia cracking 102.
  • Vent gas from inerting procedure of the fuel line with nitrogen a second source of ammonia 22’
  • a mixture of ammonia and nitrogen vent composition will vary
  • the heat from combustion will decompose ammonia into nitrogen and hydrogen. As the combustion is rich, there is no air available to burn the hydrogen.
  • the exhaust consisting of N 2 , NO, NO 2 and H 2 , will leave the cracking zone 102 stage through the outlet 18’, where air is supplied through the inlets 50, mixing with the hydrogen and being ignited by the hot surface.
  • the outlet area is made of high temperature resistant material, being not cooled by cooling fluid and the mixture will burn in the oxidizer part 104.
  • the downstream exhaust will consist of N 2 , H 2 O and small traces of NO and NO 2 (in the 10-15 ppm range).
  • Part list a cracking arrangement 10 a cracking vessel 12 a first end 12.1 of the space in the vessel a second end 12.2 of the space in the vessel a burner 14 a centre axis of the cracking vessel 16 an outlet 18 a first inlet 20 a branch feed line 21 a source of ammonia 22 a pump 23 a second inlet 24 common gas inlet 24’ a gas mixture feed line 25 a source of gas containing oxygen 26 a source of pressurized oxygen 26’ feed channels 27 a third inlet 28 a sleeve 29 a side wall 30 an end wall 32 valve 34 a heat recovery device 36 an outlet line 38 an air feed line 40 a compressor 42 a fluid jacket 44 a fluid inlet 46 a fluid outlet 48 oxidizer inlet 50 oxidizer flow channel 52 inner space of the vessel 100 a combustion zone 101 a cracking zone 102 an ammonia cracking catalytic converter 103 an oxidizer part 104

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
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Abstract

L'invention concerne un procédé de craquage d'ammoniac, comprenant : - l'introduction d'une première partie d'ammoniac dans un brûleur (14) disposé dans un réacteur de craquage (12) ; - l'introduction du gaz contenant de l'oxygène dans le brûleur (14) ; - la combustion de la première partie d'ammoniac formant une zone de combustion (101) dans le réacteur de craquage (12) de manière à produire de la chaleur ; - l'introduction d'une seconde partie d'ammoniac dans une zone de craquage (102) du réacteur de craquage (12) à l'extérieur de la zone de combustion (101), et - le craquage de la seconde partie d'ammoniac en utilisant la chaleur produite par la combustion de la première partie d'ammoniac et la production d'un produit gazeux comprenant de l'hydrogène et de l'azote à partir de la seconde partie d'ammoniac. L'invention concerne également un agencement de craquage (10) pour le craquage de l'ammoniac.
PCT/EP2022/068439 2022-07-04 2022-07-04 Procédé de craquage d'ammoniac et agencement de craquage pour le craquage de l'ammoniac WO2024008270A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2022/068439 WO2024008270A1 (fr) 2022-07-04 2022-07-04 Procédé de craquage d'ammoniac et agencement de craquage pour le craquage de l'ammoniac

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2022/068439 WO2024008270A1 (fr) 2022-07-04 2022-07-04 Procédé de craquage d'ammoniac et agencement de craquage pour le craquage de l'ammoniac

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WO2024008270A1 true WO2024008270A1 (fr) 2024-01-11

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3198604A (en) * 1962-05-28 1965-08-03 Engelhard Ind Inc Hydrogen generating system
DE2617089A1 (de) * 1976-04-17 1977-11-03 Caloric Ges Apparatebau Ammoniak-spalter
US20030129555A1 (en) * 2001-12-25 2003-07-10 Yuji Mukai Burner for hydrogen generation system and hydrogen generation system having the same
US6936363B2 (en) 2000-07-25 2005-08-30 Apollo Energy Systems, Incorporated Ammonia cracker for production of hydrogen
CN210656142U (zh) * 2019-10-16 2020-06-02 厦门大学 一种辅助氨燃烧的热裂解制氢装置

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3198604A (en) * 1962-05-28 1965-08-03 Engelhard Ind Inc Hydrogen generating system
DE2617089A1 (de) * 1976-04-17 1977-11-03 Caloric Ges Apparatebau Ammoniak-spalter
US6936363B2 (en) 2000-07-25 2005-08-30 Apollo Energy Systems, Incorporated Ammonia cracker for production of hydrogen
US20030129555A1 (en) * 2001-12-25 2003-07-10 Yuji Mukai Burner for hydrogen generation system and hydrogen generation system having the same
CN210656142U (zh) * 2019-10-16 2020-06-02 厦门大学 一种辅助氨燃烧的热裂解制氢装置

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