Patent Application
20060249101
The present invention relates to a thermal generator intended for steam production.
More particularly, it relates to a steam generator, more commonly referred to as boiler, working from the combustion of a fuel, in particular fuel containing sulfur and nitrogen, in the presence of an oxidizer, more particularly an oxidizer with a high oxygen content, generally above 80%.
Such a generator can be used notably for driving rotating machines such as steam turbines of thermal power plants, for which it is necessary to produce steam at high temperature, referred to as superheated steam, with a temperature of the order of 560° C. Another possible application of this generator is the production of steam in refineries to meet the requirements of petroleum conversion processes. It is also possible to use such a generator to produce steam for crude oil extraction.
A steam generator working from the combustion of a fuel in the presence of air is already known, notably from document FR-2,528,540. This generator comprises a combustion hearth (or combustion chamber) provided with at least one burner and includes successively, one after the other, a vaporization zone comprising at least one vaporization exchanger referred to as vaporization screen or evaporator, a superheating zone comprising a superheating exchanger or superheater, a preheating zone comprising a preheating exchanger or economizer and a fumes discharge zone and/or a fumes recirculation zone. A means for storing the water in the gas phase and in the liquid phase, referred to as drum, which supplies the evaporator with heated water and the superheater with steam, is also provided.
This type of generator generally uses two circuits, a first circuit referred to as water circuit, which comprises the exchangers of the vaporization, superheating, preheating zones and the drum, and a second circuit, referred to as fumes circuit, which uses the fumes resulting from the combustion of a fuel with an oxidizer and which is intended for transferring the thermal energy released through combustion to the various exchangers as they flow from the burner to the fumes discharge zones.
In practice, the fumes resulting from combustion are high-temperature fumes which flow through the exchangers to transfer their heat by convection and/or by radiation to the various exchangers so as to heat the water, then to vaporize it and finally to superheat the steam resulting from vaporization. In addition, these fumes can then be sent to a complex processing plant such as a dust collector, followed by a fumes processing unit, prior to being discharged to the atmosphere through a stack.
In the water circuit, the water available on the site is pumped to be injected into the economizer where it is preheated. The preheated water is then sent to either the drum (in the case of natural circulation generators) from which the preheated water feeds the evaporator, or directly to this evaporator (for forced circulation generators) by means of which a large part of the preheated water is vaporized. The two-phase liquid water-steam mixture is then sent to the drum where the liquid phase and the vapour phase are separated. The steam from the drum feeds the superheater which allows to produce steam at very high temperature.
Thus, as it is well known, vaporization of the water occurs for a large part in the evaporator of the combustion hearth, because it is the zone where the highest thermal level of the fumes is reached and where the energy requirements for converting the water to a two-phase fluid in the evaporator are the greatest. A thermal transfer of the energy of the fumes to the superheater then occurs in the superheating zone, a transfer which also requires a high temperature level to obtain superheated steam. Finally, when leaving the superheating zone, the fumes exchange their thermal energies with the economizer which uses the fumes at their lowest temperature levels to preheat the water. All these thermal exchange operations allow to maximize the generator efficiency by using at maximum the heat of the fumes.
It can also be interesting to operate this type of generator using an oxidizer with a high oxygen content, preferably above 80%, and to profit from such a combustion, notably through the reduction of the nitrogen ballast contained in this oxidizer.
In fact, when removing at least part of the nitrogen from the oxidizer, the fumes flow rate and the energy discharged by the combustion fumes through the stack are reduced, and the thermal efficiency of such a steam generator can thus be increased. Thus, for the same transferred heat amount, the fuel consumption is decreased. By way of example, the thermal losses at the stack of a generator running with air and discharging fumes at 250° C. are of the order of 10% of the thermal power provided by the fuel whereas, for identical operating conditions, the thermal losses are reduced to 3% when using pure oxygen as the oxidizer, which generates an energy efficiency increase of the order of 7%. Similarly, the fumes flow rate is reduced by a factor four at least. Furthermore, when using combustion with oxygen, emissions are greatly reduced. More particularly, nitrogen oxides emissions (NOx) resulting from both the thermal dissociation of the molecular nitrogen and from the reaction of the nitrogen contained in the fuel are decreased by a factor one to five for the same burner technology.
Besides, processing of the fumes in order to remove the sulfur oxides can also be simplified considering the increase in the sulfur oxides concentration in the combustion fumes. Significant savings can therefore be obtained as regards the cost of the sulfur oxides processing equipments.
However, the architecture of the steam generators wherein combustion takes place between air and a fuel cannot apply to the generators for which combustion takes place in the presence of an oxidizer with a high proportion of oxygen, or oxycombustion.
In fact,
The definition of the main characteristics of a generator working with oxycombustion first required calculation of the thermal exchange distribution in the various steam production stages.
This will be clear with the example of a 100-MW air generator delivering 124 ton/hour of superheated steam at a temperature of 480° C. and a pressure of 80 bars. In this case, for a fumes temperature at the economizer outlet of 250° C., the distribution of the powers obtained from the enthalpy tables is as follows:
By keeping this fumes temperature of 250° C. at the economizer outlet,
Such a temperature is harmful as regards emissions such as nitrogen oxides (NOx). More particularly, it has been shown that there is an exponential dependence between the NOx formation rate and the temperature of the fumes with a very fast increase in the conversion of the molecular nitrogen of the oxidizer to NO from a fumes temperature of the order of 1500° C. Furthermore, the fumes enter the superheater at a temperature above 2000° C. and the tubes generally making up the superheater are thus subjected to very high fumes temperatures. This solution poses a thermal resistance problem for the superheater tubes within which dry steam already circulates.
In relation to the formation of nitrogen oxides, the experience acquired by the applicant through considerable research work shows that it is preferable not to exceed a fumes temperature of about 1300° C. at the combustion hearth outlet.
It has also been observed that, in the case of conventional boilers working with air, the energy balance showed that about 30% of the thermal energy was absorbed for heating the water, about 40% for its vaporization, about 20% for superheating and about 10% for the thermal losses. In the case of boilers working with oxycombustion, a fumes temperature of the order of 1300° C. at the combustion chamber outlet requires transfer of about 80% of the energy to this combustion chamber, which leaves an insufficient residual thermal energy for the steam superheating and water preheating stage.
The present invention aims to overcome the aforementioned drawbacks by means of a generator wherein the fumes temperature level allowing to obtain steam superheated to a required temperature is obtained in a simple way using techniques and materials commonly used in boilers.
The present invention thus relates to a steam generator comprising at least two successive combustion hearths with at least one burner supplied with fuel and oxidizer, a vaporization zone comprising a vaporization exchanger, a superheating zone comprising an superheating exchanger, a preheating zone comprising a preheating exchanger and a collecting drum, characterized in that each hearth comprises at least one vaporization exchanger.
Preferably, each hearth can comprise at least one superheating exchanger.
Each hearth can also comprise at least one preheating exchanger.
One of the hearths can comprise at least one vaporization exchanger and the other hearth can comprise at least one superheating exchanger.
One of the hearths can comprise at least one vaporization exchanger whereas the other hearth can comprise at least one superheating exchanger and at least one preheating exchanger.
Alternatively, one of the hearths can comprise at least one vaporization exchanger and at least one superheating exchanger, and the other hearth can comprise at least one superheating exchanger and at least one preheating exchanger.
The steam generator can comprise a depollution chamber for the fumes from the combustion hearths.
The fumes depollution chamber can be arranged upstream from the preheating zone.
The fumes depollution chamber can include absorbent injection means.
The fumes depollution chamber can comprise reducing agent injection means.
The fumes depollution chamber can comprise at least one vaporization zone.
The absorbent injected into the fumes depollution chamber can be of calcic or magnesian type.
The reducing agent injected into the fumes depollution chamber can be of urea or ammonia type.
The oxidizer is a high oxygen content oxidizer whereas the fuel is a solid, liquid or gaseous fuel, such as heavy fuel oil, a petroleum residue, a gas, oil coke or coal.
The walls of at least one hearth can consist of a shell or of membrane walls.
Other features and advantages of the invention will be clear from reading the description hereafter, given by way of non limitative example, with reference to the accompanying figures wherein:
In connection with
At least one burner 12 supplied with fuel through a line 14 and with oxidizer through a line 16 is arranged, preferably vertically, in the upper part of primary combustion hearth F1 as shown in the figure. The layout and the amount of burners will be determined by the man skilled in the art so as to obtain a combustion with low emissions while preventing contact of the burner flame with walls 18 of this hearth. This combustion can also be performed by any other means such as grates, fluidized beds. Depending on the fuel injected, an auxiliary fluid will be judiciously used to optimize combustion, such as steam or a gas or a gas mixture, such as CO2 or O2 notably, in order to provide recycling of the fumes that could be used for vaporization of the fuel.
This primary combustion hearth F1 comprises a vaporization zone V including at least one vaporization exchanger or vaporizing screen 20, referred to as evaporator in the description hereafter, which consists, in the example described, of the walls of primary hearth F1 which are preferably of “membrane wall” type. As it is well known, these membrane walls consist of tubes connected to one another by welded fins so as to form a heat exchanger. The evaporator thus obtained is a high-temperature evaporator which provides at least partial evaporation of the fluid circulating within the tubes.
Outlet 22 of this vaporization zone V and consequently of primary hearth F1, which is arranged in the lower part of this hearth, opens into secondary combustion hearth F2, preferably vertical, containing, in the lower part thereof and in connection with outlet 22, a burner 24 supplied with fuel through a line 26 and with oxidizer through a line 28, as defined above. Also, the layout and the number of burners will be determined by the man skilled in the art so as to obtain a combustion with low emissions while preventing contact of the burner flame with the walls of secondary hearth F2.
This secondary combustion hearth comprises a high-temperature superheating zone S1 including at least one superheating exchanger or superheater 30, referred to as high-temperature superheater, for raising the temperature of the fluid, generally in the vapour phase, flowing therethrough. The walls of this hearth therefore consist of a preferably metallic shell 32 protected from the thermal radiation by an insulating material such as concrete, bricks or a fibrous material. Tube bundles 34 through which steam circulates are installed along this insulating material. This superheater is a high-temperature exchanger providing superheating of the fluid in the vapour phase that flows therethrough.
Outlet 36 of the high-temperature superheating zone communicates, in the upper part, with a housing E including an additional superheating zone S2 referred to as low-temperature superheating zone, and preferably a preheating zone P. Low-temperature superheating zone S2 comprises at least one convective type exchanger 38, referred to as low-temperature superheater. Preheating zone P also comprises at least one convective type exchanger 40, referred to as economizer. These convective exchangers 38 and 40 consist, as it is known in the art, of tube bundles connected to collectors. Thus, the steam generator comprises two successive combustion hearths, primary combustion hearth F1 and, in series with this primary combustion hearth, secondary combustion hearth F2. Primary hearth F1 comprises burner 12 and evaporator 20, whereas hearth F2 comprises burner 24, high-temperature superheater 30 and is followed by housing E consisting of low-temperature superheater 38 and economizer 40.
In the lower part of this housing E, outlet 42 of the preheating zone opens into a fumes discharge zone F which communicates with any known fumes processing means or with a stack (not shown).
Economizer 40 comprises a water inlet 44 and a preheated water outlet 46 ending through a line 48 into a fluid collecting means 50 such as a drum commonly used in this type of generator. Low-temperature superheater 38 comprises an inlet 52 for the steam coming from drum 50 through a line 54 and an outlet 56 for sending the steam to high-temperature superheater 30. High-temperature superheater 30 comprises an inlet 58 for the steam coming from low-temperature superheater 38 carried by a line 60 and an outlet 62 for a preferably superheated steam that is sent, through a line 64, to any means using such a superheated steam, such as a thermal power plant turbine. Advantageously, the economizer and the low-temperature superheater can be provided with thermal transfer increasing devices such as fins if the fumes flowing therethrough are not too much dust-laden. Evaporator 20 comprises an inlet 66 supplied with preheated water through a line 68 connecting drum 50 to this inlet and an outlet 70 for sending a water emulsion in two-phase form (liquid water-steam) to drum 50 by means of a line 72.
Thus, during operation of this generator, the water is fed into economizer 40 through inlet 44, it circulates in this economizer while being preheated, then it is collected in drum 50 by means of line 48 connecting this drum to economizer outlet 46. This hot water is then sent from drum 50 to inlet 66 of evaporator 20 through line 68 in order to be at least partly converted to a two-phase water emulsion at outlet 70. The emulsion leaving the evaporator is sent through line 72 to drum 50 where it is subjected to a separation of the gas phase and of the liquid phase. The steam contained in this drum is then sent through line 54 to inlet 52 of low-temperature superheater 38 where an increase in temperature of this steam takes place so as to obtain at outlet 56 dry steam at a first temperature level. What is understood to be dry steam is steam at a higher temperature than the saturation temperature of the water at the pressure considered. Inlet 58 of high-temperature superheater 30 receives the steam from low-temperature superheater 38 by means of line 60 and this steam flows out through outlet 62 in form of superheated steam, i.e. at a higher temperature than that of the steam from low-temperature superheater 38.
In order to obtain these different temperature rises and/or phase change of the fluid circulating in the various exchangers, it is necessary to judiciously use the thermal energy produced by the combustion. A proportion of the total amount of gaseous, liquid or solid fuel, typically ranging between 20% and 80% of this total amount, and a proportion of the total amount of the high oxygen content oxidizer, typically ranging between 20% and 80%, are therefore injected through lines 14 and 16 into burner 12 of primary combustion hearth F1. This power distribution over at least two hearths allows to provide operation under reduced running conditions and to obtain a higher generator flexibility. The fumes generated by the combustion flow through vaporization zone V and exchange part of their thermal energy with the preheated water circulating in the tubes of evaporator 20 so as to obtain, at outlet 70 of this evaporator, a fluid in two-phase liquid water-steam form.
At outlet 22 of primary hearth F1, the fumes are sent to secondary combustion hearth F2 where combustion of the remaining fraction of the total amount of fuel and of oxidizer occurs by means of burner 24 supplied with fuel and oxidizer through lines 26 and 28. The temperature of the fumes is then increased and these fumes flow through high-temperature superheating zone SI which comprises high-temperature superheater 30. The temperature of the steam circulating in the tubes of this superheater is then increased and this superheated steam is then discharged through line 64 to be used by known means such as a turbine or any process. The fumes leaving high-temperature superheating zone S1 through outlet 36 are sent to low-temperature superheating zone S2 comprising low-temperature superheater 38 wherein the steam undergoing a temperature rise circulates. Alternatively, as described more in detail in connection with
These fumes are then discharged through outlet 42 to zone F and sent to any suitable processing means or to a stack as it is known in the art.
By way of example, burner 12 generates fumes whose temperature at outlet 22 of hearth F1 is of the order of 1300° C. These fumes then enter secondary combustion hearth F2. By means of burner 24, they undergo a temperature rise and reach a temperature of the order of 1000° C., after exchange in hearth F2, at outlet 36 of zone S1. These fumes thus heated enter secondary superheating zone S2 by exchanging their thermal energies with low-temperature superheater 38 which they leave at a temperature of about 600° C., then they flush through economizer 40 present in preheating zone P and are discharged through outlet 42 to zone F at a temperature of approximately 250° C.
In parallel, the water is introduced in economizer 40 at a temperature of about 150° C. and it flows out at about 290° C. This preheated water is then partly vaporized in evaporator 20, after passage through drum 50, and it flows out at a temperature of about 305° C. prior to being sent to drum 50. The steam leaving this drum at the same temperature is injected into low-temperature superheater 38 by means of which its temperature increases up to about 375° C. at outlet 56, from which it is sent to high-temperature superheater 30 which it leaves at approximately 480° C.
Without departing from the scope of the invention, a multiplicity of combustion hearths can be installed one after the other and arranged in series in relation to one another. Furthermore, it is possible for at least one vaporization and/or superheating and/or preheating zone comprising at least one exchanger, such as an evaporator and/or a superheater and/or an economizer, connected in series to the exchangers arranged after the other combustion hearths, to be arranged in each combustion hearth.
In the example of
Advantageously, in this variant, the entire generator comprises “membrane wall” type walls so as to profit from the thermal energy contained in the fumes circulating from primary hearth F1 to outlet 42.
This generator comprises a primary combustion hearth F1 and a secondary combustion hearth F2 comprising a low-temperature superheating zone S2. This zone opens onto a preheating zone P ended by a fumes discharge zone F. Primary hearth F1 of “membrane wall” type, as described above, comprises a burner 12, a vaporization zone V with an evaporator 20 and a fumes outlet 74 which opens onto a high-temperature superheating zone S1 contained in a housing E1. This substantially vertical and elongate housing is also of “membrane wall” type and it contains a high-temperature superheater 30 of conductive type, with a steam inlet 58 and a superheated steam outlet 62. Outlet 22 of this superheating zone opens into secondary combustion hearth F2 which comprises a burner 24, as described in connection with
Preferably, low-temperature superheating zone S2 and preheating zone P comprise “membrane wall” type walls. In this configuration, intake of the preheated water in the evaporator and outflow of the two-phase fluid (liquid water-steam) can occur at different levels. Notably, there can be several preheated water inlets in the membrane walls and several two-phase fluid outlets opening into the drum.
By way of example, as shown in
In the variant where all of the walls are of “membrane wall” type, primary hearth comprises burner 12, evaporation zone V with evaporator 20, high-temperature superheating zone S1 with high-temperature superheater 30 and vaporization zone V1 comprising the tubes of the membrane wall of housing E1, whereas secondary hearth F2 comprises burner 24, low-temperature superheating zone S2 with low-temperature superheater 38, preheating zone P with economizer 40 and vaporization zones V2 and V3 comprising the tubes of the membrane walls.
Thus, as described above in connection with
The fumes leaving superheating zone S1 are sent through outlet 22 to secondary combustion hearth F2 where combustion of the remaining fraction of the total amount of fuel and of oxidizer is performed by means of burner 24. The temperature of these fumes is then increased and they are discharged through outlet 36 to secondary superheating zone S2 while exchanging their thermal energies with low-temperature superheater 38. As they flow through the secondary hearth and the high-temperature superheating zone, the fumes also transmit part of their energies to the tubes of vaporization zone V2. The fumes leaving low-temperature superheating zone S2 flow through preheating zone P in which the water circulating in economizer 40 undergoes a temperature increase through the thermal exchanges with the fumes while cooling the fumes to a suitable temperature. Similarly, the fumes transmit their thermal energies to the tubes of the membrane walls forming evaporation zone V3. These fumes are then discharged through outlet 42 into zone F and they are sent to any suitable processing means or to a stack as it is known in the art.
During operation, the water flowing into economizer 40 through inlet 44 is sent, after being heated by passing through this economizer, to drum 50 through line 48. The hot water is then sent through line 68 from this drum to inlet 66 of evaporator 20. The two-phase liquid water-steam fluid flowing from outlet 70, which has absorbed the calories of the fumes throughout their flow through the generator, from burner 12 to outlet 42, is sent through line 72 to drum 50. In this drum, the two-phase fluid is subjected to a separation between the vapour phase and the liquid phase, and the steam is sent through line 54 to inlet 52 of low-temperature superheater 38 where the temperature of this steam is raised to a first level. At outlet 56 of this superheater, the steam is sent through a line 60 to inlet 58 of high-temperature superheater 30 where the temperature of the steam is raised again to a higher level than the level of low-temperature superheater 38 prior to being discharged through outlet 62 to any device as described above.
Of course, during all these operations, burners 12 and 24 are fed as described in connection with
Still by way of example, the temperatures of the fumes are about 1300° C. at the outlet of evaporation zone V, about 500° C. at the outlet of high-temperature superheating zone S1, about 1300° C. at the inlet of low-temperature superheating zone S2, about 350° C. at the outlet of this zone and about 200° C. at outlet 42 to fumes discharge zone F. The temperatures of the fluids in the various exchangers are of the order of 150° C. at inlet 44 of economizer 40, of the order of 165° C. at outlet 46 of this economizer, of the order of 304° C. at outlet 70 of the evaporator and at inlet 52 of low-temperature superheater 38, of the order of 360° C. at outlet 56 of this superheater and at inlet 58 of high-temperature superheater 30, and of the order of 480° C. at outlet 62 of this high-temperature superheater.
This variant essentially differs from
In fact, the applicant has observed that combustion in generators generally produces fumes containing atmospheric pollutants such as sulfur oxides (SOx) and nitrogen oxides (NOx) which have a negative impact on the environment.
Many processes for treating these pollutants are known, but most of them operate at low temperatures, generally on the fumes leaving the preheating zone. However, for simplification of the nitrogen oxides processing or to prevent the condensation of sulfuric acid from the sulfur oxides, these pollutants are preferably treated at high temperatures of the order of 1000° C.
Thus, in the case of the variant of
As already described in connection with
The outlet of this zone communicates with depollution chamber 76 which, in the example shown, is a desulfurization chamber.
This chamber is equipped with at least one absorbent injector 88 allowing fast and homogeneous dispersion of a jet of absorbents in the fumes flowing through this chamber. The injected absorbent can be of calcic or magnesian type, or of any other type allowing reaction with the sulfur oxides contained in the fumes to limit their formation. The grain size and the amounts of injected absorbent will be determined by the man skilled in the art so as to obtain desulfurization rates in accordance with current regulations.
Advantageously, one will profit from this depollution chamber to also provide denitrification of the fumes flowing therethrough by injecting a reducing agent such as urea or ammonia. This reducing agent will be homogeneously dispersed in the depollution chamber by a means similar to absorbent injector 88.
The number and the layout of the absorbent injectors and/or of reducing agent will be determined by the man skilled in the art so as to provide good distribution of the absorbent and/or of the reducing agent in the depollution chamber.
The walls of this depollution chamber advantageously consist of “membrane wall” type walls and they also take part in the evaporation of the water circulating in the evaporator by forming an evaporation zone V4.
Outlet 90 of the depollution chamber communicates, as already described in connection with
During operation, the fumes generated by primary hearth F1 successively flow through primary vaporization zone V, then high-temperature superheating zone S1. At the outlet of this superheating zone, the temperature of the fumes is then raised by means of burner 24. These fumes then flow through medium-temperature superheating zone S3 and reach depollution chamber 76 where they are desulfurized and/or denitrified through injection of absorbents and/or of reducing agents. The fumes thus treated reach outlet 90 from which they enter low-temperature superheating zone S2 and preheating zone P prior to reaching fumes discharge zone F.
In parallel, the water admitted in economizer 40 is heated by passage through this economizer, then it is sent to drum 50. The hot water present in the drum is sent to evaporator 20, then the two-phase liquid water-steam fluid from this evaporator is sent to drum 50 through line 72. The steam present in the drum is sent to low-temperature superheater 38 from where it is sent through line 82 to medium-temperature superheater 78. The steam coming from this medium-temperature superheater is then sent through line 86 to high-temperature superheater which it leaves through outlet 62 and line 64.
The fumes flowing through depollution chamber 76 are at a temperature preferably ranging between 600° C. and 1100° C. so as to obtain a required desulfurization rate in accordance with the residence time of the fumes in the depollution chamber. It can be observed that this temperature range also allows denitrification of the fumes if this chamber is equipped with reducing agent injectors as described above.
Furthermore, as already described in connection with
In an example illustrating this variant, we consider a 100-MW generator working under oxycombustion and delivering 124 tons/hour of steam superheated to a temperature of the order of 480° C. The fuel used consists, in percent by mass, of about 84% carbon, about 9% hydrogen, about 6% sulfur and about 1% nitrogen. The composition by volume of the oxidizer is of the order of 95% oxygen, of the order of 3% nitrogen and of the order of 2% argon. The fuel and oxidizer flow rates are respectively about 1.29 kg/s and 4.24 kg/s for primary combustion hearth F1, whereas they are about 1.39 kg/s and 4.56 kg/s for secondary combustion hearth F2.
From such conditions, the temperature of the water at the inlet of economizer 40 being 150° C., the temperature of the heated water at the outlet of the economizer is about 180° C., whereas the temperature of the fumes upstream from preheating zone P is about 450° C. and about 250° C. downstream from this zone. The temperature of the two-phase liquid water-steam fluid after passage through evaporator 20 is about 305° C. at outlet 70 of the evaporator. The temperature of the steam at the inlet of low-temperature superheater 38 is of the order of 305° C. and of the order of 330° C. at its outlet, whereas the temperature of the fumes is of the order of 750° C. upstream from low-temperature superheating zone S2 and of the order of 450° C. downstream from this zone. The temperature of the steam at inlet 80 of medium-temperature superheater 78 is of the order of 330° C. and of the order of 420° C. at its outlet 84, whereas the temperature of the fumes is of the order of 1300° C. upstream from medium-temperature superheating zone S3 and of the order of 1000° C. downstream from this zone and at the inlet of depollution chamber 76. The temperature of the steam at the inlet of high-temperature superheater 30 is of the order of 420° C. and of the order of 480° C. at its outlet 62, whereas the temperature of the fumes is of the order of 1300° C. upstream from high-temperature superheating zone S1 and of the order of 500° C. downstream from this superheating zone.
The present invention is not limited to the embodiment examples described above and it includes all variants.
Advantageously, one may consider operating primary combustion hearth F1 below stoichiometric conditions with an excess amount of fuel in relation to the oxidizer, so as to limit nitrogen oxides emissions.
Under such conditions, in order to obtain a good combustion efficiency, secondary combustion hearth F2 can work above stoichiometric conditions with an excess amount of oxidizer in relation to the fuel.
Furthermore, considering the thermal energy available in the combustion hearths, it may be advantageous to do without the economizer and to perform preheating of the water by the evaporator which will receive the water at the temperature of the site. This water will be preheated during circulation at the start of the evaporator, then evaporated in the rest of the evaporator.
| Number | Date | Country | Kind |
|---|---|---|---|
| 0301166 | Jan 2003 | FR | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/FR04/00131 | 1/21/2004 | WO | 6/14/2006 |
