Fluidization device for solid fuel particles

A system includes a fluidization device including a flow passage configured to convey a flow of solid fuel particles in a downstream direction, and a body disposed within the flow passage. The body is configured to direct the flow of solid fuel particles between the body and an outer wall of the flow passage. The fluidization device also includes a carrier gas injection port positioned radially outward from the body. The carrier gas injection port is configured to provide a flow of carrier gas in the downstream direction to break up agglomerations within the flow of solid fuel particles.

BACKGROUND OF THE INVENTION

The subject matter disclosed herein relates to a fluidization device for solid fuel particles.

Gasifiers convert carbonaceous materials into a mixture of carbon monoxide and hydrogen, referred to as synthesis gas or syngas. For example, a power plant may include one or more gasifiers that react a feedstock at a high temperature with oxygen and/or steam to produce syngas, which may be treated prior to use as a fuel. As will be appreciated, providing the gasifier with a substantially uniform and homogeneous distribution of feedstock particles enhances efficiency of the syngas conversion process. Unfortunately, conveying the feedstock particles to the gasifier under high pressure induces the formation of agglomerations that may decrease gasifier efficiency.

BRIEF DESCRIPTION OF THE INVENTION

In a first embodiment, a system includes a fluidization device including a flow passage configured to convey a flow of solid fuel particles in a downstream direction, and a body disposed within the flow passage. The body is configured to direct the flow of solid fuel particles between the body and an outer wall of the flow passage. The fluidization device also includes a carrier gas injection port positioned radially outward from the body. The carrier gas injection port is configured to provide a flow of carrier gas in the downstream direction to break up agglomerations within the flow of solid fuel particles.

In a second embodiment, a system includes a fluidization device including a flow passage configured to convey a flow of solid particles in a downstream direction toward a gasifier, and a body disposed within the flow passage. The body is configured to direct the flow of solid particles between the body and an outer wall of the flow passage. The fluidization device also includes a trim gas injection port configured to provide a flow of trim gas in an upstream direction to enhance homogeneity of particle distribution within the flow of solid particles.

In a third embodiment, a system includes a fluidization device including a flow passage configured to convey a flow of solid fuel particles in a downstream direction, and a body disposed within the flow passage. The body is configured to direct the flow of solid fuel particles between the body and an outer wall of the flow passage. The fluidization device also includes multiple splitter vanes disposed within the flow passage and configured to enhance fragmentation within the flow of solid fuel particles and/or multiple swirler vanes disposed within the flow passage and configured to establish a recirculating or swirling flow of solid fuel particles.

DETAILED DESCRIPTION OF THE INVENTION

Embodiments of the present disclosure include a fluidization device configured to establish a substantially uniform and homogeneous flow of solid particles from a pressurization device to a gasifier, while substantially reducing or eliminating buildup of solids within the fluidization device. In certain embodiments, the fluidization device includes a flow passage configured to convey a flow of solid particles in a downstream direction, and a body disposed within the flow passage. The body is configured to direct the flow of solid particles between the body and an outer wall of the flow passage. The fluidization device also includes a carrier gas injection port configured to provide a flow of carrier gas in the downstream direction to break up agglomerations within the flow of solid particles and to carry the solid particles downstream to the gasifier. Further embodiments of the fluidization device include a trim gas injection port configured to provide a flow of trim gas in an upstream direction to enhance homogeneity of particle distribution within the flow of solid particles. Yet further embodiments of the fluidization device include multiple splitter vanes disposed within the flow passage and configured to enhance fragmentation within the flow of solid particles and/or multiple swirler vanes disposed within the flow passage and configured to establish a recirculating or swirling flow of solid particles. Still further embodiments of the fluidization device include a buffer gas injection port configured to inject buffer gas to provide a buffer boundary layer between the flow of solid fuel particles and the outer wall of the flow passage. In certain embodiments, a flow rate of carrier gas through the carrier gas injection port, a flow rate of trim gas through the trim gas injection port, a shape of the body, an angle of each splitter vane relative to the flow of solid particles and/or an angle of each swirler vane relative to the flow of solid particles is adjustable. By utilizing these mechanical and fluid-dynamic features, the fluidization device may break up agglomerations within the flow of solid particles, thereby providing the gasifier with a substantially uniform and homogeneous distribution of feedstock particles which may enhance efficiency of the syngas conversion process, and improve the availability of the solids transport system and gasifier. For example, the transport system may be less likely to experience downtime caused by agglomerated solids plugging the flow passage, and the gasifier may be less likely to experience temperature excursions that reduce the useful life of refractory lined walls or water walls.

FIG. 1is a block diagram of an exemplary power generation system10including a gasifier configured to provide syngas to a combustor. The illustrated power generation system10may be part of an integrated gasification combined cycle (IGCC) system that may produce and burn a synthetic gas, i.e., syngas. Elements of the system10include a fuel source12, such as a solid feed, that may be utilized as a source of energy for the system10. The fuel source12may include coal, petroleum coke, biomass, wood-based materials, agricultural wastes, tars, coke oven gas, and asphalt, or other carbon containing items.

The solid fuel of the fuel source12may be passed to a feedstock preparation unit14. The feedstock preparation unit14may, for example, resize or reshape the fuel source12by chopping, milling, shredding, pulverizing, briquetting, or palletizing the fuel source12to generate feedstock. In the present embodiment, the fuel source12is dry coal, and the feedstock preparation unit14is configured to provide solid particles of dry coal for processing by the gasifier.

The feedstock prepared by the feedstock preparation unit14may be passed to a pressurization device16. In certain embodiments, the pressurization device16is a posimetric solids pump configured to output solid feedstock (e.g., dry coal) particles at a pressure of more than approximately 800 PSIG. As illustrated, the pressurization device16is configured to receive a flow of buffer gas. The buffer gas (e.g., nitrogen, carbon dioxide, steam, etc.) is configured to provide a buffer between the solid particles and the pressurization device16, thereby protecting the surfaces of the pressurization device16from corrosion and/or wear, and ensuring that the carrier gas travels downstream toward the gasifier instead of upstream through the pressurization device. The high pressure solid particles then flow to a fluidization device18. As discussed in detail below, the fluidization device18is configured to inject gas into the flow of solid particles to facilitate movement of the particles in a downstream direction. The fluidization device18is also configured to break up agglomerations within the flow of solid particles, thereby providing the gasifier20with a substantially uniform and homogeneous distribution of feedstock particles which may enhance efficiency of the syngas conversion process.

Certain power generation systems employ a lock hopper to transfer feedstock from the feedstock preparation unit to the gasifier. In such configurations, the lock hopper is filled with feedstock at atmospheric pressure and then sealed. The feedstock is then transferred to a high pressure conveyance line that transports the feedstock toward the gasifier. In this manner, the feedstock may be transferred to the conveyance line without substantial fluid leakage. Unfortunately, because the lock hopper is loaded with feedstock before the transfer process is initiated, feedstock is delivered to the gasifier in a periodic manner, thereby decreasing efficiency of the syngas conversion process. Multiple lock hopper systems, such as those consisting of three vessels, reduce the effect but solids stratification and solids flow variation may still exist. Because the present embodiments employ a pressurization device16(e.g., posimetric solids pump) and a fluidization device18to pressurize and break up the feedstock into a substantially uniform and homogeneous flow, the gasifier20is provided with a substantially continuous supply of feedstock. Consequently, the lock hopper is obviated and the efficiency of the gasifier20may be enhanced.

The gasifier20may convert the feedstock (e.g., dry coal particles) into syngas, e.g., a combination of carbon monoxide and hydrogen. This conversion may be accomplished by subjecting the feedstock to a controlled amount of any moderator and oxygen at elevated pressures (e.g., from approximately 600 PSIG-1200 PSIG) and temperatures (e.g., approximately 2200° F.-2700° F.), depending on the type of gasifier utilized. The heating of the feedstock during a pyrolysis process may generate a solid (e.g., char) and residue gases (e.g., carbon monoxide, hydrogen, and nitrogen). The char remaining from the feedstock from the pyrolysis process may only weigh up to approximately 30% of the weight of the original feedstock.

The combustion reaction in the gasifier20may include introducing oxygen to the char and residue gases. The char and residue gases may react with the oxygen to form carbon dioxide and carbon monoxide, which provides heat for the subsequent gasification reactions. The temperatures during the combustion process may range from approximately 2200° F. to approximately 2700° F. In addition, steam may be introduced into the gasifier20. The gasifier20utilizes steam and limited oxygen to allow some of the feedstock to be burned to produce carbon monoxide and energy, which may drive a second reaction that converts further feedstock to hydrogen and additional carbon dioxide.

In this way, a resultant gas may be manufactured by the gasifier20. The resultant gas may include approximately 85% of carbon monoxide and hydrogen, as well as CH4, HCl, HF, COS, NH3, HCN, and H2S (based on the sulfur content of the feedstock). This resultant gas may be termed “raw syngas.” The gasifier20may also generate waste, such as a slag, which may be a wet ash material.

In certain embodiments, a gas cleaning unit may be utilized to clean the raw syngas. The gas cleaning unit may scrub the raw syngas to remove the HCl, HF, COS, HCN, and H2S from the raw syngas, which may include the separation of H2S by an acid gas removal process. Elemental sulfur may by recovered by a sulfur recovery unit from the H2S. Furthermore, the gas cleaning unit may separate salts from the raw syngas via a water treatment unit, which may utilize water purification techniques to generate usable salts from the raw syngas. Subsequently, a clean syngas may be generated from the gas cleaning unit. This clean syngas may be directed into a combustor22(e.g., a combustion chamber) of a gas turbine engine24as combustible fuel.

The gas turbine engine24includes a turbine26, a drive shaft28, and a compressor30, as well as the combustor22. The combustor22receives fuel, such as the syngas, which may be injected under pressure from fuel nozzles. This fuel is mixed with compressed air and combusted within the combustor22. This combustion creates hot pressurized exhaust gases. The combustor22directs the exhaust gases towards an exhaust outlet of the turbine26. As the exhaust gases from the combustor22pass through the turbine26, the exhaust gases force turbine blades in the turbine26to rotate the drive shaft28along an axis of the gas turbine engine24. As illustrated, the drive shaft28may be connected to various components of the gas turbine engine24, including the compressor30.

The drive shaft28connects the turbine26to the compressor30to form a rotor. The compressor30includes blades coupled to the drive shaft28. Thus, rotation of turbine blades in the turbine26causes the drive shaft28connecting the turbine26to the compressor30to rotate blades within the compressor30. The rotation of blades in the compressor30causes the compressor30to compress air received via an air intake in the compressor30. The compressed air is then fed to the combustor22and mixed with fuel to allow for higher efficiency combustion. The drive shaft28may also be connected to a load32, which may be a stationary load, such as an electrical generator, for producing electrical power in a power plant. Indeed, the load32may be any suitable device that is powered by the rotational output of the gas turbine engine24.

FIG. 2is a schematic diagram of an embodiment of a fluidization device18configured to enhance fragmentation of solid fuel particles. As illustrated, the fluidization device18includes a flow passage34configured to convey a flow of solid particles36in a downstream direction38. As previously discussed, the solid particles36may include dry fuel/feedstock solids, such as coal, that may be converted into syngas within the gasifier20. The fluidization device18is configured to break up agglomerations within the solid particles and provide a substantially homogeneous distribution of particles to the gasifier20. As will be appreciated, a substantially even distribution of dry fuel solids may increase the efficiency of the syngas conversion process, and improve the availability of the solids transport system and gasifier. For example, the transport system may be less likely to experience downtime caused by agglomerated solids plugging the flow passage, and the gasifier may be less likely to experience temperature excursions that reduce the useful life of refractory lined walls or water walls.

In the present embodiment, buffer gas40is injected through buffer gas inlets42positioned along the flow passage34. The buffer gas40may provide a buffer boundary layer between the flow of solid particles36and an outer wall48of the flow passage34, thereby ensuring that the solid particles36do not collect on the outer wall48. In addition, certain solid particles and/or gases injected into the pressurization device may be corrosive. Consequently, the buffer gas40may serve to protect the inner surface of the flow passage34from the effects of the corrosive particles and/or gases, thereby increasing the longevity of the fluidization device18and the pressurization device16(e.g., posimetric solids pump).

The illustrated fluidization device18includes a body44disposed within the flow passage34. The body44is configured to split the flow of solid particles36into multiple flow streams46and to direct each stream46between the body44and the outer wall48of the flow passage34. As illustrated, the body44includes a tapered leading edge47and a tapered trailing edge49. As will be appreciated, the tapered leading and trailing edges47and49facilitate a substantially continuous flow of solid particles36around the body44. By directing the streams46of solid particles36between the body44and the outer wall48, the body44serves to break up agglomerations within the solid particle flow. In the present embodiment, the flow passage34has a substantially circular cross section and the body44is positioned at the approximate radial center of the flow passage34. In this configuration, each stream46will pass through a region having a substantially equal cross-section. However, it should be appreciated that the body44may be positioned closer to one side of the outer wall48, thereby establishing flow passages having varying cross-sections. Furthermore, the illustrated body44is axi-symmetric with respect to the longitudinal axis45of the flow passage34, i.e., the body44includes a substantially circular radial profile centered about the longitudinal axis45. However, it should be appreciated that alternative embodiments of the body44may employ other radial profiles.

As illustrated, the body44is supported by first struts or splitter vanes50and second struts or swirler vanes52. As discussed in detail below, multiple first struts or splitter vanes50and/or multiple second struts or swirler vanes52may be circumferentially spaced about the body44. In certain embodiments, the splitter vanes50are configured to enhance fragmentation within the flow of solid particles36. In alternative embodiments, the first struts50support the body44, but have substantially no impact on fragmentation. As discussed in detail below, the configuration of the splitter vanes50may be particularly configured to provide a desired degree of fragmentation based on the particular solid particles36passing through the fluidization device18(e.g., fuel type, particle size, particle moisture content, etc.) and/or the configuration of the gasifier20. In certain embodiments, the splitter vanes50may be interchangeable to provide the desired degree of fragmentation.

In further embodiments, the angle of the splitter vanes50relative to the flow of solid particles36is adjustable. For example, an actuator may be coupled to the vanes50and configured to rotate each vane50based on a desired degree of fragmentation. For example, the splitter vanes50may be aligned with the flow of solid particles36if a smaller degree of fragmentation is desired, or rotated such that the solid particles36impact a portion of the body of each vane for a larger degree of fragmentation. In certain embodiments, the splitter vanes50may be configured to rotate a first angle51about an axis53substantially parallel to the flow of solid particles36, a second angle55about a radial axis57of the vanes50and/or a third angle59about a circumferential axis61of the vanes50. In alternative embodiments, the angle of each spiller vane50may be fixed.

As discussed in detail below, the swirler vanes52may be configured to establish a recirculating and/or swirling flow of solid particles36. In alternative embodiments, the second struts52support the body44, but have substantially no impact on the flow of solid particles36. As will be appreciated, the recirculating and/or swirling flow of solid particles36may enhance the homogeneity of particle distribution, thereby increasing gasifier efficiency. In certain embodiments, the swirler vanes52may be interchangeable to provide a desired degree of recirculation and/or swirl.

Similar to the splitter vanes50, certain embodiments of the fluidization device18may provide adjustable swirler vanes52. For example, an actuator may alter an angle of each swirler vane52relative to the flow of solid particles36to establish varying degrees of recirculation and/or swirl. For example, the swirler vanes52may be aligned with the flow of solid particles36if a smaller degree of recirculation and/or swirl is desired, or rotated to direct the flow of solid particles36in a direction that induces a large degree of recirculation and/or swirl. In this configuration, a desired degree of recirculation and/or swirl may be induced based on the particular solid particles36passing through the fluidization device18(e.g., fuel type, particle size, particle moisture content, etc.) and/or the configuration of the gasifier20. In certain embodiments, the swirler vanes52may be configured to rotate a first angle51about the axis53substantially parallel to the flow of solid particles36, a second angle55about the radial axis57of the vanes52and/or a third angle59about the circumferential axis61of the vanes52. In alternative embodiments, the angle of each swirler vane52may be fixed.

In the present embodiment, the fluidization device18includes a carrier gas injection port54positioned radially outward from the body44. The carrier gas injection port54is configured to provide a flow of carrier gas (e.g., nitrogen, carbon dioxide, steam, etc.) in the downstream direction38to break up agglomerations within the flow of solid particles36. The carrier gas also serves to urge the flow of solid particles36toward the gasifier20. As illustrated, the fluidization device18includes an inlet56configured to receive a flow of carrier gas, as indicated by the arrow58. The carrier gas passes through a flow path60adjacent to the outer wall48from the inlet56to the injection port54. By positioning the injection port54adjacent to an outer surface63of the fluidization device18, the flow of carrier gas may substantially reduce or eliminate buildup of solid particles36along the outer surface63, thereby decreasing solid particle residence time and enhancing homogeneity of the flow of solid particles36. In the present embodiment, the flow path60includes a second set of first struts or splitter vanes62and a second set of second struts or swirler vanes64. The second set of first struts or splitter vanes62supports the first set of struts or splitter vanes50, and may be configured to alter the flow of carrier gas through the port60.

The second set of swirler vanes64may be configured to establish a recirculating and/or swirling flow of solid particles36by directing the flow of carrier gas from the injection port54. In alternative embodiments, the second set of second struts64may have substantially no impact on the flow of carrier gas. As previously discussed, the recirculating and/or swirling flow of solid particles36may enhance the homogeneity of particle distribution, thereby increasing gasifier efficiency. Similar to the first set of swirler vanes52, certain embodiments may provide adjustable swirler vanes64within the carrier gas flow path60. For example, an actuator may alter an angle of each swirler vane64relative to the flow of carrier gas to establish varying degrees of recirculation and/or swirl within the flow of solid particles36. For example, the swirler vanes64may be aligned with the flow of carrier gas if a smaller degree of recirculation and/or swirl is desired, or rotated to direct the flow of carrier gas in a direction that induces a larger degree of recirculation and/or swirl. In certain embodiments, the swirler vanes64may be configured to rotate a first angle51about an axis53substantially parallel to the flow of carrier gas, a second angle55about a radial axis57of the vanes64and/or a third angle59about a circumferential axis61of the vanes64. In alternative embodiments, the angle of each swirler vane64may be fixed.

In the present embodiment, the flow path60includes a converging section66shaped to decrease the cross-sectional area of the flow path60along the downstream direction38. As will be appreciated, the decrease in cross-sectional area will increase the velocity of carrier gas passing through the injection port54, thereby providing enhanced mixing between the carrier gas and the flow of solid particles36. As illustrated, a shroud68defines the profile of the converging section66. Specifically, the shroud68is positioned such that the flow of solid particles36passes along an inner surface of the shroud68, the flow of carrier gas passes along an outer surface of the shroud68, and the carrier gas injection port54is formed at a downstream axial end69of the shroud68. In certain embodiments, the axial end69of the shroud68is shaped to establish a swirling flow of carrier gas from the injection port54. In further embodiments, the shape of the shroud68is adjustable such that the carrier gas may be directed from the injection port54to establish a desired flow pattern. In addition, the shroud68may be a continuous annular structure, or a series of discrete elements circumferentially disposed about the flow passage34.

The illustrated embodiment also includes an inlet70configured to receive a flow of trim gas, as indicated by the arrow72. In certain embodiments, the trim gas may be the same type of gas (e.g., nitrogen, carbon dioxide, steam, etc.) as the carrier gas. Alternatively, the trim gas and carrier gas may be different types of gases. As illustrated, the trim gas is directed toward a trim gas injection port74positioned downstream from the carrier gas injection port54. The trim gas injection port74is configured to provide a flow of trim gas in an upstream direction76, as indicated by the arrows78, to enhance mixing between the flow of carrier gas and the flow of solid particles36. In the present embodiment, the trim gas injection port74is positioned adjacent to a downstream end or trailing edge49of the body44, and is configured to provide the flow of trim gas along a surface of the body44. By positioning the injection port74adjacent to the body44, the flow of trim gas may substantially reduce or eliminate buildup of solid particles36along the surface of the body44, thereby decreasing solid particle residence time and enhancing homogeneity of the flow of solid particles36. As discussed in detail below, the flow rate of trim gas through the injection port74may be adjustable to vary the interaction between the trim gas and the flow of solid particles36. In certain embodiments, the flow rate of trim gas from the injection port74may be particularly adjusted to establish a swirling and/or a recirculating flow of solid particles36within the fluidization device18. In addition, the trim gas injection port74may be a continuous annular structure, or a series of discrete elements circumferentially disposed about the body44.

As illustrated, the flow of solid particles36is directed toward a transfer line80that conveys the particles to the gasifier20, as indicated by the arrow82. In certain embodiments, the fluidization device18may be arranged vertically with the transfer line80on top. Such a configuration may facilitate increased mixing between the carrier gas and the flow of solid particles36, and may enhance the homogeneity of solid particle distribution. However, it should be appreciated that the fluidization device18may be arranged horizontally, or vertically with the transfer line80at the bottom, in alternative embodiments. Because the fluidization device18is configured to break up agglomerations and to provide a substantially uniform flow of solid particles38to the gasifier20, solid particles may be continuously transferred from the pressurization device16to the gasifier20, as compared to the periodic transfers associated with lock hopper operation.

FIG. 3is a schematic diagram of the fluidization device18shown inFIG. 2, illustrating a recirculating flow pattern. As previously discussed, the velocity of the trim gas expelled from the injection port74may be varied to achieve a desired flow pattern within the fluidization device18. In certain embodiments, trim gas velocity may be particularly selected to establish a recirculating flow84. Specifically, if the trim gas velocity along the direction78is approximately equal to the carrier gas velocity along the direction86, the illustrated recirculating flow pattern84may be established. As illustrated, the recirculating flow84induces the solid particles36to move is a substantially circular formation along the axial direction88and the radial direction90, thereby enhancing the homogeneity of the particle distribution. In addition, the recirculating flow84may decrease particle residence time by reducing particle buildup along the outer surface63and/or the surface of the body44, thereby increasing the continuity of the solid particle flow.

In alternative embodiments, the trim gas velocity may be significantly lower than the velocity of the carrier gas flowing in the direction86. In such embodiments, a localized recirculation zone or turbulent area may be established adjacent to the body44, while the remaining carrier gas flows directly toward the transfer line80. Such a configuration may increase the flow rate of solid particles36through the fluidization device18. However, the localized recirculation zone or turbulent area may provide less mixing between the gases and the solid particles36, thereby providing decreased uniformity of the solid particles within the flow.

As will be appreciated, the carrier gas velocity and the shape of the shroud68may also affect the flow pattern within the fluidization device18. In certain embodiments, the velocity of carrier gas expelled from the injection port54is adjustable. In such embodiments, a higher carrier gas velocity may provide a higher flow rate and decreased particle mixing, while a lower carrier gas velocity may provide a lower flow rate and increased particle mixing. Consequently, the carrier gas flow velocity may be particularly adjusted to achieve a desired particle distribution and flow rate into the gasifier20. Further embodiments include a movable and/or rotatable shroud68configured to alter the flow of carrier gas and/or the flow of solid particles36within the fluidization device18. For example, the shroud68may be shaped to direct the carrier gas in the direction86and to direct the trim gas in the direction78to establish the illustrated recirculating flow. In certain embodiments, the shroud68may be shaped to establish the recirculating flow of carrier gas without the use of trim gas. In such embodiments, the trim gas injection ports74may be omitted.

FIG. 4is a schematic diagram of the fluidization device18shown inFIG. 2, illustrating a swirling flow pattern. As previously discussed, an angle of the second set of swirler vanes64may be varied to achieve a desired flow pattern within the fluidization device18. In certain embodiments, the swirler vanes64may be particularly angled to establish a swirling flow92. Specifically, if the swirler vanes64are shaped to direct the carrier gas in the circumferential direction94, the illustrated swirling flow pattern92may be established. As illustrated, the swirling flow92induces the solid particles36to move in a substantially spiral formation along the circumferential direction94, the axial direction88and the radial direction90, thereby enhancing the homogeneity of the particle distribution. In addition, the swirling flow92decreases particle residence time by reducing particle buildup along the outer surface63and/or the surface of the body44, thereby increasing the continuity of the solid particle flow. In the illustrated embodiment, the swirling flow92within the fluidization device18induces a corresponding swirling flow96within the transfer line80, thereby further increasing the homogeneity of the solid particles36.

In addition, the shape of the body44, the shape of the first set of swirler vanes52and the shape of the shroud68may affect the swirling flow pattern within the fluidization device18. In certain embodiments, the shape of the body44is adjustable. In such embodiments, the shape of the body44may be varied to establish the illustrated swirling flow92. For example, a diameter98of the body44may be decreased to facilitate establishment of the swirling flow pattern92. In addition, the body44may be movable along the longitudinal axis45in both the downstream direction38and the upstream direction76. Positioning the body44adjacent to the transfer line80may restrict the flow of solid particles36through the fluidization device18. Such a flow restriction may provide back-pressure to the pressurization device16during start-up and shut-down conditions, for example. Consequently, the body44may be moved along the longitudinal axis45to achieve a desired back-pressure to the pressurization device16based on flow rate to the gasifier20.

Further embodiments may include a movable and/or rotatable shroud68configured to alter the flow of carrier gas and/or the flow of solid particles36within the fluidization device18. For example, the shroud68may be movable and/or rotatable to direct the carrier gas and the flow of solid particles36in the circumferential direction94to establish the illustrated swirling flow92. Other embodiments may include an adjustable set of first swirler vanes52. In such embodiments, the angle of the swirler vanes52may be adjusted to establish the illustrated swirling flow92. In alternative embodiments, the second set of swirler vanes64may establish the swirling flow92alone, thereby obviating the first set of swirler vanes52and/or the shroud68.

In certain embodiments, the trim gas velocity, the carrier gas velocity, the shape of the body44, the shape of the shroud68, the angle of the first set of swirler vanes52and the angle of the second set of swirler vanes64may be particularly configured to establish both the recirculating flow84shown inFIG. 2and the illustrated swirling flow92. Such a configuration may further decrease residence time and enhance mixing of gases and solid particles36. By adjusting the trim gas velocity, the carrier gas velocity, the shape of the body44, the shape of the shroud68, the angle of the first set of swirler vanes52and the angle of the second set of swirler vanes64, the flow pattern within the fluidization device18may be particularly selected to achieve a desired degree of particle homogeneity and/or a desired flow rate through the fluidization device18.

FIG. 5is a schematic diagram of an alternative embodiment of the fluidization device18including downstream carrier gas injection ports. As illustrated, the buffer gas injection ports100are positioned further downstream compared to the ports42shown inFIG. 2. Specifically, the buffer gas injection ports100are located downstream from the leading edge47of the body44, and configured to inject buffer gas in the downstream direction38, as indicated by the arrows102. As previously discussed, the body44is configured to break up agglomerations within the flow of solid particles36. Consequently, by positioning the buffer gas injection ports100downstream from the leading edge47of the body44, fewer agglomerations may contact the buffer gas injection ports100, thereby reducing the possibility of particle accumulation within the ports100.

Similar to the buffer gas injection ports100, the carrier gas injection ports104are positioned further downstream compared to the ports54shown inFIG. 2. Specifically, the carrier gas injection ports104are located at the approximate axial position of the trim gas injection ports74, and configured to inject carrier gas in the downstream direction38, as indicated by the arrows106. Because the body44and the flow of trim gas are configured to break up agglomerations and enhance homogeneity of particle distribution within the flow of solid particles36, positioning the carrier gas injection ports104further downstream facilitates establishment of an even particle distribution prior to injection of carrier gas. In addition, certain carrier gases may be corrosive to elements within the pressurization device16. Because the carrier gas is injected further downstream within the fluidization device18, the possibility of carrier gas flowing into the pressurization device16is reduced, thereby substantially reducing or eliminating potential corrosive effects of the carrier gas.

While the illustrated embodiment omits the first and second sets of splitter vanes50and62, it should be appreciated that alternative embodiments may include the first set of splitter vanes50and/or the second set of splitter vanes62. Furthermore, while the illustrated embodiment omits the first and second sets of swirler vanes52and64, it should be appreciated that alternative embodiments may include the first set of swirler vanes52and/or the second set of swirler vanes64. In addition, while the illustrated embodiment includes the trim gas injection ports74, it should be appreciated that alternative embodiments may omit the ports74.

FIG. 6is a schematic diagram of a further embodiment of the fluidization device18including a carrier gas passage positioned downstream from the body44. Similar to the embodiment described above with reference toFIG. 5, the buffer gas injection ports108are positioned downstream from the leading edge47of the body44, and configured to inject buffer gas in a downstream direction38, as indicated by the arrows110. However, the illustrated fluidization device18does not include carrier gas injection ports. Instead, the carrier gas is injected into a carrier gas passage112positioned downstream from the fluidization device18. In this configuration, the agglomerations will be substantially broken up by the body44, the trim gas and/or the buffer gas prior to the flow of solid particles36entering the carrier gas passage112. Because the carrier gas is injected downstream of the fluidization device18, the possibility of carrier gas flowing into the pressurization device16is reduced, thereby substantially reducing or eliminating potential corrosive effects of the carrier gas on elements of the pressurization device16. Once the flow of solid particles36enters the carrier gas passage112, the carrier gas will transport the solid particles36to the gasifier20. In alternative embodiments, the fluidization device18may include additional carrier gas injection ports, similar to those described above with reference toFIG. 2orFIG. 5, in addition to the carrier gas passage112. Such embodiments may enhance the break up of agglomerations within the flow of solid particles36prior to the solid particles36entering the carrier gas passage112.

While the illustrated embodiment omits the first and second sets of splitter vanes50and62, it should be appreciated that alternative embodiments may include the first set of splitter vanes50and/or the second set of splitter vanes62. Furthermore, while the illustrated embodiment omits the first and second sets of swirler vanes52and64, it should be appreciated that alternative embodiments may include the first set of swirler vanes52and/or the second set of swirler vanes64. In addition, while the illustrated embodiment includes the trim gas injection ports74, it should be appreciated that alternative embodiments may omit the ports74.

FIG. 7is a front view of an embodiment of splitter vanes50that may be employed within the fluidization device ofFIG. 2. As previously discussed, the fluidization device18may include a first set of splitter vanes50within the flow passage34and a second set of splitter vanes62within the carrier gas flow path60. The splitter vanes50and62serve to support the body44and enhance fragmentation within the flow of solid particles36. While the first set of splitter vanes50is shown inFIG. 7, it should be appreciated that the vanes may extend radially outward to form the second set of splitter vanes62.

The illustrated splitter vane configuration includes a central vertical vane114extending outward along a vertical radial direction115, and a central horizontal vane116extending outward along a horizontal radial direction117. As will be appreciated, the central vertical and horizontal vanes114and116may be connected to the body44, thereby supporting the body44during operation of the fluidization device18. The illustrated configuration also includes two secondary vertical vanes118positioned radially outward from the central vertical vane114, and two secondary horizontal vanes120positioned radially outward from the central horizontal vane116. Alternative embodiments may employ more or fewer secondary vanes118and/or120. For example, certain embodiments, may employ 1, 2, 3, 4, 5, 6, 7, 8, or more secondary vertical vanes118and/or secondary horizontal vanes116. As previously discussed, the angle51,55and59of each vane114,116,118and/or120may be adjustable relative to the flow of solid particles36to vary the degree of particle fragmentation.

FIG. 8is a front view of an alternative embodiment of splitter vanes50that may be employed within the fluidization device ofFIG. 2. The illustrated vane configuration includes the central vertical vane114, as described above with reference toFIG. 7, and a series of concentric circular vanes122space along the radial directions115and117. While three circular vanes122are employed within the illustrated embodiment, it should be appreciated that more or fewer circular vanes122may be utilized within alternative embodiments. For example, certain embodiments may include 1, 2, 3, 4, 5, 6, 7, 8, or more circular vanes122. In addition, further embodiments may include a combination of circular vanes122and secondary vertical and/or secondary horizontal vanes118and/or120. Further embodiments may also include a central horizontal vane116. Similar to the vane configuration described above with reference toFIG. 7, the angle51,55and59of the circular vanes122may be adjusted relative to the flow of solid particles36. Furthermore, the circular vanes122may extend radially outward to form elements of the second set of splitter vanes62.