EP2014744B1 - Method for processing condensed fuel by gasification and a device for carrying out said method - Google Patents

Method for processing condensed fuel by gasification and a device for carrying out said method Download PDF

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Publication number
EP2014744B1
EP2014744B1 EP07747908.7A EP07747908A EP2014744B1 EP 2014744 B1 EP2014744 B1 EP 2014744B1 EP 07747908 A EP07747908 A EP 07747908A EP 2014744 B1 EP2014744 B1 EP 2014744B1
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EP
European Patent Office
Prior art keywords
reactor
fuel
zone
combustion
axis
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Not-in-force
Application number
EP07747908.7A
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German (de)
English (en)
French (fr)
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EP2014744A4 (en
EP2014744A1 (en
Inventor
Sergei Olegovich Dorofeenko
Andrei Yurievich Zaichenko
Alexandr Alexandrovich Zhirnov
Georgy Borisovich Manelis
Evgeny Viktorovich Polianchik
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Institut Problem Khimicheskoi Fiziki Rossiiskoi Ak
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Institut Problem Khimicheskoi Fiziki Rossiiskoi Ak
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Priority to PL07747908T priority Critical patent/PL2014744T3/pl
Publication of EP2014744A1 publication Critical patent/EP2014744A1/en
Publication of EP2014744A4 publication Critical patent/EP2014744A4/en
Application granted granted Critical
Publication of EP2014744B1 publication Critical patent/EP2014744B1/en
Priority to CY20161100130T priority patent/CY1117202T1/el
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Anticipated expiration legal-status Critical

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Classifications

    • 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
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • 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
    • C10J3/005—Rotary drum or kiln 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/14—Continuous processes using gaseous heat-carriers
    • 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
    • C10J3/30—Fuel charging devices
    • 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
    • C10J3/32—Devices for distributing fuel evenly over the bed or for stirring up the fuel bed
    • 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
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J1/00—Removing ash, clinker, or slag from combustion chambers
    • F23J1/02—Apparatus for removing ash, clinker, or slag from ash-pits, e.g. by employing trucks or conveyors, by employing suction devices
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/304—Burning pyrosolids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2205/00—Waste feed arrangements
    • F23G2205/18—Waste feed arrangements using airlock systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/52002—Rotary drum furnaces with counter-current flows of waste and gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/01007—Thermal treatments of ash, e.g. temper or shock-cooling for granulation

Definitions

  • the present invention generally relates to methods for processing condensed fuels, including solid fuel wastes, by pyrolysis and by gasifying the organic constituents thereof in a dense layer to produce pyrolysis products and gas fuel used for power generation.
  • condensed fuels including solid fuel wastes, by pyrolysis and by gasifying the organic constituents thereof in a dense layer to produce pyrolysis products and gas fuel used for power generation.
  • SDW solid domestic waste
  • coals coals
  • oil-slime biologic mass
  • a scheme of gasifying solid organic fuels in countercurrent flow to a gasifying agent can be generally described as follows.
  • An oxygen-containing gasifying agent which possibly containing water and/or carbon dioxide are supplied into a combustion zone where oxygen reacts with carbon in a solid fuel in the form of coke or semi-coke at temperatures about 900-1500°C.
  • the gasifying agent is admitted into the reactor in countercurrent flow to the fuel so that at least part of the oxidizing gas is preliminary passed through a layer of hot solid combustion products that are already free from carbon. In this zone the solid combustion products are cooled and the gasifying agent is heated prior to entering the combustion zone.
  • RU-2-062284 (Manelis et al. ) discloses processing worn automobile tires; RU-2079051 and RU-2152561 (Manelis et al. ) disclose processing solid domestic waste, oil-slime and similar oil waste.
  • solid lump inert material is introduced into a reactor along with the processed fuel to provide, in particular, uniform gas permeability of the feed in the reactor.
  • Kiln gas preferably mixed with air, is used as a gasifying agent, the kiln gas portion in the gasifying agent being increased when the temperature in the combustion zone exceeds 1300°C, and reduced when the temperature in the combustion zone falls below 800°C.
  • a method of gasifying wastes is proposed in US 4,732,091 (Gould ).
  • the method comprises introducing a solid fuel into an upper section of a shaft kiln.
  • the fuel is caused to move at a controlled rate through a series of chambers horizontally separated by moveable grates, where the fuel is pyrolyzed and burned in countercurrent flow of a vapor/air gasifying agent.
  • the method includes loosening the waste in the course of treatment to provide uniform gas permeability and uniform movement of the processed feed material successively to drying, pyrolysis, gasification and cooling zones.
  • a method is also proposed for controlling the fuel entry into respective zones.
  • the prior art method suffers largely from the presence of moveable grates.
  • the moveable grates will be inevitably worn fast in high-temperature zones.
  • particles of dust and tars will deposit on the moveable units of the reactor and disturb its maintenance.
  • U.S. Patent 5743196 discloses a mobile waste incinerator that has a receiving chamber arranged to receive waste to be incinerated and an incineration chamber connected with the a the receiving chamber via a preparation chamber and provided with means for mixing the fuel with air and igniting a mixture, and means for discharging the wastes from the incineration chamber, the incineration chamber being connected with the preparation chamber so that hot gases from the incineration chamber are supplied into the preparation chamber, means for connecting the chambers with one another and closing chambers from one another.
  • the axis of the said incineration chamber being made tilted relative to a horizontal plane and can incline up to 25° and the chamber can perform sway rotation by the angle up to 45° for better waste mixing, fuel saturation and burning of waste, and its unloading during and after the preparation and incineration cycles.
  • Rotary kilns are also widely known. They are extensively used for burning cement and combustion of waste. Kiln rotation provides uniform mixing of the material processed. A rotary kiln is known to be used for gasification process, e.g. as taught in US 247,322 issued 30 September, 1881 .
  • Application US-2005051066 discloses a method of gasifying a solid fuel in a parallel gas/solid flow using a rotary kiln.
  • US 3,990,865 (Cybriwsky A. & Petersen G .) discloses gasification process carried out in a slightly tilted rotary kiln having a raw material inlet end arranged higher than the outlet end. Solid carbon-containing material is continuously fed into the rotary kiln.
  • the material which is introduced at a temperature below 600°F (315°C) passes through pre-heating and devolatilizing zones and is gradually heated to 1600°F (871°C); at this temperature the material loses its caking tendency and then enters a gasifying zone, where a vapor-containing oxidizing medium is admitted under the mixed layer, this resulting in formation of combustible gases containing hydrocarbon that are removed from the kiln side where the fuel is fed.
  • the object can be attained in a method for gasifying condensed fuels.
  • the present invention provides a method for processing a condensed organic fuel by gasifying, including: feeding a fuel into a cylindrical reactor; supplying an oxygen-containing gasifying agent into the reactor at the reactor side where the resultant residual solids accumulate; moving the fuel feed along the reactor axis; discharging the resultant residual solids from the reactor; driving-off the products of drying, pyrolysis and combustion as a gas product from the reactor such that gasification is carried out as the fuel successively resides in a heating/drying zone, a pyrolysis zone, a combustion (oxidation) zone and a cooling zone, and the gas flow is filtered through the fuel feed layer while passing successively through the cooling zone, the combustion zone, the pyrolysis zone and the heating/drying zone.
  • the important distinctive feature of the invention is that the combustion process in the dense layer is stabilized by rotating the reactor about an axis tilted relative to the horizon, at an angle in the range of from 40 to 65 degrees.
  • Fig.1 is a general schematic diagram of a device for implementing an embodiment of a method in accordance with the invention.
  • a method in accordance with the invention includes the following basic steps that are implemented in respective zones.
  • a condensed fuel in solid, liquid of paste state possibly including solid noncombustible components and moisture (hereinafter referred to as "fuel") is fed into a reactor to successively perform therein drying the fuel and then pyrolysis/gasification of combustible constituents of the fuel.
  • An oxygen-containing oxidizing gas e.g. air
  • Fuel passes through a number of zones in the reactor, as described below.
  • the fuel passes through a drying zone where the fuel temperature increases to 200°C owing to the heat exchange with the flow of gas product filtering through the fuel; in this zone the fuel is dried, and the gas flow is cooled before driving-off the latter from the reactor.
  • a drying zone where the fuel temperature increases to 200°C owing to the heat exchange with the flow of gas product filtering through the fuel; in this zone the fuel is dried, and the gas flow is cooled before driving-off the latter from the reactor.
  • gaseous products of drying, pyrolysis and gasification are removed from the reactor.
  • the fuel enters the pyrolysis and coking zone where the temperature increases gradually to 800°C owing to the heat exchange with the gas flow, and combustible constituents of the fuel are pyrolyzed to produce coke.
  • the coked fuel enters then a combustion and gasification zone, where the solid phase has a temperature of 700-1400°C.
  • the coke reacts with the hot oxidizing gas to produce a fuel gas.
  • Residual solids enter a cooling zone where they are cooled by the counter flow of the gasifying agent from the combustion temperature to a discharge temperature.
  • the oxidizing gas counter flow, filtering through the dense layer of residual solids, is in turn heated to a temperature close to the combustion temperature before it enters the combustion zone.
  • zones may be defined differently, e.g. based on the gas temperature, content of agents, etc. In particular, in US-A-4,732,091 the same zones are referred to differently.
  • the essential feature is that in the countercurrent interpenetrating flows of gas and solid feed material the oxidizing gas (gasifying agent) is pre-heated on residual solids, and hot gaseous combustion products will further transfer their heat to the raw fuel.
  • the invention allows the efficient inter-phase heat exchange that is advantageously provided by the process in the dense layer to be combined with mixing the processed material by action of gravity as the reactor rotates, which is typical to rotary kilns.
  • a condensed fuel is fed into a cylindrical reactor such that to form a dense layer of the fuel feed in the reactor.
  • An oxygen-containing gasifying agent is supplied into the reactor section where the resultant residual solids accumulate, and the fuel is gasified in the reactor by successively passing through the zones of drying, pyrolysis, combustion, gasification and cooling in a gas flow filtering through the dense fuel layer countercurrent to the fuel movement along the reactor axis with a predetermined time of holding in each of the zones.
  • the cylindrical reactor is mounted with its axis tilted at an angle relative to the horizon and rotated such that the material pours in the direction perpendicular to and along the reactor axis and fills the voids formed when the low-density material bums out.
  • the gasifying agent is supplied at the bottom end of the cylindrical reactor, while the gas product is removed at the opposite end.
  • the cylindrical reactor axis is tilted at an angle from 40 to 65 degrees relative to the horizon. With a tilt angle below the lower limit, bulk material will not form a dense layer in the tilted reactor. On the opposite, a layer of solid fuel will be formed with a gas flow above it. The gas flow is not filtered through the fuel, consequently the main advantage of gasification in a dense layer, highly efficient inter-phase heat exchange, will not be realized, as well as uniform process will not be provided over the reactor section. With a tilt angle above the aforementioned range the solid material will not be adequately mixed in case of "burnouts".
  • Optimum combination of conditions for the fuel movement along the reactor axis and uniform combustion zone structure will be attained with a tilt angle of the reactor axis relative to the horizon from 40 to 50 degrees.
  • the reactor rotation period should be sufficiently small to provide mixing of materials in the combustion zone. This will enable the invented process to be implemented in a reactor having a smaller length.
  • a sufficient rotation speed of the reactor must be provided. If the bulk velocity of discharging the residual solids is V,(m 3 /h), the average time of holding the residual solids in the combustion zone will be about ⁇ D 3 /4V (hour).
  • Reactor rotation period T should be preferably no more than approximately D 3 /4V (hour) to provide no less than triple mixing of the material for the time when it stays in the combustion zone.
  • the fuel processed is preferably a solid lump material which is sufficiently permeable to the filtering gas flow. If the fuel is insufficiently permeable, in particular, when fine-dispersed, liquid or paste fuels are processed, a noncombustible solid lump material is fed into the reactor along with the fuel to provide uniform gas permeability of the fuel feed in the reactor and improve conditions of mixing the material in the combustion zone in case of burnouts.
  • a noncombustible solid lump material is fed into the reactor along with the fuel to provide uniform gas permeability of the fuel feed in the reactor and improve conditions of mixing the material in the combustion zone in case of burnouts.
  • liquid or paste materials it is not obligatory to preliminary mix them with a solid lump material before feeding into the reactor, because uniform mixing will be provided by the reactor rotation.
  • the solid inert material added to the feed should preferably have a density different from that of the processed fuel.
  • the process is performed in a device for gasifying a condensed solid fuel including a feeder, a cylindrical reactor, a discharge unit, a gasifying agent supply unit, a gas product outlet, a driver for rotating the reactor, seals to provide gas tightness in the reactor rotation, wherein the cylindrical reactor is mounted such that its axis is tilted at a tilt angle from 40 to 65 degrees relative to the horizon; the feeder and the gas product outlet are arranged in the upper section of the reactor, while the discharge unit and the gasifying agent supply unit are arranged in the lower section of the reactor.
  • the tilt angle of the rotary reactor relative to the horizon is preferably from 40 to 50 degrees.
  • the holes in the reactor side surface are preferably equipped with free passage control means, such as controlled shutters.
  • the reactor can be discharged through a cone having an opening along the reactor axis, the cone secured in the lower section of the reactor, the opening diameter being smaller than half the internal diameter of the reactor.
  • the cylindrical reactor should have a sufficient length. To arrange the respective zones in the reactor, the following relationship between geometrical dimensions of the reactor should be observed: L ⁇ sin ⁇ > 3 ⁇ D ,
  • the use may made of both measuring the actual level (e.g. by a radiation sensor) and outputting a command to introduce the next portion of the fuel, and a feeder including a vertical cylinder having a smaller diameter than that of the rotary reactor, the lower end of the cylinder extending inside the upper section of the reactor.
  • the feeder maintains a constant level of the fuel feed in the reactor at the expense of pouring the fuel out from a vertical tube as the fuel is consumed in the reactor.
  • Condensed fuel F previously milled, if necessary, and to which a noncombustible solid material is added when needed, is introduced into a reactor 1 through a feeder 2 comprising a feed-lock chamber 3.
  • the fuel enters the reactor through a vertical cylinder 4.
  • the processed fuel level is maintained constant in the reactor owing to pouring the fuel out from the cylinder 4 as the reactor 1 rotates and filling in the material consumed in combustion and removal of ashes.
  • the material passes successively through a drying zone 4, a pyrolysis zone 6, a combustion zone 7 and a cooling zone 8.
  • residual solids R pour out through holes 9 equipped with shutters 10, and then they are discharged, continuously or in batches, through a gas-tight discharge unit 11 (a hydraulic lock shown schematically in the drawing).
  • a discharge velocity of the residual solids at which the combustion zone maintains the same position in the reactor, in the middle section of the reactor, is provided by the relationship between free passages of the holes 9, rotation speed of the reactor and consumption of an oxidizer admitted into the reactor.
  • Air A along with steam if required, is supplied by a compressor 12 into the lower section of the reactor.
  • Gas product G is driven-off from the upper section of the reactor and directed to further use which may include purification and combustion in a power equipment.
  • Temperatures in the respective zones are continuously measured, and when the temperatures go beyond the specified optimal ranges the control parameters: rotation speed of the reactor, air intake flow rate, vapor flow rate, are adjusted.
  • a level sensor monitors whether the amount of fuel is sufficient in the feeder, and as the fuel is exhausted fresh portions are fed via the feed-lock chamber 3. To match the discharge velocity of residual solids, free passages of the holes 9 are adjusted: they are increased when the discharge velocity exceeds a desired one, and reduced in the opposite case.
  • a mixture of sawdust with broken firebrick in the 2:1 ratio (by weight) was subjected to gasification in an experimental laboratory reactor made of quartz.
  • a tilt angle of the reactor axis relative to the horizon was varied from 5 to 90 degrees.
  • Direct observation has revealed that with a tilt angle below 22 degrees, no filtering of gas flow through a dense fuel layer takes place because of a cavity formed along the upper generating line of the reactor, through which cavity the gas flow passes over the fuel surface.
  • burnouts form in the fuel layer along the reactor walls within a short operation time, one of the burnouts eventually extending to the feed surface. In this situation the gas product starts burning directly above the feed surface in the reactor.
  • burn-out cavities fall down gradually as the reactor rotates.
  • an axis angle relative to the horizon smaller than 65 degrees, the rise of burnouts to the surface can be completely restrained and the combustion zone can be stabilized in the middle section of the reactor.
  • stable flame burning of the gas product is observed, and the residual solids are free from unburned carbon.
  • the combustion front is stabilized best of all when a tilt angle of the axis is from 40 to 50 degrees and the combustion zone dimension along the reactor axis is no more than half the reactor diameter. To provide the stabilized front, the rotation speed should exceed a predetermined value for each tilt angle.
  • the present Invention provides an efficient method for gasifying condensed fuels with high yield of gas fuel and high power efficiency.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
EP07747908.7A 2006-05-02 2007-04-24 Method for processing condensed fuel by gasification and a device for carrying out said method Not-in-force EP2014744B1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PL07747908T PL2014744T3 (pl) 2006-05-02 2007-04-24 Metoda oraz urządzenie do przetwarzania zagęszczonego paliwa przez zgazowanie
CY20161100130T CY1117202T1 (el) 2006-05-02 2016-02-16 Μεθοδος για την επεξεργασια συμπυκνωμενου καυσιμου με αεριοποιηση και συσκευη για την εκτελεση της εν λογω μεθοδου

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2006114599/03A RU2322641C2 (ru) 2006-05-02 2006-05-02 Способ переработки конденсированного горючего путем газификации и устройство для его осуществления
PCT/RU2007/000200 WO2007126335A1 (en) 2006-05-02 2007-04-24 Method for processing condensed fuel by gasification and a device for carrying out said method

Publications (3)

Publication Number Publication Date
EP2014744A1 EP2014744A1 (en) 2009-01-14
EP2014744A4 EP2014744A4 (en) 2012-04-11
EP2014744B1 true EP2014744B1 (en) 2015-11-18

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EP07747908.7A Not-in-force EP2014744B1 (en) 2006-05-02 2007-04-24 Method for processing condensed fuel by gasification and a device for carrying out said method

Country Status (7)

Country Link
EP (1) EP2014744B1 (ja)
JP (1) JP2009535478A (ja)
CA (1) CA2650979A1 (ja)
CY (1) CY1117202T1 (ja)
PL (1) PL2014744T3 (ja)
RU (1) RU2322641C2 (ja)
WO (1) WO2007126335A1 (ja)

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Publication number Priority date Publication date Assignee Title
RU2518623C1 (ru) * 2012-10-09 2014-06-10 Общество с ограниченной ответственностью "ЕВРОПРОФИЛЬ" (ООО "ЕВРОПРОФИЛЬ") Наклонный вращающийся цилиндрический реактор для переработки сыпучих материалов
RU2496071C1 (ru) * 2012-10-09 2013-10-20 Общество с ограниченной ответственностью "ЕВРОПРОФИЛЬ" (ООО "ЕВРОПРОФИЛЬ") Наклонный вращающийся реактор
GB2527829A (en) 2014-07-03 2016-01-06 Dps Bristol Holdings Ltd A gasifier
RU2584257C1 (ru) * 2015-01-28 2016-05-20 Александр Вадимович Ивлев Способ переработки конденсированного органического топлива путем газификации
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CA2650979A1 (en) 2007-11-08
PL2014744T3 (pl) 2016-04-29
CY1117202T1 (el) 2017-04-05
EP2014744A4 (en) 2012-04-11
JP2009535478A (ja) 2009-10-01
RU2322641C2 (ru) 2008-04-20
WO2007126335A1 (en) 2007-11-08
EP2014744A1 (en) 2009-01-14
RU2006114599A (ru) 2007-11-27

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