CN118147435A - Phosphorite shaft furnace roasting production system and method - Google Patents
Phosphorite shaft furnace roasting production system and method Download PDFInfo
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- CN118147435A CN118147435A CN202311037640.5A CN202311037640A CN118147435A CN 118147435 A CN118147435 A CN 118147435A CN 202311037640 A CN202311037640 A CN 202311037640A CN 118147435 A CN118147435 A CN 118147435A
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- 239000002367 phosphate rock Substances 0.000 title claims abstract description 173
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 34
- 239000000843 powder Substances 0.000 claims abstract description 224
- 239000008188 pellet Substances 0.000 claims abstract description 103
- 238000005453 pelletization Methods 0.000 claims abstract description 48
- 238000007599 discharging Methods 0.000 claims description 138
- 238000001816 cooling Methods 0.000 claims description 123
- 230000007246 mechanism Effects 0.000 claims description 118
- 239000000428 dust Substances 0.000 claims description 92
- 238000001035 drying Methods 0.000 claims description 90
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 79
- 239000011707 mineral Substances 0.000 claims description 79
- 239000000463 material Substances 0.000 claims description 66
- 238000000227 grinding Methods 0.000 claims description 65
- 229910052710 silicon Inorganic materials 0.000 claims description 51
- 239000010703 silicon Substances 0.000 claims description 51
- 239000010902 straw Substances 0.000 claims description 49
- 238000002156 mixing Methods 0.000 claims description 45
- 239000002028 Biomass Substances 0.000 claims description 44
- 239000002245 particle Substances 0.000 claims description 41
- 239000001506 calcium phosphate Substances 0.000 claims description 40
- 229910000389 calcium phosphate Inorganic materials 0.000 claims description 40
- 239000011435 rock Substances 0.000 claims description 40
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 33
- 239000003546 flue gas Substances 0.000 claims description 33
- 238000012216 screening Methods 0.000 claims description 32
- 238000003860 storage Methods 0.000 claims description 27
- 239000010802 sludge Substances 0.000 claims description 23
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 20
- 239000011574 phosphorus Substances 0.000 claims description 20
- 229910052698 phosphorus Inorganic materials 0.000 claims description 20
- 238000007873 sieving Methods 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 239000000440 bentonite Substances 0.000 claims description 18
- 229910000278 bentonite Inorganic materials 0.000 claims description 18
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 claims description 18
- 238000002485 combustion reaction Methods 0.000 claims description 18
- 238000009826 distribution Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 15
- 238000004062 sedimentation Methods 0.000 claims description 13
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 12
- 239000011575 calcium Substances 0.000 claims description 11
- 229910052791 calcium Inorganic materials 0.000 claims description 11
- 238000012545 processing Methods 0.000 claims description 11
- 238000007789 sealing Methods 0.000 claims description 8
- 239000000779 smoke Substances 0.000 claims description 8
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 7
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 230000002441 reversible effect Effects 0.000 claims description 7
- 239000004744 fabric Substances 0.000 claims description 6
- 229910052742 iron Inorganic materials 0.000 claims description 5
- 235000014443 Pyrus communis Nutrition 0.000 claims description 4
- 239000005435 mesosphere Substances 0.000 claims description 3
- OBSZRRSYVTXPNB-UHFFFAOYSA-N tetraphosphorus Chemical compound P12P3P1P32 OBSZRRSYVTXPNB-UHFFFAOYSA-N 0.000 abstract description 17
- 239000002994 raw material Substances 0.000 abstract description 15
- 229910019142 PO4 Inorganic materials 0.000 abstract description 6
- 239000010452 phosphate Substances 0.000 abstract description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 abstract description 6
- 238000011161 development Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 61
- 230000008569 process Effects 0.000 description 19
- 239000003517 fume Substances 0.000 description 12
- 239000002956 ash Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- 239000010881 fly ash Substances 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000007596 consolidation process Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000002791 soaking Methods 0.000 description 4
- 239000002912 waste gas Substances 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 240000008042 Zea mays Species 0.000 description 3
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 3
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 3
- DLHONNLASJQAHX-UHFFFAOYSA-N aluminum;potassium;oxygen(2-);silicon(4+) Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[Al+3].[Si+4].[Si+4].[Si+4].[K+] DLHONNLASJQAHX-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000011230 binding agent Substances 0.000 description 3
- 230000009172 bursting Effects 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 235000005822 corn Nutrition 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000005054 agglomeration Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000012620 biological material Substances 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 235000013339 cereals Nutrition 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 238000004952 furnace firing Methods 0.000 description 2
- 238000010409 ironing Methods 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 238000010298 pulverizing process Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 235000014676 Phragmites communis Nutrition 0.000 description 1
- 240000006394 Sorghum bicolor Species 0.000 description 1
- 235000011684 Sorghum saccharatum Nutrition 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 244000098338 Triticum aestivum Species 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 239000003082 abrasive agent Substances 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 229910052656 albite Inorganic materials 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 229910052661 anorthite Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- GWWPLLOVYSCJIO-UHFFFAOYSA-N dialuminum;calcium;disilicate Chemical compound [Al+3].[Al+3].[Ca+2].[O-][Si]([O-])([O-])[O-].[O-][Si]([O-])([O-])[O-] GWWPLLOVYSCJIO-UHFFFAOYSA-N 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052901 montmorillonite Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229940095674 pellet product Drugs 0.000 description 1
- -1 potassium feldspar Chemical compound 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/248—Binding; Briquetting ; Granulating of metal scrap or alloys
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/02—Preparation of phosphorus
- C01B25/027—Preparation of phosphorus of yellow phosphorus
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/16—Sintering; Agglomerating
- C22B1/214—Sintering; Agglomerating in shaft furnaces
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/2406—Binding; Briquetting ; Granulating pelletizing
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/242—Binding; Briquetting ; Granulating with binders
- C22B1/243—Binding; Briquetting ; Granulating with binders inorganic
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/26—Cooling of roasted, sintered, or agglomerated ores
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a phosphorite shaft furnace roasting production system and method. The invention can pretreat low-grade powder ore produced by enterprises in the production process of obtaining natural phosphate lump ore to be used as a pelletizing raw material, and the prepared pellets can be directly used for yellow phosphorus production after being subjected to shaft furnace roasting treatment. On one hand, the invention can effectively utilize the phosphate rock powder ore resources, alleviate the problem of lack of raw materials of yellow phosphorus enterprises, on the other hand, can effectively reduce the cost of raw materials and save land resources, not only accords with national industrial policies and resource development strategy, but also has important significance for yellow phosphorus production in China.
Description
Technical Field
The invention relates to phosphorite production and processing equipment, in particular to a phosphorite shaft furnace roasting production system and method, and belongs to the technical field of phosphorite production and processing.
Background
At present, the technology for preparing yellow phosphorus by using phosphorite mainly comprises an electric furnace method: the natural phosphorite lump ore and the reducing agent are put into an electric furnace to be heated, the reducibility of the reducing agent at high temperature is utilized to enable the phosphorus simple substance to escape in the form of yellow phosphorus steam, and then the yellow phosphorus steam is cooled and collected to obtain the yellow phosphorus. However, the process has higher requirements on phosphorite raw materials and general requirements: the phosphorite charged into the furnace needs to have uniform granularity, low water content and carbonate content, the content of P 2O5 is higher than 20 percent, and certain heat strength is achieved. In order to meet the production needs, yellow phosphorus production enterprises in China mainly use blocky phosphate ores as raw materials.
Although the phosphorite reserves in China are larger, phosphorite resources in China are mainly medium-low grade phosphorite and rich mineral resources are few. According to the related statistical data, the average grade of the phosphorus ore which can be collected in China at present is 23 percent and is lower than the average level of 30 percent worldwide. Wherein, the reserve ratio of the lower-grade phosphorite with the P 2O5 content lower than 20 percent exceeds 60 percent, and the reserve ratio of the high-grade phosphorite with the P 2O5 content higher than 30 percent is less than 10 percent. With the increasing consumption of high-quality phosphorite, the high-quality phosphorite used for yellow phosphorus production is less and less, the supply of natural phosphate lump ore resources is increasingly scarce, and the market price is also increasing. The problem of ore sources in yellow phosphorus production is solved, and the method becomes a key for guaranteeing the normal production of yellow phosphorus enterprises.
Meanwhile, enterprises inevitably generate a large amount of phosphate rock powder in the production process of obtaining natural phosphate rock lump ore, and the high-quality phosphate rock powder cannot be directly used for preparing phosphorus by an electric furnace, so that the high-quality phosphate rock resource is idle, and the resource waste is caused; on the other hand, the phosphate rock powder which cannot be directly used for yellow phosphorus production is piled up in a large amount in a storage yard, so that a large amount of space is occupied, and the waste of land resources is also caused.
Disclosure of Invention
Aiming at the problems of resource waste caused by shortage of phosphate lump ore for yellow phosphorus production and insufficient utilization of high-quality powder ore in the production process of natural phosphate lump ore in the prior art, the invention provides a phosphorite shaft furnace roasting production system and method, which can be used for pretreating low-grade powder ore generated in the production process of obtaining natural phosphate lump ore by enterprises to be used as a pelleting raw material, and the prepared pellets can be directly used for yellow phosphorus production after shaft furnace roasting treatment. The system of the invention can effectively utilize the phosphate rock powder ore resources on one hand, alleviate the problem of lack of raw materials of yellow phosphorus enterprises, and on the other hand, can effectively reduce the cost of raw materials and save land resources, thereby not only conforming to national industrial policies and resource development strategy, but also having important significance for yellow phosphorus production in China.
In order to achieve the technical purpose, the technical scheme adopted by the invention is as follows:
according to a first embodiment of the present invention, there is provided a phosphorite shaft furnace roasting production system:
The system comprises a phosphorite pretreatment unit, an auxiliary material distribution unit, a pelletizing unit, a screening and distributing unit, a shaft furnace roasting unit, a cooling unit and a finished product treatment unit. The phosphorite pretreatment unit and the auxiliary material distribution unit are arranged in parallel, and are sequentially connected in series with the pelletizing unit, the screening and distributing unit, the shaft furnace roasting unit, the cooling unit and the finished product treatment unit according to the trend of materials.
Preferably, the phosphorite pretreatment unit comprises a high-calcium phosphorite powder bin, a high-silicon phosphorite powder bin, a drying device and a grinding device. The mineral powder feeding and conveying mechanism is respectively connected with the feeding end of the high-calcium phosphate rock powder bin and the high-silicon phosphate rock powder bin and is used for conveying the phosphate rock powder conveyed from the outside into the high-calcium phosphate rock powder bin or the high-silicon phosphate rock powder bin for pre-storing. The discharging ends of the high-calcium phosphate rock bin and the high-silicon phosphate rock bin are respectively connected with the drying device, the ore grinding device and the feeding end of the pelletizing unit through the mineral powder discharging and conveying mechanism. The discharging end of the drying device is connected with the feeding end of the ore grinding device through a drying discharging conveying mechanism. The discharge end of the ore grinding device is connected with the feed end of the pelletizing unit through an ore grinding discharge conveying mechanism. Preferably, a discharging vibrating hopper, a disc feeder and a quantitative feeder are respectively and independently arranged between the discharging end of the high-calcium phosphate rock bin and the high-silicon phosphate rock bin and the feeding end of the mineral powder discharging and conveying mechanism.
Preferably, the mineral powder feeding and conveying mechanism, the mineral powder discharging and conveying mechanism, the drying and discharging and conveying mechanism and the grinding and discharging and conveying mechanism independently comprise one or more belt conveyors, and a pear discharger is optionally arranged on each belt conveyor or not.
Preferably, the phosphorite pretreatment unit further comprises a mineral powder temporary storage yard, and the mineral powder temporary storage yard is connected with a discharge end of the mineral powder feeding and conveying mechanism. The temporary mineral powder storage yard is also provided with a grab bucket crane. And conveying the piled mineral powder into the high-calcium phosphate rock powder bin and/or the high-silicon phosphate rock powder bin by a grab crane.
Preferably, the drying device comprises a cylinder dryer, a wet dust collector, a drying fan and a drying exhaust drum. According to the trend of the wind flow, the cylinder dryer, the wet dust collector, the drying induced draft fan and the drying exhaust barrel are connected in series in sequence. The drying material discharging end of the cylinder dryer is connected with the feeding end of the drying discharging conveying mechanism. Preferably, the drying device further comprises a hot blast stove, a sedimentation tank and a sludge drying device. The hot air outlet of the hot air furnace is connected with an air inlet arranged at one side of the dried material discharge end of the cylinder dryer through a hot air pipe. The dust outlet of the wet dust collector is connected with the feed inlet of the sedimentation tank, the sludge outlet of the sedimentation tank is connected with the feed inlet of the sludge drying device, and the sludge outlet of the sludge drying device is connected with the mineral powder temporary storage yard through the dry sludge conveying mechanism.
Preferably, the ore grinding device comprises a roller screen, an ore grinding buffer bin and a high-pressure roller mill which are arranged in series. The feeding end of the roller screen is connected with the discharging ends of the mineral powder discharging and conveying mechanism and the drying discharging and conveying mechanism. The discharge end of the high-pressure roller mill is connected with the feed end of the ore grinding discharge conveying mechanism. Preferably, the discharge end of the ore grinding buffer bin is respectively connected with the feed end of the high-pressure roller mill and the feed end of the ore grinding discharge conveying mechanism through a reversible quantitative feeder. Further preferably, a vibration anti-blocking device is further arranged on the side wall of the discharging end of the ore grinding buffer bin. The roller screen is also provided with an iron remover.
Preferably, the auxiliary material distribution unit comprises a dust bin, a bentonite bin and a biomass straw bin which are arranged in parallel. The discharging ends of the dust bin and the bentonite bin are respectively and independently connected in series with a vibration anti-blocking device, a star-shaped ash discharging valve, a screw feeder and a sealing belt scale in sequence, and the discharging ends of all the sealing belt scales are connected with a mineral powder discharging and conveying mechanism. The discharging end of the biomass straw bin is sequentially connected with a discharging vibrating hopper, a disc feeder and a quantitative feeder in series, and the discharging end of the quantitative feeder is connected with a mineral powder discharging and conveying mechanism.
Preferably, the pelletizing unit comprises a strong mixer, a mixing bin and a disc pelletizer which are sequentially arranged in series. The feeding end of the intensive mixer is connected with the discharging end of the mineral powder discharging and conveying mechanism. The discharge end of the disc pelletizer is connected with the sieving and distributing unit through a green pellet conveying mechanism. A discharging vibrating hopper, a disc feeder and a quantitative feeder are also arranged between the mixing bin and the disc pelletizer in sequence. Preferably, the green ball conveying mechanism comprises one or more belt conveyors.
Preferably, the pelletizing unit comprises a plurality of groups of mixing bins which are arranged in parallel and a disc pelletizer.
Preferably, the screening and distributing unit comprises a roller screening machine and a natural phosphate rock ore bin. The feed end of the roller type screening machine is connected with the discharge end of the green ball conveying mechanism, and the big ball discharge end and the small ball discharge end of the roller type screening machine are connected with the feed end of the mixing bin through the ball return belt type conveyor (the discharge end of the roller type screening machine is generally provided with a crushing roller, so that the big ball and the small ball can be crushed, and the crushed big ball and small ball can directly enter the mixing bin). The middle ball discharging end of the roller type sieving machine is connected with the feeding end of the shaft furnace roasting unit through a raw ball distributing and conveying mechanism. The natural phosphate rock bin is arranged in parallel with the roller screening machine, and the discharging end of the natural phosphate rock bin is connected with the green ball distributing and conveying mechanism through a big inclination angle belt conveyor of the phosphate rock. Preferably, the green ball cloth conveying mechanism comprises one or more belt conveyors.
Preferably, the shaft furnace roasting unit comprises a shuttle distributor, a shaft furnace, an electric vibration feeder and a hot chain plate machine which are sequentially connected in series. The feeding end of the shuttle type distributing device is connected with the discharging end of the green ball distributing and conveying mechanism. The discharging end of the hot chain plate machine is connected with the feeding end of the cooling unit. Preferably, a toothed roll crusher is also arranged between the discharge end of the shaft furnace and the electric vibratory feeder. Preferably, a combustion-supporting fan and a cooling fan are further arranged on one side of the shaft furnace, the combustion-supporting fan is connected with a combustion chamber on the upper portion of the shaft furnace through a combustion-supporting air pipe, and the cooling fan is connected with a cooling chamber on the lower portion of the shaft furnace through a cooling air pipe.
Preferably, the cooling unit is a multi-section belt cooler, and comprises a first section with cooling, a second section with cooling, a third section with cooling, a fourth section with cooling and a fan cover covered above the first section with cooling, the second section with cooling, the third section with cooling and the fourth section with cooling in sequence according to the trend of materials. The feeding end of the cold section is connected with the discharging end of the hot chain plate machine, and the discharging end of the cold four sections is connected with the feeding end of the finished product processing unit.
Preferably, the lower air inlets of the third section with cooling and the fourth section with cooling are respectively connected with a blower through independent blower pipes. The upper air outlet with the cold four sections is connected with the upper air inlet with the cold two sections through a first circulating air pipe, and the lower air outlet with the cold two sections is connected with a combustion-supporting fan of the shaft furnace through a second circulating air pipe. The upper air outlet of the third section with cooling is connected with the upper air inlet of the first section with cooling through a third circulating air pipe, and the lower air outlet of the first section with cooling is connected with the air inlet of the cylinder dryer through a fourth circulating air pipe. Preferably, an exhaust fan is further arranged on the fourth circulating air pipe.
Preferably, the finished product processing unit comprises a finished product sieve, a finished product bin and a powder bin. The feeding end of the finished product sieve is connected with the discharging end with four sections of cooling. The upper screen discharge end of the finished product screen is connected with the feed end of the finished product bin, and the lower screen discharge end of the finished product screen is connected with the feed end of the powder bin. The discharging ends of the finished product bin and the powder bin are respectively provided with an electrohydraulic fan-shaped valve.
Preferably, the product processing unit comprises a plurality of product bins, and the screen discharge end of the product screen is connected with the feed ends of the product bins through an oversize material conveying mechanism. The oversize material conveying mechanism comprises one or more belt conveyors and/or heavy-duty unloading trucks.
Preferably, the shaft furnace roasting unit further comprises a main flue gas dust remover, and a flue gas inlet of the main flue gas dust remover is connected with a top flue gas outlet of the shaft furnace through a flue gas conveying pipeline. The fume outlet of the main fume dust remover is connected with a chimney through a fume exhaust pipeline, and the fume exhaust pipeline is sequentially provided with a main exhaust fan and a desulfurization and denitrification device. The bottom dust outlet of the main flue gas dust remover is connected with the feeding end of the dust bin through a pneumatic conveying bin pump and a pneumatic dust conveying pipeline.
According to a second embodiment of the invention, there is provided a method for the shaft furnace roasting production of phosphorus ore:
a method of shaft roasting production of phosphorus ore or a method of shaft roasting production of phosphorus ore using the system of the first embodiment, the method comprising:
1) Pretreating the phosphate rock powder by a phosphate rock pretreatment unit to obtain high-calcium phosphate rock powder and high-silicon phosphate rock powder; and then mixing the high-calcium phosphate rock powder and the high-silicon phosphate rock powder to obtain mixed mineral powder.
2) Mixing the mixed mineral powder, dust (system collected dust), bentonite and biomass straw particles in proportion to obtain a pelleting mixture (the average particle size is not more than 5mm, preferably not more than 4 mm).
3) Adding the pelletizing mixture into a pelletizer for pelletizing, and sieving the obtained green pellets to obtain big pellets, seed pellets and small pellets; wherein, after the big ball and the small ball are crushed, the mixture returns to the step 2) to participate in the mixing; the middle ball enters the next working procedure.
4) And 3) conveying the medium balls obtained in the step 3) into a shaft furnace for roasting treatment, and conveying the roasted finished pellets to a finished product warehouse for storage after cooling by a belt cooler and sieving by a sieving machine.
Preferably, in the step 1), the high-calcium phosphate rock powder is phosphate rock powder with the P 2O5 content not more than 15wt%, the CaO content not less than 40wt% and the water content of 6-10%. Preferably, the phosphorus ore powder contains 10-15wt% of P 2O5, 45-55wt% of CaO and 8-9% of water.
Preferably, in the step 1), the high-silicon phosphate rock powder is phosphate rock powder with the P 2O5 content not more than 15wt%, the SiO 2 content not less than 40wt% and the water content of 6-10%; preferably, the phosphorus ore powder contains 10-15wt% of P 2O5, 45-55wt% of SiO 2 and 8-9% of water.
Preferably, in step 1), the mixing mass ratio of the high-calcium phosphate rock powder to the high-silicon phosphate rock powder is 1.2-1.6:1, preferably 1.3-1.45:1. The average particle size of the mixed mineral powder is not more than 0.15mm, preferably not more than 0.125mm.
Preferably, in the step 2), the mixing mass ratio of the mixed mineral powder, the dust, the bentonite and the biomass straw particles is 92-98:3-8:1-5:0.5-2 (preferably 94-97:4-7:2-4:1-1.5). Preferably, the biomass straw particles are modified biomass straw particles modified by adopting calcium hydroxide solution.
Preferably, in step 3), the mesosphere has a particle size of 5-20mm, preferably 8-16mm; the pellets with the particle size larger than the middle balls are large balls, and the pellets with the particle size smaller than the middle balls are small balls.
Preferably, in step 4), the temperature of calcination is 1100-1300 ℃, preferably 1150-1250 ℃, and the time of calcination treatment is 1-10 hours, preferably 2-8 hours; the particle size of the pellets conveyed to the finished product bin after sieving is not less than 5mm, preferably not less than 7mm.
In the invention, the phosphorite powder is separated into high-calcium phosphorite powder and high-silicon phosphorite powder by a phosphorite pretreatment unit, and the high-calcium phosphorite powder and the high-silicon phosphorite powder are respectively stored and distributed separately. In the pretreatment process, the high-calcium phosphate rock powder and the high-silicon phosphate rock powder are selectively subjected to or not subjected to drying treatment according to the respective water content. The drying treatment is generally carried out in a cylinder dryer, and the drying hot air from a hot air furnace and/or a subsequent cooling stage is subjected to countercurrent contact heat exchange with the materials in the cylinder dryer, and the water content of the dried high-calcium phosphate rock powder and high-silicon phosphate rock powder is controlled to be 6-10% (preferably 8-9%) in general. Further, high-pressure roll grinding treatment can be selectively carried out on the high-calcium phosphate rock powder and the high-silicon phosphate rock powder according to the size of the original phosphate rock powder particle size, so that the phosphate rock fine powder with the average particle size not more than 0.15mm (preferably not more than 0.125 mm) is obtained as a pelletizing raw material. And after the dried hot air is dedusted by a deduster, clean flue gas is discharged outside by an induced draft fan and an exhaust funnel, and the collected dedusting ash is transported to a phosphorite powder temporary storage yard by an automobile. The hot air for drying mainly comes from a section with cooling, when the temperature is insufficient, the hot air furnace supplements heat, the hot air furnace adopts blast furnace gas as fuel, and hot flue gas at 750-900 ℃ is generated in the hot air furnace for drying by a cylinder dryer.
In the invention, the chemical components of the high-calcium phosphate rock powder are generally as follows: 10-15% of P 2O5, 10-15% of SiO 2, 40-55% of CaO, 0.5-1% of Fe 2O3, 3-5% of Al 2O3, 1-2% of MgO, 0.1-0.3% of F and 0.5-0.8% of S. The high-silicon phosphate rock powder generally comprises the following chemical components: 10-15% of P 2O5, 40-55% of SiO 2, 20-25% of CaO, 0.5-1% of Fe 2O3, 3-5% of Al 2O3, 1-2% of MgO, 0.1-0.3% of F and 0.5-0.8% of S.
In order to protect the safe operation of the high-pressure roller mill, the phosphorite powder is provided with an iron removing device and a sundry sieve before entering the roller press, the iron removing blocks and large-size sundries are sieved and fall into a buffer bin, the high-pressure roller mill is fed by a reversible quantitative feeder below the buffer bin, and the phosphorite powder enters a mineral powder discharging and conveying mechanism after being subjected to high-pressure roller mill. The high-pressure roller grinding process is provided with a bypass, and when the granularity of the raw materials is very fine and high-pressure roller grinding is not needed, the raw materials can directly enter the mineral powder discharging and conveying mechanism through the bypass by a reversible quantitative feeder.
In the invention, a temporary storage yard for mineral powder is also arranged, and the rock phosphate powder with high calcium content and the rock phosphate powder with high silicon content can be transported to the temporary storage yard for the rock phosphate powder with high calcium and high silicon by an automobile from the outside. And stacking high-calcium and high-silicon phosphate rock powder in the temporary storage yard by utilizing the grab crane, and grabbing the phosphate rock powder to a phosphate rock powder bin by utilizing the grab crane. Different types of phosphate rock powder are in a phosphate rock powder bin, a vibrating hopper under the phosphate rock powder bin supplies the phosphate rock powder to a powder ore disc feeder, then the phosphate rock powder is supplied to a powder ore quantitative feeder, materials are automatically proportioned, each phosphate rock powder bin is provided with a level gauge, accurate proportioning is realized by stabilizing discharge amount, and the whole proportioning process is automatically controlled by a computer according to manually set proportioning. If the granularity of the materials in the current batch is very fine and the moisture content is very low, drying treatment is not needed; if the granularity of the material in the current batch is coarse and the moisture content is low, directly performing roller grinding treatment after passing through drying; if the particle size of the material in the current batch is high in moisture content, the material is required to be dried in a cylinder dryer, and whether the roller grinding treatment is carried out on the dried material is judged according to the particle size of the dried material.
In the invention, the phosphorite with high calcium content and the phosphorite with high silicon content are mixed for high-pressure roller grinding, and after the phosphorite is rolled by the high-pressure roller grinding machine, the specific surface area of mineral powder is larger, which is beneficial to pelleting and also improves the pelleting strength. The high-silicon phosphorite has low hardness, is easy to roll grind, has poor hydrophilicity after fine grinding, has low static balling index and has weak balling; high calcium type hardness, difficult grinding, good hydrophilicity after fine grinding, high static balling index and good balling property. The specific surface area of the mineral powder after the mixing roller grinding is generally more than 2200cm 2/g, and the balling index is greatly improved. The high-calcium phosphate rock powder with high hardness and the high-silicon phosphate rock powder with low hardness are matched, and materials are used as abrasive materials in the roll grinding process, so that the energy consumption of roll grinding is reduced; meanwhile, the acidity can be well regulated, so that the acidity of the pellets obtained after pelletizing is more than 0.95, and the addition amount of flux in the subsequent electric furnace phosphorus production can be further reduced.
In the invention, the dust collected in the general electric furnace phosphorus production process has fine particle size and weaker cohesiveness, and cannot be directly used for pelletization and pelletization, and is difficult to recycle, so the invention collects dust through a dust pneumatic mechanism and conveys the dust to a dust bin to participate in the proportioning of the pelletization raw material to serve as pelletization auxiliary material, and the dust has certain cohesiveness, so that the agglomeration performance of the phosphorus ore powder can be improved to a certain extent, the dust ash contains higher content of P 2O5, the grade of the green pellets can be further improved by adding dust in the phosphorus ore powder, no loss is caused in the roasting process, and experiments show that the P 2O5 content of the phosphorus ore pellets can be improved by at least 1% by using the dust ash. Furthermore, the invention can also adopt aluminosilicate (such as potassium feldspar, albite, anorthite, montmorillonite and zeolite) to carry out modification treatment on the dust, thereby increasing the cohesiveness of the dust, improving the strength of the pellets after pelletizing and greatly reducing the dosage of additional binder.
In the invention, the bentonite bin is also arranged, bentonite is used as one of pelletizing auxiliary materials, the defect of poor cohesiveness of the fly ash can be greatly overcome, the dosage of the fly ash is further increased, the pellet grade is improved, and the problem of reduced cohesive strength of the pelletizing pellets is avoided.
In the invention, a biomass straw bin (the biomass straw comprises but is not limited to rice straw, sorghum straw, corn straw, reed straw, wheat straw and the like), the biomass straw is used as one of pelletizing auxiliary materials, the biomass straw is distributed in the green pellets, a diffusion channel can be provided for moisture in the green pellets, the escape speed of internal water vapor is greatly improved, the phenomenon that a large number of pellets burst during high-temperature roasting is avoided, and meanwhile, the adhesive force among rock phosphate particles can be improved by the fibers of the biomass straw, and the strength of a biological block can be improved; in addition, the biomass straw in the biological material block can provide partial heat in the subsequent roasting, which is helpful for the high-temperature consolidation of the biological material block and further improves the physical strength and chemical performance.
Further, in order to further improve the strength of the green pellets, the biomass straw is subjected to pretreatment before mixing, specifically, the biomass straw particles are soaked in a calcium hydroxide solution (for example, 0.01-1 mol/L) for 0.1-5 hours, the soaked biomass straw particles are subjected to draining treatment, and then the biomass straw particles participate in the mixing. Because the biomass straw is adsorbed with calcium hydroxide, the binding performance between the biomass straw and other materials can be improved in the process of batching, the strength of the green pellets is improved, and the crushing rate of the biomass straw in the process of carrying is greatly reduced; simultaneously, in the subsequent heat treatment process, the biomass straw can be heated and decomposed to release carbon dioxide and water. The released carbon dioxide and the calcium hydroxide in the interior under the action of the water vapor form a compound with a consolidation effect (the adsorbed calcium hydroxide is internally consolidated into calcium carbonate), so that the bonding strength between biomass straw and other raw materials can be further improved, the high-temperature bursting is prevented, the strength of the finished phosphorite pellets is greatly ensured and improved, and the powder ore rate is reduced. It should be noted that, the addition of biomass straw is not too high or too low, the addition is too high, which can lead to the reduction of the ratio of phosphate rock powder to dust, and the yield is reduced, and at the same time, too many straw particles form more macropores in the finished product phosphate rock pellets after heat treatment, which is easy to lead to collapse and pulverization of the finished product phosphate rock pellets, but is not beneficial to improving the strength of the finished product phosphate rock pellets; if the addition amount is too low, the bonding strength inside the green pellets is not improved, and the green pellets are easily broken up greatly before heat treatment.
In the invention, all materials are automatically mixed, each mixing tank is provided with a material level meter to stabilize the discharge amount and realize accurate mixing, and the whole mixing process is automatically controlled by a computer according to the manually set mixing ratio. After the ingredients are mixed, the pelleting mixture is mixed and pelletized by adopting a powerful mixer, so that the pelleting effect can be improved, the particle size distribution of the granules is better, and the strength of the pellets is better. By adopting a strong mixer, the trace binder can be fully and uniformly mixed with the ground phosphate rock, the uniformity of the mixture is improved, the consumption of the binder is reduced, the green ball strength is enhanced, the ball returning amount is reduced, and the green ball quality is stabilized. The pelletizing purpose is to make the mixture into green pellets meeting the granularity requirement of the final pellet product, and make the green pellets have enough mechanical strength to meet the requirement of the next process. Pelletizing is an important link in the pellet process, and the quality of green pellets directly influences the normal operation of the pellet roasting production process and the quality of finished pellets.
In the invention, the green pellets are formed into finished pellets which are subjected to transfer and high-temperature heat treatment, wherein collision and extrusion between the pellets inevitably occur in the process of carrying and distributing, and the roasting temperature is higher than 1100 ℃, so that the green pellets are required to have certain strength, and the conditions of massive collision and crushing in the transfer process and massive bursting in the heat treatment process are avoided. Therefore, when the biomass pellet is prepared, the biomass straws are uniformly distributed in the biomass pellet by adding the biomass straws, a diffusion channel is provided for internal moisture during drying, the escape speed of internal steam is greatly improved, and bursting of the biomass pellet caused by rapid evaporation of water molecules at high temperature can be effectively prevented. Meanwhile, the bonding force among the phosphorite powder particles can be improved by the biomass straw fibers in the green pellets, and the strength of the green pellets can be improved. In addition, the biomass straw in the green pellets can also provide partial heat in the subsequent roasting, which is helpful for the high-temperature consolidation of the green pellets and further improves the physical strength and chemical properties of the finished pellets.
In the invention, the materials subjected to strong mixing and unqualified raw balls are respectively discharged to each mixing bin by a conveyor, and a wear-resistant ceramic lining plate with the thickness of 20mm is paved in each mixing bin. The pelletizing equipment adopts a disc pelletizer, the pelletizer adopts variable frequency speed regulation, the residence time of materials in the disc can be regulated by changing the inclination angle and the rotation speed of the disc, the disc pelletizer adopts a mode of fixing a scraper, and the mixture rolls and grows up to form balls under the proper moisture condition in the pelletizer. Due to the action of centrifugal force, green balls reaching a certain granularity automatically overflow the disc surface and fall onto the green ball conveying mechanism in a concentrated manner to be sent to the screening and distributing unit. The green pellets are screened by a roller screening machine, the classification points are 8mm and 16mm, and the green pellets are returned to a pelletizing mixing bin through a pelletizing return belt conveyor, wherein the classification points are 8mm and 16 mm. Qualified green pellets of 8-16 mm are conveyed to a shuttle type distributing device through a green pellet distributing and conveying mechanism and uniformly distributed on a drying bed at the top of the shaft furnace through the shuttle type distributing device.
In the invention, a shuttle type material distributor of the shaft furnace is connected with a balling machine and a natural phosphate rock ore bin, and the natural phosphate rock ore bin is connected with a raw ball material distributing and conveying mechanism through a large inclination angle belt conveyor of the phosphate rock ore. When the shaft furnace is opened, the natural phosphate rock ore can be sent to the shaft furnace, or the natural phosphate rock ore and the raw pellet ore alternately enter the shaft furnace. The shaft furnace adopts countercurrent heat exchange, raw pellets are filled into the furnace from the furnace top through a shuttle distributor, and because of uniform discharging of the discharging equipment, the raw pellets move to the bottom at a uniform speed in the furnace, hot flue gas of the combustion chamber enters the furnace from a fire-spraying port, and the hot flue gas exchanges heat with the raw pellets from bottom to top. The green pellets are dried and preheated from top to bottom, then enter a roasting and heat-transfer area for high-temperature consolidation reaction, then are cooled to below 600 ℃ through the lower part of the shaft furnace, and then are discharged. The most important of the whole process is to ensure the air flow distribution of the furnace burden so as to achieve good air permeability and roasting uniformity. The qualified green pellets are graded by a roller screen and distributed on a green pellet drying bed in a furnace through a shuttle distributor, the thickness of the material layer is generally 150-200 mm, and the thickness of the material layer can be regulated according to the temperature of waste gas under a drying grate and the furnace condition. The ridge-shaped drying bed (the drying bed is a triangular roof) is adopted, the top included angle is 100-110 degrees, hot flue gas rising from the preheating belt and hot flue gas coming out from the air guide wall are mixed under the drying bed, and the mixed gas and the moved green pellets are subjected to heat exchange to achieve the drying purpose. The green pellets are dried for 5-6 min in the drying bed, then the drying process is basically completed, the green pellets reach the furnace throat and enter the preheating zone. The green pellets are preheated and then lowered to a roasting section of the shaft furnace at a roasting temperature of 1100-1300 ℃ (preferably 1150-1250 ℃). The shaft furnace supplies heat to high-temperature flue gas from round horizontal combustion chambers at two sides of the shaft furnace, and the temperature of the combustion chambers is regulated by controlling the gas flow and the air flow of the burner, so that stable roasting temperature is ensured. The hot air with the cold two sections is sent into the combustion chamber by the combustion-supporting fan to be used as combustion-supporting air, so that the combustible gas is fully combusted at high temperature, and flue gas with higher temperature is generated. The pellets move downwards from the shaft furnace roasting belt to enter the soaking belt, and most cooling air passes through the air guide wall due to the arrangement of the air guide wall, and a small amount of cooling air provides oxygen to ensure the oxidation atmosphere of the soaking section. The phosphorite grains in the homothermal belt pellets further grow up, the crystal form transformation is continued, the pellets further shrink and densify, the lattice structure is further perfected, and the strength of the pellets is improved. Meanwhile, the pellets which are not roasted in the roasting section can be roasted in the soaking section, and the soaking section is actually a continuation of the roasting section. Cooling air blown from two sides of the lower part of the shaft furnace exchanges heat with the high-temperature pellets through a cooling chamber to primarily cool the pellets, and the temperature after cooling is 300-600 ℃. After the cooling air is changed into hot smoke, most of the hot smoke rises along the air guide wall with small resistance to be converged with the smoke of the roasting section, and the hot smoke reaches the lower part of the green pellet drying bed to be used as hot air for drying the green pellets. The hydraulic transmission toothed roller discharger arranged at the lower part of the shaft furnace supports the whole material column and has the double functions of crushing (preventing caking) and discharging. The toothed roller is provided with a hydraulic station matched with the toothed roller, and the pellets are continuously and uniformly discharged out of the furnace by an electric vibration feeder after passing through a toothed roller unloader and are unloaded into a hot chain plate conveyor. When the combustion-supporting fan fails, part of air can be switched by the cooling fan through the air pipe to the combustion chamber. The temperature of low-temperature dust-containing waste gas discharged from the top of the shaft furnace is 110-150 ℃, and the low-temperature dust-containing waste gas enters a desulfurization and denitration device through a main exhaust fan after being dedusted by a main electric precipitator and is discharged outside through a chimney. The dust-removing ash discharged from the ash hopper of the electric dust remover is sent to the dust bin for recycling through a pneumatic conveying pipeline by a pneumatic conveying bin pump.
In the invention, the cooling unit is a multi-section belt cooler and sequentially comprises a first section with cooling, a second section with cooling, a third section with cooling, a fourth section with cooling and a fan cover covered above the first section with cooling, the second section with cooling, the third section with cooling and the fourth section with cooling according to the trend of materials. The pellets are transported and discharged to a belt cooler for cooling by a chain plate machine, the temperature after cooling is less than 120 ℃, and air is blown into the belt cooler by a cooling air blower below the belt cooler four sections for cooling, and air is blown into the belt cooler three sections by the cooling air blower below the belt cooler three sections for cooling. The air with the cold four sections is pumped into the second section for cooling, the air with the cold two sections is pumped into the first section for cooling, the air with the cold two sections is sent to the combustion chamber of the shaft furnace for combustion supporting, and the air with the cold one section is sent to the drying cylinder for drying mineral powder. The hot air generated during cooling is recycled to supply heat for raw material drying and a combustion chamber of the shaft furnace, and the waste heat of the system is fully recovered through cascade utilization, and the utilized waste gas is discharged after dust removal, desulfurization and denitrification, so that the heating energy consumption is greatly reduced, and the environmental protection benefit is increased.
In the invention, cooled pellets are conveyed to a finished product screening system through a belt conveyor, and bulk materials with a cooler and dust collection of a bellows are collected through a scraper machine and conveyed to the finished product screening system together with the pellets with the cooler. And screening the cooled pellets by adopting a cantilever screen bar screen, and screening out the grain fraction less than 5 mm. The undersize reject balls are stored in a powder bin, and a discharge valve is arranged at the bottom of the powder bin for being transported to a phosphorite powder temporary storage yard from outside the automobile. And conveying the qualified finished products on the screen to a finished product ore bin for storage through a belt conveyor. And an electro-hydraulic sector valve is arranged below the finished product bin for discharging. The bottom of one finished ore bin is provided with an automobile for being transported to an electric furnace, and the rest finished ore bins are transported to the electric furnace through a belt conveyor.
In the invention, various powder materials and dust generated in the process are recycled, thereby realizing the recycling of valuable resources and simultaneously avoiding direct external pollution discharge.
Compared with the prior art, the beneficial technical effects of the invention are as follows:
1: the invention couples and utilizes the high-calcium phosphate rock powder and the high-silicon phosphate rock powder which cannot be reused in the existing phosphate rock processing, solves the problem of resource waste caused by the fact that a large amount of piled phosphate rock powder cannot be reused in the existing phosphate rock processing, and the problem of land resource waste caused by the fact that a large amount of piled phosphate rock powder is piled, realizes the recycling and high-efficiency reuse of the phosphate rock powder, and also greatly saves land resources.
2: The invention greatly improves the agglomeration performance of the dust by compounding the dust and bentonite or modifying the dust, and simultaneously further improves the strength of the raw material block by bridging biomass straws, effectively ensures the quality of the finished product block mineral products, can accommodate more dust and improves the utilization efficiency of the dust.
3: According to the invention, biomass straws are added in the mixing granulation process, and the strength of the green pellets is further improved through bridging of the biomass straws, so that burst loss of the pellets in the heat treatment process can be greatly reduced, the quality and yield of finished pellet products are effectively ensured, the liquid is favorable for containing more bulk materials and powder, the resource recovery efficiency is improved, and the environmental pollution is reduced.
4: The particle size distribution of the finished pellets prepared by the invention is centralized and stable, the air permeability is good, the pulverization rate is low in the high-temperature reducing atmosphere for preparing yellow phosphorus later, and the dust content for preparing phosphorus can be greatly reduced. The lump ore has high grade, good chemical components, high strength, convenient subsequent transportation, strong portability, low water content and low carbonate content, can effectively reduce the power consumption of the subsequent lump ore for preparing phosphorus, improves the purity of the phosphorus, and further improves the economic benefit.
Drawings
FIG. 1 is a schematic diagram of the overall structure of the system according to the present invention.
Reference numerals: 1: a high-calcium phosphate rock powder bin; 2: a high-silicon phosphorite powder bin; 3: a drying device; 301: a cylinder dryer; 302: a wet dust collector; 303: a drying fan; 304: drying exhaust pipe; 305: hot blast stove; 306: a sedimentation tank; 307: a sludge drying device; 308: a dry mud conveying mechanism; 4: a grinding device; 401: a roller screen; 402: grinding and buffering bin; 403: high-pressure roller mill; 404: a reversible dosing machine; 405: an iron remover; 5: a temporary storage yard for mineral powder; 501: grab bucket cranes; 6: a dust bin; 7: a bentonite bin; 8: a biomass straw bin; 9: a powerful mixer; 10: a mixing bin; 11: a disc pelletizer; 12: a roller screen; 1201: a ball return belt conveyor; 13: a natural phosphate rock ore bin; 1301: lump ore large-inclination-angle belt conveyor; 14: shuttle type distributing device; 15: a shaft furnace; 16: an electric vibration feeder; 17: a hot chain plate machine; 18: a toothed roller crusher; 19: cooling the belt for one section; 20: a second section with cooling; 21: three sections with cooling; 22: four sections with cooling; 23: a fan housing; 24: a first circulation duct; 25: a second circulation duct; 26: a third circulating air duct; 27: a fourth circulating air duct; 28: a finished product screen; 29: a finished product bin; 30: a powder bin; 31: a main flue gas dust remover; 32: a main exhaust fan; 33: a desulfurization and denitrification device; 34: a chimney; 35: pneumatic conveying bin pump; 36: pneumatic dust conveying pipeline; a: mineral powder feeding and conveying mechanism; b: mineral powder discharging and conveying mechanism; c: a drying discharging conveying mechanism; d: grinding, discharging and conveying mechanism; e: a green ball conveying mechanism; f: raw ball cloth conveying mechanism; g: and a conveying mechanism for the oversize materials.
Detailed Description
The following examples illustrate the technical aspects of the invention, and the scope of the invention claimed includes but is not limited to the following examples.
The system comprises a phosphorite pretreatment unit, an auxiliary material distribution unit, a pelletizing unit, a screening and distributing unit, a shaft furnace roasting unit, a cooling unit and a finished product treatment unit. The phosphorite pretreatment unit and the auxiliary material distribution unit are arranged in parallel, and are sequentially connected in series with the pelletizing unit, the screening and distributing unit, the shaft furnace roasting unit, the cooling unit and the finished product treatment unit according to the trend of materials.
Preferably, the phosphorite pretreatment unit comprises a high-calcium phosphorite powder bin 1, a high-silicon phosphorite powder bin 2, a drying device 3 and a grinding device 4. The mineral powder feeding and conveying mechanism A is respectively connected with the feeding ends of the high-calcium phosphate rock powder bin 1 and the high-silicon phosphate rock powder bin 2 and is used for conveying the phosphate rock powder conveyed from the outside into the high-calcium phosphate rock powder bin 1 or the high-silicon phosphate rock powder bin 2 for pre-storing. The discharging ends of the high-calcium phosphate rock bin 1 and the high-silicon phosphate rock bin 2 are respectively connected with the feeding ends of the drying device 3, the ore grinding device 4 and the pelletizing unit through the mineral powder discharging and conveying mechanism B. The discharging end of the drying device 3 is connected with the feeding end of the grinding device 4 through a drying discharging conveying mechanism C. The discharge end of the ore grinding device 4 is connected with the feed end of the pelletizing unit through an ore grinding discharge conveying mechanism D. Preferably, a discharging vibrating hopper, a disc feeder and a quantitative feeder are respectively and independently arranged between the discharging ends of the high-calcium phosphate rock bin 1 and the high-silicon phosphate rock bin 2 and the feeding end of the mineral powder discharging conveying mechanism.
Preferably, the mineral powder feeding and conveying mechanism A, the mineral powder discharging and conveying mechanism B, the drying and discharging and conveying mechanism C and the grinding and discharging and conveying mechanism D respectively and independently comprise one or more belt conveyors, and a pear discharger is optionally arranged on each belt conveyor or not.
Preferably, the phosphorite pretreatment unit further comprises a mineral powder temporary storage yard 5, and the mineral powder temporary storage yard 5 is connected with the discharge end of the mineral powder feeding and conveying mechanism A. A grab crane 501 is also arranged on the temporary storage yard 5. The piled mineral powder is transported into the high-calcium phosphate rock bin 1 and/or the high-silicon phosphate rock bin 2 by the grab crane 501.
Preferably, the drying device 3 includes a drum dryer 301, a wet dust collector 302, a drying fan 303, and a drying exhaust drum 304. According to the trend of the wind flow, the cylinder dryer 301, the wet dust collector 302, the drying induced draft fan 303 and the drying exhaust drum 304 are connected in series in sequence. The dry material discharge end of the cylinder dryer 301 is connected to the feed end of the dry material discharge conveyor C. Preferably, the drying device 3 further comprises a hot blast stove 305, a sedimentation tank 306 and a sludge drying device 307. The hot air outlet of the hot air furnace 305 is connected with an air inlet arranged at one side of the dried material discharge end of the cylinder dryer 301 through a hot air pipe. The dust outlet of the wet dust collector 302 is connected with the feed inlet of the sedimentation tank 306, the sludge outlet of the sedimentation tank 306 is connected with the feed inlet of the sludge drying device 307, and the discharge outlet of the sludge drying device 307 is connected with the mineral powder temporary storage yard 5 through the dry sludge conveying mechanism 308.
Preferably, the ore grinding device 4 comprises a roller screen 401, an ore grinding surge bin 402 and a high-pressure roller mill 403 which are arranged in series. The feeding end of the roller screen 401 is connected with the discharging ends of the mineral powder discharging and conveying mechanism B and the drying discharging and conveying mechanism C. The discharge end of the high-pressure roller mill 403 is connected with the feed end of the ore grinding discharge conveying mechanism D. Preferably, the discharge end of the grinding surge bin 402 is connected to the feed end of the high pressure roller mill 403 and to the feed end of the grinding discharge conveyor D, respectively, by a reversible dosing machine 404. Further preferably, a vibration anti-blocking device is also provided on the side wall of the discharge end of the grinding surge bin 402. The roller screen 401 is also provided with a de-ironing separator 405.
Preferably, the auxiliary material distribution unit comprises a dust bin 6, a bentonite bin 7 and a biomass straw bin 8 which are arranged in parallel. The discharging ends of the dust bin 6 and the bentonite bin 7 are respectively and independently connected in series with a vibration anti-blocking device, a star-shaped ash discharging valve, a screw feeder and a sealing belt scale in sequence, and the discharging ends of all the sealing belt scales are connected with a mineral powder discharging and conveying mechanism B. The discharging end of the biomass straw bin 8 is sequentially connected with a discharging vibrating hopper, a disc feeder and a quantitative feeder in series, and the discharging end of the quantitative feeder is connected with a mineral powder discharging and conveying mechanism B.
Preferably, the pelletizing unit comprises a intensive mixer 9, a mixing bunker 10 and a disc pelletizer 11 which are sequentially arranged in series. The feeding end of the intensive mixer 9 is connected with the discharging end of the mineral powder discharging and conveying mechanism B. The discharge end of the disc pelletizer 11 is connected with a sieving and distributing unit through a green ball conveying mechanism E. A discharging vibrating hopper, a disc feeder and a quantitative feeder are also arranged between the mixing bin 10 and the disc pelletizer 11 in sequence. Preferably, the green ball conveying mechanism E comprises one or more belt conveyors.
Preferably, the pelletizing unit comprises a plurality of groups of mixing bins 10 which are arranged in parallel and a disc pelletizer 11.
Preferably, the sieving and distributing unit comprises a roller sieving machine 12 and a natural phosphate rock ore bin 13. The feed end of the roller screen 12 is connected with the discharge end of the green ball conveying mechanism E, and the big ball discharge end and the small ball discharge end of the roller screen 12 are connected with the feed end of the mixing bin 10 through the ball return belt conveyor 1201. The middle ball discharge end of the roller screen 12 is connected with the feed end of the shaft furnace roasting unit through a raw ball distributing and conveying mechanism F. The natural phosphate rock bin 13 is arranged in parallel with the roller screening machine 12, and the discharge end of the natural phosphate rock bin 13 is connected with the green ball distributing and conveying mechanism F through a large inclination angle belt conveyor 1301 of the phosphate rock. Preferably, the green ball cloth conveying mechanism F comprises one or more belt conveyors.
Preferably, the shaft furnace roasting unit comprises a shuttle distributor 14, a shaft furnace 15, an electric vibration feeder 16 and a hot chain scraper 17 which are arranged in series in sequence. The feeding end of the shuttle distributor 14 is connected with the discharging end of the green ball distributing and conveying mechanism F. The discharge end of the hot chain scraper 17 is connected with the feed end of the cooling unit. Preferably, a toothed roll crusher 18 is also provided between the discharge end of the shaft furnace 15 and the electric vibratory feeder 16. Preferably, a combustion fan and a cooling fan are further arranged on one side of the shaft furnace 15, the combustion fan is connected with a combustion chamber on the upper portion of the shaft furnace 15 through a combustion air pipe, and the cooling fan is connected with a cooling chamber on the lower portion of the shaft furnace 15 through a cooling air pipe.
Preferably, the cooling unit is a multi-stage belt cooler, and sequentially comprises a first belt cooling section 19, a second belt cooling section 20, a third belt cooling section 21, a fourth belt cooling section 22 and a fan cover 23 covered above the first belt cooling section and the second belt cooling section according to the trend of materials. The feeding end of the first section 19 with cooling is connected with the discharging end of the hot chain scraper 17, and the discharging end of the fourth section 22 with cooling is connected with the feeding end of the finished product processing unit.
Preferably, the lower air inlets of the third section 21 and the fourth section 22 are respectively connected with a blower through independent blower pipes. The upper air outlet of the four sections with cooling 22 is connected with the upper air inlet of the two sections with cooling 20 through a first circulating air pipe 24, and the lower air outlet of the two sections with cooling 20 is connected with a combustion-supporting fan of the shaft furnace 15 through a second circulating air pipe 25. The upper air outlet of the third section 21 with cooling is connected with the upper air inlet of the first section 19 with cooling through a third circulating air pipe 26, and the lower air outlet of the first section 19 with cooling is connected with the air inlet of the cylinder dryer 301 through a fourth circulating air pipe 27. Preferably, an exhaust fan is further provided on the fourth circulation duct 27.
Preferably, the product handling unit includes a product screen 28, a product bin 29, and a powder bin 30. The feed end of the product screen 28 is connected to the discharge end of the four sections 22. The on-screen discharge end of the product screen 28 is connected to the feed end of the product bin 29 and the under-screen discharge end of the product screen 28 is connected to the feed end of the powder bin 30. The discharge ends of the finished product bin 29 and the powder bin 30 are respectively provided with an electrohydraulic fan valve.
Preferably, the product processing unit includes a plurality of product bins 29, and the on-screen discharge end of the product screen 28 is connected to the feed ends of the plurality of product bins 29 by an on-screen material conveying mechanism G. The oversize material conveying mechanism G comprises one or more belt conveyors and/or heavy-duty dumpers.
Preferably, the shaft furnace roasting unit further comprises a main flue gas dust remover 31, and a flue gas inlet of the main flue gas dust remover 31 is connected with a top flue gas outlet of the shaft furnace 15 through a flue gas conveying pipeline. The fume outlet of the main fume dust remover 31 is connected with a chimney 34 through a fume exhaust pipeline, and the fume exhaust pipeline is sequentially provided with a main exhaust fan 32 and a desulfurization and denitrification device 33. The bottom dust outlet of the main flue gas dust remover 31 is connected with the feeding end of the dust bin 6 through a pneumatic conveying bin pump 35 and a pneumatic dust conveying pipeline 36.
Example 1
As shown in figure 1, the phosphorite shaft furnace roasting production system comprises a phosphorite pretreatment unit, an auxiliary material distribution unit, a pelletizing unit, a screening and distributing unit, a shaft furnace roasting unit, a cooling unit and a finished product treatment unit. The phosphorite pretreatment unit and the auxiliary material distribution unit are arranged in parallel, and are sequentially connected in series with the pelletizing unit, the screening and distributing unit, the shaft furnace roasting unit, the cooling unit and the finished product treatment unit according to the trend of materials.
The phosphorite pretreatment unit comprises a high-calcium phosphorite powder bin 1, a high-silicon phosphorite powder bin 2, a drying device 3 and a grinding device 4. The mineral powder feeding and conveying mechanism A is respectively connected with the feeding ends of the high-calcium phosphate rock powder bin 1 and the high-silicon phosphate rock powder bin 2 and is used for conveying the phosphate rock powder conveyed from the outside into the high-calcium phosphate rock powder bin 1 or the high-silicon phosphate rock powder bin 2 for pre-storing. The discharging ends of the high-calcium phosphate rock bin 1 and the high-silicon phosphate rock bin 2 are respectively connected with the feeding ends of the drying device 3, the ore grinding device 4 and the pelletizing unit through the mineral powder discharging and conveying mechanism B. The discharging end of the drying device 3 is connected with the feeding end of the grinding device 4 through a drying discharging conveying mechanism C. The discharge end of the ore grinding device 4 is connected with the feed end of the pelletizing unit through an ore grinding discharge conveying mechanism D. Preferably, a discharging vibrating hopper, a disc feeder and a quantitative feeder are respectively and independently arranged between the discharging ends of the high-calcium phosphate rock bin 1 and the high-silicon phosphate rock bin 2 and the feeding end of the mineral powder discharging conveying mechanism.
Example 2
Example 1 was repeated except that the ore dust feed conveyor a, the ore dust discharge conveyor B, the dry discharge conveyor C and the grinding discharge conveyor D each independently included one or more belt conveyors, with or without a pear discharger, optionally on each belt conveyor.
Example 3
Example 2 is repeated except that the phosphorite pretreatment unit further comprises a mineral powder temporary storage 5, and the mineral powder temporary storage 5 is connected with the discharge end of the mineral powder feeding and conveying mechanism A. A grab crane 501 is also arranged on the temporary storage yard 5. The piled mineral powder is conveyed into the high-calcium phosphate rock powder bin 1 and the high-silicon phosphate rock powder bin 2 by the grab crane 501.
Example 4
Example 3 is repeated except that the drying apparatus 3 includes a drum dryer 301, a wet dust collector 302, a drying blower 303, and a drying exhaust drum 304. According to the trend of the wind flow, the cylinder dryer 301, the wet dust collector 302, the drying induced draft fan 303 and the drying exhaust drum 304 are connected in series in sequence. The dry material discharge end of the cylinder dryer 301 is connected to the feed end of the dry material discharge conveyor C. The drying device 3 further comprises a hot blast stove 305, a sedimentation tank 306 and a sludge drying device 307. The hot air outlet of the hot air furnace 305 is connected with an air inlet arranged at one side of the dried material discharge end of the cylinder dryer 301 through a hot air pipe. The dust outlet of the wet dust collector 302 is connected with the feed inlet of the sedimentation tank 306, the sludge outlet of the sedimentation tank 306 is connected with the feed inlet of the sludge drying device 307, and the discharge outlet of the sludge drying device 307 is connected with the mineral powder temporary storage yard 5 through the dry sludge conveying mechanism 308.
Example 5
Example 4 is repeated except that the grinding apparatus 4 includes a roll screen 401, a grinding surge bin 402, and a high pressure roll mill 403 arranged in series. The feeding end of the roller screen 401 is connected with the discharging ends of the mineral powder discharging and conveying mechanism B and the drying discharging and conveying mechanism C. The discharge end of the high-pressure roller mill 403 is connected with the feed end of the ore grinding discharge conveying mechanism D.
Example 6
Example 5 was repeated except that the discharge end of the grinding surge bin 402 was connected to the feed end of the high pressure roller mill 403 and to the feed end of the grinding discharge conveyor D, respectively, by a reversible dosing machine 404.
Example 7
Example 6 was repeated except that vibration anti-blocking means were also provided on the side wall of the discharge end of the grinding surge bin 402. The roller screen 401 is also provided with a de-ironing separator 405.
Example 8
Example 7 was repeated except that the auxiliary material distribution unit included a dust bin 6, a bentonite bin 7 and a biomass straw bin 8 arranged in parallel with each other. The discharging ends of the dust bin 6 and the bentonite bin 7 are respectively and independently connected in series with a vibration anti-blocking device, a star-shaped ash discharging valve, a screw feeder and a sealing belt scale in sequence, and the discharging ends of all the sealing belt scales are connected with a mineral powder discharging and conveying mechanism B. The discharging end of the biomass straw bin 8 is sequentially connected with a discharging vibrating hopper, a disc feeder and a quantitative feeder in series, and the discharging end of the quantitative feeder is connected with a mineral powder discharging and conveying mechanism B.
Example 9
Example 8 was repeated except that the pelletizing unit included an intensive mixer 9, a mixing silo 10 and a disc pelletizer 11 arranged in series. The feeding end of the intensive mixer 9 is connected with the discharging end of the mineral powder discharging and conveying mechanism B. The discharge end of the disc pelletizer 11 is connected with a sieving and distributing unit through a green ball conveying mechanism E. A discharging vibrating hopper, a disc feeder and a quantitative feeder are also arranged between the mixing bin 10 and the disc pelletizer 11 in sequence. The green ball conveying mechanism E comprises one or more belt conveyors.
Example 10
Example 9 was repeated except that the pelletizing unit included a plurality of sets of mixing bins 10 arranged side by side and a disc pelletizer 11.
Example 11
Example 10 is repeated except that the screening cloth unit includes a roller screening machine 12 and a natural phosphorus ore bin 13. The feed end of the roller screen 12 is connected with the discharge end of the green ball conveying mechanism E, and the big ball discharge end and the small ball discharge end of the roller screen 12 are connected with the feed end of the mixing bin 10 through the ball return belt conveyor 1201. The middle ball discharge end of the roller screen 12 is connected with the feed end of the shaft furnace roasting unit through a raw ball distributing and conveying mechanism F. The natural phosphate rock bin 13 is arranged in parallel with the roller screening machine 12, and the discharge end of the natural phosphate rock bin 13 is connected with the green ball distributing and conveying mechanism F through a large inclination angle belt conveyor 1301 of the phosphate rock. The green ball cloth conveying mechanism F comprises one or more belt conveyors.
Example 12
Example 11 is repeated except that the shaft furnace firing unit comprises a shuttle distributor 14, a shaft furnace 15, an electric vibratory feeder 16 and a hot chain scraper 17 arranged in series. The feeding end of the shuttle distributor 14 is connected with the discharging end of the green ball distributing and conveying mechanism F. The discharge end of the hot chain scraper 17 is connected with the feed end of the cooling unit.
Example 13
Example 12 is repeated except that a toothed roll crusher 18 is also provided between the discharge end of the shaft furnace 15 and the electric vibratory feeder 16.
Example 14
The embodiment 13 is repeated, but a combustion fan and a cooling fan are further provided at one side of the shaft furnace 15, the combustion fan is connected with the combustion chamber at the upper part of the shaft furnace 15 through a combustion air pipe, and the cooling fan is connected with the cooling chamber at the lower part of the shaft furnace 15 through a cooling air pipe.
Example 15
Example 14 was repeated except that the cooling unit was a multi-stage belt cooler, comprising, in order according to the direction of the material, a first belt cooling stage 19, a second belt cooling stage 20, a third belt cooling stage 21, a fourth belt cooling stage 22, and a hood 23 covering them. The feeding end of the first section 19 with cooling is connected with the discharging end of the hot chain scraper 17, and the discharging end of the fourth section 22 with cooling is connected with the feeding end of the finished product processing unit.
Example 16
Example 15 was repeated except that the lower air inlets of the third 21 and fourth 22 stages were each connected to a blower via separate blower pipes. The upper air outlet of the four sections with cooling 22 is connected with the upper air inlet of the two sections with cooling 20 through a first circulating air pipe 24, and the lower air outlet of the two sections with cooling 20 is connected with a combustion-supporting fan of the shaft furnace 15 through a second circulating air pipe 25. The upper air outlet of the third section 21 with cooling is connected with the upper air inlet of the first section 19 with cooling through a third circulating air pipe 26, and the lower air outlet of the first section 19 with cooling is connected with the air inlet of the cylinder dryer 301 through a fourth circulating air pipe 27. An exhaust fan is also provided on the fourth circulation duct 27.
Example 17
Example 16 is repeated except that the product handling unit includes a product screen 28, a product bin 29, and a powder bin 30. The feed end of the product screen 28 is connected to the discharge end of the four sections 22. The on-screen discharge end of the product screen 28 is connected to the feed end of the product bin 29 and the under-screen discharge end of the product screen 28 is connected to the feed end of the powder bin 30. The discharge ends of the finished product bin 29 and the powder bin 30 are respectively provided with an electrohydraulic fan valve.
Example 18
Example 17 is repeated except that the product handling unit comprises a plurality of product bins 29, and the on-screen discharge end of the product screen 28 is connected to the feed ends of the plurality of product bins 29 by an on-screen material conveying mechanism G. The oversize material conveying mechanism G comprises one or more belt conveyors and a heavy-duty unloading vehicle.
Example 19
Example 18 is repeated except that the shaft furnace firing unit further comprises a main flue gas dust remover 31, the flue gas inlet of the main flue gas dust remover 31 being connected to the top flue gas outlet of the shaft furnace 15 by a flue gas transport duct. The fume outlet of the main fume dust remover 31 is connected with a chimney 34 through a fume exhaust pipeline, and the fume exhaust pipeline is sequentially provided with a main exhaust fan 32 and a desulfurization and denitrification device 33. The bottom dust outlet of the main flue gas dust remover 31 is connected with the feeding end of the dust bin 6 through a pneumatic conveying bin pump 35 and a pneumatic dust conveying pipeline 36.
Example 20
A method of conducting a phosphorite shaft furnace roasting production using the system of example 19, the method comprising:
1) Pretreating the phosphate rock powder by a phosphate rock pretreatment unit to obtain high-calcium phosphate rock powder and high-silicon phosphate rock powder; then mixing high-calcium phosphate rock powder and high-silicon phosphate rock powder to obtain mixed mineral powder;
2) Mixing the mixed mineral powder, dust (dust collected by a system), bentonite and biomass straw particles in proportion to obtain a pelleting mixture;
3) Adding the pelletizing mixture into a pelletizer for pelletizing, and sieving the obtained green pellets to obtain big pellets, seed pellets and small pellets; wherein, after the big ball and the small ball are crushed, the mixture returns to the step 2) to participate in the mixing; the middle ball enters the next working procedure;
4) And 3) conveying the medium balls obtained in the step 3) into a shaft furnace for roasting treatment, and conveying the roasted finished pellets to a finished product warehouse for storage after cooling by a belt cooler and sieving by a sieving machine.
Example 21
Example 20 is repeated except that the high-calcium phosphate rock powder is phosphate rock powder with the P 2O5 content not more than 15wt%, the CaO content not less than 40wt% and the water content of 6-10%; the high-silicon phosphate rock powder is phosphate rock powder with the P 2O5 content not more than 15wt%, the SiO 2 content not less than 40wt% and the water content of 6-10%.
Example 22
Example 21 was repeated except that the mesosphere particle size was 5-20mm; the pellets with the particle size larger than the middle balls are large balls, and the pellets with the particle size smaller than the middle balls are small balls.
Example 23
Example 22 was repeated except that the firing temperature was 1100-1300℃and the firing time was 1-10 hours, and the pellet size in the final bin after sieving was not less than 5mm.
Application example 1
The system of example 19 and the method of example 23 were used to perform the vertical kiln roasting production of phosphorite:
The high-calcium phosphate rock powder (P 2O5 content is about 13.6%, caO content is about 47.2%) and the high-silicon phosphate rock powder (P 2O5 content is about 14.4%, siO 2 content is about 45.8%) are respectively pretreated (dried and roller-ground) and then mixed to obtain mixed mineral powder (the mixing mass ratio of the high-calcium phosphate rock powder to the high-silicon phosphate rock powder is 1.3:1) with the particle size of not more than 0.125mm and the water content of about 8.2%.
The mixed mineral powder, dust, bentonite and corn stalk particles are mixed strongly according to the mass ratio of 97:6:3:1 to obtain a pelleting mixture; then pelletizing the pelletizing mixture in a disc pelletizer, sieving the obtained green pellets, putting the green pellets with the particle size of 8-16mm and natural lump ore (P 2O5 content is 22.20%) into a shaft furnace by adopting a shuttle type material distributor, roasting for 5 hours at 1200 ℃, cooling the sintered pellets, crushing the sintered pellets by a toothed roller, and conveying the sintered pellets to a multi-stage belt cooler by a hot chain plate machine for re-cooling treatment. And (3) screening the cooled pellets, and collecting and obtaining finished pellets with the particle size not less than 5 mm.
Application example 2
Application example 1 was repeated except that the fly ash and the potassium feldspar were subjected to a mixed grinding treatment to obtain modified fly ash (the addition amount of the potassium feldspar was 2.5% of the total mass of the fly ash).
Application example 3
Example 1 was repeated except that the corn straw particles were soaked in 0.02mol/L calcium hydroxide solution for 1 hour and then dried to obtain modified straw particles.
Claims (12)
1. A phosphorite shaft furnace roasting production system is characterized in that: the system comprises a phosphorite pretreatment unit, an auxiliary material distribution unit, a pelletizing unit, a screening and distributing unit, a shaft furnace roasting unit, a cooling unit and a finished product treatment unit; the phosphorite pretreatment unit and the auxiliary material distribution unit are arranged in parallel, and are sequentially connected in series with the pelletizing unit, the screening and distributing unit, the shaft furnace roasting unit, the cooling unit and the finished product treatment unit according to the trend of materials;
The phosphorite pretreatment unit comprises a high-calcium phosphorite powder bin (1), a high-silicon phosphorite powder bin (2), a drying device (3) and a grinding device (4); the mineral powder feeding and conveying mechanism (A) is respectively connected with the feeding ends of the high-calcium phosphate rock powder bin (1) and the high-silicon phosphate rock powder bin (2) and is used for conveying the phosphate rock powder conveyed from the outside into the high-calcium phosphate rock powder bin (1) or the high-silicon phosphate rock powder bin (2) for pre-storing; the discharging ends of the high-calcium phosphate rock bin (1) and the high-silicon phosphate rock bin (2) are respectively connected with the feeding ends of the drying device (3), the ore grinding device (4) and the pelletizing unit through the mineral powder discharging and conveying mechanism (B); the discharging end of the drying device (3) is connected with the feeding end of the ore grinding device (4) through a drying discharging conveying mechanism (C); the discharge end of the ore grinding device (4) is connected with the feed end of the pelletizing unit through an ore grinding discharge conveying mechanism (D); preferably, a discharging vibrating hopper, a disc feeder and a quantitative feeder are respectively and independently arranged between the discharging ends of the high-calcium phosphate rock powder bin (1) and the high-silicon phosphate rock powder bin (2) and the feeding end of the mineral powder discharging and conveying mechanism;
Preferably, the mineral powder feeding and conveying mechanism (A), the mineral powder discharging and conveying mechanism (B), the drying and discharging and conveying mechanism (C) and the grinding and discharging and conveying mechanism (D) respectively and independently comprise one or more belt conveyors, and a pear discharger is optionally arranged on each belt conveyor or not.
2. The system according to claim 1, wherein: the phosphorite pretreatment unit further comprises a mineral powder temporary storage yard (5), and the mineral powder temporary storage yard (5) is connected with a discharge end of the mineral powder feeding and conveying mechanism (A); a grab bucket crane (501) is also arranged on the mineral powder temporary storage yard (5); conveying the piled mineral powder into a high-calcium phosphate rock powder bin (1) and/or a high-silicon phosphate rock powder bin (2) through a grab bucket crane (501); and/or
The drying device (3) comprises a cylinder dryer (301), a wet dust collector (302), a drying fan (303) and a drying exhaust drum (304); according to the trend of the wind flow, the cylinder dryer (301), the wet dust collector (302), the drying induced draft fan (303) and the drying exhaust drum (304) are connected in series in sequence; the drying material discharging end of the cylinder dryer (301) is connected with the feeding end of the drying discharging conveying mechanism (C); preferably, the drying device (3) further comprises a hot blast stove (305), a sedimentation tank (306) and a sludge drying device (307); the hot air outlet of the hot air furnace (305) is connected with an air inlet arranged at one side of the dried material discharge end of the cylinder dryer (301) through a hot air pipe; the dust outlet of the wet dust collector (302) is connected with the feed inlet of the sedimentation tank (306), the sludge outlet of the sedimentation tank (306) is connected with the feed inlet of the sludge drying device (307), and the sludge outlet of the sludge drying device (307) is connected with the mineral powder temporary storage yard (5) through a dry sludge conveying mechanism (308); and/or
The ore grinding device (4) comprises a roller screen (401), an ore grinding buffer bin (402) and a high-pressure roller mill (403) which are arranged in series; the feeding end of the roller screen (401) is connected with the discharging ends of the mineral powder discharging and conveying mechanism (B) and the drying discharging and conveying mechanism (C); the discharge end of the high-pressure roller mill (403) is connected with the feed end of the ore grinding and discharging conveying mechanism (D); preferably, the discharge end of the ore grinding buffer bin (402) is respectively connected with the feed end of the high-pressure roller mill (403) and the feed end of the ore grinding discharge conveying mechanism (D) through a reversible quantitative feeder (404); further preferably, a vibration anti-blocking device is further arranged on the side wall of the discharging end of the ore grinding buffer bin (402); the roller screen (401) is also provided with an iron remover (405).
3. The system according to claim 1 or 2, characterized in that: the auxiliary material distribution unit comprises a dust bin (6), a bentonite bin (7) and a biomass straw bin (8) which are arranged in parallel; the discharging ends of the dust bin (6) and the bentonite bin (7) are respectively and independently provided with a vibration anti-blocking device, a star-shaped ash discharging valve, a screw feeder and a sealing belt scale in series, and the discharging ends of all the sealing belt scales are connected with a mineral powder discharging and conveying mechanism (B); the discharging end of the biomass straw bin (8) is sequentially and serially provided with a discharging vibrating hopper, a disc feeder and a quantitative feeder, and the discharging end of the quantitative feeder is connected with the mineral powder discharging conveying mechanism (B).
4. A system according to claim 3, characterized in that: the pelletizing unit comprises a strong mixer (9), a mixing bin (10) and a disc pelletizer (11) which are sequentially connected in series; the feeding end of the intensive mixer (9) is connected with the discharging end of the mineral powder discharging and conveying mechanism (B); the discharging end of the disc pelletizer (11) is connected with a screening and distributing unit through a green ball conveying mechanism (E); a discharging vibrating hopper, a disc feeder and a quantitative feeder are also arranged between the mixing bin (10) and the disc pelletizer (11) in sequence; preferably, the green ball conveying mechanism (E) comprises one or more belt conveyors;
Preferably, the pelletizing unit comprises a plurality of groups of mixing bins (10) which are arranged in parallel and a disc pelletizer (11).
5. The system according to claim 4, wherein: the screening and distributing unit comprises a roller screening machine (12) and a natural phosphate rock ore bin (13); the feeding end of the roller type screening machine (12) is connected with the discharging end of the green ball conveying mechanism (E), and the big ball discharging end and the small ball discharging end of the roller type screening machine (12) are connected with the feeding end of the mixing bin (10) through the ball return belt type conveyor (1201); the middle ball discharging end of the roller type screening machine (12) is connected with the feeding end of the shaft furnace roasting unit through a raw ball distributing and conveying mechanism (F); the natural phosphate rock bin (13) is arranged in parallel with the roller screening machine (12), and the discharge end of the natural phosphate rock bin (13) is connected with the green ball distributing and conveying mechanism (F) through a large inclination angle belt conveyor (1301) of the phosphate rock; preferably, the green ball cloth conveying mechanism (F) comprises one or more belt conveyors.
6. The system according to claim 5, wherein: the shaft furnace roasting unit comprises a shuttle distributor (14), a shaft furnace (15), an electric vibration feeder (16) and a hot chain plate machine (17) which are sequentially connected in series; the feeding end of the shuttle type distributing device (14) is connected with the discharging end of the raw ball distributing and conveying mechanism (F); the discharging end of the hot chain plate machine (17) is connected with the feeding end of the cooling unit; preferably, a toothed roller crusher (18) is arranged between the discharging end of the shaft furnace (15) and the electric vibration feeder (16); preferably, a combustion-supporting fan and a cooling fan are further arranged on one side of the shaft furnace (15), the combustion-supporting fan is connected with a combustion chamber on the upper portion of the shaft furnace (15) through a combustion-supporting air pipe, and the cooling fan is connected with a cooling chamber on the lower portion of the shaft furnace (15) through a cooling air pipe.
7. The system according to claim 6, wherein: the cooling unit is a multi-section belt cooler and sequentially comprises a first section (19) with cooling, a second section (20) with cooling, a third section (21) with cooling, a fourth section (22) with cooling and a fan cover (23) covered above the first section and the second section according to the trend of materials; the feeding end of the first section (19) with cooling is connected with the discharging end of the hot chain plate machine (17), and the discharging end of the fourth section (22) with cooling is connected with the feeding end of the finished product processing unit;
Preferably, the air inlets at the lower parts of the three sections (21) with cooling and the four sections (22) with cooling are respectively connected with an air blower through independent blast pipes; the upper air outlet of the four sections (22) with cooling is connected with the upper air inlet of the two sections (20) with cooling through a first circulating air pipe (24), and the lower air outlet of the two sections (20) with cooling is connected with a combustion-supporting fan of the shaft furnace (15) through a second circulating air pipe (25); the upper air outlet of the third section (21) with cooling is connected with the upper air inlet of the first section (19) with cooling through a third circulating air pipe (26), and the lower air outlet of the first section (19) with cooling is connected with the air inlet of the cylinder dryer (301) through a fourth circulating air pipe (27); preferably, an exhaust fan is also arranged on the fourth circulating air pipe (27).
8. The system according to claim 7, wherein: the finished product treatment unit comprises a finished product sieve (28), a finished product bin (29) and a powder bin (30); the feeding end of the finished product screen (28) is connected with the discharging end of the four sections (22) with cooling; the upper screen discharging end of the finished product screen (28) is connected with the feeding end of the finished product bin (29), and the lower screen discharging end of the finished product screen (28) is connected with the feeding end of the powder bin (30); the discharging ends of the finished product bin (29) and the powder bin (30) are respectively provided with an electrohydraulic sector valve;
Preferably, the finished product treatment unit comprises a plurality of finished product bins (29), and the on-screen discharging end of the finished product screen (28) is connected with the feeding ends of the plurality of finished product bins (29) through an on-screen material conveying mechanism (G); the oversize material conveying mechanism (G) comprises one or more belt conveyors and/or heavy-duty unloading trucks.
9. The system according to any one of claims 6-8, wherein: the shaft furnace roasting unit further comprises a main flue gas dust remover (31), and a flue gas inlet of the main flue gas dust remover (31) is connected with a top flue gas outlet of the shaft furnace (15) through a flue gas conveying pipeline; the smoke outlet of the main smoke dust remover (31) is connected with a chimney (34) through a smoke exhaust pipeline, and the smoke exhaust pipeline is sequentially provided with a main exhaust fan (32) and a desulfurization and denitrification device (33); the bottom dust outlet of the main flue gas dust remover (31) is connected with the feeding end of the dust bin (6) through a pneumatic conveying bin pump (35) and a pneumatic dust conveying pipeline (36).
10. A method for shaft kiln roasting production of phosphorus ore using the system of any one of claims 1 to 9, characterized in that: the method comprises the following steps:
1) Pretreating the phosphate rock powder by a phosphate rock pretreatment unit to obtain high-calcium phosphate rock powder and high-silicon phosphate rock powder; then mixing high-calcium phosphate rock powder and high-silicon phosphate rock powder to obtain mixed mineral powder;
2) Mixing the mixed mineral powder, dust (dust collected by a system), bentonite and biomass straw particles in proportion to obtain a pelleting mixture;
3) Adding the pelletizing mixture into a pelletizer for pelletizing, and sieving the obtained green pellets to obtain big pellets, seed pellets and small pellets; wherein, after the big ball and the small ball are crushed, the mixture returns to the step 2) to participate in the mixing; the middle ball enters the next working procedure;
4) And 3) conveying the medium balls obtained in the step 3) into a shaft furnace for roasting treatment, and conveying the roasted finished pellets to a finished product warehouse for storage after cooling by a belt cooler and sieving by a sieving machine.
11. The method according to claim 10, wherein: in the step 1), the high-calcium phosphate rock powder is phosphate rock powder with the P 2O5 content not more than 15wt%, the CaO content not less than 40wt% and the water content of 6-10%; preferably, the phosphorus ore powder contains 10-15wt% of P 2O5, 45-55wt% of CaO and 8-9% of water; the high-silicon phosphate rock powder is phosphate rock powder with the P 2O5 content not more than 15wt%, the SiO 2 content not less than 40wt% and the water content of 6-10%; preferably, the phosphorus ore powder contains 10-15wt% of P 2O5, 45-55wt% of SiO 2 and 8-9% of water content; the mixing mass ratio of the high-calcium phosphate rock powder to the high-silicon phosphate rock powder is 1.2-1.6:1, preferably 1.3-1.45:1; the average particle size of the mixed mineral powder is not more than 0.15mm, preferably not more than 0.125mm.
12. The method according to claim 10 or 11, characterized in that: in the step 2), mixing mineral powder, dust, bentonite and biomass straw particles in a mixing mass ratio of 92-98:3-8:1-5:0.5-2; preferably, the biomass straw particles are modified biomass straw particles modified by adopting calcium hydroxide solution; and/or
In step 3), the particle size of the mesosphere is 5-20mm, preferably 8-16mm; the pellets with the particle size larger than the middle balls are large balls, and the pellets with the particle size smaller than the middle balls are small balls; and/or
In step 4), the roasting temperature is 1100-1300 ℃, preferably 1150-1250 ℃, and the roasting treatment time is 1-10h, preferably 2-8h; the particle size of the pellets conveyed to the finished product bin after sieving is not less than 5mm, preferably not less than 7mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311037640.5A CN118147435A (en) | 2023-08-17 | 2023-08-17 | Phosphorite shaft furnace roasting production system and method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202311037640.5A CN118147435A (en) | 2023-08-17 | 2023-08-17 | Phosphorite shaft furnace roasting production system and method |
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| CN202311037640.5A Pending CN118147435A (en) | 2023-08-17 | 2023-08-17 | Phosphorite shaft furnace roasting production system and method |
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| Country | Link |
|---|---|
| CN (1) | CN118147435A (en) |
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2023
- 2023-08-17 CN CN202311037640.5A patent/CN118147435A/en active Pending
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