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    Process of producing sulfuric acid
    31.
    发明授权
    Process of producing sulfuric acid 失效
    硫酸生产工艺

    公开(公告)号：US4333917A

    公开(公告)日：1982-06-08

    申请号：US119289

    申请日：1980-02-07

    申请人： Karl H. Dorr ,  Helmut Diekmann ,  Hugo Grimm ,  Ulrich Sander ,  Michael Tacke ,  Waldemar Weber

    发明人： Karl H. Dorr ,  Helmut Diekmann ,  Hugo Grimm ,  Ulrich Sander ,  Michael Tacke ,  Waldemar Weber

    IPC分类号： C01B17/56 ,  C01B17/74 ,  C01B17/76 ,  C01B17/765 ,  B01D3/00 ,  C01B17/48 ,  C01B17/98

    CPC分类号： C01B17/76 ,  C01B17/56 ,  C01B17/7655

    摘要： A process for the production of sulfuric acid from wet sulfur dioxide containing gases is disclosed. The sulfur dioxide containing gas is initially purified and cooled, then predried with dilute sulfuric acid, finally dried with concentrated sulfuric acid, converted to sulfur trioxide catalytically and, the sulfur trioxide is absorbed in sulfuric acid. Preliminary drying removes more water than needed to maintain the water balance in the following process steps. A portion of the dilute acid from the preliminary drying is concentrated prior to recycle to the preliminary drying step and another portion of the acid from the preliminary dryer is added to the sulfur trioxide absorber to adjust the water balance in the acid circulating between the final dryer and the sulfur trioxide absorber.

    摘要翻译： 公开了一种从含有二氧化硫的气体生产硫酸的方法。 含二氧化硫的气体最初被纯化和冷却，然后用稀硫酸预干燥，最后用浓硫酸干燥，催化转化成三氧化硫，三氧化硫被吸收在硫酸中。 初步干燥除了在以下工艺步骤中维持水分平衡所需的更多的水。 将预备干燥中的一部分稀酸在再循环到预干燥步骤之前进行浓缩，并将另一部分来自预干燥器的酸加入到三氧化硫吸收器中以调节在最终干燥器之间循环的酸中的水分平衡 和三氧化硫吸收剂。

    Process for the removal of gaseous impurities from the exhaust gases of a contact-process plant for the production of sulfuric acid
    34.
    发明授权
    Process for the removal of gaseous impurities from the exhaust gases of a contact-process plant for the production of sulfuric acid 失效
    用于从用于生产硫酸的接触工艺设备的废气中除去气态杂质的方法

    公开(公告)号：US3944401A

    公开(公告)日：1976-03-16

    申请号：US467387

    申请日：1974-05-06

    申请人： Karl-Heinz Dorr ,  Hugo Grimm ,  Ulrich Sander ,  Robert Peichl ,  Michael Tacke

    发明人： Karl-Heinz Dorr ,  Hugo Grimm ,  Ulrich Sander ,  Robert Peichl ,  Michael Tacke

    IPC分类号： B01D53/48 ,  B01D47/10 ,  B01D53/34 ,  B01D53/50 ,  B01D53/77 ,  C01B17/74 ,  B01D47/14

    CPC分类号： B01D53/34 ,  B01D47/10 ,  C01B17/74 ,  Y02P70/34

    摘要： Sulfur compounds oxidizable to form sulfuric acid and organic compounds oxidizable to CO.sub.2 and H.sub.2 O are removed from an exhaust gas of a contact-process plant for producing sulfuric acid by treating the exhaust gas with a scrubbing solution consisting of dilute sulfuric acid and peroxydisulfuric acid. The peroxydisulfuric acid is produced electrolytically from fresh dilute sulfuric acid and the resulting electrolyte is continuously introduced into the scrubbing acid cycle. The exhaust gas is treated in a vertical venturi with uniflow, i.e. codirectional flow of the gas and the scrubbing solution, and the gas is then passed through a horizontal venturi and subsequently upwardly through a packing layer.CROSS-REFERENCE TO RELATED APPLICATIONThe present Application is related to the commonly assigned copending application Ser. No. 308,849 filed Nov. 22, 1972 and entitled METHOD OF REMOVING GASEOUS IMPURITIES FROM WASTE GASES now abandoned. The latter application relates to subject matter disclosed and claimed in copending application Ser. No. 74,629 filed Sept. 23, 1970 now abandoned, commonly assigned copending application Ser. No. 188,127 filed Oct. 12, 1971, and commonly assigned copending application Ser. No. 188,128 filed Oct. 12, 1971, now U.S. Pat. Nos. 3,780,499 and 3,788,043 respectively, all dealing with absorption systems and gases containing sulfur oxides and naming one or more of the present joint inventors.FIELD OF THE INVENTIONThe present invention relates to a process for the removal of sulfur compounds oxidizable to form sulfuric acid and organic compounds oxidizable to form CO.sub.2 and H.sub.2 O from the exhaust gases produced by contact-process plants for making sulfuric acid.BACKGROUND OF THE INVENTIONAs pointed out in application Ser. No. 308,849, sulfur-containing gases and particulates are a major problem in modern societies because they are released into the atmosphere from many sources and are highly toxic to the population, to vegetation and to metal, stone and other structures.In the combustion of fuel oil and coal, for example, elemental sulfur and sulfur oxides may be released into the atmosphere.From chemical plants, organic sulfur compounds, hydrogen sulfide and sulfur oxides may be released into the atmosphere.In sulfuric acid plants, the waste gases following the final absorption may contain toxic or dangerous quantities of residual sulfur dioxide and sulfur trioxide.In the roasting of metal and other metallurgical processes, the release of elemental sulfur, and sulfur compounds, especially sulfur oxides, has long been a problem.Consequently, considerable effort has been made to obtain an efficient, low-cost system for removing sulfur compounds from waste gases and capable of minimizing the release of such gases into the atmosphere.A large number of processes have been suggested for this purpose as described, for example, in the literature references cited in application Ser. No. 308,849. These processes include washing the gas with sodium carbonate solution followed by crystallization of sodium sulfite, washing the gas with a magnesia slurry followed by crystallization and recovery of the magnesia as well as concentrated sulfur dioxide, washing the gas with gaseous potassium sulfite which is then recovered by stripping from the precipitated pyrosulfite. More complex and extensive systems may also be mentioned here, although they have been more or less fully described in the aforementioned copending applications as representing the state of the art. Suffice it to say that it has been discovered by some of the present applicants jointly with another, as decribed in application Ser. No. 308,849, that waste gases can be economically treated with a dilute sulfuric acid containing peroxydisulfuric acid in such manner that sulfur trioxide results. A critical feature of the system described in the last-mentioned application is that the peroxydisulfuric acid level in the treating solution is replenished by the electrolysis of fresh dilute sulfuric acid (electrolysis-cell acid) with the peroxydisulfuric acid solution thus produced being mixed with dilute sulfuric acid to form the gas-treating liquor. The peroxydisulfuric acid which decomposes upon treatment of the gas, the sulfuric acid formed by absorption of the sulfur trioxide in the dilute sulfur acid and the dilute sulfuric acid serving as the treatment vehicle and absorber can thus be drawn off without recycling to the electrolysis cell.Best results were obtained using this system with gas streams containing sulfur dioxide and those with the exhaust gases of combustion installations such as furnaces, metal or roasting plants and sulfuric acid plants.The system of application Ser. No. 308,849 may be used, in addition, to remove sulfur-containing impurities other than sulfur dioxide from an exhaust gas. It has been found that inorganic sulfur compounds containing sulfur in an oxidation state in which it can be oxidized to elemental sulfur and/or to sulfur dioxide can be removed with that system. For example, inorganic sulfides and hydrogen sulfide can be treated with the peroxydisulfuric acid solution and oxidized to elemental sulfur and eventually sulfur trioxide.The peroxydisulfuric acid concentration was preferably between 200 and 300 grams of peroxydisulfuric acid per liter in the cell acid, most advantageously between 240 and 260 grams per liter. At these concentrations a high yield or efficiency was obtained and practically no water was introduced into the system so that local overheating and thermal degradation of the peroxydisulfuric acid was avoided.The dilute sulfuric acid had a concentration of 25 to 60% by weight, this concentration giving the efficient washing and absorption characteristics. Sulfur trioxide, present in the exhaust gas, and/or sulfuric acid mist (which is generally present when the exhaust gas is derived from a sulfuric acid plant) can be removed simultaneously in spite of the fact that these components are not oxidized. The exhaust gas may contain organic compounds which are oxidized by the peroxydisulfuric acid system to carbon dioxide and water vapor.The gas was treated with the liquid phase in uniflow by passing the gas phase and the liquid phase jointly through the constriction of a venturi absorber. As described in applications Ser. Nos. 74,629, 188,127 and 188,128 and in our earlier individual and joint efforts, for reasons which are not fully understood the intimate contact produced by forcing the liquid phase jointly through a construction and thereafter permitting the mixture of the two phases to expand past the constriction yields a far more effective interaction of the two phases than can be obtained with theoretically equivalent washing towers in which the gas and liquid have similar contact times and interflow velocity. The gas, after the treatment with and separation from dilute sulfuric acid, was conducted through a droplet separator designed to avoid entraining of acid droplets along with the gas. The droplet separator was a packed bed traversed by the gas and from an impingement, collector and interaction surfaces which not only prevent passage of the acid droplets through the layer but also bring about an intimate contact of the gas phase with the acid in the form of a liquid film of the latter or so-called after-absorption and after-reaction.Where the gas is passed upwardly through a filter bed of this type, the lowermost layer consisted of a porous packing bed with particles of a particle size of 5 to 20 millimeters, preferably 9 to 15 millimeters. In this layer precipitation and removal of entrained acid droplets occurs. The packing bodies are coated with a liquid film in which the aforementioned after-absorption takes place. When this liquid film tends to become thicker, the sulfuric acid droplets fall from the layer. The rising gas stream and the pore size maintain a thin liquid layer above the packing mass.The after-absorption is preferably effected in a layer having a height of 50 to 200 millimeters, preferably 80 to 120 millimeters, this bed height having been found to provide after-absorption with a minimum of increased flow resistance. The gas velocity furing after-absorption was 1 to 2.5 meters per second, preferably 1.3 to 1.7 meters per second.After traversing the after-absorption layer of a thickness of 50 to 200 millimeters and composed of porous packing bodies with a particle size of 5 to 20 millimeters at a gas velocity of 1 to 2.5 meters per second, the gas passed through a layer of acid-resistance nonporous packing bodies with a particle size of 20 to 50 millimeters in an after-absorption stage, the latter overlying the after-absorption bed.The after-separation bed not only loads the after-absorption bed to prevent migration of the packing bodies but also provides impingement-type liquid-separation surfaces together with narrower and random channels in which residual droplets of acid may be separated from the gas phase. The after-separation bed has a thickness of 50 to 150 millimeters, preferably 80 to 120 millimeters, a range which has been found to be effective for efficient separation of the residual liquid from the gas phase without materially increasing the flow resistance.It was found to be desirable to treat the gas (containing sulfur compounds and other compounds oxidizable by peroxydisulfuric acid to sulfur dioxide, carbon dioxide and water vapor) with a dilute sulfuric acid containing the peroxydisulfuric acid in a venturi-type apparatus in uniflow, i.e. a system in which the gas and liquid phases flow in the same direction. The venturi absorber was provided ahead of the venturi constriction and expansion chamber with a liquid-collecting chamber and means for diverting the gas stream from its axial flow direction as it emerges from the venturi chamber. The gas stream was diverted by an angle of 90.degree. or more, thereby causing droplets of high kinetic energy to pass through the bodies of liquid in the bath disposed ahead of the venturi outlet. The venturi absorber was preferably oriented vertically so that its outlet was directed downwardly into this bath and the expansion chamber was provided with lateral outlets above the bath so that the main body of gas is first directed downward toward the bath and is then diverted upwardly and laterally to shed larger droplets and high-energy particles.The acid collected in the sump was in part recirculated to the venturi. It was also advantageous to pass the gas phase into contact with the peroxydisulfuric acid/dilute sulfuric acid liquid phase by forcing the gas upwardly through a gas-permeable plate upon which the acid layer was provided. The gas-permeable plate was composed of a porous material such as sintered glass or porcelain. The gas permeability, gas-flow velocity and volume were so dimensioned that little or no sulfuric acid solution passed through the plate. Best results were obtained when the after-absorber and after-separator beds of packing were provided upon the perfoated plate or upon respective prerforated plates in cascade.The parts of the apparatus which came into contact with the acid solution were constituted from or were coated with acid resistance, preferably polyvinil chloride.OBJECTS OF THE INVENTIONIt is the principal object of the present invention to provide an improved method of removing gaseous impurities from the waste gases of a contact-process plate for producing sulfuric acid.Another object of the invention is to extend the principles originally set forth in application Ser. No. 308,849.SUMMARY OF THE INVENTIONAccording to the invention, this object is accomplished in that the exhaust gas is treated in a vertical venturi tube with cocurrent injected circulating scrubbing acid from the sump of the venturi tube, at least part of the injected scrubbing acid being separated and collected in the sump of the venturi tube.The gas is conducted into a substantially horizontal venturi tube disposed between the sump and the outlet opening of the vertical venturi tube and opening into a tower, the gas being treated in the horizontal venturi tube with cocurrent injected circulating scrubbing acid from the sump of the tower.The injected scrubbing acid is separated and is collected in the sump of the tower; the gas rising in the tower, which contains a packing layer, is treated with countercurrent circulating scrubbing acid coming from the sump of the tower and injected above the packing layer, and with the added acid electrolyte which contains peroxydisulfuric acid, and the acids fed into the tower are separated and are collected to the sump of the tower.Preferably a large part of the circulating scrubbing acid injected into the vertical venturi tube is separated and is collected in the sump of this venturi tube since even the scrubbing acid which has been entrained into the inlet of the substantially horizontal venturi tube as far as the throat thereof is recycled.The separation and recycling of the scrubbing acid which has been entrained to the narrowest part or throat of the substantially horizontal venturi tube from the vertical venturi tube may be accomplished by downwardly inclining the gas outlet conduit from the vertical venturi tube, or by the provision of baffles in the gas outlet conduit and by the provision of drain openings in the lower portion of the gas outlet conduit or in the inlet portion of the substantially horizontal venturi tube. These drain openings are connected by conduits to the sump of the vertical venturi tube.As a result of these measures, which may be used individually or in combination, a major portion of the scrubbing acid entrained from the vertical venturi tube is separated and conducted into the sump of that venturi tube so that the scrubbing acid cycles can be separated to a high degree.Advantageously, a large part of the circulating scrubbing acid injected into the vertical venturi tube is separated and is collected in the sump of the venturi tube because a packing layer is provided below the outlet opening of the venturi tube and above the inlet opening of the substantially horizontal venturi tube. This packing layer has a thickness of about 10-20 centimeter. The high turbulence produced in that layer also promotes the separation of the scrubbing acid, which is then collected in the sump of the vertical venturi tube.Scrubbing acid can be transferred from the sump of the tower via an overflow into the sump of the vertical venturi tube in a quantity which corresponds to the added electrolyte acid containing peroxydisulfuric acid and to the sulfuric acid formed as an oxidation product in the substantially horizontal venturi tube. In this simple way, a constant level is maintained in the tower sump and the entire system is operated in countercurrent of liquid and gas flow so that the active oxygen is optimally utilized. Besides, a steady-state concentration of active oxygen in the sump of the vertical venturi tube is maintained constant.The steady-state sulfuric acid concentration of the scrubbing acid in the sump of the vertical venturi tube is held constant by an addition of water. As a result, the evaporative loss of water is compensated and the heat of the resulting mixture is utilized for a hydrolysis of the residual peroxydisulfuric acid in the sump of the vertical venturi tube.The level of the sump in the vertical venturi tube is held constant by a withdrawal of scrubbing acid, which contains the oxidation product, from the sump. In that case, the product is withdrawn from the system at a point where the content of residual active oxygen is lowest.Different concentrations of sulfuric acid are maintained in the cycles of the circulating scrubbing acid, the highest concentrations of sulfuric acid and active oxygen being provided in the acid which is sprayed into the tower, a lower concentration being provided in the acid which is injected into the substantially horizontal venturi tube, and the lowest concentration being provided in the acid which is injected into the vertical venturi tube. This results in an optimum oxidation of SO.sub.2 and/or of other oxidizable gas components and an optimum utilization of the active oxygen supplied to the system.The electrolyte acid which emerges from the electrolytic unit and contains peroxydisulfuric acid consists of sulfuric acid which has a concentration of 30 - 50% by weight H.sub.2 SO.sub.4, preferably 35 - 40% by weight H.sub.2 SO.sub.4, and contains 180 - 350 grams, preferably 200 - 300 grams, peroxydisulfuric acid per liter. These concentrations give very good results in operation.Advantageously, the acid electrolyte which contains peroxydisulfuric acid is held in intermediate storage to increase the hydrolysis of the peroxydisulfuric acid. The increased hydrolysis of H.sub.2 S.sub.2 O.sub.8 to H.sub.2 SO.sub.5 and H.sub.2 SO.sub.4 results in a higher rate of oxidation of the gas components in the succeeding scrubber. Besides, the intermediate storage provides for a supply from which acid electrolyte which contains active oxygen can be withdrawn immediately at a suitable rate in case of fluctuations of the gas rate. Besides, the high SO.sub.2 content of the exhaust gas from a sulfuric acid contact process plant when being started up, may be absorbed in that the entire system is filled from the supply tank with electrolyte acid containing a high concentration of active oxygen so that there is initially a high content of active oxygen in all absorption stages.The intermediate storage is continued until a hydrolysis of 30 - 90% has been effected. That degree of hydrolysis gives good results in operation.The stationary steady-state concentration of the scrubbing acid in the sump of the tower most desirably amounts to 30 - 50% by weight, preferably 38 - 45% by weight, sulfuric and a molar concentration of active oxygen 0.4-1.26 moles, preferably 0.6-1.0 moles per liter. High degrees of oxidation are obtained with these concentrations.The stationary steady-state concentration of the scrubbing acid in the sump of the vertical venturi tube is advantageously 25 - 40% by weight sulfuric acid, preferably 28 - 32% by weight, and the active oxygen has a concentration of 0.06-0.3 moles per liter, preferably 0.1 - 0.15 moles per liter. A relatively high water vapor partial pressure in the gas phase and high degrees of oxidation are obtained with these concentrations.The residence time of the scrubbing acid which contains the residual peroxydisulfuric acid in the sump of the tower and in the sump of the vertical venturi tube is adjusted so that 20 - 90% of the residual peroxydisulfuric acid are hydrolyzed in each sump. The further hydrolysis of H.sub.2 S.sub.2 O.sub.8 to H.sub.2 SO.sub.5 and H.sub.2 SO.sub.4 improves the degree of oxidation. Besides, the volumes of the sumps can be dimensioned such that the higher SO.sub.2 content of the exhaust gases produced during the starting period of the contact process plant can be absorbed because an adequate supply of active oxygen is available.The included angle at the outlet of the vertical venturi tube and of the substantially horizontal venturi tube is 10.degree. - 20.degree., preferably 14.degree. - 17.degree.. As a result, the total gas pressure loss in the venturi tube is minimized and, in addition to the venturi effect proper, a turbulence is created to provide for an optimum gas-liquid interface allowing an optimum degree of oxidation.The gas is passed through the entire system with an average retention time of 2 - 4 seconds. This retention time allows a high degree of oxidation while keeping the dimensions of the equipment at a minimum.The withdrawn scrubbing acid which contains the oxidation product is supplied to the final absorber of the contact process plant. In this way, the residual active oxygen withdrawn from the system is utilized for an oxidation in the final absorber of the contact process plant and the content of oxidizable compounds in the exhaust gases is reduced before they enter the system.The quantity of peracids depends on the oxidation equivalent of the exhaust gas components to be oxidized and on the desired degree of oxidation and the desired purity of the exhaust gases.The packing layer in the tower has suitably a thickness of 40-80 centimeters. This results in a high degree of oxidation and in a relatively low gas pressure loss.The outlet opening of the tower is preceded by a wire mesh filter which provides for a good separation of entrained liquid in conjunction with a low pressure loss.The entire system can be made to a large extent from plastic or synthetic-resin material

    摘要翻译： 通过用由稀硫酸和过氧化二硫酸组成的洗涤溶液处理废气，可氧化形成硫酸的硫化合物和可氧化成CO 2和H 2 O的有机化合物从用于生产硫酸的接触工艺装置的废气中除去。 过氧化二硫酸由新鲜的稀硫酸电解产生，所得的电解质连续引入洗涤酸循环中。 废气在垂直文丘里管中处理，具有单流，即气体和洗涤溶液的顺向流动，然后气体通过水平文丘里管，然后通过填料层向上。

    Process for treating sulfide ores containing gold and/or silver and as accompanying metal at least iron
    36.
    发明授权
    Process for treating sulfide ores containing gold and/or silver and as accompanying metal at least iron 失效
    用于处理含有金和/或银的硫化矿石和至少铁的伴随金属的方法

    公开(公告)号：US5783158A

    公开(公告)日：1998-07-21

    申请号：US805462

    申请日：1997-02-25

    申请人： Michael Tacke ,  Walter Pierson ,  Eberhard Stolarski

    发明人： Michael Tacke ,  Walter Pierson ,  Eberhard Stolarski

    IPC分类号： C22B1/02 ,  C22B1/06 ,  C22B1/10 ,  C22B11/00 ,  C22B1/00 ,  C22B11/08

    CPC分类号： C22B1/10 ,  C22B1/06 ,  C22B11/04

    摘要： The ore which contains gold and/or silver and as accompanying metal at least iron is calcined at temperatures in the range from 500.degree. to 900.degree. C. with the addition of oxygen-containing gas. There is obtained a metal-oxide-containing solids mixture and a SO.sub.2 -containing exhaust gas. The solids mixture from the calcination is cooled, the temperature being reduced by at least 50.degree. C. The cooled solids mixture is added to a fluidized-bed reactor, and SO.sub.2 -containing exhaust gas is introduced into the fluidized-bed reactor. In the reactor, metal sulfate is produced in the solids mixture, so that at least 10% of the sulfur content are bound in the exhaust gas. Solids mixture containing metal sulfate is withdrawn from the fluidized-bed reactor, is stirred up with an aqueous acid solution, thereby dissolving metal sulfate. The remaining solids are supplied to a recovery of gold and/or silver.

    摘要翻译： 含有金和/或银以及至少铁的伴随金属的矿石在500-900℃的温度下煅烧，同时加入含氧气体。 得到含有金属氧化物的固体混合物和含SO 2的废气。 将来自煅烧的固体混合物冷却，将温度降低至少50℃。将冷却的固体混合物加入流化床反应器中，将含SO 2的废气引入流化床反应器中。 在反应器中，在固体混合物中产生金属硫酸盐，使得至少10％的硫含量结合在废气中。 从流化床反应器中取出含有金属硫酸盐的固体混合物，用酸水溶液搅拌，从而溶解金属硫酸盐。 剩余的固体被提供到金和/或银的回收。

    Process for treating gold-containing sulfide ores
    37.
    发明授权
    Process for treating gold-containing sulfide ores 失效
    处理含金硫化矿的方法

    公开(公告)号：US5804150A

    公开(公告)日：1998-09-08

    申请号：US805409

    申请日：1997-02-24

    申请人： Michael Tacke ,  Walter Pierson ,  Eberhard Stolarski

    发明人： Michael Tacke ,  Walter Pierson ,  Eberhard Stolarski

    IPC分类号： C22B1/02 ,  C22B1/10 ,  C22B11/00 ,  C22B1/00 ,  C22B3/00

    CPC分类号： C22B11/04 ,  C22B1/02

    摘要： The ore which contains gold and at least one of the metals silver, copper, nickel, zinc or iron is calcined at temperatures in the range from 500.degree. to 900.degree. C. with the addition of oxygen-containing gas, thereby producing a metal-oxide-containing solids mixture and a SO.sub.2 -containing exhaust gas. The SO.sub.2 containing exhaust gas is brought in contact with aqueous solution, thereby producing a sulfite-containing solution. The solids mixture from the calcination is cooled to temperatures in the range from 50.degree. to 300.degree. C. and is stirred up with the sulfite-containing solution. Metal oxides are dissolved, and a sulfate-containing solution os formed. In a first separating zone, the sulfate-containing solution is separated from the solids, and either the solids are supplied to a gold leaching or the sulfate-containing solution is subjected to a further treatment for the separation of nonferrous metals.

    摘要翻译： 含有金和银，铜，镍，锌或铁中的至少一种金属的矿石在加入含氧气体的同时在500-900℃的温度下煅烧， 含氧化物的固体混合物和含SO 2的废气。 使含SO 2的废气与水溶液接触，从而产生含亚硫酸盐的溶液。 将来自煅烧的固体混合物冷却至50℃至300℃的温度，并与含亚硫酸盐的溶液一起搅拌。 溶解金属氧化物，形成含硫酸盐溶液。 在第一分离区中，将含硫酸盐的溶液与固体分离，并将固体供应至金浸出，或者将含硫酸盐溶液进一步处理以分离有色金属。