EP4163352A1 - Procédé de gazéification de matière première contenant du carbone et dispositif de mise en oeuvre - Google Patents

Procédé de gazéification de matière première contenant du carbone et dispositif de mise en oeuvre Download PDF

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Publication number
EP4163352A1
EP4163352A1 EP21818532.0A EP21818532A EP4163352A1 EP 4163352 A1 EP4163352 A1 EP 4163352A1 EP 21818532 A EP21818532 A EP 21818532A EP 4163352 A1 EP4163352 A1 EP 4163352A1
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Prior art keywords
partial oxidation
oxidation
channel
vapour
gas
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English (en)
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Yurij Vladimirovich FESHCHENKO
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D1/00—Burners for combustion of pulverulent fuel
    • F23D1/005—Burners for combustion of pulverulent fuel burning a mixture of pulverulent fuel delivered as a slurry, i.e. comprising a carrying liquid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/12—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating using gaseous or liquid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/002—Supplying water
    • F23L7/005—Evaporated water; Steam
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23M—CASINGS, LININGS, WALLS OR DOORS SPECIALLY ADAPTED FOR COMBUSTION CHAMBERS, e.g. FIREBRIDGES; DEVICES FOR DEFLECTING AIR, FLAMES OR COMBUSTION PRODUCTS IN COMBUSTION CHAMBERS; SAFETY ARRANGEMENTS SPECIALLY ADAPTED FOR COMBUSTION APPARATUS; DETAILS OF COMBUSTION CHAMBERS, NOT OTHERWISE PROVIDED FOR
    • F23M20/00—Details of combustion chambers, not otherwise provided for, e.g. means for storing heat from flames
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification

Definitions

  • the given invention relates to chemical, petrochemical, coke-gas, energy and other related industries, and can be used primarily for processing carbonaceous feedstock to produce energy and process gases, particularly for gasification of carbonaceous feedstock, synthesis gas production by means of partial oxidation of a flow containing carbon.
  • synthesis gas by partial oxidation
  • a flow containing carbon such as coal, brown coal, peat, wood, coke, soot or other types of gaseous, liquid or solid fuels, or mixtures thereof
  • a gasification reactor i.e. partially oxidized using an oxygen-containing gas, such as pure oxygen or air, optionally enriched with oxygen, etc.
  • oxygen-containing gas such as pure oxygen or air, optionally enriched with oxygen, etc.
  • Coal gasification technologies are mainly divided into three types: gas producers with a fixed-bed, such as gas producers manufactured by Lurgi AG (Germany, Frankfurt am Main) [1, pp.161-167], fluidized or fluidized bed gas producers implemented using the U-GAS, Winkler technologies (USA, Institute of Gas Technology, Chicago) [1, pp. 167-173], and parallel flow gas producers, according to the Shell process (jointly Shell and Uhde companies, Buggenum installation, Netherlands) [1, pp.189-191] and Texaco (USA, Texaco GP, Cool Water and Polk installations) [1, pp.176-180].
  • gas producers with a fixed-bed such as gas producers manufactured by Lurgi AG (Germany, Frankfurt am Main) [1, pp.161-167]
  • fluidized or fluidized bed gas producers implemented using the U-GAS
  • Winkler technologies USA, Institute of Gas Technology, Chicago
  • Texaco USA, Texaco GP, Cool Water and Polk installations
  • Fluidized bed gas producers have low efficiency due to low carbon conversion, difficulties with unloading dry bottom ash and high-volatile ash.
  • Combustion temperature inside the torch is 1500-1700° C and its level is maintained depending on the melting temperature of the ash.
  • the ash in liquid form is removed from the bottom of the reaction chamber into a special device where it is cooled and granulated.
  • the disadvantages of the given gasifier include:
  • the coal-water suspension is fed into the lower part of the gas producer simultaneously mixing with oxygen. Partial oxidation of coal occurs, thus providing endothermic reactions in thermal energy gasification zone.
  • the slag formed at the first stage is removed into a water bath and then used in construction.
  • the crude producer gas enters the upper lined part of the reactor, where a coal-water suspension is additionally added. In this part, the reaction of fresh fuel with the producer gas obtained at the first stage of the process takes place.
  • the combustion temperature of the producer gas increases, and the ongoing endothermic reactions contribute to its cooling to a temperature of about 1038°C.
  • PRENFLO PRessurized Entrained-FLOw
  • PSG vapour production
  • Thyssenkrupp AG Thyssenkrupp AG
  • the gasification temperature is higher than the melting point of the ash (1400-1600° C) which allows for liquid slag removal.
  • the advantage of this process is the dry supply of fuel which is the feedstock of gasification. Finely dispersed coal (80% of volume smaller than 0.1 mm) is fed together with oxygen and vapour through four burners installed in the same horizontal plane at the bottom of the gas producer.
  • the disadvantages of this gas producer include:
  • the gasifier contains a vertical gasification chamber, a burner with nozzles for supplying carbonaceous feedstock and oxygen-containing gas, a manifold for supplying water vapour, nozzles for supplying pulverized carbonaceous feedstock, a pipe for removing gasification products (in the lower part of the gasification chamber), a slag removal chamber.
  • the gasification chamber is a cylindrical pipe ending with a conical slag removal chamber while the gasification chamber is conditionally divided into oxidizing and reduction parts.
  • the process in the oxidation zone is carried out at a temperature of 1500-3000°C, and in the reduction zone by vapour supply, the temperature drops to 1000-1600°C.
  • Oxidation of coal actually occurs under adiabatic conditions as the oxidation chamber is made in a form of a channel mounted coaxially to the outer wall of the gas producer separated from the outer wall by an annular space washed by coal oxidation products, which maintains the temperature in the oxidation chamber close to 1400-1600°C.
  • the supply of coal dust and a mixture of oxygen and water vapour is carried out through 4 horizontal burners in the upper part of the oxidation chamber.
  • the oxidation chamber merges into rapid water cooling chamber into which water is injected through vants located along the ring in the cooling chamber, cooling the oxidation products to a temperature of 200 - 250°C.
  • the closest to the proposed device is the gas producer [1, pp.186-189] employing the specified method-prototype containing a manifold for feeding water vapour and oxygen to the burners, a manifold for feeding a gas-coal mixture to the burners, an oxidation chamber that passes into a rapid water cooling chamber which is a cylindrical pipe coaxially arranged inside the gas producer housing ending with a conical slag removal chamber. There is an annular gap between the slag removal chamber and the central pipe of the rapid cooling chamber through which the raw oxidation generator gas and water vapour exit the cooling chamber then rise along the inter-wall gap between the cooling chamber pipe and the gas producer housing and exit the gas producer into the pipe for removal of gasification products for further processing.
  • a sharp change in the movement of the gas flow in the rapid cooling chamber leading to the fact that the movement of gases downwards after the passage of the slit gap between the pipe of the cooling chamber and the slag removal chamber changes into an upward movement, allows separating a significant amount of slag and ash with their insertion into the conical slag removal chamber.
  • the slag removal chamber is connected to the slag removal system.
  • Slag from the gasifier can be used as a building material.
  • the main objective of the invention is to create an effective method of gasification in a parallel flow of carbonaceous feedstock such as coal, brown coal, peat, wood, coke, soot or other types of gaseous, liquid or solid fuels, or mixtures thereof by partial oxidation of carbonaceous feedstock in a mixture of oxygen-containing gas and water vapour and a device for its implementation in order to obtain the maximum possible hydrogen yield during gasification of carbonaceous feedstock.
  • carbonaceous feedstock such as coal, brown coal, peat, wood, coke, soot or other types of gaseous, liquid or solid fuels, or mixtures thereof by partial oxidation of carbonaceous feedstock in a mixture of oxygen-containing gas and water vapour and a device for its implementation in order to obtain the maximum possible hydrogen yield during gasification of carbonaceous feedstock.
  • the technical result of the claimed invention is the production of producer gas with increased hydrogen concentration. What is more, the ignition stability is achieved and the necessary partial oxidation temperature is maintained.
  • the proposed technical result is achieved due to the fact that in the known method of gasification of carbonaceous feedstock, including partial oxidation of carbonaceous feedstock in an oxidation chamber in a mixture of oxygen-containing gas and water vapour, partial oxidation is carried out in a partial oxidation channel coaxially mounted in the oxidation chamber, and the supply of water vapour for partial oxidation of carbonaceous feedstock is carried out at the input and output of the partial oxidation channel of the combustion chamber.
  • the size dimensions of the partial oxidation channel are optimally chosen based on the ratio: L ⁇ 4 * G * T b / ⁇ * ⁇ t o * D 2 , where
  • Solid fuels in the form of coal, brown coal, peat, wood, coke, soot, or gaseous and liquid fuels, or mixtures thereof can be used as carbonaceous feedstock.
  • the well-known gas producer for gasification of carbonaceous feedstock containing a housing, a burner device, a vertical oxidation chamber, manifolds for supply of carbonaceous feedstock, water vapour and oxygen-containing gas, a pipe for discharging gasification products, a slag removal chamber, additionally contains a partial oxidation channel which is coaxially mounted in a vertical oxidation chamber and attached to the upper inner part of the housing in which the burner device is installed.
  • the upper part of the housing is made in the form of a removable lid in which a burner device is installed.
  • the pipe for discharging gasification products can be installed in the side of the gas producer housing, closer to the upper part of the gas producer.
  • the inner walls of the oxidation chamber can be made in the form of coaxially arranged toroid-shaped containers that provide the possibility of supplying water vapour from below the oxidation chamber to the gas producer lid.
  • the partial oxidation channel can be made with external thermal insulation.
  • the oxidation process is divided into 2 stages: first, partial oxidation is carried out under adiabatic conditions in a thermally insulated oxidation channel at optimal temperatures of 900-1100 0 C in a flow of oxygen and water vapour mixture, and then the resulting gases are further oxidized at the output of the partial oxidation channel only by water vapour with the temperature in this zone being maintained within the optimal temperature range of 800-1000°C.
  • the proposed device for implementing the proposed oxidation method in contrast to analogues, all processes are carried out under conditions that exclude a sharp increase in pressure in the reaction zones.
  • the proposed method allows for stable ignition and combustion in the resulting two-phase flow both on the surface of the particle and in the gas phase, due to the stable supply of additional thermal energy from combustion products coming from the built-in burner device in which liquid or gaseous fuel is burned.
  • the combustion products from the burner device enter the partial oxidation channel along the axis of the channel mixing with carbonaceous feedstock and a vapour oxygen mixture.
  • the ignition stability and maintenance of the required temperature in the oxidation channel is supported by the supply of thermal energy from the burner device built in the upper part of the gas producer housing when burning any fuel regardless of the type of carbonaceous feedstock entering the gas producer for oxidation, for example, with the help of air oxygen, unlike the prototype and other traditional methods in which stabilization is maintained by means of high oxygen consumption for burning part of the oxidized carbonaceous feedstock with obtaining high temperatures of 1400-1600°C and a pressure of 27-40 atm in them, and as a result, with a small hydrogen yield.
  • the proposed gas producer for gasification of carbonaceous feedstock contains a housing 1, an oxidation chamber 2, a housing lid 3 ( Fig. 1 ), a burner device 4 ( fig. 4 ) with a diffusion burner 7, oxygen supply pipes 5 and a mixture of water vapour and carbonaceous feedstock 6, a pipe 8 for discharging generator gases, a partial oxidation channel 9 with thermal insulation 10, with a vapour supply manifold 12 into the space at the output of the oxidation channel 9, as well as downpipes 13, ( fig. 2 ) supplying vapour from the upper vapour manifold 14 to the vapour supply manifold 12.
  • a slag removal chamber 11 is installed in the lower part of the housing.
  • Fig. 2 presents the A-A section ( Fig. 1 ) of the gas producer, which shows a variant of arrangement of the vapour supply vants 15 in the vapour supply manifold 12.
  • Fig. 3 shows a diagram of the burner device 4 with a built-in diffusion burner 7 with an air supply channel 16, with a fuel supply channel 17 (for example, fuel oil or gas fuel), with ignition electrodes 18, a mixing diffuser 19, with an oxygen supply channel 20 and a vapour supply channel 21.
  • Fig. 4 shows a diagram of the gas producer according to Fig.
  • FIG. 5 shows a diagram of the gas producer according to Fig. 1 , supplemented by toroid-shape tanks 27 for heating vapour and cooling the thermal insulation of the wall of the gas producer housing 1, a vapour input pipe 23 into the coil 22, a vapour distribution unit 24 into the vapour mixing unit with carbonaceous feedstock 25 and into the manifold 14, a coal supply pipe 26 into the mixing unit 25.
  • Fig. 5 shows a diagram of the gas producer according to Fig. 1 , supplemented by toroid-shape tanks 27 for heating vapour and cooling the thermal insulation of the wall of the gas producer housing 1, a vapour input pipe 23 into the coil 22, a vapour distribution unit 24 into the vapour mixing unit with carbonaceous feedstock 25 and into the manifold 14, a coal supply pipe 26, U-tubes 28 connecting toroid-shaped containers 27 among themselves.
  • vapour enters the coil 22 through the nozzle 23 ( Fig. 4 ) where it is heated by the outgoing producer gases through the pipe 8 discharging producer gases.
  • vapour enters the vapour distribution node 24, where it is divided into 2 flows.
  • Part of the vapour enters the mixing unit 25, where the vapour picks up fine carbonaceous feedstock for example, coal dust coming through the nozzle 26, and the resulting coal-vapour mixture enters through the nozzle 6 (an ejection device or a sluice (not shown in the drawing)) into the burner device.
  • the burner device is a combined burner 4 ( Fig.3 ) in the center of which there is a diffusion burner 7 for burning liquid or gaseous fuel in the air.
  • the combustion products of the diffusion burner with a temperature of 1500-2000°C create the centre of the gas stream whirled by the mixing diffuser 19 of the burner 7 mixing the oxygen flows entering through the nozzle 5 into the channel 20 and the vapour-coal mixture entering through the nozzle 6 into the channel 21.
  • the process according to (2) will be shifted to the right.
  • the principle of Le Chatelier establishes that in case of an outside impact on a system in a state of equilibrium by means of a change in one of the factors determining the equilibrium, the direction of the process which weakens such impact in the system increases. Since the reaction (2) produces 2 moles of gas (CO and H2 instead of one mole of H2O) with an increase in pressure as a result of an increase in the volume of gases, then by decreasing the pressure in the reactor, it is possible to force the system to return to equilibrium, accelerating the reaction (2) with production of CO and H2 gases.
  • the reaction (1) is exothermic, the temperature increase will lead to the shift of equilibrium to the left (i.e. towards the feedstock) according to the Le Chatelier principle.
  • the limit is the temperature of 1000°C (it is proved by the equilibrium constant dynamics [3, p.102] and experimental data [2, p.30]). It means that the supply of water vapour at the output of the oxidation channel will allow the reaction (1) to develop and reduce the gases temperature to 700-800°C preventing it from rising above 900-1000°C. Therefore, it is optimal to maintain the temperature at the output of the oxidation channel in the range of 800-1000 0 C.
  • the size dimensions must ensure that the burning particle stays in the channel at least for as long as its burnup time (significantly increasing thermal efficiency of the process) which critically depends on the size of the burned particle. For example, an anthracite particle with a diameter of 100 microns burns up in oxygen for 7.1 seconds, but a particle with a diameter of 50 microns burns up for 0.413 seconds [3, p.210]. Knowing the particle size of the gasified feedstock and its hourly consumption, it is easy to calculate the size dimensions of the oxidation channel.
  • the burner device preferably embedded in the lid of the gas producer, is a combined diffusion burner in the center of which along the axis the actual diffusion burner for burning gaseous or liquid fuel is embedded. It is equipped with annular channels arranged coaxially around the built-in diffusion burner designed with the possibility of supplying oxygen-containing gas, carbonaceous feedstock and water vapour to these annular channels. It means the source of additional heat for igniting the mixture and maintaining a stable oxidation process in the proposed method is the heat of the combustion products of liquid or gaseous fuel fed along the flow of the reacting oxygen vapour mixture and carbonaceous feedstock.
  • Such a scheme of combustion process allows obtaining a stable ignition of the two-phase flow and maintaining its combustion until there is stable heat generation according to reaction (3) and compensating for heat losses in the reaction of carbon and carbon monoxide with water vapour.
  • Thermodynamic calculations of variants of such process show that the power of such a built-in burner comprises 10-25% of the power of the carbon burned by the reaction (3) and it is sufficient for organizing a stable process with an inflow temperature not exceeding 1100 0 C.
  • the proposed method allows for stable ignition and combustion in the resulting two-phase flow both on the surface of the particle and in the gas phase due to the stable supply of additional thermal energy from combustion products coming from an integrated burner device in which liquid or gaseous fuel is burned.
  • the combustion products from the burner device enter the partial oxidation channel along the axis of the channel, mixing with carbonaceous feedstock and oxygen vapour mixture.
  • Adjustment of flow rates of vapour, coal and oxygen in the oxidation channel 9 helps to set the temperature of 900-1100° C monitored by thermal sensors (not shown in the drawings).
  • the second part of the vapour from the distribution unit 25 through the pipes 13 enters the vapour supply manifold 12 and through the vents 15 is fed into the space at the output of the oxidation channel 9, where carbon monoxide is oxidized to carbon dioxide to produce hydrogen.
  • the calculated amount of vapour should in total provide cooling to a temperature not higher than 900-1000°C to prevent reverse reactions according to formula (1).
  • the resulting producer gases are fed through the producer gas output pipe 8 for cooling and purification and further processing (for example, for organic synthesis or to a membrane separator with further supply of the resulting hydrogen for coal hydrogenation).
  • the bulk of the slag and ash formed as a result of coal combustion enters the slag removal chamber 11. They are disposed of by the system afterwards.
  • the selection of size dimensions of the partial oxidation channel was determined by the residence time of combustion products in the oxidation channel. This value should preferably be longer than the combustion time of the biggest particle of the feedstock.
  • the combustion time of a particle with the size of 50 microns was 0.41 seconds, and with the size of 100 microns - 7 seconds. Under the condition of the complete reaction of coal in the oxygen vapour flow about 826 liters of gases were obtained at a temperature of 1000 0 C per second.
  • the residence time of the particles in the oxidation chamber was 7.9 seconds, which exceeded the theoretical combustion time of a coal particle of the biggest size.
  • Oxygen consumption per 1 ton of dry coal was 300 m 3 per hour, vapour consumption per 1 ton of dry coal was 370 - 430 kg.
  • the oxygen consumption was 644 m 3 per ton of dry coal, and the vapour consumption was only about 100 kg per ton of dry coal. It is obvious that the hydrogen yield according to the proposed method and device is 2 times higher than that of the prototype, oxygen consumption is 2 times lower.
  • the process temperature is lower (1100° C) too, compared to the prototype in which the process takes place at a temperature of 1400-1600°C.
  • the water vapour consumption is almost 4 times higher, but the elevated hydrogen yield is precisely determined by decomposition of water.
  • the given example of a specific implementation of the claimed method and device for its implementation shows that in the installation of the proposed gas producer, the results obtained on the hydrogen yield significantly exceed the hydrogen yield indicators compared to the prototype.
  • the total consumption of water vapour for partial oxidation of coal was 370-430 kg per 1 ton of coal.
  • Oxygen consumption was 300 m 3 per ton of coal.
  • the total yield of hydrogen was about 65 kg per hour, while in the prototype it is about 32 kg per hour.
  • the proposed invention can find wide application in gasification of carbonaceous feedstock, due to ensuring efficient gasification in a parallel flow of carbonaceous feedstock, such as coal, brown coal, peat, wood, coke, soot or other types of gaseous, liquid or solid fuels, or mixtures thereof in order to obtain producer gas with the highest possible hydrogen concentration.
  • carbonaceous feedstock such as coal, brown coal, peat, wood, coke, soot or other types of gaseous, liquid or solid fuels, or mixtures thereof in order to obtain producer gas with the highest possible hydrogen concentration.
  • the required parameters of the produced gas are easily regulated by changing the flow rates of oxygen, vapour, gasified feedstock and the power of the built-in burner.
  • the gas producer can be used in the chemical, carbon and petrochemical industries (ammonia, methanol, synthetic fuels, etc.), coke and gas, energy and other related industries for processing carbonaceous feedstock to produce energy and gases. Elevated concentration of hydrogen in the technical gases produced in the proposed device will allow efficiently disposing of heavy oil residues at oil refineries together with producing high-quality motor fuels.
  • the proposed device can become the main basic device for chemical processing of coal. Such device is equally essential both for processing coal by hydrogenation and for obtaining synthesis gas from coal.
EP21818532.0A 2020-06-05 2021-05-31 Procédé de gazéification de matière première contenant du carbone et dispositif de mise en oeuvre Pending EP4163352A1 (fr)

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RU2020118732A RU2744602C1 (ru) 2020-06-05 2020-06-05 Способ газификации углеродсодержащего сырья и устройство для его осуществления
PCT/RU2021/000230 WO2021246904A1 (fr) 2020-06-05 2021-05-31 Procédé de gazéification de matière première contenant du carbone et dispositif de mise en oeuvre

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LU85468A1 (fr) * 1984-07-16 1986-02-12 Cockerill Mech Ind Sa Dispositif de gazeification de dechets
RU2237079C1 (ru) * 2003-05-19 2004-09-27 Михайлов Виктор Васильевич Газификатор углеродсодержащего сырья
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