CN212610834U - High-sulfur bauxite dry-process desulfurization device - Google Patents
High-sulfur bauxite dry-process desulfurization device Download PDFInfo
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Abstract
The utility model provides a high sulphur bauxite dry process desulphurization unit, includes feed unit, dry unit of preheating, suspension desulfurization stove, desulfurization reactor, waste heat recovery unit, combustion system, purification unit and discharge unit. The desulfurization method comprises the following steps: weighing the high-sulfur bauxite powder by a feeding unit, then feeding the weighed high-sulfur bauxite powder into a drying preheating unit, feeding the preheated material into a suspension desulfurization furnace, and feeding dust-containing waste gas into a purification unit; the preheated material is desulfurized in a suspension desulfurization furnace for one time to form a high-temperature material, then gas-solid separation is carried out, the solid material enters a desulfurization reactor, and hot waste gas is discharged into a drying and preheating unit; the solid material is secondarily desulfurized by a desulfurization reactor to form high-temperature clinker, the high-temperature clinker enters a waste heat recovery unit, and reaction waste gas enters a suspension desulfurization furnace; cooling the high-temperature clinker by a waste heat recovery unit, discharging the cooled clinker into a clinker storage bin, and feeding preheated air into a suspension desulfurization furnace; the dust-containing waste gas enters a purification unit to complete desulfurization purification and dust removal, the solid dust returns to a drying and preheating unit, and the purified waste gas is discharged into the atmosphere through a discharge unit.
Description
Technical Field
The utility model belongs to the technical field of the metallurgy, especially, relate to a high sulphur bauxite dry process desulphurization unit.
Background
In the light nonferrous metallurgy industry, bauxite with the total sulfur content of more than 0.6 percent is customarily called high-sulfur bauxite, the storage capacity of the bauxite which is proved in China is about 23 hundred million tons, wherein the high-sulfur bauxite accounts for about 7.8 percent, and the calculated storage capacity is about 1.8 hundred million tons. In these well-identified high-sulfur bauxite ores, sulfur is again predominantly pyrite (FeS)2) Exists in the form of (1), and is mainly S when dissolved2-、SO3 2-、SO4 2-And the like, the existence of the sulfur influences the dissolution process or the sintering process of the alumina, the sulfur in the production process is combined with alkali to form sodium sulfate and is crystallized and separated out, the separated sodium sulfate crystals reduce the seed decomposition rate and the AH yield, and the sulfide and thiosulfate also increase the corrosion of equipment and cause the increase of the concentration of soluble iron in the solution, and finally the quality of the aluminum hydroxide is unqualified. In addition, since pyrite (FeS)2) And pyrite easily adsorbs Al (OH)4-、Na+Ions and water, which results in poorer red mud performance. Therefore, how to solve the problem of desulfurization of high-sulfur bauxite ore used for alumina production is an urgent task to alleviate the resource shortage of alumina-producing ore and to reduce the external dependency of ore.
At present, desulfurization of high-sulfur bauxite is more frequently heavier than wet desulfurization, and a reverse flotation process is adopted to float sulfur-containing minerals by adding a collecting agent. However, wet desulphurization generally has the defects of complex process, low alumina recovery rate, difficult tailing treatment, small sulfur content per unit time yield and high desulphurization cost.
Therefore, although the process can meet the desulfurization requirement of the high-sulfur bauxite, the process has the defects of complex process, large floor area, large heat loss, high energy consumption, difficulty in realizing large scale, relative high roasting temperature and the like, and simultaneously roasting clinker has the condition of under-burning and has poor adaptability to the component change of the high-sulfur bauxite.
SUMMERY OF THE UTILITY MODEL
To the problem that prior art exists, the utility model provides a high sulphur bauxite dry process desulphurization unit has that the process is simple, area is little, the heat loss is little, the energy consumption is low, easily realize maximization, calcination temperature characteristics such as low relatively, and calcination grog's quality is higher. The utility model discloses a thermal step rational utilization, fuel are direct to burn in the suspension combustion furnace, have reduced route, desulfurization reactor's setting, have promoted powdered ore desulfurization reaction time and reaction temperature, consequently energy-conserving more, convert into per ton grog and can make the energy consumption reduce 8.1% ~ 10.2%. The utility model discloses the adaptability to high sulphur bauxite composition change is stronger, can handle the high sulphur bauxite that full sulphur content is 0.6% ~ 6%.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a high-sulfur bauxite dry desulfurization device comprises a feeding unit, a drying preheating unit, a suspension desulfurization furnace, a desulfurization reactor, a waste heat recovery unit, a combustion system, a purification unit and a discharge unit; the feeding end of the feeding unit is used for inputting high-sulfur bauxite powder, the discharging end of the feeding unit is communicated with the feeding end of the drying preheating unit through a first chute, the waste gas discharging end of the drying preheating unit is communicated with the waste gas inlet end of the purifying unit through a dust-containing waste gas discharging pipe, the ash returning end of the purifying unit is communicated with the feeding end of the drying preheating unit through an ash returning pipe, the waste gas discharging end of the purifying unit is communicated with the waste gas inlet end of the discharging unit through a purified waste gas discharging pipe, and the waste gas discharging end of the discharging unit is used for outputting waste gas; the discharge end of the drying and preheating unit is communicated with the feed end of the suspension desulfurization furnace through a first discharge pipe, the hot waste gas discharge end of the suspension desulfurization furnace is communicated with the dry preheating gas inlet end of the drying and preheating unit through a hot waste gas discharge pipe, the discharge end of the suspension desulfurization furnace is communicated with the feed end of the desulfurization reactor through a second discharge pipe, the reaction waste gas discharge end of the desulfurization reactor is communicated with the reaction waste gas inlet end of the suspension desulfurization furnace through a reaction waste gas discharge pipe, the discharge end of the desulfurization reactor is communicated with the feed end of the waste heat recovery unit through a second chute, the hot air discharge end of the waste heat recovery unit is communicated with the hot flue gas inlet end of the suspension desulfurization furnace through a hot air discharge pipe, the discharge end of the waste heat recovery unit is used for outputting clinker, and the cold air inlet end of the waste heat recovery unit is used for inputting cold air; the high-temperature flue gas discharge end of the combustion system is output in three paths, the first path is directly communicated with the hot flue gas inlet end of the suspension desulfurization furnace, the second path is communicated with the dry preheating gas inlet end of the dry preheating unit through a first high-temperature flue gas discharge pipe, and the third path is communicated with the hot flue gas inlet end of the waste heat recovery unit through a second high-temperature flue gas discharge pipe; and the gas inlet end of the combustion system is used for inputting gas.
The feeding unit comprises a buffer bin and a metering scale, a feeding port of the buffer bin is used as a feeding end of the feeding unit, a discharging port of the buffer bin is provided with a material saving valve, the discharging port of the buffer bin is externally connected with a feeding chute through the metering scale, and the discharging port of the feeding chute is used as a discharging end of the feeding unit.
The drying and preheating unit comprises a dryer and a preheater, and the dryer is communicated with the preheater through a pipeline; the preheaters adopt a single-stage structure or a multi-stage structure, and the multi-stage preheaters are communicated through pipelines; the feed inlet of the dryer is used as the feed end of the drying preheating unit; when the preheater adopts a single-stage structure, a discharge port of the single-stage preheater is used as a discharge end of the drying preheating unit; when the preheater adopts a multi-stage structure, the discharge port of the final-stage preheater is used as the discharge end of the drying preheating unit.
The suspension desulfurization furnace comprises a suspension reactor and a cyclone separator, wherein the main body structure of the suspension reactor is cylindrical, and the bottom of the suspension reactor is conical; the feeding port of the suspension reactor is used as the feeding end of the suspension desulfurization furnace, the discharging port at the top of the suspension reactor is communicated with the feeding port of the cyclone separator, and the discharging port of the cyclone separator is used as the discharging end of the suspension desulfurization furnace.
The desulfurization reactor comprises a fluidized bed, a fluidized air station and a Roots blower, wherein a feed inlet of the fluidized bed is used as a feed end of the desulfurization reactor, and a discharge outlet of the fluidized bed is used as a discharge end of the desulfurization reactor; the fluidized bed is communicated with the fluidized air station and the fluidized air station is communicated with the Roots blower through pipelines; the fluidized bed adopts a multi-chamber fluidized bed, each chamber of the fluidized bed is internally provided with an independent air chamber, and an air blower is arranged on each air chamber; air is adopted as fluidized wind, and the fluidized wind station and the Roots blower provide the fluidized wind.
The waste heat recovery unit comprises a cyclone cooler and a fluidized bed cooler, and the cyclone cooler is communicated with the fluidized bed cooler through a pipeline; the cyclone coolers adopt a single-stage structure or a multi-stage structure, and the multi-stage cyclone coolers are communicated through a pipeline; when the cyclone cooler adopts a single-stage structure, a feed inlet of the cyclone cooler is used as a feed end of the waste heat recovery unit; when the cyclone cooler adopts a multi-stage structure, the feed inlet of the first-stage cyclone cooler is used as the feed end of the waste heat recovery unit; and a discharge port of the fluidized bed cooler is used as a discharge end of the waste heat recovery unit.
The combustion system comprises a main combustion station, an auxiliary combustion station, a starting combustion station and a drying combustion station, wherein the main combustion station, the auxiliary combustion station and the starting combustion station adopt solid fuel, liquid fuel or gas fuel.
The purification unit comprises a gas desulfurization device, a dust remover, a chute, a centrifugal fan, pneumatic conveying equipment and a Roots fan, wherein the gas desulfurization device, the dust remover, the chute, the centrifugal fan, the pneumatic conveying equipment and the Roots fan are communicated through pipelines; the fluidized air in the chute is provided by a centrifugal fan; conveying wind in the pneumatic conveying equipment is provided by a Roots blower; the dust remover adopts a bag-type dust remover, a metal filter bag dust remover, an electric dust remover or an electric bag dust remover; the pneumatic conveying equipment adopts a pneumatic lifting pump, a bin type pump or a vertical spiral feeding pump.
The exhaust unit comprises an induced draft fan, an air door and a chimney, an air outlet of the induced draft fan is communicated with the chimney through the air door, and an exhaust outlet of the chimney is communicated with the atmosphere.
A high-sulfur bauxite dry desulphurization method adopts the high-sulfur bauxite dry desulphurization device, and comprises the following steps:
the method comprises the following steps: drying preheating
Feeding high-sulfur bauxite powder into a buffer bin of a feeding unit, weighing the high-sulfur bauxite powder by a weighing scale, and then feeding the high-sulfur bauxite powder into a drying preheating unit, wherein the ore powder can exchange heat with hot waste gas discharged from a cyclone separator in a suspension desulfurization furnace, the ore powder is gradually preheated to 280-400 ℃ to form a preheated material, the hot waste gas is cooled to 150-200 ℃ to form dust-containing waste gas, the preheated material directly enters the suspension desulfurization furnace, and the dust-containing waste gas directly enters a purification unit;
step two: one-time desulfurization
After the preheated material enters a suspension reactor of a suspension desulfurization furnace, the preheated material is further heated to 400-800 ℃ by high-temperature flue gas generated by a main combustion station in a combustion system to form high-temperature material, at the moment, the oxygen content of the high-temperature flue gas in the suspension reactor is 3-8%, and the high-temperature material needs to stay in the suspension desulfurization furnace for 4-20 s, so that the desulfurization reaction rate reaches 40-50%, the high-temperature material after primary desulfurization directly enters a cyclone separator of the suspension desulfurization furnace to be subjected to gas-solid separation, solid material and hot waste gas can be obtained, the solid material directly enters the desulfurization reactor, and the hot waste gas is directly discharged into a drying preheating unit to be preheated and dried with mineral powder;
step three: secondary desulfurization
After the solid material enters a fluidized bed of a desulfurization reactor, further performing desulfurization reaction on unreacted pyrite minerals in the solid material and oxygen in fluidized air for 5-30 min until all pyrite components in the solid material complete the desulfurization reaction, and further obtaining high-temperature clinker and reaction waste gas, wherein the high-temperature clinker directly enters a waste heat recovery unit, and the reaction waste gas directly enters a suspension desulfurization furnace for recycling;
step four: waste heat recovery
When the high-temperature clinker enters a cyclone cooler of the waste heat recovery unit, the high-temperature clinker exchanges heat with cold air from the outside, the high-temperature clinker is cooled to below 100 ℃ step by step to form cooling clinker, meanwhile, the cold air is heated to 320-500 ℃ step by step to form preheated air, the cooled clinker is discharged into a clinker storage bin for storage, and the preheated air directly enters a suspension desulfurization furnace for fuel combustion supporting of a combustion system;
step five: exhaust gas purification
After the dust-containing waste gas enters the purification unit, the desulfurization purification and the dust removal are sequentially completed, the formed solid dust directly returns to the drying and preheating unit to be recovered, the formed purified waste gas is discharged into the atmosphere through the discharge unit, and the recovered SO2Storing for preparing acid.
The utility model has the advantages that:
the utility model discloses a high sulphur bauxite dry process desulphurization unit has that process is simple, area is little, the heat loss is little, the energy consumption is low, easily realize maximization, calcination temperature characteristics such as low relatively, and calcination grog's quality is higher. The utility model discloses a thermal step rational utilization, fuel are direct to burn in the suspension combustion furnace, have reduced route, desulfurization reactor's setting, have promoted powdered ore desulfurization reaction time and reaction temperature, consequently energy-conserving more, convert into per ton grog and can make the energy consumption reduce 8.1% ~ 10.2%. The utility model discloses the adaptability to high sulphur bauxite composition change is stronger, can handle the high sulphur bauxite that full sulphur content is 0.6% ~ 6%.
Drawings
FIG. 1 is a schematic structural diagram of a high-sulfur bauxite dry desulfurization device of the present invention;
in the figure, 1-feeding unit, 2-drying preheating unit, 3-suspension desulfurizing furnace, 4-desulfurizing reactor, 5-waste heat recovery unit, 6-combustion system, 7-purifying unit, 8-discharging unit, 9-first chute, 10-dust-containing waste gas discharging pipe, 11-ash returning pipe, 12-purified waste gas discharging pipe, 13-first discharging pipe, 14-hot waste gas discharging pipe, 15-second discharging pipe, 16-reaction waste gas discharging pipe, 17-second chute, 18-hot air discharging pipe, 19-first high temperature flue gas discharging pipe, 20-second high temperature flue gas discharging pipe, A-high sulfur bauxite powder, B-waste gas, C-clinker, D-cold air, E-fuel gas.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
As shown in fig. 1, a high-sulfur bauxite dry desulfurization device comprises a feeding unit 1, a drying preheating unit 2, a suspension desulfurization furnace 3, a desulfurization reactor 4, a waste heat recovery unit 5, a combustion system 6, a purification unit 7 and a discharge unit 8; the feeding end of the feeding unit 1 is used for inputting high-sulfur bauxite powder A, the discharging end of the feeding unit 1 is communicated with the feeding end of the drying and preheating unit 2 through a first chute 9, the waste gas discharging end of the drying and preheating unit 2 is communicated with the waste gas inlet end of the purifying unit 7 through a dust-containing waste gas discharging pipe 10, the ash returning end of the purifying unit 7 is communicated with the feeding end of the drying and preheating unit 2 through an ash returning pipe 11, the waste gas discharging end of the purifying unit 7 is communicated with the waste gas inlet end of the discharging unit 8 through a purified waste gas discharging pipe 12, and the waste gas discharging end of the discharging unit 8 is used for outputting waste gas B; the discharge end of the drying and preheating unit 2 is communicated with the feed end of the suspension desulfurization furnace 3 through a first discharge pipe 13, the hot waste gas discharge end of the suspension desulfurization furnace 3 is communicated with the dry preheating gas inlet end of the drying and preheating unit 2 through a hot waste gas discharge pipe 14, the discharge end of the suspension desulfurization furnace 3 is communicated with the feed end of the desulfurization reactor 4 through a second discharge pipe 15, the reaction waste gas discharge end of the desulfurization reactor 4 is communicated with the reaction waste gas inlet end of the suspension desulfurization furnace 3 through a reaction waste gas discharge pipe 16, the discharge end of the desulfurization reactor 4 is communicated with the feed end of the waste heat recovery unit 5 through a second chute 17, the hot air discharge end of the waste heat recovery unit 5 is communicated with the hot flue gas inlet end of the suspension desulfurization furnace 3 through a hot air discharge pipe 18, the discharge end of the waste heat recovery unit 5 is used for outputting clinker C, and the cold air inlet end of the waste heat recovery unit 5 is used for inputting cold air D; the high-temperature flue gas discharge end of the combustion system 6 is output in three paths, the first path is directly communicated with the hot flue gas inlet end of the suspension desulfurization furnace 3, the second path is communicated with the dry preheating gas inlet end of the dry preheating unit 2 through a first high-temperature flue gas discharge pipe 19, and the third path is communicated with the hot flue gas inlet end of the waste heat recovery unit 5 through a second high-temperature flue gas discharge pipe 20; and the gas inlet end of the combustion system 6 is used for inputting gas E.
The feeding unit 1 comprises a buffering bin and a metering scale, a feeding port of the buffering bin is used as a feeding end of the feeding unit 1, a discharging port of the buffering bin is provided with a material saving valve, the discharging port of the buffering bin is externally connected with a feeding chute through the metering scale, and the discharging port of the feeding chute is used as a discharging end of the feeding unit 1. Specifically, the metering scale can adopt an electronic constant feeder, a metering screw conveyor, a punching plate flowmeter or a rotor scale, and the material saving valve can adopt a rod valve or a gate valve; when the water content of the high-sulfur bauxite powder A is less than or equal to 2 percent, a rotor scale is preferably selected by a weighing scale; when the water content of the high-sulfur bauxite powder A is more than 2%, the electronic quantitative feeder is preferably selected by the weighing machine.
The drying and preheating unit 2 comprises a dryer and a preheater, and the dryer is communicated with the preheater through a pipeline; the preheaters adopt a single-stage structure or a multi-stage structure, and the multi-stage preheaters are communicated through pipelines; the feed inlet of the dryer is used as the feed end of the drying preheating unit 2; when the preheater adopts a single-stage structure, the discharge port of the single-stage preheater is used as the discharge end of the drying preheating unit 2; when the preheater adopts a multi-stage structure, the discharge port of the final-stage preheater is used as the discharge end of the drying preheating unit 2. Specifically, the dryer can adopt a Venturi dryer or a drying and scattering machine, and the preheater can be of a single-stage, two-stage or three-stage structure; when the water content of the high-sulfur bauxite powder A is less than or equal to 8 percent, the dryer is preferably a Venturi dryer; when the water content of the high-sulfur bauxite powder A is more than 8 percent, the drier is preferably a drying and scattering machine.
The suspension desulfurization furnace 3 comprises a suspension reactor and a cyclone separator, the main structure of the suspension reactor is cylindrical, and the bottom of the suspension reactor is conical; the feed inlet of the suspension reactor is used as the feed end of the suspension desulfurization furnace 3, the discharge outlet at the top of the suspension reactor is communicated with the feed inlet of the cyclone separator, and the discharge outlet of the cyclone separator is used as the discharge end of the suspension desulfurization furnace 3.
The desulfurization reactor 4 comprises a fluidized bed, a fluidized air station and a Roots blower, a feed inlet of the fluidized bed is used as a feed end of the desulfurization reactor 4, and a discharge outlet of the fluidized bed is used as a discharge end of the desulfurization reactor 4; the fluidized bed is communicated with the fluidized air station and the fluidized air station is communicated with the Roots blower through pipelines; the fluidized bed adopts a multi-chamber fluidized bed, each chamber of the fluidized bed is internally provided with an independent air chamber, and an air blower is arranged on each air chamber; air is adopted as fluidized wind, and the fluidized wind station and the Roots blower provide the fluidized wind.
The waste heat recovery unit 5 comprises a cyclone cooler and a fluidized bed cooler, and the cyclone cooler is communicated with the fluidized bed cooler through a pipeline; the cyclone coolers adopt a single-stage structure or a multi-stage structure, and the multi-stage cyclone coolers are communicated through a pipeline; when the cyclone cooler adopts a single-stage structure, a feed inlet of the cyclone cooler is used as a feed end of the waste heat recovery unit 5; when the cyclone cooler adopts a multi-stage structure, the feed inlet of the first-stage cyclone cooler is used as the feed end of the waste heat recovery unit 5; and a discharge port of the fluidized bed cooler is used as a discharge end of the waste heat recovery unit 5. Specifically, the fluidized bed cooler is not configured according to the requirement of the final cooling temperature, when the cyclone cooler adopts a single-stage structure, the discharge port of the cyclone cooler is used as the discharge end of the waste heat recovery unit 5, and when the cyclone cooler adopts a multi-stage structure, the discharge port of the last-stage cyclone cooler is used as the discharge end of the waste heat recovery unit 5; the cyclone cooler can be provided in a single stage, two stage or three stage configuration.
The combustion system 6 comprises a main combustion station, an auxiliary combustion station, a starting combustion station and a drying combustion station, wherein the main combustion station, the auxiliary combustion station and the starting combustion station adopt solid fuel, liquid fuel or gas fuel. Specifically, the dry combustion station can determine whether to configure according to the water attached condition of the materials. The main combustion station is used for providing heat required by the production of the desulfurization device, the auxiliary combustion station is used for ensuring safe ignition and operation of the desulfurization device, the starting combustion station is used for newly building a furnace lining of equipment containing a furnace lining to bake a furnace, and the drying combustion station is used for supplementing heat with insufficient water attached to a dry mineral powder filter cake.
The purification unit 7 comprises a gas desulfurization device, a dust remover, a chute, a centrifugal fan, pneumatic conveying equipment and a Roots fan, wherein the gas desulfurization device, the dust remover, the chute, the centrifugal fan, the pneumatic conveying equipment and the Roots fan are communicated through pipelines; the fluidized air in the chute is provided by a centrifugal fan; conveying wind in the pneumatic conveying equipment is provided by a Roots blower; the dust remover adopts a bag-type dust remover, a metal filter bag dust remover, an electric dust remover or an electric bag dust remover; the pneumatic conveying equipment adopts a pneumatic lifting pump, a bin type pump or a vertical spiral feeding pump. Specifically, a metal bag dust collector is preferred, and a pneumatic lifting pump is preferred as the pneumatic conveying equipment.
The discharge unit 8 comprises an induced draft fan, an air door and a chimney, an air outlet of the induced draft fan is communicated with the chimney through the air door, and an air outlet of the chimney is communicated with the atmosphere.
In this embodiment, the equipment specification of the feeding unit 1 is as follows: the diameter of the buffer bin is phi 3800mm, and the volume of the buffer bin is 85m3The metering scale adopts a rotor scale, and the measuring capacity of the rotor scale is 30-300 t/h. The equipment specifications of the drying and preheating unit 2 are as follows: the dryer adopts a Venturi dryer, the dimension specification of the Venturi dryer is phi 2470 mm/phi 3380mm, the preheater adopts a secondary structure, the dimension specification of the first-stage preheater is phi 4290mm multiplied by phi 9960mm, and the dimension specification of the second-stage preheater is phi 5330mm multiplied by phi 11200 mm. The equipment specification of the suspension desulfurization furnace 3 is as follows: the suspension reactor has the size specification of phi 6400mm multiplied by 19200mm, and the cyclone separator has the size specification of phi 6400mm multiplied by 13800 mm. The equipment specification of the desulfurization reactor 4 is: the fluidized bed has the size specification of 2500mm multiplied by 6700mm multiplied by 3600mm, and the air supply capacity of the Roots blower is 117m3The air supply pressure is 39.4 Kpa. The equipment specification of the waste heat recovery unit 5 is as follows: the cyclone cooler adopts a two-stage structure, the size specification of the first-stage cyclone cooler is phi 6500mm multiplied by 14500mm, the size specification of the second-stage cyclone cooler is phi 5600mm multiplied by 12600mm, and the size specification of the fluidized bed cooler is 2400mm multiplied by 2800mm multiplied by 10300 mm. The equipment specifications of the combustion system 6 are: master and slaveThe fuel of the combustion station adopts coal gas, and the flow rate of the coal gas is 60000m3H, the calorific value of the gas is 1450kcal/m3. The equipment specifications of the purification unit 7 are: the dust remover adopts a bag-type dust remover, and the smoke treatment capacity of the bag-type dust remover is 350000m3H is used as the reference value. The equipment specifications of the discharge unit 8 are: the induced draft rate of the induced draft fan is 420000m3And/h, the induced air pressure is-9000 pa. The daily treatment capacity of the high-sulfur bauxite powder A of the desulfurization device is 3100 t/d-6820 t/d. When the ratio of aluminum to silicon of the high-sulfur bauxite powder A is 6.4 and the total sulfur content is 2 percent (wherein the SO content is4 2-0.08 percent, and the balance being sulfur in the pyrite), the water content is less than or equal to 15 percent, and the particle size distribution is as follows: 100 percent is less than 0.3mm, 50 percent to 75 percent is less than or equal to 0.074mm, and the total sulfur content of the clinker after the mineral powder is desulfurized is 0.2 percent. When the ratio of aluminum to silicon of the high-sulfur bauxite powder A is 5.1 and the total sulfur content is 3.2 percent (wherein the SO content is4 2-0.07% of the total content of the sulfur in the pyrite), the water content is less than or equal to 8%, and the particle size distribution is as follows: 100 percent is less than 0.3mm, 50 percent to 75 percent is less than or equal to 0.074mm, and the total sulfur content of the clinker after the mineral powder is desulfurized is 0.32 percent.
A high-sulfur bauxite dry desulphurization method adopts the high-sulfur bauxite dry desulphurization device, and comprises the following steps:
the method comprises the following steps: drying preheating
Feeding high-sulfur bauxite powder A into a buffer bin of a feeding unit 1, weighing the high-sulfur bauxite powder A by a scale, and then feeding the high-sulfur bauxite powder A into a drying preheating unit 2, wherein the ore powder can exchange heat with hot waste gas discharged from a cyclone separator in a suspension desulfurization furnace 3, the ore powder is gradually preheated to 280-400 ℃ to form a preheating material, meanwhile, the hot waste gas is cooled to 150-200 ℃ to form dust-containing waste gas, the preheating material directly enters the suspension desulfurization furnace 3, and the dust-containing waste gas directly enters a purification unit 7;
step two: one-time desulfurization
After the preheated material enters the suspension reactor of the suspension desulfurization furnace 3, the preheated material is further heated to 400-800 ℃ by high-temperature flue gas generated by a main combustion station in a combustion system 6 to form high-temperature material, at the moment, the oxygen content of the high-temperature flue gas in the suspension reactor is 3-8%, and the high-temperature material needs to stay in the suspension desulfurization furnace 3 for 4-20 s, so that the desulfurization reaction rate reaches 40-50%, the high-temperature material after primary desulfurization directly enters a cyclone separator of the suspension desulfurization furnace 3 to be subjected to gas-solid separation, solid material and hot waste gas can be obtained, the solid material directly enters the desulfurization reactor 4, and the hot waste gas is directly discharged into a drying and preheating unit 2 to be subjected to preheating and drying with mineral powder;
step three: secondary desulfurization
After the solid material enters the fluidized bed of the desulfurization reactor 4, unreacted pyrite minerals in the solid material and oxygen in fluidized air further undergo desulfurization reaction for 5-30 min until all pyrite components in the solid material complete the desulfurization reaction, so as to obtain high-temperature clinker and reaction waste gas, wherein the high-temperature clinker directly enters the waste heat recovery unit 5, and the reaction waste gas directly enters the suspension desulfurization furnace 3 for recycling;
step four: waste heat recovery
When the high-temperature clinker enters a cyclone cooler of the waste heat recovery unit 5, the high-temperature clinker exchanges heat with cold air from the outside, the high-temperature clinker is cooled to below 100 ℃ step by step to form cooling clinker, meanwhile, the cold air is heated to 320-500 ℃ step by step to form preheated air, the cooled clinker is discharged into a clinker storage bin for storage, and the preheated air directly enters a suspension desulfurization furnace 3 for fuel combustion supporting of a combustion system 6;
step five: exhaust gas purification
After the dust-containing waste gas enters the purification unit 7, the desulfurization purification and the dust removal are sequentially finished, the formed solid dust directly returns to the drying and preheating unit 2 to be recovered, the formed purified waste gas is discharged into the atmosphere through the discharge unit 8, and the recovered SO2Storing for preparing acid.
The embodiments are not intended to limit the scope of the present invention, and all equivalent implementations or modifications that do not depart from the scope of the present invention are intended to be included within the scope of the present invention.
Claims (9)
1. A high-sulfur bauxite dry desulfurization device is characterized in that: the system comprises a feeding unit, a drying and preheating unit, a suspension desulfurization furnace, a desulfurization reactor, a waste heat recovery unit, a combustion system, a purification unit and a discharge unit; the feeding end of the feeding unit is used for inputting high-sulfur bauxite powder, the discharging end of the feeding unit is communicated with the feeding end of the drying preheating unit through a first chute, the waste gas discharging end of the drying preheating unit is communicated with the waste gas inlet end of the purifying unit through a dust-containing waste gas discharging pipe, the ash returning end of the purifying unit is communicated with the feeding end of the drying preheating unit through an ash returning pipe, the waste gas discharging end of the purifying unit is communicated with the waste gas inlet end of the discharging unit through a purified waste gas discharging pipe, and the waste gas discharging end of the discharging unit is used for outputting waste gas; the discharge end of the drying and preheating unit is communicated with the feed end of the suspension desulfurization furnace through a first discharge pipe, the hot waste gas discharge end of the suspension desulfurization furnace is communicated with the dry preheating gas inlet end of the drying and preheating unit through a hot waste gas discharge pipe, the discharge end of the suspension desulfurization furnace is communicated with the feed end of the desulfurization reactor through a second discharge pipe, the reaction waste gas discharge end of the desulfurization reactor is communicated with the reaction waste gas inlet end of the suspension desulfurization furnace through a reaction waste gas discharge pipe, the discharge end of the desulfurization reactor is communicated with the feed end of the waste heat recovery unit through a second chute, the hot air discharge end of the waste heat recovery unit is communicated with the hot flue gas inlet end of the suspension desulfurization furnace through a hot air discharge pipe, the discharge end of the waste heat recovery unit is used for outputting clinker, and the cold air inlet end of the waste heat recovery unit is used for inputting cold air; the high-temperature flue gas discharge end of the combustion system is output in three paths, the first path is directly communicated with the hot flue gas inlet end of the suspension desulfurization furnace, the second path is communicated with the dry preheating gas inlet end of the dry preheating unit through a first high-temperature flue gas discharge pipe, and the third path is communicated with the hot flue gas inlet end of the waste heat recovery unit through a second high-temperature flue gas discharge pipe; and the gas inlet end of the combustion system is used for inputting gas.
2. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the feeding unit comprises a buffer bin and a metering scale, a feeding port of the buffer bin is used as a feeding end of the feeding unit, a discharging port of the buffer bin is provided with a material saving valve, the discharging port of the buffer bin is externally connected with a feeding chute through the metering scale, and the discharging port of the feeding chute is used as a discharging end of the feeding unit.
3. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the drying and preheating unit comprises a dryer and a preheater, and the dryer is communicated with the preheater through a pipeline; the preheaters adopt a single-stage structure or a multi-stage structure, and the multi-stage preheaters are communicated through pipelines; the feed inlet of the dryer is used as the feed end of the drying preheating unit; when the preheater adopts a single-stage structure, a discharge port of the single-stage preheater is used as a discharge end of the drying preheating unit; when the preheater adopts a multi-stage structure, the discharge port of the final-stage preheater is used as the discharge end of the drying preheating unit.
4. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the suspension desulfurization furnace comprises a suspension reactor and a cyclone separator, wherein the main body structure of the suspension reactor is cylindrical, and the bottom of the suspension reactor is conical; the feeding port of the suspension reactor is used as the feeding end of the suspension desulfurization furnace, the discharging port at the top of the suspension reactor is communicated with the feeding port of the cyclone separator, and the discharging port of the cyclone separator is used as the discharging end of the suspension desulfurization furnace.
5. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the desulfurization reactor comprises a fluidized bed, a fluidized air station and a Roots blower, wherein a feed inlet of the fluidized bed is used as a feed end of the desulfurization reactor, and a discharge outlet of the fluidized bed is used as a discharge end of the desulfurization reactor; the fluidized bed is communicated with the fluidized air station and the fluidized air station is communicated with the Roots blower through pipelines; the fluidized bed adopts a multi-chamber fluidized bed, each chamber of the fluidized bed is internally provided with an independent air chamber, and an air blower is arranged on each air chamber; air is adopted as fluidized wind, and the fluidized wind station and the Roots blower provide the fluidized wind.
6. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the waste heat recovery unit comprises a cyclone cooler and a fluidized bed cooler, and the cyclone cooler is communicated with the fluidized bed cooler through a pipeline; the cyclone coolers adopt a single-stage structure or a multi-stage structure, and the multi-stage cyclone coolers are communicated through a pipeline; when the cyclone cooler adopts a single-stage structure, a feed inlet of the cyclone cooler is used as a feed end of the waste heat recovery unit; when the cyclone cooler adopts a multi-stage structure, the feed inlet of the first-stage cyclone cooler is used as the feed end of the waste heat recovery unit; and a discharge port of the fluidized bed cooler is used as a discharge end of the waste heat recovery unit.
7. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the combustion system comprises a main combustion station, an auxiliary combustion station, a starting combustion station and a drying combustion station, wherein the main combustion station, the auxiliary combustion station and the starting combustion station adopt solid fuel, liquid fuel or gas fuel.
8. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the purification unit comprises a gas desulfurization device, a dust remover, a chute, a centrifugal fan, pneumatic conveying equipment and a Roots fan, wherein the gas desulfurization device, the dust remover, the chute, the centrifugal fan, the pneumatic conveying equipment and the Roots fan are communicated through pipelines; the fluidized air in the chute is provided by a centrifugal fan; conveying wind in the pneumatic conveying equipment is provided by a Roots blower; the dust remover adopts a bag-type dust remover, a metal filter bag dust remover, an electric dust remover or an electric bag dust remover; the pneumatic conveying equipment adopts a pneumatic lifting pump, a bin type pump or a vertical spiral feeding pump.
9. The dry desulfurization device for the high-sulfur bauxite according to claim 1, characterized in that: the exhaust unit comprises an induced draft fan, an air door and a chimney, an air outlet of the induced draft fan is communicated with the chimney through the air door, and an exhaust outlet of the chimney is communicated with the atmosphere.
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| CN113667519A (en) * | 2021-08-25 | 2021-11-19 | 中冶赛迪上海工程技术有限公司 | Desulfurization system for blast furnace gas and control method thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113667519A (en) * | 2021-08-25 | 2021-11-19 | 中冶赛迪上海工程技术有限公司 | Desulfurization system for blast furnace gas and control method thereof |
| CN113667519B (en) * | 2021-08-25 | 2023-06-27 | 中冶赛迪上海工程技术有限公司 | Desulfurization system for blast furnace gas and control method thereof |
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