CN113441536B - Fly ash treatment system and fly ash treatment method - Google Patents
Fly ash treatment system and fly ash treatment method Download PDFInfo
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- CN113441536B CN113441536B CN202111008199.9A CN202111008199A CN113441536B CN 113441536 B CN113441536 B CN 113441536B CN 202111008199 A CN202111008199 A CN 202111008199A CN 113441536 B CN113441536 B CN 113441536B
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- flue gas
- fly ash
- dust
- chlorine salt
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- 239000010881 fly ash Substances 0.000 title claims abstract description 216
- 238000011282 treatment Methods 0.000 title claims abstract description 95
- 238000000034 method Methods 0.000 title claims abstract description 74
- 239000003546 flue gas Substances 0.000 claims abstract description 243
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 241
- 150000001804 chlorine Chemical class 0.000 claims abstract description 177
- 239000000428 dust Substances 0.000 claims abstract description 120
- 238000002844 melting Methods 0.000 claims abstract description 75
- 230000008018 melting Effects 0.000 claims abstract description 75
- 238000001816 cooling Methods 0.000 claims description 80
- 230000008569 process Effects 0.000 claims description 33
- 238000010438 heat treatment Methods 0.000 claims description 32
- 238000004056 waste incineration Methods 0.000 claims description 32
- 239000002893 slag Substances 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 28
- 239000000779 smoke Substances 0.000 claims description 28
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 26
- 238000007664 blowing Methods 0.000 claims description 22
- 239000004615 ingredient Substances 0.000 claims description 21
- 239000002918 waste heat Substances 0.000 claims description 20
- 239000000567 combustion gas Substances 0.000 claims description 19
- 230000007797 corrosion Effects 0.000 claims description 19
- 238000005260 corrosion Methods 0.000 claims description 19
- 238000006298 dechlorination reaction Methods 0.000 claims description 19
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 18
- 238000003723 Smelting Methods 0.000 claims description 18
- 229910052760 oxygen Inorganic materials 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 17
- 239000007921 spray Substances 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 15
- 238000002485 combustion reaction Methods 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 12
- 238000005469 granulation Methods 0.000 claims description 12
- 230000003179 granulation Effects 0.000 claims description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 11
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical group [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 10
- 150000003841 chloride salts Chemical class 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 10
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 9
- 229910052802 copper Inorganic materials 0.000 claims description 9
- 239000010949 copper Substances 0.000 claims description 9
- 229910052742 iron Inorganic materials 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 9
- 238000005507 spraying Methods 0.000 claims description 9
- 239000010936 titanium Substances 0.000 claims description 9
- 229910052719 titanium Inorganic materials 0.000 claims description 9
- 239000003245 coal Substances 0.000 claims description 8
- 238000005485 electric heating Methods 0.000 claims description 8
- 239000006004 Quartz sand Substances 0.000 claims description 7
- 125000001309 chloro group Chemical group Cl* 0.000 claims description 7
- 230000004927 fusion Effects 0.000 claims description 6
- 239000002737 fuel gas Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 2
- 229910001882 dioxygen Inorganic materials 0.000 claims description 2
- 239000000155 melt Substances 0.000 claims 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 21
- 239000000460 chlorine Substances 0.000 abstract description 21
- 229910052801 chlorine Inorganic materials 0.000 abstract description 21
- 238000010309 melting process Methods 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- 239000002826 coolant Substances 0.000 description 17
- 230000000694 effects Effects 0.000 description 17
- 238000010248 power generation Methods 0.000 description 15
- 238000000746 purification Methods 0.000 description 15
- 229910001385 heavy metal Inorganic materials 0.000 description 11
- 150000003839 salts Chemical class 0.000 description 11
- 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 10
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 230000009467 reduction Effects 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 229910001069 Ti alloy Inorganic materials 0.000 description 5
- 239000003513 alkali Substances 0.000 description 5
- 230000000903 blocking effect Effects 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- GALOTNBSUVEISR-UHFFFAOYSA-N molybdenum;silicon Chemical compound [Mo]#[Si] GALOTNBSUVEISR-UHFFFAOYSA-N 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 239000012266 salt solution Substances 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 239000010882 bottom ash Substances 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 3
- 239000000853 adhesive Substances 0.000 description 3
- 230000001070 adhesive effect Effects 0.000 description 3
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- 150000001340 alkali metals Chemical class 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- 238000010791 quenching Methods 0.000 description 3
- 230000000171 quenching effect Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- XTEGARKTQYYJKE-UHFFFAOYSA-M Chlorate Chemical compound [O-]Cl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-M 0.000 description 2
- 238000005054 agglomeration Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 229910010293 ceramic material Inorganic materials 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
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 229910052745 lead Inorganic materials 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 239000007769 metal material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M potassium chloride Inorganic materials [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 229910052718 tin Inorganic materials 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- 235000017166 Bambusa arundinacea Nutrition 0.000 description 1
- 235000017491 Bambusa tulda Nutrition 0.000 description 1
- 241001330002 Bambuseae Species 0.000 description 1
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 1
- HMDDXIMCDZRSNE-UHFFFAOYSA-N [C].[Si] Chemical compound [C].[Si] HMDDXIMCDZRSNE-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 239000011425 bamboo Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 230000009920 chelation Effects 0.000 description 1
- 238000011284 combination treatment Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 1
- 229910010271 silicon carbide Inorganic materials 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- -1 steam Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a fly ash treatment system and a fly ash treatment method. The fly ash treatment system comprises: a fly ash melting unit having a fly ash inlet and a dusty flue gas outlet; the dust removal unit is provided with a dust-containing flue gas inlet and a dust-removing flue gas outlet, and the dust-containing flue gas inlet is communicated with the dust-removing flue gas outlet; the chlorine salt collecting unit is provided with a dust removal flue gas inlet and a chlorine removal flue gas outlet, the dust removal flue gas inlet is communicated with the dust removal flue gas outlet, and the chlorine salt collecting unit is provided with a heater and a cooler. Melting the fly ash by a fly ash melting unit, so that the chlorine salt is volatilized along with the flue gas in the melting process to form dust-containing flue gas; the dust removal unit removes particulate matters in the dust-containing flue gas; the cooler of the chlorine salt collecting unit cools the dust removal flue gas, so that chlorine salt in the dust removal flue gas is condensed and attached to the inner wall, after the chlorine salt is attached to a certain degree, the introduction of the dust removal flue gas is stopped, and the heater is started to melt the chlorine salt, so that the chlorine salt is collected and then discharged out of the chlorine salt collecting unit.
Description
Technical Field
The invention relates to the technical field of waste incineration fly ash treatment, in particular to a fly ash treatment system and a fly ash treatment method.
Background
The waste incineration fly ash is a secondary pollutant produced in the process of domestic waste incineration power generation, and is rich in more harmful substances such as heavy metal, dioxin, chloride and the like, and belongs to dangerous waste. The high chlorine content is a typical characteristic of the fly ash generated by incinerating the garbage in China, and the treatment difficulty of the fly ash is increased. The existing fly ash treatment method mainly comprises the methods of high-temperature melting, cement kiln cooperative treatment, low-temperature pyrolysis, water washing, chelation treatment and combination treatment in various modes, mainly aims to solve the problem that the fly ash is high in content of dioxin, chlorine salt, heavy metal and the like, and finally achieves the aim of harmless treatment of the fly ash.
Although most of chloride salt can be removed by the fly ash washing method, filter residue after washing is still dangerous waste, a corresponding sewage treatment system is needed, the process flow is complex, and the harmless disposal capability is poor. The high-temperature melting method is characterized in that fly ash is fed into a high-temperature melting furnace, dioxin can be rapidly decomposed at 1200-1400 ℃, chlorine salt can be volatilized into secondary smoke dust, most heavy metals are volatilized into the smoke dust, a small part of heavy metals are remained in molten slag, the heavy metals are solidified after water quenching, and the produced slag is general solid waste and can be used as building material raw materials. Although the high-temperature melting can realize thorough harmless treatment, the flue gas contains a large amount of chloride, so that the flue gas is easy to condense in a flue and blocks a pipeline, and great trouble is brought to a flue gas treatment system.
The chinese patent application No. 202010743433.1 discloses a fly ash disposal process and system, wherein the flue gas is washed by water after the fly ash is melted, the obtained solution is evaporated and crystallized to obtain molten salt, the method needs to consume a large amount of water, the evaporation and crystallization can also consume more energy, and the direct water washing of the high-temperature flue gas can generate a large amount of water vapor in the flue gas to corrode equipment, and the high-temperature waste heat can not be recycled.
Disclosure of Invention
The invention mainly aims to provide a fly ash treatment system and a fly ash treatment method, so as to solve the problem of high water consumption of chlorine salt recovery in fly ash in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a fly ash treatment system comprising: a fly ash melting unit having a fly ash inlet and a dusty flue gas outlet; the dust removal unit is provided with a dust-containing flue gas inlet and a dust-removing flue gas outlet, and the dust-containing flue gas inlet is communicated with the dust-containing flue gas outlet; the chlorine salt collecting unit is provided with a dust removal flue gas inlet and a chlorine removal flue gas outlet, the dust removal flue gas inlet is communicated with the dust removal flue gas outlet, and the chlorine salt collecting unit is provided with a heater and a cooler.
Furthermore, the dust-containing flue gas inlet and the dust-containing flue gas outlet are communicated through a flue, the flue is provided with a spray gun, the fly ash treatment system further comprises a fuel supply device and a combustion gas supply device, the fuel supply device and the combustion gas supply device are connected with the spray gun, and the combustion gas supply device is a compressed air supply device or an oxygen-enriched air supply device.
Further, the chlorine salt collecting unit includes: the heater and the cooler are detachably arranged in the buffer tank, and the dedusting flue gas inlet and the dechlorination flue gas outlet are arranged on the buffer tank; and the chlorine salt collector is arranged at the bottom of the buffer tank and is detachably communicated with the buffer tank.
Further, the above buffer tank includes: the minimum port of the gradually expanding part is used as a dust removal flue gas inlet; the heat exchange part is provided with an accommodating cavity, the heater and the cooler are detachably arranged in the accommodating cavity, and the chlorine salt collector is communicated with the bottom of the heat exchange part and the chlorine salt collector; the heat exchange part is communicated with the smoke exhaust part.
Further, the maximum port area of the divergent part is 5 to 20 times of the minimum port area.
Further, above-mentioned heat transfer portion includes the lateral wall, and the lower part of lateral wall has the opening, and the both ends of lateral wall respectively with divergent portion and the portion of discharging fume be connected the chlorate collector and include: the flow guide part is a funnel-shaped flow guide part, the flow guide part is connected with the side wall, and an opening at the upper part of the flow guide part corresponds to an opening of the side wall; the collecting part is detachably connected with the lower opening of the flow guide part.
Further, the heater is a corrosion-resistant heater.
Further, the corrosion-resistant heater is a titanium electric heating pipe, or the corrosion-resistant heater comprises a heating rod and a corrosion-resistant material wrapping the heating rod.
Further, the heating rod is a silicon-molybdenum rod.
Further, the corrosion-resistant material is a titanium metal material or a ceramic material.
Further, the cooler includes one or more cooling pipes arranged in parallel.
Further, the fly ash melting unit comprises a smelting furnace, the smelting furnace is provided with a fly ash inlet and a dust-containing smoke outlet, the smelting furnace is an electric furnace or a bottom blowing furnace, the fly ash treatment system further comprises a fly ash granulation unit and a batching supply unit, the batching supply unit is connected with the fly ash granulation unit and used for granulating the fly ash and batching to form lumps, the fly ash granulation unit is provided with a lump outlet, and the lump outlet is connected with the fly ash inlet; or the smelting furnace is a side-blown furnace or a bottom-blown furnace, the smelting furnace comprises a material mixing inlet and a fly ash inlet, the fly ash inlet is provided with a powder spraying gun, and the material mixing inlet is arranged at the upper part of the smelting furnace.
Furthermore, a blocking device is arranged between the dust-containing flue gas outlet and the fly ash inlet.
Furthermore, the dust removal unit is also provided with a smoke outlet which is communicated with the fly ash inlet of the fly ash melting unit.
According to another aspect of the present invention, there is provided a fly ash treatment method, including: carrying out fusion treatment on the fly ash to obtain dust-containing flue gas; carrying out dust removal treatment on the dust-containing flue gas to obtain dust-removed flue gas; cooling the dedusting flue gas to condense and attach chlorine salt in the dedusting flue gas to a chlorine salt collecting unit, and enabling the obtained dechlorination flue gas to flow out of the chlorine salt collecting unit; and heating the chlorine salt collecting unit to condense the attached chlorine salt so as to melt and discharge the chlorine salt.
Further, before the dust-containing flue gas is treated, the fly ash treatment method further comprises the step of spraying fuel and combustion gas into the dust-containing flue gas passing through the flue to perform flue gas combustion, wherein the combustion gas is compressed air or oxygen-enriched air, the combustion temperature of the flue gas is 1000-1200 ℃, and the oxygen gas volume concentration in the flue is controlled to be 1-10%.
Further, cooling the dedusting flue gas to 500-700 ℃ to condense and attach chlorine salt in the dedusting flue gas.
Further, the heating chlorine salt collecting unit condenses the attached chlorine salt to 900-1000 ℃.
Further, the cooling process of the dedusting flue gas comprises the following steps: expanding and cooling the dedusting flue gas; and cooling the expanded and cooled dedusting flue gas by adopting a concurrent cooling mode, a countercurrent cooling mode or a combined mode of concurrent cooling and countercurrent cooling.
Further, the temperature of the melting treatment is 1200 to 1400 ℃.
Further, the fly ash and the ingredients are mixed and melted, and the ingredients comprise any one or more of coal, quartz sand, iron tailings, copper slag and waste incineration bottom slag.
Further, the fly ash is derived from fly ash generated in a waste incineration process, and the waste incineration process comprises the following steps: an incineration treatment step, wherein incineration flue gas and incineration bottom slag are generated in the incineration treatment step; recovering waste heat of incineration flue gas to obtain cooling flue gas; and purifying the cooling flue gas to obtain purified flue gas and fly ash.
Furthermore, the incineration bottom slag is used as an ingredient when the fly ash is melted.
Further, the dechlorination flue gas and the incineration flue gas are subjected to waste heat recovery together, or the dechlorination flue gas and the cooling flue gas are mixed and then purified.
By applying the technical scheme of the invention, the fly ash is melted by the fly ash melting unit, so that the chlorine salt is volatilized with the flue gas in the melting process to form dust-containing flue gas; then removing the particulate matters in the dust-containing flue gas by using a dust removal unit; and then, the cooler of the chlorine salt collecting unit is used for cooling the dedusting flue gas, so that the chlorine salt in the dedusting flue gas is condensed and attached to the inner wall, and the particulate matter is removed in the prior art, so that the purity of the chlorine salt is high and the adhesive force is high, after the chlorine salt is attached to a certain degree, the introduction of the dedusting flue gas is stopped, and the heater is started to melt the chlorine salt, so that the chlorine salt is collected and then discharged out of the chlorine salt collecting unit.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 shows a schematic structural diagram of a fly ash treatment system provided according to an embodiment of the invention;
FIG. 2 shows a schematic cross-sectional view of a chlorine salt collection unit of a fly ash treatment system provided according to an embodiment of the invention;
FIG. 3 shows a top view of the chlorine salt collection unit shown in FIG. 2;
FIG. 4 shows a schematic cross-sectional view of a chlorine salt collection unit of a fly ash treatment system according to another embodiment of the present invention;
FIG. 5 shows a top view of the chlorine salt collection unit shown in FIG. 2;
FIG. 6 shows a combined block diagram of a fly ash treatment system and a waste incineration system provided according to an embodiment of the invention.
Wherein the figures include the following reference numerals:
10. a fly ash melting unit; 20. a flue; 21. a spray gun; 30. a dust removal unit;
40. a chloride salt collection unit; 411. a divergent section; 412. a heat exchanging part; 413. a smoke exhaust part; 421. a flow guide part; 422. a collecting section; 43. a heater; 44. a cooler;
01. an incineration unit; 02. a waste heat recovery unit; 03. a flue gas purification unit.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
As analyzed by the background art of the application, the prior art adopts a water washing mode to remove chlorine salt, so that the water consumption is high, the cost is high, and in order to solve the problem, the application provides a fly ash treatment system and a fly ash treatment method.
In an exemplary embodiment of the present application, there is provided a fly ash treatment system, as shown in fig. 1, comprising a fly ash melting unit 10, a dust removal unit 30 and a chloride salt collection unit 40, the fly ash melting unit 10 having a fly ash inlet and a dusty flue gas outlet; the dust removal unit 30 is provided with a dust-containing flue gas inlet and a dust-removing flue gas outlet, and the dust-containing flue gas inlet is communicated with the dust-containing flue gas outlet; the chlorine salt collecting unit 40 has a dust removal flue gas inlet and a chlorine removal flue gas outlet, the dust removal flue gas inlet is communicated with the dust removal flue gas outlet, and the chlorine salt collecting unit 40 is provided with a heater 43 and a cooler 44.
According to the fly ash treatment system, fly ash is melted through the fly ash melting unit 10, so that chlorine salt is volatilized with flue gas in the melting process to form dust-containing flue gas; then, the dust removal unit 30 is adopted to remove the particulate matters in the dust-containing flue gas; and then, the dust removal flue gas is cooled by the cooler 44 of the chlorine salt collection unit 40, so that the chlorine salt in the dust removal flue gas is condensed and attached to the inner wall, and the particulate matter is removed before the dust removal flue gas, so that the purity and the adhesive force of the chlorine salt are high, after the chlorine salt is attached to a certain degree, the introduction of the dust removal flue gas is stopped, and the heater 43 is started to melt the chlorine salt, so that the chlorine salt is collected and then discharged out of the chlorine salt collection unit 40.
The fly ash does not need to be washed by water in the process, large amount of water is avoided being consumed, the fly ash incineration melting unit 10 and the chlorine salt collecting unit 40 can be additionally arranged in the original plant area of the waste incineration system, and the fly ash incineration collected in the waste incineration power generation flue gas purification system is directly sent to the fly ash melting unit 10 of the fly ash treatment system to be treated. The flue gas dechlorinated by the chlorine salt collecting unit 40 has less harmful substance quality, can be directly merged into an incineration power generation or waste incineration flue gas purification system, and a separately constructed flue gas purification system is omitted. After the chlorine salt is collected in the chlorine salt collecting unit 40, the condensed molten salt is melted and dropped and collected by periodically adopting a heating mode, and the molten salt can be melted and electrolyzed to produce chlorine gas and alkali metal or the solution can be electrolyzed to produce chlorine gas and alkali liquor after impurity removal.
In some embodiments, the inlet of the dust-laden gas and the outlet of the dust-laden gas are communicated through a flue 20, in order to avoid the dust-laden gas from being condensed in the flue 20 due to temperature reduction before entering the dust removal unit to cause blockage of the flue 20 and to cause blockage of the dust removal pipe in subsequent dust removal, a spray gun 21 is arranged in the flue 20, and the fly ash treatment system further comprises a fuel supply device and a combustion gas supply device, wherein the fuel supply device and the combustion gas supply device are connected with the spray gun 21, and the combustion gas supply device is a compressed air supply device or an oxygen-enriched air supply device. Fuel and combustion gas are sprayed into the flue 20 through the spray gun 21, so that dust-containing flue gas is further combusted in the flue 20, complete combustion of the flue gas can be further promoted, and the resynthesis of dioxin during subsequent temperature reduction is inhibited; and the heat generated by combustion can be used to prevent the problem that the chloride is condensed to block the pipeline due to the low temperature of the flue 20 and the dust removing unit 30. The content of oxygen in the combustion gas sprayed by the spray gun 21 is adjusted, so that the proportion of the fuel to the oxygen in the combustion gas is adjusted, the oxidation or reduction of the dust-containing flue gas is realized, and in order to realize sufficient combustion, the concentration of the oxygen is controlled to be 1-10% after the combustion.
The dust removing unit 30 may be a cyclone dust removing unit 30 for performing coarse dust removal on the dust-containing flue gas, and removing most of solid particles (main components include CaO, FeO, and SiO) in the high-temperature flue gas2Etc. oxides). The dust removing unit 30 may further be provided with a smoke outlet, the smoke outlet is communicated with the fly ash inlet of the fly ash melting unit 10, and the solid particles collected by the dust removing unit 30 are returned to the fly ash melting unit 10 to be melted together with the fly ash.
In order to improve the separation effect of the chlorine salt, in some embodiments, as shown in fig. 2 to 5, the chlorine salt collecting unit 40 includes a buffer tank in which a heater 43 and a cooler 44 are detachably installed, and a flue gas dust removal inlet and a flue gas chlorine removal outlet are disposed; the chlorine salt collector is arranged at the bottom of the buffer tank and is communicated with the buffer tank. The heater 43 and the cooler 44 are detachably arranged in the buffer tank, so that the heater 43 and the cooler 44 are convenient to repair and replace, the cooler 44 can be taken out when the heater 43 works, and the heater 43 can be taken out when the cooler 44 works, so that the corrosion of the heater 43 and the cooler 44 in the buffer tank is reduced. In addition, a chlorine salt collector is independently arranged outside the buffer tank, so that condensed chlorine salt can be conveniently collected after being melted, and the collected chlorine salt can be separated out in time.
Further, in order to better achieve the cooling effect on the dedusting flue gas and reduce the use of the cooling medium, in some embodiments, as shown in fig. 2 to 5, the buffer tank includes a divergent portion 411, a heat exchanging portion 412 and a smoke exhaust portion 413, a minimum port of the divergent portion 411 is used as a dedusting flue gas inlet, and preferably, a maximum port area of the divergent portion 411 is 5 to 20 times of a minimum port area; the heat exchanging part 412 has a receiving chamber in which the heater 43 and the cooler 44 are detachably mounted, and the chlorine salt collector communicates with the bottom of the heat exchanging part 412 and with the chlorine salt collector; the heat exchanging portion 412 communicates with the smoke exhausting portion 413. By the arrangement of the gradually expanding part 411, the dedusting flue gas entering the buffer tank is cooled by utilizing the expansion effect of the gas, and is further cooled to the target temperature by further matching with the action of the cooler 44 in the heat exchanging part 412, so that the dedusting flue gas is cooled on the basis of reducing the cooling consumption. The inner wall of the buffer tank can be made of materials such as commercial pure titanium and titanium alloy which are resistant to chloride corrosion, the service life of the buffer tank can be prolonged, and the long-term stable operation of the chloride collection device can be ensured.
In order to simplify the structure of the chlorine salt collector, in the following embodiments, as shown in fig. 2 and 4, the heat exchanging part 412 includes a side wall, the lower part of the side wall has an opening, two ends of the side wall are respectively connected with the diverging part and the smoke discharging part, the chlorine salt collector includes a flow guiding part 421 and a collecting part 422, the flow guiding part 421 is a funnel-shaped flow guiding part 421, the flow guiding part 421 is connected with the side wall, and the upper opening of the flow guiding part 421 corresponds to the opening of the side wall; the collecting part 422 is detachably connected to the lower opening of the guide part 421. The flow guide part 421 is used to guide the flow of the molten chloride, so as to improve the collecting efficiency of the chloride.
The sidewall of the heat exchanging part 412 may have a cylindrical shape or a square cylinder, and is preferably a square cylinder sidewall for facilitating the arrangement of the heater 43 and the cooler 44 in the receiving chamber, and the bottom sidewall of the square cylinder sidewall may be absent to form the opening, and then the guiding part 421 is designed to have a truncated quadrangular pyramid shape to be abutted against the sidewall. In some embodiments, the end of the diverging portion 411 that connects to the sidewall is square, and the end that connects to the flue 20 has the same cross-sectional shape as the flue 20, such as circular. In order to avoid the heat exchanging unit 412 having a dead edge and thus making it difficult to separate chlorine salts, the heat exchanging unit 412 may have a chamfered edge.
Since the flue gas contains certain corrosive substances, in order to prolong the service life of the equipment, the heater 43 is a corrosion-resistant heater, preferably, the corrosion-resistant heater is a titanium electric heating tube, or preferably, the corrosion-resistant heater comprises a heating rod and a corrosion-resistant material wrapping the heating rod, preferably, the heating rod is a silicon-molybdenum rod, and preferably, the corrosion-resistant material is a titanium metal material or a ceramic material. The heater 43 is made of a corrosion-resistant and high-temperature-resistant material, so that the service life is long.
Since the cooler 44 may be selectively removed during heating, the corrosion resistance of the material of the cooler 44 is not critical. To simplify the construction and to achieve the best possible cooling effect, the cooler 44 comprises one or more cooling tubes arranged in parallel. The cooling pipe can be a coil pipe or a coiled pipe commonly used in the field, and when the cooling pipe is the coiled pipe, the flow directions of the cooling medium and the dedusting flue gas can be controlled to be the same or opposite, namely, concurrent cooling or countercurrent cooling can be adopted; when a plurality of cooling pipes are arranged in parallel, a plurality of U-shaped pipes can be arranged in parallel, the extending direction of the U-shaped pipes is parallel to the transverse direction of the buffer tank, and the flow direction of the cooling medium is controlled during cooling, for example, the flow direction of the cooling medium is controlled to be consistent in all the U-shaped pipes, so that all the U-shaped pipes can share one inlet and one outlet; when the flow direction of the cooling medium in the adjacent U-shaped tubes is controlled to be opposite, the U-shaped tubes having the same flow direction may share one inlet and one inlet.
When counter-flow cooling is adopted, as shown in fig. 2, a cooling medium enters from the low-temperature end and flows out from the high-temperature end, and a certain temperature difference exists inside the buffer tank, so that the temperature of the flowing cooling medium is high, and the waste heat recovery effect is good. When adopting the following current cooling, the arrow of figure 2 is reverse, and cooling medium gets into from the high temperature end, and the low temperature end flows out, and buffer tank inside temperature is comparatively more balanced this moment, and the front end high temperature district cooling effect is good, and the cooling medium temperature of outflow can be lower. When parallel cooling is adopted, as shown in fig. 4 and 5, cooling media flow in and out at specific positions inside the buffer tank, each cooling pipe is relatively independent, the flow rate is adjustable, the cooling mode is flexible and controllable, and the cooling effect is good; the structure can also be a metal pipe network mode and the like, and all the structural arrangements are all used for realizing good cooling effect, thus being beneficial to chloride condensation and simultaneously taking account of the heat energy recovery effect of the cooling medium. The fly ash melting unit 10 of the present application can refer to a fly ash melting device commonly used in the art, such as the fly ash melting unit 10 comprises a furnace having a fly ash inlet and a dusty flue gas outlet.
When the smelting furnace is an electric furnace or a bottom blowing furnace, the fly ash treatment system also comprises a fly ash granulation unit and an ingredient supply unit, wherein the ingredient supply unit is connected with the fly ash granulation unit and used for granulating the fly ash and ingredients to form lumps, the fly ash granulation unit is provided with a lump outlet, and the lump outlet is connected with a fly ash inlet. The fly ash is premixed with other materials (one or more of coal, quartz sand, iron tailings, copper slag, incineration bottom ash and the like) and then briquetted, and the briquettes are directly put into a molten pool from an upper charging port (namely a fly ash inlet). In order to prevent the added materials from entering the flue gas in a large amount after being pulverized, the fly ash inlet and the flue gas outlet are designed to be far away from each other. If the two are electric furnaces or bottom blowing furnaces which are close to each other, a blocking device is arranged between the dust-containing smoke outlet and the fly ash inlet for blocking.
When the smelting furnace is a side-blown furnace or a bottom-blown furnace, the smelting furnace comprises a material mixing inlet and a fly ash inlet, the fly ash inlet is provided with a powder spraying gun, and the material mixing inlet is arranged at the upper part of the smelting furnace. When a side blowing and bottom blowing furnace device is adopted, fly ash and fuel can be injected and added by adopting a powder gun, other blocky ingredients (one or more of coal, quartz sand, iron tailings, copper slag, bottom ash for incineration and the like) can be fed from a feeding port above, the smoke at the position of an ingredient inlet is not large, and a partition between the ingredient inlet and a dust-containing smoke outlet can be left or cancelled.
The fly ash of the fly ash fusion unit 10 of the present application can be from a waste incineration system. In some embodiments, as shown in fig. 6, the waste incineration system comprises an incineration unit 01, a waste heat recovery unit 02 and a flue gas purification unit 03, wherein the incineration unit 01 has an incineration flue gas outlet and an incineration bottom slag outlet; the waste heat recovery unit 02 is provided with an incineration flue gas inlet and a cooling flue gas outlet, and the incineration flue gas inlet is connected with the incineration flue gas outlet; the flue gas purification unit 03 is provided with a fly ash outlet and a purified flue gas outlet, and the fly ash outlet is connected with the fly ash inlet. In the waste incineration system, incineration flue gas generated by the incineration unit 01 enters the waste heat recovery unit 02 to recover waste heat of the incineration flue gas, and then cooling flue gas is sent to the flue gas purification unit 03 to be purified, for example, dust removal, desulfurization, denitration and the like are performed, and fly ash is obtained by dust removal.
After the chlorine salt collecting unit 40 through this application is handled, the dechlorination flue gas temperature that obtains is though greatly reduced, still has higher heat, preheats in order to retrieve this part, links to each other dechlorination exhanst gas outlet and waste heat recovery unit and preheats in order to utilize the recovery of waste heat unit, has integrated equipment, has both avoided the waste heat to waste, has practiced thrift the waste heat recovery cost again. In other embodiments, if the temperature of the dechlorination flue gas is low and the effect of waste heat recovery is not good, the dechlorination flue gas outlet can be connected with the flue gas purification unit 03 to purify the dechlorination flue gas by using the flue gas purification unit 03, and the purified flue gas is discharged after reaching the standard.
In another exemplary embodiment of the present application, there is provided a fly ash treatment method including: carrying out fusion treatment on the fly ash to obtain dust-containing flue gas; carrying out dust removal treatment on the dust-containing flue gas to obtain dust-removed flue gas; cooling the dedusting flue gas to condense and attach chlorine salt in the dedusting flue gas to the chlorine salt collecting unit 40, and enabling the obtained dechlorination flue gas to flow out of the chlorine salt collecting unit 40; the chlorine salt collecting unit 40 is heated to condense the attached chlorine salt, so that the chlorine salt is melted and discharged.
Melting the fly ash, and volatilizing chloride salt along with the smoke in the melting process to form dust-containing smoke; then removing the particulate matters in the dust-containing flue gas; and then cooling the dedusting flue gas, so that the chlorine salt in the dedusting flue gas is condensed and attached to the inner wall of the chlorine salt collecting unit 40, and because the particulate matters are removed before, the purity and the adhesive force of the chlorine salt are high, after the chlorine salt is attached to a certain degree, stopping introducing the dedusting flue gas, and heating to melt and discharge the chlorine salt.
The process does not need to consume a large amount of water, the incineration fly ash melting unit 10 and the chloride collecting unit 40 can be additionally arranged in the factory of the original waste incineration system, and the incineration fly ash collected in the waste incineration power generation flue gas purification system is directly treated by the method. The flue gas dechlorinated by the chlorine salt collecting unit 40 has less harmful substance quality, can be directly merged into an incineration power generation or waste incineration flue gas purification system, and a separately constructed flue gas purification system is omitted. And melting and falling condensed molten salt by periodically adopting a heating mode and collecting the molten salt, and melting and electrolyzing the molten salt to produce chlorine and alkali metal or electrolyzing the solution to produce chlorine and alkali liquor after impurity removal of the molten salt.
In order to avoid the blockage of the flue 20 caused by the condensation of the flue 20 due to the temperature reduction of the dust-containing flue gas before the dust-containing flue gas enters the dust-removing flue gas and the blockage of the dust-removing pipeline caused by the condensation of the dust-containing flue gas in the subsequent dust removal, before the dust-containing flue gas is treated, the fly ash treatment method further comprises the step of spraying fuel and combustion gas into the dust-containing flue gas passing through the flue 20 to perform flue gas combustion, wherein the combustion gas is compressed air or oxygen-enriched air, and the combustion temperature of the flue gas is 1000-1200 ℃. By spraying fuel and combustion gas, the dust-containing flue gas is further combusted in the flue 20, so that the complete combustion of the flue gas can be further promoted, and the resynthesis of dioxin during subsequent cooling is inhibited; and the heat generated by combustion can be used to prevent the problem that the chloride is condensed to block the pipeline due to the low temperature of the flue 20 and the dust removing unit 30. And the oxygen concentration in the flue 20 is controlled to be between 1 and 10 percent so as to ensure the safety.
This application is in order to condense chloride as far as possible to avoid cold to consume extravagantly, preferably with the dust removal flue gas cool down to 500~700 ℃ make the chloride condensation in the dust removal flue gas adhere to. In addition, in order to melt and discharge the condensed and adhered chlorine salt as much as possible, it is preferable to heat the condensed and adhered chlorine salt in the chlorine salt collecting unit 40 to 900 to 1000 ℃.
In order to reduce the cooling loss during the temperature reduction of the flue gas, in some embodiments, the temperature reduction process of the flue gas includes: expanding and cooling the dedusting flue gas; and cooling the expanded and cooled dedusting flue gas by adopting a concurrent cooling mode, a countercurrent cooling mode or a combined mode of concurrent cooling and countercurrent cooling. The above implementation manner can refer to the structural arrangement of the chlorine salt collecting unit 40 of the present application, and of course, those skilled in the art can also adopt other implementation manners, which are not described herein again. The cooling medium can be various substances such as water, water vapor, air, nitrogen and the like, is cheap and safe, can provide various options, and is easy to implement; the heat of the cooling medium can be recovered, the recovery mode is various, the heat exchanger can be used for heat exchange to generate electricity, and the heat exchanger can also be used for directly producing high-temperature steam or used as a heat source in other areas of a waste incineration plant.
The application can refer to the conventional melting treatment process in the prior art for the melting treatment of the fly ash, so that the residual chlorine in the slag is lower as much as possible in order to ensure the large volatilization of the chlorine salt, and the problems of higher chlorine content and volatile heavy metal content after water quenching of the slag are solved conveniently. The temperature of the melting treatment is preferably 1200 to 1400 ℃, which is understood by those skilled in the art as the stability of the molten pool during the melting treatment. The treated fly ash does not need to be pretreated or is pretreated by a simple method, the treatment adaptability to incineration fly ash containing more heavy metals, dioxin, chloride salts and the like is strong, the fly ash can be directly sprayed to a molten pool, and the fusion treatment can also be carried out after pelletizing and agglomeration.
In order to improve the melting treatment efficiency, the fly ash and the ingredients are preferably subjected to mixed melting treatment, and the ingredients comprise any one or more of coal, quartz sand, iron tailings, copper slag and waste incineration bottom slag. The above-mentioned mixing and melting treatment may be performed by using a melting furnace. When the smelting furnace is an electric furnace or a bottom blowing furnace, the fly ash treatment system also comprises a fly ash granulation unit and an ingredient supply unit, wherein the ingredient supply unit is connected with the fly ash granulation unit and used for granulating the fly ash and ingredients to form lumps, the fly ash granulation unit is provided with a lump outlet, and the lump outlet is connected with a fly ash inlet. The fly ash is premixed with other materials (one or more of coal, quartz sand, iron tailings, copper slag, incineration bottom ash and the like) and then briquetted, and the briquettes are directly put into a molten pool from an upper charging port (namely a fly ash inlet). In order to prevent the added materials from entering the flue gas in a large amount after being pulverized, the fly ash inlet and the flue gas outlet are designed to be far away from each other. If the two are electric furnaces or bottom blowing furnaces which are close to each other, a blocking device is arranged between the dust-containing smoke outlet and the fly ash inlet for blocking. When the smelting furnace is a side-blown furnace or a bottom-blown furnace, the smelting furnace comprises a material mixing inlet and a fly ash inlet, the fly ash inlet is provided with a powder spraying gun, and the material mixing inlet is arranged at the upper part of the smelting furnace. When a side blowing and bottom blowing furnace device is adopted, fly ash and fuel can be injected and added by adopting a powder gun, other blocky ingredients (one or more of coal, quartz sand, iron tailings, copper slag, bottom ash for incineration and the like) can be fed from a feeding port above, the smoke at the position of an ingredient inlet is not large, and a partition between the ingredient inlet and a dust-containing smoke outlet can be left or cancelled.
The fly ash treatment method of the present application is not particularly limited in the content of heavy metals, dioxin and chloride salts in the fly ash, for example, the fly ash is from fly ash generated in a waste incineration process, and the fly ash treatment method of the present application can be used for treating even if the content of heavy metals, dioxin and chloride salts in the fly ash is high. The present application provides a typical waste incineration process, this waste incineration process includes: an incineration treatment step, wherein incineration flue gas and incineration bottom slag are generated in the incineration treatment step, and the incineration bottom slag is preferably used as a material for fly ash melting; recovering waste heat of incineration flue gas to obtain cooling flue gas; and purifying the cooling flue gas to obtain purified flue gas and fly ash. After the waste heat of incineration flue gas generated by incineration is recovered, cooling flue gas is purified, for example, dust removal, desulfurization, denitration and other treatments are carried out, and fly ash is obtained by dust removal.
In some embodiments, in order to realize the collection and utilization of heat, the dechlorination flue gas and the incineration flue gas are subjected to waste heat recovery together, or the dechlorination flue gas and the cooling flue gas are mixed and then purified.
The fly ash treatment method can be realized by adopting the fly ash treatment system.
The above structures, processes and effects of the present application are described below with reference to the embodiments, which are only exemplary and should not limit the scope of the present application.
Example 1
Collecting fly ash in the process of waste incineration power generation, periodically discharging the fly ash into a charging system of a fly ash melting device, mixing the fly ash with incineration bottom slag, silica and iron tailings to prepare balls to obtain pretreated fly ash, and then putting the pretreated fly ash into a fly ash melting electric furnace in batches, wherein the melting point of the pretreated fly ash is controlled to be 1200-1400 ℃, and the smelting temperature is controlled to be 1300-1500 ℃ (ensuring the superheat degree of 100 ℃) to control CaO/SiO in slag2The proportion of the slag can be about 1.0 to ensure a lower slag melting point.
In the process of melting the fly ash, the temperature of a molten pool of the electric furnace is maintained at about 1400 ℃, the stirring of the molten pool is weak, the stirring is mainly carried out by the position near a high-temperature electrode, and a large amount of chloride is volatilized into dust-containing smoke. The flue gas of the electric furnace has strong reducibility and a large amount of unburned substances. After the flue gas enters the flue 20, the spray gun 21 positioned at the position of the temperature control pipeline sprays oxygen enrichment to ensure CO and H in the flue gas2And organic matters and the like are completely combusted, the temperature of flue gas in the flue 20 is maintained at about 1200 ℃, and O in the flue 202The concentration is about 5%. The dust-containing flue gas passing through the flue 20 enters the chlorine salt collecting unit 40 after being subjected to coarse dust removal by the cyclone dust collector, and the coarse dust returns to the feeding system and is then fed into the fly ash melting electric furnace.
The dust removal flue gas that contains the high chlorine salt after the dust removal gets into chlorine salt collection unit 40, and the circular pipeline diameter of entry is 300mm, and flue gas temperature is 1200 ℃, and chlorine salt collection unit 40's heat transfer portion 412 is square tube-shape, and the sub-unit connection is convenient for funnel-shaped water conservancy diversion portion 421 and the circular collection portion 422 of the quadrangular frustum of the pyramid that the chlorine salt was collected, and heat transfer portion 412 is 3000mm long, and the cross-section is the square that the width is 900mm, and circular pipeline entry sectional area is 11.46 with heat transfer portion 412 sectional area ratio: 1, the outlet position temperature of the chloride collection unit 40 is about 500 ℃, the cooling medium is water, the cooling pipeline is made of commercial pure titanium (CP titanium), the cooling structure is a parallel cooling mode as shown in figure 4, more than 90% of chloride is condensed in the chloride collection unit 40, and the dechlorinated smoke is coarsely dedusted and then is merged into a smoke purification system for waste incineration power generation.
After more chlorine is collected in the chlorine salt collecting device, the cooling effect is poor, the temperature of the outlet position of the chlorine salt collecting device may exceed 700 ℃, at the moment, the electric furnace is closed, and the electric heating temperature rise is started to melt and remove the condensed chlorine salt. At this time, the front and rear ends of the flue 20 of the chlorine salt collecting unit 40 are sealed, the cooling water is removed, and the power is turned on to heat the chlorine salt collecting unit 40, so that the temperature of the chlorine salt collecting unit 40 can be rapidly raised from 500 ℃ to about 1000 ℃, and the chlorine salt is melted and dropped to the lower part to be collected. The heating body is a silicon-molybdenum rod, a heat-conducting ceramic tube is sleeved outside the silicon-molybdenum rod, the heating rate is 5-10 ℃/min, the chlorine salt can be basically and completely melted and removed within 1 hour, and the maintenance and the overhaul of the fly ash melting electric furnace and supporting facilities and the like are simultaneously carried out in the period.
And the chlorine salt is stacked after being cooled or recovered by a wet method. NaCl, KCl, Pb, Zn, Sn and the like in the fly ash can be recovered by a wet method, wherein the chlorine salt solution can be electrolyzed to produce alkali liquor and chlorine for internal recycling or sale, filter residues produced in the wet method process can be returned to a fly ash melting electric furnace, and no secondary pollutant is discharged after the chlorine salt is treated.
Example 2
The method comprises the steps of collecting fly ash in the waste incineration power generation process, adding the fly ash into a feeding system of a fly ash melting furnace through a screw feeder, wherein the fly ash melting furnace is a bottom blowing furnace, sorting anthracite, fly ash, incineration bottom slag, iron tailings, copper slag and other materials, feeding powder into a powder spraying system, feeding massive materials (larger than 5 mm) into the bottom blowing furnace from the top of the bottom blowing furnace through a belt feeder, continuously feeding the materials into a melting pool of the bottom blowing furnace according to a ratio (ensuring that a slag type with a melting point of 1200-1400 ℃) can be formed, and continuously operating the bottom blowing furnace.
In the process of melting the fly ash, the temperature of a melting pool of the bottom blowing furnace is maintained at about 1400 ℃, the melting pool is stirred violently, the fly ash with high chlorine content is blown into the melting pool from the lower part of the bottom blowing melting pool, and a large amount of chlorine salt in the melting pool is volatilized into flue gas. The flue gas has strong oxidizability, after the flue gas enters the flue 20, the spray gun 21 positioned at the position of the temperature control pipeline sprays compressed air and fuel, the temperature of the flue gas in the flue 20 is ensured to be maintained at about 1200 ℃, and O in the flue 202The concentration is about 2%. Through the flueThe dust-containing flue gas of 20 enters a chlorine salt collecting unit 40 after being subjected to coarse dust removal by a cyclone dust collector, and the coarse dust is sent to a blowing system and then returns to a bottom blowing furnace molten pool.
High chlorine salt flue gas after the dust removal gets into chlorine salt collecting unit 40, and the circular pipeline diameter in entry is 500mm, and flue gas temperature 1200 ℃, chlorine salt collecting unit 40's heat transfer portion 412 is square section of thick bamboo, and the lower part connection is the guide portion 421 and the circular collecting portion 422 of the funnel-shaped of the quadrangular frustum of a pyramid that are convenient for chlorine salt to collect, and heat transfer portion 412 is long 3000mm, and the cross-section is the square that is 1000mm wide, and circular pipeline entry sectional area is 5.10 with heat transfer portion 412 sectional area ratio: 1, the temperature of the outlet position of the chlorine salt collecting unit 40 is about 600 ℃, the cooling medium is steam, the cooling pipeline is made of titanium alloy materials, the cooling structure is a downstream cooling mode as shown in figure 3, more than 80% of chlorine salt is condensed in the chlorine salt collecting unit 40, and the dechlorination flue gas is coarsely dedusted and then is merged into a flue gas purification system for waste incineration power generation. The temperature of the produced high-temperature steam is above 400 ℃, the heat in the high-temperature steam can be recovered through a heat exchanger, and the steam returns to the chlorine salt collecting unit 40 for continuous circulating cooling after being cooled to 110 ℃ and 150 ℃.
The chlorine salt collecting unit 40 is used for one time and is standby for another time, when more chlorine is collected in the chlorine salt collecting unit 40, the cooling effect is poor, the temperature of the outlet position of the chlorine salt collecting unit 40 may exceed 700 ℃, the flue gas pipeline should be switched to the standby chlorine salt collecting unit 40, the front end flue 20 and the rear end flue 20 of the chlorine salt collecting unit 40 which collects more chlorine are closed, and the condensed chlorine salt is removed by using electric heating to increase the temperature and melting. The temperature of the chlorine salt collecting device can be quickly raised from 600 ℃ to about 900 ℃ by electrifying and heating, the chlorine salt is melted and dropped to the lower part to be collected, and a plurality of heating bodies can be arranged at the lower temperature position. The heating body is made of titanium alloy sleeved outside the silicon carbide rod, the heating rate is 5-10 ℃/min, and the chlorine salt can be basically and completely melted and removed within 1 hour.
The removed chlorine salt is molten, the molten salt can be subjected to melting electrolysis after high-temperature impurity removal, a mixture of chlorine and low-melting-point metal is produced, and the product can be recycled in factories or sold for sale.
Example 3
The method comprises the steps of collecting fly ash in the waste incineration power generation process, continuously conveying the fly ash into a blowing system through a scraper, wherein a fly ash melting furnace is a side-blown furnace, feeding blocky materials (larger than 10 mm) such as blocky copper slag, silica and the like into the side-blown furnace from the top of the furnace by using a belt feeder, continuously feeding the materials into a side-blown furnace molten pool according to a ratio (ensuring that a slag type with a melting point of 1200-1400 ℃) can be formed), and continuously operating the fly ash melting furnace. The fly ash and the coal powder are sprayed into the molten pool together, air is used as carrier gas, and oxygen-enriched air and natural gas are respectively sprayed into the channels of the gas path spray gun 21 for combustion and heat supply.
In the process of melting the fly ash, the temperature of a side-blown furnace molten pool is maintained at about 1200 ℃, the molten pool is stirred violently, the fly ash with higher chlorine content is blown into the molten pool from the lower part of the side-blown molten pool, and a large amount of chlorine salt in the molten pool is volatilized into flue gas. The flue gas has strong oxidizability, after the flue gas enters the flue 20, the spray gun 21 positioned at the position of the temperature control pipeline sprays oxygen enrichment and fuel, the temperature of the flue gas in the flue 20 is kept at about 1200 ℃, and O in the flue 202The concentration is about 8%. The dust-containing flue gas passing through the flue 20 enters the chlorine salt collecting unit 40 after coarse dust removal, and coarse smoke dust is sent to the blowing system and then returns to the side-blown furnace molten pool.
The high chloride flue gas after dust removal enters a chloride collecting unit 40, the diameter of a circular pipeline at an inlet is 400mm, the flue gas temperature is 1200 ℃, the chloride collecting unit 40 is a cuboid (a cone with the lower part convenient for chloride collection) with the length of 5000mm and the side length of a square being 1500mm, and the ratio of the inlet sectional area of the circular pipeline to the sectional area of the chloride collecting unit 40 is 17.91: 1, the outlet position temperature of the chlorine salt collection unit 40 is about 650 ℃, the cooling medium is cold air, the cooling pipeline is made of titanium alloy materials, the cooling structure is a counter-flow cooling mode as shown in figure 2, more than 85% of chlorine salt is condensed in the chlorine salt collection unit 40, and the dechlorination flue gas is coarsely dedusted and then is merged into a waste heat recovery system of the waste incineration power generation. The temperature of the hot air generated at the chlorine salt collecting unit 40 is above 500 ℃, the heat in the hot air can be recovered through a heat exchanger, and the cooled cold air returns to the chlorine salt collecting unit 40 for continuous circulating cooling after being cooled to 20-50 ℃.
The chlorine salt collecting unit 40 is used for one time and is standby for another time, when more chlorine is collected in the chlorine salt collecting unit 40, the cooling effect is poor, the temperature of the outlet position of the chlorine salt collecting unit 40 may exceed 700 ℃, the flue gas pipeline should be switched to the standby chlorine salt collecting unit 40, the front end flue 20 and the rear end flue 20 of the chlorine salt collecting unit 40 which collects more chlorine are closed, and the condensed chlorine salt is removed by using electric heating to increase the temperature and melting. The temperature of the position of the chlorine salt collecting unit 40 can be quickly raised from 600 ℃ to about 900 ℃ by electrifying and heating, and the chlorine salt is melted and dropped to the lower part to be collected (a heating body can be arranged at a position with lower temperature). The heating body is a titanium-containing heating body and is made of no protective material, the heating body is inserted into the chlorine salt collecting device when in use, the heating rate is 5-10 ℃/min, chlorine salt can be basically and completely melted and removed within 1 hour, the heating body is pulled out after the chlorine salt is discharged, and the corrosion of flue gas to the heating body for a long time in the condensation process of the chlorine salt can be reduced.
And the chlorine salt is stacked after being cooled or recovered by a wet method. NaCl, KCl, Pb, Zn, Sn and the like in the fly ash can be recovered by a wet method, wherein the chlorine salt solution can be electrolyzed to produce alkali liquor and chlorine for internal recycling or sale, filter residues produced in the wet method process can be returned to fly ash melting and side blowing, and no secondary pollutant is discharged when the chlorine salt is treated.
From the above description, it can be seen that some embodiments of the present invention described above achieve the following technical effects:
(1) the fly ash melting unit at the front end can select various modes such as an electric furnace, a side-blown furnace, a bottom-blown furnace and the like, the matched fly ash melting unit at the front end is flexible and various, and the method and the device have wide application range; the chlorine salt collecting unit and the fly ash melting unit are flexibly matched, can be operated periodically or continuously, can be operated continuously, and can be switched to a standby chlorine salt collecting unit after more chlorine salt exists in the chlorine salt collecting unit, so that the continuous operation process is not influenced, and the operation method is simple and easy to realize;
(2) the treated fly ash does not need pretreatment or the pretreatment method is simple, the treated fly ash can be directly sprayed to a molten pool, and can also be added into a fly ash melting device after pelletizing and agglomeration, the raw material adaptability is strong, and the treated fly ash can be treated for incineration fly ash containing more heavy metals, dioxin, chloride and the like;
(3) when the temperature of a molten pool of the fly ash melting unit is 1200-1400 ℃, the chlorine salt can be almost completely volatilized, and the problems of high chlorine content and high content of volatilized heavy metals after water quenching of the slag are conveniently solved;
(4) when the flue connected with the fly ash melting device is a temperature-controllable flue, one or more spray guns are additionally arranged in the flue, and fuel and air (or oxygen enrichment) are injected into the flue, so that the method is simple, the temperature of the flue gas can be ensured to be stable, the phenomenon that chlorine salt is condensed at the position of the flue to block a pipeline can be prevented, the concentration of oxygen in the flue gas can be controlled to be stable, the complete release of heat can be ensured, and the inhibition of the later-stage dioxin resynthesis is favorable;
(5) when the cross section area of the airflow passing through the chlorine salt collecting unit is controlled to be 5-20 times of the cross section area when the airflow enters the flue, the chlorine salt in the dedusting flue gas in the chlorine salt collecting unit can be ensured to have a good condensation effect; when the cooler is used for cooling the dedusting flue gas, the method and the structure for rapidly cooling the dedusting flue gas are simple and various, a plurality of cooling methods and structures such as a counter-flow type, a downstream type or a parallel type can be adopted, cooling media are various substances such as water, steam, air, nitrogen and the like, the cost is low, the safety is high, a plurality of selection schemes can be provided, and the implementation is easy; the heat of the cooling medium can be recovered, the recovery mode is various, the heat exchange of the cooling medium can be performed by a heat exchanger for power generation, and the heat can also be directly used for generating high-temperature steam or used as a heat source in other areas of a plant area;
(6) the dedusting flue gas is quenched at the chlorine salt collecting unit, and can be rapidly cooled to 500-700 ℃ even from about 1200 ℃, so that the condensation of chlorine salt can be accelerated, and the concentrated collection of the chlorine salt is facilitated;
(7) when the inner wall of the chlorine salt collecting unit is made of materials such as commercial pure titanium and titanium alloy which are resistant to chlorine salt corrosion, the service life of the chlorine salt collecting unit can be prolonged, and the long-term stable operation of the chlorine salt collecting unit can be ensured;
(8) the flue gas after the chlorine salt removal can be directly merged into a waste incineration power generation system, and can also directly enter a subsequent flue gas purification system, the fly ash melting device does not need to additionally establish a flue gas treatment system, the investment is saved, the optimization and the perfection of the current waste incineration power generation system are facilitated, the open-circuit treatment of the chlorine salt and the slag can be realized, and the zero emission of pollutants in waste incineration power generation can be realized;
(9) the condensed chlorine salt removing and collecting mode can be an electric heating mode, so that chlorine salt is rapidly melted at high temperature and falls off, the heating rate is high, the preset temperature can be reached in about 1 hour, the chlorine salt is melted and falls off, a heating body can be additionally arranged at a position which is heated poorly, the molten salt is basically completely melted and falls off, no smoke is generated in the electric heating process, and the chlorine salt melting and separating method is simple, high in efficiency and thorough in separation; when the heater is a silicon-molybdenum rod, a silicon-carbon rod and the like, the heater is a conventional heating body and is low in price; the outside can be sheathed with heat-conducting metal or heat-conducting ceramic for protection, so that the service life is prolonged; the heater can be arranged in the chlorine salt collecting device for a long time, and can also be inserted into the device when the chlorine salt needs to be melted, the method is simple, the using method can be flexibly adjusted according to the actual effect, and the cost can be conveniently reduced by comparing various methods;
(10) the collected chloride salt can be cooled and then discarded; or separating valuable elements in the chlorine salt solution by a wet method after cooling to prepare chlorine salt solution, and further electrolyzing the chlorine salt solution to prepare alkali liquor and chlorine gas which are returned to a factory or sold for sale; and the collected molten salt can be subjected to molten salt electrolysis after impurity removal to obtain alkali metal and chlorine. The secondary waste in the treatment process of the chlorine salt can be returned to the melting furnace, no pollutant is discharged to the outside in the treatment process, the environment is friendly, and the reduction is obvious.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (18)
1. A fly ash treatment system, comprising:
a fly ash melting unit (10) having a fly ash inlet and a dusty flue gas outlet;
the dust removal unit (30) is provided with a dust-containing flue gas inlet and a dust-removing flue gas outlet, and the dust-containing flue gas inlet is communicated with the dust-containing flue gas outlet;
the chlorine salt collecting unit (40) is provided with a dedusting flue gas inlet and a dechlorination flue gas outlet, the dedusting flue gas inlet is communicated with the dedusting flue gas outlet, the chlorine salt collecting unit (40) is provided with a heater (43) and a cooler (44), the cooler (44) cools the dedusting flue gas to enable chlorine salts in the dedusting flue gas to be condensed and attached to the chlorine salt collecting unit (40), and the heater (43) heats the chlorine salts condensed and attached to the chlorine salt collecting unit (40) to enable the chlorine salts to be melted and discharged;
the fly ash treatment system comprises a fly ash treatment system, a dust-containing flue gas inlet, a dust-containing flue gas outlet, a flue (20), a spray gun (21), a fuel supply device and a combustion gas supply device, wherein the fuel supply device and the combustion gas supply device are connected with the spray gun (21), and the combustion gas supply device is a compressed air supply device or an oxygen-enriched air supply device.
2. A fly ash treatment system according to claim 1, wherein the chloride salt collection unit (40) comprises:
the heater (43) and the cooler (44) are detachably arranged in the buffer tank, and the dedusting flue gas inlet and the dechlorination flue gas outlet are arranged on the buffer tank;
and the chlorine salt collector is arranged at the bottom of the buffer tank and is detachably communicated with the buffer tank.
3. A fly ash treatment system according to claim 2, wherein the surge tank comprises:
a divergent part (411), wherein the minimum port of the divergent part (411) is used as the dust removal flue gas inlet;
a heat exchanging part (412), the heat exchanging part (412) having a receiving cavity in which the heater (43) and the cooler (44) are detachably installed, the chlorine salt collector communicating with a bottom of the heat exchanging part (412);
and a smoke exhaust part (413), wherein the heat exchange part (412) is communicated with the smoke exhaust part (413).
4. A fly ash treatment system according to claim 3, wherein the maximum port area of the divergent section (411) is 5-20 times the minimum port area.
5. A fly ash treatment system according to claim 3, wherein the heat exchanging part (412) comprises a side wall having an opening at a lower portion thereof, both ends of the side wall being connected to the diverging part and the smoke discharging part, respectively, the chlorine salt collector comprising:
the flow guide part (421), the flow guide part (421) is a funnel-shaped flow guide part (421), the flow guide part (421) is connected with the side wall, and an upper opening of the flow guide part (421) corresponds to the opening of the side wall;
the collecting part (422) is detachably connected with the lower opening of the flow guide part (421).
6. A fly ash treatment system according to claim 1, wherein the heater (43) is a corrosion resistant heater.
7. A fly ash treatment system according to claim 6, wherein the corrosion resistant heater is a titanium electric heating tube or comprises a heating rod and a corrosion resistant material encasing the heating rod.
8. A fly ash treatment system according to claim 1, wherein the cooler (44) comprises one or more cooling tubes in parallel.
9. A fly ash treatment system according to claim 1, wherein the fly ash melting unit (10) comprises a furnace having the fly ash inlet and the dusty flue gas outlet,
the melting furnace is an electric furnace or a bottom blowing furnace, the fly ash treatment system further comprises a fly ash granulation unit and an ingredient supply unit, the ingredient supply unit is connected with the fly ash granulation unit and used for granulating fly ash and ingredients to form lumps, the fly ash granulation unit is provided with a lump outlet, and the lump outlet is connected with the fly ash inlet;
or the smelting furnace is a side-blown furnace or a bottom-blown furnace, the smelting furnace comprises a material mixing inlet and the fly ash inlet, the fly ash inlet is provided with a powder spraying gun, and the material mixing inlet is arranged at the upper part of the smelting furnace.
10. A fly ash treatment system according to claim 1, wherein the dust removal unit (30) further has a smoke outlet communicating with the fly ash inlet of the fly ash fusion unit (10).
11. A fly ash treatment process, comprising:
carrying out fusion treatment on the fly ash to obtain dust-containing flue gas;
the dust-containing flue gas enters a dust removal unit through a flue, and the dust removal unit is used for carrying out dust removal treatment on the dust-containing flue gas to obtain dust-removing flue gas;
cooling the dedusting flue gas to condense chloride in the dedusting flue gas and attach the chloride to a chloride collecting unit (40), so that the obtained dechlorination flue gas flows out of the chloride collecting unit (40);
heating the condensed and attached chlorine salt in the chlorine salt collecting unit (40) to melt and discharge the chlorine salt,
before the dust-containing flue gas is subjected to dust removal treatment, the fly ash treatment method further comprises the step of spraying fuel and combustion gas into the dust-containing flue gas passing through the flue (20) to perform flue gas combustion, wherein the combustion gas is compressed air or oxygen-enriched air, the temperature of the flue gas combustion is 1000-1200 ℃, and the oxygen gas volume concentration in the flue (20) is controlled to be 1-10%.
12. A fly ash treatment method according to claim 11, wherein the temperature of the dedusting flue gas is reduced to 500-700 ℃ to condense and attach chloride salts in the dedusting flue gas.
13. A fly ash treatment process according to claim 11 or 12, wherein the chlorine salt condensed and adhered in the chlorine salt collecting unit (40) is heated to 900 to 1000 ℃.
14. A fly ash treatment method according to claim 11, wherein the cooling process of the dedusting flue gas comprises:
expanding and cooling the dedusting flue gas;
and cooling the expanded and cooled dedusting flue gas by adopting a concurrent cooling mode, a countercurrent cooling mode or a combined concurrent cooling and countercurrent cooling mode.
15. A fly ash treatment process according to claim 11, wherein the temperature of the melt treatment is 1200 to 1400 ℃.
16. A fly ash treatment process according to claim 11 or 15, wherein the fly ash is subjected to a mixed melting treatment with an ingredient comprising any one or more of coal, quartz sand, iron tailings, copper slag, waste incineration bottom slag.
17. A fly ash treatment process according to claim 11, wherein the fly ash is derived from fly ash produced in a waste incineration process comprising:
an incineration treatment step, wherein incineration flue gas and incineration bottom slag are generated in the incineration treatment step;
recovering the waste heat of the incineration flue gas to obtain cooling flue gas;
and purifying the cooling flue gas to obtain purified flue gas and the fly ash.
18. A fly ash treatment method according to claim 17, wherein the dechlorination flue gas and the incineration flue gas are subjected to waste heat recovery together, or the dechlorination flue gas and the cooling flue gas are mixed and then purified.
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