CN116119612A - Ammonia decomposition hydrogen production system - Google Patents

Ammonia decomposition hydrogen production system Download PDF

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Publication number
CN116119612A
CN116119612A CN202310220655.9A CN202310220655A CN116119612A CN 116119612 A CN116119612 A CN 116119612A CN 202310220655 A CN202310220655 A CN 202310220655A CN 116119612 A CN116119612 A CN 116119612A
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China
Prior art keywords
unit
ammonia
gas
preheating
hydrogen
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CN202310220655.9A
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Inventor
王业勤
叶根银
常锦
严莎
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Sichuan Yalian Hydrogen Energy Technology Co ltd
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Sichuan Yalian Hydrogen Energy Technology Co ltd
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Priority to CN202310220655.9A priority Critical patent/CN116119612A/en
Publication of CN116119612A publication Critical patent/CN116119612A/en
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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
    • C01B3/04—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
    • 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
    • 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
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

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

Abstract

The invention provides an ammonia decomposition hydrogen production system, and relates to the technical field of hydrogen production. The ammonia decomposition hydrogen production system comprises: the device comprises a liquid ammonia storage unit, a primary preheating unit, a secondary preheating unit, an ammonia decomposition unit, an ammonia adsorption unit, a hydrogen purification unit and a hydrogen storage unit; the liquid ammonia storage unit is used for providing liquid ammonia for the primary preheating unit, the secondary preheating unit is respectively communicated with the ammonia decomposition unit and the ammonia adsorption unit, and the gas distribution area of the secondary preheating unit is connected with the air pipeline; the gas in the ammonia decomposition unit is conveyed into the primary preheating unit and then is introduced into the ammonia adsorption unit; the outlet of the ammonia adsorption unit is respectively communicated with the secondary preheating unit and the hydrogen purification unit; the hydrogen outlet of the hydrogen purification unit is communicated with the hydrogen storage unit, and the waste gas outlet is communicated with the secondary preheating unit. The invention realizes vaporization and heating of liquid ammonia by electric heating and self-heating, and provides partial heat supply for ammonia decomposition by ammonia and hydrogen prepared by circulation, thereby improving the heat conversion rate of the whole system.

Description

Ammonia decomposition hydrogen production system
Technical Field
The invention relates to the technical field of hydrogen production, in particular to an ammonia decomposition hydrogen production system.
Background
The ammonia decomposing hydrogen producing technology uses ammonia as material and under the action of Ru, ni, fe and Co catalyst, the mixture is heated to 400-1000 deg.c to decompose to obtain mixed hydrogen-nitrogen gas containing 75% H2 and 25% N2. And then purifying the hydrogen-nitrogen mixed gas to obtain 99% -99.999% hydrogen.
The existing ammonia decomposition devices have great limitations. Because most of raw materials are liquid ammonia, and ammonia decomposition is an endothermic reaction, the reaction temperature is high, and a large amount of heat needs to be provided. Resulting in high energy consumption of the existing devices.
In the prior art, heat is generally provided by arranging an independent combustion module or an electric heating device, so that the energy consumption is high, the manufacturing cost is high, and the problems of insufficient energy utilization, heat loss, low conversion rate and the like of a plurality of ammonia decomposition hydrogen production systems exist at present.
Therefore, a simple structure, efficient heat utilization and reduction of external heat supply are required.
Disclosure of Invention
Aiming at the problems that the existing ammonia decomposition hydrogen production system is insufficient in energy utilization, low in heat loss and conversion rate and the like, the invention provides the ammonia decomposition hydrogen production system, which utilizes electric heating and self-heating to realize vaporization and heating of liquid ammonia, utilizes ammonia and circularly prepared hydrogen to provide a part of heat for ammonia decomposition and improves the heat conversion rate of the whole system.
The technical scheme adopted by the invention is as follows:
an ammonia decomposition hydrogen production system comprising: the device comprises a liquid ammonia storage unit, a primary preheating unit, a secondary preheating unit, an ammonia decomposition unit, an ammonia adsorption unit, a hydrogen purification unit and a hydrogen storage unit;
the liquid ammonia storage unit provides liquid ammonia for the primary preheating unit, and an ammonia medium outlet of the primary preheating unit is communicated with an ammonia medium inlet of the secondary preheating unit;
the ammonia medium outlet of the secondary preheating unit is communicated with the ammonia decomposition unit, and the reaction gas outlet of the catalytic combustion of the secondary preheating unit is communicated with the ammonia adsorption unit; the reaction gas outlet in the secondary preheating unit is connected to the ammonia adsorption unit and then is discharged through a pipeline; an air inlet pipeline is arranged at the air inlet of the secondary preheating unit;
the ammonia decomposition gas outlet of the ammonia decomposition unit is connected into the primary preheating unit through a pipeline, and the pipeline passes through the primary preheating unit to be connected into the ammonia adsorption unit;
the hydrogen-nitrogen mixed medium outlet of the ammonia adsorption unit is communicated with the air inlets of the hydrogen purification unit and the secondary preheating unit; the desorption gas outlet of the ammonia adsorption unit is communicated with the gas inlet of the secondary preheating unit;
the hydrogen outlet of the hydrogen purification unit is communicated with the hydrogen storage unit, and the waste gas outlet of the hydrogen purification unit is connected to the gas inlet of the secondary preheating unit;
wherein, the second-stage preheating unit includes:
the preheating tank is provided with two tube plates along the axial direction of the preheating tank, and the two tube plates divide the interior of the preheating tank into a gas distribution area, a reaction area and an air outlet area;
the ammonia medium outlet of the ammonia adsorption unit, the waste gas outlet of the hydrogen purification unit and the air inlet pipeline are all connected into the gas distribution area;
the reaction pipeline is arranged between the two tube plates, two ends of the reaction pipeline are respectively communicated with the gas distribution area and the gas outlet area, and the reaction pipeline is filled with a catalyst;
the ammonia gas conveying pipeline is arranged in the preheating tank, two ends of the ammonia gas conveying pipeline extend out of the preheating tank, are respectively communicated with the primary preheating unit and the ammonia decomposition unit, are spirally arranged in the reaction area, and are sleeved outside the reaction pipeline;
a heater disposed within the reaction zone;
the ventilation bracket is arranged in the air outlet area, and an air outlet is formed between the bottoms of the preheating tanks;
a filler filled in the gas outlet region;
wherein, the gas flow direction in the reaction pipeline is opposite to the ammonia flow direction in the ammonia conveying pipeline.
Optionally, the secondary preheating unit further includes:
and the gas distributor is arranged in the gas mixing area of the preheating tank and is used for distributing air and waste gas entering the preheating tank.
Optionally, the secondary preheating unit further includes:
the heat preservation layer is arranged on the side wall of the reaction area.
Optionally, the heater is a resistance heating wire, the resistance heating wire is spirally arranged along the axis of the reaction pipeline, and the ammonia gas conveying pipeline is positioned in the resistance heating wire.
Optionally, the pitch of the resistance heating wire is adjustable.
Optionally, the catalyst is Pt/TiO 2 、Pd/HZSM-5、CoO 2 、CuO 2 、LaMnO 3 Is a kind of the above-mentioned materials.
Optionally, the decomposition pipeline of the ammonia decomposition unit is filled with one of Ru, fe, co, ni, ni-Fe, non-noble metal or bimetallic catalyst.
Optionally, the ammonia adsorption unit includes:
the gas outlet end of the analysis component is communicated with the gas inlets of the hydrogen purification unit and the secondary preheating unit through a pipeline, and the gas inlet end of the analysis component is communicated with the ammonia decomposition unit;
and the air outlet end of the desorption component is communicated with the air inlet of the secondary preheating unit, and the air inlet end of the desorption component is communicated with the ammonia decomposition unit.
Optionally, the hydrogen purification unit is a PSA pressure swing adsorption unit.
Compared with the prior art, the invention has the beneficial effects that:
1. vaporization and heating of liquid ammonia are realized by utilizing electric heating and self-heating, and the ammonia and the recycled hydrogen are utilized to provide a part of heat supply for ammonia decomposition; the energy consumption of hydrogen production is reduced, the utilization rate of waste gas is improved, and the aim of saving energy is achieved.
2. The gas decomposed by ammonia at high temperature provides a large amount of heat for ammonia vaporization through the primary preheating unit, so that the extra heat required by vaporization is reduced. Reducing heat loss.
3. The desorption gas of the ammonia adsorption unit and the hydrogen purification unit is fed into the combustion of the catalytic reaction of the secondary preheater to supply heat, so that the utilization rate of heat energy is improved, and the energy loss is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of the overall structure of an ammonia decomposition hydrogen production system.
Fig. 2 is a schematic diagram of the structure of a secondary preheating unit of an ammonia decomposition hydrogen production system.
Reference numerals:
1. a liquid ammonia storage unit;
2. a primary preheating unit;
3. a secondary preheating unit; 31. a preheating tank; 32. a tube sheet; 33. a reaction pipeline; 34. an ammonia gas delivery pipe; 35. a heater; 36. a breathable support; 37. a filler; 38. a gas distributor; 39. a heat preservation layer;
4. an ammonia decomposition unit;
5. an ammonia adsorption unit;
6. a hydrogen purification unit;
7. and a hydrogen storage unit.
Detailed Description
Hereinafter, only certain exemplary embodiments are briefly described. As will be recognized by those of skill in the pertinent art, the described embodiments may be modified in various different ways without departing from the spirit or scope of the present invention. Accordingly, the drawings and description are to be regarded as illustrative in nature and not as restrictive.
In the present invention, unless explicitly specified and limited otherwise, the terms "connected," "connected," and the like are to be construed broadly, and may be fixedly connected, detachably connected, or integrally formed, for example; the device can be mechanically connected, electrically connected and communicated; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The following disclosure provides many different embodiments, or examples, for implementing different features of the invention. In order to simplify the present disclosure, components and arrangements of specific examples are described below. They are, of course, merely examples and are not intended to limit the invention. Furthermore, the present invention may repeat reference numerals and/or letters in the various examples, which are for the purpose of brevity and clarity, and which do not themselves indicate the relationship between the various embodiments and/or arrangements discussed. In addition, the present invention provides examples of various specific processes and materials, but one of ordinary skill in the art will recognize the application of other processes and/or the use of other materials.
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
As shown in fig. 1 and 2, an embodiment of the present invention provides an ammonia decomposition hydrogen production system, comprising: a liquid ammonia storage unit 1, a primary preheating unit 2, a secondary preheating unit 3, an ammonia decomposition unit 4, an ammonia adsorption unit 5, a hydrogen purification unit 6 and a hydrogen storage unit 7.
The liquid ammonia storage unit 1 provides liquid ammonia for the primary preheating unit 2, and an ammonia medium outlet of the primary preheating unit 2 is communicated with an ammonia medium inlet of the secondary preheating unit 3. The ammonia medium outlet of the secondary preheating unit 3 is communicated with the ammonia decomposition unit 4, and the reaction gas outlet of the catalytic combustion of the secondary preheating unit 3 is communicated with the ammonia adsorption unit 5; the reaction gas outlet of the secondary preheating unit 3 is connected into the ammonia adsorption unit 5 and then is discharged through a pipeline; an air inlet pipeline is arranged at the air inlet of the secondary preheating unit 3. The ammonia decomposition gas outlet of the ammonia decomposition unit 4 is connected into the primary preheating unit 2 through a pipe which passes through the primary preheating unit 2 and is connected into the ammonia adsorption unit 5. The outlet of the hydrogen-nitrogen mixed medium of the ammonia adsorption unit 5 is communicated with the air inlets of the hydrogen purification unit 6 and the secondary preheating unit 3; the desorption gas outlet of the ammonia adsorption unit 5 is communicated with the gas inlet of the secondary preheating unit 3. The hydrogen outlet of the hydrogen purification unit 6 is communicated with the hydrogen storage unit 7, and the exhaust outlet of the hydrogen purification unit 6 is connected to the air inlet of the secondary preheating unit 3.
The secondary preheating unit 3 includes: a preheating tank 31, a reaction pipe 33, an ammonia gas delivery pipe 34, a heater 35, a ventilation bracket 36 and a packing 37.
The preheating tank 31 is provided with two tube plates 32 along the axial direction of the preheating tank 31, and the two tube plates 32 divide the interior of the preheating tank 31 into a gas distribution area, a reaction area and an air outlet area. The ammonia medium outlet of the ammonia adsorption unit 5, the exhaust gas outlet of the hydrogen purification unit 6 and the air inlet pipe are all connected to the gas distribution area. And a reaction pipe 33 installed between the two tube plates 32, both ends of which are respectively communicated with the gas distribution area and the gas outlet area, wherein the reaction pipe 33 is filled with a catalyst. The ammonia gas conveying pipeline 34 is installed in the preheating tank 31, two ends of the ammonia gas conveying pipeline 34 extend out of the preheating tank 31, are respectively communicated with the primary preheating unit 2 and the ammonia decomposition unit 4, are spirally arranged in the reaction area, and are sleeved outside the reaction pipeline 33. A heater 35 disposed in the reaction region. And a ventilation bracket 36 disposed in the air outlet region, wherein the ventilation bracket 36 forms an air outlet between the bottoms of the preheating tanks 31. And a packing 37 filled in the gas outlet region. Wherein the gas flow direction in the reaction pipe 33 is opposite to the flow direction of the ammonia gas in the ammonia gas delivery pipe 34.
When in use, the liquid ammonia is preheated by the primary preheating unit 2, so that the liquid ammonia and the vaporized liquid ammonia have a certain temperatureThe degree goes into the secondary preheating unit 3. The secondary preheating unit 3 performs catalytic combustion in the reaction pipeline 33 after passing through the gas, and heat in the catalytic combustion process provides reaction heat for the mixture of the liquid ammonia and the vaporized liquid ammonia in the ammonia conveying pipeline 34. The ammonia gas delivery pipe 34 located in the reaction zone of the preheating pipe is arranged in a spiral shape in order to increase the reaction time of the mixture in the ammonia gas delivery pipe 34. The reacted gas enters an ammonia decomposition unit 4 for decomposition to obtain NH 3 +H 2 +N 2 The decomposed gas is sequentially connected into the primary preheating unit 2 and the ammonia adsorption unit 5 through pipelines, and is firstly discharged into the primary preheating unit 2 to preheat the liquid ammonia in the primary preheating unit 2 because the decomposed gas has a certain amount of heat, and then enters the ammonia adsorption unit 5 to be adsorbed. The exhaust gas after the catalytic combustion reaction of the secondary preheating unit 3 is connected into the ammonia adsorption unit 5 through a pipeline to provide heat for the ammonia adsorption unit 5. The mixed gas entering the ammonia adsorption unit 5 through the ammonia decomposition unit 4 is adsorbed and desorbed in the ammonia adsorption unit 5, and part of the hydrogen-nitrogen mixed gas obtained after adsorption is discharged into the hydrogen purification unit 6 and the other part is discharged into the secondary preheating unit 3; the ammonia gas obtained after the desorption gas is discharged into the secondary preheating unit 3 through a pipeline, and the fuel for catalytic combustion is provided for the secondary preheating unit 3. Considering the heat requirement of the ammonia adsorption unit, a part of hydrogen-nitrogen mixed gas can be separated out according to the heat requirement and enters the secondary preheating unit 3 to participate in catalytic combustion to supplement the heat of the ammonia adsorption unit. The hydrogen purified by the hydrogen purifying unit 6 enters the hydrogen storing unit 7 for storage. The other gas after purification is discharged into the secondary preheating unit 3 through a pipeline. Meanwhile, an air pipeline is also connected in the secondary preheating unit 3 to provide enough combustible gas for subsequent catalytic combustion.
The inlet of the catalytic combustion pipe of the secondary preheating unit 3 is connected to the exhaust gas outlet of the hydrogen purification unit 6, the medium outlet of the ammonia adsorption unit 5, and the air inlet through a multi-pass pipe. Thus, most of the gas in the medium outlet of ammonia adsorption unit 5 is vented into hydrogen purification unit 6.
The secondary preheating unit 3 works in more specific principle:
the preheated liquid ammonia enters the preheating tank 31 from the bottom of the preheating tank 31 through an ammonia delivery line 34. The catalyst is filled in the reaction tube 33 and the gas enters the gas distribution area through the top of the preheating tank 31, and is split by the gas distributor 38 in the gas distribution area, so as to avoid direct impact into the reaction tube 33. The heater 35 is now operated to provide a reaction temperature for the contact of the gas with the catalyst. Since the liquid ammonia entering the preheating tank 31 has a certain temperature, the temperature in the preheating tank 31 is increased, and the flow direction of the liquid ammonia is opposite to the flow direction of the gas, the working energy consumption of the heater 35 can be correspondingly reduced, and the purpose of reducing the energy consumption can be achieved.
It should be noted that, since the ammonia gas delivery pipe 34 is spirally provided to increase the residence time of the ammonia gas in the preheating pipe, the liquid ammonia in the ammonia gas delivery pipe 34 is sufficiently gasified.
The packing 37 is ceramic balls, and the ceramic balls are filled in the gas outlet area to support the tube plate 32. And the reacted gas enters the ventilating bracket 36 through the porcelain ball and then is discharged out of the preheating tank 31.
In another embodiment, as shown in fig. 2, in order to improve the mixing uniformity of multiple media, a gas distributor 38 is disposed at the inlet of the preheating pipe, so as to facilitate mixing the gas exhausted from the hydrogen purification unit 6 and the ammonia adsorption unit 5 with air, and the mixed gas is split and fills the whole gas mixing area.
In another embodiment, as shown in FIG. 2, a heat insulating layer 39 is provided on the inner side wall of the reaction region of the preheating tank 31 in order to improve the heat insulating performance of the preheating pipe. The insulating layer 39 is made of ceramic fiber cotton.
In another embodiment, as shown in fig. 2, the heater 35 is a resistance heating wire for heating the preheating tank 31 for convenience.
In one embodiment, the resistance heating wire is disposed in a spiral shape along the axis of the reaction tube 33, and the ammonia gas delivery tube 34 is disposed in the resistance heating wire. The pitch of the resistance heating wire is adjustable.
In another embodiment, the heating resistance wires have a plurality of vertically enclosed annular structures, and are enclosed outside the reaction tube 33.
In another embodiment, the catalyst is one of Pt/TiO2, pd/HZSM-5, coO2, cuO2 and LaMnO 3.
A catalyst (which is one of Pt/TiO2, pd/HZSM-5, coO2, cuO2, laMnO 3) is placed in the reaction tube 33 of the preheating tube, and the ammonia gas delivery tube 34 is spirally wound around the reaction tube 33, so that the ammonia gas can sufficiently absorb the heat of catalytic combustion. The electric heating mainly provides initial heat for catalytic combustion in the early stage, and can be turned off when the heat of the catalytic combustion is enough. In the catalytic combustion in the reaction line 33, the combustion gas is a mixture of hydrogen, nitrogen, air and a small amount of ammonia.
Meanwhile, the catalyst is convenient to replace in later period because the reaction pipeline 33 is a straight pipe. The bottom air permeable support 36 is removed during catalyst change, the ceramic balls are kept away from the preheating tube by gravity, and finally the catalyst is discharged through the bottom. When the catalyst is placed, the ceramic balls are first loaded into the gas outlet region, and then the catalyst is loaded into the reaction tube 33.
In another embodiment, the decomposition pipeline of the ammonia decomposition unit 4 is filled with one of Ru, fe, co, ni, ni-Fe, a non-noble metal or a bimetallic catalyst.
The ammonia gas has absorbed a large amount of heat before entering the ammonia decomposition unit 4, so that the reactor in the ammonia decomposition unit 4 needs only electric heating to supply a small amount of heat to reach its decomposition temperature at the time of the decomposition reaction. The ammonia decomposition catalyst can be one of noble metal such as Ru, fe, co, ni, ni-Fe, non-noble metal or bimetallic catalyst. Thus, the power consumption is reduced, and the process is simple. The decomposed gas enters the primary preheating unit 2 and the hydrogen purification unit 6 to supply heat for desorption.
In another embodiment, as shown in fig. 1, the ammonia adsorption unit 5 includes:
the gas outlet end of the analysis component is communicated with the gas inlets of the hydrogen purification unit 6 and the secondary preheating unit 3 through a pipeline, and the gas inlet end of the analysis component is communicated with the ammonia decomposition unit; and the air outlet end of the desorption component is communicated with the air inlet of the secondary preheating unit 3, and the air inlet end of the desorption component is communicated with the ammonia decomposition unit 4.
When NH 3 +H 2 +N 2 After the mixed gas of (a) enters the ammonia adsorption unit 5, a part of the gas is analyzed by an analysis module, and the analysis gas obtained by the analysis (the analysis gas means NH which has been removed 3 Is discharged into the secondary preheating unit 3 to provide waste heat and combustible gas for subsequent catalytic combustion. And the desorption component desorbs the mixed gas, and the desorbed hydrogen-nitrogen mixed gas is discharged into the hydrogen purification unit 6 for purification.
In another embodiment, the outlet of the desorption gas is connected to the hydrogen purification unit 6 and the secondary preheating unit 3 through a three-way pipe, and a metering valve is arranged on a pipeline of the secondary preheating unit 3, so that the mixed hydrogen-nitrogen gas entering the secondary preheating unit 3 can be conveniently regulated. More specifically, the adjustment is made according to the heat required by the working section of the ammonia adsorption unit 5, since one part of the hydrogen-nitrogen mixed gas can be used as a catalytic combustion reaction, and the other part provides heat supplement for the ammonia adsorption unit 5.
It should be further noted that the ammonia adsorption unit 5 sets 2 or more columns according to the size of the apparatus, wherein one column is performing NH 3 Adsorb and output H 2 +N 2 While the remaining columns are being subjected to NH 3 Is a desorption step of (a).
In another embodiment, the hydrogen purification unit 6 is a PSA pressure swing adsorption unit. The hydrogen purification unit 6 is a PSA pressure swing adsorption device for purifying hydrogen, so that the purity of the hydrogen can reach 99% -99.999%. The desorbed gas is then led into the secondary preheating unit 3 for catalytic combustion.
Finally, it should be noted that: the foregoing description is only a preferred embodiment of the present invention, and the present invention is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present invention has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (9)

1. An ammonia decomposition hydrogen production system comprising: the device comprises a liquid ammonia storage unit, a primary preheating unit, a secondary preheating unit, an ammonia decomposition unit, an ammonia adsorption unit, a hydrogen purification unit and a hydrogen storage unit; it is characterized in that the method comprises the steps of,
the liquid ammonia storage unit provides liquid ammonia for the primary preheating unit, and an ammonia medium outlet of the primary preheating unit is communicated with an ammonia medium inlet of the secondary preheating unit;
the ammonia medium outlet of the secondary preheating unit is communicated with the ammonia decomposition unit, and the reaction gas outlet of the catalytic combustion of the secondary preheating unit is communicated with the ammonia adsorption unit; the reaction gas outlet in the secondary preheating unit is connected to the ammonia adsorption unit and then is discharged through a pipeline; an air inlet pipeline is arranged at the air inlet of the secondary preheating unit;
the ammonia decomposition gas outlet of the ammonia decomposition unit is connected into the primary preheating unit through a pipeline, and the pipeline passes through the primary preheating unit to be connected into the ammonia adsorption unit;
the hydrogen-nitrogen mixed medium outlet of the ammonia adsorption unit is communicated with the air inlets of the hydrogen purification unit and the secondary preheating unit; the desorption gas outlet of the ammonia adsorption unit is communicated with the gas inlet of the secondary preheating unit;
the hydrogen outlet of the hydrogen purification unit is communicated with the hydrogen storage unit, and the waste gas outlet of the hydrogen purification unit is connected to the gas inlet of the secondary preheating unit;
wherein, the second-stage preheating unit includes:
the preheating tank is provided with two tube plates along the axial direction of the preheating tank, and the two tube plates divide the interior of the preheating tank into a gas distribution area, a reaction area and an air outlet area;
the ammonia medium outlet of the ammonia adsorption unit, the waste gas outlet of the hydrogen purification unit and the air inlet pipeline are all connected into the gas distribution area;
the reaction pipeline is arranged between the two tube plates, two ends of the reaction pipeline are respectively communicated with the gas distribution area and the gas outlet area, and the reaction pipeline is filled with a catalyst;
the ammonia gas conveying pipeline is arranged in the preheating tank, two ends of the ammonia gas conveying pipeline extend out of the preheating tank, are respectively communicated with the primary preheating unit and the ammonia decomposition unit, are spirally arranged in the reaction area, and are sleeved outside the reaction pipeline;
a heater disposed within the reaction zone;
the ventilation bracket is arranged in the air outlet area, and an air outlet is formed between the bottoms of the preheating tanks;
a filler filled in the gas outlet region;
wherein, the gas flow direction in the reaction pipeline is opposite to the ammonia flow direction in the ammonia conveying pipeline.
2. The ammonia destruction hydrogen production system of claim 1, wherein the secondary preheat unit further comprises:
and the gas distributor is arranged in the gas mixing area of the preheating tank and is used for distributing air and waste gas entering the preheating tank.
3. The ammonia destruction hydrogen production system of claim 1 or 2, wherein the secondary preheat unit further comprises:
the heat preservation layer is arranged on the side wall of the reaction area.
4. The ammonia destruction hydrogen production system according to any one of claims 1 to 3, wherein the heater is a resistance heating wire, the resistance heating wire is spirally disposed along an axis of the reaction pipe, and the ammonia gas delivery pipe is located in the resistance heating wire.
5. The ammonia destruction hydrogen production system of claim 4 wherein the pitch of the resistance heating wire is adjustable.
6. The ammonia decomposition hydrogen production system of claim 1 wherein said catalyst is Pt/TiO 2 、Pd/HZSM-5、CoO 2 、CuO 2 、LaMnO 3 Is a kind of the above-mentioned materials.
7. The ammonia decomposition hydrogen production system of claim 1 wherein the decomposition conduit of the ammonia decomposition unit is filled with one of Ru, fe, co, ni, ni-Fe, a non-noble metal or a bimetallic catalyst.
8. The ammonia decomposition hydrogen production system of claim 1, wherein the ammonia adsorption unit comprises:
the gas outlet end of the analysis component is communicated with the gas inlets of the hydrogen purification unit and the secondary preheating unit through a pipeline, and the gas inlet end of the analysis component is communicated with the ammonia decomposition unit;
and the air outlet end of the desorption component is communicated with the air inlet of the secondary preheating unit, and the air inlet end of the desorption component is communicated with the ammonia decomposition unit.
9. The ammonia destruction hydrogen production system of claim 1 wherein the hydrogen purification unit is a PSA pressure swing adsorption unit.
CN202310220655.9A 2023-03-09 2023-03-09 Ammonia decomposition hydrogen production system Pending CN116119612A (en)

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Application Number Priority Date Filing Date Title
CN202310220655.9A CN116119612A (en) 2023-03-09 2023-03-09 Ammonia decomposition hydrogen production system

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Application Number Priority Date Filing Date Title
CN202310220655.9A CN116119612A (en) 2023-03-09 2023-03-09 Ammonia decomposition hydrogen production system

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CN116119612A true CN116119612A (en) 2023-05-16

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