WO2022019787A1 - Réacteur et procédé de pyrolyse de déchets industriels ou municipaux et de réduction et de purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone - Google Patents

Réacteur et procédé de pyrolyse de déchets industriels ou municipaux et de réduction et de purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone Download PDF

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WO2022019787A1
WO2022019787A1 PCT/PL2021/000043 PL2021000043W WO2022019787A1 WO 2022019787 A1 WO2022019787 A1 WO 2022019787A1 PL 2021000043 W PL2021000043 W PL 2021000043W WO 2022019787 A1 WO2022019787 A1 WO 2022019787A1
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Prior art keywords
carbonizate
pyrolysis
reactor
compartment
pyrolysis gas
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PCT/PL2021/000043
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English (en)
Inventor
Boguslaw KUSZ
Bartosz TRAWINSKi
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Politechnika Gdanska
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Priority to EP21846667.0A priority Critical patent/EP4185658A1/fr
Publication of WO2022019787A1 publication Critical patent/WO2022019787A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/16—Features of high-temperature carbonising processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/18—Modifying the properties of the distillation gases in the oven
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the subject matter of the invention is a method and a reactor for pyrolysis of industrial or municipal waste such as materials selected from the group consisting of underwood chips - wooden railway sleepers, wood waste, forest waste, sewage sludge, petroleum coke, municipal solid waste (MSW) or refuse derived fuels (RDF) and for the reduction and purification of pyrolysis gas from heavy hydrocarbons and carbon particles.
  • industrial or municipal waste such as materials selected from the group consisting of underwood chips - wooden railway sleepers, wood waste, forest waste, sewage sludge, petroleum coke, municipal solid waste (MSW) or refuse derived fuels (RDF) and for the reduction and purification of pyrolysis gas from heavy hydrocarbons and carbon particles.
  • Fuel material called charge contains material selected from the group consisting of wood chips, wooden railway sleepers, wood waste, forest waste, sewage sludge, municipal solid waste (MSW), refuse derived fuels (RDF) or any combination of fuels from biomass.
  • the pyrolysis process requires heating the charge above the temperature of 200 0 C, which results, among others, in pyrolysis gas with significant amounts of hydrogen, methane and other heavier hydrocarbons.
  • Other gas components are also carbon monoxide and carbon dioxide, nitrogen and its compounds, and hydrogen sulfide.
  • a by-product of pyrolysis is a carbonizate containing mainly carbon.
  • the gas obtained as a result of pyrolysis can be used to produce heat, electricity or it can be a source of hydrogen.
  • the gas obtained as a result of pyrolysis In order for the gas obtained as a result of pyrolysis to be used as a source of hydrogen or for the production of electricity by e.g. combustion in an engine driving an electric current generator, it should be cleaned of heavy hydrocarbons, harmful gases and carbon particles.
  • the purification of the pyrolysis gas obtained directly from the pyrolysis reactor chamber from heavy hydrocarbons, tars and gases considered as waste materials and from carbon particles is a problematic process.
  • a three-zone biomass pyrolysis reactor comprising vertically oriented, nested cylindrical vessels which define a drying chamber, a distillation chamber and a reduction and combustion chamber, respectively.
  • the reactor is configured in such a way that the gas mixture produced in the drying chamber of the chamber and the distillation chamber can be introduced into the combined reduction chamber for additional gas combustion.
  • the reactor is complicated to build and its parts subjected to high temperature degrade quickly.
  • a device for multi-stage gasification of coal fuel comprising a hermetically sealed vertical vessel which is provided with insulation. Inside the vertical reactor chamber there is a pyrolysis chamber adapted to be filled with fuel from above. Below the pyrolysis chamber there is a partial oxidation chamber for the pyrolysis product and a chemical reduction chamber for the pyrolysis gas.
  • the reactor is very complicated in construction, it uses the process of partial oxidation of the pyrolysis product, which is difficult to control, and in the case of the air oxidant, it introduces significant amounts of nitrogen into the pyrolysis gas.
  • the patent publication CZ 28354 describes a reactor with a vertically arranged pyrolysis chamber, an oxidation chamber and a reduction chamber, in which a homogenizer is located on the lower plate of the reduction chamber. However, it is the arrangement that does not provide a uniform depth of the char bed, leading to undesirable results.
  • a method of removing ash from a gasifier is known.
  • the method consists in dosing hot ash from the bottom of the reactor through a valve to the bottom tank, where the ash mixes with water and thus gets cooled.
  • a sequence reactor is known from DEI 0216338. There are 5 zones (shelves) through which the material is poured: water evaporation (150 degrees), pyrolysis (500), coking (800), hydrocarbon cracking to CO and H2 (> 1000), oxidation (gassing of remaining carbon) . Transferring between shelves (grates) is supported by an agitator. There is no information about purification by gas filtration by char.
  • Document W02008058347 describes the design and operation of a device with a heating zone, where the material is heated in contact with expanded surface heated to high temperatures (the charge is poured over the heated conical elements). The system is not pressure tight - there are outlets from the heating zone. Heating takes place by means of blown steam.
  • the maximum temperature specified in the claims is 650 ° C, which does not allow catalyzed decomposition of hydrocarbons in the char.
  • a system for the pyrolysis of organic material and the gasification of solid pyrolysis products (and tar) is known from the document W00006671.
  • the pyrolysis ( ⁇ 500 ° C) and gasification ( ⁇ 1000 0 C) processes are carried out in structurally separate chambers.
  • the construction requires the transport of mass and heat between individual chambers.
  • the pyrolysis and gasification processes take place in separate chambers rather than in one functionally divided chamber. Gas flow through the char is not forced - gases from pyrolysis and gasification are released through the outlets.
  • the pyrolysis process requires the separation of gaseous and solid products and transfer of the solid products to the gasification chamber.
  • the design and operation of a vertical pyrolysis reactor is known from the document PL221298.
  • the reactor consists of an inner pyrolysis zone and a heating zone, which is located between the vertical wall of the pyrolysis chamber and the outer casing of the device. There are heating devices in the heating zone.
  • the charge is poured from the top, which by means of the "roof 1 is directed towards the walls of the pyrolysis chamber (so that it falls down only at the walls, and not through the entire cross-section of the chamber). During the fall, pyrolysis takes place.
  • the gases are discharged through an outlet at the top and the solid products are discharged through the rotary valve into the tank under the pyrolysis chamber.
  • Document US2017073582 describes a pyrolysis reactor, which operates in such a way that an inert gas is introduced inside, whose forced flow causes gases to escape from the chamber through openings in the side wall.
  • the disadvantage of the known solutions is the inability to purify the pyrolysis gas formed already in the reactor chamber or the possibility of only partial reduction and purification of the gas by means of a carbonizate layer permanently placed inside the reactor chamber.
  • the gas obtained from known reactor solutions is contaminated and requires an additional purification process, and the process of obtaining high-energy gas from the charge itself is inefficient.
  • the pyrolysis gas produced in the reactor chamber should be passed directly through the carbonizate layer at a set temperature of 900- 1000 ° C, hereinafter referred to as the catalyst-cabonizate layer, passing continuously into the carbonizate column with the temperature decreasing with the height of the column to the room temperature at the outlet of the purified gas.
  • the base of the carbonizate column is immersed in water that acts as an additional gas filter, the carbonizate cooling agent and as the pyrolysis gas overpressure regulator in the reactor chamber.
  • the vacuum-tight reactor chamber should contain thermal insulation inside the chamber.
  • the invention was provided in the form of a column reactor for the pyrolysis of industrial or municipal waste and for the reduction and purification of pyrolysis gas from heavy hydrocarbons and carbon particles.
  • the reactor for pyrolysis of hydrocarbon-containing materials is characterized according to the invention by the fact that the space of a vacuum-tight reactor chamber with internal thermal insulation made of low-absorbent materials is functionally divided into four compartments in which the pyrolysis of the charge takes place, as well as the reduction and purification of the gas permeating through the high temperature layer and the carbonizate column with a decreasing temperature with the height of the column towards the outlet of the purified pyrolysis gas.
  • the original features of the single-chamber reactor thanks to the possibility of continuous charge feed and continuous carbonizate removal, enables to a continuous process of charge pyrolysis as well as the reduction and purification of pyrolysis gas permeating as a result of overpressure in the chamber, in the constantly renewing carbonizate layer and column.
  • the reactor is equipped with - comprising such elements as:
  • a heating column with a heat exchanger in the third compartment: a heating column with a heat exchanger, a shelf on which the layer of carbonizate-catalyst is partially supported, and around it - thermal insulation made of non-absorbent material,
  • a carbonizate column surrounded by a thermal insulation made of non-absorbent material, a chamber with cooling and filtering water that maintains the pyrolysis gas overpressure, and a carbonizate removal system.
  • the method for carrying out the reduction and purification of pyrolysis gas from heavy hydrocarbons and carbon particles sets also invention.
  • the reactor chamber is positioned vertically, which facilitates the shifting of the charge and carbonizate towards its lower part, where the excess carbonizate is removed.
  • the charge e.g. RDF
  • the charge is supplied from the reservoir by a rotary valve through the first compartment, containing thermal insulation from insulating materials with low water absorption, to the area of the second compartment where pyrolysis occurs.
  • the reactor in the chamber space, comprises a vertical agitatorwith a set of four mixing baldes mounted at an anglethat rotate at a controlled speed and provide for the charge mixing in the second compartment and the downward movement of the pyrolysis solids reactor chamber.
  • the agitator is mounted on the top cover.
  • the pyrolysis gas prefferably maintained, by continuous pyrolysis of the charge, at a positive pressure sufficient to force the pyrolysis gas flow in the vacuum-tight tube reactor chamber closed on both sides.charge.
  • the pyrolysis gas produced as a result of the pyrolysis of the charge in the second compartment of the reactor chamber flows through the layer of carbonizate-catalyst heated to the temperature of 900-10000° C, with a minimum thickness of 10 cm, which is located in the third comartment of the reactor, and flows in the fourth compartment through the carbonizate column with a temperature decreasing along with the height of the column.
  • the layer-column system of a porous carbonizate consisting mainly of carbon and other elements, including iron, calcium or aluminum, acts as a catalyst for the breakdown of heavier hydrocarbons and as a filter for carbon particles.
  • the carbonizate-catalyst layer in the third compartment partially rests on the char column and partially on a heat-resistant steel shelf in the shape of an inverted truncated cone surface.
  • the shelf is connected to a heat-resistant steel pipe with a diameter equal to the diameter of the opening of the conical surface of the shelf.
  • the pipe is surrounded by an electric heater for heating the carbonizate and the charge.
  • the pipe with the shelf in the third comartment is extended in the area of the fourth compartment by a ceramic pipe.
  • a heating column located on the base of the reactor for heating the carbonizate in the third compartment and the charge in the second compartment.
  • the heating column is made of a heat-resistant steel pipe closed at the top, inside which there is an electric heater and thermal insulation.
  • the heating column in part of the third compartment to be made of heat-resistant steel, while in the part of the fourth compartment it is made of ceramics.
  • the heating column instead of the electric heater, there is a gas burner supplied with air and the produced pyrolysis gas, which improves the energy balance of the process.
  • a steel heat exchanger in the form of 6 to 12 radially and vertically arranged heat- resistant steel plates is placed, connected to each other on the reactor axis and on the other side to the finished shelf.
  • the carbonizate produced from the second component is directed, by the angled stirrer blades and the blades of the heating column or heat exchanger, to the third compartment to form a carbonizate layer catalyzing the gas purification reaction. Then the carbonizate is moved down, creating a carbonizate column reaching as far as the tank located under the bottom cover of the reactor chamber, in which its excess is removed outside the reactor by means of a cell valve.
  • the recirculating water kept at constant level, is introduced into the carbonizate withdrawal vessel, which cools the carbonizate and the bottom of the heating column, maintains a sufficient positive pressure in the reactor chamber, and additionally filters the pyrolysis gas.
  • the vessel with the removed carbonizate is provided with a shutter-pipe dividing the vessel into two zones with different levels of cooling water and different pyrolysis gas pressures.
  • the gas pressure is greater than the gas pressure in the second zone, where the gas outlet is located, by the hydrostatic pressure resulting from the difference in the level of cooling water in both zones of the tank.
  • Such invention advantageously leads to an additional purification of the gas in the water.
  • appropriate charge temperatures above 200° C
  • carbonizate-catalyst 900-1000° C
  • the carbonate column are maintained by means of automatic regulation using at least two temperature sensors.
  • the rate of charge feed and carbonizate removal is adjustable and sufficient to ensure a continuous pyrolysis process and keep the carbonizate-catalyst layer constant above the carbonizate column so that its thickness is not less than 10cm, which ensures a continuous breakdown reaction of heavier hydrocarbons in the carbonizate layer on the top of carbonizate column into lighter fractions and hydrogen and ensures gas filtration from carbon particles.
  • the charge has more than 5 % by weight of iron as iron increases the speed and efficiency of the reduction and purification process.
  • the charge with a lower iron concentration is preferably mixed with iron oxide in the form of micro- or nano-grains in an amount to achieve a concentration of 5% by weight of iron in the charge introduced to the reactor.
  • a thermal insulation is used, minimum 10 cm thick, made of non-absorbent materials inside the steel chamber of the reactor.
  • the invention makes it possible to efficiently carry out the pyrolysis of the charge as well as the reduction and purification of the pyrolysis gas formed. Thanks to the column structure with a vacuum-tight chamber, the reactor is cheap to make and has little emergency. Moreover, the reactor is safe because damage to the reactor chamber and / or damage to its casing will not result in uncontrolled combustion of pyrolysis gas inside the reactor.
  • Fig. 1 shows the structure of the column reactor in cross section
  • Fig. 2 shows the structure of the column reactor in cross section in another solution, with a gas burner in the heating column
  • Fig. 3 shows the structure of the reactor with a heat exchanger without a heating column.
  • Fig. 1 Structure of a column reactor in cross-section, with an electric heater in a heating column.
  • Fig. 2 Structure of a column reactor in cross section in another set-up, with a gas burner heating column.
  • Fig. 3 Structure of a column reactor in cross-section, with a heat exchanger and without a heating column.
  • Example. 1 a / construction
  • the reactor chamber (1) is made of tubular stainless steel with the following dimensions: diameter 0.3 m, height 1.0 m, wall thickness 2 mm.
  • the chamber (1) is covered from the outside with a 15 cm thick thermal insulation jacket made of ceramic wool.
  • the tubular reactor chamber is closed with the lower cover (3) and the upper cover (4) and sealed with silicone gaskets (5).
  • the covers (3) and (4) are connected to the base (6) by means of four construction threaded rods (7) with nuts (8).
  • the charge is dosed through the channel in the thermal insulation made of silicate brick (12).
  • the charge (13) heated to a temperature above 200° C undergoes pyrolysis.
  • the shelf (15) is connected to a heat-resistant steel pipe (16) with an inclined wall of min. 15° to the vertical axis.
  • the pipe (16) is surrounded by an electric heater (17) powered by electrical transitions (18), which serves to maintain the temperature of the carbonizate-catalyst (14) in the third compartment (C3) at the level of 900° C.
  • Heat resistant steel tube (16) is connected to a conical ceramic tube (19) which rests on the lower cover (3).
  • the carbonizate-catalyst layer partially rests on the carbonate column (20) collected in the tube (19).
  • the base of the carbonizate column is located in the tank (21), from which the excess carbonizate is removed by means of a cell valve (22).
  • the tank (21) contains water (38) cooling the carbonizate and the lower part of the heating column. Recirculated water is introduced through a tube (36) and exited through a tube (37) and kept constant 5 cm above the lower edge of the tube (39) regulating overpressureinside the reactor chamber.
  • the pyrolysis gas cleaned in the carbonizate column is discharged from the tank (21) through a pipe (40) placed above the cooling water level (38).
  • Thermal insulation of components (Cl), (C2), (C3) and (C4) is provided by thermal insulation (12), (23) and (45) made of silicate bricks.
  • a rotary agitator (25) with blades (26) mixing the charge On the reactor axis there is a rotary agitator (25) with blades (26) mixing the charge.
  • Four symmetrically placed agitator blades are attached at an angle of about 45° to the agitator axis.
  • the bearings (27) in the top cover (4) enable the agitator (25) to rotate around the vertical symmetry axis of the reactor at a speed of approx. 1 -2 revolutions / min.
  • the lower end of the agitator shaft (25) rotates on a plain bearing (28) located on the cover of the heating column (29).
  • the heating column (29) is a vertical heat-resistant steel pipe closed at the top, placed on the base of the reactor (6).
  • thermocouple (34) Measurement of the charge temperature in the component (C2) is provided by the thermocouple (34), and the temperature of the carbonizate-catalyst in the component (C3) is measured by the thermocouple (35), both of K-type.
  • All passages through the cover (3) and (4) of the reactor are bolted passages using silicone gaskets.
  • the working temperature of the chamber (1) at the point of contact with the covers (3) and (4) does not exceed 40° C. b / methodology
  • the charge was pyrolysed in the form of a RDF pellet (Refuse-Derived Fuel) with an iron content in the resulting carbonizate of 5% by weight.
  • RDF pellet Refuse-Derived Fuel
  • thermocouple (34) measures the temperature of the charge in compartment (C2).
  • the pyrolytic gas formed in the second (C2) and third (C3) compartments due to an overpressure of 3000Pa, penetrates through the carbonizate- catalyst layer (14) and through the carbonizate column (20), passes through the cooling water layer (38) and then is discharged through the output (40).
  • the excess carbonate from the base of the column (20) is discharged by means of a cell feeder (22).
  • the rate of carbonizate production is equal to the rate of removal from the reactor, c / process efficiency:
  • the pyrolysis gas can be used, for example, to power an internal combustion engine driving a power generator or to obtain pure hydrogen.
  • the reactor described in Example 1 stably, safely and continuously converts RDF (Refuse-Derived Fuel) pellets into pyrolysis gas.
  • RDF Refuse-Derived Fuel
  • gas is obtained with the following volumetric composition: 45% hydrogen, 48% carbon monoxide, 5% methane and 2% other gases, including carbon dioxide and nitrogen.
  • the residual liquid in this process accounts for no more than 3% by weight of the charge amount.
  • the reactor is constructed as described above and, additionally, in Fig. 2.
  • the heating column (29) instead of the electric heater (31), there is a gas burner (43) with pipes (42) supplying pyrolysis gas produced in the reactor and air, and an exhaust outlet (44).
  • Example 1 The process of supplying and pyrolysing the charge in the form of RDF pellets and heating, forming and removing the carbonizate and purifying the gas is described in Example 1, with the heating of the charge and carbonizate by burning the produced pyrolysis gas in air supplied to the burner in a heating column.
  • an additional flammable gas e.g. butane from a cylinder.
  • pyrolysis gas can be used, for example, to power an internal combustion engine driving an electric generator or to obtain pure hydrogen.
  • gas is obtained with the following volumetric composition: 43% hydrogen, 48% carbon monoxide, 7% methane and 2% other gases, including carbon dioxide and nitrogen.
  • the residual liquid in this process accounts for no more than 3% by weight of the charge amount.
  • the use of pyrolysis gas for heating increased the overall energy efficiency of the RDF to pyrolysis gas conversion process by 10%.
  • the reactor is constructed as described above and, additionally, in Fig. 3. Instead of the heating column (29), there is a heat exchanger (41) heated by an electric heater (17). b) methodology
  • pyrolysis gas can be used, for example, to power an internal combustion engine driving an electric generator or to obtain pure hydrogen.
  • gas is obtained with the following volumetric composition: 40% hydrogen, 47% carbon monoxide, 7% methane and 6% other gases, including carbon dioxide and nitrogen.
  • the residual liquid in this process accounts for no more than 4% by weight of the charge amount.
  • the reactor is constructed as described in Examples 1, 2 or 3. b) method
  • Example 1, 2 or 3 The process of supplying and pyrolysing of the cahrge in the form of RDF pellets, and heating, forming and removing the carbonizate and purifying the gas is described in Example 1, 2 or 3. Additionally, the catalytic purification of pyrolysis gas is supported by an additional catalyst, e.g. iron oxide in the form of micro- or nano-grains introduced together with the charge of up to 5% by weight to the charge. When working in a reducing atmosphere, nano and micro iron granules are preferably formed, which significantly accelerates the process of reduction and purification of pyrolysis gas. c) the effectiveness of the process
  • pyrolysis gas can be used, for example, to power an internal combustion engine driving an electric generator or to obtain pure hydrogen.
  • the use of an additional catalyst increased the percentage of hydrogen in the pyrolysis gas.
  • gas is obtained with the following volumetric composition: 50% hydrogen, 47% carbon monoxide, 1% methane and 2% other gases, including carbon dioxide and nitrogen.
  • the residual liquid in this process accounts for no more than 2% by weight of the charge amount.
  • the use of a catalyst in the process increased the overall efficiency of the RDF to pyrolysis gas conversion process by more than 12%.
  • the reactor is constructed as described in Examples 1, 2 or 3. Additionally it contains no water (38) in the vessel (21) and the pyrolysis gas after purification in the layer (14) and the column (20) of the carbonizate is directly discharged through the tube (40). b) method
  • Example 1 The process of supplying and pyrolysing of the charge in the form of RDF fpellets, and heating, forming and removing the carbonizate and purifying the gas is described in Example 1 , 2 or 3 with no additional pyrolysis gas filtration in the water layer.
  • c) the effectiveness of the process The lack of water in the tank (21) simplifies the design, however, it increases the amount of heavier hydrocarbons in the pyrolysis gas by 1 percentage point.
  • the following gas composition is obtained: 50% hydrogen, 45% carbon monoxide, 1% methane and 4% others gases including carbon dioxide and nitrogen.
  • the residual liquid in this process accounts for no more than 4% by weight of the charge amount.
  • the lack of water reduces the possibility of cooling the carbonizate and causes the temperature of the tank (21) to rise to about 80° C.
  • the pyrolysis of the charge in the form of RDF pellets takes place when the charge reaches a sufficiently high temperature of at least 200° C.
  • the heating of the charge takes place when the charge introduced into the chamber falls into the carbonizate layer heated to a temperature of at least 900° C and is stirred by means of the stirrer blades.
  • gas is released and a carbonizate is formed.
  • the carbonizate stirred by the stirrer is transferred to the third compartment and heated in this compartment to the temperature of 900-1000° C, and then it is directed down the reactor to form a carbonizate column.
  • the excess carbonizate from the carbonizate column is removed in the tank at the bottom of the reactor chamber.
  • the rate of char production is equal to the rate of removal from the reactor.
  • the pyrolysis gas produced reaches a state of overpressure caused by high resistance to penetration through the porous carbonizate and the hydrostatic pressure of the water layer.
  • the overpressure of the gas in the order of 3000 Pa causes that the pyrolysis gas on its way outside the reactor must pass through the porous layer of the carbonate-catalyst and the column of the carbonate in the third and fourth compartments.
  • the carbonizate from the third and fourth compartments, heated to high temperature has catalytic properties favoring the breakdown of heavier hydrocarbons into hydrogen and lighter hydrocarbons, and favoring the formation of carbon monoxide.
  • the pyrolysis gas is reduced and purified, as well as filtered from solid particles, e.g. coal.
  • the thermal insulation in the first compartment made of the low-water absorption insulation materials causes the gases and tar condensing near the top cover to flow by gravity into the second compartment, where they are heated, and then undergo further decomposition in the carbonizate layer into simple hydrocarbons and hydrogen.
  • the tars condensing in the lower part of the reactor fill a small space free from insulation, sealing the fourth compartment.
  • the method of reducing, purifying and filtering gas in the carbonizate-catalyst layer and in the carbonizate column, as well as the use of thermal insulation inside the chamber made of low-absorbent materials minimizes the amount of liquid waste or tars produced, which significantly increases the efficiency of the process of converting the charge into gas.

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  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé et un réacteur de pyrolyse de déchets industriels ou municipaux tels que des matériaux choisis dans le groupe constitué par des copeaux de taillis, des déchets de bois, des déchets forestiers, des boues d'épuration, du coke de pétrole, des déchets solides municipaux (MSW) ou des combustibles solides de récupération (RDF), et pour la réduction et la purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone. Un réacteur pour la pyrolyse de déchets industriels ou municipaux contenant une chambre étanche au vide est caractérisé par le fait que l'espace de la chambre elle-même est divisé en quatre compartiments, à l'intérieur desquels se trouve une isolation thermique constituée de matériaux faiblement absorbants. La charge introduite à travers le premier compartiment est pyrolysée dans le second compartiment, et dans le troisième compartiment, il y a également une étagère sur laquelle une couche de carbonisat ayant une température de 850 à 1000 °C est formée, agissant en tant que catalyseur pour la réduction et la purification de gaz de pyrolyse. La couche de carbonisat à une température de 900 à 1000 °C passe en continu dans la colonne de carbonisat dans le quatrième compartiment, la température diminuant avec la hauteur de la colonne. La colonne de carbonisat fait office de filtration supplémentaire de gaz de pyrolyse et d'isolation thermique, et est refroidie dans sa partie inférieure avec de l'eau. Le chauffage de la charge et du carbonisat, nécessaire au procédé, est fourni par des dispositifs de chauffage électriques et/ou un brûleur alimenté par un gaz de pyrolyse. Le réacteur permet le processus continu d'alimentation de la charge, de sa pyrolyse, d'élimination du carbonisat et d'obtention de gaz de pyrolyse purifié. La présente invention concerne également un procédé de réduction et de purification du gaz de pyrolyse.
PCT/PL2021/000043 2020-07-21 2021-06-29 Réacteur et procédé de pyrolyse de déchets industriels ou municipaux et de réduction et de purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone WO2022019787A1 (fr)

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EP21846667.0A EP4185658A1 (fr) 2020-07-21 2021-06-29 Réacteur et procédé de pyrolyse de déchets industriels ou municipaux et de réduction et de purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone

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PLP.434735 2020-07-21
PL434735A PL241665B1 (pl) 2020-07-21 2020-07-21 Reaktor i sposób do przeprowadzania pirolizy materiałów wybranych z grupy składającej się ze zrębków, drewna podkładowego, odpadów drzewnych, odpadów leśnych, osadów ściekowych, koksu naftowego, komunalnych odpadów stałych (MSW), paliw pochodzących z odpadów (RDF) lub dowolnej kombinacji paliw z biomasy i oczyszczania gazu pirolitycznego

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN117735646A (zh) * 2024-02-19 2024-03-22 深圳市纯水一号水处理科技有限公司 一种高浓度含盐废水深度处理装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN206721116U (zh) * 2017-04-28 2017-12-08 神雾科技集团股份有限公司 一种煤粉和生物质热解制备还原气和活性炭的系统
PL418766A1 (pl) * 2016-09-20 2018-03-26 Akademia Górniczo-Hutnicza im. Stanisława Staszica w Krakowie Sposób jednorodnej karbonizacji i aktywacji materiałów organicznych oraz urządzenie do wysokoefektywnej jednorodnej karbonizacji i aktywacji materiałów organicznych
PL429984A1 (pl) * 2019-05-21 2020-11-30 Politechnika Gdańska Reaktor do pirolizy odpadów przemysłowych lub komunalnych oraz sposób przeprowadzania pirolizy z oczyszczaniem gazu pirolitycznego z ciężkich węglowodorów i cząstek węgla

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PL418766A1 (pl) * 2016-09-20 2018-03-26 Akademia Górniczo-Hutnicza im. Stanisława Staszica w Krakowie Sposób jednorodnej karbonizacji i aktywacji materiałów organicznych oraz urządzenie do wysokoefektywnej jednorodnej karbonizacji i aktywacji materiałów organicznych
CN206721116U (zh) * 2017-04-28 2017-12-08 神雾科技集团股份有限公司 一种煤粉和生物质热解制备还原气和活性炭的系统
PL429984A1 (pl) * 2019-05-21 2020-11-30 Politechnika Gdańska Reaktor do pirolizy odpadów przemysłowych lub komunalnych oraz sposób przeprowadzania pirolizy z oczyszczaniem gazu pirolitycznego z ciężkich węglowodorów i cząstek węgla

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN117735646A (zh) * 2024-02-19 2024-03-22 深圳市纯水一号水处理科技有限公司 一种高浓度含盐废水深度处理装置
CN117735646B (zh) * 2024-02-19 2024-04-19 深圳市纯水一号水处理科技有限公司 一种高浓度含盐废水深度处理装置

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EP4185658A1 (fr) 2023-05-31
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