CN213569554U - Magnesium nitrate pyrolysis device based on resource cyclic utilization - Google Patents
Magnesium nitrate pyrolysis device based on resource cyclic utilization Download PDFInfo
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Abstract
The utility model discloses a magnesium nitrate pyrolysis device based on resource cyclic utilization belongs to metallurgical equipment technical field, and the structure includes that raw materials melts jar, raw materials melt heater, spray drier, direct combustion formula whirl developments and forges burning furnace, forges burning furnace cyclone, magnesium oxide powder material ageing feed bin and magnesium oxide powder material product feed bin, and each part is connected in order of sequence. The device structure of the utility model can realize the partial circulation of the pyrolysis gas, and utilize the oxygen generated by pyrolysis to support combustion for the fuel of the direct-combustion type rotational flow dynamic calciner; the improvement of the device can greatly simplify the process flow, has high automation degree, short calcination period, cyclic utilization of resources and environmental protection, and can realize the production of high-quality magnesium oxide.
Description
The technical field is as follows:
the utility model belongs to the technical field of metallurgical equipment, concretely relates to magnesium nitrate pyrolysis device based on resource cyclic utilization.
Background art:
the content of magnesium in the laterite-nickel ore is high, in the hydrometallurgical production of the laterite-nickel ore, most of magnesium in the ore is dissolved out together with nickel and enters a solution, a large amount of low-concentration magnesium-containing aqueous solution is produced in the subsequent processes of neutralizing a leaching solution with alkali and precipitating and separating nickel hydroxide from the leaching solution, and a byproduct magnesium nitrate can be obtained through concentration. If the byproducts can not be reasonably utilized, a large amount of resources can be wasted, the environment can be seriously harmed, and the method becomes a key engineering technical obstacle for the popularization of hydrometallurgy. And the novel equipment structure improvement based on the corresponding process change is not provided.
The utility model has the following contents:
the utility model aims at overcoming the defects existing in the prior art and providing a magnesium nitrate pyrolysis device based on resource recycling. To above-mentioned engineering problem and market demand, in order to overcome the problem that exists among the prior art, the utility model provides a new pyrolysis device based on this structural style, can further simplify process flow to realize laterite-nickel ore deposit hydrometallurgy by-product magnesium nitrate's resource rational utilization and innoxious emission.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a magnesium nitrate pyrolysis device based on resource recycling comprises a raw material melting tank, a raw material melting tank waste gas fan, a waste gas dehumidifier, a conveying pump, a raw material melt heater, a spray dryer, a spray drying bag filter, a spray drying hot air cyclone separator, a material preheating cyclone separator, a direct combustion type rotational flow dynamic calcining furnace pyrolysis gas recycling fan, a calcining furnace cyclone separator, a magnesium oxide powder aging bin, a magnesium oxide powder conveying blower, a magnesium oxide powder product bin, a magnesium oxide powder cyclone separator and a magnesium oxide powder bag filter; wherein:
the raw material melting tank, the raw material melt heater, the spray dryer, the material preheating cyclone separator, the direct-fired type cyclone dynamic calcining furnace, the calcining furnace cyclone separator, the magnesium oxide powder aging bin, the magnesium oxide powder cyclone separator and the magnesium oxide powder product bin are sequentially connected;
the spray dryer is also connected with a spray drying bag type filter, the spray drying bag type filter is respectively connected with a melt heater and a material preheating cyclone separator, the material preheating cyclone separator is connected with a spray drying hot air cyclone separator, and the spray drying hot air cyclone separator is respectively connected with the spray dryer and a direct-fired cyclone dynamic calciner pyrolysis gas recycling fan;
the calciner cyclone separator is also connected with a material preheating cyclone separator, the magnesia powder cyclone separator is also connected with a magnesia powder bag filter, and the magnesia powder bag filter is also respectively connected with a magnesia powder product bin and the direct-fired cyclone dynamic calciner.
The raw material melting tank is connected with a raw material melting tank waste gas fan, the waste gas fan is connected with a waste gas dehumidifier, the waste gas dehumidifier is connected with an acid absorption device, and the raw material melting tank is connected with a raw material melt heater through a delivery pump.
The top of the spray dryer is provided with an atomizing nozzle, the lower side of the spray dryer is provided with a magnesium nitrate powder discharger, the bottom of the spray dryer is provided with an air inlet, and the top of the spray dryer is provided with an air outlet;
the lower part of the material preheating cyclone separator is provided with a magnesium nitrate and magnesium oxide powder discharger.
An outlet pipeline of the raw material melting tank is communicated with an inlet of a delivery pump, an outlet pipeline of the delivery pump is communicated with an inlet of a raw material melt heater, and an outlet pipeline of the raw material melt heater is communicated with an atomizing nozzle; the outlet of a magnesium nitrate and magnesium oxide powder discharger at the lower side of the spray dryer is communicated with an inlet pipeline at the upper part of the material preheating cyclone separator, and the outlet of the magnesium nitrate and magnesium oxide powder discharger at the lower part of the material preheating cyclone separator is communicated with a magnesium nitrate powder feeding pipeline of the direct-fired cyclone dynamic calcining furnace; the waste gas outlet of the spray dryer is communicated with the gas inlet pipeline of the spray drying bag type filter, the gas outlet of the spray drying bag type filter is communicated with the heated gas inlet pipeline of the raw material melt heater, the heated gas outlet of the raw material melt heater is communicated with the heated gas inlet pipeline of the raw material melting tank, the heated gas outlet of the raw material melting tank is communicated with the waste gas fan inlet of the raw material melting tank, the waste gas fan outlet of the raw material melting tank is communicated with the gas inlet of the waste gas dehumidifier, and the gas outlet of the waste gas dehumidifier is communicated with the gas feeding pipeline of the acid absorption device.
The gas inlet of the direct-fired rotational flow dynamic calciner is communicated with a fuel pipeline, a combustion air pipeline and an outlet pipeline of a pyrolysis gas recycling gas fan of the direct-fired rotational flow dynamic calciner; the material outlet of the direct-fired cyclone dynamic calciner is communicated with a material inlet pipeline of a cyclone separator of the calciner, the powder outlet of the cyclone separator of the calciner is communicated with a powder inlet pipeline of a magnesia powder aging bin, the powder outlet of the magnesia powder aging bin is communicated with an outlet pipeline of a magnesia powder conveying and feeding machine, the powder outlet of the magnesia powder aging bin is also communicated with the material inlet pipeline of the magnesia powder cyclone separator, and the powder outlet of the magnesia powder cyclone separator is communicated with an inlet pipeline of a magnesia product bin; the gas outlet of the magnesia powder cyclone separator is communicated with a gas inlet pipeline of a magnesia powder bag filter, and the gas outlet of the magnesia powder bag filter is communicated with a combustion-supporting gas inlet pipeline of a direct-fired rotational flow dynamic calciner; the gas outlet of the calciner cyclone separator is communicated with a gas inlet pipeline of a material preheating cyclone separator, the gas outlet of the material preheating cyclone separator is communicated with a gas inlet pipeline of a spray drying hot air cyclone separator, the gas outlet of the spray drying hot air cyclone separator is communicated with a hot air inlet pipeline of a spray dryer, and the gas outlet of the spray drying hot air cyclone separator is also communicated with an inlet pipeline of a pyrolysis gas recycling fan of a direct-fired cyclone dynamic calciner.
A magnesium nitrate pyrolysis method based on resource recycling adopts the device, and magnesium nitrate pyrolysis is carried out in two stages; firstly, removing a large amount of water in a spray drying stage to obtain magnesium nitrate and a small amount of magnesium oxide, and secondly, pyrolyzing the magnesium nitrate in a pyrolysis stage of the direct-fired cyclone dynamic calciner to generate magnesium oxide, nitrogen dioxide and oxygen; the method specifically comprises the following steps:
(1) putting magnesium nitrate hexahydrate raw materials into a raw material melting tank 1, and heating to form a melt;
(2) conveying the melt to a raw material melt heater 14 through a conveying pump to be heated continuously to form a high-temperature melt;
(3) the high-temperature melt is atomized by an atomizing nozzle and then sprayed into a spray dryer 2 for drying and pyrolysis reaction to obtain a dried-pyrolysis product, the top of the spray dryer 2 discharges dry waste gas, at the moment, pyrolysis gas is separated from a gas outlet of a calciner cyclone 33, the preheated-pyrolysis product is preheated by a material preheating cyclone 32, discharged from the gas outlet of the material preheating cyclone and enters a spray drying hot air cyclone 21 to realize gas-solid separation, and the preheated dried-pyrolysis product is obtained at the same time;
in the step (3), the drying-pyrolysis product comprises 98.6% of magnesium nitrate and 1.4% of magnesium oxide by mass.
(4) The preheated drying-pyrolysis product enters the direct-fired rotational flow dynamic calciner 3 through a magnesium nitrate powder feeding pipeline for carrying out pyrolysis reaction, and magnesium nitrate is pyrolyzed to generate magnesium oxide, nitrogen dioxide and oxygen; pyrolysis gas containing nitrogen dioxide, nitrogen, carbon dioxide, water and oxygen enters a calciner cyclone separator 33 together with magnesia through a material outlet of a direct-fired cyclone dynamic calciner 3 to separate magnesia powder and pyrolysis gas, wherein:
(4-1) feeding the magnesium oxide powder into a magnesium oxide powder ageing bin 34 for ageing; the aged magnesia powder is sent to a magnesia powder cyclone separator 35 by air to separate magnesia and conveying gas, wherein:
(4-1-1) feeding the magnesium oxide into a magnesium oxide product bin 37;
(4-1-2) the conveying gas enters a magnesium oxide powder bag filter 36, hot air is obtained after gas-solid separation of the magnesium oxide powder bag filter 36, and the hot air enters a combustion-supporting gas inlet of the direct-fired rotational flow dynamic calciner 3 through a gas outlet to support combustion of the fuel of the direct-fired rotational flow dynamic calciner 3;
(4-2) the pyrolysis gas is circulated to the step (3), the dry-pyrolysis product powder is preheated by the material preheating cyclone separator 32, then enters the spray drying hot air cyclone separator 21, the pyrolysis gas is separated from the gas outlet, and the pyrolysis gas is circulated to the step (3), specifically:
(4-2-1) allowing 65% of pyrolysis gas in volume percentage to enter a pyrolysis gas recycling inlet of the direct-fired rotational flow dynamic calciner 3 through a pyrolysis gas recycling fan 39, and supporting combustion for fuel of the direct-fired rotational flow dynamic calciner 3 by using oxygen contained in the pyrolysis gas;
(4-2-2) feeding 35% by volume of the pyrolysis gas into the spray dryer 2, and heating the material in the spray dryer 2; the dry waste gas a coming out from the top of the spray dryer 2 enters a spray drying bag filter 22 for gas-solid separation, the dry waste gas b separated from the spray drying bag filter 22 sequentially enters a raw material melt heater 14 and a raw material melting tank 1 for heating the magnesium nitrate hexahydrate melt and melting magnesium nitrate hexahydrate crystals to generate heating waste gas, and the heating waste gas is subjected to temperature reduction, dehumidification, deacidification and absorption.
In the step (1), the magnesium nitrate raw material is magnesium nitrate hexahydrate as a byproduct in the hydrometallurgical production of the laterite nickel ore, and Mg (NO) in the magnesium nitrate hexahydrate3)2·6H2The mass content of O is more than 99 percent.
In the step (1), the temperature of the raw material melting tank 1 for melting the magnesium nitrate hexahydrate is 100-110 ℃, the pressure is 0.2-0.25 MPa, and the melting time of the magnesium nitrate hexahydrate is 1.5-2 h.
In the step (2), the temperature of the raw material melt heater 14 is 240-260 ℃, the pressure is 0.6-0.65 MPa, and the heating time of the raw material melt is 0.5-0.75 h.
In the step (3), the drying-pyrolysis product comprises 98.3-98.8% of magnesium nitrate and 1.2-1.7% of magnesium oxide by mass percent.
In the step (3), the temperature of the pyrolysis gas separated from the gas outlet of the calciner cyclone separator 33 is 600-620 ℃.
In the step (3), pyrolysis gas separated from a gas outlet after gas-solid separation by the spray drying hot air cyclone separator 21 enters a hot air inlet of the spray dryer 2 by 35% of the pyrolysis gas in volume proportion to heat the material in the spray dryer 2; 65 volume percent of the hot gas enters a pyrolysis gas recycling inlet of the direct-fired rotational flow dynamic calciner 3 to support combustion for the fuel of the direct-fired rotational flow dynamic calciner 3;
in the step (3), 35% of the pyrolysis gas enters a hot air inlet of the spray dryer 2 according to the volume ratio, the air inlet temperature is 440-450 ℃, after spray drying, the top of the pyrolysis gas discharges the drying waste gas, the temperature of the drying waste gas is 340-350 ℃, and the pressure in the spray dryer 2 is 0.05-0.1 MPa.
In the step (4), the temperature of the pyrolysis product preheated by the material preheating cyclone separator is 500-550 ℃.
In the step (4), pyrolysis gas and magnesium oxide enter the calciner cyclone separator 33 through the material outlet of the direct-fired cyclone dynamic calciner 3, and the outlet temperature of the direct-fired cyclone dynamic calciner 3 is 690-700 ℃.
In the step (4-1-1), the MgO mass percentage content in the obtained magnesium oxide product is 98.3-99.2%.
In the step (4-2-2), 35% volume of pyrolysis gas is used as heating gas for preheating materials, spray drying, melting raw materials and heating melts.
In the step (4-2-2), the temperature of the drying exhaust gas a from the top of the spray dryer 2 is 330 ℃ to 360 ℃.
In the step (4-2-2), the temperature of the heating waste gas is 280-300 ℃.
In the step (4-2-2), heating waste gas enters a jacket of the raw material melting tank 1 and a heating coil in the tank through a raw material melt heater 14, and magnesium nitrate hexahydrate crystals are heated and melted; the heated waste gas enters a waste gas dehumidifier 25 through a raw material melting tank waste gas fan 23 to be cooled and dehumidified, and the cooled and dehumidified waste gas enters an acid absorption device to be used for preparing nitric acid.
In the step (4-2-2), after the heating waste gas is cooled and dehumidified, NO is detected2The volume concentration is 29-30 percent, and the deacidification and absorption are carried out to prepare acid, so that the cost of preparing acid from nitrogen dioxide is reduced, and the investment of acid preparation equipment is reduced。
In the step (4), the temperature in the direct-fired rotational flow dynamic calcining furnace 3 is 1000-1200 ℃, the pressure in the furnace is 0.02-0.03 MPa, and the calcining time is 4-6 s.
In the step (4), the aging time of the magnesium oxide powder aging bin is 30-40 min, the temperature in the bin is 580-600 ℃, and the pressure is normal pressure.
In the step (4), the aged magnesium oxide powder is sent to a magnesium oxide powder cyclone separator 35 by using cold air, magnesium oxide and conveying gas are separated, the magnesium oxide enters a magnesium oxide product bin 37, the conveying gas enters a magnesium oxide powder bag filter 36, and the magnesium oxide enters a combustion-supporting gas inlet of the direct-fired cyclone dynamic calciner 3 through a gas outlet of the magnesium oxide powder bag filter 36 to support combustion of the fuel of the direct-fired cyclone dynamic calciner 3.
In the step (4), the pyrolysis gas comprises the following components in percentage by mol: o is2 2.30％～2.50％，N2 48.35％～50.04％，CO2 8.00％～9.00％，H2O 14.5％～16.00％，NO2 23.96％～25.50％。
In the step (4), the energy supply source based on the pyrolysis reaction in the direct-fired rotational flow dynamic calciner 3 comprises natural gas, hot air obtained after gas-solid separation of the magnesium oxide powder bag filter 36 in the step (4-1-2) and oxygen contained in 65% volume proportion of pyrolysis gas in the step (4-2-1) realize combustion supporting, and 30% of fresh oxygen can be replaced; wherein:
the molar flow of the pyrolysis gas is as follows: o is2 25.52kmol/hr～28.53kmol/hr，N2 522.00kmol/hr～535.00kmol/hr，CO2 90.57kmol/hr～93.36kmol/hr，H2O 181.58kmol/hr～187.23kmol/hr，NO2 278.54kmol/hr～289.42kmol/hr。
The molar flow of the natural gas is as follows: 48.5 kmol/hr-52.5 kmol/hr;
the hot air molar flow rate is as follows: o is2 70kmol/hr～80kmol/hr，N2 263kmol/hr～301kmol/hr。
In the steps of the method, the related cyclone separator and the bag filter are used for realizing gas-solid separation of the material entering the component so as to realize separation of gas in the material and the corresponding entrained solid material.
The utility model has the advantages that:
the device structure of the utility model can realize the partial circulation of the pyrolysis gas, and utilize the oxygen generated by pyrolysis to support combustion for the fuel of the direct-combustion type rotational flow dynamic calciner; the concentration of the nitrogen dioxide gas is improved to the maximum extent, the volume concentration of the nitrogen dioxide gas is improved from 8.5 percent of that of the nitrogen dioxide gas which is not circulated to 29 to 30 percent of that of the nitrogen dioxide gas which is circulated by adopting pyrolysis gas, so that the cost of preparing acid from the nitrogen dioxide is reduced, and the investment of acid preparing equipment is reduced; the other part of the pyrolysis gas is used as a heating gas as a heat source for preheating materials, spray drying, melting raw materials and heating melts, the pyrolysis gas has high temperature, and the heat carried by the pyrolysis gas is recycled to improve the heat efficiency of the system; the improvement of the device can greatly simplify the process flow, the automation degree is high, the calcination period is short, the resource is recycled, the environment is friendly, the high-quality magnesium oxide can be produced, the content of the magnesium oxide in the product reaches 98.3 percent (by mass), the average particle size is 450nrn, the comprehensive index of the device is superior to the chemical standard of light magnesium oxide in HGT2573-2012 industry, and the device is used for realizing reasonable utilization and harmless emission of the resource of the byproduct magnesium nitrate in the laterite-nickel ore hydrometallurgy. Compared with a system for carrying out magnesium nitrate atomization pyrolysis by adopting heat accumulating type circulation heating, the energy is saved by 50 percent.
Description of the drawings:
fig. 1 is the utility model discloses embodiment 1's magnesium nitrate pyrolysis device based on resource cyclic utilization schematic structure: wherein:
1. a raw material melting tank 11, a mechanical seal stirrer 12, a heating coil 13, a melt delivery pump 14 and a melt heater; 2. a spray dryer 21, a spray drying hot air cyclone separator 22, a spray drying bag filter 23, a raw material melting tank waste gas fan 24, an atomizing nozzle 25 and a waste gas dehumidifier; 3. the device comprises a direct-fired cyclone dynamic calciner, 31, a combustor, 32, a material preheating cyclone separator, 33, a calciner cyclone separator, 34, a magnesium oxide powder aging bin, 35, a magnesium oxide powder cyclone separator, 36, a magnesium oxide powder bag filter, 37, a magnesium oxide powder product bin, 38, a magnesium oxide powder conveying blower, 39 and a direct-fired cyclone dynamic calciner pyrolysis gas recycling fan.
The specific implementation mode is as follows:
the present invention will be described in further detail with reference to examples.
A magnesium nitrate pyrolysis device based on resource recycling comprises a raw material melting tank, a raw material melting tank waste gas fan, a waste gas dehumidifier, a conveying pump, a raw material melt heater, a spray dryer, a spray drying bag filter, a spray drying hot air cyclone separator, a material preheating cyclone separator, a direct combustion type rotational flow dynamic calcining furnace pyrolysis gas recycling fan, a calcining furnace cyclone separator, a magnesium oxide powder aging bin, a magnesium oxide powder conveying blower, a magnesium oxide powder product bin, a magnesium oxide powder cyclone separator and a magnesium oxide powder bag filter; wherein:
the raw material melting tank, the raw material melt heater, the spray dryer, the material preheating cyclone separator, the direct-fired type cyclone dynamic calcining furnace, the calcining furnace cyclone separator, the magnesium oxide powder aging bin, the magnesium oxide powder cyclone separator and the magnesium oxide powder product bin are sequentially connected;
the spray dryer is also connected with a spray drying bag type filter, the spray drying bag type filter is respectively connected with a melt heater and a material preheating cyclone separator, the material preheating cyclone separator is connected with a spray drying hot air cyclone separator, and the spray drying hot air cyclone separator is respectively connected with the spray dryer and a direct-fired cyclone dynamic calciner pyrolysis gas recycling fan;
the calciner cyclone separator is also connected with a material preheating cyclone separator, the magnesia powder cyclone separator is also connected with a magnesia powder bag filter, and the magnesia powder bag filter is also respectively connected with a magnesia powder product bin and the direct-fired cyclone dynamic calciner.
The raw material melting tank is connected with a raw material melting tank waste gas fan, the waste gas fan is connected with a waste gas dehumidifier, the waste gas dehumidifier is connected with an acid absorption device, and the raw material melting tank is connected with a raw material melt heater through a delivery pump.
The top of the spray dryer is provided with an atomizing nozzle, the lower side of the spray dryer is provided with a magnesium nitrate powder discharger, the bottom of the spray dryer is provided with an air inlet, and the top of the spray dryer is provided with an air outlet;
the lower part of the material preheating cyclone separator is provided with a magnesium nitrate powder discharger.
An outlet pipeline of the raw material melting tank is communicated with an inlet of a delivery pump, an outlet pipeline of the delivery pump is communicated with an inlet of a raw material melt heater, and an outlet pipeline of the raw material melt heater is communicated with an atomizing nozzle; an outlet of a magnesium nitrate powder discharger at the lower side of the spray dryer is communicated with an inlet pipeline at the upper part of the material preheating cyclone separator, and an outlet of the magnesium nitrate powder discharger at the lower part of the material preheating cyclone separator is communicated with a magnesium nitrate powder feeding pipeline of the direct-fired cyclone dynamic calcining furnace; the waste gas outlet of the spray dryer is communicated with the gas inlet pipeline of the spray drying bag type filter, the gas outlet of the spray drying bag type filter is communicated with the heated gas inlet pipeline of the raw material melt heater, the heated gas outlet of the raw material melt heater is communicated with the heated gas inlet pipeline of the raw material melting tank, the heated gas outlet of the raw material melting tank is communicated with the waste gas fan inlet of the raw material melting tank, the waste gas fan outlet of the raw material melting tank is communicated with the gas inlet of the waste gas dehumidifier, and the gas outlet of the waste gas dehumidifier is communicated with the gas feeding pipeline of the acid absorption device.
The gas inlet of the direct-fired rotational flow dynamic calciner is communicated with a fuel pipeline, a combustion air pipeline and an outlet pipeline of a pyrolysis gas recycling gas fan of the direct-fired rotational flow dynamic calciner; the material outlet of the direct-fired cyclone dynamic calciner is communicated with a material inlet pipeline of a cyclone separator of the calciner, the powder outlet of the cyclone separator of the calciner is communicated with a powder inlet pipeline of a magnesia powder aging bin, the powder outlet of the magnesia powder aging bin is communicated with an outlet pipeline of a magnesia powder conveying and feeding machine, the powder outlet of the magnesia powder aging bin is also communicated with the material inlet pipeline of the magnesia powder cyclone separator, and the powder outlet of the magnesia powder cyclone separator is communicated with an inlet pipeline of a magnesia product bin; the gas outlet of the magnesia powder cyclone separator is communicated with a gas inlet pipeline of a magnesia powder bag filter, and the gas outlet of the magnesia powder bag filter is communicated with a combustion-supporting gas inlet pipeline of a direct-fired rotational flow dynamic calciner; the gas outlet of the calciner cyclone separator is communicated with a gas inlet pipeline of a material preheating cyclone separator, the gas outlet of the material preheating cyclone separator is communicated with a gas inlet pipeline of a spray drying hot air cyclone separator, the gas outlet of the spray drying hot air cyclone separator is communicated with a hot air inlet pipeline of a spray dryer, and the gas outlet of the spray drying hot air cyclone separator is also communicated with an inlet pipeline of a pyrolysis gas recycling fan of a direct-fired cyclone dynamic calciner.
A magnesium nitrate pyrolysis method based on resource recycling adopts the device, and magnesium nitrate pyrolysis is carried out in two stages; firstly, removing a large amount of water in a spray drying stage to obtain magnesium nitrate and a small amount of magnesium oxide, and secondly, pyrolyzing the magnesium nitrate in a pyrolysis stage of the direct-fired cyclone dynamic calciner to generate magnesium oxide, nitrogen dioxide and oxygen; the method specifically comprises the following steps:
(1) putting magnesium nitrate hexahydrate raw material into a raw material melting tank 1, and heating to form a melt, wherein the melting temperature is 100-110 ℃, the pressure in the tank is 0.2-0.25 MPa, and the melting time is 1.5-2 h; wherein the magnesium nitrate raw material is magnesium nitrate hexahydrate byproduct in the hydrometallurgical production of laterite-nickel ore, and Mg (NO) in the magnesium nitrate hexahydrate3)2·6H2The mass content of O is more than 99 percent.
(2) Conveying the melt to a raw material melt heater 14 through a conveying pump to be heated continuously to form a high-temperature melt, wherein the temperature of the raw material melt heater 14 is 240-260 ℃, the pressure is 0.6-0.65 MPa, and the heating time of the raw material melt is 0.5-0.75 h;
(3) atomizing the high-temperature melt by an atomizing nozzle, spraying the atomized high-temperature melt into a spray dryer 2, and carrying out drying and pyrolysis reaction to obtain a drying-pyrolysis product, wherein the drying-pyrolysis product comprises 98.3-98.8% of magnesium nitrate and 1.2-1.7% of magnesium oxide in percentage by mass; at the moment, pyrolysis gas is separated from a gas outlet of a calciner cyclone separator 33, the temperature is 600-620 ℃, the pyrolysis gas is used for preheating a drying-pyrolysis product through a material preheating cyclone separator 32, the gas is discharged from a gas outlet of the material preheating cyclone separator and enters a spray drying hot air cyclone separator 21 to realize gas-solid separation, simultaneously the preheated drying-pyrolysis product is obtained, the pyrolysis gas is separated from the gas outlet after the gas-solid separation through the spray drying hot air cyclone separator 21, 35% of the pyrolysis gas in volume proportion enters a hot air inlet of a spray dryer 2, the inlet air temperature is 440-450 ℃, the material in the spray dryer 2 is heated, the pressure in the spray dryer 2 is 0.05-0.1 MPa, after spray drying, dry waste gas is discharged from the top, the temperature of the dry waste gas is 340-350 ℃, 65% of the hot gas in volume proportion enters a gas recycling inlet of a direct combustion type cyclone dynamic calciner 3, supporting combustion for the direct combustion type rotational flow dynamic calciner 3;
(4) the preheated drying-pyrolysis product is at a temperature of 500-550 ℃, enters a direct-fired rotational flow dynamic calciner 3 through a magnesium nitrate powder feeding pipeline for carrying out pyrolysis reaction, the temperature in the calciner 3 is 1000-1200 ℃, the pressure in the calciner is 0.02-0.03 MPa, the calcination time is 4-6 s, and magnesium nitrate is pyrolyzed to generate magnesium oxide, nitrogen dioxide and oxygen; pyrolysis gas containing nitrogen dioxide, nitrogen, carbon dioxide, water and oxygen and magnesium oxide enter a calciner cyclone separator 33 through a material outlet (outlet temperature is 690 ℃ -700 ℃) of a direct-fired cyclone dynamic calciner 3 to separate magnesium oxide powder and the pyrolysis gas, wherein: the pyrolysis gas comprises the following components in percentage by mole: o is2 2.30％～2.50％，N2 48.35％～50.04％，CO2 8.00％～9.00％，H2O 14.5％～16.00％，NO223.96% -25.50%, the energy supply source based on the pyrolysis reaction in the direct-fired rotational flow dynamic calciner 3 comprises natural gas, hot air obtained after gas-solid separation of the magnesium oxide powder bag filter 36 in the step (4-1-2) and oxygen contained in 65% volume proportion of pyrolysis gas in the step (4-2-1) realize combustion supporting and can replace 30% of oxygen; wherein:
molar flow of pyrolysis gas: o is2 25.52kmol/hr～28.53kmol/hr，N2 522.00kmol/hr～535.00kmol/hr，CO2 90.57kmol/hr～93.36kmol/hr，H2O 181.58kmol/hr～187.23kmol/hr，NO2 278.54kmol/hr～289.42kmol/hr。
Molar flow of natural gas: 48.5 kmol/hr-52.5 kmol/hr;
hot air molar flow: o is2 70kmol/hr～80kmol/hr，N2 263kmol/hr～301kmol/hr。
(4-1) allowing the magnesium oxide powder to enter a magnesium oxide powder aging bin 34 for aging, wherein the aging time is 30-40 min, the temperature in the bin is 580-600 ℃, and the pressure is normal pressure; the aged magnesia powder is sent to a magnesia powder cyclone separator 35 by air to separate magnesia and conveying gas, wherein:
(4-1-1) allowing the magnesium oxide to enter a magnesium oxide product bin 37, wherein the mass percentage of MgO in the obtained magnesium oxide product is 98.3% -99.2%;
(4-1-2) conveying gas into a magnesium oxide powder bag filter 36, carrying out gas-solid separation through the magnesium oxide powder bag filter 36 to obtain hot air, and feeding the hot air into a combustion-supporting gas inlet of the direct-fired rotational flow dynamic calciner 3 through a gas outlet to support combustion of fuel of the direct-fired rotational flow dynamic calciner 3;
(4-2) the pyrolysis gas is circulated to the step (3), the dry-pyrolysis product powder is preheated by the material preheating cyclone separator 32, then enters the spray drying hot air cyclone separator 21, the pyrolysis gas is separated from the gas outlet, and the pyrolysis gas is circulated to the step (3), specifically:
(4-2-1) allowing 65% of pyrolysis gas in volume percentage to enter a pyrolysis gas recycling inlet of the direct-fired rotational flow dynamic calciner 3 through a pyrolysis gas recycling fan 39, and supporting combustion for fuel of the direct-fired rotational flow dynamic calciner 3 by using oxygen contained in the pyrolysis gas;
(4-2-2) feeding 35% by volume of the pyrolysis gas into the spray dryer 2, and heating the material in the spray dryer 2; the drying waste gas a coming out from the top of the spray dryer 2 is at the temperature of 330-360 ℃, the drying waste gas a enters the spray drying bag filter 22 for gas-solid separation, and the drying waste gas b separated from the spray drying bag filter 22 enters the raw material melt heater 14 and the raw material melting tank 1 in sequence for heating sixThe magnesium nitrate melt and the magnesium nitrate hexahydrate crystal are melted, heating waste gas is generated, the temperature is 280-300 ℃, and after the heating waste gas is cooled and dehumidified, NO is detected2The volume concentration is 29-30%, and the acid is removed and absorbed.
In the embodiment of the utility model, the raw material Mg (NO)3)2·6H2The mass content of O is 99.4%. In the embodiment of the utility model, the mass content of the MgO product is more than 98%.
Example 1
A magnesium nitrate pyrolysis device based on resource recycling is shown in a schematic structural diagram of a figure 1 and comprises a raw material melting tank 1, a raw material melting tank waste gas fan 23, a waste gas dehumidifier 25, a melt conveying pump 13, a raw material melt heater 14, a spray dryer 2, a spray drying bag filter 22, a spray drying hot air cyclone separator 21, a material preheating cyclone separator 32, a direct combustion type cyclone dynamic calcining furnace 3, a direct combustion type cyclone dynamic calcining furnace pyrolysis gas recycling fan 39, a calcining furnace cyclone separator 33, a magnesium oxide powder aging bin 34, a magnesium oxide powder conveying fan 38, a magnesium oxide powder product bin 37, a magnesium oxide powder cyclone separator 35 and a magnesium oxide powder bag filter 36; a heating coil 12 is arranged in the raw material melting tank 1, a mechanical seal stirrer 11 is arranged at the bottom of the raw material melting tank, an atomizing nozzle 24 is arranged at the top of the spray dryer 2, a discharger is arranged at the lower side of the spray dryer, an air inlet is arranged at the bottom of the spray dryer, and an air outlet is arranged at the top of the spray dryer; a combustor 31 is arranged in the direct-fired rotational flow dynamic calcining furnace 3, an outlet pipeline of the raw material melting tank 1 is communicated with an inlet of a delivery pump, an outlet pipeline of the delivery pump is communicated with an inlet of a raw material melt heater 14, and an outlet pipeline of the raw material melt heater 14 is communicated with an atomizing nozzle 24; an outlet of a magnesium nitrate powder discharger at the lower side part of the spray dryer 2 is communicated with an inlet pipeline at the upper part of the material preheating cyclone separator 32, and an outlet of the magnesium nitrate powder discharger at the lower part of the material preheating cyclone separator 32 is communicated with a magnesium nitrate powder feeding pipeline of the direct-fired cyclone dynamic calciner 3; the waste gas outlet of the spray dryer 2 is communicated with a gas inlet pipeline of a spray drying bag type filter 22, the gas outlet of the spray drying bag type filter 22 is communicated with a heated gas inlet pipeline of a raw material melt heater 14, the heated gas outlet of the raw material melt heater 14 is communicated with a heated gas inlet pipeline of a raw material melting tank 1, the heated gas outlet of the raw material melting tank 1 is communicated with an inlet of a waste gas fan 23 of the raw material melting tank, the outlet of the waste gas fan 23 of the raw material melting tank is communicated with a gas inlet of a waste gas dehumidifier 25, and the gas outlet of the waste gas dehumidifier 25 is communicated with a gas feeding pipeline of an acid absorption device; the gas inlet of the direct-fired rotational flow dynamic calcining furnace 3 is communicated with a fuel pipeline, a combustion-supporting air pipeline and a pyrolysis gas recycling gas fan outlet pipeline; the material outlet of the direct-fired cyclone dynamic calciner 3 is communicated with a material inlet pipeline of a calciner cyclone separator 33, the powder outlet of the calciner cyclone separator 33 is communicated with a powder inlet pipeline of a magnesium oxide powder aging bin 34, the powder outlet of the magnesium oxide powder aging bin 34 is communicated with an outlet pipeline of a magnesium oxide powder conveying fan 38, the powder outlet of the magnesium oxide powder aging bin 34 is also communicated with a material inlet pipeline of a magnesium oxide powder cyclone separator 35, and the powder outlet of the magnesium oxide powder cyclone separator 35 is communicated with an inlet pipeline of the magnesium oxide bin; a gas outlet of the magnesia powder cyclone separator 35 is communicated with a gas inlet pipeline of the magnesia powder bag filter 36, and a gas outlet of the magnesia powder bag filter 36 is communicated with a combustion-supporting gas inlet pipeline of the direct-fired rotational flow dynamic calciner 3; the gas outlet of the calciner cyclone separator 33 is communicated with the gas inlet pipeline of the material preheating cyclone separator 32, the gas outlet of the material preheating cyclone separator 32 is communicated with the gas inlet pipeline of the spray drying hot air cyclone separator 21, the gas outlet of the spray drying hot air cyclone separator 21 is communicated with the hot air inlet pipeline of the spray dryer 2, and the gas outlet of the spray drying hot air cyclone separator 21 is also communicated with the inlet pipeline of the pyrolysis gas recycling fan.
The method for pyrolyzing the magnesium nitrate by adopting the magnesium nitrate pyrolysis device based on resource recycling comprises the following steps:
magnesium nitrate hexahydrate is pyrolyzed and is carried out according to the following steps:
putting magnesium nitrate hexahydrate raw material into a raw material melting tank, and heating to form a melt;
conveying the melt to a raw material melt heater through a conveying pump to be heated continuously to form a high-temperature melt;
thirdly, atomizing the high-temperature melt by an atomizing nozzle, spraying the atomized high-temperature melt into a spray dryer, and carrying out drying and pyrolysis reaction to obtain a drying-pyrolysis product, wherein the drying-pyrolysis product comprises 98.8% of magnesium nitrate and 1.2% of magnesium oxide in percentage by mass; at the moment, pyrolysis gas separated from a gas outlet of a cyclone separator of a calcining furnace is preheated by the gas from a gas outlet of a material preheating cyclone separator, and a pyrolysis product from a spray dryer is preheated and then enters a spray drying hot air cyclone separator; pyrolysis gas separated from a gas outlet of the spray drying hot air cyclone separator enters a hot air inlet of the spray dryer in a volume ratio of 35% to heat materials in the spray dryer; 65% volume proportion of the hot gas enters a pyrolysis gas recycling inlet of the direct-fired rotational flow dynamic calciner to support combustion for fuel of the direct-fired rotational flow dynamic calciner;
magnesium nitrate and a small amount of magnesium oxide preheated by the material preheating cyclone separator enter the direct-fired rotational flow dynamic calcining furnace through a magnesium nitrate powder feeding pipeline for carrying out pyrolysis reaction to generate magnesium oxide, nitrogen dioxide and oxygen; pyrolysis gas and magnesium oxide enter a calciner cyclone separator through a material outlet of a direct-fired cyclone dynamic calciner, and separated magnesium oxide powder enters a magnesium oxide powder aging bin for aging; conveying the aged magnesium oxide powder to magnesium oxide and conveying gas separated by a magnesium oxide powder cyclone separator by using air, wherein the magnesium oxide enters a magnesium oxide product bin; the separated conveying gas enters a magnesia powder bag filter, enters a combustion-supporting gas inlet of the direct-fired rotational flow dynamic calciner through a gas outlet of the magnesia powder bag filter, and supports combustion for fuel of the direct-fired rotational flow dynamic calciner.
Fifthly, the pyrolysis gas separated from the cyclone separator of the calcining furnace is preheated by the material preheating cyclone separator firstly and then is separated out from the gas outlet by the spray drying hot air cyclone separator, and the pyrolysis gas is circulated to the step (3), specifically:
65 percent of pyrolysis gas in volume ratio enters a pyrolysis gas recycling inlet of the direct-fired rotational flow dynamic calciner through a pyrolysis gas recycling fan, and oxygen generated by pyrolysis is used for supporting combustion of fuel of the direct-fired rotational flow dynamic calciner; in additionFeeding 35% of pyrolysis gas by volume into a spray dryer, and heating the material in the spray dryer; drying waste gas a coming out of the top of the spray dryer enters a spray drying bag filter, and drying waste gas b separated from the spray drying bag filter enters a raw material melt heater to heat magnesium nitrate hexahydrate melt; waste gas from the raw material melt heater enters a jacket of a raw material melting tank and a heating coil in the tank, and is heated and melted; heating waste gas coming out from a jacket of the raw material melting tank and a heating coil in the tank enters a waste gas dehumidifier through a waste gas fan, and the cooled and dehumidified waste gas is subjected to NO detection2The volume concentration is 29-30%, and the nitric acid enters an acid absorption device to be used for preparing nitric acid.
The temperature of the raw material melting tank for melting the magnesium nitrate hexahydrate in the step I is 100 ℃, the melting time is 2 hours, and the pressure is 0.2 MPa.
The temperature of the raw material melt heater in the step II is 240 ℃, the heating time is 0.7h, and the pressure is 0.6 MPa.
And step three, separating out pyrolysis gas from a gas outlet of the calciner cyclone separator 33, wherein the temperature is 600 ℃, the entering temperature of hot air of the spray dryer is 440 ℃, the temperature of dry waste gas discharged from the top of the spray dryer is 340 ℃, and the pressure in the spray dryer is 0.05 MPa.
And (4) the preheated drying-pyrolysis product in the step (iv) is at 500 ℃, the temperature in the direct-fired rotational flow dynamic calcining furnace is at 1000 ℃, the calcining time is 6s, the pressure in the furnace is 0.02MPa, magnesium oxide and pyrolysis gas generated by pyrolyzing magnesium nitrate pass through a material outlet of the direct-fired rotational flow dynamic calcining furnace 3, and the outlet temperature is 690 ℃.
The aging time of the magnesia powder aging bin in the step (IV) is 40 minutes, the temperature in the bin is 580 ℃, the pressure is normal pressure, and the MgO mass percentage content in the obtained magnesia product is 98.3 percent.
In the fifth step, the temperature of the dried waste gas a is 330-360 ℃, the temperature of the generated heated waste gas is 280 ℃, and the NO is detected after the heated waste gas is cooled and dehumidified2The volume concentration was 29%.
The pyrolysis gas comprises components and mole percentThe content of each component is as follows: o is2 2.30％，N2 48.35％，CO2 8.50％，H2O 15.35％，NO2 25.50％；
Molar flow of pyrolysis gas: o is2 25.52kmol/hr，N2 522.00kmol/hr，CO2 90.57kmol/hr，H2O 181.58kmol/hr，NO2 278.54kmol/hr。
Molar flow of natural gas:
CH4：48.5kmol/hr
hot air molar flow:
O2：70kmol/hr
N2：263kmol/hr。
example 2
The process flow is the same as that of example 1; the difference lies in that:
the temperature of the raw material melting tank for melting the magnesium nitrate hexahydrate in the step I is 105 ℃, the melting time is 100min, and the pressure is 0.225 MPa.
The temperature of the raw material melt heater in the step II is 250 ℃, the heating time is 0.6h, and the pressure is 0.625 MPa.
And step three, separating pyrolysis gas from a gas outlet of the calciner cyclone separator 33, wherein the temperature is 610 ℃, the entering temperature of hot air of a spray dryer is 445 ℃, the temperature of drying waste gas discharged from the top of the spray dryer is 345 ℃, the pressure in the spray dryer is 0.075MPa, and a drying-pyrolysis product comprises 98.6 mass percent of magnesium nitrate and 1.4 mass percent of magnesium oxide.
The preheated pyrolysis product in the step (IV) is heated to 520 ℃, the temperature in the direct-fired cyclone dynamic calcining furnace is 1100 ℃, the calcining time is 5s, the pressure in the furnace is 0.025MPa, magnesium oxide and pyrolysis gas generated by pyrolyzing magnesium nitrate pass through a material outlet of the direct-fired cyclone dynamic calcining furnace 3, and the outlet temperature is 695 ℃.
The aging time of the magnesium oxide powder aging bin in the step (IV) is 35 minutes, the temperature in the bin is 590 ℃, the pressure is normal pressure, and the mass percentage of MgO in the obtained magnesium oxide product is 98.6%.
Step fiveThe temperature of the medium drying waste gas a is 345 ℃, the temperature of the generated heating waste gas is 290 ℃, and NO is detected after the heating waste gas is cooled and dehumidified2The volume concentration was 29.5%.
The pyrolysis gas comprises the following components in percentage by mole: o is2 2.40％，N2 49.28％，CO2 8.00％，H2O 16.00％，NO2 24.32％；
Molar flow of pyrolysis gas: o is2 27.86kmol/hr，N2 527.00kmol/hr，CO2 92.86kmol/hr，H2O 185.71kmol/hr，NO2 282.29kmol/hr。
Molar flow of natural gas:
CH4：50kmol/hr
hot air molar flow:
O2：76kmol/hr
N2：286kmol/hr。
example 3
The process flow is the same as that of example 1; the difference lies in that:
the temperature of the raw material melting tank for melting the magnesium nitrate hexahydrate in the step I is 110 ℃, the melting time is 1.5 hours, and the pressure is 0.25 MPa.
The temperature of the raw material melt heater in the step II is 260 ℃, the heating time is 0.5h, and the pressure is 0.65 MPa.
And step three, separating pyrolysis gas from a gas outlet of the calciner cyclone separator 33, wherein the temperature is 620 ℃, the hot air inlet temperature of the spray dryer is 450 ℃, the temperature of the dry waste gas discharged from the top of the spray dryer is 350 ℃, the pressure in the spray dryer is 0.1MPa, and the dry-pyrolysis product comprises 98.3 percent of magnesium nitrate and 1.7 percent of magnesium oxide in percentage by mass.
The preheated drying-pyrolysis product in the step (IV) is heated to 550 ℃, the temperature in the direct-fired cyclone dynamic calcining furnace is 1200 ℃, the calcining time is 4s, the pressure in the furnace is 0.03MPa, magnesium oxide and pyrolysis gas generated by pyrolyzing magnesium nitrate pass through a material outlet of the direct-fired cyclone dynamic calcining furnace 3, and the outlet temperature is 700 ℃.
The aging time of the magnesia powder aging bin in the step (IV) is 30 minutes, the temperature in the bin is 600 ℃, the pressure is normal pressure, and the MgO mass percentage content in the obtained magnesia product is 99.2 percent.
In the fifth step, the temperature of the dried waste gas a is 360 ℃, the temperature of the generated heating waste gas is 300 ℃, and NO is detected after the heating waste gas is cooled and dehumidified2The volume concentration was 30%.
The pyrolysis gas comprises the following components in percentage by mole: o is2 2.50％，N2 50.04％，CO2 9.00％，H2O 14.50％，NO2 23.96％；
Molar flow of pyrolysis gas: o is2 28.53kmol/hr，N2 535.00kmol/hr，CO2 93.36kmol/hr，H2O 187.23kmol/hr，NO2 289.42kmol/hr。
Molar flow of natural gas:
CH4：52.5kmol/hr
hot air molar flow:
O2：80kmol/hr
N2：301kmol/hr。
the above-described embodiments illustrate rather than limit the invention, and that those skilled in the art will be able to design alternative embodiments without departing from the scope of the appended claims. In the claims, any reference signs placed between parentheses shall not be construed as limiting the claim. The word "comprising" does not exclude the presence of elements or steps not listed in a claim.
Claims (6)
1. A magnesium nitrate pyrolysis device based on resource recycling is characterized by comprising a raw material melting tank, a raw material melting tank waste gas fan, a waste gas dehumidifier, a delivery pump, a raw material melt heater, a spray dryer, a spray drying bag type filter, a spray drying hot air cyclone separator, a material preheating cyclone separator, a direct combustion type rotational flow dynamic calciner pyrolysis gas recycling fan, a cyclone calciner separator, a magnesium oxide powder aging bin, a magnesium oxide powder conveying and air feeding machine, a magnesium oxide powder product bin, a magnesium oxide powder cyclone separator and a magnesium oxide powder bag type filter; wherein:
the raw material melting tank, the raw material melt heater, the spray dryer, the material preheating cyclone separator, the direct-fired type cyclone dynamic calcining furnace, the calcining furnace cyclone separator, the magnesium oxide powder aging bin, the magnesium oxide powder cyclone separator and the magnesium oxide powder product bin are sequentially connected;
the spray dryer is also connected with a spray drying bag type filter, the spray drying bag type filter is respectively connected with a melt heater and a material preheating cyclone separator, the material preheating cyclone separator is connected with a spray drying hot air cyclone separator, and the spray drying hot air cyclone separator is respectively connected with the spray dryer and a direct-fired cyclone dynamic calciner pyrolysis gas recycling fan;
the calciner cyclone separator is also connected with a material preheating cyclone separator, the magnesia powder cyclone separator is also connected with a magnesia powder bag filter, and the magnesia powder bag filter is also respectively connected with a magnesia powder product bin and a direct-fired cyclone dynamic calciner.
2. The magnesium nitrate pyrolysis device based on resource recycling of claim 1, wherein:
the raw material melting tank is connected with a raw material melting tank waste gas fan, the waste gas fan is connected with a waste gas dehumidifier, the waste gas dehumidifier is connected with an acid absorption device, and the raw material melting tank is connected with a raw material melt heater through a delivery pump.
3. The magnesium nitrate pyrolysis device based on resource recycling of claim 1, wherein the spray dryer is provided with an atomizing nozzle at the top, a magnesium nitrate powder discharger at the lower side, an air inlet at the bottom and an air outlet at the top.
4. The magnesium nitrate pyrolysis device based on resource recycling of claim 1, wherein a magnesium nitrate powder discharger is arranged at the lower part of the material preheating cyclone separator.
5. The magnesium nitrate pyrolysis device based on resource recycling of claim 1, wherein an outlet pipeline of the raw material melting tank is communicated with an inlet of a delivery pump, an outlet pipeline of the delivery pump is communicated with an inlet of a raw material melt heater, and an outlet pipeline of the raw material melt heater is communicated with an atomizing nozzle; an outlet of a magnesium nitrate powder discharger at the lower side of the spray dryer is communicated with an inlet pipeline at the upper part of the material preheating cyclone separator, and an outlet of the magnesium nitrate powder discharger at the lower part of the material preheating cyclone separator is communicated with a magnesium nitrate powder feeding pipeline of the direct-fired cyclone dynamic calcining furnace; the waste gas outlet of the spray dryer is communicated with the gas inlet pipeline of the spray drying bag type filter, the gas outlet of the spray drying bag type filter is communicated with the heated gas inlet pipeline of the raw material melt heater, the heated gas outlet of the raw material melt heater is communicated with the heated gas inlet pipeline of the raw material melting tank, the heated gas outlet of the raw material melting tank is communicated with the waste gas fan inlet of the raw material melting tank, the waste gas fan outlet of the raw material melting tank is communicated with the gas inlet of the waste gas dehumidifier, and the gas outlet of the waste gas dehumidifier is communicated with the gas feeding pipeline of the acid absorption device.
6. The magnesium nitrate pyrolysis device based on resource recycling according to claim 1, characterized in that a gas inlet of the direct-fired rotational flow dynamic calciner is communicated with a fuel pipeline, a combustion air pipeline and an outlet pipeline of a pyrolysis gas recycling gas fan of the direct-fired rotational flow dynamic calciner; the material outlet of the direct-fired cyclone dynamic calciner is communicated with a material inlet pipeline of a cyclone separator of the calciner, the powder outlet of the cyclone separator of the calciner is communicated with a powder inlet pipeline of a magnesia powder aging bin, the powder outlet of the magnesia powder aging bin is communicated with an outlet pipeline of a magnesia powder conveying and feeding machine, the powder outlet of the magnesia powder aging bin is also communicated with the material inlet pipeline of the magnesia powder cyclone separator, and the powder outlet of the magnesia powder cyclone separator is communicated with an inlet pipeline of a magnesia product bin; the gas outlet of the magnesia powder cyclone separator is communicated with a gas inlet pipeline of a magnesia powder bag filter, and the gas outlet of the magnesia powder bag filter is communicated with a combustion-supporting air inlet pipeline of a direct-fired rotational flow dynamic calciner; the gas outlet of the calciner cyclone separator is communicated with a gas inlet pipeline of a material preheating cyclone separator, the gas outlet of the material preheating cyclone separator is communicated with a gas inlet pipeline of a spray drying hot air cyclone separator, the gas outlet of the spray drying hot air cyclone separator is communicated with a hot air inlet pipeline of a spray dryer, and the gas outlet of the spray drying hot air cyclone separator is also communicated with an inlet pipeline of a pyrolysis gas recycling fan of a direct-fired cyclone dynamic calciner.
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