CN105366699A - Calcination and activation method and device for high-aluminum pulverized coal furnace flyash - Google Patents
Calcination and activation method and device for high-aluminum pulverized coal furnace flyash Download PDFInfo
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- CN105366699A CN105366699A CN201410429766.1A CN201410429766A CN105366699A CN 105366699 A CN105366699 A CN 105366699A CN 201410429766 A CN201410429766 A CN 201410429766A CN 105366699 A CN105366699 A CN 105366699A
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Abstract
The invention relates to a calcination and activation method and device for high-aluminum pulverized coal furnace flyash. Industrial grade aluminum oxide can be extracted from the high-aluminum pulverized coal furnace flyash. The method includes the steps of granulating, drying, calcining activating, and material cooling; particularly, the flyash and (NH4)2SO4 are mixed by a ratio and then enter a granulator to be extruded and formed to obtain flyash-ammonium sulfate granules; the solid granules formed through granulation enter a drying bed and exchange heat with high-temperature flue gas from a calcination furnace to recover and use high-temperature heat; the dried granules are conveyed to the calcination furnace; the solid granules obtained after reactions are completed are conveyed to a cooling bed to be cooled; cold air is adopted to cool the granules, air with heat exchanged enters the calcination furnace to provide combustion air, and the process of recovering and using the heat is completed synchronously. Aluminum ammonium sulfate is used as an intermediate substance, the suitable calcination temperature is adopted to destroy the Al-Si bonds in the flyash, aluminum oxide is activated in a heated mode, and industrial grade aluminum oxide can be extracted from the high-aluminum pulverized coal furnace flyash.
Description
Technical field
The present invention relates to a kind of method and device of high alumina coal-powder boiler flyash calcination activation, realize extracting industrial grade oxygen aluminium by high alumina coal-powder boiler flyash.
Background technology
Coal-powder boiler fine coal ashes is the product of high-temp combustion in burner hearth, and major ingredient has: Al
2o
3, SiO
2, Fe
2o
3, FeO, TiO
2, CaO, K
2o, MgO etc., wherein the content of aluminum oxide generally can reach 20% ~ 40%, reaches as high as more than 50%, and bauxite can be replaced to become a kind of well alumina resource.Because temperature of combustion is greater than 1000 degree, most flyash exists with vitreum form, and its topology convergence degree is large, and chemical property is very stable.
The comprehensive utilizating research carrying out flyash has its own strategic significance, is also the study hotspot of recent domestic, by the recycling of resource, and can protecting ecology and resource environment effectively.The coal firing boiler of the source of flyash mainly power plant, the current flyash for the generation of circulating fluidized bed combustion coal boiler is domestic has achieved remarkable achievement, but because the aluminium in high alumina coal-powder boiler flyash is combined with the form of energy-rich bond with silicon, exist with vitreum form, its topology convergence degree is large, chemical property is very stable, and this just brings difficulty to the extraction realizing aluminum oxide.
Summary of the invention
The object of the present invention is to provide a kind of method and device of high alumina coal-powder boiler flyash calcination activation, to realize extracting industrial grade oxygen aluminium by high alumina coal-powder boiler flyash.
For achieving the above object, the technical solution used in the present invention is:
A device for high alumina coal-powder boiler flyash calcination activation, comprises tablets press, drying bed, stoving oven, cooling bed; Described tablets press is connected with drying bed, and drying bed is connected with stoving oven, stoving oven is connected with cooling bed.
The body of heater of described stoving oven adopts vertical columnar structured, and the principal reaction district emulsion zone of particle makes cone section, and the material inlet of stoving oven is arranged on more than cone section, and the air distribution plate being arranged on bottom adopts little blast cap, and hot wind inlet is arranged on below cone section; Cyclonic separator is arranged on body of heater, and cyclonic separator top is provided with exhanst gas outlet, is provided with returning charge leg below cyclonic separator, and returning charge leg is provided with discharge gate.
Described drying bed is fluidized drying bed, and adopt the negative pressure bubbling bed technology of low wind speed, fluidisation wind-warm syndrome is not higher than 150 DEG C.
Described stoving oven is fluidized roaster, and choosing design temperature in oven 3 stove is 370 ~ 400 DEG C, and stoving oven 3 is intermittent discharge type.
The described cooling bed temperature by particle is reduced to less than 80 DEG C.
A method for high alumina coal-powder boiler flyash calcination activation, comprises granulation, drying, calcination activation, material cooling step: flyash and (NH
4)
2sO
4enter tablets press after carrying out blending proportioning, through extrusion molding, form flyash-ammonium sulfate; The solid particulate that granulation is formed enters drying bed, carries out heat exchange, realize the recycling of heat of high temperature with the high-temperature flue gas from stoving oven; Dried particle transport is to stoving oven; The solid particulate reacted is delivered to cooling bed cooling; Adopt freezing air to cool particle, the air after heat exchange enters stoving oven and provides combustion air, synchronously completes the recycling process of heat.
Described granulation process is mechanical presses granulation process, flyash and (NH
4)
2sO
4tablets press is entered after carrying out blending proportioning according to mixing mol ratio 1:3 ~ 5.
Described drying process is realized by drying bed, drying bed is entered after grain granulation, drying mode adopts bubbling fluidization technology, equipment is fluidized drying bed, drying bed is used for reducing the water-content after granulation in particle, by the water content control of particle within 5%, reduce the thermal stresses formed in heat-processed at particle simultaneously, prevent particle from breaking at calcination activation stove; Drying bed adopts the negative pressure bubbling bed technology of low wind speed; subtract less granular fragmentation; fluidisation wind-warm syndrome is not higher than 150 DEG C; the source of the gas of drying bed comes from the high-temperature flue gas of stoving oven, effectively recycles flue gas heat, and heat smoke drying bed bottom air inlet mouth enters bed; heat exchange is carried out with the particle in bed; particle dehydration, drying bed bottom discharging mouth is discharged, and discharges after warm air and particle heat exchange.
Described calcination activation process is realized by fluidized roaster, circulating fluidized bed roasting furnace is used for the reaction of aluminum oxide and ammonium sulfate in high temperature aluminous fly-ash, the alumina conversion of the overwhelming majority is made to become Tai-Ace S 150 ammonia, according to flyash and ammonium sulfate response characteristic, choosing design temperature in stoving oven stove is 370 ~ 400 DEG C, and stoving oven is intermittent discharge type, the circulating fluidized bed technique that stoving oven adopts negative pressure to run, body of heater adopts vertical columnar structured, the principal reaction district emulsion zone of particle makes cone section, produce in order to buffer gas the empty cross section wind speed brought to increase, the material inlet of stoving oven is arranged on more than cone section, hot wind inlet is arranged on below cone section, for the fluidisation ensureing that material particles can be good, air distribution plate bottom bed adopts little blast cap, ensure that the hot blast cloth wind entered by hot wind inlet is even, ensure the powerful and vigorous of fluidized wind simultaneously, cyclonic separator is arranged on body of heater, cyclonic separator top is provided with exhanst gas outlet, returning charge leg is provided with below cyclonic separator, returning charge leg is provided with discharge gate, particle is circulated by being entrained in stove of hot blast, heat smoke and solid particulate are in cyclonic separator generation gas solid separation, solid particulate is returned in stove by the returning charge leg below cyclonic separator and proceeds reaction, reaches after certain reaction times discharge out of the furnace from the discharge gate material returning device until particle.
Described material process of cooling, by cooling bed realization, is cooling bedly used for the particle after to roasting and cools, and the temperature of particle is reduced to less than 80 DEG C; The bubbling bed technology of the malleation of the low wind speed of cooling bed employing; freezing air is adopted to cool particle; freezing air enters bed through cooling bed bottom; heat exchange is carried out with the particle in bed; particle temperature reduces; discharge through discharge gate, enter stoving oven after warm air and particle heat exchange and use as combustion air.
Beneficial effect acquired by the present invention is:
The present invention is intermediate material with exsiccated ammonium alum, adopts the Al-Si key in suitable maturing temperature destruction flyash, makes aluminum oxide thermal activation, realize the object being extracted industrial grade oxygen aluminium by high alumina coal-powder boiler flyash.The present invention adopts mechanical pelleting mode to ensure the intensity of particle, the form of multilevel drying is taked to complete the preliminary mechanical drying process of particle, by optimizing the calcination activation time of material, ensure the calcination activation extraction yield of aluminum oxide, heat recovery technique can improve capacity usage ratio, finally reach the effects of resource circle utilization of less energy-consumption, high extraction, meet the industry policy of national energy-saving environmental protection and waste material recycling.
(1) granulation process achieves reaction mass and combines with particulate state, possesses the condition of follow-up fluosolids roasting; (2) the calcination activation process of material adopts multilevel drying, classification roasting, differential temperature to run, and each technique unit can independent operating, accomplishes not interfere with each other; (3) system all carries out multistage waste heat recovery to high and low temperature flue gas and high-temperature material particle, realizes minimizing of energy consumption by the cascade utilization of heat; (4) system effectively solves the aluminum oxide activating problem in high-temperature powder coal ash, can realize the comprehensive utilization of fly ash.
Accompanying drawing explanation
Fig. 1 is the structure drawing of device of high alumina coal-powder boiler flyash calcination activation of the present invention;
Fig. 2 is the stoving oven structure iron in the device of high alumina coal-powder boiler flyash calcination activation of the present invention;
In figure: 1, tablets press; 2, drying bed; 3, stoving oven; 4, cooling bed; 5, body of heater; 6, material inlet; 7, air distribution plate; 8, hot wind inlet; 9, discharge gate; 10, returning charge leg; 11, cyclonic separator; 12, exhanst gas outlet.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
As shown in Figure 1, the device of high alumina coal-powder boiler flyash calcination activation of the present invention comprises tablets press 1, drying bed 2, stoving oven 3, cooling bed 4; Described tablets press 1 is connected with drying bed 2, and drying bed 2 is connected with stoving oven 3, stoving oven 3 is connected with cooling bed 4; The method of high alumina coal-powder boiler flyash calcination activation of the present invention comprises granulation, drying, calcination activation, material cooling step, specific as follows:
Flyash and (NH
4)
2sO
4enter tablets press 1 after carrying out blending proportioning according to mixing mol ratio 1:3 ~ 5, through extrusion molding, form flyash-ammonium sulfate; The solid particulate that granulation is formed enters drying bed 2, carries out heat exchange, realize the recycling of heat of high temperature with the high-temperature flue gas from stoving oven 3; Dried particle transport is to stoving oven 3; The solid particulate reacted is delivered to cooling bed 4 and cools; Adopt freezing air to cool particle, the air after heat exchange enters stoving oven 3 and provides combustion air, synchronously completes the recycling process of heat.
Described granulation process is mechanical presses granulation process.Flyash and (NH
4)
2sO
4enter tablets press 1 after carrying out blending proportioning according to mixing mol ratio 1:3 ~ 5, through extrusion molding, form flyash-ammonium sulfate.Due in extrusion process, relatively high squeezing action, granulated pellet temperature can be made to raise, and particle surface temperature can reach about 60 DEG C.Under the temperature action that this is high, be positioned at the ammonium sulfate of particle surface by partial melting.The fly ash grain of the ammonium sulfate and surrounding that are extruded thawing bonds mutually, makes granulated pellet have high intensity, and granulated pellet surface relative smooth.
Described drying process is realized by drying bed 2.Enter drying bed 2 after grain granulation, drying mode adopts bubbling fluidization technology, and major equipment is fluidized drying bed 2.Drying bed 2 is mainly used to reduce the water-content after granulation in particle, by the water content control of particle within 5%.Reduce the thermal stresses formed in heat-processed at particle simultaneously, prevent particle from breaking at calcination activation stove.Particle after granulation contains higher moisture, can increase thermal load and the gas production rate of stoving oven, add the possibility of particle bond simultaneously after directly entering into stoving oven 3.Drying bed 2 adopts the negative pressure bubbling bed technology of low wind speed, decreases the fragmentation of particle.In order to prevent ammonium sulfate in particle from decomposing, so fluidisation wind-warm syndrome is not higher than 150 DEG C.The source of the gas of drying bed 2 comes from the high-temperature flue gas of stoving oven 3; effectively flue gas heat is recycled; heat smoke drying bed bottom air inlet mouth enters bed; heat exchange is carried out with the particle in bed; particle dehydration; drying bed bottom discharging mouth is discharged, and discharges after warm air and particle heat exchange.
As shown in Figure 2, described calcination activation process is realized by fluidized roaster 3.Circulating fluidized bed roasting furnace is mainly used in the reaction of aluminum oxide and ammonium sulfate in high temperature aluminous fly-ash, makes the alumina conversion in the mullite of the overwhelming majority become Tai-Ace S 150 ammonia.According to flyash and ammonium sulfate response characteristic, choosing design temperature in stoving oven stove is 370 ~ 400 DEG C.Due to flyash and ammonium sulfate reaction needed certain hour, so stoving oven 3 is intermittent discharge type.The circulating fluidized bed technique that stoving oven 3 adopts negative pressure to run, body of heater 5 adopts vertical columnar structured, ensures that particle has the approximate residence time in stove.Because flyash and ammonium sulfate produce a large amount of gas in reaction process He in dehydration, need a large amount of reaction heat simultaneously, produce so this process has a large amount of gas, therefore the principal reaction district emulsion zone of particle is made cone section, producing in order to buffer gas the empty cross section wind speed brought increases.The material inlet 6 of stoving oven 3 is arranged on more than cone section, hot wind inlet 8 is arranged on below cone section, and be the fluidisation ensureing that material particles can be good, the air distribution plate 7 bottom bed adopts little blast cap, ensure that the hot blast cloth wind entered by hot wind inlet 8 is even, ensure the powerful and vigorous of fluidized wind simultaneously.Cyclonic separator 11 is arranged on body of heater 5, and cyclonic separator 11 top is provided with exhanst gas outlet 12, is provided with returning charge leg 10 below cyclonic separator 11, returning charge leg 10 is provided with discharge gate 9; Particle is circulated by being entrained in stove of hot blast, gas solid separation is there is in heat smoke and solid particulate at cyclonic separator 11, solid particulate is returned in stove by the returning charge leg 10 below cyclonic separator 11 and proceeds reaction, reaches after certain reaction times discharge out of the furnace from the discharge gate 9 material returning device until particle.
Described material process of cooling realizes by cooling bed 4.Cooling bed 4 are mainly used to the particle after to roasting cools, and the temperature of particle is reduced to less than 80 DEG C.The bubbling bed technology of the malleation of the low wind speed of cooling bed 4 employing.Freezing air is adopted to cool particle.Freezing air enters bed bottom cooling bed 4, carries out heat exchange with the particle in bed, and particle temperature reduces, and discharges through discharge gate.Enter stoving oven 3 after warm air and particle heat exchange to use as combustion air.
Claims (10)
1. a device for high alumina coal-powder boiler flyash calcination activation, is characterized in that: this device comprises tablets press (1), drying bed (2), stoving oven (3), cooling bed (4); Described tablets press (1) is connected with drying bed (2), and drying bed (2) is connected with stoving oven (3), stoving oven (3) is connected with cooling bed (4).
2. the device of high alumina coal-powder boiler flyash calcination activation according to claim 1, it is characterized in that: the body of heater (5) of described stoving oven (3) adopts vertical columnar structured, the principal reaction district emulsion zone of particle makes cone section, the material inlet (6) of stoving oven (3) is arranged on more than cone section, the air distribution plate (7) being arranged on bottom adopts little blast cap, and hot wind inlet (8) is arranged on below cone section; Cyclonic separator (11) is arranged on body of heater (5), cyclonic separator (11) top is provided with exhanst gas outlet (12), cyclonic separator (11) below is provided with returning charge leg (10), returning charge leg (10) is provided with discharge gate (9).
3. the device of high alumina coal-powder boiler flyash calcination activation according to claim 1, it is characterized in that: described drying bed (2) is fluidized drying bed, adopt the negative pressure bubbling bed technology of low wind speed, fluidisation wind-warm syndrome is not higher than 150 DEG C.
4. the device of high alumina coal-powder boiler flyash calcination activation according to claim 1, it is characterized in that: described stoving oven (3) is fluidized roaster, choosing design temperature in oven 3 stove is 370 ~ 400 DEG C, and stoving oven (3) is intermittent discharge type.
5. the device of high alumina coal-powder boiler flyash calcination activation according to claim 1, is characterized in that: the temperature of particle is reduced to less than 80 DEG C by described cooling bed (4).
6. a method for high alumina coal-powder boiler flyash calcination activation, is characterized in that: the method comprises granulation, drying, calcination activation, material cooling step: flyash and (NH
4)
2sO
4enter tablets press (1) after carrying out blending proportioning, through extrusion molding, form flyash-ammonium sulfate; The solid particulate that granulation is formed enters drying bed (2), carries out heat exchange, realize the recycling of heat of high temperature with the high-temperature flue gas from stoving oven (3); Dried particle transport is to stoving oven (3); The solid particulate reacted is delivered to cooling bed (4) and cools; Adopt freezing air to cool particle, the air after heat exchange enters stoving oven (3) and provides combustion air, synchronously completes the recycling process of heat.
7. the method for high alumina coal-powder boiler flyash calcination activation according to claim 6, is characterized in that: described granulation process is mechanical presses granulation process, flyash and (NH
4)
2sO
4tablets press (1) is entered after carrying out blending proportioning according to mixing mol ratio 1:3 ~ 5.
8. the method for high alumina coal-powder boiler flyash calcination activation according to claim 6, it is characterized in that: described drying process is realized by drying bed (2), drying bed (2) is entered after grain granulation, drying mode adopts bubbling fluidization technology, equipment is fluidized drying bed, drying bed (2) is used for reducing the water-content after granulation in particle, by the water content control of particle within 5%, reduce the thermal stresses formed in heat-processed at particle simultaneously, prevent particle from breaking at calcination activation stove; Drying bed (2) adopts the negative pressure bubbling bed technology of low wind speed; subtract less granular fragmentation; fluidisation wind-warm syndrome is not higher than 150 DEG C; the source of the gas of drying bed (2) comes from the high-temperature flue gas of stoving oven (3), effectively recycles flue gas heat, and heat smoke drying bed bottom air inlet mouth enters bed; heat exchange is carried out with the particle in bed; particle dehydration, drying bed bottom discharging mouth is discharged, and discharges after warm air and particle heat exchange.
9. the method for high alumina coal-powder boiler flyash calcination activation according to claim 6, it is characterized in that: described calcination activation process is realized by fluidized roaster (3), circulating fluidized bed roasting furnace is used for the reaction of aluminum oxide and ammonium sulfate in high temperature aluminous fly-ash, the alumina conversion of the overwhelming majority is made to become Tai-Ace S 150 ammonia, according to flyash and ammonium sulfate response characteristic, choosing design temperature in stoving oven stove is 370 ~ 400 DEG C, and stoving oven (3) is intermittent discharge type, the circulating fluidized bed technique that stoving oven (3) adopts negative pressure to run, body of heater (5) adopts vertical columnar structured, the principal reaction district emulsion zone of particle makes cone section, produce in order to buffer gas the empty cross section wind speed brought to increase, the material inlet (6) of stoving oven (3) is arranged on more than cone section, hot wind inlet (8) is arranged on below cone section, for the fluidisation ensureing that material particles can be good, air distribution plate (7) bottom bed adopts little blast cap, ensure that the hot blast cloth wind entered by hot wind inlet (8) is even, ensure the powerful and vigorous of fluidized wind simultaneously, cyclonic separator (11) is arranged on body of heater (5), cyclonic separator (11) top is provided with exhanst gas outlet (12), cyclonic separator (11) below is provided with returning charge leg (10), returning charge leg (10) is provided with discharge gate (9), particle is circulated by being entrained in stove of hot blast, gas solid separation is there is in heat smoke and solid particulate at cyclonic separator (11), solid particulate is returned in stove by the returning charge leg (10) of cyclonic separator (11) below and proceeds reaction, reaches after certain reaction times discharge out of the furnace from the discharge gate (9) material returning device until particle.
10. the method for high alumina coal-powder boiler flyash calcination activation according to claim 6, it is characterized in that: described material process of cooling is realized by cooling bed (4), cooling bed (4) are used for the particle after to roasting and cool, and the temperature of particle is reduced to less than 80 DEG C; Cooling bed (4) adopt the bubbling bed technology of the malleation of low wind speed; freezing air is adopted to cool particle; freezing air enters bed through cooling bed (4) bottom; heat exchange is carried out with the particle in bed; particle temperature reduces; discharge through discharge gate, enter stoving oven (3) after warm air and particle heat exchange and use as combustion air.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410429766.1A CN105366699A (en) | 2014-08-28 | 2014-08-28 | Calcination and activation method and device for high-aluminum pulverized coal furnace flyash |
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|---|---|---|---|
| CN201410429766.1A CN105366699A (en) | 2014-08-28 | 2014-08-28 | Calcination and activation method and device for high-aluminum pulverized coal furnace flyash |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110102151A (en) * | 2019-03-29 | 2019-08-09 | 中冶南方工程技术有限公司 | Energy saving and environment friendly oxidate powder transportation system and its operational method in spray roasting |
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| CN103086412A (en) * | 2013-02-28 | 2013-05-08 | 山东科院天力节能工程有限公司 | Method for extracting alumina through coal ash |
| CN103394308A (en) * | 2013-07-01 | 2013-11-20 | 中国华能集团清洁能源技术研究院有限公司 | Constant temperature rotary roasting system heated by molten salt and technology thereof |
| CN204185253U (en) * | 2014-08-28 | 2015-03-04 | 北京航天动力研究所 | A kind of device of high alumina coal-powder boiler flyash calcination activation |
-
2014
- 2014-08-28 CN CN201410429766.1A patent/CN105366699A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102502744A (en) * | 2011-10-26 | 2012-06-20 | 北京航天动力研究所 | Slagging-free type and multilevel differential temperature fluidized roasting system for crystallized aluminum salt and method thereof |
| CN103086412A (en) * | 2013-02-28 | 2013-05-08 | 山东科院天力节能工程有限公司 | Method for extracting alumina through coal ash |
| CN103394308A (en) * | 2013-07-01 | 2013-11-20 | 中国华能集团清洁能源技术研究院有限公司 | Constant temperature rotary roasting system heated by molten salt and technology thereof |
| CN204185253U (en) * | 2014-08-28 | 2015-03-04 | 北京航天动力研究所 | A kind of device of high alumina coal-powder boiler flyash calcination activation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110102151A (en) * | 2019-03-29 | 2019-08-09 | 中冶南方工程技术有限公司 | Energy saving and environment friendly oxidate powder transportation system and its operational method in spray roasting |
| CN110102151B (en) * | 2019-03-29 | 2022-04-08 | 中冶南方工程技术有限公司 | Energy-saving and environment-friendly oxide powder conveying system in spray roasting and operation method thereof |
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Effective date of registration: 20170116 Address after: 100076 Beijing, Fengtai District, South Road, No. 1, Applicant after: Beijing Aerospace Petrochemical Technology and Equipment Engineering Corporation Address before: 100076 Beijing, Fengtai District, South Road, No. 1, Applicant before: Beijing Aerospace Propulsion Institute |
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Application publication date: 20160302 |