CN214719281U - Resource disposal system for incineration slag and fly ash - Google Patents
Resource disposal system for incineration slag and fly ash Download PDFInfo
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- CN214719281U CN214719281U CN202120118938.9U CN202120118938U CN214719281U CN 214719281 U CN214719281 U CN 214719281U CN 202120118938 U CN202120118938 U CN 202120118938U CN 214719281 U CN214719281 U CN 214719281U
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- 239000002893 slag Substances 0.000 title claims abstract description 29
- 239000010881 fly ash Substances 0.000 title claims abstract description 20
- 239000003546 flue gas Substances 0.000 claims abstract description 120
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 119
- 238000003723 Smelting Methods 0.000 claims abstract description 68
- 238000000034 method Methods 0.000 claims abstract description 66
- 239000002918 waste heat Substances 0.000 claims abstract description 58
- 238000010791 quenching Methods 0.000 claims abstract description 55
- 239000000428 dust Substances 0.000 claims abstract description 47
- 239000001301 oxygen Substances 0.000 claims abstract description 25
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 25
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 24
- 238000011084 recovery Methods 0.000 claims abstract description 24
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000000460 chlorine Substances 0.000 claims abstract description 10
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 10
- 238000005406 washing Methods 0.000 claims description 70
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 56
- 230000000171 quenching effect Effects 0.000 claims description 49
- 239000000779 smoke Substances 0.000 claims description 48
- 239000002351 wastewater Substances 0.000 claims description 38
- 239000013049 sediment Substances 0.000 claims description 18
- 238000001704 evaporation Methods 0.000 claims description 14
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000005507 spraying Methods 0.000 claims description 11
- 239000002956 ash Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 238000006386 neutralization reaction Methods 0.000 claims description 8
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 6
- 238000002347 injection Methods 0.000 claims description 6
- 239000007924 injection Substances 0.000 claims description 6
- 239000011777 magnesium Substances 0.000 claims description 6
- 229910052749 magnesium Inorganic materials 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 239000000843 powder Substances 0.000 claims description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 4
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 4
- 238000001514 detection method Methods 0.000 claims description 4
- 239000004571 lime Substances 0.000 claims description 4
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 12
- 238000002844 melting Methods 0.000 abstract description 9
- 230000008018 melting Effects 0.000 abstract description 9
- 239000007789 gas Substances 0.000 abstract description 8
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- 229910001510 metal chloride Inorganic materials 0.000 abstract description 5
- 238000012545 processing Methods 0.000 abstract description 5
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 abstract description 3
- 239000011449 brick Substances 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 229910052751 metal Inorganic materials 0.000 abstract description 2
- 239000002184 metal Substances 0.000 abstract description 2
- 239000002910 solid waste Substances 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 abstract 1
- 238000005488 sandblasting Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 48
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 18
- 239000002699 waste material Substances 0.000 description 15
- 239000000047 product Substances 0.000 description 13
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 12
- 238000001816 cooling Methods 0.000 description 12
- 239000000126 substance Substances 0.000 description 9
- 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 7
- 239000000498 cooling water Substances 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 5
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 5
- 235000019341 magnesium sulphate Nutrition 0.000 description 5
- 230000002378 acidificating effect Effects 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 235000011116 calcium hydroxide Nutrition 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 150000003841 chloride salts Chemical class 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
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- 238000002425 crystallisation Methods 0.000 description 3
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- 239000012065 filter cake Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 229910052815 sulfur oxide Inorganic materials 0.000 description 3
- 231100000331 toxic Toxicity 0.000 description 3
- 230000002588 toxic effect Effects 0.000 description 3
- 238000004056 waste incineration Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000013043 chemical agent Substances 0.000 description 2
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- 238000010276 construction Methods 0.000 description 2
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- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 241001062472 Stokellia anisodon Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
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- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 description 1
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- HWSZZLVAJGOAAY-UHFFFAOYSA-L lead(II) chloride Chemical compound Cl[Pb]Cl HWSZZLVAJGOAAY-UHFFFAOYSA-L 0.000 description 1
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Abstract
The utility model provides a resourceful treatment system of incineration slag and flying dust, it can be handled incineration slag and flying dust with lower cost, still can improve the income simultaneously, helps the sustainable development of environmental protection processing enterprise. In the technical scheme, after the incineration slag fly ash to be treated is matched with the mixed raw material, the mixture is sent into an oxygen-enriched side-blown molten pool smelting furnace, and after the incineration slag, the fly ash and the mixed raw material are smelted by high-temperature melting, vitreous body slag is formed and discharged, wherein the vitreous body slag is general solid waste and can be used for brick making, road building, sand blasting, rust removal and other purposes; based on an oxygen-enriched side-blown molten pool smelting furnace, chlorine and heavy metals in flue gas are combined to enter a gas phase in a high-temperature smelting mode and enter a subsequent treatment procedure along with the smelting flue gas; the smelted flue gas is cooled and solidified into a metal chloride product after passing through a waste heat boiler, a quench tower and a bag-type dust collector, and the metal chloride product is used as a raw material product in the metal recovery industry for resource utilization.
Description
Technical Field
The utility model relates to a solid useless incineration disposal technical field specifically is a resourceful processing system of incineration furnace sediment and flying dust.
Background
In industries such as waste incineration power generation and hazardous waste incineration disposal, a large amount of incineration residues and fly ash are generated, and the incineration residues and the fly ash contain a large amount of pollutants such as dust, SOx, HCl, NOx, heavy metals, dioxin and the like. Currently, for the disposal of incineration slag/fly ash, many enterprises treat the incineration slag/fly ash through a harmless thought.
The harmless treatment is mainly realized by chelating solidification (mixing a curing agent and fly ash to generate a new substance, namely a solidified body, so that harmful ingredients in hazardous waste are blocked in the solidified body and have no pollution escape capacity) or a chemical agent stabilizing method (by chemical reaction of chemical agents, the toxic level of toxic and harmful substances is reduced and the toxic and harmful substances are gradually changed into substances with low toxicity and low solubility), and the substances are treated and then sent to a landfill for safe landfill treatment. The idea has high safety and reliability. However, the cost for operating and building a safe landfill is high at present, and many waste incineration plants cannot accept the high treatment cost.
Disclosure of Invention
In order to solve and handle the problem that incineration furnace sediment and flying dust expense are high based on innoxious thinking, the utility model provides a resourceful treatment system of incineration furnace sediment and flying dust, it can be handled incineration furnace sediment and flying dust with lower cost, still can improve the income simultaneously, helps the sustainable development of environmental protection processing enterprise.
The technical scheme of the utility model is like this: a resource disposal system of incineration slag and fly ash is characterized by comprising a high-temperature smelting device, a waste heat recovery device, a first denitration device, a quenching device, a dust removal device, a deacidification device and a second denitration device which are sequentially connected through a smoke exhaust channel;
the high-temperature smelting device is realized based on an oxygen-enriched side-blown molten pool smelting furnace; the waste heat recovery device realizes heat recovery of high-temperature flue gas discharged by the oxygen-enriched side-blown molten pool smelting furnace based on a waste heat boiler; the first denitration device is realized based on an SNCR denitration device, and the SNCR denitration device is arranged in an area of 850-1100 ℃ of the waste heat boiler;
the quenching device is realized based on a quenching tower; a boiler smoke discharge port of the waste heat boiler is connected with a tower top smoke inlet arranged at the top of the quenching tower, and an active carbon powder spraying device is arranged on a smoke discharge channel of the quenching tower;
the dust removal device is realized based on a bag-type dust remover, and a smoke channel of the quenching tower is communicated with a smoke inlet of the dust remover;
the deacidification device comprises a precooling washing tower and a washing deacidification tower which are connected in sequence; the smoke outlet of the dust remover is communicated with a flue gas inlet of a water washing tower of the precooling water washing tower, a multilayer circulating water spraying device is arranged in the precooling water washing tower, and the flue gas is cooled and deacidified by adopting water to elute chlorine; the top smoke outlet of the precooling water washing tower is connected with the washing tower smoke inlet of the washing deacidification tower, the top of the washing deacidification tower is provided with a demister, and deacidification of smoke is realized based on magnesium method neutralization desulfurization;
the second denitration device is realized based on an SCR reactor, a reactor flue gas inlet of the SCR reactor is communicated with a flue gas heating device, and flue gas subjected to denitration by the SCR reactor is discharged into a large device through a chimney; an induced draft fan is arranged on the flue in front of the chimney;
the waste water pipe of the precooling water washing tower is communicated with the water inlet pipe of the quenching tower; a waste water pipe of the washing deacidification tower is communicated with a waste water circulating pool, and the waste water circulating pool is communicated with a waste water evaporation system of which the heat source is the waste heat boiler;
and the sediment recovery device of the quenching tower and the return material discharge port of the dust remover are respectively connected with a running tank for receiving the sediment discharged by the quenching tower and the discharged ash of the bag-type dust remover.
It is further characterized in that:
the system also comprises a flue gas preheating device, wherein the flue gas preheating device is realized based on a GGH heat exchanger; the flue gas heating device is realized based on an SGH heat exchanger;
firstly, feeding denitration flue gas fed into the SCR reactor into a low-temperature flue gas inlet of the GGH heat exchanger, connecting a high-temperature flue gas inlet of the GGH heat exchanger with a smoke outlet of the SCR reactor, connecting a low-temperature flue gas outlet of the GGH heat exchanger with a flue gas inlet of the SGH heat exchanger, and connecting a flue gas outlet of the SGH heat exchanger with a smoke inlet of the SCR reactor; a high-temperature steam inlet of the SGH heat exchanger is connected with a steam outlet of the waste heat boiler; a high-temperature flue gas outlet of the GGH heat exchanger is communicated with a chimney;
it also comprises a demisting tower; the tower bottom flue gas inlet of the demisting tower is communicated with the washing tower flue gas outlet of the washing deacidification tower, and the tower bottom flue gas outlet of the demisting tower is communicated with the low-temperature flue gas inlet of the GGH heat exchanger;
a lime powder injection device is also arranged on the smoke exhaust channel of the quenching tower;
the precooling water washing tower and the washing deacidification tower adopt counter-flow water washing towers;
and heavy metal chloride concentration detection devices are arranged in the waste heat boiler, the quenching tower and the sediment collecting device of the bag-type dust remover.
The utility model provides a resource processing system of incineration slag and flying ash, after carrying out the ratio with the incineration slag flying ash that treats processing and mixed raw materials, send into oxygen boosting side-blown molten bath smelting furnace, after incineration slag, flying ash and mixed raw materials are smelted by high temperature melting, form vitreous body slag and discharge, this vitreous body slag is general solid useless, can be used to uses such as brickmaking, road building, sandblast rust cleaning; based on an oxygen-enriched side-blown molten pool smelting furnace, chlorine and heavy metals in flue gas are combined to enter a gas phase in a high-temperature smelting mode and enter a subsequent treatment procedure along with the smelting flue gas; the smelted flue gas is cooled and solidified into a metal chloride product after passing through a waste heat boiler, a quench tower and a bag-type dust collector, and the metal chloride product is used as a raw material product in the metal recovery industry for resource utilization;
after the dedusting process, the residual chlorine in the flue gas passes through a precooling water washing tower to be washed by water to remove the chlorine, so that the chlorine content in the flue gas is ensured to meet the emission quality requirement; the chlorine-containing washing wastewater is reused in the quenching tower, all the raw chlorine finally leaves the system in the form of metal chloride, and the wastewater does not need to be subjected to secondary treatment, so that the system operation cost is reduced; the sulfur in the flue gas is removed from the flue gas in an SCR reactor of a second-stage deacidification procedure through magnesium neutralization to form magnesium sulfate salt which enters wastewater, and finally the magnesium sulfate salt is subjected to evaporative crystallization, impurity removal and purification to be used as a magnesium sulfate product for resource utilization, so that certain benefits are brought to a system; the dioxin in the flue gas is incinerated and decomposed at high temperature for enough residence time in an oxygen-enriched side-blown molten pool smelting furnace, and then is removed by two modes of quenching inhibition regeneration and activated carbon powder adsorption, so that the content of the dioxin in the flue gas is ensured to reach the emission standard;
the heat generated by the oxygen-enriched side-blown molten pool smelting furnace in the smelting process is recovered by the waste heat boiler, and is converted into steam for recycling, so that the operation cost of the system is reduced on the whole; removing nitrogen oxides in the flue gas by SNCR and SCR two-stage denitration processes, wherein firstly, an SNCR denitration device is arranged in a 850-1100 ℃ area of a waste heat boiler, so that the first denitration process can be smoothly carried out; secondly, the waste heat boiler converts the waste heat into steam resources, and the steam resources are used in a process of evaporating and crystallizing high-salinity wastewater generated by the washing deacidification tower and a heat exchange process realized based on an SGH (steam generator) process; the precooling water washing tower adopts acid wastewater generated by water elution for acid removal as cooling water for quenching and cooling to realize wastewater self-digestion; after the wastewater generated in the washing deacidification tower is evaporated and condensed, the generated condensed water is used as reclaimed water for self-use, so that zero discharge of the wastewater is realized, and the operation cost of the system is further reduced;
based on this patent technical scheme, carry out resourceful treatment to incineration furnace sediment, flying dust, not only do not produce the secondary waste, avoided the secondary waste to deal with, reduced the cost of handling, form the resourceful product simultaneously and bring certain profit.
Drawings
FIG. 1 is a schematic view showing a construction of a system for recycling incineration slag and fly ash according to the present invention.
Detailed Description
As shown in figure 1, the resource treatment system for the incineration slag and the fly ash comprises a high-temperature smelting device, a waste heat recovery device, a first denitration device, a quenching device, a dedusting device, a deacidification device and a second denitration device which are sequentially connected through a smoke exhaust channel.
The high-temperature smelting device is realized based on an oxygen-enriched side-blown molten pool smelting furnace 1 and comprises a waste material inlet 15 to be treated, a smelting furnace flue gas outlet 16 arranged at the top and a smelting furnace slag outlet 14 arranged at the bottom of the smelting furnace; the waste heat recovery device realizes heat recovery of high-temperature flue gas discharged by the oxygen-enriched side-blown molten pool smelting furnace 1 based on the waste heat boiler 2; the furnace flue gas outlet 16 is connected with a boiler flue inlet 18 of the waste heat boiler 2; the flue gas of the oxygen-enriched side-blown molten pool smelting furnace 1 enters the waste heat recovery unit from the flue gas outlet at the upper part of the furnace body upwards, the waste heat boiler 2 is adopted to recover the heat of the high-temperature flue gas, the generated steam is used for system flue gas heating, equipment heat tracing, waste water evaporation and the like, the internal recycling of heat resources is realized, and the running cost of the system of the patent is reduced; the oxygen-enriched side-blown molten pool smelting furnace 1 is adopted to smelt the waste to be treated, and the oxygen-enriched side-blown molten pool smelting furnace occupies a small area and reduces the system construction cost; the oxygen-enriched side-blown molten pool smelting furnace does not need a secondary combustion heat supplementing system, does not burn pulverized coal, reduces the system cost, does not generate dust, does not discharge coal-fired flue gas, and does not generate secondary pollution; meanwhile, the heat energy produced by the oxygen-enriched side-blown molten pool smelting furnace can be reused by other devices in the supply system, so that the operation cost of the system is reduced on the whole; the temperature of the melting bath in the oxygen-enriched side-blown melting bath melting furnace reaches 1350 ℃, and the realization of the vitreous slag mold can be ensured.
The first-time denitration device is realized based on the SNCR denitration device 3, and the SNCR denitration device 3 is arranged in the 850-1100 ℃ area of the waste heat boiler 2.
The quenching device is realized based on the quenching tower 4, a boiler smoke discharge port 19 of the waste heat boiler 2 is connected with a tower top smoke inlet 20 arranged at the top of the quenching tower 4, and an active carbon powder injection device 24 and a lime powder injection device 25 are arranged on a smoke discharge channel 21 of the quenching tower.
The dust removal device is realized based on a bag-type dust remover 5; the bag-type dust collector 5 comprises a dust collector flue gas inlet 27, a dust collector smoke outlet 30 and a dust collector return material outlet 28 arranged at the bottom; the quench tower flue gas channel 21 communicates with a deduster flue gas inlet 27.
The deacidification device comprises a precooling water washing tower 6 and a washing deacidification tower 7 which are connected in sequence; the precooling washing tower 6 and the washing deacidification tower 7 both adopt a counter-flow washing tower, so that the occupied space is small, the cost is low, and the system cost is further reduced; the lower part of a pre-cooling water washing tower 6 at a dust remover smoke outlet 30 is communicated with a water washing tower flue gas inlet 31, a multi-layer circulating water spraying device 32 is arranged in the pre-cooling water washing tower 6, and chlorine is removed by water washing, so that the flue gas is cooled, and hydrochloric acid and chloride with better water solubility are removed; the top smoke outlet of the precooling water washing tower 6 is connected with a washing tower smoke inlet 37 from the lower part of the washing deacidification tower 7, the washing deacidification tower 7 realizes the smoke desulfurization based on the magnesium method neutralization process, and a circulating liquid spray device 41 is arranged in the washing deacidification tower 7 to realize the deep purification of smoke pollutants (mainly sulfur oxides); the top of the washing deacidification tower 7 is provided with a demister 40 for removing the water mist carried in the desulfurized flue gas.
The tower bottom flue gas inlet 43 of the demisting tower 8 is communicated with the washing tower flue gas outlet of the washing deacidification tower 7, and the tower top flue gas outlet 44 of the demisting tower 8 is communicated with the low-temperature flue gas inlet 45 of the GGH heat exchanger 9.
The second denitration device is realized based on the SCR reactor 11, the flue gas preheating device is realized based on the GGH heat exchanger 9, and the flue gas heating device is realized based on the SGH heat exchanger 10; the flue gas which is demisted by the demisting tower 8 and needs to be denitrated for the second time is firstly sent into a low-temperature flue gas inlet 45 of the GGH heat exchanger 9, a high-temperature flue gas inlet 47 of the GGH heat exchanger 9 is connected with a smoke outlet 48 of the SCR reactor 11, a low-temperature flue gas outlet 46 of the GGH heat exchanger 9 is connected with a flue gas inlet 51 of the SGH heat exchanger 10, and a flue gas outlet 50 of the SGH heat exchanger 10 is connected with a smoke inlet 49 of the SCR reactor 11; a high-temperature steam inlet 52 of the SGH heat exchanger 10 is connected with a steam outlet of the waste heat boiler 2, and a high-temperature flue gas outlet 53 of the GGH heat exchanger 9 is communicated with a chimney 12; the denitrated flue gas passing through the SCR reactor 11 is discharged to the atmosphere through a chimney 12; in the SGH heat exchanger 10, steam/flue gas heat exchange is realized by utilizing steam generated by the waste heat boiler 2; in the GGH heat exchanger 9, the high-temperature flue gas discharged by the SCR reactor 11 is utilized to realize flue gas/flue gas heat exchange; the preheated smelting flue gas in the GGH heat exchanger 9 is sent into an SGH heat exchanger 10 for heating; the smelting flue gas heated by the SGH heat exchanger 10 is sent to an SCR reactor 11 for denitration treatment.
An induced draft fan 13 is arranged on a flue in front of a chimney 12, so that the whole flue gas treatment system is ensured to be in a negative pressure state, and flue gas can run among devices according to a preset direction.
In specific implementation, a water outlet of the pre-cooling water washing tower 6 is connected with a circulating water tank 34, a water inlet pipe 36 of the water washing tower is connected with industrial water, the industrial water is introduced into the pre-cooling water washing tower 6 through a first circulating pump 33, and acidic wastewater generated after water washing of flue gas in the tower is carried out through a multilayer circulating water spraying device 32 is discharged into the circulating water tank 34; the water in the circulating water tank 34 is communicated with the water inlet pipe 26 of the quenching tower 4 through the waste water pipe 35 and is secondarily utilized in the quenching tower 4, so that the secondary decontamination treatment of the drainage water of the precooling water washing tower 6 is not required, and the operation cost of the system is reduced; a waste water pipe of the washing deacidification tower 7 is communicated with a waste water circulating pool 38, a water outlet 42 of the waste water circulating pool 38 is communicated with an evaporation and condensation device (not shown in the figure), the waste water in the waste water circulating pool 38 is subjected to steam evaporation and crystallization on high-salinity waste water in the waste water through the evaporation and condensation device based on a wet desulphurization waste water zero-discharge evaporation and crystallization process, magnesium sulfate is separated into products, and the generated condensed water is circularly led into the washing deacidification tower 7 through a second circulating pump 39 to be continuously used or is sent into a magnesium desulphurization slurry preparation system (not shown in the figure) to be continuously used; the heat source of the evaporation and condensation device is steam of the waste heat boiler 2; waste water self-digestion is realized to the waste water that precooling washing tower 6, washing deacidification tower 7 in this patent produced.
The sediment recovery device 22 of the quench tower 4 and the return material discharge port 28 of the dust remover of the bag-type dust remover 5 are respectively connected with a running tank 23 and a running tank 29 for receiving the sediment discharged from the quench tower 4 and the ash discharged from the bag-type dust remover 5; meanwhile, a heavy metal chloride concentration detection device (not marked in the figure) is arranged to detect the concentration of the heavy metal chloride in the sediment generated in the waste heat recovery process, the quenching and cooling process and the dedusting process at regular intervals.
The method for realizing the resource treatment of the incineration slag and the fly ash based on the system is characterized by comprising the following steps.
S1: proportioning the incinerator slag fly ash to be treated with the mixed raw materials, and adjusting iron, silicon and calcium components and heavy metal components to form waste to be treated; the mixed raw materials comprise: heavy metal sludge, silicon-calcium containing waste.
S2: the waste material to be treated is sent into a high-temperature smelting device, an oxygen-enriched side-blown molten pool smelting furnace 1 is used in the device, and after the incineration slag, the fly ash residue and the mixed raw material are smelted by high-temperature melting, vitreous body slag is formed and discharged.
The side surface of the lower part of the furnace body of the oxygen-enriched side-blown molten pool smelting furnace 1 is provided with uniformly distributed air inlets 17; oxygen-enriched primary air is uniformly blown in from an air inlet 17, the primary air is immersed in a melting tank of the oxygen-enriched side-blown molten pool smelting furnace 1, blown high-oxygen-enriched combustion-supporting air violently disturbs a melt in the furnace, a waste material to be treated in the furnace body emits a large amount of heat through a violent oxidation reaction, the temperature in the furnace can reach 1300-1400 ℃, substances in the furnace are melted and mixed, and finally flow out through a slag outlet and form a product after water quenching: the vitreous body slag is general solid waste, can be directly used without secondary treatment, and can be used for making bricks, building roads, blasting sand and removing rust and the like.
The melting of the fly ash in the waste to be treated in the oxygen-rich side-blown bath melting furnace 1 is a complex crystalline phase transformation process, in which the crystalline phase in the fly ash is completely destroyed and finally transformed into amorphous glass body without any crystalline phase. Heavy metal-containing waste is proportionally doped and burnt in the waste to be treated, so that chloride ions and heavy metals are combined into heavy metal chlorides, CL in the waste to be treated in the furnace is combined with the heavy metals in the melting process to form low-melting-point chloride salt (in a volatile gas phase), the content of the low-melting-point chloride salt in the molten slag is low, and most of the low-melting-point chloride salt enters a gas-phase product (smelting smoke). In the technical scheme, gas-phase chlorine salt in flue gas is cooled, solidified and separated out in a relatively low-temperature region in a waste heat recovery process of a waste heat recovery device waste heat boiler 2 at the downstream of a smelting furnace and a quenching process realized based on a quenching tower 4, and most of the gas-phase chlorine salt enters boiler ash, sediment of the quenching tower and fly ash discharged by a bag-type dust remover to form a solid state;
among this patent technical scheme, through setting up heavy metal chloride detection device, detect the concentration of the heavy metal chloride in the deposit that produces among waste heat recovery process, rapid cooling process, the dust removal process, reach and predetermine the requirement after heavy metal chloride concentration, sealed package keeps in, and regular transfer goes to the low reaches and deals with the unit, regards as product two (mainly zinc chloride, lead chloride) — heavy metal smelting raw materials resource recycle.
S3: recovering the waste heat of the high-temperature smelting device through a waste heat recovery process, and converting the waste heat into steam resources for secondary utilization; meanwhile, a primary denitration device is arranged in an area of 850-1100 ℃ of the waste heat recovery device; based on the SNCR process, the nitrogen oxides contained in the smelting flue gas formed in the high-temperature smelting process are subjected to first denitration treatment in a first denitration device.
The temperature of the high-temperature section of the oxygen-enriched side-blown molten pool smelting furnace 1 is higher, the retention time of the waste to be treated in the furnace is long, and a certain amount of NO exists in the produced smelting smokeXAnd (4) generating. For controlling NO in smelting flue gasXContent adopts "SNCR + SCR" two-stage denitration in this patent to strengthen the control to the nitrogen oxide, ensures that tail gas is up to standard. The first-time denitration device is realized by adopting an SNCR process, and the SNCR denitration device 3 is arranged in an area of 850-1100 ℃ of the waste heat boiler 2, namely, a denitration reducing agent with a certain concentration is sprayed into the waste heat boiler 2 to remove most of nitrogen oxides in flue gas.
S4, feeding the smelting flue gas subjected to the first denitration treatment into a quenching and cooling process for cooling; in the process flow of the quenching and cooling process, a spraying system is arranged at the upper part of a quenching tower 4 and is used for spraying a certain amount of quenching water, and the spraying system can ensure that the temperature of the flue gas discharged by the waste heat boiler 2 at 500-550 ℃ can be rapidly reduced to 190-200 ℃ within 1 second; the rapid cooling process ensures that the temperature of the smelting flue gas is rapidly reduced to 190-200 ℃ within 1 second, avoids the temperature range of the dioxin regeneration reaction, ensures that the dioxin regeneration can be inhibited, and reduces the concentration of the dioxin in the smelting flue gas.
S5: an activated carbon powder injection device 24 and a lime powder injection device 25 are arranged at the downstream of a smoke exhaust channel 21 of the quenching tower 4 in the quenching cooling process, and a proper amount of slaked lime and a certain amount of activated carbon powder are injected before high-speed smelting smoke passes through the downstream of the smoke exhaust channel 21 of the quenching tower and enters a bag-type dust remover 5 in the dust removal process; the high-speed flue gas wraps and clamps slaked lime powder and activated carbon powder to enter the bag-type dust collector 5, a layer of filter cake is formed on the surface of the filter bag and used for protecting the bag from being pasted, on the other hand, the slaked lime powder in the filter cake is subjected to neutralization reaction to absorb a small amount of acid pollutants, and the activated carbon powder in the filter cake filters the flue gas and adsorbs dioxin and heavy metals; the cloth bag dust remover 5 catches most of dust in the flue gas, and the ash discharged by the dust remover is collected by an ash bucket and discharged by ash conveying equipment;
s6: the smelting flue gas after dust removal treatment is sent to a two-stage wet deacidification process, the first-stage deacidification process adopts water spray washing to realize temperature reduction and harmful substance removal, and the second-stage deacidification process adopts a magnesium method to neutralize and desulfurize; most of CL-containing harmful impurities (hydrochloric acid and chlorides) contained in the flue gas are removed by water through a first-stage deacidification process, SO-containing acidic gas and a small part of residual CL-containing acidic substances in the flue gas are removed by a neutralization reaction, SO that the deacidification effect is improved on the whole, the use amount of alkaline solution in the neutralization reaction is reduced, and the operation cost of the system is greatly reduced.
Smelting flue gas firstly enters a precooling water washing tower 6, a multilayer circulating water spraying device 32 is arranged in the precooling water washing tower 6, on one hand, the temperature of the smelting flue gas is reduced to about 70 ℃ through water evaporation and heat absorption, and on the other hand, acidic pollutants (mainly harmful substances containing CL) with better water solubility are washed by excessive washing; the precooled smelting flue gas in the first-stage deacidification procedure then enters a washing deacidification tower 7 in the second-stage deacidification procedure, the washing deacidification tower 7 realizes the deep purification of flue gas pollutants (mainly sulfur oxides) through a large amount of circulating liquid spraying, and the combined demister 40 arranged at the top is matched to efficiently demist the smelting flue gas before the smelting flue gas is discharged out of the deacidification tower 7, so that the smelting flue gas emission is ensured to reach tighter emission indexes.
Before the step S7 is performed, the smelting flue gas discharged from the second-stage deacidification process is subjected to removal of mist droplets carried in the smelting flue gas by the defogging tower 8 in the defogging process, and then is sent into the second denitration treatment process, so that the smelting flue gas can be more sufficiently reacted with the catalyst when entering the second denitration treatment process by defogging the flue gas, and the energy consumption of the system is reduced on the whole.
S7: the smelting flue gas treated by the two-stage wet deacidification procedure is subjected to second denitration treatment and then harmless emission is carried out;
denitration treatment is carried out on the smelting flue gas based on an SCR (selective catalytic reduction) process in the second denitration treatment; heating the smelting flue gas through a heat exchange process before carrying out the second denitration treatment; the heat exchange process comprises two processes of waste heat and heating;
in the preheating process, based on a GGH heat exchange process, the tail gas to be discharged after denitration is used for preheating the smelting flue gas before denitration is realized in a flue gas waste heat exchange mode, and meanwhile, the temperature of the tail gas to be discharged after heat exchange of a GGH heat exchanger 9 is ensured to be kept above 130 ℃, so that the moisture content in the flue gas is ensured to be stable and unsaturated, and the condition of white smoke emission at the outlet of a chimney can be effectively reduced; in the heating procedure, based on the SGH process, the SGH heat exchanger 10 is used to heat the preheated smelting flue gas in a steam waste heat exchange manner, so as to reach the catalyst activity temperature required by the SCR denitration process, thereby ensuring that the smelting flue gas entering the SCR reactor 11 can fully react with the catalyst to perform thorough denitration; and a proper amount of denitration reducing agent is sprayed into the inlet of the SCR reactor 11, catalytic reduction reaction is carried out under the action of a catalyst, nitrogen oxide in the flue gas is reduced into nitrogen, and the nitrogen oxide is deeply removed.
Tail gas to be discharged, which is obtained after denitration in the SCR reactor 11, is sent to the GGH heat exchanger 9 to be used as a heat source for heat exchange, so that the heat generated by the reaction of the SCR reactor 11 is fully utilized, and the cooperative cost is reduced.
S8: collecting sediments generated in the waste heat recovery process, the quenching and cooling process and the dedusting process to be used as return materials, and detecting the concentration of the heavy metal chloride; if the concentration of the heavy metal chloride does not meet the preset requirement, sending the sediment into a high-temperature smelting device in the step S1, and carrying out material returning reprocessing; after the concentration of the heavy metal chloride meets the preset requirement, the sediment is sealed, packaged and temporarily stored, and is periodically transported to a downstream disposal unit to be used as a heavy metal smelting raw material for resource recycling; this patent use cost is lower quench tower 4, sack cleaner 5, through the cooperation of the well device of rapid cooling process, dust removal process, ensure not to produce heavy metal secondary pollutant, convert the heavy metal into raw materials resource recycle simultaneously, on the operating cost follow basis of the reduction system, increase system's income.
S9: introducing the wastewater generated in the first-stage deacidification process into the quenching and cooling process in the step S4, and recycling the wastewater as quenching and cooling water of the quenching tower 4; evaporating and crystallizing the high-salinity wastewater generated in the second-stage deacidification procedure through a waste heat evaporation system (not shown) in the system to produce a magnesium sulfate product; the waste heat evaporation system produces condensate water which is circularly used in the processes of quenching and cooling, secondary deacidification and the like of the system, and the system operation cost is further reduced.
However, salts are generated by neutralization reaction of the wet unit in the second-stage deacidification procedure, the salinity is increased along with the running time, and the saline wastewater needs to be periodically discharged in order to prevent salt saturated crystals from blocking pipelines and nozzles of the washing deacidification tower 7; the high-salinity wastewater generated in the secondary deacidification procedure is periodically recovered, a waste heat evaporation system works by utilizing waste heat steam generated in the waste heat recovery procedure, and the high-salinity wastewater generated in the secondary deacidification procedure is heated, evaporated and crystallized to produce a magnesium sulfate product; the secondary pollution of high-salinity wastewater to the environment is avoided, and the resource utilization of the produced magnesium sulfate product is increased, so that the system benefit is increased. Meanwhile, the waste heat generated in the waste heat recovery process is used as a heat source to provide heat exchange hot steam for the SGH heat exchanger 10 in the SGH process; through the arrangement of the waste heat boiler 2, waste heat generated by the system is converted into steam for recycling, so that the operation cost of the system is reduced on the whole.
According to the technical scheme, the incineration furnace slag and the fly ash are subjected to resource treatment, so that secondary waste is not generated, the secondary waste treatment is avoided, the treatment cost is reduced, and meanwhile, a resource product is formed to bring certain benefits.
Claims (6)
1. A resource disposal system of incineration slag and fly ash is characterized by comprising a high-temperature smelting device, a waste heat recovery device, a first denitration device, a quenching device, a dust removal device, a deacidification device and a second denitration device which are sequentially connected through a smoke exhaust channel;
the high-temperature smelting device is realized based on an oxygen-enriched side-blown molten pool smelting furnace; the waste heat recovery device realizes heat recovery of high-temperature flue gas discharged by the oxygen-enriched side-blown molten pool smelting furnace based on a waste heat boiler; the first denitration device is realized based on an SNCR denitration device, and the SNCR denitration device is arranged in an area of 850-1100 ℃ of the waste heat boiler;
the quenching device is realized based on a quenching tower; a boiler smoke discharge port of the waste heat boiler is connected with a tower top smoke inlet arranged at the top of the quenching tower, and an active carbon powder spraying device is arranged on a smoke discharge channel of the quenching tower;
the dust removal device is realized based on a bag-type dust remover, and a smoke channel of the quenching tower is communicated with a smoke inlet of the dust remover;
the deacidification device comprises a precooling washing tower and a washing deacidification tower which are connected in sequence; the smoke outlet of the dust remover is communicated with a flue gas inlet of a water washing tower of the precooling water washing tower, a multilayer circulating water spraying device is arranged in the precooling water washing tower, and the flue gas is cooled and deacidified by adopting water to elute chlorine; the top smoke outlet of the precooling water washing tower is connected with the washing tower smoke inlet of the washing deacidification tower, the top of the washing deacidification tower is provided with a demister, and deacidification of smoke is realized based on magnesium method neutralization desulfurization;
the second denitration device is realized based on an SCR reactor, a reactor flue gas inlet of the SCR reactor is communicated with a flue gas heating device, and flue gas subjected to denitration by the SCR reactor is discharged into a large device through a chimney; an induced draft fan is arranged on the flue in front of the chimney;
the waste water pipe of the precooling water washing tower is communicated with the water inlet pipe of the quenching tower; a waste water pipe of the washing deacidification tower is communicated with a waste water circulating pool, and the waste water circulating pool is communicated with a waste water evaporation system of which the heat source is the waste heat boiler;
and the sediment recovery device of the quenching tower and the return material discharge port of the dust remover are respectively connected with a running tank for receiving the sediment discharged by the quenching tower and the discharged ash of the bag-type dust remover.
2. The system of claim 1, wherein the system comprises: the system also comprises a flue gas preheating device, wherein the flue gas preheating device is realized based on a GGH heat exchanger; the flue gas heating device is realized based on an SGH heat exchanger;
firstly, feeding denitration flue gas fed into the SCR reactor into a low-temperature flue gas inlet of the GGH heat exchanger, connecting a high-temperature flue gas inlet of the GGH heat exchanger with a smoke outlet of the SCR reactor, connecting a low-temperature flue gas outlet of the GGH heat exchanger with a flue gas inlet of the SGH heat exchanger, and connecting a flue gas outlet of the SGH heat exchanger with a smoke inlet of the SCR reactor; a high-temperature steam inlet of the SGH heat exchanger is connected with a steam outlet of the waste heat boiler; and a high-temperature flue gas outlet of the GGH heat exchanger is communicated with a chimney.
3. The system of claim 2, wherein the system comprises: it also comprises a demisting tower; and the tower bottom smoke inlet of the demisting tower is communicated with the washing tower smoke outlet of the washing deacidification tower, and the tower bottom smoke outlet of the demisting tower is communicated with the low-temperature smoke inlet of the GGH heat exchanger.
4. The system of claim 1, wherein the system comprises: and a lime powder injection device is also arranged on the smoke exhaust channel of the quenching tower.
5. The system of claim 1, wherein the system comprises: the precooling water washing tower and the washing deacidification tower adopt a counter-flow water washing tower.
6. The system of claim 1, wherein the system comprises: and heavy metal chloride concentration detection devices are arranged in the waste heat boiler, the quenching tower and the sediment collecting device of the bag-type dust remover.
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