WO2006003454A1 - Procede pour traiter une matiere carbonee - Google Patents

Procede pour traiter une matiere carbonee Download PDF

Info

Publication number
WO2006003454A1
WO2006003454A1 PCT/GB2005/002657 GB2005002657W WO2006003454A1 WO 2006003454 A1 WO2006003454 A1 WO 2006003454A1 GB 2005002657 W GB2005002657 W GB 2005002657W WO 2006003454 A1 WO2006003454 A1 WO 2006003454A1
Authority
WO
WIPO (PCT)
Prior art keywords
chamber
carbonaceous material
fluid
inlet
burner
Prior art date
Application number
PCT/GB2005/002657
Other languages
English (en)
Inventor
Christopher Edward Dodson
Martin Alexander Groszek
Original Assignee
Mortimer Technology Holdings Limited
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mortimer Technology Holdings Limited filed Critical Mortimer Technology Holdings Limited
Publication of WO2006003454A1 publication Critical patent/WO2006003454A1/fr

Links

Classifications

    • 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
    • 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
    • C10J3/487—Swirling or cyclonic 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
    • 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
    • C10J2200/39—Gasifiers designed as centrifuge
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1215—Heating the gasifier using synthesis gas as fuel
    • 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
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the present invention relates to a process for treating a carbonaceous material such as waste coal or low grade coal to produce a mixture comprising volatiles and char particles, which can then be combusted.
  • a toroidal bed (TORBED (RTM) ) reactor and process is described in European Patent No. 0 068 853 and US Patent No. 4 479 920.
  • a particulate material to be treated is embedded and centrifugally retained within a compact, but turbulent, toroidally circulating bed of particles which circulate about an axis of the processing chamber.
  • the particles within the bed are circulated above a plurality of fluid inlets arranged around the base of the processing chamber.
  • the fluid inlets are preferably arranged in overlapping relationship and the particles are caused to circulate around the bed by the action of a processing fluid, for example a gas injected into the processing chamber from beneath and through the fluid inlets.
  • the fluid inlets may, for example, be a plurality of outwardly radiating, inclined vanes arranged around the base of the processing chamber.
  • the toroidal bed reactor provides a rapidly mixing bed which can be used to circulate particulates toroidally through a zone in a process chamber where an interaction occurs with a gas stream.
  • Waste coal (a term that also encompasses low grade coal) is generally considered to have little or no commercial value. It is therefore treated as a waste rial and is therefore often disposed.
  • the present invention provides a process for the combustion of carbonaceous material containing volatiles, the process comprising: (i) providing a toroidal bed reactor comprising a chamber having an inlet and an outlet;
  • the carbonaceous material will typically comprise waste , a term that also encompasses low grade coal. All s of coal from lignite to anthracite are encompassed.
  • the carbonaceous material is pyrolysed in the toroidal reactor to result in a mixture comprising a gaseous component and a fine particulate component.
  • the fine particulate component comprises at least partially devolatised particles of the carbonaceous material, for example carbonaceous char particles.
  • the particles preferably have a d50 particle size of 100 microns or less, more preferably 50 microns or less.
  • the gaseous component comprises the volatiles from the carbonaceous material.
  • the combustible volatile gas typically comprises one or more of carbon monoxide, hydrogen, and low molecular weight hydrocarbons, the proportions varying between different sources.
  • the carbonaceous material for example waste coal
  • the carbonaceous material can be introduced into the chamber of the toroidal bed reactor in a non-dry state, in other words while it is still wet or damp. Thus, no initial drying step is required.
  • the carbonaceous material typically has a particle "e size distribution of 90-100% less than 25 mm, erably less than 10 mm, more preferably less than 5 mm.
  • An important feature of the present invention is that the carbonaceous material, for example waste coal, can be introduced into the chamber of the toroidal bed reactor in a non-milled state. Thus, no initial milling step is required.
  • the carbonaceous material for example waste coal, typically has a Calorific Value of 5000 to 35000 kJ/kg, preferably 8000 to 29000 kJ/kg.
  • Waste coal is usually relatively finely divided and often arises as a byproduct of coal cleaning or beneficiation processes that are used in the production of a marketable coal product.
  • the flow of fluid within the chamber will typically have a horizontal and a vertical velocity component.
  • the chamber will typically comprise a plurality of fluid inlets at or adjacent a base thereof.
  • a fluid is directed through the fluid inlets at the base of the chamber to generate the substantially circumferentially directed flow of fluid within the chamber.
  • the fluid inlets will typically impart both a horizontal and vertical velocity component to the fluid.
  • the fluid inlets may comprise, for example, a plurality of outwardly radiating, inclined vanes at or adjacent the base of the chamber.
  • the fluid may be heated before and/or after entry into the chamber. This allows for thermal transfer between the fluid and the carbonaceous material.
  • the fluid temperature measured in the reactor may be in the range of from 500 to 'C, preferably from 550 to 750°C, still more preferably i 600 to 700°C, still more preferably from 630 to670°C, still more preferably approximately 650°C.
  • the carbonaceous material may be heated by combustion of a part thereof in the chamber.
  • the fluid may comprise, for example, air or an oxygen- containing gas such as, for example, an exhaust gas from a combustion process.
  • a restricted oxygen supply allows just enough combustion to occur to provide the heat needed for pyrolysis. If a non-oxygen containing fluid is used, then it is preferably heated to a temperature of from 750 to 1000°C to provide the necessary heat energy for the pyrolysis.
  • the fluid preferably has an oxygen content in the range of from 2 to 21% by volume, preferably from 3 to 10% by volume.
  • the oxygen content of the process gas stream entering the toroidal reactor is controlled so that just sufficient carbonaceous material and/or volatiles are combusted to maintain the reactor temperature at 600 to 700°C.
  • the fluid may react chemically with the carbonaceous material.
  • a reactant may be added to the toroidally circulating bed of particles to effect reduction of any gaseous emissions such as, for example, sulphur dioxide or oxides of rogen from the reactor.
  • gaseous emissions such as, for example, sulphur dioxide or oxides of rogen from the reactor.
  • reactants include or more of calcium carbonate, calcium oxide and ammonia.
  • the processing chamber contains a bed of particulate material which circulates about an axis of the chamber when the flow of fluid is generated, wherein the carbonaceous material interacts with the fluid.
  • the circulating bed particles will typically define substantially uniform tortuous paths along which particles of the carbonaceous material travel.
  • the mean terminal velocity of the particles of the bed may preferably be such that there is little or substantially no migration thereof to the outlet until such time as sufficient comminution of the particles has occurred.
  • the circulating bed particles provide a turbulent environment within which gas/particles heat and mass transfer properties are enhanced. This consequently enhances heat transfer to or from the carbonaceous material.
  • a tortuous/labyrinthine flow type path is provided, which increases the effective residence time of the carbonaceous material in the processing chamber, hence increasing the time for heat and/or mass transfer between the fluid and particles.
  • the circulating bed of particles may also act as a heat-sink.
  • the carbonaceous material will generally enter the chamber below and/or adjacent to the circulating bed particles in order to contact therewith.
  • the inlet is vertically spaced above the fluid inlets at the base of the chamber and the circulating bed, then the carbonaceous material will fall down through the chamber, under the action of gravity, on to the circulating bed. This may be achieved by, for example, a gravity feed mechanism provided i vertical wall of the chamber.
  • the pressure drop through the chamber of the toroidal reactor is typically less than 400 Pa.
  • the process temperature in the chamber is typically in the range of from 550 to 750 0 C, more typically from 600 to 700 0 C, still more typically from 630 to 670 0 C.
  • the burner is preferably a pulverized fuel burner and is a conventional piece of apparatus that is known in the art.
  • Commercial suppliers such as Saacke of Germany and Coen of the United States provide such pulverized fuel burners.
  • they comprise double vortex mixing between pneumatically conveyed coal particles and the requisite combustion air.
  • the burner combustion zone(s) or ⁇ flame' is preferably operated at a temperature in excess of 900 0 C, more preferably in excess of 1000 0 C, still more preferably in excess of 1100 0 C.
  • the combustion step or steps in the burner preferably results in the production of pozzolanic fly ash.
  • the mixture comprising the gaseous component and the fine particulate component is removed from the chamber through the outlet thereof, at least a portion of the fine particulate component may be removed from the mixture before the combustion step in the burner.
  • This may be achieved using, for example, a cyclone fluidly connected to the outlet of the chamber and the inlet of the burner, whereby r said mixture is removed from the chamber through the et thereof it passes to the cyclone, wherein at least a portion of the fine particulate component is separated from the gaseous component, and wherein the gaseous component and any residual fine particulate is then passed to the burner through the inlet thereof.
  • the fine particulate component thus removed is preferably substantially free of volatiles and may therefore be used as an environmentally friendly fuel.
  • the fine particulate may be supplied in any suitable form such as, for example, briquettes.
  • the present invention provides an apparatus for carrying out a process as herein described, the apparatus comprising:
  • a toroidal bed reactor comprising (i) a chamber having an inlet for introducing carbonaceous material into the chamber, (ii) means for heating the contents of the chamber, and (iii) means for generating a substantially circumferentially directed flow of fluid within the chamber to cause, in use, the carbonaceous material to circulate rapidly about an axis of the chamber in a toroidal band, whereby the carbonaceous material is pyrolysed and thermally decrepitated to result in a mixture comprising a gaseous component and a fine particulate component, and (iv) an outlet for exhausting the said mixture from the chamber; and (b) a burner having an inlet coupled either directly or indirectly to the outlet of the chamber of the toroidal bed reactor.
  • the apparatus may further comprise a cyclone in fluid unication with the outlet of the chamber and the inlet of the burner. Accordingly, after the mixture is exhausted from the chamber it passes to the cyclone, wherein at least a portion of the fine particulate component is separated from the gaseous component, and wherein the gaseous component and any residual fine particulate is then injected into the burner through the inlet thereof.
  • the inlet for the carbonaceous material may be located adjacent a base of the chamber and the outlet will generally be spaced downstream from the inlet.
  • the inlet is preferably located at a position above the fluid inlets of the chamber.
  • the outlet will generally be vertically spaced above the inlet of the processing chamber, although the inlet may be located adjacent thereto. Both the inlet and the outlet may be provided in a top portion of the chamber.
  • the carbonaceous material may be introduced into the processing chamber by injecting it through the inlet under the influence of a compressed gas such as compressed air and/or an inert gas such as nitrogen, CFC and other noble/mono-atomic gases.
  • a compressed gas such as compressed air and/or an inert gas such as nitrogen, CFC and other noble/mono-atomic gases.
  • the inlet is located above the fluid inlets at the base of the chamber and the carbonaceous rial is introduced into the chamber by a gravity feed anism, for example using an air lock device such as a rotary valve.
  • the gravity feed mechanism may be provided in a vertical wall of the chamber.
  • the flow of fluid may be generated either before or after the carbonaceous material is introduced into the chamber.
  • the flow of fluid may be generated at the same time as the carbonaceous material is introduced into the chamber.
  • Air for example, may be used as the fluid.
  • the fluid may optionally be heated. .Heating may be achieved by any suitable means.
  • separate heating means may be provided for heating the processing chamber and its contents.
  • the means for heating the carbonaceous material can be the fluid itself and/or separate heating means for heating the processing chamber. Combustion of a portion of the carbonaceous material may also be relied on to heat the material.
  • the flow of the fluid through the chamber may be generated in a manner as described in EP-B-O 382 769 and EP- B-O 068 853, i.e. by supplying a flow of fluid into and through the processing chamber and directing the flow by means of the plurality of outwardly radiating and preferably overlapping fluid inlets arranged in the form of a disc and located at or adjacent to the base of the processing chamber.
  • the fluid inlets are inclined relative to the base of the chamber so as to impart rotational motion to the heating fluid entering the chamber, hence causing the heating fluid to circulate about a substantially vertical 3 of the chamber as it rises.
  • the fluid inlets may Drise, for example, a plurality of outwardly radiating vanes at or adjacent the base of the chamber.
  • the vanes are typically inclined relative the base and preferably disposed in overlapping arrangement.
  • FIG. 1 is a schematic illustration of a TORBED process reactor for use in the process and apparatus according to the present invention
  • FIG. 2 illustrates an arrangement for a TORBED process reactor combined with a conventional pulverised fuel burner
  • FIG. 3 illustrates another arrangement for a TORBED process reactor combined with a conventional pulverised fuel burner.
  • a generally cylindrical TORBED process chamber 1 has an inlet 5 and an outlet 10 spaced downstream therefrom.
  • a circular arrangement of overlapping fluid inlets for example vanes, wherein each inlet is inclined relative to the base.
  • Two fluid inlets are shown at 20 and 25.
  • the fluid inlets 20, 25 radiate outwardly from a central point towards the vertical wall of the chamber 1 and form part of a circular disc.
  • a flow of a fluid for example air, enters the chamber 1 via an inlet 7 and passes through the fluid ⁇ ts 20, 25 at the base 15 of the chamber 1.
  • the mgement of the fluid inlets 20, 25 imparts rotational motion to the fluid entering the chamber 1 so that the fluid circulates about a substantially vertical axis of the chamber 1 as it rises.
  • the fluid swirls around the chamber 1 in a turbulent fashion and then exhausts from the chamber via outlet 10.
  • a bed of particles 30 is in the chamber 1. This is an optional feature.
  • a feed hopper 35 and venturi arrangement 40 are provided, for example, to supply a carbonaceous material such as waste coal 45 to be treated, under compressed air injection, through the inlet 5 into the chamber 1.
  • a carbonaceous material such as waste coal 45 to be treated, under compressed air injection
  • the bed particles 30 circulate about a substantially vertical axis of the chamber 1 in an annular region thereof.
  • the waste coal 45 is then injected into the chamber 1 and contacts immediately or almost immediately with the (optional) circulating bed particles 30. Because of their size, density and terminal velocity, there is little or substantially no migration of the bed particles 30 to the outlet 10 until such time as sufficient comminution of the particles has occurred.
  • the fluid may be pre-heated if desired.
  • means may be provided to heat the contents of the chamber 1.
  • the contents of the TORBED reactor chamber 1 are cally maintained at a temperature in the range of from to 700°C.
  • the effect of the TORBED reactor is to thermally shatter and devolatise the waste coal 45, thereby converting it into a fine particulate component, for example char, and a gaseous component made up of the volatiles in the waste coal.
  • the resulting mixture comprising the fine particulate component and the gaseous component may then be exhausted from the outlet 10 and then injected directly into a conventional pulverised fuel burner.
  • some or all . of the fine particulate component may be removed by means of, for example, a cyclone disposed between the TORBED reactor and the pulverised fuel burner and fluidly connected therewith. This is illustrated in Figures 2 and 3.
  • the pulverised fuel burners can achieve a temperature of at least HOO 0 C.
  • waste coal can be introduced into the chamber 1 of the TORBED reactor without any pre-treatment steps.
  • the waste coal can be provided while it is still wet or damp: no initial drying step is required.
  • the waste coal typically has an average size of from 1 to 25 mm, more typically from 1 to 15 mm.
  • An important feature of the present invention is that the waste coal can be introduced into the chamber of the TORBED reactor in a non-milled state. Thus, no initial milling step is fired.
  • FIG 2 there is shown a self-explanatory schematic flow diagram in respect of a fast pyrolysis test plant.
  • a hopper for input fuel is shown at 50, a feed rate control is shown at 51, and a FD fan is shown at 52.
  • fuel and air are fed into a TORBED reactor, which is shown at 53.
  • An optional cyclone is shown at 54, and an afterburner is shown at 55.
  • a water-cooled heat exchanger is shown at 56, an ID and recycle fan is shown at 57, and a stack shown at 58.
  • the various stages are in fluid communication with one another.
  • FIG 3 there is shown a self-explanatory schematic flow diagram in respect of fast pyrolysis and decrepitation of coal.
  • a hopper for input fuel (coal) is shown at 60 and a feed rate control mechanism is shown at 61.
  • a recycle fan is shown at 69.
  • fuel and air are fed into a TORBED reactor, which is shown at 63.
  • An optional cyclone is shown at 64, which can be used to separate devolatilised coal.
  • a boiler is shown at 65, which is coupled to the reactor 63 or the intermediate, optional cyclone 64.
  • a FD fan is shown at 62, which is coupled to the boiler 65.
  • a dust collector is shown at 66 also coupled to the boiler 65.
  • An ID fan is shown at 67 and a stack is shown at 68. Again, as shown in the diagram, the various stages are in fluid communication with one another.
  • the present invention involves the use of a toroidal bed reactor as herein described to devolatise low grade or waste coal.
  • the waste coal is thermally comminuted to result in a dust, typically having a d50 of less than 100 ⁇ m, more typically less than 50 ⁇ m.
  • the simultaneous pyrolysis and thermal decrepitation of the low grade or waste coal means that the resulting volatile laden gas stream, which contains the fine particulate coal char particles, can be passed directly to a conventional pulverised fuel burner.
  • the process of the present invention enables waste or low grade coal to be combusted at high temperatures (up to stoichiometric conditions) in a pulverised fuel burner without: (i) drying of the coal; and/or milling of the coal; and/or accretions within the combustion system.
  • This differs from the known techniques in a number of respects. Darticular, in order to operate conventional pulverised L burners, the coal needs to be dry and milled to a fine particle size prior to injection into the burner.
  • the present invention uses a rapid heat and mass transfer toroidal reactor to thermally shatter the coal so that neither drying nor milling is required.
  • any combustion system it is beneficial to operate at the highest possible temperature, normally at or around stoichiometric balance, to maximise the thermal efficiency of the subsequent heat usage.
  • pulverised fuel burners can achieve temperatures well in excess of 1100 0 C at which point the resulting fly ash is pozzolanic and has a value in the cement industry.
  • the present invention allows waste, wet and low CV coals to be combusted at high temperatures, above the slagging point, producing pozzolanic fly ash and a high thermal efficiency.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

La présente invention concerne un procédé pour la combustion d'une matière carbonée qui contient des éléments volatils. Ce procédé consiste (i) à disposer d'un réacteur à lit toroïdal (53) comprenant une chambre qui présente une entrée et une sortie, (ii) à disposer d'un brûleur à combustible pulvérisé (55) comprenant une entrée qui est couplée directement ou indirectement à la sortie de la chambre du réacteur à lit toroïdal (53), (iii) à introduire (50, 51) de la matière carbonée dans la chambre du réacteur à lit toroïdal (53) par l'entrée de celle-ci, (iv) à créer un courant de fluide dirigé de manière principalement circonférentielle à l'intérieur de la chambre, afin de forcer la matière carbonée à circuler rapidement autour d'un axe de la chambre, dans une bande toroïdale, à chauffer la matière carbonée, la transformant en un mélange qui contient un composant gazeux et un composant sous forme de fines particules, (v) à retirer ce mélange de la chambre par la sortie de celle-ci, à faire passer le mélange directement ou indirectement dans le brûleur (55) par l'entrée de celui-ci, puis (vi) à mettre en oeuvre la combustion dans ledit brûleur.
PCT/GB2005/002657 2004-07-07 2005-07-07 Procede pour traiter une matiere carbonee WO2006003454A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB0415268A GB2416583A (en) 2004-07-07 2004-07-07 A torodial reactor for converting carbonaceous material to a mixture of gases and particles for combustion
GB0415268.2 2004-07-07

Publications (1)

Publication Number Publication Date
WO2006003454A1 true WO2006003454A1 (fr) 2006-01-12

Family

ID=32865617

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB2005/002657 WO2006003454A1 (fr) 2004-07-07 2005-07-07 Procede pour traiter une matiere carbonee

Country Status (2)

Country Link
GB (1) GB2416583A (fr)
WO (1) WO2006003454A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018111151A1 (fr) 2016-12-16 2018-06-21 Сергей Юрьевич ВИЛЬЧЕК Dispositif doté d'un lit fluidisé jaillissant et procédé de son fonctionnement
WO2019092407A1 (fr) * 2017-11-07 2019-05-16 Mortimer Technology Holdings Ltd Système et procédé de traitement de matériaux
US10723627B2 (en) 2017-11-08 2020-07-28 Tigerstone Technologies Limited Production of activated carbon
CN111960526A (zh) * 2020-10-21 2020-11-20 山东神驰石化有限公司 一种丙烷脱氢用湿式氧化反应器

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB201012429D0 (en) 2010-07-23 2010-09-08 Mortimer Technology Ltd Gasification of carbonaceous feedstock

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4479920A (en) * 1981-06-29 1984-10-30 Torftech Limited Apparatus for processing matter in a turbulent mass of particulate material
WO2001030943A1 (fr) * 1999-10-25 2001-05-03 Mortimer Technology Holdings Ltd. Procede de production d'un combustible gazeux
WO2001058244A2 (fr) * 2000-02-02 2001-08-16 Coöperatief Advies En Onderzoeksburo U.A. Ecofys Systeme comprenant un appareil et un procede, destine a generer de l"energie a partir de biomasse
EP1312662A2 (fr) * 2001-05-07 2003-05-21 Cirad-Foret Procédé de gazéification de biomasse, appareil et utilisation

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020007772A1 (en) * 1995-10-13 2002-01-24 N. V. Kema Method and installation for recovering energy from biomass and waste

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4479920A (en) * 1981-06-29 1984-10-30 Torftech Limited Apparatus for processing matter in a turbulent mass of particulate material
WO2001030943A1 (fr) * 1999-10-25 2001-05-03 Mortimer Technology Holdings Ltd. Procede de production d'un combustible gazeux
WO2001058244A2 (fr) * 2000-02-02 2001-08-16 Coöperatief Advies En Onderzoeksburo U.A. Ecofys Systeme comprenant un appareil et un procede, destine a generer de l"energie a partir de biomasse
EP1312662A2 (fr) * 2001-05-07 2003-05-21 Cirad-Foret Procédé de gazéification de biomasse, appareil et utilisation

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018111151A1 (fr) 2016-12-16 2018-06-21 Сергей Юрьевич ВИЛЬЧЕК Dispositif doté d'un lit fluidisé jaillissant et procédé de son fonctionnement
CN111655364A (zh) * 2016-12-16 2020-09-11 埃姆皮瑞欧有限公司 具有环形喷动流化床的设备及其操作方法
WO2019092407A1 (fr) * 2017-11-07 2019-05-16 Mortimer Technology Holdings Ltd Système et procédé de traitement de matériaux
US10723627B2 (en) 2017-11-08 2020-07-28 Tigerstone Technologies Limited Production of activated carbon
CN111960526A (zh) * 2020-10-21 2020-11-20 山东神驰石化有限公司 一种丙烷脱氢用湿式氧化反应器
CN111960526B (zh) * 2020-10-21 2020-12-29 山东神驰石化有限公司 一种丙烷脱氢用湿式氧化反应器

Also Published As

Publication number Publication date
GB2416583A (en) 2006-02-01
GB0415268D0 (en) 2004-08-11

Similar Documents

Publication Publication Date Title
US8309052B2 (en) Carbon heat-treatment process
US5159886A (en) Process of combusting coal in a circulating fluidized bed
US6883442B1 (en) Process for the production of a gaseous fuel
US8882493B2 (en) Control of syngas temperature using a booster burner
US3508506A (en) Process and apparatus for reduction of unburned combustible in fly ash
BG64909B1 (bg) Метод и устройство за пиролиза и газифициране на органични вещества или смеси от органични вещества
JPH11501116A (ja) エネルギー生成のために生物燃料又は屑材料を利用する方法と装置
US9205406B2 (en) Operational conditions and method for production of high quality activated carbon
US20100307390A1 (en) Method and Apparatus for Incineration of Combustible Waste
WO2006003454A1 (fr) Procede pour traiter une matiere carbonee
US4986199A (en) Method for recovering waste gases from coal partial combustor
JP5118338B2 (ja) 炭化・ガス化方法並びにシステム
US7004089B2 (en) Combined fluidized bed and pulverized coal combustion method
Chyang et al. Emission of nitrogen oxides in a vortexing fluidized bed combustor
JP4396929B2 (ja) バイオマス燃料の乾燥装置及び方法
US5070821A (en) Rotary fluid bed gasifier for boilers or furnaces
RU2366861C1 (ru) Двухступенчатый способ плазменно-термической подготовки кускового топлива к сжиганию и установка для его осуществления
US5307765A (en) Rotary fluid bed used to gasify and combust oil-in water emulsions
Prompubess et al. Co-combustion of coal and biomass in a circulating fluidized bed combustor
CN112628748A (zh) 一种烘焙碳化耦合等离子体焚烧有机固废处置工艺
RU2658450C1 (ru) Способ факельного сжигания низкосортных углей в котельных установках
US20070295250A1 (en) Oxygen-enhanced combustion of unburned carbon in ash
RU2631959C1 (ru) Способ сжигания угля, подвергнутого механической и плазменной обработке
CN218348670U (zh) 危险废物处理系统的燃烧室
JP4393977B2 (ja) 難燃性炭素粉を燃焼するバーナ構造とそのバーナによる燃焼方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KM KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NG NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SM SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU LV MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
NENP Non-entry into the national phase

Ref country code: DE

WWW Wipo information: withdrawn in national office

Country of ref document: DE

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established
122 Ep: pct application non-entry in european phase