CN102384469A - Oxygen-controlled fluid bed system and operational method thereof - Google Patents
Oxygen-controlled fluid bed system and operational method thereof Download PDFInfo
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- CN102384469A CN102384469A CN2011101970533A CN201110197053A CN102384469A CN 102384469 A CN102384469 A CN 102384469A CN 2011101970533 A CN2011101970533 A CN 2011101970533A CN 201110197053 A CN201110197053 A CN 201110197053A CN 102384469 A CN102384469 A CN 102384469A
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 69
- 239000001301 oxygen Substances 0.000 title claims abstract description 69
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 23
- 239000012530 fluid Substances 0.000 title claims description 29
- 239000004449 solid propellant Substances 0.000 claims abstract description 41
- 239000007787 solid Substances 0.000 claims abstract description 30
- 239000000446 fuel Substances 0.000 claims abstract description 29
- 238000002485 combustion reaction Methods 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 16
- 239000007921 spray Substances 0.000 claims abstract description 11
- 238000004939 coking Methods 0.000 claims abstract description 8
- 239000000839 emulsion Substances 0.000 claims description 41
- 239000003795 chemical substances by application Substances 0.000 claims description 29
- 239000000969 carrier Substances 0.000 claims description 19
- 239000003517 fume Substances 0.000 claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 239000003546 flue gas Substances 0.000 claims description 13
- 238000005243 fluidization Methods 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 239000002737 fuel gas Substances 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 4
- 210000000038 chest Anatomy 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000011017 operating method Methods 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 9
- 239000000779 smoke Substances 0.000 abstract 1
- 239000003245 coal Substances 0.000 description 8
- 230000001276 controlling effect Effects 0.000 description 7
- 230000005587 bubbling Effects 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
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Abstract
一种控氧流化床系统及运行方法，包括控氧流化床、鼓风机、补燃室、换热器和风机。控氧流化床包括炉膛、布风板、风室、进料口和床上排料口，炉膛采用变截面结构，布风板处炉膛的截面积A1为炉膛上部截面积A2的0.25～0.4倍；在布风板上方密相区的炉墙设置两个以上的喷水口，风室设有两个以上的蒸汽喷口。流化床内以固体燃料作为床料，空气与烟气混合形成含氧量为5％～21％的气体流化介质，对固体燃料进行流化并部分燃烧。蒸汽和喷水作为调温手段，有效保证床层温度和炉膛温度在设定值内，避免载体温度过高而结焦。本发明为无床料全燃料燃烧，保证固体载热体的纯度；控氧措施和床温控制措施，能有效控制燃料燃烧量，并保证运行稳定。
An oxygen control fluidized bed system and its operation method, comprising an oxygen control fluidized bed, a blower, a supplementary combustion chamber, a heat exchanger and a fan. The oxygen-controlled fluidized bed includes a furnace, an air distribution plate, an air chamber, a feed inlet and a bed discharge port. The furnace adopts a variable cross-section structure, and the cross-sectional area A1 of the furnace at the air distribution plate is 0.25 to 0.4 times; more than two water nozzles are set on the furnace wall in the dense phase area above the air distribution plate, and more than two steam nozzles are set in the air chamber. Solid fuel is used as bed material in the fluidized bed, and air and smoke are mixed to form a gas fluidized medium with an oxygen content of 5% to 21%, which fluidizes and partially burns the solid fuel. Steam and water spray are used as temperature adjustment means to effectively ensure that the bed temperature and furnace temperature are within the set value, and avoid coking due to excessive carrier temperature. The invention is all-fuel combustion without bed materials, which ensures the purity of the solid heat carrier; oxygen control measures and bed temperature control measures can effectively control the amount of fuel combustion and ensure stable operation.
Description
Technical field
What the present invention relates to is a kind of combustion apparatus and combustion method, particularly relates to a kind of control oxygen flow bed system and operation method.
Background technology
Fluidized bed combustion has characteristics such as fuel tolerance is wide, efficiency of combustion height, is widely used in fire coal, biomass-burning etc.Bubbling fluidized bed bed expansion but still steady relatively has bed upper surface clearly, and gas-solid mixes fully in the emulsion zone.In fluid bed, can add the inert bed material (like quartz sand, lime stone etc.) of certain grain size scope usually, play the effect that the heat storage heating fuel is kept burning, also guaranteed material balance simultaneously.Through adjusting the oxygen content after air capacity is adjusted the burner hearth internal combustion, both guaranteed that burning fully, reduced the generation of NOx again in the combustion process.In bubbling fluidized bed, too high in order to prevent bed temperature, often adopt the mode of emulsion zone pipe laying to arrange heating surface, and the wearing and tearing of pipe laying are more serious with the reduction bed temperature.
Fluidization also is used for coal gasification in Coal Chemical Industry.Coal fully mixes with gasifying agent in fluidized-bed reactor.In fluidized-bed gasification furnace, exist evenly distribute and with the flying dust of the organic consor of coal, and almost with the ash with big spoil component of the organic separated attitude of coal.When the Winkler fluidized bed gasifying process is applied to brown coal hydrogasification, adopt oxygen and steam as gasifying agent.Fluidized bed gasifying process all improves the charcoal conversion ratio as far as possible, increases factor of created gase, and reduces tar yield.
And in the coal thermal conversion process system of coke carried heat destructive distillation; Needing a kind of is the burner of main purpose to obtain high-temperature material (thermophore); Can not introduce inert bed material, the fuel in the device is all burnt, can not as as the gasification furnace with the fuel aerogenesis that all gasifies.
Summary of the invention
The present invention is directed to the deficiency of above-mentioned prior art; A kind of fluidized system and operation method of controlling the oxygen temperature control is provided; Both avoided introducing the influence of inert bed material to product purity; Can prevent that fuel combustion is excessive too high with temperature solid thermal carriers through taking to control fluidizing agent oxygen content and the measure of two-stage desuperheat again.
The present invention realizes through following technical scheme:
A kind of control oxygen flow bed system; Said system comprises control oxygen fluid bed, is arranged on the ajutage and the air blast that links to each other with ajutage of control oxygen fluid bed bottom; Air compartment, charging aperture and bed that said control oxygen fluid bed comprises burner hearth, air distribution plate, be arranged on the air distribution plate below are gone up discharge gate; It is characterized in that: said system also comprises afterburning chamber, heat exchanger, circulating fan and fume pipe, and the afterburning chamber import links to each other with the exhanst gas outlet on control oxygen fluid bed top, and the afterburning chamber outlet links to each other with heat exchanger; Heat exchanger links to each other with control oxygen fluid bed bottom air compartment through fume pipe, and circulating fan is set on fume pipe; On the furnace wall of emulsion zone above the air distribution plate, water jet is set.
The upper furnace cross section of said control oxygen fluid bed is a rectangle, and lower furnace portion is the convergent terrace with edge; Or the upper furnace cross section is circular, and lower furnace portion is the frustum of a cone; The sectional area A of air distribution plate place burner hearth
1Be upper furnace sectional area A
20.25～0.4 times, i.e. 0.25≤A
1: A
2≤0.4.
Said water jet is more than two; Said steam nozzle is more than two.
A kind of operation method of controlling the oxygen flow bed system provided by the invention is characterized in that:
1) solid fuel gets into burner hearth from the charging aperture of control oxygen fluid bed continuously, not only acts as a fuel but also expect as bed;
2) air is sent into air compartment by air blast through ajutage, as fluidizing agent solid fuel is carried out fluidisation and burning;
3) flue gas that contains combustible dust and fuel gas after the burning gets into afterburning chamber, the completing combustion in afterburning chamber of combustible dust and fuel gas, and flue gas entering heat exchanger and heat transferring medium heat exchange after the completing combustion are lowered the temperature;
4) directly discharging of the part of the flue gas after the cooling; Another part is sent into air compartment and air by circulating fan from fume pipe and is mixed together as fluidizing agent and feeds burner hearth from air distribution plate; Through regulating the ratio of air capacity and exhaust gas volumn; The oxygen content that makes fluidizing agent is 5%～21%, and the solid fuel in the burner hearth is carried out the burning of control oxygen;
5) under the control oxygen condition, in the solid fuel ignition process, the burner hearth emulsion zone is divided into two parts carries out temperature control, the lower area temperature of burner hearth emulsion zone is controlled at 850～1050 ℃, and the upper area temperature of emulsion zone is controlled to be 900～1100 ℃; When the lower area temperature of burner hearth emulsion zone is higher than the control temperature; Spray into steam from steam nozzle, steam mixes with fluidizing agent at air compartment, is blown into from air distribution plate; To reduce the lower area temperature of burner hearth emulsion zone, prevent as the too high and coking of the fuel temperature of solid thermal carriers; When the temperature of the lower area of burner hearth emulsion zone and upper area is higher than the control temperature simultaneously; Spray water in burner hearth from the steam nozzle spraying steam with from water jet simultaneously; Reduce rapidly the lower area temperature and the upper area temperature of burner hearth emulsion zone, prevent as the too high and coking of the fuel temperature of solid thermal carriers;
6) under the control oxygen condition, have only the part solid fuel ignition in the control oxygen flow pool furnace thorax, solid fuel ignition produces all solids fuel in the heat burner hearth, obtains solid thermal carriers; Solid thermal carriers are discharge gate discharge from the bed continuously.
Compared with prior art, beneficial effect of the present invention is: guarantee that 1) the fuel combustion amount is controlled: in the bed all is fuel, if do not control the oxygen content of fluidizing agent, can increase the quantity combusted of a fuel; Through in fluidizing agent, sneaking into flue gas, the oxygen content in the adjusting fluidizing agent guarantees that the fuel combustion amount is controlled in 5%～21%.2) guarantee that bed temperature is controlled: adopt the basic temperature adjustment means of air compartment place water spray steam to stablize bed temperature, auxiliary urgent temperature adjustment means of in bed, spraying water are lowered the temperature rapidly, and are simple to operate, regulate flexibly, can effectively control bed temperature.
Description of drawings
Fig. 1 is a kind of control oxygen flow bed system sketch map involved in the present invention.
Fig. 2 is a kind of control oxygen flow bed apparatus sketch map involved in the present invention.
Among the figure: 1-control oxygen fluid bed; The 2-burner hearth; The 3-emulsion zone; The 4-air distribution plate; The 5-air compartment; The 6-steam nozzle; The 7-water jet; The 8-ajutage; The 9-fume pipe; The 10-charging aperture; Discharge gate on the 11-bed; The 12-air blast; The 13-afterburning chamber; The 14-heat exchanger; The 15-circulating fan.
The specific embodiment
Below in conjunction with accompanying drawing and embodiment concrete structure of the present invention, operation method and implementation method are discussed in detail.
As shown in Figure 1, the present invention includes control oxygen fluid bed 1, be arranged on the ajutage 8 and the air blast that links to each other with ajutage 12, afterburning chamber 13, heat exchanger 14, circulating fan 15 and fume pipe 15 of controlling oxygen fluid bed bottom.Afterburning chamber 13 imports link to each other with the exhanst gas outlet on control oxygen fluid bed 1 top, and afterburning chamber 13 outlets link to each other with heat exchanger 14, and heat exchanger 14 links to each other with control oxygen fluid bed 1 bottom air compartment 5 through fume pipe 9, and circulating fan 15 is set on fume pipe 9.
As shown in Figure 2, control oxygen fluid bed 1 of the present invention comprises upward discharge gate 11 of burner hearth 2, air distribution plate 4, air compartment 5, steam nozzle 6, water jet 7, charging aperture 10 and bed.Burner hearth 2 is divided into bottom emulsion zone 3 and top dilute-phase zone, and burner hearth 2 adopts variable section structure, and the upper furnace cross section is a rectangle, and lower furnace portion is the convergent terrace with edge; Or the upper furnace cross section is circular, and lower furnace portion is the frustum of a cone.Air distribution plate 4 is located at burner hearth 2 bottoms, i.e. emulsion zone 3 bottoms, the sectional area A of air distribution plate 4 place's burner hearths (being burner hearth bottom)
1Be upper furnace sectional area (being burner hearth dilute-phase zone sectional area) A
20.25～0.4 times, i.e. 0.25≤A
1: A
2≤0.4, both can guarantee that an amount of fluidizing agent gets into to make solid fuel keep fluidisation preferably, can make solid fuel after the fluidisation can in time separate to reduce again and carry secretly at open.Air distribution plate 4 bottoms connect air compartment 5, and air compartment 5 bottoms connect ajutage 8 and fume pipe 9, and air feeds air compartment 5 via air blast 12 from ajutage 8.Control oxygen fluid bed 1 gas fume after burning after process afterburning chamber 13 makes the combustible dust and fuel gas completing combustion that contains in the flue gas, gets into heat exchanger 14 and heat transferring medium (water or organic working medium) heat exchange cooling.Directly discharging of a flue gas part after the cooling; Another part is sent into air compartment 5 by blower fan 15 from fume pipe 9 and is mixed together as fluidizing agent with air and feeds burner hearth from air distribution plate; Through the ratio of regulation and control air capacity and exhaust gas volumn, the oxygen content that makes fluidizing agent is 5%～21%.The furnace wall of air distribution plate 4 tops is provided with water jet 7, and is bigger like control oxygen fluid bed sectional area, then need establish two and plural water jet 7 based on cooling.Air compartment 5 is provided with steam nozzle 6, and is bigger like control oxygen fluid bed sectional area, and two and plural steam nozzle 6 are set as required.Discharge gate 11 is located at the least significant end of air distribution plate 4 on the bed, is convenient to the bulk solid heat carrier is discharged burner hearth.Charging aperture 10 is located on the furnace wall with the discharge gate opposite side, in burner hearth dilute-phase zone bottom, avoids solid fuel to get into not reaching heating behind the burner hearth just being discharged from burner hearth.
The present invention is that a kind of inside all is the fluid bed of solid fuel (not having other inert bed materials); In this device, heat all solids fuel through a part of solid fuel that burns, heated unburnt solids fuel can be used as solid thermal carriers and is used for next operation and other material heat exchange.Because of fluidizing agent is an air, and, need the pairing combustion-supporting air quantity of solid fuel of burning greater than conduct as the air capacity of fluidizing agent for guaranteeing all solids fuel fluidisation in the bed.That is to say, need the burnt fuel amount relatively, air capacity is superfluous, then can consume the common fuel that this need not burn, and makes it participate in burning, causes solid fuel ignition excessive, and solid thermal carriers output reduces, and influences the stable operation of next operation.In addition, all be solid fuel in the bed, solid fuel Once you begin burns, and bed temperature raises rapidly, and wayward, and the temperature that causes solid thermal carriers is too high and coking does not meet the technological requirement or the normal operation of influence of next operation.Therefore in running, both the fuel combustion amount need be controlled, temperature in the stove need be controlled again.Therefore the operation method of above-mentioned fluidized bed combustor is:
1) solid fuel gets into burner hearth 2 from the charging aperture 10 of control oxygen fluid bed 1 continuously, not only acts as a fuel but also expect as bed.
2) air is sent into air compartment 5 by air blast 12 through ajutage 8, as fluidizing agent solid fuel is carried out fluidisation, and the igniter that is arranged in the burner hearth 2 is lighted solid fuel.
3) flue gas that contains combustible dust and fuel gas after the burning gets into afterburning chamber 13 makes combustible dust and the fuel gas completing combustion that contains in the flue gas, and the flue gas after the completing combustion gets into heat exchanger 14 and the heat transferring medium heat exchange is lowered the temperature.
4) directly discharging of the part of the flue gas after the cooling; Another part is sent into air compartment 5 by blower fan 15 from fume pipe 9 and is mixed together as fluidizing agent with air and feeds burner hearth from air distribution plate; Through regulating the ratio of air capacity and exhaust gas volumn; The oxygen content that makes fluidizing agent is 5%～21%, and the solid fuel in the burner hearth 2 is carried out the burning of control oxygen; Because fluidisation needs certain gas flow, be the required air quantity of assurance fluidisation, and prevent too much solid fuel participation burning, can not control burning by reducing air capacity, and can only realize through the oxygen content of adjusting gas fluidized medium, promptly control the oxygen burning.
5) under the control oxygen condition, in the solid fuel ignition process, the burner hearth emulsion zone is divided into two parts carries out temperature control, the lower area temperature of burner hearth emulsion zone is controlled at 850～1050 ℃, and the upper area temperature of emulsion zone is controlled to be 900～1100 ℃; Adjust and set according to the temperature of solid-fuelled classification and required solid thermal carriers.
6) under the control oxygen condition, have only the part solid fuel ignition in the control oxygen flow pool furnace thorax, solid fuel ignition produces all solids fuel in the heat burner hearth, obtains solid thermal carriers; Solid thermal carriers are discharge gate 11 discharges from the bed continuously.
7) under the control oxygen condition in the solid fuel ignition process; When the lower area temperature of burner hearth emulsion zone is higher than the control temperature; Spray into steam from steam nozzle 6, steam mixes with fluidizing agent at air compartment 5, is blown into from air distribution plate 4; To reduce the lower area temperature of burner hearth emulsion zone, prevent as the too high and coking of the fuel temperature of solid thermal carriers; When the temperature of the lower area of burner hearth emulsion zone and upper area is higher than the control temperature simultaneously; Spray water in burner hearth from steam nozzle 6 spraying steams with from water jet 7 simultaneously; Reduce rapidly the lower area temperature and the upper area temperature of burner hearth emulsion zone, prevent as the too high and coking of the fuel temperature of solid thermal carriers.
Different solid fuel, and the solid thermal carriers temperature of technological requirement is when different, corresponding fluidising air velocity and different in the foregoing description, promptly other fluidizing agent amount is different, and the temperature controlling value that sets simultaneously is that desired temperature is also different.
Embodiment with a Coal Chemical Industry process semicoke solid heat-carrying comes the present invention is done further explain below.
Present embodiment with the solid semicoke as solid fuel.Earlier the semicoke with release mesh adds in the burner hearths from charging aperture 10, and from air compartment 5 bubbling airs as fluidizing agent, make semicoke be in fluidized state, utilize the igniter that is located in the stove to light semicoke then and make its burning produce heat.Gas fume after burning gets into afterburning chamber 13 and makes combustible dust and the fuel gas completing combustion that contains in the flue gas, gets into heat exchanger 14 heat exchange cooling then.Directly discharging of a flue gas part after the cooling, another part is sent into air compartment 5 by blower fan 15 from fume pipe 9 and is mixed together as fluidizing agent with air.Heat owing to solid fuel ignition when just beginning heats all solid fuels inadequately, so the exhaust gas volumn in the fluidizing agent is less, and the oxygen content of fluidizing agent is higher.Along with the carrying out of burning, for control solid fuel ignition amount, increase the exhaust gas volumn in the fluidizing agent, reduce oxygen content.5%～21%, just the air quantity that fluidisation is required can be guaranteed according to the oxygen content of setting operating mode and needs adjusting gaseous mixture, too much solid fuel participation burning can be prevented again.Under the control oxygen condition, in the solid fuel ignition process, the burner hearth emulsion zone is divided into two parts carries out temperature control.In this embodiment, the upper area temperature controlling value of controlling oxygen fluid bed internal furnace emulsion zone is made as 1000 ℃, the lower area temperature controlling value of burner hearth emulsion zone is made as 900～920 ℃.In the process of coal-char combustion, all semicokes in the heat stove of generation all can raise emulsion zone lower area and upper area temperature.Surpass 900～920 ℃ that set when the lower area temperature of emulsion zone; And the temperature of burner hearth emulsion zone upper area adopts basic temperature adjustment means when not being higher than 1000 ℃, and promptly the steam nozzle 6 from the air compartment 5 sprays into steam; Mix with gas fluidized medium; Be blown into from air distribution plate, reduce emulsion zone lower area temperature, make them in 900～920 ℃.If but ratio of combustion is more vigorous, in the process that basic temperature adjustment means are implemented, burner hearth emulsion zone temperature still continues to rise; When emulsion zone upper area temperature has surpassed 1000 ℃, when using basic temperature adjustment means, must start auxiliary urgent temperature adjustment means; Promptly the steam nozzle 6 from the air compartment 5 sprays into steam; Mix with gas fluidized medium, be blown into, spray water in burner hearth from water jet 7 simultaneously from air distribution plate; Reduce rapidly the temperature of emulsion zone upper area and lower area, two kinds of means combinations make the temperature of emulsion zone lower area reach 900～920 ℃, the temperature of emulsion zone upper area to be lower than 1000 ℃.Solid fuel fluidisation in burner hearth is kicked up behind the bigger dilute-phase zone of sectional area, and fluidising air velocity reduces, and the solid fuel of kicking up falls back to emulsion zone.Solid fuel is heated to 900 ℃ as the unburned semicoke of solid thermal carriers in fluid mapper process, discharge gate 11 is discharged from the bed, supplies with next operation.
Claims (4)
1. control the oxygen flow bed system for one kind; Said system comprises control oxygen fluid bed (1), is arranged on the ajutage (8) and the air blast that links to each other with ajutage (12) of control oxygen fluid bed bottom; Said control oxygen fluid bed comprises burner hearth (2), air distribution plate (4), be arranged on discharge gate (11) on air compartment (5), charging aperture (10) and the bed of air distribution plate below; It is characterized in that: said system also comprises afterburning chamber (13), heat exchanger (14), circulating fan (15) and fume pipe (9); Afterburning chamber (13) import links to each other with the exhanst gas outlet on control oxygen fluid bed (1) top; Afterburning chamber (13) outlet links to each other with heat exchanger (14), and heat exchanger (14) links to each other with control oxygen fluid bed (1) bottom air compartment (5) through fume pipe (9), and circulating fan (15) is set on fume pipe (9); Water jet (7) is set on the furnace wall of emulsion zone above the air distribution plate; In air compartment (5), be provided with steam nozzle (6).
2. a kind of control oxygen flow bed system according to claim 1, it is characterized in that: the upper furnace cross section of said control oxygen fluid bed (1) is a rectangle, lower furnace portion is the convergent terrace with edge; Or the upper furnace cross section is circular, and lower furnace portion is the frustum of a cone; The sectional area A of air distribution plate place burner hearth
1Be upper furnace sectional area A
20.25～0.4 times.
3. a kind of control oxygen flow bed system according to claim 1 and 2 is characterized in that: said water jet (7) adopts more than two; Said steam nozzle (6) adopts more than two.
4. adopt a kind of control oxygen flow bed operating method of system according to claim 1, it is characterized in that this method comprises the steps:
1) makes solid fuel get into burner hearth (2) from the charging aperture (10) of control oxygen fluid bed (1) continuously, not only act as a fuel but also expect as bed;
2) air is sent into air compartment (5) by air blast (12) through ajutage (8), makes solid fuel fluidisation and burning as fluidizing agent;
3) flue gas that contains combustible dust and fuel gas after the burning gets into afterburning chamber (13), the completing combustion in afterburning chamber of combustible dust and fuel gas, and the flue gas after the completing combustion gets into heat exchanger (14) and the heat transferring medium heat exchange is lowered the temperature;
4) directly discharging of the part of the flue gas after the cooling; Another part is sent into air compartment (5) and air by circulating fan (15) from fume pipe (9) and is mixed together as fluidizing agent and feeds burner hearth from air distribution plate; Through regulating the ratio of air capacity and exhaust gas volumn, the oxygen content that makes fluidizing agent is 5%～21%;
5) under the control oxygen condition, in the solid fuel ignition process, the burner hearth emulsion zone is divided into two parts carries out temperature control, the lower area temperature of burner hearth emulsion zone is controlled at 850～1050 ℃, and the upper area temperature of emulsion zone is controlled to be 900～1100 ℃; When the lower area temperature of burner hearth emulsion zone is higher than the control temperature; Spray into steam from steam nozzle (6), steam mixes with fluidizing agent at air compartment (5), is blown into from air distribution plate (4); To reduce the lower area temperature of burner hearth emulsion zone, prevent as the too high and coking of the fuel temperature of solid thermal carriers; When the temperature of the lower area of burner hearth emulsion zone and upper area is higher than the control temperature simultaneously; Spray water in burner hearth from steam nozzle (6) spraying steam with from water jet (7) simultaneously; Reduce rapidly the lower area temperature and the upper area temperature of burner hearth emulsion zone, prevent as the too high and coking of the fuel temperature of solid thermal carriers;
6) under the control oxygen condition, have only the part solid fuel ignition in the control oxygen flow pool furnace thorax, solid fuel ignition produces all solids fuel in the heat burner hearth, obtains solid thermal carriers; Solid thermal carriers are discharge gate (11) discharge from the bed continuously.
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Cited By (9)
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| CN102798131A (en) * | 2012-09-07 | 2012-11-28 | 中国东方电气集团有限公司 | Boiler capable of preventing contaminating and coking |
| CN103471093A (en) * | 2013-09-06 | 2013-12-25 | 中国科学院工程热物理研究所 | Air distribution method of oxygen-enriched combustion of circulating fluidized bed |
| WO2015171710A1 (en) * | 2014-05-09 | 2015-11-12 | C2O Technologies, Llc | Coal char passivation process and apparatus |
| CN109735371A (en) * | 2019-02-13 | 2019-05-10 | 浙江大学 | A biomass circulating fluidized bed direct-fired boiler and its coupled power generation co-generation activated carbon system with a gasifier |
| CN109882830A (en) * | 2019-01-24 | 2019-06-14 | 国网浙江省电力有限公司电力科学研究院 | An operating method for adjusting the steam temperature of a biomass circulating fluidized bed boiler |
| CN111156500A (en) * | 2018-11-08 | 2020-05-15 | 中国科学院工程热物理研究所 | Powder feeding method and device for preheating chamber of circulating fluidized bed and fuel processing device |
| CN111237746A (en) * | 2020-03-04 | 2020-06-05 | 山东永能节能环保服务股份有限公司 | Biomass circulating fluidized bed boiler |
| CN111706857A (en) * | 2020-06-02 | 2020-09-25 | 西安交通大学 | A low NOx emission variable cross-section circulating fluidized bed staged combustion boiler system and method |
| CN115846372A (en) * | 2022-12-14 | 2023-03-28 | 亚德（上海）环保系统有限公司 | Waste salt treatment type pyrolysis device with coke block treatment function and working method thereof |
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| US4836116A (en) * | 1987-12-17 | 1989-06-06 | The Technical University Of Nova Scotia | Fluidized bed combustion system |
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| CN102798131B (en) * | 2012-09-07 | 2016-04-06 | 中国东方电气集团有限公司 | A kind of boiler preventing contamination coking |
| CN102798131A (en) * | 2012-09-07 | 2012-11-28 | 中国东方电气集团有限公司 | Boiler capable of preventing contaminating and coking |
| US10174937B2 (en) | 2013-09-06 | 2019-01-08 | Institute Of Engineering Thermophysics, Chinese Academy Of Sciences | Method for distributing gas for oxy-fuel combustion in circulating fluidized bed |
| CN103471093B (en) * | 2013-09-06 | 2016-02-24 | 中国科学院工程热物理研究所 | The air distribution method of recirculating fluidized bed oxygen-enriched combusting |
| CN103471093A (en) * | 2013-09-06 | 2013-12-25 | 中国科学院工程热物理研究所 | Air distribution method of oxygen-enriched combustion of circulating fluidized bed |
| WO2015171710A1 (en) * | 2014-05-09 | 2015-11-12 | C2O Technologies, Llc | Coal char passivation process and apparatus |
| US10119089B2 (en) | 2014-05-09 | 2018-11-06 | C2O Technologies, Llc | Coal char passivation process and apparatus |
| US20190071614A1 (en) * | 2014-05-09 | 2019-03-07 | C2O Technologies, Llc | Coal char passivation process and apparatus |
| CN111156500A (en) * | 2018-11-08 | 2020-05-15 | 中国科学院工程热物理研究所 | Powder feeding method and device for preheating chamber of circulating fluidized bed and fuel processing device |
| CN109882830A (en) * | 2019-01-24 | 2019-06-14 | 国网浙江省电力有限公司电力科学研究院 | An operating method for adjusting the steam temperature of a biomass circulating fluidized bed boiler |
| CN109735371A (en) * | 2019-02-13 | 2019-05-10 | 浙江大学 | A biomass circulating fluidized bed direct-fired boiler and its coupled power generation co-generation activated carbon system with a gasifier |
| CN111237746A (en) * | 2020-03-04 | 2020-06-05 | 山东永能节能环保服务股份有限公司 | Biomass circulating fluidized bed boiler |
| CN111706857A (en) * | 2020-06-02 | 2020-09-25 | 西安交通大学 | A low NOx emission variable cross-section circulating fluidized bed staged combustion boiler system and method |
| CN115846372A (en) * | 2022-12-14 | 2023-03-28 | 亚德（上海）环保系统有限公司 | Waste salt treatment type pyrolysis device with coke block treatment function and working method thereof |
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