WO2007061668A2 - Circulating fluidized bed boiler having improved reactant utilization - Google Patents
Circulating fluidized bed boiler having improved reactant utilization Download PDFInfo
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- WO2007061668A2 WO2007061668A2 PCT/US2006/044016 US2006044016W WO2007061668A2 WO 2007061668 A2 WO2007061668 A2 WO 2007061668A2 US 2006044016 W US2006044016 W US 2006044016W WO 2007061668 A2 WO2007061668 A2 WO 2007061668A2
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- WIPO (PCT)
- Prior art keywords
- circulating fluidized
- fluidized bed
- furnace
- reactant
- air injection
- Prior art date
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Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J7/00—Arrangement of devices for supplying chemicals to fire
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2206/00—Fluidised bed combustion
- F23C2206/10—Circulating fluidised bed
- F23C2206/103—Cooling recirculating particles
Definitions
- the present invention relates generally to a circulating fluidized bed boilers and, more particularly to a circulating fluidized bed boiler having improved reactant utilization for reduction of undesirable combustion products.
- sulfur-containing carbonaceous compounds especially coal
- a combustion product gas containing unacceptably high levels of sulfur dioxide.
- Sulfur dioxide is a colorless gas, which is moderately soluble in water and aqueous liquids. It is formed primarily during the combustion of sulfur-containing fuel or waste. Once released to the atmosphere, sulfur dioxide reacts slowly to form sulfuric acid (H 2 SO 4 ), inorganic sulfate compounds, and Organic sulfate compounds. Atmospheric SO 2 or H 2 SO 4 results in undesirable "acid rain.”
- acid rain causes acidification of lakes and streams and contributes to damage of trees at high elevations and many sensitive forest soils.
- acid rain accelerates the decay of building materials and paints, including irreplaceable buildings, statues, and sculptures.
- SO 2 and NOx gases and their particulate matter derivatives, sulfates and nitrates Prior to falling to the earth, SO 2 and NOx gases and their particulate matter derivatives, sulfates and nitrates, also contribute to visibility degradation and harm public health.
- Air pollution control systems for sulfur dioxide removal generally rely on neutralization of the absorbed sulfur dioxide to an inorganic salt by alkali to prevent the sulfur from being emitted into the environment.
- the alkali for the reaction most frequently used include either calcitic or dolomitic limestone, slurry or dry quick and hydrated liine, and commercial and byproducts from Theodoric lime and trona magnesium hydroxide.
- the SO 2 once absorbed by limestone, is captured in the existing particle capture equipment such as an electrostatic precipitator or baghouse.
- Circulating fluidized bed boilers utilize a fluidized bed of coal ash and limestone or similar alkali to reduce SO 2 emissions.
- the bed may include other added particulate such as sand or refractory.
- Circulating fluidized bed boilers are effective at reducing SO 2 and NOx emissions.
- a 92% reduction in SO 2 emissions is typical, but can be as high as 98%.
- the stoichiometric ratio of Ca/S needed to achieve this reduction is designed to be approximately 2.2.
- the ratio often increases to 3.0 or more to achieve desired levels of SO 2 capture.
- the higher ratio of Ca/S requires more limestone to be utilized in the process, thereby increasing operating costs.
- inefficient mixing results in the formation of combustion "hotspots" that promote the formation of NOx.
- the present invention is directed to a circulating fluidized bed boiler having improved reactant utilization.
- the circulating fluidized bed boiler may include a circulating fluidized bed.
- the circulating fluidized bed may include a dense bed portion, a lower furnace portion adjacent to the dense bed portion, and an upper furnace portion.
- the dense bed portion of the circulating fluidized bed boiler is preferably maintained below the stoichiometric ratio (fuel rich stage) and the lower furnace portion is preferably maintained above the stoichiometric ratio (fuel lean stage), thereby reducing the formation of NOx.
- the circulating fluidized bed boiler may also include a reactant to reduce the emission of at least one combustion product in the flue gas, a plurality of secondary air injection ports downstream of the circulating fluidized bed for providing mixing of the reactant and the flue gas in the furnace above the dense bed, wherein the amount of reactant required for the reduction of the emission of the combustion product is reduced, and a return system for returning carry over particles from the flue gas to the circulating fluidized bed.
- the reactant is selected from the group consisting of: caustic, lime, limestone, fly ash, magnesium oxide, soda ash, sodium bicarbonate, sodium carbonate, double alkali, sodium alkali, and the calcite mineral group which includes calcite (CaCO3), gaspeite ( ⁇ Ni, Mg, Fe ⁇ .CO3), magnesite (MgCO3), otavite (CdCO3), rhodochrosite (MnC03), siderite (FeCO3), smithsonite (ZnCO3), sphaerocobaltite (CoCO3), and mixtures thereof.
- the reactant is limestone.
- the secondary air injection ports are located in the lower furnace portion of the circulating fluidized bed boiler.
- the secondary air injection ports may be asymmetrically positioned with respect to one another.
- the secondary air injection ports may be arranged in a way selected from the group consisting of opposed inline, opposed staggered, and combinations thereof.
- the secondary air injection ports are positioned between about 10 feet and 30 feet above the dense bed.
- the secondary air injection ports may be positioned at a height in the furnace wherein the ratio of the exit column density to the density of the dense bed top is greater than about 0.7.
- the secondary air injection ports may be positioned at a height in the furnace wherein the gas and particle density is greater than about 140% of the exit gas column density.
- each secondary air injection port when unopposed, is greater than about 50% of the furnace width.
- the jet penetration maybe greater than about 15 inches of water above the furnace pressure.
- the jet penetration may be between about 15 inches and 40 inches of water above the furnace pressure.
- the secondary air injection ports deliver between about 10% and 35% of the total air flow to the boiler.
- the return system includes a separator for removing the carry over particles from the flue gas.
- the separator may be a cyclone separator.
- the separator may be a cyclone separator.
- the return system may also include a fines collector downstream from the separator.
- the fines collector may be a bag house or an electrostatic precipitator.
- the circulating fluidized bed boiler includes: (a) a circulating fluidized bed including: a dense bed portion; a lower furnace portion adjacent to the dense bed portion; and an upper furnace portion; (b) a reactant to reduce the emission of at least one combustion product in the flue gas; and (c) a plurality of secondary air injection ports downstream of the circulating fluidized bed for providing mixing of the reactant and the flue gas in the furnace above the dense bed, wherein the amount of reactant required for the reduction of the emission of the combustion product is reduced.
- the circulating fluidized bed boiler includes: (a) a circulating fluidized bed including a dense bed portion, a lower furnace portion adjacent to the dense bed portion, and an upper furnace portion, wherein the dense bed portion of the circulating fluidized bed boiler is maintained below the stoichiometric ratio (fuel rich stage) and the lower furnace portion is maintained above the stoichiometric ratio (fuel lean stage), thereby reducing the formation of NOx ; (b) a reactant to reduce the emission of at least one combustion product in the flue gas; and (c) a plurality of secondary air injection ports downstream of the circulating fluidized bed for providing mixing ' of the reactant and the flue gas in the furnace above the dense bed, wherein the amount of reactant required for the reduction of the emission of the combustion product is reduced.
- Still another aspect of the present invention is to provide a circulating fluidized bed boiler having improved reactant utilization.
- the circulating fluidized bed boiler includes: (a) a circulating fluidized bed including: a dense bed portion; a lower furnace portion adjacent to the dense bed portion; and an upper furnace portion, wherein the dense bed portion of the circulating fluidized bed boiler is maintained below the stoichiometric ratio (fuel rich stage) and the lower furnace portion is maintained above the stoichiometric ratio (fuel lean stage), thereby reducing the formation of NOx ; (b) a reactant to reduce the emission of at least one combustion product in the flue gas; (c) a plurality of secondary air injection ports downstream of the circulating fluidized bed for providing mixing of the reactant and the flue gas in the furnace above the dense bed, wherein the amount of reactant required for the reduction of the emission of the combustion product is reduced; and (d) a return system for returning carry over particles from the flue gas to the circulating fluidized bed.
- FIG 1 is an illustration of a prior art circulating fluidized bed boiler (CFB);
- Figure 2 is an illustration of a circulating fluidized bed boiler having improved limestone utilization constructed according to the present inventions;
- Figure 3 is a graphical representation of the relationship of gas and particle density versus furnace height in the CFB.
- Figure 4 is a graphical representation of the relationship of mass weighted CO versus height for the baseline case and the present invention case
- Figure 5 is a graphical representation of the relationship of the are-averaged particle volume fraction versus height for the baseline case and the present invention case.
- Figure 6 is a graphical representation of the relationship of the mass weighted turbulent kinetic energy versus height for the baseline case and the present invention case.
- reducible acid refers to acids in which the acidity can be reduced or eliminated by the electrochemical reduction of the acid.
- port is used to describe a reagent injection passageway without any constriction on the end.
- injector is used to describe a reagent injection passageway with a constrictive orifice on the end.
- the orifice can be a hole or a nozzle.
- An injection device is a device that incorporates ducts, ports, injectors, or a combination thereof.
- the circulating fluidized bed boiler may include a furnace 2, a cyclone dust collector 3, a seal box 4, and an optional external heat exchanger 6. Flue gas, which is generated by the combustion in the furnace 2 flows into the cyclone dust collector 3. The cyclone dust collector 3 also separates particles from the flue gas. Particles which are caught by the cyclone dust collector 3 flow into the seal box 4. An external heat exchanger 6 performs heat exchange between the circulating particles and in-bed tubes in the heat exchanger 6.
- the furnace 2 consists of a water cooled furnace wall 2a and air distribution nozzles 7.
- the air distribution nozzles 7 introduce fluidizing air A to the furnace 2 to create a fluidizing condition in the furnace 2, and are arranged in a bottom part of the furnace 2.
- the cyclone dust collector 3 is connected with an upper part of the furnace 2.
- An upper part of the cyclone dust collector 3 is connected with the heat recovery area 8 into which flue gas which is generated by the combustion in the furnace 2 flows, and a bottom part of the cyclone dust collector 3 is connected with the seal box 4 into which the caught particles flows.
- a super heater and economizer are contained in the heat recovery area 8.
- An air box 10 is arranged in a bottom of the seal box 4 so as to intake upward fluidizing air B through an air distribution plate 9.
- the particles in the seal box 4 are introduced to the optional external heat exchanger 6 and are in-bed tube 5 under fluidizing condition.
- the present inventions are based on the discovery that there may be insufficient mixing in the upper furnace (i.e., above the dense bed) to more fully utilize the reactants added to reduce the emissions in the flue gases.
- the top of the dense bed is generally where the gas and particle density is greater than about twice the boiler exit gas/particle density.
- bed materials 11 which comprise ash, sand, and/or limestone etc. are under suspension by the fluidizing condition. Most of the particles entrained with flue gas escape the furnace 2 and are caught by the cyclone dust collector 3 and are introduced to the seal box 4. The particles thus introduced to the seal box 4 are aerated by the fluidizing air B and are heat exchanged with the in-bed tubes 5 of the optional external heat exchanger 6 so as to be cooled. The particles are returned to the bottom of the furnace 2 through a duct 12 so as to re-circulate through the furnace 2.
- high velocity mixing air injection is utilized above the dense bed to both reduce limestone usage and reduce the NOx emissions in a circulating fluidized bed boiler. Additionally, Hg and Acid gas emissions can be reduced.
- the high velocity mixing air injection above the dense bed provides a vigorous mixing of the fluidized bed space, resulting in greater combustion and reaction efficiencies, thereby reducing the amount of limestone or other basic reagent needed to neutralize the flue acids to acceptable levels.
- the circulating fluidized bed boiler of the present invention includes a series of secondary air injection ports 20 advecting the secondary air into the fluidized bed.
- the ports are positioned in a predetermined, spaced-apart manner to create rotational flow of the fluidized bed zone. More preferably, the secondary air injection ports are spaced asymmetrically to generate rotation in the boiler. Since many boilers are wider than they are deep, in an embodiment, a user may set up two sets of nozzles to promote counter rotating.
- the secondary air injection ports are positioned between about 10 feet and 30 feet above the dense bed.
- the air injection ports are preferably arranged to act at mutually separate levels or stages on the mutually opposing walls of the reactor. This system thus provides a vigorous mixing of the fluidized bed space, resulting in greater reaction efficiency between the SO 2 and limestone and thereby permitting the use of less limestone to achieve a given SO 2 reduction level.
- the enhanced mixing permits the reduction of the stoichiometric ratio of Ca/S to achieve the same level of SO 2 reduction.
- the primary elements of high velocity mixing air injection above the dense bed design are:
- the location of the high velocity mixing air ports is well above the dense bed portion of the CFB where the dense bed is defined as the portion having a density greater than twice the furnace exit (cyclone entrance) density
- the high velocity mixing air ports are preferably designed to give rotation of the flue gas, thus further increasing downstream mixing
- the high velocity mixing air ports are high pressure air injection nozzles that introduce high velocity, high momentum, and high kinetic energy turbulent jet flow.
- the vigorous mixing produced by the present invention may also prevents channels or plumes and consequential lower residence time of sulfur compounds, thereby allowing them more time to react in the reactor and further increasing the reaction efficiency.
- the vigorous mixing also provides for more homogeneous combustion of fuel, thereby reducing "hot spots" in the boiler that can create NOx.
- the mass flow of air through the high velocity mixing air ports should introduce between about 15% and 40% of the total air flow. More preferably, the high velocity mixing air ports should introduce between about 20% and 30% of the total air flow.
- the exit velocities for the nozzles should be in excess of about 50 m/s. More preferably, the exit velocities should be iii excess of about 100 m/s.
- the air flow can be hot (drawn downstream of the air heater (air-side)), ambient (drawn upstream of the air heater (air side) at the FD fan outlet), or ambient
- Prior art high-velocity over-fired air applications are limited to mixing combustion zones composed primarily of flue gases and therefore do not increase the efficiency of limestone usage.
- mixing is directed to the furnace combustion zone containing a large mass of inert particles, namely the coal ash and limestone particles.
- the prior art utilizes staging for NOx reduction or high velocity jet mixing for chemical addition.
- staging may be used in addition to mixing and is used to increase the reaction time, control bed temperature control, and reduce the effects of "chimneys" in the furnace.
- Example 1 FLUENT a computational fluid dynamics analytic software program available from Fluent, Inc. of Lebanon, NH, was used to model two-phase thermo- fluid phenomena in a CFB power plant. FLUENT solves for the velocity, temperature, and species concentrations fields for gas and particles in the furnace. Since the volume fraction of particle phase in a CFB is typically between about 0.1% and 0.3%, a granular model solving multi-phase flow was applied to this case. In contrast to conventional pulverized-fuel combustion models, where the particle phase is solved by a discrete phase model in a granular model both gas phase and particle phase conservation equations are solved in an Eulerian reference frame.
- the solved conservation equations included continuity, momentum, turbulence, and enthalpy for each phase.
- the gas phase (>99.7% of the volume) is the primary phase, while the particle phases with its individual size and/or particle type are modeled as secondary phases.
- a volume fraction conservation equation was solved between the primary and secondary phases.
- a granular temperature equation accounting for kinetic energy of particle phase was solved, taking into account the kinetic energy loss due to strong particle interactions in a CFB.
- the present model took five days to converge to a steady solution, running on six CPUs in parallel. While ash and limestone were treated in the particle phase, coal combustion was modeled in the gas phase. Coal was modeled as a gaseous volatile matter with an equivalent stoichiometric ratio and heat of combustion. The following two chemical reactions are considered in the CFB combustion system:
- the chemical-kinetic combustion model included several gas species, including the major products of combustion: CO, CO 2 , and H 2 O.
- the species conservation equations for each gas species were solved. These conservation laws have been described and formulated extensively in computational fluid dynamics (CFD) textbooks.
- CFD computational fluid dynamics
- the CFD computational domain used for modeling is 100 feet high, 22 feet deep, and 44 feet wide.
- the furnace has primary air inlet through.grid and 14 primary ports on all four walls. It also has 18 secondary ports, 8 of them with limestone injection, and 4 start-up burners on both front and back walls.
- Two coal feeders on the front wall convey the waste coal into the furnace. The other two coal feeders connect to each of the cyclone ducts after the loop seal.
- Two cyclones connecting to the furnace through two ducts at the top of the furnace collect the solid materials, mainly coal ash and limestone, and recycle back into the furnace at the bottom.
- the flue gas containing major combustion products and fly ash and fine reacted (and/or unreacted) limestone particles leaves the top of the cyclone and continue in the backpass.
- Water walls run from the top to the bottom of all four-side walls of the furnace.
- the cyclone was not included in the CFB computational domain because the hydrodynamics of particle phase in the cyclone is too complex to practically include in the computation.
- the superheat pendants are included in the model to account for heat absorption and flow stratification, and are accurately depicted by the actual number of pendants in the furnace with the actual distance. Note that the furnace geometry was symmetric in width, so the computational domain only represents one half of the furnace. Consequently, the number of computational grid is only half, which reduced computational time.
- Table 1 shows the baseline system operating conditions including key inputs for the model furnace CFD baseline simulations.
- Table 2 shows the coal composition of the baseline case.
- the coal is modeled as a gaseous fuel stream and a solid particle ash stream with the flow rates calculated from the total coal flow rate and coal analysis.
- the gaseous fuel is modeled as CH 0-85 O 0-14 N 0-07 S 0-02 and is given a heat of combustion of - 3.47 x 10 7 J/kmol . This is equivalent to the elemental composition and the heating value of the coal in the tables.
- the baseline case results are compared to the invention case results.
- High velocity injection significantly improves the mixing by relatively uniformly distributing air into the furnace.
- the mixing of the furnace can be quantified by a coefficient of variance (CoV), which is defined as standard deviation of O 2 mole fraction averaged over a cross section divided by the mean O 2 mole fraction.
- CoV coefficient of variance
- ⁇ /x The Coefficient of Variance ( ⁇ /x ) in O 2 distribution for the baseline case and invention case over four horizontal planes are compared in Table 3. As can be seen, all four planes have high CoV in the baseline case with a range from 66% to 100%, but are significantly lower in both invention cases, indicating that the mixing is significantly improved.
- the mass weighted CO versus height for the baseline case and invention case is compared. Due to staging in the invention case, the CO concentration is higher than that in the baseline case in the low bed below the high velocity air ports. Above the high velocity air ports, the CO concentration rapidly decreases, and the furnace exit CO is even lower than that in the baseline case. The rapid reduction in CO indicates better and more complete mixing.
- the particle fraction distributions of the baseline case and the present invention case are shown in Fig. 5.
- the solid volume fraction in the upper furnace is between 0.001 to 0.003.
- the distribution also reveals particle clusters in the bed, which is one of the typical features of particle movement in CFBs. The air and flue gas mixtures move upward through these clusters. Similar particle flow characteristics can be seen in the present invention case; however, it is also observed that the lower bed below the high velocity air injection is slightly denser than the baseline case, due to low total air flow in the lower bed.
- the upper bed in the present invention case shows similar particle volume fraction distribution to the baseline case.
- the turbulent mixing of air jets and bed particles for both the baseline case and invention case are compared in Fig. 6.
- the enhanced mixing achieved using the present invention is predicted to reduce the stoichiometric ratio of Ga/S in the CFB from -3.0 to -2.4, while achieving the same level of SO 2 reduction (92%).
- the reduction in Ca/S corresponds to reduced limestone required to operate the boiler and meet SO 2 regulations. Since limestone for CFB units often costs more than the fuel (coal or gob), this is a significant reduction on the operational budget for a CFB plant.
- secondary air ports could be installed inline and only some of the secondary air injection ports may operate at any given time. Alternatively, all of the secondary air injection ports may be run, with only some of the air ports running at full capacity. It should be understood that all such modifications and improvements have been deleted herein for the sake of conciseness and readability but are properly within the scope of the following claims.
Abstract
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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EP06827761.5A EP1957866A4 (en) | 2005-11-17 | 2006-11-09 | Circulating fluidized bed boiler having improved reactant utilization |
CN2006800089911A CN101292115B (en) | 2005-11-17 | 2006-11-09 | Circulating fluidized bed boiler having improved reactant utilization |
AU2006316618A AU2006316618A1 (en) | 2005-11-17 | 2006-11-09 | Circulating fluidized bed boiler having improved reactant utilization |
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US11/281,915 | 2005-11-17 | ||
US11/281,915 US7410356B2 (en) | 2005-11-17 | 2005-11-17 | Circulating fluidized bed boiler having improved reactant utilization |
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WO2007061668A2 true WO2007061668A2 (en) | 2007-05-31 |
WO2007061668A3 WO2007061668A3 (en) | 2008-01-03 |
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US (2) | US7410356B2 (en) |
EP (1) | EP1957866A4 (en) |
KR (1) | KR20080084976A (en) |
CN (1) | CN101292115B (en) |
AU (1) | AU2006316618A1 (en) |
PL (1) | PL211124B1 (en) |
RU (1) | RU2008122212A (en) |
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Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2008112345A1 (en) * | 2007-03-13 | 2008-09-18 | Alstom Technology Ltd | Secondary air flow biasing apparatus and method for circulating fluidized bed boiler systems |
US7938071B2 (en) | 2007-03-13 | 2011-05-10 | Alstom Technology Ltd. | Secondary air flow biasing apparatus and method for circulating fluidized bed boiler systems |
DE102009013713A1 (en) * | 2009-03-20 | 2010-09-23 | Mvv Biopower Gmbh | Method for operating a biomass cogeneration plant with a fluidized bed combustion |
EP2634484B1 (en) | 2010-10-29 | 2022-01-26 | Institute Of Engineering Thermophysics, Chinese Academy Of Sciences | Circulating fluidized bed boiler |
US10591155B2 (en) | 2016-08-25 | 2020-03-17 | Doosan Lentjes Gmbh | Circulating fluidized bed apparatus |
Also Published As
Publication number | Publication date |
---|---|
US20070119387A1 (en) | 2007-05-31 |
AU2006316618A1 (en) | 2007-05-31 |
US7410356B2 (en) | 2008-08-12 |
PL211124B1 (en) | 2012-04-30 |
EP1957866A2 (en) | 2008-08-20 |
CN101292115B (en) | 2010-09-22 |
EP1957866A4 (en) | 2013-09-11 |
PL384257A1 (en) | 2008-07-21 |
KR20080084976A (en) | 2008-09-22 |
RU2008122212A (en) | 2009-12-27 |
CN101292115A (en) | 2008-10-22 |
WO2007061668A3 (en) | 2008-01-03 |
US8069825B1 (en) | 2011-12-06 |
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