WO1997033828A1 - Method for the manufacture of ammonia - Google Patents

Method for the manufacture of ammonia Download PDF

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Publication number
WO1997033828A1
WO1997033828A1 PCT/NL1997/000127 NL9700127W WO9733828A1 WO 1997033828 A1 WO1997033828 A1 WO 1997033828A1 NL 9700127 W NL9700127 W NL 9700127W WO 9733828 A1 WO9733828 A1 WO 9733828A1
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WO
WIPO (PCT)
Prior art keywords
flow
hydrogen
oxygen
nitrogen
air
Prior art date
Application number
PCT/NL1997/000127
Other languages
French (fr)
Inventor
Gerhard Pieter Jan Dijkema
Original Assignee
Technische Universiteit Delft
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Technische Universiteit Delft filed Critical Technische Universiteit Delft
Priority to AU20462/97A priority Critical patent/AU2046297A/en
Publication of WO1997033828A1 publication Critical patent/WO1997033828A1/en

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Classifications

    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • 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
    • 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
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/14—Fuel cells with fused electrolytes
    • H01M2008/147—Fuel cells with molten carbonates
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M2300/00—Electrolytes
    • H01M2300/0002—Aqueous electrolytes
    • H01M2300/0005—Acid electrolytes
    • H01M2300/0008—Phosphoric acid-based
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M2300/00—Electrolytes
    • H01M2300/0017—Non-aqueous electrolytes
    • H01M2300/0048—Molten electrolytes used at high temperature
    • H01M2300/0051—Carbonates
    • 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
    • Y02E60/50—Fuel cells
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/50—Manufacturing or production processes characterised by the final manufactured product

Definitions

  • the present invention relates to a method for the production of ammonia, wherein a nitrogen-comprising flow is brought together with a hydrogen-comprising flow and nitrogen and hydrogen are catalytically reacted.
  • water gas is produced by reacting a carbon source, such as methane, with water at an elevated temperature and pres ⁇ sure.
  • the water gas is the hydrogen-comprising flow.
  • the nitro ⁇ gen-comprising flow is applied in the form of air which, however, first has to be stripped to a considerable extent of oxygen. This is done by deliberately retaining CH 4 in the water gas, known as the methane slip, in the amount necessary to remove all oxygen from the supplied air by selective, catalytic oxidation under increased pressure. Sub-sequently a CO-shift reaction is carried out, in which CO is converted into C0 2 which is removed, yielding a mix ⁇ ture (synthesis gas) which is rich in nitrogen and hydrogen in a for the production of ammonia stoichiometric ratio.
  • An additional object is to provide a method by which the capacity of an existing plant for the production of synthesis gas can be expanded, or how, when building a new plant of a certain capacity, a smaller installation can be made to suffice.
  • the method according to the invention is characterized in that the nitrogen-comprising flow is obtained by means of a fuel cell installation having a cathode and an anode, by feeding air to the cathode and a fuel-containing flow to the anode, resulting at the cathode in oxygen-depleted air and at the anode in a fuel-depleted flow, after which the oxygen-depleted air as the nitrogen- comprising flow is combined with the hydrogen-comprising flow and the oxygen present in the oxygen-depleted air is used for the catalytic conversion of a hydrocarbon present in the hydrogen-comprising flow.
  • reaction (1) can be carried out at elevated temperature. Because the amount of methane in the water gas is decreased, a gas mixture is provided having less volume, a lower concentration of CO and C0 2 , and a higher concentration of H 2 and N 2 . Energy is saved through the fact that for the removal of oxygen by selective oxidation of methane and later for the ammonia production less air or rather, according to the invention, oxygen-depleted air has to be brought up to an increased pressure and temperature.
  • US 4,578,214 discloses a method for the production of ammonia using a fuel cell.
  • a flow coming from a secondary reformer is subjected to a catalytic shift reac ⁇ tion yielding a hydrogen-comprising flow.
  • oxygen depletion of air takes place with the aid of a fuel cell, while the fuel is supplied by an offshoot of the hydrogen- comprising flow.
  • the oxygen-depleted air is subsequently fed to a unit for the complete removal of oxygen, yielding a nitrogen-comprising flow from which oxygen is substan ⁇ tially completely removed.
  • a second hydrogen-comprising flow in particular a hydrogen- comprising process flow from the ammonia production, is applied.
  • hydrogen-comprising discharge gas is used as the hydrogen- comprising process flow of the ammonia production.
  • This discharge gas having a high energy content is used for the generation of high-grade electric energy, while the remaining energy content of the resulting hydro ⁇ gen-depleted flow being released at the anode of the fuel cell installation can be used by combustion.
  • This reaction is carried out at a temperature of 475-600°C and greatly increased pressure (100-200 bar) in the presence of a catalyst. Compression requires much energy.
  • the flow used to obtain nitrogen is air.
  • the use of pure nitrogen is known in itself.
  • the production of nitrogen from air by means of gas separ ⁇ ation requires much energy and is expensive.
  • An important advantage of the method according to the present invention is that by feeding to the secondary reformer, a further separation, in particular a further separation or conver ⁇ sion of oxygen from (oxygen-depleted) air is avoided.
  • air A is oxygen-depleted by supplying the same to a fuel cell 2, which has a cathode at a cathode side 3 and an anode at an anode side 4.
  • a fuel-containing flow B is sup ⁇ plied to the anode.
  • Such operation of the fuel cell 2 effi ⁇ ciently provides high-grade electric energy.
  • the heat released in the fuel cell 2 may optionally be utilized in the production process. Any kind of fuel cell having suf ⁇ ficient capacity may be used as fuel cell 2 for the oxygen depletion of air A.
  • Suitable fuel cell 2 is the phosphoric acid fuel cell (PAFC) which is capable of removing more than 50% of oxygen from air A.
  • PAFC phosphoric acid fuel cell
  • the type of fuel to be supplied depends on the kind of fuel cell used. Often hydrogen is suitable. In the pro ⁇ duction of ammonia there are various hydrogen-comprising gas flows that can be used as fuel for the fuel cell 2, for instance water gas. Some kinds of fuel cells, such as the molten carbonate fuel cell (MCFC) , are also able to use CO as fuel, therefore they will be preferred when using CO- containing gas flows.- The so-called “direct-reforming" fuel cells, such as DIR-MCFC, are able to use methane as fuel.
  • MCFC molten carbonate fuel cell
  • this hydrogen- comprising discharge gas is supplied to the anode of the fuel cell 2.
  • the method according to the invention results in a larger amount of synthesis gas, so that it is possible to increase the production capacity of existing installations for the production of nitrogen-hydrogen mixtures which are required for the production of ammonia, by providing them with a fuel cell device 2 for the production of oxygen-depleted air. If 50% of the oxygen present in air is removed, the maximal capacity increase is 8.8%. A removal of 67% results in a capacity increase of maximally 12%. Newly to be built installations having a particular capacity may be dimen ⁇ sioned smaller, which lowers costs. If the installation for the production of ammonia cannot accommodate the capacity increase, the up-stream installation for the production of nitrogen-hydrogen mixture can be operated with a reduced energy consumption.
  • the volume of oxygen-depleted air is smaller than that of the air used in accordance with the invention, therefore less energy is required for its compression. Com ⁇ pression is necessary for the removal of the remaining oxy ⁇ gen through selective oxidation of methane.
  • a primary reformer 1 running on steam is unable to convert all the methane.
  • further removal of methane which is present in the water gas is necessary in order to limit the amount of gas discharged from the ammo ⁇ nia production.
  • this is done by means of selec ⁇ tive oxidation in a secondary reformer 5, whereby the oxy- gen of the air is completely used up. This leaves the required nitrogen, which nitrogen together with hydrogen will be converted into ammonia.
  • the operation conditions of the primary reformer 1 are chosen such that after the methane present in the water gas has been converted with oxygen from the air, a for the production of ammonia stoichiometric ratio of hydrogen and nitrogen (3:1) is obtained.
  • the prior art fuel cells are not able to use all the oxygen from the supplied air.
  • more methane can be converted in the first reformer 1 and the remaining methane in the secondary reformer 5 is removed with the aid of a still oxigen-com- prising nitrogen flow coming from the fuel cell.
  • syn ⁇ thesis gas which results from the selective oxidation of methane, contains less CO and C0 2 .
  • Carbon monoxide is cata- lytically converted into carbon dioxide (CO-shift, not shown) according to the prior art, which is removed in the usual manner in an absorption column 6.
  • a suitable absorbent liquid such as Selexol ® may be used, which is continuously regenerated in a second desorption and regeneration column 7. Because the concentration of CO and C0 2 in the synthesis gas according to the invention is lower, it can be more easily regenerated.
  • the capacity of the absorption column described below may be smaller and the operation of column 7 costs less energy. Traces of car ⁇ bon dioxide which could interfere with the conversion of nitrogen and hydrogen into ammonia, are removed by convert ⁇ ing them into methane in a methanizer 8.
  • the mixture of nitrogen and hydrogen thus purified is fed to reactor 9.
  • the reaction yield is low, so that, after separation of the ammonia that has been formed, non-reacted nitrogen and hydrogen have to be fed back via pipe 11 to reactor 9.
  • this hydrogen-com ⁇ prising discharge gas is utilized as the fuel flow B.
  • this discharge gas whose energy content accor ⁇ ding to the prior art can only be converted into low-grade heat energy, is utilized for the generation of high-grade electric energy while, at the same time process air is depleted of oxygen.
  • This advantage is partly due to the fact that the amount of hydrogen in discharge gas comple ⁇ ments the amount of oxygen to be depleted from air A.
  • the fuel cells according to the state of the art do not convert all the fuel supplied, the fuel-depleted gas flow is still combustible. It is also possible to recover the remaining hydrogen by means of the pressure swing absorp ⁇ tion technique.
  • the PSA technique could also be used to directly extract hydrogen from the hydrogen-com ⁇ prising discharge flow, part of this hydrogen will only become available under low pressure.
  • the hydrogen is used to generate high-grade energy. Separation over a membrane yields hydrogen which is under low pressure. To compress it again requires much energy. According to the invention the hydrogen can indeed be separated over a membrane and yet be used for the gener ⁇ ation of high-performance energy.
  • the hydrogen-comprising discharge gas will be purified, for instance by means of a membrane separation unit 13, a pres ⁇ sure swing absorption unit or simply by washing with water.
  • the hydrogen-depleted flow D can advantageously be utilized as starting material for the recovery of inert gasses.
  • the starting material used for the recovery of inert gasses is the hydrogen-depleted flow C released at the cathode. This is possible if interfering contaminants are removed from the fuel flow B which is to be fed to the anode.

Abstract

The invention relates to a method for the production of ammonia, wherein a hydrogen-comprising discharge flow is utilized for the depletion of oxygen in air. Subsequently the oxygen-depleted air is - as nitrogen-comprising flow - brought into contact with water gas, which is the hydrogen - comprising flow. Oxygen depletion is carried out with the aid of a fuel cell installation (2). The method according to the invention is energy-saving.

Description

Method for the manufacture of ammonia
The present invention relates to a method for the production of ammonia, wherein a nitrogen-comprising flow is brought together with a hydrogen-comprising flow and nitrogen and hydrogen are catalytically reacted.
Such a method is generally known in the field. For the preparation of the hydrogen-comprising flow, so-called water gas is produced by reacting a carbon source, such as methane, with water at an elevated temperature and pres¬ sure.
CH4 + H20 + energy → CO + 3 H2 (1)
The water gas is the hydrogen-comprising flow. The nitro¬ gen-comprising flow is applied in the form of air which, however, first has to be stripped to a considerable extent of oxygen. This is done by deliberately retaining CH4 in the water gas, known as the methane slip, in the amount necessary to remove all oxygen from the supplied air by selective, catalytic oxidation under increased pressure. Sub-sequently a CO-shift reaction is carried out, in which CO is converted into C02 which is removed, yielding a mix¬ ture (synthesis gas) which is rich in nitrogen and hydrogen in a for the production of ammonia stoichiometric ratio. After the conversion of remaining CO traces into methane (methanization) , the mixture is further compressed and reacted at 450-600°C, yielding ammonia. The measure of con¬ version is limited. Non-reacted nitrogen and hydrogen are fed back. The accumulation of non-reactants such as inert gasses and methane requires these to be discharged in the form of a hydrogen-comprising discharge flow or to remove them from the synthesis gas by means of further treatment . The energy content of this hydrogen-comprising discharge flow is utilized by, for instance, combustion.
It is the object of the present invention to improve the method according to the preamble. A particular object is to improve the energy efficiency. An additional object is to provide a method by which the capacity of an existing plant for the production of synthesis gas can be expanded, or how, when building a new plant of a certain capacity, a smaller installation can be made to suffice. To this end the method according to the invention is characterized in that the nitrogen-comprising flow is obtained by means of a fuel cell installation having a cathode and an anode, by feeding air to the cathode and a fuel-containing flow to the anode, resulting at the cathode in oxygen-depleted air and at the anode in a fuel-depleted flow, after which the oxygen-depleted air as the nitrogen- comprising flow is combined with the hydrogen-comprising flow and the oxygen present in the oxygen-depleted air is used for the catalytic conversion of a hydrocarbon present in the hydrogen-comprising flow.
As a result of oxygen-depleted air being fed to the hydrogen-comprising flow, the amount of hydrocarbon (usually methane) in the water gas required for the removal of oxygen may be reduced. This means that reaction (1) can be carried out at elevated temperature. Because the amount of methane in the water gas is decreased, a gas mixture is provided having less volume, a lower concentration of CO and C02, and a higher concentration of H2 and N2. Energy is saved through the fact that for the removal of oxygen by selective oxidation of methane and later for the ammonia production less air or rather, according to the invention, oxygen-depleted air has to be brought up to an increased pressure and temperature.
US 4,578,214 discloses a method for the production of ammonia using a fuel cell. Herein a flow coming from a secondary reformer is subjected to a catalytic shift reac¬ tion yielding a hydrogen-comprising flow. According to the method known from this US patent specification, oxygen depletion of air takes place with the aid of a fuel cell, while the fuel is supplied by an offshoot of the hydrogen- comprising flow. The oxygen-depleted air is subsequently fed to a unit for the complete removal of oxygen, yielding a nitrogen-comprising flow from which oxygen is substan¬ tially completely removed. The part of the hydrogen-com- 97/33828 PC1 NL 7
3 prising flow which is not fed to the fuel cell, is fed to a pressure swing adsorption unit for the removal of carbon dioxide, carbon monoxide, water and methane. Hereby, how¬ ever, part of the hydrogen and an even larger part of the nitrogen are also discharged from the hydrogen-comprising flow. To further the recovery of hydrogen and to compensate the loss of nitrogen, the pressure swing adsorption unit is washed with the substantially completely oxygen-depleted nitrogen flow. Although the opposite is intended, the known method requires relatively much energy. With the present invention an oxygen-depleted nitrogen flow coming from a fuel cell and (without further separation or conversion of oxygen) is fed to the secondary reformer.
According to a preferred embodiment of the method in accordance with the invention, as fuel-containing flow a second hydrogen-comprising flow, in particular a hydrogen- comprising process flow from the ammonia production, is applied.
Such an application makes the method more economic. According to a particularly advantageous embodiment hydrogen-comprising discharge gas is used as the hydrogen- comprising process flow of the ammonia production.
This discharge gas having a high energy content is used for the generation of high-grade electric energy, while the remaining energy content of the resulting hydro¬ gen-depleted flow being released at the anode of the fuel cell installation can be used by combustion.
Other goals and advantages of the invention are described and elucidated with reference to the drawing which is a schematic representation of an embodiment of the method according to the invention.
Methane and excess steam are reacted in a reformer l yielding a mixture of CO and H2 with in addition small amounts of C02, so-called water gas. This conversion usually takes place at 20-30 bar and 800°C. This water gas provides the hydrogen required for the production of ammo¬ nia in accordance with the reaction equation:
N2 + 3 H2 → 2 NH3 + energy (2) This reaction is carried out at a temperature of 475-600°C and greatly increased pressure (100-200 bar) in the presence of a catalyst. Compression requires much energy. In practice, the flow used to obtain nitrogen is air. The use of pure nitrogen is known in itself. However, the production of nitrogen from air by means of gas separ¬ ation requires much energy and is expensive. An important advantage of the method according to the present invention is that by feeding to the secondary reformer, a further separation, in particular a further separation or conver¬ sion of oxygen from (oxygen-depleted) air is avoided.
By using the method according to the present inven¬ tion, air A is oxygen-depleted by supplying the same to a fuel cell 2, which has a cathode at a cathode side 3 and an anode at an anode side 4. A fuel-containing flow B is sup¬ plied to the anode. Such operation of the fuel cell 2 effi¬ ciently provides high-grade electric energy. The heat released in the fuel cell 2 may optionally be utilized in the production process. Any kind of fuel cell having suf¬ ficient capacity may be used as fuel cell 2 for the oxygen depletion of air A. Naturally those fuel cells are pre¬ ferred which generate electricity with the most efficiency, optimally oxygen-deplete the air A and exhibit the least sensitivity to possible impurities present in the supplied air A and fuel flow B. An example of a suitable fuel cell 2 is the phosphoric acid fuel cell (PAFC) which is capable of removing more than 50% of oxygen from air A.
Outside the field of ammonia production the applica- tion of fuel cells for the removal of oxygen from air is known from US 5,330,857 and 4,767,606.
The type of fuel to be supplied depends on the kind of fuel cell used. Often hydrogen is suitable. In the pro¬ duction of ammonia there are various hydrogen-comprising gas flows that can be used as fuel for the fuel cell 2, for instance water gas. Some kinds of fuel cells, such as the molten carbonate fuel cell (MCFC) , are also able to use CO as fuel, therefore they will be preferred when using CO- containing gas flows.- The so-called "direct-reforming" fuel cells, such as DIR-MCFC, are able to use methane as fuel.
As will be explained later, during the production of ammonia a hydrogen-comprising discharge gas is formed, and according to a very favourable embodiment this hydrogen- comprising discharge gas is supplied to the anode of the fuel cell 2.
In relation to the starting amount of methane, the method according to the invention results in a larger amount of synthesis gas, so that it is possible to increase the production capacity of existing installations for the production of nitrogen-hydrogen mixtures which are required for the production of ammonia, by providing them with a fuel cell device 2 for the production of oxygen-depleted air. If 50% of the oxygen present in air is removed, the maximal capacity increase is 8.8%. A removal of 67% results in a capacity increase of maximally 12%. Newly to be built installations having a particular capacity may be dimen¬ sioned smaller, which lowers costs. If the installation for the production of ammonia cannot accommodate the capacity increase, the up-stream installation for the production of nitrogen-hydrogen mixture can be operated with a reduced energy consumption.
The volume of oxygen-depleted air is smaller than that of the air used in accordance with the invention, therefore less energy is required for its compression. Com¬ pression is necessary for the removal of the remaining oxy¬ gen through selective oxidation of methane.
A primary reformer 1 running on steam is unable to convert all the methane. However, further removal of methane which is present in the water gas is necessary in order to limit the amount of gas discharged from the ammo¬ nia production. In practice this is done by means of selec¬ tive oxidation in a secondary reformer 5, whereby the oxy- gen of the air is completely used up. This leaves the required nitrogen, which nitrogen together with hydrogen will be converted into ammonia. The operation conditions of the primary reformer 1 are chosen such that after the methane present in the water gas has been converted with oxygen from the air, a for the production of ammonia stoichiometric ratio of hydrogen and nitrogen (3:1) is obtained. The prior art fuel cells are not able to use all the oxygen from the supplied air. By using the method according to the invention, more methane can be converted in the first reformer 1 and the remaining methane in the secondary reformer 5 is removed with the aid of a still oxigen-com- prising nitrogen flow coming from the fuel cell.
Consequently, the nitrogen and hydrogen mixture called syn¬ thesis gas, which results from the selective oxidation of methane, contains less CO and C02. Carbon monoxide is cata- lytically converted into carbon dioxide (CO-shift, not shown) according to the prior art, which is removed in the usual manner in an absorption column 6. For this purpose a suitable absorbent liquid such as Selexol® may be used, which is continuously regenerated in a second desorption and regeneration column 7. Because the concentration of CO and C02 in the synthesis gas according to the invention is lower, it can be more easily regenerated. The capacity of the absorption column described below may be smaller and the operation of column 7 costs less energy. Traces of car¬ bon dioxide which could interfere with the conversion of nitrogen and hydrogen into ammonia, are removed by convert¬ ing them into methane in a methanizer 8.
The mixture of nitrogen and hydrogen thus purified is fed to reactor 9. As mentioned above, the reaction yield is low, so that, after separation of the ammonia that has been formed, non-reacted nitrogen and hydrogen have to be fed back via pipe 11 to reactor 9. This causes an accumula¬ tion of non-reactants, such as inert gasses. Therefore they have to be discharged as a hydrogen-comprising discharge gas via pipe 12. According to a very favourable embodiment of the method according to the invention this hydrogen-com¬ prising discharge gas is utilized as the fuel flow B. In this manner this discharge gas, whose energy content accor¬ ding to the prior art can only be converted into low-grade heat energy, is utilized for the generation of high-grade electric energy while, at the same time process air is depleted of oxygen. This advantage is partly due to the fact that the amount of hydrogen in discharge gas comple¬ ments the amount of oxygen to be depleted from air A. As the fuel cells according to the state of the art do not convert all the fuel supplied, the fuel-depleted gas flow is still combustible. It is also possible to recover the remaining hydrogen by means of the pressure swing absorp¬ tion technique. Although the PSA technique could also be used to directly extract hydrogen from the hydrogen-com¬ prising discharge flow, part of this hydrogen will only become available under low pressure. Both the PSA technique and raising the pressure demands energy, while according to the invention hydrogen is used to generate high-grade energy. Separation over a membrane yields hydrogen which is under low pressure. To compress it again requires much energy. According to the invention the hydrogen can indeed be separated over a membrane and yet be used for the gener¬ ation of high-performance energy. Depending on the sensitivity of the fuel cell installation 2 to contaminants, such as residual NH3, the hydrogen-comprising discharge gas will be purified, for instance by means of a membrane separation unit 13, a pres¬ sure swing absorption unit or simply by washing with water. The hydrogen-depleted flow D can advantageously be utilized as starting material for the recovery of inert gasses. According to an alternative embodiment, the starting material used for the recovery of inert gasses is the hydrogen-depleted flow C released at the cathode. This is possible if interfering contaminants are removed from the fuel flow B which is to be fed to the anode.

Claims

1. A method for the production of ammonia, wherein a nitrogen-comprising flow is brought together with a hydro¬ gen-comprising flow and nitrogen and hydrogen are catalyti- cally reacted, characterized in that the nitrogen-compri¬ sing flow is obtained by means of a fuel cell installation (2) having a cathode and an anode, by feeding air (A) to the cathode and a fuel-containing flow (B) to the anode, resulting at the cathode in oxygen-depleted air and at the anode in a fuel-depleted flow (C) , after which the oxy¬ gen-depleted air as the nitrogen-comprising flow is com¬ bined with the hydrogen-comprising flow and the oxygen pre- sent in the oxygen-depleted air is used for the catalytic conversion of a hydrocarbon present in the hydrogen-com¬ prising flow.
2. A method according to claim 1, characterized in that the fuel flow (B) is a second hydroge -comprising flow.
3. A method according to claim 2, characterized in that as the second hydrogen-comprising flow (B) a hydrogen- comprising process flow from the ammonia production is applied.
4. A method according to claim 3, characterized in that the hydrogen-comprising process flow from the ammonia production is subjected to a purification treatment prior to being fed to the anode.
5. A method according to claim 3 or 4, characterized in that as the hydrogen-comprising process flow from the ammonia production hydrogen-comprising discharge gas is applied.
6. A method according to one of the preceding claims, characterized in that the hydrogen-depleted flow C released at the anode of the fuel cell installation (2) is used as the starting material for the recovery of inert gasses.
7. A method according to claim 4 or 5, characterized in that the purification treatment comprises the formation of a second hydrogen-comprising flow and a flow containing the pollutants, and the flow containing the pollutants is utilized as starting material for the recovery of inert gasses.
PCT/NL1997/000127 1996-03-12 1997-03-12 Method for the manufacture of ammonia WO1997033828A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU20462/97A AU2046297A (en) 1996-03-12 1997-03-12 Method for the manufacture of ammonia

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL1002582A NL1002582C2 (en) 1996-03-12 1996-03-12 Process for the preparation of ammonia.
NL1002582 1996-03-12

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WO (1) WO1997033828A1 (en)

Cited By (16)

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WO2000046150A1 (en) * 1999-02-03 2000-08-10 Texaco Development Corporation Utilizing purge gas from ammonia synthesis
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US20140356744A1 (en) * 2013-05-29 2014-12-04 Mcalister Technologies, Llc Energy storage and conversion with hot carbon deposition
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