CN116571075B - Method and device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder - Google Patents
Method and device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder Download PDFInfo
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- CN116571075B CN116571075B CN202310843476.0A CN202310843476A CN116571075B CN 116571075 B CN116571075 B CN 116571075B CN 202310843476 A CN202310843476 A CN 202310843476A CN 116571075 B CN116571075 B CN 116571075B
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- flue gas
- gangue powder
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- OBSZRRSYVTXPNB-UHFFFAOYSA-N tetraphosphorus Chemical compound P12P3P1P32 OBSZRRSYVTXPNB-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 239000000843 powder Substances 0.000 title claims abstract description 88
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 239000011574 phosphorus Substances 0.000 title claims abstract description 50
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000007789 gas Substances 0.000 claims abstract description 132
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 87
- 239000003546 flue gas Substances 0.000 claims abstract description 87
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- 238000001354 calcination Methods 0.000 claims abstract description 39
- 238000002485 combustion reaction Methods 0.000 claims abstract description 36
- 239000003245 coal Substances 0.000 claims abstract description 31
- 239000002893 slag Substances 0.000 claims abstract description 25
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000001301 oxygen Substances 0.000 claims abstract description 17
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 17
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 18
- 229910001919 chlorite Inorganic materials 0.000 claims description 15
- 229910052619 chlorite group Inorganic materials 0.000 claims description 15
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 claims description 15
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 claims description 15
- 229910052622 kaolinite Inorganic materials 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 229910052799 carbon Inorganic materials 0.000 claims description 13
- 229910044991 metal oxide Inorganic materials 0.000 claims description 13
- 150000004706 metal oxides Chemical class 0.000 claims description 13
- 239000000047 product Substances 0.000 claims description 13
- 239000002245 particle Substances 0.000 claims description 9
- 239000010453 quartz Substances 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000005995 Aluminium silicate Substances 0.000 claims description 2
- 235000012211 aluminium silicate Nutrition 0.000 claims description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 abstract description 20
- 229910000147 aluminium phosphate Inorganic materials 0.000 abstract description 10
- 238000005260 corrosion Methods 0.000 abstract description 7
- 230000007797 corrosion Effects 0.000 abstract description 7
- 239000000126 substance Substances 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 22
- 239000000292 calcium oxide Substances 0.000 description 12
- 230000000052 comparative effect Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 5
- 229910021532 Calcite Inorganic materials 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- -1 al) 6 (Si Inorganic materials 0.000 description 3
- 239000001506 calcium phosphate Substances 0.000 description 3
- 229910000389 calcium phosphate Inorganic materials 0.000 description 3
- 235000011010 calcium phosphates Nutrition 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000013064 chemical raw material Substances 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 3
- 229910001392 phosphorus oxide Inorganic materials 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- YWEUIGNSBFLMFL-UHFFFAOYSA-N diphosphonate Chemical compound O=P(=O)OP(=O)=O YWEUIGNSBFLMFL-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- DLYUQMMRRRQYAE-UHFFFAOYSA-N phosphorus pentoxide Inorganic materials O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 description 2
- VSAISIQCTGDGPU-UHFFFAOYSA-N tetraphosphorus hexaoxide Chemical compound O1P(O2)OP3OP1OP2O3 VSAISIQCTGDGPU-UHFFFAOYSA-N 0.000 description 2
- OCKGFTQIICXDQW-ZEQRLZLVSA-N 5-[(1r)-1-hydroxy-2-[4-[(2r)-2-hydroxy-2-(4-methyl-1-oxo-3h-2-benzofuran-5-yl)ethyl]piperazin-1-yl]ethyl]-4-methyl-3h-2-benzofuran-1-one Chemical compound C1=C2C(=O)OCC2=C(C)C([C@@H](O)CN2CCN(CC2)C[C@H](O)C2=CC=C3C(=O)OCC3=C2C)=C1 OCKGFTQIICXDQW-ZEQRLZLVSA-N 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 229910001579 aluminosilicate mineral Inorganic materials 0.000 description 1
- 229910052661 anorthite Inorganic materials 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- XAAHAAMILDNBPS-UHFFFAOYSA-L calcium hydrogenphosphate dihydrate Chemical compound O.O.[Ca+2].OP([O-])([O-])=O XAAHAAMILDNBPS-UHFFFAOYSA-L 0.000 description 1
- 239000000378 calcium silicate Substances 0.000 description 1
- 229910052918 calcium silicate Inorganic materials 0.000 description 1
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004891 communication 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
- 229910001649 dickite Inorganic materials 0.000 description 1
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052621 halloysite Inorganic materials 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 238000009616 inductively coupled plasma Methods 0.000 description 1
- 238000002354 inductively-coupled plasma atomic emission spectroscopy Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 229910052863 mullite Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/55—Compounds of silicon, phosphorus, germanium or arsenic
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of phosphorus chemical industry and environmental protection, in particular to a method and a device for removing phosphorus in yellow phosphorus tail gas boilers by using coal gangue powder, wherein the method comprises the following steps: (1) Carrying out combustion reaction on yellow phosphorus tail gas and oxygen-containing gas to obtain high-temperature flue gas; (2) Under the thermal action of the combustion reaction, the gangue powder is fluidized and is subjected to calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorized slag, and the obtained high Wen Tuolin flue gas is subjected to heat exchange to obtain boiler flue gas. The method utilizes the coal gangue powder with low heat value to realize the removal of phosphorus in the yellow phosphorus tail gas while recovering the reaction heat of the yellow phosphorus tail gas; meanwhile, the method avoids phosphoric acid corrosion generated by taking yellow phosphorus tail gas as boiler gas, and prolongs the operation period of gas boiler equipment.
Description
Technical Field
The invention relates to the technical field of phosphorus chemical industry and environmental protection, in particular to a method for removing phosphorus in a yellow phosphorus tail gas boiler by using coal gangue powder and a device for removing phosphorus in the yellow phosphorus tail gas boiler by using the coal gangue powder.
Background
Yellow phosphorus is an important chemical raw material and is indispensable in electronic grade chemicals, medicines, pesticides, extractants, military industry, battery materials and other industries. At present, the industrial method for producing yellow phosphorus is an electric furnace method, the energy consumption per 1 ton of yellow phosphorus produced is up to 3.2 tons of standard coal, and the byproduct of the phosphorus furnace tail gas 2800-3200m containing 85% -90% of CO 3 Is a high-quality chemical raw material and fuel gas, but has low cost competitiveness as chemical raw material gas because of the yellow phosphorus tail gas purification technology and small amount of single phosphorus furnace gas. At present, yellow phosphorus tail gas is mainly used for fuel gas, but is used as boiler fuel gas, because the yellow phosphorus tail gas contains elemental phosphorus and phosphine gas, phosphorus pentoxide is produced after the combustion of the elemental phosphorus and the phosphine gas with air, phosphoric acid is produced by combining the phosphorus pentoxide with water, and the phosphoric acid is attached to the wall of a boiler pipe to cause equipment corrosion, so that the low-cost solution of the corrosion of the yellow phosphorus tail gas fuel gas boiler is one of key technologies for utilizing the yellow phosphorus tail gas.
Disclosure of Invention
The invention aims to solve the problems that equipment is damaged due to corrosion of phosphoric acid generated by the existing yellow phosphorus tail gas serving as fuel of a gas boiler and the large-scale of the yellow phosphorus tail gas boiler is realized, and provides a method for removing phosphorus in the yellow phosphorus tail gas boiler by using coal gangue powder and a device for removing phosphorus in the yellow phosphorus tail gas boiler by using the coal gangue powder.
In order to achieve the above purpose, the first aspect of the present invention provides a method for removing phosphorus in yellow phosphorus tail gas boilers by using coal gangue powder, the method comprising the following steps:
(1) Carrying out combustion reaction on yellow phosphorus tail gas and oxygen-containing gas to obtain high-temperature flue gas;
(2) Under the thermal action of the combustion reaction, the gangue powder is fluidized and is subjected to calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorized slag, and the obtained high Wen Tuolin flue gas is subjected to heat exchange to obtain boiler flue gas.
Preferably, the gangue powder contains carbonate, kaolinite, chlorite, carbon and quartz.
Preferably, the calcination reaction comprises the following steps: s1, performing the calcination reaction on carbonate in the gangue powder to obtain metal oxide; s2, performing the calcination reaction on the kaolinite and the chlorite in the gangue powder to obtain an amorphous product; s3, reacting carbon in the gangue powder to provide heat for the calcination reaction; wherein the calcined reaction product comprises the metal oxide and an amorphous product.
The invention provides a device for removing phosphorus in yellow phosphorus tail gas boilers by using coal gangue powder, which comprises: a fluidized bed gas boiler;
the fluidized bed gas boiler is used for carrying out combustion reaction on yellow phosphorus tail gas and oxygen-containing gas to obtain high-temperature flue gas; under the thermal action of the combustion reaction, the gangue powder is fluidized and is subjected to calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorized slag, and the obtained high Wen Tuolin flue gas is subjected to heat exchange to obtain boiler flue gas.
Compared with the prior art, the invention has the following advantages:
(1) The method provided by the invention adopts the gangue powder as the dephosphorizing agent, and carries out dephosphorizing treatment with the yellow phosphorus tail gas under the high-temperature combustion of the gas boiler to remove the elemental phosphorus and the PH contained in the yellow phosphorus tail gas 3 Dephosphorization slag is obtained, and the method utilizes coal gangue powder with low heat value to realize the removal of phosphorus in yellow phosphorus tail gas, namely, a pot while recovering the reaction heat of the yellow phosphorus tail gasP in furnace flue gas 2 O 5 The content is less than or equal to 5mg/Nm 3 ；
Specifically, carbonate in gangue powder is subjected to calcination reaction, and the obtained metal oxide is subjected to chemical reaction to remove P 2 O 5 The method comprises the steps of carrying out a first treatment on the surface of the The calcination reaction is carried out on the kaolin and the chlorite in the gangue powder, and the obtained amorphous product is subjected to physical adsorption P 2 O 5 ；
(2) The method provided by the invention not only avoids the corrosion of phosphoric acid generated by taking yellow phosphorus tail gas as boiler gas, prolongs the operation period of gas boiler equipment, but also effectively reduces the energy consumption and the production cost.
Drawings
Fig. 1 is a schematic structural diagram of a device for removing phosphorus in yellow phosphorus tail gas boilers by using coal gangue powder.
Description of the reference numerals
I. A fluidized bed gas boiler; II. A separator; 1. yellow phosphorus tail gas; 2. an oxygen-containing gas; 3. coal gangue powder; 4. dephosphorizing slag; 5. boiler flue gas; 6. low-temperature dephosphorization flue gas.
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
The invention provides a method for removing phosphorus in yellow phosphorus tail gas boilers by using coal gangue powder, which comprises the following steps:
(1) Carrying out combustion reaction on yellow phosphorus tail gas and oxygen-containing gas to obtain high-temperature flue gas;
(2) Under the thermal action of the combustion reaction, the gangue powder is fluidized and is subjected to calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Carrying out the strippingAnd (3) phosphorus treatment to obtain dephosphorized slag, and heat exchanging the obtained high Wen Tuolin flue gas to obtain boiler flue gas.
The inventors of the present invention studied and found that: the main components of the gangue powder are aluminosilicate minerals and coal quality, and the gangue powder is rich in SiO 2 And Al 2 O 3 The main component is kaolinite (Al 2 Si 2 O 5 (OH) 4 ) Quartz (SiO) 2 ) Calcite (CaCO) 3 ) Chlorite ((Mg, al) 6 (Si,Al) 4 O 10 (OH) 8 ) Carbon (C), etc. Under the thermal action of the combustion reaction of the yellow phosphorus tail gas and the oxygen-containing gas, the gangue powder is in a fluidized state in the fluidized bed and is subjected to calcination reaction, and a small amount of elemental phosphorus (P) is entrained in the yellow phosphorus tail gas 4 ) And pH (potential of Hydrogen) 3 P produced by combustion 2 O 5 ，P 2 O 5 Immediately reacting with the moisture carried in the tail gas to produce phosphoric acid, which reacts with the calcined product of carbonate (e.g., calcite) in the gangue powder, and metal oxide (e.g., calcium oxide) to produce phosphoxycalcium compounds (e.g., calcium phosphate, white phosphocalcite, etc.); in addition, in the process of converting kaolinite and chlorite in the gangue into quartz, mullite, anorthite, calcium silicate and the like in the calcining process, the structure is converted from a polygonal layered stacked structure with better crystallinity into an amorphous state, the layered structure collapses to form a microporous structure with internal and external communication and adsorption function, and P is further absorbed 2 O 5 To make P in the boiler flue gas 2 O 5 The content is less than or equal to 5mg/Nm 3 Avoiding the corrosion of high-temperature phosphoric acid to boiler materials.
In the invention, the yellow phosphorus tail gas contains P besides CO 4 、PH 3 Etc. Preferably, in the step (1), the content of CO in the yellow phosphorus tail gas is 85-90 vol%, and P 4 The content is 300-700 mg/Nm 3 ，PH 3 The content is 500-9000 mg/Nm 3 。
In the invention, under the condition of no special description, P in yellow phosphorus tail gas and boiler flue gas 2 O 5 The three-stage absorption of the content sample is carried out by adopting an inductively coupled plasma emission spectrometer (ICP-AES method)Determination, first stage absorption tube was filled with 75mL (1+3) HNO 3 The second stage absorber tube was filled with 50mL (1+3) HNO 3 The third stage absorption tube contained 75mL distilled water.
In the present invention, the oxygen-containing gas includes, but is not limited to, air, oxygen, and the like.
In some embodiments of the invention, preferably, in step (1), the temperature of the combustion reaction is any value in the range of 750-950 ℃, e.g., 750 ℃, 800 ℃, 850 ℃, 900 ℃, 950 ℃, and any two numbers, preferably 800-900 ℃.
In the present invention, in the step (1), the combustion reaction aims at converting CO in the yellow phosphorus tail gas into CO 2 ，P 4 And pH (potential of Hydrogen) 3 Conversion to P 2 O 5 Obtaining the product containing CO and CO 2 、P 2 O 5 Is a high temperature flue gas.
In some embodiments of the invention, preferably, in step (1), the temperature of the high temperature flue gas is any value in the range of 750-950 ℃, e.g., 750 ℃, 800 ℃, 850 ℃, 900 ℃, 950 ℃, and any two numbers, preferably 800-900 ℃.
In some embodiments of the present invention, preferably, in the step (2), a mass ratio of the gangue powder calculated as CaO to the yellow phosphorus tail gas calculated as P is 3 to 8:1, e.g., 3:1, 4:1, 5:1, 6:1, 8:1, and any value in the range of any two values. The mass ratio in the range is satisfied, so that the dephosphorization agent not only has better dephosphorization effect, but also has lower energy consumption.
In the present invention, the gangue powder as CaO refers to the mass of carbonate as CaO in the gangue powder.
In the invention, the gangue powder needs to be screened before entering the furnace. Preferably, the average particle size of the gangue powder is less than or equal to 13mm. The smaller the particle size, the faster the dephosphorization reaction, but the external circulation amount and fly ash are increased; the particle size is too large, so that the mass transfer and reaction efficiency is reduced, and the abrasion of the boiler is increased.
In some embodiments of the present invention, preferably, the coal gangue powder contains carbonate, kaolinite, chlorite, carbon, and quartz; further preferably, in the gangue powder, the carbonate content is 1.5-20wt%, the kaolinite content is 15-35wt%, the chlorite content is 6-15wt%, the carbon content is 10-35wt%, and the quartz content is 8-20wt%. In the present invention, the carbonate in the gangue powder includes, but is not limited to, calcite.
In some embodiments of the present invention, preferably, in step (2), the calcining reaction comprises: s1, performing the calcination reaction on carbonate in the gangue powder to obtain metal oxide; s2, performing the calcination reaction on the kaolinite and the chlorite in the gangue powder to obtain an amorphous product; s3, reacting carbon in the gangue powder to provide heat for the calcination reaction; wherein the calcined reaction product comprises the metal oxide and an amorphous product.
In the present invention, the dephosphorization treatment not only comprises the step of adding the metal oxide in the calcined reaction product and the P in the high-temperature flue gas 2 O 5 Dephosphorizing to obtain phosphocalcic compounds, wherein the phosphocalcic compounds include but are not limited to calcium phosphate, white brushite and the like; the method further comprises the step of further removing P in the high-temperature flue gas from the amorphous product in the calcined reaction product through physical adsorption 2 O 5 。
In the invention, under the condition of no special condition, the temperature of the calcination reaction is mainly provided by the heat of the yellow phosphorus tail gas combustion reaction, and a small part of the heat is provided by carbon in the gangue powder, and the dephosphorization agent gangue powder has a certain heating value, so that the calcination reaction of carbonate and the reaction of phosphoric acid and metal oxide are accelerated. Preferably, in step (2), the temperature of the calcination reaction is in the range of from 750 to 950 ℃, for example 750 ℃, 800 ℃, 850 ℃, 900 ℃, 950 ℃, and any value in the range of any two values, preferably 800 to 900 ℃.
In one specific embodiment of the invention, the elemental phosphorus and phosphine gas contained in the yellow phosphorus tail gas react with air to produce P after combustion 2 O 5 ，P 2 O 5 And then combining with water to produce phosphoric acid, and combining with the aboveFurther reacting carbonate (such as calcite) in the gangue powder with metal oxide (calcium oxide) obtained by high-temperature calcination reaction to obtain phosphorus-oxygen-calcium compounds such as calcium phosphate, white phosphorus calcium stone and the like; and carrying out the calcination reaction with the kaolinite and chlorite in the gangue powder, and further absorbing P by the obtained amorphous product 2 O 5 Thereby achieving the purpose of dephosphorization.
In the present invention, the dephosphorization treatment aims at removing P in the high-temperature flue gas 2 O 5 . Preferably, P in the boiler flue gas 2 O 5 The content is less than or equal to 5mg/Nm 3 。
In some embodiments of the invention, preferably, in P 2 O 5 The phosphorus content in the dephosphorized slag is 0.5-5wt%.
In some embodiments of the present invention, preferably, in step (2), the heat exchange process includes: and carrying out heat exchange on the high-temperature dephosphorization flue gas and water to obtain the boiler flue gas and steam. In the invention, the boiler flue gas mainly contains CO 2 Trace of P 2 O 5 、SO 2 、NO，SO 2 NO is treated by a matched desulfurization and denitrification device.
In some embodiments of the invention, the temperature of the boiler flue gas is preferably any value in the range of 120-160 ℃, e.g., 120 ℃, 130 ℃, 140 ℃, 150 ℃, 160 ℃, and any two values.
In some embodiments of the invention, preferably, the method further comprises: and separating the low Wen Tuolin flue gas obtained by heat exchange to obtain the boiler flue gas. In the present invention, the separation is intended to remove ash and the like from the boiler flue gas.
The second aspect of the present invention provides a device for removing phosphorus from yellow phosphorus tail gas boiler with coal gangue powder, the structure of which is shown in fig. 1, and as can be seen from fig. 1, the device comprises: a fluidized bed gas boiler I;
the fluidized bed gas boiler I is used for carrying out combustion reaction on yellow phosphorus tail gas 1 and oxygen-containing gas 2 to obtain high-temperature flue gas; at the saidUnder the thermal action of the combustion reaction, the gangue powder 3 is fluidized and is subjected to the calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorization slag 4, and the obtained high Wen Tuolin flue gas is subjected to heat exchange to obtain boiler flue gas 5.
According to the invention, preferably, as shown in fig. 1, the device further comprises: and the separator II is connected with the fluidized bed gas boiler I and is used for separating the low-temperature dephosphorized flue gas 6 obtained by heat exchange to obtain the boiler flue gas 5.
According to a particularly preferred embodiment of the invention, a method for removing phosphorus in yellow phosphorus tail gas boilers by using coal gangue powder comprises the following steps:
(1) Carrying out combustion reaction on yellow phosphorus tail gas and oxygen-containing gas to obtain high-temperature flue gas;
(2) Under the thermal action of the combustion reaction, the gangue powder is fluidized and is subjected to calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorized slag, and the obtained high Wen Tuolin flue gas is subjected to heat exchange to obtain boiler flue gas;
wherein the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 3-8:1, a step of;
wherein the gangue powder contains carbonate, kaolinite, chlorite, carbon and quartz; the content of carbonate in the gangue powder is 1.5-20wt%; 15-35wt% of kaolinite, 6-15wt% of chlorite, 10-35wt% of carbon and 8-20wt% of quartz;
wherein the calcination reaction comprises the following steps: s1, performing the calcination reaction on carbonate in the gangue powder to obtain metal oxide; s2, performing the calcination reaction on the kaolinite and the chlorite in the gangue powder to obtain an amorphous product; s3, reacting carbon in the gangue powder to provide heat for the calcination reaction; wherein the calcined reaction product comprises the metal oxide and an amorphous product;
wherein, P in the boiler flue gas 2 O 5 The content is less than or equal to 5mg/Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the With P 2 O 5 The phosphorus content in the dephosphorized slag is 0.5-5wt%.
The present invention will be described in detail by examples.
Example 1
The structural schematic diagram of a device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder is shown in fig. 1, and the device comprises: and the fluidized bed gas boiler I and the separator II are connected in sequence.
The method for removing phosphorus in the yellow phosphorus tail gas boiler by using the gangue powder is carried out in the device, and comprises the following steps:
(1) The yellow phosphorus tail gas and oxygen are subjected to combustion reaction (the temperature is 750 ℃) to obtain high-temperature flue gas with the temperature of 750 ℃;
wherein the content of CO in the yellow phosphorus tail gas is 85% by volume, and P 4 The content is 300 mg/Nm 3 ，PH 3 The content is 500 mg/Nm 3 ；
(2) Under the heat of the combustion reaction, coal gangue powder (with the average grain diameter of 13mm, the content of each component is shown in table 1) is fluidized and calcined (with the temperature of 750 ℃), and the obtained calcined reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorization slag Q1 (the content of each component is shown in table 1), and the obtained high Wen Tuolin flue gas is subjected to heat exchange and separation in sequence to obtain boiler flue gas S1 (the temperature is 130 ℃);
the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 3:1;
wherein, P is 2 O 5 The phosphorus content in the dephosphorized slag Q1 is 2.83wt%; p in the boiler flue gas S1 2 O 5 The content is 5mg/Nm 3 。
TABLE 1
Example 2
The structural schematic diagram of a device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder is shown in fig. 1, and the device comprises: and the fluidized bed gas boiler I and the separator II are connected in sequence.
The method for removing phosphorus in the yellow phosphorus tail gas boiler by using the gangue powder is carried out in the device, and comprises the following steps:
(1) The yellow phosphorus tail gas and oxygen are subjected to combustion reaction (the temperature is 850 ℃) to obtain high-temperature flue gas with the temperature of 850 ℃;
wherein the content of CO in the yellow phosphorus tail gas is 88% by volume, and P 4 The content is 500 mg/Nm 3 ，PH 3 The content is 4000 mg/Nm 3 ；
(2) Under the thermal action of the combustion reaction, coal gangue powder (the average particle diameter is 10mm, the content of each component is shown in table 2) is fluidized and calcined (the temperature is 850 ℃), and the obtained calcined reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorization slag Q2 (the content of each component is shown in table 2), and the obtained high Wen Tuolin flue gas is subjected to heat exchange and separation in sequence to obtain boiler flue gas S2 (the temperature is 120 ℃);
the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 4:1;
wherein, P is 2 O 5 The phosphorus content in the dephosphorized slag Q2 is 2.75wt%; p in the boiler flue gas S2 2 O 5 The content is 4mg/Nm 3 。
TABLE 2
Example 3
The structural schematic diagram of a device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder is shown in fig. 1, and the device comprises: and the fluidized bed gas boiler I and the separator II are connected in sequence.
The method for removing phosphorus in the yellow phosphorus tail gas boiler by using the gangue powder is carried out in the device, and comprises the following steps:
(1) The yellow phosphorus tail gas and oxygen are subjected to combustion reaction (the temperature is 850 ℃) to obtain high-temperature flue gas with the temperature of 850 ℃;
wherein the content of CO in the yellow phosphorus tail gas is 88% by volume, and P 4 The content was 600 mg/Nm 3 ，PH 3 The content is 6000 mg/Nm 3 ；
(2) Under the thermal action of the combustion reaction, coal gangue powder (the average particle diameter is 9mm, the content of each component is shown in table 3) is fluidized and calcined (the temperature is 850 ℃), and the obtained calcined reaction product is matched with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorization slag Q3 (the content of each component is shown in table 3), and the obtained high Wen Tuolin flue gas is subjected to heat exchange and separation in sequence to obtain boiler flue gas S3 (the temperature is 140 ℃);
the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 6:1;
wherein, P is 2 O 5 The phosphorus content in the dephosphorized slag Q3 is 3.3wt%; p in the boiler flue gas S3 2 O 5 The content is 1mg/Nm 3 。
TABLE 3 Table 3
Example 4
The structural schematic diagram of a device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder is shown in fig. 1, and the device comprises: and the fluidized bed gas boiler I and the separator II are connected in sequence.
The method for removing phosphorus in the yellow phosphorus tail gas boiler by using the gangue powder is carried out in the device, and comprises the following steps:
(1) The yellow phosphorus tail gas and oxygen are subjected to combustion reaction (the temperature is 900 ℃) to obtain high-temperature flue gas with the temperature of 900 ℃;
wherein the content of CO in the yellow phosphorus tail gas is 90% by volume, and P 4 The content was 600 mg/Nm 3 ，PH 3 The content is 7000 mg/Nm 3 ；
（2）Under the thermal action of the combustion reaction, coal gangue powder (the average particle diameter is 10mm, the content of each component is shown in table 4) is fluidized and calcined (the temperature is 900 ℃), and the obtained calcined reaction product is matched with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorization slag Q4 (the content of each component is shown in table 4), and the obtained high Wen Tuolin flue gas is subjected to heat exchange and separation in sequence to obtain boiler flue gas S4 (the temperature is 140 ℃);
the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 6:1;
wherein, P is 2 O 5 The phosphorus content in the dephosphorized slag Q4 is 3.94wt%; p in the boiler flue gas S4 2 O 5 The content is 5mg/Nm 3 。
TABLE 4 Table 4
Example 5
The structural schematic diagram of a device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder is shown in fig. 1, and the device comprises: and the fluidized bed gas boiler I and the separator II are connected in sequence.
The method for removing phosphorus in the yellow phosphorus tail gas boiler by using the gangue powder is carried out in the device, and comprises the following steps:
(1) The yellow phosphorus tail gas and oxygen are subjected to combustion reaction (the temperature is 950 ℃) to obtain high-temperature flue gas with the temperature of 950 ℃;
wherein the content of CO in the yellow phosphorus tail gas is 90% by volume, and P 4 The content is 700 mg/Nm 3 ，PH 3 The content is 9000 mg/Nm 3 ；
(2) Under the heat of the combustion reaction, coal gangue powder (with the average particle diameter of 10mm, the content of each component is shown in table 5) is fluidized and calcined (with the temperature of 950 ℃), and the obtained calcined reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment was carried out to obtain dephosphorized slag Q5 (content of each component is shown in Table 5) and a high yield was obtainedWen Tuolin flue gas is subjected to heat exchange and separation in sequence to obtain boiler flue gas S5 (the temperature is 160 ℃);
the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 8:1;
wherein, P is 2 O 5 The phosphorus content in the dephosphorized slag Q5 is 4.21wt%; p in the boiler flue gas S5 2 O 5 The content is 5mg/Nm 3 。
TABLE 5
Example 6
The structural schematic diagram of a device for removing phosphorus in yellow phosphorus tail gas boiler by using gangue powder is shown in fig. 1, and the device comprises: and the fluidized bed gas boiler I and the separator II are connected in sequence.
The method for removing phosphorus in the yellow phosphorus tail gas boiler by using the gangue powder is carried out in the device, and comprises the following steps:
(1) The yellow phosphorus tail gas and oxygen are subjected to combustion reaction (the temperature is 950 ℃) to obtain high-temperature flue gas with the temperature of 950 ℃;
wherein the content of CO in the yellow phosphorus tail gas is 90% by volume, and P 4 The content is 700 mg/Nm 3 ，PH 3 The content is 9000 mg/Nm 3 ；
(2) Under the heat of the combustion reaction, coal gangue powder (with the average particle diameter of 10mm and the content of each component shown in Table 6) is fluidized and calcined (with the temperature of 950 ℃), and the obtained calcined reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorization slag Q6 (the content of each component is shown in table 6), and the obtained high Wen Tuolin flue gas is subjected to heat exchange and separation in sequence to obtain boiler flue gas S6 (the temperature is 160 ℃);
the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 8:1;
wherein, P is 2 O 5 The phosphorus content in the dephosphorized slag Q6 is 3.98wt%;p in the boiler flue gas S6 2 O 5 The content is 5mg/Nm 3 。
TABLE 6
Comparative example 1
Dephosphorization treatment is carried out on yellow phosphorus tail gas provided in example 3 according to a method of CN200910094045.9 to obtain P 2 O 5 The content is 5mg/Nm 3 Is characterized by dephosphorizing tail gas.
Compared with the embodiment 3, the comparative example 1 adopts different processes, has poorer dephosphorization effect, needs to use a special dephosphorization, desulfurization and dearsenization ternary catalytic oxidation catalyst, is formed by integrating a turbulent flow small amount of lime water washing dust removal system, a washing tower lime milk washing system for removing fluoride, part of arsenide and phosphorus and sulfur oxide systems, has more complex system and higher operation cost; meanwhile, in the dephosphorization process, the temperature of yellow phosphorus tail gas is heated to 110 ℃ by using steam, so that the energy consumption is high.
In example 3, the yellow phosphorus tail gas is directly used as fuel gas without being treated, so that the extra treatment of P in the yellow phosphorus tail gas is not needed 4 And pH (potential of Hydrogen) 3 The cost of the coal gangue solid waste can be fully utilized, the heat of the low-heat-value coal gangue can be recovered, and the operation is simple; the dephosphorization cost is mainly the transportation and grinding cost of the gangue, and the cost for treating yellow phosphorus tail gas per cubic meter can be as low as 0.02 yuan.
Comparative example 2
Purifying yellow phosphorus tail gas provided in example 3 according to the method of CN202010349884.7 to obtain P 2 O 5 The content is 1mg/Nm 3 Is characterized by dephosphorizing tail gas.
Comparative example 2A different process was used as compared with example 3, and while dephosphorization was the same, comparative example 2 heated yellow phosphorus tail gas to 450℃by a gas (nitrogen, inert gas or steam) circulation heating system, and then P was selectively catalyzed by a catalyst 4 And pH (potential of Hydrogen) 3 Is phosphorus oxide, and the tail gas is cooled and then passes through a spray absorbentAbsorbing the phosphorus oxide. Obviously, comparative example 2 has a long process flow, and the heating of the gas to 450 ℃ requires a large energy consumption and also requires the use of a catalyst.
While in example 3, under the condition of realizing the same dephosphorization effect, the dephosphorization cost is mainly the transportation and ore grinding cost of the coal gangue, and the cost for treating the yellow phosphorus tail gas per cubic meter can be as low as 0.02 yuan.
Compared with comparative examples 1-2, examples 1-6 adopt coal gangue as dephosphorizing agent, dephosphorize with yellow phosphorus tail gas in high temperature combustion of gas boiler, remove elemental phosphorus and PH contained in yellow phosphorus tail gas 3 Dephosphorization slag is obtained, and the method utilizes coal gangue with low heat value to realize the removal of phosphorus in yellow phosphorus tail gas, namely P in boiler flue gas while recovering the reaction heat of the yellow phosphorus tail gas 2 O 5 The content is less than or equal to 5mg/Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the The method provided by the invention avoids the phosphoric acid corrosion generated by taking yellow phosphorus tail gas as boiler gas, prolongs the operation period of gas boiler equipment, and effectively reduces the energy consumption and the production cost.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (8)
1. The method for removing phosphorus in yellow phosphorus tail gas boiler by using coal gangue powder is characterized by comprising the following steps:
(1) Carrying out combustion reaction on yellow phosphorus tail gas and oxygen-containing gas to obtain high-temperature flue gas;
(2) Under the thermal action of the combustion reaction, the gangue powder is fluidized and is subjected to calcination reaction, and the obtained calcination reaction product is mixed with P in the high-temperature flue gas 2 O 5 Dephosphorization treatment is carried out to obtain dephosphorized slag, and the obtained high Wen Tuolin flue gas is subjected to heat exchange to obtain boiler flue gas;
wherein the mass ratio of the gangue powder calculated by CaO to the yellow phosphorus tail gas calculated by P is 3-8:1, the coal gangue powder calculated by CaO refers to the mass of carbonate calculated by CaO in the coal gangue powder; the gangue powder contains carbonate, kaolinite, chlorite, carbon and quartz;
wherein the calcination reaction comprises the following steps: s1, performing the calcination reaction on carbonate in the gangue powder to obtain metal oxide; s2, performing the calcination reaction on the kaolinite and the chlorite in the gangue powder to obtain an amorphous product; s3, reacting carbon in the gangue powder to provide heat for the calcination reaction; wherein the calcined reaction product comprises the metal oxide and an amorphous product.
2. The method according to claim 1, wherein in the step (1), the content of CO in the yellow phosphorus tail gas is 85-90% by volume, and P 4 The content is 300-700 mg/Nm 3 ，PH 3 The content is 500-9000 mg/Nm 3 。
3. The method of claim 1, wherein the gangue powder has an average particle size of 13mm or less.
4. The method of claim 1, wherein in the step (2), the carbonate content is 1.5-20wt%, the kaolin content is 15-35wt%, the chlorite content is 6-15wt%, the carbon content is 10-35wt%, and the quartz content is 8-20wt%.
5. The method of claim 1, wherein the temperature of the combustion reaction, high temperature flue gas, and calcination reaction are all 750-950 ℃.
6. The method of any one of claims 1-5, wherein P in the boiler flue gas 2 O 5 The content is less than or equal to 5mg/Nm 3 ；
And/or, with P 2 O 5 The phosphorus content in the dephosphorized slag is 0.5-5wt%.
7. The method of any of claims 1-5, wherein the heat exchanging process comprises: carrying out the heat exchange on the high-temperature dephosphorization flue gas and water to obtain the boiler flue gas and steam;
and/or the temperature of the boiler flue gas is 120-160 ℃.
8. The method of any of claims 1-5, wherein the method further comprises: and separating the low Wen Tuolin flue gas obtained by heat exchange to obtain the boiler flue gas.
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