WO2023284292A1 - 一种含锡物料熔炼的系统及方法 - Google Patents

一种含锡物料熔炼的系统及方法 Download PDF

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Publication number
WO2023284292A1
WO2023284292A1 PCT/CN2022/075947 CN2022075947W WO2023284292A1 WO 2023284292 A1 WO2023284292 A1 WO 2023284292A1 CN 2022075947 W CN2022075947 W CN 2022075947W WO 2023284292 A1 WO2023284292 A1 WO 2023284292A1
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WIPO (PCT)
Prior art keywords
tin
furnace
smelting
bin
spray gun
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PCT/CN2022/075947
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English (en)
French (fr)
Inventor
唐都作
宋兴诚
袁海滨
徐万立
张驰
王建伟
陈云
刘庆东
王明江
李俊杰
宋戈
Original Assignee
云南锡业股份有限公司锡业分公司
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Priority to EP22840938.9A priority Critical patent/EP4265758A4/en
Priority to US17/692,059 priority patent/US20230015594A1/en
Publication of WO2023284292A1 publication Critical patent/WO2023284292A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B25/00—Obtaining tin
    • C22B25/02—Obtaining tin by dry processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B25/00—Obtaining tin
    • C22B25/06—Obtaining tin from scrap, especially tin scrap
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/10—Dry methods smelting of sulfides or formation of mattes by solid carbonaceous reducing agents
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/001—Dry processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/02—Working-up flue dust
    • 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
    • Y02P10/20—Recycling

Definitions

  • the invention relates to the technical field of tin concentrate pyromelting crude tin, and more specifically relates to a system and method for smelting tin-containing materials.
  • the increase in moisture content will not only occupy smelting productivity and increase smelting energy consumption, but also increase the processing capacity of the flue gas treatment system due to the vaporization of the water in the mixed material after high temperature, resulting in a large amount of high-temperature steam that enters the subsequent process flue gas treatment system and processing costs.
  • pre-refining pretreatments such as desulfurization and arsenic removal are usually required to produce various tin-containing fine-grained dry materials such as tin-containing fine-grained dry materials produced by fluidized fluidized furnace roasting, smoke High tin content fumes produced by melting furnaces, high tin content fumes produced by other smelting furnaces, etc.
  • All kinds of tin-containing fine-grained dry materials need to be transported by pneumatic pipelines or special vehicles to the batching ore bin for pre-furnace batching, and then transported to the smelting furnace by belts for smelting.
  • the reverse transportation process of various tin-containing fine-grained dry materials is prone to losses such as splashing and leakage.
  • the falling distance in the smelting furnace exceeds 10 meters, and it is easy to be drawn into the tail gas dust collector with the furnace flue gas, and then the dust collector The device returns to the batching ore bin to enter the next batching into the furnace process.
  • Multiple and repeated in-process reverse transportation will further accelerate the loss of materials, resulting in a low comprehensive recovery rate of tin smelting, and at the same time lead to poor environmental sanitation on site and damage to operators. physical condition.
  • the present invention provides a tin-containing material smelting system and method, which can significantly improve the tin smelting production environment, increase the recovery rate of tin-containing fine-grained dry materials, and achieve green and energy-saving effects.
  • the invention provides a tin-containing material smelting system, which includes a pretreatment mechanism, a screening mechanism, a feeding mechanism, a smelting mechanism, a slag processing mechanism and an exhaust gas processing mechanism;
  • the screening mechanism includes a screening machine, a fine material bin and a coarse material bin;
  • the upstream of the screening machine is connected to the downstream of the pretreatment mechanism, the oversize material outlet of the screening machine is connected to the coarse material bin, the undersize material outlet of the screening machine is connected to the fine material bin, and the coarse material
  • the bin and the fine material bin are respectively connected to the smelting mechanism through the feeding mechanism;
  • the feeding mechanism includes a feeding device, a batching bin, a first furnace front feed bin, a second furnace front feed bin, a spray gun and a pulverized coal bunker;
  • the coarse material bin communicates with the batching bin through the feeding device
  • the batching bin communicates with the smelting mechanism through the feeding device;
  • the upstream of the first front feed bin communicates with the fine material bin, and the downstream communicates with the smelting mechanism through the spray gun;
  • the second The front feed bunker communicates with the slag processing mechanism and the tail gas processing mechanism respectively upstream, and the downstream communicates with the smelting mechanism through the spray gun;
  • the pulverized coal bunker communicates with the smelting mechanism through the spray gun.
  • the feeding device includes a special feeding cart and a belt.
  • the present invention screens the tin-containing dry materials, so that the tin-containing materials with larger particle size can be directly transported into the top-blowing furnace melting pool for smelting through the belt, while the tin-containing materials with finer particle size
  • the material is sprayed into the molten pool through the top-blowing lance, which can reduce the splashing or leakage loss of the tin-containing material with fine particle size during the transfer process, and can also avoid the mechanical inclusion or flying loss caused by the belt furnace top being put into the top-blowing furnace.
  • it avoids the addition of moisture to fine-grained dry materials before entering the furnace, thereby reducing smelting energy consumption and smelting flue gas volume, and achieving greener, environmentally friendly, and energy-saving smelting.
  • the pretreatment mechanism includes a fluidized furnace, a cooler and a fluidized furnace scraper;
  • the cooler is connected downstream of the fluidized fluidized furnace
  • the fluidized furnace scraper machine is connected downstream of the cooler;
  • the sieving machine is connected downstream of the scraper machine of the fluidized fluidized furnace.
  • the cooler is used to cool the tin-containing intermediate material roasted by the fluidized fluidized furnace
  • the present invention can classify and process high-sulfur and arsenic-containing tin ore fluidized furnace separately through the pretreatment mechanism, and provide low-sulfur, low-arsenic and tin-containing materials for the top-blown furnace, and at the same time, the materials roasted by the fluidized fluidized furnace pass through Pneumatic conveying to the top-blowing furnace for smelting, and airtight pneumatic conveying of materials can reduce the flying or splashing loss of materials in the process of conveying and reversing through the belt, create favorable conditions for the top-blowing furnace to realize powder injection, and also help improve the recovery rate of tin material smelting .
  • the feeding mechanism further includes a first pneumatic pipeline, a first feeding pipe, a second pneumatic pipeline, a second feeding pipe, a mixing air pipe and a metal hose;
  • the first pneumatic pipeline is connected to the fine material bin and the first feed bin, and the first feed bin is connected to the mixing air duct through the first feeding pipe;
  • the upstream of the second pneumatic pipeline is respectively connected to the slag processing mechanism and the tail gas processing mechanism, and the downstream is connected to the second feed bin, and the second feed bin is connected to the Mixing air duct;
  • the mixing air pipe is at an angle of 70-75° to the first feeding pipe and the second feeding pipe respectively, and the mixing air pipe is connected to the spray gun through the metal hose.
  • the mixing air pipe and the first and second feeding pipes are designed according to the best bevel angle to ensure that the powder is fully mixed and the feeding is smooth without clogging.
  • the smelting mechanism includes a top-blowing furnace, a furnace top sample rod, a thick tin port, a transfer tin bun and a slag port;
  • the top of the top-blowing furnace is connected to one end of the belt, and at the same time is connected to the exhaust gas treatment mechanism; and the spray gun extends into the top-blowing furnace through the top surface of the top-blowing furnace, while The furnace top sample rod extends into the top-blowing furnace through the top surface of the top-blowing furnace; the bottom of the top-blowing furnace is connected with the transfer tin bun through the thick tin port, while the top-blowing furnace The bottom of the slag is connected to the slag processing mechanism through the slag port.
  • top-blowing furnace is used to efficiently smelt and recover tin-containing materials, and the produced top-blowing furnace slag is sent to the next process for recycling.
  • the slag treatment mechanism includes a slag chute, a fuming furnace, a fuming furnace waste heat boiler, a fuming furnace surface cooler, a fuming furnace bag filter, a fuming dust scraper, and a fuming dust bin;
  • the fuming furnace is connected to the slag outlet through the slag chute, the bottom of the fuming furnace is provided with a fuming furnace slag outlet, and the top of the fuming furnace is connected to the waste heat boiler of the fuming furnace; the fuming furnace
  • the downstream of the furnace waste heat boiler is connected to the surface cooler of the fuming furnace; the downstream of the fuming furnace is connected to the bag filter of the fuming furnace; the upstream of the fuming dust scraper is respectively connected to the waste heat boiler of the fuming furnace, the The surface cooler of the fuming furnace and the bag filter of the fuming furnace are connected downstream to the fuming dust bin; the downstream of the fuming dust bin is connected to the second furnace front feed bin through the second pneumatic pipeline .
  • the beneficial effect of the above preferred technical solution is: to realize the full fuming recovery of the tin contained in the top-blown furnace slag, and to avoid the loss of tin.
  • the tail gas treatment mechanism includes a flue, a top-blown furnace waste heat boiler, a temperature measuring device, a top-blown furnace electric dust collector, a top-blown furnace dust scraper, and a top-blown furnace dust bin; one end of the flue Connect the top of the top-blown furnace, the other end is connected to the waste heat boiler of the top-blown furnace, and the end of the flue connected to the top of the top-blown furnace is installed with the temperature measuring device; the downstream of the waste heat boiler of the top-blown furnace is connected to the The top-blown furnace electric dust collector; the top-blown furnace dust scraper is connected upstream to the top-blown furnace waste heat boiler and the top-blown furnace electric dust collector respectively, and the downstream is connected to the top-blown furnace dust bin; The downstream of the top-blowing furnace dust bin is connected to the second front feed bin through the second pneumatic pipeline.
  • the beneficial effects of the above preferred technical solution are: realizing efficient recovery of the tin-containing tail gas in the flue gas of the top-blown furnace, and reducing the loss caused by the tin-containing tail gas entering the back-end acid making system.
  • the present invention also provides a method for smelting tin-containing materials, using the above-mentioned system, specifically comprising the following steps:
  • the tin-containing dry material is transported to a screening machine for screening, and the tin-containing fine-grained dry material is sprayed into the top-blowing furnace through a spray gun, and the tin-containing coarse-grained dry material is transported to the batching bin through a special feeder;
  • the low-sulfur and arsenic-containing tin ore and the tin-containing coarse-grained dry material, quartz sand and limestone flux are fed into the top-blown furnace roof via a belt after batching according to the proportion in the batching bin
  • the amount of the tin-containing fine-grained dry material sprayed into the top-blowing furnace through the spray gun and the amount of the recovered tin-containing material are controlled to obtain a mixed melt after smelting in the top-blowing furnace; then stop feeding and enter the reduction process.
  • the amount of lump coal fed through the belt and the pulverized coal fed through the spray gun are adjusted ;
  • steps (2) to (3) can be repeated.
  • a tin-containing material smelting method disclosed in the present invention classifies and screens the tin-containing dry material, and the obtained low-sulfur arsenic-containing tin ore and tin-containing coarse-grained dry material can be directly It is transported to the top-blowing furnace by a special skip and a belt for smelting.
  • tin-containing fine-grained dry materials and recycled tin-containing materials are transported through fully enclosed pneumatic pipelines and sprayed into the molten pool of the top-blown furnace through spray guns.
  • the finer-grained materials are spilled or lost due to material leakage in the process of reloading. It can also avoid mechanical inclusion or flying loss caused by being thrown into the top-blowing furnace through the belt.
  • the low-sulfur arsenic-containing tin ore described in step (1) has Sn>30wt.%, Pb at 0.2 to 3.0wt.%, S ⁇ 1.0wt.%, As ⁇ 1.0wt.%, and Fe at 10 to 30wt.%, Bi at 0.1-0.2wt.%;
  • the high-sulfur arsenic-containing tin ore has Sn>30wt.%, Pb at 0.2-3.0wt.%, S>2.0wt.%, As>2.0wt.%. , Fe at 10-30wt.%, Bi at 0.1-0.5wt.%;
  • the pretreatment is roasting at 650-720°C for 2-2.5 hours, the moisture content of the tin-containing dry material is ⁇ 1%, Sn>40wt.%, Pb is 0.5-3.0wt.%, S ⁇ 1.0wt.%. , As ⁇ 1.0wt.%, Fe at 12-28wt.%, Bi at 0.05-0.20wt.%;
  • the sieving uses a 5-mesh sieve, the particle size of the tin-containing fine-grained dry material is 5-300 mesh, the particle size of the tin-containing coarse-grained dry material is ⁇ 5 mesh, and the bulk density is 2-3 g/cm 3 .
  • Sn is 30 to 50wt.%
  • Pb is 0.2 to 3.0wt.%
  • Fe is 2 to 50wt.%. 6wt.%
  • Bi at 0.1-0.3wt.%
  • moisture ⁇ 5.0% particle size 100-300 mesh, bulk density 0.5-1.0g/cm3;
  • the low-sulfur and arsenic-containing tin ore, the tin-containing fine-grained dry material, the tin-containing coarse-grained dry material and the recovered tin-containing material are comprehensively calculated in the batching bin according to the batching principle and put into the furnace mixture batching Ratio, and through the DCS feeding system of the batching bin, accurately control the addition of the low-sulfur arsenic-containing tin ore and the tin-containing coarse-grained dry material input through the belt, and at the same time control the input of the top-blown furnace through the spray gun.
  • the low-sulfur and arsenic-containing tin ore, the tin-containing fine-grained dry material, the tin-containing coarse-grained dry material and the recovered tin-containing material are 30-40wt.%, 0-40wt.%, respectively, based on 100wt.%. 45wt.%, 5 ⁇ 10wt.%, 0 ⁇ 20wt.%;
  • the back pressure of the spray gun is 20-30kPa
  • the flue gas temperature is 400-500°C
  • the furnace negative pressure of the top-blown furnace is -10-0Pa
  • the oxygen-enriched concentration of the spray gun wind is 37-39wt.%.
  • the CO concentration is 0-500ppm
  • the pulverized coal feeding amount of the spray gun is 5.0-5.5t/h
  • the lump coal feeding amount of the belt is 2.0-2.5t/h;
  • the back pressure of the spray gun is 30-40kPa
  • the flue gas temperature is 500-550°C
  • the furnace negative pressure of the top-blown furnace is -10-0Pa
  • the oxygen-enriched concentration of the spray gun wind is 33-36wt.%
  • the CO concentration of the tail gas is At 2000-5000ppm
  • the amount of pulverized coal fed by the spray gun is 4.0-5.0t/h
  • the amount of lump coal fed by the belt is 4.0-5.0t/h;
  • the low-sulfur and arsenic-containing tin ore and the tin-containing coarse-grained dry material are first fed into the top-blown furnace through a belt to make the depth of the molten pool in the furnace ⁇ 500mm, and then start the spray gun to dry the tin-containing fine grains.
  • the material and the reclaimed tin-containing material are input into the top-blowing furnace;
  • the feeding cycle is as follows: the low-sulfur and arsenic-containing tin ore and the tin-containing coarse-grained dry material start to be conveyed by a belt, and end when the depth of the molten pool is 1500-1800 mm.
  • the beneficial effect of the above-mentioned preferred technical solution is: first input the coarse-grained dry material into the molten pool of the top-blowing furnace through the belt, and after the depth of the molten pool reaches 500mm, start the spray gun to spray the fine-grained dry material into the top-blown furnace to avoid the depth of the molten pool Insufficient activation of the spray gun to spray the material will cause the fine-grained dry material to fly in the top-blown furnace and not fall into the molten pool, so as to avoid affecting the improvement of the comprehensive recovery index of smelting.
  • the depth of the molten pool is measured by inserting a furnace top sample rod into the molten pool.
  • the beneficial effect of the above optimal technical solution is: real-time monitoring of the depth of the molten pool by inserting the top sample rod into the molten pool to ensure optimal control of the smelting process parameters.
  • the fuming process in step (3) is to add a vulcanizing agent in the fuming furnace to fume and volatilize the tin in the slag of the top-blown furnace;
  • the ratio is 1:3, the excess coefficient is 1.2-1.3, and the vulcanizing agent is added within 90-120 minutes until the high-temperature melt in the fuming furnace contains tin ⁇ 0.3wt.%. Sampling and analysis show that the fuming furnace When the internal high-temperature melt contains more than 0.3wt.% tin, continue to add vulcanizing agent to volatilize tin until the high-temperature melt contains tin ⁇ 0.3wt.%.
  • the present invention discloses a system and method for smelting tin-containing materials, which have the following beneficial effects:
  • the present invention classifies tin-containing dry materials, and transports tin-containing materials with finer particle size through a fully enclosed pneumatic pipeline, and then sprays them directly into the molten pool through a spray gun, which can reduce the loss of spilling or material leakage in the process. , and it can also avoid the mechanical inclusion or flying loss caused by the belt being thrown into the top blowing furnace;
  • Tin-containing materials with fine particle size are transported through fully enclosed pneumatic pipelines, sprayed into the molten pool by spray guns for reduction and smelting, no need to add water for granulation, not only less material loss due to reverse transportation, smooth material transportation, and good occupational hygiene at the job site , the operation is also simple, the recovery rate of crude tin smelting is high, and the energy consumption of adding water to granulate the dust material with fine particle size of tin is reduced, the dust rate of top blowing furnace is reduced, and the technical and economic indicators and production efficiency of tin smelting are further improved;
  • FIG. 1 is a schematic diagram of the structure provided by Embodiment 1 of the present invention.
  • 1 is the top blowing furnace
  • 2 is the belt
  • 3 is the flue
  • 4 is the temperature measuring device
  • 5 is the furnace top sample rod
  • 6 is the spray gun
  • 7 is the metal hose
  • 8 is the second furnace front feed bin
  • 9 is the feed bin in front of the first furnace
  • 10 is the pulverized coal bin
  • 11 is the mixing air duct
  • 12 is the fluidized furnace
  • 13 is the cooler
  • 14 is the scraper machine for the fluidized furnace
  • 15 is the screening machine
  • 16 is the fine material bin
  • 17 is the coarse material warehouse
  • 18 is the special feeder
  • 19 is the first pneumatic pipeline
  • 20 is the crude tin port
  • 21 is the tin transfer bun
  • 22 is the slag port
  • 23 is the slag chute
  • 24 is the fuming furnace waste heat boiler
  • 25 Top blowing furnace electric dust collector
  • 26 is top blowing furnace dust scraper
  • 27 is top blowing furnace dust bin
  • 28 is fuming furnace
  • 30 is fuming
  • the embodiment of the invention discloses a tin-containing material smelting system, which includes a pretreatment mechanism, a screening mechanism, a feeding mechanism, a smelting mechanism, a slag processing mechanism and an exhaust gas processing mechanism;
  • the downstream of the pretreatment mechanism is connected to the screening mechanism
  • the screening mechanism includes a screening machine, a fine material bin and a coarse material bin.
  • the upstream of the screening machine is connected to the downstream of the pretreatment mechanism.
  • the material bin and the fine material bin are connected to the melting mechanism through the feeding mechanism;
  • the feeding mechanism includes a feeding device, a batching bin, the first furnace front feed bin, the second furnace front feed bin, a spray gun and a pulverized coal bin; the feeding device includes a special feeding car and a belt
  • the coarse material bin is connected to the batching bin through a special feeder, and the batching bin is connected to the smelting mechanism through a belt; the upstream of the first furnace front bin is connected to the fine material bin, and the downstream is connected to the smelting mechanism through a spray gun; at the same time, the upstream of the second furnace front bin is respectively connected to The downstream of the slag processing mechanism and the tail gas processing mechanism are connected to the smelting mechanism through the spray gun; and the pulverized coal bunker is connected to the smelting mechanism through the spray gun.
  • the pretreatment mechanism includes a fluidized furnace, a cooler and a fluidized furnace scraper; the downstream of the fluidized furnace is connected to a cooler; the downstream of the cooler is connected to a fluidized furnace scraper; the downstream of the fluidized furnace scraper is connected to a screening machine.
  • the feeding mechanism also includes a first pneumatic pipeline, a first feeding pipe, a second pneumatic pipeline, a second feeding pipe, a mixing air pipe and a metal hose; the first pneumatic pipeline connects the fine material bin and the first furnace front material
  • the first furnace feed bin is connected to the mixing air pipe through the first feeding pipe; the upstream of the second pneumatic pipeline is respectively connected to the slag processing mechanism and the tail gas processing mechanism, and the downstream is connected to the second furnace feed bin, and the second furnace feed bin
  • the mixing air pipe is connected through the second feeding pipe; the mixing air pipe is 75° to the first feeding pipe and the second feeding pipe respectively, and the mixing air pipe is connected to the spray gun through a metal hose.
  • the smelting mechanism includes a top-blowing furnace, a furnace top sample rod, a thick tin port, a transfer tin bun and a slag port; the top of the top-blowing furnace is connected to the belt and is connected to the exhaust gas treatment mechanism; and the spray gun extends through the top surface of the top-blowing furnace. into the top-blowing furnace, and at the same time, the top-blowing furnace passes through the top surface of the top-blowing furnace and extends into the top-blowing furnace; the bottom of the top-blowing furnace is connected with the transfer tin bun through the thick tin port, and at the same time, the bottom of the top-blowing furnace passes through the slag port Connect the slag handling mechanism.
  • the slag treatment mechanism includes slag chute, fuming furnace, fuming furnace waste heat boiler, fuming furnace surface cooler, fuming furnace bag filter, fuming dust scraper, fuming dust bin; fuming furnace passes through the slag chute Connected to the slag port, the bottom of the fuming furnace is provided with a fuming furnace slag outlet, and the top of the fuming furnace is connected to the waste heat boiler of the fuming furnace; the downstream of the waste heat boiler of the fuming furnace is connected to the surface cooler of the fuming furnace; the downstream of the fuming furnace is connected to the fuming furnace Furnace cloth bag dust collector; the upstream of the fuming dust scraper is respectively connected to the preheating pot of the fireworks road, the surface cooler of the fuming furnace and the bag filter of the fuming furnace, and the downstream is connected to the fuming dust bin; the downstream of the fuming dust bin passes through the second Pneumatic pipelines are connected to the feed bin in front of the second furnace.
  • the exhaust gas treatment mechanism includes flue, top-blown furnace waste heat boiler, temperature measuring device, top-blown furnace electric dust collector, top-blown furnace dust scraper, top-blown furnace dust bin; one end of the flue is connected to the top of the top-blown furnace, and the other is One end is connected to the waste heat boiler of the top-blown furnace, and a temperature measuring device is installed at the end of the flue connected to the top of the top-blown furnace; the downstream of the waste heat boiler of the top-blown furnace is connected to the electric precipitator of the top-blown furnace; The furnace waste heat boiler and the top-blowing furnace electric dust collector are connected downstream to the top-blowing furnace dust bin; the downstream of the top-blowing furnace dust bin is connected to the second furnace front feed bin through the second pneumatic pipeline.
  • Embodiment 2 of the present invention discloses a method for smelting tin-containing materials, using the system disclosed in Embodiment 1, specifically comprising the following steps:
  • the tin-containing dry material is transported to a screening machine for screening, and the tin-containing fine-grained dry material is sprayed into the top-blowing furnace through a spray gun, and the tin-containing coarse-grained dry material is transported to the batching bin through a special feeder;
  • the low-sulfur and arsenic-containing tin ore has Sn>30wt.%, Pb at 0.2-3.0wt.%, S ⁇ 1.0wt.%, As ⁇ 1.0wt.%, Fe at 10-30wt.%, and Bi at 0.1-3.0wt.%. 0.2wt.%; high sulfur and arsenic tin ore Sn>30wt.%, Pb at 0.2 ⁇ 3.0wt.%, S>2.0wt.%, As>2.0wt.%, Fe at 10 ⁇ 30wt.%, Bi In 0.1 ⁇ 0.5wt.%;
  • Pretreatment roasting at 650-720°C for 2-2.5 hours, moisture content of tin-containing dry material ⁇ 1%, Sn>40wt.%, Pb at 0.5-3.0wt.%, S ⁇ 1.0wt.%, As ⁇ 1.0wt .%, Fe at 12 ⁇ 28wt.%, Bi at 0.05 ⁇ 0.20wt.%;
  • Screening adopts a 5-mesh sieve, the particle size of the tin-containing fine-grained dry material is 5-300 mesh, the particle size of the tin-containing coarse-grained dry material is ⁇ 5 mesh, and the bulk density is 2-3g/cm3
  • the low-sulfur and arsenic-containing tin ore and the tin-containing coarse-grained dry material, quartz sand and limestone flux are fed into the top-blown furnace roof via a belt after batching according to the proportion in the batching bin
  • the amount of the tin-containing fine-grained dry material sprayed into the top-blowing furnace through the spray gun and the amount of the recovered tin-containing material are controlled to obtain a mixed melt after smelting in the top-blowing furnace; then stop feeding and enter the reduction process.
  • the amount of lump coal fed through the belt and the pulverized coal fed through the spray gun are adjusted ;
  • Sn is 30 ⁇ 50wt.%
  • Pb is 0.2 ⁇ 3.0wt.%
  • Fe is 2 ⁇ 6wt.%
  • Bi is 0.1 ⁇ 0.3wt.%
  • moisture ⁇ 5.0% particle size 100-300 mesh, bulk density 0.5-1.0g/cm3;
  • the low-sulfur and arsenic-containing tin ore, the tin-containing fine-grained dry material, the tin-containing coarse-grained dry material and the recovered tin-containing material are comprehensively calculated in the batching bin according to the batching principle and put into the furnace mixture batching Ratio, and through the DCS feeding system of the batching bin, accurately control the addition of the low-sulfur arsenic-containing tin ore and the tin-containing coarse-grained dry material input through the belt, and at the same time control the input of the top-blown furnace through the spray gun.
  • Low-sulfur and arsenic-containing tin ore, tin-containing fine-grained dry materials, tin-containing coarse-grained dry materials and recycled tin-containing materials are calculated according to 100wt.%, respectively 30-40wt.%, 0-45wt.%, 5-10wt. %, 0 ⁇ 20wt.%;
  • the tin-containing fine-grained dry materials and recycled tin-containing materials are input into the top-blowing furnace through the spray gun to make the depth of the molten pool in the furnace ⁇ 500mm, and then the low-sulfur arsenic-containing tin ore and tin-containing coarse-grained dry materials are input into the top-blowing furnace through the belt.
  • Furnace; the feeding cycle is: the belt conveys low-sulfur arsenic-containing tin ore and tin-containing coarse-grained dry materials, and ends when the depth of the molten pool is 1500-1800 mm; and the depth of the molten pool is measured by inserting the furnace top sample rod into the molten pool
  • the back pressure of the spray gun is 20-30kPa
  • the flue gas temperature is 400-500°C
  • the furnace negative pressure of the top-blown furnace is -10-0Pa
  • the oxygen-enriched concentration of the spray gun wind is 37-39wt.%
  • the CO concentration of the tail gas 0 ⁇ 500ppm
  • the amount of pulverized coal fed by the spray gun is 5.0 ⁇ 5.5t/h
  • the amount of lump coal fed by the belt is 2.0 ⁇ 2.5t/h
  • the back pressure of the spray gun is 30-40kPa
  • the flue gas temperature is 500-550°C
  • the negative pressure of the top-blown furnace is -10-0Pa
  • the oxygen-enriched concentration of the spray gun wind is 33-36wt.%
  • the CO concentration of the tail gas is 2000 ⁇ 5000ppm
  • the amount of powdered coal fed by the spray gun is 4.0 ⁇ 5.0t/h
  • the amount of lump coal fed by the belt is 4.0 ⁇ 5.0t/h;
  • the fuming process is to add a vulcanizing agent in the fuming furnace to fume and volatilize the tin in the slag of the top-blowing furnace; Add the vulcanizing agent within 90 to 120 minutes until the high-temperature melt in the fuming furnace contains tin ⁇ 0.3wt.%. Add vulcanizing agent to volatilize tin until the content of tin in the high temperature melt is ⁇ 0.3wt.%.
  • steps (2) to (3) can be repeated.
  • Embodiment 3 of the present invention discloses a method for smelting tin-containing materials, using the system disclosed in Embodiment 1, specifically comprising the following steps:
  • tin-containing materials should be classified and treated: Sn>30wt.%, Pb at 0.2-3.0wt.%, S ⁇ 1.0wt.%, As ⁇ 1.0wt.%, Fe at 10-30wt.%, The low-sulfur and arsenic-containing tin ore with Bi at 0.1-0.2wt.% is transported to the batching bin through a special feed truck; Sn30wt.%, Pb at 0.2wt.%, S at 2.0wt.%, As at 2.0wt.
  • % Fe at 10wt.%, Bi at 0.1wt.%, high-sulfur and arsenic-containing tin ore is added to a fluidized furnace and roasted at 650-720°C for 2-2.5 hours for desulfurization and arsenic removal, and the output contains Sn at 40wt.%, Pb Tin-containing dry materials at 0.5wt.%, S at 0.8wt.%, As at 0.80wt.%, Fe at 12wt.%, Bi at 0.05wt.%, and moisture less than 1wt.%.
  • the dry material is screened, the material under the 5-mesh sieve is tin-containing fine-grained dry material, and the screened material is tin-containing coarse-grained dry material;
  • the particle size of tin-containing fine-grained dry material is 15 mesh
  • the particle size of tin-containing coarse-grained dry material is 4 mesh
  • the bulk density is 2g/cm 3
  • the tin-containing fine-grained dry material is transported to the first furnace through the first pneumatic pipeline Stored in the front silo, the tin-containing coarse-grained dry material is transferred to the batching bin by a special feed truck, and after comprehensive batching in the ore bin, it is transported to the top-blown furnace by a belt.
  • the DCS feeding system in the batching bin can accurately control the addition of the low-sulfur and arsenic-containing tin ore and the tin-containing coarse dry material that are fed into the roof of the top-blown furnace through the belt, and at the same time control the input into the top-blown furnace through the spray gun
  • the added amount of the tin-containing fine-grained dry material and the reclaimed tin-containing material; the proportions of low-sulfur arsenic-containing tin ore, tin-containing fine-grained dry material, tin-containing coarse-grained dry material and recycled tin-containing material are respectively It is 40wt.%, 30wt.%, 10wt
  • the composition of low sulfur and arsenic tin ore is: Sn 35wt.%, Pb 0.2wt.%, S 1.0wt.%, As ⁇ 1.0wt.%, Fe 10wt.%, Bi 0.1wt.%.
  • the recovered tin-containing materials are composed of fumed dust and recovered tail gas, which are directly transported through the second pneumatic pipeline to the storage bin in front of the second furnace.
  • the particle size of fume dust is 100 mesh, the bulk density is 0.5g/cm 3 , the moisture is less than 5wt.%, and the composition is: Sn 45wt.%, Pb 0.2wt.%, S 0.9wt.%, As 1.5wt.% , Fe 2wt.%, Bi 0.1wt.%; the particle size of recovered exhaust gas is 150 mesh, the bulk density is 0.6g/cm 3 , the moisture is less than 5wt.%, and the composition is: Sn 38wt.%, Pb1.0wt.%, S 0.75wt.%, As 1.8wt.%, Fe 3wt.%, Bi 0.1wt.%.
  • Tin-containing fine-grained dry materials and recycled tin-containing materials are connected from the feeding pipe of the furnace front silo to the common furnace front mixing air duct, and connected to the spray gun through a metal hose.
  • the air pressure of the mixing air duct should be lower than that of each furnace front silo
  • the wind pressure of the feeding pipe is 5-10%, and the feeding pipe of each furnace front silo is connected with the mixing air pipe at a tangent angle of 70-75 degrees.
  • the timing of the smelting of tin-containing fine-grained dry materials and recycled tin-containing materials into the molten pool through the spray gun of the top-blowing furnace needs to be started after the depth of the molten pool in the top-blown furnace reaches 500 mm, and the feeding is stopped after a complete feeding cycle is completed. Adjust the amount of low-sulfur arsenic-containing tin ore and the amount of tin-containing coarse-grained dry materials conveyed by the furnace top belt; the depth of the molten pool is detected by inserting the top-blown furnace top sample rod into the molten pool.
  • the feeding period is that the top-blowing furnace top feeding belt starts feeding until the height of the molten pool reaches 1500mm. During the feeding period, the smelting process is completed, and then enters the reduction stage of smelting high-temperature mixed melt.
  • the smelting process is controlled, the back pressure of the spray gun is controlled at 20 ⁇ 30kPa, the temperature measurement temperature of the flue gas of the top blowing furnace is controlled at 420°C, the negative pressure of the furnace is -10 ⁇ 0Pa, the oxygen enrichment concentration of the spray gun wind is 37 ⁇ 39wt.%, and the CO concentration of the tail gas is at 0 ⁇ 500ppm, 5.0 ⁇ 5.5t/h for pulverized coal by spray gun, 2.0 ⁇ 2.5t/h for lump coal by belt.
  • the reduction process is controlled, the spray gun back pressure is controlled at 30-40kPa, the top-blown furnace flue gas temperature measurement temperature is controlled at 500-550°C, the furnace negative pressure is -10-0Pa, the spray gun wind oxygen concentration is 33-36wt.%, the tail gas CO concentration At 2000-5000ppm, the spray gun feeds pulverized coal 4.0-5.0t/h, and the top-blown furnace feeds lump coal through the belt at 4.0-5.0t/h.
  • the fuming process is to add a vulcanizing agent in the fuming furnace to fume and volatilize the tin in the slag of the top-blowing furnace; Add the vulcanizing agent within 90 to 120 minutes until the high-temperature melt in the fuming furnace contains tin ⁇ 0.3wt.%. Add vulcanizing agent to volatilize tin until the content of tin in the high temperature melt is ⁇ 0.3wt.%.
  • steps (2) to (3) can be repeated.
  • Embodiment 4 of the present invention discloses a method for smelting tin-containing materials, using the system disclosed in Embodiment 1, specifically comprising the following steps:
  • tin-containing materials should be classified and treated: Sn>30wt.%, Pb at 0.2-3.0wt.%, S ⁇ 1.0wt.%, As ⁇ 1.0wt.%, Fe at 10-30wt.%,
  • the low-sulfur and arsenic-containing tin ore with a Bi content of 0.1-0.2wt.% is transported to the batching bin through a special feed truck; Fe15wt.%, Bi 0.2wt.% high-sulfur and arsenic-containing tin ore is desulfurized and dearsenized in a fluidized furnace at 650-720 ° C for 2-2.5 hours, and the output tin-containing dry material contains Sn 45wt.%, Pb 1.5wt.%, S 0.7wt.%, As 0.5wt.%, Fe18wt.%, Bi 0.08wt.%, moisture less than 1%, use a sieving machine to sieve the dry material containing tin, and the material under
  • the particle size of tin-containing fine-grained dry material is 300 mesh
  • the particle size of tin-containing coarse-grained dry material is 4 mesh
  • the bulk density is 2.5g/cm3.
  • the DCS feeding system in the batching bin can accurately control the addition of the low-sulfur and arsenic-containing tin ore and the tin-containing coarse dry material that are fed into the roof of the top-blown furnace through the belt, and at the same time control the input into the top-blown furnace through the spray gun
  • the adding amount of the described tin-containing fine-grained dry material and the reclaimed tin-containing material; the proportions of low-sulfur arsenic-containing tin ore, tin-containing fine-grained dry material, tin-containing coarse-grained dry material and reclaimed tin-containing material are respectively 35wt.%, 45wt.%, 10w
  • the composition of low-sulfur and arsenic-containing tin ore is: Sn 50wt.%, Pb 3.0wt.%, S ⁇ 1.0wt.%, As0.3wt.%, Fe 30wt.%, Bi 0.2wt.%.
  • the recovered tin-containing materials are composed of fumed dust and recovered tail gas, which are directly transported through the second pneumatic pipeline to the storage bin in front of the second furnace.
  • the particle size of fume dust is 200 mesh, and the bulk density is 0.8g/cm. wt.%.
  • the particle size of recovered exhaust gas is 300 mesh, the bulk density is 1.0g/cm 3 , and the composition is: Sn 42wt.%, Pb1.5wt.%, S 0.5wt.%, As 1.8wt.%, Fe6wt.%, Bi 0.3wt .%, moisture is less than 5wt.%.
  • Tin-containing fine-grained dry materials and recycled tin-containing materials are connected from the feeding pipe of the furnace front silo to the common furnace front mixing air duct, and connected to the spray gun through a metal hose.
  • the air pressure of the mixing air duct should be lower than that of each furnace front silo
  • the wind pressure of the feeding pipe is 5-10%, and the feeding pipe of each furnace front silo is connected with the mixing air pipe at a tangent angle of 70-75 degrees.
  • the timing of the smelting of tin-containing fine-grained dry materials and recycled tin-containing materials into the molten pool through the spray gun of the top-blowing furnace needs to be started after the depth of the molten pool in the top-blown furnace reaches 500 mm, and the feeding is stopped after a complete feeding cycle is completed. Adjust the amount of low-sulfur arsenic-containing tin ore and the amount of tin-containing coarse-grained dry materials conveyed by the furnace top belt; the depth of the molten pool is detected by inserting the top-blown furnace top sample rod into the molten pool.
  • the feeding period is that the top-blowing furnace top feeding belt starts feeding until the height of the molten pool reaches 1500mm. During the feeding period, the smelting process is completed, and then enters the reduction stage of smelting high-temperature mixed melt.
  • the smelting process of the molten pool of tin-containing materials is controlled, the back pressure of the spray gun is controlled at 20-30kPa, the temperature measurement temperature of the flue gas of the top-blown furnace is controlled at 500°C, the negative pressure of the furnace is -10-0Pa, and the oxygen-enriched concentration of the spray gun air is 37-39wt.%. , the tail gas CO concentration is 0-500ppm, the spray gun feeds pulverized coal 5.0-5.5t/h, and the top-blown furnace top belt feeds lump coal 2.0-2.5t/h.
  • the reduction process control of smelting high-temperature mixed melt the back pressure of the spray gun is controlled at 30-40kPa, the temperature measurement temperature of the top-blown furnace flue gas is controlled at 500-550°C, the negative pressure of the furnace is -10-0Pa, and the oxygen-enriched concentration of the spray gun air is 33-36wt .%, tail gas CO concentration is 2000-5000ppm, 4.0-5.0t/h pulverized coal is fed to the spray gun, and 4.0-5.0t/h lump coal is fed to the top belt of the top-blown furnace.
  • the fuming process is to add a vulcanizing agent in the fuming furnace to fume and volatilize the tin in the slag of the top-blowing furnace; Add the vulcanizing agent within 90 to 120 minutes until the high-temperature melt in the fuming furnace contains tin ⁇ 0.3wt.%. Add vulcanizing agent to volatilize tin until the content of tin in the high temperature melt is ⁇ 0.3wt.%.
  • steps (2) to (3) can be repeated.
  • each embodiment in this specification is described in a progressive manner, each embodiment focuses on the difference from other embodiments, and the same and similar parts of each embodiment can be referred to each other.
  • the description is relatively simple, and for the related information, please refer to the description of the method part.

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Abstract

一种含锡物料熔炼系统，包括预处理机构、筛分机构、进料机构、熔炼机构、炉渣处理机构和尾气处理机构；本申请还公开了采用上述含锡物料熔炼系统进行熔炼的方法。本申请可以对含锡干物料进行筛分，使颗粒度较大的含锡物料可直接通过皮带输送入顶吹炉熔池熔炼，而颗粒度较细的含锡物料通过经顶吹喷枪喷入熔池，可减少颗粒度较细的含锡物料在转运过程中的泼洒或漏料损失，还可避免皮带炉顶投入顶吹炉造成的机械夹杂或飞扬损失；并且，避免细粒干物料在入炉前加入水分，从而降低冶炼能耗和冶炼烟气量，实现更绿色、环保、节能的冶炼。

Description

一种含锡物料熔炼的系统及方法 技术领域
本发明涉及锡精矿火法熔炼粗锡技术领域，更具体的说是涉及一种含锡物料熔炼的系统及方法。
背景技术
目前，含锡物料熔炼粗锡的生产过程中，所有含锡物料均通过皮带输送至炉顶，然后投入冶炼炉内进行还原熔炼生产粗锡。而且，水分低、颗粒度较细的含锡物料还需要加水制粒，使入炉的混合物料中水分含量达到10％～12％。而水分含量增加不仅会占用冶炼生产力、增加冶炼能源消耗，而且由于混合物料中水分经过高温后汽化，生成高温蒸汽大量进入到后续工艺烟气处理系统中，还会增加烟气处理系统的处理量和处理成本。
同时，由于各类含锡物料成分及性质较为复杂，通常需要进行脱硫脱砷等炼前预处理，产出各类含锡细粒干物料如沸腾炉焙烧产出的含锡细粒干物料、烟化炉产出的高含锡烟尘、其他冶炼炉产出的高含锡烟尘等。各类含锡细粒干物料需经气力管道输送或专用汽车转运至配料矿仓内，进行炉前配料，然后经皮带输送至冶炼炉内进行熔炼。其中，各类含锡细粒干物料的倒运过程，容易出现泼洒、漏料等损失。而且，颗粒度较细的含锡细粒干物料经皮带输送进冶炼炉过程中，在冶炼炉内下落距离超过10米，容易随炉膛烟气抽进尾气收尘器内，然后再由收尘器返回配料矿仓内进入下一次配料入炉流程，多次、反复的流程内倒运，又将进一步加速物料的损失，造成锡冶炼综合回收率低，同时还导致现场环境卫生差、损害操作人员身体等情况。
因此，针对以上各含锡细粒干物料在冶炼生产过程中存在的冶炼能耗增加、尾气处理系统负担增加、反复倒运造成金属损失以及烟尘飞扬所带来的金属损失和卫生环境差、锡冶炼综合回收率低等现象，提供一种新的含锡物料熔炼系统及方法是本领域技术人员亟需解决的问题。
发明内容
有鉴于此，本发明提供了一种含锡物料熔炼系统及方法，能够明显改善锡冶炼生产作业环境，提高含锡细粒干物料回收率，达到绿色节能的效果。
为了实现上述目的，本发明采用如下技术方案：
本发明提供了一种含锡物料熔炼系统，包括预处理机构、筛分机构、进料机构、熔炼机构、炉渣处理机构和尾气处理机构；
所述筛分机构包括筛分机、细物料仓和粗物料仓；
所述筛分机上游连接所述预处理机构的下游，所述筛分机的筛上物料出口连接所述粗物料仓，所述筛分机的筛下物料出口连接所述细物料仓，所述粗物料仓和所述细物料仓分别通过所述进料机构连接所述熔炼机构；
所述进料机构包括上料装置、配料仓、第一炉前料仓、第二炉前料仓、喷枪和粉煤仓；所述粗物料仓通过所述上料装置与所述配料仓连通，所述配料仓通过所述上料装置连通所述熔炼机构；所述第一炉前料仓上游连通所述细物料仓，下游通过所述喷枪连通所述熔炼机构；同时，所述第二炉前料仓上游分别连通所述炉渣处理机构和所述尾气处理机构，下游通过所述喷枪连通所述熔炼机构；并且，所述粉煤仓通过所述喷枪与所述熔炼机构连通。
进一步优选的，所述上料装置包括专用料车和皮带。
上述优选技术方案的有益效果是：本发明对含锡干物料进行筛分，使颗粒度较大的含锡物料可直接通过皮带输送入顶吹炉熔池熔炼，而颗粒度较细的含锡物料通过经顶吹喷枪喷入熔池，可减少颗粒度较细的含锡物料在转运过程中的泼洒或漏料损失，还可避免皮带炉顶投入顶吹炉造成的机械夹杂或飞扬损失。并且，避免细粒干物料在入炉前加入水分，从而降低冶炼能耗和冶炼烟气量，实现更绿色、环保、节能的冶炼。
优选的，所述预处理机构包括沸腾炉、冷却器和沸腾炉刮板机；
所述沸腾炉下游连接所述冷却器；
所述冷却器下游连接所述沸腾炉刮板机；
所述沸腾炉刮板机下游连接所述筛分机。
其中，冷却器是用于对沸腾炉焙烧含锡中间物料进行冷却处理
上述优选技术方案的有益效果是：本发明通过预处理机构可将高含硫含砷锡矿沸腾炉分类单独处理，为顶吹炉提供低硫低砷含锡物料，同时经沸腾炉焙烧后的物料通过气力输送至顶吹炉熔炼，密闭气力输送物料，可减少物料经皮带输送倒运过程中的飞扬或泼洒损失，为顶吹炉实现粉料喷吹创造有利条件，还有利于提高锡物料熔炼回收率。
优选的，所述进料机构还包括第一气力管道、第一下料管、第二气力管道、第二下料管、混料风管和金属软管；
所述第一气力管道连接所述细物料仓和所述第一炉前料仓，所述第一炉前料仓通过所述第一下料管连接所述混料风管；
所述第二气力管道上游分别连接所述炉渣处理机构和所述尾气处理机构，下游连接所述第二炉前料仓，所述第二炉前料仓通过所述第二下料管连接所述混料风管；
所述混料风管分别与所述第一下料管和所述第二下料管呈70～75°，所述混料风管通过所述金属软管与所述喷枪连接。
上述优选技术方案的有益效果是：混料风管与第一下料管和第二下料管之间按照最佳斜角设计，确保粉料充分混合、下料顺畅而不堵塞。
进一步优选的，所述熔炼机构包括顶吹炉、炉顶样杆、粗锡口、转锡包子和炉渣口；
所述顶吹炉的顶部与所述皮带的一端连接，同时与所述尾气处理机构连接；且所述喷枪穿过所述顶吹炉的顶面伸入所述顶吹炉内，同时所述炉顶样杆穿过所述顶吹炉的顶面伸入所述顶吹炉内；所述顶吹炉的底部通过所述粗锡口与所述转锡包子连接，同时所述顶吹炉的底部通过所述炉渣口连接所述炉渣处理机构。
上述优选技术方案的有益效果是：利用顶吹炉实现对含锡物料的高效熔炼回收粗锡，产出的顶吹炉炉渣送下一道工序进行回收处理。
优选的，所述炉渣处理机构包括炉渣溜槽、烟化炉、烟化炉余热锅炉、烟化炉表冷器、烟化炉布袋收尘器、烟化尘刮板机、烟化尘仓；所述烟化炉通过所述炉渣溜槽连接所述炉渣口，所述烟化炉的底部设置烟化炉排渣口，所述烟化炉的顶部连接所述烟化炉余热锅炉；所述烟化炉余热锅炉下游连接所述烟化炉表冷器；所述烟化炉下游连接所述烟化炉布袋收尘器；所述烟化刮尘机上游分别连接所述烟化炉余热锅炉、所述烟化炉表冷器和所述烟化炉布袋收尘器，下游连接所述烟化尘仓；所述烟化尘仓下游通过所述第二气力管道连接所述第二炉前料仓。
上述优选技术方案的有益效果是：实现对顶吹炉炉渣含锡的充分烟化回收，避免锡的损失。
优选的，所述尾气处理机构包括烟道、顶吹炉余热锅炉、测温装置、顶吹炉电收尘器、顶吹炉烟尘刮板机、顶吹炉烟尘仓；所述烟道的一端连接所述顶吹炉顶部，另一端连接所述顶吹炉余热锅炉，并且所述烟道连接所述顶吹炉顶部的一端安装所述测温装置；所述顶吹炉余热锅炉下游连接所述顶吹炉电收尘器；所述顶吹炉烟尘刮板机上游分别连接所述顶吹炉余热锅炉和所述顶吹炉电收尘器，下游连接所述顶吹炉烟尘仓；所述顶吹炉烟尘仓下游通过所述第二气力管道连接所述第二炉前料仓。
上述优选技术方案的有益效果是：实现对顶吹炉烟气中的含锡尾气的高效回收，减少含锡尾气进入后端制酸系统造成损失。
本发明还提供了一种含锡物料熔炼方法，利用上述系统，具体包括如下步骤：
(1)对各类锡矿进行分类，得到低含硫含砷锡矿经由专用料车输送至配料仓，得到高含硫含砷锡矿输送至沸腾炉进行预处理，得到含锡干物料；所述含锡干物料输送至 筛分机进行筛分，得到含锡细粒干物料经由喷枪喷入所述顶吹炉，得到含锡粗粒干物料经由专用料车输送至配料仓；
(2)在进料周期内将所述低含硫含砷锡矿和所述含锡粗粒干物料与石英砂和石灰石熔剂在配料仓内按照配比配料后经由皮带输入顶吹炉炉顶，同时按照配比控制经喷枪喷入顶吹炉的所述含锡细粒干物料量和回收含锡物料量，在顶吹炉内进行熔炼后得到混合熔体；然后停止进料，进入还原阶段，得到粗锡产品和顶吹炉炉渣；同时，根据测温装置测量的烟气温度以及CO尾气在线监测仪测定的尾气CO浓度变化，调整经皮带给块煤量和经喷枪给粉煤量；
(3)还原结束后停止经皮带给块煤和经喷枪给粉煤，并将喷枪提升至混合熔体的液面之上；然后打开粗锡口将所述粗锡产品输入转锡包子内；至出渣后，堵塞粗锡口、打开炉渣口将所述顶吹炉炉渣排放至烟化炉进行烟化处理，得到烟化尘；同时，顶吹炉冶炼产生的尾气经过尾气处理得到回收尾气；所述回收尾气和所述烟化尘分别经由第二气力管道输送至第二炉前料仓形成所述回收含锡物料；
(4)所述顶吹炉炉渣排放完毕后，可重复步骤(2)～(3)。
上述优选技术方案的有益效果是：本发明公开的一种含锡物料熔炼方法对含锡干物料进行分类和筛分处理，得到的低含硫含砷锡矿和含锡粗粒干物料可直接通过专用料车和皮带输送至顶吹炉内进行熔炼。而含锡细粒干物料、和回收含锡物料颗粒度较细通过全封闭气力管道输送，经喷枪喷入顶吹炉的熔池内，粒度较细物料在倒运过程中发生泼洒或漏料损失，还可避免通过皮带投入顶吹炉内造成机械夹杂或飞扬损失。
优选的，步骤(1)中所述低含硫含砷锡矿Sn>30wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<1.0wt.％、Fe在10～30wt.％，Bi在0.1～0.2wt.％；所述高含硫含砷锡矿Sn>30wt.％、Pb在0.2～3.0wt.％、S>2.0wt.％、As>2.0wt.％、Fe在10～30wt.％，Bi在0.1～0.5wt.％；
所述预处理是在650～720℃下焙烧2～2.5h，所述含锡干物料的水分＜1％，Sn>40wt.％、Pb在0.5～3.0wt.％，S<1.0wt.％，As<1.0wt.％，Fe在12～28wt.％，Bi在0.05～0.20wt.％；
所述筛分采用5目筛，所述含锡细粒干物料粒度5～300目，所述含锡粗粒干物料的粒度<5目、堆积密度在2～3g/cm 3。
优选的，步骤(2)中所述回收含锡物料中Sn在30～50wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<2.0wt.％、Fe在2～6wt.％、Bi在0.1～0.3wt.％，水分<5.0％，颗粒度为100～300目、堆积密度为0.5～1.0g/cm 3；
所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料和所述回收含锡物料在配料矿仓内按照配料原则经综合计算入炉混合物料配比，并通过配料仓的DCS给料系统准确控制经皮带输入所述低含硫含砷锡矿和所述含锡粗粒干物料的加入量，同时控制经喷枪输入顶吹炉的所述含锡细粒干物料和所述回收含锡物料的加入量；
所述配料原则为：Sn含量为38～48wt.％、Pb含量为1.0～5.0wt.％，S含量<1.0wt.％、Bi含量为0.1～0.2wt.％，As/Fe比为0.07～0.12，石英砂和石灰石熔剂按照硅酸度K＝1.2～1.4、熔点为1150～1320℃配入；
所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料以及所述回收含锡物料按照100wt.％计，分别为30～40wt.％、0～45wt.％、5～10wt.％、0～20wt.％；
所述熔炼过程中：喷枪的背压为20～30kPa，烟气温度为400～500℃，顶吹炉的炉膛负压为-10～0Pa，喷枪风富氧浓度为37～39wt.％，尾气CO浓度为0～500ppm，喷枪给粉煤量为5.0～5.5t/h，皮带给块煤量2.0～2.5t/h；
所述还原过程中，喷枪的背压为30～40kPa，烟气温度为500～550℃，顶吹炉的炉膛负压-10～0Pa，喷枪风富氧浓度33～36wt.％，尾气CO浓度在2000～5000ppm，喷枪给粉煤量为4.0～5.0t/h，皮带给块煤量为4.0～5.0t/h；
当尾气CO浓度＞5000ppm后持续升高至20000ppm还原过程终止。
优选的，先经皮带将所述低含硫含砷锡矿和所述含锡粗粒干物料输入顶吹炉使炉内熔池深度≥500mm，然后开始启动喷枪将所述含锡细粒干物料和所述回收含锡物料输入顶吹炉；
所述进料周期为：经皮带输送所述低含硫含砷锡矿和所述含锡粗粒干物料开始，熔池深度为1500～1800mm时终止。
上述优选技术方案的有益效果是：先通过皮带输入粗粒干物料入顶吹炉熔池内，待熔池深度达500mm后，再启动喷枪喷细粒干物料输入顶吹炉内，避免熔池深度不够启动喷枪喷料而导致细粒干物料在顶吹炉内飞扬而不落入熔池，避免影响冶炼综合回收指标提高。
优选的，所述熔池深度是通过炉顶样杆插入所述熔池内测量。
上述优选技术方案的有益效果是：实时使用炉顶样杆插入熔池监测熔池深度，确保冶炼工艺参数的控制为最佳。
优选的，步骤(3)中所述烟化过程为在烟化炉内加硫化剂使所述顶吹炉炉渣中的锡烟化挥发；所述硫化剂按照S/(Sn+Cu)摩尔比为1:3、过剩系数为1.2～1.3投加，所述硫化剂在90～120min内投加完，至烟化炉内高温熔体含锡≤0.3wt.％；取样化验分 析得烟化炉内高温熔体含锡＞0.3wt.％时，继续补加硫化剂挥发锡至高温熔体含锡≤0.3wt.％。
经由上述的技术方案可知，与现有技术相比，本发明公开提供了一种含锡物料熔炼系统及方法，具有如下有益效果：
(1)本发明对含锡干物料分类，将颗粒度较细的含锡物料通过全封闭气力管道输送，后经喷枪直接喷入熔池内，可减少在流程内倒运发生的泼洒或漏料损失，且还可避免皮带投入顶吹炉内造成机械夹杂或飞扬损失；
(2)对水分较干、颗粒度较细的含锡物料直接经喷枪喷入熔池，可省去加水制粒过程，避免在熔炼过程引入大量的水分，从而避免多余水分占用冶炼生产能力，从而降低冶炼能源消耗；同时避免引入的水变成高温蒸汽进入到后续工艺烟气处理系统，从而降低烟气处理系统的处理量和处理成本。
(3)颗粒度较大的含锡物料与颗粒度较细的含锡物料分别从顶吹炉炉顶皮带输送入炉、顶吹炉喷枪入炉，充分发挥了顶吹炉处理复杂物料的适应能力，实现绿色环保冶炼生产；
(4)颗粒度较细的含锡物料经全封闭气力管道输送，由喷枪喷入熔池还原熔炼，不再需要加水制粒，不仅物料的倒运损失少、物料输送顺畅、作业现场职业卫生良好，操作还简便，粗锡冶炼回收率高，还减少了含锡颗粒度较细的粉尘物料加水制粒能耗，降低了顶吹炉烟尘率，锡冶炼技术经济指标和生产效益得到进一步提高；
(5)避免因加水制粒带入冶炼烟气中水分，使烟气含水率降低10wt.％，从而减少制粒能耗，使制粒能耗占冶炼综合能耗百分比降低5％，并且顶吹炉烟尘率降低了5％，锡冶炼技术经济指标提高了2-3个百分点。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据提供的附图获得其他的附图。
图1附图为本发明实施例1提供的结构示意图。
在图中：1为顶吹炉、2为皮带、3为烟道、4为测温装置、5为炉顶样杆、6为喷枪、7为金属软管、8为第二炉前料仓、9为第一炉前料仓、10为粉煤仓、11为混料风管、12为沸腾炉、13为冷却器、14为沸腾炉刮板机、15为筛分机、16为细物料仓、17为粗物料仓、18为专用料车、19为第一气力管道、20为粗锡口、21为转锡包子、22为炉渣口、23为炉渣溜槽、24为烟化炉余热锅炉、25为顶吹炉电收尘器、26为顶 吹炉烟尘刮板机、27为顶吹炉烟尘仓、28为烟化炉、30为烟化炉表冷器、31为烟化炉布袋收尘器、32为烟化尘刮板机、33为烟化尘仓、34为烟化炉排渣口、35为第二气力管道、36第一下料管、37为第二下料管、38为配料仓。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
实施例1
本发明实施例公开了一种含锡物料熔炼系统，包括预处理机构、筛分机构、进料机构、熔炼机构、炉渣处理机构和尾气处理机构；
预处理机构下游连接筛分机构；
筛分机构包括筛分机、细物料仓和粗物料仓，筛分机上游连接预处理机构的下游，筛分机的筛上物料出口连接粗物料仓，筛分机的筛下物料出口连接细物料仓，粗物料仓和细物料仓通过进料机构连接熔炼机构；
进料机构包括上料装置、配料仓、第一炉前料仓、第二炉前料仓、喷枪和粉煤仓；其中上料装置包括专用料车和皮带
粗物料仓通过专用料车与配料仓连通，配料仓通过皮带连通熔炼机构；第一炉前料仓上游连通细物料仓，下游通过喷枪连通熔炼机构；同时，第二炉前料仓上游分别连通炉渣处理机构和尾气处理机构，下游通过喷枪连通熔炼机构；并且，粉煤仓通过喷枪与熔炼机构连通。
预处理机构包括沸腾炉、冷却器和沸腾炉刮板机；沸腾炉下游连接冷却器；冷却器下游连接沸腾炉刮板机；沸腾炉刮板机下游连接筛分机。
进料机构还包括第一气力管道、第一下料管、第二气力管道、第二下料管、混料风管和金属软管；第一气力管道连接细物料仓和第一炉前料仓，第一炉前料仓通过第一下料管连接混料风管；第二气力管道上游分别连接炉渣处理机构和尾气处理机构，下游连接第二炉前料仓，第二炉前料仓通过第二下料管连接混料风管；混料风管分别与第一下料管和第二下料管呈75°，混料风管通过金属软管与喷枪连接。
熔炼机构包括顶吹炉、炉顶样杆、粗锡口、转锡包子和炉渣口；顶吹炉的顶部与皮带连接，同时与尾气处理机构连接；且喷枪穿过顶吹炉的顶面伸入顶吹炉内，同时炉顶样杆穿过顶吹炉的顶面伸入顶吹炉内；顶吹炉的底部通过粗锡口与转锡包子连接，同时顶吹炉的底部通过炉渣口连接炉渣处理机构。
炉渣处理机构包括炉渣溜槽、烟化炉、烟化炉余热锅炉、烟化炉表冷器、烟化炉布袋收尘器、烟化尘刮板机、烟化尘仓；烟化炉通过炉渣溜槽连接炉渣口，烟化炉的底部设置烟化炉排渣口，烟化炉的顶部连接烟化炉余热锅炉；烟化炉余热锅炉下游连接烟化炉表冷器；烟化炉下游连接烟化炉布袋收尘器；烟化刮尘机上游分别连接烟花路预热锅、烟化炉表冷器和烟化炉布袋收尘器，下游连接烟化尘仓；烟化尘仓下游通过第二气力管道连接第二炉前料仓。
尾气处理机构包括烟道、顶吹炉余热锅炉、测温装置、顶吹炉电收尘器、顶吹炉烟尘刮板机、顶吹炉烟尘仓；烟道的一端连接顶吹炉顶部，另一端连接顶吹炉余热锅炉，并且烟道连接顶吹炉顶部的一端安装测温装置；顶吹炉余热锅炉下游连接顶吹炉电收尘器；顶吹炉烟尘刮板机上游分别连接顶吹炉余热锅炉和顶吹炉电收尘器，下游连接顶吹炉烟尘仓；顶吹炉烟尘仓下游通过第二气力管道连接第二炉前料仓。
实施例2
本发明实施例2公开了一种含锡物料熔炼方法，利用实施例1公开的系统，具体包括如下步骤：
(1)对各类锡矿进行分类，得到低含硫含砷锡矿经由专用料车输送至配料仓，得到高含硫含砷锡矿输送至沸腾炉进行预处理，得到含锡干物料；所述含锡干物料输送至筛分机进行筛分，得到含锡细粒干物料经由喷枪喷入所述顶吹炉，得到含锡粗粒干物料经由专用料车输送至配料仓；
其中，低含硫含砷锡矿Sn>30wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<1.0wt.％、Fe在10～30wt.％，Bi在0.1～0.2wt.％；高含硫含砷锡矿Sn>30wt.％、Pb在0.2～3.0wt.％、S>2.0wt.％、As>2.0wt.％、Fe在10～30wt.％，Bi在0.1～0.5wt.％；
预处理在650～720℃下焙烧2～2.5h，含锡干物料的水分＜1％，Sn>40wt.％、Pb在0.5～3.0wt.％，S<1.0wt.％，As<1.0wt.％，Fe在12～28wt.％，Bi在0.05～0.20wt.％；
筛分采用5目筛，含锡细粒干物料粒度5～300目，含锡粗粒干物料的粒度<5目、堆积密度在2～3g/cm 3
(2)在进料周期内将所述低含硫含砷锡矿和所述含锡粗粒干物料与石英砂和石灰石熔剂在配料仓内按照配比配料后经由皮带输入顶吹炉炉顶，同时按照配比控制经喷枪喷入顶吹炉的所述含锡细粒干物料量和回收含锡物料量，在顶吹炉内进行熔炼后得到混合熔体；然后停止进料，进入还原阶段，得到粗锡产品和顶吹炉炉渣；同时，根据 测温装置测量的烟气温度以及CO尾气在线监测仪测定的尾气CO浓度变化，调整经皮带给块煤量和经喷枪给粉煤量；
其中，回收含锡物料中Sn在30～50wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<2.0wt.％、Fe在2～6wt.％、Bi在0.1～0.3wt.％，水分<5.0％，颗粒度为100～300目、堆积密度为0.5～1.0g/cm 3；
所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料和所述回收含锡物料在配料矿仓内按照配料原则经综合计算入炉混合物料配比，并通过配料仓的DCS给料系统准确控制经皮带输入所述低含硫含砷锡矿和所述含锡粗粒干物料的加入量，同时控制经喷枪输入顶吹炉的所述含锡细粒干物料和所述回收含锡物料的加入量；
配料原则为：Sn含量为38～48wt.％、Pb含量为1.0～5.0wt.％，S含量<1.0wt.％、Bi含量为0.1～0.2wt.％，As/Fe比为0.07～0.12，石英砂和石灰石熔剂按照硅酸度K＝1.2～1.4、熔点为1150～1320℃配入；
低含硫含砷锡矿、含锡细粒干物料、含锡粗粒干物料以及回收含锡物料按照100wt.％计，分别为30～40wt.％、0～45wt.％、5～10wt.％、0～20wt.％；
先经喷枪将含锡细粒干物料和回收含锡物料输入顶吹炉使炉内熔池深度≥500mm，然后开始经皮带将低含硫含砷锡矿和含锡粗粒干物料输入顶吹炉；进料周期为：经皮带输送低含硫含砷锡矿和含锡粗粒干物料开始，熔池深度为1500～1800mm时终止；且熔池深度是通过炉顶样杆插入熔池内测量
熔炼过程中：喷枪的背压为20～30kPa，烟气温度为400～500℃，顶吹炉的炉膛负压为-10～0Pa，喷枪风富氧浓度为37～39wt.％，尾气CO浓度为0～500ppm，喷枪给粉煤量为5.0～5.5t/h，皮带给块煤量2.0～2.5t/h；
还原过程中，喷枪的背压为30～40kPa，烟气温度为500～550℃，顶吹炉的炉膛负压-10～0Pa，喷枪风富氧浓度33～36wt.％，尾气CO浓度在2000～5000ppm，喷枪给粉煤量为4.0～5.0t/h，皮带给块煤量为4.0～5.0t/h；
当尾气CO浓度＞5000ppm后持续升高至20000ppm还原过程终止。
(3)还原结束后停止经皮带给块煤和经喷枪给粉煤，并将喷枪提升至混合熔体的液面之上；然后打开粗锡口将粗锡产品输入转锡包子内；至出渣后，堵塞粗锡口、打开炉渣口将顶吹炉炉渣排放至烟化炉进行烟化处理，得到烟化尘；同时，顶吹炉冶炼产生的尾气经过尾气处理得到回收尾气；回收尾气和烟化尘分别经由第二气力管道输送至第二炉前料仓形成回收含锡物料；
其中，烟化过程为在烟化炉内加硫化剂使顶吹炉炉渣中的锡烟化挥发；硫化剂按照S/(Sn+Cu)摩尔比为1:3、过剩系数为1.2～1.3投加，硫化剂在90～120min内投加 完，至烟化炉内高温熔体含锡≤0.3wt.％；取样化验分析得烟化炉内高温熔体含锡＞0.3wt.％时，继续补加硫化剂挥发锡至高温熔体含锡≤0.3wt.％；
(:4)顶吹炉炉渣排放完毕后，可重复步骤(2)～(3)。
实施例3
本发明实施例3公开了一种含锡物料熔炼方法，利用实施例1公开的系统，具体包括如下步骤：
(1)首先应对含锡物料进行分类处理：将Sn>30wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<1.0wt.％、Fe在10～30wt.％、Bi在0.1～0.2wt.％的低含硫含砷锡矿经由专用料车输送至配料仓；将含Sn30wt.％、Pb在0.2wt.％、S在2.0wt.％、As在2.0wt.％、Fe在10wt.％、Bi在0.1wt.％高含硫含砷锡矿加入沸腾炉在650～720℃下焙烧2～2.5h，进行脱硫脱砷，产出含Sn在40wt.％、Pb在0.5wt.％、S在0.8wt.％、As在0.80wt.％、Fe在12wt.％、Bi在0.05wt.％、水分小于1wt.％的含锡干物料；使用筛分机将含锡干物料进行筛分，过5目筛下物料为含锡细粒干物料，筛上物料为含锡粗粒干物料；
其中，含锡细粒干物料粒度为15目，含锡粗粒干物料的颗粒度为4目、堆积密度为2g/cm 3，含锡细粒干物料经第一气力管道输送至第一炉前料仓内储存，含锡粗粒干物料经专用料车转运至配料仓，经矿仓综合配料后，由皮带输送至入顶吹炉内。
(2)按照配料原则综合计算所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料和所述回收含锡的物料配比，在配料矿仓内通过配料仓的DCS给料系统准确控制经皮带输入顶吹炉炉顶的所述低含硫含砷锡矿和所述含锡粗粒干物料的加入量，同时控制经喷枪输入顶吹炉的所述含锡细粒干物料和所述回收含锡物料的加入量；低含硫含砷锡矿、含锡细粒干物料、含锡粗粒干物料以及回收含锡物料的配料比例分别是40wt.％、30wt.％、10wt.％、20wt.％，综合计算入炉混合物料中：Sn 38wt.％、含Pb 1.0wt.％、S1.0wt.％，As/Fe比控制在0.07，Bi 0.1wt.％；石英砂和石灰石熔剂的配入按照硅酸度K＝1.4，熔点为1150℃。
其中，低含硫含砷锡矿组成为：Sn 35wt.％、Pb 0.2wt.％、S 1.0wt.％、As<1.0wt.％、Fe 10wt.％、Bi 0.1wt.％。
回收含锡物料是由烟化尘和回收尾气组成，均直接经第二气力管道输送至第二炉前料仓内储存。烟化尘颗粒度为100目、堆积密度为0.5g/cm 3，水分小于5wt.％，组成为：含Sn 45wt.％、Pb 0.2wt.％、S 0.9wt.％、As 1.5wt.％、Fe 2wt.％、Bi 0.1wt.％；回收尾气颗粒度为150目、堆积密度为0.6g/cm 3，水分小于5wt.％，组 成为：Sn 38wt.％、Pb1.0wt.％、S 0.75wt.％、As 1.8wt.％、Fe 3wt.％、Bi 0.1wt.％。
含锡细粒干物料和回收含锡物料由炉前料仓下料管与共用炉前混料风管，经金属软管与喷枪联结，混料风管风压应低于各炉前料仓下料管风压的5～10％，各炉前料仓下料管与混料风管呈70～75度切线夹角联结。
含锡细粒干物料和回收含锡物料经顶吹炉喷枪入熔池熔炼的时间控制，需顶吹炉内熔池深度达500mm后开始启动至一个完整的进料周期结束后停止给料，调整炉顶皮带输送的低含硫含砷锡矿配入量和含锡粗粒干物料配入量；熔池深度是通过顶吹炉炉顶样杆，插入熔池内来探测。
其中进料周期是，顶吹炉炉顶进料皮带开始进料，至熔池高度达1500mm止，进料周期时间内，完成熔炼过程，之后进入熔炼高温混合熔体的还原阶段。
熔炼过程控制，喷枪背压控制在20～30kPa，顶吹炉烟气测温温度控制在420℃，炉膛负压-10～0Pa，喷枪风富氧浓度37～39wt.％，尾气CO浓度在0～500ppm，喷枪给粉煤5.0～5.5t/h，皮带给块煤2.0～2.5t/h。
还原过程控制，喷枪背压控制在30～40kPa，顶吹炉烟气测温温度控制在500～550℃，炉膛负压-10～0Pa，喷枪风富氧浓度33～36wt.％，尾气CO浓度在2000～5000ppm，喷枪给粉煤4.0～5.0t/h，顶吹炉经皮带给块煤量为4.0～5.0t/h。
(3)当尾气CO浓度自高于5000ppm后持续升高至20000ppm，还原结束，停止经皮带给块煤和经喷枪给粉煤，并将喷枪提升至混合熔体的液面之上；然后打开粗锡口将粗锡产品输入转锡包子内；至出渣后，堵塞粗锡口、打开炉渣口将顶吹炉炉渣排放至烟化炉进行烟化处理，得到烟化尘；同时，顶吹炉冶炼产生的尾气经过尾气处理得到回收尾气；回收尾气和烟化尘分别经由第二气力管道输送至第二炉前料仓形成回收含锡物料；
其中，烟化过程为在烟化炉内加硫化剂使顶吹炉炉渣中的锡烟化挥发；硫化剂按照S/(Sn+Cu)摩尔比为1:3、过剩系数为1.2～1.3投加，硫化剂在90～120min内投加完，至烟化炉内高温熔体含锡≤0.3wt.％；取样化验分析得烟化炉内高温熔体含锡＞0.3wt.％时，继续补加硫化剂挥发锡至高温熔体含锡≤0.3wt.％；
(4)顶吹炉炉渣排放完毕后，可重复步骤(2)～(3)。
实施例4
本发明实施例4公开了一种含锡物料熔炼方法，利用实施例1公开的系统，具体包括如下步骤：
(1)首先应对含锡物料进行分类处理：将Sn>30wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<1.0wt.％、Fe在10～30wt.％、Bi在0.1～0.2wt.％的低含硫含砷锡矿经由专用料车输送至配料仓；将含Sn 35wt.％、Pb 2.0wt.％、S 3.0wt.％、As 2.5wt.％、Fe15wt.％、Bi 0.2wt.％的高含硫含砷锡矿进行沸腾炉在650-720℃，焙烧时间2-2.5h，进行脱硫脱砷，产出含锡干物料含Sn 45wt.％、Pb 1.5wt.％、S 0.7wt.％、As 0.5wt.％、Fe18wt.％、Bi 0.08wt.％、水分小于1％，使用筛分机将含锡干物料筛分，过5目筛下物料为含锡细粒干物料，筛上物料为含锡粗粒干物料。
其中，含锡细粒干物料颗粒度300目，含锡粗粒干物料颗粒度4目，堆积密度为2.5g/cm 3，含锡细粒干物料经第一气力管道输送至第一炉前料仓内储存，含锡粗粒干物料经专用料车转运至配料矿仓，经矿仓综合配料后，由皮带输送至入顶吹炉内。
(2)按照配料原则综合计算所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料和所述回收含锡的物料配比，在配料矿仓内通过配料仓的DCS给料系统准确控制经皮带输入顶吹炉炉顶的所述低含硫含砷锡矿和所述含锡粗粒干物料的加入量，同时控制经喷枪输入顶吹炉的所述含锡细粒干物料和所述回收含锡物料的加入量；低含硫含砷锡矿、含锡细粒干物料、含锡粗粒干物料以及回收含锡物料配料比例分别是35wt.％、45wt.％、10wt.％、10wt.％，综合计算入炉混合物料中：Sn48wt.％、Pb5.0wt.％、S0.9wt.％、As/Fe比为0.12、Bi 0.2wt.％；石英砂和石灰石熔剂的配入按照硅酸度K＝1.2，熔点为1320℃。
其中，低含硫含砷锡矿组成为：Sn 50wt.％、Pb 3.0wt.％、S<1.0wt.％、As0.3wt.％、Fe 30wt.％、Bi 0.2wt.％。
回收含锡物料是由烟化尘和回收尾气组成，均直接经第二气力管道输送至第二炉前料仓内储存。烟化尘颗粒度为200目、堆积密度为0.8g/cm 3组成为：Sn 45wt.％、Pb0.3wt.％、S 0.50wt.％、As 1.2wt.％、Fe 3wt.％、Bi 0.12wt.％。回收尾气颗粒度为300目、堆积密度为1.0g/cm 3，组成为：Sn 42wt.％、Pb1.5wt.％、S 0.5wt.％、As 1.8wt.％、Fe6wt.％、Bi 0.3wt.％、水分小于5wt.％。
含锡细粒干物料和回收含锡物料由炉前料仓下料管与共用炉前混料风管，经金属软管与喷枪联结，混料风管风压应低于各炉前料仓下料管风压的5～10％，各炉前料仓下料管与混料风管呈70～75度切线夹角联结。
含锡细粒干物料和回收含锡物料经顶吹炉喷枪入熔池熔炼的时间控制，需顶吹炉内熔池深度达500mm后开始启动至一个完整的进料周期结束后停止给料，调整炉顶皮带输送的低含硫含砷锡矿配入量和含锡粗粒干物料配入量；熔池深度是通过顶吹炉炉顶样杆，插入熔池内来探测。
其中进料周期是，顶吹炉炉顶进料皮带开始进料，至熔池高度达1500mm止，进料周期时间内，完成熔炼过程，之后进入熔炼高温混合熔体的还原阶段。
含锡物料的熔池熔炼过程控制，喷枪背压控制在20～30kPa，顶吹炉烟气测温温度控制在500℃，炉膛负压-10～0Pa，喷枪风富氧浓度37～39wt.％，尾气CO浓度在0～500ppm，喷枪给粉煤5.0～5.5t/h，顶吹炉炉顶皮带给块煤2.0～2.5t/h。
熔炼高温混合熔体的还原过程控制，喷枪背压控制在30～40kPa，顶吹炉烟气测温温度控制在500～550℃，炉膛负压-10～0Pa，喷枪风富氧浓度33～36wt.％，尾气CO浓度在2000～5000ppm，喷枪给粉煤4.0～5.0t/h，顶吹炉炉顶皮带给块煤4.0～5.0t/h。
(3)当尾气CO浓度自高于5000ppm后持续升高至20000ppm，还原结束，停止经皮带给块煤和经喷枪给粉煤，并将喷枪提升至混合熔体的液面之上；然后打开粗锡口将粗锡产品输入转锡包子内；至出渣后，堵塞粗锡口、打开炉渣口将顶吹炉炉渣排放至烟化炉进行烟化处理，得到烟化尘；同时，顶吹炉冶炼产生的尾气经过尾气处理得到回收尾气；回收尾气和烟化尘分别经由第二气力管道输送至第二炉前料仓形成回收含锡物料；
其中，烟化过程为在烟化炉内加硫化剂使顶吹炉炉渣中的锡烟化挥发；硫化剂按照S/(Sn+Cu)摩尔比为1:3、过剩系数为1.2～1.3投加，硫化剂在90～120min内投加完，至烟化炉内高温熔体含锡≤0.3wt.％；取样化验分析得烟化炉内高温熔体含锡＞0.3wt.％时，继续补加硫化剂挥发锡至高温熔体含锡≤0.3wt.％；
(4)顶吹炉炉渣排放完毕后，可重复步骤(2)～(3)。
本说明书中各个实施例采用递进的方式描述，每个实施例重点说明的都是与其他实施例的不同之处，各个实施例之间相同相似部分互相参见即可。对于实施例公开的装置而言，由于其与实施例公开的方法相对应，所以描述的比较简单，相关之处参见方法部分说明即可。
对所公开的实施例的上述说明，使本领域专业技术人员能够实现或使用本发明。对这些实施例的多种修改对本领域的专业技术人员来说将是显而易见的，本文中所定义的一般原理可以在不脱离本发明的精神或范围的情况下，在其它实施例中实现。因此，本发明将不会被限制于本文所示的这些实施例，而是要符合与本文所公开的原理和新颖特点相一致的最宽的范围。

Claims (10)

  1. 一种含锡物料熔炼系统，其特征在于，包括预处理机构、筛分机构、进料机构、熔炼机构、炉渣处理机构和尾气处理机构；
    所述筛分机构包括筛分机、细物料仓和粗物料仓；
    所述筛分机上游连接所述预处理机构的下游，所述筛分机的筛上物料出口连接所述粗物料仓，所述筛分机的筛下物料出口连接所述细物料仓，所述粗物料仓和所述细物料仓分别通过所述进料机构连接所述熔炼机构；
    所述进料机构包括上料装置、配料仓、第一炉前料仓、第二炉前料仓、喷枪和粉煤仓；所述粗物料仓通过所述上料装置与所述配料仓连通，所述配料仓通过所述上料装置连通所述熔炼机构；所述第一炉前料仓上游连通所述细物料仓，下游通过所述喷枪连通所述熔炼机构；同时，所述第二炉前料仓上游分别连通所述炉渣处理机构和所述尾气处理机构，下游通过所述喷枪连通所述熔炼机构；并且，所述粉煤仓通过所述喷枪与所述熔炼机构连通。
  2. 根据权利要求1所述一种含锡物料熔炼系统，其特征在于，所述预处理机构包括沸腾炉、冷却器和沸腾炉刮板机；
    所述沸腾炉下游连接所述冷却器；
    所述冷却器下游连接所述沸腾炉刮板机；
    所述沸腾炉刮板机下游连接所述筛分机。
  3. 根据权利要求2所述的一种含锡物料熔炼系统，其特征在于，所述进料机构还包括第一气力管道、第一下料管、第二气力管道、第二下料管、混料风管和金属软管；
    所述第一气力管道连接所述细物料仓和所述第一炉前料仓，所述第一炉前料仓通过所述第一下料管连接所述混料风管；
    所述第二气力管道上游分别连接所述炉渣处理机构和所述尾气处理机构，下游连接所述第二炉前料仓，所述第二炉前料仓通过所述第二下料管连接所述混料风管；
    所述混料风管分别与所述第一下料管和所述第二下料管呈70～75°，所述混料风管通过所述金属软管与所述喷枪连接。
  4. 根据权利要求3所述的一种含锡物料熔炼系统，其特征在于，所述熔炼机构包括顶吹炉、炉顶样杆、粗锡口、转锡包子和炉渣口；
    所述顶吹炉的顶部与所述上料装置连通，同时与所述尾气处理机构连接；且所述喷枪穿过所述顶吹炉的顶面伸入所述顶吹炉内，同时所述炉顶样杆穿过所述顶吹炉的 顶面伸入所述顶吹炉内；所述顶吹炉的底部通过所述粗锡口与所述转锡包子连接，同时所述顶吹炉的底部通过所述炉渣口连接所述炉渣处理机构。
  5. 根据权利要求4所述的一种含锡物料熔炼系统，其特征在于，所述炉渣处理机构包括炉渣溜槽、烟化炉、烟化炉余热锅炉、烟化炉表冷器、烟化炉布袋收尘器、烟化尘刮板机、烟化尘仓；
    所述烟化炉通过所述炉渣溜槽连接所述炉渣口，所述烟化炉的底部设置烟化炉排渣口，所述烟化炉的顶部连接所述烟化炉余热锅炉；
    所述烟化炉余热锅炉下游连接所述烟化炉表冷器；所述烟化炉下游连接所述烟化炉布袋收尘器；
    所述烟化刮尘机上游分别连接所述烟花路预热锅、所述烟化炉表冷器和所述烟化炉布袋收尘器，下游连接所述烟化尘仓；
    所述烟化尘仓下游通过所述第二气力管道连接所述第二炉前料仓。
  6. 根据权利要求5所述的一种含锡物料熔炼系统，其特征在于，所述尾气处理机构包括烟道、顶吹炉余热锅炉、测温装置、顶吹炉电收尘器、顶吹炉烟尘刮板机、顶吹炉烟尘仓；
    所述烟道的一端连接所述顶吹炉顶部，另一端连接所述顶吹炉余热锅炉，并且所述烟道连接所述顶吹炉顶部的一端安装所述测温装置；
    所述顶吹炉余热锅炉下游连接所述顶吹炉电收尘器；
    所述顶吹炉烟尘刮板机上游分别连接所述顶吹炉余热锅炉和所述顶吹炉电收尘器，下游连接所述顶吹炉烟尘仓；
    所述顶吹炉烟尘仓下游通过所述第二气力管道连接所述第二炉前料仓。
  7. 一种含锡物料熔炼方法，其特征在于，利用权利要求 6任一项所述系统，具体包括如下步骤：
    (1)对各类锡矿进行分类，得到低含硫含砷锡矿经由专用料车输送至配料仓，得到高含硫含砷锡矿输送至沸腾炉进行预处理，得到含锡干物料；所述含锡干物料输送至筛分机进行筛分，得到含锡细粒干物料经由喷枪喷入所述顶吹炉，得到含锡粗粒干物料经由专用料车输送至配料仓；
    (2)在进料周期内将所述低含硫含砷锡矿和所述含锡粗粒干物料与石英砂和石灰石熔剂在配料仓内按照配比配料后经由皮带输入顶吹炉炉顶，同时按照配比控制经喷枪喷入顶吹炉的所述含锡细粒干物料量和回收含锡物料量，在顶吹炉内进行熔炼后得到混合熔体；然后停止进料，进入还原阶段，得到粗锡产品和顶吹炉炉渣；同时，根据 测温装置测量的烟气温度以及CO尾气在线监测仪测定的尾气CO浓度变化，调整经皮带给块煤量和经喷枪给粉煤量；
    (3)还原结束后停止经皮带给块煤和经喷枪给粉煤，并将喷枪提升至混合熔体的液面之上；然后打开粗锡口将所述粗锡产品输入转锡包子内；至出渣后，堵塞粗锡口、打开炉渣口将所述顶吹炉炉渣排放至烟化炉进行烟化处理，得到烟化尘；同时，顶吹炉冶炼产生的尾气经过尾气处理得到回收尾气；所述回收尾气和所述烟化尘分别经由第二气力管道输送至第二炉前料仓形成所述回收含锡物料；
    (4)所述顶吹炉炉渣排放完毕后，可重复步骤(2)～(3)。
  8. 根据权利要求7所述的一种含锡物料熔炼方法，其特征在于，步骤(1)中所述低含硫含砷锡矿Sn>30wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<1.0wt.％、Fe在10～30wt.％，Bi在0.1～0.2wt.％；所述高含硫含砷锡矿Sn>30wt.％、Pb在0.2～3.0wt.％、S>2.0wt.％、As>2.0wt.％、Fe在10～30wt.％，Bi在0.1～0.5wt.％；
    所述预处理是在650～720℃下焙烧2～2.5h，所述含锡干物料的水分＜1％，Sn>40wt.％、Pb在0.5～3.0wt.％，S<1.0wt.％，As<1.0wt.％，Fe在12～28wt.％，Bi在0.05～0.20wt.％；
    所述筛分采用5目筛，所述含锡细粒干物料粒度5～300目，所述含锡粗粒干物料的粒度<5目、堆积密度在2～3g/cm 3。
  9. 根据权利要求7所述的一种含锡物料熔炼方法，其特征在于，步骤(2)中所述回收含锡物料中Sn在30～50wt.％、Pb在0.2～3.0wt.％、S<1.0wt.％、As<2.0wt.％、Fe在2～6wt.％、Bi在0.1～0.3wt.％，水分<5.0％，颗粒度为100～300目、堆积密度为0.5～1.0g/cm 3；
    所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料和所述回收含锡物料在配料矿仓内按照配料原则经综合计算入炉混合物料配比，并通过配料仓的DCS给料系统准确控制经皮带输入所述低含硫含砷锡矿和所述含锡粗粒干物料的加入量，同时控制经喷枪输入顶吹炉的所述含锡细粒干物料和所述回收含锡物料的加入量；
    所述配料原则为：Sn含量为38～48wt.％、Pb含量为1.0～5.0wt.％，S含量<1.0wt.％、Bi含量为0.1～0.2wt.％，As/Fe比为0.07～0.12，石英砂和石灰石熔剂按照硅酸度K＝1.2～1.4、熔点为1150～1320℃配入；
    所述低含硫含砷锡矿、所述含锡细粒干物料、所述含锡粗粒干物料以及所述回收含锡物料按照100wt.％计，分别为30～40wt.％、0～45wt.％、5～10wt.％、0～20wt.％；
    所述熔炼过程中：喷枪的背压为20～30kPa，烟气温度为400～500℃，顶吹炉的炉膛负压为-10～0Pa，喷枪风富氧浓度为37～39wt.％，尾气CO浓度为0～500ppm，喷枪给粉煤量为5.0～5.5t/h，皮带给块煤量2.0～2.5t/h；
    所述还原过程中，喷枪的背压为30～40kPa，烟气温度为500～550℃，顶吹炉的炉膛负压-10～0Pa，喷枪风富氧浓度33～36wt.％，尾气CO浓度在2000～5000ppm，喷枪给粉煤量为4.0～5.0t/h，皮带给块煤量为4.0～5.0t/h；
    当尾气CO浓度＞5000ppm后持续升高至20000ppm还原过程终止。
  10. 根据权利要求9所述的一种含锡物料熔炼方法，其特征在于，步骤(2)中先经皮带将所述低含硫含砷锡矿和所述含锡粗粒干物料输入顶吹炉使炉内熔池深度≥500mm，然后开始启动喷枪将所述含锡细粒干物料和所述回收含锡物料输入顶吹炉；
    所述进料周期为：经皮带输送所述低含硫含砷锡矿和所述含锡粗粒干物料开始，熔池深度为1500～1800mm时终止。
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