COMBUSTION APPARATUS
The present invention relates to a combustion apparatus, in particular to a burner
for the combustion of carbonaceous fuel. In the preferred case the invention relates
to a burner for particulate solid carbonaceous fuel having an indirect firing system
and is for example an indirect fired pulverous coal fired burner. In particular, but
not exclusively, the invention relates to a combustion apparatus capable of air and
oxyfuel firing and utilizing flue gas recirculation. For example the invention relates
to a burner for use in a power generation apparatus and to a power generation
apparatus including one or more such burners.
In the field of power generation from fossil fuels, and in particular from coal,
conventional plant generally operate a direct firing system, where raw coal is fed
from a bunker to the mill and pulverized and then the pulverized coal is conveyed
directly from the mill to the burner. However, with the development of
technologies, such as coal pre drying, and particularly lignite pre drying, it is
becoming more common that plant operate an indirect firing system, where the raw
coal is milled to a bunker and then the dried pulverized coal fed from the bunker to
the burner. This allows for conveying of the coal at a higher solid to gas mass ratio
than conventionally used in direct fired systems. Conventionally and hereafter this
is referred to as "dense phase" conveying of the pulverized fuel.
There is significant prior experience relating to the efficient combustion of solid
fuels for steam raising applications. There has been a strong drive in recent years to
reduce levels of emissions of oxides of nitrogen from carbonaceous fuel burners,
especially in the field of power generation. Low NOx burners have been developed
which reduce the formation of NOx combustion gases.
In general terms, a low NOx burner for coal firing may comprise a number of
components, which may include:
• a pipe to supply the pulverized fuel and the conveying air (often known as
"primary" air)
• a number of channels arranged concentrically around the pulverized fuel
supply, through which the burner combustion air is supplied; in a low NOx
burner there will typically be two or more channels for the combustion air,
these are often known as "secondary" air, "tertiary" air, etc.
• devices to induce a swirling motion in the combustion air may be placed in
the secondary and tertiary (etc.) channels, these devices may (optionally) be
adjustable
· devices to stabilise the flame, often placed on the end of the fuel supply pipe
and sometimes known as the "flame-holder"
• devices placed inside the fuel supply pipe to control the fuel distribution at
the outlet of that pipe
• supplementary equipment, such as igniters, light-up burners, flame
monitoring sensors, etc., optionally installed in a separate tube, which may
be located centrally within the fuel pipe where it is known as the "core" air
tube; the core air tube may have its own air supply; alternatively
supplementary equipment may be installed in other locations in the burner
or close by.
Where "air" is used herein the skilled person will readily appreciate that other
oxygen containing comburant gases may be substituted in the familiar way for
example for oxyfuel firing including a comburant gas having a reduced nitrogen
content relative to air, for example comprising mixtures of pure oxygen and/ or
recycled flue gas and/ or air.
Figure 1 (prior art) shows one specific implementation of low NOx burner
technology; it is known by those knowledgeable in this area that there are a number
of variant low NOx burner designs available.
Implicit in the design of any low NOx burner is the presumption that there must be
sufficient oxidant in the primary (transport) stream to support the early combustion
of the solid fuel; a natural progression from the use of direct fired combustion
systems is that the air flow required to convey the solid fuel from the pulverizing
mill is also sufficient for the early combustion of that solid fuel. It has been shown
that reducing the amount of air (oxidant) available in the early stages of combustion
has a detrimental impact upon the stability of the flame and, at a certain level, the
flame will extinguish, even though a sufficient quantity of air is supplied to the
burner as a whole.
This has tended to discourage consideration of the use of indirect firing for low NOx
burners.
US2009/0000532 describes a low-NOx burner suitable for firing the furnace of a
steam generator which is equipped with a dense phase conveyance of the fuel.
However, the arrangement requires burner redesign to provide for separate
conveying of primary fuel and primary oxidant into the burner via concentric
primary air and fuel conduits and to provide for mixing of the fuel and primary
oxidant streams within the burner downstream of the burner entrance and towards
the burner outlet by provision of swirl devices in the primary conduit. This leads to
a more complex design of burner.
An arrangement which is simpler and/ or more immediately compatible with
existing low-NOx burner designs is desirable.
According to the invention there is provided a combustion apparatus comprising:
a burner having a burner inlet for receiving a supply of combustible pulverous fuel
and a supply of comburant gas and a burner outlet in the vicinity of which
combustion of the fuel is supported during use;
at least a primary conduit defining a flow channel for conveying a mixture of fuel
and comburant gas from the burner inlet to the burner outlet;
a fuel feed line defining a flow channel which conveys a pulverous combustible fuel
in a dense phase; and
a supply conduit fluidly connecting a comburant gas supply to the primary conduit
and defining with the primary conduit a primary flow stream;
wherein the fuel feed line is provided with a fuel feed outlet into the supply conduit
upstream of the burner inlet to supply pulverous combustible fuel in a dense phase;
and wherein the primary flow stream is provided with a mixing device downstream
of the fluid supply outlet and in particular at or in the vicinity of the burner inlet.
Fundamentally, the burner of the invention is an indirectly fired burner in that the
fuel feed line conveys pulverous fuel to the burner in a dense phase for mixing with
a supply of comburant gas at the burner, rather than a direct firing system. The
invention offers a capability of providing a low-NOx burner, which is suitable for
firing the furnace of a steam generator, with a dense phase conveyance of fuel,
without disadvantageously affecting the low-NOx combustion characteristic of the
burner.
However, it can be contrasted with US2009/0000532, where the burner has
separate primary fuel and primary oxidant tubes and where mixing of dense phase
primary fuel and oxidant takes place within the burner towards the outlet/
combustion end by means of swirl devices specifically provided for such a purpose.
By contrast, in accordance with the present invention, mixing of the dense phase
primary fuel and oxidant is effected upstream of the main body of the burner and in
particular at or about the burner inlet and for example immediately upstream of the
burner inlet by means of a suitable flow stream mixing device. In particular this is
done in combination with a duct arrangement upstream of the burner, whereby a
dense phase stream of solid pulverous fuel is introduced to a stream containing the
oxidant (air or other oxygen containing gas) upstream of the mixing device, so as to
create a mixture capable of sustaining a stable flame in a solid fuel burner after
these two streams are mixed within the burner following their interaction with a
suitable mixing device. The mixing device is conveniently a static mixing device but
may additionally or alternatively include a variable mixing device.
The resultant mixture capable of sustaining a stable flame is conveyed along a
primary conduit in essentially conventional manner to a burner outlet, for example
letting into a combustion chamber in familiar manner, in the vicinity of which a
combustion site is defined at which combustion of the fuel is supported during use.
The general design of the burner may thus otherwise be relatively conventional. In
particular, conventional low NOx burner designs may be readily adapted in
accordance with the principles of the invention. This is particularly advantageous in
the case where the low NOx burner design to which the invention is to be applied
already includes a suitable static or other mixing device (such as the scroll plate in
the low NOx burner design given by way of example in figure 1) in the primary
conduit at or about the burner inlet. In such cases, the existing mixing device may be
used to complete the process of mixing the dense phase fuel stream and the primary
comburant gas stream as it feeds into the primary conduit. Conveniently therefore, a
suitable mixing device such as a suitable static mixing device is provided within the
primary conduit in the vicinity of the burner inlet. Alternatively it is a relatively
simple design matter to provide a suitable mixing device in the primary stream at or
about the burner inlet.
In all cases, the invention is distinctly characterised in that fuel is supplied in dense
phase but that mixing of the fuel and primary comburant gas stream is effected
upstream of and/ or in the vicinity of the burner inlet, rather than within the burner
and/ or towards the outlet, and that the primary conduit within the burner carries
in use a fuel and oxidant mix capable of supporting combustion. This is effected by
the combination of injection of fuel in dense phase to the supply conduit carrying
oxidant upstream of the burner inlet and by provision of a suitable mixing device
such as a static mixing device downstream thereof and for example at or about the
burner inlet and for example immediately upstream of the burner inlet.
In the context of the art of the invention, the term "dense phase" will be readily
understood by the person skilled in the art. It includes for example conveying flows
of pulverous fuel and transport gas with pulverous fuel to transport gas mass ratio
of at least 3 and for example at least 5, at pressures of for example 0.5 to 5 bar, and
at flow speeds of for example 10 to 30 ras 1 or more. It should be emphasised that
these parameters are examples only. The skilled person will readily be able to
determine whether a particular conveying flow constitutes a dense phase flow as it
would be understood in the art.
In accordance with the invention a mixing device is provided in stream in the
primary flow stream to facilitate mixing of the dense phase pulverous fuel stream
and the primary comburant gas stream upstream of the burner or in the vicinity of
the burner inlet. Conveniently the mixing device comprises a static mixing device.
A suitable static mixing device comprises a static formation located in the primary
flow stream, and for example in the primary conduit at or towards a burner inlet
end thereof, configured to effect at least a partial obstruction of flow of the primary
flow stream. In a preferred case a static mixing device comprises a static formation
configured to impart a swirling motion to the primary flow stream.
For example a static mixing device may comprise one or more bladed formations
presenting a flow deflection surface at an angle to a primary flow direction of the
stream, for example at an angle to an axial flow direction. A static mixing device
may comprise one or more helical bladed formations. A static mixing device may
comprise a scroll plate such as is familiar for example from the prior art illustration
of figure 1.
Additionally, the supply conduit may be fluidly linked to the primary conduit at an
angle thereto, for example such there is an angle between an axial flow direction in
the supply conduit and an axial flow direction in the primary conduit. This produces
a deviation in flow direction in the primary flow stream downstream of the fuel
outlet and at the burner inlet which may therefore assist in mixing of the dense
phase pulverous fuel stream and the primary comburant gas stream. A mixing
device such as a static mixing device is conveniently located at or about this
deviation in flow direction.
In the preferred case, the fuel feed line is provided with a fuel feed outlet into the
supply conduit closely upstream of the mixing device. The mixing device may be
provided closely upstream of the burner inlet and/ or within the primary conduit of
the burner in the vicinity of the inlet such that mixing is effected before or about the
burner inlet region and such that for at least a substantially major part of the burner
length the primary conduit carries in use a mixed fuel and primary comburant gas
supply.
The temperature of the mixture is below the devolatilisation initiation temperature
of the solid fuel.
It is a particular advantage although not a requirement of the invention that it can
be applied to low-NOx pulverized coal burners following general known design
principles without major additional modification.
In a preferred case, the burner of the invention is a pulverized coal burner. The
invention is suitable for pulverous fuel burners for pulverized bituminous coals and
for dried pulverized lower rank coals such as brown coals/ lignites. The invention is
particularly suited to application for pulverous fuel burners for dried pulverized
lignites.
In a preferred case, the burner of the invention is a low-NOx burner. Known
principles of low-NOx burner design may be embodied.
For example the burner may comprise one or more secondary and/ or one or more
tertiary or higher order conduits comprising flow channels for the supply of further
gases such as further comburant gases to the combustion site at the burner outlet.
For example, as will be familiar, one or more secondary and/ or one or more tertiary
or higher order conduits may be disposed annularly in concentric manner about a
primary conduit.
For example the burner may comprise a core tube about which the primary conduit
is annularly disposed. The core conduit may comprise a flow channel for the supply
of further gases such as further comburant gases to the combustion site at the
burner outlet and/ or may include an ignition lance for example coaxially arranged
in the core tube.
Preferably, the combustion apparatus is adapted for oxyfuel firing. That is, the
combustion apparatus comprises a comburant gas supply apparatus adapted to
supply a comburant gas to at least one conduit of the burner having a reduced
nitrogen content relative to air. Preferably the comburant gas supply apparatus is
adapted to supply a comburant gas to at least one conduit of the burner that does
not contain air. Preferably the comburant gas supply apparatus is adapted to supply
a comburant gas to at least one conduit of the burner that is substantially free of
nitrogen.
Optionally, the comburant gas supply apparatus may include a source of pure
oxygen, such that the comburant gas supply apparatus is adapted to supply an
oxidant mixture comprising pure oxygen and other gases to at least one conduit of
the burner.
Optionally, the comburant gas supply apparatus may additionally be adapted to
supply comburant air. The comburant gas supply apparatus may be adapted to
switchably supply either air or the comburant gas having a reduced nitrogen
content relative to air to at least one conduit of the burner.
Preferably the combustion apparatus includes a flue gas recirculation conduit.
Preferably the flue gas recirculation conduit is fluidly connected in series or parallel
to the comburant gas supply apparatus such that a comburant gas mixture including
recycled flue gas may be supplied to at least one conduit of the burner.
Such a comburant gas supply apparatus facilitates control of the fuel/ oxidant
stoichiometry within the burner.
The parameters that are understood to affect the ignition and stability of the flame
include, for example, the following;
• the primary and secondary stream velocities
· secondary / primary velocity ratio
• the ignition zone stoichiometry
• the ignition zone temperature / heat availability
• the burner geometry, e.g. ratio of core air to primary air tubes or ratio of
primary air to secondary air tubes
Overall stoichiometry, the ratio of the total oxygen supplied for combustion divided
by the theoretical total oxygen required for complete combustion, and burner zone
stoichiometry, the ratio of the total oxygen supplied to all (e.g. core, primary,
secondary and tertiary) the burner streams for combustion divided by the
theoretical total oxygen required for complete combustion, are common
stoichiometry parameters assigned to control the performance of the burner in
terms of combustion efficiency and NOc production.
However, in relation to ignition of the flame it is possible to derive to other
stoichiometry parameters. One such parameter is the ignition zone stoichiometry,
the ratio of the total oxygen supplied to the core and primary burner streams for
combustion divided by the theoretical total oxygen required for complete
combustion. A second parameter is the ignition zone volatile matter stoichiometry,
the ratio of the total oxygen supplied to the core and primary burner streams for
combustion divided by the theoretical total oxygen required for complete
combustion of the volatile matter in the coal.
If the oxidant is air, then the stoichiometry parameters are directly related to the
mass, or volume, flow of air since the concentration of oxygen in air is constant at
20.95 %v/v or 23.14 %w/w.
However, if the oxidant is a mixture of an inert gas (that could be nitrogen, carbon
dioxide, moisture, argon, etc., or a mixture of these in, for example, flue gas) and
oxygen, then the stoichiometry parameters are related to both the mass, or volume,
flow of oxidant and the concentration of oxygen in oxidant. For this application the
concentration of oxygen in oxidant is preferably in the range 10 %v/v to 35 %v/v.
It has been found that mixing the dense phase solid fuel stream containing
insufficient oxidant to support combustion by itself, with a primary air (oxidant)
stream to achieve the desired ignition zone stoichiometry and concentration of
oxygen in oxidant allows the safe, stable, and efficient combustion of a solid fuel
stream that is supplied via a dense phase conveying system. Significantly the
arrangement tested allowed the primary air (oxidant) and solid fuel stream to
replicate the typical conditions exiting the pulverizing mills and commonly applied
to burners of this type.
It has been found that relatively small instantaneous variations in the fuel flow to a
burner have a substantial impact upon the residual oxygen level after combustion
(example: for a typical power station burner with ~40MWt thermal input firing coal
the coal flow is around 5 tonne/h; an instantaneous increase in the coal flow of just
~200g reduces the exit oxygen level from 3%v/v to zero, with the localised impact
being considerably greater in the early combustion region). Such variations can
have a destabilising effect on the flame as the early combustion is temporarily
starved of oxygen. It is therefore shown to be important that, in a dense phase
combustion system, the amount of primary air (oxidant) supplied to the burner is
sufficient to accommodate the effect of the fluctuations in solid fuel feed rate that
arise from the dense phase feeding system.
It is well known by those familiar with the operation of pulverized solid fuel
combustion systems that there is a risk of the fuel burning in an uncontrolled
manner within the equipment should the temperature be too high. To ensure that
such uncontrolled burning does not occur, it is necessary to maintain temperatures
that are lower than the "devolatilisation initiation temperature", that is the
temperature at which the volatile material in the coal starts to be released. This
devolatilisation initiation temperature is dependant upon the solid fuel; for lignite
coals it is typically around 250°C, for bituminous coals it is ranges between ~300°C
to ~380°C, for low volatile & anthracitic coals it is around ~400°C to ~520°C, and
for certain types of petroleum coke it is around ~350°C to ~380°C. Thus, in addition
to ensuring that a desirable ignition zone stoichiometry is achieved, the mixing of
the dense phase stream and the primary air (oxidant) stream must be such that the
mixture temperature is lower than the devolatilisation initiation temperature by a
reasonable margin.
In accordance with the invention in a further aspect a method for combusting
pulverous combustible fuel in a burner having at least a primary conduit defining a
flow channel for conveying a mixture of fuel and comburant gas from a burner inlet
to a burner outlet comprises:
feeding comburant gas to the primary conduit via a supply conduit fluidly
continuous therewith;
feeding the fuel to the supply conduit by a dense phase conveyance, via a fuel supply
outlet within the supply conduit in particular to a point upstream and for example
closely upstream of the burner inlet;
disposing a mixing device downstream of the fluid supply outlet and for example at
or in the vicinity of the burner inlet and in particular immediately upstream of the
burner inlet to effect mixing of the pulverous combustible fuel and comburant gas.
In accordance with the method of this aspect of the invention the burner is an
indirectly fired burner. Mixing of the dense phase primary fuel and oxidant is
effected upstream of the main body of the burner and in particular at or about the
burner inlet, by supplying a dense phase stream of solid pulverous fuel into a stream
containing the oxidant and by interaction with a suitable flow stream mixing device.
The mixing device is conveniently a static mixing device but may additionally or
alternatively include a variable mixing device. Thus, fuel is supplied in dense phase
but mixing of the fuel and primary oxidant is effected upstream of and/ or in the
vicinity of the burner inlet, rather than within the burner towards the outlet.
In particular, the mixing device, for example the static mixing device, is used to
effect at least a partial obstruction of flow of the primary flow stream of pulverous
fuel in dense phase and comburant gas to facilitate mixing thereof. In a preferred
case the mixing device is used to impart a swirling motion to the primary flow
stream of pulverous fuel in dense phase and comburant gas to facilitate mixing
thereof. Additionally, the primary flow stream may be caused to deviate in flow
direction at the mixing device and/ or at the burner inlet to assist in mixing of the
dense phase pulverous fuel stream and the primary comburant gas stream.
Preferably, the pulverous fuel burner is a pulverized coal burner, for example a
burner for pulverized bituminous coal or dried pulverized lower rank coal.
Consequently preferably the pulverous fuel is pulverized coal, for example
pulverized bituminous coal or dried pulverized lower rank coal. Preferably, the
pulverous fuel is dried pulverized lignite.
Preferably, the burner is operated in low-NOx operation, in particular in that the
supply of comburant gas is split between supply of comburant gas mixed with fuel
to a primary conduit and supply of comburant gas to one or more secondary and/ or
one or more tertiary or higher order conduits.
The method is suitable for air and/ or oxyfuel firing and is particularly suitable for
oxyfuel firing. Preferably the comburant gas is one or more of: air; oxygen; a
comburant gas having a reduced nitrogen content relative to air; recycled flue gas.
Suitable mixtures of the foregoing may be used to control the fuel/ oxidant
stoichiometry within the burner.
In the particular case, the method of this aspect of the invention is a method of
operation of a burner of the first aspect of the invention and preferred features of
the method will be understood by analogy.
An embodiment of the present invention will now be described, by way of example
only, with reference to the accompanying drawings, in which:
Figure 1 is a sectional side view of a prior art burner to which the principles
according to the invention could be applied;
Figure 2 is a simplified diagrammatic view of a combustion apparatus according to
the invention such as it might be applied for example to a burner of the type
illustrated in Figure 1.
Figure 1 is a sectional side view of a prior art low-NOx burner 52 fitted to a boiler
wall 12.
Each burner 52 has five co-axially arranged tubular partitions defining annular
passages for one, or a mixture, of fuel, oxygen, flue gas, and air.
Each burner 52 has a primary tube 90 which is fluidly connected to the primary fuel
input conduit 42. In the prior art the burner 52 is described for direct firing. The
burner is adapted for air or oxyfuel firing. A mixture of pulverized coal fuel and
comburant gas, for example air for air firing, or a mixture of recycled flue gas and
oxygen for oxyfuel firing, is supplied to a scroll plate 94 of the primary tube 90 via a
tangential connection 92.
Each burner 52 also has a secondary tube 100 which is fluidly connected to the
secondary input conduit 50. Comburant gas, for example air for air firing, or a
mixture of recycled flue gas and oxygen for oxyfuel firing, is supplied to apertures
102 provided in the secondary tube 100 from a wind box 40 surrounding the burner
52.
Each burner 52 includes two tertiary tubes 106, 108. Also, a core tube 110 is
provided, which includes a radial connection 112. These tubes may be fluidly
connected to one or both of the combustion gas supply means and the flue gas
recirculation system, which is not shown on Figure 1.
In operation, fuel within the primary tube 90 is given an axial and a circumferential
momentum by the scroll plate 94. The scroll plate is intended to impart this axial
and circumferential momentum to fuel in a fuel gas mix which has already been
mixed prior to transport to the burner.
The flow is discharged past a lip 114 as a vigorously eddying flow which ignites at
the lip 114 defining an initial combustion region. Reducing conditions prevail
within this region such that there is minimal oxidation of the nitrogen in the fuel.
The amount of oxygen in the core tube 110 is also limited to maintain these
conditions.
Flow from the secondary 100 and tertiary 106, 108 tubes forms an envelope around
the initial combustion region so that combustion of the fuel is completed
downstream under oxidising conditions.
Such a burner and the general principles it embodies for low-NOx combustion, will
be familiar.
Figure 2 shows how the principles of the invention might be applied to a burner of
the type illustrated in Figure 1.
A supply tube 1 carrying a concentrated stream of pulverous solid fuel and a small
amount of transport gas in dense phase is introduced into a larger tube 2 carrying
the primary oxidant to the burner. Figure 2 shows a typical arrangement for the
dense phase solid fuel injection into the primary stream and its subsequent mixing
at the burner entry.
In a typical "dense phase" suitable for application of the principles of the invention,
the transport gas stream could be air, inert gas, or a gas mixture containing up to
21%v/v oxygen, including flue gas. Typically the mass ratio of solid fuel to gas
would be of the order of 5:1.
A suitable primary oxidant stream for application of the principles of the invention
could be air or a gas mixture, including flue gas, containing oxygen, for example air
for air firing, or a mixture of recycled flue gas and oxygen for oxyfuel firing. The
concentration of oxygen in the primary stream is preferably in the range 10 to
35%v/v.
Because mixing between two parallel streams is poor, especially when their
velocities are similar, a suitable mixing device and preferably a static mixing device
is introduced. Conveniently in this embodiment the scroll casting 21, shown at the
solid fuel and primary oxidant entry to the burner 22, serves as a static mixing
device. The scroll 21 provides an obstruction to the inlet flow, and imparts a
swirling motion. In this embodiment there is also a 90° change in direction between
an axial flow direction for the primary supply flow 2 and an axial flow direction for
the primary flow within the burner 2a which further enhances the mixing of the
solid fuel and primary oxidant.
Advantageously therefore in this embodiment a static mixing device is employed
which was already present in the direct fired design. However, the invention
encompasses additionally or alternatively the provision of specific to purpose static
and/ or other mixing devices in the primary stream upstream of or at or about the
inlet to the burner.
At the outlet of the scroll 21 the solid fuel and oxidant are well mixed in a controlled
fashion, giving the desired solid fuel concentration distribution to promote stable
combustion. The mixture forms a primary flow 2a through a primary tube to a
burner outlet 30 in a furnace wall 31 in familiar manner.
It is a particular advantage of the invention that it can be applied to low-NOx
pulverized coal burners following general known design principles without major
additional modification. Thus, the remainder of the burner, as illustrated
schematically, may include in any suitable combination those features of the prior
art burner illustrated in figure 1.
For example the illustrated burner comprises secondary and tertiary conduits 4 and
5 for introduction of supplies of secondary and tertiary oxidant gas, for example air
for air firing, or a mixture of recycled flue gas and oxygen for oxyfuel firing.
For example the illustrated burner comprises a core tube 3 about which the primary
conduit is annularly disposed. The core tube may be used to supply further oxidant
gases or may include an ignition lance for example coaxially arranged in the core
tube.
The ignition zone stoichiometry at the outlet of a static mixing device in an
embodiment of the invention would be preferably in the range 0.1 to 0.3 and for
example about 0.2.
The benefit of the invention is that, by the use of a combination of a dense phase fuel
inlet pipe and a suitable flow mixing device in the primary flow and in particular a
suitable static mixing device, the process conditions (i.e. the solid concentration and
ignition zone stoichiometry) may be modified to create conditions that favour the
ignition of the solid fuel and thereby enhance the flame stability in the burner; this
characteristic leads to improved operational flexibility of the low NOx burner by
allowing it to be used over a wide range of load, and ensuring that flame stability is
robust with respect to the instantaneous variations in solid fuel feed rate as
observed in practical combustion systems. Additionally the mixture temperature is
maintained at a level lower than the devolatilisation initiation temperature to
ensure that uncontrolled burning does not occur within the combustion equipment
hardware.
In accordance with the invention a solid fuel entry located immediately upstream of
a mixer is thus used to deliver a controlled mixture of solid fuel and primary oxidant
containing sufficient oxygen to sustain combustion (including when the fuel flow is
subject to fluctuation), and at a temperature lower than the devolatilisation
initiation temperature.
CLAIMS
1. Acombustion apparatus comprising:
a burner having a burner inlet for receiving a supply of combustible
pulverous fuel and a supply of comburant gas and a burner outlet in the
vicinity of which combustion of the fuel is supported during use;
at least a primary conduit defining a flow channel for conveying a mixture of
fuel and comburant gas from the burner inlet to the burner outlet;
a fuel feed line defining a flow channel which conveys a pulverous
combustible fuel in a dense phase; and
a supply conduit fluidly connecting a comburant gas supply to the primary
conduit and defining with the primary conduit a primary flow stream;
wherein the fuel feed line is provided with a fuel feed outlet into the supply
conduit upstream of the burner inlet to supply pulverous combustible fuel in
a dense phase;
and wherein the primary flow stream is provided with a mixing device
downstream of the fluid supply outlet.
2. A combustion apparatus in accordance with claim 1 wherein the primary
flow stream is provided with a mixing device at or about the burner inlet.
3. A combustion apparatus in accordance with claim 1 or claim 2 further
adapted to effect mixing of the dense phase pulverous combustible fuel and
the comburant gas upstream of the burner inlet by means of a duct
arrangement upstream of the burner, whereby a dense phase stream of solid
pulverous fuel is introduced to a primary stream containing the comburant
gas.
4. Acombustion apparatus in accordance with any preceding claim wherein the
mixing device comprises a static mixing device.
A combustion apparatus in accordance with claim 4 wherein the static
mixing device comprises a static formation located in the primary flow
stream and configured to effect at least a partial obstruction of flow of the
primary flow stream.
A combustion apparatus in accordance with claim 4 or claim 5 wherein the
static mixing device comprises a static formation located in the primary
conduit at or towards a burner inlet end thereof.
Acombustion apparatus in accordance with one of claims 4 to 6 wherein the
static mixing device comprises a static formation configured to impart a
swirling motion to the primary flow stream.
Acombustion apparatus in accordance with one of claims 4 to 7 wherein the
static mixing device comprises one or more bladed formations presenting a
flow deflection surface at an angle to a primary flow direction of the stream,
for example at an angle to an axial flow direction.
Acombustion apparatus in accordance with one of claims 4 to 8 wherein the
static mixing device comprises one or more helical bladed formations.
Acombustion apparatus in accordance with one of claims 4 to 9 wherein the
static mixing device comprises a scroll plate.
Acombustion apparatus in accordance with any preceding claim wherein the
fuel feed line is adapted to convey a pulverous combustible fuel in a dense
phase with pulverous fuel to transport gas mass ratio of at least 3 at
pressures of 0.5 to 5 bar and at flow speeds of at least 10 ms .
12. Acombustion apparatus in accordance with any preceding claim wherein the
supply conduit is fluidly linked to the primary conduit at an angle thereto,
such that there is an angle between an axial flow direction in the supply
conduit and an axial flow direction in the primary conduit.
13. A combustion apparatus in accordance with claim 12 wherein a mixing
device is located at or about the deviation in flow direction.
14. Acombustion apparatus in accordance with any preceding claim wherein the
burner is a pulverized coal burner.
15. Acombustion apparatus in accordance with any preceding claim wherein the
burner is a low-NOx burner.
16. Acombustion apparatus in accordance with any preceding claim wherein the
burner comprises one or more secondary and/ or one or more tertiary or
higher order conduits comprising flow channels for the supply of further
gases such as further comburant gases to the combustion site at the burner
outlet.
17. A combustion apparatus in accordance with claim 16 wherein one or more
secondary and/ or one or more tertiary or higher order conduits are
disposed annularly in concentric manner about a primary conduit.
18. Acombustion apparatus in accordance with any preceding claim wherein the
burner comprises a core tube about which the primary conduit is annularly
disposed.
19. Acombustion apparatus in accordance with any preceding claim adapted for
oxyfuel firing.
20. Acombustion apparatus in accordance with claim 19 wherein the comburant
gas supply apparatus includes a source of comburant gas having a reduced
nitrogen content relative to air.
21. Acombustion apparatus in accordance with claim 20 wherein the comburant
gas supply apparatus is additionally adapted to supply comburant air.
22. Acombustion apparatus in accordance with claim 21 wherein the comburant
gas supply apparatus is adapted to switchably supply either air or the
comburant gas having a reduced nitrogen content relative to air to at least
one conduit of the burner.
23. A combustion apparatus in accordance with any preceding claim including a
flue gas recirculation conduit fluidly connected in series or parallel to the
comburant gas supply apparatus such that a comburant gas mixture
including recycled flue gas may be supplied to at least one conduit of the
burner.
24. A method for combusting pulverous combustible fuel in a burner having at
least a primary conduit defining a flow channel for conveying a mixture of
fuel and comburant gas from a burner inlet to a burner outlet comprising the
steps of:
feeding comburant gas to the primary conduit via a supply conduit fluidly
continuous therewith;
feeding the fuel to the supply conduit by a dense phase conveyance, via a fuel
supply outlet within the supply conduit in particular to a point closely
upstream of the burner inlet;
disposing a mixing device downstream of the fluid supply outlet to effect
mixing of the pulverous combustible fuel and comburant gas.
25. A method in accordance with claim 24 comprising the step of disposing a
mixing device at or about the burner inlet.
26. Amethod in accordance with claim 24 or 25 wherein mixing of the pulverous
combustible fuel and comburant gas is effected by supplying a dense phase
stream of solid pulverous fuel into a stream containing the oxidant and by
causing subsequent interaction of the flow of combustible fuel and
comburant gas is with a suitable flow stream mixing device.
27. A method in accordance with any one of claims 24 to 26 wherein the mixing
device is a static mixing device.
28. A method in accordance with any one of claims 24 to 27 wherein the mixing
device is used to effect at least a partial obstruction of flow of the primary
flow stream of pulverous fuel in dense phase and comburant gas to facilitate
mixing thereof.
29. A method in accordance with any one of claims 24 to 28 wherein the mixing
device is used to impart a swirling motion to the primary flow stream of
pulverous fuel in dense phase and comburant gas to facilitate mixing thereof.
30. Amethod in accordance with any one of claims 24 to 29 wherein the primary
flow stream is caused to deviate in flow direction at the mixing device and/
or at the burner inlet to assist in mixing of the dense phase pulverous fuel
stream and the primary comburant gas stream.
31. Amethod in accordance with any one of claims 24 to 30 wherein the burner
is operated in low-NOx operation.
32. A method in accordance with any one of claims 24 to 31 wherein the
comburant gas is one or more of: air; oxygen; a comburant gas having a
reduced nitrogen content relative to air; recycled flue gas.