CN112207121A - Incineration fly ash grading thermal purification method and device based on carbothermic reduction - Google Patents
Incineration fly ash grading thermal purification method and device based on carbothermic reduction Download PDFInfo
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- CN112207121A CN112207121A CN202011187899.4A CN202011187899A CN112207121A CN 112207121 A CN112207121 A CN 112207121A CN 202011187899 A CN202011187899 A CN 202011187899A CN 112207121 A CN112207121 A CN 112207121A
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- 239000010881 fly ash Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000000746 purification Methods 0.000 title claims abstract description 19
- 239000002245 particle Substances 0.000 claims abstract description 43
- 239000001301 oxygen Substances 0.000 claims abstract description 28
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 28
- 239000007859 condensation product Substances 0.000 claims abstract description 21
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 16
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 15
- 238000001354 calcination Methods 0.000 claims abstract description 8
- 230000001965 increasing effect Effects 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 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 claims abstract description 5
- 239000000428 dust Substances 0.000 claims description 96
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 43
- 239000003546 flue gas Substances 0.000 claims description 42
- 239000012798 spherical particle Substances 0.000 claims description 20
- 239000007789 gas Substances 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000012159 carrier gas Substances 0.000 claims description 12
- 239000000919 ceramic Substances 0.000 claims description 9
- 239000013589 supplement Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 4
- 229910052783 alkali metal Inorganic materials 0.000 claims description 3
- 150000001340 alkali metals Chemical class 0.000 claims description 3
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 3
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 239000000047 product Substances 0.000 claims description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims 1
- 238000003825 pressing Methods 0.000 claims 1
- 238000007873 sieving Methods 0.000 claims 1
- 239000000779 smoke Substances 0.000 abstract description 6
- 238000004064 recycling Methods 0.000 abstract description 4
- 125000001309 chloro group Chemical class Cl* 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 description 15
- 238000005265 energy consumption Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 239000010813 municipal solid waste Substances 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 238000009270 solid waste treatment Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000002738 chelating agent Substances 0.000 description 1
- 230000009920 chelation Effects 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/30—Incineration ashes
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a method and a device for graded thermal purification of incineration fly ash based on carbothermic reduction, which comprises the following steps: uniformly mixing and granulating incineration fly ash and carbon particles, sequentially calcining the mixed particles in a low-oxygen atmosphere through a front-level rotary kiln, sequentially increasing the temperature of the front-level rotary kiln, sequentially collecting condensation products in the smoke of each level of kiln, finally crushing the mixed particles calcined by a fourth-level rotary kiln, feeding the crushed mixed particles into a fifth-level rotary kiln, calcining in an air atmosphere to remove the carbon particles, and recycling the condensation products and the incineration fly ash in the smoke of each level of kiln. According to the incineration fly ash grading thermal purification method and device based on carbothermic reduction, dioxin and heavy metals in fly ash can be removed at a lower temperature, and the heavy metals and chlorine salt volatilized from the purified fly ash in grades can be recycled.
Description
Technical Field
The invention relates to the field of solid waste treatment, in particular to a method and a device for graded thermal purification of incineration fly ash based on carbothermic reduction.
Background
Along with the economic development of China, the substance living level of people is continuously improved, the yield of municipal solid waste is increased day by day and is increased by 8-10% per year. At present, the main modes of municipal solid waste treatment are landfill and incineration. Among them, incineration is becoming the first choice in a large number of cities because of its remarkable reduction and harmless effects.
Because domestic waste classification in China is not widely implemented, and a lot of waste components contain heavy metals, the incineration fly ash also contains dioxin, the incineration fly ash is listed in national hazardous waste lists, the cost for directly entering a safe landfill site is very high, after harmless treatment is carried out on the incineration fly ash, the treatment requirement of the fly ash can be reduced, and even resource utilization can be realized.
At present, fly ash harmless treatment modes are as follows: plasma melting treatment, chelating agent chelating cement solidification synergistic treatment and water washing pretreatment. The melting temperature of plasma melting treatment is higher, generally above 1400 ℃, the energy consumption is very high, and the secondary fly ash generated by the volatilization of heavy metals and salts is still dangerous waste. After the chelation and solidification cooperative treatment, the long-term stability of pollutants is questioned after the fly ash after landfill is stored for a long time, the pollutants can be released again, the volume of the fly ash after the solidification treatment is increased, a large amount of landfill treatment sites are occupied, and the fly ash is not recycled. The water washing pretreatment process is complex and mainly aims at removing chloride salt, and pollutants are basically left in the fly ash.
Therefore, the invention aims to provide a method and a device for graded thermal purification of incineration fly ash based on carbothermic reduction, so as to realize the treatment of the incineration fly ash under the condition of lower energy consumption, and the method and the device can not cause secondary pollution, and can realize the resource utilization of the treated condensation product and the entrained fly ash.
Disclosure of Invention
The invention aims to overcome the defects of the existing incineration fly ash treatment technology, and develops a novel incineration fly ash treatment method which has no secondary pollution, is low in energy consumption compared with the fly ash fusion heat treatment technology and can realize resource utilization based on the principle of the classification heat purification of incineration fly ash by carbon heat reduction.
In order to achieve the purpose, the invention provides the following technical scheme:
a method for classifying and thermally purifying incineration fly ash based on carbothermic reduction comprises the following steps: uniformly mixing and granulating incineration fly ash and carbon particles, sequentially calcining the mixed particles in a low-oxygen atmosphere through a front-level rotary kiln, sequentially increasing the temperature of the front-level rotary kiln, sequentially collecting condensation products in the smoke of each level of kiln, finally crushing the mixed particles calcined by a fourth-level rotary kiln, feeding the crushed mixed particles into a fifth-level rotary kiln, calcining in an air atmosphere to remove the carbon particles, and recycling the condensation products and the incineration fly ash in the smoke of each level of kiln.
Preferably, the incineration fly ash passing through a 200-mesh sieve and the carbon particles passing through the 200-mesh sieve are uniformly mixed in a mass ratio of 1:1-2:1 to form a mixture, and the mixture is pressed into 10-20mm spherical particles under the pressure of 8-12 MPa.
Preferably, the spherical particles are added into a first-stage rotary kiln, the temperature in the kiln is 350-400 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 150-200 ℃ by a heat exchanger, a first dust remover is used for collecting condensation products in the flue gas;
adding the spherical particles discharged from the first-stage rotary kiln into a second-stage rotary kiln, wherein the temperature in the kiln is 500-550 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 350-400 ℃ by a heat exchanger, collecting condensation products in the flue gas by using a second dust remover;
adding the spherical particles discharged from the second-stage rotary kiln into a third-stage rotary kiln, wherein the temperature in the kiln is 700-750 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 550 ℃ by a heat exchanger, collecting condensation products in the flue gas by using a third dust remover;
and adding the spherical particles discharged by the third-stage rotary kiln into a fourth-stage rotary kiln, wherein the temperature in the kiln is 950-fold-year-old 1000 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 700-fold-old 750 ℃ by a heat exchanger, collecting condensation products in the flue gas by using a fourth dust remover.
Preferably, kiln tail flue gas discharged by the first-stage rotary kiln enters a fourth-stage rotary kiln after passing through a heat exchanger and a first dust remover, and is used as carrier gas in the kiln, and the fourth-stage rotary kiln needs air supplement to maintain low-oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the second-stage rotary kiln enters the first-stage rotary kiln after passing through a heat exchanger and a second dust remover, and is used as carrier gas in the kiln, and the first-stage rotary kiln needs air supplement to maintain low-oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the third-stage rotary kiln enters a second-stage rotary kiln after passing through a heat exchanger and a third dust remover, and is used as carrier gas in the kiln, and the second-stage rotary kiln needs air supplement to maintain low-oxygen atmosphere in the kiln;
and (3) allowing kiln tail flue gas discharged by the fourth-stage rotary kiln to pass through a heat exchanger and a fourth dust remover, and then entering the third-stage rotary kiln to be used as carrier gas in the kiln, wherein the third-stage rotary kiln needs to be supplemented with air to maintain low-oxygen atmosphere in the kiln.
Preferably, the spherical particles discharged from the fourth-stage rotary kiln are crushed, the crushed particles are sieved by a 200-mesh screen, the crushed particles are added into the fifth-stage rotary kiln, the temperature in the kiln is 600 ℃ plus materials, the residence time of the particles in the kiln is 60-120min, the atmosphere in the kiln is air, the gas flow speed in the kiln is 0.02-0.05m/s, the kiln tail gas is cooled to 200 ℃ plus materials by a heat exchanger, and then the entrained fly ash in the gas is collected by a fifth low-temperature dust collector.
Preferably, the first dust remover is a low-temperature bag dust remover, the second dust remover is a high-temperature ceramic dust remover, the third dust remover is a high-temperature ceramic dust remover, and the fourth dust remover is a high-temperature ceramic dust remover.
Preferably, the collected condensation product is heavy metal and chloride thereof or chloride of alkali metal and alkaline earth metal, so that the method has a resource utilization value, and the collected calcined fly ash and the collected cloth bag fly ash have the heavy metal and dioxin removed, so that the method has a resource utilization value.
On the other hand, the incineration fly ash grading heat purification device based on carbon thermal reduction comprises a first-stage rotary kiln, a second-stage rotary kiln, a third-stage rotary kiln, a fourth-stage rotary kiln, a fifth-stage rotary kiln, a first dust remover, a second dust remover, a third dust remover, a fourth dust remover and a fifth dust remover, wherein an exhaust port of the first-stage rotary kiln is connected with one end of the first dust remover, the other end of the first dust remover is connected with an air inlet of the fourth-stage rotary kiln, an exhaust port of the second-stage rotary kiln is connected with one end of the second dust remover, the other end of the second dust remover is connected with an air inlet of the first-stage rotary kiln, an exhaust port of the third-stage rotary kiln is connected with one end of the third dust remover, and the other end of the third dust remover is connected with an air inlet of the second-stage rotary kiln, the exhaust port of the fourth-stage rotary kiln is connected with one end of a fourth dust remover, the other end of the fourth dust remover is connected with the air inlet of the third-stage rotary kiln, and the exhaust port of the fifth-stage rotary kiln is connected with the fifth dust remover.
Preferably, a particle crusher is arranged between the discharge hole of the fourth-stage rotary kiln and the feed hole of the fifth-stage rotary kiln.
The invention has the beneficial effects that:
the incineration fly ash grading thermal purification method and the device based on the carbothermic reduction use the carbothermic reduction method of mixing and calcining carbon particles and fly ash to ensure that part of heavy metals are subjected to reduction reaction, reduce the volatilization temperature of the heavy metals and save energy consumption;
by adopting the method of mixing, pressurizing and granulating, the contact area of the carbon and the heavy metal in the fly ash is increased, the reduction reaction is enhanced, and the flying dust of the fly ash in the furnace is reduced;
the front-level rotary kiln furnace is in a low-oxygen atmosphere, which is beneficial to oxidizing carbon to generate carbon monoxide, enhancing the weak reducing atmosphere in the furnace and enhancing the reduction reaction;
different heavy metal compounds are separated and recovered by adopting a method of fractional thermal volatilization, condensation and collection, thereby being beneficial to resource utilization of the compounds;
high-temperature dust removal is used, and the cooling requirement of the flue gas is reduced, so that the hot flue gas after dust removal can be recycled, and the energy consumption is reduced.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a schematic structural diagram of an incineration fly ash classification thermal purification device based on carbothermic reduction;
in the figure: 1. the device comprises a first-stage rotary kiln, a first dust remover, a second-stage rotary kiln, a second dust remover, a third-stage rotary kiln, a fourth-stage rotary kiln, a dust remover, a fourth-stage rotary kiln, a fifth-stage rotary kiln, a dust remover, a heat exchanger, a particle crusher, a 13, an air inlet, a 14, a discharge hole, a 15, a feed inlet, a 16 and an exhaust hole.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Unless otherwise indicated, all references to up, down, left, right, front, back, inner and outer directions herein are to be interpreted as referring to up, down, left, right, front, back, inner and outer directions in the drawings to which the invention is directed.
The invention provides a method for classifying and thermally purifying incineration fly ash based on carbothermic reduction, which comprises the following steps of: uniformly mixing and granulating incineration fly ash and carbon particles, sequentially calcining the mixed particles in a low-oxygen atmosphere through a front-level rotary kiln, sequentially increasing the temperature of the front-level rotary kiln, sequentially collecting condensation products in the smoke of each level of kiln, finally crushing the mixed particles calcined by a fourth-level rotary kiln, feeding the crushed mixed particles into a fifth-level rotary kiln, calcining in an air atmosphere to remove the carbon particles, and recycling the condensation products and the incineration fly ash in the smoke of each level of kiln.
Specifically, the incineration fly ash passing through a 200-mesh sieve and the carbon particles passing through the 200-mesh sieve are uniformly mixed according to the mass ratio of 1:1-2:1 to form a mixture, and the mixture is pressed into 10-20mm spherical particles under the pressure of 8-12 MPa.
Specifically, spherical particles are added into a first-stage rotary kiln 1, the temperature in the kiln is 350-400 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after kiln tail flue gas is cooled to 150-200 ℃ through a heat exchanger 11, a first dust remover 2 is used for collecting condensation products in the flue gas;
adding the spherical particles discharged from the first-stage rotary kiln 1 into a second-stage rotary kiln 3, wherein the temperature in the kiln is 500-550 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 350-400 ℃ through a heat exchanger 11, collecting condensation products in the flue gas by using a second dust remover 4;
adding the spherical particles discharged from the second-stage rotary kiln 3 into a third-stage rotary kiln 5, wherein the temperature in the kiln is 700-750 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 550 ℃ by a heat exchanger 11, collecting condensation products in the flue gas by using a third dust remover 6;
and adding the spherical particles discharged from the third-stage rotary kiln 5 into a fourth-stage rotary kiln 7, wherein the temperature in the kiln is 950-fold-sand 1000 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 700-fold-sand 750 ℃ through a heat exchanger 11, collecting condensation products in the flue gas by using a fourth dust remover 8.
Specifically, kiln tail flue gas discharged by the first-stage rotary kiln 1 passes through a heat exchanger 11 and a first dust remover 2, then enters a fourth-stage rotary kiln 7 to be used as carrier gas in the kiln, and the fourth-stage rotary kiln 7 needs to be supplemented with air to maintain low-oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the second-stage rotary kiln 3 passes through a heat exchanger 11 and a second dust remover 4 and then enters the first-stage rotary kiln 1 to be used as carrier gas in the kiln, and the first-stage rotary kiln 1 needs to be supplemented with air to maintain low-oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the third-stage rotary kiln 5 passes through a heat exchanger 11 and a third dust remover 6 and then enters the second-stage rotary kiln 3 to be used as carrier gas in the kiln, and the second-stage rotary kiln 3 needs air supplement to maintain low oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the fourth-stage rotary kiln 7 enters the third-stage rotary kiln 5 after passing through a heat exchanger 11 and a fourth dust remover 8, and is used as carrier gas in the kiln, and the third-stage rotary kiln 5 needs air supplement to maintain low-oxygen atmosphere in the kiln.
Specifically, the spherical particles discharged from the fourth-stage rotary kiln 7 are crushed, and are added into a fifth-stage rotary kiln 9 after passing through a 200-mesh screen, the temperature in the kiln is 500-plus-material 600 ℃, the residence time of the particles in the kiln is 60-120min, the atmosphere in the kiln is air, the gas flow speed in the kiln is 0.02-0.05m/s, and the kiln tail flue gas is cooled to 150-plus-material 200 ℃ through a heat exchanger 11, and then the entrained fly ash in the flue gas is collected by using a fifth-stage low-temperature dust collector 10.
Specifically, the first dust remover 2 is a low-temperature bag dust remover, the second dust remover 4 is a high-temperature ceramic dust remover, the third dust remover 6 is a high-temperature ceramic dust remover, and the fourth dust remover 8 is a high-temperature ceramic dust remover.
Specifically, condensed products collected by the first to fifth dust collectors are heavy metals and chlorides thereof or chlorides of alkali metals and alkaline earth metals, the treated and collected calcined fly ash and cloth bag fly ash are detected, wherein the content of soluble chlorine is not more than 1%, the content of dioxin is less than 50 ng-TEQ/kg, leachate is prepared according to the HJ557 method, the leaching concentration of the heavy metals is not more than the maximum allowable discharge concentration limit value specified in GB 8978, the heavy metals meet the technical specification HJ 1134-2020 (trial), and the recycling value is achieved.
On the other hand, the invention provides a incineration fly ash grading heat purification device based on carbon heat reduction as shown in figure 2, which comprises a first-stage rotary kiln 1, a second-stage rotary kiln 3, a third-stage rotary kiln 5, a fourth-stage rotary kiln 7, a fifth-stage rotary kiln 9, a first dust remover 2, a second dust remover 4, a third dust remover 6, a fourth dust remover 8 and a fifth dust remover 10, wherein an exhaust port 16 of the first-stage rotary kiln 1 is connected with one end of the first dust remover 2, the other end of the first dust remover 2 is connected with an air inlet 13 of the fourth-stage rotary kiln 7, an exhaust port 16 of the second-stage rotary kiln 3 is connected with one end of the second dust remover 4, the other end of the second dust remover 4 is connected with the air inlet 13 of the first-stage rotary kiln 1, an exhaust port 16 of the third-stage rotary kiln 5 is connected with one end of the third dust remover 6, the other end of the third-stage rotary kiln 6 is connected with the air inlet 13 of the second-stage rotary kiln 3, the exhaust port 16 of the fourth-stage rotary kiln 7 is connected with one end of the fourth-stage rotary kiln 8, the other end of the fourth-stage rotary kiln 8 is connected with the air inlet 13 of the third-stage rotary kiln 5, and the exhaust port 16 of the fifth-stage rotary kiln 9 is connected with the fifth-stage rotary kiln 9.
Specifically, a particle crusher 12 is arranged between a discharge port 14 of the fourth-stage rotary kiln 7 and an inlet 15 of the fifth-stage rotary kiln 9.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the invention.
Claims (9)
1. A classification thermal purification method of incineration fly ash based on carbothermic reduction is characterized by comprising the following steps:
(1) uniformly mixing and granulating incineration fly ash and carbon particles;
(2) the mixed particles are sequentially calcined in a low-oxygen atmosphere in a front-level rotary kiln, and the furnace temperature of the front-level rotary kiln is sequentially increased;
(3) sequentially collecting condensation products in the flue gas of each stage of kiln;
(4) finally, crushing the mixed particles calcined in the fourth-stage rotary kiln, feeding the crushed mixed particles into a fifth-stage rotary kiln, and calcining in an air atmosphere to remove carbon particles;
(5) the condensation products and the incineration fly ash in the flue gas of each stage of the kiln can be recycled.
2. The method for the graded thermal purification of incineration fly ash based on carbothermic reduction according to claim 1, wherein the step (1) is specifically:
(1.1) uniformly mixing the incineration fly ash screened by a 200-mesh sieve and the carbon granules screened by the 200-mesh sieve in a mass ratio of 1:1-2:1 to form a mixture;
(1.2) pressing the mixture in step (1.1) into 10-20mm spherical particles at a pressure of 8-12 MPa.
3. The method for the graded thermal purification of incineration fly ash based on carbothermic reduction according to claim 1, wherein the step (2) is specifically:
(2.1) adding the spherical particles into a first-stage rotary kiln, wherein the temperature in the kiln is 350-400 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 150-200 ℃ by a heat exchanger, collecting condensation products in the flue gas by using a first dust remover;
(2.2) adding the spherical particles discharged from the first-stage rotary kiln in the step (2.1) into a second-stage rotary kiln, wherein the temperature in the kiln is 500-550 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 350-400 ℃ by a heat exchanger, collecting condensation products in the flue gas by using a second dust remover;
(2.3) adding the spherical particles discharged from the second-stage rotary kiln in the step (2.2) into a third-stage rotary kiln, wherein the temperature in the kiln is 700-;
(2.4) adding the spherical particles discharged from the third-stage rotary kiln in the step (2.3) into a fourth-stage rotary kiln, wherein the temperature in the kiln is 950-fold-year-temperature 1000 ℃, the residence time of the particles in the kiln is 30-45min, the oxygen concentration in the kiln is 5-10%, the gas flow speed in the kiln is 0.02-0.05m/s, and after the kiln tail flue gas is cooled to 700-fold-temperature 750 ℃ by a heat exchanger, collecting condensation products in the flue gas by using a fourth dust remover.
4. The method for the staged thermal purification of incineration fly ash based on carbothermic reduction according to claim 3, characterized in that:
kiln tail flue gas discharged by the first-stage rotary kiln enters a fourth-stage rotary kiln after passing through a heat exchanger and a first dust remover, and is used as carrier gas in the kiln, and the fourth-stage rotary kiln needs air supplement to maintain low-oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the second-stage rotary kiln enters the first-stage rotary kiln after passing through a heat exchanger and a second dust remover, and is used as carrier gas in the kiln, and the first-stage rotary kiln needs air supplement to maintain low-oxygen atmosphere in the kiln;
kiln tail flue gas discharged by the third-stage rotary kiln enters a second-stage rotary kiln after passing through a heat exchanger and a third dust remover, and is used as carrier gas in the kiln, and the second-stage rotary kiln needs air supplement to maintain low-oxygen atmosphere in the kiln;
and (3) allowing kiln tail flue gas discharged by the fourth-stage rotary kiln to pass through a heat exchanger and a fourth dust remover, and then entering the third-stage rotary kiln to be used as carrier gas in the kiln, wherein the third-stage rotary kiln needs to be supplemented with air to maintain low-oxygen atmosphere in the kiln.
5. The method for the staged thermal purification of incineration fly ash based on carbothermic reduction according to claim 1, wherein said step (4) is specifically:
crushing the spherical particles discharged from the fourth-stage rotary kiln, sieving the crushed spherical particles by a 200-mesh sieve, adding the crushed spherical particles into a fifth-stage rotary kiln, keeping the temperature in the kiln at 500-600 ℃, keeping the particles in the kiln for 60-120min, keeping the gas flow speed in the kiln at 0.02-0.05m/s under the air atmosphere in the kiln, cooling the kiln tail flue gas to 150-200 ℃ through a heat exchanger, and collecting the entrained fly ash in the flue gas by using a fifth low-temperature dust collector.
6. The method for the staged thermal purification of incineration fly ash based on carbothermic reduction according to claim 3, characterized in that:
the first dust remover is a low-temperature bag dust remover;
the second dust remover is a high-temperature ceramic dust remover;
the third dust remover is a high-temperature ceramic dust remover;
the fourth dust remover is a high-temperature ceramic dust remover.
7. The method for the staged thermal purification of incineration fly ash based on carbothermic reduction according to claim 1, characterized in that:
the condensed product collected in the step (3) is heavy metal and chloride thereof or chloride of alkali metal and alkaline earth metal, and has a resource utilization value;
the heavy metals and dioxin are removed from the calcined fly ash and the cloth bag fly ash collected in the step (5), and the method has a resource utilization value.
8. The utility model provides an incineration fly ash grades heat purifier based on carbothermic reduction which characterized in that includes:
the kiln comprises a first-stage rotary kiln, a second-stage rotary kiln, a third-stage rotary kiln, a fourth-stage rotary kiln, a fifth-stage rotary kiln, a first dust remover, a second dust remover, a third dust remover, a fourth dust remover and a fifth dust remover;
the exhaust port of the first-stage rotary kiln is connected with one end of a first dust remover, and the other end of the first dust remover is connected with the air inlet of the fourth-stage rotary kiln;
an exhaust port of the second-stage rotary kiln is connected with one end of a second dust remover, and the other end of the second dust remover is connected with an air inlet of the first-stage rotary kiln;
an exhaust port of the third-stage rotary kiln is connected with one end of a third dust remover, and the other end of the third dust remover is connected with an air inlet of the second-stage rotary kiln;
an exhaust port of the fourth-stage rotary kiln is connected with one end of a fourth dust remover, and the other end of the fourth dust remover is connected with an air inlet of the third-stage rotary kiln;
and an exhaust port of the fifth-stage rotary kiln is connected with a fifth dust remover.
9. The incineration fly ash classified thermal purification device based on carbothermic reduction according to claim 8, wherein:
and a particle crusher is arranged between the discharge hole of the fourth-stage rotary kiln and the feed hole of the fifth-stage rotary kiln.
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