CN104878193B - A kind of system and method for Low grade manganese ore fluidized reduction roasting - Google Patents
A kind of system and method for Low grade manganese ore fluidized reduction roasting Download PDFInfo
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- CN104878193B CN104878193B CN201510243104.XA CN201510243104A CN104878193B CN 104878193 B CN104878193 B CN 104878193B CN 201510243104 A CN201510243104 A CN 201510243104A CN 104878193 B CN104878193 B CN 104878193B
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Abstract
The invention discloses a kind of system of Low grade manganese ore fluidized reduction roasting, the system is main by feed bin, screw feeder, one cyclonic preheater, two grades of cyclone preheaters, venturi Powder Preheater, three-stage cyclone separator, inlet valve, cyclone separator material returning valve, bagroom material returning valve, fluidized-bed reactor, fluidized-bed reactor heat exchanger tube, outlet valve, venturi gas preheater, preheating gas cyclone separator, gas cyclone preheater, reduced ore cooler, primary cyclone, secondary cyclone, combustion chamber and bagroom are formed according to intended manner connection combination；Present invention also offers a kind of restoring method based on said system, it is adaptable to the low-grade manganese dioxide ore of full manganese grade 20 30%, and reduction temperature is 600 700 DEG C, and the reduction reaction time is 20 35 minutes.
Description
Technical field
The invention belongs to chemical industry, field of metallurgy, in particular it relates to a kind of low-grade manganese dioxide ore fluidized reduction
The system and method for roasting.
Background technology
Electrolytic manganese metal is to produce stainless steel and the important source material of other manganese alloys, is widely used in the neck such as chemical industry metallurgical
Domain.Traditional electrolyte manganese metal is produced using manganese carbonate ore as raw material, is electrolysed by direct sulfuric acid leaching, manganese sulfate solution purification
Liquid, electrolyte electrolysis obtain manganese metal.Due to manganese carbonate resource-constrained, the carbon that some enterprises of China production electrolytic manganese metal is used
Sour manganese ore, manganese grade is reduced to 10%~15% by 18%~20%, and some are less than 10% carbonic acid even with manganese grade
Manganese ore, causes acid consumption height, deficiency in economic performance.
Compared with manganese carbonate ore, the manganese grade height of dioxide ore for manganese, reserves are big, and manganese carbonate ore is substituted using dioxide ore for manganese
Production electrolytic manganese metal is following inevitable choice of China.However, under conventional leaching condition manganese dioxide hardly with sulfuric acid
React, it is necessary to the manganese dioxide in manganese oxide ore first is reduced into manganese monoxide to be leached by sulfuric acid, therefore, reduction
It is that dioxide ore for manganese is used for the most key step of electrolytic manganese metal production.
The method of dioxide ore for manganese reduction mainly includes reverberatory furnace reduction method, rotary kiln reducing process, Tecnored Process, Liang Kuang
Method, fluidized reduction method etc., wherein fluidized reduction method are recognized because having the advantages that reduction efficiency is high, be adapted to large-scale production
To be dioxide ore for manganese reduction calcination method the most efficient, by the extensive attention of domestic and international academic and industrial circle.The U.S. is special
Sharp US4044094 discloses a kind of technique of manganese oxide ore fluidized reduction, by fluidized drying, fluidizing calcination, fluidization
The parts such as reduction, fluidization cooling are constituted, and the manganese oxide ore raw material that particle diameter is less than 6 mesh (3.35mm) initially enters fluidized drying
Device, using the heat smoke formed after heavy oil combustion as fluidizing agent, while to dry the most of trip provided in heat, manganese ore
Discharged from after water vapor；Dried manganese ore enters fluidizing calcination device, and in 730 DEG C or so calcinings, calcination process is also using weight
The heat smoke that oil and air burning are formed is as thermal source and fluidizing agent, and the tail gas of fluidizing calcination device is through cyclone separator dedusting
After be discharged into exhaust gas purification system；Manganese ore after calcining enters fluidized reduction furnace, is reduced with synthesis gas at 730 DEG C or so,
The tail gas of fluidized reduction furnace is discharged into exhaust gas purification system after cyclone separator dedusting；It is cold that manganese ore after reduction enters fluidization
But device, using inert gas as fluidizing gas, inert gas is recycled, to cool down the manganese ore after water cooling reduction.The technique
Weak point includes：(1) reduction tail gas and calcining tail gas are directly discharged, and not only tail gas sensible heat is not utilized, in reduction tail gas
H2, the use of also not making a profit such as CO, cause energy waste.(2) MnO in ore deposit2Mn is easily decomposed into high-temperature burning process2O3, and MnO2
Decomposition reaction is endothermic process, need to consume substantial amounts of heat；But Mn simultaneously2O3Reduction is exothermic process, by heat absorption and exothermic process
Separately entering guild increases the heat consumption of system, increases processing cost.(3) manganese oxide ore particle diameter it is relatively thick (<3.35mm), inner transmission matter resistance
Larger, reaction efficiency is low, and reducing gas utilization rate can be caused low.
Chinese patent CN101591731 discloses a kind of reduction calcination method and device for high price manganese mineral, including
Following steps：(1) fuel gas and air burns in hot-blast stove by burner, control coefficient of excess air uses hot blast
The gas of stove is the reducing atmosphere and temperature that need, then passes to fluidized roaster；(2) manganese ore feed after fine grinding and hanged
Multiple sufficient heat exchange is carried out in floating preheating assembly and gas and mineral powder granular are separated, fluidized roaster is entered finally into and enters
Row reduction reaction；(3) the CO contents and solid-gas ratio in control fluidized roaster；Manganese mineral powder is reduced into fluidized roaster
Solid material discharging opening discharge through afterbody cyclone preheater after the molten manganese monoxide of theobromine.Described " fluosolids roasting
Stove " practical operation is not in feed status (operation lines speed is higher than the terminal velocity of particle, and powder is all blown reactor)
Proper fluosolids roasting, in addition, reduction reaction is carried out also in mulitistage cyclone, is carried out in cyclone preheater
Reduction be also not belonging to fluidized reduction, therefore, this method is not belonging to fluidized reduction substantially.Chinese patent CN101475219
A kind of fluidized reduction method of powdery manganese dioxide ore is disclosed, including：1) granularity is less than to 1.0mm powdery manganese dioxide
Ore is first preheated, then suspended state, temperature be 750-950 DEG C, reducing atmosphere, solid-gas ratio be 0.6-1.0kg/Nm3Condition
Lower reaction 5-10 seconds, obtains calcining matter；The reducing atmosphere is to contain CO in gas, CO volume content 4.5-6.5% in gas；2)
By calcining matter through low intensity magnetic separation, iron ore concentrate byproduct is isolated, manganese monoxide also original product is obtained.The restoring method with
CN101591731 is more similar.
Chinese invention patent application CN102363837 disclose a kind of powdery manganese oxide ore fluidization low-temperature reduction technique and
Its device, using coal gas as reducing agent, at 500~600 DEG C in fluid bed by the powdery manganese dioxide ore deposit of 60~400 mesh for reduction
For manganese monoxide, reduction tail gas produces heat smoke by combustion chambers burn, and heat smoke is through two stage cyclone preheater in preheating ore
While cooled exhaust gas, although make use of reduction tail gas in CO and H2, but the sensible heat of roasted ore is not utilized.
Existing dioxide ore for manganese fluidized reduction technique and technology all do not utilize the sensible heat of high temperature reduction ore deposit, and this portion
The economy of process can be improved by dividing the utilization of heat.In addition, existing fluidized reduction technique and technology all do not illustrate to be applicable
In the dioxide ore for manganese of what grade, generally imply suitable for manganese grade more than from 20% or so to 40% manganese oxide ore (such as
The dioxide ore for manganese of processing more than 20% to 40% is given in embodiment).However, because manganese dioxide is reduced to strongly exothermic mistake
Journey, significantly changing for manganese grade can not only cause the significantly change of system temperature, and required reducing gas amount is also with big
Amplitude variation, such as compared with reducing the manganese ore of manganese grade 20%, the process of the manganese ore of reduction manganese grade 40% not only liberated heat
Double, and required reducing gas amount is also doubled, it means that if not taking any heat exchange measure (existing
Dioxide ore for manganese fluidized reduction technology the hot equipment of shifting is set all not in fluid bed), the temperature meeting of fluidized-bed reactor
Rise by about one time, is such as elevated above 1000 DEG C from 500-600 DEG C, and the operation lines speed of fluidized-bed reactor will increase to four
Times, this is by the temperature that can bear far beyond a fluidized reduction device and fluidization gas excursion.It is therefore desirable to root
According to different manganese grade intervals, develop corresponding fluidized reduction technology, could preferably promote manganese dioxide fluidized reduction
The practicalization of system and technique.
In summary, this area is badly in need of a kind of can solve the problem that the upper of existing dioxide ore for manganese fluidized reduction technique and technology
State deficiency and can more make full use of the system and technique of roasting process energy.
The content of the invention
The present invention provides a kind of system and method for Low grade manganese ore fluidized reduction roasting, to solve existing skill
Defect in art, it is high with reaction efficiency and utilization rate of waste heat, the advantages of roasting process good economy performance, it is adapted to large-scale industry
Production.
The purpose of the present invention is achieved through the following technical solutions：
A kind of system of Low grade manganese ore fluidized reduction roasting, is mainly revolved by feed bin 1, screw feeder 2, one-level
Wind preheater 3, two grades of cyclone preheaters 4, venturi Powder Preheater 5, three-stage cyclone separator 6, inlet valve 7, cyclonic separations
Device material returning valve 8, bagroom material returning valve 9, fluidized-bed reactor 10, fluidized-bed reactor heat exchanger tube 10-1, outlet valve 11, text
Gas preheater 12, preheating gas cyclone separator 13, gas cyclone preheater 14, reduced ore cooler 15, one-level rotation in mound
Wind separator 16, secondary cyclone 17, combustion chamber 18 and bagroom 19 connect combination and formed as follows：
The discharging opening of the feed bin 1 is connected by pipeline with the charging aperture of screw feeder 2, the screw feeder 2
Discharging opening be connected by pipeline with the air inlet of one cyclonic preheater 3；
The gas outlet of the one cyclonic preheater 3 is connected by pipeline with the air inlet of bagroom 19, described
The discharging opening of one cyclonic preheater 3 is connected by pipeline with the air inlet of two grades of cyclone preheaters 4；
The air inlet of two grades of cyclone preheaters 4 is revolved by the gas outlet and one-level of pipeline and three-stage cyclone separator 6
The discharging opening of wind preheater 3 is connected, and the discharging opening of two grades of cyclone preheaters 4 passes through pipeline and venturi Powder Preheater
5 charging aperture is connected, and the gas outlet of two grades of cyclone preheaters 4 passes through pipeline and the discharging opening and one of screw feeder 2
The air inlet of level cyclone preheater 3 is connected；
The air inlet of the venturi Powder Preheater 5 is connected with the gas outlet of combustion chamber 18 by pipeline, described
The gas outlet of venturi Powder Preheater 5 is connected by pipeline with the air inlet of three-stage cyclone separator 6；
The discharging opening of the three-stage cyclone separator 6 is connected by pipeline with the charging aperture of inlet valve 7, the three-level rotation
The gas outlet of wind separator 6 passes through pipeline and the air inlet of two grades of cyclone preheaters 4 and the discharging opening phase of one cyclonic preheater 3
Connection；
The air inlet of the inlet valve 7 is connected by pipeline with gas main, and the discharging opening of the inlet valve 7 passes through pipe
Road is connected with the charging aperture of fluidized-bed reactor 10；
The air inlet of the cyclone separator material returning valve 8 is connected by pipeline with gas main, described cyclonic separation
The charging aperture of device material returning valve 8 passes through pipeline and the discharging opening and the discharging opening of secondary cyclone 17 of primary cyclone 16
It is connected, the discharging opening of the cyclone separator material returning valve 8 is connected by pipeline with the whirlwind feedback outlet of fluidized-bed reactor 10
Connect；
The air inlet of the bagroom material returning valve 9 is connected by pipeline with gas main, the bagroom
The charging aperture of material returning valve 9 is connected by pipeline with the discharging opening of bagroom 19, and the bagroom material returning valve 9 goes out
Material mouth is connected by pipeline with the feedback outlet of bagroom 19 of fluidized-bed reactor 10；
The discharging opening of the fluidized-bed reactor 10 is connected by pipeline with the charging aperture of outlet valve 11, the fluid bed
The air inlet of reactor 10 is connected with the gas outlet of preheating gas cyclone separator 13 by pipeline, the fluidized-bed reactor
10 gas outlet is connected by pipeline with the air inlet of primary cyclone 16, described fluidized-bed reactor heat exchanger tube
10-1 water inlet is connected by pipeline with technique supply mains, and the water vapour produced in fluidized-bed reactor heat exchanger tube 10-1 leads to
Cross fluidized-bed reactor heat exchanger tube 10-1 steam (vapor) outlet discharge；
The air inlet of the outlet valve 11 is connected by pipeline with gas main, and the discharging opening of the outlet valve 11 passes through
Pipeline is connected with the charging aperture of venturi gas preheater 12；
The air inlet of the venturi gas preheater 12 is connected with the gas outlet of gas cyclone preheater 14 by pipeline
Connect, the gas outlet of the venturi gas preheater 12 is connected by pipeline with the air inlet of preheating gas cyclone separator 13
Connect；
The air inlet phase that the discharging opening of the preheating gas cyclone separator 13 passes through pipeline and gas cyclone preheater 14
Connection；
The air inlet of the gas cyclone preheater 14 by pipeline simultaneously with gas main and preheating gas cyclonic separation
The discharging opening of device 13 is connected, and the discharging opening of the gas cyclone preheater 14 passes through the charging of pipeline and reduced ore cooler 15
Mouth is connected；
The water inlet of the reduced ore cooler 15 is connected with technique supply mains by pipeline, the reduced ore cooler
15 delivery port is connected by pipeline with technique water cooling system, and reduced ore is after the cooling of reduced ore cooler 15 from reduced ore
The discharging opening discharge of cooler 15.
The air inlet of the primary cyclone 16 is connected with the gas outlet of fluidized-bed reactor 10 by pipeline, institute
The gas outlet for stating primary cyclone 16 is connected by pipeline with the air inlet of secondary cyclone 17, the one-level rotation
The discharging opening of wind separator 16 is connected by pipeline with the charging aperture of cyclone separator material returning valve 8；
The gas outlet of the secondary cyclone 17 passes through pipeline by the primary air inlet of pipeline and the burner of combustion chamber 18
It is connected, the discharging opening of the secondary cyclone 17 is connected by pipeline with the charging aperture of cyclone separator material returning valve 8；
The combustion air inlet of the combustion chamber 18 is connected by pipeline with air header, the combustion chamber 18 it is combustion-supporting
Gas inlet is connected by pipeline with gas main, and the gas outlet of the combustion chamber 18 is preheated by pipeline and venturi powder
The air inlet of device 5 is connected；
The air inlet of the bagroom 19 is connected by pipeline with the gas outlet of one cyclonic preheater 3, is gathered dust
Tail gas afterwards is discharged by the gas outlet of bagroom 19.
The present invention's thes improvement is that：Coal gas passes through successively in gas cyclone preheater 14, venturi gas preheater
12 and preheating gas cyclone separator 13 in directly contacted with high temperature reduction ore deposit, reduced ore is cooled down while coal gas is preheated, return
Receive the sensible heat of high temperature reduction ore deposit.
The present invention another improvement be：The reduction tail gas that fluidized-bed reactor 10 is discharged first burns in combustion chamber 18 to be produced
Raw high-temperature flue gas, then by high-temperature flue gas in venturi Powder Preheater 5, three-stage cyclone separator 6, two grades of cyclone preheaters 4
With directly contacted with cold low-grade manganese dioxide ore powder in one cyclonic preheater 3, reclaim high temperature reduction tail gas sensible heat and latent
Low-grade manganese dioxide ore powder is heated while hot.
The present invention further improvement is that：Heat exchanger tube is provided with fluidized-bed reactor 10, by being produced in heat exchanger tube
The mode of producing water vapor reclaims the waste heat of reduction reaction generation, controls the temperature of fluidized-bed reactor 10.
Present invention also offers the restoring method for the system being calcined based on above-mentioned Low grade manganese ore fluidized reduction, institute
The method of stating refers to low-grade manganese dioxide ore powder and gas while entering into and through said system as follows, and step is：
1) powder low grade dioxide ore for manganese sequentially enters one cyclonic preheater 3, two by feed bin 1 through screw feeder 2
Level cyclone preheater 4, venturi Powder Preheater 5 and three-stage cyclone separator 6, then enter fluidized-bed reaction through inlet valve 7
Device 10；After the powder carried secretly in the discharge gas of one cyclonic preheater 3 is collected through bagroom 19, by bagroom feed back
Valve 9 enters fluidized-bed reactor 10；The powder carried secretly in the high-temperature tail gas that fluidized-bed reactor 10 is discharged is separated through one cyclonic
After device 16 and secondary cyclone 17 are collected, enter fluidized-bed reactor 10 through cyclone separator material returning valve 8；Oxygen after reduction
Change manganese mineral powder to discharge from the discharging opening of fluidized-bed reactor 10, enter venturi gas preheater 12, Ran Houjin through outlet valve 11
Enter preheating gas cyclone separator 13, then discharged through gas cyclone preheater 14, after finally being cooled down in reduced ore cooler 15
Discharge；
2) coal gas is preheated through gas cyclone preheater 14, venturi gas preheater 12, preheating gas cyclone separator 13
Afterwards, fluidized-bed reactor 10 is entered from the air inlet of fluidized-bed reactor 10, with low-grade dioxy in fluidized-bed reactor 10
Change manganese ore powder to occur after reduction reaction, discharged from the gas outlet of fluidized-bed reactor 10, through primary cyclone 16 and two
Enter combustion chamber 18 after level cyclone separator 17, occur combustion reaction with combustion air, combustion-supporting coal gas in combustion chamber 18, formed
High warm flue gas discharged from the gas outlet of combustion chamber 18, the air inlet through venturi Powder Preheater 5 enters venturi powder
Preheater 5, after being mixed in venturi Powder Preheater 5 with low-grade manganese dioxide ore powder, from venturi Powder Preheater 5
Gas outlet is discharged into three-stage cyclone separator 6, is preheated by entering two grades of whirlwind after the gas outlet discharge of three-stage cyclone separator 6
Device 4, then from the gas outlet discharge of two grades of cyclone preheaters 4, into one cyclonic preheater 3, then from one cyclonic preheater 3
Gas outlet be discharged into bagroom 19, discharged after the dedusting of bagroom 19 from the gas outlet of bagroom 19；
3) process water from fluidized-bed reactor heat exchanger tube 10-1 that technique supply mains comes water inlet enter fluidized-bed reaction
The heat exchanger tube of device 10, is vaporized in fluidized-bed reactor heat exchanger tube 10-1, and the water vapour of generation is exchanged heat by fluidized-bed reactor
Pipe 10-1 steam (vapor) outlet discharge；Water inlet of the process water through reduced ore cooler 15 that another road is come from technique supply mains enters
Reduced ore cooler 15, is discharged from the delivery port of reduced ore cooler 15.
The inventive method preferably one of be：The full manganese grade of described low-grade manganese dioxide ore is 20-30%.
The present invention another method be preferably：Described reduction reaction temperature is 600-700 DEG C, and the reduction reaction time is
20-35 minutes.
The present invention's another is preferably：Described coal gas is with CO and H2As active ingredient, calorific value requirement is more than
1250kcal/Nm3。
Brief description of the drawings
Fig. 1 is a kind of configuration schematic diagram of the system of Low grade manganese ore fluidized reduction roasting of the present invention.
Reference：1. feed bin；2. screw feeder；3. one cyclonic preheater；4. two grades of cyclone preheaters；5. literary mound
In Powder Preheater；6. three-stage cyclone separator；7. inlet valve；8. cyclone separator material returning valve；9. bagroom material returning valve；
10. fluidized-bed reactor；10-1. fluidized-bed reactor heat exchanger tubes；11. outlet valve；12. venturi gas preheater；13. preheating
Gas cyclone separator；14. gas cyclone preheater；15. reduced ore cooler；16. primary cyclone；17. two grades of rotations
Wind separator；18. combustion chamber；19. bagroom.
Embodiment
To make the object, technical solutions and advantages of the present invention clearer, below in conjunction with the accompanying drawing of the present invention, to this hair
Technical scheme in bright embodiment carries out clear, complete description.
Embodiment 1
Refer to Fig. 1, the system of Low grade manganese ore fluidized reduction disclosed in the present embodiment roasting, by feed bin 1,
Screw feeder 2, one cyclonic preheater 3, two grades of cyclone preheaters 4, venturi Powder Preheater 5, three-stage cyclone separators
6th, inlet valve 7, cyclone separator material returning valve 8, bagroom material returning valve 9, fluidized-bed reactor 10, fluidized-bed reactor heat exchange
Pipe 10-1, outlet valve 11, venturi gas preheater 12, preheating gas cyclone separator 13, gas cyclone preheater 14, reduction
Ore deposit cooler 15, primary cyclone 16, secondary cyclone 17, combustion chamber 18 and bagroom 19 are according to such as lower section
Formula connection combination is formed：
The discharging opening of the feed bin 1 is connected by pipeline with the charging aperture of screw feeder 2, the screw feeder 2
Discharging opening be connected by pipeline with the air inlet of one cyclonic preheater 3；
The gas outlet of the one cyclonic preheater 3 is connected by pipeline with the air inlet of bagroom 19, described
The discharging opening of one cyclonic preheater 3 is connected by pipeline with the air inlet of two grades of cyclone preheaters 4；
The air inlet of two grades of cyclone preheaters 4 is revolved by the gas outlet and one-level of pipeline and three-stage cyclone separator 6
The discharging opening of wind preheater 3 is connected, and the discharging opening of two grades of cyclone preheaters 4 passes through pipeline and venturi Powder Preheater
5 charging aperture is connected, and the gas outlet of two grades of cyclone preheaters 4 passes through pipeline and the discharging opening and one of screw feeder 2
The air inlet of level cyclone preheater 3 is connected；
The air inlet of the venturi Powder Preheater 5 is connected with the gas outlet of combustion chamber 18 by pipeline, described
The gas outlet of venturi Powder Preheater 5 is connected by pipeline with the air inlet of three-stage cyclone separator 6；
The discharging opening of the three-stage cyclone separator 6 is connected by pipeline with the charging aperture of inlet valve 7, the three-level rotation
The gas outlet of wind separator 6 passes through pipeline and the air inlet of two grades of cyclone preheaters 4 and the discharging opening phase of one cyclonic preheater 3
Connection；
The air inlet of the inlet valve 7 is connected by pipeline with gas main, and the discharging opening of the inlet valve 7 passes through pipe
Road is connected with the charging aperture of fluidized-bed reactor 10；
The air inlet of the cyclone separator material returning valve 8 is connected by pipeline with gas main, described cyclonic separation
The charging aperture of device material returning valve 8 passes through pipeline and the discharging opening and the discharging opening of secondary cyclone 17 of primary cyclone 16
It is connected, the discharging opening of the cyclone separator material returning valve 8 is connected by pipeline with the whirlwind feedback outlet of fluidized-bed reactor 10
Connect；
The air inlet of the bagroom material returning valve 9 is connected by pipeline with gas main, the bagroom
The charging aperture of material returning valve 9 is connected by pipeline with the discharging opening of bagroom 19, and the bagroom material returning valve 9 goes out
Material mouth is connected by pipeline with the bagroom feedback outlet of fluidized-bed reactor 10；
The discharging opening of the fluidized-bed reactor 10 is connected by pipeline with the charging aperture of outlet valve 11, the fluid bed
The air inlet of reactor 10 is connected with the gas outlet of preheating gas cyclone separator 13 by pipeline, the fluidized-bed reactor
10 gas outlet is connected by pipeline with the air inlet of primary cyclone 16, described fluidized-bed reactor heat exchanger tube
10-1 water inlet is connected by pipeline with technique supply mains, and the water vapour produced in fluidized-bed reactor heat exchanger tube 10-1 leads to
Cross fluidized-bed reactor heat exchanger tube 10-1 steam (vapor) outlet discharge；
The air inlet of the outlet valve 11 is connected by pipeline with gas main, and the discharging opening of the outlet valve 11 passes through
Pipeline is connected with the charging aperture of venturi gas preheater 12；
The air inlet of the venturi gas preheater 12 is connected with the gas outlet of gas cyclone preheater 14 by pipeline
Connect, the gas outlet of the venturi gas preheater 12 is connected by pipeline with the air inlet of preheating gas cyclone separator 13
Connect；
The air inlet phase that the discharging opening of the preheating gas cyclone separator 13 passes through pipeline and gas cyclone preheater 14
Connection；
The air inlet of the gas cyclone preheater 14 by pipeline simultaneously with gas main and preheating gas cyclonic separation
The discharging opening of device 13 is connected, and the discharging opening of the gas cyclone preheater 14 passes through the charging of pipeline and reduced ore cooler 15
Mouth is connected；
The water inlet of the reduced ore cooler 15 is connected with technique supply mains by pipeline, the reduced ore cooler
15 delivery port is connected by pipeline with technique water cooling system, and reduced ore is after the cooling of reduced ore cooler 15 from reduced ore
The discharging opening discharge of cooler 15.
The air inlet of the primary cyclone 16 is connected with the gas outlet of fluidized-bed reactor 10 by pipeline, institute
The gas outlet for stating primary cyclone 16 is connected by pipeline with the air inlet of secondary cyclone 17, the one-level rotation
The discharging opening of wind separator 16 is connected by pipeline with the charging aperture of cyclone separator material returning valve 8；
The gas outlet of the secondary cyclone 17 passes through pipeline by the primary air inlet of pipeline and the burner of combustion chamber 18
It is connected, the discharging opening of the secondary cyclone 17 is connected by pipeline with the charging aperture of cyclone separator material returning valve 8；
The combustion air inlet of the combustion chamber 18 is connected by pipeline with air header, the combustion chamber 18 it is combustion-supporting
Gas inlet is connected by pipeline with gas main, and the gas outlet of the combustion chamber 18 is preheated by pipeline and venturi powder
The air inlet of device 5 is connected；
The air inlet of the bagroom 19 is connected by pipeline with the gas outlet of one cyclonic preheater 3, is gathered dust
Tail gas afterwards is discharged by the gas outlet of bagroom 19.
Embodiment 2
Using the reducing process of the system of the Low grade manganese ore fluidized reduction roasting described in embodiment 1, including with
Lower step：Powder low grade dioxide ore for manganese sequentially enters one cyclonic preheater 3, two grades of rotations by feed bin 1 through screw feeder 2
Wind preheater 4, venturi Powder Preheater 5 and three-stage cyclone separator 6, then enter fluidized-bed reactor 10 through inlet valve 7；
After the powder carried secretly in the discharge gas of one cyclonic preheater 3 is collected through bagroom 19, entered by bagroom material returning valve 9
Fluidized bed reactor；The powder carried secretly in the high-temperature tail gas that fluidized-bed reactor 10 is discharged is through primary cyclone 16 and two
After level cyclone separator 17 is collected, enter fluidized-bed reactor 10 through cyclone separator material returning valve 8；Manganese oxide powder after reduction
Discharged from the discharging opening of fluidized-bed reactor 10, enter venturi gas preheater 12 through outlet valve 11, subsequently into preheated
Gas cyclone separator 13, then discharged through gas cyclone preheater 14, discharged after finally being cooled down in reduced ore cooler 15.Coal
It is anti-from fluid bed after gas is preheated through gas cyclone preheater 14, venturi gas preheater 12, preheating gas cyclone separator 13
Answer the air inlet of device 10 to enter fluidized-bed reactor 10, occur in fluidized-bed reactor 10 with low-grade manganese dioxide ore powder
After reduction reaction, discharged from the gas outlet of fluidized-bed reactor 10, through primary cyclone 16 and secondary cyclone 17
Enter combustion chamber 18 afterwards, occur combustion reaction with combustion air, combustion-supporting coal gas in combustion chamber 18, the high warm flue gas of formation from
The gas outlet discharge of combustion chamber 18, the air inlet through venturi Powder Preheater 5 enters venturi Powder Preheater 5, in Wen Qiu
In mixed with low-grade manganese dioxide ore powder in Powder Preheater 5 after, be discharged into from the gas outlet of venturi Powder Preheater 5
Three-stage cyclone separator 6, by entering two grades of cyclone preheaters 4 after the gas outlet discharge of three-stage cyclone separator 6, then revolves from two grades
The gas outlet discharge of wind preheater 4, into one cyclonic preheater 3, then from the gas outlet of one cyclonic preheater 3 discharge into
Enter bagroom 19, discharged after the dedusting of bagroom 19 from the gas outlet of bagroom 19.What technique supply mains came
Process water enters the heat exchanger tube 10-1 of fluidized-bed reactor from fluidized-bed reactor heat exchanger tube 10-1 water inlets, in fluidized-bed reaction
Vaporized in device heat exchanger tube 10-1, the water vapour of generation is discharged by fluidized-bed reactor heat exchanger tube 10-1 steam (vapor) outlet；It is another
Water inlet of the process water through reduced ore cooler 15 that road is come from technique supply mains enters reduced ore cooler 15, cold from reduced ore
But the delivery port discharge of device 15.
The dioxide ore for manganese of full manganese content 20-30% (weight/mass percentage composition) is handled using present invention process, by titanium dioxide
Manganese ore is milled to -100 mesh and accounts for 80%；To constitute (volumn concentration) for 26%CO, 6%CO2, 3%CH4, 17%H2And 48%N2
Producer gas as fluidisation and reducing medium, coal gas amount is needed for be theoretical and 1.25-1.35 times of commercial weight；Pass through controlling stream
In fluidized bed reactor heat exchanger tube 10-1 the yield of water vapour make the temperature control of fluidized-bed reactor 10 600-700 DEG C it
Between, when reduction temperature is 600 DEG C, the recovery time is 35 minutes, and when reduction temperature is 650 DEG C, the recovery time is 25 minutes, reduction
Temperature is 700 DEG C, and the recovery time is 20 minutes；Above-mentioned reducing condition can be by more than 96% in above-mentioned dioxide ore for manganese
MnO2It is reduced to MnO.
Finally it should be noted that：The above embodiments are merely illustrative of the technical solutions of the present invention, rather than its limitations；Although
The present invention is described in detail with reference to the foregoing embodiments, it will be understood by those within the art that, it still may be used
To be modified to the technical scheme described in foregoing embodiments, or to which part technical characteristic progress equivalent,
And these modification or replace, do not make appropriate technical solution essence depart from various embodiments of the present invention technical scheme spirit and
Scope.
Claims (7)
1. a kind of system of Low grade manganese ore fluidized reduction roasting, it is characterised in that the system is main by feed bin
(1), screw feeder (2), one cyclonic preheater (3), two grades of cyclone preheaters (4), venturi Powder Preheater (5), three
Level cyclone separator (6), inlet valve (7), cyclone separator material returning valve (8), bagroom material returning valve (9), fluidized-bed reaction
Device (10), fluidized-bed reactor heat exchanger tube (10-1), outlet valve (11), venturi gas preheater (12), preheating gas whirlwind
Separator (13), gas cyclone preheater (14), reduced ore cooler (15), primary cyclone (16), two grades of whirlwind point
Combination is connected as follows from device (17), combustion chamber (18) and bagroom (19) to be formed：
The discharging opening of the feed bin (1) is connected by pipeline with the charging aperture of screw feeder (2), the screw feeder
(2) discharging opening is connected by pipeline with the air inlet of one cyclonic preheater (3)；
The gas outlet of the one cyclonic preheater (3) is connected by pipeline with the air inlet of bagroom (19), described
The discharging opening of one cyclonic preheater (3) is connected by pipeline with the air inlet of two grades of cyclone preheaters (4)；
The air inlet of two grades of cyclone preheaters (4) is revolved by the gas outlet and one-level of pipeline and three-stage cyclone separator (6)
The discharging opening of wind preheater (3) is connected, and the discharging opening of two grades of cyclone preheaters (4) is pre- by pipeline and venturi powder
The charging aperture of hot device (5) is connected, and the gas outlet of two grades of cyclone preheaters (4) passes through pipeline and screw feeder (2)
Discharging opening is connected with the air inlet of one cyclonic preheater (3)；
The air inlet of the venturi Powder Preheater (5) is connected with the gas outlet of combustion chamber (18) by pipeline, the text
The gas outlet of Powder Preheater (5) is connected by pipeline with the air inlet of three-stage cyclone separator (6) in mound；
The discharging opening of the three-stage cyclone separator (6) is connected by pipeline with the charging aperture of inlet valve (7), the three-level rotation
The gas outlet of wind separator (6) passes through pipeline and two grades of air inlets of cyclone preheater (4) and going out for one cyclonic preheater (3)
Material mouth is connected；
The air inlet of the inlet valve (7) is connected by pipeline with gas main, and the discharging opening of the inlet valve (7) passes through pipe
Road is connected with the charging aperture of fluidized-bed reactor (10)；
The air inlet of the cyclone separator material returning valve (8) is connected by pipeline with gas main, and the cyclone separator is returned
Expect that the charging aperture of valve (8) passes through the discharging of pipeline and the discharging opening and secondary cyclone (17) of primary cyclone (16)
Mouth is connected, and the discharging opening of the cyclone separator material returning valve (8) passes through the whirlwind feed back of pipeline and fluidized-bed reactor (10)
Mouth is connected；
The air inlet of the bagroom material returning valve (9) is connected by pipeline with gas main, and the bagroom is returned
The charging aperture of material valve (9) is connected by pipeline with the discharging opening of bagroom (19), the bagroom material returning valve (9)
Discharging opening be connected by pipeline with bagroom (19) feedback outlet of fluidized-bed reactor (10)；
The discharging opening of the fluidized-bed reactor (10) is connected by pipeline with the charging aperture of outlet valve (11), the fluid bed
The air inlet of reactor (10) is connected with the gas outlet of preheating gas cyclone separator (13) by pipeline, and the fluid bed is anti-
The gas outlet of device (10) is answered to be connected by pipeline with the air inlet of primary cyclone (16), the fluidized-bed reactor is changed
The water inlet of heat pipe (10-1) is connected by pipeline with technique supply mains, is produced in fluidized-bed reactor heat exchanger tube (10-1)
Water vapour is discharged by the steam (vapor) outlet of fluidized-bed reactor heat exchanger tube (10-1)；
The air inlet of the outlet valve (11) is connected by pipeline with gas main, and the discharging opening of the outlet valve (11) passes through
Pipeline is connected with the charging aperture of venturi gas preheater (12)；
The air inlet of the venturi gas preheater (12) is connected with the gas outlet of gas cyclone preheater (14) by pipeline
Connect, the air inlet phase that the gas outlet of the venturi gas preheater (12) passes through pipeline and preheating gas cyclone separator (13)
Connection；
The air inlet phase that the discharging opening of the preheating gas cyclone separator (13) passes through pipeline and gas cyclone preheater (14)
Connection；
The air inlet of the gas cyclone preheater (14) by pipeline simultaneously with gas main and preheating gas cyclone separator
(13) discharging opening is connected, and the discharging opening of the gas cyclone preheater (14) passes through pipeline and reduced ore cooler (15)
Charging aperture is connected；
The water inlet of the reduced ore cooler (15) is connected with technique supply mains by pipeline, the reduced ore cooler
(15) delivery port is connected by pipeline with technique water cooling system, and reduced ore is after reduced ore cooler (15) cooling from also
The discharging opening discharge of raw ore cooler (15)；
The air inlet of the primary cyclone (16) is connected with the gas outlet of fluidized-bed reactor (10) by pipeline, institute
The gas outlet for stating primary cyclone (16) is connected by pipeline with the air inlet of secondary cyclone (17), and described one
The discharging opening of level cyclone separator (16) is connected by pipeline with the charging aperture of cyclone separator material returning valve (8)；
The gas outlet of the secondary cyclone (17) passes through pipeline by the primary air inlet of pipeline and combustion chamber (18) burner
It is connected, the charging aperture phase that the discharging opening of the secondary cyclone (17) passes through pipeline and cyclone separator material returning valve (8)
Connection；
The combustion air inlet of the combustion chamber (18) is connected by pipeline with air header, the combustion chamber (18) it is combustion-supporting
Gas inlet is connected by pipeline with gas main, and the gas outlet of the combustion chamber (18) is pre- by pipeline and venturi powder
The air inlet of hot device (5) is connected；
The air inlet of the bagroom (19) is connected by pipeline with the gas outlet of one cyclonic preheater (3), is gathered dust
Tail gas afterwards is discharged by the gas outlet of bagroom (19)；
The full manganese grade of described low-grade manganese dioxide ore is 20-30%.
2. the system of Low grade manganese ore fluidized reduction according to claim 1 roasting, it is characterised in that coal gas according to
It is secondary by gas cyclone preheater (14), venturi gas preheater (12) and preheating gas cyclone separator (13), with high temperature
Reduced ore is directly contacted, and reduced ore is cooled down while coal gas is preheated, and reclaims the sensible heat of high temperature reduction ore deposit.
3. the system of Low grade manganese ore fluidized reduction roasting according to claim 1, it is characterised in that fluid bed
First burning produces high-temperature flue gas to the reduction tail gas of reactor (10) discharge in combustion chamber (18), then by high-temperature flue gas in Wen Qiu
In in Powder Preheater (5), three-stage cyclone separator (6), two grades of cyclone preheaters (4) and one cyclonic preheater (3) with it is cold
Low-grade manganese dioxide ore powder directly contact, reclaim high temperature reduction tail gas sensible heat and latent heat.
4. the system of Low grade manganese ore fluidized reduction roasting according to claim 1, it is characterised in that in fluidisation
Heat exchanger tube is provided with bed reactor (10), many of reduction reaction generation are reclaimed by way of producing water vapour in heat exchanger tube
The temperature of waste heat amount, control fluidized-bed reactor (10).
5. a kind of method that system using described in claim 1 carries out Low grade manganese ore fluidized reduction roasting, described
Method comprises the following steps：
1) powder low grade dioxide ore for manganese by feed bin (1) through screw feeder (2) sequentially enter one cyclonic preheater (3),
Two grades of cyclone preheaters (4), venturi Powder Preheater (5) and three-stage cyclone separator (6), then enter through inlet valve (7)
Fluidized-bed reactor (10)；After the powder carried secretly in one cyclonic preheater (3) discharge gas is collected through bagroom (19),
Fluidized-bed reactor (10) is entered by bagroom material returning valve (9)；Pressed from both sides in the high-temperature tail gas of fluidized-bed reactor (10) discharge
After the powder of band is collected through primary cyclone (16) and secondary cyclone (17), through cyclone separator material returning valve (8)
Into fluidized-bed reactor (10)；Manganese oxide powder after reduction is discharged from the discharging opening of fluidized-bed reactor (10), through discharging
Valve (11) enters venturi gas preheater (12), subsequently into preheating gas cyclone separator (13), then pre- through gas cyclone
Hot device (14) discharge, is discharged after finally being cooled down in reduced ore cooler (15)；
2) coal gas is pre- through gas cyclone preheater (14), venturi gas preheater (12), preheating gas cyclone separator (13)
After heat, enter fluidized-bed reactor (10) from the air inlet of fluidized-bed reactor (10), in fluidized-bed reactor (10) with it is low
Grade dioxide ore for manganese powder occurs after reduction reaction, is discharged from the gas outlet of fluidized-bed reactor (10), through one cyclonic point
Enter combustion chamber (18) afterwards from device (16) and secondary cyclone (17), with combustion air, combustion-supporting coal in combustion chamber (18)
Combustion reaction occurs for gas, and the high warm flue gas of formation is discharged from the gas outlet of combustion chamber (18), through venturi Powder Preheater (5)
Air inlet enter venturi Powder Preheater (5), it is mixed with low-grade manganese dioxide ore powder in venturi Powder Preheater (5)
After conjunction, three-stage cyclone separator (6) is discharged into from the gas outlet of venturi Powder Preheater (5), by three-stage cyclone separator
(6) enter two grades of cyclone preheaters (4) after gas outlet discharge, then from the gas outlet discharge of two grades of cyclone preheaters (4), enter
One cyclonic preheater (3), is then discharged into bagroom (19), through cloth from the gas outlet of one cyclonic preheater (3)
Discharged after bag collector (19) dedusting from the gas outlet of bagroom (19)；
3) water inlet of process water from fluidized-bed reactor heat exchanger tube (10-1) that technique supply mains comes enters fluidized-bed reactor
(10) heat exchanger tube, is vaporized in fluidized-bed reactor heat exchanger tube (10-1), and the water vapour of generation is changed by fluidized-bed reactor
The steam (vapor) outlet discharge of heat pipe (10-1)；Water inlet of the process water through reduced ore cooler (15) that another road is come from technique supply mains
Mouth enters reduced ore cooler (15), is discharged from the delivery port of reduced ore cooler (15).
6. the method for Low grade manganese ore fluidized reduction roasting according to claim 5, it is characterised in that described
Reduction reaction temperature is 600-700 DEG C in fluidized-bed reactor, and the reduction reaction time is 20-35 minutes.
7. the method for Low grade manganese ore fluidized reduction roasting according to claim 5, it is characterised in that described
Coal gas is with CO and H2As active ingredient, calorific value requirement is more than 1250kcal/Nm3。
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| CN107099680B (en) * | 2017-06-23 | 2019-04-02 | 中国科学院过程工程研究所 | A kind of manganese oxide ore fluidized reduction process system |
| CN108807884B (en) * | 2018-05-31 | 2020-10-23 | 中国科学院过程工程研究所 | Device and method for carbon-coated modification of lithium ion battery negative electrode material |
| CN111500854B (en) * | 2020-05-29 | 2021-07-27 | 东北大学 | Suspension roasting system and method for industrial treatment of iron-manganese ore |
| CN114655988A (en) * | 2022-04-06 | 2022-06-24 | 广西锰华新能源科技发展有限公司 | Method for producing manganese-based material through carbon zero emission |
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