CN103013573A - System for supplying high temperature air for fluidized bed coal gasification furnace - Google Patents
System for supplying high temperature air for fluidized bed coal gasification furnace Download PDFInfo
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- CN103013573A CN103013573A CN 201110280668 CN201110280668A CN103013573A CN 103013573 A CN103013573 A CN 103013573A CN 201110280668 CN201110280668 CN 201110280668 CN 201110280668 A CN201110280668 A CN 201110280668A CN 103013573 A CN103013573 A CN 103013573A
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Abstract
The present invention relates to a system for supplying high temperature air for a fluidized bed coal gasification furnace. The system mainly comprises a circulation fluidized bed burn furnace, a low speed burn-out fluidized bed and a cross-flow gas-solid fluidized bed heat exchanger, wherein the circulation fluidized bed burn furnace burns carbon-containing residue and fine ash discharged by a fluidized bed coal gasification furnace. The system is characterized in that the circulation fluidized bed burn furnace and the low speed burn-out fluidized bed are adopted to burn out carbon-containing residue and fine ash discharged by the fluidized bed coal gasification furnace, and with circulation of a solid heat carrier among the circulation fluidized bed burn furnace, the low speed burn-out fluidized bed and the cross-flow gas-solid fluidized bed heat exchanger, most of burning calories is provided for generating high temperature air for the fluidized bed coal gasification furnace through the cross-flow gas-solid fluidized bed heat exchanger.
Description
Affiliated technical field
The present invention is a kind of system that high temperature air is provided, and the system of high temperature air is provided in particular for the fluidized bed coal steam stove.
Background technology
All there is the not high and excessive deficiency of carbon loss of caloric power of gas in existing fluidized bed air gas furnace (also with a small amount of water-gas reaction).
Cause the not high reason of caloric power of gas to be that used air brings a large amount of nitrogen in oxygen supply, their heat up needs a lot of heats, has also diluted combustiblematerials concentration.The caloric power of gas that existing fluidized bed air gas furnace produces only is 4800～6000kJ/m
3, be difficult to satisfy the requirement of high Heating temperature technique, often can only adopt the measure raising calorific values such as oxygen enrichment, thereby increase investment and cost.People know that entering the stove air themperature by raising can improve caloric power of gas, but in the existing preheating of air equipment, tubular type or rotary type are limit by metal material all, use the equipment of carbon steel, and air preheating temperature is the highest to be no more than 350 ℃; Will obtain at present high temperature air and can only adopt regenerative heat-exchange equipment, they are bulky, the air themperature fluctuation, and cost is also high.The present invention comprises that the solid thermal carriers of circulating fluidized bed combustion stove circulating ash are heating agent, and heat-carrying thing material heatproof degree is all above 1000 ℃, can be with gasification with more than the preheating of air to 700 ℃, and the process continous-stable.After gasification reaches more than 700 ℃ with air themperature, caloric power of gas will reach 7300～9000kJ/m
3, can satisfy many heat processing requirements.
Fluidized bed coal steam stove carbon loss is from two aspects, and one is that emulsion zone must keep the carbon content more than 30%, the high carbon loss that causes of material carbon containing of therefrom discharging; Be a large amount of duff particles on the other hand, carbon content was very high when they were taken out of by coal gas.The reason that duff particle reaction degree is low, at first be since fluid bed furnace internal reaction district temperature limited in ash fusion point, low temperature cause speed of reaction on the low side due to, when tiny carbonaceous particles surrounding temperature is lower than 1000 ℃, they are in the chemomotive force reaction zone, and speed of reaction is not high.Even in the combustion chamber of excess of oxygen is arranged, also need residence time of quite growing can after-flame, and above vapourizing furnace, do not had oxygen to exist, gasification reaction is again strong endothermic reaction, and is poorer than combustion chamber internal reaction condition.Many technological lines all are conceived to reduce carbon loss in gasification, such as ash reunion, high temperature Winkler etc., and the result is all not satisfactory.
Summary of the invention
Starting point of the present invention is with above-mentioned two not enough integrated complementaries, namely set up in addition the circulating fluidized bed combustion stove of an after-flame carbon loss, its furnace high-temperature section heat is used for heating and gasifying by means of solid thermal carriers to be made it to reach more than 700 ℃ with air, the combustion product gases heat then for generation of and overheated gasification with steam and preheated air to 300～350 ℃.These carbonaceous materials are placed on circulating fluidized bed combustion stove internal combustion, and except excess of oxygen was arranged, high temperature cyclone separator made the particle iterative cycles, and efficiency of combustion can reach more than 95%.
The unburnt slag of fluidized bed coal steam stove and thin ash are placed on this no problem of circulating fluidized bed combustion stove after-flame, if but want the heat hot carrier simultaneously and will run into some problems by the thermal barrier preheated air.The circulating fluidized bed combustion stove needs high gas speed in order to promote solid thermal carriers; more uncombusted particle can be taken out of with thermal barrier; if use simply the higher heating material air of these carbon containings; will be with burning in heating; air themperature has raise; partial oxygen has wherein also consumed, and this situation is not desirable.A low speed after-flame fluidized-bed is set in system for this reason; promote the material that separates the flue gas from burning and at first enter low speed after-flame fluidized-bed; thicker uncombusted particle is after-flame therein; can carry secretly by elutriation and by low speed after-flame fluidized bed smoke than fine particle and again to enter high temperature cyclone separator; after-flame after repeatedly circulating, they do not participate in the process that adds warm air.The material that is used for adding warm air then is that wherein carbon containing is very low from the thicker material of low speed after-flame fluidized-bed, and oxygen consumption is few when doing heat exchange with air.
The solid thermal carriers particle of temperature about up to 1000 ℃ enters a gas-solid fluidized bed interchanger of cross-stream.For reducing the back-mixing of solid particulate, bed transverse section long-width ratio is very large, and the air that enters interchanger has been preheated to 300～350 ℃ in tubular air preheater, and the air that leaves interchanger is heated to more than 700 ℃, and is admitted to vapourizing furnace.The solid thermal carriers particle that leaves interchanger has been reduced to below 650 ℃, and they are sent back to the roasting kiln heating, promote, and finish circulation.
Description of drawings
Fig. 1 is the system diagram of this invention;
Wherein respectively representative of numbering: (1) carbonous residue and thin ash, (2) circulating fluidized bed combustion stove, (3) low speed after-flame fluidized-bed, the gas-solid fluidized bed interchanger of (4) cross-stream, (5) are heat-resisting and solid thermal carriers, (6) uncombusted particle, (7) combustion product gases, (8) high temperature cyclone separator, (9) and (10) of the granulometric composition of higher hardness are arranged is combustion air by coal ash particle and other.(11) low speed after-flame fluidized bed smoke, (12) circulating fluidized bed combustion stove top, (13) drainage conduit, (14) air, (15) high temperature air, (16) solid thermal carriers.
Embodiment
The present invention is achieved in that the present invention is a kind of system that high temperature air is provided for the fluidized bed coal steam stove, and this system (such as Fig. 1) comprises that mainly one uses the carbonous residue of fluidized bed coal gasifier discharge and circulating fluidized bed combustion stove (2), a low speed after-flame fluidized-bed (3), the gas-solid fluidized bed interchanger of cross-stream (4) of thin ash (1).This system finishes two targets, the carbonous residue that namely the after-flame fluidized bed coal gasifier is discharged in circulating fluidized bed combustion stove and low speed after-flame fluidized-bed and thin ash and by means of solid thermal carriers between circulating fluidized bed combustion stove, low speed after-flame fluidized-bed and the gas-solid fluidized bed interchanger of cross-stream, circulate major part with heat output by the gas-solid fluidized bed interchanger of cross-stream for generation of high temperature air, these air are for fluidized bed coal gasifier.Circulating fluidized bed combustion stove chamber temperature is 800～950 ℃, and empty tower gas velocity is 4～10m/s.Heat-resisting and have the solid thermal carriers (5) of the granulometric composition of higher hardness to be heated in roasting kiln and to promote by coal ash particle and other, solid thermal carriers and uncombusted particle (6) are finished in high temperature cyclone separator (8) with combustion product gases (7) and are separated.High-temperature solid particle (5)+(6) are admitted to low speed after-flame fluidized-bed, and low speed bed empty tower gas velocity is 0.7～1.5m/s, and bed temperature is 950～1050 ℃.Combustion air (9) and (10) are sent into respectively in circulating fluidized bed combustion stove and low speed after-flame fluidized-bed bottom.Low speed after-flame fluidized bed smoke (11) imports circulating fluidized bed combustion stove top (12).Coarse particles after-flame in low speed after-flame fluidized-bed from the uncombusted particle that high temperature cyclone separator separates, formed ash particle is the part of solid thermal carriers; Again enter high temperature cyclone separator than small-particle with flue gas, so circulation can reach higher after-flame degree, and its ash content will export flue gas with high temperature cyclone separator and discharge.A drainage conduit (13) is arranged at low speed after-flame fluidized-bed bottom, and the high-temp solid thermal barrier is admitted to the gas-solid fluidized bed interchanger of cross-stream by it.The transverse section long-width ratio of the gas-solid fluidized bed interchanger of cross-stream is 5～20, and the high-temp solid thermal material enters from length direction one end, flows out from the other end, and static bed thickness is 0.2～0.4m in the bed, and empty tower gas velocity is 0.5～1.2m/s.From tubular air preheater, temperature is that 300～350 ℃ air (14) feeds for airduct by blast cap or the tubular type that is positioned at the interchanger bottom, they and high-temp solid thermal barrier carry out heat exchange, the high temperature air (15) that temperature reaches more than 700 ℃ flows out from the gas-solid fluidized bed interchanger of cross-stream top, is used for fluidized bed coal gasifier.The solid thermal carriers of having lowered the temperature (16) that flow out from the gas-solid fluidized bed interchanger of cross-stream are sent back to the circulating fluidized bed combustion stove and are heated, promote iterative cycles.The high-temperature flue gas that leaves high temperature cyclone separator for generation of with overheated gasification with water vapor and with tubular air preheater with air heating to 300～350 ℃.
Claims (5)
1. system that high temperature air is provided for the fluidized bed coal steam stove, this system comprise that mainly one uses carbonous residue that fluidized bed coal gasifier discharges and circulating fluidized bed combustion stove, a low speed after-flame fluidized-bed, gas-solid fluidized bed interchanger of cross-stream of thin ash.It is characterized in that the carbonous residue of discharging with circulating fluidized bed combustion stove and low speed after-flame fluidized-bed after-flame fluidized bed coal gasifier and thin ash and by means of solid thermal carriers between circulating fluidized bed combustion stove, low speed after-flame fluidized-bed and the gas-solid fluidized bed interchanger of cross-stream, circulate major part with heat output by the gas-solid fluidized bed interchanger of cross-stream for generation of high temperature air, these air are for fluidized bed coal gasifier.
2. according to claim one, circulating fluidized bed combustion stove chamber temperature is 800～950 ℃, and empty tower gas velocity is 4～10m/s.Low speed bed empty tower gas velocity is 0.7～1.5m/s, and bed temperature is 950～1050 ℃.
3. according to claim one.Heat-resisting and have the solid thermal carriers of the granulometric composition of higher hardness to be heated in roasting kiln and to promote by coal ash particle and other, solid thermal carriers and uncombusted particle are finished in high temperature cyclone separator with combustion product gases and are separated.High-temperature solid particle is admitted to low speed after-flame fluidized-bed.Combustion air is sent into respectively in circulating fluidized bed combustion stove and low speed after-flame fluidized-bed bottom.Low speed after-flame fluidized bed smoke imports circulating fluidized bed combustion stove top.Coarse particles after-flame in low speed after-flame fluidized-bed from the uncombusted particle that high temperature cyclone separator separates, formed ash particle is the part of solid thermal carriers; Again enter high temperature cyclone separator than small-particle with flue gas, so circulation can reach higher after-flame degree, and its ash content will export flue gas with high temperature cyclone separator and discharge.
4. according to claim one, a drainage conduit is arranged at low speed after-flame fluidized-bed bottom, and the high-temp solid thermal barrier is admitted to the gas-solid fluidized bed interchanger of cross-stream by it.The transverse section long-width ratio of the gas-solid fluidized bed interchanger of cross-stream is 5～20, and the high-temp solid thermal material enters from length direction one end, flows out from the other end, and static bed thickness is 0.2～0.4m in the bed, and empty tower gas velocity is 0.5～1.2m/s.From tubular air preheater, temperature is that 300～350 ℃ air feeds for airduct by blast cap or the tubular type that is positioned at the interchanger bottom, they and high-temp solid thermal barrier carry out heat exchange, the high temperature air that temperature reaches more than 700 ℃ flows out from the gas-solid fluidized bed interchanger of cross-stream top, is used for fluidized bed coal gasifier.The solid thermal carriers of having lowered the temperature that flow out from the gas-solid fluidized bed interchanger of cross-stream are sent back to the circulating fluidized bed combustion stove and are heated, promote iterative cycles.
5. according to claim one, the high-temperature flue gas that leaves high temperature cyclone separator for generation of with overheated gasification with water vapor and with tubular air preheater with air heating to 300～350 ℃.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201110280668 CN103013573A (en) | 2011-09-21 | 2011-09-21 | System for supplying high temperature air for fluidized bed coal gasification furnace |
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| CN 201110280668 CN103013573A (en) | 2011-09-21 | 2011-09-21 | System for supplying high temperature air for fluidized bed coal gasification furnace |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105444163A (en) * | 2014-09-30 | 2016-03-30 | 中国科学院工程热物理研究所 | Circulating fluidized bed combustion device for ultralow-volatile superfine fuel and combustion method |
| CN108120623A (en) * | 2018-01-12 | 2018-06-05 | 西华大学 | A kind of diesel engine particulate object grading sampling device and its control method |
| CN110144602A (en) * | 2019-06-04 | 2019-08-20 | 甘肃东兴铝业有限公司 | A kind of carbon slag in Aluminium electrolysis treatment process |
-
2011
- 2011-09-21 CN CN 201110280668 patent/CN103013573A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105444163A (en) * | 2014-09-30 | 2016-03-30 | 中国科学院工程热物理研究所 | Circulating fluidized bed combustion device for ultralow-volatile superfine fuel and combustion method |
| CN105444163B (en) * | 2014-09-30 | 2017-09-29 | 中国科学院工程热物理研究所 | Ultralow volatile matter superfine fuel burning device of circulating fluidized bed and combustion method |
| CN108120623A (en) * | 2018-01-12 | 2018-06-05 | 西华大学 | A kind of diesel engine particulate object grading sampling device and its control method |
| CN108120623B (en) * | 2018-01-12 | 2023-09-01 | 西华大学 | Hierarchical sampling device for exhaust particulate matters of diesel engine and control method thereof |
| CN110144602A (en) * | 2019-06-04 | 2019-08-20 | 甘肃东兴铝业有限公司 | A kind of carbon slag in Aluminium electrolysis treatment process |
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Application publication date: 20130403 |