CN104911334A - High-grade manganese dioxide ore fluidized reduction system and method - Google Patents
High-grade manganese dioxide ore fluidized reduction system and method Download PDFInfo
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- CN104911334A CN104911334A CN201510243112.4A CN201510243112A CN104911334A CN 104911334 A CN104911334 A CN 104911334A CN 201510243112 A CN201510243112 A CN 201510243112A CN 104911334 A CN104911334 A CN 104911334A
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Abstract
The invention discloses a high-grade manganese dioxide ore fluidized reduction system. The system is mainly formed by a bunker, a spiral feeder, a feed valve, a fluidized bed reactor, a fluidized bed reactor heat exchange tube, a discharge valve, a venturi gas preheater, a preheating gas cyclone separator, a gas cyclone preheater, a reduction ore cooler, a venturi powder preheater, a primary cyclone separator, a secondary cyclone separator, a third cyclone separator and an exhaust-heat recovery boiler according to established combination. The invention also provides a reduction method based on the system. The method is suitable for high-grade manganese dioxide ore with 35%-45% of full manganese grade, the reduction temperature is 600-700 DEG C, and the reduction reaction time is 20-35min.
Description
Technical field
The invention belongs to chemical industry, field of metallurgy, particularly, the present invention relates to a kind of system and method for higher-grade dioxide ore for manganese fluidized reduction.
Background technology
Electrolytic metal Mn is the important source material of producing stainless steel and other manganese alloys, is widely used in the fields such as chemical industry metallurgical.It is raw material that traditional electrolyte manganese metal is produced with manganese carbonate ore, and by direct sulfuric acid leaching, manganese sulfate solution purification obtains electrolytic solution, electrolytic solution electrolysis obtains manganese metal.Due to manganous carbonate resource-constrained, some enterprises of China produce the manganese carbonate ore that electrolytic metal Mn uses, and manganese grade is reduced to 10% ~ 15% by 18% ~ 20%, and some even uses manganese grade lower than the manganese carbonate ore of 10%, causes high, the deficiency in economic performance of acid consumption.
Compared with manganese carbonate ore, the manganese of dioxide ore for manganese is of high grade, reserves large, adopts dioxide ore for manganese to substitute manganese carbonate ore and produces the inevitable choice that electrolytic metal Mn is China's future.But, under conventional leaching condition, Manganse Dioxide reacts with sulfuric acid hardly, need first the Manganse Dioxide in manganese oxide ore to be reduced to manganese monoxide to be leached by sulfuric acid, therefore, reduction is that dioxide ore for manganese produces a most key step for electrolytic metal Mn.
The method of dioxide ore for manganese reduction mainly comprises reverberatory furnace reduction method, rotary kiln reduction method, Tecnored Process, two-control region, fluidized reduction method etc., wherein fluidized reduction method is because having the advantages such as high, the applicable scale operation of reduction efficiency, be considered to dioxide ore for manganese reduction calcination method the most efficiently, be subject to the extensive attention of science and industrial community both at home and abroad.US Patent No. 4044094 discloses a kind of technique of manganese oxide ore fluidized reduction, be made up of parts such as fluidized drying, fluidizing calcination, fluidized reduction, fluidization coolings, the manganese oxide ore raw material that particle diameter is less than 6 orders (3.35mm) first enters fluidized drying device, the heat smoke formed after adopting heavy oil combustion is as fluidizing medium, simultaneously for drying provides heat, discharge after the most of free-water vaporization in manganese ore; Dried manganese ore enters fluidizing calcination device, and about 730 DEG C calcinings, the heat smoke that calcination process also adopts heavy oil and air combustion to be formed is as thermal source and fluidizing medium, and the tail gas of fluidizing calcination device enters exhaust gas purification system after cyclonic separator dedusting; Manganese ore after calcining enters fluidized reduction furnace, reduces at about 730 DEG C with synthetic gas, and the tail gas of fluidized reduction furnace enters exhaust gas purification system after cyclonic separator dedusting; Manganese ore after reduction enters fluidizing cooler, and be fluidizing agent with rare gas element, rare gas element recycles, with the manganese ore after water quench reduction.The weak point of this technique comprises: (1) reduction tail gas and calcining tail gas directly discharge, and not only tail gas sensible heat is not utilized, the H in reduction tail gas
2, the use of also not making a profit such as CO, cause energy dissipation.(2) MnO in ore deposit
2easily Mn is decomposed at high-temperature burning process
2o
3, and MnO
2decomposition reaction is endothermic process, need consume a large amount of heats; But Mn simultaneously
2o
3reduction is exothermic process, heat absorption and release process is separately carried out the hear rate that can increase system, increases processing cost.(3) manganese oxide ore particle diameter comparatively thick (<3.35mm), inner transmission matter resistance is comparatively large, and reaction efficiency is low, and reducing gas utilization ratio can be caused low.
Chinese patent CN101591731 discloses a kind of reduction calcination method for value Mn mineral and device, comprise the steps: that inflammable gas and air are burnt in hotblast stove by burner by (1), control coefficient of excess air, the gas of using hotblast stove is the reducing atmosphere and temperature that need, then passes into fluidized roaster; (2) feed after fine grinding being carried out to manganese ore in suspension preheating assembly and carry out repeatedly sufficient heat exchange and gas is separated with mineral powder granular, finally enter into fluidized roaster and carry out reduction reaction; (3) the CO content in fluidized roaster and solid-gas ratio is controlled; Manganese mineral powder be reduced in fluidized roaster can be acid-soluble manganese monoxide after discharge through the solid materials discharge port of last step cyclone preheater.In feed status, (pilot wire speed is higher than the terminal velocity of particle in described " fluidized roaster " actually operating, powder is all blown reactor), it is not proper fluosolids roasting, in addition, reduction reaction is also carried out in mulitistage cyclone, the reduction carried out in cyclone preheater does not belong to fluidized reduction, and therefore, the method does not belong to fluidized reduction substantially.Chinese patent CN101475219 discloses a kind of fluidized reduction method of powdery manganese dioxide ore, comprise: the first preheating of powdery manganese dioxide ore 1) granularity being less than 1.0mm, then suspended state, temperature be 750-950 DEG C, reducing atmosphere, solid-gas ratio be 0.6-1.0kg/Nm
3react 5-10 second under condition, obtain calcining matter; Described reducing atmosphere is containing CO, the volume content 4.5-6.5% of CO in gas in gas; 2) by calcining matter through low intensity magnetic separation, separating ferrum concentrate byproduct, obtains manganese monoxide also original product.This method of reducing and CN101591731 are comparatively similar.
Chinese invention patent application CN102363837 discloses a kind of powdery manganese oxide ore fluidization low-temperature reduction technique and device thereof, take coal gas as reductive agent, at 500 ~ 600 DEG C in fluidized-bed by 60 ~ 400 object powdery manganese dioxide ore deposits for being reduced to manganese monoxide, reduction tail gas produces heat smoke by combustion chambers burn, heat smoke through two stage cyclone preheater cooled exhaust gas while preheating ore, although make use of reduction tail gas in CO and H
2, 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 in high temperature reduction ore deposit, and the utilization of this part heat can improve the economy of process.In addition, existing fluidized reduction technique and technology all do not illustrate the dioxide ore for manganese being applicable to what grade, usually imply the manganese oxide ore (as given the dioxide ore for manganese of process more than 20% to 40% in an embodiment) being applicable to manganese grade more than from about 20% to 40%.But, because Manganse Dioxide is reduced to strong exothermic process, manganese grade significantly change the significantly change that not only can cause system temperature, and the required reducing gas scale of construction also significantly changes thereupon, such as compared with the manganese ore of reduction manganese grade 20%, the process of reduction manganese grade 40% manganese ore not only liberated heat doubles, and the required reducing gas scale of construction also doubles, this means if do not take any heat exchange measure (existing dioxide ore for manganese fluidized reduction technology does not all have to arrange in fluidized-bed to move hot equipment), the temperature of fluidized-bed reactor can raise nearly one times, as risen to higher than 1000 DEG C from 500-600 DEG C, and the pilot wire 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 variation range.So, need, according to different manganese grade intervals, to develop corresponding fluidized reduction technology, the practicalization of Manganse Dioxide fluidized reduction system and technique could be advanced better.
In sum, this area be badly in need of a kind of can solve existing dioxide ore for manganese fluidized reduction technique and technology above-mentioned deficiency and more can make full use of the system and method for roasting process energy.
Summary of the invention
The invention provides a kind of system and method for higher-grade dioxide ore for manganese fluidized reduction, in order to solve defect of the prior art, the advantage such as have reaction efficiency and utilization rate of waste heat is high, roasting process good economy performance, is applicable to large-scale commercial production.
Object of the present invention is achieved through the following technical solutions:
A system for higher-grade dioxide ore for manganese fluidized reduction, primarily of feed bin 1, screw feeder 2, feed valve 3, fluidized-bed reactor 4, fluidized-bed reactor heat transfer tube 4-1, bleeder valve 5, Venturi gas preheater 6, preheating gas cyclonic separator 7, gas cyclone preheater 8, reduced ore water cooler 9, Venturi Powder Preheater 10, primary cyclone 11, secondary cyclone 12, three-stage cyclone separator 13, waste heat boiler 14 connects in the following manner and is combined to form:
The discharge port of described feed bin 1 is connected by the opening for feed of pipeline with screw feeder 2, and the discharge port of described screw feeder 2 is connected by the opening for feed of pipeline with Venturi Powder Preheater 10;
The inlet mouth of described Venturi Powder Preheater 10 is connected by pipeline with the air outlet of fluidized-bed reactor 4, and the air outlet of described Venturi Powder Preheater 10 is connected by the inlet mouth of pipeline with primary cyclone 11;
The air outlet of described primary cyclone 11 is connected by pipeline with the inlet mouth of described secondary cyclone 12, and the discharge port of described primary cyclone 11 is connected by the opening for feed of pipeline with feed valve 3;
The air outlet of described secondary cyclone 12 is connected by the inlet mouth of pipeline with described three-stage cyclone separator 13, and the discharge port of described secondary cyclone 12 is connected by the opening for feed of pipeline with feed valve 3;
The air outlet of described three-stage cyclone separator 13 is connected by the reduction inlet exhaust gas of pipeline with described waste heat boiler 14, and the discharge port of described three-stage cyclone separator 13 is connected by the opening for feed of pipeline with feed valve 3;
The air outlet of described waste heat boiler 14 is connected by pipeline with follow-up dust-removal system, the combustion air inlet of described waste heat boiler 14 is connected with air main by pipeline, the water-in of described waste heat boiler 14 is connected by pipeline with process water house steward, and the water vapor that waste heat boiler 14 produces is discharged by the vapour outlet of waste heat boiler 14;
The inlet mouth of described feed valve 3 is connected with gas main by pipeline, and the discharge port of described feed valve 3 is connected by the opening for feed of pipeline with fluidized-bed reactor 4;
The discharge port of described fluidized-bed reactor 4 is connected by the opening for feed of pipeline with bleeder valve 5, the inlet mouth of described fluidized-bed reactor 4 is connected by pipeline with the air outlet of preheating gas cyclonic separator 7, the water-in of described fluidized-bed reactor heat transfer tube 4-1 is connected with process water house steward by pipeline, and the water vapor produced in fluidized-bed reactor heat transfer tube 4-1 is discharged by the vapour outlet of fluidized-bed reactor heat transfer tube 4-1;
The inlet mouth of described bleeder valve 5 is connected with gas main by pipeline, and the discharge port of described bleeder valve 5 is connected by the opening for feed of pipeline with Venturi gas preheater 6;
The inlet mouth of described Venturi gas preheater 6 is connected by pipeline with the air outlet of gas cyclone preheater 8, and the air outlet of described Venturi gas preheater 6 is connected by the inlet mouth of pipeline with preheating gas cyclonic separator 7;
The discharge port of described preheating gas cyclonic separator 7 is connected by the inlet mouth of pipeline with gas cyclone preheater 8;
The inlet mouth of described gas cyclone preheater 8 is connected with the discharge port of gas main with preheating gas cyclonic separator 7 by pipeline simultaneously, and the discharge port of described gas cyclone preheater 8 is connected by the opening for feed of pipeline with reduced ore water cooler 9;
The water-in of described reduced ore water cooler 9 is connected by pipeline with process water house steward, the water outlet of described reduced ore water cooler 9 is connected with process water cooling system by pipeline, and reduced ore is discharged from the discharge port of reduced ore water cooler 9 after reduced ore water cooler 9 cools.
One of improvement of the present invention is: coal gas by directly contacting with high temperature reduction ore deposit successively in gas cyclone preheater 8, Venturi gas preheater 6 and preheating gas cyclonic separator 7, cool reduced ore while coal gas is preheated, reclaim the sensible heat in high temperature reduction ore deposit.
Another improvement of the present invention is: the high temperature reduction tail gas that fluidized-bed reactor 4 is discharged, by directly contacting with cold higher-grade Manganse Dioxide breeze in Venturi Powder Preheater 10, primary cyclone 11, secondary cyclone 12 and three-stage cyclone separator 13, heats higher-grade Manganse Dioxide breeze while reclaiming high temperature reduction tail gas sensible heat.
An improvement more of the present invention is: in fluidized-bed reactor 4, be provided with heat transfer tube, reclaim the waste heat of reduction reaction generation, the temperature of control flow check fluidized bed reactor 4 by the mode producing water vapor in heat transfer tube.
Another improvement of the present invention is: the mode being produced water vapor by waste heat boiler 14 reclaims CO and H in fluidized-bed reactor 4 discharge reduction tail gas
2latent heat.
Present invention also offers the method for reducing of the system based on above-mentioned higher-grade dioxide ore for manganese fluidized reduction, described method refers to that the gentle body of higher-grade Manganse Dioxide breeze enters simultaneously as follows and by said system, concrete steps are:
1) powdery higher-grade dioxide ore for manganese enters Venturi Powder Preheater 10 by feed bin 1 through screw feeder 2, after primary cyclone 11, secondary cyclone 12 and three-stage cyclone separator 13 are collected, enters fluidized-bed reactor 4 through feed valve 3; After discharging from the discharge port of fluidized-bed reactor 4, enter Venturi gas preheater 6 through bleeder valve 5, then discharge through preheating gas cyclonic separator 7, gas cyclone preheater 8, finally discharge after cooling in reduced ore water cooler 9;
2) coal gas is through gas cyclone preheater 8, Venturi gas preheater 6, after preheating gas cyclonic separator 7 preheating, fluidized-bed reactor 4 is entered from the inlet mouth of fluidized-bed reactor 4, with higher-grade dioxide ore for manganese powder generation reduction reaction in fluidized-bed reactor 4, discharge from the air outlet of fluidized-bed reactor 4 again, through Venturi Powder Preheater 10, primary cyclone 11, after secondary cyclone 12 and three-stage cyclone separator 13, enter waste heat boiler 14, the combustion air simultaneously come from air main also enters waste heat boiler 14, after reduction tail gas generation combustion reactions, discharge from the air outlet of waste heat boiler 14, enter follow-up dust-removal system,
3) process water come from process water house steward is entered by the water-in of waste heat boiler 14, and vaporize in the heat transfer tube of waste heat boiler 14, the water vapor of generation is discharged by the vapour outlet of waste heat boiler 14; The process water that process water house steward comes enters the heat transfer tube of fluidized-bed reactor 4 from the water-in of fluidized-bed reactor heat transfer tube 4-1, vaporize in fluidized-bed reactor heat transfer tube 4-1, the water vapor of generation is discharged by the vapour outlet of fluidized-bed reactor heat transfer tube 4-1; The process water come from process water house steward enters reduced ore water cooler 9 through the water-in of reduced ore water cooler 9, discharges from the water outlet of reduced ore water cooler 9.
The one of preferred of the inventive method is: the full manganese grade of described higher-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 minute.
Another of the inventive method is preferably: described coal gas is with CO and H
2as effective constituent, calorific value requires to be greater than 1250kcal/Nm
3.
Accompanying drawing explanation
Fig. 1 is the configuration schematic diagram of the system of higher-grade dioxide ore for manganese fluidized reduction of the present invention.
Reference numeral 1. feed bin; 2. screw feeder; 3. feed valve; 4. fluidized-bed reactor; 4-1. fluidized-bed reactor heat transfer tube; 5. bleeder valve; 6. Venturi gas preheater; 7. preheating gas cyclonic separator; 8. gas cyclone preheater; 9. reduced ore water cooler; 10. Venturi Powder Preheater; 11. primary cyclones; 12. secondary cyclones; 13. three-stage cyclone separators; 14. waste heat boilers.
Embodiment
For making the object, technical solutions and advantages of the present invention clearly, below in conjunction with accompanying drawing of the present invention, clear, complete description is carried out to the technical scheme in the embodiment of the present invention.
Embodiment 1
Refer to Fig. 1, the system of the higher-grade dioxide ore for manganese fluidized reduction disclosed in the present embodiment, comprising: feed bin 1, screw feeder 2, feed valve 3, fluidized-bed reactor 4, fluidized-bed reactor heat transfer tube 4-1, bleeder valve 5, Venturi gas preheater 6, preheating gas cyclonic separator 7, gas cyclone preheater 8, reduced ore water cooler 9, Venturi Powder Preheater 10, primary cyclone 11, secondary cyclone 12, three-stage cyclone separator 13 and waste heat boiler 14;
The discharge port of described feed bin 1 is connected by the opening for feed of pipeline with screw feeder 2, and the discharge port of described screw feeder 2 is connected by the opening for feed of pipeline with Venturi Powder Preheater 10;
The inlet mouth of described Venturi Powder Preheater 10 is connected by pipeline with the air outlet of fluidized-bed reactor 4, and the air outlet of described Venturi Powder Preheater 10 is connected by the inlet mouth of pipeline with primary cyclone 11;
The air outlet of described primary cyclone 11 is connected by pipeline with the inlet mouth of described secondary cyclone 12, and the discharge port of described primary cyclone 11 is connected by the opening for feed of pipeline with feed valve 3;
The air outlet of described secondary cyclone 12 is connected by the inlet mouth of pipeline with described three-stage cyclone separator 13, and the discharge port of described secondary cyclone 12 is connected by the opening for feed of pipeline with feed valve 3;
The air outlet of described three-stage cyclone separator 13 is connected by the reduction inlet exhaust gas of pipeline with described waste heat boiler 14, and the discharge port of described three-stage cyclone separator 13 is connected by the opening for feed of pipeline with feed valve 3;
The air outlet of described waste heat boiler 14 is connected by pipeline with follow-up dust-removal system, the combustion air inlet of described waste heat boiler 14 is connected with air main by pipeline, the water-in of described waste heat boiler 14 is connected by pipeline with process water house steward, and the water vapor that waste heat boiler 14 produces is discharged by the vapour outlet of waste heat boiler 14;
The inlet mouth of described feed valve 3 is connected with gas main by pipeline, and the discharge port of described feed valve 3 is connected by the opening for feed of pipeline with fluidized-bed reactor 4;
The discharge port of described fluidized-bed reactor 4 is connected by the opening for feed of pipeline with bleeder valve 5, the inlet mouth of described fluidized-bed reactor 4 is connected by pipeline with the air outlet of preheating gas cyclonic separator 7, the water-in of described fluidized-bed reactor heat transfer tube 4-1 is connected with process water house steward by pipeline, and the water vapor produced in fluidized-bed reactor heat transfer tube 4-1 is discharged by the vapour outlet of fluidized-bed reactor heat transfer tube 4-1;
The inlet mouth of described bleeder valve 5 is connected with gas main by pipeline, and the discharge port of described bleeder valve 5 is connected by the opening for feed of pipeline with Venturi gas preheater 6;
The inlet mouth of described Venturi gas preheater 6 is connected by pipeline with the air outlet of gas cyclone preheater 8, and the air outlet of described Venturi gas preheater 6 is connected by the inlet mouth of pipeline with preheating gas cyclonic separator 7;
The discharge port of described preheating gas cyclonic separator 7 is connected by the inlet mouth of pipeline with gas cyclone preheater 8;
The inlet mouth of described gas cyclone preheater 8 is connected with the discharge port of gas main with preheating gas cyclonic separator 7 by pipeline simultaneously, and the discharge port of described gas cyclone preheater 8 is connected by the opening for feed of pipeline with reduced ore water cooler 9;
The water-in of described reduced ore water cooler 9 is connected by pipeline with process water house steward, the water outlet of described reduced ore water cooler 9 is connected with process water cooling system by pipeline, and reduced ore is discharged from the discharge port of reduced ore water cooler 9 after reduced ore water cooler 9 cools.
Embodiment 2
Adopt the method for reducing of the system of the higher-grade dioxide ore for manganese fluidized reduction described in embodiment 1, comprise the following steps: powdery higher-grade dioxide ore for manganese enters Venturi Powder Preheater 10 by feed bin 1 through screw feeder 2, after primary cyclone 11, secondary cyclone 12 and three-stage cyclone separator 13 are collected, enter fluidized-bed reactor 4 through feed valve 3; After discharging from the discharge port of fluidized-bed reactor 4, enter Venturi gas preheater 6 through bleeder valve 5, discharge through preheating gas cyclonic separator 7, gas cyclone preheater 8, discharge after reduced ore water cooler 9 cools.Coal gas is through gas cyclone preheater 8, Venturi gas preheater 6, after preheating gas cyclonic separator 7 preheating, fluidized-bed reactor 4 is entered from the inlet mouth of fluidized-bed reactor, with higher-grade dioxide ore for manganese powder generation reduction reaction in fluidized-bed reactor 4, discharge from the air outlet of fluidized-bed reactor 4 again, through Venturi Powder Preheater 10, primary cyclone 11, after secondary cyclone 12 and three-stage cyclone separator 13, enter waste heat boiler 14, the combustion air simultaneously come from air main also enters waste heat boiler 14, after reduction tail gas generation combustion reactions, discharge from the air outlet of waste heat boiler, enter follow-up dust-removal system.The process water come from process water house steward enters from the water-in of waste heat boiler 14, and vaporize in the heat transfer tube of waste heat boiler 14, the water vapor of generation is discharged by the vapour outlet of waste heat boiler 14; The process water that process water house steward comes enters the heat transfer tube 4-1 of fluidized-bed reactor from the water-in of fluidized-bed reactor heat transfer tube 4-1, vaporize in fluidized-bed reactor heat transfer tube 4-1, the water vapor of generation is discharged by the vapour outlet of fluidized-bed reactor heat transfer tube 4-1; The process water come from process water house steward enters reduced ore water cooler 9 through the water-in of reduced ore water cooler 9, discharges from the water outlet of reduced ore water cooler 9.
Adopt the dioxide ore for manganese of the full Fe content 35-45% (mass percentage) of the inventive method process, dioxide ore for manganese is milled to-100 orders and accounts for 80%; To form (volumn concentration) for 26%CO, 6%CO
2, 3%CH
4, 17%H
2and 48%N
2producer gas as fluidisation and reducing medium, coal gas amount be the 1.25-1.35 of theoretical required also commercial weight doubly; The temperature of fluidized-bed reactor 4 is made to control between 600-700 DEG C by the generation of water vapor in control flow check fluidized bed reactor heat transfer tube 4-1, when reduction temperature is 600 DEG C, recovery time is 35 minutes, when reduction temperature is 650 DEG C, recovery time is 25 minutes, reduction temperature is 700 DEG C, and the recovery time is 20 minutes; Above-mentioned reductive condition can by above-mentioned dioxide ore for manganese more than 96% MnO
2be reduced to MnO.
Last it is noted that above embodiment is only in order to illustrate technical scheme of the present invention, be not intended to limit; Although with reference to previous embodiment to invention has been detailed description, those of ordinary skill in the art is to be understood that, it still can be modified to the technical scheme described in foregoing embodiments, or equivalent replacement is carried out to wherein portion of techniques feature, and these amendments or replacement, do not make the essence of appropriate technical solution depart from the spirit and scope of various embodiments of the present invention technical scheme.
Claims (9)
1. the system of a higher-grade dioxide ore for manganese fluidized reduction, it is characterized in that, primarily of feed bin (1), screw feeder (2), feed valve (3), fluidized-bed reactor (4), fluidized-bed reactor heat transfer tube (4-1), bleeder valve (5), Venturi gas preheater (6), preheating gas cyclonic separator (7), gas cyclone preheater (8), reduced ore water cooler (9), Venturi Powder Preheater (10), primary cyclone (11), secondary cyclone (12), three-stage cyclone separator (13) is connected in the following manner with waste heat boiler (14) and is combined to form:
The discharge port of described feed bin (1) is connected by the opening for feed of pipeline with screw feeder (2), and the discharge port of described screw feeder (2) is connected by the opening for feed of pipeline with Venturi Powder Preheater (10);
The inlet mouth of described Venturi Powder Preheater (10) is connected by pipeline with the air outlet of fluidized-bed reactor (4), and the air outlet of described Venturi Powder Preheater (10) is connected by the inlet mouth of pipeline with primary cyclone (11);
The air outlet of described primary cyclone (11) is connected by pipeline with the inlet mouth of described secondary cyclone (12), and the discharge port of described primary cyclone (11) is connected by the opening for feed of pipeline with feed valve (3);
The air outlet of described secondary cyclone (12) is connected by the inlet mouth of pipeline with described three-stage cyclone separator (13), and the discharge port of described secondary cyclone (12) is connected by the opening for feed of pipeline with feed valve (3);
The air outlet of described three-stage cyclone separator (13) is connected by the reduction inlet exhaust gas of pipeline with described waste heat boiler (14), and the discharge port of described three-stage cyclone separator (13) is connected by the opening for feed of pipeline with feed valve (3);
The air outlet of described waste heat boiler (14) is connected by pipeline with follow-up dust-removal system, the combustion air inlet of described waste heat boiler (14) is connected with air main by pipeline, the water-in of described waste heat boiler (14) is connected by pipeline with process water house steward, and the water vapor that waste heat boiler (14) produces is discharged by the vapour outlet of waste heat boiler (14);
The inlet mouth of described feed valve (3) is connected with gas main by pipeline, and the discharge port of described feed valve (3) is connected by the opening for feed of pipeline with fluidized-bed reactor (4);
The discharge port of described fluidized-bed reactor (4) is connected by the opening for feed of pipeline with bleeder valve (5), the inlet mouth of described fluidized-bed reactor (4) is connected by pipeline with the air outlet of preheating gas cyclonic separator (7), the water-in of described fluidized-bed reactor heat transfer tube (4-1) is connected with process water house steward by pipeline, and the water vapor produced in fluidized-bed reactor heat transfer tube (4-1) is discharged by the vapour outlet of fluidized-bed reactor heat transfer tube (4-1);
The inlet mouth of described bleeder valve (5) is connected with gas main by pipeline, and the discharge port of described bleeder valve (5) is connected by the opening for feed of pipeline with Venturi gas preheater (6);
The inlet mouth of described Venturi gas preheater (6) is connected by pipeline with the air outlet of gas cyclone preheater (8), and the air outlet of described Venturi gas preheater (6) is connected by the inlet mouth of pipeline with preheating gas cyclonic separator (7);
The discharge port of described preheating gas cyclonic separator (7) is connected by the inlet mouth of pipeline with gas cyclone preheater (8);
The inlet mouth of described gas cyclone preheater (8) is connected with the discharge port of gas main with preheating gas cyclonic separator (7) by pipeline simultaneously, and the discharge port of described gas cyclone preheater (8) is connected by the opening for feed of pipeline with reduced ore water cooler (9);
The water-in of described reduced ore water cooler (9) is connected by pipeline with process water house steward, the water outlet of described reduced ore water cooler (9) is connected with process water cooling system by pipeline, and reduced ore is discharged from the discharge port of reduced ore water cooler (9) after reduced ore water cooler (9) cooling.
2. the system of higher-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterized in that, coal gas is successively by gas cyclone preheater (8), Venturi gas preheater (6) and preheating gas cyclonic separator (7), directly contact with high temperature reduction ore deposit, cool reduced ore while coal gas is preheated, reclaim the sensible heat in high temperature reduction ore deposit.
3. the system of higher-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterized in that, the high temperature reduction tail gas that fluidized-bed reactor (4) is discharged, by directly contacting with cold higher-grade Manganse Dioxide breeze in Venturi Powder Preheater (10), primary cyclone (11), secondary cyclone (12) and three-stage cyclone separator (13), heats higher-grade Manganse Dioxide breeze while reclaiming high temperature reduction tail gas sensible heat.
4. the system of higher-grade dioxide ore for manganese fluidized reduction according to claim 1, it is characterized in that, heat transfer tube is set in fluidized-bed reactor (4), reclaims the waste heat of reduction reaction generation, the temperature of control flow check fluidized bed reactor (4) by the mode producing water vapor in heat transfer tube.
5. the system of higher-grade dioxide ore for manganese fluidized reduction according to claim 1, is characterized in that, the mode being produced water vapor by waste heat boiler (14) reclaims CO and H in fluidized-bed reactor (4) discharge reduction tail gas
2latent heat.
6. utilize the system described in claim 1 to carry out a method for higher-grade dioxide ore for manganese fluidized reduction, it is characterized in that, said method comprising the steps of:
1) powdery higher-grade dioxide ore for manganese enters Venturi Powder Preheater (10) by feed bin (1) through screw feeder (2), after primary cyclone (11), secondary cyclone (12) and three-stage cyclone separator (13) are collected, enter fluidized-bed reactor (4) through feed valve (3); After discharging from the discharge port of fluidized-bed reactor (4), Venturi gas preheater (6) is entered through bleeder valve (5), discharge through preheating gas cyclonic separator (7), gas cyclone preheater (8) again, finally discharge after cooling in reduced ore water cooler (9);
2) coal gas is through gas cyclone preheater (8), Venturi gas preheater (6), after preheating gas cyclonic separator (7) preheating, fluidized-bed reactor (4) is entered from the inlet mouth of fluidized-bed reactor (4), with higher-grade dioxide ore for manganese powder generation reduction reaction in fluidized-bed reactor (4), discharge from the air outlet of fluidized-bed reactor (4) again, through Venturi Powder Preheater (10), primary cyclone (11), after secondary cyclone (12) and three-stage cyclone separator (13), enter waste heat boiler (14), the combustion air simultaneously come from air main also enters waste heat boiler (14), after reduction tail gas generation combustion reactions, discharge from the air outlet of waste heat boiler (14), enter follow-up dust-removal system,
3) process water come from process water house steward is entered by the water-in of waste heat boiler (14), and vaporize in the heat transfer tube of waste heat boiler (14), the water vapor of generation is discharged by the vapour outlet of waste heat boiler (14); The process water that process water house steward comes enters the heat transfer tube of fluidized-bed reactor (4) from the water-in of fluidized-bed reactor heat transfer tube (4-1), vaporization in fluidized-bed reactor heat transfer tube (4-1), the water vapor of generation is discharged by the vapour outlet of fluidized-bed reactor heat transfer tube (4-1); The process water come from process water house steward enters reduced ore water cooler (9) through the water-in of reduced ore water cooler (9), discharges from the water outlet of reduced ore water cooler (9).
7. method according to claim 6, is characterized in that, the full manganese grade of described higher-grade dioxide ore for manganese is 35-45%.
8. method according to claim 6, is characterized in that, the reduction reaction temperature in described fluidized-bed reactor is 600-700 DEG C, and the reduction reaction time is 20-35 minute.
9. method according to claim 6, is characterized in that, described coal gas is with CO and H
2as effective constituent, calorific value requires to be greater than 1250kcal/Nm
3.
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