PL240266B1 - Method for producing nitrogen compounds from organic waste and the system for producing nitrogen compounds from organic waste - Google Patents

Description

Description of the invention

The present invention relates to a method for producing ammonia and urea from organic waste and to a system for carrying out the method.

Among the pollutants generated in the combustion processes of solid, liquid and gaseous fuels, there are pollutants with gases such as CO2 or nitrogen oxides at various degrees of oxidation (N2O, NO, N2O3, NO2, N2O5, NO3), generally referred to as NOx. Basically, the aim is to reduce the emission of carbon dioxide (CO2) and nitrogen oxides (NOx) by introducing emission standards regulating the permissible level of emissions of these compounds into the atmosphere, as well as imposing financial penalties in the event of non-compliance with these standards. The most common method of neutralizing nitrogen oxides is their reduction with urea, with the release of carbon dioxide as a by-product, which leads to a reduction in nitrogen oxide emissions, but increases CO2 emissions. In addition, also in the known processes of the synthesis of ammonia and ammonium compounds, significant amounts of CO2 are emitted into the atmosphere, in which, in order to produce molecular hydrogen (H2), which, apart from nitrogen, is a substrate for the synthesis of NH3, considerable amounts of heat and / or electricity are consumed. is typically produced by burning fuels with CO2 emissions to the atmosphere.

Typically, hydrogen for the synthesis of ammonia is obtained from methane or other hydrocarbons in processes involving the evolution of CO and CO2, as well as from synthesis gas, also known as syngas, which is a product of gasification of raw materials such as coal, brown coal or coke.

There are also known methods of obtaining hydrogen for the production of ammonia from synthesis gas from the gasification of waste materials, such as biomass or municipal waste. In this process, hydrogen is typically obtained from synthesis gas containing: H 2, CO and CO 2 by converting CO to CO 2 and subsequent removal of CO 2 by a potassium washing process, yielding a final purified hydrogen containing CO and CO 2 at a concentration below 10 ppm. The purity of hydrogen obtained from syngas is important due to the fact that some pollutants can deactivate the catalysts used in the synthesis of ammonia.

Nitrogen for the synthesis of ammonia is obtained from the air in a physical way: by condensation and rectification.

The patent literature describes methods of producing ammonia from synthesis gas from biomass and air gasification.

From the US patent description US8679439 there is known a method of producing ammonia from biomass, in which the biomass is gasified in the presence of oxygen which is supplied to the gasification process from an air separator. Syngas obtained as a result of the gasification process is successively subjected to catalytic reforming to obtain a gas stream rich in hydrogen (H2) and with a low content of hydrocarbons. The gas obtained is used as a hydrogen source for the production of ammonia, while nitrogen obtained by condensation and rectification from air is used as the nitrogen feed.

The known methods of producing ammonium compounds from syngas from gasification of organic waste such as biomass are therefore two-stage processes involving the separation of hydrogen from the syngas and the supply of nitrogen obtained from the air by condensation and rectification.

Therefore, it would be advisable to develop a method for the synthesis of ammonia and urea from syngas from the processing of organic waste, including biomass, municipal waste or waste plastics, which would ensure the reduction of CO2 emissions to the atmosphere both in the process of hydrogen separation and nitrogen separation, thus enabling improvement process energy efficiency.

The subject of the invention is a system for the production of ammonia and urea from organic waste, containing a mineralizer for gasification of organic waste to produce syngas containing: nitrogen (N2), carbon monoxide (CO), carbon dioxide (CO2), hydrogen (H2) and water vapor ( H2O (g)), the mineralizer comprising supplying oxygen-enriched air as a gasifying agent to the reaction chamber of the mineralizer. The system is characterized by the fact that it also includes: a catalyst at the output of syngas from the mineralizer for the catalytic combustion of the syngas components: carbon monoxide (CO) to carbon dioxide (CO2) and hydrogen (H2) to water (H2O) to produce exhaust gases containing: nitrogen (N2) ), carbon dioxide and water; a freezing system with flue gas supply from the catalyst for condensation and / or freezing of water and carbon dioxide from the flue gas and nitrogen gas (N2) separation, connected with nitrogen and carbon dioxide tanks; electrolyser for electrolysis

Water with oxygen evolution for enrichment of air for gasification of organic waste in a mineralizer and hydrogen evolution for the synthesis of ammonia for collection in the hydrogen tank; and a reactor for the synthesis of ammonia from nitrogen separated from the flue gas in the freezing system and hydrogen from the electrolysis of water in the electrolyser with nitrogen supply from the nitrogen tank and hydrogen supply from the hydrogen tank, the system also includes at least one of the following urea synthesizers: urea synthesizer for synthesis urea from ammonia and carbon dioxide with an ammonia feed from the ammonia synthesis reactor and a carbon dioxide feed from the carbon dioxide reservoir; urea synthesizer for urea synthesis from carbon dioxide, nitrogen and hydrogen with supply of carbon dioxide from the carbon dioxide tank, supply of nitrogen from the nitrogen tank and supply of hydrogen from the hydrogen tank.

The subject of the invention is also a method of producing ammonia and urea from organic waste, characterized by the fact that in a system containing: a mineralizer for gasifying organic waste to produce syngas containing: nitrogen (N2), carbon monoxide (CO), carbon dioxide (CO2), hydrogen (H 2) and water vapor (H 2 O (g)), with oxygen-enriched air supplied as the gasifying agent to the reaction chamber of the mineralizer; a catalyst at the syngas outlet from a mineralizer to catalytically burn off the syngas components: carbon monoxide (CO) to carbon dioxide (CO2) and hydrogen (H2) to water (H2O) to produce flue gases containing nitrogen (N2), carbon dioxide and water; freezing system with flue gas supply from the catalyst for condensation and / or freezing of water and carbon dioxide from the flue gas and separation of gaseous nitrogen (N2); electrolyser for the electrolysis of water with oxygen evolution for enriching air for gasification of organic waste in the mineralizer and hydrogen separation for collection in the hydrogen tank for ammonia synthesis; and a reactor for the synthesis of ammonia from nitrogen separated from the flue gas in the freezing system and hydrogen from the electrolysis of water in the electrolyser with the supply of nitrogen from the nitrogen tank and the supply of hydrogen from the hydrogen tank; this process involves the gasification of organic waste with oxygen-enriched air, where nitrogen (N2) from the air is an inert gas in the gasification process, and the electrolysis of water into oxygen (O2) and hydrogen (H2) is carried out in the electrolyser, wherein oxygen from the electrolysis is enriched in the air for gasification, and hydrogen (H2) from the electrolysis of water is collected in the hydrogen tank; and producing syngas in the mineralizer containing: nitrogen (N2), carbon monoxide (CO), carbon dioxide, hydrogen (H2) and steam with water (H2O (g)); then the syngas is catalytically burned on the catalyst to obtain exhaust gas containing nitrogen (N2), carbon dioxide and water; then, in the freezing process, water and carbon dioxide are separated from the flue gas and nitrogen gas is separated; wherein the separated components of the exhaust gas are collected in separate tanks: nitrogen and carbon dioxide; and ammonia synthesis is carried out in an ammonia synthesis reactor with the use of nitrogen stored in the nitrogen reservoir and hydrogen from the electrolysis of water collected in the hydrogen reservoir, furthermore, urea synthesis is carried out in at least one of the following urea synthesizers: in a urea synthesizer for urea synthesis from ammonia and carbon dioxide with the supply of ammonia from the ammonia synthesis reactor and the supply of carbon dioxide from the carbon dioxide tank, where urea synthesis is carried out with the use of ammonia obtained in the ammonia synthesis process in the reactor and carbon dioxide accumulated in the carbon dioxide tank; in urea synthesizer for urea synthesis from carbon dioxide, nitrogen and hydrogen with supply of carbon dioxide from the carbon dioxide tank, supply of nitrogen from the nitrogen tank and supply of hydrogen from the hydrogen tank, in which urea synthesis is carried out with the use of nitrogen stored in the nitrogen tank, carbon dioxide the carbon dioxide collected in the tank and the hydrogen stored in the hydrogen tank.

The subject of the invention is presented in an embodiment in the drawing in which: Fig. 1 schematically shows a plant for the synthesis of ammonia and urea from organic waste; Fig. 2 shows an exemplary diagram of a mineralizer for mineralization (gasification) of waste materials: biomass, municipal waste, plastic waste.

The system for the synthesis of ammonium compounds from organic waste, shown schematically in Fig. 1, can work continuously or periodically, depending on the needs, on the current raw material balances, i.e. the amount of available raw materials, as well as the possibility of collecting the manufactured products: ammonia and ammonium compounds, such as for example urea.

The system for the synthesis of ammonium compounds includes a mineralizer 110 for the production of synthesis gas (syngas) in the gasification of organic waste, such as municipal waste, plastic waste or biomass - for example, biomass of agricultural origin, in the presence of

Gasification agent. As schematically shown in Fig. 1, organic waste constituting the input in the mineralization process may contain: silica: (SO2), hydrocarbons: aromatic, aliphatic, alicyclic, branched, saturated or unsaturated (CnHm), biomass: for example n (C6Hi2Oe) cellulosic materials and water. The system uses a mineralizer 110 for the mineralization of coal fuel with a structure similar to the mineralizer described in the Polish patent application P.405601, while the construction of the chamber of such a mineralizer is shown schematically in Fig. 2. The mineralizer 110 for the production of synthesis gas from organic waste has a substantially horizontal form rotating pipe constituting the mineralizer chamber 210 with arranged inside fixed and / or adjustable elements 212, 213, 214 for pouring the batch material during the rotation of the pipe 210. The mineralizer 110 conducts a continuous process of mineralization (gasification) of the charge (organic waste) supplied to the mineralizer chamber 210 to produce gaseous combustion products - syngas - according to the process described in the application P.405601. The mineralizer 110 comprises nozzles for supplying a gasifying agent into the chamber 210, for example in the form of one or more flow-regulated inlet ports. According to the invention, air or oxygen-enriched air is used as the gasifying agent.

The supply of nitrogen with the gasifying agent to the mineralizer 110 does not require additional technological operations and energy expenditure, because nitrogen is taken together with the air, and the share of nitrogen in the gasifying agent is regulated by the amount of oxygen enriching the air.

In order to increase the efficiency of the reactions involving the mineralization process (gasification) taking place during the mineralization, the air introduced as the gasifying agent can be enriched with oxygen, the higher the proportion of oxygen in the gasifying agent, the higher the gasification efficiency.

Oxygen enriching the air is obtained from the electrolysis of water into hydrogen and oxygen, which is carried out by means of an electrolyser 140 cooperating with a system for the synthesis of nitrogen compounds.

Various conventional systems for electrolysis of water may be used as the electrolyser 140. Oxygen obtained during electrolysis, which is a gasifying agent in the mineralization process, can be supplied directly to the oxygen supply system to the mineralizer chamber 110, where oxygen is mixed with air in appropriate proportions, or the excess oxygen can be collected in the oxygen tank and used depending on the needs process. Hydrogen from the water electrolysis process, on the other hand, can be stored in the hydrogen tank 134.

The electrolyser 140 is powered by electricity, preferably electricity from renewable sources, for example produced by solar cells or wind farms, or in biomass-fired CHP plants. It should be noted that the installation in question can also use electricity of its own production, produced in the steam cycle heated with heat from the catalytic oxidation of 112 syngas produced in the mineralizer 110. Moreover, if it is important to meet certain legal requirements related to ecology, then during electrolysis powered by its own The mineralizer can be powered with electricity from biomass. Most preferably, the electrolyser 140 is powered under conditions of excess electricity production by solar or wind installations, which surpluses cannot be utilized in any other conventional economically viable manner. Such a solution enables the optimal use of surplus electricity from renewable sources for the production of ammonia and ammonium compounds for environmental reasons.

Thus, in the process according to the invention, the gasifying agent in the organic waste mineralization process is oxygen, which is introduced into the mineralizer chamber 110 as a mixture with air. Nitrogen contained in the gas mixture is inert: ballast, which does not participate in the reactions taking place during gasification in the mineralizer and leaves the mineralizer 110 unchanged through the outlet as an addition to the synthesis gas. Synthesis gas, which is a product of gasification of organic waste, obtained in the process contains: carbon dioxide (CO2), nitrogen (N2), water vapor (H2O (g)) and may contain hydrogen (H2) or carbon monoxide (CO) - depending on the selection of parameters gasification process.

The synthesis gas produced is subsequently burned up, for example with a conventional burn-up catalyst 112, preferably installed at the syngas outlet of the mineralizer 110. The catalyst 112 burns CO to CO2 and H2 to H2O. Various conventional post-combustion catalysts 112 may be used to post-burn the syngas, for example catalysts in which the active layer is noble metals such as platinum, palladium or mixtures thereof with other elements.

PL 240 266 B1

Afterburning at the outlet of the catalyst 112 produces exhaust gas containing N2, CO2 and H2O. The synthesis gas exiting the mineralizer 110 also does not contain molecular oxygen which has been bound to the carbon in the gasification process to form carbon monoxide or dioxide. The shares of the individual syngas components depend on the composition of the raw materials introduced into the mineralizer 110 or the amount of oxygen supplied. On the other hand, the amount of nitrogen in the syngas as well as in the exhaust gases, which are a product of the syngas afterburning, is equal to the amount of nitrogen introduced into the mineralizer chamber.

After burning the syngas on the catalyst 112, the flue gas is successively fed to the condensation and freezing system 121 cooperating with the mineralizer 110 in order to freeze and / or condense the higher solidifying components of the exhaust gas - i.e. condensation or freezing of water vapor H2O (g) and the freezing or condensation of carbon dioxide. For example, the freezing system 121 may be equipped with a conventional heat exchanger or a system of heat exchangers adapted to freeze and / or condense water and carbon dioxide sequentially. Water is frozen at a temperature of at most 0 ° C or water is condensed at a temperature below 100 ° C and ice or drops are separated from the gas mixture, while carbon dioxide is released - by freezing or condensation (depending on the temperature used) from gas mixture at a temperature of at most -56.56 ° C, and preferably -80 ° C, and the evolved carbon dioxide is collected in the carbon dioxide tank 133. After the freezing process, cooled pure nitrogen is obtained, which is collected in the nitrogen tank 132 .

The freezing system 121 can cooperate with one or more installations implementing processes in which "cold" is a waste product, which additionally reduces the energy expenditure of the process of producing nitrogen compounds and reduces CO2 emissions to the atmosphere, due to the lack of need or a limited need to use electricity or heat. for the separation of exhaust gas components. Advantageously, the freezing system 121 can cooperate with an LNG regasification plant, where "cold" is generated during the boiling and evaporation of the liquid methane to gaseous form. In addition, "cold", which is a waste product of LNG regasification, is characterized by an appropriately low temperature, favorable for the separation of the lower-solidifying components of the exhaust gas from the syngas (to CO2 and H2O) in the freezing process.

Preferably cooperating systems: freezing 121 components of the syngas exhaust gas and regasification of LNG 120 should be located at a distance that will ensure the reduction of losses during the "cold" transmission - used as a cooling factor in the freezing process. "Cold" can be delivered to the freezing system 121, for example, by a system of heat exchangers and antifreeze circulating therebetween.

The flue gas (syngas components) before being introduced into the freezing system 121 can be additionally enriched with other fumes, for example from SCV regasifiers (Submerged Combustion Vaporizers), i.e. gas-fired LNG regasification devices, which provides an additional reduction of exhaust emissions generated by these equipment during LNG regasification. The exhaust gas containing carbon dioxide may be collected and supplied via the conduit 111 to the exhaust gas transport system.

The exhaust gases produced by catalytic oxidation of syngas 112 or exhaust gases enriched with other exhaust gases - coming from LNG regasification, are separated in the freezing system 121 by separation, i.e. condensation and / or freezing of higher solidifying exhaust gas components - i.e. CO2 and H2O, while the separated water can be used to power the electrolyser 140, while the carbon dioxide is collected in the tank 133. The remaining components of the exhaust gas that have not been frozen as a result of the temperature reduction, i.e. nitrogen, are collected in the nitrogen tank 132.

Thus, the applied process enables nitrogen separation in the process of H2O and CO2 separation that does not require energy-consuming rectification of both air - to separate nitrogen and to separate hydrogen - as used in the so far known processes involving the production of ammonium compounds from syngas obtained from organic waste, which ensures reducing the energy consumption necessary to carry out these operations, and therefore reducing CO2 emissions to the atmosphere.

Thus, the solution according to the invention reduces the energy consumption necessary for the separation of individual components of the gas mixture (exhaust gas), since nitrogen extraction is carried out in a single separation process (condensation and / or freezing) of higher solidifying components from the exhaust gas (water and carbon dioxide). In addition, the solution according to the invention provides a reduction in equipment and machine maintenance costs due to the use of a single freezing system 121.

PL 240 266 B1

The solution involves the release of nitrogen from the flue gas (i.e. syngas subjected to a catalytic afterburning process) in a single process, which is carried out in the case of nitrogen removal from the air. The exhaust gases produced according to the invention do not contain molecular oxygen or carbon monoxide, and the components of the exhaust gases separated in the condensation and / or freezing process can be fully used for the production of nitrogen compounds, without the need to incur additional energy costs related to the need to separate oxygen.

Furthermore, due to the presence of the electrolyser 140 in the system 140, the hydrogen for the production of ammonia is obtained from the electrolysis of water, which is stored in the hydrogen tank 134.

The production process of ammonia and other nitrogen compounds can be carried out with the use of various techniques. For example, the ammonia production process may be run in an ammonia synthesis reactor 151 with nitrogen and hydrogen supplied from vessels 132 and 134, respectively. The hydrogen produced by the electrolysis of water is supplied to the ammonia synthesis reactor 151 from the hydrogen vessel 134, preferably in the amount necessary to run the process. ammonia synthesis from nitrogen and hydrogen. The hydrogen is fed from the vessel 134 to the reactor 151 in an amount sufficient to obtain a stoichiometric composition of the N2 and H2 gases in the reactor chamber 151, i.e. preferably a N2: H2 molar ratio of 1: 3.

The nitrogen accumulated in the nitrogen tank 132 is characterized by high purity, therefore the process of synthesizing ammonia from nitrogen and hydrogen obtained from the electrolysis process can be carried out in a conventional way with the use of catalysts, even catalysts sensitive to contamination, such as, for example, iron (Fe) containing promoters: aluminum oxide (Al2O3), potassium oxide (K2O) and calcium oxide (CaO), at a temperature range: 380-550 ° C.

The ammonia produced can be successively cooled down to a suitable temperature by means of a heat exchanger 161 and stored or delivered directly to consumers. In addition, the ammonia produced can be used for the synthesis of other ammonium compounds, for example urea. The heat given off in the ammonia cooling process, on the other hand, can be supplied to other technological processes.

For urea synthesis, some or all of the ammonia produced may be routed from reactor 151 to urea synthesizer 153 in the form of a conventional reactor fed with ammonia and carbon dioxide (CO2). The urea synthesis process can be carried out in a conventional way with an excess of ammonia: NH3: CO2 preferably 5: 1, under a pressure of 14 to 42 MPa, in a temperature range: 160-210 ° C. The produced urea can be stored in appropriate tanks or directed to recipients. Water, which is a by-product of the urea synthesis process, can be directed to the electrolyser and used as a source of oxygen and hydrogen.

If market conditions do not allow for a financially effective sale of ammonia, the plant in question can only produce urea by direct synthesis from nitrogen, hydrogen and carbon dioxide, for example according to the method described in the patent description PL200856. For this purpose, it has a reactor (urea synthesizer) 152 to which the said gases are fed and urea and water are discharged.

In addition, ammonia produced from the synthesis gas from the treatment of organic waste can also be used for the synthesis of other ammonium compounds such as nitric acid, ammonium nitrate, ammonium sulphate or melamine.

An unquestionable advantage of the synthesis system according to the invention is the reduction of carbon dioxide emissions to the atmosphere, which was achieved by producing a synthesis gas containing nitrogen, and oxygen-free - by introducing nitrogen into the mineralizer chamber as an inert gas ensuring the elimination of low-temperature rectification processes - according to the invention, nitrogen is released from the gas mixture by condensation and / or freezing of water and carbon dioxide.

Also, the use of "cold" from LNG regasification as a power supply to the liquefaction and freezing system made it possible to additionally reduce energy expenditure related to the freezing process, while ensuring the utilization of "cold", which is a by-product of LNG regasification.

In addition, the use of the flue gas from the regasification process of liquefied natural gas (LNG) to the freezing system in the duct system ensured the management of fumes from the LNG regasification process, reducing the emission of carbon dioxide to the atmosphere.

PL 240 266 B1

The system according to the invention also provides for the separation and collection of CO2, which is stored and can be used for the production of urea, or can also be used as a substrate in other technological processes.

The system according to the invention also allows the use of energy from renewable energy sources (Renewable Energy Sources) as well as waste cold - a by-product of other technological processes, such as LNG regasification.

List of markings:

110 - mineralizer

111 - channel

112 - catalyst

120 - regasification system

121 - freezing system

132 - nitrogen tank

133 - carbon dioxide tank

134 - hydrogen tank

140 - electrolyser

151 - a reactor for the synthesis of ammonia

152, 153 - urea synthesizers

161 - heat exchanger

210 - mineralizer chamber

212, 213, 214 - elements for pouring the mineralizer charge material

Claims (2)

1. System for the production of ammonia and urea from organic waste, containing a mineralizer for gasification of organic waste to produce syngas containing: nitrogen (N2), carbon monoxide (CO), carbon dioxide (CO2), hydrogen (H2) and water vapor (H2O) (g)), wherein the mineralizer comprises supplying oxygen-enriched air as a gasifying agent to the reaction chamber of the mineralizer, characterized in that the system further comprises: - a catalyst (112) at the output of syngas from the mineralizer (110) for catalytic combustion of the syngas components: carbon monoxide (CO) to carbon dioxide (CO2) and hydrogen (H2) to water (H2O) to produce exhaust gases containing: nitrogen (N2), carbon dioxide (CO2), and water (H2O); - a freezing system (121) with exhaust gas supply from the catalyst (112) for condensation and / or freezing of water (H2O) and carbon dioxide (CO2) from the exhaust gas and nitrogen gas (N2) separation, connected with nitrogen (132) and dioxide tanks carbon (133); - an electrolyser (140) for electrolysis of water with oxygen evolution for enriching air for gasification of organic waste in a mineralizer (110) and separation of hydrogen for collection in a hydrogen tank (134) for ammonia synthesis; and - a reactor (151) for the synthesis of ammonia from nitrogen separated from the flue gas in the freezing system (121) and hydrogen from the electrolysis of water in the electrolyser (140), with nitrogen supply from the nitrogen tank (132) and hydrogen supply from the hydrogen tank (134), where the system further comprises at least one of the following urea synthesizers (152, 153): - a urea synthesizer (153) for the synthesis of urea from ammonia and carbon dioxide with an ammonia feed from an ammonia synthesis reactor (151) and a carbon dioxide feed from a carbon dioxide reservoir (133); - a urea synthesizer (152) for synthesizing urea from carbon dioxide, nitrogen and hydrogen with a carbon dioxide supply from a carbon dioxide reservoir (133), a nitrogen supply from a nitrogen reservoir (132), and a hydrogen supply from a hydrogen reservoir (134). 2. A method for producing ammonia and urea from organic waste, characterized in that - in a system containing: PL 240 266 B1 - mineralizer (110) for gasification of organic waste to produce syngas containing: nitrogen (N2), carbon monoxide (CO), carbon dioxide (CO2), hydrogen (H2) and water vapor (H2O (g)), with air supply an oxygen-enriched gasification agent to the reaction chamber (210) of the mineralizer (110); - catalyst (112) at the output of syngas from the mineralizer (110) for catalytic combustion of the syngas components: carbon monoxide (CO) to carbon dioxide (CO2) and hydrogen (H2) to water (H2O) to produce flue gases containing nitrogen (N2), dioxide carbon (CO2) and water (H2O); - a freezing system (121) with exhaust gas supply from the catalyst (112) for the condensation and / or freezing of water (H2O) and carbon dioxide (CO2) from the exhaust gas and nitrogen gas (N2) separation; - an electrolyser (140) for electrolysis of water with oxygen evolution for enriching air for gasification of organic waste in a mineralizer (110) and separation of hydrogen for collection in a hydrogen tank (134) for ammonia synthesis; and - a reactor (151) for the synthesis of ammonia from nitrogen separated from the flue gas in a freezing system (121) and hydrogen from electrolysis of water in an electrolyser (140) with a nitrogen supply from a nitrogen reservoir (132) and a hydrogen supply from a hydrogen reservoir (134); where in this method: - in the mineralizer (110), the organic waste gasification process is carried out with oxygen-enriched air, with nitrogen (N2) from the air being an inert gas in the gasification process, - where the electrolysis of water into oxygen (O2) and hydrogen (H2) is carried out in the electrolysis, where the oxygen (O2) from the electrolysis enriches the air for gasification, and the hydrogen (H2) from the electrolysis of water is collected in the hydrogen tank (134) ; - and producing in the mineralizer (110) syngas containing: nitrogen (N2), carbon monoxide (CO), carbon dioxide (CO2), hydrogen (H2) and steam with water (H2O (g)); the syngas is then catalytically burned on a catalyst (112) to obtain exhaust gas containing nitrogen (N2), carbon dioxide (CO2) and water (H2O); - then, in the freezing process, water and carbon dioxide are separated from the flue gas and nitrogen gas (N2) is separated; - wherein the separated exhaust gas components are collected in separate tanks: nitrogen (132) and carbon dioxide (133); - ammonia synthesis is carried out in the ammonia synthesis reactor (151) with the use of nitrogen separated from the flue gas and accumulated in the nitrogen tank (132) and hydrogen from the electrolysis of water collected in the hydrogen tank (134), - furthermore, urea synthesis is carried out in at least one of the following urea synthesizers (152, 153): - in the urea synthesizer (153) for urea synthesis from ammonia and carbon dioxide with ammonia supply from the ammonia synthesis reactor (151) and carbon dioxide supply from the carbon dioxide tank (133), in which urea synthesis is carried out with the use of ammonia obtained in the process synthesizing ammonia in the reactor (151) and carbon dioxide stored in the carbon dioxide reservoir (133); - in a urea synthesizer (152) for the synthesis of urea from carbon dioxide, nitrogen and hydrogen with the supply of carbon dioxide from the carbon dioxide reservoir (133), the supply of nitrogen from the nitrogen reservoir (132) and the supply of hydrogen from the hydrogen reservoir (134) in which it is conducted urea is synthesized with the use of nitrogen stored in the nitrogen tank (132), carbon dioxide collected in the carbon dioxide tank (133) and hydrogen stored in the hydrogen tank (134).