CN111442261A - Combustion system of ascending bed coal pyrolysis co-production circulating fluidized bed boiler and working method thereof - Google Patents
Combustion system of ascending bed coal pyrolysis co-production circulating fluidized bed boiler and working method thereof Download PDFInfo
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- 239000002817 coal dust Substances 0.000 claims abstract description 17
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- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
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- F23C10/00—Fluidised bed combustion apparatus
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- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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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
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Abstract
The invention discloses a combustion system of an ascending bed coal pyrolysis co-production circulating fluidized bed boiler and a working method thereof. According to the invention, the pyrolysis product high-temperature semicoke in the ascending bed pyrolysis furnace is recycled and used as a heat carrier, the heat of the semicoke is recovered, the heat required by coal dust pyrolysis is supplied, and meanwhile, the pyrolysis product high-temperature semicoke is used as a raw material of the combustion furnace, so that the contamination, abrasion and corrosion of a heating surface of the boiler caused by the excessive alkali metal content in the boiler when high-alkali coal is directly combusted are reduced, and the safety and the heat exchange effect of the heating surface are ensured.
Description
Technical Field
The invention relates to the fields of coal chemical industry, energy and thermal power generation, in particular to a circulating fluidized bed boiler combustion system for combined production of upward bed coal pyrolysis and a working method thereof.
Background
Coal is one of the most abundant conventional resources in the world, and low-rank coal accounts for a large proportion. The low-rank coal has more side chains in the chemical structure, higher hydrogen and oxygen contents, has the characteristics of large moisture, low calorific value, good chemical reactivity, flammability, frangibility and the like, and is not suitable for long-distance transportation and storage. The existing low-rank coal processing and utilizing technologies comprise direct combustion power generation, direct liquefaction, gasification, quality improvement and the like. At present, low-rank coal is mainly used for pithead power generation, and a small amount of low-rank coal is dried, pyrolyzed or made into molded coal and then is transported out for combustion or chemical utilization of various industrial boilers. The low-rank coal is directly combusted as a power fuel, so that not only are rich oil and gas resources contained in the coal wasted, but also the economy is low, the energy efficiency is low, and the pollution is serious, so that the development of a more efficient, cleaner and more economic low-rank coal utilization technology is necessary.
The method combines the structural characteristics of energy in China, changes the existing coal utilization mode, and realizes the efficient and clean conversion of low-rank coal resources, thereby being an important research direction in the energy field in China. According to the characteristic of high volatile and hydrogen contents in the low-rank coal, oil, gas and chemicals with high added values can be obtained through graded conversion, and the upgraded coal is recycled to perform combustion power generation, so that the gradient utilization of low-rank coal resources is realized. Therefore, the method not only improves the utilization efficiency of coal, but also greatly reduces the pollutant discharge, and has important significance for realizing high-efficiency, clean and large-scale application of low-rank coal in China and promoting the sustainable development of the coal industry in China.
Chinese patent publication No. CN204005964U discloses a system for solving the problem of high-sodium coal contamination during pulverized coal furnace combustion by self-heating downer pyrolysis combustion, which comprises a downer pyrolysis furnace and a combustion furnace, wherein oxygen is introduced into the top of the downer pyrolysis furnace to make part of raw coal undergo oxidation combustion reaction, so as to provide heat to make the rest of raw coal undergo pyrolysis reaction, and the pyrolysis gas separated after pyrolysis is sent into the combustion furnace for combustion through a purification device. The disadvantages are that: (1) oxygen is introduced into the downer pyrolysis furnace, so that the raw coal is pyrolyzed in an aerobic state, and the yield of pyrolysis oil gas is reduced; (2) pyrolysis oil gas after pyrolysis of raw coal in the downer pyrolysis furnace is not fully recycled.
Chinese patent application publication No. CN105505419A discloses a coal pyrolysis reactor-pulverized coal boiler combined system and its application, the system includes a coal pyrolysis reactor, and a multilayer heat accumulating type radiant tube is arranged inside the coal pyrolysis reactor. The disadvantages are that: (1) the coal powder in the coal pyrolysis reactor is contacted with the radiant tube for heat exchange, and the coal powder is pyrolyzed to generate semicoke and oil gas. The semi-coke and oil gas are easy to adhere and accumulate on the surface of the radiant tube, so that the heat transfer effect and the service life of the radiant tube are influenced; (2) a plurality of radiant tubes are arranged in the coal pyrolysis reactor, so that the whole device is complex in structure, complex to operate and high in energy consumption.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, and provides the combustion system of the ascending bed coal pyrolysis co-production circulating fluidized bed boiler, which has reasonable structural design and simple process flow, so as to solve the problems of high-efficiency, clean and comprehensive utilization of low-rank coal resources, obtain pyrolysis oil and pyrolysis gas with high added values, greatly reduce the serious pollution, high-temperature corrosion and abrasion of convection heating surfaces of a combustion furnace hearth when the existing power station boiler directly combusts high-alkali coal, ensure the heat exchange effect of the heating surfaces, reduce the occurrence of pipe explosion accidents, prolong the service life of the boiler and prolong the safe and stable operation period of the boiler.
The technical scheme adopted by the invention for solving the problems is as follows: a combustion system of an ascending bed coal pyrolysis co-production circulating fluidized bed boiler is characterized by comprising a pulverized coal bin, a bin pump, an ascending bed pyrolysis furnace, a turbulent coalescer, a high-temperature centrifuge, a cyclone separator, a pyrolysis oil-gas cooling device, a pyrolysis oil-gas purification and separation device, a pyrolysis gas collector, a pyrolysis water collector, a pyrolysis tar collector and a circulating fluidized bed boiler;
the upgoing bed pyrolysis furnace is provided with a coal powder inlet, a heat carrier inlet, a guide cylinder, a guide flow area, an annular space area, a lifting gas inlet, an air chamber, an air distribution plate and a bottom slag outlet; the coal powder inlet and the heat carrier inlet are positioned on two sides of the ascending bed pyrolysis furnace; the guide cylinder is positioned inside the ascending bed pyrolysis furnace, the guide area is positioned inside the guide cylinder, and the annular space area is positioned between the guide cylinder and the ascending bed pyrolysis furnace; the guide cylinder divides the ascending bed pyrolysis furnace into a guide flow area and an annular space area, so that the mixing and heat exchange behaviors of large-particle coal powder and a heat carrier are strengthened, the retention time of the large-particle coal powder in the descending bed pyrolysis furnace is prolonged, the large-particle coal powder is fully pyrolyzed, and the yield of pyrolysis oil gas is improved; the air chamber is positioned at the bottom of the upgoing bed pyrolysis furnace, an air pressure stabilizing area is provided before lifting gas enters the air distribution plate, and the air chamber is a place for converting dynamic pressure and static pressure and is beneficial to the uniformity of air distribution; the lifting air inlet is positioned at the outer side of the air chamber; the air distribution plate is positioned at the top of the air chamber and below the guide cylinder; the air distribution plate is provided with a plurality of air outlets; the bottom slag outlet vertically penetrates through the air distribution plate and the air chamber, the top end of the bottom slag outlet is flush with the top end of the air distribution plate, and the bottom end of the bottom slag outlet is positioned below the air chamber;
the outlet of the pulverized coal bin is connected with the inlet of a bin pump, the outlet of the bin pump is connected with a pulverized coal inlet, and the bin pump is used for conveying pulverized coal in the pulverized coal bin into an annular space area of the upper-bed pyrolysis furnace through the pulverized coal inlet; go upward the top export of bed pyrolysis stove and the import of torrent coalescer link to each other, the export of torrent coalescer links to each other with the import of high temperature centrifuge, the export of high temperature centrifuge links to each other with cyclone's import, cyclone's top export links to each other with pyrolysis oil gas cooling device's entry, pyrolysis oil gas cooling device's export links to each other with pyrolysis oil gas purification and separation device's entry and promotion gas import simultaneously, pyrolysis oil gas purification and separation device's export links to each other with pyrolysis gas collector, pyrolysis water collector, pyrolysis tar collector respectively, pyrolysis gas collector's export links to each other with pyrolysis oil gas cooling device's import, cyclone's bottom export links to each other with heat carrier import and circulating fluidized bed boiler simultaneously, the end sediment export links to each other with circulating fluidized bed boiler, circulating fluidized bed boiler is used for circulating combustion to come from the high temperature semicoke after the bed pyrolysis stove that goes upward the pyrolysis and come from going upward the bed boiler A heat carrier and a solid product mixture at a bottom slag outlet of the pyrolysis furnace.
Furthermore, a heat exchanger is arranged in the pyrolysis oil gas cooling device and used for realizing heat exchange between pyrolysis gas from the pyrolysis gas collector and pyrolysis products, so that the function of preheating the pyrolysis gas is achieved.
The working method of the combustion system of the ascending bed coal pyrolysis co-production circulating fluidized bed boiler is characterized by comprising the following steps:
the low-order coal powder is conveyed into the annular space area of the upper-moving bed pyrolysis furnace from the coal powder inlet through the coal powder bin under the action of the bin pump, and the heat carrier semicoke is conveyed into the annular space area of the upper-moving bed pyrolysis furnace from the heat carrier inlet at the bottom of the cyclone separator; the low-rank coal dust and the heat carrier semicoke move downwards to the bottom of the diversion area along the annular space area under the action of gravity; lifting gas enters the air chamber from the top of the pyrolysis oil-gas cooling device through a lifting gas inlet, and continues to enter the bottom of the flow guide area from an air outlet on the air distribution plate along the air chamber; under the action of the lifting gas, the low-rank coal dust and the heat carrier semicoke at the bottom of the diversion area move upwards along the diversion area, the mixing and the heat exchange of the low-rank coal dust and the heat carrier semicoke are completed, and the low-rank coal dust after the heat exchange is subjected to a pyrolysis reaction; the reacted pyrolysis product sequentially enters a turbulent flow coalescer, a high-temperature centrifuge and a cyclone separator through a reducing section at the top of the upgoing bed pyrolysis furnace, and the processes of dust agglomeration in the pyrolysis product, pre-centrifugal force generation of pyrolysis oil gas and separation of the pyrolysis oil gas and semicoke are respectively completed; the unreacted large-particle low-rank coal powder returns to the flow guide area and the annular space area inside the ascending bed pyrolysis furnace along the top of the ascending bed pyrolysis furnace because the gravity of the unreacted large-particle low-rank coal powder is larger than the drag force of gas on the unreacted large-particle low-rank coal powder, and is continuously mixed with a semicoke heat carrier and exchanges heat;
the apparent velocity of the lifting gas in the flow guide area is larger than that of the lifting gas in the annular space area by regulating and controlling the lifting gas quantity at the lifting gas inlet, so that the pressure of the flow guide area at the bottom of the flow guide cylinder is larger than that of the annular space area, coal and a heat carrier respectively from the coal powder inlet and the heat carrier inlet flow directionally in the ascending bed pyrolysis furnace, and multiple circulations are formed, namely the coal and the heat carrier flow downwards in the annular space area and move upwards in the flow guide area, so that the flow environment of large-particle low-rank coal powder and the heat carrier is improved, uniform mixing and heat exchange of low-rank coal powder particles and the heat carrier are ensured, meanwhile, the pyrolysis time of the low-rank coal powder can be effectively controlled according to different target products, the effective control on the pyrolysis reaction depth and reaction process of;
high-temperature semicoke generated by pyrolysis in the upgoing bed pyrolysis furnace is separated by a cyclone separator and then is conveyed to a heat carrier inlet from an outlet of the cyclone separator; pyrolysis products (pyrolysis oil gas, pyrolysis water and semicoke) in the upgoing bed pyrolysis furnace are separated by a cyclone separator and enter a pyrolysis oil gas cooling device from the top of the cyclone separator; the pyrolysis water and the pyrolysis oil gas cooled by the pyrolysis oil gas cooling device are further conveyed to a pyrolysis oil gas purification and separation device, the purification and separation steps are sequentially completed in the pyrolysis oil gas purification and separation device, and the separated pyrolysis gas, pyrolysis water and pyrolysis oil respectively enter a pyrolysis gas collector, a pyrolysis water collector and a pyrolysis tar collector; a part of pyrolysis gas in the pyrolysis gas collector is used as lifting gas, enters the pyrolysis oil gas cooling device from the pyrolysis gas collector, exchanges heat with pyrolysis products in the pyrolysis oil gas cooling device, and is finally conveyed to a lifting gas inlet;
the high-temperature semicoke separated by the cyclone separator is discharged from a bottom outlet of the cyclone separator, a part of the high-temperature semicoke is used as a heat carrier for supplying the heat of the pulverized coal in the ascending bed pyrolysis furnace to enter a heat carrier inlet, and the rest high-temperature semicoke, namely upgraded coal, is used as a raw material of the circulating fluidized bed boiler to enter the circulating fluidized bed boiler for combustion reaction; a small amount of heat carriers, solid products and the like in the ascending bed pyrolysis furnace are discharged from a bottom slag outlet and enter a circulating fluidized bed boiler to carry out combustion reaction.
Compared with the prior art, the invention has the following advantages and effects:
(1) by adopting the coal pyrolysis and combustion co-production process method, the utilization efficiency of coal is improved, the pollutant discharge is greatly reduced, and the method has important significance for realizing high-efficiency, clean and large-scale application of low-rank coal.
(2) In the process of the up-going bed pyrolysis, the semicoke pyrolyzed in the process is used as a heat carrier, so that the heat of the semicoke is recovered, and the heat is provided for the pulverized coal pyrolysis.
(3) Through setting up the draft tube in going up bed pyrolysis furnace inside for low order coal granule and heat carrier are directional to flow in the pyrolysis furnace, and form circulation many times, the flow environment of large granule low order buggy and heat carrier has effectively been improved, the homogeneous mixing of large granule low order buggy and heat carrier, the heat transfer has been guaranteed, can be according to the pyrolysis time of the different effective control low order buggy of target product simultaneously, thereby realize the effective control to low order coal pyrolysis reaction degree of depth and reaction process, the conversion rate has been improved, target product yield has been improved.
(4) The semicoke and the bottom slag after pyrolysis of the upgoing bed pyrolysis furnace are used as raw materials of the circulating fluidized bed boiler, so that the alkali metal content in the boiler when some high-alkali coal is directly combusted is fundamentally reduced, the serious pollution, high-temperature corrosion and abrasion of a convection heating surface of the boiler due to the action of the alkali metal are reduced, the safety and the heat exchange effect of the heating surface are ensured, and the output and the efficiency of the boiler are improved.
(5) The system has simple structural design and convenient operation, is easy to realize large-scale production, has strong adaptability to coal types, and can adapt to non-caking coal, weak caking coal and strong caking coal.
Drawings
Fig. 1 is a schematic system structure according to an embodiment of the present invention.
In the figure: the device comprises a pulverized coal bin 1, a bin pump 2, a pulverized coal inlet 3, an ascending bed pyrolysis furnace 4, a guide cylinder 5, a guide zone 6, an annular space zone 7, a lifting gas inlet 8, a wind chamber 9, a wind distribution plate 10, a wind outlet 11, a bottom slag outlet 12, a heat carrier inlet 13, a turbulent coalescer 14, a high-temperature centrifuge 15, a cyclone separator 16, a pyrolysis oil-gas cooling device 17, a pyrolysis oil-gas purification and separation device 18, a pyrolysis gas collector 19, a pyrolysis water collector 20, a pyrolysis tar collector 21 and a circulating fluidized bed boiler 22.
Detailed Description
The present invention will be described in further detail below by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and are not to be construed as limiting the present invention.
Examples are given.
Referring to fig. 1, in this embodiment, an ascending bed coal pyrolysis co-production circulating fluidized bed boiler combustion system includes a pulverized coal bunker 1, a bunker pump 2, an ascending bed pyrolysis furnace 4, a turbulent coalescer 14, a high-temperature centrifuge 15, a cyclone separator 16, a pyrolysis oil-gas cooling device 17, a pyrolysis oil-gas purification and separation device 18, a pyrolysis gas collector 19, a pyrolysis water collector 20, a pyrolysis tar collector 21, and a circulating fluidized bed boiler 22;
the upgoing bed pyrolysis furnace 4 is provided with a coal powder inlet 3, a heat carrier inlet 13, a guide cylinder 5, a guide area 6, an annular space area 7, a lifting gas inlet 8, an air chamber 9, an air distribution plate 10 and a bottom slag outlet 12; the coal powder inlet 3 and the heat carrier inlet 13 are positioned at two sides of the ascending bed pyrolysis furnace 4; the guide shell 5 is positioned inside the ascending bed pyrolysis furnace 4, the guide area 6 is positioned inside the guide shell 5, and the annular space area 7 is positioned between the guide shell 5 and the ascending bed pyrolysis furnace 4; the guide cylinder 5 divides the ascending bed pyrolysis furnace 4 into a guide flow area 6 and an annular space area 7, so that the mixing and heat exchange behaviors of large-particle coal powder and a heat carrier are enhanced, the retention time of the large-particle coal powder in the descending bed pyrolysis furnace is prolonged, the large-particle coal powder is fully pyrolyzed, and the yield of pyrolysis oil gas is improved; the air chamber 9 is positioned at the bottom of the upgoing bed pyrolysis furnace 4, provides an air pressure stabilizing area before lifting gas enters the air distribution plate 10, is a place for dynamic and static pressure conversion, and is beneficial to the uniformity of air distribution; the lifting air inlet 8 is positioned outside the air chamber 9; the air distribution plate 10 is positioned at the top of the air chamber 9 and below the guide cylinder 5; the air distribution plate 10 is provided with a plurality of air outlets 11; the bottom slag outlet 12 vertically penetrates through the air distribution plate 10 and the air chamber 9, the top end of the bottom slag outlet 12 is flush with the top end of the air distribution plate 10, and the bottom end of the bottom slag outlet 12 is positioned below the air chamber 9;
the outlet of the coal powder bin 1 is connected with the inlet of a bin pump 2, the outlet of the bin pump 2 is connected with a coal powder inlet 3, and the bin pump 2 is used for conveying coal powder in the coal powder bin 1 to an annular space area 7 of an upper bed pyrolysis furnace 4 through the coal powder inlet 3; the top outlet of the upgoing bed pyrolysis furnace 4 is connected with the inlet of a turbulent flow coalescer 14, the outlet of the turbulent flow coalescer 14 is connected with the inlet of a high temperature centrifuge 15, the outlet of the high temperature centrifuge 15 is connected with the inlet of a cyclone separator 16, the top outlet of the cyclone separator 16 is connected with the inlet of a pyrolysis oil-gas cooling device 17, the outlet of the pyrolysis oil-gas cooling device 17 is simultaneously connected with the inlet of a pyrolysis oil-gas purification and separation device 18 and a lifting gas inlet 8, the outlet of the pyrolysis oil-gas purification and separation device 18 is respectively connected with a pyrolysis gas collector 19, a pyrolysis water collector 20 and a pyrolysis tar collector 21, the outlet of the pyrolysis gas collector 19 is connected with the inlet of the pyrolysis oil-gas cooling device 17, the bottom outlet of the cyclone separator 16 is simultaneously connected with a heat carrier inlet 13 and a circulating fluidized bed boiler 22, the bottom slag outlet 12 is connected with the circulating fluidized bed boiler 22, and the circulating fluidized bed boiler 22 is used for circularly combusting high temperature semicoke pyrolyzed A heat carrier and solid product mixture from the bottom slag outlet 12 of the upgoing bed pyrolysis furnace 4.
The working method of the combustion system of the ascending bed coal pyrolysis co-production circulating fluidized bed boiler comprises the following steps:
the low-order coal powder is conveyed to the annular space area 7 of the upper bed pyrolysis furnace 4 from the coal powder inlet 3 through the coal powder bin 1 under the action of the bin pump 2, and the heat carrier semicoke is conveyed to the annular space area 7 of the upper bed pyrolysis furnace 4 from the bottom of the cyclone separator 16 through the heat carrier inlet 13; the low-rank coal dust and the heat carrier semi-coke move downwards to the bottom of the diversion area 6 along the annular space area 7 under the action of gravity; the lifting gas enters the air chamber 9 from the top of the pyrolysis oil-gas cooling device 17 through the lifting gas inlet 8 and continues to enter the bottom of the flow guide area 6 along the air chamber 9 from the air outlet 11 on the air distribution plate 10; under the action of the lifting gas, the low-rank coal dust and the heat carrier semicoke at the bottom of the diversion area 6 move upwards along the diversion area 6, the mixing and the heat exchange of the low-rank coal dust and the heat carrier semicoke are completed, and the low-rank coal dust after the heat exchange is subjected to a pyrolysis reaction; the reacted pyrolysis product sequentially enters a turbulent coalescer 14, a high-temperature centrifuge 15 and a cyclone separator 16 through a diameter reducing section at the top of the upgoing bed pyrolysis furnace 4, and the processes of dust agglomeration in the pyrolysis product, generation of a pre-centrifugal force by pyrolysis oil gas and separation of the pyrolysis oil gas and semicoke are respectively completed; the unreacted large-particle low-rank coal powder returns to the flow guide area 6 and the annular space area 7 inside the ascending bed pyrolysis furnace 4 along the top of the ascending bed pyrolysis furnace because the gravity of the unreacted large-particle low-rank coal powder is larger than the drag force of gas on the unreacted large-particle low-rank coal powder, and is continuously mixed with a semicoke heat carrier and subjected to heat exchange;
the apparent velocity of the lifting gas of the flow guide area 6 is larger than that of the lifting gas of the annular space area 7 by regulating and controlling the lifting gas quantity of the lifting gas inlet 8, the pressure of the flow guide area 6 at the bottom of the flow guide cylinder 5 is larger than that of the annular space area 7, coal and a heat carrier respectively from the coal powder inlet 3 and the heat carrier inlet 13 are continuously enabled to flow directionally in the ascending bed pyrolysis furnace 4 and form multiple circulations, namely flow downwards in the annular space area 7 and move upwards in the flow guide area 6, so that the flow environment of large-particle low-rank coal powder and the heat carrier is improved, the uniform mixing and heat exchange of low-rank coal particles and the heat carrier are ensured, meanwhile, the pyrolysis time of the low-rank coal can be effectively controlled according to different target products, the effective control on the pyrolysis reaction depth and reaction process of the low-rank coal is realized;
high-temperature semicoke generated by pyrolysis in the upgoing bed pyrolysis furnace 4 is separated by the cyclone separator 16 and then is conveyed to the heat carrier inlet 13 from the outlet of the cyclone separator 16; pyrolysis products (pyrolysis oil gas, pyrolysis water and semicoke) in the upgoing bed pyrolysis furnace 4 are separated by the cyclone separator 16 and then enter the pyrolysis oil gas cooling device 17 from the top of the cyclone separator 16; a heat exchanger is arranged in the pyrolysis oil gas cooling device 17 and is used for realizing heat exchange between pyrolysis gas from the pyrolysis gas collector 19 and pyrolysis products, so that the function of preheating the pyrolysis gas is achieved; the pyrolysis water and the pyrolysis oil gas cooled by the pyrolysis oil gas cooling device 17 are further conveyed to a pyrolysis oil gas purification and separation device 18, the purification and separation steps are sequentially completed in the pyrolysis oil gas purification and separation device, and the separated pyrolysis gas, pyrolysis water and pyrolysis oil respectively enter a pyrolysis gas collector 19, a pyrolysis water collector 20 and a pyrolysis tar collector 21; a part of the pyrolysis gas in the pyrolysis gas collector 19 is used as lifting gas, enters the pyrolysis oil gas cooling device 17 from the pyrolysis gas collector 19, exchanges heat with pyrolysis products in the pyrolysis oil gas cooling device, and is finally conveyed to the lifting gas inlet 8;
the high-temperature semicoke separated by the cyclone separator 16 is discharged from the outlet at the bottom of the cyclone separator 16, a part of the high-temperature semicoke is used as a heat carrier for supplying the heat of the pulverized coal in the upgoing bed pyrolysis furnace 4 and enters the heat carrier inlet 13, and the rest high-temperature semicoke, namely upgraded coal, is used as a raw material of the circulating fluidized bed boiler 22 and enters the circulating fluidized bed boiler for combustion reaction; a small amount of heat carrier, solid products and the like in the upgoing bed pyrolysis furnace 4 are discharged from the bottom slag outlet 12 and enter the circulating fluidized bed boiler 22 for combustion reaction.
Those not described in detail in this specification are well within the skill of the art.
Although the present invention has been described with reference to the above embodiments, it should be understood that the scope of the present invention is not limited thereto, and that various changes and modifications can be made by those skilled in the art without departing from the spirit and scope of the present invention.
Claims (3)
1. An ascending bed coal pyrolysis co-production circulating fluidized bed boiler combustion system is characterized by comprising a pulverized coal bin (1), a bin pump (2), an ascending bed pyrolysis furnace (4), a turbulent coalescer (14), a high-temperature centrifuge (15), a cyclone separator (16), a pyrolysis oil-gas cooling device (17), a pyrolysis oil-gas purification and separation device (18), a pyrolysis gas collector (19), a pyrolysis water collector (20), a pyrolysis tar collector (21) and a circulating fluidized bed boiler (22);
the upgoing bed pyrolysis furnace (4) is provided with a coal powder inlet (3), a heat carrier inlet (13), a guide cylinder (5), a guide area (6), an annular space area (7), a lifting gas inlet (8), an air chamber (9), an air distribution plate (10) and a bottom slag outlet (12); the coal powder inlet (3) and the heat carrier inlet (13) are positioned at two sides of the upgoing bed pyrolysis furnace (4); the guide shell (5) is positioned inside the upgoing bed pyrolysis furnace (4), the guide area (6) is positioned inside the guide shell (5), and the annular space area (7) is positioned between the guide shell (5) and the upgoing bed pyrolysis furnace (4); the air chamber (9) is positioned at the bottom of the upgoing bed pyrolysis furnace (4), and the lifting gas inlet (8) is positioned at the outer side of the air chamber (9); the air distribution plate (10) is positioned at the top of the air chamber (9) and below the guide cylinder (5); the air distribution plate (10) is provided with a plurality of air outlets (11); the bottom slag outlet (12) vertically penetrates through the air distribution plate (10) and the air chamber (9), the top end of the bottom slag outlet (12) is flush with the top end of the air distribution plate (10), and the bottom end of the bottom slag outlet (12) is positioned below the air chamber (9);
the outlet of the pulverized coal bin (1) is connected with the inlet of a bin pump (2), the outlet of the bin pump (2) is connected with a pulverized coal inlet (3), and the bin pump (2) is used for conveying pulverized coal in the pulverized coal bin (1) into an annular space area (7) of an upper-bed pyrolysis furnace (4) through the pulverized coal inlet (3); the top outlet of the upgoing bed pyrolysis furnace (4) is connected with the inlet of a turbulent coalescer (14), the outlet of the turbulent coalescer (14) is connected with the inlet of a high-temperature centrifuge (15), the outlet of the high-temperature centrifuge (15) is connected with the inlet of a cyclone separator (16), the top outlet of the cyclone separator (16) is connected with the inlet of a pyrolysis oil-gas cooling device (17), the outlet of the pyrolysis oil-gas cooling device (17) is simultaneously connected with the inlet of a pyrolysis oil-gas purification and separation device (18) and a lifting gas inlet (8), the outlet of the pyrolysis oil-gas purification and separation device (18) is respectively connected with a pyrolysis gas collector (19), a pyrolysis water collector (20) and a pyrolysis tar collector (21), the outlet of the pyrolysis gas collector (19) is connected with the inlet of the pyrolysis oil-gas cooling device (17), and the bottom outlet of the cyclone separator (16) is simultaneously connected with a heat carrier inlet (13) and a fluidized bed circulating boiler (c) 22) And the bottom slag outlet (12) is connected with a circulating fluidized bed boiler (22), and the circulating fluidized bed boiler (22) is used for circularly combusting high-temperature semicoke from the pyrolysis of the upward bed pyrolysis furnace (4) and a heat carrier and solid product mixture from the bottom slag outlet (12) of the upward bed pyrolysis furnace (4).
2. The combustion system of an upgoing bed coal pyrolysis co-production circulating fluidized bed boiler as claimed in claim 1, wherein a heat exchanger is installed in the pyrolysis oil gas cooling device (17) for realizing heat exchange between pyrolysis gas and pyrolysis products from the pyrolysis gas collector (19).
3. A method for operating the combustion system of the ascending bed coal pyrolysis co-production circulating fluidized bed boiler according to claim 1 or 2, characterized by comprising the following steps:
the low-order coal dust is conveyed into an annular space area (7) of the upper-bed pyrolysis furnace (4) through a coal dust inlet (3) under the action of a bin pump (2) through a coal dust bin (1), and heat carrier semicoke is conveyed into the annular space area (7) of the upper-bed pyrolysis furnace (4) from a heat carrier inlet (13) from the bottom of a cyclone separator (16); the low-rank coal dust and the heat carrier semicoke move downwards to the bottom of the diversion area (6) along the annular space area (7) under the action of gravity; lifting gas enters the air chamber (9) from the top of the pyrolysis oil-gas cooling device (17) through a lifting gas inlet (8), and continues to enter the bottom of the flow guide area (6) along the air chamber (9) from an air outlet (11) on the air distribution plate (10); under the action of the lifting gas, the low-rank coal dust and the heat carrier semicoke at the bottom of the diversion area (6) move upwards along the diversion area (6) and complete mixing and heat exchange of the low-rank coal dust and the heat carrier semicoke, and the low-rank coal dust after heat exchange is subjected to pyrolysis reaction; the reacted pyrolysis product sequentially enters a turbulent flow coalescer (14), a high-temperature centrifuge (15) and a cyclone separator (16) through a diameter reducing section at the top of the upgoing bed pyrolysis furnace (4) to respectively finish the processes of dust agglomeration in the pyrolysis product, generation of a pre-centrifugal force by pyrolysis oil gas and separation of the pyrolysis oil gas and semicoke; the unreacted large-particle low-rank coal powder returns to the flow guide area (6) and the annular space area (7) inside the ascending bed pyrolysis furnace (4) along the top of the ascending bed pyrolysis furnace because the gravity of the unreacted large-particle low-rank coal powder is larger than the drag force of gas to the unreacted large-particle low-rank coal powder, and is continuously mixed with a semicoke heat carrier and subjected to heat exchange;
by regulating and controlling the lifting gas amount of the lifting gas inlet (8), the apparent lifting gas speed of the flow guide area (6) is higher than that of the annular space area (7), the pressure of the flow guide area (6) at the bottom of the flow guide cylinder (5) is higher than that of the annular space area (7), so that coal and heat carriers respectively from the coal powder inlet (3) and the heat carrier inlet (13) flow directionally in the ascending bed pyrolysis furnace (4) and form multiple circulations, namely flow downwards in the annular space area (7) and move upwards in the flow guide area (6), the flow environment of large-particle low-order coal powder and the heat carrier is improved, the uniform mixing and heat exchange of the large-particle low-order coal powder and the heat carrier are ensured, meanwhile, the pyrolysis time of the low-order coal powder can be effectively controlled according to different target products, the effective control on the pyrolysis reaction depth and reaction process of the low-order coal powder is realized, the yield of the target product is improved;
high-temperature semicoke generated by pyrolysis in the upgoing bed pyrolysis furnace (4) is separated by the cyclone separator (16) and then is conveyed to the heat carrier inlet (13) from the outlet of the cyclone separator (16); pyrolysis products in the upgoing bed pyrolysis furnace (4) are separated by the cyclone separator (16) and then enter the pyrolysis oil-gas cooling device (17) from the top of the cyclone separator (16); the pyrolysis water and the pyrolysis oil gas cooled by the pyrolysis oil gas cooling device (17) are further conveyed to a pyrolysis oil gas purification and separation device (18), the purification and separation steps are sequentially completed in the pyrolysis oil gas purification and separation device, and the separated pyrolysis gas, the pyrolysis water and the pyrolysis oil respectively enter a pyrolysis gas collector (19), a pyrolysis water collector (20) and a pyrolysis tar collector (21); a part of pyrolysis gas in the pyrolysis gas collector (19) is used as lifting gas, enters the pyrolysis oil gas cooling device (17) from the pyrolysis gas collector (19), exchanges heat with pyrolysis products in the pyrolysis oil gas cooling device, and is finally conveyed to the lifting gas inlet (8);
the high-temperature semicoke separated by the cyclone separator (16) is discharged from a bottom outlet of the cyclone separator (16), a part of the high-temperature semicoke is used as a heat carrier for supplying the heat of the coal dust in the upgoing bed pyrolysis furnace (4) and enters a heat carrier inlet (13), and the rest high-temperature semicoke, namely upgraded coal, is used as a raw material of a circulating fluidized bed boiler (22) and enters the circulating fluidized bed boiler for combustion reaction; a small amount of heat carrier and solid products in the upgoing bed pyrolysis furnace (4) are discharged from a bottom slag outlet (12) and enter a circulating fluidized bed boiler (22) for combustion reaction.
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