US20060249101A1 - Steam generator comprising successive combustion chambers - Google Patents

Steam generator comprising successive combustion chambers Download PDF

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Publication number
US20060249101A1
US20060249101A1 US10/543,809 US54380904A US2006249101A1 US 20060249101 A1 US20060249101 A1 US 20060249101A1 US 54380904 A US54380904 A US 54380904A US 2006249101 A1 US2006249101 A1 US 2006249101A1
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United States
Prior art keywords
fumes
exchanger
temperature
steam generator
zone
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US10/543,809
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English (en)
Inventor
Tidjani Niass
Nicolas Boudet
Gerard Martin
Jacques Dugue
Jacques Segret
Maguelonne Hammel
Umesh Goel
Valerie Naudet
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IFP Energies Nouvelles IFPEN
Air Liquide SA
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IFP Energies Nouvelles IFPEN
Air Liquide SA
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Assigned to INSTITUT FRANCAIS DU PETROLE reassignment INSTITUT FRANCAIS DU PETROLE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: NAUDET, VALERIE, MARTIN, GERARD, BOUDET, NICOLAS, NIASS, TIDJANI, SEGRET, JACQUES, DUGUE, JACQUES, HAMMEL, MAGUELONNE, GOEL, UMESH
Assigned to AIR LIQUIDE, INSTITUT FRANCAIS DU PETROLE reassignment AIR LIQUIDE RE-RECORD TO ADD A 2ND ASSIGNEE ON A DOCUMENT PREVIOUSLY RECORDED AT REEL 018128, FRAME 0248. (ASSIGNMENT OF ASSIGNOR'S INTEREST) Assignors: NAUDET, VALERIE, MARTIN, GERARD, BOUDET, NICOLAS, NIASS, TIDJANI, SEGRET, JACQUES, DUGUE, JACQUES, HAMMEL, MAGUELONNE, GOEL, UMESH
Assigned to AIR LIQUIDE, INSTITUT FRANCAIS DU PETROLE reassignment AIR LIQUIDE CORRECTIVE ASSIGNMENT TO CORRECT THE 7TH & 8TH INVENTORS AND THEIR EXECUTION DATE, PREVIOUSLY RECORDED AT REEL 018353 FRAME 0101. Assignors: SEGRET, JACQUES, GOEL, UMESH, MARTIN, GERARD, BOUDET, NICOLAS, NIASS, TIDJANI, DUGUE, JACQUES, HAMMEL, MAGUELONNE, NAUDET, VALERIE
Publication of US20060249101A1 publication Critical patent/US20060249101A1/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22G—SUPERHEATING OF STEAM
    • F22G1/00—Steam superheating characterised by heating method
    • F22G1/16—Steam superheating characterised by heating method by using a separate heat source independent from heat supply of the steam boiler, e.g. by electricity, by auxiliary combustion of fuel oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B21/00—Water-tube boilers of vertical or steeply-inclined type, i.e. the water-tube sets being arranged vertically or substantially vertically
    • F22B21/34—Water-tube boilers of vertical or steeply-inclined type, i.e. the water-tube sets being arranged vertically or substantially vertically built-up from water tubes grouped in panel form surrounding the combustion chamber, i.e. radiation boilers
    • F22B21/348—Radiation boilers with a burner at the top
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
    • F22B31/04—Heat supply by installation of two or more combustion apparatus, e.g. of separate combustion apparatus for the boiler and the superheater respectively

Definitions

  • the present invention relates to a thermal generator intended for steam production.
  • 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.
  • 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.
  • 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.
  • water circuit which comprises the exchangers of the vaporization, superheating, preheating zones and the drum
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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%.
  • the fumes flow rate is reduced by a factor four at least.
  • 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.
  • 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.
  • FIG. 1 which is a graph showing, in abscissa, the temperature of the fumes (in ° C.) and, in ordinate, the combustion efficiency (in %), shows the efficiency difference between a combustion with air (curve I) and oxycombustion (curve II).
  • FIG. 1 gives a 90.2% thermal efficiency for a fumes temperature of 250° C. (point A) at the economizer outlet.
  • FIG. 1 shows that the temperature of the fumes at the outlet of an evaporator consuming 43.8% of the power delivered by an oxycombustion generator using an oxidizer whose composition is of the order of 95% oxygen, of the order of 3% nitrogen and of the order of 2% argon, is greatly above 2000° C. (line B).
  • 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.
  • NOx nitrogen oxides
  • FIG. 1 shows that the thermal efficiency associated with this temperature is of the order of 80.9% (point C) for a combustion chamber working under oxycombustion, which is markedly higher than the efficiency required by the evaporator, which is 43.8% for a temperature of about 1200° C. (point D).
  • 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.
  • 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.
  • 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.
  • FIG. 2 shows a generator according to an embodiment of the invention
  • FIG. 3 shows a first variant of the invention
  • FIG. 4 shows another variant of the invention.
  • steam generator 10 comprises two successive combustion hearths F 1 and F 2 wherein a fuel burns in the presence of an oxidizer.
  • the fuel is a solid, liquid or gaseous fuel containing notably sulfur and nitrogen, such as heavy fuel oil, a petroleum residue, a gas, oil coke or coal, whereas the oxidizer is preferably a gas with a very high oxygen content, preferably above 80%, or pure oxygen.
  • 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 F 1 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.
  • an auxiliary fluid will be judiciously used to optimize combustion, such as steam or a gas or a gas mixture, such as CO 2 or O 2 notably, in order to provide recycling of the fumes that could be used for vaporization of the fuel.
  • This primary combustion hearth F 1 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 F 1 which are preferably of “membrane wall” type.
  • 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 F 1 which is arranged in the lower part of this hearth, opens into secondary combustion hearth F 2 , 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.
  • 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 F 2 .
  • This secondary combustion hearth comprises a high-temperature superheating zone S 1 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 S 2 referred to as low-temperature superheating zone, and preferably a preheating zone P.
  • Low-temperature superheating zone S 2 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.
  • the steam generator comprises two successive combustion hearths, primary combustion hearth F 1 and, in series with this primary combustion hearth, secondary combustion hearth F 2 .
  • Primary hearth F 1 comprises burner 12 and evaporator 20
  • hearth F 2 comprises burner 24 , high-temperature superheater 30 and is followed by housing E consisting of low-temperature superheater 38 and
  • 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.
  • 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 .
  • 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.
  • 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 .
  • 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.
  • the fumes are sent to secondary combustion hearth F 2 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 S 1 through outlet 36 are sent to low-temperature superheating zone S 2 comprising low-temperature superheater 38 wherein the steam undergoing a temperature rise circulates.
  • the fumes are sent to a fumes processing zone with absorbent injection prior to passage into low-temperature superheater 38 .
  • These fumes then flow through preheating zone P wherein the water circulating in economizer 40 undergoes a temperature rise by thermal exchange with the fumes while cooling these fumes to a suitable temperature, generally of the order of 250° C.
  • burner 12 generates fumes whose temperature at outlet 22 of hearth F 1 is of the order of 1300° C. These fumes then enter secondary combustion hearth F 2 . By means of burner 24 , they undergo a temperature rise and reach a temperature of the order of 1000° C., after exchange in hearth F 2 , at outlet 36 of zone S 1 . These fumes thus heated enter secondary superheating zone S 2 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.
  • 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.
  • 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.
  • 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.
  • FIG. 3 showing a variant of FIG. 2 , and which therefore comprises the same reference numbers, a “membrane wall” type secondary combustion hearth F 2 is used and the high-temperature superheating zone is arranged in primary combustion hearth F 1 .
  • the entire generator comprises “membrane wall” type walls so as to profit from the thermal energy contained in the fumes circulating from primary hearth F 1 to outlet 42 .
  • This generator comprises a primary combustion hearth F 1 and a secondary combustion hearth F 2 comprising a low-temperature superheating zone S 2 .
  • This zone opens onto a preheating zone P ended by a fumes discharge zone F.
  • Primary hearth F 1 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 S 1 contained in a housing E 1 .
  • 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 F 2 which comprises a burner 24 , as described in connection with FIG. 2 , and which also consists of membrane walls.
  • Fumes outlet 36 opens, as described above, onto a low-temperature superheating zone S 2 with a low-temperature superheater 38 comprising a steam inlet 52 and a steam outlet 56 , said zone communicating with a preheating zone P including an economizer 40 provided with a water inlet 44 and a preheated water outlet 46 , this preheating zone communicating with a fumes discharge zone F through an outlet 42 .
  • low-temperature superheating zone S 2 and preheating zone P comprise “membrane wall” type walls.
  • intake of the preheated water in the evaporator and outflow of the two-phase fluid (liquid water-steam) can occur at different levels.
  • evaporator 20 comprises a preheated water inlet 66 at primary hearth F 1 and a two-phase fluid (liquid water-steam) outlet 70 located at outlet 42 of the preheating zone, and connected by a line 72 to drum 50 .
  • Combustion hearths F 1 and F 2 , high-temperature superheating zone S 1 , low-temperature superheating zone S 2 and preheating zone P therefore each comprise part of evaporator 20 distributed in the evaporation zones bearing reference numbers V, V 1 , V 2 and V 3 in the figure.
  • two-phase fluid outlet 70 will be located at the outlet of secondary hearth F 2 , this outlet being connected by line 72 to drum 50 as shown in dotted line in the figure, and only evaporation zones V, V 1 and V 2 will remain.
  • primary hearth comprises burner 12 , evaporation zone V with evaporator 20 , high-temperature superheating zone S 1 with high-temperature superheater 30 and vaporization zone V 1 comprising the tubes of the membrane wall of housing E 1
  • secondary hearth F 2 comprises burner 24 , low-temperature superheating zone S 2 with low-temperature superheater 38 , preheating zone P with economizer 40 and vaporization zones V 2 and V 3 comprising the tubes of the membrane walls.
  • burner 12 of primary hearth F 1 is fed by a proportion of the total amount of gaseous, liquid or solid fuel, and a proportion of the total amount of high oxygen amount oxidizer.
  • the fumes of hearth F 1 flow through vaporization zone V and exchange their thermal energies with the preheated water circulating in the tubes of evaporator 20 so as to obtain at the outlet of this exchanger a fluid in a first two-phase liquid-water-steam form.
  • the fumes flow through high-temperature superheating zone S 1 where they transmit their heat energies, on the one hand, to high-temperature superheater 30 so as to obtain, at the outlet of this superheater, steam at a first temperature level and, on the other hand, to the fluid circulating in the tubes of vaporization zone V 1 .
  • the fumes leaving superheating zone S 1 are sent through outlet 22 to secondary combustion hearth F 2 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 S 2 while exchanging their thermal energies with low-temperature superheater 38 .
  • the fumes also transmit part of their energies to the tubes of vaporization zone V 2 .
  • the fumes leaving low-temperature superheating zone S 2 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 V 3 . 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.
  • 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 .
  • 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.
  • 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.
  • burners 12 and 24 are fed as described in connection with FIG. 2 .
  • 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 S 1 , about 1300° C. at the inlet of low-temperature superheating zone S 2 , 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.
  • FIG. 4 shows a variant of the embodiment of the invention according to FIG. 3 , which therefore comprises the same reference numbers.
  • This variant essentially differs from FIG. 3 in the presence of a housing E 2 containing a fumes depollution chamber 76 and a medium-temperature superheating zone S 3 .
  • 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.
  • SOx sulfur oxides
  • NOx nitrogen oxides
  • 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.
  • fumes depollution chamber 76 like a desulfurization chamber, is arranged after outlet 36 of the fumes generated by burner 24 so as to profit from the temperature of the fumes which is at a high level considering the action of this secondary hearth.
  • primary hearth F 1 of “membrane wall” type comprises a burner 12 , a vaporization zone V with an evaporator 20 , a high-temperature superheating zone S 1 with a high-temperature superheater 30 and a fumes outlet 22 .
  • Outlet 22 of this superheating zone opens into secondary combustion hearth F 2 .
  • Outlet 36 of the fumes generated by burner 24 of hearth F 2 opens onto a medium-temperature superheating zone S 3 with a medium-temperature superheater 78 comprising an inlet 80 connected by a line 82 to outlet 56 of low-temperature superheater 38 and a steam outlet 84 connected by a line 86 to inlet 58 of high-temperature superheater 30 .
  • 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.
  • this depollution chamber 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.
  • 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 V 4 .
  • Outlet 90 of the depollution chamber communicates, as already described in connection with FIG. 3 , with a low-temperature superheating zone S 2 and a preheating zone P which opens through outlet 42 onto fumes processing zone F.
  • the fumes generated by primary hearth F 1 successively flow through primary vaporization zone V, then high-temperature superheating zone S 1 .
  • the temperature of the fumes is then raised by means of burner 24 .
  • These fumes then flow through medium-temperature superheating zone S 3 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 S 2 and preheating zone P prior to reaching fumes discharge zone F.
  • 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.
  • the fumes transmit their thermal energies to the tubes of the various vaporization zones V, V 1 , V 2 , V 3 and V 4 .
  • 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 F 1 , whereas they are about 1.39 kg/s and 4.56 kg/s for secondary combustion hearth F 2 .
  • 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.
  • 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.
  • 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 S 3 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
  • the temperature of the fumes is of the order of 1300° C. upstream from high-temperature superheating zone S 1 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.
  • secondary combustion hearth F 2 can work above stoichiometric conditions with an excess amount of oxidizer in relation to the fuel.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Treating Waste Gases (AREA)
US10/543,809 2003-01-31 2004-01-21 Steam generator comprising successive combustion chambers Abandoned US20060249101A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0301166 2003-01-31
FR0301166A FR2850733A1 (fr) 2003-01-31 2003-01-31 Generateur a foyers de combustion successifs destine a la production de vapeur
PCT/FR2004/000131 WO2004079260A1 (fr) 2003-01-31 2004-01-21 Generateur a foyers de combustion successifs destine a la productiion de vapeur

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US (1) US20060249101A1 (fr)
EP (1) EP1592919A1 (fr)
JP (1) JP2007526976A (fr)
CA (1) CA2514891A1 (fr)
FR (1) FR2850733A1 (fr)
WO (1) WO2004079260A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008073765A3 (fr) * 2006-12-07 2008-11-06 Michael S Bruno Procédé de réduction de l'émission de gaz à effet de serre dans l'atmosphère
US20090158976A1 (en) * 2005-03-01 2009-06-25 Patrick Brian R Module-based oxy-fuel boiler
CN103620304A (zh) * 2010-08-23 2014-03-05 沙特阿拉伯石油公司 具有多个燃烧室的蒸汽产生系统及干燥废气净化
JP2019113234A (ja) * 2017-12-22 2019-07-11 三菱重工業株式会社 ボイラ

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2488903C1 (ru) * 2012-05-03 2013-07-27 Рашид Зарифович Аминов Система сжигания водорода в цикле аэс с регулированием температуры водород-кислородного пара
CN110160036B (zh) * 2019-06-03 2021-01-29 浙江麦知网络科技有限公司 一种钢包专用冶金型精炼渣设备
RU2744607C1 (ru) * 2020-07-20 2021-03-11 Акционерное общество "Конструкторское бюро химавтоматики" Установка для получения горячей воды и пара с использованием водородного парогенератора

Citations (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2402993A (en) * 1939-07-29 1946-07-02 Foster Wheeler Corp Steam generator
US2677354A (en) * 1948-03-25 1954-05-04 Combustion Eng Equalization of temperature in separately fired superheaters
US3017870A (en) * 1958-03-12 1962-01-23 Sulzer Ag Steam or vapor generator having at least two firing systems
US3135244A (en) * 1961-07-27 1964-06-02 Combustion Eng Vapor generator
US3135246A (en) * 1961-07-27 1964-06-02 Combustion Eng Twin furnace unit and method of operation
US3195306A (en) * 1962-12-17 1965-07-20 Combustion Eng Gas-steam power plant
US3213831A (en) * 1963-12-23 1965-10-26 Combustion Eng Vapor generating apparatus
US3263422A (en) * 1965-06-10 1966-08-02 Foster Wheeler Corp Power plant vapor generator
US4829938A (en) * 1987-09-28 1989-05-16 Mitsubishi Jukogyo Kabushiki Kaisha Exhaust boiler
US5047220A (en) * 1989-03-27 1991-09-10 Foster Wheeler Energy Corporation Catalytic denitrification control process and system for combustion flue gases
US5247907A (en) * 1992-05-05 1993-09-28 The M. W. Kellogg Company Process furnace with a split flue convection section
US5293841A (en) * 1992-03-06 1994-03-15 Gea Luftkuhler Gmbh Arrangement for utilizing the heat contained in the exhaust gas of a coal-fired boiler
US5568793A (en) * 1994-01-14 1996-10-29 Abb Management Ag Steam generator
US5605118A (en) * 1994-11-15 1997-02-25 Tampella Power Corporation Method and system for reheat temperature control
US6598399B2 (en) * 2000-01-19 2003-07-29 Alstom (Switzerland) Ltd Integrated power plant and method of operating such an integrated power plant
US6619041B2 (en) * 2001-06-29 2003-09-16 L'air Liquide - Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Steam generation apparatus and methods
US20060065213A1 (en) * 2003-05-23 2006-03-30 Acs Engineering Technologies Inc. Steam generation apparatus and method

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB594389A (en) * 1945-07-06 1947-11-10 Babcock & Wilcox Ltd Improvements in or relating to vapour generating and heating units
GB528783A (en) * 1938-05-20 1940-11-06 Foster Wheeler Ltd Improvements in steam generators
GB569094A (en) * 1942-07-01 1945-05-03 Foster Wheeler Ltd Improvements in or relating to vapour generators particularly steam generators
GB581738A (en) * 1942-12-17 1946-10-23 Foster Wheeler Ltd Improvements in water tube steam boilers
GB632011A (en) * 1948-01-08 1949-11-15 Superheater Co Ltd Improvements in or relating to water tube boiler and steam superheater arrangements
FR1211352A (fr) * 1956-10-23 1960-03-16 Fairfield Shipbuilding And Eng Installations de chaudières à vapeur

Patent Citations (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2402993A (en) * 1939-07-29 1946-07-02 Foster Wheeler Corp Steam generator
US2677354A (en) * 1948-03-25 1954-05-04 Combustion Eng Equalization of temperature in separately fired superheaters
US3017870A (en) * 1958-03-12 1962-01-23 Sulzer Ag Steam or vapor generator having at least two firing systems
US3135244A (en) * 1961-07-27 1964-06-02 Combustion Eng Vapor generator
US3135246A (en) * 1961-07-27 1964-06-02 Combustion Eng Twin furnace unit and method of operation
US3195306A (en) * 1962-12-17 1965-07-20 Combustion Eng Gas-steam power plant
US3213831A (en) * 1963-12-23 1965-10-26 Combustion Eng Vapor generating apparatus
US3263422A (en) * 1965-06-10 1966-08-02 Foster Wheeler Corp Power plant vapor generator
US4829938A (en) * 1987-09-28 1989-05-16 Mitsubishi Jukogyo Kabushiki Kaisha Exhaust boiler
US5047220A (en) * 1989-03-27 1991-09-10 Foster Wheeler Energy Corporation Catalytic denitrification control process and system for combustion flue gases
US5293841A (en) * 1992-03-06 1994-03-15 Gea Luftkuhler Gmbh Arrangement for utilizing the heat contained in the exhaust gas of a coal-fired boiler
US5247907A (en) * 1992-05-05 1993-09-28 The M. W. Kellogg Company Process furnace with a split flue convection section
US5568793A (en) * 1994-01-14 1996-10-29 Abb Management Ag Steam generator
US5605118A (en) * 1994-11-15 1997-02-25 Tampella Power Corporation Method and system for reheat temperature control
US6598399B2 (en) * 2000-01-19 2003-07-29 Alstom (Switzerland) Ltd Integrated power plant and method of operating such an integrated power plant
US6619041B2 (en) * 2001-06-29 2003-09-16 L'air Liquide - Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Steam generation apparatus and methods
US20060065213A1 (en) * 2003-05-23 2006-03-30 Acs Engineering Technologies Inc. Steam generation apparatus and method

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090158976A1 (en) * 2005-03-01 2009-06-25 Patrick Brian R Module-based oxy-fuel boiler
US8082737B2 (en) 2005-03-01 2011-12-27 Jupiter Oxygen Corporation Module-based oxy-fuel boiler
US8752383B2 (en) 2005-03-01 2014-06-17 Jupiter Oxygen Corporation Module-based oxy-fuel boiler
WO2008073765A3 (fr) * 2006-12-07 2008-11-06 Michael S Bruno Procédé de réduction de l'émission de gaz à effet de serre dans l'atmosphère
US20090062593A1 (en) * 2006-12-07 2009-03-05 Bruno Michael S Method for reducing the emission of green house gases into the atmosphere
US7922643B2 (en) 2006-12-07 2011-04-12 Bruno Michael S Method for reducing the emission of green house gases into the atmosphere
EA015025B1 (ru) * 2006-12-07 2011-04-29 Роман Билак Способ уменьшения выбросов парниковых газов в атмосферу
CN103620304A (zh) * 2010-08-23 2014-03-05 沙特阿拉伯石油公司 具有多个燃烧室的蒸汽产生系统及干燥废气净化
JP2019113234A (ja) * 2017-12-22 2019-07-11 三菱重工業株式会社 ボイラ
JP6995609B2 (ja) 2017-12-22 2022-01-14 三菱重工マリンマシナリ株式会社 ボイラ

Also Published As

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EP1592919A1 (fr) 2005-11-09
CA2514891A1 (fr) 2004-09-16
JP2007526976A (ja) 2007-09-20
WO2004079260A1 (fr) 2004-09-16
FR2850733A1 (fr) 2004-08-06

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