CN114111359A - Stone coal navajoite gradient oxidizing roasting vanadium extraction system and oxidizing roasting method - Google Patents

Stone coal navajoite gradient oxidizing roasting vanadium extraction system and oxidizing roasting method Download PDF

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CN114111359A
CN114111359A CN202111274119.4A CN202111274119A CN114111359A CN 114111359 A CN114111359 A CN 114111359A CN 202111274119 A CN202111274119 A CN 202111274119A CN 114111359 A CN114111359 A CN 114111359A
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roasting
reactor
cyclone separator
heat exchange
stone coal
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高占奎
韩跃新
李艳军
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Shanghai Fengshi Technology Co ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/10—Roasting processes in fluidised form
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/20—Obtaining niobium, tantalum or vanadium
    • C22B34/22—Obtaining vanadium
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D19/00—Arrangements of controlling devices

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  • Mechanical Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
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Abstract

The invention provides a stone coal vanadium ore gradient oxidizing roasting vanadium extraction system and an oxidizing roasting method, wherein the system comprises: the feeding system consists of a bin, a weightlessness scale and a spiral feeding pipe; the material circulating heat storage system consists of a primary cyclone separator, a flow seal valve, a main furnace and a secondary cyclone separator; a step oxidizing roasting system consisting of a decarburization roasting reactor, a crystal breaking roasting reactor and an ore discharge heat exchange pipe; the negative pressure dust removal system consists of a three-stage cyclone separator, an ash bucket, a bag-type dust collector, a Roots blower and a chimney; the invention can realize the purpose of sectional suspension roasting of materials by connecting the decarburization roasting reactor and the crystal breaking roasting reactor in series; in addition, the system comprises four stages of heat exchange processes and a first stage of self-heating utilization process, and the whole energy utilization rate is extremely high, so the stepped oxidation roasting system has the advantages of independent and controllable two-stage roasting, full gas-solid contact, high energy utilization rate, high mass and heat transfer efficiency, low operation cost, high efficiency, environmental protection and the like.

Description

Stone coal navajoite gradient oxidizing roasting vanadium extraction system and oxidizing roasting method
Technical Field
The invention belongs to the technical field of vanadium extraction from stone coal vanadium ore, and particularly relates to a stone coal vanadium ore step oxidizing roasting vanadium extraction system and an oxidizing roasting method.
Background
At present, the vanadium extraction process of stone coal has more types, and mainly comprises sodium roasting-water leaching, calcification roasting-acid (alkali) leaching, composite additive roasting-leaching, additive-free oxidation roasting-acid (alkali) leaching, direct leaching and other processes. For the carbonaceous stone coal vanadium ore, the roasting process is a ring which is crucial to improving the leaching rate, and the existing roasting equipment mainly comprises a horizontal kiln and a vertical kiln.
Suspension roasting is used as a fluidized roasting technology and has the advantages of full gas-solid contact, high mass and heat transfer efficiency, low operation cost, environmental protection and the like. Particularly, the NEUH series suspension roasting industrial equipment and technology make a certain technical breakthrough in the aspect of high-efficiency utilization of refractory mineral products such as refractory iron ores, iron-manganese ores, high-iron bauxite, high-iron red mud, carbon-containing gold ores, stone coal vanadium ores and the like, and part of projects are industrially applied. The related patents are as in application No. 200720014578.8 suspension magnetization roasting furnace, CN106868292A multi-stage suspension magnetization roasting-magnetic separation system device and method for refractory iron ore, CN111644267A complex iron ore reinforced separation method based on mineral phase subsection precise control, CN111500854A suspension roasting system and method for industrial processing of iron manganese ore, CN107460307A alumina suspension roasting furnace, CN111485100A method for carbon-containing gold ore suspension roasting and gold leaching rate enhancement, CN111304465A method for vanadium-containing stone coal decarburization-crystal breaking roasting and reinforced acid leaching vanadium extraction, and CN111304464A method for acid leaching vanadium extraction enhancement by acid mixing and aging of stone coal vanadium ore multistage roasting, and the existing sodiumizing roasting, calcifying roasting and composite additive roasting processes have the problems of serious pollution, poor roasting effect and low vanadium rate.
The existing roasting equipment is a flat kiln and a vertical kiln, which can not feed fine ore, and the ball or brick must be made, and the gas-solid contact is insufficient; the roasted product needs to be cooled and then crushed and ground, so that most of heat is wasted, the mass and heat transfer efficiency is low, and the operation cost is higher.
For the stone coal vanadium ore with higher carbon content, the existing suspension roasting equipment only has one reactor, and the temperature-controllable sectional roasting cannot be realized. The low-temperature decarburization and the high-temperature crystal breaking process occur in one reactor, and the sintering problem is easy to occur.
The existing suspension roasting equipment has high ore discharge and exhaust temperature, waste heat is not effectively recovered, and the heat utilization rate needs to be improved.
Disclosure of Invention
Aiming at the problems of a suspension roasting system in the prior art, the invention aims to provide a stone coal vanadium ore gradient oxidation roasting vanadium extraction system and an oxidation roasting method.
In order to achieve the above purpose, the solution of the invention is as follows:
the invention provides a stone coal vanadium ore step oxidation roasting vanadium extraction system, which comprises a feeding system, a material circulation heat storage system, a step oxidation roasting system and a negative pressure dust removal system.
The feeding system comprises a storage bin and a spiral feeding pipe which are connected through a weight loss scale.
The material circulation heat storage system comprises a primary cyclone separator, a flow sealing valve, a main furnace and a secondary cyclone separator, a feed inlet above the primary cyclone separator is communicated to the bottom end of a spiral feeding pipe through a pipeline, a discharge outlet at the bottom of the primary cyclone separator is communicated with the flow sealing valve, the flow sealing valve is communicated to the bottom end of the main furnace, a heat exchange air inlet pipe and a combustion port of a burner are arranged on the side wall of a feed inlet at the bottom end of the main furnace, the top end of the main furnace is communicated to a feed inlet above the secondary cyclone separator through a pipeline, and the feed inlet above the secondary cyclone separator is connected with the feed inlet above the primary cyclone separator through a pipeline.
The stepped oxidizing roasting system comprises a decarburization roasting reactor, a crystal breaking roasting reactor and an ore discharge heat exchange pipe which are sequentially connected in series, wherein the decarburization roasting reactor is connected to the bottom end of the secondary cyclone separator, and the ore discharge heat exchange pipe is communicated with a heat exchange air inlet pipe.
The negative pressure dust removal system comprises a three-level cyclone separator, an ash bucket, a bag-type dust collector, a Roots blower and a chimney, wherein the three-level cyclone separator is communicated with a one-level cyclone separator through an exhaust heat exchanger, the exhaust heat exchanger is communicated with a heat exchange air inlet pipe, the ash bucket is connected to the bottom end of the three-level cyclone separator, the bag-type dust collector is communicated to a feed inlet above the three-level cyclone separator, and the bag-type dust collector, the Roots blower and the chimney are sequentially communicated.
As a preferred embodiment of the invention, the flow seal valve, the decarburization roasting reactor and the crystal breaking roasting reactor have the same structure and respectively comprise a reactor cavity and an electric heating furnace sleeve wrapping the reactor cavity, a central partition plate, a loosening chamber, a fluidization chamber and an air distribution plate are arranged in the reactor cavity, the reactor cavity is separated by the central partition plate at the top, a gap is reserved between the bottom end of the central partition plate and the reactor cavity, the air distribution plate is arranged on the air distribution plate, the air distribution plate is parallel to the bottom of the reactor cavity, the fluidization chamber is arranged on the left side of the central partition plate, a discharge hole is arranged at the middle upper part of the outer side of the fluidization chamber, the loosening chamber is arranged on the right side of the central partition plate, and a feed hole is arranged at the center of the top of the loosening chamber.
As a preferred embodiment of the invention, fluidized air and loose air are introduced into the flow seal valve, the decarburization roasting reactor and the crystal breaking roasting reactor, and the volume flow of the fluidized air is 10-20m3H, fluidizing wind is mixed gas of air and oxygen; the volume flow of the loosening wind is 3-8m3And h, loosening wind is air.
As a preferred embodiment of the invention, the temperature of the electric heating furnace sleeve is 600-1050 ℃.
As a preferred embodiment of the invention, the roasting temperature in the decarburization roasting reactor is 550-650 ℃, and the roasting time is 1-2 h; the roasting temperature in the crystal breaking roasting reactor is 850-950 ℃, and the roasting time is 8-20 h.
As a preferred embodiment of the invention, the negative pressure of the Roots blower is (-2.0) - (-2.5) kpa.
As a preferred embodiment of the present invention, the heat exchange inlet pipe is a shell-and-tube type heat exchange inlet pipe; the ore discharging heat exchange pipe is a dividing wall type ore discharging heat exchange pipe.
As a preferred embodiment of the invention, V in the stone coal vanadium powder ore in the stone coal vanadium ore step oxidation roasting vanadium extraction system2O5The content is 0.6-1.5%.
A method for carrying out stone coal navajoite oxidizing roasting by using the stone coal navajoite step oxidizing roasting vanadium extraction system comprises the following steps:
(1) the materials enter a first-stage cyclone separator of the material circulating heat storage system through a feeding system, the fine ores subjected to primary cyclone separation enter a flow sealing valve and then enter a feeding port at the lower part of a main furnace, the materials are lifted in the main furnace and enter a second-stage cyclone separator through an upper pipeline and are discharged from a discharge port at the bottom of the second-stage cyclone separator;
(2) the material discharged from the secondary cyclone separator enters a decarburization roasting reactor, the decarburization roasting material is discharged from a discharge port of the reactor, then enters a crystal breaking roasting reactor, the crystal breaking roasting material is discharged from a discharge port of the reactor, and finally enters an ore discharge heat exchange pipe to be cooled and then discharged;
(3) and materials discharged from the first-stage cyclone separator sequentially pass through the exhaust heat exchanger and the third-stage cyclone separator in the negative pressure dust removal system and are stocked in the ash hopper and the bag-type dust remover, and gas is discharged through the Roots blower and the chimney.
Due to the adoption of the scheme, the invention has the beneficial effects that:
the system realizes the low-temperature decarburization and the high-temperature crystal breaking sectional roasting of the stone coal by connecting two suspension roasting reactors (namely a decarburization roasting reactor and a crystal breaking roasting reactor) in series, so that the carbon-containing stone coal can be removed in the decarburization roasting reactor and then enters the crystal breaking roasting reactor for high-temperature roasting, and the sectional step roasting, the preferential decarburization and the sintering prevention can be realized; in addition, the electric heating furnace sleeves are arranged outside the decarburization roasting reactor and the crystal breaking roasting reactor, so that the temperature can be accurately controlled. Compared with the prior art, on one hand, the method avoids the phenomena of local overheating and sintering easily caused by directly carrying out high-temperature roasting in one reactor, and on the other hand, the operation parameters of the two sections of roasting processes can be independently controlled, thereby improving the leaching rate of vanadium in the roasted sample, such as reaction temperature, reaction time, roasting gas amount, oxygen concentration and the like.
Secondly, the system comprises a four-stage heat exchange and one-stage self-heating utilization process, namely, an exhaust heat exchanger and an ore discharge heat exchange pipe are arranged, the exhaust and ore discharge temperature of the system is reduced to be below 100 ℃, and part of heat is transferred to a heat exchange air inlet pipe for recycling; the exothermic heat of combustion of the carbonaceous materials in the raw ore also provides a part of heat source for the decarburization roasting reactor. Compared with the prior art, the energy utilization rate of the whole system is greatly improved, and the consumption of natural gas and electric energy of the system is obviously reduced, so that the energy utilization rate is greatly improved, and the energy consumption of the system is obviously reduced.
In a word, the invention belongs to an additive-free oxidizing roasting process, and can achieve the aim of efficiently extracting vanadium by two-stage step oxidizing roasting of stone coal fine ore, namely, low-temperature decarburization roasting is firstly carried out, and then high-temperature crystal breaking roasting is carried out, so that the leaching rate of a roasted sample is improved. The step oxidizing roasting system has the advantages of independent and controllable two-stage roasting, full gas-solid contact, high energy utilization rate, high mass and heat transfer efficiency, low operation cost, high efficiency, environmental protection and the like.
Drawings
FIG. 1 is a schematic diagram of a stone coal vanadium ore step oxidizing roasting vanadium extraction system of the invention.
FIG. 2 is a schematic structural view of a flow seal valve, a decarburization roasting reactor and a decrystallization roasting reactor of the present invention.
FIG. 3 is a schematic diagram of the energy flow of the stone coal vanadium ore step oxidizing roasting vanadium extraction system of the present invention.
Reference numerals: 1-a storage bin, 2-a weightlessness scale, 3-a spiral feeding pipe, 4-a primary cyclone separator, 5-a flow seal valve, 6-a main furnace, 7-a secondary cyclone separator, 8-a decarburization roasting reactor, 9-a crystal breaking roasting reactor, 10-a heat exchange air inlet pipe, 11-a burner, 12-a tertiary cyclone separator, 13-an ash bucket, 14-an exhaust heat exchanger, 15-a bag dust collector, 16-a Roots blower, 17-a chimney, 18-an ore discharge heat exchange pipe, 19-a central partition plate, 20-a loosening chamber, 21-a fluidizing chamber, 22-an air distribution plate and 23-an electric heating furnace sleeve.
Detailed Description
The invention provides a stone coal vanadium ore gradient oxidizing roasting vanadium extraction system and an oxidizing roasting method.
The stone coal vanadium ore step oxidizing roasting vanadium extraction system comprises a feeding system, a material circulating heat storage system, a step oxidizing roasting system and a negative pressure dust removal system.
As shown in figure 1, the feeding system comprises a storage bin 1 and a lower end spiral feeding pipe 3 connected with the storage bin through a weightlessness scale 2, and the feeding amount can be accurately adjusted through the motor frequency of the weightlessness scale 2.
The material circulation heat storage system comprises a primary cyclone separator 4, a flow seal valve 5, a main furnace 6 and a secondary cyclone separator 7, wherein a feed inlet above the primary cyclone separator 4 is communicated to the bottom end of a spiral feeding pipe 3 through a pipeline, a discharge outlet at the bottom of the primary cyclone separator 4 is communicated with the flow seal valve 5 (namely ore discharge at the bottom of the primary cyclone separator 4 passes through the flow seal valve 5), the flow seal valve 5 is communicated to the bottom end of the main furnace 6, a heat exchange air inlet pipe 10 (specifically a shell-and-tube heat exchange air inlet pipe) and a combustion port of a combustor 11 are arranged on the side wall of a feed inlet at the bottom end of the main furnace 6, room-temperature air is heated by the heat exchange air inlet pipe 10 and then enters the main furnace 6, and the combustor 11 continuously combusts natural gas serving as fuel to further heat the air. The top end of the primary furnace 6 is connected to the feed inlet above the secondary cyclone 7 through a top horizontal pipe, so that the primary cyclone 4, the flow seal valve 5, the primary furnace 6 and the secondary cyclone 7 form a closed loop. The feed inlet above the secondary cyclone separator 7 is connected with the feed inlet above the primary cyclone separator 4 through a pipeline.
The step oxidizing roasting system comprises a decarburization roasting reactor 8, a crystal breaking roasting reactor 9 and an ore discharge heat exchange pipe 18 (specifically, a dividing wall type ore discharge heat exchange pipe) which are sequentially connected in series, wherein the decarburization roasting reactor 8 is connected to the bottom end of the secondary cyclone separator 7, the ore discharge heat exchange pipe 18 is communicated with a heat exchange air inlet pipe 10, the upper end of the ore discharge heat exchange pipe 18 is a hot end, and the lower end of the ore discharge heat exchange pipe 18 is a cold end.
Specifically, as shown in fig. 2, the flow seal valve 5, the decarburization roasting reactor 8 and the crystal breaking roasting reactor 9 have the same structure, and each of them includes a reactor cavity and an electric heating furnace jacket 23 wrapping the reactor cavity, that is, the electric heating furnace jacket 23 wraps around the outer wall of the reactor cavity to provide auxiliary heating for the reactor cavity, and the temperature control range is 600-. Reactor cavity is internal to be equipped with central baffle 19, not hard up room 20, fluidization chamber 21 and air distribution plate 22, reactor cavity is middle to be separated by the central baffle 19 at top, leave the space (be that the 19 downside of central baffle leaves the passageway, be used for the material circulation) between the bottom of central baffle 19 and the reactor cavity and set up air distribution plate 22, air distribution plate 22 has certain distance and is on a parallel with reactor cavity bottom apart from reactor cavity bottom, fluidization chamber 21 sets up the left side at central baffle 19, upper portion is equipped with the discharge gate in the outside of fluidization chamber 21, not hard up room 20 sets up the right side at central baffle 19, the top center of not hard up room 20 is equipped with the feed inlet. The loosening wind and the fluidizing wind blown from the lower part penetrate the wind distribution plate 22, so that the materials in the reactor cavity are in a suspended state.
In fact, the fluidized air and the loosening air are introduced into the flow seal valve 5, the decarburization roasting reactor 8 and the crystal breaking roasting reactor 9, and the materials therein form a non-mechanical lock under the action of the fluidized air and the loosening air, so that a good sealing effect can be achieved and air blowby can be prevented. Specifically, the volume flow of the fluidized wind is 10-20m3H, fluidizing wind is mixed gas of air and oxygen; the volume flow of the loosening wind is 3-8m3And h, loosening wind is air. The roasting temperature in the decarburization roasting reactor 8 is 550-650 ℃, and the roasting time is 1-2 h; the roasting temperature in the crystal breaking roasting reactor 9 is 850 ℃ and 950 ℃, and the roasting time is 8-20 h. Specifically, the decarburization roasting reactor 8 and the decrystallization roasting reactor 9 have the same structure but different sizes, and need to be adjusted according to actual conditions. Since the longer the calcination reaction time, the larger the required reactor size should be. Since the crystal breaking roasting time of the stone coal vanadium ore is much longer than the decarburization roasting time, the size of the crystal breaking roasting reactor 9 is larger. And the roasting time of each section can be adjusted by the size and the gas quantity of the reactor.
The negative pressure dust removal system comprises a three-stage cyclone separator 12, an ash bucket 13, a bag-type dust remover 15, a Roots blower 16 and a chimney 17, wherein the Roots blower 16 provides negative pressure for the whole system, and the negative pressure is (-2.0) - (-2.5) kpa. The three-stage cyclone separator 12 is communicated with the one-stage cyclone separator 4 through an exhaust heat exchanger 14, the exhaust heat exchanger 14 is communicated with a heat exchange air inlet pipe 10, the left end of the exhaust heat exchanger 14 is a hot end, the right end of the exhaust heat exchanger 14 is a cold end, an ash bucket 13 is connected to the bottom end of the three-stage cyclone separator 12, a bag-type dust remover 15 is communicated to a feed inlet above the three-stage cyclone separator 12, and the bag-type dust remover 15, a Roots blower 16 and a chimney 17 are communicated in sequence. The gas flow direction in the whole system is as follows: the heat exchange intake pipe 10 → the main furnace 6 → the secondary cyclone 7 → the primary cyclone 4 → the tertiary cyclone 12 → the bag-type dust collector 15 → the roots blower 16 → the chimney 17. Fine materials in raw ores are collected in an ash hopper 13 and a bag-type dust collector 15 at the lower end of a three-stage cyclone separator 12, and gas is discharged through a Roots blower 16 and a chimney 17.
The material flow direction of the system is as follows: the material bin 1 feeds materials into a pipeline through a spiral feeding pipe 3, then the materials enter a primary cyclone separator 4, the materials discharged from the lower portion of the primary cyclone separator 4 are fed into the bottom of a main furnace 6 through a flow sealing valve 5, the materials are lifted in the main furnace 6, enter a secondary cyclone separator 7 through an upper portion transverse pipe, then are fed into a decarburization roasting reactor 8 and a crystal breaking roasting reactor 9, and finally the roasted products are cooled through an ore discharging heat exchange pipe 18 and then are discharged.
The following are specifically mentioned: the stone coal vanadium ore step oxidizing roasting vanadium extraction system comprises a four-stage heat exchange process and a first-stage self-heating utilization process, and has extremely high energy utilization rate.
First-stage heat exchange: in the conduit to the primary cyclone 4. The room temperature material enters the initial end of the pipeline, and is heated to 400 ℃ from the room temperature while being transported by hot air, and the gas temperature is reduced to about 400 ℃ from 600 ℃.
Two-stage heat exchange: the main furnace 6 to a secondary cyclone 7. The material heated primarily is fed from the bottom of the main furnace 6 and lifted under the action of combustion hot gas and negative pressure of a fan, the high-temperature hot gas transfers heat to the material, so that the temperature of the material is raised to about 500 ℃, and the residual temperature of the hot gas is continuously used for heat exchange in one stage.
Three-stage heat exchange: an ore discharge heat exchange pipe 18 and a heat exchange air inlet pipe 10. The high temperature material discharged through the crystal breaking roasting reactor 9 is about 950 ℃, and the material is cooled to less than 100 ℃ under the cooling action of the ore discharging heat exchange pipe 18, and the part of heat is used for preheating the air entering the furnace at room temperature in the heat exchange air inlet pipe 10.
And (4) four-stage heat exchange: an exhaust heat exchanger 14 and a heat exchange intake pipe 10. The hot gas exiting the primary cyclone 4 is at about 400 c and the gas is cooled to <100 c by the cooling action of the exhaust gas heat exchanger 14. This portion of the heat is also used to preheat the incoming furnace air in the heat exchange inlet duct 10.
Self-heating utilization: in the decarbonizing roasting reactor 8. The decarburization roasting process is essentially carbon combustion, and since the raw ore itself contains carbon, part of the heat source in the decarburization roasting reactor 8 is released from the combustion of the raw ore itself, thereby achieving efficient utilization of the carbon.
As shown in fig. 3, during steady operation of the system, the heat input to the system can be considered to be used only for materials and gases that heat room temperature materials, room temperature gases to <100 ℃. The system has extremely high heat utilization rate and low energy consumption.
The invention relates to a method for carrying out stone coal navajoite oxidizing roasting by utilizing a stone coal navajoite step oxidizing roasting vanadium extraction system, which comprises the following steps:
(1) and starting the Roots blower 16, controlling the negative pressure of the blower to be (-2.0) - (-2.5) kpa, and providing the negative pressure for the interior of the system. The burner 11 is started to ignite the natural gas, the introduced air is burnt and heated, and high-temperature flue gas is formed and enters the main furnace 6.
(2) And introducing a certain amount of fluidized air and loosening air to the bottoms of the flow seal valve 5, the decarburization roasting reactor 8 and the crystal breaking roasting reactor 9. The loosening wind is air (3-8 m)3H), the fluidized wind is a mixed gas of air and oxygen (10-20 m)3H). The air source is provided by an air compressor.
(3) Mixing the coal vanadium powder ore (V) containing carbon stone2O5The content is 0.6-1.5 percent, -0.1mm, the carbon content is more than 3.5 percent) is fed into a bin 1 of a weightlessness scale 2, the weightlessness scale 2 is started, the powder ore is conveyed into a primary cyclone separator 4 through a spiral feeding pipe 3, and the material is heated to 350-400 ℃ in a first step. The powder ore separated by the primary cyclone enters the flow seal valve 5, and the material stocked in the flow seal valve 5 forms a non-mechanical lock under the action of loosening wind and fluidizing wind to play a role in material sealing.
(4) The materials enter the main furnace 6 from the outlet of the flow seal valve 5, and are lifted upwards under the action of negative pressure and hot air flow to enter the secondary cyclone separator 7. At this point the material is heated to about 500 ℃. The mineral powder is partially freed from adsorbed water, interlayer water and other volatile constituents. The product obtained after the two-stage heat exchange is the preheating roasting material.
(5) The preheated roasting material enters a decarburization roasting reactor 8. Setting the roasting temperature at 550 ℃ and 650 ℃, and adjusting the retention time of the materials in the reactor to be 1-2 h. In the decarbonizing roasting process, the reducing substances such as carbon, adsorption water, crystal water, pyrite and the like in the stone coal are almost completely removed, and the decarbonizing roasted material is discharged from a discharge port of the reactor.
(6) The decarbonization roasting material enters a crystal breaking roasting reactor 9 with larger size. Setting the roasting temperature at 850 ℃ and 950 ℃, and controlling the retention time of the materials in the reactor to be 8-20 h. During the crystal breaking roasting process, the crystal structure of the layered silicate vanadium-containing mineral (usually muscovite, sericite, illite and the like) is destroyed. The process of lattice destruction is: two OH in Al-O octahedron-Is heated to generate H2O escapes to form ion vacancy. This distorts the six-membered ring structure in an unbalanced manner on the one hand and elongates the lattice in the c-axis direction on the other hand. The octahedron where the V atom is located is elongated and deformed, and the binding energy is reduced, so that the octahedron is easier to leach out. And finally, discharging the crystal breaking roasting material from a discharge hole of the reactor.
(7) And the crystal breaking roasted material is cooled to be lower than 100 ℃ through an ore discharge heat exchange pipe 18 and then discharged, and a final stone coal vanadium ore roasted product is obtained.
(8) And the stone coal vanadium ore crystal breaking roasting product is used for extracting vanadium by subsequent sulfuric acid leaching.
The technical scheme in the embodiment of the invention is clearly and completely described below. It should be noted that the described embodiments of the present invention are provided for further explanation and illustration only, and do not limit the scope of the application thereof. All other embodiments, which can be derived by a person skilled in the art without making creative efforts, based on the present invention, belong to the protection scope of the present patent.
Example 1:
suspension roasting of a stone coal vanadium ore, wherein V2O5The content is 1.30%, the carbon content is 4.8%, and the content of minus 0.1mm is 90%.
(1) And starting the Roots blower 16, controlling the negative pressure of the Roots blower to be-2.0 kpa, providing negative pressure for the inside of the system, starting the burner 11 to ignite natural gas, and enabling high-temperature flue gas to enter the main furnace 6. The temperature of the top of the main furnace is kept at about 710 ℃.
(2) Introducing 3m into the flow seal valve 5310 m/h loosening wind (air)3H fluidized wind (air); 6m of gas is introduced into the decarburization roasting reactor 8319 m/h loosening wind (air)3H fluidized wind (16 m)3H air, 3m3H oxygen); 8m is introduced into the crystal breaking roasting reactor 93Wind (air) of the wind/h loosening, 20m3H fluidized wind (air).
(3) And setting a weight loss scale 2 to feed 100kg/h, and performing material sealing operation. When the discharge amount is stabilized at 100kg/h, the material sealing is completed, the ore feeding amount is reduced to 40kg/h, and the roasting operation is formally started.
(4) And the raw ore is conveyed into a first-stage cyclone separator 4 through a pipeline. The batch was then heated in one stage to 400 ℃. The fine ore subjected to the primary cyclone separation enters the flow seal valve 5. The internal materials form a suspended U-shaped material column under the action of air flow, and the material sealing effect is achieved. The smoke is sucked by the Roots blower 16, and the materials are accumulated in the ash hopper 13 and the bag-type dust collector 15.
(5) The materials enter from the main furnace 6, are driven by negative pressure to move upwards and enter the secondary cyclone separator 7. At this point the material is heated to about 500 ℃. The mineral powder is partially freed from adsorbed water, interlayer water and other volatile constituents. The product obtained at this time is a preheated calcine.
(6) The preheated roasting material enters a decarburization roasting reactor 8. The materials form a suspended U-shaped material column under the action of loosening wind and fluidizing wind. The roasting time of the material is about 1h, and the roasting temperature is set to be 650 ℃. In the process, reducing substances such as carbon, adsorption water, crystal water, pyrite and the like in the stone coal are almost completely removed. Discharging the decarbonized roasting material from a discharge hole of the reactor.
(7) The decarbonization roasting material enters a crystal breaking roasting reactor 9 with larger size. Similarly, the materials form a suspended U-shaped material column under the action of air flow. The retention time of the materials in the reactor is controlled to be 15h, and the roasting temperature is set to be 950 ℃. And finally, discharging the crystal breaking roasting material from a discharge hole of the reactor.
(8) The crystal breaking roasted material is cooled to be lower than 100 ℃ through an ore discharge heat exchange pipe 18 and then discharged, and the stone coal vanadium ore roasted product is used for subsequent sulfuric acid leaching. Under the same leaching conditions (the dosage of concentrated sulfuric acid is 10 wt%, the liquid-solid ratio is 1.25:1, the dosage of leaching aid (calcium fluoride) is 3%, the leaching temperature is 70 ℃, the leaching time is 8h, and the stirring speed is 800r/min), the leaching rate of the cascade oxidation roasting material is 88.51%, compared with the original ore, the leaching rate is improved by 35.51%, and compared with the original section of suspension roasting material, the leaching rate is improved by 10.21%.
Example 2:
example 2 the method is the same as example 1 except that:
(1) to a certain V2O5The high-carbon stone coal vanadium ore with the content of 0.95 percent and the carbon content of 12.6 percent is subjected to suspension roasting. The content of raw ore-0.045 mm accounts for 85 percent.
(2) The feeding amount of the weightlessness scale 2 is 20kg/h, the temperature of the first-stage decarburization roasting reactor 8 is 630 ℃, the time is 1.5h, the temperature of the second-stage decrystallization roasting reactor 9 is 940 ℃, and the time is 12 h.
(3) The leaching rate of vanadium of a roasted sample reaches 82.32 percent under the conditions that the dosage of concentrated sulfuric acid is 15wt percent, the liquid-solid ratio is 1:1, the dosage of an auxiliary leaching agent (calcium fluoride) is 2.5 percent, the leaching temperature is 75 ℃, the leaching time is 8 hours, and the stirring speed is 600r/min, and the leaching rate of vanadium is improved by 30.55 percent compared with that of the original ore and 14.25 percent compared with that of the original section of suspension roasting material.
Example 3:
example 3 differs from example 1 in that:
(1) to a certain V2O5The stone coal vanadium ore with the content of 1.50 percent and the carbon content of 8.5 percent is subjected to suspension roasting. The content of raw ore-0.045 mm accounts for 90 percent.
(2) The feeding amount of the weightlessness scale 2 is 35kg/h, the temperature of the first-stage decarburization roasting reactor 8 is 600 ℃, the time is 1.2h, the temperature of the second-stage decrystallization roasting reactor 9 is 950 ℃, and the time is 10 h.
(3) The leaching rate of vanadium of a roasted sample reaches 89.62 percent under the conditions that the dosage of concentrated sulfuric acid is 10 weight percent, the liquid-solid ratio is 1.25:1, the dosage of an auxiliary leaching agent (calcium fluoride) is 0.5 percent, the leaching temperature is 85 ℃, the leaching time is 6 hours, and the stirring speed is 1000r/min, the leaching rate of vanadium is improved by 28.54 percent compared with that of the original ore, and the leaching rate of the original section of suspended roasting material is improved by 18.15 percent compared with that of the original section of suspended roasting material.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. It will be readily apparent to those skilled in the art that various modifications to these embodiments and the generic principles defined herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments. Those skilled in the art should appreciate that many modifications and variations are possible in light of the above teaching without departing from the scope of the invention.

Claims (9)

1. The utility model provides a stone coal navajoite step oxidation roasting vanadium extraction system which characterized in that: the device comprises a feeding system, a material circulating heat storage system, a step oxidizing roasting system and a negative pressure dust removal system;
the feeding system comprises a storage bin (1) and a spiral feeding pipe (3) which is connected with the storage bin through a weightlessness scale (2);
the material circulating heat storage system comprises a primary cyclone separator (4), a flow sealing valve (5), a main furnace (6) and a secondary cyclone separator (7), wherein a feed inlet above the primary cyclone separator (4) is communicated to the bottom end of a spiral feeding pipe (3) through a pipeline, a discharge outlet at the bottom of the primary cyclone separator (4) is communicated with the flow sealing valve (5), the flow sealing valve (5) is communicated to the bottom end of the main furnace (6), a heat exchange air inlet pipe (10) and a combustion port of a combustor (11) are arranged on the side wall of a feed inlet at the bottom end of the main furnace (6), the top end of the main furnace (6) is communicated to a feed inlet above the secondary cyclone separator (7) through a pipeline, and a feed inlet above the secondary cyclone separator (7) is connected with a feed inlet above the primary cyclone separator (4) through a pipeline;
the step oxidizing roasting system comprises a decarburization roasting reactor (8), a crystal breaking roasting reactor (9) and an ore discharge heat exchange pipe (18) which are sequentially connected in series, wherein the decarburization roasting reactor (8) is connected to the bottom end of the secondary cyclone separator (7), and the ore discharge heat exchange pipe (18) is communicated with a heat exchange air inlet pipe (10);
the negative pressure dust removal system comprises a three-level cyclone separator (12), an ash bucket (13), a bag-type dust collector (15), a Roots fan (16) and a chimney (17), wherein the three-level cyclone separator (12) is communicated with a first-level cyclone separator (4) through an exhaust heat exchanger (14), the exhaust heat exchanger (14) is communicated with a heat exchange air inlet pipe (10), the ash bucket (13) is connected to the bottom end of the three-level cyclone separator (12), the bag-type dust collector (15) is communicated to a feed inlet above the three-level cyclone separator (12), and the bag-type dust collector (15), the Roots fan (16) and the chimney (17) are communicated in sequence.
2. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 1, characterized in that: the flow seal valve (5), the decarburization roasting reactor (8) and the crystal breaking roasting reactor (9) have the same structure and respectively comprise a reactor cavity and an electric heating furnace sleeve (23) wrapping the reactor cavity, a central clapboard (19), a loosening chamber (20), a fluidizing chamber (21) and an air distribution plate (22) are arranged in the reactor cavity, the reactor cavity is separated by a central clapboard (19) at the top, a gap is left between the bottom end of the central clapboard (19) and the reactor cavity, and an air distribution plate (22) is arranged, the air distribution plate (22) is parallel to the bottom of the reactor cavity, the fluidization chamber (21) is arranged on the left side of the central partition plate (19), the middle-upper part of the outer side of the fluidization chamber (21) is provided with a discharge hole, the loosening chamber (20) is arranged on the right side of the central partition plate (19), and the top center of the loosening chamber (20) is provided with a feed hole.
3. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 2, characterized in that: fluidized air and loose air are introduced into the flow seal valve (5), the decarburization roasting reactor (8) and the crystal breaking roasting reactor (9), and the volume flow of the fluidized air is 10-20m3The fluidized wind is a mixed gas of air and oxygen; the volume flow of the loosening wind is 3-8m3And h, loosening wind is air.
4. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 2, characterized in that: the temperature of the electric heating furnace sleeve (23) is 600-1050 ℃.
5. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 2, characterized in that: the roasting temperature in the decarburization roasting reactor (8) is 550-650 ℃, and the roasting time is 1-2 h; the roasting temperature in the crystal breaking roasting reactor (9) is 850-950 ℃, and the roasting time is 8-20 h.
6. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 1, characterized in that: the negative pressure of the Roots blower (16) is (-2.0) - (-2.5) kpa.
7. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 1, characterized in that: the heat exchange air inlet pipe (10) is a shell-and-tube heat exchange air inlet pipe; the ore discharging heat exchange pipe (18) is a dividing wall type ore discharging heat exchange pipe.
8. The stone coal navajoite gradient oxidizing roasting vanadium extraction system according to claim 1, characterized in that: v in stone coal vanadium powder ore in stone coal vanadium ore step oxidizing roasting vanadium extraction system2O5The content is 0.6-1.5%.
9. A method for carrying out stone coal navajoite oxidizing roasting by using the stone coal navajoite step oxidizing roasting vanadium extraction system of claim 1, which is characterized by comprising the following steps: which comprises the following steps:
(1) the materials enter a primary cyclone separator (4) of the material circulating heat storage system through a feeding system, the fine ores subjected to primary cyclone separation enter a flow sealing valve (5), then enter a feeding port at the lower part of a main furnace (6), are lifted in the main furnace (6), enter a secondary cyclone separator (7) through an upper pipeline and are discharged from a discharge port at the bottom of the secondary cyclone separator;
(2) the material discharged from the secondary cyclone separator (7) enters a decarburization roasting reactor (8), the decarburization roasting material is discharged from a discharge port of the reactor, then enters a crystal breaking roasting reactor (9), the crystal breaking roasting material is discharged from a discharge port of the reactor, and finally enters an ore discharge heat exchange pipe (18) to be cooled and then is discharged;
(3) the materials discharged from the first-stage cyclone separator (4) sequentially pass through an exhaust heat exchanger (14) and a third-stage cyclone separator (12) in a negative pressure dust removal system and are accumulated in an ash hopper (13) and a bag-type dust remover (15), and the gas is discharged through a Roots blower (16) and a chimney (17).
CN202111274119.4A 2021-10-29 2021-10-29 Stone coal navajoite gradient oxidizing roasting vanadium extraction system and oxidizing roasting method Pending CN114111359A (en)

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Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020112968A1 (en) * 2000-12-15 2002-08-22 Chiyoda Corporation Production of high purity vanadium compound from vanadium-containing carbonaceous residues
CN101551199A (en) * 2009-04-13 2009-10-07 杭州锅炉集团股份有限公司 Recovery method of steel slag residual heat and system thereof
CN101948954A (en) * 2010-09-25 2011-01-19 广西地博矿业集团股份有限公司 Gold recovery technology for processing arsenious S-C gangue coated gold concentrate by microwave fluidized roasting
CN107523685A (en) * 2017-07-19 2017-12-29 东北大学 A kind of suspension roasting utilization system and method containing Ferromanganese Ore
JP2018079456A (en) * 2016-11-18 2018-05-24 住友金属鉱山株式会社 Exhaust gas processing method in zinc oxide ore production plant
CN111304465A (en) * 2020-02-28 2020-06-19 东北大学 Method for extracting vanadium by decarburization-crystal breaking roasting enhanced acid leaching of vanadium-containing stone coal
CN111304464A (en) * 2020-02-28 2020-06-19 东北大学 Method for extracting vanadium by multistage roasting, acid mixing and curing of stone coal vanadium ore
CN111455165A (en) * 2020-05-29 2020-07-28 东北大学 Suspension magnetization roasting cyanogen breaking-low intensity magnetic separation iron extraction device for high-iron cyanidation tailings
CN111500852A (en) * 2020-05-29 2020-08-07 东北大学 Carbon-containing gold ore suspension roasting system
CN111621638A (en) * 2020-06-03 2020-09-04 东北大学 Suspension roasting system for strengthening reduction of iron-containing materials through heating and cracking
CN111719054A (en) * 2020-07-27 2020-09-29 东北大学 Oxidation, crystal breaking and roasting comprehensive utilization method of stone coal vanadium ore
CN111876589A (en) * 2020-08-04 2020-11-03 东北大学 Method and device for desulfurization and reduction of sulfur-containing iron ore
CN112941306A (en) * 2021-01-28 2021-06-11 东北大学 Selective roasting-magnetic separation device and method for micro-fine-particle ilmenite

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020112968A1 (en) * 2000-12-15 2002-08-22 Chiyoda Corporation Production of high purity vanadium compound from vanadium-containing carbonaceous residues
CN101551199A (en) * 2009-04-13 2009-10-07 杭州锅炉集团股份有限公司 Recovery method of steel slag residual heat and system thereof
CN101948954A (en) * 2010-09-25 2011-01-19 广西地博矿业集团股份有限公司 Gold recovery technology for processing arsenious S-C gangue coated gold concentrate by microwave fluidized roasting
JP2018079456A (en) * 2016-11-18 2018-05-24 住友金属鉱山株式会社 Exhaust gas processing method in zinc oxide ore production plant
CN107523685A (en) * 2017-07-19 2017-12-29 东北大学 A kind of suspension roasting utilization system and method containing Ferromanganese Ore
CN111304464A (en) * 2020-02-28 2020-06-19 东北大学 Method for extracting vanadium by multistage roasting, acid mixing and curing of stone coal vanadium ore
CN111304465A (en) * 2020-02-28 2020-06-19 东北大学 Method for extracting vanadium by decarburization-crystal breaking roasting enhanced acid leaching of vanadium-containing stone coal
CN111455165A (en) * 2020-05-29 2020-07-28 东北大学 Suspension magnetization roasting cyanogen breaking-low intensity magnetic separation iron extraction device for high-iron cyanidation tailings
CN111500852A (en) * 2020-05-29 2020-08-07 东北大学 Carbon-containing gold ore suspension roasting system
CN111621638A (en) * 2020-06-03 2020-09-04 东北大学 Suspension roasting system for strengthening reduction of iron-containing materials through heating and cracking
CN111719054A (en) * 2020-07-27 2020-09-29 东北大学 Oxidation, crystal breaking and roasting comprehensive utilization method of stone coal vanadium ore
CN111876589A (en) * 2020-08-04 2020-11-03 东北大学 Method and device for desulfurization and reduction of sulfur-containing iron ore
CN112941306A (en) * 2021-01-28 2021-06-11 东北大学 Selective roasting-magnetic separation device and method for micro-fine-particle ilmenite

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