CN211345331U - Device for co-processing incineration fly ash and gasification fly ash - Google Patents
Device for co-processing incineration fly ash and gasification fly ash Download PDFInfo
- Publication number
- CN211345331U CN211345331U CN201921974956.6U CN201921974956U CN211345331U CN 211345331 U CN211345331 U CN 211345331U CN 201921974956 U CN201921974956 U CN 201921974956U CN 211345331 U CN211345331 U CN 211345331U
- Authority
- CN
- China
- Prior art keywords
- fly ash
- gasification
- entrained flow
- flow bed
- storage tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000010881 fly ash Substances 0.000 title claims abstract description 184
- 238000002309 gasification Methods 0.000 title claims abstract description 77
- 238000012545 processing Methods 0.000 title claims description 8
- 238000003860 storage Methods 0.000 claims abstract description 48
- 238000001816 cooling Methods 0.000 claims abstract description 32
- 239000000428 dust Substances 0.000 claims abstract description 26
- 238000000746 purification Methods 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 58
- 239000002893 slag Substances 0.000 claims description 56
- 238000004056 waste incineration Methods 0.000 claims description 51
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 31
- 239000002920 hazardous waste Substances 0.000 claims description 27
- 238000007599 discharging Methods 0.000 claims description 21
- 229910052757 nitrogen Inorganic materials 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 239000002826 coolant Substances 0.000 claims description 3
- 238000005453 pelletization Methods 0.000 abstract description 5
- 238000002844 melting Methods 0.000 description 19
- 239000007788 liquid Substances 0.000 description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 15
- 229910052760 oxygen Inorganic materials 0.000 description 15
- 239000001301 oxygen Substances 0.000 description 15
- 239000002956 ash Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 14
- 238000000034 method Methods 0.000 description 11
- 239000003546 flue gas Substances 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 9
- 239000000463 material Substances 0.000 description 9
- 239000002245 particle Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 7
- 239000004566 building material Substances 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 230000008018 melting Effects 0.000 description 6
- 238000010309 melting process Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 229910001385 heavy metal Inorganic materials 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000004458 analytical method Methods 0.000 description 4
- 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 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 229910017053 inorganic salt Inorganic materials 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000002738 chelating agent Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 210000004127 vitreous body Anatomy 0.000 description 2
- 238000004017 vitrification Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N Na2O Inorganic materials [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Landscapes
- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The utility model provides a device that incineration fly ash and gasification fly ash dealt with jointly belongs to the fly ash and deals with technical field. The utility model provides a device that incineration fly ash and gasification fly ash dealt with altogether, including storage tank, feeding storehouse and the entrained flow bed that communicates in order, the parallelly connected ignition system and the wind pipeline of being provided with in top of entrained flow bed, the bottom of entrained flow bed is provided with row sediment-cooling system, the gas vent of entrained flow bed communicates in order has gas cooling system, gaseous dust pelletizing system and gas purification system. The device provided by the utility model is rational in infrastructure, need not special or expensive part, easy operation can realize burning flying dust and gasification flying dust and deal with altogether.
Description
Technical Field
The utility model relates to a flying dust deals with technical field, especially relates to a device that flying dust and gasification flying dust dealt with jointly burns.
Background
The incineration fly ash comprises waste incineration fly ash and hazardous waste incineration fly ash, and the two types of fly ash are listed in 2016 edition of national hazardous waste records and belong to hazardous waste (HW18) due to the enrichment of various heavy metals and dioxin pollutants.
The waste incineration fly ash is a residue collected by a flue gas purification system of a domestic waste incineration plant, and the waste incineration fly ash has a large production amount and is one of the key points and difficulties in hazardous waste management in China. At present, more than 300 urban domestic garbage incineration plants in China have been produced, the annual incineration treatment capacity reaches 7000 ten thousand tons, the yield of the waste incineration fly ash is related to the types of the waste, the incineration conditions, the type of the incinerator and the flue gas treatment process, and 350-560 ten thousand tons of waste incineration fly ash are produced every year according to the proportion of 5-8% of the fly ash. The waste incineration fly ash is dark gray or grey white, the average particle size is generally 40-60 mu m, the content of soluble salt taking chlorides of K, Na and Ca as main bodies is 15-25%, and the waste incineration fly ash contains various heavy metals, dioxin and other hazardous substances.
The hazardous waste incineration fly ash is a residue collected by a flue gas purification system of a hazardous waste incineration plant, is large in production amount and strong in harmfulness, and is also one of the key points and difficulties in hazardous waste management in China. In 2018, the amount of hazardous waste in China is 400 ten thousand tons in an incineration mode, the amount of fly ash generated by incinerating the hazardous waste is 20-40 ten thousand tons according to the calculation of the fly ash generation proportion of 5-10%. The hazardous waste incineration fly ash and the waste incineration fly ash have the characteristics of low water content, irregular shape, high porosity, small particle size (average particle size is generally 40-60 mu m), large specific surface area and the like, and the main components are Na, Ca, K, Cl, S, Si and the like.
At present, incineration fly ash is mainly stabilized and solidified for safe landfill, but the storage capacity of a landfill site is limited, and the solidification mode needs to be improved, for example, the incineration fly ash is solidified by adopting a chelating agent, so that the stability of the chelating agent needs to be improved. Based on this, expert scholars actively research and develop the harmless and resource treatment method of incineration fly ash, most typically is the fly ash high-temperature melting vitrification technique, the technique can stably solidify heavy metals in incineration fly ash through heat treatment processes such as electricity, fuel melting vitrification and the like, but needs to consume more energy for realizing incineration fly ash melting; in addition, in order to reduce the ash melting point and facilitate the formation of a glass body, a certain amount of Ca, Al and Si inorganic salt is additionally added in the melting process, so that the material consumption is increased. Therefore, the technology needs to consume a large amount of energy and has higher treatment cost.
In recent years, coal gasification technology plays an extremely important role in economic development of China, but part of unreacted carbon and fine slag in the gasification process can be brought out by synthesis gas to generate a certain amount of gasification fly ash, and the annual output is preliminarily estimated to be 50-100 ten thousand tons. The gasification fly ash has a calorific value of 2500-4000 kCal/kg and an average particle size of 30-50 μm. At present, gasified fly ash is usually used for road engineering, mine backfilling or soil improvement, so that the calorific value of the gasified fly ash and the contained unburned carbon cannot be directly utilized, and resource waste is caused.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a device that incineration fly ash and gasification fly ash dealt with altogether, the utility model provides a device is rational in infrastructure, need not special or expensive part, and easy operation can realize incineration fly ash and gasification fly ash and deal with altogether.
In order to realize the purpose of the utility model, the utility model provides a following technical scheme:
the utility model provides a device that incineration fly ash and gasification fly ash dealt with altogether, including storage tank, feeding storehouse and the entrained flow bed that communicates in order, the parallelly connected ignition system and the wind pipeline of being provided with in top of entrained flow bed, the bottom of entrained flow bed is provided with row sediment-cooling system, the gas vent of entrained flow bed communicates in order has gas cooling system, gaseous dust pelletizing system and gas purification system.
Preferably, the device further comprises a nitrogen production system, and two air outlets of the nitrogen production system are respectively communicated with the feeding bin and the gas dedusting system.
Preferably, the storage tanks comprise an incineration fly ash storage tank and a gasification fly ash storage tank, and the incineration fly ash storage tank and the gasification fly ash storage tank are both communicated with the feeding hole of the feeding bin.
Preferably, the storage tanks comprise a hazardous waste incineration fly ash storage tank, a waste incineration fly ash storage tank and a gasification fly ash storage tank, and the hazardous waste incineration fly ash storage tank, the waste incineration fly ash storage tank and the gasification fly ash storage tank are all communicated with the feeding hole of the feeding bin.
Preferably, the slag discharging-cooling system comprises a slag discharging valve and a slag discharging tank, the slag discharging tank is connected with the entrained flow bed through the slag discharging valve, and the cooling medium in the slag discharging tank is water.
The utility model provides a device that incineration fly ash and gasification fly ash dealt with altogether, including storage tank, feeding storehouse and the entrained flow bed that communicates in order, the parallelly connected ignition system and the wind pipeline of being provided with in top of entrained flow bed, the bottom of entrained flow bed is provided with row sediment-cooling system, the gas vent of entrained flow bed communicates in order has gas cooling system, gaseous dust pelletizing system and gas purification system. The device provided by the utility model is rational in infrastructure, need not special or expensive part, easy operation can realize burning flying dust and gasification flying dust and deal with altogether.
Drawings
FIG. 1 is a schematic structural diagram of a device for co-processing incineration fly ash and gasification fly ash in the present invention;
FIG. 2 is another schematic structural diagram of the apparatus for co-processing incineration fly ash and gasification fly ash in the present invention;
FIG. 3 is a flow chart of the gasification-melting process of the co-disposed incineration fly ash and gasification fly ash of the present invention;
FIG. 4 is a flow chart of the combustion-melting process of the co-disposed incineration fly ash and gasification fly ash of the present invention;
in the figure, 1-1 is an incineration fly ash storage tank, 1-1-1 is a waste incineration fly ash storage tank, 1-1-2 is a hazardous waste incineration fly ash storage tank, 1-2 is a gasification fly ash storage tank, 2 is a feeding bin, 3 is an entrained flow bed, 4 is an ignition system, 5 is a primary air pipeline, 6 is a slag discharge-cooling system, 7 is a gas cooling system, 8 is a gas dedusting system, 9 is a gas purification system, and 10 is a nitrogen production system.
Detailed Description
The utility model provides a device that incineration fly ash and gasification fly ash dealt with altogether, including storage tank, feeding storehouse and the entrained flow bed that communicates in order, the parallelly connected ignition system and the wind pipeline of being provided with in top of entrained flow bed, the bottom of entrained flow bed is provided with row sediment-cooling system, the gas vent of entrained flow bed communicates in order has gas cooling system, gaseous dust pelletizing system and gas purification system.
The device for co-processing incineration fly ash and gasification fly ash provided by the utility model comprises a storage tank for storing raw materials; the utility model discloses do not do special restrictions to the material of storage tank, size etc..
As an embodiment of the utility model, when the fly ash that burns that adopts is useless fly ash or waste incineration fly ash of danger, the storage tank includes fly ash storage tank and gasification fly ash storage tank, fly ash storage tank with gasification fly ash storage tank all with the feed inlet intercommunication in feeding storehouse. As an embodiment of the utility model, when the fly ash that burns that adopts is useless fly ash and the waste incineration fly ash of danger, the storage tank includes useless fly ash storage tank of burning of danger, waste incineration fly ash storage tank and gasification fly ash storage tank, useless fly ash storage tank of burning of danger, waste incineration fly ash storage tank and gasification fly ash storage tank all with the feed inlet intercommunication in feeding storehouse.
The utility model provides a device for disposing incineration fly ash and gasification fly ash together, which comprises a feeding bin, a material feeding bin and a material discharging bin, wherein the feeding bin is used for uniformly mixing raw materials from a storage tank and then conveying the raw materials to an entrained flow bed for gasification-melting reaction or combustion-melting reaction; the utility model discloses do not do special limit to the material in feeding storehouse, size etc.. As an embodiment of the utility model, the device that incineration fly ash and gasification fly ash dealt with jointly still includes the nitrogen system, a gas outlet of nitrogen system with the feeding storehouse intercommunication is convenient for carry the raw materials to the entrained flow from the feeding storehouse through nitrogen gas.
The utility model provides a device for disposing incineration fly ash and gasification fly ash together, which comprises an entrained flow bed, wherein gasification-melting reaction or combustion-melting reaction occurs in the entrained flow bed; the entrained flow is preferably a steel, cylindrical reactor, and the size of the entrained flow is not particularly limited by the present invention.
In the utility model discloses, the top of entrained flow bed connects in parallel and is provided with ignition system and a wind pipeline, is used for igniteing respectively and lets in the gasification agent to make incineration fly ash and gasification fly ash carry out gasification-melting reaction or burning-melting reaction in the entrained flow bed.
As an embodiment of the present invention, the ignition system is an ignition burner, and is composed of an ignition oil gun, a high-energy igniter, and a flame detection device; the ignition oil gun is an air pressure atomization type ignition oil gun, and fuel required by the ignition oil gun is 0# light diesel oil.
The utility model discloses it does not have special restriction to once wind pipeline, adopt the once wind pipeline that technical personnel in the field are familiar with can.
In the utility model, the bottom of the entrained flow bed is provided with a slag discharge-cooling system for discharging liquid slag from the entrained flow bed and cooling the liquid slag into glassy state slag.
As an embodiment of the present invention, the slag discharging-cooling system includes a slag discharging valve and a slag discharging tank, the slag discharging tank is connected to the entrained flow bed through the slag discharging valve, and a cooling medium in the slag discharging tank is water; the slag discharging valve can control the discharging rate and the discharging amount of the liquid slag, and if the liquid slag can be intermittently discharged to the slag discharging tank for cooling, the cooling effect is ensured, and the glassy state slag meeting the use requirement of building materials is formed.
The utility model discloses in, the gas vent of entrained flow communicates in order has gas cooling system, gaseous dust pelletizing system and gas purification system to the realization is to cooling, dust removal and the purification of gas mixture result.
As an embodiment of the present invention, the gas cooling system is a water cooler; the high-temperature mixed gas product discharged from the exhaust port of the entrained flow bed is cooled to be less than or equal to 160 ℃ after passing through a water cooler, and then enters a subsequent gas dust removal system.
As an embodiment of the invention, the gas dust removal system comprises a bag-type dust remover and an ash bucket, has a nitrogen back-blowing function, and is used for performing gas dust removal treatment on a cooled mixed gas product. As an embodiment of the invention, the other air outlet of the nitrogen making system is communicated with the gas dust removal system, so that nitrogen can be conveniently provided to realize the back flushing of the nitrogen.
As an embodiment of the present invention, the gas purification system includes a desulfurization tower or a scrubber, and specifically, when the mixed gas product is a combustible gas, the gas purification system employs a desulfurization tower to remove sulfides in the combustible gas; when the mixed gas product is flue gas, the gas purification system adopts a washing tower which has a deacidification function and can remove NO in the flue gasxAnd SO2。
The following describes the method of using the device for co-processing incineration fly ash and gasification fly ash according to the present invention with reference to fig. 1 to 4: gasification fly ash and incineration fly ash (including waste incineration fly ash and/or hazardous waste incineration fly ash) enter a feeding bin from respective storage tanks according to a certain proportion, then the mixture is conveyed to the entrained flow bed from the feeding bin through nitrogen, a gasifying agent is introduced from a primary air pipe at the top of the entrained flow bed to provide oxygen-containing atmosphere for the entrained flow bed, and the mixture is ignited by an ignition system arranged at the top of the entrained flow bed to initiate reaction, when the oxygen supply is insufficient, the gasified fly ash is gasified in the entrained flow bed, the temperature of a hearth of the entrained flow bed can reach 1350-1550 ℃, the ash content of the gasified fly ash and the incineration fly ash are fully melted under the high temperature condition to form liquid slag, the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to form glassy slag which can be used as building materials, meanwhile, a certain amount of combustible gas (the heat value is 1500-2000 kCal/kg, and the contained combustible components comprise CO and H) is generated in the gasification process.2) After being discharged from an exhaust port of the entrained flow bed, the air is sequentially treated by the air cooling system, the air dedusting system and the air purifying system and then can be conveyed to a user for recycling; when the oxygen supply is excessive, the gasified fly ash is fully combusted in the hearth, the temperature of the hearth of the entrained flow bed can reach 1400-1600 ℃, the ash content of the gasified fly ash and the incineration fly ash are fully melted under the high-temperature condition to form liquid slag, the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled (to be less than or equal to 100 ℃) to form glassy slag, and the glassy slag can be used as building materialsMeanwhile, a certain amount of flue gas is generated in the combustion process, and is discharged from an exhaust port of the entrained flow bed, and then is treated by a gas cooling system (cooled to less than or equal to 160 ℃), a gas dust removal system and a gas purification system in sequence and then is discharged after reaching the standard.
The utility model discloses in, the chemical reaction process that the system takes place after burning flying dust and gasification flying dust's ratio, oxygen quantity can influence the ignition, and is specific: the mass of the incineration fly ash is 5-15% of that of the gasification fly ash, when the system is in an oxygen-poor state (namely the oxygen content is relatively insufficient), gasification-melting reaction mainly occurs in the system, the temperature of the system can reach 1350-1550 ℃ by utilizing the heat released by gasification of the gasification fly ash (carbon is generated into CO through gasification reaction), and the ash content of the incineration fly ash and the gasification fly ash is fully melted; the mass of the incineration fly ash is 20-50% of that of the gasification fly ash, when the system is in an oxygen-rich state (namely the oxygen content is relatively excessive), combustion-melting reaction mainly occurs in the system, and the heat released by full combustion of the gasification fly ash (carbon is fully combusted to generate CO)2) The temperature of the system can reach 1400-1600 ℃, and the ash contents of the incineration fly ash and the gasification fly ash are fully melted.
The utility model has no special limitation to the type of the gasification agent providing oxygen-containing atmosphere and the oxygen content, and can select proper gasification agent according to actual needs, in particular to air, pure oxygen or oxygen-enriched gas, the utility model has no special limitation to the oxygen-enriched gas, and can adopt the oxygen-enriched gas well known by technicians in the field; the amount of the gasifying agent is determined according to actual needs so as to ensure that the gasification-melting reaction or the combustion-melting reaction can be smoothly carried out, and the utility model is not specially limited to this.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the embodiments described are only some embodiments of the invention, and not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The following examples used the following raw materials with the specific ingredients:
the average particle size of the waste incineration fly ash produced by a certain waste incineration plant is 40-60 μm, and the main chemical components and the heavy metal content are respectively shown in tables 1 and 2:
table 1 main component of refuse incineration fly ash (%)
| Fe2O3 | MgO | Na2O | SiO2 | CaO | K2O | Al2O3 | Cl | S |
| 1.14 | 1.23 | 2.88 | 8.16 | 29.11 | 2.97 | 2.80 | 18.21 | 0.97 |
TABLE 2 heavy metal content (ppm) in the fly ash from waste incineration
| Pb | Zn | Cu | Ni | Mn | Cr |
| 3039.8 | 22670.5 | 1480.1 | 181.7 | 76 | 609.6 |
The average particle size of the hazardous waste incineration fly ash generated by a hazardous waste incineration plant is 40-60 mu m, and the analysis of the main chemical components is shown in Table 3:
table 3 analysis of part of chemical composition in fly ash from incineration of hazardous wastes (%)
| Fly ash type | Na | Ca | K | Cl | S | Si | Al | Fe |
| Bag collector | 13.1 | 20.1 | 2.1 | 9.8 | 8.48 | 0.8 | 0.2 | 0.2 |
| Collecting by quenching | 1.4 | 36.9 | 0.1 | 3.3 | 1.0 | 0.3 | 0.3 | 0.2 |
The average particle size of gasification fly ash produced by a certain coal gasification plant is 30-50 μm, and the analysis of main chemical components is shown in tables 4-6:
TABLE 4 gasification fly ash Industrial analysis (air dry basis)
| Item | Unit of | Numerical value |
| Moisture content | ％ | 0.48 |
| Volatile component | ％ | 2.68 |
| Fixed carbon | ％ | 46.25 |
| Ash content | ％ | 50.59 |
TABLE 5 gasification fly ash elemental analysis (air dry basis)
| Item | Unit of | Numerical value |
| C | ％ | 47.86 |
| H | ％ | 0.43 |
| O | ％ | - |
| N | ％ | 0.44 |
| S | ％ | 0.52 |
TABLE 6 gasification fly ash major ash component
Example 1
The co-disposal of gasification fly ash and waste incineration fly ash using the apparatus shown in fig. 1 and according to the flow scheme shown in fig. 3 comprises the following steps:
inputting gasification fly ash and waste incineration fly ash into a feeding bin according to a certain proportion, wherein the adding amount of the waste incineration fly ash is 5% of the mass of the gasification fly ash, and the two materials are fully mixed in the feeding bin and then are conveyed to an entrained flow bed through nitrogen; from the top of the air-flow bedAir is introduced into a primary air pipe of the part (the introduced amount of the air is controlled to enable the entrained flow bed to be in an oxygen-deficient state), the air is ignited through an ignition system arranged at the top of the entrained flow bed, gasified fly ash is gasified in the entrained flow bed, the temperature of a hearth of the entrained flow bed is about 1350 ℃, ash content of the gasified fly ash and waste incineration fly ash are fully melted under the high-temperature condition to form liquid slag, the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100 ℃ with normal warm water to form glassy slag, and the glassy slag can be used as building materials; the gasification process also produces a certain amount of combustible gas (with a calorific value of about 1780kCal/kg and combustible components including CO and H2) After being discharged from an exhaust port of the entrained flow bed, the gas is cooled to about 150 ℃ by a gas cooling system, and then is treated by a gas dedusting system and a gas purification system to obtain purified combustible gas which can be conveyed to a user for reuse.
Example 2
The device shown in figure 1 is used for co-processing gasified fly ash and hazardous waste incineration fly ash according to the flow shown in figure 4, and comprises the following steps:
the gasification fly ash and the waste incineration fly ash are input into a feed bin according to a certain proportion, the adding amount of the hazardous waste incineration fly ash is 50 percent of the mass of the gasification fly ash, and the two materials are fully mixed in the feed bin and then are conveyed to an entrained flow bed through nitrogen; introducing pure oxygen from a primary air pipe at the top of the entrained flow bed (controlling the introduction amount of the pure oxygen to enable the entrained flow bed to be in an oxygen-enriched state), igniting by an ignition system arranged at the top of the entrained flow bed, fully burning gasified fly ash in the entrained flow bed, wherein the temperature of a hearth of the entrained flow bed is about 1500 ℃, the ash content of the gasified fly ash and hazardous waste incineration fly ash are fully melted to form liquid slag under the high-temperature condition, and the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100 ℃ with normal temperature water to form glassy slag which can be used as building materials; and simultaneously, a certain amount of flue gas is generated in the gasification process, and is cooled to about 150 ℃ by a gas cooling system after being discharged from an exhaust port of the entrained flow bed, and then is treated by a gas dust removal system and a gas purification system to obtain purified flue gas which reaches the standard and is discharged.
Example 3
The co-disposal of the gasification fly ash, the waste incineration fly ash and the hazardous waste incineration fly ash by using the device shown in FIG. 2 and referring to the flow chart shown in FIG. 4 comprises the following steps:
inputting gasification fly ash, waste incineration fly ash and hazardous waste incineration fly ash into a feeding bin according to a certain proportion, wherein the addition amount of the waste incineration fly ash is 30% of the mass of the gasification fly ash, the addition amount of the hazardous waste incineration fly ash is 20% of the mass of the gasification fly ash, and the three materials are fully mixed in the feeding bin and then are conveyed to an entrained flow bed through nitrogen; introducing pure oxygen from a primary air pipe at the top of the entrained flow bed (controlling the introduction amount of the pure oxygen to enable the entrained flow bed to be in an oxygen-enriched state), igniting by an ignition system arranged at the top of the entrained flow bed, fully burning the gasified fly ash in the entrained flow bed, wherein the temperature of a hearth of the entrained flow bed is about 1600 ℃, the fly ash of the gasified fly ash, the waste incineration fly ash and the hazardous waste incineration fly ash are fully melted under the high-temperature condition to form liquid slag, and the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100 ℃ with normal temperature to form glassy slag which can be used as building materials; and simultaneously, a certain amount of flue gas is generated in the gasification process, and is cooled to about 150 ℃ by a gas cooling system after being discharged from an exhaust port of the entrained flow bed, and then is treated by a gas dust removal system and a gas purification system to obtain purified flue gas which reaches the standard and is discharged.
According to the above embodiment, utilize the utility model provides a device handles gasification flying dust and waste incineration flying dust altogether, has following beneficial effect:
1) the gasified fly ash is gasified or combusted through the entrained flow bed, and finally formed glassy slag can be used as building materials, so that resource utilization is realized;
2) the particle size of the incineration fly ash is similar to that of the gasification fly ash, the ash content of the gasification fly ash and the incineration fly ash are melted by using the high temperature generated during gasification or combustion of the gasification fly ash, and the obtained liquid slag is cooled to form a glassy substance, so that harmless treatment is realized;
3) by using elements such as Na, K and the like in the incineration fly ash, the ash content of the gasification fly ash and the ash melting point of the incineration fly ash can be reduced, and the full melting of the gasification fly ash and the incineration fly ash is facilitated to form liquid slag;
3) the self heat value of the gasified fly ash is fully utilized in the gasification-melting and combustion-melting processes, no external energy source, additional auxiliary fuel and the like are needed, and the cost is reduced;
4) the system temperature can reach 1350-1600 ℃ in the gasification-melting and combustion-melting processes, so that the incineration of dioxin in the incineration fly ash is realized;
5) the combustible gas generated in the gasification-melting reaction process can be used as secondary energy;
6) when the incineration fly ash is treated by the conventional method, SiO is added into the incineration fly ash2The fluxing agent is beneficial to the formation of the molten slag vitreous body, and the viscosity of the vitreous body is reduced; because of SiO in the gasified fly ash2The content can reach 50%, and also contains Al2O3Inorganic salt compositions such as CaO, the utility model discloses utilize the inorganic salt composition of self in two kinds of flying ashes, the melting process need not additionally to add and makes it form the auxiliary material that has the glass composition, is favorable to further reduction in production cost, suitable large-scale production.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (5)
1. The device for co-processing the incineration fly ash and the gasification fly ash is characterized by comprising a storage tank, a feeding bin and an entrained flow bed which are sequentially communicated, wherein the top of the entrained flow bed is connected with an ignition system and a primary air pipeline in parallel, the bottom of the entrained flow bed is provided with a slag discharging-cooling system, and an exhaust port of the entrained flow bed is sequentially communicated with a gas cooling system, a gas dedusting system and a gas purification system.
2. The apparatus of claim 1, further comprising a nitrogen generation system, wherein two gas outlets of the nitrogen generation system are respectively communicated with the feed bin and the gas dust removal system.
3. The apparatus of claim 1, wherein the storage tanks comprise an incineration fly ash storage tank and a gasification fly ash storage tank, both of which are in communication with the feed inlet of the feed bin.
4. The apparatus of claim 1, wherein the storage tanks comprise a hazardous waste incineration fly ash storage tank, a waste incineration fly ash storage tank and a gasification fly ash storage tank, and the hazardous waste incineration fly ash storage tank, the waste incineration fly ash storage tank and the gasification fly ash storage tank are all communicated with the feed inlet of the feed bin.
5. The apparatus according to any one of claims 1 to 4, wherein the slag discharging-cooling system comprises a slag discharging valve and a slag discharging tank, the slag discharging tank is connected with the entrained flow bed through the slag discharging valve, and the cooling medium in the slag discharging tank is water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921974956.6U CN211345331U (en) | 2019-11-15 | 2019-11-15 | Device for co-processing incineration fly ash and gasification fly ash |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921974956.6U CN211345331U (en) | 2019-11-15 | 2019-11-15 | Device for co-processing incineration fly ash and gasification fly ash |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211345331U true CN211345331U (en) | 2020-08-25 |
Family
ID=72100113
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921974956.6U Active CN211345331U (en) | 2019-11-15 | 2019-11-15 | Device for co-processing incineration fly ash and gasification fly ash |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211345331U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110762537A (en) * | 2019-11-15 | 2020-02-07 | 中科合肥煤气化技术有限公司 | A method and device for co-processing incineration fly ash and gasification fly ash |
-
2019
- 2019-11-15 CN CN201921974956.6U patent/CN211345331U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110762537A (en) * | 2019-11-15 | 2020-02-07 | 中科合肥煤气化技术有限公司 | A method and device for co-processing incineration fly ash and gasification fly ash |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108300516B (en) | Process system for cooperatively treating household garbage by utilizing plasma gasification furnace in coal-fired power plant | |
| CN101201167B (en) | Garbage gasification and fly ash high-temperature melting treatment device and method | |
| CN109469903B (en) | Incineration treatment method for industrial solid waste | |
| CN101469866B (en) | Industrial dangerous waste incineration processing system for realizing multiple physical states | |
| CN107008731B (en) | Waste treatment process based on biomass solid waste and hazardous waste | |
| CN104211274A (en) | Sludge reduction and recycling treatment device and sludge treatment method | |
| CN103608115B (en) | The processing method and equipment of incinerator ash | |
| CN100424415C (en) | Method and system for gasification, melting and incineration treatment of municipal solid waste | |
| CN110762537A (en) | A method and device for co-processing incineration fly ash and gasification fly ash | |
| CN101629722B (en) | Pesticide waste residue fluidized bed incinerating process and pesticide waste residue fluidized bed incinerating device | |
| CN110699124A (en) | Method and system for organic solid waste gasification melting harmless treatment | |
| CN201152531Y (en) | Industrial dangerous waste incineration processing equipment for realizing multiple physical states | |
| CN107120657A (en) | Solid waste incineration system and its technique | |
| CN201903064U (en) | Plasma refuse incinerator | |
| CN211345331U (en) | Device for co-processing incineration fly ash and gasification fly ash | |
| CN211170607U (en) | System for organic solid waste gasification melting innocent treatment | |
| CN215062095U (en) | Hazardous waste burns melting system | |
| CN114234200A (en) | Dangerous waste treatment device for rotary kiln and plasma melting furnace | |
| CN2795672Y (en) | Three burning type burning processing system for liquid and solid waste materials | |
| CN104315519A (en) | Low-pollution self-cleaning combustion method and device for high-nitrogen content combustible waste | |
| CN103822211A (en) | Gelatinization sintering treatment method of waste incineration fly ash and waste treatment method | |
| CN219279811U (en) | Bulk solid waste gasification melting furnace | |
| CN208562252U (en) | Coal-burning power plant handles the process system of house refuse using plasma gasification furnace collaboration | |
| CN216384193U (en) | Waste incineration fly ash plasma melting disposal system | |
| CN213630428U (en) | High-temperature melting and solidifying disposal system for coupling waste gasification fly ash with coal burning |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |