PL245093B1 - Duo hydrothermal method of processing biomass substrates and system for its implementation - Google Patents

Abstract

The subject of the invention is a duo-hydrothermal method of transforming biomass substrates into liquid products that are used as motor fuels or components of fuels or electricity and heat. The invention also concerns a duo-hydrothermal biomass processing system, which is used in the fuel industry, energy industry and waste treatment. The duo hydrothermal biomass processing system includes a technological node (1) in the form of a two-pipe reactor (12) with pipes placed concentrically with water in its subcritical state, which supplies thermal energy to the substrates through thermal radiation, and a technological node (2) in the form of a cyclone reactor ( 13) with water in a supercritical state, supplying energy to the chemical compounds and metals contained therein both by thermal radiation and microwave radiation, gas purification unit (3) with water scrubbers (16), power generator (4) with an internal combustion engine ( 19) and an electrical energy generator (20), an exhaust gas treatment node (5) containing both three-way catalytic reactors (23), ceramic filters (22) and electromagnetic filters (21), as well as heat exchangers (24), an organic Rankine cycle node a ORC (6) containing a system for converting thermal energy into electricity, a water purification node (7) containing a complex of devices (31-35) for mechanical and chemical purification, a vitrification node (8) containing a microwave reactor (36) and an air purification node (9) containing mechanical filters; ceramic (29) and non-woven (30) and electromagnetic (28).

Description

Description of the invention

The subject of the invention is a method of transforming biomass substrates into liquid products that are used as motor fuels or components of fuels or electricity and heat. The invention also relates to a biomass processing system that is used in the fuel industry, energy industry and waste transformation, in which biomass found in a field of radiation, especially thermal and/or microwave radiation, is transformed using water in its sub- and supercritical state, and derived from biomass solid products are disposed of by microwave vitrification.

The substrates are biomass, including waste contained in plants, municipal waste, sewage sludge, etc.

The energy of flammable products generated during transformation is partially used for the installation's own needs to implement the duo hydrothermal technology in question, so that the installation can be energy autonomous.

The method by design is particularly useful for converting wet biomass.

Given the threat to the world resulting from excessive CO2 emissions, i.e. emissions that cannot be fully used in the CO2 cycle in nature, there is an urgent need to balance them, and this means the need to use only renewable resources for energy purposes.

These resources include, among others: biomass in its various forms and forms, including as a component of municipal waste and sewage sludge.

There are many ways to liquefy biomass and transform it into energy carriers such as flammable gases or flammable liquids. These methods differ in the complexity of the process, installation costs and the scale of implementation (laboratory, pilot, demonstration, industrial). In these methods, heat is most often used to convert substrates into forms with higher energy density.

In current practice and operating technological installations, the above-mentioned substrates are either directly burned or pre-thermally transformed in high-temperature tarification or pyrolysis processes. Biological methods of transforming substrates in biogasification processes (composting or accelerated fermentation) are also known. The disadvantage of these processes is low energy efficiency and the creation of problematic products, most often waste. Low energy efficiency results from the fact that the substrates must achieve a very low moisture content before being introduced into the processes. Drying them is very energy-consuming. In biological processes in which wet biomass is transformed, only a small part (less than 20% m/m) of the substrates is converted into gases. The formation of problematic products also results from the fact that the above-mentioned substrates, as fuels, are not cleaned before combustion, especially chemically. Therefore, in the combustion process they are dirty fuel. The exhaust gases resulting from this combustion contain a number of toxic components that are difficult to separate and dispose of.

Residues from combustion processes, i.e. slags and ashes, are also problematic. These residues are difficult to manage and are most often landfilled - with all its negative consequences.

The remains of biotransformation processes are also questionable. For example, in biogas plants, such residue constitutes over 80% of the input. This residue is treated as fertilizer, but as it turns out, the environment can only absorb a limited amount of it.

Tarification or pyrolysis processes are more favorable than direct combustion. These processes are also relatively energy inefficient. This is due to the fact that the substrates used in the above-mentioned processes must be practically moisture-free, but also to the fact that thermal energy for torrefaction or pyrolysis of biomass is provided, in existing technological solutions, both by (thermal) radiation and in through conduction and transport. However, it is known that biomass conducts heat poorly, so providing energy in the above-mentioned way means a long process implementation time and high energy losses. A problematic product of the torrefaction and pyrolysis process is the carbon produced in this process in the form of coke breeze. It occurs as a result of locally too high temperatures (in the absence of air). This carbon absorbs, especially heavy metals contained in the substrates. Therefore, it is not possible to burn it directly, and its disposal in other processes is difficult and energy-intensive. Of course, post-process ash residues are also problematic. Those used for combustion are most often stored.

Many forms of substrates are characterized by very high moisture content (up to 60-80%). This makes them difficult to store and transport, as well as to transform.

Therefore, the disadvantage is that wet substrates (biomass, waste and sludge), in order to be the substrate of many currently developed technologies, e.g. pyrolysis, require preliminary preparation by drying, which is complicated and generates additional energy, ecological and economic costs.

One of the processes of thermal conversion of biomass that uses input that does not require preliminary drying is the so-called hydrothermal liquefaction of wet biomass.

This process generally takes place at a temperature of 280-370°C and a pressure of 10-25 MPa. These are subcritical conditions, i.e. close to the critical conditions (existence) of water in liquid form, i.e. critical temperature Tk = 374.2°C = 647.35 K and critical pressure pk = 22.1 MPa = 22,131,360 Pa.

It is important that at temperatures higher than the critical value, water does not exist in liquid form regardless of the pressure value. However, it exists as a gas, i.e. it is water vapor. At a temperature of approximately 3000°C, water (water vapor) undergoes thermal decomposition into oxygen and hydrogen.

Water in subcritical conditions has properties intermediate between a liquid and a gas. Under these conditions, e.g. biomass, undergoes depolymerization. The main depolymerization products are (bio)gases, bio-oil, biochar (coke), water-soluble compounds and minerals. The formation of biochar (coke breeze) is unfavorable in the process. However, they can be limited, among others: by introducing alkaline catalysts.

The process is carried out in classic reactors (usually boilers) heated externally (jacket). These reactors are characterized by a large capacity and, at the same time, a relatively small volume of heat supplied to the substrates via thermal radiation. Since the thermal radiation zone covers a relatively small volume near the reactor wall, it also means that heat, through radiation (absorbed by biomass), is delivered to a small percentage of the volume of substrates. Since the thermal conductivity of the substrates is relatively low, this means that a larger amount of the supplied heat is absorbed by the biomass by convection and rising, i.e. very slowly and with large losses, which in turn means the need to carry out the process for a long time, during which excessive coking occurs. substrates. These are inconveniences.

Due to the difficult conditions of the depolymerization process in water with subcritical parameters, its use in industry is limited. This process is still in the research phase and in most cases it is carried out on a laboratory scale. However, there are several technologies on a pilot or demonstration scale in which the process is implemented.

An example is the HTU (hydrothermal upgrading) method. Work on it was carried out by Shell laboratories in Amsterdam in the 1980s. In 2004, a pilot installation was launched in Apeldoorn in the Netherlands. In this technology, the wet feed material is depolymerized in water with subcritical parameters. The depolymerization time is 5-20 minutes. As a result, approximately 45% (in relation to the input) of bio-oil is obtained, which can be further processed, e.g. deoxidation and hydrogenation in the presence of a catalyst, cracking and distillation to a fraction similar in composition to gasoline, kerosene and diesel oil.

A separate achievement is the method of CWT (Changing World Technology), in which the biomass transformation process takes place in subcritical water conditions.

The installation consists of several technological nodes, which can be described as follows: First, there is the grinding node, where the charge is ground to such a degree of grinding that, after mixing with water, it can be pumped with standard pumps for pumping dirty liquids. This is an inconvenience, not only in terms of energy but also technologically, because grinding contaminated substrates is associated with accelerated wear of the grinding elements and the need for their frequent replacement, which in turn causes downtime of the installation. The feed mixed with water is pumped to the first reactor, which is under high pressure (above 20 MPa) at a relatively low temperature (approx. 300°C). Particles of materials such as plastics, organic waste and others are dispersed into smaller ones. In the next reactor, the pressure is suddenly lowered, and in these conditions most of the water evaporates (with less energy required than during heating). The steam is recycled and heats the reactor. Solids settle and are then separated. In the next stage, the dirty liquid from the previous reactor, which is similar to crude oil, evaporates in two reactors at a higher temperature (approx. 500°C). The particles of this mixture break down into even smaller elements and, together with the vapors from the previous reactor, enter the distillation towers, where they condense depending on their specific gravity. In this way, carbon, water, heavier oil, lighter oil and, on top, gas are extracted. Individual fractions are transferred to appropriate tanks. CWT technology, in its essence, only involves the process of transforming biomass in subcritical water conditions. The disadvantage of this type of process is that the transformation is too energy-intensive, and at the same time not all the substrates are transformed in such a way that the process residues are not burdensome to the environment, in particular there is the phenomenon of transforming "waste into waste".

From the Ukrainian patent description No. UA81562 U, a method of hydrothermal processing of renewable biomass, organic agricultural waste, wood and chemical industry waste, waste of public utility facilities, divot, substandard coal for the production of hydrogen, methane and syngas containing H+CO or H+ is known CO +CO, which involves the gasification of aqueous suspensions of hydrocarbon compounds in the presence of a catalyst based on activated carbon from coconut shells to produce H, CO, CO, CH and C-Cat carbohydrates in supercritical conditions of water at a temperature of 500- and a pressure of 34.5 MPa. A 20% aqueous suspension of molasses with a mass flow of 1.5 g/g of catalyst is processed on an industrial aluminum-copper-zinc catalyst of the CHM-U type with similar efficiency in relation to hydrogen under conditions of temperature reduced to 200°C and pressure reduced to 24 .0 MPa.

Chinese patent No. CN103386411 B discloses a method for hydrothermal processing of biomass waste and its system. The method includes the following stages: the material is successively treated by preheating the suspension, hydrothermal treatment with high-pressure steam and treatment by flash evaporation. The steam used in the hydrothermal process includes raw steam and secondary steam. According to the secondary steam, with the steam pressure difference between the hydrothermal reaction equipment, the equalization of the steam pressure and temperature of the two hydrothermal reaction equipment is completed. By multi-level pressure equalization between hydrothermal reaction devices, the efficiency of heat transfer is improved and the consumption of raw steam can be reduced.

A method of hydrothermal liquefaction of biomass is known from the Polish patent application No. P. 399911 A1, in which the biomass taken from the tank is pumped into the reactor, where the biomass is heated in order to obtain reactor products in the form of volatile, liquid and solid fractions, which separates in the separator. The biomass taken from the tank is compressed in pumps to a pressure ranging from 220 atm. up to 250 atm, then the compressed biomass is preheated in a heat exchanger to a temperature of at least 374-400°C with the thermal energy of the hot reactor products, and then the preheated biomass is heated in the reactor using microwave radiation emitted from the generators with a frequency in the band from 900 MHz to 4 GHz through polarized wave radiators placed along the reactor chamber, the polarization directions of which are perpendicular to the adjacent radiators, and the width of the radiator slot is smaller than half the wavelength of the radiation emitted from the generators, and the reflections of the electromagnetic wave fed to the radiators are measured using reflectometers placed between the radiators and the generators, and the temperature of the biomass inside the reactor is measured using temperature sensors and using the controller; based on the readings of the temperature sensors and reflectometers, the power of radiation generated by the generators is regulated, maintaining the biomass inside the reactor at a temperature ranging from 374° C to 400°C.

US Patent No. 10,689,282 B2 describes a process based on hydrothermal liquefaction (HTL) treatment for the co-processing of high-water sewage sludge and other lignocellulosic biomass for the co-production of biogas and bio-crude oil. A mixture of waste activated sludge and lignocellulosic biomass such as birch sawdust/corn stalk/MSW was converted under HTL conditions in the presence of KOH as a homogeneous catalyst. Operating conditions, including reaction temperature, reaction time and solids concentration, were optimized based on the reaction surface methodology for maximum biocrude oil production. The highest yield of biocrude oil is approximately 34% by weight. was obtained by co-feeding waste activated sludge with lignocellulosic biomass at the optimal temperature of 310°C, reaction time of 10 min and solids concentration of 10% by weight. Two by-products of this process (biochar and water-soluble products) can also be used to produce energy. Water-soluble products were used to produce biogas under the Biomethane Potential (BMP) test. Over the days, they were found to have produced a total of approximately 800 ml of biomethane per 0.816 g of total organic carbon (TOC) or 2.09 g of chemical oxygen demand (COD) of water-soluble products.

The aim of the invention was therefore to develop a new method for processing biomass substrates and a system for its implementation, which would solve the disadvantages described above.

It was decided to ensure that all biomass was liquefied (to a mixture of gases, including synthesis gas and light liquid vapors) in a field of thermal and/or microwave radiation, using water in its sub- and supercritical state, where it may locally undergo thermal dissociation , while the post-process mineral fraction is partially transformed in the microwave vitrification process into the ceramic and metallic phase.

The method of transforming biomass substrates according to the invention includes the following steps:

a) two-stage compression of biomass substrates, with the first stage taking place in a piston press, the second stage taking place in a screw press along with low-temperature heating of the biomass at 90°C,

b) injecting the substrates into the inter-pipe space of the technological node, in the form of a two-pipe reactor with concentrically placed pipes, and mixing the biomass with water in its subcritical state, at a temperature of 350-370°C and a pressure greater than 20 MPa, as a result of which two streams of substrates are created, i.e. . flammable phase and solid phase,

c) the flammable and solid phase are directed to the next technological node, in the form of a cyclone reactor with water in its supercritical state at a temperature from 500°C to 3500°C, resulting in further depolymerization of the flammable and solid phase into gas and light liquid vapors , with simultaneous zone introduction of energy in the form of microwave radiation in a microwave reactor with a tubular tank, in order to liquefy part of the solid phase, i.e. coke (K),

d) the flammable phase consisting of gases and vapors of light liquids and the solid phase are directed to the gas purification center with water scrubbers and a magnetic filter, where it is rinsed with demineralized water and chemically cleaned and separated from impurities in a centrifugal separator,

e) the purified mixture of gases and vapors of light liquids is directed to a power generator with an internal combustion engine and an electricity generator in the internal combustion engine, in the intake manifold of which it is mixed with the air sucked in by the engine, previously purified in the air filtration node, and the resulting mixture is burned,

f) exhaust gases from the combustion engine are directed to the catalytic exhaust gas purification unit, where the remains of gases not burned in the engine are oxidized, the exhaust gases are separated into two streams: an energy stream and a heat stream,

g) thermal stream, the heat of which is used for the system's own needs in technological nodes,

h) the energy stream is directed to the organic node of the Rankine cycle ORC, where thermal energy is converted into electricity, after which the exhaust gas streams are combined and discharged outside,

i) contaminated water is supplied to a water treatment center containing a complex of devices for mechanical and chemical purification,

j) in the vitrification node containing a microwave reactor in which the substrates reach temperatures above 1500°C, the solid phase is melted, the metallic phase is separated from the ceramic phase by gravity in a semi-open drain channel, and shock cooling of both phases takes place in a sedimentation well containing demineralized water,

k) water pollutants in the form of a mineral fraction consisting of a ceramic phase and a metallic phase are either used as the mineral fraction of fertilizers and/or subjected to vitrification by heating in a microwave to a temperature above their melting point and then shock-cooled in water.

The biomass conversion system according to the invention includes a technological node in the form of a two-pipe reactor with pipes placed concentrically with water in its subcritical state, which supplies thermal energy to the substrates through thermal radiation, and a technological node in the form of a cyclone reactor with supercritical water, supplying energy to the chemical compounds and metals by means of thermal radiation and microwave radiation, a gas purification node with water scrubbers, a power generator with an internal combustion engine and an electricity generator, an exhaust gas purification node containing both three-way catalytic reactors, ceramic filters and electromagnetic filters, as well as heat exchangers, an organic Rankine cycle ORC node containing a system for converting thermal energy into electricity, a water purification node containing a complex of devices for mechanical and chemical purification, a vitrification node containing a microwave reactor and an air purification node containing mechanical filters; ceramic, non-woven and electromagnetic.

Preferably, the system includes a technological node in which the water reaches a temperature of 350-370°C and a pressure greater than 20 MPa.

Preferably, in the technological node, thermal energy is supplied to at least 90% of the biomass volume by thermal radiation.

Preferably, the system includes a technological node with supercritical water at a temperature from 500°C to 3500°C.

Preferably, the gas purification node has at least one water scrubber and at least one magnetic filter.

Preferably, the generating set includes at least one internal combustion engine and an electricity generator driven by this engine.

Preferably, the internal combustion engine is a multi-fuel engine.

Preferably, the exhaust gas treatment node includes at least one three-way catalytic converter, at least one electromagnetic filter and at least one ceramic filter and a heat exchanger.

Preferably, the exhaust gas treatment unit contains at least one exhaust gas heat exchanger with other heat carriers, including low-melting metals and/or their salts.

Preferably, the node of the organic Rankine cycle ORC includes a system for converting thermal energy into electrical energy: an ORC heat exchanger, an ORC turbine and an ORC electric current generator.

Preferably, the water purification node includes at least one sedimentation stage, at least one water centrifuge, at least one ion exchange stage and at least one filtration stage, including using a reverse osmosis membrane.

Preferably, the vitrification node, where the substrates reach a temperature above 1500°C, contains at least one microwave vitrification reactor.

Preferably, the air purification node contains at least one electromagnetic filter and at least one filter with a mechanical partition.

Preferably, the air purification node contains a filter with a non-woven and/or ceramic partition.

Preferably, the air purification node includes an electromagnetic filter placed in front of the mechanical partition.

The advantage of the solution according to the invention is the low-energy transformation of substrates into electricity and heat, and a large excess of these energies can be transferred to third parties as energy exclusively from renewable resources. It is important that electricity from renewable resources is obtained in a distributed system and can be transferred to e-mobility. The advantage of the solution is also that the solid metallic and ceramic phases are vitrifieds rinsed in water and as such they can constitute a raw material for the metallurgical industry (metallic phase) and construction industry (ceramic phase), the latter of which can be transferred directly to the environment because does not generate leachate. The advantage of the project solution is also the possibility of obtaining microelements (in the process of purifying circulating water) that can be used, among others, as fertilizers. The solution according to the invention is characterized by virtually zero environmental impact. Energy is obtained from renewable resources, while exhaust gases contain virtually no toxic components and particulate matter. Taking into account the extensive filtration system of the air supplied to the engine and the extensive exhaust gas filtration system, it is expected that the exhaust gases leaving the engine will contain fewer particulate matter than those contained in the ambient air supplied to the engine. Another advantage of the solution according to the invention is the deodorization of the installation surroundings (due to the intake of possibly polluted air surrounding the installation for the combustion process in the engine).

The subject of the invention is presented in more detail in an embodiment and in Fig. 1, which shows a system for implementing the method in which the streams of substrates and products are marked, as well as the streams of electric and thermal energy.

Example 1

The biomass conversion system is shown in Fig. 1, which shows the technological node 1 in the form of a two-pipe reactor 12 with concentrically placed pipes between which biomass is introduced, with water in its subcritical state in which the water reaches a temperature of 350-370°C and a pressure greater than 20 MPa characterized by the supply of thermal energy to the substrates by thermal radiation, technological node 2 in the form of a cyclone reactor 13 with supercritical water at a temperature from 500°C to 3500°C, characterized by the supply of energy to the chemical compounds and metals contained therein both by thermal radiation and by microwave radiation, a gas purification node 3 with one water scrubber 16 and one magnetic filter 17, a power generator 4 with a multi-fuel internal combustion engine 19 and an electric energy generator 20, an exhaust gas purification node 5 containing both one three-way reactor catalytic filter 23, one ceramic filter 22 and one electromagnetic filter 21, as well as heat exchangers 24, the node of the organic Rankine cycle ORC 6 containing a system for converting thermal energy into electricity - the ORC 25 heat exchanger, the ORC 26 turbine and the ORC 27 electric current generator , water purification node 7 containing a complex of devices for mechanical and chemical purification, in the form of one sedimentation stage 31, one water centrifuge, one ion exchanger 34 and one reverse osmosis membrane 35, vitrification node 8 in which the substrates S reach a temperature above 1500° C containing a microwave reactor 36 and an air purification node 9 containing one electromagnetic filter 28 and a filter with a non-woven partition 30 and a ceramic partition 29.

Fig. 1 also shows the streams; substrates S, air P, water W, contaminated water Wb, demineralized water Wd, additives D, as well as gases G, liquid L, and carbon (coke) K, solid phase Fs. Fig. 1 also shows the flows of electric energy Ee, thermal energy Ec and low-temperature thermal energy Ecn. Moreover, the ceramic phase Fc, the metallic phase Fm and the microelement ME are marked in Fig. 1.

Example 2

Substrates S in the form of biomass, waste biomass and sewage sludge are delivered to the technological node 1 in the form of a two-pipe reactor 12 with concentrically placed pipes, where they are compressed in two stages, with the first stage taking place in a piston press 10, the second stage taking place in a screw press 11 together with low-temperature heating of the biomass at 90°C, then mixed with water in a subcritical state at a temperature of 360°C and a pressure greater than 20 MPa, and this mixture is heated in a thermal radiation field so as to reach the proper temperature and pressure for the subcritical state of water, and at the same time ensuring the destruction of biomass molecules and, for example, plastics contained in the mixture. As a result of this destruction, we obtain two streams of substrates, i.e. the flammable phase G, L, K and the solid phase Fs. In technological node 1, mechanical separation takes place, as a result of which dirty water Wb is released. This water is discharged through a pipe to the collector and further to the water treatment plant 7.

The mixture of gas G, liquid L, coke K and solid phase Fs is directed through a pre-insulated pipe to the technological node 2, in the form of a cyclone reactor 13, where the pressure is reduced from 20 MPa to 10 MPa and the temperature is increased from 500°C to point 3500°C. Under these conditions, mechanical separation of the mixture components is carried out. Next, microwave heating is introduced in zones in a microwave reactor (14) with a tubular container 15 of coke K and the remains of the solid phase Fs to a point temperature of 3500°C. The heat from the coke cake K and the solid phase Fs, as well as from the energy of microwaves, is transported to the surrounding steam so that on the surface of both the coke cake K and the solid phase Fs, thermal decomposition of water into oxygen O2 and hydrogen H2 occurs. Oxygen reacts with carbon (coke K) to form carbon monoxide and partly carbon dioxide. Oxygen also reacts with heavier hydrocarbons. Gases and vapors, including water vapor, from the technological node 2 are directed through a pipe to the gas purification node 3 with water scrubbers 16 and a magnetic filter 17, where they are rinsed with Wd demineralized water and chemically cleaned and separated from impurities in the centrifugal separator 18. Average the composition of the gas directed to gas purification node 3 is: hydrogen (H2) 30-35%, hydrocarbons (CmHn) 10-15%, carbon monoxide (CO) 35-40%, carbon dioxide (CO2) 15-20%, methane ( CH4) approx. 2%, water vapor (H2O) up to 3%, nitrogen (N2) up to 4%. The calorific value of this mixture is approximately 12 GJ/Mg. The solid phase Fs, which sediments in the technological node 2, is pumped through a pipe to the collector and then to the water purification node 7. Demineralized water Wd from the water purification node 7 is supplied to the gas purification node 3 via a pipe. the gases are washed in excess demineralized water Wd. As a result, the gas leaving the scrubber 16 shocks to a temperature of 250°C. This prevents de novo reactions from the formation of dioxins and furans (PCDD/F). Part of the water vapor is dissolved in the demineralized water Wd of the scrubber 16. This water is also contaminated, mainly with the solid phase Fs, and then as dirty water Wd, it is discharged through a pipe to the water purification node 7. In the gas purification node 3, a magnetic filter 17 operates, which separates the solid phase Fs from the gas. The solid phase Fs is pumped through a pipe to the collector and then to the water purification node 7. Purified but moist gas, at a temperature of 250°C, is directed to the multi-fuel combustion engine 19 of the power generator 4, where in the engine intake manifold 19 and in the combustion chamber of this engine 19 is mixed with air P. The air P supplied to the engine 19 is previously cleaned in the air purification node 9, in which, in addition to the filter with a non-woven partition 30 and ceramic 29, there is also an electromagnetic filter 28. Electrical energy Ee is supplied to the air purification node 9 electric cable. The solid phase Fs separated on the electromagnetic filter 29 is directed to the collector and further to the vitrification node 8.

As a result of combustion of gas G in the oxygen contained in the air P in the multi-fuel internal combustion engine 19 of the generating set 4, hot exhaust gas Sp is produced, containing thermal energy Ec and electrical energy Ee produced by the electric energy generator 20 driven by this engine 19. Moreover, energy is generated in the engine cooling system 19 low-temperature thermal Ecn (with a temperature not exceeding 100°C). The exhaust gases Sp are directed to the exhaust gas purification node 5, where, as a result of the oxidation reaction of the unburned gas components G in the combustion chamber of the engine 19, their catalytic oxidation takes place, which results in an increase in the exhaust gas temperature Sp to 600°C. The appropriate part of the thermal energy of exhaust gases Ec is separated in the heat exchanger 24 located in the exhaust gas treatment node 5 and further transported through pre-insulated pipes to technological node 1 and technological node 2. Low-temperature thermal energy Ecn is also transported to technological node 1 via pre-insulated pipes. An appropriate part (approx. 20% by volume) of the exhaust gases Sp is directed to the organic node of the Rankine cycle ORC 6, where the thermal energy of the exhaust gases Sp is converted into electrical energy Ee. Sp exhaust gases are discharged into the air through the exhaust pipe. The electrical energy Ee obtained in the generator set 4 and the electrical energy obtained in the node of the organic Rankine cycle ORC 6 are used for the operating needs of the system according to the invention, and its excess is transferred to third parties. In particular, the electrical energy Ee for the system's own needs is transmitted through electric cables to elements 1, 2, 3, 5, 6, 7, 8, 9.

Contaminated water Wb from the technological node 1 and from the gas purification node 3 is transported through pipes to the water purification node 7, where the water is purified both physically and chemically. This cleaning is very thorough and the cleaning process is multi-stage. There are three stages of sedimentation 31-33, an ion exchanger 34 and a reverse osmosis membrane 35. Purified, demineralized water Wd is the circulating water of the system. Since the gas G, directed to the engine 19 in the generating set 4, is moist, water is lost, hence it is replenished from the outside, i.e. supplied through a pipe to the water purification node 7 as stream W. In the first sedimentation stage 31, water is added to sodium hydroxide (Na(OH)), which increases its acidity to a pH of approximately 5.5. The addition of hydrogen peroxide H2O2 facilitates the formation of iron (Fe(OH)3) and aluminum (Al(OH)3) hydroxides. These hydroxides are deposited in the first stage settling tank. In the second stage of sedimentation 32, by further adding sodium hydroxide (Na(OH)), the acidity of water increases to 5.5>pH>9.5, hydroxides of metals such as zinc (Zn(OH)2), lead are formed (Pb(OH)2), copper (Cu(OH)2). In the third sedimentation stage 33, calcium hydroxide (Ca(OH)2) is removed, which reacts with carbon dioxide (CO2) to form calcium carbonate CaCO3. In the next stage of water purification, metals such as calcium (Ca), magnesium (Mg) and zinc (Zn) are retained in the ion exchanger 34. To carry out ion exchange, an appropriate pH value of water is necessary (due to the concentration of the mentioned metals), which is obtained by adding hydrochloric acid (HCl) to it. The next stage of water purification in the water purification node 7 is reverse osmosis in the reverse osmosis membrane 35. In this process, the water pressure is increased to approximately 6 MPa and at this pressure it is forced through the reverse osmosis membrane 35. In the reverse osmosis process, it is separated from water sodium chloride (NaCl). All streams of D additives for individual stages of water purification in the water treatment plant 7 are marked in the diagram Fig. 1, collectively as D additives. The conducted research and analyzes show that water contamination constitutes approximately 0.003 of its mass (3 kg/Mg Wb). Demineralized water Wd is discharged through pipes from the water purification node 7 to technological nodes 1 and 2, and to the gas purification node 3. Sediments from the water purification node 7 are divided into two streams of microelements ME and the solid phase Fs. Me microelements are directed outside the installation to recipients. The residue, as the solid phase Fs, is directed to the vitrification node 8, containing a microwave reactor 36, where the batch is heated to a temperature of 1600°C by microwave. At this temperature, the solid phase Fs melts into a liquid form, which is led through a semi-open drain channel 37, approximately 3 m long, to the sedimentation well 38. In this channel 37, the ceramic phase Fc is separated from the metallic phase Fm by gravity. Then, liquid Fs is introduced into the sedimentation well 38 containing demineralized water Wd at ambient temperature. As a result of faster heat dissipation (due to better thermal conductivity) by the metallic phase Fm, it solidifies earlier than the remainder, i.e. the ceramic phase Fc. Both phases are separated automatically. At the same time, both phases are washed out in Wd water. This water becomes dirty and is transported as Wb through a pipe to the Wb collector and further to the water treatment plant 7. After being drained from the sedimentation well 38, using a scraper conveyor, both phases are magnetically separated (the metallic phase is usually ferromagnetic because it most often contains iron). separated phases, i.e. the ceramic phase Fc and the metallic phase Fm, are directed outside the system to external recipients.

List of symbols in the drawing

Technology node 1

Piston press 10

Screw press 11

Two-pipe reactor 12

Technology node 2

Cyclone reactor 13

Microwave reactor 14

Collector pipe 15

Gas purification node 3

Water scrubber set 16

Magnetic filter 17

Centrifugal separator 18

Power generator 4

Internal combustion engine 19

Electric current generator 20

Exhaust gas treatment unit 5

Exhaust gas electromagnetic filter 21

Ceramic exhaust gas filter 22

Catalytic three-way reactor 23

Heat exchanger 24

Organic Rankine Cycle ORC 6 node

ORC 25 heat exchanger

ORC 26 turbine

ORC 27 electric generator

Water purification node 7

First stage of sedimentation 31

Second stage of sedimentation 32

Third degree of sedimentation 33

Ion exchanger 34

Reverse osmosis membrane 35

Vitrification node 8

Microwave vitrification reactor 36

Drain channel 37

Sedimentation well 38

Air purification node 9

Air purification electromagnetic filter 28

Air purification ceramic filter 29

Air purification non-woven filter 30

Claims (16)

1. A method for processing biomass substrates, characterized in that it includes the following stages: a) two-stage compression of substrates (S) from biomass, with the first stage taking place in a piston press (10), the second stage taking place in a screw press (11) along with low-temperature heating of the biomass at 90°C, b) injecting substrates (S) into the space between the pipes of the technological node (1), in the form of a two-pipe reactor (12) with concentrically placed pipes and mixing the biomass with water in its subcritical state, at a temperature of 350-370°C and a pressure greater than 20 MPa , as a result of which two streams of substrates are created, i.e. the flammable phase (G, L, K) and the solid phase (Fs), c) the flammable phase (G, L, K) and the solid phase (Fs) are directed to the next technological node (2), in the form of a cyclone reactor (13) with water in its supercritical state at a temperature from 500°C to 3500°C, as a result, further depolymerization of the flammable solid phase (L) (Fs) into gas and light liquid vapors occurs, with the simultaneous introduction of zone energy in the form of microwave radiation in the microwave reactor (14) with a tubular tank (15) to liquefy part of the solid phase ( Fs) i.e. coke (K), d) the flammable phase (G) consisting of gases and vapors of light liquids and the solid phase (Fs) are directed to the gas purification node (3) with water scrubbers (16) and a magnetic filter (17), where it is rinsed with demineralized water (Wd ) and chemically purified and separated from impurities in a centrifugal separator (18), e) the purified mixture of gases and vapors of light liquids is directed to the power generator (4) with the combustion engine (19) and the electricity generator (20) in the combustion engine (19), in the intake manifold of which it is mixed with the previously purified air filtration node (9) with air (P) sucked in by the engine (19) and combustion of the resulting mixture, f) exhaust gases (Sp) from the combustion engine (19) are directed to the catalytic exhaust gas treatment unit (5), where the remains of gases not burned in the engine are oxidized, the exhaust gases are separated into two streams: energy stream (Se) and heat stream (Sc ), g) heat flow (Sc), the heat of which is used for the system's own needs in technological nodes 1 and 2, h) the energy stream (Se) is directed to the node of the organic Rankine cycle ORC (6), where thermal energy is converted into electrical energy, after which the exhaust gas streams are combined and discharged outside, i) contaminated water (Wb) is supplied to the water treatment center (7) containing a complex of devices for mechanical and chemical purification, j) in the vitrification node (8) containing a microwave reactor (36) in which the substrates (S) reach a temperature above 1500°C, the solid phase (Fs) is melted, the metallic phase (Fm) is separated from the ceramic phase (Fc) by gravity in a semi-open channel drain (37) and shock cooling of both phases in the sedimentation well (38) containing demineralized water (Wd), k) water pollutants in the form of a mineral fraction consisting of a ceramic phase (Fc) and a metallic phase (Fm) are either used as the mineral fraction of fertilizers and/or subjected to vitrification by heating in a microwave to a temperature higher than their melting point and then shock-cooled in water . 2. Biomass conversion system, characterized in that it includes a technological node (1) in the form of a two-pipe reactor (12) with pipes placed concentrically with water in its subcritical state, and a technological node (2) in the form of a cyclone reactor (13) with water in its subcritical state. supercritical, gas purification node (3) with water scrubbers (16), power generator (4) with an internal combustion engine (19) and electricity generator (20), exhaust gas purification node (5) containing both three-way catalytic reactors (23), filters ceramic (22) and electromagnetic filters (21), as well as heat exchangers (24), the organic Rankine cycle ORC node (6) containing a system for converting thermal energy into electricity, the water purification node (7) containing a complex of devices (31- 35) for its mechanical and chemical purification, a vitrification node (8) containing a microwave reactor (36) and an air purification node (9) containing mechanical filters; ceramic (29) and non-woven (30) and electromagnetic (28). 3. System according to claim 2, characterized in that it contains a technological node (1) in which the water reaches a temperature of 350-370°C and a pressure greater than 20 MPa. 4. System according to claim 2, characterized in that in the technological node (1) thermal energy is supplied to at least 90% of the biomass volume by thermal radiation. 5. System according to claim 2, characterized in that it contains a technological node (2) with supercritical water at a temperature from 500°C to 3500°C. 6. System according to claim 2, characterized in that the gas purification node (3) includes a water scrubber (16) and a magnetic filter (17). 7. System according to claim 2, characterized in that the generator (4) includes an internal combustion engine (19) and an electric energy generator (20) driven by this engine (19). 8. System according to claim 7, characterized in that the internal combustion engine (19) is a multi-fuel engine. 9. System according to claim 2, characterized in that the exhaust gas treatment node (5) includes a three-way catalytic reactor (23), an electromagnetic filter (21) and a ceramic filter (22) and a heat exchanger (24). 10. System according to claim 2, characterized in that the exhaust gas treatment unit (5) includes an exhaust gas heat exchanger (24) with other heat carriers, including low-melting metals and/or their salts. 11. System according to claim 2, characterized in that the node of the organic Rankine cycle ORC (6) contains a system for converting thermal energy into electricity: ORC heat exchanger (25), ORC turbine (26) and ORC electric current generator (27). 12. System according to claim. 2, characterized in that the water purification node (7) includes a sedimentation stage (31), a water centrifuge, an ion exchange stage (34) and a filtration stage, including the use of a reverse osmosis membrane (35). 13. System according to claim 2, characterized in that the vitrification node (8), in which the substrates (S) reach a temperature above 1500°C, contains a microwave vitrification reactor (36). 14. System according to claim 2, characterized in that the air purification node (9) includes an electromagnetic filter (28) and a filter with a mechanical partition. 15. System according to claim. 13, characterized in that it contains a filter with a non-woven (30) and/or ceramic (29) partition. 16. System according to claim. 13, characterized in that the electromagnetic filter (28) is placed before the mechanical partition.