CN101844809A - System and method for producing vanadium trioxide - Google Patents
System and method for producing vanadium trioxide Download PDFInfo
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- CN101844809A CN101844809A CN201010162947A CN201010162947A CN101844809A CN 101844809 A CN101844809 A CN 101844809A CN 201010162947 A CN201010162947 A CN 201010162947A CN 201010162947 A CN201010162947 A CN 201010162947A CN 101844809 A CN101844809 A CN 101844809A
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- 238000004519 manufacturing process Methods 0.000 title abstract description 17
- QUEDYRXQWSDKKG-UHFFFAOYSA-M [O-2].[O-2].[V+5].[OH-] Chemical compound [O-2].[O-2].[V+5].[OH-] QUEDYRXQWSDKKG-UHFFFAOYSA-M 0.000 title abstract 5
- 239000007789 gas Substances 0.000 claims abstract description 78
- 230000009467 reduction Effects 0.000 claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical group [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000003546 flue gas Substances 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 238000007599 discharging Methods 0.000 claims abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 10
- 239000000463 material Chemical group 0.000 claims abstract description 9
- 238000002485 combustion reaction Methods 0.000 claims abstract description 6
- 230000008878 coupling Effects 0.000 claims abstract description 4
- 238000010168 coupling process Methods 0.000 claims abstract description 4
- 238000005859 coupling reaction Methods 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 21
- 239000000843 powder Substances 0.000 claims description 16
- 239000003795 chemical substances by application Substances 0.000 claims description 15
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 claims description 14
- UNTBPXHCXVWYOI-UHFFFAOYSA-O azanium;oxido(dioxo)vanadium Chemical compound [NH4+].[O-][V](=O)=O UNTBPXHCXVWYOI-UHFFFAOYSA-O 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000003034 coal gas Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- 238000005243 fluidization Methods 0.000 claims description 7
- 230000008676 import Effects 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 4
- 238000013459 approach Methods 0.000 claims description 4
- 235000009508 confectionery Nutrition 0.000 claims description 4
- 239000003345 natural gas Substances 0.000 claims description 4
- 230000001590 oxidative effect Effects 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000010419 fine particle Substances 0.000 claims description 2
- 238000010304 firing Methods 0.000 claims description 2
- 238000002309 gasification Methods 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 229910052720 vanadium Inorganic materials 0.000 abstract description 16
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 abstract description 16
- 238000011084 recovery Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 238000006722 reduction reaction Methods 0.000 description 37
- 238000005516 engineering process Methods 0.000 description 10
- 230000008569 process Effects 0.000 description 7
- 230000002829 reductive effect Effects 0.000 description 7
- 238000012546 transfer Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000002826 coolant Substances 0.000 description 4
- 239000004744 fabric Substances 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- LOUBVQKDBZRZNQ-UHFFFAOYSA-M [O-2].[O-2].[OH-].O.[V+5] Chemical compound [O-2].[O-2].[OH-].O.[V+5] LOUBVQKDBZRZNQ-UHFFFAOYSA-M 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000011031 large-scale manufacturing process Methods 0.000 description 2
- INZDTEICWPZYJM-UHFFFAOYSA-N 1-(chloromethyl)-4-[4-(chloromethyl)phenyl]benzene Chemical compound C1=CC(CCl)=CC=C1C1=CC=C(CCl)C=C1 INZDTEICWPZYJM-UHFFFAOYSA-N 0.000 description 1
- 241000628997 Flos Species 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- SKKMWRVAJNPLFY-UHFFFAOYSA-N azanylidynevanadium Chemical compound [V]#N SKKMWRVAJNPLFY-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 239000010431 corundum Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- PNXOJQQRXBVKEX-UHFFFAOYSA-N iron vanadium Chemical compound [V].[Fe] PNXOJQQRXBVKEX-UHFFFAOYSA-N 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
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- 238000001149 thermolysis Methods 0.000 description 1
- 150000003682 vanadium compounds Chemical class 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention discloses a system and a method for producing vanadium trioxide, and belongs to the technical field of chemical industry. The system comprises a fluidized reduction furnace, a feeding system, a combustion system, a cooling system, a tail gas treatment system, and a discharging system. A heat exchange member is arranged inside the fluidized reduction furnace, and is in a U shape; the heat exchange member makes flue gas and materials exchange heat in a mode of coupling reverse flow with cross flow; the fluidized gas enters the furnace from a fluidized air inlet and the raw materials enter the furnace from a feed inlet; the fluidized gas moves from bottom to top to suspend the raw materials in the furnace body and drive the raw materials to move upwards and be discharged from a discharge hole, and the reaction tail gas is exhausted from a tail gas outlet; the heat exchange member has the functions of improving the fluidized state and exchanging heat simultaneously; and high-temperature flue gas enters the furnace from a flue gas inlet, and after heat exchange, the high-temperature flue gas is exhausted from a flue gas outlet. The system for producing the vanadium trioxide has the advantages of applicability to mass production of vanadium trioxide, good device tightness, high safety, high reaction efficiency, vanadium recovery rate of over 99.4 percent, and vanadium grade in the vanadium trioxide of 67.9 percent.
Description
Technical field
The invention belongs to chemical technology field, refer more particularly to a kind of system and method thereof of producing vanadous oxide.
Background technology
Vanadous oxide is a kind of grey black that is, and the crystalline powder of metalluster is arranged, the hexagonal with corundum structure.Vanadous oxide can slow oxidation change vanadium tetraoxide in air, and vanadous oxide can violent burning generate vanadium tetraoxide during heating.Vanadous oxide is a kind of important vanadium compound, and it has important use in fields such as metallurgy, electronics, chemical industry.Vanadous oxide can be used for producing vanadium iron, also can make vanadium carbide or vanadium nitride etc. to vanadous oxide and directly produce special steel material in the adding molten steel.Vanadous oxide also can be used for producing the vanadium metal powder.In addition, vanadous oxide also can be directly used in electronic products such as producing thermoelectric converter.
Industrially produce vanadous oxide by reduction ammonium meta-vanadate or Vanadium Pentoxide in FLAKES usually, shown in reaction formula (1), (2):
2NH
4VO
3+2H
2＝2NH
3+V
2O
3+3H
2O 800℃ -330.4kJ/mol (1)
V
2O
5+2H
2＝V
2O
3+2H
2O 800℃ -6.9kJ/mol (2)
By reaction formula (1), (2) as can be seen, produce vanadous oxide with normal temperature (25 ℃) ammonium meta-vanadate, 1 mole of product needed of every acquisition is replenished the heat of 330.4kJ; Produce vanadous oxide with normal temperature (25 ℃) Vanadium Pentoxide in FLAKES, 1 mole of product of every acquisition also need replenish the heat of 6.9kJ.As seen, producing vanadous oxide, particularly is that the reaction that raw material is produced vanadous oxide is a strong endothermic reaction with the ammonium meta-vanadate, and a main difficult problem that is faced with in the industrial production provides heat for reaction exactly.
It is that the ammonium vanadate thermolysis cracking process of reactor is produced vanadous oxide with the rotary kiln that U.S. Pat 3410652 discloses, this kind technology is comparatively simple, but temperature of reaction adopts the mode of naked light heating that heat is provided up to 900 ℃, and promptly the mode with flame calcination rotary kiln shell provides heat.The Flos Bombacis Malabarici iron and steel group of China is a reactor with the rotary kiln, is that reductive agent is produced vanadous oxide with the coke-oven gas under 850 ℃ temperature condition, adopts the mode of naked light heating that heat is provided equally.Rotary kiln shell is often burnt in process of production, operating rate, low casualty ratio of accidents height, has serious potential safety hazard.In addition, also there is following problem in the production method that with the rotary kiln is reactor: 1. rotary kiln high temperature dynamic seal difficulty, in fact the rotary kiln that carries out at present the suitability for industrialized production vanadous oxide does not both at home and abroad fundamentally solve sealing problem, and producing all is to carry out to guarantee safety in the airy workshop fully; 2. service temperature height (general requirement reaches more than 850 ℃), material filling ratio low (5%), reaction efficiency is low, and the reducing gas waste is serious; Recovery time longer, generally need more than 1 hour, product grade lower (product vanadium grade is about 64%) is not suitable for producing high-purity vanadous oxide.
People are exploring vanadous oxide production method more efficiently always, Chinese patent CN101028938A discloses a kind of method that adopts fluidization process to produce vanadous oxide, its method is powder ammonium vanadate or Vanadium Pentoxide in FLAKES to be joined add in the hot fluidized bed furnace boiler tube, in boiler tube, feed industrial gas from the fluidized bed furnace bottom, boiler tube is heated to 600～650 ℃ simultaneously, reduced 3～9 minutes, and under nonoxidizing atmosphere, be cooled to below 100 ℃ subsequently and come out of the stove, obtain vanadous oxide.This kind process stream filling ratio can arrive 50%, the gas effciency height, and reduction temperature is low, the time is short, can obtain grade and surpass 67% vanadous oxide product.The heating of this kind process using electric furnace, heat of reaction is provided, the main problem that has two aspects: (1) heat interchanging area is little, heat interchanging area equals the fluidized bed furnace boiler tube and places surface-area within the electric furnace, and promptly heat transfer area and boiler tube diameter are linear, and reaction institute's heat requirement and boiler tube diameter are quadratic relation, therefore, heat transfer area becomes the principal element that limited reactions device diameter amplifies, and this structure only is fit to laboratory and small-scale production, can not be used for large-scale production; (2) electrically heated cost height.In addition, this fluidization process only exists simple opening for feed, discharge port, can't realize the successive charging and discharging, can only periodical operation, and only be adapted at laboratory scale and produce vanadous oxide.Efficient, the economic heat of reaction that provides still is provided the scale operation vanadous oxide, and fluidizing reactor amplifies, and problems such as continuous charging and discharging need to be resolved hurrily.
At present, a kind of production technique of safe, efficient, low-cost, the vanadous oxide that can be mass-produced is badly in need of in this area.
Summary of the invention
The purpose of this invention is to provide a kind of system and method thereof of producing vanadous oxide, existing equipment and technology are expensive, efficient is low to overcome, can't realize defectives such as scale operation.
System of the present invention comprises fluidized reduction furnace, feed system, firing system, cooling system, exhaust treatment system, discharge system; Fluidizing agent import, opening for feed, discharge port, tail gas mouth, exhanst gas outlet, gas approach are arranged on the fluidized reduction furnace; Heat exchange component is set in the fluidized reduction furnace, and heat exchange component is the U type; Heat exchange component makes flue gas and material with the mode of coupling reverse flow with cross flow heat exchange; Fluidizing agent is entered by the fluidizing agent import, and raw material is entered by opening for feed, and fluidizing agent from bottom to top moves, and raw material is suspended in the body of heater, and drives raw material and move upward, and discharges from discharge port, and reaction end gas is discharged by the tail gas mouth; Heat exchange component has the effect that improves fluidized state and heat exchange simultaneously, and high-temperature flue gas is entered by gas approach, after the heat exchange, is discharged by exhanst gas outlet.
Method of the present invention as shown in Figure 2.Comprise following processing step:
1, raw material is arranged in feed bin, enters in the fluidized reduction furnace through screw feeder, charging dipleg; Feeding rate is 100～500kg/h;
2, coal gas is in 700～1200 ℃ high-temperature flue gas in combustion chamber internal combustion formation temperature, and high-temperature flue gas is by the heat exchange component in the fluidized reduction furnace, and discharge subsequently heating fluidized reduction furnace to 600～800 ℃;
3, fluidizing agent (also being reducing medium) enters from the fluidizing agent import of fluidized reduction furnace, blows afloat raw material, makes it to be in fluidized state, and reduction V
5+5～30 minutes, obtain the vanadous oxide product;
4, vanadous oxide enters fluidization cooling classifier via the discharging dipleg, is heat-eliminating medium with gas and water in non-oxidizing gas, below the cooling vanadous oxide to 100 ℃, enters the product feed bin via the discharge with endless screw device subsequently;
5, reaction end gas is through burning and exhausting after gas cooler cooling, the sack cleaner dedusting, and the vanadous oxide particle in the tail gas is via the discharge with endless screw device, the fine particle product feed bin that enters.
Raw material of the present invention is meant any in ammonium vanadate powder or the Vanadium Pentoxide in FLAKES powder; Described coal gas is meant any in coke-oven gas, blast furnace gas, town gas, Sweet natural gas, coal gas of converter, the producer gas; Described fluidizing agent is meant any one or more mixing in hydrogen, carbon monoxide, ammonia, gasification synthetic gas, coke-oven gas, blast furnace gas, coal gas of converter, the producer gas; Described non-oxidizing gas is meant any in nitrogen, coke-oven gas, blast furnace gas, town gas, Sweet natural gas, coal gas of converter, the producer gas.
The advantage of system of the present invention is:
1, provides a kind of efficient, reliable heat-supplying mode, make it to satisfy the demand of scale operation vanadous oxide.
2, heat exchange component is dismountable, can keep in repair, replace, and has the effect that improves fluidized state and heat exchange simultaneously.
3, material is in fluidized state in the stove, and heat transmission resistance is little.
4, in the fluidized reduction furnace flue gas and material with the mode of coupling reverse flow with cross flow heat exchange, the heat exchange efficiency height.
5, major technique thought of the present invention is that also to improve rate of mass transfer be that means are enhanced productivity, reduction V
5+The reaction process of producing vanadous oxide is improved rate of mass transfer and can be enhanced productivity by mass transfer process control.The present invention is the resistance that raw material reduces internal diffusion with the powder, is reactor with the fluidized reduction furnace, increases the contact area between the gas-solid two-phase, reduces the resistance of external diffusion, thereby can greatly enhance productivity.
6, major technique thought of the present invention is that also the filling ratio to improve reactor is that means are enhanced productivity, and the filling ratio of rotary kiln is about 5%, and the filling ratio of fluidized reduction furnace can reach 50%, increases substantially the utilising efficiency of space reactor.
7, fluidized reduction furnace of the present invention has heat exchange function simultaneously and the function of fluidization reaction conditions is provided, and equipment is simple, and the production efficiency height is fit to large-scale production, meets the requirement of producing high-purity vanadous oxide technology simultaneously again.With the fluidized reduction furnace is that reactor is produced vanadous oxide, under 800 ℃ temperature of reaction, can finish reduction reaction within 5 minutes, even under 600 ℃ temperature of reaction, also only needed 30 minutes can finish reduction reaction, therefore, the reaction efficiency height, reaction conditions is comparatively gentle, requirement to the material of fluidized reduction furnace is lower, is easy to processing and fabricating, has also improved production security.
Technology of the present invention is with the beneficial effect that the existing rotary kiln technology that is used for vanadous oxide production is compared:
1. substitute moving equipment with static equipment, good airproof performance, safe;
2. service temperature low (600～800 ℃), equipment is reliable, the operating rate height;
3. material filling ratio height can reach 50%, and the reaction efficiency height has increased substantially the utilization ratio (usage quantity of reducing gas reduce than rotary kiln 50%) of reducing gas;
Recovery time shorter, 5～30 minutes, product vanadium grade higher (＞67%);
5. output is big, is easy to mass-producing.
Technology of the present invention is with the beneficial effect that the existing laboratory fluidization technology that is used for vanadous oxide production is compared:
1. realize the amplification of fluidizing reactor, can be used for the scale operation of vanadous oxide;
2. solved the problem that heat of reaction is provided for scale operation, reduced production costs;
3. by charging dipleg, discharging dipleg, realize realizing serialization production by continuously feeding, the discharging continuously of normal pressure to high-tension apparatus.
Description of drawings
Fig. 1 fluidized reduction furnace structure iron.
Fig. 2 vanadous oxide technological process of production figure.Wherein, feed bin 1, screw feeder 2, charging dipleg 3, combustion chamber 4, fluidized reduction furnace 5, discharging dipleg 6, fluidization cooling classifier 7, discharge with endless screw device 8, gas cooler 9, sack cleaner 10, discharge with endless screw device 11.
Embodiment
The present invention is described further below in conjunction with drawings and Examples.
Embodiment 1: with the feeding rate of 300kg/h, the Vanadium Pentoxide in FLAKES powder enters Φ 900 * 3500mm fluidized reduction furnace as shown in Figure 1 via feed auger, charging dipleg.Form 1200 ℃ flue gas after the coke-oven gas burning, flue gas enters fluidized reduction furnace, by heat exchange heating fluidized reduction furnace to 800 ℃.160Nm
3The coke-oven gas of/h is entered by fluidized reduction furnace bottom wind scoop, blow afloat the Vanadium Pentoxide in FLAKES powder, reduced 5 minutes, obtain vanadous oxide, vanadous oxide is via discharging dipleg, fluidizing cooler subsequently, be that heat-eliminating medium is cooled to 80 ℃ to vanadous oxide with nitrogen and water coolant simultaneously, enter the product feed bin via the discharging spiral again.Reaction end gas is through burning and exhausting after the sack cleaner dedusting, and the vanadous oxide particle in the tail gas enters the feed bin under the cloth bag.
After testing, the vanadium grade 67.9% of product vanadous oxide, vanadium recovery 99.7%.
Embodiment 2: with the feeding rate of 400kg/h, the ammonium vanadate powder enters Φ 900 * 3500mm fluidized reduction furnace as shown in Figure 1 via feed auger, charging dipleg.Form 1000 ℃ flue gas after the coke-oven gas burning, flue gas enters fluidized reduction furnace, by heat exchange heating fluidized reduction furnace to 700 ℃.180Nm
3The producer gas generator coal gas of/h is entered by fluidized reduction furnace bottom wind scoop, blow afloat the ammonium vanadate powder, reduced 10 minutes, obtain vanadous oxide, vanadous oxide is via discharging dipleg, fluidizing cooler subsequently, be that heat-eliminating medium is cooled to 100 ℃ to vanadous oxide with nitrogen and water coolant simultaneously, enter the product feed bin via the discharging spiral again.Reaction end gas is through burning and exhausting after the sack cleaner dedusting, and the vanadous oxide particle in the tail gas enters the feed bin under the cloth bag.
After testing, the vanadium grade 67.6% of product vanadous oxide, vanadium recovery 99.4%.
Embodiment 3: with the feeding rate of 200kg/h, the ammonium vanadate powder enters Φ 900 * 3500mm fluidized reduction furnace as shown in Figure 1 via feed auger, charging dipleg.Form 700 ℃ flue gas after the blast furnace gas burning, flue gas enters fluidized reduction furnace, by heat exchange heating fluidized reduction furnace to 600 ℃.90Nm
3The CO (carbon monoxide converter) gas of/h is entered by fluidized reduction furnace bottom wind scoop, blow afloat the ammonium vanadate powder, reduced 30 minutes, obtain vanadous oxide, vanadous oxide is via discharging dipleg, fluidizing cooler subsequently, be that heat-eliminating medium is cooled to 50 ℃ to vanadous oxide with nitrogen and water coolant simultaneously, enter the product feed bin via the discharging spiral again.Reaction end gas is through burning and exhausting after the sack cleaner dedusting, and the vanadous oxide particle in the tail gas enters the feed bin under the cloth bag.
After testing, the vanadium grade 67.2% of product vanadous oxide, vanadium recovery 99.6%.
Embodiment 4: with the feeding rate of 400kg/h, the ammonium vanadate powder enters Φ 900 * 3500mm fluidized reduction furnace as shown in Figure 1 via feed auger, charging dipleg.Form 1100 ℃ flue gas after the producer gas generator gas-fired, flue gas enters fluidized reduction furnace, by heat exchange heating fluidized reduction furnace to 750 ℃.140Nm
3The hydrogen of/h is entered by fluidized reduction furnace bottom wind scoop, blow afloat the ammonium vanadate powder, reduced 8 minutes, obtain vanadous oxide, vanadous oxide is via discharging dipleg, fluidizing cooler subsequently, be that heat-eliminating medium is cooled to 70 ℃ to vanadous oxide with nitrogen and water coolant simultaneously, enter the product feed bin via the discharging spiral again.Reaction end gas is through burning and exhausting after the sack cleaner dedusting, and the vanadous oxide particle in the tail gas enters the feed bin under the cloth bag.
After testing, the vanadium grade 67.7% of product vanadous oxide, vanadium recovery 99.6%.
By above example as seen compared with prior art, the present invention has the following advantages: be applicable to the scale operation vanadous oxide; Equipment good airproof performance, safe; The reaction efficiency height, the shortest only need can be finished reaction in 5 minutes; Good product quality, vanadium recovery are greater than 99.4%, and the vanadium grade can reach 67.9%. in the vanadous oxide, exceed near 4% than rotary kiln product vanadium grade; The reducing gas consumption is lower by 50% than rotary kiln, and production cost is low.Technology of the present invention and equipment obviously are better than prior art, are fit to the high-purity vanadous oxide of scale operation, have broad application prospects.
Claims (6)
1. a system that produces vanadous oxide comprises fluidized reduction furnace, feed system, firing system, cooling system, exhaust treatment system, discharge system; Fluidizing agent import, opening for feed, discharge port, tail gas mouth, exhanst gas outlet, gas approach are arranged on the fluidized reduction furnace; It is characterized in that heat exchange component is set in the fluidized reduction furnace, and heat exchange component is the U type; Heat exchange component makes flue gas and material with the mode of coupling reverse flow with cross flow heat exchange; Fluidizing agent is entered by the fluidizing agent import, and raw material is entered by opening for feed, and fluidizing agent from bottom to top moves, and raw material is suspended in the body of heater, and drives raw material and move upward, and discharges from discharge port, and reaction end gas is discharged by the tail gas mouth; Heat exchange component has the effect that improves fluidized state and heat exchange simultaneously, and high-temperature flue gas is entered by gas approach, after the heat exchange, is discharged by exhanst gas outlet.
2. a method that adopts the described system of claim 1 to produce vanadous oxide is characterized in that, comprises following processing step:
(1) raw material is arranged in feed bin, enters in the fluidized reduction furnace through screw feeder, charging dipleg; Feeding rate is 100～500kg/h;
(2) coal gas is in 700～1200 ℃ high-temperature flue gas in combustion chamber internal combustion formation temperature, and high-temperature flue gas is by the heat exchange component in the fluidized reduction furnace, and discharge subsequently heating fluidized reduction furnace to 600～800 ℃;
(3) fluidizing agent enters from the fluidizing agent import of fluidized reduction furnace, blows afloat raw material, makes it to be in fluidized state, and reduction V
5+5～30 minutes, obtain the vanadous oxide product;
(4) vanadous oxide enters fluidization cooling classifier via the discharging dipleg, is heat-eliminating medium with gas and water in non-oxidizing gas, below the cooling vanadous oxide to 100 ℃, enters the product feed bin via the discharge with endless screw device subsequently;
(5) reaction end gas is through burning and exhausting after gas cooler cooling, the sack cleaner dedusting, and the vanadous oxide particle in the tail gas is via the discharge with endless screw device, the fine particle product feed bin that enters.
3. method according to claim 2 is characterized in that: described raw material is a kind of in ammonium vanadate powder or the Vanadium Pentoxide in FLAKES powder.
4. method according to claim 2 is characterized in that described coal gas is meant any in coke-oven gas, blast furnace gas, town gas, Sweet natural gas, coal gas of converter, the producer gas.
5. method according to claim 2 is characterized in that, described fluidizing agent is meant any one or more mixing in hydrogen, carbon monoxide, ammonia, gasification synthetic gas, coke-oven gas, blast furnace gas, coal gas of converter, the producer gas.
6. method according to claim 2 is characterized in that described non-oxidizing gas is meant any in nitrogen, coke-oven gas, blast furnace gas, town gas, Sweet natural gas, coal gas of converter, the producer gas.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102557134A (en) * | 2011-12-23 | 2012-07-11 | 中国科学院过程工程研究所 | Fluidized reduction furnace for producing high-purity vanadium trioxide and production method |
| CN103058279A (en) * | 2012-12-17 | 2013-04-24 | 攀钢集团攀枝花钢钒有限公司 | Method for preparing vanadium pentoxide through fluidization |
| CN103695954A (en) * | 2013-12-12 | 2014-04-02 | 中国科学院过程工程研究所 | Method for preparing vanadium trioxide from vanadate by direct electrolysis |
| CN103922403A (en) * | 2014-03-24 | 2014-07-16 | 攀钢集团攀枝花钢铁研究院有限公司 | Method for producing powdery vanadic anhydride by ammonium polyorthovanadate in fluidization state |
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| CN102557134A (en) * | 2011-12-23 | 2012-07-11 | 中国科学院过程工程研究所 | Fluidized reduction furnace for producing high-purity vanadium trioxide and production method |
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| CN103695954A (en) * | 2013-12-12 | 2014-04-02 | 中国科学院过程工程研究所 | Method for preparing vanadium trioxide from vanadate by direct electrolysis |
| CN103922403A (en) * | 2014-03-24 | 2014-07-16 | 攀钢集团攀枝花钢铁研究院有限公司 | Method for producing powdery vanadic anhydride by ammonium polyorthovanadate in fluidization state |
| CN103922403B (en) * | 2014-03-24 | 2015-09-16 | 攀钢集团攀枝花钢铁研究院有限公司 | The method of powdery Vanadium Pentoxide in FLAKES is produced in a kind of ammonium poly-vanadate fluidization |
| CN105984899A (en) * | 2015-01-30 | 2016-10-05 | 中国科学院过程工程研究所 | System and method for purifying vanadium pentoxide |
| CN105986126A (en) * | 2015-01-30 | 2016-10-05 | 中国科学院过程工程研究所 | System and method for high-efficiency extraction of vanadium from vanadium slag through chlorination |
| CN105984899B (en) * | 2015-01-30 | 2017-05-17 | 中国科学院过程工程研究所 | System and method for purifying vanadium pentoxide |
| CN105986126B (en) * | 2015-01-30 | 2017-10-03 | 中国科学院过程工程研究所 | A kind of system and method for the efficient chlorination vanadium extraction of vanadium slag |
| US10294118B2 (en) | 2015-01-30 | 2019-05-21 | Institute Of Process Engineering, Chinese Academy Of Sciences | System and method for purifying vanadium pentoxide |
| CN106006734A (en) * | 2016-05-16 | 2016-10-12 | 武汉理工大学 | Method of using vanadium-containing solution for preparing vanadium trioxide |
| CN111634945A (en) * | 2020-06-12 | 2020-09-08 | 承德锦科科技股份有限公司 | Device and method for producing low-valence vanadium oxide |
| CN111634945B (en) * | 2020-06-12 | 2021-08-31 | 承德锦科科技股份有限公司 | Device and method for producing low-valence vanadium oxide |
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