WO1986001821A1 - Dispositif de gazeification - Google Patents

Dispositif de gazeification Download PDF

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Publication number
WO1986001821A1
WO1986001821A1 PCT/GB1985/000412 GB8500412W WO8601821A1 WO 1986001821 A1 WO1986001821 A1 WO 1986001821A1 GB 8500412 W GB8500412 W GB 8500412W WO 8601821 A1 WO8601821 A1 WO 8601821A1
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WO
WIPO (PCT)
Prior art keywords
bed gasifier
fixed bed
fuel
grate
gasifier
Prior art date
Application number
PCT/GB1985/000412
Other languages
English (en)
Inventor
Jeremy Patrick Hagan
Original Assignee
The English Electric Company 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 The English Electric Company Limited filed Critical The English Electric Company Limited
Publication of WO1986001821A1 publication Critical patent/WO1986001821A1/fr

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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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • 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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—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
    • C10J3/72—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
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • 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
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • 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
    • C10J2300/0943—Coke
    • 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
    • C10J2300/0963—Ozone
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas

Definitions

  • the present invention relates to gasifiers in which a hydrocarbon fuel in solid or liquid form is converted into a combustible fuel gas.
  • the principal combustible product is usually carbon monoxide together 5 with hydrogen and some methane and higher hydrocarbons.
  • the best known example of gasification technology is in the gasification of coal.
  • the most well established gas technique i.e. fixed bed gasification, suffers from a number of drawbacks, principally the requirement 0 for a graded size of coal feed and limitations on "swelling number 1 gas content and ash fusion temper ⁇ ature.
  • a 'fixed bed' gasifier is one in which the fuel bed is relatively stable.
  • a 'fluidised bed' in contrast, is one in which the oxygenating gas/air flow rate is high, the fuel particles are of limited size, and they are kept in eff-eetively constant fluid motion. The basic difference is therefore the size of the fuel 2.0 particles and the gas flow rate through the bed.
  • a fluidised bed gasifier produces a gas without tars and oils and can tolerate a wide range of feedstock size (after an initial crushing below a particular top size), ash content and ash fusion temperature. It also allows the use of lime or dolomite in the bed as a sorbent for sulphur. However, it still suffers from a tendency for defluidization to occur with caking coals and a considerable quantity of fine material may be ejected from the bed, leading to a requirement for a high freeboard above the bed in order to consume these particles by reaction.
  • An object of the present invention is to provide gasification apparatus which at least partially avoids the disadvantages of both fixed and fluidised beds.
  • gasification apparatus comprises a fixed bed gasifier arranged in the path of hot exhaust gases from a fluidised bed gasifier whereby solid fuel in the fixed bed gas- ifier acts as a filter for the gases and, on partial devolatilisation, falls into the fluidised bed gasifier to feed it.
  • the invention thus incorporates features of both fixed and fluidised beds in a reciprocally advantageous manner.
  • the fixed bed fuel typically coal
  • the fixed bed fuel is devolatilised so that no caking tendency (which might defluidise the fluidised bed) is left in the fuel which falls through the grate.
  • the fixed bed gasifier may be arranged above the fluidised bed gasifier so that fuel from the fixed bed gasifier is urged towards the fluidised bed gasifier by gravity.
  • the gas path from the fluidised bed gasifier to the fixed bed gasifier may have an upward portion from the fluidised bed gasifier and a downward portion through the fixed bed gasifier, means being provided for ' driving solid fuel in the fixed bed gasifier upwards to a point at which it can fall into the fluidised bed gasifier.
  • the fixed bed gasifier may be contained within an inclined container, the angle of inclination of the container being such, in conjunction with the nature of the fuel in the fixed bed gasifier in operation, that the fuel in the fixed bed gasifier maintains its position in the container against gravity.
  • the apparatus may then include a ram arranged to drive fuel in the fixed bed gasifier up the inclined container, and to retract and allow the admission of fresh, fuel between the ram and the existing bed fuel.
  • the fixed bed gasifier may comprise .a main gas output at an intermediate postiion in the gas path and an output for volatile-rich gases at the end of the gas path. There may then be means for recycling the volatile-rich gases to the fluidised bed gasifier.
  • the gas path from the fluidised bed gasifier may separate into a main path through the initial part of the fixed bed gasifier to the gas output at the intermediate position in the fixed bed, and a diver ⁇ sion path around this initial part of the fixed bed gasifier to a re-entry position after the intermediate position.
  • the fixed bed gasifier may incorporate a grate which in use supports a bed of solid fuel, the grate having apertures of controllable size.
  • the grate may also be adapted to feed fuel positively through the apertures.
  • the grate may comprise a plurality of co-operating grate members, one or more of which grate members comprises at least two relatively inclined grids, and is rotatable about an axis lying in the plane of the grate so as to position one or other of the grids substantially in the plane of the grate and to positively feed fuel by engagement of the grid lying out of the plane of the grate with the fuel.
  • Each grid may comprise two or more sets of spaced rods the rod spacings being different so as to define different sized grate apertures according to which set lies in the plane of the grate.
  • a gasification system may incorporate apparatus as aforesaid, and a separator arranged to feed fuel of relatively coarse particle size to the fixed bed gasifier and to feed fuel of relatively fine particle size to the fluidised bed gasifier.
  • the system may also comprise a reaction vessel arranged to devolatilise fuel and feed devolatilised fuel to the separator.
  • the gasifier may function at atmospheric or elevated pressure.
  • Figure 1 is a diagrammatic sectional elevation of gasification apparatus in accordance with the invention. ⁇ "
  • Figures 2(a) and 2(b) are plan views showing in more detail the grate in the gasifier of Figure 1;
  • Figure 3 is a diagrammatic representation of a gasification system in accordance with the invention;
  • Figure 4 is a diagrammatic sectional view of a modification of the gasification apparatus of Figure 1;
  • FIG. 5 is a diagrammatic sectional view of alternative apparatus according to the invention.
  • the gasifier shown comprises a fluidised bed FB of burning coal and coke above which is supported an upper, fixed, bed UB of coal on a stainless steel feed grate 6.
  • the gasifier is lined with refractory material R at its high temper ⁇ ature sections, as is conventional.
  • the fixed bed is fed with coal at an inlet 14 and a temperature distri ⁇ bution is maintained by the hot exhaust gases from the * fluidised bed FB such that the temperature 'of the fixed bed decreases gradually with height from a maximum of approximately 1000 C at its base.
  • Fluidised bed FB is fed with fine coal from a secondary inlet 5 and with coke (formed by devolatilisation of the coal in bed UB) via feed grate 6, as will subsequently be described in more detail.
  • the gravity feed of coke from the fixed bed is contrasted with an alternative transport arrangement to be described with reference to Figure 5.
  • the gasifier operates as follows.
  • a bed FB which comprises a mixture of ash and sand, and/or a sorbent for H-S, , if required, such as limestone, through a distributor 2, and fluidises the bed.
  • Propane admitted at inlet 3 via valve V2 is ignited in the bed by an overbed torch (not shown) for initial warm-up purposes.
  • the exhaust gases exit initially through a bypass outlet 4.
  • Small coal, of particle diameter less than 12mm in this particular embodiment is then substituted for propane, entering the fluidised bed at inlet 5.
  • Larger coal, in this embodiment sized between 12mm and 20mm is supported in the fixed upper bed UB by feed grate 6 which is cooled initially by air flow through the hollow grate bars, as will be explained further.
  • product gas from outlet 9 (in conjunction with steam if required) is used to cool the grate. Additional cooling is provided as required by injection'- of overbed steam at inlet 8, ensuring that the temperature immediately above grate 6 is below that required for ignition of coal.
  • the feed rate of coal via inlet 5 is increased, with cooling as necessary via steam from inlet 7, until the oxygen content in the effluent gases from the fluidised bed, i.e. the Off-gas', is too low to permit combustion to occur in bed UB.
  • Gasification is then initiated by diverting flow through bed UB by closing bypass 4, and feeding coal from this bed by operation of the grate 6, as will be described with reference to Figure 2.
  • Coal feed through inlet 5 and through grate 6 can be performed in parallel.
  • Steam is admitted into the fluidised bed at 7 as required and reacts with the coal in the fluidised bed to generate carbon monoxide and hydrogen.
  • Second ⁇ ary air may be admitted at inlet 8.
  • the running condition corresponds to a ratio of total air to total coal in which the proportion of air is about 20% of that required for a stoichiometric ratio.
  • Gaseous exhaust from the fluidised bed section passes via grate 6 through the lower half of bed UB and is then divided into two streams; one stream passes directly through the bed to exit at fuel gas outlet 9, and the other passes through apertures 10 in the bed wall and exits at 11, where it is fed to an engine or process plant, or can be diverted through an annular passage 12 to promote heat transfer from the gas stream, through the inner wall, to the top half of the fixed bed, the gas stream then exiting at 13- Coal is. supplied to bed UB at inlet 14 at a rate sufficient to maintain a constant level.
  • the hot fluidised bed off-gases devolatilise coal in the fixed bed UB, thereby destroying its caking properties, which would otherwise cause defluidisation of the fluidised bed when this coal was dropped into it.
  • the fixed bed also acts reciprocally to condition the fluidised bed effluent gases by acting as a filter and removing the large quantities of char and ash carried over, and contributes to some additional carbon monoxide formation by reaction of C0_in the fluidised bed off-gases with carbon.
  • the upward velocity through bed UB is sufficiently high to ensure good inertial collection efficiency, and the sticky porous surface of coal in various stages of conversion to char or coke promotes high particle retention efficiencies.
  • the gas velocity in the fixed bed UB depends upon the change in area between the fluidised and fixed beds .
  • the surface coatings of the larger coal/coke particles in the upper bed with small non-caking char and ash particles from the fluidised bed may reduce 5 the tendency of these larger particles to agglomerate and hence to interfere with the downward flow of coal in the upper bed.
  • the material, char, ash etc, ejected from the fluidised bed is returned with the large feed coal through the grate, and ash is rejected at 15.
  • the top gas stream exiting at 9 is a significant exhaust component, and is rich in heavy volatiles and tars. This may be reinjected into the fluidised bed at 3 to crack these components into lighter gaseous compo ⁇ nents.
  • the fluidised bed is run with a lower dense
  • region at the distributor at a temperature of about 900°C.
  • the injection of secondary air or a hot oxygen-containing exhaust stream at inlet 8 creates a zone ' of high temperature and high velocity in which there is a high concentration of suspended fuel particles,
  • Such a high-temperature zone also contributes to increased gasification by carbon monoxide and hydrogen formation in the fixed bed UB.
  • the fuel gas produced in the gasifier is fed
  • the gasifier of Figure 1 has the following advantages; (i) The use of a fluidised bed means that sulphur
  • FIG 2 shows in more detail a part of the feed grate of Figure 1.
  • Grate 6 comprises a plurality of adjacent elongate grate members 17 lying parallel in the plane of the grate, three of these grate members being shown in Figure 2.
  • the grate members are shown rotated by 90 relative to those in Figure 2(a).
  • Each grate member 17 comprises a stainless steel main tube 18 which communicates with a bypass tube 19. Coolant gas "(air and/or steam and/or product-gas from outlet 9) is passed through the tubes as shown.
  • Each grate member 17 is provided with two sets of inconel cross rods lying in respective perpendi ⁇ cular planes; namely one set a, b, c, d, e, f, g lying in the plane of the drawing in Figure 2(a) and another set (h and i on the two outer grate members and h, j, i, k on the central grate member) lying per- pendicular to this plane.
  • each set of cross rods forms a grid which with the adjacent grate members defines a set of grate apertures whose size is determined by the length.and spacing of the cross rods.
  • the central grate member 17 shown in Figure 2 differs from the two outer grate members in that additional cross rods j , k of twice the usual length are provided in one set, as can best be seen in part b).
  • additional cross rods j , k of twice the usual length are provided in one set, as can best be seen in part b).
  • the upwardly projecting ends of the cross rods h, i, j, k rake the fuel supported on the grid and positively feed it through the larger apertures being formed as the cross- rods a to g swing "out of the plane of the grate.
  • Apertures of intermediate size can be formed by rotating the grate members by less than 90°.
  • fuel can be positively fed through the grate by rotating the grate members by approximately 90 or the fuel can be merely allowed to fall through the grate at a controlled rate by a suitable intermediate rotation of the grate members .
  • the larger lumps of coal split and break up into smaller sizes which can then fa.1 through the grate.
  • FIG 3 shows a gasification system comprising a gasifier A substantially as shown in Figure 1.
  • the system utilises coal fed into a hopper H and air fed into gasifier A (at the fluidisation inlet 1) and into a reaction vessel D to generate combustible gas at outlet 11.
  • the combustible gas which consists mainly of carbon monoxide, hydrogen, methane and nitro- gen ⁇ may be fed to an engine or to a process plant for example.
  • a volatile-rich outlet stream of gas from gasifier A is drawn through a line 29 into an auxiliary air supply for vessel D through a venturi at B. This gas is ignited and burns stoichiometrically in a - combustion chamber C.
  • Coarsely crushed feed coal fed into vessel D via a hopper H forms a vigorously spouted bed in the vessel D. Drying and devolatili ⁇ sation of the coal by rapid heating takes place here, and the vigorous recirculation within the reaction vessel, caused by spouted entry of fuel and gases, discourages agglomeration of the coal as it passes through the plastic regime.
  • the design of the cyclone separator is such that the oversize 'cut* (i.e.
  • the proportion of material of size greater than the separation level) rejected to the gasifier via feed line 22 is of the particle size range required for the fixed bed UB of gasifier A.
  • the upper limit.of this size range is fixed by the initial coal crushing.
  • the complementary undersize stream containing the undersize particles (conveyed by a mixture of exhaust gases and volatiles) is injected'into the base of gasifier A as a central spout (i.e. by way of a spout or nozzle entering the bed) via line 28, the secondary coal input 5 of Figure 1 being dispensed with.
  • Feed grate 6 is included in a loop 24, (comprising grate 6, path 24, valve V3 , gas entry 3, fluidised bed FB, fixed bed UB, product gas exit 9 and grate 6,) controlled by valves VI and V3, and is cooled " by circulation of product-gas through this loop. Additional cooling may be provided by injecting steam or air at inlet 23-
  • This extended system provides the following additional advantages: (i) The ability to make full use of swelling coal without need for mechanical agitators to prevent seizing in the upper bed UB of the gasifier. (ii) The need for minimal solids treatment and handling. The reduction to a coarse top size can be achieved by a simple size reduction without need for grading,and the coal * is pneumatically transported by a process gas stream for most of its passage.
  • FIG. 4 shows a modification of the apparatus of Figure 1.
  • the arrangement again comprises a fixed bed gasifier UB mounted over a fluidised bed gasifier FB so that coal in the fixed, upper, bed is urged downwardly by gravity through the grate 6 and into the fluidised bed.
  • the outlet 4 is closed and remains closed.
  • the main stream of effluent gases from the fluidised bed takes a 'main path' up through the grate 6, through the initial part of the fixed bed UB and (largely)out of the ports 10 as in Figure 1.
  • Figure 5 shows gasification apparatus incorporat ⁇ ing a fluidised bed gasifier FB and a fixed bed gasifier UB as before, but in this case the fixed bed is arranged not above the fluidised bed but alongside it in a kind of folded arrangement.
  • the path from the fluidised bed to the fixed bed has an initial upward portion 25 and a following downward portion 27 which includes the fixed bed gasifier UB.
  • the fixed bed UB is positioned. in an inclined duct or container terminating at the top of the fluidised bed section.
  • a ram 29 alternately retracts to admit large coal and advarices" ' to drive the bed upwards.
  • the angle of slope is less than the angle of repose for the bed: in other words, the angle of inclination of the slope/container is such that, in conjunction with the nature of the fuel in the bed in operation, (its size, form, adhesion etc.) the bed maintains its position in the container against gravity.
  • the diverted stream, that in Figure 4 exits from outlet 4 passes along an internal duct 31 thus bypassing the initial part 27(a) of the fixed bed and opening into the bed at the re-entry point 16.
  • the diverted stream then passes through the latter part 27(b) of the fixed, bed to the volatile gas outlet 9.
  • the main stream passes through the initial part 27(a) of the fixed bed and emerges at an intermediate position, as before,at port 10.
  • this intermediate position of port 10 is arranged before the re-entry of the diverted stream at point 16.
  • a primary cyclone 33 is shown in the undiverted stream, from which fines are recycled (on path 34) via an ejector stream provided by a source 35.
  • This unit may also, of course, be employed in the previously described embodiments.
  • the cleaned product gas is then produced by the cyclone separator 33 at output 37.
  • the diverted stream, containing volatiles and unfiltered fines, emerges at outlet 9 and is recircul ⁇ ated to the fluidised bed via an ejecting fluid stream from the source 35 (e.g. air, a combustor or engine exhaust gas, or steam) which is itself a gasifying agent. Injection may be .

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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)
  • Industrial Gases (AREA)

Abstract

Dans un générateur de gaz à lit fluidisé (FB) et à lit fixe (UB) combinés, le lit fixe est agencé dans le trajet des gaz effluents du générateur de gaz à lit fluidisé. Le combustible (charbon) du lit fixe agit comme un filtre pour les particules entraînées, matières carbonisées, cendres, etc du lit fluidisé et à leur tour les gaz effluents dévolatilisent le combustible du lit fixe. Celui-ci se fragmente et tombe, ou est poussé, dans le lit fluidisé. Le lit fixe (UB) peut être monté soit (Fig. 1) directement au-dessus du lit fluidisé (FB) soit (Fig. 5) dans une conduite adjacente (27) d'où il doit être entraîné avant de tomber dans le lit fluidisé.
PCT/GB1985/000412 1984-09-21 1985-09-11 Dispositif de gazeification WO1986001821A1 (fr)

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GB8423949A GB8423949D0 (en) 1984-09-21 1984-09-21 Fluidised-bed gasifier
GB8423949 1984-09-21

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WO1986001821A1 true WO1986001821A1 (fr) 1986-03-27

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EP0554529A1 (fr) * 1992-02-03 1993-08-11 Deutsche Babcock Energie- und Umwelttechnik Aktiengesellschaft Procédé et appareil pour la gazéification de matériaux combustibles
CN101978031A (zh) * 2008-03-18 2011-02-16 卡尔-海因茨·特茨拉夫 采用生物质制取合成气的方法和装置
CN102076830A (zh) * 2008-05-29 2011-05-25 博胜能源股份有限公司 两段高温预热蒸汽气化器
CN103534339A (zh) * 2011-03-18 2014-01-22 埃克洛普有限公司 移动床反应器
CN105087077A (zh) * 2014-05-05 2015-11-25 汪春雷 一种内热立式垃圾全气化炉

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PL192012B1 (pl) 1999-06-09 2006-08-31 Tech Uni Muenchen Lehrstuhl F Urządzenie do zgazowywania zawierających węgiel substancji wsadowych
ES2343167T3 (es) * 2000-12-04 2010-07-26 Emery Energy Company L.L.C. Gasificador de multiples facetas y procedimientos relacionados.
DE102006022265A1 (de) * 2006-04-26 2007-10-31 Spot Spirit Of Technology Ag Verfahren und Vorrichtung zur optimierten Wirbelschichtvergasung
GR20080100220A (el) * 2008-04-02 2009-11-19 Μεθοδος και διαταξεις παραγωγης καυσιμων αεριων
DE102008032166A1 (de) 2008-07-08 2010-01-14 Karl-Heinz Tetzlaff Verfahren und Vorrichtung zur Herstellung von teerfreiem Synthesgas aus Biomasse
DE102011119386A1 (de) * 2011-11-25 2013-05-29 Ligento green power GmbH Verfahren zum An- und Abfahren einer Vergasungsanlage
FI123665B (fi) * 2012-02-20 2013-09-13 Raute Oyj Menetelmä kaasugeneraattorin toiminnan optimoimiseksi ja kaasugeneraattori
CN104284966B (zh) * 2012-05-18 2016-10-26 日本蓝色能源株式会社 生物质的气化装置
DE102014004465B3 (de) * 2014-03-28 2015-04-09 Ettenberger Gmbh & Co. Kg Vergasungsreaktor
ITMO20150099A1 (it) * 2015-05-05 2016-11-05 Syn Gas Gruppo S R L Impianto di gassificazione

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GB933481A (en) * 1960-12-14 1963-08-08 Campbell Herbert Secord Improvements in or relating to furnaces
US4057402A (en) * 1976-06-28 1977-11-08 Institute Of Gas Technology Coal pretreatment and gasification process
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Publication number Priority date Publication date Assignee Title
EP0554529A1 (fr) * 1992-02-03 1993-08-11 Deutsche Babcock Energie- und Umwelttechnik Aktiengesellschaft Procédé et appareil pour la gazéification de matériaux combustibles
CN101978031A (zh) * 2008-03-18 2011-02-16 卡尔-海因茨·特茨拉夫 采用生物质制取合成气的方法和装置
US8790428B2 (en) 2008-03-18 2014-07-29 Karl-Heinz Tetzlaff Method and device for producing synthesis gas from biomass
CN102076830A (zh) * 2008-05-29 2011-05-25 博胜能源股份有限公司 两段高温预热蒸汽气化器
CN103534339A (zh) * 2011-03-18 2014-01-22 埃克洛普有限公司 移动床反应器
CN105087077A (zh) * 2014-05-05 2015-11-25 汪春雷 一种内热立式垃圾全气化炉

Also Published As

Publication number Publication date
AU4800985A (en) 1986-04-08
GB2164660B (en) 1988-04-27
GB2164660A (en) 1986-03-26
GB8522523D0 (en) 1985-10-16
EP0195032A1 (fr) 1986-09-24
GB8423949D0 (en) 1984-10-31

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