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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Abstract
The invention relates to an oxygen-controlled fluid bed system and an operational method thereof. The oxygen-controlled fluid bed system comprises an oxygen-controlled fluid bed, a blast blower, an afterburning chamber, a heat exchanger and a fan, wherein the oxygen-controlled fluid bed comprises a furnace cavity, a grid plate, an air chamber, a feed port and an on-bed discharge port, wherein the furnace cavity adopts a variable cross-section structure, and the sectional area A1 of the furnace cavity at the grid plate is 0.25-0.4 times of the sectional area A2 of the upper part of the furnace cavity; a dense-phase region above the grid plate is provided with two or more water spouts on a furnace wall, and the air chamber is provided with two or more steam spouts; the fluid bed uses solid fuel as a bed material; air and fume are mixed to form a gas fluidizing medium with the oxygen content of 5-21%, and the solid fuel is fluidized and partially combusted; and steaming and spraying water are used as means of temperature regulation, which effectively ensures that the bed temperature and the furnace cavity temperature are within the range of set values, and avoids carrier from coking due to an excess temperature. According to the invention, the fluid bed system has the characteristics of full fuel combustion without a bed material, which ensures the purity of a solid heat carrier. In addition, oxygen control measures and bed temperature control measures can effectively control the quantity of fuel combustion, and ensures stability in 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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| 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 kind of biomass circulating fluidized bed direct-combustion boiler and its with gasification furnace coupled electricity-generation co-producing active carbon system |
| 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 | A kind of operation method adjusting biomass recirculating fluidized bed boiler vapor (steam) temperature |
| 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 |
| CN111706857A (en) * | 2020-06-02 | 2020-09-25 | 西安交通大学 | Low-NOx-emission variable-section circulating fluidized bed staged combustion boiler system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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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 |
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| 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 | A kind of operation method adjusting biomass recirculating fluidized bed boiler vapor (steam) temperature |
| CN109735371A (en) * | 2019-02-13 | 2019-05-10 | 浙江大学 | A kind of biomass circulating fluidized bed direct-combustion boiler and its with gasification furnace coupled electricity-generation co-producing active carbon system |
| CN111706857A (en) * | 2020-06-02 | 2020-09-25 | 西安交通大学 | Low-NOx-emission variable-section circulating fluidized bed staged combustion boiler system and method |
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