CN104911334B - A kind of system and method for high-grade dioxide ore for manganese fluidized reduction - Google Patents
A kind of system and method for high-grade dioxide ore for manganese fluidized reduction Download PDFInfo
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Abstract
The invention discloses a kind of system of high-grade dioxide ore for manganese fluidized reduction, mainly formed by feed bin, screw feeder, inlet 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, venturi Powder Preheater, primary cyclone, secondary cyclone, three-stage cyclone separator and waste heat boiler according to given combinations；Present invention also offers a kind of restoring method based on the system, it is adaptable to the high-grade dioxide ore for manganese of full manganese grade 35 45%, 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 high-grade dioxide ore for manganese fluidized reduction
System and method.
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, manganese grade height, the reserves of dioxide ore for manganese 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 not belonging to fluidized reduction, therefore, this method is not belonging to fluidized reduction substantially.Chinese patent CN101475219 is public
A kind of fluidized reduction method of powdery manganese dioxide ore has been opened, including：1) granularity is less than to 1.0mm powdery manganese dioxide ore deposit
Stone is first preheated, then suspended state, temperature be 750-950 DEG C, reducing atmosphere, solid-gas ratio be 0.6-1.0kg/Nm3Under the conditions of
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) will
Calcining matter isolates iron ore concentrate byproduct through low intensity magnetic separation, obtains manganese monoxide also original product.The restoring method and CN101591731
It 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 system and method that are not enough and can more making full use of roasting process energy.
The content of the invention
The present invention provides a kind of system and method for high-grade dioxide ore for manganese fluidized reduction, to solve prior art
In defect, it is high with reaction efficiency and utilization rate of waste heat, the advantages of roasting process good economy performance, be adapted to large-scale industry life
Production.
The purpose of the present invention is achieved through the following technical solutions：
A kind of system of high-grade dioxide ore for manganese fluidized reduction, mainly by feed bin 1, screw feeder 2, inlet valve 3,
Fluidized-bed reactor 4, fluidized-bed reactor heat exchanger tube 4-1, outlet valve 5, venturi gas preheater 6, preheating gas whirlwind point
From device 7, gas cyclone preheater 8, reduced ore cooler 9, venturi Powder Preheater 10, primary cyclone 11, two grades
Cyclone separator 12, three-stage cyclone separator 13, waste heat boiler 14 connects 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 charging aperture of venturi Powder Preheater 10；
The air inlet of the venturi Powder Preheater 10 is connected with the gas outlet of fluidized-bed reactor 4 by pipeline,
The gas outlet of described venturi Powder Preheater 10 is connected by pipeline with the air inlet of primary cyclone 11；
The gas outlet of described primary cyclone 11 and the air inlet of described secondary cyclone 12 pass through pipe
Road is connected, and the discharging opening of described primary cyclone 11 is connected by pipeline with the charging aperture of inlet valve 3；
The air inlet that the gas outlet of described secondary cyclone 12 passes through pipeline and described three-stage cyclone separator 13
Mouth is connected, and the discharging opening of described secondary cyclone 12 is connected by pipeline with the charging aperture of inlet valve 3；
The gas outlet of described three-stage cyclone separator 13 is entered by the reduction tail gas of pipeline and described waste heat boiler 14
Mouth is connected, and the discharging opening of described three-stage cyclone separator 13 is connected by pipeline with the charging aperture of inlet valve 3；
The gas outlet of described waste heat boiler 14 is connected with follow-up dust pelletizing system by pipeline, described waste heat boiler
14 combustion air inlet is connected by pipeline with air header, and the water inlet of described waste heat boiler 14 leads to technique supply mains
Piping is connected, and the water vapour that waste heat boiler 14 is produced is discharged by the steam (vapor) outlet of waste heat boiler 14；
The air inlet of described inlet valve 3 is connected by pipeline with gas main, and the discharging opening of described inlet valve 3 leads to
Piping is connected with the charging aperture of fluidized-bed reactor 4；
The discharging opening of described fluidized-bed reactor 4 is connected by pipeline with the charging aperture of outlet valve 5, described fluidisation
The air inlet of bed reactor 4 is connected with the gas outlet of preheating gas cyclone separator 7 by pipeline, described fluidized-bed reaction
Device heat exchanger tube 4-1 water inlet is connected by pipeline with technique supply mains, the water produced in fluidized-bed reactor heat exchanger tube 4-1
Steam is discharged by fluidized-bed reactor heat exchanger tube 4-1 steam (vapor) outlet；
The air inlet of described outlet valve 5 is connected by pipeline with gas main, and the discharging opening of described outlet valve 5 leads to
Piping is connected with the charging aperture of venturi gas preheater 6；
The air inlet of described venturi gas preheater 6 is connected with the gas outlet of gas cyclone preheater 8 by pipeline
Connect, the gas outlet of described venturi gas preheater 6 is connected by pipeline with the air inlet of preheating gas cyclone separator 7
Connect；
The air inlet phase that the discharging opening of described preheating gas cyclone separator 7 passes through pipeline and gas cyclone preheater 8
Connection；
The air inlet of described gas cyclone preheater 8 by pipeline simultaneously with gas main and preheating gas cyclonic separation
The discharging opening of device 7 is connected, and the discharging opening of described gas cyclone preheater 8 passes through the charging of pipeline and reduced ore cooler 9
Mouth is connected；
The water inlet of described reduced ore cooler 9 is connected with technique supply mains by pipeline, and described reduced ore is cold
But the delivery port of device 9 is connected by pipeline with technique water cooling system, and reduced ore is after the cooling of reduced ore cooler 9 from reduction
The discharging opening discharge of ore deposit cooler 9.
One of improvement of the present invention is：Coal gas passes through successively in gas cyclone preheater 8, venturi gas preheater 6
With directly contacted with high temperature reduction ore deposit in preheating gas cyclone separator 7, cool down reduced ore while coal gas is preheated, reclaim high
The sensible heat of warm reduced ore.
The another improvement of the present invention is：The high temperature reduction tail gas that fluidized-bed reactor 4 is discharged passes through in venturi powder
With cold high-grade two in preheater 10, primary cyclone 11, secondary cyclone 12 and three-stage cyclone separator 13
Manganese oxide powder is directly contacted, and high-grade manganese dioxide breeze is heated while reclaiming high temperature reduction tail gas sensible heat.
The still another refinement of the present invention is：Heat exchanger tube is provided with fluidized-bed reactor 4, by being produced in heat exchanger tube
The mode of water vapour reclaims the waste heat of reduction reaction generation, controls the temperature of fluidized-bed reactor 4.
The present invention further improvement is that：Fluidized-bed reactor 4 is reclaimed by way of waste heat boiler 14 produces water vapour
CO and H in discharge reduction tail gas2Latent heat.
It is described present invention also offers the restoring method of the system based on above-mentioned high-grade dioxide ore for manganese fluidized reduction
Method refers to high-grade manganese dioxide breeze and gas while entering into and through said system as follows, concretely comprises the following steps：
1) powdery high-grade dioxide ore for manganese enters venturi Powder Preheater 10 by feed bin 1 through screw feeder 2, through one
After level cyclone separator 11, secondary cyclone 12 and three-stage cyclone separator 13 are collected, enter fluidized bed through inlet valve 3 anti-
Answer device 4；After the discharging opening discharge of fluidized-bed reactor 4, enter venturi gas preheater 6, then preheated coal through outlet valve 5
Cyclonic wind separator 7, gas cyclone preheater 8 are discharged, and are discharged after finally being cooled down in reduced ore cooler 9；
2) after coal gas is preheated through gas cyclone preheater 8, venturi gas preheater 6, preheating gas cyclone separator 7,
Enter fluidized-bed reactor 4 from the air inlet of fluidized-bed reactor 4, with high-grade dioxide ore for manganese in fluidized-bed reactor 4
Reduction reaction occurs for powder, then is discharged from the gas outlet of fluidized-bed reactor 4, through venturi Powder Preheater 10, one cyclonic
After separator 11, secondary cyclone 12 and three-stage cyclone separator 13, into waste heat boiler 14, while coming from air header
Combustion air also enter waste heat boiler 14, occur with reduction tail gas after combustion reaction, discharged from the gas outlet of waste heat boiler 14,
Into follow-up dust pelletizing system；
3) process water come from technique supply mains is entered by the water inlet of waste heat boiler 14, in the heat exchanger tube of waste heat boiler 14
Middle vaporization, the water vapour of generation is discharged by the steam (vapor) outlet of waste heat boiler 14；The process water that technique supply mains comes is from fluid bed
Reactor heat exchanger tube 4-1 water inlet enters the heat exchanger tube of fluidized-bed reactor 4, the vapour in fluidized-bed reactor heat exchanger tube 4-1
Change, the water vapour of generation is discharged by fluidized-bed reactor heat exchanger tube 4-1 steam (vapor) outlet；The process water come from technique supply mains
Water inlet through reduced ore cooler 9 enters reduced ore cooler 9, is discharged from the delivery port of reduced ore cooler 9.
The inventive method preferably one of be：The full manganese grade of described high-grade dioxide ore for manganese is 35-45%.
The another of the inventive method is preferably：Described reduction reaction temperature is 600-700 DEG C, and the reduction reaction time is
20-35 minutes.
The another of the inventive method 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 the configuration schematic diagram of the system of the high-grade dioxide ore for manganese fluidized reduction of the present invention.
The feed bin of reference 1.；2. screw feeder；3. inlet valve；4. fluidized-bed reactor；4-1. fluidized-bed reactor
Heat exchanger tube；5. outlet valve；6. venturi gas preheater；7. preheating gas cyclone separator；8. gas cyclone preheater；9. also
Raw ore cooler；10. venturi Powder Preheater；11. primary cyclone；12. secondary cyclone；13. three-level is revolved
Wind separator；14. waste heat boiler.
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
Fig. 1 is referred to, the system of the high-grade dioxide ore for manganese fluidized reduction disclosed in the present embodiment, including：Feed bin
1st, screw feeder 2, inlet valve 3, fluidized-bed reactor 4, fluidized-bed reactor heat exchanger tube 4-1, outlet valve 5, venturi coal gas
Preheater 6, preheating gas cyclone separator 7, gas cyclone preheater 8, reduced ore cooler 9, venturi Powder Preheater 10,
Primary cyclone 11, secondary cyclone 12, three-stage cyclone separator 13 and waste heat boiler 14；
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 charging aperture of venturi Powder Preheater 10；
The air inlet of the venturi Powder Preheater 10 is connected with the gas outlet of fluidized-bed reactor 4 by pipeline,
The gas outlet of described venturi Powder Preheater 10 is connected by pipeline with the air inlet of primary cyclone 11；
The gas outlet of described primary cyclone 11 and the air inlet of described secondary cyclone 12 pass through pipe
Road is connected, and the discharging opening of described primary cyclone 11 is connected by pipeline with the charging aperture of inlet valve 3；
The air inlet that the gas outlet of described secondary cyclone 12 passes through pipeline and described three-stage cyclone separator 13
Mouth is connected, and the discharging opening of described secondary cyclone 12 is connected by pipeline with the charging aperture of inlet valve 3；
The gas outlet of described three-stage cyclone separator 13 is entered by the reduction tail gas of pipeline and described waste heat boiler 14
Mouth is connected, and the discharging opening of described three-stage cyclone separator 13 is connected by pipeline with the charging aperture of inlet valve 3；
The gas outlet of described waste heat boiler 14 is connected with follow-up dust pelletizing system by pipeline, described waste heat boiler
14 combustion air inlet is connected by pipeline with air header, and the water inlet of described waste heat boiler 14 leads to technique supply mains
Piping is connected, and the water vapour that waste heat boiler 14 is produced is discharged by the steam (vapor) outlet of waste heat boiler 14；
The air inlet of described inlet valve 3 is connected by pipeline with gas main, and the discharging opening of described inlet valve 3 leads to
Piping is connected with the charging aperture of fluidized-bed reactor 4；
The discharging opening of described fluidized-bed reactor 4 is connected by pipeline with the charging aperture of outlet valve 5, described fluidisation
The air inlet of bed reactor 4 is connected with the gas outlet of preheating gas cyclone separator 7 by pipeline, described fluidized-bed reaction
Device heat exchanger tube 4-1 water inlet is connected by pipeline with technique supply mains, the water produced in fluidized-bed reactor heat exchanger tube 4-1
Steam is discharged by fluidized-bed reactor heat exchanger tube 4-1 steam (vapor) outlet；
The air inlet of described outlet valve 5 is connected by pipeline with gas main, and the discharging opening of described outlet valve 5 leads to
Piping is connected with the charging aperture of venturi gas preheater 6；
The air inlet of described venturi gas preheater 6 is connected with the gas outlet of gas cyclone preheater 8 by pipeline
Connect, the gas outlet of described venturi gas preheater 6 is connected by pipeline with the air inlet of preheating gas cyclone separator 7
Connect；
The air inlet phase that the discharging opening of described preheating gas cyclone separator 7 passes through pipeline and gas cyclone preheater 8
Connection；
The air inlet of described gas cyclone preheater 8 by pipeline simultaneously with gas main and preheating gas cyclonic separation
The discharging opening of device 7 is connected, and the discharging opening of described gas cyclone preheater 8 passes through the charging of pipeline and reduced ore cooler 9
Mouth is connected；
The water inlet of described reduced ore cooler 9 is connected with technique supply mains by pipeline, and described reduced ore is cold
But the delivery port of device 9 is connected by pipeline with technique water cooling system, and reduced ore is after the cooling of reduced ore cooler 9 from reduction
The discharging opening discharge of ore deposit cooler 9.
Embodiment 2
Using the restoring method of the system of the high-grade dioxide ore for manganese fluidized reduction described in embodiment 1, including it is following
Step：Powdery high-grade dioxide ore for manganese enters venturi Powder Preheater 10 by feed bin 1 through screw feeder 2, is revolved through one-level
After wind separator 11, secondary cyclone 12 and three-stage cyclone separator 13 are collected, enter fluidized-bed reactor through inlet valve 3
4；After the discharging opening discharge of fluidized-bed reactor 4, enter venturi gas preheater 6, preheated gas cyclone through outlet valve 5
Separator 7, gas cyclone preheater 8 are discharged, and are discharged after being cooled down through reduced ore cooler 9.Coal gas through gas cyclone preheater 8,
After venturi gas preheater 6, preheating gas cyclone separator 7 are preheated, fluidized bed is entered from the air inlet of fluidized-bed reactor
Reactor 4, occurs reduction reaction in fluidized-bed reactor 4 with high-grade dioxide ore for manganese powder, then from fluidized-bed reactor 4
Gas outlet discharge, through venturi Powder Preheater 10, primary cyclone 11, secondary cyclone 12 and three-level whirlwind
After separator 13, into waste heat boiler 14, while the combustion air come from air header also enters waste heat boiler 14, with going back protocercal tail
Gas occurs after combustion reaction, is discharged from the gas outlet of waste heat boiler, into follow-up dust pelletizing system.The work come from technique supply mains
Skill water enters from the water inlet of waste heat boiler 14, is vaporized in the heat exchanger tube of waste heat boiler 14, and the water vapour of generation passes through used heat
The steam (vapor) outlet discharge of boiler 14；The process water that technique supply mains comes enters from fluidized-bed reactor heat exchanger tube 4-1 water inlet
The heat exchanger tube 4-1 of fluidized-bed reactor, is vaporized in fluidized-bed reactor heat exchanger tube 4-1, and the water vapour of generation passes through fluid bed
Reactor heat exchanger tube 4-1 steam (vapor) outlet discharge；Water inlet of the process water through reduced ore cooler 9 come from technique supply mains enters
Enter reduced ore cooler 9, discharged from the delivery port of reduced ore cooler 9.
The dioxide ore for manganese of full manganese content 35-45% (weight/mass percentage composition) is handled using the inventive method, 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
The yield of water vapour makes the temperature control of fluidized-bed reactor 4 between 600-700 DEG C in fluidized bed reactor heat exchanger tube 4-1,
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
Spend for 700 DEG C, the recovery time is 20 minutes；Above-mentioned reducing condition can be by above-mentioned dioxide ore for manganese more than 96% MnO2
It 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 equivalent substitution is carried out to which part technical characteristic,
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 (8)
1. a kind of system of high-grade dioxide ore for manganese fluidized reduction, it is characterised in that mainly by feed bin (1), screw feeding
Device (2), inlet valve (3), fluidized-bed reactor (4), fluidized-bed reactor heat exchanger tube (4-1), outlet valve (5), venturi coal gas
Preheater (6), preheating gas cyclone separator (7), gas cyclone preheater (8), reduced ore cooler (9), venturi powder
Preheater (10), primary cyclone (11), secondary cyclone (12), three-stage cyclone separator (13) and waste heat boiler
(14) connection combination is 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 is connected by pipeline with the charging aperture of venturi Powder Preheater (10)；
The air inlet of the venturi Powder Preheater (10) is connected with the gas outlet of fluidized-bed reactor (4) by pipeline,
The gas outlet of described venturi Powder Preheater (10) is connected by pipeline with the air inlet of primary cyclone (11)；
The gas outlet of described primary cyclone (11) and the air inlet of described secondary cyclone (12) pass through pipe
Road is connected, and the discharging opening of described primary cyclone (11) is connected by pipeline with the charging aperture of inlet valve (3)；
The air inlet that the gas outlet of described secondary cyclone (12) passes through pipeline and described three-stage cyclone separator (13)
Mouth is connected, and the discharging opening of described secondary cyclone (12) is connected by pipeline with the charging aperture of inlet valve (3)；
The gas outlet of described three-stage cyclone separator (13) is entered by the reduction tail gas of pipeline and described waste heat boiler (14)
Mouth is connected, and the discharging opening of described three-stage cyclone separator (13) is connected by pipeline with the charging aperture of inlet valve (3)；
The gas outlet of described waste heat boiler (14) is connected with follow-up dust pelletizing system by pipeline, described waste heat boiler
(14) combustion air inlet is connected by pipeline with air header, and the water inlet and process water of described waste heat boiler (14) are total
Pipe is connected by pipeline, and the water vapour that waste heat boiler (14) is produced is discharged by the steam (vapor) outlet of waste heat boiler (14)；
The air inlet of described inlet valve (3) is connected by pipeline with gas main, and the discharging opening of described inlet valve (3) leads to
Piping is connected with the charging aperture of fluidized-bed reactor (4)；
The discharging opening of described fluidized-bed reactor (4) is connected by pipeline with the charging aperture of outlet valve (5), described fluidisation
The air inlet of bed reactor (4) is connected with the gas outlet of preheating gas cyclone separator (7) by pipeline, described fluid bed
The water inlet of reactor heat exchanger tube (4-1) is connected by pipeline with technique supply mains, in fluidized-bed reactor heat exchanger tube (4-1)
The water vapour of generation is discharged by the steam (vapor) outlet of fluidized-bed reactor heat exchanger tube (4-1)；
The air inlet of described outlet valve (5) is connected by pipeline with gas main, and the discharging opening of described outlet valve (5) leads to
Piping is connected with the charging aperture of venturi gas preheater (6)；
The air inlet of described venturi gas preheater (6) is connected with the gas outlet of gas cyclone preheater (8) by pipeline
Connect, the air inlet phase that the gas outlet of described venturi gas preheater (6) passes through pipeline and preheating gas cyclone separator (7)
Connection；
The air inlet phase that the discharging opening of described preheating gas cyclone separator (7) passes through pipeline and gas cyclone preheater (8)
Connection；
The air inlet of described gas cyclone preheater (8) by pipeline simultaneously with gas main and preheating gas cyclone separator
(7) discharging opening is connected, and the discharging opening of described gas cyclone preheater (8) passes through pipeline and reduced ore cooler (9)
Charging aperture is connected；
The water inlet of described reduced ore cooler (9) is connected with technique supply mains by pipeline, described reduced ore cooling
The delivery port of device (9) is connected by pipeline with technique water cooling system, and reduced ore is after reduced ore cooler (9) cooling from also
The discharging opening discharge of raw ore cooler (9)；
The full manganese grade of described high-grade dioxide ore for manganese is 35-45%.
2. the system of high-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterised in that coal gas is successively
By gas cyclone preheater (8), venturi gas preheater (6) and preheating gas cyclone separator (7), with high temperature reduction ore deposit
Directly contact, reduced ore is cooled down while coal gas is preheated, reclaim the sensible heat of high temperature reduction ore deposit.
3. the system of high-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterised in that fluid bed is anti-
The high temperature reduction tail gas that device (4) is discharged is answered to pass through in venturi Powder Preheater (10), primary cyclone (11), two grades of rotations
Directly contacted with cold high-grade manganese dioxide breeze in wind separator (12) and three-stage cyclone separator (13), reclaim high temperature also
High-grade manganese dioxide breeze is heated while protocercal tail gas sensible heat.
4. the system of high-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterised in that in fluid bed
Heat exchanger tube is set in reactor (4), many waste heats that reduction reaction is produced are reclaimed by way of producing water vapour in heat exchanger tube
The temperature of amount, control fluidized-bed reactor (4).
5. the system of high-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterised in that pass through used heat
The mode that boiler (14) produces water vapour reclaims CO and H in fluidized-bed reactor (4) discharge reduction tail gas2Latent heat.
6. a kind of system using described in claim 1 carries out the method for high-grade dioxide ore for manganese fluidized reduction, its feature
It is, the described method comprises the following steps：
1) powdery high-grade dioxide ore for manganese enters venturi Powder Preheater (10), warp by feed bin (1) through screw feeder (2)
After primary cyclone (11), secondary cyclone (12) and three-stage cyclone separator (13) are collected, enter through inlet valve (3)
Fluidized bed reactor (4)；After the discharging opening discharge of fluidized-bed reactor (4), enter venturi coal gas through outlet valve (5) pre-
Hot device (6), then the discharge of preheated gas cyclone separator (7), gas cyclone preheater (8), finally in reduced ore cooler (9)
Discharged after middle cooling；
2) coal gas is preheated through gas cyclone preheater (8), venturi gas preheater (6), preheating gas cyclone separator (7)
Afterwards, fluidized-bed reactor (4) is entered from the air inlet of fluidized-bed reactor (4), with high-grade two in fluidized-bed reactor (4)
Reduction reaction occurs for manganese oxide ore powder, then is discharged from the gas outlet of fluidized-bed reactor (4), through venturi Powder Preheater
(10), after primary cyclone (11), secondary cyclone (12) and three-stage cyclone separator (13), into waste heat boiler
(14), while the combustion air come from air header also enters waste heat boiler (14), occur with reduction tail gas after combustion reaction, from
The gas outlet discharge of waste heat boiler (14), into follow-up dust pelletizing system；
3) process water come from technique supply mains is entered by the water inlet of waste heat boiler (14), the heat exchanger tube in waste heat boiler (14)
Middle vaporization, the water vapour of generation is discharged by the steam (vapor) outlet of waste heat boiler (14)；The process water that technique supply mains comes is from fluidisation
The water inlet of bed reactor heat exchanger tube (4-1) enters the heat exchanger tube of fluidized-bed reactor (4), in fluidized-bed reactor heat exchanger tube
Vaporized in (4-1), the water vapour of generation is discharged by the steam (vapor) outlet of fluidized-bed reactor heat exchanger tube (4-1)；It is total from process water
Water inlet of the process water through reduced ore cooler (9) that pipe comes enters reduced ore cooler (9), from reduced ore cooler (9)
Delivery port is discharged.
7. method according to claim 6, it is characterised in that the reduction reaction temperature in the fluidized-bed reactor is
600-700 DEG C, the reduction reaction time is 20-35 minutes.
8. method according to claim 6, it is characterised in that described coal gas is with CO and H2As active ingredient, calorific value will
Ask more than 1250kcal/Nm3。
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