CN106675658B - High-flux circulating fluidized bed low-order coal gasification device and method - Google Patents
High-flux circulating fluidized bed low-order coal gasification device and method Download PDFInfo
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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- C10J2300/0909—Drying
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1628—Ash post-treatment
Abstract
The invention discloses a high-flux circulating fluidized bed low-order coal gasification device and a method, belonging to the field of clean utilization of coal. The coal gasification reaction device consists of a jet flow reinforced bottom ash separation zone, a low-rank coal strong mixing pyrolysis, gasification and combustion zone, a residual carbon lifting pipe deep gasification zone, a two-stage cyclone separator and a material returning mechanism. The coal gasification method is characterized in that a high gas velocity and a secondary material returning mechanism are directly connected with a lifting pipe gasification area, so that the deep gasification of carbon residue in fine ash under the condition of high flux is realized, and a high-speed jet pipe and separation column coupling structure is adopted to realize the high-efficiency separation of bottom ash. The invention has the advantages of high carbon conversion rate, high gasification strength, high device utilization rate and easy ash discharge, and is particularly suitable for upgrading low-rank coal such as lignite.
Description
Technical Field
The invention belongs to the field of clean coal utilization equipment, and particularly relates to a high-flux circulating fluidized bed low-rank coal gasification device and a method.
Background
The natural resource of rich coal, lean oil and less gas determines that coal is still an important basic energy source in China in the foreseeable future, wherein the gasification technology is one of important ways for clean and efficient utilization of coal. According to the report, the low-rank coal mainly comprising brown coal and long-flame coal in China accounts for about 45% of the recoverable reserves of the residual coal, but the characteristics of high two-high three-low (high volatile matter, high water content, low ash melting point, low density and low heat value) of the low-rank coal such as brown coal and the like cause serious environmental pollution and are difficult to be utilized on a large scale, so that the development of the gasification technology of the low-rank coal is an important support and guarantee for realizing clean conversion and utilization of energy.
The coal gasification technologies that are commercialized today can be classified into three types, a fixed bed, an entrained flow bed, and a fluidized bed. The fixed bed gasification uses weak caking coal as a raw material, the methane content in the coal gas is high, the cold coal gas efficiency is high, and the fixed bed gasification is particularly suitable for coal-based natural gas, but a tar wastewater purification system is relatively complex; the entrained flow bed is operated at high temperature, the gasification intensity and the quality of the synthesis gas are higher, but the low-ash coal powder is generally used as the raw material, and the oxygen consumption and the equipment investment are higher; the fluidized bed gasification uses small-particle coal as a raw material, has relatively large gas-solid contact area, moderate reaction temperature, low oxygen consumption and low investment, and is particularly suitable for low-rank coal such as lignite, long-flame coal and the like with high reaction activity. Therefore, the development of fluidized bed gasification technology suitable for low rank coals is undoubtedly a very important task.
The existing fluidized bed gasification technology inevitably encounters the following difficulties when gasifying low-rank coals such as brown coal, long flame coal and the like: 1. the carbon conversion rate is low (about 90%); 2. the gasification strength is low; 3. the bottom ash is difficult to discharge.
Disclosure of Invention
The invention aims to provide a high-flux circulating fluidized bed low-rank coal gasification device and a method, which are characterized in that,
the high-flux circulating fluidized bed low-order coal gasification device mainly comprises a jet flow reinforced bottom ash separation zone A, a low-order coal strong mixing pyrolysis, gasification and combustion zone B, a carbon residue riser pipe deep gasification zone C, a two-stage cyclone separator and a material returning mechanism.
The jet flow reinforced bottom ash separation area A is composed of a V-shaped gas distribution plate 1, a V-shaped distribution plate gas chamber 2, a distribution plate gas inlet pipe 3, a central jet pipe 4, a fluidization separation column 5, a slag discharge port 6 and a separation column gas inlet 7; the V-shaped gas distribution plate 1 is positioned at the upper part of the V-shaped distribution plate gas chamber 2 and is funnel-shaped, gas outlets are distributed on the V-shaped distribution plate 1, and the lower part of the V-shaped distribution plate is connected with the fluidization separation column 5; a distribution plate air inlet pipe 3 is arranged in the V-shaped distribution plate air chamber 2; the central jet pipe 4 is positioned on the central axis of the fluidization separation column 5; the lower part of the fluidization separation column 5 is connected with a slag discharge port 6, and the bottom of the fluidization separation column is provided with a separation column air inlet 7;
the low-rank coal strong mixing pyrolysis, gasification and combustion zone B and the residual carbon riser deep gasification zone C are main parts of a fluidized bed gasification furnace, the low-rank coal strong mixing pyrolysis, gasification and combustion zone B is positioned between the jet flow reinforced bottom ash separation zone A and the residual carbon riser deep gasification zone C, a primary circulating ash returning unit 8, a coal-as-fired feeding pipe 9, a gasifying agent air inlet pipe 10 and a secondary circulating ash returning unit 11 are sequentially arranged in the low-rank coal strong mixing pyrolysis, gasification and combustion zone B and the residual carbon riser deep gasification zone C from bottom to top, wherein the coal-as-fired feeding pipe 9 is positioned in the middle of the low-rank coal strong mixing pyrolysis, gasification and combustion zone B, and the gasifying agent air inlet pipe 10 is positioned at the upper part of the low-rank coal strong mixing pyrolysis, gasification and combustion zone B; the secondary circulating ash returning unit 11 is connected to the lower part of the deep gasification zone C of the carbon residue lifting pipe.
The two-stage cyclone separator and the material returning mechanism are circulating ash conveying units, the primary cyclone separator 13 is connected with a top end outlet 12 of the gasification furnace through a pipeline, the lower end of the primary cyclone separator is sequentially connected with a primary circulating vertical pipe 14, a U-shaped valve 15 and a primary circulating ash material returning unit 8, and then the primary cyclone separator returns to a low-rank coal strong-mixing pyrolysis, gasification and combustion area B; an exhaust port of the primary cyclone separator 13 is connected with a secondary cyclone separator 16 through a pipeline, the top end of the secondary cyclone separator 16 is a synthesis gas outlet 17, and the lower end of the secondary cyclone separator 16 is connected with a secondary circulation vertical pipe 18 and a secondary circulation ash returning unit 11 and finally returns to the lower part of the deep gasification zone C of the carbon residue riser pipe.
The ratio of the cross sections of the deep gasification area C of the carbon residue riser and the low-rank coal in the strong mixing pyrolysis, gasification and combustion area B is 0.5: 1-0.75: 1.
And a loosening air inlet pipe 19 and a conveying air inlet pipe 20 are arranged in the secondary circulating ash returning unit 11, so that the air locking and feeding functions of the unit are realized. A low-rank coal gasification method of a high-flux circulating fluidized bed low-rank coal gasification device is characterized in that a high-speed jet gas and a secondary material returning mechanism are directly connected with a deep gasification zone C of a carbon residue riser, so that the deep gasification of carbon residue in fine ash under the high-flux condition is realized; introducing high-speed jet gas into the lower part of the gasification furnace to promote the bottom ash to be melted into balls, and then efficiently separating the balls through a separation column; the method comprises the following steps:
continuously adding coal as fired with the moisture content of less than 10 wt% and the granularity of less than 15mm into a gasification furnace through a feeding pipe 9, simultaneously continuously introducing air into a distribution plate air inlet pipe 3, a central jet pipe 4 and a separation column air inlet 7 of a jet flow reinforced bottom ash separation area A at the bottom of the gasification furnace, firstly cracking or pyrolyzing low-rank coal, then partially gasifying or burning to generate high-temperature semi-coke with smaller particle size, and entering a riser gasification area C under an air flow zone to react with a gasifying agent consisting of oxygen and water vapor; solid particles brought out from the top of the gasification furnace are successively returned to the gasification furnace through a two-stage cyclone separator and a material returning mechanism, wherein particles with larger particle sizes are sent into a strong mixing pyrolysis, gasification and combustion area B through a primary circulating ash material returning unit 8 after gas-solid separation is realized in a primary cyclone separator 13, and are further gasified and combusted; particles with smaller particle size enter a riser pipe gasification area C through a secondary cyclone separator 16 and a secondary circulating ash returning unit 11, so that the effective deep gasification of carbon residues in small particles is realized, and the overall gasification efficiency of low-rank coal is improved; a synthesis gas outlet 17 at the top of the secondary cyclone 16 results in a high quality synthesis gas with a very low dust concentration.
In the jet flow reinforced bottom ash separation area A, a high-speed jet pipe and a separation column coupling structure are adopted to realize the high-efficiency separation of bottom ash; air and oxygen are introduced from the central jet pipe 4, and a high-temperature combustion area is formed near the jet nozzle to promote the ash to agglomerate into balls; introducing air into the V-shaped gas distribution plate 1 to maintain the bed layer in a fluidized state, separating ash lumps from bed materials such as semicoke and the like by the air introduced from the air inlet 7 of the separation column at a proper air speed, and discharging the ash lumps out of the gasification furnace; the slag discharge amount can be controlled by adjusting the gas velocity of the separation column and the outlet height of the central jet pipe.
The invention has the beneficial effects that: compared with the prior art, the method has the following advantages:
(1) the incompletely gasified coal and semicoke circulate in the gasification furnace for multiple times, so that the retention time is prolonged, and the carbon conversion rate is effectively improved;
(2) the circulating fluidized bed gasification furnace is operated under the condition of high flux, so that the processing capacity and gasification intensity of the device are obviously improved;
(3) the coupling structure of the high-speed jet pipe and the separation column is adopted, the problem of bottom ash discharge is solved, and the method is particularly suitable for low-rank coal with high ash content.
Drawings
FIG. 1 is a schematic diagram of a high-throughput circulating fluidized bed low-rank coal gasification apparatus according to the present invention.
As shown in the figure, 1-V type gas distribution plate, 2-V type gas chamber of distribution plate, 3-air inlet pipe of distribution plate, 4-central jet pipe, 5-fluidization separation column, 6-slag outlet, 7-air inlet of separation column, 8-first stage circulation ash return unit, 9-coal as fired inlet pipe, 10-gasification agent inlet pipe, 11-second stage circulation ash return unit, 12-gasification furnace outlet, 13-first stage cyclone separator, 14-first stage circulation vertical pipe, 15-U type valve, 16-second stage cyclone separator, 17-synthesis gas outlet, 18-second stage circulation vertical pipe, 19-loosening air inlet pipe, 20-conveying air inlet pipe; a-jet flow strengthening bottom ash separation zone, B-low-rank coal strong mixing pyrolysis/gasification/combustion zone and C-carbon residue riser pipe deep gasification zone.
Detailed Description
The invention provides a high-flux circulating fluidized bed low-order coal gasification device and a method thereof, which are further described with reference to the attached drawings.
FIG. 1 shows a high-throughput circulating fluidized bed low-rank coal gasification plant. The device mainly comprises a jet flow reinforced bottom ash separation zone A, a low-rank coal strong mixing pyrolysis, gasification and combustion zone B, a carbon residue riser deep gasification zone C, a two-stage cyclone separator and a material returning mechanism.
The jet flow reinforced bottom ash separation area A is composed of a V-shaped gas distribution plate 1, a V-shaped distribution plate gas chamber 2, a distribution plate gas inlet pipe 3, a central jet pipe 4, a fluidization separation column 5, a slag discharge port 6 and a separation column gas inlet 7. The V-shaped gas distribution plate 1 is positioned at the upper part of the V-shaped distribution plate gas chamber 2 and is funnel-shaped, gas outlets are distributed on the V-shaped distribution plate 1, and the lower part of the V-shaped distribution plate is connected with the fluidization separation column 5; a distribution plate air inlet pipe 3 is arranged in the V-shaped distribution plate air chamber 2; the central jet pipe 4 is positioned on the central axis of the fluidization separation column 5, and the outlet of the central jet pipe 4 is as high as the bottom of the V-shaped gas distribution plate 1.
The lower part of the fluidization separation column 5 is connected with a slag discharge port 6, and the bottom of the fluidization separation column is provided with a separation column air inlet 7. The low-rank coal strong-mixing pyrolysis, gasification and combustion area B and the residual carbon riser pipe deep gasification area C are main parts of the fluidized bed gasification furnace, the low-rank coal strong-mixing pyrolysis, gasification and combustion area B is positioned between the jet flow reinforced bottom ash separation area A and the residual carbon riser pipe deep gasification area C, and the ratio of the sectional area of the residual carbon riser pipe deep gasification area C to the sectional area of the low-rank coal strong-mixing pyrolysis, gasification and combustion area B is 0.5: 1. A primary circulating ash returning unit 8, a coal as fired feeding pipe 9, a gasifying agent inlet pipe 10 and a secondary circulating ash returning unit 11 are sequentially arranged in a low-rank coal strong mixing pyrolysis, gasification and combustion zone B and a residual carbon riser deep gasification zone C from bottom to top, wherein the coal as fired feeding pipe 9 is positioned in the middle of the low-rank coal strong mixing pyrolysis, gasification and combustion zone B, and the gasifying agent inlet pipe 10 is positioned at the upper part of the low-rank coal strong mixing pyrolysis, gasification and combustion zone B; the secondary circulating ash returning unit 11 is connected with the lower part of the deep gasification zone C of the carbon residue lift pipe. The two-stage cyclone separator and the material returning mechanism are circulating ash conveying units, the one-stage cyclone separator 13 is connected with a gasification furnace top end outlet 12 through a pipeline, the lower end of the one-stage cyclone separator is sequentially connected with a one-stage circulating vertical pipe 14, a U-shaped valve 15 and a one-stage circulating ash material returning unit 8, and then the low-stage coal is returned to a low-rank coal strong-mixing pyrolysis, gasification and combustion area B of the gasification furnace; an exhaust port of the primary cyclone separator 13 is connected with a secondary cyclone separator 16 through a pipeline, the top end of the secondary cyclone separator 16 is a synthesis gas outlet 17, and the lower end of the secondary cyclone separator 16 is connected with a secondary circulation vertical pipe 18 and a secondary circulation ash returning unit 11 and finally returns to the lower part of the deep gasification zone C of the carbon residue riser pipe. A loosening air inlet pipe 19 and a conveying air inlet pipe 20 are arranged in the secondary circulating ash returning unit 11, so that the air locking and feeding functions of the unit are realized.
Example 1
In the embodiment, the ratio of the cross sections of the deep gasification area C of the carbon residue riser and the low-rank coal in the strong mixing pyrolysis, gasification and combustion area B is 0.5:1, and the outlet of the central jet pipe 4 is as high as the bottom of the V-shaped gas distribution plate 1.
Feeding Mongolian lignite into a pulverizing system, crushing by a coal mill and drying by a dryer to ensure that the granularity of the Mongolian lignite is less than 15mm and the moisture content of the Mongolian lignite is less than 10 wt%; the coal as fired is subjected to strong mixing pyrolysis and gasification of low-rank coalThe coal as fired feeding pipe 9 in the middle of the combustion zone B is continuously fed, meanwhile, air is continuously fed into a distribution plate air inlet pipe 3 at the bottom of the gasification furnace, a central jet pipe 4 and a separation column air inlet 7, low-rank coal is firstly cracked or pyrolyzed, then part of the low-rank coal is gasified or combusted, and generated high-temperature semicoke with small particle size enters a lifting pipe gasification zone C under the condition of air flow pinch; a gasifying agent consisting of oxygen and water vapor is injected from a gasifying agent inlet pipe 10 and flows upwards in parallel with the high-temperature semicoke particles in the lifting pipe to generate a gasification reaction; and maintaining the temperature of the gasification zone C of the riser at 850-1000 ℃. The gas-solid reaction in the low-rank coal strong mixing pyrolysis, gasification and combustion zone B mainly comprises the following steps: coal pyrolysis reaction: coal → C + H2+CH4+H2O+CO2+ CO, etc. The independent reactions in the coal gasification process of the carbon residue lifting pipe deep gasification zone C are as follows: c + O2→CO，C+O2→CO2，C+CO2→CO，C+H2O→CO+H2，C+H2→CH4，CO+H2O→H2+CO2. The proper operating gas velocity is maintained for the gasifying agent 10 and the gas inlets at the bottom of the gasifier, so that higher solid flux is obtained in the riser.
The synthesis gas generated by gasification enters a primary cyclone separator 13 through a gasification furnace outlet 12, the primary cyclone separator 13 captures solid particles such as ash, coke and the like carried by the synthesis gas, most of the solid particles fall into a U-shaped valve 15 through a primary circulation vertical pipe 14, and the solid particles are sent to the lower part of a low-rank coal strong-mixing pyrolysis, gasification and combustion area B through a primary circulation ash return unit 8; wherein a small part of fine particles enter a secondary cyclone separator 16 through an exhaust port of a primary cyclone separator 13, and after being captured by the secondary cyclone separator 16, the fine particles fall into a secondary circulation vertical pipe 18 and are sent to the lower part of a riser gasification zone C through a secondary circulation ash returning unit 11 with the gas locking and feeding functions; the solid particles sent back to the gasification furnace participate in the reaction and circulation again, and finally, high-quality synthesis gas with extremely low dust concentration is obtained at a synthesis gas outlet 17 at the top end of the secondary cyclone separator 16.
In the jet flow reinforced bottom ash separation area A, air and oxygen are introduced from a central jet flow pipe 4, and a high-temperature combustion area at 1100-1300 ℃ is formed near a jet flow nozzle to promote ash residues to agglomerate into balls; air is introduced into the V-shaped gas distribution plate 1 to maintain the bed layer in a fluidized state, and then the air introduced from the air inlet 7 of the separation column separates the ash balls from bed materials such as semicoke and the like at a proper air speed, and then the ash balls are discharged out of the gasification furnace. The slag discharge amount can be controlled by adjusting the gas velocity of the separation column and the outlet height of the central jet pipe.
Example 2:
the ratio of the cross sections of the gasification zone C of the riser and the strong mixing pyrolysis, gasification and combustion zone B is 0.75: 1; the outlet of the central jet pipe 4 is slightly higher than the bottom of the V-shaped gas distribution plate 1. The rest of the apparatus was the same as in example 1.
In the example, the Fuxin flame coal is sent into a powder preparation system, and after being crushed by a coal mill and dried by a dryer, the particle size of the Fuxin flame coal is less than 15mm, and the moisture content of the Fuxin flame coal is less than 10 wt%; coal as fired is continuously added through a coal as fired feeding pipe 9 in the middle of the low-rank coal strong-mixing pyrolysis/gasification/combustion area B, air is continuously introduced into a distribution plate air inlet pipe 3, a central jet pipe 4 and a separation column air inlet 7 at the bottom of the gasification furnace, the low-rank coal is firstly cracked or pyrolyzed, then part of the low-rank coal is gasified or combusted, and generated high-temperature semicoke with smaller particle size enters a riser gasification area C under the condition of air flow pinch; a gasifying agent consisting of oxygen and steam is injected from a gasifying agent inlet pipe 10 and flows upwards in parallel with the high-temperature semicoke particles in the lifting pipe to generate a gasification reaction; and maintaining the temperature of the gasification zone C of the riser at 900-1050 ℃. The gas-solid reaction in the low-rank coal strong mixing pyrolysis/gasification/combustion area B mainly comprises the following steps: coal pyrolysis reaction: coal → C + H2+CH4+H2O+CO2+ CO, etc. The independent reactions in the coal gasification process of the carbon residue lifting pipe deep gasification zone C are as follows: c + O2→CO，C+O2→CO2，C+CO2→CO，C+H2O→CO+H2，C+H2→CH4，CO+H2O→H2+CO2. The proper operating gas velocity is maintained for the gasifying agent 10 and the gas inlets at the bottom of the gasifier, so that higher solid flux is obtained in the riser.
The synthesis gas generated by gasification enters a primary cyclone separator 13 through a gasification furnace outlet 12, the primary cyclone separator 13 captures solid particles such as ash/coke and the like carried by the synthesis gas, most of the solid particles fall into a U-shaped valve 15 through a primary circulation vertical pipe 14, and the solid particles are sent to the lower part of a low-rank coal strong-mixing pyrolysis, gasification and combustion area B through a primary circulation ash return unit 8; wherein a small part of fine particles enter a secondary cyclone separator 16 through an exhaust port of a primary cyclone separator 13, and after being captured by the secondary cyclone separator 16, the fine particles fall into a secondary circulation vertical pipe 18 and are sent to the lower part of a riser gasification zone C through a secondary circulation ash returning unit 11 with the gas locking and feeding functions; the solid particles sent back to the gasifier take part in the reaction and circulation again. Finally, high-quality synthesis gas with extremely low dust concentration is obtained at a synthesis gas outlet 17 at the top end of the secondary cyclone separator 16.
In the jet flow reinforced bottom ash separation area A, air/oxygen is introduced from a central jet flow pipe 4, and a high-temperature combustion area at 1100-1300 ℃ is formed near a jet flow nozzle to promote ash residues to agglomerate into balls; air is introduced into the V-shaped gas distribution plate 1 to maintain the bed layer in a fluidized state, and then the air introduced from the air inlet 7 of the separation column separates the ash balls from bed materials such as semicoke and the like at a proper air speed, and then the ash balls are discharged out of the gasification furnace. The slag discharge amount can be controlled by adjusting the gas velocity of the separation column and the outlet height of the central jet pipe.
Claims (1)
1. A low-order coal gasification device of a high-flux circulating fluidized bed mainly comprises a jet flow reinforced bottom ash separation zone (A), a low-order coal strong mixing pyrolysis, gasification and combustion zone (B), a residual carbon riser pipe deep gasification zone (C), two-stage cyclone separators and a material returning mechanism;
the jet flow reinforced bottom ash separation zone (A) is composed of a V-shaped gas distribution plate (1), a V-shaped distribution plate gas chamber (2), a distribution plate gas inlet pipe (3), a central jet pipe (4), a fluidization separation column (5), a slag discharge port (6) and a separation column gas inlet (7); the V-shaped gas distribution plate (1) is positioned at the upper part of the V-shaped distribution plate gas chamber (2) and is funnel-shaped, gas outlets are distributed on the V-shaped distribution plate (1), and the lower part of the V-shaped distribution plate is connected with the fluidization separation column (5); a distribution plate air inlet pipe (3) is arranged in the V-shaped distribution plate air chamber (2); the central jet pipe (4) is positioned on the central axis of the fluidization separation column (5); of fluidised separation columns (5)The lower part is connected with a slag discharge port (6), and the bottom of the slag discharge port is provided with a separation column air inlet (7); the low-rank coal strong mixing pyrolysis, gasification and combustion area (B) and the carbon residue lifting pipe deep gasification area (C) are the main parts of the fluidized bed gasification furnace, the low-rank coal strong mixing pyrolysis, gasification and combustion area (B) is positioned between the jet flow reinforced bottom ash separation area (A) and the carbon residue lifting pipe deep gasification area (C),it is characterized in that the preparation method is characterized in that,the system is characterized in that a first-stage circulating ash returning unit (8), a coal-as-fired feeding pipe (9), a gasifying agent inlet pipe (10) and a second-stage circulating ash returning unit (11) are sequentially arranged in a low-rank coal strong-mixing pyrolysis, gasification and combustion area (B) and a residual carbon riser deep gasification area (C) from bottom to top, wherein the coal-as-fired feeding pipe (9) is positioned in the middle of the low-rank coal strong-mixing pyrolysis, gasification and combustion area (B), and the gasifying agent inlet pipe (10) is positioned at the upper part of the low-rank coal strong-mixing pyrolysis, gasification and combustion area (B); the secondary circulating ash returning unit (11) is connected to the lower part of the deep gasification zone (C) of the carbon residue lifting pipe; the secondary circulating ash returning unit (11) is internally provided with a loosening air inlet pipe (19) and a conveying air inlet pipe (20) to realize the air locking and feeding functions of the unit;
the two-stage cyclone separator and the material returning mechanism are circulating ash conveying units, the primary cyclone separator (13) is connected with a top end outlet (12) of the gasification furnace through a pipeline, and the lower end of the primary cyclone separator is sequentially connected with a primary circulating vertical pipe (14), a U-shaped valve (15) and a primary circulating ash material returning unit (8) and then returns to a low-rank coal strong-mixing pyrolysis, gasification and combustion area (B); an exhaust port of the primary cyclone separator (13) is connected with a secondary cyclone separator (16) through a pipeline, the top end of the secondary cyclone separator (16) is a synthesis gas outlet (17), and the lower end of the secondary cyclone separator is connected with a secondary circulation vertical pipe (18) and a secondary circulation ash returning unit (11) and finally returns to the lower part of the deep gasification zone (C) of the carbon residue riser pipe;
the ratio of the cross sections of the deep gasification zone (C) of the carbon residue riser and the low-rank coal strong mixing pyrolysis, gasification and combustion zone (B) is 0.5: 1-0.75: 1.
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| CN107057771A (en) * | 2017-06-27 | 2017-08-18 | 哈尔滨工业大学 | A kind of Two-way Cycle Circulating Fluidized Bed Gasifier For Biomass |
| CN107418635B (en) * | 2017-07-27 | 2020-06-05 | 新奥科技发展有限公司 | Slag discharging system, fluidized bed gasification furnace and coal gasification slag discharging method |
| CN110205164B (en) * | 2019-06-11 | 2020-11-03 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device and circulating fluidized bed gasification method |
| CN110452740B (en) * | 2019-08-21 | 2021-04-23 | 青岛科技大学 | Rapid fluidization reaction system for strengthening mixing of bi-component solid particles |
| CN112824501B (en) * | 2019-11-21 | 2022-02-08 | 中国科学院工程热物理研究所 | Circulating fluidized bed partial gasification device and circulating fluidized bed partial gasification method |
| CN113088336A (en) * | 2021-04-14 | 2021-07-09 | 安徽科达洁能股份有限公司 | Graded gasification pure oxygen circulating fluidized bed gas generator and working method |
| CN114774169A (en) * | 2022-04-26 | 2022-07-22 | 中国科学院工程热物理研究所 | Gasification apparatus, gasification method, and thermochemical reaction apparatus |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101372635A (en) * | 2008-10-15 | 2009-02-25 | 东南大学 | High-density pressurized fluidized bed coal gasification apparatus and method |
| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
| CN202968502U (en) * | 2012-10-11 | 2013-06-05 | 田原宇 | Pulverized-coal grading and pyrolyzing gasifier with combined circulating fluidized bed |
| CN103740409A (en) * | 2014-01-23 | 2014-04-23 | 东南大学 | Multi-stage gas distribution high-temperature coal gasification device and method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060130401A1 (en) * | 2004-12-16 | 2006-06-22 | Foster Wheeler Energy Corporation | Method of co-producing activated carbon in a circulating fluidized bed gasification process |
-
2016
- 2016-12-15 CN CN201611160553.9A patent/CN106675658B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101372635A (en) * | 2008-10-15 | 2009-02-25 | 东南大学 | High-density pressurized fluidized bed coal gasification apparatus and method |
| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
| CN202968502U (en) * | 2012-10-11 | 2013-06-05 | 田原宇 | Pulverized-coal grading and pyrolyzing gasifier with combined circulating fluidized bed |
| CN103740409A (en) * | 2014-01-23 | 2014-04-23 | 东南大学 | Multi-stage gas distribution high-temperature coal gasification device and method |
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