Combustion method and apparatus

Abstract: An apparatus for incinerating waste material comprising means (32) for feeding waste material in batches to a main combustion region (29), burners (26, 28) for burning said batches thereby to form gaseous combustion products, a secondary combustion region (30) for burning combustibles in said combustion products, means (40) for supplying oxygen to said secondary combustion region to support combustion and means (56) for controlling the supply of oxygen. The quantity of oxygen supplied being altered as a function of monitored concentration of a least one component of the combustion product or the flue gas thereby to compensate for the variation in calorific value of different batches of waste.

Description: This invention relates to a method and apparatus for the combustion of waste material. It is particularly concerned with the incineration in batches of waste material whose calorific value may vary randomly from batch to batch. A need to handle such waste arises for example in the incineration of hospital wastes. These wastes are typically packaged in plastics sacks that are fed at regular intervals to the incinerator. US patent specification 4 976 207 discloses apparatus for carrying out a combustion process including a combustion chamber and a secondary or post-combustion chamber. Air is injected into the post-combustion chamber. If desired, the air may be preheated. Sensors are provided within the combustion chamber, the post-combustion chamber and an air supply conduit so as to control operation of a device for preheating the air in response to detected sensed signals from the sensors. US-A-4 279 208 relates to method and apparatus for the treatment of industrial wastes. At least some of the constituent materials of the wastes are subjected to combustion or pyrolysis to produce flue gases. The supply of an oxygenated combustion-supporting gas to the wastes is regulated as a function of at least one predetermined characteristic of the flue gas. For example, the oxygenated gas may be a mixture of air and substantially pure oxygen, and the feed rate of one or both of these may be regulated in response to either the sensed temperature or the oxygen content of the flue gases. US 4 870 910 discloses all the pre-characterising features of Claim 4 but fails to provide any method of controlling the flow of oxygen in accordance with demand and is therefore somewhat wasteful. The control systems disclosed in US-A-4 976 207 and US-A-4 279 208 are essentially reactive in nature. They suffer from the disadvantage that if the waste material is of randomly varying calorific value, occasions can arise when there is a temporary deficiency of oxygen in the secondary combustion region with the result that for a period of time the flue gases can contain an unacceptably high concentration of carbon monoxide or of residual particles of carbonaceous material. Moreover, by the time the reactive control system has adjusted the oxygen concentration (in the case of the apparatus disclosed in US-A-4 279 208) or the temperature of the air (in the case of the apparatus shown in US-A-4 976 207) the demand for oxygen may have subsided. As a result, such control systems may be wasteful and yet fail to result in adequate quality of flue gas. It is an aim of the present invention to provide a method and apparatus that overcome or ameliorate the above mentioned problems. According to the present invention there is provided a method for incinerating waste material characterised by feeding to a main combustion region batches of combustible waste material whose ease of burning may vary randomly from batch to batch, burning said batches of waste material in said main combustion region and thereby forming gaseous combustion products, burning in a secondary combustion region combustibles in said combustion products and supplying oxygen to support the combustion of said combustibles, and discharging flue gas from said secondary combustion region, characterised in that in a first set of periods of time the oxygen supply rate is determined independently of the composition of the combustion products or the flue gas, and in a second set of periods of time which each alternate with periods in the first set, the oxygen supply rate is determined as a function of monitored concentration of at least one component of the combustion products or flue gas and in which each first period of time is set so as to comprise a period immediately before a batch of waste is fed to the main combustion region. The invention also provides apparatus for -incinerating waste material comprising means for feeding in batches to a main apparatus for incinerating waste material including means for feeding in batches to a main combustion region combustible waste material whose calorific value may vary randomly from batch to batch, at least one burner for burning said batches of waste material in a main combustion region and thereby forming gaseous combustion products, a secondary combustion region being heated by a burner for burning combustibles in said combustion products, means for supplying oxygen to said secondary combustion region to support combustion therein, an outlet from the secondary combustion region for discharging flue gas from the apparatus, characterised by a control system for controlling the supply of oxygen to the secondary combustion region,means for detecting a batch of waste material at the entrance and means for monitoring in real time the concentration of a chosen gaseous component of the combustion product or flue gas, such that in a first set of periods of time the oxygen supply rate is determined independently of the composition of the combustion products or the flue gas, and in a second set of periods of time which each alternate with periods in the first set, the rate of supplying oxygen determined as a function of monitored concentration of at least one component of the combustion products or the flue gas. The batches of waste material are typically fed to the incineration apparatus according to the invention at regular intervals. For most of the duration of each period of time between successive batches being fed to the furnace, the supply of oxygen to the secondary combustion region is preferably determined by monitoring the concentration of at least one component of the flue gases or combustion products, but at the end of each period, and if desired at the start of the next period, the rate of supply of oxygen is preferably determined independently of the composition of the flue gases or combustion products. Such independent supply of oxygen enables the oxygen concentration in the secondary combustion region to be set so as to cope adequately with the combustion products that are likely to be encountered from even the most difficult to burn of the batches of waste. If in fact the concentration of combustibles is lower, then the rate of oxygen supply may be reduced in accordance with the monitored concentration of at least one component of the flue gases or combustion products. The oxygen supply rate is preferably determined in response to the concentration of carbon monoxide or in response to the ratio of carbon monoxide concentration to oxygen concentration. Preferably, the oxygen supply rate is controlled automatically. Preferably, the automatic control system includes means for detecting a batch of waste material at an entrance to the main combustion region, a timer for setting the duration of each first period, means for automatically monitoring in real time the concentration of at least one chosen gaseous component of the combustion products or flue gas, and one or more automatically-operable valves in a conduit or conduits for supplying oxygen to the secondary combustion region, wherein the detection means is able to generate a signal which starts the first period and actuates the valve or valves to adjust the oxygen supply rate as necessary to a chosen value, the timer is able to generate a signal that ends the first period and starts a second period, and the gas monitoring means is able to generate a signal which actuates the valve or valves as necessary to adjust the oxygen supply rate during the second period in response to the concentration of the chosen component or a function of such concentration. Preferably, the first combustion region is defined in a chamber having an outer door and inner door for feeding batches of waste material into the main combustion region, opening of the outer door actuating the detecting means to generate a signal. Alternatively, entry of a batch of material through the outer door may break a beam of electro-magnetic radiation and thereby enable a signal to be generated to start a first period. The main and secondary combustion regions may be defined in the same or different chambers. The method and apparatus according to the present invention are particularly suitable for incinerators of a kind in which both regions are defined in the same chamber, such incinerators having in the past given rise to particular pollution problems. The or each control valve is preferably solenoid-actuated. Preferably, the apparatus according to the invention is able to change the oxygen supply rate only in increments. For example, the oxygen may be supplied through a plurality of automatically-operable on-off valves in parallel with one another, the arrangement being such that the oxygen flow rate is proportional to the number of valves that are open any one time. The oxygen is preferably introduced with a swirling motion about an axis that extends in the general direction of flow of the combustion products through the secondary combustion region. The oxygen may be supplied as air, oxygen-enriched air or pure oxygen. The method and apparatus according to the present invention will now be described by way of example with reference to the accompanying drawing, in which: Figure 1 is a schematic side elevation, partly in section, of an incinerator; Figure 2 is a schematic section through the line II-II in Figure 1, and Figure 3 is a schematic flow diagram illustrating an oxygen supply control apparatus for use in association with the incinerator shown in Figures 1 and 2. The drawings are not to scale. Referring to Figures 1 and 2 of the drawings, there is shown a boiler-cum-incinerator comprising a furnace 2 having a refractory lining 4. The top of the furnace 2 has an outlet 6 for flue gases which communicates with a three-pass heat exchanger 8 which functions as a boiler of water and provides a jacket for the furnace 2. As shown in Figure 2, the heat exchanger 8 comprises down passes 10 and 12 and an up pass 14 for flue gases from the furnace 2. As shown in Figure 2, in each pass a multiplicity of boiler tubes 16 is located. In operation, the flue gases give up heat to the boiler tubes 16 and are thus effective to raise steam. Near the bottom of the furnace 2 are located water cooled bars 18 which form a grate for supporting waste plastics sacks (not shown) to be incinerated. The sacks may for example contain hospital wastes. The bars 18 are typically arranged so that they form a sloping grate. The furnace 2 has a plenum chamber 20 at its bottom beneath a hearth 22 for a flow of air to support combustion of the sacks and their contents. The chamber 22 has an inlet 24 communicating with a blower (not shown) or fan (not shown) for supplying combustion air. The furnace 2 has two burners 26 and 28 associated with it. The burners preferably both burn natural gas and may for example be of the kind sold under the trade mark NUWAY. The lower burner 26 (as shown in Figure 1) fires, in operation, into a main combustion region 29 a little above the grate defined by the bars 18. The upper burner fires into a secondary combustion region 30. The furnace 2 has a chute 32 for feeding plastics sacks containing waste to be incinerated into the main combustion region 29. The chute 32 has an outer door 34 and an inner door 36. The doors 34 and 36 may be of a guillotine kind and their opening and closing may be actuated automatically. In operation, the burners 26 and 28 may be lit and fired continuously. If desired, the burner 28 may have alternative high and low intensity firing modes, with means (not shown) for selecting the firing mode in response to the temperature of the flue gases. Thus, for example, the burner 28 may operate in its high intensity mode unless and until the sensed temperature of the flue gases at the outlet 6 exceeds, say, 1000°C. Batches of hospital waste each contained in a plastics sack are admitted to the furnace at regular intervals, say every three minutes, via the chute 32. Air is supplied to the furnace via the plenum chamber 20. The burner 26 raises a temperature in the main combustion region 29 for each sack fed from the chute 32 onto the grate defined by the bars 20 and its combustible content to burn and therefore form gaseous combustion products. Given the nature of the sack and typical hospital wastes, the combustion products typically contain a sizeable proportion of combustible gases, for example carbon monoxide and volatile organic compounds, and some particles of carbon. Such combustibles burn in the secondary combustion region 30 which is heated by the burner 28. The resulting flue gas flows out of the furnace 2 through the outlet 6, typically at a temperature in the order of 850°C. The flue gas then flows through the passes 10, 14 and 12 in that order and passes to a stack (not shown) at a temperature near to the prevailing ambiert temperature. If necessary, a fan (not shown) may be operated to facilitate the flow of flue gas through the passes 10, 14 and 12 and into the stack (not shown). In flowing through the passes 10, 14 and 12 the flue gas gives up heat to the boiler tubes 16 and is thereby able to raise steam. In a typical commercial installation, such raising of steam is able to meet a sizeable part of the demand for space heating in the hospital in which the illustrated incinerator is located. It is often found that the composition of the flue gas is undesirable in that notwithstanding the provision of the secondary combustion region 30 it may still contain appreciable quantities of carbon monoxide or other poisonous gas or appreciable quantities of particles of carbon. In accordance with the invention, this problem is solved by introducing commercially pure oxygen or oxygen-enriched air into the secondary combustion region 30 through one or more lances 40. The or each lance 40 is positioned above the burner 26 but below the burner 28 and extends into the second combustion region 30. Typically, just one lance 40 is used. The lance 40 preferably terminates in a 45° elbow (not shown) directed towards the furnace wall so as to create a swirling flow about a vertical axis. The end of the lance 40 preferably points horizontally or at a small (e.g. 20°) angle upwardly. The swirling flow helps to increase the residence time of the gases in the secondary combustion region and thus makes more time available for the oxidation of carbon monoxide, other combustible gases in the gaseous combustion products ascending from the combustion region 29, and particles of carbon. In practice, however, the composition of the combustion products can vary widely. Typical hospital practice is to employ black plastics sacks for normal office waste composed mainly of paper, yellow plastics sacks containing waste from wards, which will typically vary in make up from sack to sack but which typically contains a high proportion of plastics, and red sacks containing waste from operating theatres including dressings and organic and infectious tissue. The combustion properties of each kind of waste differ. If commercially pure oxygen is supplied to the secondary combustion region 30 at a rate such as to ensure complete combustion of all combustibles in the gaseous combustion products ascending from the main combustion region 29 even when the most difficult to burn waste is received (typically one having a high content of both water and plastics) then there will be considerable over-supply of oxygen during periods in which readily combustible waste is burned (typically one with a high content of paper and a low content of water). In order to overcome this problem, the oxygen supply apparatus shown in Figure 3 is used. This apparatus includes an upstream oxygen supply manifold 50 that communicates with a source (not shown) of commercially pure oxygen, and a downstream oxygen supply manifold communicating with the lance 40 that extends into the interior of the furnace 2 (not shown in Figure 3). The manifolds 50 and 52 are inter-connected by and are able to be placed in communication with one another via four substantially identical conduits 54, each having an inlet end terminating in the manifold 50 and an outlet terminating in the manifold 52. Each conduit 54 has its own solenoid actuated stop valve 56 located therein. Each stop valve has but two positions, fully open, when there is a substantially unrestricted flow of oxygen therethrough, and fully closed, when flow of oxygen from the upstream manifold 50 to the downstream manifold 52 therethrough is prevented. Each valve 56 is preferably such that its valve member (not shown) may move from its fully open position to its fully closed position substantially instantaneously, and back again substantially instantaneously. Assuming a constant pressure oxygen supply, the rate of flow of oxygen to the lance 40 (see Figure 1) is thus proportional to the number of the valves 56 that are open at any one time and can be changed incrementally by changing the number of the valves 56 that are open. The valves 56 each have a solenoid actuating mechanism 58 which is operatively associated with a programmable valve controller 60. The controller 60 is also operatively associated with a position sensor 62 (see also Figure 1) which is actuated once the outer door 34 of the incinerator has been raised say a few centimetres, and a real time carbon monoxide analyser 64 which has a detector 66 positioned close to but upstream of the outlet 6 (see Figure 1). The detector 66 is able to generate a signal proportional either to the concentration of carbon monoxide or to the ratio of carbon monoxide concentration to oxygen concentration in the flue gas at the region where it is positioned. The optimum position for the detector 66 is believed to be the closes to the main combustion region 29 at which the rate of reaction in the flue gases has subsided to a level at which meaningful gas concentration measurements can be taken. By a meaningful gas concentration measurement is meant a measurement of gas concentration from which the ultimate concentration that gas in the flue gases finally emitted from the incinerator can be assessed with reasonable accuracy. In general, the closer the detector 66 to the main combustion region 29 the faster the response time of the oxygen supply apparatus to receipt of an abnormal batch of waste material in the main combustion region 29. The valve controller 60 is able to be programmed so as to ensure that the valves 56 are operated in the following manner. First, when the outer door 34 starts to open a signal is generated by the sensor 62 and the controller sends a signal to the valves 56 effective to open sufficient of the valves to bring three of the four to the open position. The opening of the doors 34 and 36 is controlled automatically such that the outer door 34 opens at intervals of, say, three minutes, it taking say 10 seconds for the door to travel from its closed to its fully opened position and back again. On the door 34 opening, a plastics sack is then fed into the chute 32. The door 34 then closes. Once the door 34 has reached its fully closed position the inner door 36 beings to open. The inner door reaches its fully open position and the sack falls under gravity into the main combustion region 29 and starts to burn and/or pyrolyse. The inner door 36 then starts to close again. The valve controller has a timer circuit (not shown) which is actuated by the signal from the position sensor 62. It generates a signal upon the expiration of, say, twenty five seconds from the generation of the signal by the position sensor 62. During this period of twenty five seconds, oxygen is supplied the secondary combustion region 30 at a relatively high flow rate since three of the four valves 56 are open. Thus, a relatively high concentration of oxygen is built up in the secondary combustion region in advance of a sack containing combustible waste being received by the main combustion region 29. The dimensions of the conduits 54 and the manifolds 50 and 52, and the oxygen supply pressure are chosen such that this level of oxygen will typically be adequate to cope with the combustion products emanating from the kind of waste that is the most difficult to burn of the different kinds to be fed to the incinerator. On the timer generating its 25 second signal, the programmable controller 60 switches in control circuits that are responsive to signals from the carbon monoxide analyser 64. The oxygen supply control thus becomes reactive to the level of carbon monoxide in the flue gas. The controller 60 may be programmed such that when it is in a mode responsive to the analyser 64, it will open and close valves according to the sensed carbon monoxide level. For example, if the sensed carbon monoxide level is less than, say, 100 parts per million by volume, all the valves 56 are in their shut positions; if the carbon monoxide level reaches say 100 parts per million by volume, one of the valves 56 is opened; if the sensed carbon monoxide level reaches, say, 500 parts per million by volume, then a second valve 56 is opened; should the carbon monoxide level reach, say, 1000 parts per million by volume a third valve 56 is opened, and should the sensed carbon monoxide level reach, say, 1500 parts per million by volume the fourth valve 56 is opened. In normal operation, many of the plastic sacks and their contents will be relatively easy to burn, so that immediately the controller 60 becomes responsive to the analyser 64, the carbon monoxide concentration is less than 2% by volume and one or more of the valves 56 are closed according to the precise level of carbon monoxide sensed by the analyser. Thus the oxygen supply rate to the lance 40 is reduced. On the other hand if any particular sack is difficult to burn such that the combustion products from the main combustion region 29 are relatively rich in carbon monoxide, the oxygen concentration in the secondary combustion region 30 will normally be sufficient to prevent significant quantities of carbon monoxide remaining unreacted and entering the flue gas. Accordingly, the apparatus shown in Figure 3 is able to keep down oxygen consumption while enabling the incineration to be performed without giving rise to for any prolonged period of time to flue gas of unacceptable quality. Each time the outer door is opened, the valve controller 60 receives a signal from the position sensor 62, it reverts to a mode of operation independent of the carbon monoxide analyser, with three of the four valves 56 open. If desired, the air supplied to the plenum chamber 20 may be enriched in oxygen. Experiments that have been conducted on a CORSAIR incinerator of the kind shown in Figures 1 and 2 having a single chamber whose internal diameter was approximately 1 metre and whose height was approximately 2.5 metres. The burners 26 and 28 were NUWAY natural gas burners. The total rate of natural gas consumption was 1563 standard cubic feet per hour. Air was supplied to the plenum chamber 20 at a rate of 770 standard cubic feed per hour. Commercially pure oxygen was mixed at a rate of 100 standard cubic feet per hour with the air supplied to the plenum chamber 20. Plastics sacks containing hospital waste of varying composition were fed to the incinerator one every three minutes. By supplying commercially pure oxygen at a basic rate of 3400 standard cubic feet per hour to the lance 40 (which was disposed facing upwards at an angle of 45° to the horizontal) during a first set of periods each extending from, say, 30s before a bag enters the combustion region 29 to 30s after the entry of the bag into the combustion region 29, and thereafter controlling the oxygen supply rate by means of signals representative of the carbon monoxide concentration generated by the detector 66 it is possible to eliminate or a keep to a minimum the number of times the carbon monoxide concentration in the flue gases leaving the incinerator exceed 150 parts per million by volume. In the absence of any supply of commercially pure oxygen the carbon monoxide concentration regularly exceeded 1000 parts per million by volume. A further advantage arising from the use of oxygen in accordance with the invention is that failure to burn some parts of the plastics sacks is avoided and therefore there is no accumulation of unburnt plastics material on the heart 22. Moreover, there is a reduced ash accumulation when the air supplied to the plenum chamber 20 is enriched in oxygen. The ability of a supply of oxygen through the lance 40 to decrease the concentration of carbon monoxide in the flue gas is illustrated in the following Table: The tests whose results are summarised in the Table above were performed on bags of hospital waste. In Test A, yellow bags containing waste from the hospital wards were incinerated. 26 such bags were incinerated over a period of 70 minutes, the bags being fed to an incinerator of the kind shown in Figures 1 and 2 of the drawings one at a time with there being an interval of about 3 minutes between the receipt of one bag and then the next in the series. During Test A, no oxygen was introduced into the incinerator through the lance 40, and no oxygen was added to the air flowing into the incinerator from under the hearth. In Test B, 22 black bags containing normal office waste (mainly paper) were fed one at a time into the incinerator. The experimental procedure adopted was the same as for Test A. In Test C, 8 black bags containing normal office waste (mainly paper) were burned. The bags were fed to the incinerator at intervals of three minutes. The air flow into the hearth of the incinerator was enriched in oxygen so as to increase its oxygen concentration to approximately 30 per cent by volume. Such oxygen enrichment appeared to increase hearth temperature and improve the combustion of carbonaceous material in the waste thus reducing the volume of ash. Oxygen was injected into the incinerator through the lance 40 which was positioned with its outlet horizontal. Oxygen was not introduced continuously through the lance 40. Rather, it was supplied for approximately the first 120 seconds of each 180 second between successive bags being received on the incinerator grate. The results obtained show that the carbon monoxide concentration in the flue gas was decreased in comparison to Test B. In Test D, a similar experimental procedure to that of Test C was adopted. The test was performed on a mixture of bags of the different binds of waste that can arise in a hospital. Since some of these bags contained "difficult to burn" refuse, a higher rate of introduction of oxygen into the incinerator through the lance 40 was chosen. In addition, the lance 40 was disposed with its outlet facing upwards at an angle of 45° to the horizontal. The results obtained show that there was a decreased carbon monoxide concentration in the flue gas in comparison to the results of Test A. Carbon monoxide peaks above 150 ppm in the flue gas were not however entirely eliminated. This result is attributed to the fact that the start of each 120 second pulse of oxygen from the lance 40 tended to lag receipt on the incinerator grate of a respective bag of refuse to be incinerated. Since C0 evolution was extremely rapid once a bag was received on the incinerator grate there was a tendency for some carbon monoxide to "miss" the oxygen injected through the lance 40. It is believed that this problem can be ameliorated by operating the incinerator in accordance with the invention with the receipt of each bag on the incinerator grate lagging behind commencement of a respective pulse of oxygen through the lance 40.

Claims: A method for incinerating waste material by feeding to a main combustion region (29) batches of combustible waste material whose ease of burning may vary randomly from batch to batch, burning said batches of waste material in said main combustion region (29) and thereby forming gaseous combustion products, burning in a secondary combustion region (30) combustibles in said combustion products and supplying oxygen to support the combustion of said combustibles, and discharging flue gas from said secondary combustion region (30), characterised in that in a first set of periods of time the oxygen supply rate is determined independently of the composition of the combustion products or the flue gas, and in a second set of periods of time which each alternate with periods in the first set, the oxygen supply rate is determined as a function of monitored concentration of at least one component of the combustion products or flue gas and in which each first period of time is set so as to comprise a period immediately before a batch of waste is fed to the main combustion region (29). A method as claimed in Claim 1, further characterised in that said component is carbon monoxide. A method as claimed in any one of Claims 1 to 2, further characterised in that the oxygen is introduced into the secondary combustion region (30) with a swirling motion about an axis that extends in the general direction of flow of the combustion products. Apparatus for incinerating waste material including means (32) for feeding in batches to a main combustion region (29) combustible waste material whose calorific value may vary randomly from batch to batch, at least one burner (26) for burning said batches of waste material in a main combustion region (29) and thereby forming gaseous combustion products, a secondary combustion region (30) being heated by a burner (28) for burning combustibles in said combustion products, means (40) for supplying oxygen to said secondary combustion region (30) to support combustion therein, an outlet (14) from the secondary combustion region for discharging flue gas from the apparatus, characterised by a control system (56) for controlling the supply of oxygen to the secondary combustion region, means (62) for detecting a batch of waste material at the entrance and means (66) for monitoring in real time the concentration of a chosen gaseous component of the combustion product or flue gas, such that in a first set of periods of time the oxygen supply rate is determined independently of the composition of the combustion products or the flue gas, and in a second set of periods of time which each alternate with periods in the first set, the rate of supplying oxygen determined as a function of monitored concentration of at least one component of the combustion products or the flue gas. Apparatus as claimed in Claim 4, further characterised in that the control system is automatic and further includes a timer for setting the duration of each first period and one or more automatically-operable valves (56) in a conduit or conduits for supplying oxygen to the secondary combustion region, wherein the detection means (66) is able to generate a signal which starts a first period and actuates the valve or valves (56) to adjust the oxygen supply rate as necessary to a chosen valve, the timer is able to generate a signal that ends the first period and starts a second period, and the gas monitoring means (66) is able to generate a signal which actuates the valve or valves (56) as necessary during the second period to adjust the oxygen supply rate in response to the concentration of the chosen component. Apparatus as claimed in Claim 5, further characterised in that the valves (56) are on-off valves in parallel with one another, the arrangement being such that the oxygen flow rate is determined by the number of the valves that are open at any one time. Apparatus as claimed in Claim 5 or Claim 6, further characterised in that the first combustion region (29) is defined in a chamber having an outer door (34) and an inner door (36) for feeding batches of waste material into the main combustion region, the arrangement being such that opening of the outer door (34) causes the detecting means (62) to generate a signal. Apparatus as claimed in any one of Claims 4 to 7, further characterised in that the main and secondary combustion regions (29, 30) are defined in the same chamber. Apparatus as claimed in any one of Claims 4 to 8, further characterised in that the oxygen supply means is adapted to introduced region with a swirling motion about an axis that extends in the general direction of flow of the combustion products through the secondary combustion region.

Inventors: CHAPMAN ROBERT DAVID, GREDLEY PAUL, CHAPMAN, ROBERT DAVID, GREDLEY, PAUL
Applicants: BOC GROUP PLC, THE BOC GROUP PLC
Application year: 1993
Main classification: F23G5
IPC codes: F23G5, F23N5, F23L7