WO2017108629A2 - Procédé de synthèse de composés azotés à partir de déchets organiques et système de synthèse de composés azotés à partir de déchets organiques - Google Patents

Procédé de synthèse de composés azotés à partir de déchets organiques et système de synthèse de composés azotés à partir de déchets organiques Download PDF

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Publication number
WO2017108629A2
WO2017108629A2 PCT/EP2016/081544 EP2016081544W WO2017108629A2 WO 2017108629 A2 WO2017108629 A2 WO 2017108629A2 EP 2016081544 W EP2016081544 W EP 2016081544W WO 2017108629 A2 WO2017108629 A2 WO 2017108629A2
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Prior art keywords
nitrogen
hydrogen
carbon dioxide
container
ammonia
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PCT/EP2016/081544
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English (en)
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WO2017108629A3 (fr
Inventor
Tadeusz Bak
Rafal Chmielewski
Marek GOSCICKI
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Tadeusz Bak
Rafal Chmielewski
Goscicki Marek
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Publication of WO2017108629A2 publication Critical patent/WO2017108629A2/fr
Publication of WO2017108629A3 publication Critical patent/WO2017108629A3/fr

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    • 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
    • C01C1/0488—Processes integrated with preparations of other compounds, e.g. methanol, urea or with processes for power generation
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
    • C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
    • C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight
    • 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

Definitions

  • the present disclosure relates to a method for synthesizing nitrogenous compounds from organic waste as well as a system for synthesizing nitrogenous compounds from organic waste, such as ammonia, urea or nitrogen acid.
  • Gases such as CO2 and nitrogen oxides of various oxidation degrees (i.e.: N2O, NO, N2O3, NO2, N2O5, NO3) - referred to as NO x , form a group of pollutants that are generated during the combustion of solid, liquid and gaseous fuels.
  • Emission limiting norms related to air pollutants released into the atmosphere, set quantitative limits on a permissible amount of carbon dioxide (CO2) and nitrogen oxides (NO x ) that may be released from particular sources.
  • hydrogen used for ammonia synthesis is obtained in a process of production of CO or CO2 from methane or other hydrocarbons, as well as from a synthesis gas, also referred to as a syngas, which constitutes a product of gasification of hard coal, brown coal or coke.
  • the purity of the obtained hydrogen is important, because some impurities may cause inactivation of the catalysts that are used in synthesis of ammonia.
  • the nitrogen used in the ammonia synthesis process may be obtained from the air by means of physical condensation and rectification processes.
  • a US patent US8679439 discloses a method for synthesis of ammonia from biomass, which employs a gasification process conducted in the presence of oxygen from an air separator. A syngas obtained in this process is subsequently subjected to a catalytic reforming process yielding a hydrogen-richgas stream, comprising minor amount of hydrocarbons. The obtained hydrogen-reach gas serves as a source of hydrogen in various processes of ammonia synthesis involving air condensation and rectification process to obtain nitrogen - constituting a second reactant in ammonia synthesis.
  • a European patent application EP031 1932 discloses a method for production of ammonia syngas comprising a desired stoichiometric ratio of hydrogen and nitrogen.
  • the process of production of the syngas is carried out in a multi-column pressure swing system comprising a first group of columns for adsorption of CO2 and a second group of columns for adsorption of minor impurities.
  • the process involves introduction, into the system, a raw gas comprising mainly hydrogen, carbon dioxide and nitrogen, and minor amounts of carbon monoxide, methane and argon, wherein the three latter components together constitute about 1 % of the total volume of the raw gas.
  • the raw gas enters a first group of columns wherein CO2 is selectively adsorbed.
  • a CO2-free gas enters a second group of columns filled with an absorber for selectively absorbing minor impurities, i.e. argon, methane and carbon monoxide.
  • a purified syngas leaving the second group of absorption columns consists of nitrogen and hydrogen in a ratio suitable for ammonium synthesis. Therefore, this process involves neither after-combustion processes nor condensation/solidification processes of the raw gas components, and the obtained gas constitutes a mixture of nitrogen and hydrogen, thereby, not providing pure nitrogen or pure hydrogen, stored separately, to be used thereafter, depending on special technological needs.
  • a US patent US5523483 discloses an integrated system for synthesis of ammonia and urea.
  • the system comprises an ammonia syngas unit including primary and autothermal reformers, a shift converter, and a CO2 removal unit, for reacting hydrocarbon feedstock with steam and air to form a CO2 stream and a syngas makeup stream comprising hydrogen and nitrogen.
  • the system further comprises an ammonia conversion unit including a synthesis loop for mixing a recycle stream with the syngas makeup stream to form an ammonia converter feed stream.
  • the ammonia converter feed stream is fed into an ammonia synthesis reactor and the obtained ammonia stream from the synthesis reactor is recovered from effluent, and the recovered purge stream from the effluent stream forms a recycle stream.
  • the system further comprises an urea unit for reacting the CO2 stream with the ammonia stream to form urea at a relatively high pressure of above 14 MPa in the presence of a passivating amount of oxygen and a minor amount of nitrogen.
  • the urea unit comprises a high pressure scrubber for separating oxygen and nitrogen from an urea-containing stream to form a high pressure nitrogen stream containing minor amounts of oxygen, CO2 and ammonia. Therefore, the system does not contain any condensation/solidification unit. Moreover, the obtained ammonia and urea are produced from natural gas, and not from organic waste materials.
  • the known processes for synthesizing ammonia compounds from a syngas obtained through gasification of organic waste such as biomass are two-stage processes involving both the process ofseparation of hydrogen from the syngas and the process of providing nitrogen obtained in the process of condensation and rectification of the air.
  • the aim of the present disclosure is to provide a method for synthesizing ammonium compounds, such as ammonia or its derivatives, such as urea, from a syngas, comprising i.a. CO, CO2 and H2, obtained in the process of treating organic waste, including: biomass, municipal waste or waste plastics.
  • the aim is also to limit CO2 emission into an atmosphere both in the process of separation of nitrogen and the process of separation of hydrogen, providing at the same time improvement in the process energetic efficiency.
  • the mineralization device for producing a syngas by gasification of the organic waste, the mineralization device comprising a reaction chamber having a gasifying agent inlet, an air inlet and a syngas outlet;
  • catalyzer for after-combusting the syngas components comprising carbon monoxide and hydrogen to obtain an exhaust gas composition comprising nitrogen, carbon dioxide and water, the catalyzer being installed at the syngas outlet of the mineralization device;
  • the freezing-up system for condensing and/or freezing up of water and carbon dioxide from the exhaust gas, the freezing-up system comprising an exhaust gas inlet and outlets connected to a nitrogen container and a carbon dioxide container;
  • an electrolyzer for electrolyzing water to obtain hydrogen and oxygen, the electrolyzer having an oxygen outlet connected to the mineralization device and a hydrogen outlet connected to a hydrogen container;
  • ammonia synthesis reactor for synthesizing ammonia from nitrogen and hydrogen, the ammonia synthesis reactor comprising a nitrogen inlet connected to the nitrogen container and a hydrogen inlet connected to the hydrogen container.
  • the system may further comprise an urea synthesis device for synthesizing urea from ammonia and carbon dioxide, the urea synthesis device comprising an ammonia inlet connected to an outlet of the ammonia synthesis reactor and a carbon dioxide inlet connected to the carbon dioxide container.
  • an urea synthesis device for synthesizing urea from ammonia and carbon dioxide, the urea synthesis device comprising an ammonia inlet connected to an outlet of the ammonia synthesis reactor and a carbon dioxide inlet connected to the carbon dioxide container.
  • the system may further comprise an urea synthesis device for synthesizing urea from carbon dioxide, nitrogen and hydrogen, the urea synthesis device comprising a carbon dioxide inlet connected to the carbon dioxide container, a nitrogen inlet connected to the nitrogen container and a hydrogen inlet connected to the hydrogen container.
  • the system may further comprise a channel for feeding an exhaust gas generated in a Liquid Natural Gas regasification process to the freezing-up system.
  • a method for synthesizing of nitrogenous compounds from organic waste in a system comprising: - a mineralization device for producing a syngas by gasification of the organic waste, the mineralization device comprising a reaction chamber having a gasifying agent inlet, an air inlet and a syngas outlet;
  • catalyzer for after-combusting the syngas components comprising carbon monoxide and hydrogen to obtain an exhaust gas composition comprising nitrogen, carbon dioxide and water, the catalyzer being installed at the syngas outlet of the mineralization device;
  • the freezing-up system for condensing and/or freezing up of water and carbon dioxide from the exhaust gas, the freezing-up system comprising an exhaust gas inlet and outlets connected to a nitrogen container and a carbon dioxide container;
  • an electrolyzer for electrolyzing water to obtain hydrogen and oxygen, the electrolyzer having an oxygen outlet connected to the mineralization device and to a hydrogen outlet connected to a hydrogen container;
  • ammonia synthesis reactor for synthesizing ammonia from nitrogen and hydrogen, the ammonia synthesis reactor comprising a nitrogen inlet connected to the nitrogen container and a hydrogen inlet connected to the hydrogen container;
  • syngas comprising nitrogen, carbon oxide, carbon dioxide, hydrogen and steam
  • the method may be conducted in a system further comprising an urea synthesis device for synthesizing urea from ammonia and carbon dioxide, the urea synthesis device comprising an ammonia inlet connected to an outlet of the ammonia synthesis reactor and a carbon dioxide inlet connected to the carbon dioxide container, wherein the method further comprises a step of synthetizing urea using the ammonia obtained in the ammonia synthesis reactor and carbon dioxide collected in the carbon dioxide container.
  • Fig. 1 presents schematically a system for synthesis of ammonium compounds from the organic waste
  • Fig. 2 presents schematically a mineralization device for mineralization (gasification) of carbon fuel.
  • FIG. 1 A system for a synthesizing ammonium compounds from organic waste is presented schematically in Fig. 1 .
  • the system can operate interchangeably in both continuous and batch mode, depending on process needs, current raw material balances (which constitute the quantity of the available raw material) and available capacity for storage of the products, i.e. ammonia and ammonium compounds, such as urea.
  • the system for synthesizing ammonium compounds comprises a mineralization device 1 10 for production of a synthesis gas (a syngas) in a process involving gasification of organic waste in a presence of a gasifying factor.
  • the waste that may be gasified in the mineralization device 1 10 includes: municipal waste, plastics waste or biomass - for example, biomass of agricultural origin.
  • the organic waste that constitutes the raw material subject to the mineralization process may comprise silica (S1O2), hydrocarbons (C n H m ) including: aromatic, aliphatic, alicyclic, branched, saturated or unsaturated hydrocarbons, as well as biomass comprising cellulosic materials n(C6Hi2O6) and water.
  • the mineralization device 1 10 as used herein can have a construction as disclosed in a European patent application EP2860450.
  • the construction of the that mineralization device is shown schematically in Fig. 2.
  • the mineralization device 1 10 for production of synthesis gas from organic waste comprises a substantially horizontal rotary tube that serves as a reaction chamber 210 of the mineralization device.
  • the reaction chamber 210 comprises elements 212, 213, 214 which are fixedly and/or adjustably mounted inside the reaction chamber 210.
  • the elements provide appropriate transfer of the feedstock through the rotating reactor tube during the gasification process. Therefore, the process of mineralization (gasification) of the organic waste is carried out in a continuous mode, according to the process parameters described in EP2860450, providing organic waste as a feedstock to form gaseous combustion products.
  • the mineralization device 1 10 comprises nozzles through which the gasifying agent may be introduced into the reaction chamber.
  • the nozzles may have, for example, the form of inlet ports allowing regulation of the flow.
  • the air or oxygen- enriched air is used therein as the gasifying agent, whereas the nitrogen content present in the gasifying agent is selected so as to obtain a suitable hydrogen percentage in the obtained gasification product, i.e. the syngas.
  • the introduction of nitrogen together with the gasifying agent into the mineralization device 1 10 requires neither additional processing operations nor additional energy input, because the nitrogen is introduced into the reaction chamber as one of the air stream components, wherein the nitrogen share in the gasifying agent stream is adjusted by the addition of pure oxygen to the air stream.
  • the air introduced into the reaction chamber may be oxygen- enriched, wherein the greater the oxygen share in the gasifying agent, the higher the gasifying efficiency.
  • the oxygen that is used for enriching the air stream is obtained in the process of water electrolysis in which oxygen and hydrogen are obtained.
  • the electrolysis is carried out in an electrolyzer 140 cooperating with the system for synthesis of the ammonium compounds.
  • Various conventional systems enabling electrolysis of water may serve as the electrolyzing device 140 in the system.
  • the oxygen obtained in the electrolysis which is thereafter used as the gasifying agent in the mineralization (gasification) process, may be supplied directly to the reaction chamber of the mineralization device 1 10 by means of an oxygen supply system, wherein oxygen is mixed with air in a particular ratio.
  • the excess oxygen, produced in the electrolyzer 140 may be collected and stored in the oxygen container to be used later on, depending on the process needs.
  • the hydrogen which is also obtained in the electrolysis process, is collected and stored in the hydrogen container 134.
  • the electrolyzer 140 is preferably powered by energy obtained from renewable sources, such as: solar batteries, wind farms or heat and power plants powered by biomass.
  • renewable sources such as: solar batteries, wind farms or heat and power plants powered by biomass.
  • the system according to the present disclosure may additionally use a power of its own production generated in a steam loop supplied with the heat energy from the process of catalytic oxidation of the syngas produced in the mineralization device 1 10.
  • the electrolyzer may be powered by the energy from the biomass in order to meet particular environmental requirements.
  • the electrolyzer 140 is powered by the surplus energy from the renewable sources, such as solar or wind plants, when the surplus energy cannot be utilized in another, economically justified manner.
  • This solution provides optimal utilization of the surplus energy from renewable sources that cannot be collected and stored in another, environmentally friendly manner. Therefore, the present disclosure utilizes the surplus energy form renewable source for producing ammonium and ammonia compounds, taking into account environmental considerations.
  • the oxygen is used as the gasifying agent in the process of gasification of organic waste. Therefore, the oxygen that enters the reaction chamber of the mineralization device 1 10 is a component of an air stream. In this air stream, nitrogen is present as well. However, the nitrogen contained in the air stream introduced into the reaction chamber of the mineralization device 1 10 constitutes an inert ballast, which does not participate in the reactions that occur during the gasification process. Thus, the nitrogen passes the reaction chamber unchanged and exits the reaction chamber as the inert additive to the syngas generated within the reactor.
  • the syngas which constitutes the product of gasification of organic waste in the mineralization device, comprises: carbon dioxide (CO2), nitrogen (N2), steam (H2O( g )), and it may also comprise hydrogen (H2) or carbon oxide (CO) - depending on the selected parameters of the gasification process.
  • the obtained syngas is subsequently after-combusted, for example with a conventionally utilized after-combusting catalyzer 1 12 which is preferably installed at the syngas outlet of the mineralization device 1 10.
  • the catalyzer 1 12 after-combusts CO to CO2 and H2 to H2O.
  • the catalyzer may comprise various compounds suitable for after-combusting CO and H2, such as for example conventionally utilized catalyzer, e.g. the catalyzer comprising an active layer made of noble metals, such as for example platinum or palladium or their mixtures with different elements.
  • the exhaust gas is the product of the after-combustion process.
  • the exhaust gas comprises: N2, CO2 and H2O.
  • the syngas at the outlet of the mineralization device 1 10 does not comprise molecular oxygen (O2), as the molecular oxygen had been bonded with carbon to form carbon monoxide or carbon dioxide in the gasification process.
  • O2 molecular oxygen
  • the contents of respective syngas components depend on the composition of raw materials (feedstock) introduced into the chamber of the mineralization device 1 10 and the amount of oxygen introduced into the chamber together with the gaseous mixture, i.e. air or oxygen-enriched air.
  • the content of nitrogen in both the syngas and the exhaust gas is constant and unchanged - as compared to the amount of nitrogen introduced into the reaction chamber of the mineralization device together with the stream of the gasifying agent (i.e. air or oxygen-enriched air).
  • the gasifying agent i.e. air or oxygen-enriched air
  • the obtained exhaust gas enters a freezing-up system 121 for condensing and/or freezing up the exhaust gas components having higher solidification temperature.
  • the freezing-up system 121 the following components may be condensed or frozen: steam H Ofg), carbon dioxide.
  • the freezing-up system 121 may be provided with a conventional heat exchanger or a system of heat exchangers suitable for condensing and/or freezing up the steam and carbon dioxide in succession.
  • Steam may be frozen at a temperature not higher than 0°C.
  • Steam may be condensed at a temperature lower than 100°C.
  • the obtained water or ice is subsequently separated from the exhaust gas and collected, whereas the carbon dioxide may be separated from the exhaust gas by freezing up or condensing CO2 (depending on the applied temperature conditions) at a temperature not higher than -56,56°C, and preferably at the temperature of -80°C.
  • the separated carbon dioxide is subsequently collected in a carbon dioxide (CO2) container 133.
  • the cooled gaseous nitrogen constituting the sole non-condensed component of the exhaust gas, is fed into a nitrogen container 132.
  • the freezing-up system 121 may further cooperate with one or several plants which carry out the processes in which cold energy is obtained as the by-product. This solution additionally provides the reduction of the total energy outlay that is necessary to carry out the process for producing the nitrogenous compounds according to the present disclosure.
  • the freezing up process also provides reduction of energy output.
  • the freezing up process may be supplied, as a whole or partially, with the by-product cold energy from various low-temperature processes, thereby reducing the consumption of power, necessary for producing the cold energy, generated by non-renewable energy sources (consequently it reduces the emission of carbon dioxide into the atmosphere).
  • the freezing-up system 121 may cooperate with an LNG (liquid natural gas) regasification plant, wherein the cold energy is generated during the process of boiling and evaporating liquid methane to obtain gaseous methane.
  • LNG liquid natural gas
  • the cold energy which constitutes the by-product of LNG regasification, features adequately low temperature, which is suitable for freezing up of the lower solidifying exhaust gas components, i.e. CO2 and H2O.
  • the cooperating systems: the freezing-up system 121 and the LNG regasification system 120 should be located near each other, i.e. at a distance enabling reduction of losses of the cold energy that is utilized in the freezing up process.
  • the cold energy may be supplied to the freezing-up system 121 , for example, by means of a system of heat exchangers which employs a liquid having a low freezing point, as the cooling medium.
  • the exhaust gas Prior to introduction of the exhaust gas into the freezing-up system 121 , the exhaust gas may be optionally mixed with a different exhaust gas, for example, generated by Submerged Combustion Vaporizers (SVC), i.e. the gas-powered apparatus for regasification of LNG. This provides additional constraint of emission of various flue gases generated by these apparatus, during the regasification of LNG.
  • SVC Submerged Combustion Vaporizers
  • the exhaust gas comprising carbon dioxide may be collected and fed to the exhaust gas transport system by means of a channel 1 1 1 .
  • the exhaust gas generated in the process of catalytic oxidation or the exhaust gas mixed with the other exhaust gases, generated in the processes of LNG regasification, is subjected to condensation or solidification to condense and/or freeze up of the higher solidifying exhaust gas components, i.e.: CO2 and H2O.
  • the obtained condensed water may be subsequently fed to an electrolyzer 140, and the CO2, isolated from the exhaust gas, may be collected in a container 133.
  • the remaining component of the exhaust gas i.e.: gaseous nitrogen, which is a non- condensed exhaust gas component, is collected in a nitrogen container 132. Therefore, the process of condensation and/or solidification provides separation of the nitrogen from the other components of exhaust gas, i.e.: H2O and CO2.
  • the disclosed separation process does not require energy-consuming rectification of the air in order to separate nitrogen (the exhaust gas does not comprise oxygen), and it does not involve complex processes of hydrogen separation from the syngas generated in the processes of organic waste treatment according to the processes known in the art. Therefore, the method according to the present disclosure provides a process which features a reduced expenditure of total energy, thereby providing reduced emission of CO2 into the atmosphere.
  • the present disclosure provides reduction of the amount of energy consumed in the process of separation of respective components of the exhaust gas composition. This is achieved by implementation of the condensation/solidification process carried out by the freezing-up system 121 .
  • This system 121 enables separation of the nitrogen in a one process of condensing and/or freezing up of water and carbon dioxide from the exhaust gas.
  • the disclosed process features reduced apparatus and maintenance costs due to the utilization of a single freezing- up system 121 .
  • the presented method involves separation of nitrogen from the exhaust gas composition (i.e. form the syngas that has been subjected to the catalytic after- combustion process), in a single process.
  • the exhaust gas composition generated according to the present disclosure comprises neither molecular oxygen (O2) nor carbon monoxide (CO), and the exhaust gas components that are separated during condensation and/or solidification process may be utilized in the whole, as a raw material, for the production of the nitrogen compounds, without the need to separate oxygen.
  • the hydrogen for ammonia synthesis, is generated in the electrolysis process and collected in the hydrogen container 134.
  • the method for synthesizing ammonia and other nitrogen compounds may be carried out in various ways.
  • the method for synthesizing ammonia may be carried out in an ammonia synthesis reactor 151 equipped with nitrogen and hydrogen inlets that supply the gases from the respective containers 132 and 134.
  • the hydrogen, generated in the process of water electrolysis, is supplied to the reactor of ammonia synthesis 151 from the hydrogen container 134.
  • the volume or respective gaseous reactants is selected so as to obtain a stoichiometric ratio of N2 and H2 in the ammonia synthesis reaction which is preferably 1 :3 (N2:H2).
  • the nitrogen collected in the nitrogen container 132 features high purity, therefore, the process for synthesizing ammonia from the nitrogen and hydrogen, wherein the latter is obtained in the process of electrolysis of water, may be carried out in a conventional manner, i.e. at the temperature range 380 - 550°C, in the presence of the catalyst, even impurities-sensitive catalyst, such as for instance iron (Fe) comprising catalyst promoters: aluminum oxide (AI2O3), potassium oxide (K2O) and calcium oxide (CaO).
  • impurities-sensitive catalyst such as for instance iron (Fe) comprising catalyst promoters: aluminum oxide (AI2O3), potassium oxide (K2O) and calcium oxide (CaO).
  • the synthesized ammonia may be cooled to a required temperature by the heat exchanger 161 , and then the ammonia may be collected or directly supplied to recipients. Moreover, the obtained ammonia may be utilized as a reactant in various processes, such as for example urea synthesis. Moreover, the heat generated in the process of cooling ammonia may be utilized in different technological processes.
  • a portion of the obtained ammonia may be transferred from the reactor 151 to the urea synthesizing device 153 which may have a form of a conventional reactor provided with a carbon dioxide (CO2) feeding system.
  • the urea synthesis may be carried out in a conventional manner, i.e. with an excess of ammonia, and preferably at a NH3:CO2 ratio of 5:1 , under a pressure form 14 to 42 MPa, at the temperature range of 160-210°C.
  • the obtained urea may be stored in suitable containers, or it may be supplied to recipients, whereas the water constituting the by-product of the urea synthesis may be transferred to the electrolyzer, and therefore utilized as a source of hydrogen and oxygen.
  • the disclosed system may be configured to produce only urea by means of the direct synthesis of the urea from nitrogen, hydrogen and carbon dioxide, according to the known methods.
  • the system may comprise a reactor (an urea synthesizing device) 152 wherein the aforementioned gases are fed as the reactants, and the urea and water are received as the reaction products.
  • ammonia obtained in the process that utilizes the syngas generated in the process for reprocessing the organic waste, may be additionally utilized in various process of synthesis of various nitrogen compounds, such as for example: nitric acid, ammonium nitrate (V), ammonium sulphate (VI) or melamine.
  • various nitrogen compounds such as for example: nitric acid, ammonium nitrate (V), ammonium sulphate (VI) or melamine.
  • the system presented herein provides reduction of carbon dioxide emission into the atmosphere.
  • the reduced emission is achieved by generating the syngas that comprises nitrogen and does not comprise oxygen.
  • the syngas is generated in the mineralization device, in the process involving introduction of nitrogen as an inert to the reaction chamber of the mineralization device. Therefore in the presented process, the low-temperature rectification of the air is not carried out.
  • the nitrogen is separated from the exhaust gas by condensing or/and freezing up the water and carbon dioxide.
  • the implementation of the inlet channel that enables transfer of the exhaust gas composition from the LNG regasification station to the freezing-up system provides improvement in the exhaust gases management, as well as restriction of carbon dioxide emission into the atmosphere.
  • the system according to the present disclosure provides purification of CO2, which may be collected, stored and utilized in the synthesis of urea, or it may be utilized as a reactant in various technological processes.
  • system according to the present disclosure provides enhanced utilization of the energy from renewable energy sources (RES) and well as improved utilization of the cold energy being by-product in various technological processes, such as for example LNG regasification process.
  • RES renewable energy sources

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Processing Of Solid Wastes (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

Système de synthèse de composés azotés à partir de déchets organiques, le système comprenant : un dispositif de minéralisation (110); un catalyseur (112); un système de congélation (121); un électrolyseur (140); et un réacteur de synthèse d'ammoniac (151) pour la synthèse d'ammoniac à partir d'azote et d'hydrogène, le réacteur de synthèse d'ammoniac (151) comprenant une entrée d'azote reliée à un récipient d'azote (132) et une entrée d'hydrogène reliée à un récipient d'hydrogène (134).
PCT/EP2016/081544 2015-12-21 2016-12-16 Procédé de synthèse de composés azotés à partir de déchets organiques et système de synthèse de composés azotés à partir de déchets organiques WO2017108629A2 (fr)

Applications Claiming Priority (2)

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PL415312A PL240266B1 (pl) 2015-12-21 2015-12-21 Sposób wytwarzania amoniaku i mocznika z odpadów organicznych oraz układ do wytwarzania amoniaku i mocznika z odpadów organicznych
PL415312 2015-12-21

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WO2017108629A2 true WO2017108629A2 (fr) 2017-06-29
WO2017108629A3 WO2017108629A3 (fr) 2017-08-03

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108977841A (zh) * 2018-08-30 2018-12-11 中国科学院长春应用化学研究所 一种氮气和二氧化碳气体同步电化学还原合成尿素的方法
CN113860329A (zh) * 2021-10-29 2021-12-31 西安热工研究院有限公司 一种基于合成氨的化学储能系统及方法
LU103016B1 (de) * 2022-09-23 2024-03-25 Thyssenkrupp Ind Solutions Ag Verfahren zur Herstellung von grünem Harnstoff

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