CN116538507A - System and method for cooperatively disposing organic hazardous waste through temperature-control oxygen-control combustion - Google Patents
System and method for cooperatively disposing organic hazardous waste through temperature-control oxygen-control combustion Download PDFInfo
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- CN116538507A CN116538507A CN202210086536.4A CN202210086536A CN116538507A CN 116538507 A CN116538507 A CN 116538507A CN 202210086536 A CN202210086536 A CN 202210086536A CN 116538507 A CN116538507 A CN 116538507A
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- kiln
- rotary kiln
- air duct
- sintering
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- 238000002485 combustion reaction Methods 0.000 title claims abstract description 155
- 239000002920 hazardous waste Substances 0.000 title claims abstract description 145
- 238000000034 method Methods 0.000 title claims description 110
- 239000000463 material Substances 0.000 claims abstract description 170
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 106
- 239000001301 oxygen Substances 0.000 claims abstract description 106
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 106
- 238000000197 pyrolysis Methods 0.000 claims abstract description 101
- 239000002994 raw material Substances 0.000 claims abstract description 31
- 238000005245 sintering Methods 0.000 claims description 175
- 239000002893 slag Substances 0.000 claims description 172
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 117
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 95
- 239000003546 flue gas Substances 0.000 claims description 95
- 239000007789 gas Substances 0.000 claims description 64
- 229910052742 iron Inorganic materials 0.000 claims description 57
- 230000008569 process Effects 0.000 claims description 43
- 239000002826 coolant Substances 0.000 claims description 24
- 238000001514 detection method Methods 0.000 claims description 23
- 230000001502 supplementing effect Effects 0.000 claims description 19
- 239000013589 supplement Substances 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 9
- 239000005416 organic matter Substances 0.000 claims description 9
- 239000000779 smoke Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 8
- 230000008859 change Effects 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 6
- 238000012544 monitoring process Methods 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 230000000295 complement effect Effects 0.000 claims description 5
- 238000011278 co-treatment Methods 0.000 claims 1
- 229910000831 Steel Inorganic materials 0.000 description 17
- 239000010959 steel Substances 0.000 description 17
- 238000004056 waste incineration Methods 0.000 description 14
- 230000001276 controlling effect Effects 0.000 description 12
- 239000002910 solid waste Substances 0.000 description 11
- 230000000694 effects Effects 0.000 description 9
- 239000002699 waste material Substances 0.000 description 8
- 238000009826 distribution Methods 0.000 description 7
- 230000007613 environmental effect Effects 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 229910001385 heavy metal Inorganic materials 0.000 description 5
- 230000003247 decreasing effect Effects 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000005496 eutectics Effects 0.000 description 4
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- 239000010802 sludge Substances 0.000 description 4
- 230000002195 synergetic effect Effects 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
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- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
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- 238000005338 heat storage Methods 0.000 description 1
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- 239000007924 injection Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/50—Control or safety arrangements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L1/00—Passages or apertures for delivering primary air for combustion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L9/00—Passages or apertures for delivering secondary air for completing combustion of fuel
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B19/00—Combinations of furnaces of kinds not covered by a single preceding main group
- F27B19/04—Combinations of furnaces of kinds not covered by a single preceding main group arranged for associated working
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B9/00—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity
- F27B9/30—Details, accessories, or equipment peculiar to furnaces of these types
- F27B9/38—Arrangements of devices for charging
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2201/00—Pretreatment
- F23G2201/30—Pyrolysing
- F23G2201/302—Treating pyrosolids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2203/00—Furnace arrangements
- F23G2203/20—Rotary drum furnace
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B9/00—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity
- F27B9/30—Details, accessories, or equipment peculiar to furnaces of these types
- F27B9/38—Arrangements of devices for charging
- F27B2009/382—Charging
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27M—INDEXING SCHEME RELATING TO ASPECTS OF THE CHARGES OR FURNACES, KILNS, OVENS OR RETORTS
- F27M2003/00—Type of treatment of the charge
- F27M2003/04—Sintering
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Incineration Of Waste (AREA)
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
A system for cooperatively disposing organic hazardous waste by controlling temperature and oxygen and burning, which comprises a rotary kiln; the rotary kiln comprises a kiln head, a kiln body and a kiln tail; a material inlet is arranged on the kiln head; the kiln body comprises a kiln lining and a kiln chamber; a material outlet and a kiln tail air duct are arranged on the kiln tail; along the trend of the materials, the hearth is divided into a pyrolysis chamber and an incineration chamber; an air flue in the kiln is arranged in the furnace lining corresponding to the pyrolysis chamber; one end of the air duct in the kiln extends into the kiln head, and the other end of the air duct in the kiln is communicated with the incineration chamber; the kiln head is also provided with an annular air duct; the kiln inner air channel is communicated with a primary air channel arranged outside the rotary kiln through an annular air channel; a secondary air duct is separated from the primary air duct; the secondary air channel passes through the kiln head and is communicated with the pyrolysis chamber. The invention provides a concurrent and countercurrent dual-purpose rotary kiln, which adopts different combustion modes aiming at different raw materials and expands the adaptability of the rotary kiln to different materials.
Description
Technical Field
The invention relates to a treatment process of organic hazardous waste, in particular to a system and a method for cooperatively treating the organic hazardous waste by controlling temperature and oxygen combustion, belonging to the technical field of the cooperative sintering treatment of the organic hazardous waste.
Background
The rotary incineration kiln can be used for incinerating organic hazardous waste and is an important component device of a hazardous waste incineration system. The organic hazardous waste contains organic matters and has a certain heat value, so that the organic hazardous waste is suitable for being disposed in an incineration mode, the purpose of reducing the volume of the hazardous waste can be achieved, and the heat energy in the waste can be recovered, so that the comprehensive utilization of resources is achieved.
The existing hazardous waste incineration rotary kiln is mainly used for incinerating municipal hazardous waste, including organic resin, municipal sludge and the like, but with the improvement of the requirement of 'solid waste not leaving factory' of steel enterprises, part of steel factories begin to build hazardous waste incineration engineering in the factory for incinerating hazardous waste generated by the steel enterprises. However, the iron content of dangerous waste produced by iron and steel enterprises is high, slag bonding and caking are easy to occur, and meanwhile, the existing municipal dangerous waste incineration rotary kiln also has the phenomena of uneven temperature distribution and lower incineration efficiency.
In the prior art, rotary kilns are mostly used for disposing municipal organic hazardous waste, and the iron content is low. The hazardous waste incineration and flue gas purification treatment process of 'rotary kiln + secondary combustion chamber + exhaust-heat boiler (SNCR denitration) +flue gas quenching + dry deacidification (slaked lime and active carbon injection) +bag-type dust remover + induced draft fan + pre-wash tower + wet-type washing tower + flue gas reheater + chimney' is generally adopted. The process takes the main purpose of fully burning organic matters in hazardous waste, and adopts a rotary kiln as incineration equipment, as shown in figure 1. In the figure, the zone I is a kiln head feeding zone, the zone II is an incineration zone, the kiln head feeding zone is provided with a hazardous waste feeding port and an air inlet, and the kiln tail is provided with a material outlet. In practical application, the rotary kiln has an inclination angle of about 5 degrees (about high and low in fig. 1), so that materials and air enter the rotary kiln from the kiln head (zone I), and under the action of rotation and inclination angle of the kiln body, the materials move to the kiln tail, are mixed with air and burnt, and finally residues are discharged from the material outlet. At present, residues in the market are discharged out of a rotary kiln and then directly fall into a water tank for wet cooling, and the cooled residues are fished out and solidified for landfill.
The main incineration temperature of the hazardous waste in the rotary kiln is about 850-950 ℃ and the residence time is 30-40 min, under the condition, the organic matters in the hazardous waste can be fully combusted. According to the current standard and the environmental requirements, the burning rate of the incineration residue must reach below 5 percent.
The prior art hazardous waste incineration technology mainly treats municipal organic hazardous waste, however, when the organic hazardous waste of the steel plant is treated, the iron content is higher in the organic hazardous waste of the steel plant, such as steel rolling oil sludge, and the iron content reaches 50% -60%. If the prior art is still adopted to burn the iron-containing fatlute, the iron element and the metal oxide in the ash form low-temperature eutectic, and slag and ring are extremely easy to form in the rotary kiln at the burning temperature of 850-950 ℃. The iron-containing residues are formed into large blocks in the rotary kiln, so that the strength is high, the rotary kiln is blocked, and normal production cannot be performed.
In the prior art, all organic matters are fully burnt and released in the rotary kiln, and the waste heat of the rotary kiln is recovered by the waste incineration disposal line of the hazardous waste of the rotary kiln, but the heat dissipation of the rotary kiln is large, and the heat utilization rate of the organic matters is low.
In the prior art, incineration residues and fly ash of municipal hazardous waste usually adopt cement, lime and water to carry out simple and stable solidification due to higher heavy metals and certain dioxin pollutants, and then are safely buried, so that the disposal process is waste of residue resources, particularly iron resources in hazardous waste of steel works, has high content and high recovery value, and the iron resources are not effectively recycled. And landfill does not completely eliminate the environmental influence, and the risk of secondary pollution still exists.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a system for cooperatively disposing organic hazardous waste by controlling temperature and oxygen combustion. The system comprises the rotary kiln, wherein the rotary kiln can be used for downstream and countercurrent for different types of organic hazardous waste, when the material to be treated is high-volatile organic hazardous waste, the rotary kiln can be used as a pyrolysis-incineration two-section countercurrent rotary kiln, and when the material to be treated is low-volatile organic hazardous waste, the rotary kiln can be directly changed into the downstream rotary kiln under the condition of not changing any matter, so that the adaptability of the rotary kiln to different materials is enlarged. The system also comprises a sintering machine, namely, the invention distributes the incineration residues after the hazardous waste incineration of the rotary kiln to the sintering machine for disposal, and the residual organic matters in the incineration residues can be used in a grading manner in the sintering process.
Correspondingly, the invention also provides a method for cooperatively disposing the organic hazardous waste based on the temperature-control oxygen-control combustion of the rotary kiln-sintering machine. Compared with the prior art, the method has the advantages that by controlling the incineration temperature in the rotary kiln, hazardous waste is incinerated at a temperature lower than the low-temperature eutectic point, and the phenomenon of ring-forming and slag-forming when the iron-containing organic solid waste is incinerated by the rotary kiln is effectively relieved. The incineration residue of the rotary kiln is cooperatively treated by utilizing the sintering process of the iron and steel enterprises, so that iron elements in the iron-containing solid waste can be effectively recovered, and heavy metals in the residue are treated by the sintering process, thereby thoroughly eliminating the environmental influence and secondary pollution risk of the solid waste. In addition, the temperature-control oxygen-control incineration in the rotary kiln also enables organic matters in hazardous waste to be partially preserved, fully utilized in the sintering process and improves the heat energy utilization rate.
According to a first embodiment of the present invention, a system for the synergistic disposal of organic hazardous waste by temperature-controlled oxygen-controlled combustion is provided.
A system for cooperatively disposing organic hazardous waste by controlling temperature and oxygen and burning comprises a rotary kiln. The rotary kiln comprises a kiln head, a kiln body and a kiln tail. The kiln head is provided with a material inlet. The kiln body comprises a furnace lining and a hearth. The kiln tail is provided with a material outlet and a kiln tail air duct. Along the material trend, the furnace is divided into a pyrolysis chamber and an incineration chamber. And an air duct in the kiln is arranged in the furnace lining corresponding to the pyrolysis chamber. One end of the air duct in the kiln extends into the kiln head, and the other end is communicated with the incineration chamber. The kiln head is also provided with an annular air duct. The air duct in the kiln is communicated with the primary air duct arranged outside the rotary kiln through the annular air duct. And a secondary air duct is separated from the primary air duct. The secondary air channel passes through the kiln head and is communicated with the pyrolysis chamber.
In the present invention, the system further comprises a sintering machine disposed downstream of the rotary kiln. Along the trend of the materials, a lower layer distributing machine, a middle layer distributing machine and an upper layer distributing machine are sequentially arranged above the sintering trolley at the feeding section of the sintering machine. The material outlet of the rotary kiln is connected to a lower layer material distributor, a middle layer material distributor or an upper layer material distributor.
In the present invention, the system further comprises a hot slag cooler disposed between the rotary kiln and the sintering machine. The hot slag cooler is provided with a hot slag inlet, a cold slag outlet, a cold medium inlet and a hot medium outlet. The material outlet of the rotary kiln is connected to the hot slag inlet of the hot slag cooler. The cold slag outlet of the hot slag cooler is connected to a lower layer distributor, a middle layer distributor or an upper layer distributor on the sintering machine. Preferably, the hot slag cooler is a dry hot slag cooler, preferably a dividing wall type heat exchanger.
Preferably, n kiln inner air channels are arranged in the rotary kiln. The n kiln inner air channels are uniformly distributed along the circumferential direction of the rotary kiln. The air duct in each kiln is communicated with the annular air duct arranged at the kiln head. Wherein: n is 2 to 30, preferably 3 to 20.
Preferably, a three-way valve is arranged at the position of the primary air channel, which is separated from the secondary air channel. An air extractor is arranged on the secondary air channel. Preferably, the kiln tail of the rotary kiln is also provided with a heat supplementing burner.
Preferably, a temperature detecting device is provided in the incineration chamber of the rotary kiln. And a material iron content detection device is arranged at the material inlet of the kiln head. And a gas analyzer is arranged on the primary air duct and close to the annular air duct.
According to a second embodiment of the present invention, a method for the synergistic disposal of organic hazardous waste by temperature-controlled oxygen-controlled combustion is provided.
A method of controlling temperature and oxygen combustion to co-dispose of organic hazardous waste or using the system described in the first embodiment, the method comprising the steps of:
1) And (3) pyrolysis: the high volatile organic hazardous waste is conveyed into the rotary kiln through a material inlet of the kiln head. Combustion air enters the rotary kiln through the kiln tail air duct. The high volatile organic hazardous waste firstly enters a pyrolysis cavity of the rotary kiln for drying and pyrolysis. And the material residues and pyrolysis gas after pyrolysis are fed into the incineration chamber.
2) And (3) incineration: the material residues, the pyrolysis gas and the combustion air are mixed in the incineration chamber and combusted. And discharging the burned hot slag out of the rotary kiln through a material outlet at the kiln tail. The burned flue gas is discharged out of the rotary kiln through the air duct in the kiln, the annular air duct and the primary air duct.
3) And (3) smoke circulation: and 2) part of the flue gas entering the primary air duct in the step 2) enters the rotary kiln again through the secondary air duct, and the pyrolysis and incineration processes are completed together with the materials in the rotary kiln.
Preferably, the high-volatile organic hazardous waste is organic hazardous waste with the mass percentage content of dry volatile being more than or equal to H%. Wherein: h is 6 to 12, preferably 7 to 10.
In the present invention, the method further comprises:
4) And (3) cooling: and 2) conveying the hot slag discharged from the rotary kiln in the step 2) to a hot slag cooler, and introducing a cooling medium into the hot slag cooler. And carrying out heat exchange on the hot slag and the cooling medium in a hot slag cooler, and obtaining cold slag and the heating medium after the heat exchange is completed.
5) Sintering: and (3) distributing the cold slag and the sintering raw materials obtained in the step (4) onto a sintering trolley, and igniting and sintering.
Preferably, in step 4), the cooling medium introduced into the hot slag cooler is cold air. The cold air is discharged from the hot medium outlet after heat exchange in the hot slag cooler to become hot air, and the hot air is used as combustion air to be conveyed to a kiln tail air duct of the rotary kiln.
Preferably, in step 4), the cooling medium introduced into the hot slag cooler is cooling water. The cooling water is heat-exchanged in the slag cooler to be hot water, which is then discharged from the heat medium outlet, and the hot water is used as boiler feed water.
In the invention, in the step 2), the iron content w of the high-volatile organic hazardous waste entering the rotary kiln is detected by a material iron content detection device. Determining the combustion temperature T to be controlled in the combustion chamber according to the detected iron content of the material 0 . The method comprises the following steps:
when w is more than 50%, T 0 550-650 ℃.
When 25% < w.ltoreq.50%, T 0 650-750 ℃.
When w is more than or equal to 5% and less than or equal to 25%, T 0 750-850 ℃.
When w is less than 5%, T 0 Is 850-950 ℃.
In the present invention, in step 1), the pyrolysis temperature in the pyrolysis chamber of the rotary kiln is 200 to 550 ℃, preferably 300 to 500 ℃.
In the present invention, the combustion temperature T is controlled according to the need in the incineration chamber in step 2) 0 And determining the type of the cold slag obtained in the step 4). The method comprises the following steps:
when T is 0 At 550-650 ℃, the cold slag obtained in the step 4) is high-carbon slag.
When T is 0 And at 650-850 ℃, the cold slag obtained in the step 4) is low-carbon slag.
When T is 0 And at 850-950 ℃, the cold slag obtained in the step 4) is carbon-free slag.
Preferably, the organic matter content of the high-carbon residue is more than Z%, and the organic matter content of the low-carbon residue is less than or equal to Z%. Wherein: z is 4 to 12, preferably 5 to 10.
In the invention, according to the cold slag category obtained in the step 4), the step 5) specifically comprises the following steps:
when the cold slag obtained in the step 4) is high-carbon residue, the high-carbon residue is placed in an upper layer distributing machine on a sintering machine, namely, the sintering raw material is distributed on a sintering trolley, and then the high-carbon residue is distributed above the sintering raw material through the upper layer distributing machine, and ignition sintering is performed.
When the cold slag obtained in the step 4) is low-carbon residue, at the moment, placing the sintering mixture obtained by uniformly mixing the low-carbon residue and the sintering raw material into a middle layer distributing machine on a sintering machine, distributing the sintering mixture onto a sintering trolley through the middle layer distributing machine, and igniting and sintering.
When the cold slag obtained in the step 4) is carbon-free residue, the carbon-free residue is placed into a lower layer distributing machine on a sintering machine, the carbon-free residue is distributed on a sintering trolley as a bedding material through the lower layer distributing machine, and then sintering raw materials are distributed above the bedding material, and ignition sintering is performed.
In the invention, in the burning procedure of the step 2), when the material residues, the pyrolysis gas and the combustion air are burnt, the change condition of the temperature in the burning chamber is monitored in real time, and the oxygen content and the combustible component content in the burnt flue gas are monitored in real time, so that the air intake and/or the feed amount in the rotary kiln and/or the heat supplement amount of the heat supplement burner are regulated, thereby realizing the control of the technological conditions of the burning procedure and the burning temperature in the burning chamber.
In the invention, the process conditions of the incineration procedure are controlled, and the combustion temperature in the incineration chamber is controlled, specifically comprising the following substeps:
201 When the material residues, the pyrolysis gas and the combustion air are combusted, the temperature detection device monitors the combustion temperature in the incineration chamber in real time. In the real-time monitoring process, the detected real-time combustion temperature T in the incineration chamber and the combustion temperature T required to be controlled in the incineration chamber are detected 0 A comparison is made.
201a) If the real-time combustion temperature T in the incineration chamber=the combustion temperature T to be controlled 0 The incineration procedure is normally operated at this time, and the temperature detection device continues to monitor.
201b) If the real-time combustion temperature T in the incineration chamber is less than the combustion temperature T to be controlled 0 I.e. the temperature in the incineration chamber needs to be increased. At the moment, the real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by a gas analyzer.
If the real-time oxygen content and the combustible component content in the incinerated flue gas are detected to be normal, starting a supplementary heating burner at the moment, or increasing the feeding amount in the rotary kiln and simultaneously increasing the air inlet amount in the rotary kiln, so that T=T 0 。
If the real-time oxygen content in the burnt flue gas is detected to be low, increasing the air inlet amount in the rotary kiln at the moment, and simultaneously increasing the feeding amount in the rotary kiln, or starting a complementary heat burner, so that T=T 0 。
If the real-time oxygen content in the burnt flue gas is detected to be higher and the real-time combustible component content is normal, at the moment, the air inlet amount in the rotary kiln is reduced, or the feeding amount in the rotary kiln is increased, or a complementary heat burner is started, so that T=T 0 。
201c) If the real-time combustion temperature T in the incineration chamber is more than the combustion temperature T to be controlled 0 I.e. the temperature in the incineration chamber needs to be reduced. At the moment, the real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by a gas analyzer.
If the real-time oxygen content and the combustible component content in the burnt flue gas are detected to be normal, the heat supplement amount of the heat supplement burner is reduced, or the feeding amount in the rotary kiln is reduced, and the air intake in the rotary kiln is reduced at the same time, so that T=T 0 。
If the real-time oxygen content in the burnt flue gas is detected to be low, increasing the air inlet amount in the rotary kiln, and simultaneously reducing the feeding amount in the rotary kiln or reducing the heat supplementing amount of the heat supplementing burner, so that T=T 0 。
If the real-time oxygen content in the burnt flue gas is detected to be higher and the real-time combustible component content is normal, the air inlet amount in the rotary kiln is reduced, the feeding amount in the rotary kiln is reduced, or the heat supplementing amount of the heat supplementing burner is reduced, so that T=T 0 。
According to a third embodiment of the present invention, a method for the synergistic disposal of organic hazardous waste by temperature-controlled oxygen-controlled combustion is provided.
A method of temperature-controlled oxygen-controlled combustion co-disposal of organic hazardous waste or a method of using the system of the first embodiment, the method comprising the steps of:
a) The low-volatile organic hazardous waste is conveyed into the rotary kiln through a material inlet of the kiln head. Combustion air enters the rotary kiln through a secondary air channel of the kiln head. The low-volatile organic hazardous waste and combustion air are mixed in the hearth and combusted.
b) And discharging the burned hot slag out of the rotary kiln through a material outlet at the kiln tail. And the incinerated flue gas is discharged out of the rotary kiln through a kiln tail air duct.
c) And b) conveying the hot slag discharged from the rotary kiln in the step b) to a hot slag cooler, and introducing a cooling medium into the hot slag cooler. And carrying out heat exchange on the hot slag and the cooling medium in a hot slag cooler, and obtaining cold slag and the heating medium after the heat exchange is completed.
d) And c) distributing the cold slag and the sintering raw materials obtained in the step c) onto a sintering trolley, and igniting and sintering.
Preferably, the low-volatile organic hazardous waste is organic hazardous waste with the mass percentage content of dry volatile less than H%. Wherein: h is 6 to 12, preferably 7 to 10.
Preferably, in the step a), the combustion air also enters the incineration chamber of the rotary kiln through a primary air duct, an annular air duct and an in-kiln air duct.
Preferably, the air quantity of the combustion air entering the rotary kiln through the secondary air channel accounts for 20% -45% of the total air quantity required in the rotary kiln, and preferably 30% -40%.
In the prior art, the hazardous waste incineration rotary kiln is mainly used for incinerating municipal hazardous waste, including organic resin, municipal sludge and the like, but with the improvement of the requirement of 'solid waste not leaving factory' of steel enterprises, part of steel plants start to build hazardous waste incineration engineering in the factory for incinerating hazardous waste generated by the steel enterprises. However, the iron content of dangerous waste produced by iron and steel enterprises is higher, slag bonding and caking are easy to occur, the rotary kiln is blocked, and meanwhile, the existing municipal dangerous waste incineration rotary kiln also has the phenomena of uneven temperature distribution and lower incineration efficiency. In addition, all organic matters in the hazardous waste in the prior art are fully burnt and released in the rotary kiln, and the waste heat is recovered by the waste heat boiler arranged on the hazardous waste incineration disposal line of the rotary kiln, but the heat dissipation of the rotary kiln is large, so that the heat utilization rate of the organic matters is low. In addition, the incineration residue and fly ash of municipal hazardous waste usually adopt cement, lime and water to carry out simple and stable solidification due to higher heavy metals and certain dioxin pollutants, and then carry out safe landfill, so that the disposal process is waste of residue resources, especially iron resources in hazardous waste of steel works, has high content and high recovery value, and the iron resources are not effectively recycled. And landfill does not completely eliminate the environmental influence, and the risk of secondary pollution still exists.
Aiming at the defects existing in the hazardous waste disposal process in the prior art, the invention provides a system for cooperatively disposing organic hazardous waste by controlling temperature and oxygen combustion. The system comprises a rotary kiln, wherein the rotary kiln comprises a kiln head, a kiln body and a kiln tail. The kiln head is provided with a material inlet, the kiln body comprises a furnace lining and a hearth, and the kiln tail is provided with a material outlet and a kiln tail air duct. Along the course of the material, the furnace is divided into a pyrolysis chamber and an incineration chamber. And an air flue in the kiln is arranged in the furnace lining corresponding to the pyrolysis chamber, one end of the air flue in the kiln stretches into the kiln head, and the other end of the air flue in the kiln is communicated with the incineration chamber. The kiln head is also provided with an annular air duct. The air duct in the kiln is communicated with the primary air duct arranged outside the rotary kiln through the annular air duct. And a secondary air channel is separated from the primary air channel, and the secondary air channel passes through the kiln head and is communicated with the pyrolysis chamber. In the invention, the rotary kiln can be used for carrying out forward flow and reverse flow against different types of organic hazardous waste.
When the material to be treated is high-volatile organic hazardous waste (such as iron-containing fatlute), the rotary kiln can be used as a pyrolysis-incineration two-section countercurrent rotary kiln, and at the moment, the kiln head, the pyrolysis chamber, the incineration chamber and the kiln tail are correspondingly a feeding section, a material pyrolysis section, a full incineration section and a discharging section. The high volatile organic hazardous waste is sent into the rotary kiln from the material inlet of the kiln head by a hydraulic push rod or other forms, and the combustion air reversely (opposite to the material trend) enters the rotary kiln from the kiln tail air duct. The high-volatile organic hazardous waste entering the rotary kiln firstly enters a pyrolysis chamber for drying and pyrolysis. The pyrolysis chamber is an anoxic, high temperature environment having a temperature of about 200 to 550 c (preferably 300 to 500 c). The heat source of the pyrolysis chamber is mainly heat exchange of high-temperature flue gas generated in the burning process in the hearth after the high-temperature flue gas enters the air duct in the kiln. The high-volatile organic hazardous waste is dried and pyrolyzed in a pyrolysis chamber, and the volatile matters in the material are CH 4 、H 2 And the combustible gas such as CO is separated out. The air flow direction of the material pyrolysis section is the direction from the kiln head to the kiln tail, namely the material residues and pyrolysis gas after pyrolysis enter the full burning section, and the material residues and the pyrolysis gas are mixed with combustion air entering the burning chamber and are subjected to severe burning. The burned hot slag is discharged out of the rotary kiln through a material outlet at the kiln tail, and the burned flue gas is discharged out of the rotary kiln through an air duct in the kiln, an annular air duct and a primary air duct and provides heat required by pyrolysis for the pyrolysis chamber in the process. The invention aims at the pyrolysis-incineration two-stage countercurrent incineration rotary kiln where the high-volatile organic hazardous waste is located, improves the combustion efficiency, and solves the problems that the hazardous waste containing oil sludge and the like is easy to agglomerate, slag and block the rotary kiln at present.
The secondary air duct is arranged at the kiln head position, and has the main functions of: the combustible pyrolysis gas pyrolyzed by the pyrolysis chamber (from the kiln head to the kiln tail) is mixed intensively with the mixed gas of the air and the flue gas from the incineration chamber (from the kiln tail to the kiln head), but partial combustible gas is possibly still not burnt out and is directly brought into the air duct in the kiln, so that a great amount of combustible substances are contained in the flue gas, and when the flue gas passes through the three-way valve at the connection position of the primary air duct and the secondary air duct, a part of flue gas is pumped into the secondary air duct by the air pumping device (such as an air pump) and returns to the rotary kiln again for re-reaction. The circulating flue gas also has the following functions: the pyrolysis gas volume that the material produced in pyrolysis cavity pyrolysis compares with the mixed gas of the flue gas that burns the interior material burning of burning cavity and air, and the tolerance of pyrolysis gas is very little, and like this when mixing with the mixed gas of flue gas and air, the pyrolysis gas velocity of flow is too little, is difficult to reach fine mixing combustion effect, and circulated flue gas and pyrolysis gas mixing can increase the tolerance of pyrolysis gas, increases the kinetic energy that pyrolysis gas moved to kiln tail direction, strengthens the gas mixing effect in the kiln for combustion reaction. Meanwhile, the circulating flue gas can also provide a part of heat for material pyrolysis.
When the material to be treated is low-volatile organic hazardous waste (such as converter mud), the rotary kiln can be directly changed into a concurrent rotary kiln without any change. Because the organic hazardous waste with low volatile matter has low volatile matter per se, even if the volatile matter is pyrolyzed, the volatile matter does not generate much, so the meaning of passing through the material pyrolysis section is low, and at the moment, the kiln head, the pyrolysis chamber, the incineration chamber and the kiln tail are correspondingly a feeding section, a primary incineration section, a secondary incineration section and a discharging section, wherein the secondary incineration section is a main combustion zone. The low-volatile organic hazardous waste is sent into the rotary kiln from the material inlet of the kiln head by a hydraulic push rod or other forms, a part of combustion air enters the rotary kiln from the secondary air channel of the kiln head in the same direction (the same direction as the material), and the rest of combustion air enters the incineration chamber through the primary air channel, the annular air channel and the air channel in the kiln, namely, the rest of combustion air enters the rotary kiln from the middle of the kiln body. The low-volatile organic hazardous waste entering the rotary kiln is firstly mixed with combustion air in a pyrolysis chamber (namely a primary incineration section) and combusted for the first time, and then enters the incineration chamber (namely a secondary incineration section) to be mixed with the combustion air entering from the kiln body and further combusted. And the burned hot slag is discharged out of the rotary kiln through a material outlet at the kiln tail, and the burned flue gas is discharged out of the rotary kiln through a kiln tail air duct. In the invention, the forward-flow rotary kiln can be directly changed from the original reverse-flow rotary kiln through the combustion air and the burnt flue gas, the original rotary kiln is changed into the forward-flow and reverse-flow rotary kiln, the forward-flow rotary kiln is used for disposing the low-volatile organic hazardous waste, and the reverse-flow rotary kiln is used for disposing the high-volatile organic hazardous waste, so that the adaptability of the rotary kiln to different materials is improved.
As a preferable scheme, the system for cooperatively disposing the organic hazardous waste by controlling the temperature and the oxygen and burning also comprises a sintering machine. The sintering machine is arranged downstream of the rotary kiln. Along the material trend, a lower layer distributor, a middle layer distributor and an upper layer distributor are sequentially arranged above the sintering trolley at the feeding section of the sintering machine (the number of specific distributors can be set according to specific sintering technology). The material outlet of the rotary kiln is connected to a lower layer material distributor, a middle layer material distributor or an upper layer material distributor. According to the invention, the incineration residues of the rotary kiln after the incineration of the hazardous waste are conveyed to the sintering machine for disposal, and the incineration residues are selectively distributed to the lower layer, the middle layer or the upper layer of the sintering trolley according to the incineration degree of the organic hazardous waste and the residual condition of organic matters in the incineration residues. The incineration residue after the incineration in the rotary kiln is cooperatively treated by utilizing the sintering process of the iron and steel plant, so that the iron element in the iron-containing solid waste can be effectively recovered, and the heavy metal in the residue is treated by the sintering process, thereby thoroughly eliminating the environmental influence and secondary pollution risk of the solid waste. Compared with the prior art, the temperature-control oxygen-control incineration in the rotary kiln also enables organic matters in hazardous waste to be partially preserved, fully utilized in the sintering process and improves the heat energy utilization rate.
In the invention, since the residue after the burning in the rotary kiln is co-processed in the sintering machine, if the humidity of the residue is too high, the sintering production is greatly affected, and thus the residue must be dried before being mixed into the sintering. Based on this, the system of the invention further comprises a hot slag cooler arranged between the rotary kiln and the sintering machine. The hot slag cooler is a dry hot slag cooler, such as a dividing wall heat exchanger. The dry hot slag cooler does not increase the humidity of the slag compared to the existing wet cooling. The cooling medium adopted by the hot slag cooler can adopt air or water according to the heat exchange capacity or actual needs, if the air is adopted as the cooling medium, the cold air can be fed into the rotary kiln through a kiln tail air duct of the rotary kiln to be used as combustion air after entering the hot slag cooler to be changed into hot air; if water is used as the cooling medium, the heated hot water can also be used as boiler feed water in the plant. Therefore, the heat energy recovery of the hot slag can be realized whether air or water is used as a cooling medium.
In the rotary kiln, a plurality of in-kiln air channels are arranged in the rotary kiln, and the in-kiln air channels are uniformly distributed along the circumferential direction of the rotary kiln, namely, the in-kiln air channels are uniformly arranged in the rotary kiln in a rotationally symmetrical manner. The air duct in each kiln is communicated with the annular air duct, namely, the air duct in each kiln is communicated with the primary air duct through the annular air duct. In the actual production process, the specific number and the specific size of the air channels in the kiln are determined according to the flue gas flow (or air quantity) and the size of the rotary kiln. In general, the number of air passages in the kiln may be from 2 to 30, preferably from 3 to 20, for example 12, 16, 20.
In order to facilitate the exhaust of the flue gas after the incineration in the countercurrent rotary kiln through the primary air duct and the circulation of the flue gas into the rotary kiln through the secondary air duct, and also facilitate the delivery of the combustion air of the concurrent rotary kiln into the rotary kiln through the primary air duct and the secondary air duct, the invention is provided with a three-way valve at the position of the primary air duct for separating the secondary air duct, and is provided with an air extracting device (such as an air extracting pump) for controlling the flue gas quantity circulated into the rotary kiln, and the air extracting device in the concurrent rotary kiln can control the quantity of the combustion air entering the rotary kiln through the secondary air duct.
Based on the system for cooperatively disposing the organic hazardous waste by the temperature-control oxygen-control combustion of the rotary kiln-sintering machine, the invention also provides a method for cooperatively disposing the organic hazardous waste by the temperature-control oxygen-control combustion matched with the system. When the material to be treated is high-volatile organic hazardous waste, the method for disposing the high-volatile organic hazardous waste is a method for cooperatively disposing organic hazardous waste based on temperature-control oxygen-control combustion of a counter-flow rotary kiln-sintering machine. In the method, the high-volatile organic hazardous waste is organic hazardous waste with the mass percentage content of dry volatile being more than or equal to H%; wherein: h is 6 to 12, preferably 7 to 10. The method mainly comprises the steps (or working procedures) of pyrolysis, incineration, flue gas circulation, cooling, sintering and the like. Aiming at the problems that the rotary kiln basically adopts 850-950 ℃ for burning and is extremely easy to cause slag bonding and caking phenomenon when the organic hazardous waste with higher iron content in the steel plant is treated in the prior art, the method adjusts and controls the temperature in the burning chamber (namely the main burning zone) of the rotary kiln according to the iron content of the organic hazardous waste. The adjusting method is mainly to control the air quantity and the material quantity entering the hearth of the rotary kiln and adjust the heat supplementing quantity of the heat supplementing burner when necessary. The adjustment is based on the real-time combustion temperature in the incineration chamber of the rotary kiln, the real-time oxygen content in the incinerated flue gas and the real-time combustible component content. In general, the normal oxygen content in the flue gas is 6% -10%, and if the normal oxygen content exceeds 10%, the air is excessive (namely, the oxygen content is higher), and if the normal oxygen content is lower than 6%, the air is insufficient (namely, the oxygen content is lower). The less the combustible component content in the flue gas should be, the better, if the combustible component content exceeds 5%, the higher the combustible component content is. For clean combustion, the exceeding of the combustible component content and the exceeding of the oxygen content do not generally occur simultaneously, because oxygen and the combustible component react at high temperatures.
According to the invention, the oxygen content and the temperature in the rotary kiln are controlled, so that the organic hazardous waste is burnt below the low-temperature eutectic point, the phenomenon of ring-forming and slag-forming when the iron-containing organic solid waste is burnt in the rotary kiln is effectively relieved, and the combustion efficiency is improved. In the incineration process of the invention, the specific regulation strategy of the combustion temperature in the incineration chamber of the rotary kiln is as follows:
firstly, detecting the iron content w of high-volatile organic hazardous waste entering a rotary kiln through an iron content detection device arranged at a material inlet, and determining the combustion temperature T required to be controlled in an incineration chamber according to the detected iron content of the material 0 . The method comprises the following steps:
when w is more than 50%, T 0 550-650 ℃.
When 25% < w.ltoreq.50%, T 0 650-750 ℃.
When w is more than or equal to 5% and less than or equal to 25%, T 0 750-850 ℃.
When w is less than 5%, T 0 Is 850-950 ℃.
And then the combustion temperature in the incineration chamber is monitored in real time through a temperature detection device. The detected real-time combustion temperature T in the incineration chamber and the combustion temperature T required to be controlled in the incineration chamber are processed 0 A comparison is made. If t=t 0 The normal operation of the incineration procedure at this time is explained, namely the current combustion temperature in the incineration chamber does not need to be adjusted, and the temperature detection device continues to monitor.
If T is less than T 0 This means that the temperature in the incineration chamber is low and the temperature in the incineration chamber needs to be increased. At the moment, the real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by a gas analyzer.
If the gas analyzer detects that the real-time oxygen content in the burned flue gas is normal (i.e. the oxygen content is 6% -10%), the combustible component content is also normal (i.e. the combustible component content is less than or equal to 5%), which indicates that the heat in the burning chamber is insufficient and a heat source needs to be supplemented, so that the heat supply can be supplemented by starting a heat supplementing burner at the moment, so that T=T 0 . Or, at this time, the heat supply can be increased by increasing the feeding amount in the rotary kiln (i.e. increasing the amount of material entering the rotary kiln from the material inlet of the kiln head), and the air inlet amount in the rotary kiln (i.e. increasing the amount of combustion air entering the rotary kiln from the kiln tail air duct) can be increased simultaneously to ensure the combustion of the incremental fuel, so that the total amount of the material in the rotary kiln is t=t 0 。
If the gas analyzer detects that the real-time oxygen content in the incinerated flue gas is low (i.e. the oxygen content is less than 6%), no matter the content of the combustible components, the gas analyzer indicates that the oxygen content required by the reaction in the incineration chamber is insufficient, and simultaneously considers that the combustion temperature in the incineration chamber needs to be increased, so that the air inlet amount in the rotary kiln can be increased to increase the oxygen content, and the feeding amount in the rotary kiln can be increased to ensure the temperature increase, so that T=T 0 . Alternatively, if temperature control is mainly considered, heat can be increased by turning on the supplementary heating burner so that t=t 0 。
If the gas analyzer detects that the real-time oxygen content in the incinerated flue gas is higher (namely, the oxygen content is more than 10%), and the real-time combustible component content is normal, the gas analyzer indicates that the combustible component in the incineration chamber is basically burnt completely. The lower temperature in the incineration chamber may be caused by insufficient heat in the kiln or excessive heat absorption of combustion air, so that the air intake in the rotary kiln can be reduced, the feeding amount in the rotary kiln can be increased, or a complementary heat burner can be started, and finally, t=t 0 。
If T > T 0 This means that the temperature in the incineration chamber is high, and the temperature in the incineration chamber needs to be reduced. At the moment, the real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by a gas analyzer.
If the gas analyzer detects that the real-time oxygen content and the combustible component content in the burnt flue gas are normal, the gas analyzer shows that the current combustion is under the condition of equivalent ratio combustion, the combustion condition is good, and the heat in the kiln is excessive. Thus, the heat supplement amount of the heat supplement burner can be directly reduced at this time, or the feeding amount in the rotary kiln is reduced, and the air inlet amount in the rotary kiln is simultaneously reduced, so that T=T 0 。
If the gas analyzer detects that the real-time oxygen content in the incinerated flue gas is low, the gas analyzer indicates that the current fuel is excessive and the air is insufficient, and considers that the combustion temperature in the incineration chamber needs to be reduced, so that the air inlet amount in the rotary kiln can be increased to increase the oxygen content, and the feeding amount in the rotary kiln can be reduced to ensure the reduction of the temperature, so that T=T 0 . Alternatively, if temperature control is mainly considered, the heat compensation amount of the heat compensation nozzle can be reduced so that t=t 0 。
If the gas analyzer detects that the real-time oxygen content in the burnt flue gas is higher and the real-time combustible component content is normal, the gas analyzer indicates that the current kiln air quantity is excessive and the heat quantity is also excessive, so that the oxygen content can be reduced by reducing the air inlet quantity in the rotary kiln, and the feeding quantity in the rotary kiln is reduced simultaneously to reduce the heat input so as to ensure the temperature reduction, so that T=T 0 . Alternatively, it can be directly reduced byLess heat supplement of the burner so that t=t 0 。
In the case where the oxygen content is normal in the incineration process, 6 to 10% of oxygen is contained, and oxygen is sufficient for complete combustion. It is therefore theorized that if the combustible component content is too high, the oxygen content will not be normal (even less than 3%), so that this situation of normal oxygen content and too high combustible component content will not normally occur under normal conditions.
For the temperature adjustment strategy, after the combustion temperature is adjusted according to the iron content of the material, the residence time of the material in the kiln is not obviously changed theoretically because the rotating speed of the rotary kiln is unchanged. Compared with the prior art, after the combustion temperature is reduced, insufficient incineration of dangerous waste residues possibly occurs, and the condition of organic matter residues exists. In addition, the lower the theoretical temperature is, the more organic matters remain in the residues, and the requirement that the burning rate of the residues is less than 5% can not be met in the prior burning technology. However, the requirement of the prior incineration technology that the burning rate of the residue is less than 5 percent is aimed at the current situation that the incineration residue is commonly used for safe landfill. In the technical scheme, the incineration residue is treated by continuing to enter the sintering system, so that the residual organic matters can be utilized in sintering, and the residue can be graded and utilized according to different residual organic matters in the residue.
Practical experience shows that organic matters in incineration residues with the incineration temperature of above 850 ℃ basically disappear, and only iron resources in the residues can be sintered and utilized, so that the residues can be called carbon-free residues. The incineration residue with the incineration temperature of 650 ℃ has more organic residues, and the residue amount can reach more than 5 percent, which is called high-carbon residue. The organic matter content of the incineration residue at the incineration temperature of 650-850 ℃ is relatively reduced, and the organic matter content is between high-carbon residue and carbon-free residue, which is called low-carbon residue.
That is, the iron content of the material is different corresponding to different combustion temperatures, and the different combustion temperatures correspond to different types of residues after the incineration is completed. The method comprises the following steps:
when T is 0 And when the temperature is 550-650 ℃, the cold slag obtained after the incineration is completed and the cooling is high-carbon residue.
When T is 0 And when the temperature is 650-850 ℃, the cold slag obtained after the incineration is completed and the cooling is low-carbon residue.
When T is 0 And at 850-950 ℃, the cold slag obtained after the incineration is completed and cooled is carbon-free residue.
FIG. 5 is a block diagram of a sintering machine for co-disposal of organic hazardous waste in the present invention. The sintering trolley positioned at the feeding section of the sintering machine is sequentially provided with a lower layer material distributor, a middle layer material distributor and an upper layer material distributor. Along the running direction of the sintering trolley, the downstream of the distributor is the ignition heat preservation furnace. The lower part of the sintering machine is provided with a sintering main exhaust fan, and the sintering machine trolley is not shown in the figure. In the existing sintering production, due to the air suction effect of a main air suction fan in the traveling process of a sintering trolley, a heat storage effect exists in a sintered lower layer material layer, namely, heat distribution is more and less, so that the heat of an upper layer material is possibly insufficient, raw materials are more, the lower layer material is excessively melted due to too much heat, and even the lower layer material is possibly burnt out of a trolley grate bar due to too much heat.
Based on the sintering principle and the practical experience, in the utilization process of the incineration residue, the carbon-free residue can be placed in a lower-layer distributing machine, and laid on the lower layer of the sintering material to play a role of laying a bottom material, so that the heat of the lower layer of the sintering is effectively reduced, and the trolley grate bars are protected. The low-carbon residue and the sintering raw material can be uniformly mixed and then placed into a middle layer distributor to be subjected to co-mineralization with the sintering raw material. The high-carbon residue can be placed into the upper cloth machine, the upper heat can be increased, and the ignition effect is improved. The layered cloth can relieve the current situation of uneven heat distribution in the original sinter bed, effectively reduce energy consumption and reduce sinter return.
It should be noted that the counter-flow type incineration rotary kiln in the above proposal aims at high volatile and iron-containing hazardous waste. However, the system of the invention can be used for two purposes or is also provided with a set of equipment, and the rotary kiln can also be changed into a downstream rotary kiln aiming at low-volatile-hazard waste incineration under the condition that the system does not change. Because the low-volatile-matter-risk waste is low in volatile matter, if pyrolyzed, less volatile matter is generated, and the meaning of passing through the pyrolysis section is low. The forward-flow rotary kiln is changed, so that the application range of the system for incinerating dangerous waste is enlarged.
When the material to be treated is low-volatile organic hazardous waste, the method for disposing the low-volatile organic hazardous waste is a method for disposing organic hazardous waste cooperatively based on temperature-control oxygen-control combustion of a downstream rotary kiln-sintering machine. In the method, the low-volatile organic hazardous waste is organic hazardous waste with the mass percentage content of dry volatile less than or equal to H%. Wherein: h is 6 to 12, preferably 7 to 10. The method mainly comprises the steps (or working procedures) of primary incineration, secondary incineration, cooling, sintering and the like as the pyrolysis stage of the materials is not needed.
When low-volatile organic hazardous waste is burned, as shown in fig. 7, the primary air channel is changed from the exhaust channel of the burned flue gas into the channel for the combustion air to enter the rotary kiln, and the secondary air channel is changed from the circulating flue gas channel into the other channel for the combustion air to enter the rotary kiln, and at the moment, the source of the combustion air can still be the heat medium (namely hot air or hot air) exhausted from the hot slag cooler. The secondary air channel conveys combustion air from the kiln head into the rotary kiln, and the primary air channel conveys combustion air from the kiln body into the rotary kiln through the annular air channel and the kiln inner air channel. The kiln tail air channel is changed into a discharge channel of the burnt flue gas from a channel of the combustion air entering the rotary kiln. When the downstream rotary kiln shown in fig. 7 is used for disposing low-volatile organic hazardous waste, the trend of the flue gas and the trend of the air in the primary air duct and the kiln tail air duct are only required to be reversed on the basis of the upstream rotary kiln, and the upstream rotary kiln is changed into the downstream rotary kiln (namely, the trend of the materials is the same as that of the combustion air). The low-volatile organic hazardous waste still enters the rotary kiln from the material inlet of the kiln head, primary air enters the pyrolysis chamber of the rotary kiln from the secondary air channel of the kiln head, and the low-volatile organic hazardous waste and combustion air are burned once in the pyrolysis chamber. The ratio of the primary air is controlled to be 0.3-0.4 of the theoretical air quantity required in the kiln, the size of the primary air is regulated by an air pump on the secondary air channel, and the rest of air enters the incineration chamber of the kiln body in the form of the secondary air through the primary air channel, the annular air channel and the kiln inner air channel for further incineration. And the burned residues are discharged from a material outlet at the kiln tail and enter a hot slag cooler for cooling, and the burned flue gas is discharged from an air duct at the kiln tail. And conveying the cooled cold slag to a sintering process for use. The functions of the other parts in the rotary kiln are consistent with those of the counter-flow rotary kiln, the secondary incineration section corresponding to the incineration chamber is a main combustion zone, the temperature of the main combustion zone is regulated according to the iron content of the material, and the original temperature regulation rule is still applicable.
In the invention, the forward-flow rotary kiln is directly formed by reversing air and smoke by using the original reverse-flow rotary kiln, the original external heating type smoke heat exchange pipeline (namely an inner kiln air flue) is changed into the secondary air supply pipeline by the forward-flow rotary kiln, the secondary air inlet of the kiln body is realized, the original combustion air is changed to enter from the kiln head, the kiln head is burnt severely and the temperature is higher, the air at the kiln tail is less and the temperature is lower, namely the secondary air inlet of the kiln body reduces the air inlet of the kiln head, the temperature of the kiln head is reduced, the temperature of the kiln tail is improved, the temperature distribution of the rotary kiln is more uniform, and the reduction of nitrogen oxides is facilitated.
Compared with the prior art, the invention has the following beneficial technical effects:
1. the invention provides a concurrent-flow and countercurrent dual-purpose rotary kiln, which adopts different combustion modes aiming at different raw materials, uses concurrent flow to burn low-volatile organic hazardous waste, uses countercurrent flow to burn high-volatile organic hazardous waste, and expands the adaptability of the rotary kiln to different materials.
2. According to the pyrolysis-incineration two-stage countercurrent incineration rotary kiln provided by the invention, aiming at high-volatile organic hazardous waste, the oxygen content and the temperature in the rotary kiln are controlled, so that the organic hazardous waste is incinerated at a temperature lower than a low-temperature eutectic point, the phenomenon of loop formation and slag formation when the iron-containing organic solid waste is incinerated in the rotary kiln is effectively relieved, and the combustion efficiency is improved.
3. According to the invention, the incineration residue of the rotary kiln is cooperatively treated by utilizing the sintering process of the iron and steel plant, so that the iron element in the iron-containing solid waste can be effectively recovered, and the heavy metal in the residue is treated by the sintering process, thereby thoroughly eliminating the environmental influence and secondary pollution risk of the solid waste. Compared with the prior art, the temperature-control oxygen-control incineration in the rotary kiln also enables organic matters in hazardous waste to be partially preserved, fully utilized in the sintering process, and also improves the heat energy utilization rate.
4. According to the invention, the sintering process is used for carrying out cascade utilization and layered distribution on the residues burnt at different temperatures, so that the heat accumulation effect of the existing sintering material layer is relieved, soaking sintering is promoted, and the sintering quality is improved.
5. In the invention, the forward-flow rotary kiln is directly formed by reversing air and smoke by the original reverse-flow rotary kiln, the original external heating type smoke heat exchange pipeline is changed into the secondary air supply pipeline by the forward-flow rotary kiln, the secondary air inlet of the kiln body is realized, the original combustion-supporting air is changed to enter from the kiln head, the kiln head is burnt vigorously and the temperature is higher, the air at the kiln tail is less and the temperature is lower, namely, the secondary air inlet of the kiln body reduces the air inlet at the kiln head, the temperature of the kiln head is reduced, the temperature of the kiln tail is improved, the graduation distribution of the rotary kiln is more uniform, and the reduction of nitrogen oxides is facilitated.
Drawings
FIG. 1 is a schematic diagram of a hazardous waste incineration rotary kiln in the prior art;
FIG. 2 is a schematic diagram of a countercurrent rotary kiln for disposing of high volatile organic hazardous waste in accordance with the present invention;
FIG. 3 is a cross-sectional view taken along the direction A-A in FIG. 2;
FIG. 4 is a cross-sectional view taken along the direction B-B in FIG. 2;
FIG. 5 is a schematic structural view of a sintering machine for co-disposing of organic hazardous waste in the present invention;
FIG. 6 is a schematic diagram of a system for co-disposing of organic hazardous waste by a counter-current rotary kiln-sintering machine in accordance with the present invention;
FIG. 7 is a schematic diagram of a downstream rotary kiln for disposing of low volatile organic hazardous waste in accordance with the present invention;
FIG. 8 is a flow chart of a method for adjusting the incineration temperature in a rotary kiln according to the present invention.
Reference numerals:
c1: a rotary kiln; 1: kiln heads; 101: a material inlet; 2: a kiln body; 201: a furnace lining; 202: a furnace; 20201: a pyrolysis chamber; 20202: an incineration chamber; 3: kiln tail; 301: a material outlet; 302: a kiln tail air duct; 303: supplementary heating burner; 4: an air duct in the kiln; 5: an annular air duct; 6: a primary air duct; 7: a secondary air duct; c2: a sintering machine; 801: a lower layer material distributor; 802: a middle layer material distributor; 803: an upper layer material distributor; 9: a hot slag cooler; 901: a hot slag inlet; 902: a cold slag outlet; 903: a cold medium inlet; 904: a thermal medium outlet; 10: a three-way valve; 11: an air extracting device; 12: a temperature detecting device; 13: a material iron content detection device; 14: a gas analyzer.
Detailed Description
The following examples illustrate the technical aspects of the invention, and the scope of the invention claimed includes but is not limited to the following examples.
According to a first embodiment of the present invention, a system for the synergistic disposal of organic hazardous waste by temperature-controlled oxygen-controlled combustion is provided.
A system for cooperatively disposing organic hazardous waste by controlling temperature and oxygen and burning, which comprises a rotary kiln C1. The rotary kiln C1 comprises a kiln head 1, a kiln body 2 and a kiln tail 3. The kiln head 1 is provided with a material inlet 101. The kiln body 2 comprises a furnace lining 201 and a furnace 202. The kiln tail 3 is provided with a material outlet 301 and a kiln tail air duct 302. Along the material run, the furnace 202 is divided into a pyrolysis chamber 20201 and an incineration chamber 20202. An in-kiln air duct 4 is arranged in the furnace lining 201 corresponding to the pyrolysis chamber 20201. One end of the kiln inner air duct 4 extends into the kiln head 1, and the other end is communicated with the incineration chamber 20202. The kiln head 1 is also provided with an annular air duct 5. The in-kiln air duct 4 is communicated with a primary air duct 6 arranged outside the rotary kiln C1 through an annular air duct 5. The secondary air duct 7 is separated from the primary air duct 6. The secondary air channel 7 passes through the kiln head 1 and is communicated with the pyrolysis chamber 20201.
In the present invention, the system further includes a sintering machine C2 disposed downstream of the rotary kiln C1. Along the material trend, a lower layer distributor 801, a middle layer distributor 802 and an upper layer distributor 803 are sequentially arranged above the sintering trolley positioned at the feeding section of the sintering machine C2. The material outlet 301 of the rotary kiln C1 is connected to a lower layer spreader 801, a middle layer spreader 802 or an upper layer spreader 803.
In the present invention, the system further comprises a hot slag cooler 9 provided between the rotary kiln C1 and the sintering machine C2. The hot slag cooler 9 is provided with a hot slag inlet 901, a cold slag outlet 902, a cold medium inlet 903 and a hot medium outlet 904. The material outlet 301 of the rotary kiln C1 is connected to the hot slag inlet 901 of the hot slag cooler 9. The cold slag outlet 902 of the hot slag cooler 9 is connected to the lower layer distributor 801, the middle layer distributor 802 or the upper layer distributor 803 on the sintering machine C2. Preferably, the hot slag cooler 9 is a dry hot slag cooler, preferably a dividing wall heat exchanger.
Preferably, n kiln inner air channels 4 are arranged in the rotary kiln C1. The n kiln inner air channels 4 are uniformly distributed along the circumferential direction of the rotary kiln C1. Each kiln inner air duct 4 is communicated with an annular air duct 5 arranged at the kiln head 1. Wherein: n is 2 to 30, preferably 3 to 20.
Preferably, a three-way valve 10 is arranged at the position of the primary air duct 6, which is separated from the secondary air duct 7. An air extractor 11 is arranged on the secondary air channel 7. Preferably, the kiln tail 3 of the rotary kiln C1 is further provided with a heat supplementing burner 303.
Preferably, the temperature detecting device 12 is provided in the incineration chamber 20202 of the rotary kiln C1. A material iron content detection device 13 is arranged at a material inlet 101 of the kiln head 1. A gas analyzer 14 is provided on the primary air duct 6 at a position close to the annular air duct 5.
Example 1
As shown in fig. 2-3, a system for the coordinated disposal of organic hazardous waste by temperature-controlled oxygen-controlled combustion includes a rotary kiln C1. The rotary kiln C1 comprises a kiln head 1, a kiln body 2 and a kiln tail 3. The kiln head 1 is provided with a material inlet 101. The kiln body 2 comprises a furnace lining 201 and a furnace 202. The kiln tail 3 is provided with a material outlet 301 and a kiln tail air duct 302. Along the material run, the furnace 202 is divided into a pyrolysis chamber 20201 and an incineration chamber 20202. An in-kiln air duct 4 is arranged in the furnace lining 201 corresponding to the pyrolysis chamber 20201. One end of the kiln inner air duct 4 extends into the kiln head 1, and the other end is communicated with the incineration chamber 20202. The kiln head 1 is also provided with an annular air duct 5. The in-kiln air duct 4 is communicated with a primary air duct 6 arranged outside the rotary kiln C1 through an annular air duct 5. The secondary air duct 7 is separated from the primary air duct 6. The secondary air channel 7 passes through the kiln head 1 and is communicated with the pyrolysis chamber 20201.
Example 2
As shown in fig. 5, example 1 is repeated except that the system further includes a sintering machine C2 disposed downstream of the rotary kiln C1. Along the material trend, a lower layer distributor 801, a middle layer distributor 802 and an upper layer distributor 803 are sequentially arranged above the sintering trolley positioned at the feeding section of the sintering machine C2. The material outlet 301 of the rotary kiln C1 is connected to an upper layer spreader 803.
Example 3
Example 1 was repeated except that the system further included a sintering machine C2 disposed downstream of the rotary kiln C1. Along the material trend, a lower layer distributor 801, a middle layer distributor 802 and an upper layer distributor 803 are sequentially arranged above the sintering trolley positioned at the feeding section of the sintering machine C2. The material outlet 301 of the rotary kiln C1 is connected to the lower distributor 801.
Example 4
Example 1 was repeated except that the system further included a sintering machine C2 disposed downstream of the rotary kiln C1. Along the material trend, a lower layer distributor 801, a middle layer distributor 802 and an upper layer distributor 803 are sequentially arranged above the sintering trolley positioned at the feeding section of the sintering machine C2. The material outlet 301 of the rotary kiln C1 is connected to a middle layer distributor 802.
Example 5
As shown in fig. 6, example 2 is repeated except that the system further includes a hot slag cooler 9 disposed between the rotary kiln C1 and the sintering machine C2. The hot slag cooler 9 is provided with a hot slag inlet 901, a cold slag outlet 902, a cold medium inlet 903 and a hot medium outlet 904. The material outlet 301 of the rotary kiln C1 is connected to the hot slag inlet 901 of the hot slag cooler 9. The cold slag outlet 902 of the hot slag cooler 9 is connected to an upper layer spreader 803 on the sintering machine C2.
Example 6
Example 5 is repeated except that the hot slag cooler 9 is a divided wall heat exchanger.
Example 7
Example 6 was repeated except that 4 in-kiln air ducts 4 were provided in the rotary kiln C1. The 4 kiln inner air channels 4 are uniformly distributed along the circumferential direction of the rotary kiln C1. Each kiln inner air duct 4 is communicated with an annular air duct 5 arranged at the kiln head 1.
Example 8
As shown in fig. 4, example 6 is repeated except that 16 in-kiln air ducts 4 are provided in the rotary kiln C1. The 16 kiln inner air passages 4 are uniformly distributed along the circumferential direction of the rotary kiln C1. Each kiln inner air duct 4 is communicated with an annular air duct 5 arranged at the kiln head 1.
Example 9
Example 8 is repeated except that a three-way valve 10 is provided at the position of the primary air duct 6 where the secondary air duct 7 is branched. An air extractor 11 is arranged on the secondary air channel 7.
Example 10
Embodiment 9 is repeated, except that the kiln tail 3 of the rotary kiln C1 is further provided with a heat supplementing burner 303.
Example 11
Example 10 is repeated except that a temperature detecting device 12 is provided in the incineration chamber 20202 of the rotary kiln C1. A material iron content detection device 13 is arranged at a material inlet 101 of the kiln head 1. A gas analyzer 14 is provided on the primary air duct 6 at a position close to the annular air duct 5.
Example 12
A method of controlling temperature and oxygen combustion to co-dispose of organic hazardous waste using the system described in example 1, the method comprising the steps of:
1) And (3) pyrolysis: the high-volatile organic hazardous waste is conveyed into the rotary kiln C1 through the material inlet 101 of the kiln head 1. Combustion air enters the rotary kiln C1 through the kiln tail duct 302. The high volatile organic hazardous waste first enters the pyrolysis chamber 20201 of rotary kiln C1 for drying and pyrolysis. The residue of the material after pyrolysis and pyrolysis gas enter the incineration chamber 20202.
2) And (3) incineration: the material residues, pyrolysis gas and combustion air are mixed and burned in the incineration chamber 20202. And the burned hot slag is discharged out of the rotary kiln C1 through a material outlet 301 of the kiln tail 3. The incinerated flue gas is discharged out of the rotary kiln C1 through the kiln inner air duct 4, the annular air duct 5 and the primary air duct 6.
3) And (3) smoke circulation: and 2) part of the flue gas entering the primary air duct 6 in the step 2) enters the rotary kiln C1 again through the secondary air duct 7, and the pyrolysis and incineration processes are completed together with the materials in the rotary kiln C1.
Example 13
A method of controlling temperature and oxygen combustion to co-dispose of organic hazardous waste using the system described in example 11, the method comprising the steps of:
1) And (3) pyrolysis: the high-volatile organic hazardous waste is conveyed into the rotary kiln C1 through the material inlet 101 of the kiln head 1. Combustion air enters the rotary kiln C1 through the kiln tail duct 302. The high volatile organic hazardous waste first enters the pyrolysis chamber 20201 of rotary kiln C1 for drying and pyrolysis. The residue of the material after pyrolysis and pyrolysis gas enter the incineration chamber 20202.
2) And (3) incineration: the material residues, pyrolysis gas and combustion air are mixed and burned in the incineration chamber 20202. And the burned hot slag is discharged out of the rotary kiln C1 through a material outlet 301 of the kiln tail 3. The incinerated flue gas is discharged out of the rotary kiln C1 through the kiln inner air duct 4, the annular air duct 5 and the primary air duct 6.
3) And (3) smoke circulation: and 2) part of the flue gas entering the primary air duct 6 in the step 2) enters the rotary kiln C1 again through the secondary air duct 7, and the pyrolysis and incineration processes are completed together with the materials in the rotary kiln C1.
4) And (3) cooling: the hot slag discharged from the rotary kiln C1 in the step 2) is conveyed to a hot slag cooler 9, and a cooling medium is introduced into the hot slag cooler 9. The hot slag and the cooling medium exchange heat in the hot slag cooler 9, and cold slag and the heating medium are obtained after the heat exchange is completed.
5) Sintering: and (3) distributing the cold slag and the sintering raw materials obtained in the step (4) onto a sintering trolley, and igniting and sintering.
Example 14
Example 13 is repeated except that the high-volatile organic hazardous waste is an organic hazardous waste with a mass percentage content of dry volatile of H% or more. Wherein: h is 6.
Example 15
Example 14 was repeated except that H was 8.
Example 16
Example 14 is repeated, except that in step 4) the cooling medium introduced into the hot slag cooler 9 is cold air. The cold air is discharged from the heat medium outlet 904 after being heat-exchanged in the hot slag cooler 9 to become hot air, and the hot air is sent as combustion air to the kiln tail duct 302 of the rotary kiln C1.
Example 17
Example 14 is repeated, except that in step 4) the cooling medium introduced into the hot slag cooler 9 is cooling water. The cooling water is heat-exchanged in the slag cooler 9 to be hot water, which is then discharged from the heat medium outlet 904, and the hot water is used as boiler feed water.
Example 18
Example 16 was repeated except that in step 2), the iron content w of the high volatile organic hazardous waste entering the rotary kiln C1 was detected by the material iron content detection means 13. Determining the combustion temperature T in the incineration chamber 20202 to be controlled based on the detected iron content of the material 0 . The method comprises the following steps:
when w is more than 50%, T 0 The temperature range of (2) is 550-650 ℃.
When 25% < w.ltoreq.50%, T 0 The temperature range of (2) is 650-750 ℃.
When w is more than or equal to 5% and less than or equal to 25%, T 0 The temperature range of (2) is 750-850 ℃.
When w is less than 5%, T 0 The temperature range of (2) is 850-950 ℃.
Example 19
Example 18 was repeated except that in step 1), the pyrolysis temperature in the pyrolysis chamber 20201 of rotary kiln C1 was 400 ℃.
Example 20
Example 18 was repeated except that in step 1), the pyrolysis temperature in the pyrolysis chamber 20201 of rotary kiln C1 was 350 ℃.
Example 21
Example 19 is repeated, only according to the combustion temperature T which is to be controlled in the incineration chamber 20202 in step 2) 0 And determining the type of the cold slag obtained in the step 4). The method comprises the following steps:
when T is 0 When the temperature range of (2) is 550-650 ℃, the cold slag obtained in the step (4) is high-carbon residue.
When T is 0 When the temperature range is 650-850 ℃, the cold slag obtained in the step 4) is low-carbon residue.
When T is 0 The temperature range of (2) isAt 850-950 ℃, the cold slag obtained in the step 4) is carbon-free slag.
The organic matter content of the high-carbon residue is more than Z percent, and the organic matter content of the low-carbon residue is less than or equal to Z percent. Wherein: z is 5.
Example 22
Example 21 was repeated except that the cold slag type obtained according to step 4) was specified as step 5):
When the cold slag obtained in the step 4) is high-carbon residue, the high-carbon residue is placed in an upper layer distributor 803 on a sintering machine C1, namely, the sintering raw material is distributed on a sintering trolley, and then the high-carbon residue is distributed above the sintering raw material through the upper layer distributor 803, and ignition sintering is performed.
When the cold slag obtained in the step 4) is low-carbon residue, at the moment, placing the sintering mixture obtained by uniformly mixing the low-carbon residue and the sintering raw material into a middle layer distributor 802 on a sintering machine C1, distributing the sintering mixture onto a sintering trolley through the middle layer distributor 802, and igniting and sintering.
When the cold slag obtained in the step 4) is carbon-free slag, the carbon-free slag is placed into a lower layer distributing machine 801 on a sintering machine C1, the carbon-free slag is distributed on a sintering trolley through the lower layer distributing machine 801 as a bedding material, and then sintering raw materials are distributed above the bedding material, and ignition sintering is performed.
Example 23
Example 22 was repeated, except that in the burning process of step 2), the process conditions of the burning process and the burning temperature in the burning chamber 20202 were controlled by monitoring the temperature change condition in the burning chamber 20202 in real time and monitoring the oxygen content and the combustible component content in the burned flue gas in real time, so as to adjust the air intake and the feed amount in the rotary kiln C1 and the heat supplement amount of the heat supplement burner 303.
Example 24
As shown in fig. 8, example 23 is repeated except that the process conditions of the incineration process are controlled, and the combustion temperature in the incineration chamber 20202 is controlled, specifically comprising the following sub-steps:
201 Residue of materials, pyrolysis gasThe temperature detecting device 12 monitors the combustion temperature in the incineration chamber 20202 in real time as combustion air is combusted. In the real-time monitoring process, the detected real-time combustion temperature T in the incineration chamber 20202 and the combustion temperature T required to be controlled in the incineration chamber 20202 are detected 0 A comparison is made.
201a) If the real-time combustion temperature T in the incineration chamber 20202=the combustion temperature T to be controlled 0 I.e. the incineration process is running normally at this time, the temperature detection device 12 continues to monitor.
201b) If the real-time combustion temperature T in the incineration chamber 20202 is less than the combustion temperature T to be controlled 0 I.e. the temperature inside the incineration chamber 20202 needs to be increased. The real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by the gas analyzer 14.
If the real-time oxygen content and the combustible component content in the burned flue gas are detected to be normal, the supplementary heating burner 303 is started at the moment, so that t=t 0 。
If the real-time oxygen content in the incinerated flue gas is detected to be low, increasing the air inlet amount in the rotary kiln C1 and simultaneously increasing the feeding amount in the rotary kiln A1, so that T=T 0 。
If the real-time oxygen content in the burnt flue gas is detected to be higher and the real-time combustible component content is normal, the air inlet amount in the rotary kiln C1 is reduced at the moment, so that T=T 0 。
201c) If the real-time combustion temperature T in the incineration chamber 20202 is greater than the combustion temperature T to be controlled 0 I.e. the temperature in the incineration chamber 20202 needs to be reduced. The real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by the gas analyzer 14.
If the real-time oxygen content and the combustible component content in the burned flue gas are detected to be normal, the heat supplement quantity of the heat supplement burner 303 is reduced at the moment, so that t=t 0 。
If the real-time oxygen content in the incinerated flue gas is detected to be low, increasing the air inlet amount in the rotary kiln C1 and reducing the feeding amount in the rotary kiln C1 at the same time, so that T=T 0 。
If checkThe real-time oxygen content in the burnt flue gas is higher and the real-time combustible component content is normal, at the moment, the air inlet amount in the rotary kiln C1 is reduced, and the feeding amount in the rotary kiln C1 is reduced, so that T=T 0 。
Example 25
Example 24 was repeated except that in step 201 b), if it was detected that both the real-time oxygen content and the combustible component content in the incinerated flue gas were normal, the feed rate in rotary kiln C1 was increased and the air intake rate in rotary kiln C1 was increased at the same time, so that t=t 0 。
Example 26
Example 24 was repeated except that in step 201 b), if it was detected that the real-time oxygen content in the incinerated flue gas was low, then the supplemental heating burner 303 was turned on so that t=t 0 。
Example 27
Example 24 was repeated except that in step 201 b), if it was detected that the real-time oxygen content in the incinerated flue gas was too high and the real-time combustible component content was normal, the feed rate in rotary kiln C1 was increased so that t=t 0 。
Example 28
Example 24 was repeated except that in step 201 b), if it was detected that the real-time oxygen content in the incinerated flue gas was too high and the real-time combustible component content was normal, then the supplemental heating burner 303 was turned on so that t=t 0 。
Example 29
Example 24 was repeated except that in step 201C), if it was detected that both the real-time oxygen content and the combustible component content in the incinerated flue gas were normal, the feed rate in rotary kiln C1 was reduced and the air intake rate in rotary kiln C1 was reduced at the same time, so that t=t 0 。
Example 30
Example 24 was repeated except that in step 201 c), if the real-time oxygen content in the burned flue gas was detected to be low, the heat make-up of the make-up burner 303 was reduced so that t=t 0 。
Example 31
Example 24 is repeated, except that in step 201 c), if detected The real-time oxygen content in the burned flue gas is higher, the real-time combustible component content is normal, and the heat supplement quantity of the heat supplement burner 303 is reduced at the moment, so that T=T 0 。
Example 32
A method for co-disposal of organic hazardous waste by controlled temperature controlled oxygen combustion using the system described in example 11, wherein the rotary kiln C1 is as shown in fig. 7, comprising the steps of:
a) The low-volatile organic hazardous waste is conveyed into the rotary kiln C1 through the material inlet 101 of the kiln head 1. Combustion air enters the rotary kiln C1 through the secondary air duct 7 of the kiln head 1. The low volatile organic hazardous waste is mixed with combustion air in the furnace 202 and burned.
b) And the burned hot slag is discharged out of the rotary kiln C1 through a material outlet 301 of the kiln tail 3. The incinerated flue gas is discharged out of the rotary kiln C1 through a kiln tail air duct 302.
c) The hot slag discharged from the rotary kiln C1 in the step b) is transferred to the hot slag cooler 9, and a cooling medium is introduced into the hot slag cooler 9. The hot slag and the cooling medium exchange heat in the hot slag cooler 9, and cold slag and the heating medium are obtained after the heat exchange is completed.
d) And c) distributing the cold slag and the sintering raw materials obtained in the step c) onto a sintering trolley, and igniting and sintering.
Example 33
Example 32 is repeated except that the low volatile organic hazardous waste is an organic hazardous waste with a mass percent of dry volatile < H%. Wherein: h is 7.
Example 34
Example 33 was repeated except that H was 10.
Example 35
Example 33 is repeated except that in step a) the combustion air also enters the incineration chamber 20202 of the rotary kiln C1 through the primary air duct 6, the annular air duct 5, the kiln inner air duct 4.
Example 36
Example 35 is repeated except that the air volume of the combustion air entering the rotary kiln C1 through the secondary air duct 7 is 30% of the total air volume required in the rotary kiln C1.
Example 37
Example 35 is repeated except that the air volume of the combustion air entering the rotary kiln C1 through the secondary air duct 7 is 40% of the total air volume required in the rotary kiln C1.
Application example 1
A method for co-disposing organic hazardous waste by controlling temperature and oxygen combustion, comprising the following steps:
1) And (3) pyrolysis: the high-volatile organic hazardous waste is conveyed into the rotary kiln C1 through the material inlet 101 of the kiln head 1. Combustion air enters the rotary kiln C1 through the kiln tail duct 302. The high volatile organic hazardous waste first enters the pyrolysis chamber 20201 of rotary kiln C1 for drying and pyrolysis. The residue of the material after pyrolysis and pyrolysis gas enter the incineration chamber 20202.
2) And (3) incineration: the material residues, pyrolysis gas and combustion air are mixed and burned in the incineration chamber 20202. And the burned hot slag is discharged out of the rotary kiln C1 through a material outlet 301 of the kiln tail 3. The incinerated flue gas is discharged out of the rotary kiln C1 through the kiln inner air duct 4, the annular air duct 5 and the primary air duct 6.
3) And (3) smoke circulation: and 2) part of the flue gas entering the primary air duct 6 in the step 2) enters the rotary kiln C1 again through the secondary air duct 7, and the pyrolysis and incineration processes are completed together with the materials in the rotary kiln C1.
4) And (3) cooling: the hot slag discharged from the rotary kiln C1 in the step 2) is conveyed to a hot slag cooler 9, and a cooling medium is introduced into the hot slag cooler 9. The hot slag and the cooling medium exchange heat in the hot slag cooler 9, and cold slag and the heating medium are obtained after the heat exchange is completed.
5) Sintering: and (3) distributing the cold slag and the sintering raw materials obtained in the step (4) onto a sintering trolley, and igniting and sintering.
In the burning procedure of step 2), when the material residues, the pyrolysis gas and the combustion air are burned, the change condition of the temperature in the burning chamber 20202 is monitored in real time, and the oxygen content and the combustible component content in the burned flue gas are monitored in real time, so that the air intake and the feeding amount in the rotary kiln C1 and the heat supplementing amount of the heat supplementing burner 303 are regulated, and the technological conditions of the burning procedure and the burning temperature in the burning chamber 20202 are controlled. The method specifically comprises the following substeps:
201 The temperature detection device 12 monitors the combustion temperature in the incineration chamber 20202 in real time as the material residues, pyrolysis gas and combustion air are combusted. In the real-time monitoring process, the detected real-time combustion temperature T in the incineration chamber 20202 and the combustion temperature T required to be controlled in the incineration chamber 20202 are detected 0 A comparison is made.
Wherein, the iron content w=34% of the high-volatile organic hazardous waste entering the rotary kiln C1 is detected by the material iron content detection device 13. Determining the combustion temperature T in the incineration chamber 20202 to be controlled based on the detected iron content of the material 0 ＝680℃。
The real-time combustion temperature t=680 ℃ in the incineration chamber 20202 detected by the temperature detecting device 12, obviously t=t 0 I.e. the incineration process is running normally at this time, the temperature detection device 12 continues to monitor.
Due to T 0 =680 ℃, at this time, the cold slag obtained in step 4) is a low carbon residue, so the sintering process described in step 5) is specifically: and (3) placing the sintering mixture obtained in the step (4) after uniformly mixing the low-carbon residues and the sintering raw materials into a middle layer distributor 802 on a sintering machine C1, distributing the sintering mixture to a sintering trolley through the middle layer distributor 802, and igniting and sintering. The low-carbon residue and the sintering raw material are evenly mixed and distributed to the middle layer of the sintering raw material, so that the low-carbon residue and the sintering raw material can be subjected to co-mineralization.
Application example 2
Application example 1 was repeated except that in the incineration step of step 2), the iron content w=53% of the high-volatile organic hazardous waste entering the rotary kiln C1 was detected by the material iron content detection device 13. Determining the combustion temperature T in the incineration chamber 20202 to be controlled based on the detected iron content of the material 0 ＝620℃。
The real-time combustion temperature t=540 ℃, obviously T < T, in the incineration chamber 20202 detected by the temperature detection device 12 0 I.e. the temperature inside the incineration chamber 20202 needs to be increased. The real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by the gas analyzer 14.
The gas analyzer 14 detects that the real-time oxygen content in the incinerated flue gas is 8% and the real-time combustible component content is 1%, that is, the real-time oxygen content and the combustible component content are normal, and at the moment, the supplementary heating burner 303 is turned on to supplement the heat supply in the rotary kiln C1, so that t=t 0 。
Due to T 0 The cold slag obtained in step 4) is a high carbon residue at 620 ℃, so the sintering process described in step 5) is specifically: placing the high-carbon residue obtained in the step 4) into an upper layer distributor 803 on a sintering machine C1, namely distributing sintering raw materials onto a sintering trolley, distributing the high-carbon residue to the upper side of the sintering raw materials through the upper layer distributor 803, and igniting and sintering. The high-carbon residues are distributed to the upper layer of the sintering material, so that the heat of the upper layer can be increased, and the ignition effect is improved.
Application example 3
Application example 2 was repeated except that the gas analyzer 14 detected that the real-time oxygen content in the incinerated flue gas was 4%, i.e., the real-time oxygen content was low, at which time the air intake in the rotary kiln C1 was increased and the feed rate in the rotary kiln C1 was increased simultaneously, thereby increasing the oxygen content in the rotary kiln C1 and making t=t 0 。
Application example 4
Example 2 was repeated except that the gas analyzer 14 detected that the real-time oxygen content in the incinerated flue gas was 12% and the real-time combustible component content was 2%, i.e., the real-time oxygen content was too high and the real-time combustible component content was normal, and at this time the air intake in the rotary kiln C1 was reduced to thereby reduce the oxygen content in the rotary kiln C1 and to thereby make t=t 0 。
Application example 5
Application example 4 was repeated except that the gas analyzer 14 detected that the real-time oxygen content in the incinerated flue gas was too high and the real-time combustible component content was normal, and the feed rate in the rotary kiln C1 was increased at this time, so that the oxygen content in the rotary kiln C1 was reduced by incineration of the material, and t=t 0 。
Application example 6
Application example 1 was repeated except that in the incineration step of step 2), the iron content detection device was used for the material13 detects the iron content w=3% of the high volatile organic hazardous waste entering the rotary kiln C1. Determining the combustion temperature T in the incineration chamber 20202 to be controlled based on the detected iron content of the material 0 ＝890℃。
The real-time combustion temperature t=967 ℃ in the incineration chamber 20202 detected by the temperature detecting device 12, obviously T > T 0 I.e. the temperature in the incineration chamber 20202 needs to be reduced. The real-time oxygen content and the real-time combustible component content in the incinerated flue gas are detected by the gas analyzer 14.
The gas analyzer 14 detects that the real-time oxygen content in the burned flue gas is 7% and the real-time combustible component content is 2.5%, that is, the real-time oxygen content and the combustible component content are both normal, and at this time, the heat supplement amount of the heat supplement burner 303 is reduced, so that t=t 0 。
Due to T 0 At 890 ℃, the cold slag obtained in step 4) is carbon-free residue, so the sintering process described in step 5) is specifically: and (3) placing the carbon-free residues obtained in the step (4) into a lower layer distributing machine 801 on a sintering machine C1, distributing the carbon-free residues serving as a bedding material onto a sintering trolley through the lower layer distributing machine 801, distributing a sintering raw material to the position above the bedding material, and igniting and sintering. The carbon-free residues are distributed to the lower layer of the sintering material, so that the effect of paving the bottom material is achieved, the heat of the lower layer of the sintering can be effectively reduced, and the sintering trolley grate bars are protected.
Application example 7
Application example 6 was repeated except that the gas analyzer 14 detected that the real-time oxygen content in the incinerated flue gas was 3%, i.e., the real-time oxygen content was low, at which time the air intake in the rotary kiln C1 was increased and the feed rate in the rotary kiln C1 was decreased simultaneously, thereby increasing the oxygen content in the rotary kiln C1 and making t=t 0 。
Application example 8
The application of example 6 was repeated except that the gas analyzer 14 detected that the real-time oxygen content in the incinerated flue gas was 11% and the real-time combustible component content was 1.5%, i.e., the real-time oxygen content was too high and the real-time combustible component content was normal, and at this time, the air intake in the rotary kiln C1 was decreased, and the feed rate in the rotary kiln C1 was decreased, thereby decreasing the revolution Oxygen content in kiln C1 and such that t=t 0 。
Claims (13)
1. A system for the co-treatment of organic hazardous waste by temperature-controlled oxygen-controlled combustion, comprising a rotary kiln (C1); the rotary kiln (C1) comprises a kiln head (1), a kiln body (2) and a kiln tail (3); a material inlet (101) is arranged on the kiln head (1); the kiln body (2) comprises a kiln lining (201) and a hearth (202); a material outlet (301) and a kiln tail air duct (302) are arranged on the kiln tail (3); along the material direction, the furnace (202) is divided into a pyrolysis chamber (20201) and an incineration chamber (20202); an in-kiln air duct (4) is arranged in the furnace lining (201) corresponding to the pyrolysis chamber (20201); one end of the kiln inner air duct (4) extends into the kiln head (1), and the other end is communicated with the incineration chamber (20202); an annular air duct (5) is also arranged on the kiln head (1); the kiln inner air duct (4) is communicated with a primary air duct (6) arranged outside the rotary kiln (C1) through an annular air duct (5); a secondary air duct (7) is separated from the primary air duct (6); the secondary air channel (7) passes through the kiln head (1) to be communicated with the pyrolysis chamber (20201).
2. The system according to claim 1, wherein: the system further comprises a sintering machine (C2) arranged downstream of the rotary kiln (C1); a lower layer distributor (801), a middle layer distributor (802) and an upper layer distributor (803) are sequentially arranged above a sintering trolley positioned at the feeding section of the sintering machine (C2) along the trend of the materials; the material outlet (301) of the rotary kiln (C1) is connected to a lower layer distributor (801), a middle layer distributor (802) or an upper layer distributor (803).
3. The system according to claim 2, wherein: the system also comprises a hot slag cooler (9) arranged between the rotary kiln (C1) and the sintering machine (C2); the hot slag cooler (9) is provided with a hot slag inlet (901), a cold slag outlet (902), a cold medium inlet (903) and a hot medium outlet (904); a material outlet (301) of the rotary kiln (C1) is connected to a hot slag inlet (901) of the hot slag cooler (9); a cold slag outlet (902) of the hot slag cooler (9) is connected to a lower layer distributor (801), a middle layer distributor (802) or an upper layer distributor (803) on the sintering machine (C2); preferably, the hot slag cooler (9) is a dry hot slag cooler, preferably a dividing wall type heat exchanger.
4. A system according to any one of claims 1-3, characterized in that: n kiln inner air channels (4) are arranged in the rotary kiln (C1); n kiln inner air channels (4) are uniformly distributed along the circumferential direction of the rotary kiln (C1); each kiln inner air channel (4) is communicated with an annular air channel (5) arranged at the kiln head (1); wherein: n is 2 to 30, preferably 3 to 20; and/or
A three-way valve (10) is arranged at the position of the secondary air channel (7) on the primary air channel (6); an air extracting device (11) is arranged on the secondary air channel (7); preferably, the kiln tail (3) of the rotary kiln (C1) is also provided with a heat supplementing burner (303); and/or
A temperature detection device (12) is arranged in the incineration chamber (20202) of the rotary kiln (C1); a material iron content detection device (13) is arranged at a material inlet (101) of the kiln head (1); and a gas analyzer (14) is arranged on the primary air duct (6) and near the annular air duct (5).
5. A method of temperature-controlled oxygen-controlled combustion co-disposal of organic hazardous waste or a method of using the system of any one of claims 1-4, the method comprising the steps of:
1) And (3) pyrolysis: the high-volatile organic hazardous waste is conveyed into the rotary kiln (C1) through a material inlet (101) of the kiln head (1); combustion air enters the rotary kiln (C1) through a kiln tail air duct (302); firstly, the high-volatile organic hazardous waste enters a pyrolysis chamber (20201) of a rotary kiln (C1) for drying and pyrolysis; the material residues and pyrolysis gas after pyrolysis are fed into an incineration chamber (20202);
2) And (3) incineration: mixing and burning the material residues, the pyrolysis gas and the combustion air in an incineration chamber (20202); the burnt hot slag is discharged out of the rotary kiln (C1) through a material outlet (301) of the kiln tail (3); the burnt flue gas is discharged out of the rotary kiln (C1) through the kiln inner air duct (4), the annular air duct (5) and the primary air duct (6);
3) And (3) smoke circulation: part of the flue gas entering the primary air duct (6) in the step 2) enters the rotary kiln (C1) again through the secondary air duct (7), and the pyrolysis and incineration processes are completed together with the materials in the rotary kiln (C1);
Preferably, the high-volatile organic hazardous waste is organic hazardous waste with the mass percentage content of dry volatile being more than or equal to H%; wherein: h is 6 to 12, preferably 7 to 10.
6. The method according to claim 5, wherein: the method further comprises the steps of:
4) And (3) cooling: conveying the hot slag discharged from the rotary kiln (C1) in the step 2) to a hot slag cooler (9), and introducing a cooling medium into the hot slag cooler (9); the hot slag and the cooling medium are subjected to heat exchange in a hot slag cooler (9), and cold slag and the heating medium are obtained after the heat exchange is completed;
5) Sintering: distributing the cold slag and the sintering raw materials obtained in the step 4) onto a sintering trolley, and igniting and sintering;
preferably, in step 4), the cooling medium introduced into the hot slag cooler (9) is cold air; the cold air is discharged from a heat medium outlet (904) after being subjected to heat exchange in a hot slag cooler (9) to become hot air, and the hot air is used as combustion air to be conveyed to a kiln tail air duct (302) of the rotary kiln (C1); or (b)
In the step 4), the cooling medium introduced into the hot slag cooler (9) is cooling water; the cooling water is heat-exchanged in the slag cooler (9) to hot water, which is then discharged from the heat medium outlet (904) and used as boiler feed water.
7. The method according to claim 5 or 6, characterized in that: in the step 2), detecting the iron content w of the high-volatile organic hazardous waste entering the rotary kiln (C1) through a material iron content detection device (13); determining the combustion temperature T in the incineration chamber (20202) to be controlled based on the detected iron content of the material 0 The method comprises the steps of carrying out a first treatment on the surface of the The method comprises the following steps:
when w is more than 50%, T 0 550-650 ℃;
when 25% < w.ltoreq.50%, T 0 650-750 ℃;
when w is more than or equal to 5% and less than or equal to 25%, T 0 750-850 ℃;
when w is less than 5%, T 0 850-950 ℃; and/or
In step 1), the pyrolysis temperature in the pyrolysis chamber (20201) of the rotary kiln (C1) is 200 to 550 ℃, preferably 300 to 500 ℃.
8. The method according to claim 7, wherein: according to the combustion temperature T required to be controlled in the incineration chamber (20202) in step 2) 0 Determining the type of the cold slag obtained in the step 4); the method comprises the following steps:
when T is 0 At 550-650 ℃, the cold slag obtained in the step 4) is high-carbon residue;
when T is 0 At 650-850 ℃, the cold slag obtained in the step 4) is low-carbon slag;
when T is 0 At 850-950 ℃, the cold slag obtained in the step 4) is carbon-free slag;
preferably, the organic matter content of the high-carbon residue is more than Z percent, and the organic matter content of the low-carbon residue is less than or equal to Z percent; wherein: z is 4 to 12, preferably 5 to 10.
9. The method according to claim 8, wherein: according to the cold slag category obtained in the step 4), the step 5) specifically comprises the following steps:
when the cold slag obtained in the step 4) is high-carbon residue, placing the high-carbon residue into an upper layer distributor (803) on a sintering machine (C1), namely distributing sintering raw materials onto a sintering trolley, distributing the high-carbon residue to the position above the sintering raw materials through the upper layer distributor (803), and igniting and sintering;
when the cold slag obtained in the step 4) is low-carbon residue, placing the sintering mixture obtained by uniformly mixing the low-carbon residue and the sintering raw material into a middle layer distributor (802) on a sintering machine (C1), distributing the sintering mixture onto a sintering trolley through the middle layer distributor (802), and igniting and sintering;
when the cold slag obtained in the step 4) is carbon-free slag, the carbon-free slag is placed into a lower layer distributing machine (801) on a sintering machine (C1), the carbon-free slag is distributed on a sintering trolley through the lower layer distributing machine (801) as a bedding material, and then sintering raw materials are distributed above the bedding material, and ignition sintering is performed.
10. The method according to any one of claims 7-9, characterized in that: in the burning procedure of the step 2), when the material residues, the pyrolysis gas and the combustion air are burnt, the change condition of the temperature in the burning chamber (20202) is monitored in real time, and the oxygen content and the combustible component content in the burnt flue gas are monitored in real time, so that the air inlet quantity and/or the feeding quantity in the rotary kiln (C1) and/or the heat supplementing quantity of the heat supplementing burner (303) are adjusted, the process condition of the burning procedure is controlled, and the burning temperature in the burning chamber (20202) is controlled.
11. The method according to claim 10, wherein: the process conditions of the incineration procedure are controlled, and the combustion temperature in the incineration chamber (20202) is controlled, specifically comprising the following substeps:
201 When the material residues, the pyrolysis gas and the combustion air are combusted, the temperature detection device (12) monitors the combustion temperature in the incineration chamber (20202) in real time; in the real-time monitoring process, the detected real-time combustion temperature T in the incineration chamber (20202) and the combustion temperature T required to be controlled in the incineration chamber (20202) are detected 0 Comparing;
201a) If the real-time combustion temperature T in the incineration chamber (20202) is equal to the combustion temperature T to be controlled 0 Namely, the incineration process runs normally at the moment, and the temperature detection device (12) continues to monitor;
201b) If the real-time combustion temperature T in the incineration chamber (20202) is less than the combustion temperature T to be controlled 0 I.e. the temperature inside the incineration chamber (20202) needs to be increased; at the moment, detecting the real-time oxygen content and the real-time combustible component content in the incinerated flue gas by a gas analyzer (14);
if the real-time oxygen content and the combustible component content in the burnt flue gas are detected to be normal, starting a complementary heating burner (303) at the moment, or increasing the feeding amount in the rotary kiln (C1) and simultaneously increasing the air inlet amount in the rotary kiln (C1) so that T=T 0 ；
If the real-time oxygen content in the burnt flue gas is detected to be low, the air inlet amount in the rotary kiln (C1) is increased at the moment, and the air inlet amount in the rotary kiln (C1) is increased at the same timeThe charge, or the make-up burner (303) is turned on so that t=t 0 ；
If the real-time oxygen content in the burnt flue gas is detected to be higher and the real-time combustible component content is normal, at the moment, the air inlet amount in the rotary kiln (C1) is reduced, or the feeding amount in the rotary kiln (C1) is increased, or a complementary heat burner (303) is started, so that T=T 0 ；
201c) If the real-time combustion temperature T in the incineration chamber (20202) is greater than the combustion temperature T to be controlled 0 I.e. the temperature inside the incineration chamber (20202) needs to be reduced; at the moment, detecting the real-time oxygen content and the real-time combustible component content in the incinerated flue gas by a gas analyzer (14);
if the real-time oxygen content and the combustible component content in the burnt flue gas are detected to be normal, the heat supplement quantity of the heat supplement burner (303) is reduced, or the feeding quantity in the rotary kiln (C1) is reduced, and the air inlet quantity in the rotary kiln (C1) is reduced at the same time, so that T=T 0 ；
If the real-time oxygen content in the burnt flue gas is detected to be low, the air inlet amount in the rotary kiln (C1) is increased, and the feeding amount in the rotary kiln (C1) is reduced, or the heat supplementing amount of the heat supplementing burner (303) is reduced, so that T=T 0 ；
If the real-time oxygen content in the burnt flue gas is detected to be higher and the real-time combustible component content is normal, the air inlet amount in the rotary kiln (C1) is reduced, and the feeding amount in the rotary kiln (C1) is reduced, or the heat supplementing amount of the heat supplementing burner (303) is reduced, so that T=T 0 。
12. A method of temperature-controlled oxygen-controlled combustion co-disposal of organic hazardous waste or a method of using the system of any one of claims 1-4, the method comprising the steps of:
a) The low-volatile organic hazardous waste is conveyed into the rotary kiln (C1) through a material inlet (101) of the kiln head (1); combustion air enters the rotary kiln (C1) through a secondary air duct (7) of the kiln head (1); the low-volatile organic hazardous waste and combustion air are mixed in a hearth (202) and burnt;
b) The burnt hot slag is discharged out of the rotary kiln (C1) through a material outlet (301) of the kiln tail (3); the burnt flue gas is discharged out of the rotary kiln (C1) through a kiln tail air duct (302);
c) Conveying the hot slag discharged from the rotary kiln (C1) in the step b) to a hot slag cooler (9), and introducing a cooling medium into the hot slag cooler (9); the hot slag and the cooling medium are subjected to heat exchange in a hot slag cooler (9), and cold slag and the heating medium are obtained after the heat exchange is completed;
d) Distributing the cold slag and the sintering raw material obtained in the step c) onto a sintering trolley, and igniting and sintering;
Preferably, the low-volatile organic hazardous waste is organic hazardous waste with the mass percentage content of dry volatile less than H%; wherein: h is 6 to 12, preferably 7 to 10.
13. The method according to claim 12, wherein: in the step a), the combustion air also enters an incineration chamber (20202) of the rotary kiln (C1) through a primary air duct (6), an annular air duct (5) and an in-kiln air duct (4);
preferably, the air quantity of the combustion air entering the rotary kiln (C1) through the secondary air channel (7) accounts for 20% -45%, preferably 30% -40% of the total air quantity required in the rotary kiln (C1).
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