CN104596294A - Platinum and palladium concentrate roasting device - Google Patents
Platinum and palladium concentrate roasting device Download PDFInfo
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- CN104596294A CN104596294A CN201510081526.1A CN201510081526A CN104596294A CN 104596294 A CN104596294 A CN 104596294A CN 201510081526 A CN201510081526 A CN 201510081526A CN 104596294 A CN104596294 A CN 104596294A
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- roasting
- steam
- roaster
- platinum
- molybdenum
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
The invention relates to a platinum and palladium concentrate roasting device which comprises a feed screw (1), an adding guide tube (2), a roasting furnace (3), a spiral driving device (4), inner screws (5), a heating jacket (6), a steam inlet (7), a steam outlet (8), a steam-water separator (9), a draft fan (10) and a pipeline (11). By adoption of the platinum and palladium concentrate roasting device, hardening in the roasting process is avoided, produced roasted sand is uniform in granularity, the pollution of generated volatile acid gases to the environment is eliminated, and the platinum and palladium concentrate roasting device is reasonable in structural arrangement, small in occupied space, simple to manufacture, convenient to repair, simple to operate and small in operator number.
Description
Technical field
The invention belongs to Non-ferrous Metallurgy field, particularly relate to a kind of Pt Pd concentrate calciner.
Background technology
The sulfuration essence molybdenum ore that have of current domestic and international application about has 96% first will change into industrial molybdenum oxide by roasting, could extract the molybdenum salt of solubility further, and then smelting becomes molybdenum or its alloy, and major part is used for Ferrous Metallurgy.Calcining molybdenum ore concentrate is when oxygen is not enough, and molybdenum sulfide and oxygen reaction generate brown molybdenum oxide, and release heat; When oxygen is sufficient, generates faint yellow molybdenum trioxide, release heat simultaneously.
Visible, the aerial roasting of molybdenum concntrate is significant exothermal reaction process, can self-heating complete completely, and roasting process does not need consume heat energy and should not generate low concentration SO
2flue gas.But in the roasting process of the production of calcining molybdenum concentrate, be that easy reverberatory furnace roasting in early days or the rotary kiln baking of extensive use at present, multiple hearth furnace roasting, the Flash Smelting Furnace roasting even comprising unrealized commercial Application and the roasting of interpolation auxiliary agent etc. all need to adopt external heat source to provide roasting heat to ensure carrying out smoothly of reaction.Roasting heat is generally provided by external heat source such as coal, oil, various coal gas, natural gas, electricity.
At present, Some Domestic small enterprise still adopts reverberatory furnace explained hereafter molybdenum oxide, reinforced, discharging during calcining molybdenum concentrate and the stirring of furnace charge are all manual operations, and roasting heat is supplied by coal, heavy oil or gas-fired, and controls sintering temperature in conjunction with the switch of fire door.The advantage of reverberatory furnace roasting technique is that equipment investment is few, the construction period is short, but because fuel flue gas and technique flue gas are discharged from same flue in roasting process, causes flue dust complicated component in discharge flue gas, the bad recovery of rhenium of association and SO
2concentration too low (being generally only 0.44 ~ 0.6%) and bad process, easily cause the severe contamination of environment.In addition, the heat utilization efficiency of reverberatory furnace is low, has the shortcomings such as energy consumption is large, working condition is poor, labour intensity is large, and energy consumption 1t industrial molybdenum oxide consumes coal up to 480kg standard coal, therefore this technique is day by day eliminated.
Domestic large and medium-sized enterprise's many employings multiple hearth furnace calcining molybdenum concentrate.Multiple hearth furnace general 8-16 layer siege is formed, molybdenum concntrate feeds from the 1st layer, 1st layer and the 2nd layer of siege heated by natural gas, carry out preheating and remove the flotation oil (as vapor oil or kerosene etc.) in molybdenum concntrate, then molybdenum concntrate rotates people the 3rd layer to the 5th layer, be oxidized by molybdenum concntrate exothermic reaction at these 3 layers, the molybdenum dioxide be oxidized to afterwards and molybdenum trioxide fall into the 3rd layer, oxidation is continued through external heat, now molybdenum dioxide continuous oxidation major part is converted into molybdenum trioxide, finally two-layerly usually to be filled with oxygen or oxygen-enriched air comes the unoxidized molybdenum dioxide of oxidation and a small amount of unoxidized molybdenum bisuphide.And make desulfurization complete gradually.The industrial molybdenum oxide roasting rate of recovery about 98% of current most multiple hearth furnace output, higher reaches 99%, desulfurization degree > 99.8%, containing S be 0.05-0.07%, energy consumption 1t industrial molybdenum oxide consume natural gas be 30-50m
3, be individually 100m
3(being decided by the chemical constituent of people's stove molybdenum concntrate, granularity and flotation oil content).But multiple hearth furnace structure is more complicated, and in body of heater, movable part is more.And each layer burner hearth exothermic heat of reaction is uneven.When temperature controls bad more than MoO
3sublimation temperature (795 DEG C) time, easily cause MoO
3distillation loss, but also furnace charge can be caused to sinter, cause feed opening to block, necessary regularly prepurging, not only increases labour intensity, and also impact is normal produces.SO during multiple hearth furnace roasting in outer last person's gas
2concentration lower (about 1.5%), relieving haperacidity is uneconomical, easily causes SO
2pollution, formed social effects of pollution.
In China, medium-sized and small enterprises mostly adopt rotary kiln baking technique.During roasting, material is under the rotation and tilting action of kiln body, and moved by kiln Caudad kiln hood, molybdenite starts to carry out oxidation reaction thereupon.The chemical reaction occurred in kiln according to molybdenum concntrate and the fuel factor of heating furnace, can be divided into three sections in kiln, and the position of every section changes with the difference of charging rate, concentrate physical property and chemical composition.Preheating and drying band is positioned at kiln afterbody, and temperature is between 250 ~ 450 DEG C, material at this preheating and drying, except deoiling, water; Reaction zone is in the middle part of kiln, temperature is between 500 ~ 700 DEG C, molybdenum concntrate reaches burning-point in this section, chemical reaction heat by itself carries out oxidation reaction, generates molybdenum oxide, when the residual sulphur of material is down to below 3.5%, hypergolic reaction can not be leaned on to continue desulfurization, high temperature or the high-temperature flue gas of now outer heating source supply make residual sulphur continue to take off, and this section of furnace temperature is 350 ~ 650 DEG C, and roasting material is this section of discharging.
The heat-supplying mode of rotary kiln has electrical heating, heavy-oil heating, heated by gas, coal heating, and energy consumption 1t industrial molybdenum oxide consumes coal up to 275kg standard coal.In rotary kiln baking technique, material is in and stirs state continuously in stove, and roasting is abundant, and in product, sulfur-bearing rate is less; SO in tail gas
2the height of concentration ratio reverberatory furnace roasting technique, is about 1.5%, but still does not reach the concentration conditions of 2 ~ 4% required for unstably manufacturing acid, unsuitable relieving haperacidity.
Visible, the roasting technique of the molybdenum concntrate of current extensive use not only significantly consume fuel or other energy, and provide oxidant to calcination because of the oxygen deprivation flue gas replacement air produced with fuel combustion, cause baking flue gas volumetric expansion, define dilution effect, make SO in baking flue gas
2on the whole volumetric concentration only has about 1%, and this concentration is obviously too low, does not reach the concentration requirement of relieving haperacidity, and be not easy to recycling, direct discharge can cause again the waste of resource and the severe contamination of environment.Meanwhile, in molybdenum concntrate the more valuable resource rare element rhenium of association along with low concentration SO
2flue gas is almost exposed to light accidentally, only have few producer recovery rhenium, meanwhile, molybdenum concntrate about has the loss of 3% in roasting process, wherein about 2/3rds be with a large amount of flue gas emptying contain molybdenum powder dirt.In actual production, first general molybdenum concntrate enters people's drying and preheating phase after entering stove, and in common adverse current roasting, the main fume afterheat that relies on just can reach required preheat temperature; Interim in main reaction, exothermic heat of reaction significantly and the fusing point of product molybdenum oxide and boiling point low all especially, consider that these situations just avoid high temperature as far as possible, therefore need again timely heat extraction-be usually close to furnace high-temperature district to be blended into cold wind even to spray water and utilize water jacket to conduct heat and realize, these measures make response intensity be suppressed, course of reaction extends, and reaction heat loss increases; In the desulfurization later stage de-residual sulphur section of back segment (namely in stove) of key, although residual sulphur relative quantity declines rapidly, but definitely rate of sulphur expulsion is more and more little, therefore conversely also will to being about to become the material concurrent heating of product-usually utilize above-mentioned heat extraction or fume afterheat cannot meet this requirement and ad hoc burning or electric calorifie installation need be relied on.Therefore after entering the main reaction phase, turning to the process of discharging opening to see along molybdenum-containing material material, the important measures of existing roasting are first heat extraction, rear concurrent heating.This thermal technology's measure adopted and dependence fuel combustion heat up, and rely on air draught spray cooling, the flue gas weight of multiple hearth furnace, reverberatory furnace and most of rotary kiln just constantly expands, and fluidized bed furnace is also like this, wherein SO
2and dust constantly " dilution ", defines dilution effect, common concentration, comprehensive utilization and relieving haperacidity is made all to become very difficult and cost sharp increase.
In the production of smelting enterprise's treatment of Pt-Pd concentrate, need to carry out roasting pretreatment to carry out follow-up removing impurities to a large amount of Pt Pd concentrate containing impurity.The calciners such as the electric furnace of current employing can not meet technological requirement, and roasting process exists and gives out macro-corrosion gas and have a strong impact on environment, and cause Pt Pd concentrate to harden the phenomena impair such as the agglomerating problems such as roasting effect.
Summary of the invention
Technical problem to be solved by this invention is that roasting process exists and gives out macro-corrosion gas and have a strong impact on environment, and causes Pt Pd concentrate to harden the phenomena impair such as the agglomerating problems such as roasting effect.
The invention provides a kind of Pt Pd concentrate calciner.
The object of the present invention is to provide one both to meet manufacturing technique requirent, possess again the eco-friendly Pt Pd concentrate calciner of roasting process.
A kind of Pt Pd concentrate calciner, comprise feed, roasting and smoke absorption three part composition, the pressure feeding spiral of feed section is connected by the roaster of feed conduit with roasting part, and smoke absorption part is connected with roaster by pipeline; Described roasting part comprises roaster, heating jacket, inside spin; Described heating jacket is also provided with steam inlet and outlet; Described smoke absorption part comprises steam-water separator and air-introduced machine.
In order to prevent acidic liquid and gas to the corrosion of equipment, in described Pt Pd concentrate calciner, the equipment and materials of roasting part and feed section all adopts stainless steel.
The invention has the advantages that: 1), the present invention adopt pressure feeding spiral control material add speed, avoid hardening in roasting process, the calcining epigranular of output, moisture reach production requirement.
2), adopt device of the present invention after, the volatile acidic gas eliminating generation, to the pollution of environment, improves operating environment.3), appliance arrangement structural allocation of the present invention is reasonable, floor space is little, it is simple to make, easy to maintenance.4), simple to operate, the operating personnel of needs are few.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Fig. 2 is side view of the present invention.
Wherein, 1-pressure feeding spiral, 2-feed conduit, 3-roaster, 4-driving device for slow-run, 5-inside spin, 6-heating jacket, 7-steam inlet, 8-steam (vapor) outlet, 9-steam-water separator, 10-air-introduced machine, 11-pipeline.
Detailed description of the invention
The present invention is further described according to following embodiment, and those skilled in the art can understand, following embodiment only plays the effect of explanation to the present invention.Without departing from the premise in the spirit of the present invention, any improvement the present invention done and substituting all within the scope of protection of the invention.
As shown in the figure, a kind of Pt Pd concentrate calciner, comprise feed, roasting and smoke absorption three part composition, the pressure feeding spiral 1 of feed section is connected with the roaster 3 of roasting part by feed conduit 2, and smoke absorption part is connected with roaster 3 by pipeline 11; Described roasting part comprises roaster 3, heating jacket 6, inside spin 5; Described heating jacket 6 is also provided with steam inlet 7 and outlet 8; Described smoke absorption part comprises steam-water separator 9 and air-introduced machine 10.
Operation principle of the present invention is as follows: open after the steam inlet valve of heating on chuck and spiral carries out intensification preheating to roaster and continue to pass into automatic steam control sintering temperature; Pt Pd concentrate in hopper enters in roaster continuously, equably and carries out roasting under the drive of reinforced spiral; Pt Pd concentrate after roasting, under the effect of roaster inside spin, is discharged from discharging opening; And the escaping gas that dry run produces escapes and enter in steam-water separator from exhaust outlet and collects, realize being separated of escaping gas and Pt Pd concentrate, reach the object of the continuous roasting of Pt Pd concentrate.
More specifically:
Unlatching steam inlet 7 pairs of roasters 3 on chuck 6 and spiral 5 of heating carry out preheating;
When in roaster 3, temperature reaches 400 DEG C, start pressure feeding spiral 1 and the Pt Pd concentrate continuous uniform in hopper is added in roaster 3 carry out roasting; Control pressure feeding spiral 1 rotary speed, making to add inventory in roaster 3 is 0.3 ~ 0.5kg/s;
Continue to pass into steam, make roasting in-furnace temperature remain between 400 ~ 450 DEG C; Open driving device for slow-run 4, the material in roaster 3 was stopped after 2 ~ 4 hours in inside spin 5, discharge, for the production of the noble metal such as platinum, palladium at discharging opening;
The flue gas that roasting process produces realizes gas-water separation by pipeline 11 in steam-water separator 9; Gas after separation carries out qualified discharge after subsequent treatment after air-introduced machine 10 is discharged; Corrosive liquids is recycled by bottom valve after collecting in steam-water separator 9;
Method of the present invention, have employed enclosed roasting device, carries out centralized collection process by flue gas absorbing device to the flue gas that roasting process produces, and overcomes original calciner escaping gas disposal difficulties.
More preferably:
Unlatching steam inlet 7 pairs of roasters 3 on chuck 6 and spiral 5 of heating carry out preheating;
When in roaster 3, temperature reaches 400 DEG C, the Pt Pd concentrate in hopper joins in φ 850 × 5000mm roaster 3 with 0.3 ~ 0.5kg/s charging rate continuous uniform and carries out roasting by startup pressure feeding spiral 1; Control pressure feeding spiral 1 rotary speed, making to add inventory in roaster 3 is 0.3 ~ 0.5kg/s; Continue to pass into steam, make roasting in-furnace temperature remain between 400 ~ 450 DEG C; Open driving device for slow-run 4, the material in roaster 3 was stopped after 2 ~ 4 hours in inside spin 5, discharge, for the production of the noble metal such as platinum, palladium at discharging opening; Obtain canescence uniform particles, granularity is less than 120 object fired slags, and wet weight is less than 2%.
The flue gas that roasting process produces realizes gas-water separation by pipeline 11 in steam-water separator 9; Gas after separation carries out qualified discharge after subsequent treatment after air-introduced machine 10 is discharged; Corrosive liquids is recycled by bottom valve after collecting in steam-water separator 9.
Claims (1)
1. a Pt Pd concentrate calciner, it is characterized in that comprising following part: pressure feeding spiral (1), feed conduit (2), roaster (3), driving device for slow-run (4), inside spin (5), heating jacket (6), steam inlet (7), steam (vapor) outlet (8), steam-water separator (9), air-introduced machine (10), pipeline (11), wherein the pressure feeding spiral (1) of feed section is connected with the roaster (3) of roasting part by feed conduit (2), smoke absorption part is connected with roaster (3) by pipeline (11), described roasting part comprises roaster (3), heating jacket (6), inside spin (5), described heating jacket (6) is also provided with steam inlet (7) and outlet (8), described smoke absorption part comprises steam-water separator (9) and air-introduced machine (10).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510081526.1A CN104596294B (en) | 2015-02-15 | 2015-02-15 | A kind of Pt Pd concentrate calciner |
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| CN201510081526.1A CN104596294B (en) | 2015-02-15 | 2015-02-15 | A kind of Pt Pd concentrate calciner |
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| CN104596294A true CN104596294A (en) | 2015-05-06 |
| CN104596294B CN104596294B (en) | 2016-06-01 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109338097A (en) * | 2018-11-26 | 2019-02-15 | 东北大学 | A kind of calcining molybdenum ore concentrate device and roasting technique |
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| DE3227891A1 (en) * | 1982-07-26 | 1984-01-26 | Peter 7869 Holzinshaus Voelskow | Rotary drum for the thermal treatment of loose materials |
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| CN1267738A (en) * | 1999-03-18 | 2000-09-27 | 电子科技大学 | Pretreatment microwave technology for coated composite platinum-palladium ore |
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| CN102305528A (en) * | 2011-07-01 | 2012-01-04 | 福建省诏安县绿洲生化有限公司 | Spiral promoting drier |
| CN102352432A (en) * | 2011-08-30 | 2012-02-15 | 杨佳定 | Concentrate drying and roasting device and method for directly drying and roasting concentrate by using same |
| CN102874850A (en) * | 2012-10-25 | 2013-01-16 | 西安三瑞实业有限公司 | Roasting system and roasting method for lithium-ore acidification by using externally-heated type rotary furnace |
-
2015
- 2015-02-15 CN CN201510081526.1A patent/CN104596294B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3227891A1 (en) * | 1982-07-26 | 1984-01-26 | Peter 7869 Holzinshaus Voelskow | Rotary drum for the thermal treatment of loose materials |
| CN1267738A (en) * | 1999-03-18 | 2000-09-27 | 电子科技大学 | Pretreatment microwave technology for coated composite platinum-palladium ore |
| CN2367621Y (en) * | 1999-04-09 | 2000-03-08 | 电子科技大学 | Continuous microwave mineral-roasting apparatus |
| CN201105221Y (en) * | 2007-08-24 | 2008-08-27 | 宜宾天原集团股份有限公司 | Self-cleaning type reactor for producing formic acid |
| CN201858864U (en) * | 2010-07-21 | 2011-06-08 | 洛阳栾川钼业集团股份有限公司 | Molybdenum concentrate self-heating roasting device |
| CN102305528A (en) * | 2011-07-01 | 2012-01-04 | 福建省诏安县绿洲生化有限公司 | Spiral promoting drier |
| CN102352432A (en) * | 2011-08-30 | 2012-02-15 | 杨佳定 | Concentrate drying and roasting device and method for directly drying and roasting concentrate by using same |
| CN102874850A (en) * | 2012-10-25 | 2013-01-16 | 西安三瑞实业有限公司 | Roasting system and roasting method for lithium-ore acidification by using externally-heated type rotary furnace |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109338097A (en) * | 2018-11-26 | 2019-02-15 | 东北大学 | A kind of calcining molybdenum ore concentrate device and roasting technique |
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| CN104596294B (en) | 2016-06-01 |
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