CN103604121A - Oil shale semicoke fluidized bed combustion system adopting triple-channel shunting control refeeder - Google Patents
Oil shale semicoke fluidized bed combustion system adopting triple-channel shunting control refeeder Download PDFInfo
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- CN103604121A CN103604121A CN201310620445.5A CN201310620445A CN103604121A CN 103604121 A CN103604121 A CN 103604121A CN 201310620445 A CN201310620445 A CN 201310620445A CN 103604121 A CN103604121 A CN 103604121A
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- 239000004058 oil shale Substances 0.000 title claims abstract description 66
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 34
- 239000002893 slag Substances 0.000 claims abstract description 32
- 239000000571 coke Substances 0.000 claims description 38
- 239000000463 material Substances 0.000 claims description 33
- 238000005192 partition Methods 0.000 claims description 31
- 238000010438 heat treatment Methods 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 238000009826 distribution Methods 0.000 claims description 10
- 239000012530 fluid Substances 0.000 claims description 7
- 230000005587 bubbling Effects 0.000 abstract description 4
- 239000000446 fuel Substances 0.000 abstract description 2
- 239000000779 smoke Substances 0.000 abstract 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 21
- 239000003546 flue gas Substances 0.000 description 21
- 238000007599 discharging Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 10
- 239000000203 mixture Substances 0.000 description 10
- 238000000926 separation method Methods 0.000 description 6
- 235000014171 carbonated beverage Nutrition 0.000 description 5
- 230000003134 recirculating effect Effects 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 239000003079 shale oil Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 3
- 238000012216 screening Methods 0.000 description 3
- 239000004566 building material Substances 0.000 description 2
- 239000004567 concrete Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
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- 239000003245 coal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
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- 230000000630 rising effect Effects 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention provides an oil shale semicoke fluidized bed combustion system adopting a triple-channel shunting control refeeder. The oil shale semicoke fluidized bed combustion system comprises a semicoke conveying pipe (1), a hearth (2), a stock bin (3), a feeding machine (4), a primary air box (5), a slag cooler (6), a secondary air port (7), the triple-channel shunting control refeeder (8), a riser pipe (9), a steam pocket (10), a separator (11), a tail smoke channel (12), an ash cooler (13), an air preheater (14), a deduster (15) and a smoke pipe (16). The triple-channel shunting control refeeder (8) is adopted for performing directional control on an ash returning path; the whole system can effectively switch between different operating states (a bubbling fluidized bed and a circulating fluidized bed), so that the combustion system has high combustion efficiency, and also has stable fuel ignition characteristic, and thus the efficient and clean combustion utilization of oil shale semicoke can be realized within a large calorific value range.
Description
Technical field
The present invention relates to a kind of oil shale semi-coke fluidized bed combustion syste that adopts triple channel flow-dividing control material returning device, can be according to entering the thin slag heat value of mixture size of furnace oil shale semicockes or oil shale semi-coke and oil shale, by triple channel flow-dividing control material returning device, change returning charge ash path, thereby in more wide in range thermal value range, realize efficient, the clean combustion utilization of oil shale semi-coke, the invention belongs to low-calorific-value solid fuel field of combustion technology.
Background technology
Oil shale is a kind of high ash content, the organic ore body of low-calorie solid combustible, is close-grained black or brown sheet, and low temperature distillation can obtain the shale oil of similar natural oil.According to current global oil shale resources reserve statistics result, it is converted to shale oil, can reach more than 4,000 hundred million tons, be equivalent to current world natural crude oil and verify 5.4 times of recoverable reserves; Its reserves are converted to caloric value and are only second to coal and row second.Wherein, China's oil shale resources proved reserves are converted into shale oil and are about 2,400,000,000 tons.Therefore,, from reserves and value, oil shale is rising important alternative energy source.Along with the relative reduction of the relative cost of crude oil production of oil shale retorting cost, oil shale with its huge reserves, more causes global concern as a kind of important alternative energy source.The Devoting Major Efforts To Developing of oil shale resources, for China alleviate energy shortage pressure, the strategy that promotes economic sustainable and healthy development, energy development diversification is significant.The exploitation of oil shale at present mainly be take destructive distillation extraction shale oil as main.The solid matter generating after oil shale retorting is called oil shale semi-coke.Oil shale semi-coke is containing the organic matter of some and compared with the ash content of great share, due to the difference in distillation process condition and original oil shale physical property, causes after destructive distillation the calorific value fluctuation of semicoke larger, approximately 2500 ~ 5000kJ/kg.For low heat value (being less than 3600kJ/kg) semicoke, because heat is difficult to develop, the thin slag of oil shale conventionally and after screening is together backfilling in exploitation pond, and environmental pollution is larger.If can be to the exploitation of burning of low heat value semicoke, the oil shale waste slag producing after burning can be used as cement additire and realizes comprehensive utilization.Meanwhile, the heat energy that burning produces can also provide the thermal mediums such as hot blast, hot flue gas, can meet the requirement of different process.Therefore, how, when guaranteeing high heating value oil shale semi-coke utilization rate, strengthening the exploitation to low heat value oil shale semi-coke, is a problem in the urgent need to address.Not yet there is at present correlation technique openly to report.
Summary of the invention
The object of the invention is to for prior art not enough, a kind of oil shale semi-coke fluidized bed combustion syste that adopts triple channel flow-dividing control material returning device is proposed, when guaranteeing that high heating value coal-char combustion utilizes, take into account burning utilization to low heat value semicoke (minimum can pure combustion calorific value 2500kJ/kg oil shale semi-coke), realize efficient, the clean utilization of oil shale semi-coke.
For realizing this purpose, in fluidized bed combustion syste of the present invention, in burner hearth, do not arrange any heating surface, for difference, enter the oil shale semi-coke of stove calorific value and the mixture of oil shale semi-coke and the thin slag of oil shale, adopting triple channel flow-dividing control material returning device to carry out orientation to returning charge ash path controls, whole system can effectively be switched between different running status (bubbling fluidized bed and recirculating fluidized bed), make burner both there is higher efficiency of combustion, there is again more stable fuel fire characteristic, thereby in larger thermal value range, realize the efficient of oil shale semi-coke, clean combustion utilizes.
A kind of oil shale semi-coke fluidized bed combustion syste that adopts triple channel flow-dividing control material returning device involved in the present invention, comprises semicoke carrier pipe, burner hearth, feed bin, batcher, wind bellows, slag cooler, overfiren air port, triple channel flow-dividing control material returning device, standpipe, drum, separator, back-end ductwork, device for cooling ash, air preheater, deduster, chimney.Because oil shale semi-coke calorific value is very low, for guaranteeing the smooth combustion operating mode in burner hearth, in burner hearth, do not arrange any heating surface.By adopting triple channel flow-dividing control material returning device, regulate ash amount and the ash temperature of the returning charge ash that enters burner hearth, control the ignition temperature of burner hearth, reclaim the heat of returning charge ash simultaneously.Triple channel flow-dividing control material returning device is comprised of three returning charge storehouses (one storehouse, returning charge storehouse, two storehouses, returning charge storehouse and three storehouses, returning charge storehouse) and a heat exchange storehouse, the returning charge ash that separator separates is in first standpipe enters two storehouses, returning charge storehouse, according to combustion conditions different in burner hearth, in conjunction with the difference of different lime-ash mobile (overflow or underflow) and partition wall height, by blast cap air distribution, realize the mobile orientation of returning charge ash is controlled.In heat exchange storehouse, be provided with the pipe laying tube bank of being heated, being subject to hot working fluid is saturation water or subcooled water.The Area Ratio of burner hearth air distribution plate and triple channel flow-dividing control material returning device heat exchange storehouse air distribution plate is 0.5 ~ 2.Difference in height between the low partition wall of the returning charge storehouse one high partition wall in storehouse and heat exchange storehouse is 100mm ~ 500mm.
Principle of the present invention and the course of work are as follows:
Oil shale semi-coke after destructive distillation directly enters in burner hearth and burns through semicoke carrier pipe, and the thin slag of oil shale (being less than 3mm) producing after screening is stored in feed bin, by batcher, sends into burner hearth internal combustion.Combustion temperature in hearth is 800 ℃ ~ 950 ℃, according to entering the thin slag heat value of mixture of furnace oil shale semicockes and oil shale semi-coke and oil shale, by triple channel flow-dividing control material returning device, returning charge ash flow path being carried out to orientation controls, thereby in wide in range thermal value range, realize efficient, the clean utilization of semicoke.Concrete mode is:
When oil shale semi-coke or oil shale semi-coke and the thin slag heat value of mixture of oil shale are 2500kJ/kg ~ 3600kJ/kg, in burner hearth, in bubbling fluidized bed state, flue gas carries a small amount of flying dust and enters high-temperature separator.First the returning charge ash that separator separates enters two storehouses, returning charge storehouse of triple channel flow-dividing control material returning device through standpipe.Now one storehouse, returning charge storehouse, two storehouses, returning charge storehouse and three storehouses, returning charge storehouse are all in fluidized state, and heat exchange storehouse is in fluidized state not.Returning charge ash enters one storehouse, returning charge storehouse and three storehouses, returning charge storehouse in underflow mode through underflow partition wall.Returning charge storehouse is provided with ash discharging hole in three storehouses, and all returning charge ash is in ash discharging hole enters the device for cooling ash that is fluid bed state.The heat exchanger tube that now first the required air of hearth combustion enters in device for cooling ash carries out heat exchange with the heat ash from three storehouses, returning charge storehouse, air preheater and high-temperature flue gas that air after heating continues to enter in back-end ductwork carry out heat exchange, air after heat exchange enters in the heat exchanger tube in the portable slag cooler of being with vibration, choke preventing function, and the high temperature bottom slag of discharging with burner hearth carries out heat exchange.The high temperature air completing after heat exchange all enters wind bellows one time as fluidized wind.Convection heating surface and high-temperature flue gas that first feedwater enters in back-end ductwork carry out heat exchange, and the hot water producing after heat exchange directly can be used as user's process water.
When oil shale semi-coke or oil shale semi-coke and the thin slag heat value of mixture of oil shale are greater than 3600kJ/kg and the grey temperature of returning charge and are greater than 600 ℃, first the returning charge ash that separator separates enters two storehouses, returning charge storehouse of triple channel flow-dividing control material returning device through standpipe.Now one storehouse, returning charge storehouse, two storehouses, returning charge storehouse, three storehouses, returning charge storehouse and heat exchange storehouse are all in fluidized state, and returning charge ash enters in heat exchange storehouse by the underflow hole between three storehouses, returning charge storehouse and heat exchange storehouse.Because the partition wall height of the low partition wall in heat exchange storehouse is low compared with the partition wall height of the returning charge storehouse one high partition wall in storehouse, so returning charge ash can not return in burner hearth through high partition wall in overflow mode from one storehouse, returning charge storehouse, can only in overflow mode, through low partition wall, return in burner hearth from heat exchange storehouse.Now burner hearth operates in recirculating fluidized bed state.According to combustion temperature in hearth, the circulating ash in heat exchange storehouse can all be returned to burner hearth, also can partly return to burner hearth.When returning charge ash part is returned to burner hearth, remaining returning charge ash also can enter in the device for cooling ash that is fluid bed state.The heat exchanger tube that first the required air that burns enters in device for cooling ash carries out heat exchange (if device for cooling ash puts into operation) with the heat ash from heat exchange storehouse, or air preheater and high-temperature flue gas that burning required air directly enters in back-end ductwork through air bypass carry out heat exchange (if device for cooling ash does not put into operation), the air completing after heat exchange enters in the heat exchanger tube in the portable slag cooler of being with vibration, choke preventing function, and the high temperature bottom slag of discharging with burner hearth carries out heat exchange.The high temperature air part completing after heat exchange enters in burner hearth from overfiren air port as Secondary Air, and another part directly enters wind bellows one time as fluidized wind.Convection heating surface and high-temperature flue gas that first feedwater enters in back-end ductwork carry out heat exchange, first feedwater after heat exchange enters drum, pipe laying heating surface influent header, the pipe laying that high-temperature water in drum is flowed through in heat exchange storehouse be successively heated tube bank, pipe laying heating surface outlet header, carry out heat exchange with the returning charge ash in heat exchange storehouse, the steam water interface producing after heat exchange is got back in drum and is carried out carbonated drink separation, and the final steam producing can be used as user's process steam (as dry, heating, generating etc.).
When oil shale semi-coke or oil shale semi-coke and the thin slag heat value of mixture of oil shale are greater than 3600kJ/kg and the grey temperature of returning charge and are less than 600 ℃, first the returning charge ash that separator separates enters two storehouses, returning charge storehouse of triple channel flow-dividing control material returning device through standpipe.Now one storehouse, returning charge storehouse, two storehouses, returning charge storehouse and three storehouses, returning charge storehouse are all in fluidized state, and heat exchange storehouse is in fluidized state not.Returning charge ash enters one storehouse, returning charge storehouse and three storehouses, returning charge storehouse in underflow mode through underflow partition wall.Ash discharging hole in three storehouses, returning charge storehouse is in closed condition, and all returning charge ash returns in burner hearth through high partition wall in overflow mode from one storehouse, returning charge storehouse.Now burner hearth operates in recirculating fluidized bed state, and the heat exchange storehouse of device for cooling ash and triple channel flow-dividing control material returning device is in shut down condition.Air preheater and high-temperature flue gas that the required air that burns directly enters in back-end ductwork through air bypass carry out heat exchange, the air completing after heat exchange enters the heat exchanger tube in the portable slag cooler of being with vibration, choke preventing function, and the high temperature bottom slag of discharging with burner hearth carries out heat exchange.The high temperature air part completing after heat exchange enters in burner hearth from overfiren air port as Secondary Air, and another part directly enters wind bellows one time as fluidized wind.Convection heating surface and high-temperature flue gas that first feedwater enters in back-end ductwork carry out heat exchange, the steam water interface producing after heat exchange enters and in drum, carries out carbonated drink separation, the process steam that the final hot water producing and part steam can be used as user (as dry, heating, generating etc.).
In above-mentioned three kinds of situations, the high-temperature flue gas that burning produces, after separator carries out gas solid separation, carries out heat exchange successively with the heating surface in back-end ductwork, and the flue gas that completes heat exchange enters atmosphere by chimney after deduster dedusting.The ash temperature that slag cooler and device for cooling ash are discharged, all not higher than 150 ℃, is sent in ash silo with the flying dust that deduster is caught, in the lump as building materials deposit.
Advantage of the present invention is: (1), by adopting triple channel flow-dividing control material returning device, regulates ash amount and the ash temperature of the returning charge ash that enters burner hearth, thereby controls the ignition temperature of burner hearth; Make full use of the difference of mobile (overflow or the underflow) characteristic of lime-ash and partition wall height simultaneously, by blast cap air distribution, realize the mobile orientation of returning charge ash is controlled.Strengthening the different adaptive whiles of calorific value semicoke, take into account different process energy requirements, and whole fluidized bed combustion syste is simple, efficient, workable; (2) strengthen the UTILIZATION OF VESIDUAL HEAT IN to tail flue gas, end slag, returning charge ash, arrange that multi-stage heat exchanger reclaims above-mentioned waste heat and final foldback melts down thorax, guaranteed to the full extent the continous-stable burning of low heat value semicoke in stove; (3) by what change device for cooling ash, enter grey mode (enter ash and enter ash from heat exchange storehouse from three storehouses, returning charge storehouse) and the heat exchange storehouse of whether putting into operation, can not only regulate greatly combustion temperature in hearth, also can regulate to a certain extent the heat absorption ratio of working medium (carbonated drink or air), thereby improve burner to the adaptability of different calorific value semicokes and further meet the particular requirement of user's technique to variety of energy sources (hot water, steam, high temperature air, high-temperature flue gas etc.).(4) adopt fluidized bed combustion to develop and utilize oil shale semi-coke, efficiency of combustion is high and belong to low-temperature burning, can effectively control NO
xand SO
2generation and discharge, be conducive to keep the activity of lime-ash simultaneously.(5) native system is equally applicable to have with oil shale semi-coke the low-calorific-value solid fuel of similar physical property.
accompanying drawing explanation:
Fig. 1 is system architecture schematic diagram of the present invention;
Fig. 2 is the A-A cutaway view of Fig. 1;
Fig. 3 is the structural representation of triple channel flow-dividing control material returning device;
Fig. 4 is the B-B cutaway view of Fig. 3;
In above-mentioned figure, 1 is semicoke carrier pipe, 2 is burner hearth, 3 is feed bin, 4 is batcher, 5 is wind bellows, 6 is slag cooler, 7 is overfiren air port, 8 is triple channel flow-dividing control material returning device, 8-1 is pipe laying heating surface influent header, 8-2 is pipe laying heating surface outlet header, 8-3 is heat exchange storehouse, 8-4 is the pipe laying tube bank of being heated, 8-5 is underflow hole, 8-6 is three storehouses, returning charge storehouse, 8-7 is ash discharging hole, 8-8 is two storehouses, returning charge storehouse, 8-9 is underflow partition wall, 8-10 is blast cap, 8-11 is one storehouse, returning charge storehouse, 8-12 is high partition wall, 8-13 is low partition wall, 9 is standpipe, 10 is drum, 11 is separator, 12 is back-end ductwork, 13 is device for cooling ash, 14 is air preheater, 15 is deduster, 16 is chimney.
the specific embodiment:
Below in conjunction with Figure of description, technical scheme of the present invention is further described.
A kind of oil shale semi-coke fluidized bed combustion syste that adopts triple channel flow-dividing control material returning device, as shown in Figure 1, Figure 2, Figure 3, Figure 4, this system comprises semicoke carrier pipe 1, burner hearth 2, feed bin 3, batcher 4, wind bellows 5, slag cooler 6, overfiren air port 7, triple channel flow-dividing control material returning device 8, standpipe 9, drum 10, separator 11, back-end ductwork 12, device for cooling ash 13, air preheater 14, deduster 15, chimney 16.Because oil shale semi-coke calorific value is very low, for guaranteeing the smooth combustion operating mode in burner hearth 2, in burner hearth 2, do not arrange any heating surface.By adopting triple channel flow-dividing control material returning device 8, regulate ash amount and the ash temperature of the returning charge ash that enters burner hearth, control the ignition temperature of burner hearth 2, reclaim the heat of returning charge ash simultaneously.Triple channel flow-dividing control material returning device 8 is comprised of three returning charge storehouses (returning charge storehouse one storehouse 8-11, returning charge storehouse two storehouse 8-8 and returning charge storehouse three storehouse 8-6) and a heat exchange storehouse 8-3, the returning charge ash that separator 11 separates is in first standpipe 9 enters returning charge storehouse two storehouse 8-8, according to the interior different combustion conditions of burner hearth 2, in conjunction with the difference of different lime-ash mobile (overflow or underflow) and partition wall height, by blast cap 8-10 air distribution, realize the mobile orientation of returning charge ash is controlled.In the 8-3 of heat exchange storehouse, be provided with pipe laying be heated tube bank 8-4, being subject to hot working fluid is saturation water or subcooled water.The Area Ratio of burner hearth 2 air distribution plates and triple channel flow-dividing control material returning device 8 heat exchange storehouse air distribution plates is 0.5 ~ 2.Difference in height between the returning charge storehouse high partition wall 8-12 of one storehouse 8-11 and the low partition wall 8-13 of heat exchange storehouse 8-3 is 100mm ~ 500mm.
Principle and the course of work of native system are as follows:
Oil shale semi-coke after destructive distillation burns in semicoke carrier pipe 1 directly enters burner hearth 2, and the thin slag of oil shale (being less than 3mm) producing after screening is stored in feed bin 3, by batcher 4, sends into burner hearth 2 internal combustion.Burner hearth 2 ignition temperatures are 800 ℃ ~ 950 ℃, according to entering the thin slag heat value of mixture of furnace oil shale semicockes and oil shale semi-coke and oil shale, by 8 pairs of returning charge ash flow paths of triple channel flow-dividing control material returning device, carrying out orientation controls, thereby in wide in range thermal value range, realize efficient, the clean utilization of semicoke.Concrete mode is:
When oil shale semi-coke or oil shale semi-coke and the thin slag heat value of mixture of oil shale are 2500kJ/kg ~ 3600kJ/kg, in burner hearth 2, in bubbling fluidized bed state, flue gas carries a small amount of flying dust and enters high-temperature separator 11.First the returning charge ash that separator 11 separates enters the returning charge storehouse two storehouse 8-8 of triple channel flow-dividing control material returning device 8 through standpipe 9.Now returning charge storehouse one storehouse 8-11, returning charge storehouse two storehouse 8-8 and returning charge storehouse three storehouse 8-6 are all in fluidized state, and heat exchange storehouse 8-3 is in fluidized state not.Returning charge ash enters returning charge storehouse one storehouse 8-11 and returning charge storehouse three storehouse 8-6 in underflow mode through underflow partition wall 8-9.In the three storehouse 8-6 of returning charge storehouse, be provided with ash discharging hole 8-7, all returning charge ash is in ash discharging hole 8-7 enters the device for cooling ash 13 that is fluid bed state.The heat exchanger tube that first the required air of now burner hearth 2 burning enters in device for cooling ash 13 carries out heat exchange with the heat ash from returning charge storehouse three storehouse 8-6, the air preheater 14 that air after heating continues to enter in back-end ductwork 12 carries out heat exchange with high-temperature flue gas, air after heat exchange enters in the heat exchanger tube in the portable slag cooler 6 of being with vibration, choke preventing function, and the high temperature bottom slag of discharging with burner hearth 2 carries out heat exchange.The high temperature air completing after heat exchange all enters wind bellows 5 one time as fluidized wind.Convection heating surface and high-temperature flue gas that first feedwater enters in back-end ductwork 12 carry out heat exchange, and the hot water producing after heat exchange directly can be used as user's process water.
When oil shale semi-coke or oil shale semi-coke and the thin slag heat value of mixture of oil shale are greater than 3600kJ/kg and the grey temperature of returning charge and are greater than 600 ℃, first the returning charge ash that separator 11 separates enters the returning charge storehouse two storehouse 8-8 of triple channel flow-dividing control material returning device 8 through standpipe 9.Now returning charge storehouse one storehouse 8-11, returning charge storehouse two storehouse 8-8, returning charge storehouse three storehouse 8-6 and heat exchange storehouse 8-3 are all in fluidized state, and returning charge ash enters in the 8-3 of heat exchange storehouse by the underflow hole between returning charge storehouse three storehouse 8-6 and heat exchange storehouse 8-3.Because the partition wall height of the low partition wall 8-13 of heat exchange storehouse 8-3 is low compared with the partition wall height of the high partition wall 8-12 of returning charge storehouse one storehouse 8-11, therefore returning charge ash can not return in burner hearth 2 through high partition wall 8-12 in overflow mode by one storehouse 8-11 from returning charge storehouse, can only in overflow mode, through low partition wall 8-13, return in burner hearth 2 from heat exchange storehouse 8-3.Now burner hearth 2 operates in recirculating fluidized bed state.According to burner hearth 2 ignition temperatures, the circulating ash in the 8-3 of heat exchange storehouse can all be returned to burner hearth 2, also can partly return to burner hearth 2.When returning charge ash part is returned to burner hearth 2, remaining returning charge ash also can enter in the device for cooling ash 13 that is fluid bed state.The heat exchanger tube that first the required air that burns enters in device for cooling ash 13 carries out heat exchange (if device for cooling ash 13 puts into operation) with the heat ash from heat exchange storehouse 8-3, or the air preheater 14 of burning required air in air bypass directly enters back-end ductwork 12 carries out heat exchange (if device for cooling ash 13 does not put into operation) with high-temperature flue gas, the high temperature air part completing after heat exchange enters in burner hearth 2 from overfiren air port 7 as Secondary Air, and another part directly enters wind bellows 5 one time as fluidized wind.Convection heating surface and high-temperature flue gas that first feedwater enters in back-end ductwork 12 carry out heat exchange, first feedwater after heat exchange enters drum 10, pipe laying heating surface influent header 8-1, the pipe laying that high-temperature water in drum 10 is flowed through in heat exchange storehouse be successively heated tube bank 8-4, pipe laying heating surface outlet header 8-2, carry out heat exchange with the returning charge ash in the 8-3 of heat exchange storehouse, the steam water interface producing after heat exchange is got back in drum 10 and is carried out carbonated drink separation, and the final steam producing can be used as user's process steam (as dry, heating, generating etc.).
When oil shale semi-coke or oil shale semi-coke and the thin slag heat value of mixture of oil shale are greater than 3600kJ/kg and the grey temperature of returning charge and are less than 600 ℃, first the returning charge ash that separator 11 separates enters the returning charge storehouse two storehouse 8-8 of triple channel flow-dividing control material returning device 8 through standpipe 9.Now returning charge storehouse one storehouse 8-11, returning charge storehouse two storehouse 8-8 and returning charge storehouse three storehouse 8-6 are all in fluidized state, and heat exchange storehouse 8-3 is in fluidized state not.Returning charge ash enters returning charge storehouse one storehouse 8-11 and returning charge storehouse three storehouse 8-6 in underflow mode through underflow partition wall 8-9.Ash discharging hole in the three storehouse 8-6 of returning charge storehouse is in closed condition, and all from returning charge storehouse, one storehouse 8-11 returns in burner hearth 2 through high partition wall 8-12 in overflow mode returning charge ash.Now burner hearth 2 operates in recirculating fluidized bed state, and the heat exchange storehouse 8-3 of device for cooling ash 13 and triple channel flow-dividing control material returning device 8 is in shut down condition.The air preheater 14 of required air in air bypass directly enters back-end ductwork 12 that burn carries out heat exchange with high-temperature flue gas, the air completing after heat exchange enters the heat exchanger tube in the portable slag cooler 6 of being with vibration, choke preventing function, and the high temperature bottom slag of discharging with burner hearth 2 carries out heat exchange.The high temperature air part completing after heat exchange enters in burner hearth 2 from overfiren air port 7 as Secondary Air, and another part directly enters wind bellows 5 one time as fluidized wind.Convection heating surface and high-temperature flue gas that first feedwater enters in back-end ductwork 12 carry out heat exchange, the steam water interface producing after heat exchange enters and in drum 10, carries out carbonated drink separation, the process steam that the final hot water producing and part steam can be used as user (as dry, heating, generating etc.).
In above-mentioned three kinds of situations, the high-temperature flue gas that burning produces carries out after gas solid separation through separator 11, carries out successively heat exchange with the heating surface in back-end ductwork 12, and the flue gas that completes heat exchange enters atmosphere by chimney 16 after deduster 15 dedustings.The ash temperature that slag cooler 6 and device for cooling ash 13 are discharged, all not higher than 200 ℃, is sent in ash silo with the flying dust that deduster 15 is caught, in the lump as building materials deposit.
Claims (2)
1. an oil shale semi-coke fluidized bed combustion syste that adopts triple channel flow-dividing control material returning device, comprise semicoke carrier pipe (1), burner hearth (2), feed bin (3), batcher (4), wind bellows (5), slag cooler (6), overfiren air port (7), triple channel flow-dividing control material returning device (8), standpipe (9), drum (10), separator (11), back-end ductwork (12), device for cooling ash (13), air preheater (14), deduster (15), chimney (16), it is characterized in that: because oil shale semi-coke calorific value is very low, for guaranteeing the smooth combustion operating mode in burner hearth (2), burner hearth is not arranged any heating surface in (2), by adopting triple channel flow-dividing control material returning device (8), regulate ash amount and the ash temperature of the returning charge ash that enters burner hearth, control the ignition temperature of burner hearth (2), reclaim the heat of returning charge ash simultaneously, triple channel flow-dividing control material returning device (8) is comprised of three returning charge storehouses (one storehouse, returning charge storehouse (8-11), two storehouses, returning charge storehouse (8-8) and three storehouses, returning charge storehouse (8-6)) and a heat exchange storehouse (8-3), the returning charge ash that separator (11) separates is in standpipe (9) first enters two storehouses, returning charge storehouse (8-8), according to different combustion conditions in burner hearth (2), in conjunction with the difference of different lime-ash mobile (overflow or underflow) and partition wall height, by blast cap (8-10) air distribution, realize the mobile orientation of returning charge ash is controlled, in heat exchange storehouse (8-3), be provided with the pipe laying tube bank (8-4) of being heated, being subject to hot working fluid is saturation water or subcooled water.
2. according to claim 1, the Area Ratio of burner hearth (2) air distribution plate and triple channel flow-dividing control material returning device (8) heat exchange storehouse air distribution plate is 0.5 ~ 2; High 100mm ~ the 500mm of height of the low partition wall in aspect ratio heat exchange storehouse (8-3) (8-13) of the high partition wall in one storehouse, returning charge storehouse (8-11) (8-12).
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