WO2012065327A1 - 连续炼铅装置及连续炼铅工艺 - Google Patents
连续炼铅装置及连续炼铅工艺 Download PDFInfo
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- WO2012065327A1 WO2012065327A1 PCT/CN2010/079731 CN2010079731W WO2012065327A1 WO 2012065327 A1 WO2012065327 A1 WO 2012065327A1 CN 2010079731 W CN2010079731 W CN 2010079731W WO 2012065327 A1 WO2012065327 A1 WO 2012065327A1
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- zone
- reduction zone
- lead
- oxidation
- reduction
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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
- C22B13/00—Obtaining lead
- C22B13/02—Obtaining lead by dry processes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B3/00—Hearth-type furnaces, e.g. of reverberatory type; Tank furnaces
- F27B3/04—Hearth-type furnaces, e.g. of reverberatory type; Tank furnaces of multiple-hearth type; of multiple-chamber type; Combinations of hearth-type furnaces
- F27B3/045—Multiple chambers, e.g. one of which is used for charging
Definitions
- the present invention relates to a lead smelting apparatus and process, and more particularly to a continuous lead smelting apparatus and a continuous lead smelting process. Background technique
- the lead-smelting processes that have been used in industrial production at home and abroad mainly include QSL method, SKS method, Kivcet method, top-blown immersion melting pool smelting technology (mainly Ausmel t method, ISA method and Caldo method). .
- the Caldo smelting lead method is difficult to promote and apply due to its short life, low operating rate and high cost.
- SKS method, ISA-blast furnace reduction lead-smelting method is a method of redox smelting in two separate furnaces.
- Ausmel t method is a method of redoxing in a single furnace
- QSL method and Kivcet method are The redox process is realized in a sub-area in a single furnace.
- the Ausmel t method has a high smoke rate and a complicated gas-liquid and ionic liquid absorption gas distribution system.
- the Kivcet method requires a strict material preparation process. The flux needs a grinding system. The water content of the raw material needs to be dried to less than 0.5%. The coke also needs to be dry, the preparation is complicated, the energy consumption is high, the slag contains lead, and the investment cost is high. SKS method, ISA - blast furnace reduction Lead smelting method, blast furnace needs to consume expensive metallurgical coke, high energy consumption, long process, high smoke rate and other shortcomings.
- the QSL method realizes a redox process in a reaction vessel, and thus is widely used.
- the QSL method has a soot rate of 25-30%, and the crude lead portion which has been reduced is repeatedly oxidized and reduced due to the bottom blowing.
- the lead in the final slag is difficult to control, the final slag index is not ideal, and the energy consumption is high.
- the reaction vessel needs to be rotated and replaced, the cost is high. Summary of the invention
- the present invention aims to solve at least one of the technical problems existing in the prior art.
- Another object of the present invention is to provide a continuous lead smelting process which completes the oxidation and reduction process of lead smelting in a reaction furnace, that is, one-step lead smelting, so that the process is short and environmentally friendly.
- a continuous lead smelting apparatus comprising: a reaction furnace, wherein a partition wall is disposed in the reaction furnace to divide a furnace chamber of the reaction furnace into an oxidation zone and a reduction zone, the furnace The lower part of the cavity constitutes a molten pool, and the bottom of the partition wall is provided with a communication passage connecting the oxidation zone and the reduction zone, and the top wall of the oxidation zone is respectively provided with an oxidation zone feeding port and an oxidation zone outlet port.
- the top wall of the reduction zone is provided with a reducing agent inlet port and a reduction zone outlet port, and a siphon discharge lead port and a slag discharge port are arranged on the furnace wall of the furnace chamber; an oxidation zone side blowing spray gun, the oxidation zone side a blowing gun is connected to the side wall of the oxidation zone of the reaction furnace to blow the oxygen side into the molten pool of the oxidation zone; and a reduction zone side blowing spray gun, the reduction zone side blowing spray gun and the reduction zone side of the reaction furnace The walls are connected to blow the fuel and oxygen sides into the molten pool of the reduction zone.
- oxidation and reduction can be achieved in a single reaction furnace, and since the side blowing is performed, the fuel and oxygen blown to the inside of the reduction zone do not pass through the crude lead which has been reduced, and therefore The crude lead is repeatedly oxidized, and the lead content in the slag is lowered and stabilized. Moreover, the oxidation zone and the reduction zone are separated, and only communicate through the communication channel at the bottom of the partition wall, and the communication channel is immersed in the melt during operation, so the oxidation zone and the upper part of the reduction zone are isolated, and the smoke in the oxidation zone and the reduction zone is not Will be mixed and can be processed separately. Since continuous lead smelting is realized in a single closed reaction furnace, the sealing performance is good, the environmental protection is high, the enthalpy of the slag is fully utilized, and the energy consumption is reduced.
- the continuous lead smelting apparatus may have the following additional technical features.
- An oxidation zone spray gun port is disposed on the sidewall of the oxidation zone, and a reduction zone spray gun port is disposed on the sidewall of the reduction zone, wherein the oxidation zone side spray gun is connected to the oxidation zone spray gun port and the reduction zone side A blow gun is coupled to the spray port of the reduction zone.
- the siphon discharge lead is disposed on a side wall of the reaction furnace adjacent to the partition wall, and the slag discharge port is disposed on an end wall of the reduction zone of the reaction furnace.
- a sedimentation zone is provided on a bottom wall of the furnace chamber adjacent to the siphon discharge port.
- the bottom wall of the furnace chamber is concavely curved.
- the upper part of the side wall of the reduction zone of the reaction furnace is provided with a secondary air outlet.
- a furnace wall cooling device is disposed in the side wall of the reaction furnace adjacent to the slag line.
- the continuous lead-smelting apparatus further includes an oxidation zone burner nozzle formed on an end wall of the oxidation zone of the reaction furnace, and a reduction zone burner nozzle formed on an end wall of the reduction zone of the reaction furnace, respectively. .
- a partition wall cooling device is arranged in the partition wall.
- the continuous lead-smelting apparatus further includes an oxidation zone waste heat boiler and an electric precipitator, wherein the oxidation zone waste heat boiler is connected to the oxidation zone outlet and the electric precipitator and the oxidation zone waste heat The boiler is connected.
- the continuous lead-smelting apparatus further includes a reduction zone waste heat boiler, a cooler and a bag filter, wherein the reduction zone waste heat boiler is connected to the reduction zone outlet, the cooler and the reduction zone A waste heat boiler is connected and the bag filter is connected to the cooler.
- a continuous lead smelting process using a continuous lead smelting apparatus wherein the continuous smelting lead apparatus includes a reaction furnace, and a partition wall is disposed in the reaction furnace to set the reaction furnace
- the furnace chamber is divided into an oxidation zone and a reduction zone, a lower portion of the furnace cavity constitutes a molten pool, and a bottom of the partition wall is provided with a communication passage connecting the oxidation zone and the reduction zone, wherein the continuous lead-smelting process
- the method comprises the steps of: adding a lead-containing material and a flux to an oxidation zone of the reaction furnace; spraying oxygen from a side of the oxidation zone into a molten pool of the oxidation zone to smelt the lead-containing material to obtain crude lead and rich Lead slag; a reducing agent and a flux are added to the reduction zone of the reaction furnace; oxygen and fuel are injected from the side of the reduction zone into the molten pool of the
- the continuous lead smelting process according to an embodiment of the present invention further includes feeding air from a side of the reduction zone to an upper portion of the molten pool of the reduction zone to oxidize excess combustible components generated during the reduction process in the reduction zone.
- the continuous lead smelting process further includes discharging oxidizing zone flue gas generated in the oxidizing zone from the top of the oxidizing zone; recovering waste heat of the oxidizing zone flue gas; and performing oxidizing zone flue gas after recovering waste heat Dust removal; and the use of flue gas in the oxidation zone after dedusting to produce acid.
- the continuous lead smelting process further includes discharging the reducing zone flue gas generated in the reducing zone from the top of the reducing zone; recovering waste heat of the reducing zone flue gas; and cooling the reducing zone flue gas after recovering the residual heat; And discharge the flue gas in the cooled reduction zone and discharge it.
- the dust in the oxidation zone and the flue gas in the reduction zone are dedusted to obtain soot and returned to the oxidation zone.
- the reducing agent is granular coal.
- the fuel is pulverized coal, or natural gas, or gas, or kerosene.
- FIG. 1 is a cross-sectional view of a continuous lead smelting apparatus according to an embodiment of the present invention
- FIG. 2 is a top plan view of a continuous lead smelting apparatus according to an embodiment of the present invention.
- Figure 3 is a cross-sectional view taken along line A-A of Figure 2;
- FIG. 4 is a flow chart of a continuous lead smelting process in accordance with an embodiment of the present invention.
- FIG. 5 is a flow diagram of a continuous lead smelting process in accordance with another embodiment of the present invention. detailed description
- connection shall be understood broadly, and may be, for example, a mechanical connection or an electrical connection, or may be internal communication of two elements, either directly or through Intermediaries are connected, and the meaning of the above terms may be understood by those skilled in the art on a case-by-case basis.
- a continuous lead smelting apparatus includes a reaction furnace 1, an oxidation zone side blowing lance 1 and a reduction zone side blowing lance 3.
- the reaction furnace 1 is provided with a partition wall 4, and the partition wall 4 divides the furnace chamber of the reaction furnace 1 into an oxidation zone Y and a reduction zone H, and a communication passage 41 connecting the oxidation zone Y and the reduction zone H is provided at the bottom of the partition wall 4.
- the lower portion of the furnace chamber of the reaction furnace 1 constitutes a molten pool.
- L1 is the liquid surface of the slag
- L2 is the liquid surface of the crude lead.
- the reaction furnace 1 may be a long oval fixed horizontal reaction vessel. Therefore, the reaction furnace 1 according to an embodiment of the present invention may also be referred to as a fixed horizontal furnace.
- the bottom wall of the furnace chamber reflecting the furnace 1 may have a concave curved shape as shown in FIG.
- An oxidation zone feed port 1 1 and an oxidation zone outlet port 12 are respectively disposed on the top wall of the oxidation zone Y.
- the reducing wall H is provided with a reducing agent inlet port 13 and a reducing zone outlet port 14 on the top wall of the reduction zone H.
- a siphon discharge lead 18 and a slag discharge port 20 are provided on the furnace wall of the furnace chamber of the reaction furnace 1.
- the oxidation zone side blowing lance 2 is connected to the side wall of the oxidation zone of the reaction furnace 1 to blow industrial oxygen (or oxygen-enriched air) side into the molten pool of the oxidation zone Y, thereby smelting the lead-containing material.
- the reduction zone side blowing lance 3 is connected to the side wall of the reduction zone of the reaction furnace 1 to blow the fuel and oxygen sides into the molten pool of the reduction zone H.
- the oxidation zone side blowing lance 2 injects industrial oxygen into the liquid surface L1 above the liquid surface L2 of the crude lead in the molten pool of the oxidized Y, in other words, the oxidation zone side
- the blowing gun 2 injects industrial oxygen into the lead-rich slag in the oxidation zone Y
- the reducing zone side blowing lance 3 injects fuel and oxygen into the slag in the reduction zone H, thereby in the reduction zone H, the reduction zone side
- the fuel and oxygen in the molten pool blown into the reduction zone H on the side of the blow gun 3 do not repeatedly oxidize the crude lead which has been reduced.
- the continuous lead smelting apparatus may also be referred to as a continuous side blowing lead apparatus, and a lead-containing material (for example, lead concentrate) and a flux are added from the oxidation zone feed port 11 to the oxidation zone Y through the oxidation zone side.
- a lead-containing material for example, lead concentrate
- the industrial oxygen injected by the blow gun 2 smelts the lead concentrate to obtain crude lead and lead-rich slag.
- the lead-rich slag in the oxidation zone Y flows into the reduction zone H from the communication passage 41 at the bottom of the partition wall 4 (i.e., the passage between the bottom surface of the partition wall 4 and the bottom surface of the furnace chamber).
- the lead in the lead-rich slag is reduced by adding a reducing agent such as granulated coal from the reducing agent inlet port 13 to the reduction zone H, and the fuel and oxygen are injected into the slag inside the reduction zone H through the reducing zone side blowing lance 3
- a reducing agent such as granulated coal from the reducing agent inlet port 13
- the temperature of the reduction zone H is maintained. It is to be understood that by controlling the amount of injection, a part of the fuel injected by the reduction zone side blowing lance 3 can also be used as a reducing agent to simultaneously reduce the lead-rich slag together with the added pulverized coal.
- oxidation and reduction can be realized in a single reaction furnace 1, and since the side blowing is performed, the fuel and oxygen blown to the H side in the reduction zone do not pass through the crude lead which has been reduced. So won't The crude lead is repeatedly oxidized, and the lead content in the slag is lowered and stabilized. Moreover, the oxidation zone Y and the reduction zone H are separated, and only communicate through the communication passage 41 at the bottom of the partition wall 4, and the communication passage 41 is immersed in the melt during operation, so that the oxidation zone Y and the upper portion of the reduction zone H are isolated, the oxidation zone The flue gas in the reduction zone will not be mixed and can be treated separately. Since continuous lead smelting is realized in a single closed reaction furnace, the sealing performance is good, the environmental protection is high, the enthalpy of the slag is fully utilized, and the energy consumption is reduced.
- the crude lead produced in the reduction zone H and the crude lead produced in the oxidation zone Y are discharged through the siphon discharge port 18, and the slag generated in the reduction zone H (i.e., the slag which has been reduced in the reduction zone H) is discharged from the slag discharge port. 20 discharge regularly.
- the flue gas generated in the oxidation zone Y contains a large amount of sulfur dioxide, which is discharged from the venting port 12 of the oxidation zone, and is recovered and dedusted by waste heat to produce acid.
- the flue gas generated in the reduction zone H is discharged from the flue outlet 14 of the reduction zone, and is subjected to waste heat recovery and dust removal.
- the soot recovered from the flue gas in the oxidation zone Y and the reduction zone H is returned to the oxidation zone Y.
- the continuous lead smelting apparatus of the embodiment of the present invention realizes continuous lead smelting and periodic slag discharge, and the oxidized zone Y and the reduction zone H communicate only through the communication passage 41, and the communication passage 41 is immersed in the melt, Therefore, the flue gas generated in the oxidation zone Y and the flue gas generated in the reduction zone H are not mixed, which is favorable for the continuous acid production of the high concentration S0 2 flue gas in the oxidation zone Y and the retention of the oxidation zone Y and the reduction zone H, respectively. Smelting system.
- the side blowing spray gun is used, the side blowing of the oxidation zone Y and the reduction zone H does not affect the already produced crude lead, so the lead content in the slag is easily controlled and lowered, for example, the lead content can be stably reduced to 2 -3%, and in the existing QSL lead-smelting method, the lead content in the slag is 5% or more and unstable.
- an oxidation zone spray gun port is disposed on the sidewall of the oxidation zone, and a reduction zone spray gun port is disposed on the sidewall of the reduction zone, and the oxidation zone side spray gun 2 is connected to the oxidation zone spray gun port and the reduction zone side
- the blow gun 3 is connected to the spray port of the reduction zone.
- the oxidizing zone side blowing lance 2 is connected to the oxidizing zone lance opening, and the oxidizing zone side blowing lance 2 is inserted into the oxidizing zone lance opening, and the reduction zone side blowing lance 3 is connected to the reduction zone lance opening to be the reduction zone side blowing lance. 3 Insert into the spray gun port of the reduction zone.
- the siphon discharge port 18 is disposed on the side wall of the reaction furnace 1 adjacent to the partition wall 4, and the slag discharge port 20 is disposed on the end wall of the reduction zone (reflecting the left end wall of the furnace 1 in Fig. 1). .
- a settling zone 19 is provided adjacent the siphon discharge opening 18 on the bottom wall of the furnace chamber.
- the upper portion of the side wall of the reduction zone of the reaction furnace 1 is provided with a secondary tuyeres 15.
- the flue gas generated in the reduction zone H is discharged from the flue gas outlet 14 of the reduction zone by the excess combustibles such as CO in the secondary air combustion flue gas fed through the secondary tuyere 15 in the upper portion of the reduction zone H, thereby improving environmental performance and Security performance.
- a furnace wall cooling device such as a cooling water jacket 5 is provided in a portion of the furnace wall of the reaction furnace 1 adjacent to the slag line L1, thereby cooling the reaction furnace 1 and extending the reaction furnace 1 Life expectancy.
- the continuous lead smelting apparatus may further include an oxidizing zone burner nozzle 17 formed on the end wall of the oxidation zone of the reaction furnace 1 (the right end wall in FIG. 1) and a reduction zone end formed in the reaction furnace 1 Wall (in Figure 1 Reduction zone burner spout 16 on the left end wall).
- Fuel such as heavy oil, may be injected into the oxidation zone Y and the reduction zone H by the oxidation zone burner and the reduction zone burner, respectively, through the oxidation zone burner orifice 17 and the reduction zone burner orifice 16.
- a partition wall cooling device is provided in the partition wall 4, whereby the partition wall 4 can be cooled.
- the continuous lead-smelting apparatus may further include an oxidation zone waste heat boiler and an electric precipitator, wherein the oxidation zone waste heat boiler is connected to the oxidation zone outlet 12 and the electric precipitator and the oxidation zone waste heat The boilers are connected, thereby recovering and dusting the waste gas from the oxidation zone discharged from the vent 12 of the oxidation zone, and then sending the acid to the acid.
- the recovered waste heat can be used for power generation or for residential use, and the smoke can return to the oxidation zone Y.
- the continuous lead smelting apparatus may further include a reduction zone waste heat boiler, a cooler, and a bag filter, the reduction zone waste heat boiler being connected to the reduction zone outlet port 14, the cooler such as a surface cooler and The reduction zone waste heat boiler is connected and the bag filter is connected to the cooler.
- the waste heat boiler in the reduction zone recovers the waste heat of the flue gas in the reduction zone, and then is cooled by the cooler, and then discharged by the bag filter to remove dust, and the recovered soot can be returned to the oxidation zone.
- the continuous lead-smelting process in the embodiment of the present invention includes the following steps: adding a lead-containing material and a flux to the oxidation zone of the reaction furnace 1;
- Oxygen is injected from the side of the oxidation zone of the reaction furnace 1 into the molten pool of the oxidation zone (i.e., below the slag line L2 and above the thick lead line L1) to smelt the lead-containing material to obtain crude lead and lead-rich slag;
- Oxygen and fuel are injected from the side of the reduction zone ⁇ of the reaction furnace 1 into the molten pool of the reduction zone to reduce the lead-rich slag flowing through the communication passage 41 into the reduction zone ⁇ molten pool to obtain crude lead and slag;
- the slag is periodically discharged from the slag discharge port 20.
- the continuous lead-smelting process may further include feeding secondary air from the side of the reduction zone of the reaction furnace 1 to the upper part of the molten zone of the reduction zone to oxidize in the reduction zone.
- Excessive carbon monoxide and other combustible components produced by the reduction process exhausting the oxidation zone flue gas generated in the oxidation zone from the top of the oxidation zone; recovering the waste heat of the oxidation zone; and removing dust from the oxidation zone after recovering the waste heat;
- Using the flue gas in the oxidation zone after dedusting to produce acid discharging the flue gas in the reduction zone generated in the reduction zone from the top of the reduction zone; recovering the waste heat of the flue gas in the reduction zone; cooling the flue gas in the reduction zone after recovering the waste heat; and after cooling
- the flue gas in the reduction zone is discharged after dust removal.
- the flue gas dedusting in the oxidation zone and the flue gas de-dusting in the reduction zone are returned to the oxidation zone.
- the reducing agent may be granulated coal, thereby eliminating the need for relatively expensive metallurgical coke, further Reduced costs.
- Lead-containing materials can be lead concentrates and can be used in conjunction with other lead-containing materials.
- the fuel is pulverized coal, natural gas, gas or kerosene.
- the continuous lead smelting apparatus and process according to an embodiment of the present invention is a continuous side blowing lead apparatus and process, which has outstanding technical advantages as compared with the prior art.
- the continuous lead-smelting apparatus and process are continuously oxidized and reduced and smelted in a single-stage side-blown reaction furnace, and therefore belong to the molten pool smelting technology, and the grain size and water content of the furnace are not high.
- the preparation system is simple, the process flow is short, the dust point and the dispersion point are small, the system is sealed, which is beneficial to the environment.
- the two melting zones, namely the oxidation zone Y and the reduction zone H, use industrial oxygen, and the reduction zone H fuel consumption is low, and the reduction can be Control, less smoke, low smoke rate and low energy consumption.
- the continuous lead smelting apparatus and process according to an embodiment of the present invention is a continuous side blow pool smelting technique for sulphide sulphide concentrate (and can be used in combination with a portion of lead-containing materials) to directly smelt lead.
- the oxidation and reduction smelting process is completed in a single side-blown reaction furnace, and the lead concentrate and lead-containing materials, flux, dust return, etc. are metered and granulated, and then continuously added to the oxidation zone Y of the side-blown smelting furnace, passing through the oxidation zone side.
- the blow gun 2 is fed with industrial oxygen to complete the smelting, oxidation and desulfurization operations, and the high-concentration sulfur dioxide flue gas is discharged from the venting port 12 of the oxidation zone. After the waste heat recovery and dust removal, the acid plant is sent to the acid plant for production, and the exhaust gas reaches the standard discharge and oxidizes.
- the crude lead produced in the zone Y is discharged from the siphon discharge port 18, the lead-rich slag enters the reduction zone H, and the reduction zone side blow gun 3 injects fuel (for example, pulverized coal, natural gas, gas or fuel) into the reduction zone H and Industrial oxygen, increasing the temperature of reducing and maintaining the reduction zone H, the reducing agent granulated coal required for the process is added by the reducing agent addition port 13 to ensure that the reduced slag contains lead to 2-3% and is stable.
- fuel for example, pulverized coal, natural gas, gas or fuel
- the flue gas generated in the reduction zone H is discharged from the flue gas outlet 14 of the reduction zone in the upper part of the reduction zone H by the secondary air to burn excess CO and other combustibles in the flue gas, and is discharged after the waste heat recovery, cooling and dust removal.
- the slag in the reduction zone H is periodically discharged (for example, once every 1.5-2 hours), and the slag can be sent to the smelting furnace to recover valuable metals such as zinc in the slag.
- the lead concentrate smelting process is carried out in a single closed smelting side blowing reaction furnace 1 to avoid flue gas escape.
- the S0 2 flue gas in the oxidation zone Y is recovered by waste heat and collected by electricity. After that, the exhaust emissions meet the environmental requirements.
- Lead concentrate or other lead materials are directly into the furnace after granulation, and the material preparation process is single.
- the lead dust generated in the production process is sealed and transported and returned to the ingredients, effectively preventing the dispersion of lead dust; After the flue gas is recovered and collected by the waste heat, the exhaust gas is discharged to the standard.
- the crude lead produced in the oxidation zone Y and the reduction zone H is discharged from the siphon discharge port 18, and the produced slag is periodically discharged from the slag discharge port 20, and a ventilating chamber can be provided at the siphon discharge lead port 18 and the slag discharge port 20 to prevent The diffusion of lead vapor. It can completely solve the problem of lead smelting flue gas and lead dust pollution.
- High recovery rate In the continuous side blowing reactor 1, due to the full utilization of the enthalpy of the slag, the reduction zone H will be eliminated.
- Continuous side blowing lead method is the method of all lead smelting methods, including material preparation system, the shortest process, process equipment, and investment.
- the description of the terms “one embodiment”, “some embodiments”, “example”, “specific example”, or “some examples” and the like means a specific feature described in connection with the embodiment or example.
- a structure, material or feature is included in at least one embodiment or example of the invention.
- the schematic representation of the above terms does not necessarily mean the same embodiment or example.
- the particular features, structures, materials, or characteristics described may be combined in a suitable manner in any one or more embodiments or examples.
Description
连续炼铅装置及连续炼铅工艺 技术领域
本发明涉及一种炼铅装置和工艺， 尤其是涉及一种连续炼铅装置和连续炼铅工艺。 背景技术
今年来， 为改善环境， 国内外已用于工业化生产的炼铅工艺主要有 QSL法、 SKS 法、 Kivcet法、 顶吹浸没熔池熔炼技术（主要为 Ausmel t法、 ISA法和卡尔多法）。 卡尔多炼铅 法由于炉寿命短， 作业率低， 成本高诸多因素， 因此难以推广应用。 SKS法， ISA—鼓风炉 还原炼铅法是在两台单独的炉中分别进行氧化还原熔炼的方法， Ausmel t 法是在单台炉中 分阶区进行氧化还原的方法， QSL法和 Kivcet法是在单台炉内分区域实现氧化还原过程。 但是， Ausmel t 法分阶区氧化还原法烟尘率高且烟气制酸和离子液吸收配气系统复杂。 Kivcet法需要严格的物料制备过程， 熔剂需要磨矿系统， 原料含水需千燥到 0. 5%以下， 焦 炭也需千燥， 备料复杂， 能耗高， 渣含铅不稳定， 投资成本高。 SKS法， ISA—鼓风炉还原 炼铅法， 鼓风炉需要消耗昂贵的冶金焦， 能耗偏高， 流程较长， 烟尘率高等不足。
QSL法在一个反应容器内实现氧化还原过程， 从而应用较广。 但是， QSL法烟尘率高达 25-30%, 而且由于釆用底吹， 已经还原出的粗铅部分被反复氧化和还原， 终渣中的含铅难 以控制， 终渣指标不理想、 能耗高， 此外， 由于反应容器需要旋转换枪， 造价高。 发明内容
本发明旨在至少解决现有技术中存在的技术问题之一。
为此， 本发明的一个目的在于提出一种能耗低、 环保、 铅的直收率高、 筒单且成本低 的连续炼铅装置。
本发明的另一目的在于提出一种连续炼铅工艺， 该连续炼铅工艺在一台反应炉内完成 铅冶炼的氧化、 还原过程， 即一步炼铅， 从而流程短、 环保好。
根据本发明第一方面的实施例提出一种连续炼铅装置， 包括： 反应炉， 所述反应炉内 设有隔墙以将所述反应炉的炉腔分成氧化区和还原区， 所述炉腔的下部构成熔池， 所述隔 墙的底部设有连通所述氧化区和还原区的连通通道， 所述氧化区的顶壁上分别设有氧化区 加料口和氧化区出烟口， 所述还原区的顶壁上设有还原剂加入口和还原区出烟口， 所述炉 腔的炉壁上设有虹吸放铅口和放渣口； 氧化区侧吹喷枪， 所述氧化区侧吹喷枪与所述反应 炉的氧化区侧壁相连以将氧气侧吹到所述氧化区的熔池内； 和还原区侧吹喷枪， 所述还原 区侧吹喷枪与所述反应炉的还原区侧壁相连以将燃料和氧气侧吹到所述还原区的熔池内。
根据本发明实施例的连续炼铅装置， 在单个反应炉内能够实现氧化和还原， 并且由于 釆取侧吹， 因此向还原区内侧吹的燃料和氧气不经过已经还原出来的粗铅 , 因此不会反复 氧化粗铅， 渣中含铅量降低并且稳定。 而且， 氧化区和还原区隔开， 仅通过隔墙底部的连 通通道连通， 连通通道在操作时浸没在熔体内， 因此氧化区和还原区的上部隔离， 氧化区 和还原区的烟气不会混合， 可以分别单独处理。 由于在单个封闭的反应炉内实现了连续炼 铅， 因此密封性能好， 环保性高， 充分利用了渣的热焓， 降低了能耗。
根据本发明实施例的连续炼铅装置可以具有如下附加技术特征。
所述氧化区侧壁上设有氧化区喷枪口， 所述还原区侧壁上设有还原区喷枪口， 其中所 述氧化区侧吹喷枪与所述氧化区喷枪口相连且所述还原区侧吹喷枪与所述还原区喷枪口相 连。
所述虹吸放铅口设置在所述反应炉的侧壁上且邻近所述隔墙， 所述放渣口设置在所述 反应炉的还原区端壁上。
在所述炉腔的底壁上在邻近所述虹吸放铅口的位置设有沉淀区。
所述炉腔的底壁为下凹的弧形。
所述反应炉的还原区侧壁的上部设有二次风口。
在所述反应炉的侧壁内邻近渣线部位设有炉壁冷却装置。
根据本发明实施例的连续炼铅装置进一步包括分别形成在所述反应炉的氧化区端壁上 的氧化区燃烧器喷口和形成在所述反应炉的还原区端壁上的还原区燃烧器喷口。
所述隔墙内设有隔墙冷却装置。
根据本发明实施例的连续炼铅装置进一步包括氧化区余热锅炉和电收尘器， 所述氧化 区余热锅炉与所述氧化区出烟口相连且所述电收尘器与所述氧化区余热锅炉相连。
根据本发明实施例的连续炼铅装置进一步包括还原区余热锅炉、冷却器和布袋收尘器， 所述还原区余热锅炉与所述还原区出烟口相连， 所述冷却器与所述还原区余热锅炉相连且 所述布袋收尘器与所述冷却器相连。
根据本发明第二方面的实施例提出一种利用连续炼铅装置进行的连续炼铅工艺， 其中 所述连续炼铅装置包括反应炉， 所述反应炉内设有隔墙以将所述反应炉的炉腔分成氧化区 和还原区， 所述炉腔的下部构成熔池， 所述隔墙的底部设有连通所述氧化区和还原区的连 通通道， 其特征在于， 所述连续炼铅工艺包括步骤： 将含铅物料和熔剂加入到所述反应炉 的氧化区内； 从所述氧化区的侧面向所述氧化区的熔池内喷入氧气以对含铅物料进行熔炼 得到粗铅和富铅渣； 将还原剂和熔剂加入到所述反应炉的还原区内； 从所述还原区的侧面 向所述还原区的熔池内喷入氧气和燃料以对通过所述连通通道从所述氧化区流到所述还原 区的富铅渣进行还原得到粗铅和渣； 从所述反应炉的虹吸放铅口排出所述粗铅； 和从所述
反应炉的放渣口间断地排出所述渣。
根据本发明实施例的连续炼铅工艺可以包括如下附加技术特征：
根据本发明实施例的连续炼铅工艺进一步包括从所述还原区内的侧面向所述还原区的 熔池上部送入空气以氧化在还原区内还原过程产生的过剩可燃成分。
根据本发明实施例的连续炼铅工艺进一步包括从所述氧化区的顶部排出氧化区内产生 的氧化区烟气； 回收所述氧化区烟气的余热； 对回收余热后的氧化区烟气进行除尘； 和利 用除尘后的氧化区烟气制酸。
根据本发明实施例的连续炼铅工艺进一步包括从所述还原区的顶部排出还原区内产生 的还原区烟气； 回收所述还原区烟气的余热； 冷却回收余热后的还原区烟气； 和对冷却的 还原区烟气进行除尘后排放。
将氧化区烟气除尘和还原区烟气除尘得到烟尘返回到所述氧化区内。
所述还原剂为粒煤。
所述燃料为粉煤、 或天然气、 或煤气、 或煤油。
本发明的附加方面和优点将在下面的描述中部分给出， 部分将从下面的描述中变得明 显， 或通过本发明的实践了解到。 附图说明
本发明的上述和 /或附加的方面和优点从结合下面附图对实施例的描述中将变得明显 和容易理解， 其中：
图 1是根据本发明实施例的连续炼铅装置的剖视图；
图 2是根据本发明实施例的连续炼铅装置的俯视图；
图 3是沿图 2中的线 A-A的剖视图；
图 4是根据本发明实施例的连续炼铅工艺的流程图； 和
图 5是根据本发明另一实施例的连续炼铅工艺的流程图。 具体实施方式
下面详细描述本发明的实施例， 所述实施例的示例在附图中示出， 其中自始至终相同 或类似的标号表示相同或类似的元件或具有相同或类似功能的元件。 下面通过参考附图描 述的实施例是示例性的， 仅用于解释本发明， 而不能理解为对本发明的限制。
在本发明的描述中， 术语 "纵向"、 "横向"、 "上，，、 "下，，、 "前，，、 "后，，、 "左，，、 "右，，、 "竖直"、 "水平"、 "顶"、 "底" 等指示的方位或位置关系为基于附图所示的方位或位置关 系， 仅是为了便于描述本发明而不是要求本发明必须以特定的方位构造和操作， 因此不能
理解为对本发明的限制。
在本发明的描述中， 术语 "相连，，、 "连接，， 应做广义理解， 例如， 可以是机械连接或 电连接， 也可以是两个元件内部的连通， 可以是直接相连， 也可以通过中间媒介相连， 对 于本领域的普通技术人员而言， 可以根据具体情况理解上述术语的具体含义。
下面参考图 1-3描述根据本发明实施例的连续炼铅装置。
如图 1-3 所示， 根据本发明实施例的连续炼铅装置包括反应炉 1 , 氧化区侧吹喷枪 1 和还原区侧吹喷枪 3。
反应炉 1内设有隔墙 4 , 隔墙 4将反应炉 1的炉腔分成氧化区 Y和还原区 H , 隔墙 4的 底部设有连通氧化区 Y和还原区 H的连通通道 41。 反应炉 1的炉腔的下部构成熔池， 在熔 池内， L1为渣的液面， L2为粗铅的液面。 在本发明的一个具体示例中， 反应炉 1可以为长 椭形的固定卧式反应容器。 因此， 根据本发明实施例的反应炉 1也可以称为固定卧式炉。 反映炉 1的炉腔的底壁可以为下凹的弧形， 如图 3所示。
氧化区 Y的顶壁上分别设有氧化区加料口 1 1和氧化区出烟口 12。还原区 H的顶壁上设 有还原剂加入口 1 3和还原区出烟口 14。 反应炉 1的炉腔的炉壁上设有虹吸放铅口 18和放 渣口 20。
氧化区侧吹喷枪 2与反应炉 1的氧化区侧壁相连以将工业氧气（或富氧空气）侧吹到 氧化区 Y的熔池内， 从而对含铅物料进行熔炼。 还原区侧吹喷枪 3与反应炉 1的还原区侧 壁相连以将燃料和氧气侧吹到还原区 H的熔池内。
如图 1所示， 更具体而言， 氧化区侧吹喷枪 2将工业氧气喷入到氧化去 Y的熔池内粗 铅的液面 L2之上渣的液面 L1之下， 换言之， 氧化区侧吹喷枪 2将工业氧气喷入到氧化区 Y内的富铅渣内， 还原区侧吹喷枪 3将燃料和氧气喷入到还原区 H 内的渣内, 从而在还原 区 H内， 还原区侧吹喷枪 3侧吹入还原区 H的熔池内的燃料和氧气不会反复氧化已经还原 出来的粗铅。
根据本发明实施例的连续炼铅装置， 也可以称为连续侧吹炼铅装置， 含铅物料（例如 铅精矿）和熔剂从氧化区加料口 11加入到氧化区 Y内， 通过氧化区侧吹喷枪 2喷入的工业 氧气对铅精矿进行熔炼得到粗铅和富铅渣。 氧化区 Y内的富铅渣从隔墙 4底部的连通通道 41 (即隔墙 4的底面与炉腔底面之间的通道）流入还原区 H内。 从还原剂加入口 1 3向还原 区 H内加入还原剂例如粒煤对富铅渣中的铅进行还原， 并且通过还原区侧吹喷枪 3向还原 区 H内的渣内侧喷入燃料和氧气以维持还原区 H的温度。 需要理解的是， 通过控制喷入量， 还原区侧吹喷枪 3喷入的部分燃料也可以作还原剂与加入的粒煤一起同时还原富铅渣。
根据本发明实施例的连续炼铅装置， 在单个反应炉 1 内能够实现氧化和还原， 并且由 于釆取侧吹， 因此向还原区内 H侧吹的燃料和氧气不经过已经还原出来的粗铅， 因此不会
反复氧化粗铅， 渣中含铅量降低并且稳定。 而且， 氧化区 Y和还原区 H隔开， 仅通过隔墙 4底部的连通通道 41连通， 连通通道 41在操作时浸没在熔体内， 因此氧化区 Y和还原区 H 的上部隔离， 氧化区和还原区的烟气不会混合， 可以分别单独处理。 由于在单个封闭的反 应炉内实现了连续炼铅， 因此密封性能好， 环保性高， 充分利用了渣的热焓， 降低了能耗。
还原区 H内产生的粗铅和氧化区 Y内产生的粗铅通过虹吸放铅口 18排出，还原区 H内 产生的渣（即在还原区 H内已经被还原后的炉渣）从放渣口 20定期排出。
氧化区 Y内产生的烟气含有大量的二氧化硫， 从氧化区出烟口 12排出， 经过余热回收 和除尘， 用以制酸。 还原区 H内产生的烟气从还原区出烟口 14排出， 经过余热回收和除尘 排放。 从氧化区 Y和还原区 H内的烟气中回收的烟尘返回到氧化区 Y内。
由此， 居本发明实施例的连续炼铅装置， 实现了连续炼铅和定期排渣， 而且氧化区 Y 与还原区 H仅通过连通通道 41连通， 而连通通道 41由于浸没在熔体内， 因此氧化区 Y内 产生的烟气与还原区 H内产生的烟气不会混合，有利于氧化区 Y内的高浓度 S02烟气的连续 制酸和保持氧化区 Y和还原区 H各自的熔炼制度。 并且由于釆用侧吹喷枪， 因此氧化区 Y 和还原区 H的侧吹不会影响已经产生的粗铅， 因此渣中的含铅量容易控制并且降低， 例如 含铅量可以稳定地降低到 2-3% , 而现有的 QSL炼铅法中， 渣中含铅量为 5%以上且不稳定。
在本发明的一些具体实施例中， 氧化区侧壁上设有氧化区喷枪口， 还原区侧壁上设有 还原区喷枪口， 氧化区侧吹喷枪 2与氧化区喷枪口相连且还原区侧吹喷枪 3与所述还原区 喷枪口相连。 这里， 氧化区侧吹喷枪 2与氧化区喷枪口相连可以是氧化区侧吹喷枪 2插入 到氧化区喷枪口内， 还原区侧吹喷枪 3与所述还原区喷枪口相连可以是还原区侧吹喷枪 3 插入到所述还原区喷枪口内。
如图 2和 3所示， 虹吸放铅口 18设置在反应炉 1的侧壁上且邻近隔墙 4 , 放渣口 20 设置在还原区端壁 （图 1中反映炉 1的左端壁）上。
在本发明的一些实施例中， 在炉腔的底壁上邻近虹吸放铅口 18的位置设有沉淀区 19。 由此， 氧化区 Y和还原区 H产生的粗铅聚集在沉淀区 19内， 然后从虹吸放铅口 18连续排 出， 减少了渣中的含铅量。
在本发明的一些实施例中， 反应炉 1的还原区侧壁的上部设有二次风口 15。 还原区 H 产生的烟气在还原区 H上部由通过二次风口 1 5供入的二次风燃烧烟气中过剩的 CO等可燃 物后由还原区出烟口 14排出， 提高了环保性能和安全性能。
在本发明的一些实施例中，在反应炉 1的炉壁内邻近渣线 L1的部位设有炉壁冷却装置， 例如冷却水套 5 , 由此对反应炉 1进行冷却， 延长了反应炉 1的寿命。
根据本发明实施例的连续炼铅装置可以进一步包括分别形成在反应炉 1 的氧化区端壁 (图 1中的右端壁）上的氧化区燃烧器喷口 17和形成在反应炉 1的还原区端壁（图 1中的
左端壁）上的还原区燃烧器喷口 16。 通过氧化区燃烧器喷口 17和还原区燃烧器喷口 16可 以分别在开炉时由氧化区燃烧器和还原区燃烧器向氧化区 Y和还原区 H内喷入燃料， 例如 重油。
在本发明的一些实施例中， 隔墙 4内设有隔墙冷却装置， 由此可以对隔墙 4进行冷却。 根据本发明实施例的连续炼铅装置可以进一步包括氧化区余热锅炉和电收尘器， 所述 氧化区余热锅炉与氧化区出烟口 12相连且所述电收尘器与所述氧化区余热锅炉相连， 由此 对从氧化区出烟口 12排出的氧化区烟气进行余热回收和除尘， 然后送去制酸。 回收的余热 可以发电或供居民生活用， 烟尘可以返回氧化区 Y。
根据本发明实施例的连续炼铅装置可以进一步包括还原区余热锅炉、 冷却器和布袋收 尘器， 所述还原区余热锅炉与还原区出烟口 14相连， 所述冷却器例如表面冷却器与所述还 原区余热锅炉相连且所述布袋收尘器与所述冷却器相连。 还原区余热锅炉回收还原区烟气 的余热， 然后经过冷却器冷却， 接着经过布袋收尘器除尘后排放， 回收的烟尘可以返回氧 化区 Υ。
下面描述根据本发明实施例的连续炼铅工艺。
如图 4所示， 结合图 1-3 , 居本发明实施例的连续炼铅工艺包括以下步骤： 将含铅物料和熔剂加入到反应炉 1的氧化区 Υ内；
从反应炉 1的氧化区 Υ的侧面向氧化区 Υ的熔池内（即渣线 L2下面和粗铅线 L1上方） 喷入氧气以对含铅物料进行熔炼得到粗铅和富铅渣；
将还原剂和熔剂加入到反应炉 1的还原区 Η内；
从反应炉 1的还原区 Η的侧面向还原区 Η的熔池内喷入氧气和燃料以对通过连通通道 41流到还原区 Η熔池内的富铅渣进行还原得到粗铅和渣；
从虹吸放铅口 18排出粗铅； 和
从放渣口 20定期排出渣。
如图 5所示， 根据本发明另一实施例的连续炼铅工艺可以进一步包括从反应炉 1的还 原区侧面向还原区 Η的熔池的上部送入二次空气以氧化在还原区 Η内还原过程产生的过剩 的一氧化碳等可燃成分； 从氧化区 Υ的顶部排出氧化区 Υ内产生的氧化区烟气； 回收氧化 区烟气的余热； 对回收余热后的氧化区烟气进行除尘； 和利用除尘后的氧化区烟气制酸； 从还原区 Η的顶部排出还原区 Η内产生的还原区烟气； 回收还原区烟气的余热； 冷却回收 余热后的还原区烟气； 和冷却后的还原区烟气进行除尘后排放。
在本发明的一个实施例中， 将氧化区烟气除尘和还原区烟气除尘得到烟尘返回到氧化 区 Υ内。
在本发明的一个示例中， 还原剂可以为粒煤， 由此不需要相对较贵的冶金焦， 进一步
降低了成本。 含铅物料可以为铅精矿， 并且可以搭配处理其他含铅物料。 燃料为粉煤， 天 然气， 煤气或煤油。
根据本发明实施例的连续炼铅装置和工艺为连续侧吹炼铅装置和工艺， 与现有技术相 比具有突出的技术优势。
才艮据本发明实施例的连续炼铅装置和工艺在单台侧吹反应炉内 , 实现分区域连续进行 氧化、 还原熔炼， 因此属于熔池熔炼技术， 对入炉粒度、 含水要求不高， 备料系统筒单， 工艺流程短， 扬尘点和弥散点少， 系统密闭， 有利于环保， 两个熔炼区即氧化区 Y和还原 区 H均釆用工业氧气， 还原区 H燃料消耗低， 还原可控， 烟气量少， 烟尘率低， 能耗低。
更加具体而言， 根据本发明实施例的连续炼铅装置和工艺是连续侧吹熔池熔炼技术， 用于硫化铅精矿（并可搭配处理部分含铅物料）直接炼铅。 在单台侧吹反应炉内完成氧化、 还原熔炼过程， 铅精矿及含铅物料、 熔剂、 返尘等经计量配料制粒后， 连续加入侧吹熔炼 炉的氧化区 Y, 通过氧化区侧吹喷枪 2送入工业氧气， 完成熔炼、 氧化、 脱硫作业， 产出 高浓度的二氧化硫烟气由氧化区出烟口 12排出， 经余热回收和除尘后送酸厂制酸， 尾气达 标排放， 氧化区 Y产出的粗铅由虹吸放铅口 18排出， 富铅渣进入还原区 H , 还原区侧吹喷 枪 3往还原区 H内喷入燃料（例如， 粉煤、 天然气、 煤气或燃油）和工业氧气， 提高还原 和维持还原区 H的温度， 过程所需的还原剂粒煤由还原剂加入口 13加入， 以保证还原后的 渣含铅降到 2-3%且稳定。 还原区 H产生的烟气在还原区 H上部由二次风燃烧烟气中过剩的 CO等可燃物后， 由还原区出烟口 14排出， 经余热回收、 降温除尘后达标排放。 还原区 H 内的渣定期排放 (例如， 每 1. 5-2h排放一次）， 渣可送烟化炉回收渣中的锌等有价金属。
根据本发明实施例的连续炼铅装置和工艺的技术优势在于：
1、 能耗低： 在在单台侧吹反应炉 1里面实现了从铅精矿到粗铅的熔炼过程， 在氧化区 Y不需要补充其它的燃料， 充分利用反应热， 在还原区 H充分利用了渣的热焓， 消耗较少 的燃料， 使用粒煤作为还原剂， 不需要相对较贵的冶金焦， 同时回收氧化区和还原区烟气 中的余热。
2、环保好：铅精矿熔炼过程在单台密闭的熔炼侧吹反应炉 1中进行，避免了烟气外逸， 氧化区 Y内的 S02烟气经余热回收和电收尘送制酸后，尾气排放达到了环保要求。铅精矿或 其它铅原料配合制粒后直接入炉， 物料制备过程筒单， 生产过程中产出的铅烟尘均密封输 送并返回配料，有效防止了铅尘的弥散； 还原区 H产出的烟气经余热回收和收尘后， 尾气达 标排放。 氧化区 Y和还原区 H产出的粗铅从虹吸放铅口 18排出， 产出的渣从放渣口 20定 期排出， 同时在虹吸放铅口 18和放渣口 20可以设通风室， 防止铅蒸气的扩散。 可以很彻 底解决铅冶炼烟气、 铅尘污染的问题。
3、 回收率高： 在连续侧吹反应炉 1中， 由于充分的利用了渣的热焓， 在还原区 H将消
耗较少的燃料进行补热， 使用粒煤作为还原剂， 有效的降低了烟气量和烟尘率、 降低了渣 中的铅含量， 提高了铅的直收率和回收率。
4. 连续侧吹炼铅法是所有炼铅方法中， 包括物料制备系统， 流程最短的工艺， 工艺装 置筒单、 投资省。
在本说明书的描述中， 参考术语 "一个实施例"、 "一些实施例"、 "示例"、 "具体示 例"、 或 "一些示例" 等的描述意指结合该实施例或示例描述的具体特征、 结构、 材料或者 特点包含于本发明的至少一个实施例或示例中。 在本说明书中， 对上述术语的示意性表述 不一定指的是相同的实施例或示例。 而且， 描述的具体特征、 结构、 材料或者特点可以在 任何的一个或多个实施例或示例中以合适的方式结合。
尽管已经示出和描述了本发明的实施例， 本领域的普通技术人员可以理解： 在不脱离 本发明的原理和宗旨的情况下可以对这些实施例进行多种变化、 修改、 替换和变型， 本发 明的范围由权利要求及其等同物限定。
Claims
1、 一种连续炼铅装置， 其特征在于， 包括：
反应炉， 所述反应炉内设有隔墙以将所述反应炉的炉腔分成氧化区和还原区， 所述炉 腔的下部构成熔池， 所述隔墙的底部设有连通所述氧化区和还原区的连通通道， 所述氧化 区的顶壁上分别设有氧化区加料口和氧化区出烟口， 所述还原区的顶壁上设有还原剂加入 口和还原区出烟口， 所述炉腔的炉壁上设有虹吸放铅口和放渣口；
氧化区侧吹喷枪， 所述氧化区侧吹喷枪与所述反应炉的氧化区侧壁相连以将氧气侧吹 到所述氧化区的熔池内； 和
还原区侧吹喷枪， 所述还原区侧吹喷枪与所述反应炉的还原区侧壁相连以将燃料和氧 气侧吹到所述还原区的熔池内。
2、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 所述氧化区侧壁上设有氧化区 喷枪口， 所述还原区侧壁上设有还原区喷枪口， 其中所述氧化区侧吹喷枪与所述氧化区喷 枪口相连且所述还原区侧吹喷枪与所述还原区喷枪口相连。
3、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 所述虹吸放铅口设置在所述反 应炉的侧壁上且邻近所述隔墙， 所述放渣口设置在所述反应炉的还原区端壁上。
4、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 在所述炉腔的底壁上在邻近所 述虹吸放铅口的位置设有沉淀区。
5、根据权利要求 1所述的连续炼铅装置，其特征在于，所述炉腔的底壁为下凹的弧形。
6、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 所述反应炉的还原区侧壁的上 部设有二次风口。
7、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 在所述反应炉的侧壁内邻近渣 线部位设有炉壁冷却装置。
8、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 进一步包括分别形成在所述反 应炉的氧化区端壁上的氧化区燃烧器喷口和形成在所述反应炉的还原区端壁上的还原区燃 烧器喷口。
9、根据权利要求 1所述的连续炼铅装置，其特征在于，所述隔墙内设有隔墙冷却装置。
10、 根据权利要求 1 所述的连续炼铅装置， 其特征在于， 进一步包括氧化区余热锅炉 和电收尘器， 所述氧化区余热锅炉与所述氧化区出烟口相连且所述电收尘器与所述氧化区 余热锅炉相连。
11、 根据权利要求 1所述的连续炼铅装置， 其特征在于， 进一步包括还原区余热锅炉、 冷却器和布袋收尘器， 所述还原区余热锅炉与所述还原区出烟口相连， 所述冷却器与所述 还原区余热锅炉相连且所述布袋收尘器与所述冷却器相连。
12、 一种利用连续炼铅装置进行的连续炼铅工艺， 其中所述连续炼铅装置包括反应炉， 所述反应炉内设有隔墙以将所述反应炉的炉腔分成氧化区和还原区， 所述炉腔的下部构成 熔池， 所述隔墙的底部设有连通所述氧化区和还原区的连通通道， 其特征在于， 所述连续 炼铅工艺包括以下步骤：
将含铅物料和熔剂加入到所述反应炉的氧化区内；
从所述氧化区的侧面向所述氧化区的熔池内喷入氧气以对含铅物料进行熔炼得到粗铅 和富铅渣；
将还原剂和熔剂加入到所述反应炉的还原区内；
从所述还原区的侧面向所述还原区的熔池内喷入氧气和燃料以对通过所述连通通道从 所述氧化区流到所述还原区的富铅渣进行还原得到粗铅和渣；
从所述反应炉的虹吸放铅口排出所述粗铅； 和
从所述反应炉的放渣口间断地排出所述渣。
13、 根据权利要求 12所述的连续炼铅工艺， 其特征在于， 进一步包括从所述还原区内 的侧面向所述还原区的熔池上部送入空气以氧化在还原区内还原过程产生的过剩可燃成 分。
14、 根据权利要求 13所述的连续炼铅工艺， 其特征在于， 进一步包括：
从所述氧化区的顶部排出氧化区内产生的氧化区烟气；
回收所述氧化区烟气的余热；
对回收余热后的氧化区烟气进行除尘； 和
利用除尘后的氧化区烟气制酸。
15、 根据权利要求 14所述的连续炼铅工艺， 其特征在于， 进一步包括：
从所述还原区的顶部排出还原区内产生的还原区烟气；
回收所述还原区烟气的余热；
冷却回收余热后的还原区烟气； 和
对冷却的还原区烟气进行除尘后排放。
16、 根据权利要求 15所述的连续炼铅工艺， 其特征在于， 将氧化区烟气除尘和还原区 烟气除尘得到烟尘返回到所述氧化区内。
17、 根据权利要求 12所述的连续炼铅工艺， 其特征在于， 所述还原剂为粒煤。
18、根据权利要求 12所述的连续炼铅工艺， 其特征在于， 所述燃料为粉煤、或天然气、 或煤气、 或煤油。
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| CN103937985A (zh) * | 2014-04-18 | 2014-07-23 | 中国恩菲工程技术有限公司 | 连续式烟化炉及采用它的连续烟化工艺 |
| CN103937985B (zh) * | 2014-04-18 | 2016-03-30 | 中国恩菲工程技术有限公司 | 连续式烟化炉及采用它的连续烟化工艺 |
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| CN102011014B (zh) | 2012-11-14 |
| CN102011014A (zh) | 2011-04-13 |
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