CN101430094A - Wet sludge incineration processing method with condensing type drying - Google Patents
Wet sludge incineration processing method with condensing type drying Download PDFInfo
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- CN101430094A CN101430094A CNA2008102388694A CN200810238869A CN101430094A CN 101430094 A CN101430094 A CN 101430094A CN A2008102388694 A CNA2008102388694 A CN A2008102388694A CN 200810238869 A CN200810238869 A CN 200810238869A CN 101430094 A CN101430094 A CN 101430094A
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- fluidized bed
- dividing wall
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- 239000010802 sludge Substances 0.000 title claims abstract description 45
- 238000001035 drying Methods 0.000 title claims abstract description 41
- 238000003672 processing method Methods 0.000 title claims description 23
- 239000003546 flue gas Substances 0.000 claims abstract description 64
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 63
- 239000007789 gas Substances 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000009833 condensation Methods 0.000 claims abstract description 17
- 230000005494 condensation Effects 0.000 claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 17
- 239000000779 smoke Substances 0.000 claims description 9
- 238000005243 fluidization Methods 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000000428 dust Substances 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract 1
- 239000000446 fuel Substances 0.000 description 7
- 239000003517 fume Substances 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 239000010865 sewage Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 102000002322 Egg Proteins Human genes 0.000 description 1
- 108010000912 Egg Proteins Proteins 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 244000000010 microbial pathogen Species 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 210000004681 ovum Anatomy 0.000 description 1
- 230000003071 parasitic effect Effects 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Treatment Of Sludge (AREA)
- Drying Of Solid Materials (AREA)
Abstract
The invention discloses a wet sludge incineration treatment method with condensing type drying relates to the environmental protection technology, a circulating fluidized bed incinerator is used for carrying out the incineration treatment on the wet sludge with water content of 60-90 percent, a dividing wall type heat exchanger is arranged behind a dust remover, flue gas and the wet sludge which are discharged by the incinerator are respectively introduced into the dividing wall type heat exchanger, thereby cooling the flue gas to dew point in the heat exchanger and condensing water vapor in the flue gas; the sensible heat which is released by utilizing the wet sludge to absorb the flue gas to reduce the temperature and the latent heat which is released by water vapor condensation increase the temperature, and water is evaporated and dried; the sludge after the drying is sent to a furnace chamber of the circulating fluidized bed incinerator for incineration at the temperature of 850-900 DEG C; exhaust gas which is exhausted by the dividing wall type heat exchanger and contains the water vapor and small amount of non-condensable gas is cooled, thereby condensing the water vapor and introducing the non-condensable gas to the upper part of the furnace chamber of the incinerator for incineration. The wet sludge incineration treatment method deeply utilizes waste heat of flue gas exhaust of the incinerator for pre-drying the wet sludge, so as to achieve the purpose of energy conservation.
Description
Technical field
The present invention relates to the offal treatment technical field, particularly relate to a kind of incineration treatment method of wet mud.
Background technology
Mud is the solid residue after the sewage disposal, and sludge quantity accounts for about 1 ‰ (in moisture content 80%) of sewage load.Along with the continuous construction of sewage treatment plant, industry of China and sanitary sewage disposal amount increase sharply, and will produce more mud.The composition of mud is very complicated, except that containing a large amount of moisture, also contains organic matter, various trace elements, pathogenic microorganism and the compositions such as parasitic ovum, heavy metal of great number of organic matters, difficult degradation.How that output is huge, the sewage sludge harmlessness of complicated component, resource have become one of problem that whole world environment circle attractes attention.
It with the burning target that the method for sludge treatment of core can reach minimizing, stabilisation, innoxious and resource.The more sludge incineration method of external at present application is the method for burning after the first mummification, earlier mud is carried out burning again after the preliminary treatment such as mummification, the mummification of mud is finished by the essentially independent system of two covers with burning, complex process, the investment of equipment height, and the drying process of mud also needs to consume big energy (being generally the heat energy that the burning of electric energy or auxiliary fuel provides), thereby operating cost is high, is difficult to adapt to the national conditions of China.
Except the sludge incineration processing method that burns after the first mummification, also have in the prior art wet mud is directly added the method that burner hearth burns.Because common dewatered sludge moisture content is generally about 80%, calorific value is very low, needs to add auxiliary fuel and could keep fire box temperature, finishes sludge incineration.But so, though fire box temperature has guaranteed that the high-temperature flue gas that burner hearth is discharged must be cooled to the temperature range that deduster can bear and could discharge.If do not have hot user near the sludge incineration plant area, will cause heat waste.
Waste heat by utilizing flue gas carries out burning after the drying to wet mud again, and prior art can realize that moisture content is not higher than wet mud about 75% and does not need to add auxiliary fuel and get final product self-sustaining burning.But the dewatered sludge moisture content and the calorific value of sewage treatment plant usually fluctuate bigger at present, moisture content is more above 75% situation, as not guaranteeing the mud self-sustaining burning, still the auxiliary fuel system need be set in the sludge incineration device, in servicely also still need add auxiliary fuel, this will make investment of equipment and operating cost still high.If can on the basis that the fume afterheat that does not influence prior art utilizes, dewatered sludge be dried to moisture content earlier below 75%, can cancel the auxiliary fuel system, the investment of equipment of sludge incineration treatment system and operating cost are descended significantly.
Summary of the invention
The purpose of this invention is to provide a kind of wet sludge incineration processing method with condensing type drying, the degree of depth is utilized the waste heat predry eliminating dampness mud of incinerator smoke evacuation, to reach purpose of energy saving.
For achieving the above object, technical solution of the present invention is as follows:
A kind of wet sludge incineration processing method with condensing type drying is 60～90% wet mud with circulating fluidized bed incinerator burning disposal moisture content:
A) dividing wall type heat exchanger is set behind deduster, flue gas and wet mud that incinerator is discharged are introduced dividing wall type heat exchanger respectively, make flue gas in heat exchanger, be cooled to dew point, the steam in the flue gas is condensed; Wet mud absorbs the sensible heat of flue gas cool-down release and the latent heat that steam condenses and discharges, and elevates the temperature, and water evaporates is dried; Wherein, the steam that absorbs of the wet mud sensible heat that the latent heat that discharges discharges more than the flue gas cool-down of its absorption that condenses;
B) dried mud is sent into the circulating fluidized bed incinerator burner hearth, burns under 850～900 ℃ temperature;
C) the weary gas that contains steam and a small amount of on-condensible gas that dividing wall type heat exchanger is discharged cools off, and makes water vapor condensation, and on-condensible gas feeds the incinerator upper furnace and burns;
D) simultaneously, the flue gas after the use is discharged from dividing wall type heat exchanger.
The wet sludge incineration processing method of described band condensing type drying, its described d) step, after flue gas is discharged from dividing wall type heat exchanger, mix with the air of process preheating, again through smoke stack emission; The flue gas that the air utilization enters before the dividing wall type heat exchanger carries out preheating.The wet sludge incineration processing method of described band condensing type drying, its described d) step is after flue gas is discharged from dividing wall type heat exchanger, partly or entirely through back-end ductwork again after the heat, again through smoke stack emission.
The wet sludge incineration processing method of described band condensing type drying, its described b) step, through the mud behind the condensing type drying, send into incinerator again through redrying again and burn.
The wet sludge incineration processing method of described band condensing type drying, its described redrying, be in fluidized bed dryer, to carry out, heat release coil pipe in the fluidized bed dryer communicates with the heat exchanger in the incinerator back-end ductwork, the heat transferring medium that wherein is filled with absorbs heat from the flue gas of back-end ductwork, heat release in fluidized bed dryer; The fluidized bed dryer bottom feeds fluidization air; The weary gas that fluidized bed dryer is discharged feeds the incinerator lower furnace portion as burner hearth secondary wind; Operating temperature in the fluidized bed dryer is 75～95 ℃.
The wet sludge incineration processing method of described band condensing type drying, its described fluidized bed dryer communicates with the incinerator material returning device, and a part of circulating ash is introduced fluidized bed dryer as drying source.
The sludge incineration processing method of described band condensing type drying, its described b) step, through the mud behind the condensing type drying, moisture content is reduced to≤and 75%.
The sludge incineration processing method of described band condensing type drying, its described wet mud is through redrying, and moisture content is reduced to 5～25%.
Advantage of the present invention:
The sludge incineration processing method of band condensing type drying of the present invention, the ingenious mutual matching relationship that has utilized condensation and evaporation process, the degree of depth has been utilized residual heat from boiler fume, helps energy savings, improves system economy.
Description of drawings
Fig. 1 is the schematic diagram of the embodiment of the invention 1;
Fig. 2 is the schematic diagram of the embodiment of the invention 2;
Fig. 3 is the schematic diagram of the embodiment of the invention 3.
The specific embodiment
Principle of the present invention is:
Utilize the wet drying of mud of incinerator smoke waste heat in the prior art, only utilized the sensible heat of flue gas, temperature still is higher than the steam dew point behind the flue gas cool-down, and steam wherein can not condense, but with fume emission, steam will be taken away a large amount of latent heats of vaporization like this.The present invention is on the basis that the fume afterheat that does not influence prior art utilizes, utilize the latent heat of vaporization of steam in the flue gas, carry out predrying to wet mud, reduce its moisture content, improve its calorific value, mud after predrying is reached do not add moisture content and calorific value requirement that auxiliary fuel can self-sustaining burning.
Water vapour content (by volume) in the plain cylindrical furnace smoke evacuation generally can not surpass 20%, and this moment, the dew point of flue gas was lower than 60 ℃, and this makes the flue gas condensing heat utilize approach very limited.And water vapour content is more in the flue gas of sludge incinerator, usually surpasses 30%, and dew point is near 70 ℃; Water vapour content reaches at 50% o'clock, and then dew point can reach 80 ℃; Because contain micro-flying dust and sour gas in the flue gas, dew point also may rise to 90 ℃.Simultaneously, because the dry run of high-moisture percentage material, it mainly is the evaporation process of the moisture in the material, this process need absorbs a large amount of latent heats of vaporization, keep temperature-resistant simultaneously, this exactly can mate mutually with the steam condensation process in the flue gas: the evaporation heat absorption takes place in a side generation condensation heat release in the heat exchanger, opposite side, keeps the temperature difference constant substantially simultaneously.Therefore, the sludge incineration processing method of the band condensing type drying that utilizes the mutual coupling of this condensation and evaporation and invent can the degree of depth utilize fume afterheat, on the existing basis that utilizes fume afterheat dry wet mud, from system, reclaim a part of heat again, pushed the wet sludge anhydration burning technology to new energy-conservation height again.
Dividing wall type heat exchanger is discharged weary gas and is mainly vapor evaporated from mud, and a small amount of on-condensible gas, will lack air cooling but, makes water vapor condensation wherein; On-condensible gas directly feeds upper furnace and burns because amount is considerably less.
Wet mud is behind condensing type drying, and moisture content is reduced to below 75%, generally can reach self-sustaining burning.At this moment, mud also needs to carry out redrying, recycle the sensible heat of flue gas, mud is continued to be dried to moisture content 5～25%, reentering stove burns, help keeping fire box temperature at 850～900 ℃ like this, this temperature province all is relatively more suitable to abolishing issuable harmful substance in the sludge incineration process and carrying out desulfuration in furnace.
Redrying adopts fluidized bed dryer, feed the air that fluidisation is used from its bottom, therefore the fluidized bed dryer weary gas of discharging is mainly air and steam, also contains the foul smell that the volatile component in the mud forms simultaneously and be fluidized the mud fine powder that gas is carried secretly in drying process.Remaining moisture in steam in the weary gas and the mud after the redrying, to become the steam in the flue gas after the burning, weary gas directly feeds burner hearth will provide water vapour content higher flue gas for condensing type drying, guarantee that wet mud is dried to moisture content below 75% in the condensing type drying process.
To lack gas and feed the incinerator lower furnace portion, the intersection of emulsion zone and dilute-phase zone as burner hearth secondary wind, can directly carry out the high temperature incineration processing with foul smell and the mud fine powder that lacks in the gas; Simultaneously, the steam specific heat in the weary gas is much larger than air, burns the high-temperature flue gas that contains a large amount of steam that the back produces and brings a large amount of heats into back-end ductwork from burner hearth, the heat exchanger in the back-end ductwork thereby can absorb more heats and offer fluidized bed dryer; In addition, owing to contain a large amount of nitrogen in the mud, if adopt conventional secondary wind, the N0x concentration of emission is still very high; Feed burner hearth as secondary wind and will lack gas, both utilized the air in the weary gas to carry out staged air distribution, more utilized a large amount of water vapours contained in the weary gas to form NH
3Thereby, further reduce the NOx concentration of emission.
Because the flue gas that dividing wall type heat exchanger is discharged is a saturation state, flue gas will have steam in chimney reduces along with temperature and continues condensation, for fear of this problem, after needing heat to flue gas again through smoke stack emission.The means that flue gas is heated can be to mix with the hot-air of process preheating, also can be that part or all of flue gas is heated.No matter be preheating of air, or the heat again of flue gas, heat all comes from the higher flue gas of temperature before the feeding dividing wall type heat exchanger.Contain more steam owing to feed in the flue gas before the dividing wall type heat exchanger, so enthalpy is higher, therefrom the absorption portion heat is used for directly or by a large amount of condensed flue gases of indirect steam, its temperature is reduced significantly.
Therefore, the sludge incineration processing method of band condensing type drying of the present invention, the ingenious mutual matching relationship that has utilized condensation and evaporation process, the degree of depth has been utilized residual heat from boiler fume, helps energy savings, improves system economy.
Embodiment 1
In circulating fluidized bed incinerator, burn wet mud through super-dry, incinerator is discharged 150 ℃, humidity are 50% flue gas D, after deduster 6 dedustings, feeding a side of dividing wall type heat exchanger 7, is the opposite side that 80% wet mud A sends into dividing wall type heat exchanger 7 simultaneously with 25 ℃, moisture content.Flue gas D is cooled off by mud A, is cooled to dew point, water vapor condensation, and be chilled to 70 ℃ excessively, draw dividing wall type heat exchanger 7.Mud A is by the flue gas indirect, and water evaporates is dried to moisture content 75%, 85 ℃, discharges dividing wall type heat exchanger 7, delivers to incinerator burner hearth 1 and burns.
The weary gas E that dividing wall type heat exchanger 7 is discharged sprays cooling, makes water vapor condensation wherein, and a small amount of on-condensible gas F feeds incinerator burner hearth 1 top burning disposal.
Be the steam-laden flue gas further condensation in chimney avoid dividing wall type heat exchanger 7 to discharge, with its all after back-end ductwork 4 is reheated to 130 ℃ again by smoke stack emission.
Burn the wet mud through super-dry in circulating fluidized bed incinerator, the hot flue gas D with incinerator is discharged after deduster 6 dedustings, feeds a side of dividing wall type heat exchanger 7, is the opposite side that 80% wet mud A sends into dividing wall type heat exchanger 7 simultaneously with moisture content.Flue gas D is cooled off by mud, is cooled to dew point, water vapor condensation; Mud A is by the flue gas indirect, and water evaporates is dried to moisture content 75%; The weary gas E that dividing wall type heat exchanger 7 is discharged sprays cooling in cooler 9, make water vapor condensation wherein, and a small amount of on-condensible gas F feeds incinerator burner hearth 1 top burning disposal.
Deliver to fluidized bed dryer 5 through the mud B of condensing type drying and carry out redrying.Heat release coil pipe in the fluidized bed dryer 5 communicates with the heat exchanger in the incinerator back-end ductwork 4, and the heat transferring medium that wherein is filled with absorbs heat from the flue gas of back-end ductwork 4, heat release in fluidized bed dryer 5; Fluidized bed dryer 5 bottoms feed fluidization air I; The weary gas G that fluidized bed dryer 5 is discharged feeds incinerator burner hearth 1 bottom as burner hearth secondary wind; Operating temperature in the fluidized bed dryer 5 is 75 ℃.Mud is the dewatered sludge C of moisture content 15% through fluidized bed dryer 5 redryings, sends in the incinerator burner hearth 1 again and burns.
The flue gas that dividing wall type heat exchanger 7 is discharged mixes the back by chimney 10 dischargings with the hot-air H that is preheating to 200 ℃; Hot-air H comes from the air heater that is arranged in the boiler back end ductwork 4, utilizes dividing wall type drier 7 flue gas before of flowing through to heat.
Embodiment 3
Burn the wet mud through super-dry in circulating fluidized bed incinerator, the hot flue gas D with incinerator is discharged after deduster 6 dedustings, feeds a side of dividing wall type heat exchanger 7, is the opposite side that 78% wet mud A sends into dividing wall type heat exchanger 7 simultaneously with moisture content.Flue gas D is cooled off by mud, is cooled to dew point, water vapor condensation; Mud A is by the flue gas indirect, and water evaporates is dried to moisture content 74%; The weary gas E that dividing wall type heat exchanger 7 is discharged sprays cooling in cooler 9, make water vapor condensation wherein, and a small amount of on-condensible gas F feeds incinerator burner hearth 1 top burning disposal.
Deliver to fluidized bed dryer 5 through the mud B of condensing type drying and carry out redrying.Heat release coil pipe in the fluidized bed dryer 5 communicates with the heat exchanger in the incinerator back-end ductwork 4, and the heat transferring medium that wherein is filled with absorbs heat from the flue gas of back-end ductwork 4, heat release in fluidized bed dryer 5; Fluidized bed dryer 5 communicates with the material returning device 3 of separator 2 bottoms, and a part of circulating ash J is introduced fluidized bed dryer 5 as drying source.Fluidized bed dryer 5 bottoms feed fluidization air I; The weary gas G that fluidized bed dryer 5 is discharged feeds incinerator burner hearth 1 bottom as burner hearth secondary wind; Operating temperature in the fluidized bed dryer 5 is 95 ℃.Mud is the dewatered sludge C of moisture content 12% through fluidized bed dryer 5 redryings, sends in the incinerator burner hearth 1 again and burns.
The flue gas that dividing wall type heat exchanger 7 is discharged mixes the back by chimney 10 dischargings with the hot-air H that is preheating to 180 ℃; Hot-air H comes from the air heater that is arranged in the boiler back end ductwork 4, utilizes dividing wall type drier 7 flue gas before of flowing through to heat.
Claims (8)
1. wet sludge incineration processing method with condensing type drying is 60～90% wet mud with circulating fluidized bed incinerator burning disposal moisture content, it is characterized in that:
A) dividing wall type heat exchanger is set behind deduster, flue gas and wet mud that incinerator is discharged are introduced dividing wall type heat exchanger respectively, make flue gas in heat exchanger, be cooled to dew point, the steam in the flue gas is condensed; Wet mud absorbs the sensible heat of flue gas cool-down release and the latent heat that steam condenses and discharges, and elevates the temperature, and water evaporates is dried; Wherein, the steam that absorbs of the wet mud sensible heat that the latent heat that discharges discharges more than the flue gas cool-down of its absorption that condenses;
B) dried mud is sent into the circulating fluidized bed incinerator burner hearth, burns under 850～900 ℃ temperature;
C) the weary gas that contains steam and a small amount of on-condensible gas that dividing wall type heat exchanger is discharged cools off, and makes water vapor condensation, and on-condensible gas feeds the incinerator upper furnace and burns;
D) flue gas is discharged from dividing wall type heat exchanger.
2. by the wet sludge incineration processing method of the described band condensing type drying of claim 1, it is characterized in that described d) step, after flue gas is discharged from dividing wall type heat exchanger, mix with the air of process preheating, again through smoke stack emission; The flue gas that the air utilization enters before the dividing wall type heat exchanger carries out preheating.
3. by the wet sludge incineration processing method of the described band condensing type drying of claim 1, it is characterized in that described d) step, after flue gas is discharged from dividing wall type heat exchanger, partly or entirely through back-end ductwork again after the heat, again through smoke stack emission.
4. by the wet sludge incineration processing method of the described band condensing type drying of claim 1, it is characterized in that described b) step, through the mud behind the condensing type drying, send into incinerator again through redrying again and burn.
5. press the wet sludge incineration processing method of the described band condensing type drying of claim 4, it is characterized in that, described redrying, be in fluidized bed dryer, to carry out, heat release coil pipe in the fluidized bed dryer communicates with the heat exchanger in the incinerator back-end ductwork, the heat transferring medium that wherein is filled with absorbs heat from the flue gas of back-end ductwork, heat release in fluidized bed dryer; The fluidized bed dryer bottom feeds fluidization air; The weary gas that fluidized bed dryer is discharged feeds the incinerator lower furnace portion as burner hearth secondary wind; Operating temperature in the fluidized bed dryer is 75～95 ℃.
6. by the wet sludge incineration processing method of the described band condensing type drying of claim 5, it is characterized in that described fluidized bed dryer communicates with the incinerator material returning device, a part of circulating ash is introduced fluidized bed dryer as drying source.
7. by the sludge incineration processing method of the described band condensing type drying of claim 1, it is characterized in that described b) step, through the mud behind the condensing type drying, moisture content is reduced to≤and 75%.
8. by the sludge incineration processing method of the described band condensing type drying of claim 4, it is characterized in that described wet mud is through redrying, moisture content is reduced to 5～25%.
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103712220A (en) * | 2013-12-26 | 2014-04-09 | 四川四通欧美环境工程有限公司 | Waste incineration smoke waste heat utilization system |
| CN106017064A (en) * | 2016-06-29 | 2016-10-12 | 浙江瑞丰环保科技股份有限公司 | Combined deodorization technology of biomass heat source |
| CN108328901A (en) * | 2018-03-29 | 2018-07-27 | 天津大学 | A kind of sludge drying mechanism integrated based on waste heat |
| CN111170608A (en) * | 2019-12-05 | 2020-05-19 | 大连绿诺集团有限公司 | Municipal sludge dewatering, drying and burning treatment system without adding fuel |
| CN111288463A (en) * | 2020-03-11 | 2020-06-16 | 东南大学 | Sludge drying and incinerating system and drying and incinerating method |
| CN111895415A (en) * | 2020-07-30 | 2020-11-06 | 山东大学 | Wet garbage drying system |
| CN112013638A (en) * | 2020-07-30 | 2020-12-01 | 国网山东省电力公司电力科学研究院 | Garbage drying system and method utilizing flue gas waste heat |
| CN112197278A (en) * | 2020-10-28 | 2021-01-08 | 西安热工研究院有限公司 | System for coupling sludge drying incineration of secondary reheating power station boiler |
| CN112390504A (en) * | 2020-12-06 | 2021-02-23 | 哈尔滨华崴重工有限公司 | Fluidized bed reactor and system and method for drying and incinerating sludge by using same |
| CN112672983A (en) * | 2019-03-01 | 2021-04-16 | 月岛机械株式会社 | Treatment equipment and treatment method for organic sludge |
| CN115677374A (en) * | 2022-11-15 | 2023-02-03 | 北京科技大学 | Method for condensing wet flue gas at condensation section of ceramsite roasting kiln |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103712220A (en) * | 2013-12-26 | 2014-04-09 | 四川四通欧美环境工程有限公司 | Waste incineration smoke waste heat utilization system |
| CN103712220B (en) * | 2013-12-26 | 2017-01-18 | 四川四通欧美环境工程有限公司 | Waste incineration smoke waste heat utilization system |
| CN106017064A (en) * | 2016-06-29 | 2016-10-12 | 浙江瑞丰环保科技股份有限公司 | Combined deodorization technology of biomass heat source |
| CN108328901A (en) * | 2018-03-29 | 2018-07-27 | 天津大学 | A kind of sludge drying mechanism integrated based on waste heat |
| CN112672983A (en) * | 2019-03-01 | 2021-04-16 | 月岛机械株式会社 | Treatment equipment and treatment method for organic sludge |
| CN111170608A (en) * | 2019-12-05 | 2020-05-19 | 大连绿诺集团有限公司 | Municipal sludge dewatering, drying and burning treatment system without adding fuel |
| CN111288463A (en) * | 2020-03-11 | 2020-06-16 | 东南大学 | Sludge drying and incinerating system and drying and incinerating method |
| CN111895415A (en) * | 2020-07-30 | 2020-11-06 | 山东大学 | Wet garbage drying system |
| CN112013638A (en) * | 2020-07-30 | 2020-12-01 | 国网山东省电力公司电力科学研究院 | Garbage drying system and method utilizing flue gas waste heat |
| CN112197278A (en) * | 2020-10-28 | 2021-01-08 | 西安热工研究院有限公司 | System for coupling sludge drying incineration of secondary reheating power station boiler |
| CN112390504A (en) * | 2020-12-06 | 2021-02-23 | 哈尔滨华崴重工有限公司 | Fluidized bed reactor and system and method for drying and incinerating sludge by using same |
| CN115677374A (en) * | 2022-11-15 | 2023-02-03 | 北京科技大学 | Method for condensing wet flue gas at condensation section of ceramsite roasting kiln |
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| CN101430094B (en) | 2010-06-23 |
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