RU2602150C2 - Method of producing hydrogen from biomass - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing hydrogen from biomass and can be used for producing hydrogen-containing products by producing hydrogen from pyrolysis products of vegetal biofuel in systems of energy accumulation and transport, as well as in systems for production of fuel for vehicles and stationary power plants. Method involves biomass grinding and drying, its further pyrolysis using heated solid heat carrier and superheated steam, separation of hydrogen-containing gases of pyrolysis and pyrolysis mass, which is subjected to high-temperature gasification. Solid heat carrier used is carbonates, forming oxides at high-temperature gasification, solid heat carrier heating is performed by combustion of pyrolysis mass of oxygen produced during electrolysis of water formed during biomass drying process.

EFFECT: technical result consists in reduction of heat consumption, as well as allowing to produce various energy carriers of various biomass in the absence of oxygen consumption from the atmosphere.

10 cl, 1 dwg, 1 tbl

Description

The invention relates to a method for producing hydrogen from biomass and can be used to produce hydrogen-containing products by producing hydrogen from products of pyrolysis of vegetable biofuel, as well as in energy storage and transport systems, in fuel production systems for transport, and in stationary power plants.

Solar energy is the main energy resource on our planet: approximately 7 × 10 ¹⁷ kWh / year reaches the Earth’s surface, which is about 10,000 times more than what is actually used by terrestrial civilization (a little less than 8.5 × 10 is bought and sold on the world commercial market ¹³ kWh of energy per year). Almost all renewable types of energy used on Earth are generated by solar energy, including wind and hydropower, biofuels and the use of thermal resources of the oceans.

Along with photovoltaic energy converters, the most suitable source for producing hydrogen-containing products is vegetable biofuel, which already contains bound hydrogen and carbon obtained from water and carbon dioxide using solar energy.

A known method of producing hydrogen and carbon dioxide from biomass, in particular from brown algae, which consists in the fact that brown algae is processed into methane using enzymes that dissolve the biomass, characterized in that brown algae are collected as biomass, which are collected in the Sargasso Atlantic Sea ocean, the main technological processes for the production of hydrogen and carbon dioxide are carried out on a floating ship in the Sargasso Sea, and the collection and supply of brown algae to the floating base is carried out using assembly trawlers, and the separation of hydrogen is carried out with its purification on a palladium membrane and feeding it into a modular system of metal hydride storage hydrogen, and carbon dioxide is collected in cylinders in a compressed or liquid state, while the resulting products in metal hydride containers and cylinders on transport ships in ports, and the generation of electricity for technological processes is carried out using fuel cell technology (patent RU 2282582, publ. 08/27/2006. Bull. No. 24). The disadvantage of this method is the complexity and high cost of the process, its low volumetric productivity, the need for filtration and purification of hydrogen and carbon dioxide as final products, dumping of fermentation waste into the environment, low hydrogen content in metal hydride storage rings.

A known method of producing hydrogen from biomass by pyrolysis using superheated water vapor and high-temperature gasification of the pyrolysis mass, which is subjected to high-temperature gasification, including:

a) grinding biomass, feeding biomass into the pyrolysis furnace while spraying low-temperature superheated water vapor in the pyrolysis furnace, regulating the pyrolysis furnace in the range of operating temperature 500-800 ° C, contacting the biomass with low-temperature superheated steam to conduct the pyrolysis reaction with the release of crude synthetic gas and ash containing coke;

b) cooling the ash and separating the coke from the ash;

c) supplying the crude synthetic gas and coke to the gasifier, spraying the high temperature superheated water vapor in the gasifier, regulating the gasifier in the range of the working temperature of 1200-1600 ° C, contacting the biomass with the high temperature superheated water vapor to conduct the gasification reaction with the release of the primary synthetic gas; and

d) cooling, dust removal, deoxidation and drying of the primary synthetic gas to obtain pure synthetic gas (patent RU 2526387, publ. 08.20.2014. Bull. No. 23) - analogue. The disadvantage of this method is the complexity and high cost of the process, its low volumetric productivity, the need for filtration and purification of hydrogen and carbon dioxide as final products, large energy losses associated with the need to supply a large flow rate of superheated water vapor used as a coolant.

There is also a method of producing synthesis gas from biomass by pyrolysis, including:

1) pre-treatment of biomass feedstock, including grinding of biomass feedstock to obtain particles 1-6 mm in size and drying the feedstock to a moisture content of 10-20 wt.%;

2) the pyrolysis of biomass feedstock using fast biomass pyrolysis technology, wherein the product of the pyrolysis layer is pyrolysis gas and coal powder, where the temperature of the pyrolysis layer is 400-600 ° C and the residence time of the gas phase on the pyrolysis layer is 0.5-5 s;

3) the separation of the pyrolysis gas from coal powder and solid coolant using a cyclone separator;

4) separation of the coal powder and the solid coolant in the separator for separating solid phases, loading the coal powder into the coal powder hopper for storage, heating the solid coolant in the fluidized bed heating chamber and supplying the solid coolant to the pyrolysis layer for reuse;

5) supplying the formed pyrolysis gas to the condensate collector for aerosol condensation, condensation of the condensed part of the pyrolysis gas to form biooil, injecting the resulting biooil with a high pressure oil pump, and supplying it to the gasification furnace for gasification; and

6) the supply of one part of non-condensable pyrolysis gas to the combustion layer for combustion with air, the supply of another part of non-condensable pyrolysis gas to the pyrolysis layer as a fluidizing medium (patent RU 2519441, publ. 06/10/2014. Bull. No. 16) - prototype. The disadvantage of this method is the complexity and high cost of the process, its low volumetric productivity, the need for filtration and purification of hydrogen and carbon dioxide as final products, large energy losses associated with the need for convective heating of a solid coolant.

The purpose of the present invention is to create a new method for producing hydrogen and carbon dioxide, which can be used both as separate products and as the main components of the synthesis gas, which allows to reduce the heat costs of the hydrogen production process, as well as efficiently produce various energy carriers from various biomass in the absence of oxygen consumption from the atmosphere.

The problem is solved in that a method for producing hydrogen from biomass is proposed, including grinding and drying of biomass, its subsequent pyrolysis using heated solid heat carrier and superheated water vapor, separation of hydrogen-containing pyrolysis gases and pyrolysis mass, which is subjected to high-temperature gasification, using solid heat carrier carbonates forming oxides during high-temperature gasification; heating of a solid heat carrier is carried out by burning pyrolysis mass into oxygen Was prepared by the electrolysis of water generated during the drying of the biomass.

Besides:

- pyrolysis is carried out in a fluidized bed created by a stream of superheated water vapor, heated by the utilization of heat energy taken from hydrogen-containing pyrolysis gases and carbon dioxide generated during high-temperature gasification of the pyrolysis mass,

- part of the hydrogen is separated from the hydrogen-containing pyrolysis gases as an additional target product added to the hydrogen produced by electrolysis of water,

- the pressure during the pyrolysis of biomass is maintained at a level of 0.2-0.8 MPa, and the temperature is not higher than 550 ° C,

- heating of the solid heat carrier is carried out at a temperature of 800-1000 ° C in a fluidized bed mode,

- electrolysis of water is carried out at elevated pressure during periods of lowering the electrical load of the power system supplying the electrolyzer,

- carbon dioxide formed during the high-temperature gasification of the pyrolysis mass is isolated in gaseous, liquid or solid form, as a separate product sent for burial or sale,

- when heating a solid coolant, it is decomposed with the formation of oxide,

- the selection of oxygen produced during the electrolysis of water is carried out in a mixture with water vapor,

- electrolysis of water lead during periods of lowering the electrical load of the power system supplying the electrolyzer.

The drawing shows a diagram of the implementation of the method, where 1 is a biomass feed, 2 is a drying and grinding apparatus for biomass, 3 is a flow of crushed biomass, 4 is a pyrolyzer, 5 is a solid phase flow, 6 is oxygen, 7 is an electrolyzer, 8 is electricity supply, 9 - hydrogen-containing gases, 10 - unit for the separation of hydrogen and carbon dioxide and water heating, 11 - hydrogen, 12-1 - crude carbon dioxide, 12-2 - product carbon dioxide, 13 - water vapor, 14 - gasifier, 15 - solid heat carrier , 16 - hydrogen flow, 17 - hydrogen storage, 18 - hydrogen consumer. An example implementation of the invention is the method of producing hydrogen from biomass, described below.

A preferred solid biomass material according to the present invention is waste and by-products of the wood processing industry, such as logging waste, urban wood waste, lumber waste, wood chips, sawdust, straw, firewood, wood materials, by-products of paper or building lumber processes, crops short rotation, etc. In the described embodiment of the invention, wood is used as biomass, which allows us to characterize the features of the invention as applied to the processes of hydrogen and carbon dioxide production from wood waste, which can be used as part of the alternative energy concept using modern energy technologies.

The annual increase in plant biomass on Earth is from 170 to 200 billion tons, counting on dry matter, which in terms of the oil equivalent corresponds to about 70-80 billion tons, which is about an order of magnitude higher than the world’s needs for the future.

Russia has a huge bioenergy potential. First of all, it is a forest that occupies 60% of the country's territory and annually produces almost a quarter of the world biomass growth.

Using solar energy, biomass is grown or harvested on natural lands, then biomass 1 is supplied, biomass is prepared (dried using solar energy or a heat carrier and milled) in a drying and milling apparatus for biomass 2, after which the flow of milled biomass 3 is sent to the pyrolyzer 4 , in which the biomass is subjected to a catalytic pyrolysis reaction by heating with a solid coolant 15 to obtain reaction products, including a gaseous phase (hydrogen-containing gases) - 9, containing hydrogen and carbon dioxide, and a solid phase stream 5, consisting of a solid coolant with pyrolysis products deposited on it. The flow of solid phase 5 is directed to the gasification of the pyrolysis products, which is carried out in a gasifier 14 in a water vapor environment with oxygen 6 supplied from an electrolyzer 7, to which electricity 8 is supplied, mainly during periods of falling load of the power supply system, which reduces the cost of producing hydrogen. Hydrogen-containing gases obtained in the pyrolyzer 4 are sent to a unit for separating hydrogen and carbon dioxide and heating water 10, from which hydrogen 11, product carbon dioxide 12-2, and water vapor 13 obtained from water by removing heat as from hydrogen-containing gases are removed 9, as well as from the stream of crude carbon dioxide 12-1 discharged from the gasifier 14. Water vapor is supplied from the drying and grinding apparatus of biomass 2, from which water vapor is also supplied to the electrolysis in the electrolyzer 7. In the gasifier 14 due to the reaction of products pyrolysis with oxygen 6, heating of the solid heat carrier 15 is carried out with the formation of crude carbon dioxide 12-1 supplied to the unit for the separation of hydrogen and carbon dioxide and heating water 10. From the electrolyzer 7, the hydrogen stream 16 is directed to a hydrogen storage 17, from which hydrogen 18 is supplied to the consumer 18. Hydrogen 11 is also fed to the hydrogen storage 17, which is separated in a unit for separating hydrogen and carbon dioxide and heating water 10, from which product carbon dioxide 12-2, converted into n, is also removed as a separate product crawled form (a compressed, liquid or solid form).

The supply of biomass 1 to the drying and grinding apparatus of biomass 2 is carried out in the form, for example, of raw granular wood with a grain size of 10-20 mm through the first lock hopper (not shown). The pressure in the pyrolyzer 4 is increased, for example, to 2-8 MPa, and therefore a second lock hopper with a shutter is also used to increase the pressure in the drying and grinding apparatus for biomass 2, at least to a pressure in the pyrolyzer 4. The heat carrier used to heat biomass up to 100-150 ° C in the apparatus for drying and grinding biomass 2, preferably, but not necessarily, is carbon dioxide supplied to the heat exchange elements of the apparatus for drying and grinding biomass 2.

In the wet state, most conifers contain 52-65%, soft hardwood 45-55%, hard 38-45% water. The average composition of air-dried wood in% wt. (kg / kg): 43.8 carbon, 5.3 hydrogen, 0.2 nitrogen, 38.2 oxygen, 12.0 hydrated water, 0.5 ash. When drying biomass, not only water is released at high temperature, but also a change in some of the components of wood. When wood is heated to 100-150 ° C and water is released from it, cracking of granules easily occurs, which increases their reactivity. In the apparatus for drying and grinding biomass 2, preliminary processing of biomass raw materials is carried out: grinding of biomass raw materials to obtain particles of 2-8 mm and drying of the raw materials to a moisture content of 10-20 wt.% With the removal of water vapor in the electrolytic cell 7 and for heating and obtaining water vapor 13 supplied to the pyrolyzer 4. The selection of oxygen 6 produced during the electrolysis of water is carried out in a mixture with water vapor, which can dramatically reduce the technical risks associated with the increased danger of oxygen, and simplify the hardware design of the process.

The biomass fed to the pyrolyzer 4 usually contains 80 wt.% Volatile components and 20 wt.% Carbon, it contains a significant content of fiber C ₆ H ₁₀ O ₅ (cellulose). Heating said biomass to a suitable temperature in an oxygen-depleted or oxygen-free environment leads to pyrolysis at a temperature usually not higher than 800 ° C. The pyrolysis of volatile components leads to the formation of hydrogen-containing gases 9, which contain CO, H ₂ , CH ₄ , CO ₂ .

The pyrolysis reaction of biomass is carried out in a pyrolysis reactor - pyrolyzer 4 - with the supply of thermal energy using a solid heat carrier at an elevated temperature and pressure of biomass conversion of at least 0.2-0.8 MPa. It is possible and advisable to conduct the process in the presence of a catalyst based on metals selected from the group of iron, nickel, rhodium, platinum, iridium, palladium, their mixtures or compounds. Taking into account the need to increase the hydrogen output, pyrolyzer 4 is predominantly supplied with high-pressure water vapor 13, which is heated during heat removal from hydrogen-containing gases 9 in a unit for separating hydrogen and carbon dioxide and heating water 10. In the same unit 10, hydrogen and carbon dioxide are separated due to adsorption or membrane separation of gases. From installation 10, product carbon dioxide 12-2 is withdrawn as a separate product, converted to the desired form (in compressed, liquid, or solid form). Part of carbon dioxide 12-2 (not shown) in a gaseous form heated to 100-150 ° C is fed to the drying and grinding apparatus of biomass 2.

It is known [S. Vincent, "Carbonization des bois en vases clos." (1873)] that at 260-280 ° C, mainly aqueous distillate containing acetic acid C ₂ H ₄ O ₂ and other volatile organic compounds are obtained from wood raw materials. acids, methyl alcohol CH ₄ O, acetone C ₃ H ₆ O, furfural C ₅ H ₄ O ₂ , methylamine CH ₃ NH ₂ , etc., i.e. predominantly oxygen organic substances, non-condensable gases and resinous substances are released in this period in a limited amount; the total amount of volatile products is about 60%, the remainder is brown (see table - product yield during pyrolysis):

Table Pyrolysis temperature Yield,% wt. In the dry residue of the pyrolysis mass,% Volatile products Coal Carbon Hydrogen Oxygen and nitrogen Ash 260 ° 59.77 40,23 67.89 6.04 26.57 0.56 280 ° 63.84 36.16 72.64 4.70 22.09 0.57 330 ° 68,23 31.77 73.55 4.63 21.34 0.48 432 ° 81.13 18.87 81.97 2,30 14.13 1,60

The process of pyrolysis of biomass in the pyrolyzer 4 is carried out by heating with a solid heat carrier 15 in a medium of water vapor 13. As a solid heat carrier 15, metal oxide, for example calcium oxide, is used, which during pyrolysis is combined with carbon dioxide obtained from biomass pyrolysis products to form carbonate calcium and the release of thermal energy that compensates for the endothermic reaction of water vapor with biomass.

All volatile compounds formed during pyrolysis are subjected to steam conversion in the pyrolyzer 4, the total reaction can be written as:

An important role is played by the shift reaction:

which, in essence, is a carbon monoxide vapor conversion reaction. It is this reaction [2] that is used in the present invention to obtain the main amount of hydrogen, for which purpose calcium oxide, which forms calcium carbonate with carbon dioxide according to the reaction, is fed into the pyrolyzer 4 as heated solid heat carrier 15:

which leads in the reaction [2] to a shift of the process towards hydrogen 11 according to the Le Chatelier principle.

Previously, this approach was proposed in relation to steam methane conversion due to heat from HTGR [Stolyarevsky A.Ya., Mikhailova SA, Brun-Tsekhovoy AR, Katsobashvili Ya.R. et al. On one of the promising directions for improving the process of steam conversion of hydrocarbons // Issues of Atomic Science and Technology, ser .: Hydrogen and Atomic Energy and Technology, vol. 2 (9). - M., 1981, p. 96-98].

Thus, it was proposed to use a sorbent with a high and stable capacity based on CaO when pyrolyzing biomass. It was shown that calcination of powdered calcium carbonate at a temperature of 1150 ° C and above allows to obtain absorbers with a capacity of up to 25 wt. %, stable over several thousand cycles [A.I. Lysikov, B.N. Lukyanov A.G. Okunev. Absorption-catalytic conversion of hydrocarbons: reactors, sorbents and catalysts // Chemistry in the interests of sustainable development, 18 (2010), 691-704].

In addition to lowering the temperature in the gasifier 14, where the thermolysis of calcium carbonate is carried out and CaO is produced as a heated solid heat carrier 15 to 800 ° C, a decrease in CaO sintering can be achieved by using texture promoters that reduce the speed of this process. The temperature treatment of the mixture of 80-90 wt. % CaO with SiO ₂ allows to obtain a durable material suitable for use in a fluidized bed. During the heat treatment of mixed oxides and subsequent sorption of CO ₂ , a phase of interaction of the composition Ca ₅ (SiO ₄ ) ₂ CO ₃ is stable under gasifier 14 conditions. The absorption of carbon dioxide occurs with the participation of unbound calcium oxide, while the carrier determines the high mechanical strength of the chemisorbent. The capacity of this system reaches up to 50 wt. % in terms of unbound calcium oxide and 40 wt. % in terms of the total mass of chemisorbent. At the same time, the use of materials containing SiO ₂ under conditions of steam conversion of hydrocarbons is undesirable due to the formation of volatile silicon hydroxide at temperatures above 500 ° C, which leads to the destruction of the material and dust formation. Alumina may be used as another additive. Calcium oxide supported on Al ₂ O ₃ has high strength due to its similarity with the cement composition [Li Ζ.S., Cai NS and Yang published by JB // Ind. Eng. Chem. Res. 2006. Vol. 45, No. 26. P. 8788]. At the same time, for 75 wt. % CaO / Ca ₁₂ Al ₁₄ O ₃₃ , a drop in capacity is more than doubled during 56 sorption / regeneration cycles, in addition, when regenerating under conditions of gasifier 14, overheating above 1000 ° C cannot be allowed due to the accelerated reaction of CaO with the carrier [Ibid .].

It is possible to use mixed oxides, however, the resistance of the mixed oxides to sintering is lower compared to the stability of the initial CaO. An exception is heat-resistant magnesium oxide, which does not form phases of interaction with CaO. A significant amount of work has been devoted to the production of high-temperature chemisorbent CO ₂ by calcining dolomites, which are mixed calcium and magnesium carbonate (CaCO ₃ · MgCO ₃ ). The decomposition of dolomite during calcination occurs in steps: first, magnesium carbonate decomposes, which at high temperatures forms a chemically inert and stable periclase phase, then calcium carbonate. In this way, a chemosorbent based on CaO supported on MgO is formed. Due to the periclase framework, which has high mechanical strength and abrasion resistance, such an absorber can be used in fluidized bed reactors for pyrolyzer 4. The calcined dolomite capacity for CO _{2 is} slightly lower than for pure CaO, due to the significant amount of ballast MgO. Despite the presence of an inert support in the CaO / MgO system, sintering of the active component is also observed, and one of the ways to increase the capacity is to regenerate the absorber by steam at elevated pressure under conditions of gasifier 14, which makes it possible to convert calcium carbonate not to oxide, but to more easily carbonized hydroxide. The reaction of carbonization of calcium hydroxide proceeds with virtually no change in the molar volume of the absorber (the Pilling-Bedwards criterion for this reaction is 1.12), due to which it is possible to achieve a higher dynamic capacity of the absorber.

Both the pyrolysis of biomass in the pyrolyzer 4 and the high-temperature gasification of the pyrolysis mass in the gasifier 14 are expediently carried out in a fluidized bed, which significantly improves mass transfer and increases the productivity of reactors.

In the gasifier 14, the solid phase flow from the pyrolyzer 4 includes both calcium carbonate CaCO ₃ and a pyrolysis mass deposited on calcium carbonate, which is a non-volatile carbon compound. Using oxygen 6 coming from the electrolyzer 7, it is possible to carry out high-temperature gasification of the pyrolysis mass in gasifier 14, using the heat energy released in this process for thermolysis of CaCO ₃ and its heating with the formation of calcium oxide CaO as a heated solid heat carrier 15 supplied to the pyrolyzer 4 The gasifier 14 used is a fluidized bed gasifier in which the fluidization of the bed is carried out using fluidizing agents that feed the gasifier into the bulk. 14 below. The construction of the pyrolyzer 4 is similarly constructed. In both devices, water vapor 13 or oxygen 6, respectively, can be used as the fluidizing agent. Hydrogen-containing gases 9 containing hydrogen and carbon dioxide are fed to a unit for separating hydrogen and carbon dioxide and heating water 10, in which product hydrogen 11 is sent to the hydrogen storage 17, from where it is supplied to the hydrogen consumer 18 as needed. In the hydrogen storage 17 also direct the hydrogen stream 16 produced by supplying electricity 8 in the electrolyzer 7, which also receive oxygen 6, sent to the gasifier 14. The main reaction in the gasifier 14, along with the oxidation of the pyrolysis mass, odyaschey the solid phase 5 until carbon dioxide is also the thermochemical decomposition of calcium carbonate used as the solid heat carrier 15, to form calcium oxide and carbon dioxide. The stream of crude carbon dioxide 12-1 is sent for cleaning to the installation of the separation of hydrogen and carbon dioxide and heating water 10.

Hydrogen-containing gases 9 are mixtures of carbon oxides and hydrogen with small amounts of methane and other hydrocarbons: 2-4% (vol.) СО, СО ₂ , 93-95% (vol.) Н ₂ , СН ₄ - the rest. Non-volatile pyrolysis products are planted on ceramic particles of calcium carbonate used as solid heat carrier 15, and are sent to a gasifier 14 as a solid phase stream. In the case of using solid catalysts in the pyrolysis process, separators are used to separate the catalyst from the solid phase stream 5.

Thus, in the proposed invention, it was possible to create a new method for producing hydrogen, which allows to reduce the heat costs of the hydrogen production process, as well as to efficiently produce various energy carriers from different biomass in the absence of oxygen consumption from the atmosphere.

Claims (10)

1. A method of producing hydrogen from biomass, including grinding and drying the biomass, its subsequent pyrolysis using a heated solid heat carrier and superheated water vapor, separation of hydrogen-containing pyrolysis gases and pyrolysis mass, which is subjected to high-temperature gasification, characterized in that carbonates are used as a solid heat carrier forming oxides during high-temperature gasification, heating of the solid heat carrier is carried out by burning the pyrolysis mass in oxygen obtained by electro Ys water formed in the process of drying the biomass. 2. The method of producing hydrogen from biomass according to claim 1, characterized in that the pyrolysis is carried out in a fluidized bed created by a stream of superheated water vapor, heated by the utilization of heat energy taken from hydrogen-containing pyrolysis gases and carbon dioxide generated during high-temperature gasification of the pyrolysis mass . 3. The method of producing hydrogen from biomass according to claim 1, characterized in that a part of the hydrogen is separated from the hydrogen-containing pyrolysis gases as an additional target product added to the hydrogen produced by electrolysis of water. 4. The method of producing hydrogen from biomass according to claim 1, characterized in that the pressure during the pyrolysis of biomass is maintained at 0.2-0.8 MPa, and the temperature is not higher than 550 ° C. 5. The method of producing hydrogen from biomass according to claim 1, characterized in that the heating of the solid heat carrier is carried out at a temperature of 800-1000 ° C in a fluidized bed mode. 6. The method of producing hydrogen from biomass according to claim 1, characterized in that the electrolysis of water is carried out at elevated pressure during periods of lowering the electrical load of the power system supplying the electrolyzer. 7. The method of producing hydrogen from biomass according to claim 1, characterized in that the carbon dioxide generated during the high-temperature gasification of the pyrolysis mass is isolated in gaseous, liquid or solid form as a separate product sent for disposal or sale. 8. The method of producing hydrogen from biomass according to claim 1, characterized in that when the solid coolant is heated, it decomposes with the formation of oxide. 9. The method of producing hydrogen from biomass according to claim 1, characterized in that the selection of oxygen produced during the electrolysis of water is carried out in a mixture with water vapor. 10. The method of producing hydrogen from biomass according to claim 1, characterized in that the electrolysis of water is carried out in periods of lowering the electrical load of the power system supplying the electrolyzer.

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