CN110872102A - Method and system for controlling calcination conditions to ensure qualified calcined phosphorite - Google Patents
Method and system for controlling calcination conditions to ensure qualified calcined phosphorite Download PDFInfo
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- CN110872102A CN110872102A CN201811009309.1A CN201811009309A CN110872102A CN 110872102 A CN110872102 A CN 110872102A CN 201811009309 A CN201811009309 A CN 201811009309A CN 110872102 A CN110872102 A CN 110872102A
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- 239000002367 phosphate rock Substances 0.000 title claims abstract description 161
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 238000001354 calcination Methods 0.000 title claims abstract description 123
- 238000000034 method Methods 0.000 title claims abstract description 46
- 239000000446 fuel Substances 0.000 claims abstract description 142
- 229910019142 PO4 Inorganic materials 0.000 claims abstract description 101
- 239000010452 phosphate Substances 0.000 claims abstract description 101
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims abstract description 101
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 36
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 18
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims abstract description 18
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims abstract description 18
- 239000001095 magnesium carbonate Substances 0.000 claims abstract description 18
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims abstract description 18
- 239000000292 calcium oxide Substances 0.000 claims abstract description 17
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 16
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 16
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims abstract description 16
- DLYUQMMRRRQYAE-UHFFFAOYSA-N tetraphosphorus decaoxide Chemical compound O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 claims description 28
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 25
- 239000011574 phosphorus Substances 0.000 claims description 25
- 229910052698 phosphorus Inorganic materials 0.000 claims description 25
- 239000003245 coal Substances 0.000 claims description 24
- 238000002485 combustion reaction Methods 0.000 claims description 20
- 238000002679 ablation Methods 0.000 claims description 11
- 238000005265 energy consumption Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 238000002386 leaching Methods 0.000 abstract description 15
- 229910001425 magnesium ion Inorganic materials 0.000 abstract description 8
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 7
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 abstract description 7
- 230000009286 beneficial effect Effects 0.000 abstract description 7
- 239000011575 calcium Substances 0.000 abstract description 7
- 229910001424 calcium ion Inorganic materials 0.000 abstract description 7
- 239000000843 powder Substances 0.000 description 10
- 239000012141 concentrate Substances 0.000 description 8
- 238000001514 detection method Methods 0.000 description 8
- 239000002245 particle Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- 239000003337 fertilizer Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- RPASNPADOARUAP-UHFFFAOYSA-N calcium magnesium tetranitrate Chemical compound [Mg++].[Ca++].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O RPASNPADOARUAP-UHFFFAOYSA-N 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000011737 fluorine Substances 0.000 description 2
- 229910052731 fluorine Inorganic materials 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 1
- KMQAPZBMEMMKSS-UHFFFAOYSA-K calcium;magnesium;phosphate Chemical compound [Mg+2].[Ca+2].[O-]P([O-])([O-])=O KMQAPZBMEMMKSS-UHFFFAOYSA-K 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 238000005456 ore beneficiation Methods 0.000 description 1
- 239000002686 phosphate fertilizer Substances 0.000 description 1
- 150000003017 phosphorus Chemical class 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- OBSZRRSYVTXPNB-UHFFFAOYSA-N tetraphosphorus Chemical compound P12P3P1P32 OBSZRRSYVTXPNB-UHFFFAOYSA-N 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Images
Classifications
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- 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
- C01B25/01—Treating phosphate ores or other raw phosphate materials to obtain phosphorus or phosphorus compounds
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention provides a method for controlling calcination conditions to ensure that phosphorite calcination is qualified, which comprises the steps of providing fuel from a fuel feeding unit to a calcination unit, wherein the calcination unit comprises a rotary kiln; providing phosphate ore from a phosphate ore feed unit to a calcination unit; and calcining the fuel and the phosphorite in a rotary kiln in the calcining unit to obtain target phosphorite, and controlling the quality of the target phosphorite to be preset quality according to the fuel feeding unit, the phosphorite feeding unit and the calcining unit, wherein the preset quality refers to that the ratio of the total molar weight of calcium oxide and magnesium oxide to the total molar weight of calcium carbonate and magnesium carbonate in the target phosphorite is 50-270: 1. The invention also provides a system for controlling the calcination condition to ensure that the calcined phosphorite is qualified. The method provided by the invention enables the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate to be 50-270: 1, and the target phosphorite with the ratio is beneficial to efficiently leaching calcium and magnesium ions in subsequent processes.
Description
Technical Field
The invention relates to the technical field of fertilizers, in particular to a method and a system for controlling calcination conditions to ensure that calcined phosphorite is qualified.
Background
Phosphorite is an important raw material mineral for producing phosphate fertilizer, yellow phosphorus, phosphoric acid and other various phosphatized products, is a double raw material of basic chemical industry and branch agriculture industry, and has important position and function in national economic development. Many of the current research on phosphate ore beneficiation processes focus on the subsequent leaching and purification of phosphate concentrate processes, and there is little research on the calcination conditions that will be used to calcine the raw ore to obtain a phosphate concentrate that is advantageous for subsequent leaching and purification.
The patent CN201410563330.1 provides a method for preparing a calcium magnesium nitrate fertilizer by using phosphate tailings, and the specific technical scheme is as follows: adding a certain amount of distilled water into a certain amount of tailing powder with a certain granularity to prepare tailing pulp with a certain solid content, gradually adding nitric acid, reacting under a certain condition, filtering after the reaction is finished, adding lime or calcium hydroxide into filtrate to adjust the pH value of the filtrate to 6.5-7, filtering again, and carrying out vacuum concentration drying on the filtrate to obtain the calcium magnesium nitrate fertilizer. The patent only discloses how to worth the calcium magnesium phosphate fertilizer and does not relate to controlling the calcination conditions.
ZL201510226362.7 patent provides a method for processing middle-low grade phosphorite to remove calcium and magnesium impurities in the middle-low grade phosphorite, which comprises the steps of calcining the middle-low grade phosphorite serving as a main raw material at 900-1100 ℃, sequentially digesting calcined slag with water at 60-100 ℃, leaching with an ammonium nitrate solution, and finally leaching with an ammonium sulfate solution to obtain phosphate concentrate, wherein calcium oxide and calcium and magnesium elements in the calcined slag can be effectively separated, and the content of phosphorus pentoxide in the phosphate concentrate can be improved. This patent also discloses only calcination temperature conditions, and does not relate to controlling other conditions, nor to the requirement of raw material quality for the leaching process.
CN107697894A and CN107673320A also only disclose particle size of calcined phosphate ore and do not relate to the requirement of raw material quality for leaching processes.
Disclosure of Invention
In view of the above, the invention provides a method capable of controlling the calcination conditions to ensure that the calcined phosphorite is qualified. The specific technical scheme is as follows.
A method for qualifying a calcined phosphate ore by controlling the calcination conditions, the method comprising:
providing fuel from a fuel feed unit to a calcination unit, wherein the calcination unit comprises a rotary kiln;
providing phosphate ore from a phosphate ore feed unit to a calcination unit;
and calcining the fuel and the phosphorite in a rotary kiln in a calcining unit to obtain target phosphorite, and controlling the quality of the target phosphorite to be preset quality according to the fuel feeding unit, the phosphorite feeding unit and the calcining unit, wherein the preset quality refers to that the ratio of the total molar weight of calcium oxide and magnesium oxide to the total molar weight of calcium carbonate and magnesium carbonate in the target phosphorite is 50-270: 1.
Preferably, the method further comprises:
the production efficiency of the target phosphate ore is also controlled to be a preset production efficiency according to the fuel feeding unit, the phosphate ore feeding unit and the calcining unit.
Preferably, the method further comprises:
and when the target phosphorite with preset quality is obtained, controlling the energy consumption of the fuel feeding unit to be lower than the preset energy consumption according to the phosphorite feeding unit and the calcining unit.
Preferably, the rotary kiln is hollow and cylindrical, an included angle between the rotary kiln and the plane is a preset angle, the rotary kiln comprises a phosphate rock feed port and a fuel feed port, the phosphate rock feed port is higher than the fuel feed port, phosphate rock enters the rotary kiln through the phosphate rock feed port and enters a calcination area under the rotation of the rotary kiln, the calcination area is located between the phosphate rock feed port and the fuel feed port, and fuel enters the rotary kiln through the fuel feed port;
the "controlling the quality of the target phosphate ore to a preset quality according to the fuel feeding unit, the phosphate ore feeding unit, and the calcining unit" includes:
controlling the quality of target phosphorite to be preset quality according to the fuel feeding speed and the fuel quality of the fuel feeding unit, the phosphorite feeding speed and the phosphorite quality of the phosphorite feeding unit and the rotating speed of a rotary kiln in the calcining unit; the fuel quality is the combustion value of each kilogram of fuel, and the phosphorite quality is the weight content value of the phosphorus pentoxide in the phosphorite.
Preferably, the "controlling the quality of the target phosphate ore to a preset quality according to the fuel feeding unit, the phosphate ore feeding unit, and the calcining unit" includes:
and controlling the quality of target phosphorite to be preset quality according to the fuel feeding speed and the fuel quality of the fuel feeding unit, the phosphorite feeding speed and the phosphorite quality of the phosphorite feeding unit, the rotating speed of a rotary kiln in the calcining unit and the specification parameters of the rotary kiln, wherein the specification parameters of the rotary kiln comprise the diameter of the rotary kiln, the length of the rotary kiln and a preset angle, and the phosphorite quality also comprises the ablation rate of the phosphorite.
Preferably, when the length of the rotary kiln is 18-22 meters, the diameter is 1.3-1.7 meters, the rotating speed is 4.5-5.5 Hz, the preset angle is 4-5 degrees, the fuel is coal powder, the combustion value of the coal powder is 4500-5500J/kg, the mass content of the phosphorus pentoxide in the phosphorus ore is 20-25 percent, and the ablation rate of the phosphorus ore is 16-20 percent;
the fuel feeding speed and the phosphorite feeding speed satisfy the following relational expression:
V1＝(0.078-0.082)*V2+K；
wherein V1Is the fuel feed rate in tons/hour, V2Is the phosphorite feed rate in tons/hour, where K is a constant and ranges from (-0.001) to 0.002.
Preferably, when the length of the rotary kiln is 20 meters, the diameter is 1.5 meters, the rotating speed is 5 Hz, the combustion value of the coal powder is 4638 joules/kg, the mass content of the phosphorus pentoxide in the phosphorite is 22.69%, and the ablation rate of the phosphorite is 18.22%;
the fuel feeding speed and the phosphorite feeding speed satisfy the following relational expression:
V1＝0.08*V2；
wherein V1Is the fuel feed rate in tons/hour, V2The unit is ton/hour, which is the phosphorite feeding speed.
Preferably, when the rotating speed of the rotary kiln is a preset rotating speed, the fuel feeding speed is a preset fuel feeding speed, and the fuel quality is a preset fuel quality, the lower the quality of the phosphorite is, the lower the phosphorite feeding speed is.
Preferably, the preset quality means that the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphorite is 60-180: 1.
The invention also provides a system for controlling the calcination condition to ensure that the calcined phosphorite is qualified, which comprises a fuel feeding unit, a phosphorite feeding unit, a calcination unit and a control unit;
the fuel feed unit is used for providing fuel to the calcining unit, and the phosphorite feed unit is used for providing phosphorite to the calcining unit;
the calcining unit comprises a rotary kiln, and the fuel and the phosphorite are calcined in the rotary kiln to obtain target phosphorite;
the control unit is used for controlling the quality of the target phosphorite to be preset quality according to the fuel feeding unit, the phosphorite feeding unit and the calcining unit, wherein the preset quality refers to that the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphorite is 50-270: 1, and preferably 60-180: 1.
The invention has the beneficial effects that: according to the method for controlling the calcination condition to ensure that the calcined phosphorite is qualified, the ratio of the total molar quantity of the calcium oxide and the magnesium oxide to the total molar quantity of the calcium carbonate and the magnesium carbonate is 50-270: 1 by controlling the fuel feeding unit, the phosphorite feeding unit and the calcination unit, and the target phosphorite with the ratio is beneficial to efficiently leaching calcium and magnesium ions in the subsequent process so as to obtain the phosphate concentrate with higher purity.
Drawings
FIG. 1 is a flow chart of the method for controlling the calcination conditions to ensure that the calcined phosphorite is qualified.
FIG. 2 is a schematic diagram of an apparatus for calcining phosphorus ore according to the present invention.
FIG. 3 is a sub-flow diagram of the phosphorite calcination process in step S300 of FIG. 1.
FIG. 4 is a block diagram of a system for controlling the calcination conditions to qualify the calcined phosphorus ore.
Detailed Description
While the following is a description of the preferred embodiments of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention.
Referring to fig. 1 and 2, the present invention provides a method for controlling the calcination conditions to qualify the phosphorite for calcination, which includes steps S100, S200 and S300. The steps are described in detail below.
Step S100, providing fuel from the fuel feeding unit 100 to the calcining unit 200, wherein the calcining unit 200 comprises a rotary kiln 210. It will be appreciated that the size and dimensions of the rotary kiln 210 may be set according to the actual throughput. It can be understood that the fuel includes but is not limited to one of pulverized coal, diesel oil, gasoline and natural gas, preferably, the fuel is pulverized coal, and the particle size and the combustion value of the pulverized coal are not limited, and more preferably, the particle size of the pulverized coal is 10-20mm, so that the pulverized coal can be rapidly combusted, high heat can be released, and the time for calcining the phosphate ore is saved. It will be appreciated that the fuel feed unit 100 includes a fuel feed detection unit for detecting the fuel feed rate.
In step S200, phosphate ore is provided from the phosphate ore feed unit 300 to the calcination unit 200. The phosphorite comprises various phosphorites with different qualities, such as high-grade (the phosphorus pentoxide content is more than 30 percent), medium-grade (the phosphorus pentoxide content is between 26 and 30 percent) phosphorite and low-grade (the phosphorus pentoxide content is less than 26 percent). It is understood that the phosphorite refers to the phosphorite obtained by primarily processing, crushing and screening raw phosphorite. Preferably, the particle size of the phosphorite is between 3 and 6mm, more preferably between 3.5 and 4.5mm, and the particle size range enables the phosphorite to be calcined better without increasing the crushing and screening process time. It is understood that the phosphate rock feeding unit 300 includes a feed hopper conveyor (not shown) for conveying phosphate rock and a phosphate rock feeding detection unit for detecting the feed rate of the phosphate rock.
And S300, calcining the fuel and the phosphorite in the rotary kiln 210 in the calcining unit 200 to obtain the target phosphorite, and controlling the quality of the target phosphorite to be preset quality according to the fuel feeding unit 100, the phosphorite feeding unit 300 and the calcining unit 200, wherein the preset quality refers to that the ratio of the total molar weight of calcium oxide and magnesium oxide to the total molar weight of calcium carbonate and magnesium carbonate in the target phosphorite is 50-270: 1. Preferably, the preset quality means that the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphorite is 60-180: 1.
Phosphorus ore generally contains phosphorus salts, calcium carbonate, magnesium carbonate, sulfur, silicon, fluorine, and the like, and the phosphorus ore is calcined in the calcination unit 200 to remove mainly carbon dioxide, sulfur dioxide, fluorine, and the like. However, if the calcination condition cannot be controlled well, the phosphorite is over-burnt or under-calcined, which is not beneficial to the subsequent calcium-magnesium ion leaching process. When the phosphorite is over-burnt, namely the calcination time is too long or the calcination temperature is too high, the silicon in the phosphorite is over-burnt to sinter the phosphorite into blocks, which is not beneficial to the subsequent calcium and magnesium ion leaching process. When the phosphorite is not sufficiently calcined, it still contains a larger content of calcium carbonate and magnesium carbonate, which are disadvantageous for the subsequent calcium and magnesium ion leaching process compared with calcium oxide and magnesium oxide.
The method provided by the invention can obtain the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate by controlling the fuel feeding unit 100, the phosphorite feeding unit 300 and the calcining unit 200, and the target phosphorite with the ratio is favorable for efficiently leaching calcium ions and magnesium ions in subsequent processes to obtain the phosphate concentrate with higher purity.
In a further embodiment, the method further comprises step S400.
Step S400, the production efficiency of the target phosphate ore is controlled to be a preset production efficiency according to the fuel feeding unit 100, the phosphate ore feeding unit 300 and the calcining unit 200. it is understood that the control can be performed by the fuel feeding speed of the fuel feeding unit 100, the phosphate ore feeding speed of the phosphate ore feeding unit 300 or the rotation speed of the rotary kiln 210, wherein the rotary kiln 210 rotates to convey the phosphate ore to the calcining zone 213, and after the completion of the calcining, the target phosphate ore continues to be conveyed to the cooling kiln by the rotation. it is understood that the rotary kiln 210 is provided with a rotation speed detecting unit 700 for detecting the rotation speed of the rotary kiln, wherein the rotation direction β of the rotary kiln 210 is shown in FIG. 2.
In a further embodiment, the method further comprises step S500.
In step S500, when the target phosphate ore having the preset quality is obtained, the power consumption of the fuel feeding unit 100 is also controlled to be lower than the preset power consumption according to the phosphate ore feeding unit 300 and the calcining unit 200. That is, the energy consumption of the fuel feeding unit 100 is minimized to save energy consumption, particularly, to reduce the amount of fuel, such as pulverized coal, while obtaining the target phosphate ore having a predetermined quality.
Referring again to fig. 2, in a further embodiment, the rotary kiln 210 is hollow and cylindrical, the angle between the rotary kiln 210 and the plane is a predetermined angle α, the rotary kiln 210 includes a phosphate ore feed port 211 and a fuel feed port 212, the phosphate ore feed port 211 is higher than the fuel feed port 212, the phosphate ore enters the rotary kiln 210 through the phosphate ore feed port 211 and enters a calcination zone 213 under the rotation of the rotary kiln 210, the calcination zone 213 is located between the phosphate ore feed port 211 and the fuel feed port 212, and the fuel enters the rotary kiln 210 through the fuel feed port 212, wherein the predetermined angle α is 4-6 °, preferably 4.5 °, after the phosphate ore enters the rotary kiln 210, the phosphate ore falls to the lowest part of the rotary kiln 210 due to the weight of the phosphate ore after the side wall of the rotary kiln 210 rises to a certain height under the rotation of the rotary kiln 210, and the rising height affects the calcination time of the phosphate ore in the rotary kiln 210.
The "controlling the quality of the target phosphate ore to a preset quality according to the fuel feeding unit 100, the phosphate ore feeding unit 300, and the calcining unit 200" includes:
controlling the quality of the target phosphate ore to be a preset quality according to the fuel feeding speed and the fuel quality of the fuel feeding unit 100, the phosphate ore feeding speed and the phosphate ore quality of the phosphate ore feeding unit 300, and the rotating speed of the rotary kiln 210 in the calcining unit 200; the quality of the fuel is the combustion value of each kilogram of fuel, and the quality of the phosphorite is the weight content value of the phosphorus pentoxide in the phosphorite. Wherein the fuel quality determines the amount of heat energy that the fuel can provide to the phosphate ore during combustion, the greater the combustion value, the greater the heat energy that is provided to the phosphate ore after combustion.
Referring to fig. 3 and 2, in a further embodiment, the "calcining the fuel and the phosphate ore in the rotary kiln 210 of the calcining unit 200 to obtain the target phosphate ore" includes steps S310 and S320. The detailed procedure is as follows.
In step S310, the phosphate ore is preheated in the preheating zone 214 of the rotary kiln 210 in the calcination unit 200. The preheating zone 214 is located between the calcination zone 213 and the phosphate rock feed inlet 211. The rotary kiln 210 is hollow, the heat generated by burning fuel and phosphorus ore is diffused along the periphery, when the phosphorus ore enters from the phosphorus ore feed inlet of the rotary kiln 210, the heat generated by burning in the calcining zone 213 is transferred to the preheating zone 214 to preheat the phosphorus ore, although the temperature does not reach the calcining temperature, the phosphorus ore can be heated, so that the phosphorus ore can be effectively calcined when reaching the calcining zone 213. If the phosphorus ore is not preheated, the temperature of the surface of the phosphorus ore is increased rapidly, the temperature of the interior of the phosphorus ore particles is increased slowly, and finally the calcination is not uniform.
In step S320, the fuel and the preheated phosphate ore are calcined in the calcining zone 213 of the rotary kiln 210. Wherein the fuel is preferably ignited and combusted above the calcination area 213, and the heat after combustion is transferred to the calcination area 213 to heat the phosphate ore, so as to calcine the phosphate ore. Compared with the contact combustion of fuel and phosphorite, the temperature of the fuel after ignition combustion is too high, and the risk of sintering and agglomeration caused by high-temperature and over-combustion of the phosphorite can be avoided. Wherein the temperature of the fuel after ignition and combustion is 1200-1500 ℃, and the temperature when the fuel is transferred to the calcining zone 213 is 900-1000 ℃ through heat transfer.
In a further embodiment, the "controlling the quality of the target phosphate ore to a preset quality according to the fuel feed unit 100, the phosphate ore feed unit 300, and the calcination unit 200" includes:
the quality of the target phosphorite is controlled to be preset quality according to the fuel feeding speed and the fuel quality of the fuel feeding unit 100, the phosphorite feeding speed and the phosphorite quality of the phosphorite feeding unit 300, the rotating speed of the rotary kiln 210 in the calcining unit 200 and the specification parameters of the rotary kiln 210, wherein the specification parameters of the rotary kiln 210 comprise the diameter of the rotary kiln, the length of the rotary kiln and a preset angle α, the phosphorite quality also comprises the ablation rate of the phosphorite, and the ablation rate refers to the weight content value lost by the phosphorite after calcining.
In a further embodiment, when the length of the rotary kiln is 18-22 meters, the diameter is 1.3-1.7 meters, the rotating speed is 4.5-5.5 Hz, the preset angle is 4-5 degrees, the fuel is coal powder, the combustion value of the coal powder is 4500-5500 joules/kg, the mass content of the phosphorus pentoxide in the phosphorus ore is 20-25 percent, and the ablation rate of the phosphorus ore is 16-20 percent;
the fuel feeding speed and the phosphorite feeding speed satisfy the following relational expression:
V1＝(0.078-0.082)*V2+K；
wherein V1Is the fuel feed rate in tons/hour, V2Is the phosphorite feed rate in tons/hour, where K is a constant and K isHas a value in the range of (-0.001) to 0.002.
In this embodiment, a large number of experiments prove that the fuel feeding speed and the phosphate rock feeding speed satisfy the relation V under the parameter conditions of the rotary kiln and the quality conditions of the coal powder and the phosphate rock1＝(0.078-0.082)*V2+ K. Through the relational expression, the two conditions in the relational expression can be adjusted when the phosphorite is calcined so as to obtain the calcined target phosphorite with preset quality, and further realize controllable calcining conditions.
In a further embodiment, when the length of the rotary kiln is 20 meters, the diameter is 1.5 meters, the rotating speed is 5 Hz, the fuel is coal powder, the combustion value of the coal powder is 4638 joules/kg, the mass content of the phosphorus pentoxide in the phosphorus ore is 22.69%, and the ablation rate of the phosphorus ore is 18.22%;
the fuel feeding speed and the phosphorite feeding speed satisfy the following relational expression:
V1＝0.08*V2；
wherein V1Is the fuel feed rate in tons/hour, V2The unit is ton/hour, which is the phosphorite feeding speed.
This embodiment provides a more accurate relationship and conditions for performing the relationship to provide more effective and precise control of the calcination of the phosphate ore.
Reference may be made specifically to the following specific example 1.
The following will illustrate, by way of specific example 1 and experimental data, that the fuel feed rate and the phosphate feed rate satisfy the relationship in the above example: v1＝0.08*V2In this case, the target phosphate ore having a predetermined quality can be obtained.
Example 1
In example 1, the fuel used was pulverized coal, the pulverized coal used was pulverized coal having the same combustion value or within a predetermined range, and the phosphate ore used was phosphate ore of yiyang, guizhou, wherein the rotary kiln had a length of 20m, a diameter of 1.5 m, and a rotation speed of 5 hz, the fuel was pulverized coal, the combustion value of the pulverized coal was 4638 j/kg, the phosphorus ore had a phosphorus pentoxide content of 22.69% by mass, and the phosphate ore had an ablation rate of 18.22%. A number of different coal fines feed rates and phosphate rock feed rates are listed in table 1 below, and the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphate rock after calcination was examined after calcination in rotary kiln 210. See table 1 for details.
TABLE 1
As can be seen from Table 1 above, when the fuel feed rate and the phosphate ore feed rate satisfy the relation V1＝0.08*V2When the relation is not satisfied, the obtained target phosphorite does not have the preset quality, for example, the 8 th to the 10 th group, when the phosphorite feed speed is too fast, the phosphorite calcination is insufficient, the preset quality of the target phosphorite is influenced, for example, the 6 th group, when the coal powder feed speed is too fast, the phosphorite overburning can be caused, the phosphorite surface is sintered into blocks, the calcination of the internal phosphorite is not facilitated, and the quality of the finally formed target phosphorite still cannot reach the preset quality. Therefore, the relation provided by the invention can realize the control of the calcining condition so as to ensure that the calcined phosphorite has preset quality.
In addition, after the obtained target phosphorite is subjected to subsequent calcium ion and magnesium ion leaching processes, the purity of 1-5 groups in the finally obtained phosphate concentrate is higher than that of 6-10 groups. This indicates that the calcined target phosphate ore is beneficial to the leaching process.
In a further embodiment, when the rotation speed of the rotary kiln 210 is a preset rotation speed, the fuel feeding speed is a preset fuel feeding speed, and the fuel quality is a preset fuel quality, the lower the phosphate rock feeding speed. It will be appreciated that the lower the quality of the phosphate ore, indicating that the lower the phosphorus-containing salts in the phosphate ore, the higher the relative amounts of calcium carbonate and magnesium carbonate in the phosphate ore, and therefore, in order to obtain the target phosphate ore of the predetermined quality, the lower the feed rate of the phosphate ore is required to achieve adequate calcination of the phosphate ore.
Referring to fig. 2 and 4, the present invention also provides a system 10 for controlling the calcination conditions to qualify the calcination of phosphate ore, wherein the system 10 includes a fuel feed unit 100, a phosphate ore feed unit 300, a calcination unit 200, and a control unit 400. The fuel feed unit 100 is used to provide fuel to the calcination unit 200 and the phosphate ore feed unit 300 is used to provide phosphate ore to the calcination unit 200. The calcination unit 200 includes a rotary kiln 210 (see fig. 2), and the fuel and the phosphate ore are calcined in the rotary kiln 210 to obtain the target phosphate ore. Wherein the rotary kiln 210 may be the rotary kiln 210 described in any of the embodiments above.
The control unit 400 is used for controlling the quality of the target phosphate ore to be a preset quality according to the fuel feeding unit 100, the phosphate ore feeding unit 300 and the calcining unit 200, wherein the preset quality is that the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphate ore is 50-270: 1, preferably 60-180: 1.
The system 10 for controlling the calcination condition to ensure that the phosphorite is qualified for calcination provided by the invention obtains the ratio of the total molar quantity of calcium oxide and magnesium oxide to the total molar quantity of calcium carbonate and magnesium carbonate after calcination to be 50-270: 1, preferably 60-180: 1, and the target phosphorite with the ratio is beneficial to efficiently leaching calcium and magnesium ions in subsequent processes so as to obtain the phosphate concentrate with higher purity.
In a further embodiment, the system 10 includes a fuel feed detection unit 500 for detecting a fuel feed rate. In some embodiments, the fuel feed detection unit 500 is further configured to transmit the detected fuel feed rate information to the control unit 400.
The system 10 includes a phosphate rock feed detection unit 600 for detecting the fuel feed rate. In some embodiments, the phosphorite feed detection unit 600 is further configured to transmit the detected phosphorite feed rate information to the control unit 400.
The system 10 further includes a rotation speed detecting unit 700 for detecting the rotation speed of the rotary kiln 210. In some embodiments, the rotation speed detecting unit 700 is further configured to transmit the detected rotation speed information of the rotary kiln to the control unit 400.
The control unit 400 controls the quality of the target phosphate ore based on the received fuel feed rate information, phosphate ore feed rate information, and rotational speed information.
In a further embodiment, the side wall of the rotary kiln 210 close to the phosphate rock feed inlet is provided with an exhaust gas discharge outlet 230, and the outlet of the exhaust gas discharge outlet 230 faces upwards. The system further comprises a temperature detection unit 800, wherein the temperature detection unit 800 is used for detecting the temperature of the exhaust emission outlet 230, and the control unit 400 determines the temperature of the calcining zone 213 in the rotary kiln 210 according to the temperature of the exhaust emission outlet 230. Better control the calcining condition to obtain the target phosphorite with preset quality.
The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.
Claims (10)
1. A method for qualifying calcined phosphate ore by controlling the calcination conditions, the method comprising:
providing fuel from a fuel feed unit to a calcination unit, wherein the calcination unit comprises a rotary kiln;
providing phosphate ore from a phosphate ore feed unit to a calcination unit;
and calcining the fuel and the phosphorite in a rotary kiln in a calcining unit to obtain target phosphorite, and controlling the quality of the target phosphorite to be preset quality according to the fuel feeding unit, the phosphorite feeding unit and the calcining unit, wherein the preset quality refers to that the ratio of the total molar weight of calcium oxide and magnesium oxide to the total molar weight of calcium carbonate and magnesium carbonate in the target phosphorite is 50-270: 1.
2. The method of claim 1, wherein the method further comprises:
the production efficiency of the target phosphate ore is also controlled to be a preset production efficiency according to the fuel feeding unit, the phosphate ore feeding unit and the calcining unit.
3. The method of claim 1, wherein the method further comprises:
and when the target phosphorite with preset quality is obtained, controlling the energy consumption of the fuel feeding unit to be lower than the preset energy consumption according to the phosphorite feeding unit and the calcining unit.
4. The method according to claim 1, wherein the rotary kiln is hollow cylindrical, the included angle between the rotary kiln and the plane is a preset angle, the rotary kiln comprises a phosphate ore feed port and a fuel feed port, the phosphate ore feed port is higher than the fuel feed port, phosphate ore enters the rotary kiln through the phosphate ore feed port and enters a calcination zone under the rotation of the rotary kiln, the calcination zone is located between the phosphate ore feed port and the fuel feed port, and the fuel enters the rotary kiln through the fuel feed port;
the "controlling the quality of the target phosphate ore to a preset quality according to the fuel feeding unit, the phosphate ore feeding unit, and the calcining unit" includes:
controlling the quality of target phosphorite to be preset quality according to the fuel feeding speed and the fuel quality of the fuel feeding unit, the phosphorite feeding speed and the phosphorite quality of the phosphorite feeding unit and the rotating speed of a rotary kiln in the calcining unit; the fuel quality is the combustion value of each kilogram of fuel, and the phosphorite quality is the weight content value of the phosphorus pentoxide in the phosphorite.
5. The method of claim 4, wherein the controlling the quality of the target phosphate ore to a predetermined quality according to the fuel feed unit, the phosphate ore feed unit, and the calcination unit comprises:
and controlling the quality of target phosphorite to be preset quality according to the fuel feeding speed and the fuel quality of the fuel feeding unit, the phosphorite feeding speed and the phosphorite quality of the phosphorite feeding unit, the rotating speed of a rotary kiln in the calcining unit and the specification parameters of the rotary kiln, wherein the specification parameters of the rotary kiln comprise the diameter of the rotary kiln, the length of the rotary kiln and a preset angle, and the phosphorite quality also comprises the ablation rate of the phosphorite.
6. The method as claimed in claim 5, wherein when the length of the rotary kiln is 18-22 m, the diameter is 1.3-1.7 m, the rotation speed is 4.5-5.5 Hz, the preset angle is 4-5 °, the fuel is pulverized coal, the combustion value of the pulverized coal is 4500-5500J/kg, the mass content of the phosphorus pentoxide in the phosphorus ore is 20-25%, and the ablation rate of the phosphorus ore is 16-20%;
the fuel feeding speed and the phosphorite feeding speed satisfy the following relational expression:
V1＝(0.078-0.082)*V2+K；
wherein V1Is the fuel feed rate in tons/hour, V2Is the phosphorite feed rate in tons/hour, where K is a constant and ranges from (-0.001) to 0.002.
7. The method of claim 6, wherein when the rotary kiln has a length of 20 meters, a diameter of 1.5 meters, a rotation speed of 5 hz, the pulverized coal has a combustion value of 4638 joules/kg, the phosphorus pentoxide content in the phosphorus ore is 22.69% by mass, and the ablation rate of the phosphorus ore is 18.22%;
the fuel feeding speed and the phosphorite feeding speed satisfy the following relational expression:
V1＝0.08*V2；
wherein V1Is the fuel feed rate in tons/hour, V2The unit is ton/hour, which is the phosphorite feeding speed.
8. The method of claim 4 wherein the lower the phosphate ore quality, the lower the phosphate ore feed rate when the rotary kiln is at a predetermined rotational speed, the fuel feed rate is at a predetermined fuel feed rate, and the fuel quality is at a predetermined fuel quality.
9. The method of claim 1, wherein the predetermined quality is that the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphate ore is 60-180: 1.
10. A system for controlling calcination conditions to ensure that the calcined phosphorite is qualified is characterized by comprising a fuel feeding unit, a phosphorite feeding unit, a calcination unit and a control unit;
the fuel feed unit is used for providing fuel to the calcining unit, and the phosphorite feed unit is used for providing phosphorite to the calcining unit;
the calcining unit comprises a rotary kiln, and the fuel and the phosphorite are calcined in the rotary kiln to obtain target phosphorite;
the control unit is used for controlling the quality of the target phosphorite to be preset quality according to the fuel feeding unit, the phosphorite feeding unit and the calcining unit, wherein the preset quality refers to that the ratio of the total molar amount of calcium oxide and magnesium oxide to the total molar amount of calcium carbonate and magnesium carbonate in the target phosphorite is 50-270: 1, and preferably 60-180: 1.
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