JP6541050B2 - High temperature oxygen combustion apparatus and high temperature oxygen combustion method - Google Patents

Description

  The present invention relates to a high temperature oxyfuel combustion apparatus and a high temperature oxygen combustion method, and more particularly, a pure oxygen or an oxidant containing pure oxygen is heated to an ultrahigh temperature range of 800 ° C. or higher to obtain a hydrocarbon fuel and The present invention relates to a high temperature oxygen combustion apparatus and a high temperature oxygen combustion method for mixing.

  Industrial heating furnaces such as tube furnaces, metal furnaces, ceramic furnaces, metal melting furnaces, gasification melting furnaces or boilers, or combustion heating type heat dissipation devices such as radiant tube burners are fuels that supply hydrocarbon fuels. A supply device, an air supply device for supplying combustion air, and a combustion device such as a burner for mixing fuel and combustion air and burning the fuel. The fuel and combustion air mixed in the combustion device generate a flame by diffusion combustion in the combustion zone.

In order to achieve complete combustion of fuel in a general combustion device, it is necessary to set the actual amount of air for combustion air to an excess air ratio exceeding the theoretical amount of air for fuel, and therefore, the air and fuel for combustion are The mixing ratio (air fuel efficiency) of is set to approximately 14 to 15. For example, the fuel volume of methane fuel supplied to the combustion device is set to about 1/15 of the required air amount. Many combustion equipments are provided with a flame holder such as a swirl flow type or a flame holding plate type in order to mix the fuel injection stream having such flow rate difference and the air flow as desired. A flame holder is disposed in the mixing zone of fuel and air to form an ignitable high temperature circulating flow, thereby preventing flame blowout and ensuring flame stability.

  As a combustion method developed by the applicants of the present invention, combustion air is set to 800 ° C. using a heat storage regenerative burner system (a regenerative burner system) equipped with a switching heat storage type heat exchanger of a honeycomb structure or the like. A high-temperature air combustion method is known in which the above-described ultra-high temperature region is preheated and high-temperature preheated air is introduced into the mixing region or combustion region (Japanese Patent Laid-Open No. 6-2135895 (Patent Document 1)). The combustion mode of the flame by high temperature preheated air heated to 800 ° C or higher is the combustion mode of a normal flame by preheated air of 400 ° C or lower, or the combustion of transition flame by preheated air heated to the temperature range of 400 to 800 ° C. As compared with the mode, stable combustion occurs in a combustion atmosphere of a very wide range of air ratios. According to such a high temperature air combustion method, not only the combustion field of extremely low oxygen concentration (3 to 10%) can be formed in the furnace, but also the heat dispersion flame in which the local heat generation phenomenon is suppressed is As a result, the temperature field in the furnace can be made uniform, and the amount of NOx generated can be reduced.

  The applicant also filed a high temperature air combustion method in which the combustion gas (in-furnace gas) led out of the furnace or the steam generated separately is mixed with fuel (or fuel and combustion air) as an international patent application PCT / It is proposed in JP 00/05454 (WO 01/13042 (patent document 2)). According to the high temperature air combustion method described in this publication, the momentum (momentum) of the fuel injected into the furnace is increased, and the controllability of the mixing process and the mixing ratio of the fuel and the combustion air is improved, whereby It is possible to control the flame characteristics effectively.

  According to such a high temperature air combustion method, the heat recovery rate is improved to 80 to 90% close to the theoretical limit, the energy consumption amount is reduced by about 30% and the NOx generation amount is reduced by 50% or more. Furthermore, the improvement of the heat transfer efficiency makes it possible to reduce the overall size of the facility by about 20%.

  In addition, the applicant of the present invention, as a furnace gas circulation unit usable in the high temperature air combustion method, includes a circulation fan for delivering the furnace gas to the supply / discharge port via the heat storage device, the furnace gas outlet position or the internal gas injection. Japanese Patent Laid-Open No. 2004-354041 (Patent Document 3) proposes an in-furnace gas circulation unit having a feed / discharge switching valve device that can be switched to a position. The in-furnace gas circulation unit described in the publication can be disposed at any position of the furnace body to control in-furnace circulation or agitation of in-furnace gas.

  Furthermore, in the heat storage and regeneration type burner system provided with the switching type heat storage type heat exchanger, pure oxygen is added to the combustion air to raise the flame temperature, and the oxygen concentration in the combustion air is increased to achieve high oxygen concentration and Japanese Patent Application Laid-Open No. 8-94064 (Patent Document 4) describes a technique for forming a combustion flame from high-temperature combustion air in a furnace. In addition, as an application of such a heat storage and regeneration type burner system, an oxyfuel combustion method of supplying pure oxygen into a furnace through a switchable heat storage type heat exchanger is described in European Patent Application Publication No. EP0928938 (Patent Document 5) ing. In this oxyfuel combustion method, pure oxygen is heated to a high temperature by the switchable heat storage type heat exchanger, and the high temperature pure oxygen is mixed and contacted with the hydrocarbon-based fuel in the furnace region to cause an in-furnace combustion reaction. In such a high temperature oxy-fuel combustion method, a part of the furnace gas is constantly exhausted outside the furnace in order to secure the supply and discharge balance and the heat balance of the switchable heat storage type heat exchanger.

Japanese Patent Laid-Open No. 6-2135895 WO 01/13042 Japanese Patent Application Laid-Open No. 2004-354041 JP-A-8-94064 European Patent Application Publication No. EP0928938

  As mentioned above, according to the high temperature air combustion method, the heat recovery rate is improved to 80 to 90% close to the theoretical limit, and the energy consumption is reduced by about 30% compared to the conventional rate, and the NOx generation amount is 50% or more It is possible to reduce the size of the entire equipment by about 20% by reducing the heat transfer efficiency. Such improvement of energy efficiency and downsizing of equipment are considered to be close to the limit as a combustion method and a combustion apparatus. However, for further advancement of combustion technology, it is desirable to develop a new combustion method which can further improve such energy efficiency and further miniaturize the combustion equipment and further suppress the generation of NOx. Be

  In this regard, it is conceivable to adopt an oxyfuel combustion method in which pure oxygen preheated to a high temperature is supplied to a combustion furnace by sensible heat possessed by combustion exhaust gas, as in the oxyfuel combustion method described in Patent Document 5. According to the oxyfuel combustion method using the heat storage and regeneration type burner system, it is possible to substantially completely prevent the generation of NOx in the combustion zone.

  However, oxygen heated to 800 ° C. or higher is extremely reactive, and therefore, oxidation / corrosion of metals or ceramics of a heat exchanger constituting a heat storage regenerative burner system, oxidation of a furnace body of a combustion furnace, Since the corrosion and the like easily occur, there is a circumstance that it is difficult to adopt such an oxyfuel combustion method as a general industrial furnace combustion facility.

  In addition, conventional oxyfuel combustion methods are intended to produce mainly high temperature flames by the combustion reaction of oxygen and fuel. However, in many industrial furnaces, the flame temperature does not exceed the heat resistance temperature of the fireproof and heat insulating material applied to the inner surface of the furnace, while preventing or suppressing the local increase in temperature of the flame, And it is desirable to produce a relatively low temperature diffusion combustion flame in the furnace. For this reason, it is desirable to produce such a diffusion combustion flame by a high temperature oxy-fuel combustion method.

  The present invention has been made in view of such circumstances, and the object of the present invention is to supply pure oxygen to a regenerative thermal burner system and heat it to an ultra-high temperature range of 800 ° C. or higher to obtain high-temperature oxygen High temperature oxygen combustion apparatus and high temperature oxygen combustion method of an industrial furnace which causes a combustion reaction with hydrocarbon fuel, which substantially completely prevents the generation of NOx in the combustion zone, and compared with the high temperature air combustion method. An object of the present invention is to provide a high temperature oxygen combustion apparatus and a high temperature oxygen combustion method which can further reduce energy consumption and further miniaturize a combustion furnace and a combustion facility, and can be preferably used in a general industrial furnace.

To achieve the above object, the present invention, the combustion system having a combustion zone, an oxidant supply device for supplying to the combustion zone of pure oxygen as an oxidizing agent, the combustion gas generated in the combustion zone and an exhaust system device or equipment for exhausting to the outside of the combustion system, the hot oxygen combustion device for combustion reaction in the combustion zone and heated with the oxidant and hydrocarbon fuel to a temperature above 800 ° C. ,
The combustion zone, a fuel supply unit for supplying the hydrocarbon-based fuel to the combustion zone, the pure oxygen and the combustion gas, the sensible heat held by the combustion gas is transferred to the pure oxygen to be transferred to the pure oxygen A heat storage and regeneration type heat exchanger for heating pure oxygen to a temperature of 800 ° C. or higher, an oxidant introduction path for introducing pure oxygen of the oxidant supply device into the combustion zone through the heat exchanger, and The combustion gas is added to the pure oxygen heated to a temperature of 800 ° C. or more, and a combustion gas lead-out path for leading the combustion gas out of the combustion zone and delivering it to an exhaust system or facility via a heat exchanger or constitute the combustion system by the air-fuel mixture generating means for generating a mixture of the said combustion gas and said pure oxygen the pure oxygen diluted with the combustion gases,
The mixing a portion of the combustion gas by the gas generating means is recirculated in the system of the combustion system to produce the mixture, the mixture that by the catalytic combustion reaction between the hydrocarbon fuel and the mixture the cause in the combustion zone to provide a high-temperature oxygen combustion apparatus according to claim Rukoto.
The present invention also provides a combustion system having a combustion zone, an oxidant supply device for supplying pure oxygen as an oxidant to the combustion zone, and a combustion gas generated in the combustion zone outside the system of the combustion system. A high temperature oxygen combustion apparatus having an exhaust system or an exhaust system for exhausting, wherein the oxidizing agent heated to a temperature of 800 ° C. or more and a hydrocarbon based fuel are burned and reacted in the combustion zone,
The combustion zone, fuel supply means for supplying the hydrocarbon-based fuel to the combustion zone, the combustion gas is added to the pure oxygen, or the pure oxygen is diluted with the combustion gas to produce the pure oxygen and the combustion A mixture generation means for generating a mixture with a gas, the mixture and the combustion gas are brought into contact, the sensible heat held by the combustion gas is transferred to the mixture, and the mixture is heated to a temperature of 800 ° C. or more A regenerative heat exchanger for heating, an oxidant introduction path for introducing pure oxygen of the oxidant supply device into the combustion zone through the heat exchanger, and the combustion through the heat exchanger The combustion system is constituted by a combustion gas lead-out path for leading gas out of the combustion zone and delivering it to an exhaust system or facility;
A part of the combustion gas is recirculated in the system of the combustion system by the mixture generation means to generate the mixture, and the combustion is performed by mixed contact of the mixture after heating and the hydrocarbon fuel. There is provided a high temperature oxy-fuel combustion apparatus characterized by causing a combustion reaction in a zone .

Preferably, the mixture generation means sets the oxygen concentration of the mixture within a range of 20 to 60% by volume (preferably, within a range of 30 to 50%). Optionally , the combustion gas is mixed with pure oxygen heated or preheated to 150 ° C. or higher.

Further, the present invention is to combustion zone constituting the combustion system, the pure oxygen supplied from the oxidizing agent supply device is supplied to the combustion zone as the oxidizing agent, and the oxidizing agent heated to a temperature above 800 ° C. carbide a hydrogen-based fuel is combusted reaction by the combustion zone, the hot oxygen combustion method of evacuating to the outside of the combustion system by the exhaust system apparatus or installation the combustion gas generated in the combustion zone,
The combustion zone, a fuel supply unit for supplying the hydrocarbon-based fuel to the combustion zone, the pure oxygen and the combustion gas, the sensible heat held by the combustion gas is transferred to the pure oxygen to be transferred to the pure oxygen A heat storage and regeneration type heat exchanger for heating pure oxygen to a temperature of 800 ° C. or higher, an oxidant introducing path for introducing the pure oxygen into the combustion zone via the heat exchanger, and the heat exchanger via the heat exchanger wherein the combustion gases derived from the combustion zone exhaust system device or combustion gas outlet passage for delivering the equipment, addition of the combustion gas to the pure oxygen which was heated to a temperature above 800 ° C. or the pure oxygen Te The combustion system is constituted by mixture generation means for diluting the mixture with the combustion gas to generate a mixture of pure oxygen and the combustion gas ;
The mixing a portion of the combustion gas by the gas generating means is recirculated in the system of the combustion system to produce the mixture, the mixture that by the catalytic combustion reaction between the hydrocarbon fuel and the mixture The present invention provides a high temperature oxygen combustion method characterized in that it is generated in the combustion zone .
Furthermore, according to the present invention, pure oxygen supplied from the oxidant supply device is supplied to the combustion zone as an oxidant to the combustion zone constituting the combustion system, and the oxidant and carbonized are heated to a temperature of 800 ° C. or higher A high-temperature oxygen combustion method in which a hydrogen-based fuel is burned and reacted in the combustion zone, and the combustion gas generated in the combustion zone is exhausted out of the system of the combustion system by an exhaust system or equipment.
The combustion zone, a fuel supply means for supplying the hydrocarbon-based fuel to the combustion zone, the combustion gas added to the pure oxygen, or the pure oxygen diluted with the combustion gas to obtain pure oxygen and combustion gas A mixture producing means for producing a mixture, the mixture and the combustion gas are contacted, and the sensible heat held by the combustion gas is transferred by the mixture to heat the mixture to a temperature of 800 ° C. or more A heat storage / regeneration type heat exchanger, an oxidant introduction path for introducing the pure oxygen into the combustion area through the heat exchanger, and the combustion gas is discharged from the combustion area through the heat exchanger. The combustion system from the combustion gas lead-out path for delivery to the exhaust system or equipment;
A part of the combustion gas is recirculated in the system of the combustion system by the mixture generation means, and a combustion reaction due to mixed contact of the mixture after heating and the hydrocarbon fuel is generated in the combustion zone The present invention provides a high temperature oxygen combustion method characterized by

Preferably, the oxygen concentration of the mixture is set in the range of 20 to 60% by volume (preferably in the range of 30 to 50% by volume). Optionally , the combustion gas is mixed with pure oxygen heated or preheated to 150 ° C. or higher.

  According to the above configuration of the present invention, since the combustion reaction of pure oxygen and hydrocarbon fuel proceeds in the combustion zone, the volume of the flue gas to be discharged to the outside of the furnace is reduced, therefore the heat quantity discharged to the outside of the system Decreases. Further, since the water vapor and carbon dioxide generated in the combustion area are both radiation gases, the heating performance or heat transfer performance for the object to be heated or the like disposed in the combustion area is improved. These matters are clearly different from hot air combustion. That is, according to the present invention, energy consumption can be further reduced and the combustion furnace and the combustion equipment can be further miniaturized as compared with the high temperature air combustion method.

  Also, pure oxygen is mixed with the combustion gas generated in the combustion zone by high temperature oxygen combustion, and a mixture of pure oxygen and combustion gas is supplied to the combustion zone. The mixture comes into mixed contact with the hydrocarbon-based fuel and burns and reacts. Since the combustion gas of pure oxygen and hydrocarbon fuel substantially contains only carbon dioxide and water vapor, the mixture is a mixture of pure oxygen, carbon dioxide and water vapor. Therefore, there is no possibility that nitrogen oxides are generated in the combustion zone except for a small amount of ambient air entering the furnace due to an unintended leak or the like and a slight nitrogen oxide derived from a nitrogen compound contained in the fuel. Therefore, according to the above configuration of the present invention, it is possible to substantially completely prevent the generation of NOx in the combustion zone. According to the present invention, as will be described later, the phenomenon that the temperature of the flame does not become extremely high, and therefore nitrogen oxides are formed in the combustion zone due to nitrogen contained in such ambient air and fuel. Is also suppressed.

  Furthermore, in the present invention, pure oxygen is mixed with the combustion gas (carbon dioxide and water vapor), so that the oxidant with a reduced concentration of oxygen (for example, an oxidant with an oxygen concentration of 20 to 50% by volume) As a result, it is possible to prevent the flame temperature from becoming extremely high. Thus, by preventing the temperature of the flame from becoming extremely high, a conventional fireproof and heat insulating material having known fire resistance performance can be used as a fireproof and heat insulating material that divides or defines the combustion zone and the flow passage. It becomes possible to use or form an industrial furnace, a flow path, etc. In the combustion reaction between the above-mentioned mixture heated to an ultra-high temperature range of 800 ° C. or more and the hydrocarbon fuel, the oxygen concentration (volume ratio) of the mixture is 20% or more (preferably 30% or more). In the case, it was found by experiments of the present inventors that a stable combustion reaction is obtained and the flame shape is stabilized in a substantially equal shape.

From another aspect, the present invention has an oxidant feed device for feeding the furnace with pure oxygen as an oxidizing agent, and an exhaust system for exhausting the combustion exhaust gas out of the system, the combustion exhaust gas is held In the high-temperature oxygen combustion apparatus, the sensible heat is transferred to the oxidizing agent to heat the oxidizing agent to a temperature of 800 ° C. or higher, and the heated oxidizing agent and the hydrocarbon fuel are burned and reacted in the furnace region,
Heat storage and regeneration, alternately connected to the pure oxygen supply source of the oxidant supply device and the exhaust system, for leading out the furnace combustion gas to the outside of the furnace and supplying the pure oxygen of the pure oxygen supply source to the furnace region First and second heat exchangers of a type;
A flow path switching device which causes the heat storage bodies of the respective heat exchangers to be alternately in fluid communication with the exhaust system or the pure oxygen source;
The flow passage in the first heat exchanger and the flow passage in the second heat exchanger are interconnected with each other, and a part of the combustion exhaust gas exhausted from the one heat exchanger to the outside of the system is exchanged with the other heat exchange And a communication passage for supplying the flue gas to the pure oxygen to be supplied to the flow path of the
There is provided a high-temperature oxygen combustion apparatus characterized in that the mixture of the pure oxygen and the combustion exhaust gas and the hydrocarbon-based fuel are burned and reacted in a furnace area.
Preferably, the communication passage attracts the flue gas by the fluid pressure of pure oxygen and mixes the flue gas with pure oxygen. If desired, the flue gas is mixed with pure oxygen heated or preheated to 150 ° C. or higher.

The present invention also supplied to and combustion exhaust gas into the furnace while the exhaust from the system as the oxidant of pure oxygen, the oxidizing agent 800 ° C. or higher by heating transferred to the oxidant the sensible heat flue gas's High-temperature oxygen combustion method in which the oxidant after heating and the hydrocarbon fuel are burned and reacted in the furnace region,
The heat storage and regeneration type first and second heat exchangers are alternately connected to the pure oxygen source and the exhaust system, and the heat storage bodies of the respective heat exchangers are alternately fluidly connected to the pure oxygen source and the exhaust system,
The flow passage in the first heat exchanger and the flow passage in the second heat exchanger are interconnected with each other, and a part of the combustion exhaust gas exhausted out of the system from one heat exchanger is transferred to the other heat exchanger features and supplied to the flow path, with the addition of flue gas in the pure oxygen to produce a mixture of pure oxygen and combustion exhaust gas, that burning reaction of hydrocarbon fuel and said mixture in a furnace region To provide a high temperature oxygen combustion method.
Preferably, the flue gas is attracted by the fluid pressure of pure oxygen and mixes with it. If desired, the flue gas is mixed with pure oxygen heated or preheated to 150 ° C. or higher.

  According to the above configuration of the present invention, a part of the flue gas exhausted out of the system via one heat exchanger is supplied to the other heat exchanger. The heat storage body of each heat exchanger receives heat in heat transfer contact with combustion exhaust gas and stores it, and then heat transfer contact with pure oxygen or a mixture of pure oxygen and combustion exhaust gas to dissipate heat, pure oxygen or mixture Heat your mind. The mixture of pure oxygen and the combustion exhaust gas after heating, or the mixture after heating mixes and contacts the hydrocarbon-based fuel supplied into the furnace, and causes a combustion reaction in the furnace area. The mixture of pure oxygen and its flue gas does not contain nitrogen, so that it is possible to substantially completely prevent the generation of NOx in the combustion zone. Further, according to the combustion reaction of pure oxygen and hydrocarbon fuel, the volume of the flue gas to be discharged to the outside of the furnace is reduced, and hence the amount of heat discharged to the outside of the system is reduced. Moreover, since the steam and carbon dioxide generated by the combustion reaction are both radiation gases, the heating performance or heat transfer performance of the combustion furnace is improved. For this reason, energy consumption is further reduced as compared with the high temperature air combustion method. Moreover, in the high temperature oxygen combustion method of the present invention, the flow rates of the intake fluid and the exhaust fluid and the flow rate of the circulating fluid in the system are reduced compared to high temperature air combustion, so the combustion furnace and the combustion equipment are It can be further miniaturized.

  In addition, according to the above configuration of the present invention, since the pure oxygen diluted by the combustion exhaust gas (carbon dioxide and steam) burns and reacts with the hydrocarbon fuel, the oxygen and the fuel slowly react and the flame temperature becomes local A wide range of relatively low temperature diffusion combustion flames can be produced in the furnace while suppressing the temperature rise.

  Further, according to the above configuration of the present invention, since high temperature pure oxygen is diluted by the combustion exhaust gas, oxidation / corrosion is prevented from occurring in the furnace body of the combustion furnace or the like by high temperature pure oxygen of 800 ° C. or higher. Can. Preferably, the flue gas is added to the pure oxygen before heating, or to the pure oxygen of the heating process heated to an intermediate temperature (for example, about 400 ° C.). Thereby, it is possible to reliably prevent oxidation and corrosion of the flow path wall and the like in the heat exchanger by high temperature pure oxygen of 800 ° C. or higher.

Even more another aspect, the present invention has an oxidant feed device for feeding the furnace with pure oxygen as an oxidizing agent, and an exhaust system for exhausting the combustion exhaust gas from the system, and the oxidizing agent In a high temperature oxy-fuel combustion apparatus that burns and reacts with hydrocarbon fuel in the furnace region,
Pure oxygen injection means disposed on the inner wall surface of the furnace to inject pure oxygen into the furnace area and induce furnace gas by a pure oxygen jet to dilute and heat pure oxygen with the furnace gas;
Fuel injection means disposed on the inner wall surface of the furnace and injecting hydrocarbon fuel into the furnace so as to mix and contact hydrocarbon fuel with pure oxygen after dilution;
The in-furnace gas is led out of the furnace to exhaust a part of the in-furnace gas out of the system, and the in-furnace gas exhausting / circulating device is provided to recirculate the remainder of the in-furnace gas to the in-furnace region. ,
The in-furnace gas exhaust and circulation device has a heat storage body of a heat storage and regeneration type heat exchanger which is heated in heat transfer contact with the in-furnace gas led to the outside of the furnace and cools the in-furnace gas. A high temperature oxygen combustion apparatus characterized in that a part of the internal gas is exhausted to the outside of the system, and the remaining part of the furnace gas is brought into heat transfer contact with the heat storage body to be reheated and then returned to the furnace area. Do.
Preferably, the in-furnace gas exhaust and circulation device leads out-furnace gas having a flow rate of at least 9 times the total flow rate of pure oxygen and fuel out of the furnace.

The present invention also relates to a high temperature oxygen combustion method in which pure oxygen is supplied as an oxidant into the furnace, the oxidant and the hydrocarbon fuel are burned and reacted in the furnace region, and the combustion exhaust gas is exhausted out of the system
Pure oxygen is injected into the in-furnace region by pure oxygen injection means disposed on the inner wall surface of the furnace, and in-furnace gas is induced by pure oxygen jet to dilute and heat pure oxygen with in-furnace gas;
The hydrocarbon fuel is injected into the furnace area by the fuel injection means disposed on the inner wall of the furnace, and the pure oxygen diluted in the furnace gas is mixed with the hydrocarbon fuel to cause combustion reaction of the oxygen and the fuel.
The in-furnace gas is led out of the furnace, and the in-furnace gas is cooled by the heat storage material of the heat storage / regeneration type heat exchanger which makes heat transfer contact with the in-furnace gas led out of the furnace. Sensible heat is stored in the heat storage body,
A portion of the furnace gas after cooling is exhausted as combustion exhaust gas to the outside of the system, and the remaining portion of the furnace gas after cooling is brought into heat transfer contact with the heat storage body to reheat the remaining portion of the furnace gas. A high temperature oxy-fuel combustion method characterized by refluxing to the inner region.
Preferably, in-furnace gas having a flow rate of at least nine times the total flow rate of pure oxygen and fuel injected into the in-furnace region is led out of the furnace.

  According to the above configuration of the present invention, since the mixed fluid of in-furnace gas (carbon dioxide and water vapor) and pure oxygen undergoes a combustion reaction with the hydrocarbon fuel, the oxygen and the fuel undergo a combustion reaction slowly, and the flame temperature is localized A wide range of relatively low temperature diffusion combustion flames can be produced in the furnace while suppressing the temperature rise. Also, the mixture of pure oxygen and its combustion exhaust gas does not contain nitrogen, and therefore, the generation of NOx in the combustion zone can be substantially completely prevented. Furthermore, since this combustion reaction is an in-furnace combustion reaction of pure oxygen and hydrocarbon fuel, the volume of the flue gas to be discharged to the outside of the furnace is reduced, and the steam and carbon dioxide generated by the combustion reaction are either Are also radiant gases, and thus improve the heating performance or heat transfer performance of the combustion furnace. Therefore, according to the present invention, energy consumption can be further reduced compared to the high temperature air combustion method. Furthermore, in the high temperature oxy-fuel combustion method, the flow rates of the supply fluid and the exhaust fluid and the flow rate of the in-system circulating fluid are reduced compared to high temperature air combustion, so the combustion furnace and the combustion facility are smaller than Can be

  In addition, according to the above configuration of the present invention, pure oxygen is diluted and heated with the furnace gas in the furnace area, so that the oxidation / corrosion of the metal or ceramic material constituting the heat exchanger, the combustion furnace Oxidation and corrosion of the furnace body can be reliably prevented. In addition, the flow balance and heat balance of the entire combustion system can be optimized by appropriately setting the gas circulation amount of the heat storage and regeneration type heat exchanger and exhausting an appropriate amount of combustion exhaust gas out of the system.

  In addition, although it is desirable that "pure oxygen" is oxygen with a concentration of 100% that does not contain any impurities ideally, normal "pure oxygen" produced by techniques such as PSA (Pressure Swing Adsorption) is In reality, it contains minor or trace amounts of impurities and is usually at a concentration of 95% or less. In addition, in the pure oxygen supply path, it is also practically assumed that a small amount or a small amount of ambient air and the like inevitably enter the pure oxygen supply flow path. However, even if such a small amount or a small amount of impurities and the like are mixed into pure oxygen, the intention of the present invention is not greatly impaired. Therefore, in the present specification, the term "pure oxygen" is intended to mean a fluid (gas) having an oxygen concentration of 90% or more (weight ratio).

  INDUSTRIAL APPLICABILITY The high temperature oxygen combustion apparatus and the high temperature oxygen combustion method according to the present invention is an industrial that supplies pure oxygen to a regenerative thermal burner system and heats it to a very high temperature range of 800 ° C. or more to cause combustion reaction of high temperature oxygen with hydrocarbon fuel. A high temperature oxy-fuel combustion apparatus and a high temperature oxy-fuel combustion method of a furnace The high temperature oxygen combustion apparatus and the high temperature oxygen combustion method of the present invention can be suitably used for a general industrial furnace, and moreover, substantially completely prevent NOx from being generated in the combustion zone, and high temperature air Energy consumption can be further reduced as compared with the combustion method, and the combustion furnace and the combustion equipment can be further miniaturized.

FIG. 1 is a block diagram of a high temperature air combustion system schematically showing the configuration of a conventional high temperature air combustion method. FIG. 2 is a block diagram schematically showing the configuration of a high temperature oxy-fuel combustion system to which the configuration of a conventional high temperature air combustion method is applied. FIG. 3 is a block diagram schematically showing a high temperature oxy-fuel combustion system configured to exhaust a part of in-furnace combustion gas out of the furnace directly outside the furnace in the combustion system shown in FIG. FIG. 4 is a block diagram schematically showing the configuration of a high temperature oxy-fuel combustion system according to a preferred embodiment of the present invention. FIG. 5 is a block diagram schematically showing the configuration of a high temperature oxy-fuel combustion system according to another preferred embodiment of the present invention. FIG. 6 is a block diagram schematically showing the configuration of a high temperature oxy-fuel combustion system according to still another preferred embodiment of the present invention. FIG. 7 is a system configuration diagram showing the configuration of the high temperature oxygen combustion system shown in FIG. 5 more specifically. FIG. 8 is a system configuration diagram showing a modified example of the high temperature oxygen combustion system shown in FIG. FIG. 9 is a system configuration diagram showing the configuration of the high temperature oxygen combustion system shown in FIG. 6 more specifically. FIG. 10 is a longitudinal sectional view schematically showing an entire configuration of the heat storage and regeneration type heat exchanger of the high-temperature oxygen combustion system shown in FIGS. 4, 5, 7 and 8. FIG. 11 is a longitudinal sectional view specifically showing the structure of the heat exchanger shown in FIG. FIG. 12 is a cross-sectional view showing the structure of the dividing / mixing means of the communication passage shown in FIG. FIG. 13 is a longitudinal sectional view showing the heat exchanger shown in FIG. 11 after switching the position of the feed / discharge switching valve device. FIG. 14 is a longitudinal cross-sectional view showing the state of the communication passage in the heat exchanger shown in FIG. FIG. 15 is a cross-sectional view showing a modification of the diverting and mixing means. FIG. 16 is a cross-sectional view illustrating the configuration of mixing means for mixing the exhaust gas circulation flow with pure oxygen. FIG. 17 is a cross-sectional view showing a modification of the mixing means shown in FIG. FIG. 18 is a cross-sectional view showing another modification of the mixing mechanism shown in FIG. FIG. 19 is a longitudinal sectional view schematically showing an entire configuration of the heat storage and regeneration type heat exchanger shown in FIGS. 6 and 9. FIG. 20 is a longitudinal cross-sectional view specifically showing the structure of the heat storage and regeneration type heat exchanger shown in FIG. FIG. 21 is a longitudinal sectional view showing the heat exchanger shown in FIG. 20 after switching the position of the feed / discharge switching valve device.

  Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

  FIG. 1 is a block diagram of a high temperature air combustion system schematically showing the configuration of a conventional high temperature air combustion method. FIG. 1 (A) shows a first combustion mode of the high temperature air combustion system, and FIG. 1 (B) shows a second combustion mode of the high temperature air combustion system.

  In the high temperature air combustion method, the combustion furnace C includes first and second heat storage type heat exchangers H1 and H2 that constitute a heat storage and regeneration type burner system. In the first combustion mode (FIG. 1A), the combustion air A at atmospheric pressure and atmospheric temperature (normal pressure and normal temperature) is supplied to the second heat exchanger H2, and the combustion gas R in the furnace is subjected to the first heat It is led out of the furnace through the exchanger H1 and exhausted out of the system as the flue gas E. In the second combustion mode (FIG. 1B), the combustion air A at normal pressure and normal temperature is supplied to the first heat exchanger H1, and the combustion gas R in the furnace is transferred to the furnace via the second heat exchanger H2. It is led out and exhausted out of the system as combustion exhaust gas E. The first and second combustion modes are alternately switched at a predetermined time interval (for example, 30 seconds interval) set within 60 seconds, and heated to an ultra-high temperature range of 800 ° C. or higher by the heat exchangers H1 and H2. Combustion air is supplied substantially continuously to the in-furnace region α. The hydrocarbon-based fuel F is supplied to the in-furnace region α, mixed with the combustion air A, and in-furnace combustion reaction occurs.

For example, as shown by the chemical formula in FIG. 1, when methane (CH ₄ ) is used as the fuel F, the stoichiometry of the combustion reaction is 10 moles of air (2 moles of oxygen) to 1 mole of fuel, the theory The fuel / air ratio is 1/10. Therefore, in each of the first and second combustion modes, the flow rate ratio of the gas flowing through each heat exchanger H1, H2 is as follows: charge air flow rate: exhaust flow rate = 10: 11, which corresponds to the combustion with a substantially even flow rate. It means that the air and combustion exhaust gas always flow through the heat exchangers H1 and H2. Although a flow rate difference of approximately 10% occurs in air supply and exhaust, the overall flow rate is relatively large, so that in the case of this flow rate difference, the flow rate balance and heat balance of the entire combustion system are not substantially affected. It has already been confirmed. In the case of a flow rate difference of about 10%, if necessary, a small amount of in-furnace combustion gas R is exhausted from the in-furnace combustion zone directly out of the system, so that the entire combustion system It becomes possible to secure the flow rate balance and the heat balance.

  FIG. 2 is a block diagram schematically showing the configuration of a high temperature oxygen combustion system in which the configuration of such a high temperature air combustion method is applied to the high temperature oxygen combustion method.

  The combustion system shown in FIG. 2 is a combustion system configured to supply pure oxygen O to the combustion system instead of the combustion air A. Pure oxygen O is supplied to the in-furnace region α after being heated to an ultra-high temperature range of 800 ° C. or more by the heat exchangers H1 and H2. The hydrocarbon-based fuel F is supplied into the furnace and mixed with the heated pure oxygen O to cause an in-furnace combustion reaction.

For example, as shown by the chemical formula in FIG. 1, when methane (CH ₄ ) is used as the fuel F, the stoichiometric ratio of the combustion reaction is 2 moles of oxygen to 1 mole of fuel, and therefore the stoichiometric ratio is , 1/2. For this reason, in both the first combustion mode (FIG. 2A) and the second combustion mode (FIG. 2B), the flow ratio of the gas flowing through each heat exchanger H1, H2 is: Since the air flow rate is 3: 2, the flow rate difference between the air supply and the exhaust is large, and it is difficult to secure the flow rate balance and heat balance of the entire combustion system as desired. For example, in the combustion system of the high temperature air combustion method (FIG. 1), the combustion exhaust gas E can be cooled to a temperature of 200 to 300 ° C., but in the combustion system of the high temperature oxygen combustion method shown in FIG. The combustion exhaust gas temperature can not be lowered to the area, and as a result, an excessive heat load is imposed on the flow path and equipment of the exhaust system, or overheating of the heat storage material constituting the heat exchangers H1 and H2 It is easy to occur.

  FIG. 3 is a block diagram schematically showing a high temperature oxy-fuel combustion system configured to exhaust part of in-furnace combustion gas directly out of the system in the combustion system shown in FIG.

In the high-temperature oxygen combustion system shown in FIG. 3, the furnace is designed to equalize the flow ratio of pure oxygen O and flue gas E flowing through the heat exchangers H1 and H2, and set the exhaust flow rate: the charge air flow rate 1: 1. This is a combustion system configured to exhaust part of the internal combustion gas R directly out of the system from the in-furnace region α. For example, when methane (CH ₄ ) is used as the fuel, the flue gas Ea having a flow rate equivalent to 1/3 of the charge air flow rate (total amount of oxygen supply amount and fuel supply amount) is directly discharged from the furnace combustion zone to the outside of the system. Exhausted. According to such a configuration, in each of the first and second combustion modes, the flow rates of the pure oxygen O and the combustion exhaust gas E flowing through the heat exchangers H1 and H2 are maintained at equal amounts (supply flow rate = exhaust flow rate) It is possible to maintain flow rate balance and heat balance throughout the combustion system. In addition, since the amount of combustion gas generated by the combustion reaction of oxygen and hydrocarbon fuel is relatively small relative to the calorific value in the furnace, even if the combustion exhaust gas Ea is discharged directly out of the system as described above, combustion is still possible. The heat loss of the whole system does not increase significantly, so that a significant reduction in the thermal efficiency can be avoided.

  According to the high temperature oxy-fuel combustion system shown in FIGS. 2 and 3, the components of the combustion gas generated in the in-furnace region α are substantially only water vapor and carbon dioxide, and therefore the generation of NOx is substantially completely eliminated. Since the flow rate of the combustion gas circulating through the entire combustion system and the amount of combustion exhaust gas exhausted outside the system can be reduced, the furnace and the combustion equipment can be miniaturized. Moreover, since the sensible heat held by the combustion exhaust gas is efficiently recovered by the heat storage and regeneration type heat exchangers H1 and H2, it is possible to reduce the fuel consumption (energy consumption).

  However, oxygen heated to an ultra-high temperature range of 800 ° C. or higher is extremely reactive, and therefore, the heat exchangers H1, H2 and the oxidation / corrosion of the metal or ceramic material constituting the high temperature gas flow path, and the combustion Since there is concern about oxidation, corrosion, etc. of the furnace body of the furnace, the high temperature oxy-fuel combustion method with such configuration is premised on the development of the fireproof / insulation material that constitutes the furnace body, or the material or material that constitutes the combustion equipment. There is no choice but to adopt it as a condition, and it is difficult to adopt it as a general industrial furnace combustion method at present. In addition, in such an oxygen combustion method, there is a concern that the flame in the combustion zone may be locally heated to high temperature, and the fireproof and heat insulating material constituting the furnace body and the flow path of a general industrial furnace may be worn or damaged. Ru.

  FIG.4 and FIG.5 is a block diagram which shows roughly the structure of the high temperature oxygen combustion system which concerns on this invention.

  FIGS. 4 and 5 schematically illustrate the high temperature oxy-fuel combustion system of the present invention configured to recirculate a portion of the furnace gas and add to pure oxygen in order to dilute the pure oxygen with the flue gas. It is shown. In the combustion system shown in FIGS. 4 and 5, a part of the flue gas E immediately after being discharged outside the furnace is added to the feed stream of pure oxygen O as the bypass stream B, and the bypass stream B and the oxygen O are mixed. Air M is supplied to the furnace area α.

  In the high temperature oxygen combustion system shown in FIG. 4, the high temperature side (furnace inside) flow paths of the heat exchangers H1 and H2 are in communication with each other. In the first combustion mode (FIG. 4 (A)), pure oxygen O is supplied to the second heat exchanger H2, and a part of the combustion exhaust gas E drawn out of the furnace serves as the bypass flow B and is heated after pure oxygen O. Is added to The remainder of the combustion exhaust gas E is exhausted out of the system after being cooled by the first heat exchanger H1. The mixture M of the bypass flow B and the oxygen O mixes and contacts the hydrocarbon-based fuel F in the in-furnace region α to cause a combustion reaction. In the second combustion mode (FIG. 4 (B)), pure oxygen O is supplied to the first heat exchanger H1, and a part of the combustion exhaust gas E drawn out of the furnace is treated as the bypass flow B pure oxygen after heating. Added to O. The remainder of the combustion exhaust gas E is exhausted out of the system after being cooled by the second heat exchanger H2. The mixture M of the bypass flow B and the pure oxygen O mixes and contacts the hydrocarbon-based fuel F in the in-furnace region α to cause a combustion reaction. If desired, a relatively small amount of flue gas Ea is exhausted directly from the furnace region α to the outside of the system in order to ensure the flow rate balance and heat balance of the entire combustion system.

  In the high temperature oxygen combustion system shown in FIG. 5, the low temperature side (furnace outside) flow paths of the heat exchangers H1 and H2 communicate with each other. In the first combustion mode (FIG. 5A), part of the combustion exhaust gas E supplied with pure oxygen O to the second heat exchanger H2 and cooled by the first heat exchanger H1 is divided as the bypass flow B. It is added to pure oxygen O before flowing and heating. The remainder of the combustion exhaust gas E is exhausted out of the system. After the mixture M of the bypass flow B and pure oxygen O is heated by the second heat exchanger H2, the mixture M is supplied to the in-furnace region α, mixed with the hydrocarbon fuel F in the in-furnace region α, and combusted. Do. In the second combustion mode (FIG. 5B), part of the combustion exhaust gas E supplied with pure oxygen O to the first heat exchanger H1 and cooled by the second heat exchanger H2 is used as the bypass flow B. It is divided and added to pure oxygen O before heating. The remainder of the combustion exhaust gas E is exhausted out of the system. After the mixture M of the bypass flow B and pure oxygen O is heated by the first heat exchanger H1, the mixture M is supplied to the in-furnace region, mixes and contacts the hydrocarbon-based fuel F in the in-furnace region α, and burns and reacts . If desired, a relatively small amount of flue gas Ea is exhausted directly from the furnace region α to the outside of the system in order to ensure the flow rate balance and heat balance of the entire combustion system.

In the high-temperature oxygen combustion system shown in FIGS. 4 and 5, for example, when methane (CH ₄ ) is used as the fuel F, the combustion gas generated by the combustion reaction of the hydrocarbon fuel and oxygen is substantially carbon dioxide. And a mixture of steam, and therefore, the mixture M is supplied to the in-furnace region α as an air-supply stream formed by diluting pure oxygen O with carbon dioxide and steam. For example, the flow rate of the bypass flow B is set equal to the oxygen supply amount, and the oxygen concentration of the mixture M is set to 50% by volume. If desired, it is also possible to reduce the oxygen concentration of the air-fuel mixture M to about 20% by volume. Since a mixture of pure oxygen O diluted with in-furnace combustion gas R burns slowly with fuel F, a broad-area, relatively low temperature diffusion combustion flame which suppresses the local increase in flame temperature is used. Can be generated within.

  In the combustion system shown in FIG. 4, a part of the combustion exhaust gas E immediately after being derived from the in-furnace region α circulates as the bypass flow B in the high temperature side (furnace inside) flow path of the heat exchangers H1 and H2, It mixes with pure oxygen O heated by exchanger H1, H2. On the other hand, in the combustion system shown in FIG. 5, the combustion exhaust gas E derived from the in-furnace region α is partially added to pure oxygen O as bypass flow B after being cooled by heat exchangers H1 and H2. Pure oxygen O diluted with carbon dioxide and steam is brought into heat transfer contact with the heat exchangers H1 and H2 and heated.

  In the combustion system shown in FIG. 4, except for a part of the heat exchangers H1 and H2, they do not directly contact the highly reactive high temperature pure oxygen, thus suppressing the oxidation and corrosion of the flow path and the furnace body. In the combustion system shown in FIG. 5, all the flow paths including the heat exchangers H1 and H2 and the inner wall surface of the furnace do not directly contact the high temperature pure oxygen of 800.degree. C. or more. Corrosion can be reliably prevented.

  As shown in FIG. 4C, in the heat exchangers H1 and H2, the heat storage bodies of the respective heat exchangers are divided in the air flow direction (back and forth), and the bypass flow B is converted into pure oxygen O in the middle portion of each heat storage body. You may comprise so that it may add. According to such a configuration, as in the combustion system shown in FIG. 5, it is possible to prevent all the flow paths including the heat exchangers H1 and H2 and the inner wall surface of the furnace from being in direct contact with high temperature pure oxygen Become. Moreover, according to such a configuration, since pure oxygen O is preheated by the low temperature side heat storage body portion, the water vapor in bypass flow B is surely prevented from mixing with pure oxygen O at normal temperature and condensing. be able to.

  FIG. 6 is a block diagram schematically showing the configuration of a high temperature oxy-fuel combustion system according to another embodiment of the present invention.

  The embodiment shown in FIG. 4 and FIG. 5 is a system in which pure oxygen O or the mixture M thereof is heated by the heat storage and regeneration type heat exchangers H1 and H2, but as in the embodiment shown in FIG. It is also possible to heat and dilute pure oxygen O in the in-furnace region α by the in-furnace combustion gas R of In FIG. 6, injection nozzles of pure oxygen O and fuel F are disposed on the inner wall surface of the furnace, pure oxygen O and fuel F are directly injected into the in-furnace region α, and pure oxygen O is generated by in-furnace combustion gas R. A combustion system of the heating and dilution type is shown.

  The furnace area α is generally a high temperature atmosphere of 1200 ° C. or higher. Pure oxygen O is injected from the injection port of the oxygen injection nozzle into the furnace region α. The jet of pure oxygen O injected from the oxygen injection nozzle into the in-furnace region α mixes with in-furnace combustion gas R and is heated by the in-furnace combustion gas R while attracting ambient in-furnace gas. Such mixing / heating action rapidly progresses in a region within a distance range equivalent to about 10 times the nozzle diameter (diameter) from the jet part of the oxygen jet nozzle.

  6A and 6B, the pure oxygen O injected into the in-furnace region α is mixed with the in-furnace combustion gas R and heated to the same temperature as the in-furnace combustion gas R. After that, the fuel F mixed with the fuel F injected into the in-furnace region α makes a combustion reaction in the in-furnace region α. A mixture obtained by diluting pure oxygen O with in-furnace combustion gas R burns slowly with fuel F, thereby suppressing local temperature increase of the flame temperature, and spreading a wide range and relatively low temperature. A combustion flame can be generated in the furnace.

  The combustion system shown in FIG. 6 also includes an in-furnace gas exhaust and circulation device that exhausts a part of the in-furnace combustion gas R to the outside of the furnace and refluxes the remainder of the in-furnace combustion gas R into the furnace. The in-furnace gas exhaust / circulation device is composed of a pair of heat exchangers H1 and H2. For example, the in-furnace gas exhaust / recirculation apparatus leads out the in-furnace combustion gas R at a flow rate corresponding to about 10 times the total flow rate of pure oxygen O and fuel F to the outside of the furnace and reflux it in the furnace.

  As shown in FIG. 6, the in-furnace gas exhausting and circulating apparatus includes first and second heat storage type heat exchangers H1 and H2. In the first circulation mode (FIG. 6A), the in-furnace gas exhaust / recirculation apparatus brings out the in-furnace combustion gas R from the first heat exchanger H1 to the outside of the furnace and retains the in-furnace combustion gas R. Heat is stored in the first heat exchanger H1, most of the furnace combustion gas R after cooling is introduced into the second heat exchanger H2, reheated by the second heat exchanger H2 and returned to the furnace area α Let In the second circulation mode (FIG. 6B), the in-furnace gas exhaust / recirculation apparatus brings out the in-furnace combustion gas R from the second heat exchanger H2 to the outside of the furnace, and holds the in-furnace combustion gas R retained. Heat is stored in the second heat exchanger H2 and most of the furnace combustion gas R after cooling is introduced into the first heat exchanger H1 and reheated by the first heat exchanger H1 to be returned to the furnace area α Let In each of the exhaust and circulation modes, part of the furnace combustion gas R after cooling is exhausted out of the system as the combustion exhaust gas Ex.

  The first and second circulation modes are alternately switched at predetermined time intervals (for example, 30 seconds) set within 60 seconds. The flow rate of the combustion exhaust gas Ex is set to a flow rate equal to the total flow rate of the pure oxygen O and the fuel F supplied to the in-furnace region α. For example, the flow rate of the combustion exhaust gas Ex is set to about 10% of the in-furnace gas discharge amount, and about 90% of the in-furnace combustion gas R drawn out of the furnace is returned to the in-furnace region α. That is, most of the in-furnace combustion gas R drawn out of the furnace is refluxed to the in-furnace region α at a temperature substantially equal to the temperature at the time of drawing out of the furnace. Since the flue gas Ex is exhausted out of the system after being cooled by the heat exchangers H1 and H2, the flue gas Ex only has a temperature of about 200 to 300 ° C. According to such a combustion system, the flow rate of the in-furnace combustion gas R flowing through the heat exchangers H1 and H2 outside the furnace, and the in-furnace combustion gas flowing through the heat exchangers H1 and H2 in the furnace direction The ratio of R to the flow rate is approximately 10: 9, which is substantially equal, so that the flow rate balance and heat balance of the entire combustion system can be substantially ensured.

  FIG. 7 is a system configuration diagram showing the configuration of the high temperature oxygen combustion system shown in FIG. 5 more specifically.

  The high temperature oxygen combustion system 1 includes a pair of regenerative heat storage type heat exchangers 2 (2A: 2B), a supply / discharge switching valve device 3 (3A: 3B: 3C: 3D) and an exhaust fan 4. The heat exchanger 2 is disposed in a furnace body 9 of heat-resistant and refractory material that divides the furnace area α. The heat exchanger 2 has a structure in which the heat storage body 21 is accommodated in the heat storage case 22.

  Each heat storage body 21 is made of a ceramic heat storage body having a honeycomb structure having a cylindrical outer shape, and has a large number of narrow flow paths. The many narrow flow paths of the heat storage body 21 penetrate the heat storage body 21 in the axial direction of the heat exchanger 2. The heat storage body 21 has a temperature efficiency of 0.9 or more. The structure, function, and the like of such a heat storage body 21 are disclosed in detail in, for example, Japanese Patent Application No. 5-6911 (Japanese Patent Application Laid-Open No. 6-213585 (Patent Document 1)) by the applicant of the present application. Further detailed description is omitted.

  The supply / discharge switching valve device 3 is configured of a switching valve 3A: 3B: 3C: 3D that can be opened and closed under the control of a control unit (not shown). Exhaust pipes 44, 45 interposing the switching valves 3A, 3B are connected to the furnace outer side (low temperature side) flow passage of the heat storage body 21. The exhaust pipes 44, 45 are alternately connected to the suction port of the exhaust fan 4. An exhaust pipe 47 for exhausting the furnace gas to the outside of the system is connected to the discharge port of the exhaust fan 4. An oxygen injection nozzle 6 is disposed in each heat exchanger 2 concentrically with the heat storage body 21. The nozzle 6 injects pure oxygen O toward the furnace outer side (low temperature side) end face of the heat storage body 21. The oxygen supply pipes 42 and 43 are connected to the nozzle 6 respectively. The oxygen supply pipes 42, 43 are provided with switching valves 3C, 3D, respectively. The oxygen supply pipes 42, 43 are alternately connected to a pure oxygen O supply source (not shown). The low temperature side (furnace outside) flow paths of the heat storage body 21 communicate with each other by the communication path 7. In the communication passage 7, a differential pressure control means, a differential pressure control mechanism, differential pressure forming means 70 such as an orifice (shown conceptually in FIG. 7) are interposed.

  7A shows a first combustion mode in which pure oxygen O is supplied to the nozzle 6 of the heat exchanger 2B, and FIG. 7B shows pure oxygen O in the nozzle 6 of the heat exchanger 2A. A first mode of combustion is shown. The hydrocarbon-based fuel F is continuously injected from the fuel injection port of the fuel injection nozzle 5 into the in-furnace region α.

  In the first combustion mode shown in FIG. 7A, the combustion exhaust gas E is drawn out of the furnace through the heat exchanger 2A and cooled by the heat storage body 21 of the heat exchanger 2A. The sensible heat possessed by the combustion exhaust gas E is stored in the heat storage body 21 of the heat exchanger 2A. Part of the flue gas E after cooling is attracted by the jet of pure oxygen O injected from the nozzle 6 of the heat exchanger 2B, and flows through the communication passage 7 as shown in FIG. It flows into the low temperature side (furnace outside) flow passage of the heat exchanger 2B and mixes with pure oxygen O. The remaining portion of the combustion exhaust gas E is sucked by the exhaust fan 4 through the exhaust pipe 44 and exhausted out of the system through the exhaust pipe 47 as shown in FIG. 7A.

  On the other hand, in the second combustion mode shown in FIG. 7B, the combustion exhaust gas E is drawn out of the furnace by the heat exchanger 2B and cooled by the heat storage body 21 of the heat exchanger 2B. The sensible heat possessed by the combustion exhaust gas E is stored in the heat storage body 21 of the heat exchanger 2B. A part of the flue gas E after cooling is attracted to the jet of pure oxygen O injected from the nozzle 6 of the heat exchanger 2A, and is connected to the low temperature side (furnace outside) flow path of the heat exchanger 2A via the communication path 7 It flows in and mixes with pure oxygen O. The remaining portion of the combustion exhaust gas E is sucked by the exhaust fan 4 through the exhaust pipe 45 as shown in FIG. 7B, and is exhausted out of the system from the exhaust pipe 47 as the combustion exhaust gas Ex.

  The switching valves 3A: 3B: 3C: 3D constituting the supply / discharge switching valve device 3 are controlled to open and close at predetermined time intervals within 60 seconds under the control of a control unit (not shown), and the high temperature oxygen combustion system 1 is The first and second combustion modes are alternately switched. Further, an exhaust system for directly exhausting the combustion exhaust gas Ea to the outside of the furnace is provided, and a part of the combustion gas R in the furnace is constantly exhausted outside the furnace.

  According to such a configuration, the flow rate of the charge air flow circulating in each furnace in the furnace direction of the heat exchangers 2A and 2B, and the flow rate of the exhaust flow circulating in the furnace outside the heat exchangers 2A and 2B at all times, etc. The flow rate balance and heat balance of the entire combustion system can be secured by setting the amount, and moreover, the sensible heat possessed by the combustion exhaust gas E can be efficiently recovered. In addition, since pure oxygen O is heated after being diluted by the combustion exhaust gas E, oxidation and corrosion of constituent materials such as the heat storage body 21 and the furnace body 9 can be reliably prevented.

  FIG. 8 is a system configuration diagram showing a modified example of the high temperature oxygen combustion system shown in FIG. Note that FIG. 8 shows only the first combustion mode of the combustion system. The combustion system shown in FIG. 7 includes an ejector 4 ′ in place of the exhaust fan 4. The ejector 4 ′ includes an injection nozzle 4 ′ ′ for injecting a driving fluid J such as high pressure air and high pressure steam, and attracts the combustion exhaust gas Ex with a jet of the driving fluid J and exhausts it out of the system.

  FIG. 9 is a system configuration diagram showing the configuration of the high temperature oxygen combustion system shown in FIG. 6 more specifically.

  Similar to the combustion system shown in FIGS. 7 and 8, the high temperature oxygen combustion system 1 exhausts the combustion exhaust gas Ex to the outside of the system, as well as a pair of regenerative heat storage type heat exchangers 2 (2A: 2B) disposed in the furnace body 9. And an exhaust fan 4 for However, the oxygen injection nozzle 6 is disposed in the furnace body 9 so as to directly inject pure oxygen O into the in-furnace region α, and the communication passage 7 extending between the low temperature side (furnace outside) flow paths of each heat storage body 21. In addition, a four-way valve type feed switching valve device 3 'is disposed to switch the feed / discharge direction of the heat exchanger 2 (2A, 2B) at predetermined time intervals within 60 seconds. The heat exchanger 2 is alternately switched to the first circulation mode shown in FIG. 9 (A) and the second circulation mode shown in FIG. 9 (B) by the operation of the supply / discharge switching valve device 3 '.

  In the first circulation mode (FIG. 9A), the in-furnace combustion gas R is drawn out of the heat exchanger 2B as the out-furnace derived gas E 'under the suction pressure of the exhaust fan 4 from the heat exchanger 2B. The sensible heat possessed by the in-furnace gas E 'is stored in the heat storage body 21 of the heat exchanger 2B. The in-furnace gas E ′ after cooling is introduced into the heat exchanger 2A, reheated to the same temperature as the time of discharge by the heat storage body 21 of the heat exchanger 2A, and then returned to the in-furnace region α. In the second circulation mode (FIG. 9 (B)), the in-furnace combustion gas R is drawn out of the heat exchanger 2A as the out-furnace derived gas E ′. The sensible heat held by the out-furnace derived gas E ′ is stored in the heat storage body 21 of the heat exchanger 2A. The cooled out gas E 'is introduced into the heat exchanger 2B, reheated to the same temperature as the time of discharge by the heat storage body 21 of the second heat exchanger H2, and then returned to the furnace area α. . In each circulation mode, the exhaust fan 4 exhausts a part of the out-furnace derived gas E 'after cooling out as a combustion exhaust gas Ex.

  As described above, the flow rate of the combustion exhaust gas Ex is set equal to the total flow rate of the pure oxygen O and the fuel F supplied to the in-furnace region α, and the flow rate of the outgassing gas E ′ is, for example, the combustion exhaust gas Ex And 90% of the out-furnace derived gas E ′ derived from the in-furnace region α is returned to the in-furnace region α.

  Next, a heat storage and regeneration type heat exchanger of a high temperature oxygen combustion system according to a preferred embodiment of the present invention will be described.

  The high temperature oxygen combustion system 1 shown in FIG. 4, FIG. 5, FIG. 7 and FIG. 8 adds a portion of the combustion exhaust gas E exhausted by the heat storage regenerative heat exchanger 2 to pure oxygen O as a bypass flow B The remaining portion of the exhaust gas E is exhausted out of the system by the exhaust fan 4. FIG. 10 is a longitudinal sectional view showing the configuration of the heat storage and regeneration type heat exchanger 2 having such a function. FIG. 10A shows a first combustion mode for supplying pure oxygen O to the heat exchanger 2B, and FIG. 10B shows a second combustion mode for supplying pure oxygen O to the heat exchanger 2A. It is shown. The basic configuration of the heat exchanger 2 shown in FIG. 10 corresponds to the configurations shown in FIG. 5, FIG. 7 and FIG. 8. The heat exchanger 2 cools the combustion exhaust gas E by the heat exchanger 2 A part (the exhaust gas circulation flow Er) is added to the pure oxygen O as the bypass flow B. 11 is a longitudinal sectional view specifically showing the structure of the heat exchanger 2A, and FIG. 12 is a transverse sectional view showing the structure of the communication passage 7. As shown in FIG. Furthermore, FIG.13 and FIG.14 is the longitudinal cross-sectional view and cross-sectional view of the heat exchanger 2A which show the state which switched the combustion mode, and the communication path 7. As shown in FIG.

  Each of the heat exchangers 2A and 2B has a heat storage case 22 containing a heat storage 21 and a support substrate 23 made of a heat-resistant / refractory material of the same quality as the furnace body 9, and the heat storage case 22 is a support substrate 23 Penetrate. The supporting substrate 23 is integrated with the furnace body 9 and faces the in-furnace region α, and the furnace inner wall surface 92 of the furnace body 9 is formed together with the furnace body 9. The heat storage body 22 is made of a metal cylindrical member penetrating the support substrate 23 and is integrally supported by the support substrate 23. The tip end portion of the heat storage body case 22 further extends from the tip end surface of the heat storage body 21 to the inside of the furnace, and is slightly reduced in diameter to open in the furnace inside region α. The tip circular opening of the heat storage case 22 constitutes an in-furnace gas supply / discharge port 20. The supply / discharge port 20 functions as a furnace gas suction port for suctioning the furnace combustion gas R in the furnace area 9 and supplies the mixture M of pure oxygen O and exhaust gas circulating flow Er to the furnace area α. Acts as a mixture injection port.

  The feed / discharge switching valve device 3 of each heat exchanger 2 is disposed outside the furnace coaxially with the heat storage case 22. Between the valve device 3 and the heat storage body 21, a flow dividing / mixing device 8 constituting the communication passage 7 is interposed. The structure of the heat exchanger 2A is specifically shown in FIG. The structure of the heat exchanger 2B is substantially the same as the structure of the heat exchanger 2A.

  As shown in FIG. 11, the diverting and mixing device 8 includes a furnace inner flange 81 airtightly connected to the heat storage case 22, a furnace outer flange 82 airtightly connected to the supply and discharge pipe 61 of the valve device 3, and a flange It comprises an outer tube 83 of a true circular cross section extending between the portions 81 and 82, and an inner tube 84 of a true circular cross section disposed concentrically inside the outer tube 83. As shown in FIG. 12, the inner pipe 84 is provided with a large number of supply and discharge holes 85 radially penetrating the pipe wall of the inner pipe 84. A communication pipe 71 constituting the communication passage 7 is integrally connected to the outer pipe 83, and an end circular opening 72 of the communication pipe 71 is opened to a hollow area 86 between the outer pipe 83 and the inner pipe 84. The supply and discharge holes 85 are circumferentially aligned around the central axis of the inner pipe 84 at an angular interval of about 30 °. As shown in FIG. 11, the supply and discharge holes 85 are arranged in two rows at a predetermined interval L, and are arranged at positions generally offset to the inside of the furnace, and the end circular opening 72 of the communicating pipe 71 is It is positioned at the longitudinal center of the outer tube 83. Such a double pipe structure of the flow dividing / mixing device 8 constitutes the above-described differential pressure forming means 70 (FIG. 7).

  The valve device 3 includes a valve mechanism 30, a pure oxygen inlet 31, a furnace gas outlet 32, and a valve driving device 33. The valve device 3 has a structure in which the supply and discharge pipe 61, the valve housing 51 and the valve drive device 33 are connected in series. The valve drive 33 comprises an actuator 50 integrally attached to the valve housing 51 by a support member 58. The supply and discharge pipe 61 is concentrically connected to the furnace outer flange portion 82 of the flow dividing and mixing device 8. An elbow pipe 36 having a valve seat 35 is disposed in the water supply and discharge channel 60 of the water supply and discharge pipe 61. The elbow pipe 36 penetrates the pipe wall of the water supply and discharge pipe 61 and protrudes out of the pipe. An exhaust pipe 44 (shown by a broken line) is connected to a connecting flange portion formed at the projecting end of the elbow pipe 36.

  The valve housing 51 is airtightly connected to the furnace outer end of the supply and discharge pipe 61, and a pure oxygen O supply region 56 is formed in the housing 51. The valve housing 51 includes a valve seat 55, and the piston rod 53 of the actuator 50 penetrates the opening of the valve seat 55. The piston rod 53 is slidably inserted into the rod insertion portion 52. The supply / discharge pipe 61, the valve seat 35, the valve body 54, the valve seat 55, the actuator 50, the rod insertion portion 52, and the piston rod 53 are concentrically arranged around the central axis CL of the supply / discharge switching valve device 3. Ru.

  The valve seat portion 35, the valve body 54 and the valve seat portion 55 constitute the switching valves 3A and 3C shown in FIG. The driver 33 is connected to the control unit C / U (FIG. 10) via a control signal line 59. The valve seat portion 35, the valve body 54 and the valve seat portion 55 function as a two-position control valve which selectively opens and closes the openings of the valve seat portions 34 and 35 under the control of the control unit C / U.

  In the valve position of the heat exchanger 2A shown in FIG. 11, the valve body 54 fixed to the tip of the piston rod 53 opens the opening of the valve seat 35 and closes the opening of the valve seat 55, The combustion exhaust gas E of the supply and discharge passage 60 in the supply and discharge pipe 61 flows into the in-pipe region 37 of the elbow pipe 36 and is exhausted to the exhaust pipe 44. This state corresponds to the first combustion mode shown in FIG.

  A state in which the drive device 33 of the heat exchanger 2A extends the piston rod 53, opens the opening of the valve seat 55, and closes the opening of the valve seat 35 by the valve 54 is shown in FIG. In this state, pure oxygen O of the oxygen supply pipe 42 jets into the supply / discharge flow path 60 and is supplied to the in-furnace region α through the in-pipe flow path 80 of the flow dividing device 8 and the honeycomb flow path of the heat storage body 21. This state corresponds to the second combustion mode shown in FIG. 10 (B).

For example, in each combustion mode, the fluid temperature of each part is set as follows.
Furnace gas temperature at the time of delivery (supply / discharge port 20) Ti = 1200 ° C
In-furnace gas temperature (valve mechanism 30) after heat storage medium passage T1 = 200 ° C
Oxygen temperature at the time of valve installation (inlet 31) T2 = 20 ° C
Gas temperature of mixture M (supply / discharge port 20) To = 1100 ° C.

  As shown in FIG. 10, since the attraction pressure of the fluid flow of pure oxygen O flowing in the in-pipe channel 80 of the other dividing / mixing apparatus 8 acts on the in-pipe channel 80 of one dividing / mixing apparatus 8, As shown in FIG. 12 and FIG. 14, a part of the combustion exhaust gas E flows into the communication pipe 71 of the communication path 7 as the exhaust gas circulation flow Er, and flows into the pipe flow path 80 of the diversion and mixing device 8 on the opposite side. Mix with pure oxygen O. The flow rate of the exhaust gas circulation flow Er is mainly set by the flow path resistance of each of the flow dividing / mixing devices 8 of the double pipe structure.

  FIG. 15 is a cross-sectional view showing a modification of the flow dividing device 8. In the flow dividing device 8 shown in FIGS. 11 to 14, the supply and discharge holes 85 pass through the inner wall of the inner pipe 84 in the radial direction. However, as shown in FIG. You may orientate in the direction which makes a predetermined inclination angle.

  16 to 18 are cross-sectional views illustrating a mixing mechanism for mixing the exhaust gas circulating flow Er with pure oxygen O. The mixing mechanism shown in FIG. 16 to FIG. 18 is a mechanism that only mixes the exhaust gas circulating flow Er and pure oxygen O, and does not have a diversion function like the diversion and mixing device 8. For this reason, the exhaust gas circulation flow Er is diverted from the combustion exhaust gas E by the separately provided flow dividing means (not shown), and is fed to the communication pipe 71 as shown by the arrows in each drawing.

  The mixing mechanism shown in FIG. 16 has a circular plate 100 with an oval opening 101 in order to efficiently mix the exhaust gas circulating flow Er with pure oxygen O. The mixing mechanism shown in FIG. 17 has a circular plate 102 provided with a large number of small diameter and circular openings 103 in order to efficiently mix the exhaust gas circulating flow Er with pure oxygen O. The mixing mechanism shown in FIG. 18 includes a circular plate 104 having a large number of small diameter and circular openings 105 and an extension pipe of the supply and discharge pipe 61 in order to efficiently mix the exhaust gas circulation flow Er with pure oxygen O. And a circular plate 106 disposed at 108. The circular plate 106 is provided with a number of small diameter and round openings 107.

  FIG. 19 is a longitudinal sectional view showing the configuration of the heat storage and regeneration type heat exchanger 2 shown in FIGS. 6 and 9, and FIGS. 20 and 21 show the structure of the heat storage and regeneration type heat exchanger 2 shown in FIG. It is a longitudinal cross-sectional view.

  The high temperature oxygen combustion system 1 shown in FIG. 6 and FIG. 9 exhausts a part of the outgassing gas E 'out of the furnace as the combustion exhaust gas Ex by the heat storage and regeneration type heat exchanger 2 and The remainder is configured to be reintroduced into the in-furnace region α. Pure oxygen O and hydrocarbon fuel F are discharged or injected directly into the in-furnace region α. FIG. 19 is a longitudinal sectional view showing the configuration of the heat storage and regeneration type heat exchanger 2 for circulation and exhaustion of such out-furnace derived gas E ′.

  The heat storage / regeneration type heat exchanger 2 sucks in-furnace combustion gas R as out-of-furnace out gas E 'from one of the supply / discharge ports 20, cools it by the heat storage body 21, and circulates out-furnace out gas E' after cooling It is pressurized by the fan 4, reheated by the other heat storage body 21, and injected from the other supply / discharge port 20 into the furnace area α. Each heat exchanger 2 has a structure in which the communication passage 7 and the flow dividing / mixing device 8 are removed from the heat exchanger 2 shown in FIG. 10, FIG. 11 and FIG.

  In the valve position of the valve device 3 shown in FIG. 20, the valve body 54 opens the opening of the valve seat 35 and closes the opening of the valve seat 55. In this state, the out-furnace derived gas E ′ of the supply and discharge passage 60 in the supply and discharge pipe 61 flows into the in-pipe region 37 of the elbow pipe 36 and is drawn out to the exhaust pipe 44. On the other hand, in the valve position shown in FIG. 21, the drive device 33 extends the piston rod 53 to open the opening of the valve seat 55 and close the opening of the valve seat 35 by the valve body 54. In this state, the out-furnace derived gas E ′ of the air supply pipe 42 jets into the supply and discharge flow passage 60 and is introduced into the in-furnace region α through the honeycomb flow passage of the heat storage body 21.

  In the first circulation mode shown in FIG. 19 (A), the combustion gas R in the furnace (FIG. 9) is led out of the heat exchanger 2A as the outlet gas E 'outside the furnace under the suction pressure of the exhaust fan 4, It is led to the exhaust pipe 44 via the switching valve 3A. The sensible heat of the out-furnace derived gas E 'is stored in the heat storage body 21 of the heat exchanger 2A. The out-furnace derived gas E 'after cooling is supplied to the air supply port 31 of the heat exchanger 2B through the air supply pipe 43, and is introduced into the honeycomb flow path of the heat storage body 21 through the switching valve 3D of the heat exchanger 2B. And after being reheated to the same temperature as at the time of discharge, it is returned to the furnace area α. In the second circulation mode shown in FIG. 19B, the in-furnace combustion gas R (FIG. 9) is led out of the heat exchanger 2B from the heat exchanger 2B as the out-furnace out gas E ′ under the suction pressure of the exhaust fan 4 , And is discharged to the exhaust pipe 45 via the switching valve 3B. The sensible heat of the out-furnace derived gas E 'is stored in the heat storage body 21 of the heat exchanger 2B. The out-furnace derived gas E 'after cooling is supplied to the air supply port 31 of the heat exchanger 2A through the air supply pipe 42, and introduced into the honeycomb flow path of the heat storage body 21 through the switching valve 3C of the heat exchanger 2A. And after being reheated to the same temperature as at the time of discharge, it is returned to the furnace area α. In each circulation mode, the exhaust fan 4 exhausts a part of the outside-furnace derived gas E ′ after cooling out of the system as the combustion exhaust gas Ex.

  The preferred embodiments and examples of the present invention have been described above in detail, but the present invention is not limited to the above embodiments and examples, and is within the scope of the present invention as set forth in the claims. It goes without saying that various modifications or alterations are possible, and such modifications or variations are also included in the scope of the present invention.

  For example, although the heat exchanger provided with the switching heat storage body having a honeycomb structure has been described in the above embodiment and examples, a switching heat exchanger provided with a large number of granular heat storage bodies, or a rotary heat storage body A heat exchanger provided may be used in the present invention. When a heat exchanger using a rotary heat storage body is used, each portion or each region of the rotary heat storage body that repeats heat reception and heat release corresponds to the first and second heat exchangers and the heat storage body thereof. It can be understood as a component to

  In the above embodiments and examples, the high temperature oxy-fuel combustion method of the present invention has been described as a combustion apparatus for an industrial furnace, but the high temperature oxygen combustion method of the present invention is a combustion heating type heat radiation device such as a radiant tube burner. It is possible to apply to

  The present invention is a high-temperature oxygen combustion apparatus and a high-temperature oxygen combustion method that can be preferably used in a general industrial furnace, and the combustion reaction in the furnace is achieved by mixed contact of pure oxygen heated to an extremely high temperature range and a hydrocarbon fuel. Configured to occur. According to the high temperature oxy-fuel combustion apparatus and the high temperature oxygen combustion method of the present invention, the generation of NOx is substantially completely prevented in the combustion zone, and the energy consumption is further reduced as compared with the high temperature air combustion method. Since the combustion furnace and the combustion equipment can be further miniaturized, their practical effects are remarkable.

Reference Signs List 1 high temperature oxygen combustion system 2 heat exchanger 3 supply / discharge switching valve device 4 exhaust fan 5 fuel injection nozzle 6 oxygen injection nozzle 7 communication passage 8 diverting device 9 furnace body 21 heat storage body 70 differential pressure forming means C combustion furnace H1: H2 heat Exchanger area in the furnace O Pure oxygen F Hydrocarbon fuel M Mixture E: Ea: Ex Combustion exhaust gas B Bypass flow Er Exhaust gas circulation flow R In-furnace combustion gas

Claims (18)

Exhaust for exhausting a combustion system having a combustion zone, an oxidant supply device for supplying to the combustion zone of pure oxygen as an oxidizing agent, the combustion gas generated in the combustion zone to the outside of the combustion system and a system device or equipment, in the high-temperature oxygen combustion device for combustion reaction in the combustion zone and heated with the oxidant and hydrocarbon fuel to a temperature above 800 ° C.,
The combustion zone, a fuel supply unit for supplying the hydrocarbon-based fuel to the combustion zone, the pure oxygen and the combustion gas, the sensible heat held by the combustion gas is transferred to the pure oxygen to be transferred to the pure oxygen A heat storage and regeneration type heat exchanger for heating pure oxygen to a temperature of 800 ° C. or higher, an oxidant introduction path for introducing pure oxygen of the oxidant supply device into the combustion zone through the heat exchanger, and The combustion gas is added to the pure oxygen heated to a temperature of 800 ° C. or more, and a combustion gas lead-out path for leading the combustion gas out of the combustion zone and delivering it to an exhaust system or facility via a heat exchanger or constitute the combustion system by the air-fuel mixture generating means for generating a mixture of the said combustion gas and said pure oxygen the pure oxygen diluted with the combustion gases,
The mixing a portion of the combustion gas by the gas generating means is recirculated in the system of the combustion system to produce the mixture, the mixture that by the catalytic combustion reaction between the hydrocarbon fuel and the mixture hot oxygen combustion apparatus according to claim Rukoto causing the combustion zone. Exhaust for exhausting a combustion system having a combustion zone, an oxidant supply device for supplying to the combustion zone of pure oxygen as an oxidizing agent, the combustion gas generated in the combustion zone to the outside of the combustion system and a system device or equipment, in the high-temperature oxygen combustion device for combustion reaction with the combustion zone and heated with the oxidant and hydrocarbon fuel to a temperature above 800 ° C.,
The combustion zone, fuel supply means for supplying the hydrocarbon-based fuel to the combustion zone, the combustion gas is added to the pure oxygen, or the pure oxygen is diluted with the combustion gas to produce the pure oxygen and the combustion A mixture generation means for generating a mixture with a gas, the mixture and the combustion gas are brought into contact, the sensible heat held by the combustion gas is transferred to the mixture, and the mixture is heated to a temperature of 800 ° C. or more A regenerative heat exchanger for heating, an oxidant introduction path for introducing pure oxygen of the oxidant supply device into the combustion zone through the heat exchanger, and the combustion through the heat exchanger The combustion system is constituted by a combustion gas lead-out path for leading gas out of the combustion zone and delivering it to an exhaust system or facility;
Wherein a portion of the combustion gas by air-fuel mixture producing means and recycled in the system of the combustion system to generate the air-fuel mixture, the combustion by the mixing contact of the mixture after heating and the hydrocarbon fuel hot oxygen combustion apparatus according to claim Rukoto cause combustion reaction in the range. The high temperature oxygen combustion device according to claim 1 or 2 , wherein the mixture generation means sets the oxygen concentration of the mixture within a range of 20 to 50% by volume. The relative combustion zone constituting the combustion system, the pure oxygen supplied from the oxidizing agent supply device is supplied to the combustion zone as the oxidizing agent, the said oxidizing agent heated to a temperature above 800 ° C. and hydrocarbon fuel by combustion reaction in the combustion zone, the hot oxygen combustion method of evacuating to the outside of the combustion system by the exhaust system apparatus or installation the combustion gas generated in the combustion zone,
The combustion zone, a fuel supply unit for supplying the hydrocarbon-based fuel to the combustion zone, the pure oxygen and the combustion gas, the sensible heat held by the combustion gas is transferred to the pure oxygen to be transferred to the pure oxygen A heat storage and regeneration type heat exchanger for heating pure oxygen to a temperature of 800 ° C. or higher, an oxidant introducing path for introducing the pure oxygen into the combustion zone via the heat exchanger, and the heat exchanger via the heat exchanger wherein the combustion gases derived from the combustion zone exhaust system device or combustion gas outlet passage for delivering the equipment, addition of the combustion gas to the pure oxygen which was heated to a temperature above 800 ° C. or the pure oxygen Te The combustion system is constituted by mixture generation means for diluting the mixture with the combustion gas to generate a mixture of pure oxygen and the combustion gas ;
The mixing a portion of the combustion gas by the gas generating means is recirculated in the system of the combustion system to produce the mixture, the mixture that by the catalytic combustion reaction between the hydrocarbon fuel and the mixture The high temperature oxygen combustion method characterized by making it produce in the said combustion zone . The relative combustion zone constituting the combustion system, the pure oxygen supplied from the oxidizing agent supply device is supplied to the combustion zone as the oxidizing agent, the said oxidizing agent heated to a temperature above 800 ° C. and hydrocarbon fuel by combustion reaction in the combustion zone, the hot oxygen combustion method of evacuating to the outside of the combustion system by the exhaust system apparatus or installation the combustion gas generated in the combustion zone,
The combustion zone, a fuel supply means for supplying the hydrocarbon-based fuel to the combustion zone, the combustion gas added to the pure oxygen, or the pure oxygen diluted with the combustion gas to obtain pure oxygen and combustion gas A mixture producing means for producing a mixture, the mixture and the combustion gas are contacted, and the sensible heat held by the combustion gas is transferred by the mixture to heat the mixture to a temperature of 800 ° C. or more A heat storage / regeneration type heat exchanger, an oxidant introduction path for introducing the pure oxygen into the combustion area through the heat exchanger, and the combustion gas is discharged from the combustion area through the heat exchanger. The combustion system from the combustion gas lead-out path for delivery to the exhaust system or equipment;
Wherein a portion of the combustion gas by air-fuel mixture producing means and recycled in the system of the combustion system, the combustion zone to by that combustion reaction in the mixing and contacting of the mixture after heating and the hydrocarbon fuel hot oxygen combustion method characterized by causing the. The high-temperature oxygen combustion apparatus according to claim 4 or 5 , wherein the volume ratio of the oxygen concentration of the mixture is set in the range of 20 to 50%. It has an oxidant supply device for supplying pure oxygen into the furnace as an oxidant, and an exhaust system for exhausting combustion exhaust gas out of the system, and transfers the sensible heat held by the combustion exhaust gas to the oxidant. In the high temperature oxygen combustion apparatus, the oxidant is heated to a temperature of 800 ° C. or more, and the oxidant and the hydrocarbon fuel after the heating are burned and reacted in the furnace region,
Heat storage and regeneration, alternately connected to the pure oxygen supply source of the oxidant supply device and the exhaust system, for leading out the furnace combustion gas to the outside of the furnace and supplying the pure oxygen of the pure oxygen supply source to the furnace region First and second heat exchangers of a type;
A flow path switching device which causes the heat storage bodies of the respective heat exchangers to be alternately in fluid communication with the exhaust system or the pure oxygen source;
The flow passage in the first heat exchanger and the flow passage in the second heat exchanger are interconnected with each other, and a part of the combustion exhaust gas exhausted from the one heat exchanger to the outside of the system is exchanged with the other heat exchange And a communication passage for supplying the flue gas to the pure oxygen to be supplied to the flow path of the
A high-temperature oxygen combustion apparatus characterized in that a mixture of the pure oxygen and the combustion exhaust gas and a hydrocarbon-based fuel are burned and reacted in a furnace region. Pure oxygen is supplied as an oxidant into the furnace and exhaust the flue gas to the outside of the system, and sensible heat held by the flue gas is transferred to the oxidant to heat the oxidant to a temperature of 800 ° C. or higher. A high temperature oxygen combustion method in which the oxidant after heating and the hydrocarbon fuel are burned and reacted in a furnace area,
The heat storage and regeneration type first and second heat exchangers are alternately connected to the pure oxygen source and the exhaust system, and the heat storage bodies of the respective heat exchangers are alternately fluidly connected to the pure oxygen source and the exhaust system,
The flow passage in the first heat exchanger and the flow passage in the second heat exchanger are interconnected with each other, and a part of the combustion exhaust gas exhausted out of the system from one heat exchanger is transferred to the other heat exchanger features and supplied to the flow path, with the addition of flue gas in the pure oxygen to produce a mixture of pure oxygen and combustion exhaust gas, that burning reaction of hydrocarbon fuel and said mixture in a furnace region High temperature oxygen combustion method. An oxidant supply device for supplying pure oxygen into the furnace as an oxidant, and an exhaust system for exhausting combustion exhaust gas out of the system, wherein the oxidant and the hydrocarbon-based fuel in the furnace region In a high-temperature oxygen combustion apparatus that causes a combustion reaction,
Pure oxygen injection means disposed on the inner wall surface of the furnace to inject pure oxygen into the furnace area and induce furnace gas by a pure oxygen jet to dilute and heat pure oxygen with the furnace gas;
Fuel injection means disposed on the inner wall surface of the furnace and injecting hydrocarbon fuel into the furnace so as to mix and contact hydrocarbon fuel with pure oxygen after dilution;
The in-furnace gas is led out of the furnace to exhaust a part of the in-furnace gas out of the system, and the in-furnace gas exhausting / circulating device is provided to recirculate the remainder of the in-furnace gas to the in-furnace region. ,
The in-furnace gas exhaust and circulation device has a heat storage body of a heat storage and regeneration type heat exchanger which is heated in heat transfer contact with the in-furnace gas led to the outside of the furnace and cools the in-furnace gas. A high temperature oxygen combustion apparatus characterized in that a part of the internal gas is exhausted out of the system, and the remaining part of the furnace internal gas is brought into heat transfer contact with the heat storage body to be reheated, and then returned to the furnace internal region. In a high temperature oxygen combustion method in which pure oxygen is supplied as an oxidant into a furnace, the oxidant and a hydrocarbon fuel are burned and reacted in the furnace region, and the flue gas is exhausted out of the system,
Pure oxygen is injected into the in-furnace region by pure oxygen injection means disposed on the inner wall surface of the furnace, and in-furnace gas is induced by pure oxygen jet to dilute and heat pure oxygen with in-furnace gas;
The hydrocarbon fuel is injected into the furnace area by the fuel injection means disposed on the inner wall of the furnace, and the pure oxygen diluted in the furnace gas is mixed with the hydrocarbon fuel to cause combustion reaction of the oxygen and the fuel.
The in-furnace gas is led out of the furnace, and the in-furnace gas is cooled by the heat storage material of the heat storage / regeneration type heat exchanger which makes heat transfer contact with the in-furnace gas led out of the furnace. Sensible heat is stored in the heat storage body,
A portion of the furnace gas after cooling is exhausted as combustion exhaust gas to the outside of the system, and the remaining portion of the furnace gas after cooling is brought into heat transfer contact with the heat storage body to reheat the remaining portion of the furnace gas. A high temperature oxygen combustion method characterized by refluxing to the inner region. The high-temperature oxygen combustion device according to claim 2 or 7 , wherein the combustion gas or the combustion exhaust gas is mixed with the pure oxygen heated or preheated to 150 ° C or more. 9. The high-temperature oxygen combustion method according to claim 5 , wherein the combustion gas or the combustion exhaust gas is mixed with the pure oxygen heated or preheated to 150 ° C. or more.   The high-temperature oxygen combustion device according to claim 7, wherein the oxygen concentration of the mixture is set in the range of 20 to 50% by volume.   The high temperature oxygen combustion device according to claim 7 or 13, wherein the communication passage attracts the combustion exhaust gas by a fluid pressure of the pure oxygen and mixes the combustion exhaust gas with the pure oxygen.   9. The high temperature oxygen combustion method according to claim 8, wherein the oxygen concentration of the mixture is set in the range of 20 to 50% by volume.   The high temperature oxygen combustion method according to claim 8 or 15, wherein the flue gas is attracted by the fluid pressure of the pure oxygen, and the flue gas is mixed with the pure oxygen.   10. The high-temperature oxygen combustion apparatus according to claim 9, wherein the in-furnace gas exhausting / circulating device leads out-furnace gas whose flow rate is 9 times or more of the total flow rate of the pure oxygen and fuel out of the furnace.   The high-temperature oxygen combustion method according to claim 10, wherein the in-furnace gas having a flow rate equal to or more than 9 times the total flow rate of the pure oxygen and fuel injected into the in-furnace region is led out of the furnace.

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