CN102679371B - Sludge drying and incineration device and method - Google Patents
Sludge drying and incineration device and method Download PDFInfo
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- CN102679371B CN102679371B CN 201210189962 CN201210189962A CN102679371B CN 102679371 B CN102679371 B CN 102679371B CN 201210189962 CN201210189962 CN 201210189962 CN 201210189962 A CN201210189962 A CN 201210189962A CN 102679371 B CN102679371 B CN 102679371B
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Abstract
The invention discloses a sludge drying and incineration device and a sludge drying and incineration method. A sludge inlet and a flue gas outlet are formed at the upper end of a device body, a drying chamber, an upper-bed air distribution plate, a combustion chamber, a lower-bed air distribution plate and a slag discharge opening are sequentially arranged in the device body from top to bottom, replenished air inlets are formed on a side wall of the device body on the upper part of the upper-bed air distribution plate, an auxiliary fuel inlet is formed on the side wall of the device body above the lower-bed air distribution plate, a primary air opening is formed on the side wall of the device body below the lower-bed air distribution plate, and the upper part of the drying chamber is connected with the bottom of the combustion chamber through a discharge opening, an upper-bed discharge tube, a feeder, a high-pressure air opening, a lower-bed return tube and a return opening. The quantity of drying equipment outside a furnace is decreased, thermal loss due to low heat exchange efficiency of the drying equipment in sludge drying and incineration technology is reduced, the investment and running cost of the drying equipment outside the furnace are lowered, the complexity of a system is reduced, and sludge can be combusted stably in a single fluidized bed furnace.
Description
Technical field
The present invention relates to incinerator and method thereof, relate in particular to a kind of sludge anhydration burning devices and methods therefor.
Background technology
China's sludge disposal technology is at present take agricultural and landfill as main.But mud is used for the agricultural safety problem that the most important thing is to use.Owing to contain a large amount of malignant bacterias in the mud, enrichment heavy metal, and in dehydration, added again chemical agent, so the effect of sludge manure and innocuousness wait further research.For landfill, owing to contain a large amount of harmful substances in the mud, also have the water content height, easily stop up the shortcoming such as landfill yard percolating pipe, so that forbidden admitting sewage sludge as the landfill yard on the ground such as Hangzhou, Shenzhen.Recent years, the domestic research that the sludge building material utilization also occurs, but treating capacity is less, and because the difficult quality identification of building material product, market becomes restraining factors.Can say that the harmless treatment of mud has become governments at all levels' solution, instant significant problem in China.Therefore, a kind ofly can stablize in the urgent need to seeking, clean, the technological means of extensive lignin-sludge, the difficult problem of a large amount of sewage sludge harmlessness recycling treatment that face with effective processing China.
Processing method take burning as core is processing method the most thoroughly, and this is because burning method is compared with other method and had outstanding advantage:
(1) burn the volume can make excess sludge and reduce to and minimize, thereby finally need the material disposed seldom, burning ash can be made into useful product, is relatively safe sludge treating method.
(2) the burning and processing sludge processing speed is fast, does not need long term storage.
(3) but the mud on-site incineration does not need long-distance transportation.
(4) can recover energy, be used for mummification and the power generation and heat supply of mud self.
(5) can make the whole carbonizations of organic matter and burning fully, pathogen kill, the environmental contaminants discharging is controlled.
Sludge incineration is burned two kinds after being divided into direct burning and mummification.The direct burning of mud is that high humidity (moisture content is more than 80%) mud is directly burned in incinerator in the situation as thermal source of auxiliary fuel.Burning high humidity (moisture content is more than 80%) after the mummification of mud is to burn after mud is cured to certain moisture content in advance again.The direct burning of mud is because sludge moisture content is large, calorific value is low, and burning can't keep the siege temperature in the stove, needs to consume a large amount of auxiliary fuels and just can keep stable burning.From aspects such as operating cost and equipment investments, the direct burning of mud is replaced by burning after the mummification just gradually.
Burning disposal adopts the mode that desiccation machine and incinerator arrange respectively usually behind traditional sludge drying, outside stove with moisture content up to 80% above wet sludge anhydration after guarantee smooth combustion, but the outer mummification of stove is burned and is had following shortcoming:
(1) the general drying equipment thermal efficiency only has 80%, produces extra thermal loss with directly burning ratio in the stove, therefore usually needs to drop into extra auxiliary fuel.
(2) the drying equipment power consumption is higher.
(3) the drying equipment price is high, and it is larger to account for share in system's investment.
(4) in the stove heating surface is arranged, the boiler consumptive material is larger.
(5) systematic comparison is complicated, and year running time is low.
This shows, for processing cost and the energy consumption of mud, although burning disposal improves to some extent than the direct burning of mud behind traditional sludge drying, but still be quite high, demands urgently reducing.
Summary of the invention
The objective of the invention is to overcome deficiency of the prior art, a kind of sludge anhydration burning devices and methods therefor is provided.
The device of sludge anhydration burning comprises mummification chamber, mud entrance, exhanst gas outlet, discharge gate, replenishes wind entrance, the air distribution plate of going to bed, combustion chamber, auxiliary fuel entrance, feedback outlet, the air distribution plate of leaving the bed, slag-drip opening, primary air nozzle, the drainage conduit of going to bed, batcher, high pressure air port, the feed back pipe of leaving the bed; The device body upper end is provided with mud entrance, exhanst gas outlet, be provided with in turn from top to bottom mummification chamber, the air distribution plate of going to bed, combustion chamber, the air distribution plate of leaving the bed, slag-drip opening in the device body, the device body sidewall of air distribution plate top of going to bed is provided with and replenishes the wind entrance, the device body sidewall of air distribution plate top of leaving the bed is provided with the auxiliary fuel entrance, the device body sidewall of air distribution plate below of leaving the bed is provided with primary air nozzle, and top, mummification chamber links to each other with the bottom, combustion chamber by discharge gate, the drainage conduit of going to bed, batcher, high pressure air port, the feed back pipe of leaving the bed, feedback outlet.
Described discharge gate is arranged on 0.65～0.67 place of mummification chamber height.
Totally 4 of described additional wind entrances lay respectively at four jiaos of the device body sidewalls of the air distribution plate top of going to bed.
Described mummification chamber volume is 4.9～5.1:1 with the ratio of combustion chamber volume, and the long-pending ratio with chamber cross section of mummification chamber cross-section is 2.9～3.1:1, and mummification chamber height is 1.58～1.75:1 with the ratio of combustion chamber height
The sludge anhydration burning method: the gas flow rate of combustion chamber is 1.5～2.5 times of combustion chamber critical fludization velocities, combustion chamber fluidisation excess air coefficient is 1.38～1.42, moisture content is that the high moisture sluge of 75%-85% drops on the air distribution plate of going to bed after furnace roof mud entrance feeds, mummification heats up under the heating from leave the bed combustion chamber high temperature flue gas and high hotbed material, move to discharge gate on bed surface owing to fluidization simultaneously, the mud of removing moisture content behind the part moisture and be 38%-42% with the bed material through discharge gate, under the control of batcher, enter the combustion chamber, continue mummification and burning in the combustion chamber, burning can be kept in the assurance combustion chamber, and ignition temperature reaches 800～900 ℃, gas residence time 〉=2 second, when mud butt calorific value is crossed when low, it is combustion-supporting to add the auxiliary fuel coal by the auxiliary fuel entrance, the flying dust that burning produces, flue gas is expected heat exchange through the bed that the blast cap on the air distribution plate of going to bed enters on mummification chamber and the mummification chamber, high-temperature flue gas, become temperature after flying dust and the wet mud heat exchange and be 250～350 ℃ middle temperature flue gas and flying dust, because the indoor mud of mummification and bed material granularity are larger, therefore the mud that carries of flue gas, the bed material can fall along the burner hearth wall, and middle temperature flue gas and flying dust enter air preheater by exhanst gas outlet and are used for heating fresh air to 120～150 ℃, fresh air enters the combustion chamber by primary air nozzle and high pressure air port, enter the mummification chamber by replenishing the wind entrance, replenish wind entrance air quantity should be primary air nozzle and high pressure tuyere air volume and 2.1～2.3 times, to guarantee the realization of combustion chamber and mummification chamber 1 fluidisation.
The present invention has reduced the outer drying equipment of stove, reduced the sludge anhydration burning technology because the heat loss that the drying equipment heat exchange efficiency produces, reduce investment and the operating cost of the outer drying equipment of stove, reduced the complexity of system, in single fluidised bed stove, can realize the smooth combustion of mud.
Description of drawings
Fig. 1 is sludge anhydration burning apparatus structure schematic diagram;
Among the figure, mummification chamber 1, mud entrance 2, exhanst gas outlet 3, discharge gate 4, additional wind entrance 5, the air distribution plate 6 of going to bed, combustion chamber 7, auxiliary fuel entrance 8, feedback outlet 9, the air distribution plate 10 of leaving the bed, slag-drip opening 11, primary air nozzle 12, the drainage conduit of going to bed 13, batcher 14, high pressure air port 15, the feed back pipe 16 of leaving the bed.
The specific embodiment
As shown in Figure 1, the device of sludge anhydration burning comprises mummification chamber 1, mud entrance 2, exhanst gas outlet 3, discharge gate 4, replenishes wind entrance 5, the air distribution plate 6 of going to bed, combustion chamber 7, auxiliary fuel entrance 8, feedback outlet 9, the air distribution plate 10 of leaving the bed, slag-drip opening 11, primary air nozzle 12, the drainage conduit of going to bed 13, batcher 14, high pressure air port 15, the feed back pipe 16 of leaving the bed; The device body upper end is provided with mud entrance 2, exhanst gas outlet 3, be provided with in turn from top to bottom mummification chamber 1 in the device body, the air distribution plate 6 of going to bed, combustion chamber 7, the air distribution plate 10 of leaving the bed, slag-drip opening 11, the device body sidewall of air distribution plate 6 tops of going to bed is provided with and replenishes wind entrance 5, the device body sidewall of air distribution plate 10 tops of leaving the bed is provided with auxiliary fuel entrance 8, the device body sidewall of air distribution plate 10 belows of leaving the bed is provided with primary air nozzle 12, and 1 top, mummification chamber is by discharge gate 4, the drainage conduit 13 of going to bed, batcher 14, high pressure air port 15, the feed back pipe 16 of leaving the bed, feedback outlet 9 links to each other with 7 bottoms, combustion chamber.
Described discharge gate (4) is arranged on 0.65～0.67 place of mummification chamber (1) height.Totally 4 of described additional wind entrances 5 lay respectively at four jiaos of the device body sidewalls of air distribution plate 6 tops of going to bed.Described mummification chamber 1 volume is 4.9～5.1:1 with the ratio of combustion chamber 7 volumes, and mummification chamber 1 cross-sectional area is 2.9～3.1:1 with the ratio of combustion chamber 7 cross-sectional areas, and mummification chamber 1 height is 1.58～1.75:1 with the ratio of combustion chamber 7 height.
The sludge anhydration burning method: the gas flow rate of combustion chamber 7 is 1.5～2.5 times of combustion chamber 7 critical fludization velocities, combustion chamber 7 fluidisation excess air coefficients are 1.38～1.42, moisture content is that the high moisture sluge of 75%-85% drops on the air distribution plate 6 of going to bed after furnace roof mud entrance 2 feeds, mummification heats up under the heating from lower bed combustor 7 high-temperature flue gas and high hotbed material, simultaneously owing to fluidization is moved to discharge gate 4 on bed surface, the mud of removing moisture content behind the part moisture and be 38%-42% with the bed material through discharge gate 4, under the control of batcher 14, enter combustion chamber 7,7 continue mummification and burning in the combustion chamber, burning can be kept in assurance combustion chamber 7, and ignition temperature reaches 800～900 ℃, gas residence time 〉=2 second, when mud butt calorific value is crossed when low, it is combustion-supporting to add the auxiliary fuel coal by auxiliary fuel entrance 8, the flying dust that burning produces, flue gas enters mummification chamber 1 through the blast cap on the air distribution plate 6 of going to bed and expects heat exchange with the bed on the mummification chamber 1, high-temperature flue gas, become temperature after flying dust and the wet mud heat exchange and be 250～350 ℃ middle temperature flue gas and flying dust, because mummification chamber 1 interior mud and bed material granularity are larger, therefore the mud that carries of flue gas, the bed material can fall along the burner hearth wall, and middle temperature flue gas and flying dust enter air preheater by exhanst gas outlet 3 and are used for heating fresh air to 120～150 ℃, fresh air enters combustion chamber 7 by primary air nozzle 12 and high pressure air port 15, enter mummification chamber 1 by replenishing wind entrance 5, replenish wind entrance 5 air quantity should be primary air nozzle 12 and high pressure air port 15 air quantity and 2.1～2.3 times, to guarantee the realization of combustion chamber 7 and mummification chamber 1 fluidisation.
Take the device of the sludge anhydration burning of scale 100 ton per days as example, the moisture percentage in sewage sludge of access to plant is 75-85%, the butt higher calorific value is 12-13 million Jiao/kilograms, combustion chamber 7 fluidisation excess air coefficients are 1.4, combustion chamber 7 gas flow rates are 2 times of combustion chamber 7 critical fludization velocities, complete oxidation index≤50 milligram/cubic metre, combustion chamber 7 outlet oxygen content of smoke gas (percentage by volume) are 6-10%, deslagging, the hot burn decrement rate of flying dust≤3%; It is 40% that moisture percentage in sewage sludge is discharged in mummification chamber 1, enter the sludge quantity of combustion chamber 7 according to the 1 mud liquid level adjustment of mummification chamber, the flue gas that discharge mummification chamber 1 is sent to the deduster dedusting behind air preheater, be sent to smoke processing system (multistage flue gas washing tower) again and process rear qualified discharge.
In above-mentioned example, with moisture content 80%, the mud of butt higher calorific value 12.5 million Jiao/kilograms is example, and described sludge anhydration burning device is calculated.Process mud per ton and need 0.8 ton of transpiring moisture (moisture content drops to 0 by 80%), can get 0.2 ton of dewatered sludge; By 20 ℃ of water vapours that are heated to 300 ℃ of room temperature, institute's energy requirement is (3074.54-334.99) kilojoule per kilogram with 0.8 ton of water
800 kilograms=2191640 kilojoules; The thermal efficiency of dewatered sludge burning is in 88%, and the heat that sludge incineration produces is 12.5
10
3Kilojoule per kilogram
200 kilograms
The 88%=2200000 kilojoule.Hence one can see that, and to described sludge anhydration burning device, mud is substantially can keep smooth combustion, only needs too high at moisture percentage in sewage sludge or sludge calorific value is crossed and added auxiliary fuel when low and get final product.
Claims (5)
1. the device of a sludge anhydration burning is characterized in that comprising mummification chamber (1), mud entrance (2), exhanst gas outlet (3), discharge gate (4), replenishes wind entrance (5), the air distribution plate of going to bed (6), combustion chamber (7), auxiliary fuel entrance (8), feedback outlet (9), the air distribution plate of leaving the bed (10), slag-drip opening (11), primary air nozzle (12), the drainage conduit of going to bed (13), batcher (14), high pressure air port (15), the feed back pipe (16) of leaving the bed; The device body upper end is provided with mud entrance (2), exhanst gas outlet (3), be provided with in turn from top to bottom mummification chamber (1) in the device body, the air distribution plate (6) of going to bed, combustion chamber (7), the air distribution plate (10) of leaving the bed, slag-drip opening (11), the device body sidewall of air distribution plate (6) top of going to bed is provided with and replenishes wind entrance (5), the device body sidewall of air distribution plate (10) top of leaving the bed is provided with auxiliary fuel entrance (8), the device body sidewall of air distribution plate (10) below of leaving the bed is provided with primary air nozzle (12), and top, mummification chamber (1) is by discharge gate (4), the drainage conduit of going to bed (13), batcher (14), high pressure air port (15), the feed back pipe (16) of leaving the bed, feedback outlet (9) links to each other with combustion chamber (7) bottom.
2. the device of a kind of sludge anhydration burning according to claim 1 is characterized in that described discharge gate (4) is arranged on 0.65～0.67 place of mummification chamber (1) height.
3. the device of a kind of sludge anhydration burning according to claim 1 is characterized in that totally 4 of described additional wind entrances (5), lays respectively at four jiaos of the device body sidewalls of the air distribution plate of going to bed (6) top.
4. the device of a kind of sludge anhydration burning according to claim 1, the ratio that it is characterized in that described mummification chamber (1) volume and combustion chamber (7) volume is 4.9～5.1:1, the ratio of mummification chamber (1) cross-sectional area and combustion chamber (7) cross-sectional area is 2.9～3.1:1, and mummification chamber (1) height is 1.58～1.75:1 with the ratio of combustion chamber (7) height.
5. sludge anhydration burning method that use is installed as claimed in claim 1, it is characterized in that: the gas flow rate of combustion chamber (7) is 1.5～2.5 times of combustion chambers (7) critical fludization velocities, combustion chamber (7) fluidisation excess air coefficient is 1.38～1.42, moisture content is that the high moisture sluge of 75%-85% drops on the air distribution plate of going to bed (6) after mud entrance (2) feeds, intensification mummification under from the heating of combustion chamber (7) high-temperature flue gas and high hotbed material, move to discharge gate (4) on bed surface owing to fluidization simultaneously, the mud of removing moisture content behind the part moisture and be 38%-42% with the bed material through discharge gate (4), under the control of batcher (14), enter combustion chamber (7), (7) continue mummification and burning in the combustion chamber, burning can be kept in assurance combustion chamber (7), and ignition temperature reaches 800～900 ℃, gas residence time 〉=2 second, when mud butt calorific value is crossed when low, it is combustion-supporting to add the auxiliary fuel coal by auxiliary fuel entrance (8), the flying dust that burning produces, flue gas enters mummification chamber (1) through the blast cap on the air distribution plate of going to bed (6) and expects heat exchange with the bed on the mummification chamber (1), high-temperature flue gas, become temperature after flying dust and the wet mud heat exchange and be 250～350 ℃ middle temperature flue gas and flying dust, because the interior mud in mummification chamber (1) and bed material granularity are larger, therefore the mud that carries of flue gas, the bed material can fall along the burner hearth wall, and middle temperature flue gas and flying dust enter air preheater by exhanst gas outlet (3) and are used for heating fresh air to 120～150 ℃, fresh air enters combustion chamber (7) by primary air nozzle (12) and high pressure air port (15), enter mummification chamber (1) by replenishing wind entrance (5), replenish wind entrance (5) air quantity should be primary air nozzle (12) and high pressure air port (15) air quantity and 2.1～2.3 times, with the realization of assurance combustion chamber (7) and mummification chamber (1) fluidisation.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104456583A (en) * | 2014-11-24 | 2015-03-25 | 南京工大环境科技有限公司 | Chemical sludge incinerating technology and device |
Families Citing this family (4)
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| CN103175198B (en) * | 2013-04-08 | 2016-03-23 | 河北省电力勘测设计研究院 | CFBB continuous supplementation bed materials device |
| CN104819474B (en) * | 2015-05-12 | 2017-01-25 | 江苏中世环境科技股份有限公司 | Efficient smoke-free carbonization device |
| CN104848230B (en) * | 2015-05-31 | 2017-01-25 | 北京四维天拓技术有限公司 | Cyclone incinerator |
| CN110822452B (en) * | 2019-12-03 | 2021-05-14 | 北京能大环保科技有限公司 | Sludge treatment equipment based on environmental protection |
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Cited By (2)
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| CN104456583A (en) * | 2014-11-24 | 2015-03-25 | 南京工大环境科技有限公司 | Chemical sludge incinerating technology and device |
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Application publication date: 20120919 Assignee: Zhejiang Wuhua Tianbao Energy Environmental Protection Co., Ltd. Assignor: Zhejiang University Contract record no.: 2018330000056 Denomination of invention: Sludge drying and incineration device and method Granted publication date: 20130424 License type: Common License Record date: 20180522 |