BACKGROUND OF THE INVENTION 
     The present invention relates to apparatus for heating a blast furnace stove having a combustion region and a combustion gas outlet associated with the combustion region. 
     Blast furnaces are primarily but not exclusively used for the reduction of iron oxide ore to molten iron. The purpose of blast furnace stoves is to provide the blast furnace with a consistent hot-blast temperature, at a desired flow rate, in a safe and environmentally responsible manner over a protracted period of many years. The operation of a blast furnace stove is in principle simple. An air-fuel burner is typically used to burn a fuel gas (typically, predominantly blast furnace gas) and the combustion products are passed through a large mass of refractory brick that captures the sensible heat of the combustion product. Once the refractory bricks have reached the desired operating temperature the burner is shut down and cold air is passed through stove, passing over the bricks, so as to be preheated before being sent to the blast furnace as the hot-blast air. Typically, the stoves are operated in banks of three or four so that some stoves are being heated while others are providing hot blast to the blast furnace. 
     The blast furnace stoves may have any of a number of different configurations. Typically, each stove comprises a first vertical chamber in which combustion takes place along side a second vertical chamber in which the refractory bricks are located. Such a stove is often referred to as being of the external combustion chamber kind. Stoves in which the combustion region is housed in the refractory chamber are also known. These are called “internal” combustion stoves. In another configuration, the combustion chamber is placed on top of the refractory chamber, typically being located within a dome-shaped structure. 
     In current practice, there are three main approaches to try to maximise the amount of heat that can be transferred from the stove to the hot-blast. Providing a hot-blast with as high a heat content as possible reduces the coke rate for iron-making in the blast furnace. To achieve a high hot-blast temperature, the refractory or checker bricks in the stoves need to be heated to as high a temperature as is possible within the physical constraints set by the permissible dome temperature of the stove. In consequence, the calorific value of the fuel gas delivered to the burner must be capable of generating a suitably hot flame. 
     Blast furnace top-gas (often referred to as blast furnace gas) is conventionally the primary fuel used to heat the blast furnace stoves, but the use of this fuel has the drawback that its calorific value is variable, being strongly dependent upon the blast furnace operating practices. The variability of the blast furnace gas&#39; calorific value is such that it is well known to blend the blast furnace gas with a higher calorific value fuel gas such as coke oven gas, converter gas or natural gas, in order to boost its heating value and generate the required flame temperature. It is alternatively known to preheat the fuel gas and air upstream of combustion by the stove burner. Indeed, the combustion gas exiting the stoves during the heating cycle typically has a temperature between 250° and 400° C. and contains about 18% of the energy input to the stoves. In some plants, this relatively hot flue gas is routed to a waste heat recovery unit where a portion of its sensible heat content is capture and used to perform the preheating. Another alternative method of heating the blast furnace stoves is to enrich the combustion air with oxygen. Adding oxygen to replace part of the combustion air increases the flame temperature as, at constant total molecular oxygen flow, the nitrogen ballast in the combustion products is reduced. Commonly, oxygen enrichment of the air is used to facilitate a reduction in the amount of coke oven, converter or natural gas needed to generate the desired flame temperature. 
     It is desirable to improve the operation of blast furnace stoves but in a flexible manner that is able to take account of changes in the availability and cost of fuel and other gases during an operating campaign. 
     SUMMARY 
     According to the present invention there is provided apparatus for heating a blast furnace stove having a combustion region and a combustion gas outlet associated with the combustion region, the apparatus comprising:
         a) a source of lower calorific value fuel;   b) a first pipeline operable to distribute the lower calorific value fuel from the source thereof to the combustion region;   c) a source of air;   d) a second pipeline operable to distribute the air from the source thereof to the combustion region;   e) a source of oxidant comprising at least 85% by volume of oxygen;   f) a third pipeline operable to distribute the oxidant from the source thereof to the combustion region;   g) a fourth pipeline operable to conduct combustion gas from the combustion gas outlet away from the stove; and   h) a fifth pipeline operable to return a portion of the combustion gas to the combustion region.       

     The term “combustion gas” is meant to include the gaseous product of combustion. 
     The apparatus according to the invention is capable of operation in a plurality of different modes, according to the second, third and fifth pipelines that are selected for communication with the combustion region. The most important of these modes is one in which the oxidant comprising at least 85% by volume of oxygen is a sole oxidant used to support combustion and combustion gas is recirculated to the combustion region via the fifth pipeline. A number of advantages can be obtained by operating in this mode. First, desired flame temperatures can be achieved simply by using blast furnace gas as the fuel gas without enrichment with a higher calorific gas such as coke oven gas or natural gas. Second, recycle of the combustion gas makes possible a net reduction in the rate at which carbon dioxide is evolved. Third, advantages analogous to those obtained from the oxygen-enrichment of air (see above) can be obtained. 
     The apparatus according to the invention may be operated with recovery of heat from the combustion gas by passing said gas through a heat recovery heat exchanger. 
     The recirculation of combustion gas to the combustion region dilutes the mixture of fuel and oxidant therein and hence modifies the temperature and reducing the risk of damage to the materials of the stove as a result of the combustion. The combustion may in fact be flameless. 
     The apparatus according to the invention gives the operator of the blast furnace the flexibility to switch to conventional operation employing air to support combustion and raising the calorific value of a blast furnace fuel by employing in addition to the blast furnace fuel a higher calorific value fuel such as coke oven gas, converter gas or natural gas. 
     The apparatus according to the invention may therefore include a source of higher calorific value fuel and a sixth pipeline operable to distribute the higher calorific value fuel to the combustion region. 
     The term “low(er) calorific value fuel” is meant to include a fuel which typically has a calorific value of 9 MJ/Nm 3  or less. As previously mentioned, blast furnace gas is the lower calorific value fuel that is typically used. The term “high(er) calorific value gas” indicates a gas which typically has a calorific value in excess of 9 MJ/Nm 3 . Coke oven gas, converter gas or natural gas is a suitable higher calorific value fuel for use in the apparatus according to the invention. 
     If desired, the apparatus according to the invention may additionally include means for selectively introducing oxidant from the third pipeline into the second pipeline. Such an arrangement offers the operator of the blast furnace the option of operating the stove with oxygen-enriched air. 
     The apparatus according to the invention desirably includes a vent pipe for combustion gas, typically terminating in a stack, which vent pipe typically communicates with the fourth pipeline. When the apparatus according to the invention is operated with recirculation of combustion gas to the combustion region, venting of a portion of the combustion gas limits buildup of impurities in the circulating gas. 
     The source of the lower calorific value fuel gas is typically a blast furnace with which the blast furnace stove forming part of the apparatus according to the invention is associated. 
     The source of air is typically at least one compressor, blower or fan. The compressor is typically separate from the compressor or compressors that supply the air blast to the blast furnace. 
     The source of oxidant comprising at least 85% by volume of oxygen is typically an air separation plant. The oxidant may therefore comprise at least 95% by volume of oxygen. The air separation plant may, for example, separate air by fractional distillation or by pressure swing adsorption. 
     Each of the first to sixth pipelines may include a valve or series of valves which when open gives the desired flow and when closed prevents that flow. The valves may all be associated with a common control apparatus, which if desired may operate automatically and which may be programmable. Each of the first to the sixth pipelines may also include transmitters, safety valves and other control devices which aid the overall operation of the apparatus. 
     If desired, the fourth and fifth pipelines may both communicate with means for treating the combustion gas. The treatment of the combustion gas may comprise recovery of waste heat from it, or recompression, or both. The apparatus according to the invention may therefore comprise a heat exchanger for recovering waste heat from the combustion gas, and a blower or compressor for passing combustion gas from the fourth pipeline to the fifth. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       The apparatus according to the invention will now be described by way of example with reference to the accompanying drawings, in which: 
         FIG. 1  is a simplified illustration of a blast furnace and its associated stoves in a conventional iron works; 
         FIG. 2  is a schematic sectional drawing of a blast furnace stove having an external combustion chamber; and 
         FIG. 3  is a schematic flow diagram illustrating an apparatus of the invention for operation of blast furnace stoves. 
     
    
    
     The drawings are not to scale. Various transmitters, safety valves and other control devices, all well known in the art of gas supply, are omitted from the drawings. 
     DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS 
     Referring to  FIG. 1 , there is shown schematically an arrangement of a blast furnace  120  and three stoves  100  in an iron works. The operation of the blast furnace  120  produces molten iron by reduction of iron oxide with carbon provided by materials such as coke. The reduction of the iron oxide ore to iron causes the formation of carbon monoxide and a gas mixture comprising carbon monoxide, carbon dioxide and nitrogen flows from the top of the blast furnace  120  to a fuel supply control device  110  which controls the supply of the blast furnace top gas to each one of three blast furnace stoves  100 . Each stove  100  has a chamber for the combustion of the top gas from the blast furnace  120  and a chamber for heating an air blast. The air blast is supplied via an air supply control device  130 . The chamber for heating of the air blast comprises refractory material in the form of ceramic bricks or the like, often referred to as checker work. Combustion gases from the combustion chamber of each stove  100  flow through the air heating chamber and give up heat to the refractory bricks. Typically, each stove is operated in accordance with a predetermined cycle such that at any point in time at least one of the stoves is being used to heat the air blast and the rest of the stoves are being heated by combustion of the blast furnace gas. 
     When the refractory bricks are being heated, the resultant combustion or flue gases are fed to a flue gas disposal device  150 . The purpose of the stoves  100  is to provide the blast furnace  120  with a consistent hot-blast temperature, at a desired blow rate over a protracted period of many years. It is well known in the art to control the combustion so as to obtain a consistent stove performance, to reduce energy consumption and to promote both safe operation and an extended campaign life. The combustion chamber of each stove  100  is provided with a burner to effect the combustion. The refractory bricks capture the sensible heat of the combustion product. Once the checker bricks have reached the operating temperature, the burner is shut down and cold air is passed over the refractory bricks where it is preheated before being sent to the blast furnace as “hot blast” air. Typically, the stoves are operating in banks of 3 or 4 so that some stoves are being heated while others are providing hot blasts to the blast furnace. 
       FIG. 2  shows a conventional Cowper stove  100  having an external combustion chamber  101 , refractory material  102  and a dome  103 . The stove is operated so as to ensure that the temperature of the dome  103  does not become so high that damage is caused to the stove  100 . It is to be understood that there are also stoves with internal combustion chambers, and that the apparatus according to the present invention is equally applicable to the operation of such stoves. 
     When the refractory material is being heated, blast furnace top gas is fed to a burner  108  via a fuel inlet  105  and oxidant to the burner  108  via an oxidant inlet  104 . The resulting hot combustion gases flow upwards through the chamber  101  and pass through the dome  103  and down through the chamber lined with the refractory bricks  102 . As a result, the refractory bricks  102  are heated. The resulting combustion gases exit the stove  100  through a port  106 . Typically the temperature of the exiting combustion gases is conventionally about 200°-350° C. When the refractory material of the bricks has reached a predetermined temperature, the operation is switched to heating the air blast. Then, air is introduced through the port  106 , flowing through the chamber lined with the refractory bricks  102 . As a result, the air is heated. The heated air flows though the dome  103 , the combustion chamber  101  and out through an outlet port  107 . At this point, the blast air typically has a temperature of 1100-1200° C. The top gas is preferably taken from a blast furnace to which blast air is provided from the stove  100 . This allows for the arrangement for the stoves  100  near the blast furnace  120 , is energy efficient and helps to make it possible to reduce total emissions from the plant. 
     The blast furnace top gas typically has a calorific value of about 3.2 MJ/Nm 3 . If desired, an alternative low calorific value fuel may be used instead. 
     In general, if air is supplied as the oxidant to the burner  108  in each stove difficulties can arise in obtaining flame temperature sufficiently high to heat the air to the required blast temperature. 
     In order to provide additional heat, the blast furnace gas is supplemented with a fuel gas of higher calorific value. Typically coke oven gas is used for this purpose, but other gases such as converter gas or natural gas can be used instead. The amount of higher calorific value gas that is used is less than that necessary to raise the calorific value of the blast furnace gas to 9 MJ/Nm 3 . 
     Various techniques are available for reducing the amount of higher calorific fuel gas that needs to be added. In one example, the relatively hot flue gas from the stoves, which typically has a temperature between 250° and 450° C., is passed to a waste heat recovery unit where a portion of its sensible heat content is captured and used to preheat the fuel gas prior to combustion by the stove burners. 
     In a second methodology, an oxidant containing at least 85% by volume of oxygen (typically at least 95% by volume of oxygen) is used to replace part of the combustion air. This replacement has the effect of increasing the flame temperature as, at constant total oxygen flow, nitrogen ballast in the combustion products is reduced. If the permissible dome temperature of the stove has not been reached, a higher flame temperature can be exploited to reduce the amount of higher calorific value gas that needs to be added in order to generate the desired flame temperature. Although the desired flame temperature can be maintained at reduced flow rate of higher calorific value gas by virtue of the oxygen enrichment, the energy input to the stoves tends to be reduced. In practice, this is remedied by increasing the flow of blast furnace gas to the stove burner. The higher mass flow rate of blast furnace gas compensates for the reduced air mass flow. As a result, convective heat transfer conditions within the stoves are not seriously effected. 
     There is, however, a practical limit to the amount of oxygen enrichment than can be used in a stove (that is based on current technology) before the flame temperature becomes too high, typically risking damage to the refractory bricks and to the dome of the stove. 
     According to co-pending international patent application PCT/SE2010/051301, the entire contents of which is incorporated herein by reference, the use of the higher calorific value gas may be eliminated altogether by employing an oxidant comprising at least 85% oxygen instead of air and causing combustion gases to be recirculated into the combustion region of the stove. The recirculated combustion gases dilute the mixture of fuel and oxidant sufficiently for the combustion not to cause damage to the materials of the stoves. In fact, the combustion may if desired be flameless. Typically, about one third of the combustion gases generated in the stoves is so recirculated. Although operation with recirculated combustion gases and an oxidant containing at least 85% by volume of oxygen is quite different from operation with the use of air to support combustion and without recirculation of combustion gases, relatively little modification is required of a conventional blast furnace stove to accommodate the change. Typically, the fuel gas will still flow through the existing fuel gas ports and the recirculated combustion gases and the oxidant containing at least 85% by volume of oxygen would be premixed to form a “synthetic air” which can be introduced through the existing air ports. In all cases, the total mass flow through the stoves is maintained at or very close to the mass flow for the conventional air-fuel operation. Although the quantity of blast furnace gas increases, there is a corresponding reduction in the flow of other gases into the stoves with the result that the overall mass flow is not substantially altered. 
     The formation of a “synthetic air” comprising recirculated combustion gases and oxidant containing at least 85% by volume of oxygen may form a gas mixture which, in comparison with air, has a relatively high concentration of oxygen. If desired, those parts of the necessary gas pipeline for handling such a gas mixture may be formed of materials such as copper or other materials which are safe for the use with oxygen. Alternatively, if it is wished to avoid having to form the inlet pipe to the “synthetic air” ports of such material, some of the oxygen may be introduced into the combustion chamber via one or more lances. 
     Blast furnaces are conventionally operated continuously for a period of several years. During the period of such an operating campaign, the cost and availability of the various feeds to the blast furnace and to the blast furnace stoves may vary. Accordingly, although it is believed by us that operation with recirculation of combustion gases is generally desirable, an operator of a blast furnace may require a certain flexibility in the way in which the blast furnace stoves are operated. The heating apparatus embodiment according to the invention provides this flexibility. An example of this apparatus is shown in  FIG. 3 . Various one-way valves, flow control valves and the like are omitted from  FIG. 3  so as to facilitate an understanding of the inventive embodiment. 
     Referring to  FIG. 3 , a plurality of for example four blast furnace stoves  302 ,  304 ,  306  and  308  is shown. The stoves  302 ,  304 ,  306  and  308  are connected in parallel with each other. The apparatus comprises a main air pipeline  310 , a main low calorific value fuel (blast furnace gas) pipeline  320 , a main high calorific value fuel (coke oven gas) pipeline  330 , a main combustion gas pipeline  340 , a main oxygen pipeline  350  and a main recycle gas pipeline  360 . The pipelines are associated with gas headers or distributors (not shown) which afford appropriate communication between the various pipelines and the inlets and outlets to the stoves, these inlets and outlets being essentially similar to those of the stove shown in  FIG. 2 . Thus, the main air inlet pipeline  310  receives air from a compressor  309  and communicates with the respective inlet ports of the stoves  302 ,  304 ,  306  and  308  via distribution pipes  312 ,  314 ,  316  and  318 , respectively. Blast furnace gas is distributed from the main blast furnace gas pipeline  320  to the stoves  302 ,  304 ,  306  and  308  via blast furnace gas distribution pipes  322 ,  324 ,  326  and  328 , respectively. Similarly, coke oven gas or other high calorific value fuel may be distributed to the stoves  302 ,  304 ,  306  and  308  via coke oven distribution pipes  332 ,  334 ,  336  and  338 , respectively. Combustion gases flow out of the stoves  302 ,  304 ,  306  and  308  through combustion gas distribution pipes  342 ,  344 ,  346  and  348  respectively, all of which communicate with the main combustion pipeline  340 . 
     The pipeline  340  terminates in a recycle gas blower  370  and extends through an operational waste heat recovery unit  380 . Intermediate a waste heat recovery unit  380  and the recycle gas blower  370  there is a vent pipeline  390  which leads waste gas to a stack (not shown) for discharge to the atmosphere. 
     The outlet of the blower  370  communicates with the combustion gas recirculation pipeline  360 . The recirculation gas pipeline  360  is connected to each of the air distribution pipes  312 ,  314 ,  316  and  318 . The main oxygen pipeline  350  can supply oxygen produced in air separation plant  351  to each of the distribution pipes  312 ,  314 ,  316  and  318 . Alternatively or additionally, it can supply the oxygen directly to the stoves  302 ,  304 ,  306  and  308  via oxygen distribution pipes  352 ,  354 ,  356 ,  358  respectively. 
     If desired, a by-pass pipe may be used allowing the combustion gases of the pipeline  340  to by-pass the waste heat recovery unit  380 . The waste heat recovery unit  380  is typically arranged to transfer heat from the combustion gas to the gas air fed to the blast furnace. 
     The apparatus shown in  FIG. 3  is capable of being operated in a plurality of different modes, which have been described above. These modes include:
         a) with blast furnace gas, high calorific value fuel gas, for example, coke oven gas, and air supplied to the stoves, but without oxygen supply combustion gas recycle and waste heat recovery from the combustion gas;   b) as (a), but with waste heat recovery with the combustion gas;   c) as (b), but with oxygen-enrichment of the air, and without high calorific value fuel gas supply;   d) with blast furnace supply, oxygen supply and combustion gas recycle but without air supply, without high calorific value gas supply and without waste heat recovery from the combustion gas;   e) as (d), but with waste heat recovery from the combustion gas; and   f) as (e), but with air supply as well.       

     Example (f) above is essentially similar to example (e) but without total replacement of the combustion air with oxygen and recirculated combustion gas, the combustion air only being partially replaced with these gases. 
     The source of oxygen is preferably an air separation plant producing oxygen of at least 95% purity and typically at least 99.9% purity. 
     To enable the apparatus to be operated in any one of the above mentioned modes, an array of on/off valves is provided. Referring again to  FIG. 3 , there are provided of supply valves  313 ,  315 ,  317  and  319  in the pipelines  312 ,  314 ,  316  and  318  respectively; high calorific value fuel gas (coke oven gas) distribution valves  333 ,  335 ,  337  and  339  in the high calorific value fuel gas pipes  332 ,  334 ,  336  and  338  respectively; a recycle gas shut off valve  341 ; main oxygen supply valves  353 ,  355 ,  357  and  359  in the oxygen supply pipes  352 ,  354 ,  356  and  358  respectively; oxygen enrichment valves  393 ,  395 ,  387  and  399  operable to enrich in oxygen the air flowing through the pipes  312 ,  314 ,  316  and  318  respectively; recirculated gas valves  363 ,  365 ,  367  and  369  communicating with the pipes  312 ,  314 ,  316  and  318  respectively; a waste heat recovery valve  382  and a waste heat recovery unit by-pass valve  384 . 
     The above mentioned valves can be opened and closed in order to operate the illustrated apparatus in any one of the modes according to examples (a)-(f) above so as to heat the stoves. The necessary valve positions are provided in Table 1 one below. Typically, only one (or possibly two) of the stoves is heated at any one time. 
     In example (c) in Table 1, in addition to enriching the air in oxygen through valves  393 ,  395 ,  397  and  399  according to which of the stoves is being heated, oxygen may optionally be lanced directly into the stoves  302 ,  304 ,  306 ,  308 , in which case valves  353 ,  355 ,  357  and  359  are opened. 
     It is to be appreciated that the apparatus may be operated in modes other than (a)-(f) described above. For example, waste heat recovery may be employed in all modes, not just in (b) and (c). 
     Some illustrative operating parameters are given for the modes of operation (a)-(e) in Table 2. 
     It can be seen that there is no need for the blast furnace gas to be supplemented with coke oven gas in example (c)-(e). Examples (d) and (e) are preferred to example (c) because of the higher carbon dioxide content of the stack gas if the carbon dioxide is to be captured or recovered. 
     A particular advantage of operating in mode (d) is that a rate at which nitrogen molecules enter the stoves is less than in other of the modes, thereby resulting in reduced formation of oxides of nitrogen. Even when the apparatus shown in  FIG. 3  is operated with a recycle, there should be no need to subject the combustion gas to chemical treatment to remove oxides of nitrogen. 
     
       
         
               
               
             
               
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                   
                 Valves Open 
               
             
          
           
               
                   
                 Stove 302 
                 Stove 304 
                 Stove 306 
                 Stove 308 
               
               
                 Example 
                 being heated 
                 being heated 
                 being heated 
                 being heated 
               
               
                   
               
               
                 a) 
                 313 
                 315 
                 317 
                 319 
               
               
                   
                 323 
                 325 
                 327 
                 329 
               
               
                   
                 333 
                 335 
                 337 
                 339 
               
               
                   
                 384 
                 384 
                 384 
                 384 
               
               
                 b) 
                 313 
                 315 
                 317 
                 319 
               
               
                   
                 323 
                 325 
                 327 
                 329 
               
               
                   
                 333 
                 335 
                 337 
                 339 
               
               
                   
                 382 
                 382 
                 382 
                 382 
               
               
                 c) 
                 313 
                 315 
                 317 
                 319 
               
               
                   
                 323 
                 325 
                 327 
                 329 
               
               
                   
                 (353) 
                 (355) 
                 (357) 
                 (359) 
               
               
                   
                 393 
                 395 
                 397 
                 399 
               
               
                   
                 382 
                 382 
                 382 
                 382 
               
               
                 d) 
                 323 
                 325 
                 327 
                 329 
               
               
                   
                 353 
                 355 
                 357 
                 359 
               
               
                   
                 363 
                 365 
                 367 
                 369 
               
               
                   
                 393 
                 395 
                 397 
                 399 
               
               
                   
                 341 
                 341 
                 341 
                 341 
               
               
                   
                 384 
                 384 
                 384 
                 384 
               
               
                 e) 
                 323 
                 325 
                 327 
                 329 
               
               
                   
                 353 
                 355 
                 357 
                 359 
               
               
                   
                 363 
                 365 
                 367 
                 369 
               
               
                   
                 393 
                 395 
                 397 
                 399 
               
               
                   
                 341 
                 341 
                 341 
                 341 
               
               
                   
                 384 
                 384 
                 384 
                 384 
               
               
                 f) 
                 313 
                 315 
                 317 
                 319 
               
               
                   
                 323 
                 325 
                 327 
                 329 
               
               
                   
                 353 
                 355 
                 357 
                 359 
               
               
                   
                 363 
                 365 
                 367 
                 369 
               
               
                   
                 393 
                 395 
                 397 
                 399 
               
               
                   
                 341 
                 341 
                 341 
                 341 
               
               
                   
                 384 
                 384 
                 384 
                 384 
               
               
                   
               
             
          
         
       
     
     
       
         
               
               
               
               
               
               
             
               
               
               
               
               
               
             
           
               
                 TABLE 2 
               
               
                   
               
               
                   
                 a) 
                 b) 
                 c) 
                 d) 
                 e) 
               
               
                   
               
             
             
               
                   
               
             
          
           
               
                 Blast Furnace Gas Nm 3 /h 
                 44370 
                 54461 
                 64000 
                 64000 
                 64000 
               
               
                 Blast Furnace Gas 
                 120 
                 215 
                 215 
                 120 
                 120 
               
               
                 Temperature. ° C. 
                   
                   
                   
                   
                   
               
               
                 Coke Oven Gas Nm 3 /h 
                 3100 
                 1457 
                 0 
                 0 
                 0 
               
               
                 Coke Oven Gas 
                 5 
                 5 
                 — 
                 — 
                 — 
               
               
                 Temperature. ° C. 
                   
                   
                   
                   
                   
               
               
                 Air Flow Nm 3 /h 
                 43000 
                 39095 
                 28000 
                 0 
                 14000 
               
               
                 Air Temperature ° C. 
                 120 
                 215 
                 215 
                 — 
                 120 
               
               
                 Oxygen Flow Nm 3 /h 
                 0 
                 0 
                 1900 
                 8000 
                 5250 
               
               
                 Oxygen Temperature 
                 — 
                 — 
                 20 
                 20 
                 20 
               
               
                 ° C. 
                   
                   
                   
                   
                   
               
               
                 Flue Gas Recycle 
                 0 
                 0 
                 0 
                 12987 
                 4000 
               
               
                 Flue Gas Temperature 
                 — 
                 — 
                 — 
                 300 
                 300 
               
               
                 ° C. 
                   
                   
                   
                   
                   
               
               
                 Flame Temperature ° C. 
                 1444 
                 1453 
                 1456 
                 1460 
                 1448 
               
               
                 Heat of Combustion GJ&#39;h 
                 184 
                 182 
                 181 
                 181 
                 182 
               
               
                 Stack Gas Oxygen 
                 1 
                 0.5 
                 0.5 
                 1 
                 1 
               
               
                 Content % 
                   
                   
                   
                   
                   
               
               
                 Stack Gas CO2 
                 23.5 
                 28 
                 32 
                 43.5 
                 37 
               
               
                 Content %
An apparatus for heating a blast furnace stove having a combustion region and a combustion gas outlet associated with the combustion region includes a source of lower calorific value fuel; a first pipeline for supplying the lower calorific value fuel to the combustion region; a source of air; a second pipeline for supplying the air to the combustion region; a source of oxidant comprising at least 85% by volume of oxygen; a third pipeline to supply the oxidant to the combustion region; a fourth pipeline communicating with the combustion gas outlet for conducting combustion gas away from the stove; and a fifth pipeline operable to recirculate combustion gas to the combustion region. The apparatus may operate in different modes according to which of the pipelines are placed in communication with the combustion region.