CN103058279B - Method for preparing vanadium pentoxide through fluidization - Google Patents
Method for preparing vanadium pentoxide through fluidization Download PDFInfo
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- CN103058279B CN103058279B CN201210547782.1A CN201210547782A CN103058279B CN 103058279 B CN103058279 B CN 103058279B CN 201210547782 A CN201210547782 A CN 201210547782A CN 103058279 B CN103058279 B CN 103058279B
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Abstract
The invention provides a method for preparing vanadium pentoxide through fluidization. The method comprises the following steps of: drying ammonium vanadate by using first hot air to control the weight percentage content of moisture in the ammonium vanadate to be not greater than 1%; adding the dried ammonium vanadate into a fluidization reacting furnace and providing compressed air in the fluidization reacting furnace to fluidize the ammonium vanadate; providing second hot air to a heat exchange unit arranged in the fluidization reacting furnace so as to control the temperature in the fluidization reacting furnace to 650-750 DEG C; controlling the pressure in the fluidization reacting furnace to 5-8 kPa so as to generate ammonium vanadate; discharging the ammonium vanadate from a fluidization reactor; and then cooling and collecting the ammonium vanadate. The method for preparing the vanadium pentoxide through fluidization, disclosed by the invention, has the advantages of high production efficiency, long service life of devices, fast reaction speed, easy realization of continuous and automatic operation, and the like.
Description
Technical field
The present invention relates to the extractive technique of Vanadium Pentoxide in FLAKES, more particularly, relate to a kind of in the industrial method of producing continuously Vanadium Pentoxide in FLAKES in fluidization mode.
Background technology
In the prior art, conventionally the major equipment using rotary kiln as production Vanadium Pentoxide in FLAKES, but its life-span is shorter, and its basic reason is that the performance of manufactured materials can not meet processing requirement, rotary kiln is high temperature operation under corrosive gases condition, because of stressed excessive fracture.Simultaneously the specification of rotary kiln is less, production capacity is low, gas effciency is low, energy consumption and cost all higher.In addition, the gas leakage of rotary kiln technology in order to prevent that equipment from may occur, requirement has stricter sealing, but due to the factor of processing and manufacturing and installation, on large-sized rotary kiln, be generally not easy to realize, this just requires factory building must keep good ventilation state, therefore, utilizes rotary kiln to produce Vanadium Pentoxide in FLAKES and has some limitations.
Summary of the invention
For prior art above shortcomings, the invention provides a kind of fluidization and produce the method for Vanadium Pentoxide in FLAKES.
The invention provides a kind of fluidization and produce the method for Vanadium Pentoxide in FLAKES.Said method comprising the steps of: use the first warm air drying ammonium vanadate, control moisture weight percentage≤1% in ammonium vanadate; Dried ammonium vanadate is added to fluidization Reaktionsofen, in co-current flow state Reaktionsofen, provide pressurized air so that ammonium vanadate is fluidization; By answering the heat exchange unit in stove that the second hot blast is provided to being arranged on fluidization, taking by the temperature control in fluidization Reaktionsofen as 650～750 DEG C; The pressure of controlling in fluidization Reaktionsofen is 5～8kPa, to generate Vanadium Pentoxide in FLAKES; From fluidizing reactor, discharge Vanadium Pentoxide in FLAKES, then Vanadium Pentoxide in FLAKES is carried out cooling and collected.
In one exemplary embodiment of the present invention, in the step of described use warm air drying ammonium vanadate, the bulk density control of ammonium vanadate is 0.5～0.7g/cm
3; Drying temperature control is 120～300 DEG C.
In one exemplary embodiment of the present invention, in the described step that dried ammonium vanadate is added to fluidization Reaktionsofen, feed in raw material and control feed rate as 200～400kg/h in the mode of spiral charging.
In one exemplary embodiment of the present invention, described compressed-air actuated pressure-controlling is at 75～90kPa, and its flow control is 100～150Nm
3/ h, and excessive pressurized air is discharged by dust-removal cloth-bag.
In one exemplary embodiment of the present invention, described cooling step is down to the temperature of Vanadium Pentoxide in FLAKES≤and 150 DEG C.
In one exemplary embodiment of the present invention, described the second hot blast is provided by hotblast stove, and pressure-controlling in hotblast stove is-50～-150Pa.
Compared with prior art, the beneficial effect of method of the present invention comprises: production efficiency is high, equipment life is long, speed of response is fast, be easy to realize serialization and automated operation etc.
Brief description of the drawings
By the description of carrying out below in conjunction with accompanying drawing, above and other object of the present invention and feature will become apparent, wherein:
Fig. 1 shows fluidization according to an exemplary embodiment of the present invention and produces the structural representation of the fluidization equipment that the method for Vanadium Pentoxide in FLAKES adopts;
Fig. 2 shows the cross sectional representation of the heat exchange unit of the fluidization equipment of Fig. 1.
Description of reference numerals:
11-retort, 12-gas feed, 13-pneumatic outlet, the import of 14-solid particle material, the outlet of 15-solid particle material, 16-gas distributor
21-solid particle material feed bin, 22-positive feed spiral
The import of 31-hot blast, 32-hot-blast outlet, 33-heat exchange pipeline, 34-flange
The cooling classifier of 41-, 42-opening for feed, 43-inlet mouth, 44-the first discharge nozzle, 45-the second discharge nozzle, 46-the 3rd gas distribution grid
51-the first dipleg, 52-the second dipleg, 53-the first expansion joint, 54-the second expansion joint, 55-the 3rd expansion joint
Embodiment
Hereinafter, describe fluidization of the present invention in detail and produce the method for Vanadium Pentoxide in FLAKES in connection with exemplary embodiment.
The method that Vanadium Pentoxide in FLAKES is produced in fluidization according to the present invention comprises the following steps: use the first warm air drying ammonium vanadate, control moisture weight percentage≤1% in ammonium vanadate; Dried ammonium vanadate is added to fluidization Reaktionsofen, in co-current flow state Reaktionsofen, provide pressurized air so that ammonium vanadate is fluidization; By answering the heat exchange unit in stove that the second hot blast is provided to being arranged on fluidization, taking by the temperature control in fluidization Reaktionsofen as 650～750 DEG C; The pressure of controlling in fluidization Reaktionsofen is 5～8kPa, to generate Vanadium Pentoxide in FLAKES; From fluidizing reactor, discharge Vanadium Pentoxide in FLAKES, then Vanadium Pentoxide in FLAKES is carried out cooling and collected.
The method that Vanadium Pentoxide in FLAKES is produced in fluidization of the present invention can adopt fluidization equipment to realize, described fluidization equipment comprises feed unit, fluidizing reactor, aerodynamic force feed unit, heat exchange unit, cooling and go out material unit, wherein, described fluidizing reactor comprises retort, gas feed, pneumatic outlet, solid particle material import, solid particle material outlet and gas distributor, described aerodynamic force feed unit is connected with the gas feed of fluidizing reactor and for making solid particle material be fluidization, described feed unit is connected with the solid particle material import of fluidizing reactor and for the solid particle material of question response is provided to fluidizing reactor, described heat exchange unit is arranged in the retort of fluidizing reactor and for heat solid granule materials, described solid materials outlet cooling and that go out material unit and fluidizing reactor is connected and for reaction product cooling and discharge fluidizing reactor.
In another exemplary embodiment, described fluidization equipment can also comprise the first dipleg and the second dipleg, wherein, described the first dipleg comprises the first gas distribution grid, the first left arm and the first right arm, the bottom of the bottom of the first left arm and the first right arm is communicated with, the first gas distribution grid is arranged on the connectivity part of the first left arm and the first right arm, the bottom that is positioned at the first gas distribution grid below of the first left arm and the first right arm is provided with gas inlet, the height of the first right arm is higher than the height of the first left arm, the upper end of the first right arm is communicated with feed unit, the upper end of the first left arm is communicated with the solid particle material import of fluidizing reactor, described the second dipleg comprises the second gas distribution grid, the second left arm and the second right arm, the bottom of the bottom of the second left arm and the second right arm is communicated with, the second gas distribution grid is arranged on the connectivity part of the second left arm and the second right arm, the bottom that is positioned at the second gas distribution grid below of the second left arm and the second right arm is provided with gas inlet, the height of the second right arm is higher than the height of the second left arm, the outlet of the upper end of the second right arm and the solid particle material of fluidizing reactor is communicated with, and the upper end of the second left arm is with cooling and go out material unit and be communicated with.
In another exemplary embodiment, described fluidization equipment can also comprise the first expansion joint, the second expansion joint and the 3rd expansion joint, and wherein, the first expansion joint connects the upper end of the first left arm and the solid particle material import of fluidizing reactor; The second expansion joint connects the upper end of right arm of the second dipleg and the outlet of the solid particle material of fluidizing reactor, and the 3rd expansion joint connects the upper end of the second left arm and cooling and go out material unit.
In another exemplary embodiment, fluidization equipment cooling and go out material unit and comprise cooling classifier, opening for feed, inlet mouth, the first discharge nozzle, the second discharge nozzle and the 3rd gas distribution grid, wherein, opening for feed is communicated with cooling classifier with the solid materials outlet of fluidizing reactor, the 3rd gas distribution grid is arranged on the bottom of cooling classifier along the radial direction of cooling classifier, the first discharge nozzle is arranged on the middle and lower part of cooling classifier and is positioned at the top of the 3rd gas distribution grid, the second discharge nozzle is arranged on the top of cooling classifier, inlet mouth and cooling classifier bottom are communicated with and are positioned at the below of the 3rd gas distribution grid.
Generally speaking, method of the present invention adds ammonium vanadate in fluidization Reaktionsofen, and under hot conditions, deamination decomposes, and obtains powdery Vanadium Pentoxide in FLAKES product.Specifically, another exemplary embodiment of the present invention also can realize in the following ways:
A, utilize hot blast to be dried ammonium vanadate
Wherein, ammonium vanadate bulk density is controlled to 0.5～0.7g/cm
3; Dry temperature is controlled to 120～300 DEG C; By dried ammonium vanadate water content≤1%.
B, dried ammonium vanadate is added in fluidized reaction stove
For example, adopt the mode of spiral charging to carry out positive feed; Can also be by the input speed of the electric machine frequency control ammonium vanadate of feed auger; And the input speed of ammonium vanadate can be controlled at 200～400kg/h.
C, provide power by pressurized air, make ammonium vanadate in Reaktionsofen, realize fluidisation
For example, pressurized air sees through gas distribution grid and enters in Reaktionsofen, makes ammonium vanadate in Reaktionsofen, form uniform flow field.Compressed-air actuated pressure can be controlled at 75～90kPa, and its flow control can be at 100～150Nm
3/ h.In addition, excessive pressurized air can be by discharging after dust-removal cloth-bag, to collect the particulate reaction product of discharging with pressurized air.
After D, the powdery Vanadium Pentoxide in FLAKES of reaction after finishing are cooling, enter finished product bin
The temperature of Vanadium Pentoxide in FLAKES is cooled to≤150 DEG C after discharging be advisable.For example, can carry out further cooling to Vanadium Pentoxide in FLAKES by water jacket.
E, the hot blast producing by Combustion of Hot Air Furnace ensure temperature of reaction
For example, the temperature of hotblast stove can be controlled at 650～750 DEG C; Hotblast stove internal pressure can be controlled at-50～-150Pa; The temperature that the material outlet of fluidization Reaktionsofen goes out can be controlled at 500～600 DEG C.
F, control the reaction times by Reaktionsofen internal pressure
For example, Reaktionsofen internal pressure is controlled to 5～8kPa, to control the rational reaction times.For example, the reaction times of material in fluidization Reaktionsofen can be controlled at 5～30min.
Fig. 1 shows fluidization according to an exemplary embodiment of the present invention and produces the structural representation of the fluidization equipment that the method for Vanadium Pentoxide in FLAKES adopts.
As shown in Figure 1, comprise at a fluidization equipment that exemplary embodiment adopts of method of the present invention: fluidizing reactor, feed unit, heat exchange unit, cooling and go out material unit and aerodynamic force feed unit.
Wherein, fluidizing reactor comprises retort 11, gas feed 12, pneumatic outlet 13, solid particle material import 14, solid particle material outlet 15 and gas distributor 16.Gas distributor 16 can be conventional gas distribution grid, and its along continuous straight runs is arranged on the bottom of retort 11.Gas inlet is arranged on the bottom of retort 11 and is positioned at the below of gas distribution grid; Solid particle material import 14 is arranged on a sidepiece (for example, left side) of retort 11, and the residing position of solid particle material import 14 is higher than the residing position of gas distribution grid; Solid particle material outlet 15 is arranged on another sidepiece (for example, right side) of retort 11, and the height that solid particle material exports 15 residing positions is higher than the residing height location of solid particle material import 14; Pneumatic outlet 13 is arranged on top or the top of retort 11, and the residing position of pneumatic outlet 13 exports 15 residing positions higher than solid particle material.
In this exemplary embodiment, feed unit comprises solid particle material feed bin 21 and positive feed spiral 22.Positive feed spiral 22 be arranged on solid particle material feed bin 21 discharge port below and for example, for the solid particle material of solid particle material feed bin 21 (, ammonium vanadate particle) is delivered in the solid particle material import 14 of fluidizing reactor.But feed unit of the present invention is not limited to this, other device that can make solid particle material enter fluidizing reactor also can be used as feed unit of the present invention.
Fig. 2 shows the cross sectional representation of the heat exchange unit of the fluidization equipment of Fig. 1.As illustrated in fig. 1 and 2, in this exemplary embodiment, heat exchange unit comprises the hot blast import 31, hot-blast outlet 32 and the heat exchange pipeline 33 that are communicated with successively.Heat exchange pipeline 33 is arranged in the retort 11 of fluidizing reactor, and comprises many heat exchange arms.Hot blast import 31 is for providing hot blast to heat exchange pipeline 33, and the gas that hot-blast outlet 32 completes heat exchange for heat exchange pipeline 33 is derived.In addition, heat exchange unit can be connected with fluidizing reactor by flange 34.
For example, hot blast is provided by coal gas or coal combustion, enters heat exchange pipeline 33 by hot air duct entrance, bending in fluidizing reactor, leaves fluidization equipment from hot air duct outlet.But, the invention is not restricted to this, also can be by other heat exchange device (for example, electrical heating element etc.) replace as heat exchange unit of the present invention, as long as it can heat the fluidised solid particle material that is in retort 11, so that solid particle material reaches suitable temperature of reaction.
In this exemplary embodiment, cooling and go out material unit and comprise cooling classifier 41, opening for feed 42, inlet mouth 43, the first discharge nozzle 44, the second discharge nozzle 45 and the 3rd gas distribution grid 46.Wherein, cooling classifier 41 can have bilayer structure (that is, inside and outside layer), and solid particulate is in cooling classifier 41 inside, and between interlayer, has recirculated cooling water, carries out cooling for the solid particulate that reaction is finished.Opening for feed 42 is communicated with cooling classifier 41 with the solid materials outlet of fluidizing reactor.The 3rd gas distribution grid 46 is arranged on the bottom of cooling classifier 41 along the radial direction of cooling classifier 41.Inlet mouth 43 and cooling classifier 41 bottoms are communicated with and are positioned at the below of the 3rd gas distribution grid 46.The first discharge nozzle 44 is arranged on the middle and lower part of cooling classifier 41, so that cooled coarse grained anti-product product is discharged.The second discharge nozzle 45 is arranged on the top of cooling classifier 41, so that the fine particle reaction product rising after cooling, with gas is discharged.Inlet mouth 43 is realized in cooling classifier 41 and is provided steady air flow (for example together with the 3rd gas distribution grid 46, high normal pressure and temperature stream of nitrogen gas), thereby can make from the first discharge nozzle 44, to discharge in fluidization mode through the cooled reaction product of overcooling classifier 41, and described stable air-flow can also be gas at normal temperature, like this can further cooling reaction product.In this exemplary embodiment, described the second discharge nozzle 45 is also communicated with the pneumatic outlet 13 of fluidizing reactor, and finally also can be connected with sack cleaner, thus be convenient to from the second discharge nozzle 45 discharge fine particle reaction product and the fine particle reaction product of discharging from the pneumatic outlet 13 of fluidizing reactor reclaim together.
In this exemplary embodiment, fluidization equipment also comprises the first dipleg 51 and the second dipleg 52.
Wherein, the first dipleg 51 comprises the first gas distribution grid, the first left arm and the first right arm, the bottom of the bottom of the first left arm and the first right arm is communicated with, the first gas distribution grid is arranged on the connectivity part of the first left arm and the first right arm, the bottom that is positioned at the first gas distribution grid below of the first left arm and the first right arm (is for example provided with gas, nitrogen) entrance, the height of the first right arm is higher than the height of the first left arm, the upper end of the first right arm is communicated with positive feed spiral 22, the upper end of the first left arm is communicated with the solid particle material import 14 of fluidizing reactor.The second dipleg 52 comprises the second gas distribution grid, the second left arm and the second right arm, the bottom of the bottom of the second left arm and the second right arm is communicated with, the second gas distribution grid is arranged on the connectivity part of the second left arm and the second right arm, the bottom that is positioned at the second gas distribution grid below of the second left arm and the second right arm (is for example provided with gas, nitrogen) entrance, the height of the second right arm is higher than the height of the second left arm, the upper end of the second right arm is communicated with the solid particle material of fluidizing reactor outlet 15, the upper end of the second left arm is with cooling and go out material unit and be communicated with.The first dipleg 51 and the second dipleg 52 mainly play the effect of sealing gland, that is, avoid in fluidized reaction stove, provide the gas trains of fluidisation power to go out, and can make fluidization reaction of the present invention carry out with more continuous, stable state.The gas feeding in the first dipleg 51 and the second dipleg 52 can provide by another aerodynamic force feed unit.
In this exemplary embodiment, fluidization equipment also comprises the first expansion joint 53, the second expansion joint 54 and the 3rd expansion joint 55.Wherein, the first expansion joint 53 connects the upper end of the first left arm and the solid particle material import 14 of fluidizing reactor; The second expansion joint 54 connects the upper end of right arm and the solid particle material of the fluidizing reactor outlet 15 of the second dipleg 52; The 3rd expansion joint 55 connects the upper end of the second left arm and cooling and go out material unit.The first expansion joint 53, the second expansion joint 54 and the 3rd expansion joint 55 are set can make fluidization equipment of the present invention adapt to Yin Gaowen and the expansion that produces.
Aerodynamic force feed unit is communicated with the gas feed 12 of fluidizing reactor, and for stable compressed air is provided to fluidizing reactor.The gas that aerodynamic force feed unit feeds has two Main Functions, and the one, for the suspension of solid particle material in whole fluidizing reactor provides dynamic condition, the 2nd, participate in the reaction of solid particulate.
That is to say, the air-flow that aerodynamic force feed unit provides provides uniform air-flow to the solid particle material in fluidizing reactor by gas feed 12 from bottom to top from fluidizing reactor lower end, make solid particle material keep good suspension mobility, thereby ensure fully carrying out of reaction.After reaction finishes, reaction product (, Vanadium Pentoxide in FLAKES) flows into the second dipleg 52 of discharge end, and then the second dipleg 52 bottoms blow through the gas of gas distribution grid, keep a kind of suspended state, finally enter in cooling classifier 41, carry out cooling and classification.It should be noted that, the residence time of solid particle material in fluidizing reactor is by the pressure difference control in fluidizing reactor.
On the whole, fluidization equipment of the present invention utilizes gas as propulsion source, makes gas and solid, fully contacts, evenly mixes, and then complete reaction between solid and solid.Utilize the temperature-stable of heat exchange pipeline guarantee gas-solid reaction system simultaneously, and the work-ing life of extension device.In addition, fluidization equipment of the present invention can be realized from solid particle material and enter fluidization equipment, leaves in the whole process of fluidization equipment to solid particulate, and solid particulate is the state in a kind of suspension all, have the mobile physical property of fluid, the generation and the serialization that are conducive to reaction are produced.In addition, the gas that fluidization equipment of the present invention can also be used in heating does not directly contact with solid particle material, has ensured the temperature controllability of gas-solid reaction body.
Method of the present invention can be produced powdery Vanadium Pentoxide in FLAKES continuously to comprise that the fluidization equipment of fluidization Reaktionsofen is realized, and more than its output can reach 280kg/h, thereby has greatly improved the production efficiency of powdery Vanadium Pentoxide in FLAKES, has reduced production cost.
Further describe fluidization of the present invention and produce the method for Vanadium Pentoxide in FLAKES below in conjunction with concrete example.In following example, the composition of powdery Vanadium Pentoxide in FLAKES records according to GB 3238-87 method.
Example 1
Be 0.6g/cm by bulk density
3ammonium vanadate (being abbreviated as APV) at 200 DEG C of temperature, be dried to water content 1%, then by feed auger, APV is entered in fluidized reaction stove, inlet amount is controlled at 220kg/h.Control compressed-air actuated pressure 80kPa, flow 100Nm
3/ h, makes material in fluidized furnace, form a uniform flow field.By controlling hot-blast furnace temperature at 650 DEG C, material outlet temperature is at 520 DEG C, for dehydration, deamination, the oxygenolysis of ammonium vanadate provide good condition.To the reaction times be controlled at 10min, the Vanadium Pentoxide in FLAKES of generation, through pressure-air cooling to 120 DEG C, obtains product.This Vanadium Pentoxide in FLAKES output is 160kg/h, V in product
2o
5content is 98.13 % by weight, and Si content is 0.15 % by weight, and Fe is that content is 0.05 % by weight, P content <0.01 % by weight, and S content is 0.02 % by weight, As content is 0.01 % by weight, Na
2o+K
2o content is 0.8 % by weight, V
2o
4content is 1.2 % by weight.
Example 2
Produce powdery Vanadium Pentoxide in FLAKES according to the method for example 1, difference is, inlet amount is controlled at 300kg/h, and hot-blast furnace temperature is at 700 DEG C, and material outlet temperature is at 550 DEG C.And the powdery Vanadium Pentoxide in FLAKES output obtaining is 210kg/h, the composition in product meets the requirement in GB 3238-87.
Example 3
Produce powdery Vanadium Pentoxide in FLAKES according to the method for embodiment 1, difference is, inlet amount is controlled at 400kg/h, and compressed air pressure is controlled at 90kPa, and hot-blast furnace temperature is at 750 DEG C, and material outlet temperature is at 580 DEG C.Material reaction times in Reaktionsofen is controlled at 7min; And the powdery Vanadium Pentoxide in FLAKES output obtaining reaches 285kg/h, the composition in product still meets the requirement in GB 3238-87.
To sum up, the method tool that Vanadium Pentoxide in FLAKES is produced in fluidization of the present invention has the following advantages:
(1) can make solid particulate suspend and flow, thereby ensure steady, efficient, the reaction of fluidization fully;
(2) compared with the rotary kiln technology of prior art, the present invention is simple in structure, on-the-spot easy for installation, simultaneously because fluidizing reactor itself is fixed, therefore, is conducive to extension device work-ing life.
(3), compared with the rotary kiln technology of prior art, the present invention has that production efficiency is high, speed of response fast, operation is easy to realize the advantage such as serialization and automatization.
Although described the present invention with exemplary embodiment by reference to the accompanying drawings above, those of ordinary skill in the art should be clear, in the case of not departing from the spirit and scope of claim, can carry out various amendments to above-described embodiment.
Claims (10)
1. a method for Vanadium Pentoxide in FLAKES is produced in fluidization, it is characterized in that, said method comprising the steps of:
Use the first warm air drying ammonium vanadate, control moisture weight percentage≤1% in ammonium vanadate;
Dried ammonium vanadate is added to fluidization Reaktionsofen, in co-current flow state Reaktionsofen, provide pressurized air so that ammonium vanadate is fluidization;
By answering the heat exchange unit in stove that the second hot blast is provided to being arranged on fluidization, taking by the temperature control in fluidization Reaktionsofen as 650～750 DEG C, described the second hot blast not be fluidised ammonium vanadate and directly contact;
The pressure of controlling in fluidization Reaktionsofen is 5～8kPa, to generate Vanadium Pentoxide in FLAKES;
From fluidizing reactor, discharge Vanadium Pentoxide in FLAKES, then Vanadium Pentoxide in FLAKES is carried out cooling and collected.
2. the method for Vanadium Pentoxide in FLAKES is produced in fluidization according to claim 1, it is characterized in that, in the step of described use warm air drying ammonium vanadate, the bulk density control of ammonium vanadate is 0.5～0.7g/cm
3; Drying temperature control is 120～300 DEG C.
3. the method for Vanadium Pentoxide in FLAKES is produced in fluidization according to claim 1, it is characterized in that, in the described step that dried ammonium vanadate is added to fluidization Reaktionsofen, feeds in raw material and controls feed rate as 200～400kg/h in the mode of spiral charging.
4. the method for Vanadium Pentoxide in FLAKES is produced in fluidization according to claim 1, it is characterized in that, described compressed-air actuated pressure-controlling is at 75～90kPa, and its flow control is 100～150Nm
3/ h, and excessive pressurized air is discharged by dust-removal cloth-bag.
5. the method for Vanadium Pentoxide in FLAKES is produced in fluidization according to claim 1, it is characterized in that, and described cooling step is down to the temperature of Vanadium Pentoxide in FLAKES≤and 150 DEG C.
6. the method for Vanadium Pentoxide in FLAKES is produced in fluidization according to claim 1, it is characterized in that, described the second hot blast is provided by hotblast stove, and pressure-controlling in hotblast stove is-50～-150Pa.
7. produce the method for Vanadium Pentoxide in FLAKES according to the fluidization described in any one in claim 1 to 6, it is characterized in that, described method adopts fluidization equipment to realize, described fluidization equipment comprises feed unit, fluidizing reactor, aerodynamic force feed unit, heat exchange unit, cooling and go out material unit, wherein, described fluidizing reactor comprises retort, gas feed, pneumatic outlet, solid particle material import, solid particle material outlet and gas distributor, described aerodynamic force feed unit is connected with the gas feed of fluidizing reactor and for making solid particle material be fluidization, described feed unit is connected with the solid particle material import of fluidizing reactor and for the solid particle material of question response is provided to fluidizing reactor, described heat exchange unit is arranged in the retort of fluidizing reactor and for heat solid granule materials, described solid materials outlet cooling and that go out material unit and fluidizing reactor is connected and for reaction product cooling and discharge fluidizing reactor.
8. fluidization equipment according to claim 7, it is characterized in that, described fluidization equipment also comprises the first dipleg and the second dipleg, wherein, described the first dipleg comprises the first gas distribution grid, the first left arm and the first right arm, the bottom of the bottom of the first left arm and the first right arm is communicated with, the first gas distribution grid is arranged on the connectivity part of the first left arm and the first right arm, the bottom that is positioned at the first gas distribution grid below of the first left arm and the first right arm is provided with gas inlet, the height of the first right arm is higher than the height of the first left arm, the upper end of the first right arm is communicated with feed unit, the upper end of the first left arm is communicated with the solid particle material import of fluidizing reactor, described the second dipleg comprises the second gas distribution grid, the second left arm and the second right arm, the bottom of the bottom of the second left arm and the second right arm is communicated with, the second gas distribution grid is arranged on the connectivity part of the second left arm and the second right arm, the bottom that is positioned at the second gas distribution grid below of the second left arm and the second right arm is provided with gas inlet, the height of the second right arm is higher than the height of the second left arm, the outlet of the upper end of the second right arm and the solid particle material of fluidizing reactor is communicated with, and the upper end of the second left arm is with cooling and go out material unit and be communicated with.
9. fluidization equipment according to claim 8, it is characterized in that, described fluidization equipment also comprises the first expansion joint, the second expansion joint and the 3rd expansion joint, and wherein, the first expansion joint connects the upper end of the first left arm and the solid particle material import of fluidizing reactor; The second expansion joint connects the upper end of right arm of the second dipleg and the outlet of the solid particle material of fluidizing reactor, and the 3rd expansion joint connects the upper end of the second left arm and cooling and go out material unit.
10. fluidization equipment according to claim 7, it is characterized in that, described cooling and go out material unit and comprise cooling classifier, opening for feed, inlet mouth, the first discharge nozzle, the second discharge nozzle and the 3rd gas distribution grid, wherein, opening for feed is communicated with cooling classifier with the solid materials outlet of fluidizing reactor, the 3rd gas distribution grid is arranged on the bottom of cooling classifier along the radial direction of cooling classifier, the first discharge nozzle is arranged on the middle and lower part of cooling classifier and is positioned at the top of the 3rd gas distribution grid, the second discharge nozzle is arranged on the top of cooling classifier, inlet mouth and cooling classifier bottom are communicated with and are positioned at the below of the 3rd gas distribution grid.
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| CN100582257C (en) * | 2007-11-26 | 2010-01-20 | 攀枝花钢铁(集团)公司 | Method for roasting high calcium vanadium slag with fluidizing apparatus |
| CN101844809B (en) * | 2010-04-28 | 2014-09-17 | 深圳中科九台资源利用研究院有限公司 | System and method for producing vanadium trioxide |
| CN102616848A (en) * | 2012-02-27 | 2012-08-01 | 河北钢铁股份有限公司承德分公司 | Production method and production system for vanadium pentoxide |
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