CN102424365B - Recycling method of tail gas from pyrolusite reduction and sulfuric acid coproduction in fluidized bed furnace - Google Patents
Recycling method of tail gas from pyrolusite reduction and sulfuric acid coproduction in fluidized bed furnace Download PDFInfo
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- CN102424365B CN102424365B CN 201110211610 CN201110211610A CN102424365B CN 102424365 B CN102424365 B CN 102424365B CN 201110211610 CN201110211610 CN 201110211610 CN 201110211610 A CN201110211610 A CN 201110211610A CN 102424365 B CN102424365 B CN 102424365B
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Abstract
The invention provides a recycling method of tail gas from pyrolusite reduction in a fluidized bed furnace, belonging to the technical field of ore product processing. In order to improve the conversion of manganese peroxide to manganese monoxide in the fluidized bed furnace, the reduction reaction is necessarily carried out under a low-oxygen condition, and the mixed gas formed by air and tail gas of the fluidized bed furnace is blown from the lower segment of the fluidized bed furnace so as to guarantee that the oxygen content in the mixed gas is very low. The technique is simple and easy in operation, has high manganese peroxide conversion rate, recycles the tail gas, and reduces the environmental pollution.
Description
Technical field
The present invention relates to a kind of tail gas recycle method of fluidizing furnace reducing pyrolusite, reduce the pollution of tail gas greatly, belong to mineral products deep processing field environment.
Background technology
Manganous sulfate is a kind of important basic chemical industry raw material, is widely used in chemical field such as medicine, papermaking, catalyzer, fodder additives and produces field of metallurgy such as electrolytic manganese and produce other manganese salt etc.Along with manganese is that product is more and more wider in international and domestic purposes, its throughput enlarges rapidly, and with regard to China, the development of electrolytic manganese is very fast, and throughput has reached more than 2,300,000 tons/year.Many manganese products such as manganous sulfate, electrolytic manganese will use the material of bivalent manganese to be raw material, as manganous carbonate or manganese monoxide; Because occurring in nature manganese monoxide quantity seldom, the consumption of manganese carbonate ore increases considerably, and causes ore resource constantly poor, and price goes up year by year.Producing electrolytic manganese the eighties uses the manganese content requirement of manganese carbonate ore more than 24%, the content requirement of the nineties is more than 20%, required content more than 18% in 2000～2006 years, the content major part is below 16% at present, and raw materials for production are serious day by day with the production demand contradictory.The ore consumption is big, and corresponding subsidiary material and power consumption be also along with increase, thereby causes the cost straight line to rise, and brings great existence crisis to manufacturing enterprise.Therefore will look for new substitution of resources manganese carbonate ore extremely urgent, also be to keep a kind of effective way that electrolytic manganese enterprise produces existence.
The pyrolusite of occurring in nature tetravalence manganese (mainly being Manganse Dioxide) ore deposit amount is more, manganese content height, and price is low.But the Manganse Dioxide in the pyrolusite is insoluble to sulfuric acid, must be reduced into manganese monoxide (MnO) ability and sulfuric acid reaction generation manganous sulfate to it by reduction reaction, and manganese sulfate solution is the main raw material of manganese products such as preparation industrial manganic sulfate and electrolytic manganese.The method that existing pyrolusite reduction prepares manganous sulfate mainly contains two kinds:
1. coal reducing roasting-sulfuric acid leaching: this method is traditional production technique, and the history of existing nearly half a century, technology are ripe, and sulfuric acid leaches, the manganese sulfate solution quality of gained is good after the removal of impurities.But the SO that it produces
2, serious dust pollution of the environment, coal consumption amount is big, labour intensity is big, reduction cost height.
2. two ore deposit roasting methods: with pyrolusite and sulfurous iron ore separated pulverizing, mix 500 ℃～800 ℃ roasting temperatures 0.5～1 hour, then with the clear water leaching, separates, obtains manganese sulfate solution after the removal of impurities.This method equally also can produce SO
2And dust, contaminate environment, labour intensity is big.
Above-mentioned pyrolusite roasting reduction technology need disappear fine coal as reductive agent, production process energy consumption height, long flow path, and produce a large amount of CO
2, CO and SO
2Waste gas and dust, operational condition is poor, and environmental pollution is more serious.
Publication number is that the Chinese patent of CN101837959A has been introduced a kind of novel method of utilizing the sulphur reducing pyrolusite and co-producing sulfuric acid in fluidizing furnace in addition, burning sulphur is as thermal source and reductive agent, the Manganse Dioxide temperature that reduction needs is provided, has saved fuel greatly, can not discharge CO
2With CO waste gas, but tail gas also contains the sulfurous gas of quite a few, if tail gas is directly discharged, can influence local environment.
Summary of the invention
The objective of the invention is in, local environment influence is reduced to minimum, a kind of tail gas recycle method of fluidizing furnace reducing pyrolusite is provided the pyrolusite course of processing.Technology at former boiling furnace combustion sulphur roasting reduction pyrolusite and co-producing sulfuric acid is transformed, and has realized the waste gas zero release.Directly advance air mode with regard to guaranteeing the condition of hypoxemia if adopt for normal reduction reaction in the fluidizing furnace, can only regulate intake velocity and reach, will have influence on the interior sulphur of fluidizing furnace and pyrolusite boiling and burning, reduced manganese monoxide production output.
Technical scheme of the present invention is:
(1) with sulphur and pyrolusite in proportion blending send in the fluidizing furnace;
(2) blast mixed gas at the fluidizing furnace hypomere, make material under the strength effect of furnace bottom air-flow and furnace roof negative pressure, boiling in fluidizing furnace, burning, the control fluidized layer temperature is about 500～1000 ℃, and control fluidizing furnace hypomere oxygen content is about 10%;
(3) manganese monoxide of discharging from the fluidizing furnace discharge port secluding air cooling that falls into the water prevents that manganese monoxide is oxidized to Manganse Dioxide, also manganese monoxide directly can be entered pulp in the sulphuric acid soln (or electrolytic manganese anolyte), leach manganous sulfate;
(4) blast air at the fluidizing furnace epimere, delivery of supplemental oxygen, the sublimed sulphur that fully burns, reaction generates sulfurous gas; 600～900 ℃ of fluidizing furnace temperature outs, the concentration of fluidizing furnace outlet this moment sulfurous gas is 10～13%;
(5) its furnace gas send cleaning section after dedusting, and sulfurous gas forms sulphur trioxide through catalyst, generates sulfuric acid with the water reaction;
(6) at the mixed gas of fluidizing furnace hypomere access air and tail gas, regulated valve control enters oxygen content in the fluidizing furnace hypomere.
It is excessive to add sulphur, the then direct and Manganse Dioxide reaction of sulphur, and it is more to generate manganese sulfide, unfavorable to producing, and therefore needs to control the mixing proportion of sulphur and pyrolusite.
Therefore in one embodiment, wherein the mixing proportion scope of middle sulphur of step (1) and pyrolusite is 1: 0.5～20.
If the oxygen in the furnace gas is too many, then easily be oxidized to Manganse Dioxide under the manganese monoxide high temperature that reduction forms by excess of oxygen, unfavorable to reducing.
So in one embodiment, wherein the oxygen content in step (2) the control fluidizing furnace hypomere furnace gas is about 10%.
In another embodiment, wherein the operation control condition of fluidizing furnace is in the step (2): 500～1000 ℃ of fluidized layer temperatures, 600～900 ℃ of fluidizing furnace temperature outs, the concentration 8～14% of fluidizing furnace outlet sulfurous gas;
In another embodiment, wherein the manganese monoxide that the fluidizing furnace discharge port is discharged in the step (2) the secluding air cooling that falls into the water prevents that manganese monoxide is oxidized to Manganse Dioxide, also manganese monoxide directly can be entered pulp in the sulphuric acid soln (or electrolytic manganese anolyte), leach manganous sulfate.
In another embodiment, wherein tail gas and air mixed specific operation process in the step (6): 7. blast air at the fluidizing furnace epimere, delivery of supplemental oxygen, the sublimed sulphur that fully burns, reaction generation sulfurous gas; The high-temperature furnace gas that contains sulfurous gas is lowered the temperature through waste heat boiler or burner-gas cooler, send cleaning section after dedusting, and sulfurous gas forms sulphur trioxide through catalyst in the furnace gas, forms sulfuric acid with water.And 1. the residue furnace gas has formed tail gas and has been stored in two absorption towers, and 8. tail gas insert the fluidizing furnace hypomere through piping after opening butterfly valve and 4. 9. blast air mixed with the stokehold blower fan by pipeline
The amount that inserts tail gas shows by air flowmeter, in order to guarantee the fluidizing furnace hypomere
Oxygen content is about 10% in the gas, can not cross low can not be too high, by regulate butterfly valve 4., the control flashboard 2., 6. 5. the control flashboard control tail gas with stopping valve and enter speed in the fluidizing furnace.Fluidizing furnace epimere furnace gas 7. by pipe-line transportation behind the absorption tower, not absorbent furnace gas by pipe-line transportation 1. to two absorption towers, Fig. 1 is seen if too much can 3. discharge by valve in two absorption towers 1. inner exhaust gas.
Therefore in one embodiment, wherein tail gas air inlet ratio is foundation about 10% by oxygen content in the control fluidizing furnace hypomere furnace gas, and the ratio of general tail gas and air is 1: 1-1: 4, oxygen content is controlled at 9.5%-10.5%.
Technique effect
1, after production technique of the present invention is utilized air and tail gas is mixed, send in the fluidizing furnace, be easy to reach by control tail gas speed and regulate concentration of oxygen in the fluidizing furnace, guarantee normal boiling in the fluidizing furnace, improve reduction reaction efficient in the fluidizing furnace, reduced the production cost of manganous sulfate.
2, compare with disclosed technology, can not discharge CO
2, CO and SO
2Waste gas and dust, operational condition is good, does not pollute local environment.
Description of drawings
The present invention will further specify with following diagram, wherein:
Fig. 1 is the tail gas connection diagram of fluidizing furnace hypomere of the present invention, 1. is two absorption towers; 2. be the control flashboard; 3. be valve; 4. be the valve of talking endlessly; 5. be the control flashboard; 6. be stopping valve; 7. be fluidizing furnace; 8. for entering fluidizing furnace; 9. be the stokehold blower fan
Fig. 2 is a fluidizing furnace structural representation of the present invention.
Embodiment:
Following examples only in order to further specify the present invention, do not limit content of the present invention, and affiliated technical field can also take other concrete mode to implement.Therefore, embodiment can not be interpreted as the only embodiment of the present invention.
Embodiment 1
500kg sulphur and 250kg pyrolusite (1: 0.5 in proportion) blending are sent in the fluidizing furnace, blast air at the fluidizing furnace hypomere, make material under the strength effect of furnace bottom air-flow and furnace roof negative pressure, in fluidizing furnace, seethe with excitement, burning, the control fluidized layer temperature is about 850～950, control fluidizing furnace hypomere oxygen content is about 10%, the sulfur burning of blending in pyrolusite generates sulfurous gas, produce a large amount of heats, Manganse Dioxide in the pyrolusite is reduced to manganese monoxide, manganese monoxide is directly entered pulp in the sulphuric acid soln (or electrolytic manganese anolyte), leach manganous sulfate, adopt ordinary method to measure the content of manganous sulfate.Anoxic in the hypomere furnace gas contains sublimed sulphur, blasts air at the fluidizing furnace epimere, delivery of supplemental oxygen, and the sublimed sulphur that fully burns, reaction generates sulfurous gas; Fluidizing furnace temperature out 850～900, the concentration of fluidizing furnace outlet this moment sulfurous gas is 10～13%.Its furnace gas send cleaning section after dedusting, sulfurous gas forms sulphur trioxide through catalyst, generate sulfuric acid with the water reaction, the unabsorbed furnace gas of part is as tail gas, after air mixes, insert the fluidizing furnace hypomere again, by regulating the tail gas valve, to enter the boiling furnace gas in oxygen content be controlled at 10.5%, tail gas and AIR Proportional are 1: 2.5.The output 148kg of manganese monoxide, the manganese utilization ratio reaches 98.5%.
Comparative examples:
500kg sulphur and 250kg pyrolusite (1: 0.5 in proportion) blending are sent in the fluidizing furnace, blast air at the fluidizing furnace hypomere, make material under the strength effect of furnace bottom air-flow and furnace roof negative pressure, in fluidizing furnace, seethe with excitement, burning, the control fluidized layer temperature is about 850～950, control fluidizing furnace hypomere oxygen content is about 10%, the sulfur burning of blending in pyrolusite generates sulfurous gas, produce a large amount of heats, Manganse Dioxide in the pyrolusite is reduced to manganese monoxide, manganese monoxide is directly entered pulp in the sulphuric acid soln (or electrolytic manganese anolyte), leach manganous sulfate, adopt ordinary method to determine the content of manganous sulfate.Anoxic in the hypomere furnace gas contains sublimed sulphur, blasts air at the fluidizing furnace epimere, delivery of supplemental oxygen, and the sublimed sulphur that fully burns, reaction generates sulfurous gas; Fluidizing furnace temperature out 850～900, the concentration of fluidizing furnace outlet sulfurous gas is 10～13%.The furnace gas that contains sulfurous gas send cleaning section after dedusting, its furnace gas send cleaning section after dedusting, and sulfurous gas forms sulphur trioxide through catalyst, generates sulfuric acid with the water reaction, the output 105kg of manganese monoxide, and the manganese utilization ratio reaches 90.1%.
Embodiment 2: the something in common with embodiment 1 is no longer narrated, and difference is:
400kg sulphur and 800kg pyrolusite (1: 2 in proportion) blending are sent in the fluidizing furnace, 750～850 ℃ of control fluidized layer temperatures, fluidizing furnace temperature out 800～850, the concentration of fluidizing furnace outlet this moment sulfurous gas is 10～13%.Its furnace gas send cleaning section after dedusting, its furnace gas send cleaning section after dedusting, sulfurous gas forms sulphur trioxide through catalyst, generate sulfuric acid with the water reaction, the unabsorbed furnace gas of part is as tail gas, after air mixes, again insert the fluidizing furnace hypomere, by regulating the tail gas valve, oxygen content is controlled at 9.5%, tail gas and AIR Proportional are 1: 1.2.The output 458kg of manganese monoxide, the manganese utilization ratio reaches 98.6%.
Embodiment 3: the something in common with embodiment 1 is no longer narrated, and difference is:
400kg sulphur and 1600kg pyrolusite (1: 4 in proportion) blending are sent in the fluidizing furnace, control fluidized layer temperature 600～700, fluidizing furnace temperature out 700～800, the concentration of fluidizing furnace outlet this moment sulfurous gas is 10～13%.Its furnace gas send cleaning section after dedusting, its furnace gas send cleaning section after dedusting, sulfurous gas forms sulphur trioxide through catalyst, generate sulfuric acid with the water reaction, the unabsorbed furnace gas of part is as tail gas, after air mixes, again insert the fluidizing furnace hypomere, by regulating the tail gas valve, oxygen content is controlled at 9.8%, tail gas and AIR Proportional are 1: 1.4.The output 924kg of manganese monoxide, the manganese utilization ratio reaches 98.7%, the results are shown in Table 1.
Table 1
| Sulphur | Pyrolusite | Oxygen content | Manganese monoxide output | The manganese utilization ratio |
| 500kg | 250kg | 10.5％ | 148kg | 93％ |
| 400kg | 800kg | 9.5％ | 458kg | 98.6％ |
| 400kg | 1600kg | 9.8％ | 924kg | 98.7％ |
In conjunction with above example, the present invention compares with existing technology and has the following advantages:
1. adopt this method to carry out pyrolusite processing, required equipment is simple, and easy to operate, safety has significantly reduced environmental pollution.
2. adopt this method to carry out pyrolusite processing, improved manganous sulfate output and utilising efficiency, reduce production costs.
Claims (3)
1. the tail gas recycle method of a fluidizing furnace reducing pyrolusite, step comprises:
(1) with sulphur and pyrolusite in proportion blending send in the fluidizing furnace;
(2) blast the mixed gas of air and tail gas at the fluidizing furnace hypomere, make material under the strength effect of furnace bottom air-flow and furnace roof negative pressure, boiling in fluidizing furnace, burning, the control fluidized layer temperature is at 500～1000 ℃, and control fluidizing furnace hypomere oxygen content is 10%;
(3) manganese monoxide of discharging from the fluidizing furnace discharge port secluding air cooling that falls into the water prevents that manganese monoxide is oxidized to Manganse Dioxide, or manganese monoxide is directly entered pulp in the sulphuric acid soln, leaches manganous sulfate;
(4) blast air at the fluidizing furnace epimere, delivery of supplemental oxygen, the sublimed sulphur that fully burns, reaction generates sulfurous gas; 600～900 ℃ of fluidizing furnace temperature outs, the concentration of fluidizing furnace outlet this moment sulfurous gas is 10～13%;
(5) its furnace gas send cleaning section after dedusting, and sulfurous gas forms sulphur trioxide through catalyst, generates sulfuric acid with the water reaction;
(6) at the mixed gas of fluidizing furnace hypomere access air and tail gas, regulated valve control enters oxygen content in the fluidizing furnace hypomere.
2. according to the process of claim 1 wherein that the proportional range of sulphur and pyrolusite is 1: 0.5～20 in the step 1.
3. according to the method for claim 1 or 2, wherein the ratio of tail gas and air is 1: 1～1: 2.5 in the step 6, and oxygen content is 9.5%～10.5%.
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| CN 201110211610 CN102424365B (en) | 2011-07-27 | 2011-07-27 | Recycling method of tail gas from pyrolusite reduction and sulfuric acid coproduction in fluidized bed furnace |
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| CN105217580B (en) * | 2015-09-18 | 2018-04-10 | 石朝军 | A kind of method for preparing sulfuric acid with electrolytic manganese residues high temperature desulfurizing enriched flue gas |
| CN106745288A (en) * | 2016-12-14 | 2017-05-31 | 石朝军 | A kind of production method of high-purity manganese sulphate |
| CN106745290B (en) * | 2017-01-17 | 2018-02-02 | 石朝军 | A kind of technique for applying of manganese spar |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3348912A (en) * | 1963-09-23 | 1967-10-24 | Utah Construction & Mining Co | Method of preparing manganese sulfate from pyrite reduced manganese dioxide ores |
| CN101157481A (en) * | 2007-07-24 | 2008-04-09 | 汪云华 | Method for preparing manganese sulfate by manganese oxide ore |
| CN101220312A (en) * | 2008-01-29 | 2008-07-16 | 广西庆荣耐火材料有限公司 | Coal powder injection catalytic combustion burning-rate accelerator of blast furnace |
| CN101837959A (en) * | 2010-05-14 | 2010-09-22 | 湖南省泸溪县金旭冶化有限责任公司 | Method for reducing pyrolusite and co-producing sulfuric acid by utilizing sulfur in fluidized bed furnace |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3348912A (en) * | 1963-09-23 | 1967-10-24 | Utah Construction & Mining Co | Method of preparing manganese sulfate from pyrite reduced manganese dioxide ores |
| CN101157481A (en) * | 2007-07-24 | 2008-04-09 | 汪云华 | Method for preparing manganese sulfate by manganese oxide ore |
| CN101220312A (en) * | 2008-01-29 | 2008-07-16 | 广西庆荣耐火材料有限公司 | Coal powder injection catalytic combustion burning-rate accelerator of blast furnace |
| CN101837959A (en) * | 2010-05-14 | 2010-09-22 | 湖南省泸溪县金旭冶化有限责任公司 | Method for reducing pyrolusite and co-producing sulfuric acid by utilizing sulfur in fluidized bed furnace |
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