Improved process for producing high purity lead

专利摘要:
A method is disclosed for the production of a purified soft lead product, comprising a) a first distillation step (200) for distilling lead from a molten solder mixture (6) to produce as a top stream a first concentrated lead stream (7), and as first bottoms (8) a molten crude tin mixture, and b) a soft lead refining step (700) for removing at least one contaminant selected from arsenic, tin and / or antimony from the first concentrated lead stream by treating the stream at a temperature of less than 600 ° C with a first base (24) and a first oxidant (25) that is stronger than air, resulting in the formation of a third supernatant scratch (26) containing a metalate compound of the impurity, followed by separating the third supernatant scratch (26) from the purified soft lead stream or the purified soft lead product (27), wherein the third supernatant scratch (26) from step (b) is at most contains 1.0% by weight of chlorine.
公开号:BE1027002B1
申请号:E20205055
申请日:2020-01-30
公开日:2020-08-28
发明作者:Koen Govaerts；Pelle Lemmens；Bert Coletti；Jan Dirk A Goris；Charles Geenen；Kris Mannaerts；Visscher Yves De
申请人:Metallo Belgium；
IPC主号:

专利说明:

BE2020 / 5055 Improved process for producing high purity lead
FIELD OF THE INVENTION The present invention relates to the production by pyrometallurgy of non-ferrous metals, in particular lead (Pb), and optionally in combination with the production of copper (Cu) and tin (Sn), from primary sources and / or secondary basic materials. More specifically, the present invention relates to the production and recovery of a high purity lead product from a mixture containing predominantly lead and tin.
BACKGROUND OF THE INVENTION The metal lead is an important non-ferrous raw material in modern industry, and has been since ancient times. Today's lead market is mainly based on its use in the lead battery, and in particular the lead acid battery. The use of lead in other areas of application including lead sheet for construction, lead as a radiation barrier, as dead weight, as protection for underwater cables, as ammunition and as an alloy metal in brass, is insignificant to its use in the car -industry. Lead has been mined since 5000 BC, from the ancient Egyptians; For centuries it was extracted from primary raw materials, mainly galena (lead sulphide - PbS). Minerals rich in lead are common with other metals, especially silver, zinc, copper, and sometimes gold. In modern society, lead has also become the most recycled of all commonly used metals. Lead is also often present in secondary base materials, in combination with other metals. For example, the lead present in brazing materials is combined with significant amounts of other metals, mainly tin, and hard lead can easily contain up to 10% by weight of other metals, of which antimony is the most common. The recovery of high purity lead products from primary and secondary feedstocks therefore requires the refining of a mixture of lead with other nonferrous metals in order to obtain a high purity lead product.
Ancient processes used air, at sufficiently high temperatures, to oxidize the contaminants such as arsenic, antimony, tin, zinc and other easily oxidizable metals, as part of the process of “softening or improving” lead. However, a large part of the lead is oxidized at the same time in that method. Henry Harris describes, in British patent GB 189013 and US patent US 1573830, and with reference to US patent US 1674642, a process for the more selective removal of small amounts of As, Sn and / or Sb at "low" temperatures, ie about 450 ° C. The gradual addition of a sufficiently strong oxidizing agent, more specifically NaNO3, in addition to the NaOH and NaCl already in contact with the raw lead, allows the formation of oxides of the impurities while minimizing lead oxidation. limited. After the treatment step, the caustic melt phase, including the contaminants in an oxidized form, is contacted with water. The remaining NaOH and NaCl form the molten solute and, along with the oxi salts formed, end up in the aqueous by-product.
The sodium chloride in the resulting caustic soda solution is believed to lower the solubility of the antimony compound in this solution. When the molten mass from the lead treatment is dissolved in water, and the resulting aqueous solution is saturated with sodium chloride, as is preferred, then substantially all of the antimony compound remains insoluble in the solution, and precipitates substantially completely as a separate phase. Therefore, in the lead treatment, a large amount of sodium chloride is added, preferably more than required for saturation, as used in the examples, although it is indicated that more sodium chloride can be added to the solution. The tin and arsenic compounds are reported to remain soluble in solution. For more details on the caustic molten mass processing, reference is made to USSN 1923/0676261, later published as US Patent US 1674642. Patent US 1674642 describes a number of wet chemical processes involving at least 4 and up to 7 steps, generating the following product streams: (i) lead granules, (ii) oxal salt of Sb, (iii) oxal salts of As and Sn, (iv) NaCl crystals and (v) sodium hydroxide solution. Optionally, the oxide salts of As and Sn (iii) can be further processed, using CaCO 3 and / or CaO, to recover the Sn and As separately as deposits, leaving a new caustic soda solution. Both caustic soda solutions are considered suitable for recirculation to the lead refining process. All process steps involve solid / liquid separations, and many of them also include salt crystallizations, all requiring long residence times, and thus long hold times and volumes in the equipment, optionally in combination with complex equipment such as centrifuges or filtration.
The sodium chloride is disclosed in U.S. Patent No. 1573830 to also mechanically aid in separating the insoluble antimony compounds from the resulting solution by causing the sediment to settle more easily by gravity or to precipitate in a better physical form.
U.S. Patent No. 1,779,272 describes a simplified wet chemical process for the selective recovery of sodium stannate, sodium arsenate and sodium antimonite from a salt mixture resulting from the purification of lead by the "so-called Harris process". The starting material is stated to contain sodium chloride and water.
Another effect of the sodium chloride is, according to U.S. Patent No. 1573830, to increase the viscosity of the molten alkaline hydroxide mass, which is described as an advantage when the molten lead is circulated in the molten reagent. We believe that the presence of NaCl also lowers the melting temperature of the mixture.
In British Patent GB 189013 and US Patent US 1573 830, as well as in US Patent US 1674642, the presence of sodium chloride is considered highly desirable and is present in all examples.
U.S. Patent No. 3,479,179, as an alternative to the Harris process, describes a continuous lead refining process for removing the impurities tin, antimony, zinc and arsenic.
The method described comprises 3 steps, in which each time the liquid lead is brought into intimate contact with a supernatant layer of molten sodium hydroxide.
In the first step, access to oxygen is prevented by the addition of a protective gas, and at a temperature of 420 ° C, only As and Zn are selectively removed largely in a precipitating slag phase, alleged by the formation of sodium zincate and sodium arsenate .
In step 2, under an oxygen atmosphere of 16% and also at 420 ° C, tin is selectively oxidized and can be removed.
In step 3, under an oxygen atmosphere of 26% and at 500 ° C, antimony is oxidized.
The removal rates achieved for As, Zn, Sn and Sb are 98%, 98%, 80-90% and 80%, respectively. The slags formed in each process step can be withdrawn, preferably from a slag recirculation system in place in each of the steps, and "taken to further processing". The document does not mention what that further processing would be.
The process yields 3 separate slag phases, each with a high concentration of a different metal (or metals). That means that the slag phases are further processed along different process paths.
In all of the above-described processes, the recovery of at least one of the contaminating metals (and lead in oxidized form) would still require the reduction of the metals from their oxy salt form.
The inventors have found that the presence of NaCl in the "Harris" process, according to the cited documents, significantly limits the further processing of the caustic molten mass or any of its oxalate containing derivatives for the recovery of some or all of it. its components, especially when it involves at least one pyrometallurgical step.
Another disadvantage of the conventional Harris process and its alternatives for lead purification is their complexity, the use of large amounts of chemicals and energy in the processing of the caustic molten mass, while the recovered metals (Sb, Sn and As ) arise from them in their oxide salts or other solid precipitated forms, and not yet as metal.
At a secondary level, the cumulative amounts of chemicals added, the consumption of which may be spread over several consecutive iterations to obtain the desired lead purity, are thus significantly higher than the stoichiometric amount. The object of the present invention is to reduce the consumption of chemicals per tonne of pure ("soft") lead produced.
The consumption of chemicals in the "Harris" process or equivalent processes represents a significant economic burden. In addition, where the scratch is recycled upstream in the process, such as in a top blown rotary converter or top blown rotary converter (TBRC), at the point where the slag contains most of the PbO and SnO: , is reduced to form a mixture of predominantly lead and tin often referred to as crude solder, the sodium hydroxide is corrosive to the refractory materials used in the upstream metallurgical process steps when in contact with the hot liquid streams.
It is an object of the present invention to obviate or at least alleviate the above-described problem, and / or to provide improvements in general.
SUMMARY OF THE INVENTION According to the invention there is provided a method as defined in any of the appended claims.
In one embodiment, the present invention provides a process for the production of a purified soft lead product, comprising) a first distillation step of distilling lead from a molten solder mixture comprising lead and tin to produce as the overhead product a first concentrated lead stream, and as a first bottom product, a molten crude tin mixture, and b) a soft lead refining step for removing at least one impurity selected from the metals arsenic, tin and antimony from the first concentrated lead stream obtained in step a) by treating the first concentrated lead stream at a temperature of less than 600 ° C with a first base and a first oxidant stronger than air, resulting in the formation of a third supernatant scratch containing a metalate compound of the respective contaminant metal, followed by the separation of the third supernatant scratch of the purified soft lead stream or the purified soft lead product, wherein the third supernatant scratch from step (b) contains up to 1.0% by weight of chlorine, and preferably up to 1.0% by weight of total halogens.
Applicants have found that, in the process for producing a purified lead soft product from a molten solder mixture of tin and lead, the precursor of the chemical treatment step (b) by the first distillation step (a), wherein the first distillation step is the first concentrated lead stream, to be further purified, as top condensate, has the advantage of reducing the amounts of chemicals and energy required in the chemical treatment step to obtain a soft lead end product.
An additional advantage is that the process of the present invention is capable of incorporating much more tin into the base stock, compared to the Harris process and its alternatives known in the art and described above. A further advantage is that most of the tin in the process of the present invention is kept in its elemental metal form, and is not converted to a chemically bonded form. As will be seen, the process of the present invention can easily form part of a general process which also produces a high purity high quality tin product. Thus, the additional advantage of the process of the present invention is that most of the tin in the process is made available in a more concentrated form which is better suited as a starting base for the recovery of a high purity high quality tin product.
In the first distillation step (a), most of the tin in the feed stream ends up in the first bottoms product. In addition, significant amounts of As and Sb also tend to remain together with the tin in the first bottoms from first distillation step (a). Applicants have found that the distillation conditions in step (a) can be further selected such that even smaller amounts of the As, Sb and / or Sn in the feed stream end up in the overhead stream as a first concentrated lead stream.
Another advantage of the method of the present invention is that the first bottoms product of step (a), which contains most of the tin and a large proportion of any other impurities, is made available as a molten liquid stream of elemental metals. Only a small portion of the tin, arsenic and antimony present in the feed to step (a) ends up in a chemically bound form as part of the third supernatant scratch obtained from step (b). This is very beneficial for the recovery and upgrading of any of these elements, compared to the methods described in the art.
It will be explained later in this document that the first bottoms product from step (a) can be a high quality candidate for the further recovery of non-ferrous metals, initially a high quality tin product. It will also be appreciated that a larger amount of As and / or Sb remaining together with the Sn in the first bottoms product of step (a) does not necessarily lead to a higher consumption of chemicals further downstream.
The present invention has the additional advantage of reducing complexity in the recovery of the metals removed from the first concentrated lead stream by soft lead refining step (b).
Applicants have found these advantages to be particularly important in producing a soft lead end product as a by-product of non-ferrous metal production from secondary feedstocks, especially copper production.
As explained below in the detailed description section, the third supernatant scratch produced in step (b) contains the removed at least one impurity selected from arsenic, tin and antimony as a metalate compound thereof. The third supernatant scratch may further contain residual plumbate, a compound that can be formed as an intermediate in the step of removing impurities, and of which an excess can form, and therefore a surplus. The third supernatant scratch is formed in step (b) as a solid that floats on the molten lead below. When this scratch is removed from the liquid bath, a, albeit quite limited, amount of lead is usually also entrained. Thus, the third supernatant scratch also contains lead metal, because the separation of the scratch from the liquid is usually not quite ideal, and upon separation preferably some lead metal remains in the third supernatant scratch rather than scratch in the high purity lead product.
Thus, the third supernatant scratch also contains interesting metals, in particular lead and / or tin, in quantities that make their recovery interesting for economic and ecological reasons. The third supernatant scratch is therefore preferably recycled upstream of the process of the present invention, in a suitable pyrometallurgical step that is part of the upstream process that produces the lead / tin mixture used as the feedstock for the first distillation step (a).
Applicants have found that the stated low content of chlorine and / or other halogens in the third supernatant scratch makes the third supernatant scratch more suitable to be introduced in a pyrometallurgical process step, preferably in a process step in which at least one of the sodium metalates of Sn , Sb and As can be reduced to the respective metal Sn, Sb or As, preferably also getting the Pb in its elemental form.
The third supernatant scratch is more acceptable in the pyrometallurgical process step due to its limited chlorine and / or halogen content.
The low chlorine content of the third supernatant scratch reduces the risk of valuable metals being entrained in the exhaust gas from a pyrometallurgical process step in which an exhaust gas is produced, and thus the risk of sticky solid deposits forming on coolers, filters and other items equipment in the exhaust gas treatment equipment associated with such a pyrometallurgical process step.
It is expected that the metals Sn, Sb and / or As recovered from the recycled third supernatant scratch, and the associated Pb, will become part of the feed to first distillation step (a). In the first distillation step (a), that extra Pb mainly ends up in the first concentrated lead stream as top condensate and in the high quality “soft” lead metal product derived therefrom, and the majority of the Sn and Sb metals, as well as a significant amount of the As metal, preferably remains in the Sn-containing first bottoms stream.
A significant part of these metals therefore no longer return as contaminants in soft lead refining step (b). The contaminating metals recovered from the recirculation of the third supernatant scratch can then be easily upgraded by conventional means, and upgraded to give them economic value.
For example, the recovered Sn can be recovered as part of a highly purified Sn metal final product obtained from the first bottoms product remaining from first distillation step (a). The advantage of this scratch recycle capacity is that it allows for a general process of much lower complexity, especially when compared to the highly complex wet chemical recovery pathways described in U.S. Patent No. 1,674,642 and discussed above.
The ability of the third supernatant scratch to be recycled to a pyrometallurgical process step enables the process of the present invention to simultaneously remove, in a single process step (b), more than one contaminant from the first concentrated lead stream. This represents a significant improvement over the many complex lead refining steps described in the art.
Another effect of the method of the present invention is a lower consumption of chemicals per unit weight of lead supplied to soft lead refining step (b). Applicants have found that, in comparison with British Patent GB 189013, US Patent US 1573830 and US Patent US 1674642, the consumption of chemicals can be significantly reduced in most circumstances. Initially, the process of the present invention does not require the addition of significant amounts of sodium chloride, an additional compound which is highly desirable (especially in U.S. Patent No. 1573830) because of its beneficial effects in further processing the caustic molten mass from the chemical treatment of the lead stream.
In the first distillation step (a), many of the contaminants commonly present in lead production tend to remain in the bottom stream. The upstream first distillation step (a) therefore already functions as a partial purification step for the lead product. This additional process step thus reduces the load on soft lead refining step (b), resulting in a lower consumption of chemicals relative to the amount of high quality soft lead metal product obtainable from soft lead refining step (b).
In addition, in first distillation step (a), taking into account their respective presences in the feed and bottom streams, there is relatively more tin (Sn) going into the first concentrated Pb overhead stream, as compared to antimony (Sb). The vapor pressure of Sb is higher than that of Sn under the distillation conditions, but the concentration of Sn in the liquid phase is significantly higher, usually an order of magnitude higher, than that of Sb. Another reason is that, under the distillation conditions, Sb tends to form metal-metal bonds with Sn, and the bound Sb is not available for evaporation. These factors explain why, relative to their presence in the feed and / or bottoms residue from first distillation step (a), Applicants generally find much more Sn than Sb in the first concentrated lead overhead stream. Sn is more reactive in soft lead refining step (b), and therefore easier to remove in step (b), than Sb. The presence of first distillation step (a) upstream of soft lead refining step (b) thus facilitates step (b), as it not only affects the amounts thereof reaching the first distillation step (a), as explained above, but also affects its nature. of impurities present in the feed to soft lead refining step (b), and more particularly yields a mixture of impurities that is easier to remove, due to the relatively lower presence of Sb as compared to Sn.
BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 shows a flow chart of a larger general method comprising a preferred embodiment of the method of the present invention.
DETAILED DESCRIPTION The present invention will be described below in specific embodiments and with possible reference to specific drawings; however, it is not limited thereto, but is determined solely by the claims. The drawings described are only schematic and are non-limiting. In the drawings, the size of some elements may be enlarged for illustrative purposes and not drawn to scale. The dimensions and relative dimensions do not necessarily correspond to actual practical embodiments of the invention.
Furthermore, the terms first, second, third, and the like, are used in the specification and claims to distinguish between similar elements, and not necessarily to describe a sequential or chronological order. The terms are interchangeable in appropriate circumstances, and the embodiments of the invention may function in sequences other than those described or illustrated herein. Furthermore, the terms top, bottom, top, bottom, and the like are used in the description and claims for descriptive purposes, and not necessarily to describe relative positions. The terms so used are interchangeable in appropriate circumstances, and the embodiments of the invention described herein may function in orientations other than those described or illustrated herein.
The term "comprising", as used in the claims, is not to be construed as being limited to the means enumerated in its context. He does not exclude other elements or steps. The term should be interpreted as the required presence of the listed properties, numbers, steps or components, but does not preclude the presence or addition of one or more other properties, numbers, steps or components, or groups thereof. Thus, the scope of the phrase "an item comprising means A and B" need not be limited to an article composed only of components A and B. It means that in the context of the present invention, A and B are the only relevant components. Accordingly, the terms "comprise" or "include" also include the more restrictive terms "consist essentially of" and "consist of". Accordingly, when “comprise” or “contents” is replaced by “consist of”, these terms represent the basis of preferred, but constrained embodiments, which are also provided as part of the contents of this document relating to the present invention.
Unless otherwise specified, all value ranges set forth in this document include the range up to and including the indicated endpoints, and the values of the ingredients or components of the compositions are expressed in weight percent, or weight%, of each ingredient in the composition.
Terms such as "weight percent," "weight%" "weight%" "percent by weight," "% by weight", "ppm by weight", "ppm by weight", "ppm by weight", "wt. ppm ”or“ ppm ”and variations thereof, as used in this document, refer to the concentration of a substance as the weight of that substance divided by the total weight of the composition and multiplied by 100 or one million, as appropriate case, unless otherwise noted It should be understood that the terms "percent", "%," used herein are intended to be synonyms of "percent by weight", "percent by weight", etc.
It should further be noted that, in the present description and the appended claims, the singular forms “a”, “the” and “it” may also refer to plural matters, unless the contents clearly indicate otherwise. For example, reference to a composition comprising "a compound" includes a composition having two or more compounds. It should also be noted that the term "or" is generally used in the sense that "and / or" implies, unless the content clearly indicates otherwise.
Furthermore, each compound used here can be interchangeably discussed by its chemical formula, chemical name, abbreviation, etc.
Most of the metal streams in the process of the present invention contain a high proportion of lead, often in combination with a significant amount of tin. Such currents have a relatively low melting point and have been used for centuries to attach one solid to another solid, through a process often referred to as “soldering”. Such currents are therefore often referred to as so-called "solder" currents or "solder", and that term is also used in this document to designate such currents.
Among the target metals recovered by the present invention, Sn and Pb are considered as "the brazing metals". These metals are distinguished from other metals, especially copper and nickel, in that mixtures containing large amounts of these metals generally have a much lower melting point than mixtures containing large amounts of copper and / or nickel.
Such compounds were used millennia ago to form a permanent bond between two pieces of metal by first melting the “solder”, then applying and solidifying.
To this end, the solder had to have a lower melting temperature than the metal of the pieces that were connected by it.
In the context of the present invention, by a solder product or a solder metal composition, two terms used interchangeably herein, are meant metal compositions in which the combination of the solder metals, i.e. the content of Pb plus Sn, makes up the majority of the composition, ie at least 50% by weight and preferably at least 65% by weight. The solder product may further contain minor amounts of the other target metals copper and / or nickel, and non-target metals such as Sb, As, Bi, Zn, Al and / or Fe, and / or elements such as Si.
Unless otherwise noted, amounts of metals and oxides in this document are expressed in accordance with common pyrometallurgic practice.
The presence of each metal is generally expressed as its total presence, regardless of whether the metal is present in its elemental form (oxidation state = 0) or in a chemically bound form, usually in an oxidized form (oxidation state> 0). For the metals which can be relatively easily reduced to their elemental form, and which can exist as molten metal in the pyrometallurgical process, it is quite common to express their presence in terms of their elemental metal form, even when the composition of a slag or scratch is indicated, where the majority of such metals may in fact be present in an oxidized and / or chemically bound form.
Therefore, in the composition of the metal mixture as feed to step (a), the content of Fe, Zn, Pb, Cu, Sb, Bi is expressed as elemental metals.
Less noble metals are more difficult to reduce under nonferrous pyrometallurgical conditions and occur mostly in an oxidized form. These metals are usually expressed in terms of their most common oxide form. Therefore, in slag or scratch compositions, the content of Si, Ca, Al, Na is usually expressed as SiO2, CaO, Al2O3, Na2O, respectively. In soft lead refining step (b), the crude Pb feed stream is preferably contacted with a combination of NaOH and NaNO3. The chemical process aimed at with these chemicals can be represented by the following reactions: 5 Pb + 6 NaOH + 4 NaNO: 3 -> 5 Na2PbO3 + 2 Ns + 3 H: O (1) 5 Nas2PbOs + 4 As + 2 NaOH -> 4 NasAsO4 + 5 Pb + H: O (I) Na2PbOs3 + Sn -> Na2SnO3 + Pb (II) 5 NazPbO; + 3 H2O + 4 Sb -> 4 NaSbO3 + 6 NaOH + 5 Pb (IV) Crucial to this chemical process is the formation of the intermediate sodium plumbate (Na: PbOs) by reaction (|). This plumbate intermediate is capable of reacting with the impurities As, Sn and Sb according to the respective reactions (II) to (IV) and entraps them each time in the respective sodium metalate compound, while releasing the Pb again. The sodium metalate compounds formed are sodium arsenate, sodium stannate and sodium antimonate, respectively.
The respective sodium metalate compounds collect in a supernatant phase, commonly referred to as the "scratch" or sometimes also "slag". Those terms are often used interchangeably, although the term "slag" is generally used for a liquid phase, while "scratch" usually means a phase of a less fluid, firmer consistency.
The term "slag" is more common in the context of the production of nonferrous metals with a high melting point, such as copper, and thus usually refers to a fluid, which often mainly comprises metal oxides. The term "scratch" is more commonly used in the context of lower melting point non-ferrous metals such as Sn, Pb, Zn, Al, which are often in solid or dust form. However, the boundary between these two terms in terms of consistency is not always clear.
The scratch from soft lead refining step (b) can be scraped off, and can be further processed to recover at least some of its components.
In one embodiment of the method according to the present invention, the soft lead refining step (b) is performed at a temperature of at most 550 ° C, preferably at most 500 ° C, more preferably at most 450 ° C and optionally at least 370 ° C , preferably at least 390 ° C, more preferably at least 400 ° C. Respecting the stated temperature upper limit has the advantage that the feed stream, since that stream usually becomes available from the first distillation step (a) at a temperature of about 960-970 ° C, is cooled. This cooling has the advantage that copper that may have ended up in the top condensate of the first distillation step (a) can come out of solution and can float to the top, so that it can be removed by skimming, possibly together with the skimming of the third. supernatant scratch. Performing this step at a temperature that meets the lower limit brings the advantage of faster reaction kinetics. Any additional copper remaining after cooling and skimming can be removed by adding sulfur to form a scratch containing CuS, as well as skimming off that scratch containing CuS from the liquid metal.
In one embodiment of the method of the present invention, Applicants preferably use a strong oxidant as the first oxidant of soft lead refining step (b). Preferably the first oxidant in soft lead refining step (b) is selected from NaNO3, Pb ({NO: 3) 2, KNO: 3, ozone, nitric acid, sodium and potassium manganate, sodium and potassium (per) manganate, chromic acid, calcium carbonate ( CaCO3), sodium and potassium dichromate, preferably NaNO: 3, CaCO3, Pb (NOs) 2 or KNO3, more preferably NaNO :. Applicants preferably use an oxidant stronger than air containing 21% oxygen by volume. Applicants have found that the selection of a sufficiently strong oxidant, such as the elements in the proposed list, has the advantage of speeding up the desired chemical processes. The higher reaction kinetics has the advantage that a shorter residence time is required to achieve a desired conversion, such that a smaller reaction vessel can be used, or that a given reaction vessel can handle a higher flow rate.
In the process of the invention, due to the nature of first distillation step (a), there is always a trace of it present in the lead concentrate to be treated in soft lead refining step (b), and usually at least one of the other impurities is also present. such as arsenic, antimony or zinc. In particular, a small amount of antimony is usually also present when the method is based on secondary base materials. The method of the invention does not intend to selectively remove the contaminants where more than one is present. The method aims at the simultaneous removal of all impurities together capable of participating in the reaction chemistry. Only one third supernatant scratch is formed in soft lead refining step (b), which is removed as a single by-product from the process, and made available for recycling, preferably in a pyrometallurgical process step somewhere upstream of first distillation step (a). This object entails the advantage that a strong oxidant, which need not exhibit selectivity, nor be made selective, is acceptable for a specific element of the group Zn, As, Sn and Sb.
In one embodiment of the process of the present invention, Applicants preferably use a strong base as the first base of soft lead refining step (b). Preferably the first base in soft lead refining step (b) is selected from NaOH, Ca (OH): and Na: CO: and combinations thereof, preferably NaOH. Applicants have found that the use of a strong base contributes to fast reaction kinetics and thereby allows smaller reaction equipment and, consequently, lower capital costs. Because the process does not require selective removal of any of the target impurities, the first base need not exhibit, nor be made selective, for a specific element of the group Zn, As, Sn and Sb. Applicants prefer a (hydr) oxide as the first base because it avoids extraneous by-products such as CO 2.
The build-up of carbon dioxide leads to foaming on the bath and to the creation of a scratch of much greater volume, which can spill over the edge and pose a safety risk.
Applicants prefer to use NaOH because it does not generate carbon dioxide like sodium carbonate, and because of its wider availability.
Applicants prefer to use solid sodium hydroxide in soft lead refining step b) as it facilitates phase separation between the mass to be skimmed and the molten lead stream.
Sand can be added to stiffen the scratch and make it easier to remove.
Applicants have found that NaOH as the first base has the advantage of promoting agglutination of the floating scoop masses, which facilitates the selective removal of the third supernatant scratch.
In one embodiment of the process according to the present invention, in addition to NaOH and NaNOs, an amount of Ca (OH) 2 is also added as a reagent in soft lead refining step (b). Applicants have found that this improves the physical characteristics of the scratch as it becomes "drier" and less adheres to the equipment.
A "drier" scratch is a scratch that contains less liquid, the latter being entrained molten lead from the underlying liquid phase.
A "drier" scratch therefore brings the advantage of an improved separation between lead and scratch, and that less (metallic) lead is removed with the third supernatant scratch and has to be recovered.
In one embodiment of the method of the present invention, the weight ratio of the first base to the first oxidant used in soft lead refining step (b) is in the range of 1.5: 1.0 to 4.0: 1 , 0, preferably in the range of 2: 1 to 3: 1 when NaOH is used as the first base and NaNO: 3 is used as the first oxidant, respectively, and recalculated by stoichiometry for when other compounds are used as first base and / or first oxidant.
Alternatively, Applicants prefer to use a molar ratio of the first base to the first oxidant in the range of 3.18-8.5, preferably 4.25-6.38. Applicants have found that respecting this prescribed range for the ratio of first base to first oxidant has the advantage that the viscosity of the third supernatant scratch is sufficiently high, but that the scratch does not become too hard.
In one embodiment of the method of the present invention, the weight ratio of the first base to the first oxidant used in soft lead refining step (b) is at most 2.90, preferably at most 2.80, more preferably at most 2.70, even more preferably at most 2.60, preferably at most 2.50, more preferably at most 2.40, even more preferably at most 2.30, preferably at most 2.25, with more preferably at most 2.20, even more preferably at most 2.15, preferably at most 2.10, more preferably at most 2.05, even more preferably at most 2.00.
These limits apply to NaOH as the first base and NaNO: as the first oxidant, and can be converted by stoichiometry if one or more other compounds are used. The limits can also be converted to a molar ratio using the factor “85/40. Applicants prefer to keep the amount of first base, and in particular the amount of NaOH, limited in view of recycling the third supernatant scratch to an upstream metallurgical process step, and because the NaOH or other strong base is corrosive. is for the refractory lining of the equipment of that step. Less NaOH or less of the other base can therefore result in less wear and tear and damage to the refractory lining of the equipment to which the third supernatant scratch is recycled.
In one embodiment of the process of the present invention, the first bottoms residue or product of first distillation step (a) remains at least 0.10% by weight of lead, preferably at least 0.20% by weight, more preferably at least at least 0.10% by weight. at least 0.30 wt%, even more preferably at least 0.50 wt%, preferably at least 0.60 wt%, more preferably at least 0.70 wt%, even more preferably at least 0.80% by weight, preferably at least
0.90% by weight, preferably at least 1.00% by weight, more preferably at least 1.5% by weight, even more preferably at least 2.0% by weight, preferably at least 3.0 wt%, more preferably at least 4.0 wt%, even more preferably at least 5.0 wt%, and even more preferably at least 6.0 wt% lead. Applicants have found that maintaining the prescribed minimum amount of lead in the first bottoms residue or product from first distillation step (a) has the advantage that less of the tin, arsenic and antimony will enter the feed to step (a) in the first concentrated lead stream as top condensate which is treated in soft lead refining step (b). This brings the advantage that chemical and energy requirements in step (b) per processed unit weight of soft lead in step (b) are reduced compared to a method in the art that does not meet the requirements of the method of the present invention. invention.
Applicants believe that higher levels of Pb remaining in the Sn product from the first distillation step (a) can act as an additional solvent, for example for the amount of antimony that may be present in the feed to the first distillation step. This influence on the solubility can be advantageous for the separation in the first distillation step (a). An important purpose of the first distillation step (a) as part of the process of the present invention is to vaporize lead (Pb) and produce a lead-containing overhead product suitable for subsequent purification by conventional means to produce a product of produce high purity lead called “soft lead”. Applicants believe that leaving a quantity of lead in the first bottoms of the first distillation stage (a) helps to achieve that goal, by providing a liquid phase that remains attractive to many of the metals other than lead, and thereby tends to reduce those metals to volatilize, as well as their tendency to escape from the liquid phase and end up in the top product of the first distillation step (a). Applicants believe that this beneficial effect is enhanced by leaving a higher concentration of lead in the first bottoms from the first distillation step (a). Applicants believe that this beneficial effect is particularly important for any antimony present in the feed to the first distillation step (a) of the process of the present invention.
Applicants have further found that the problems of metal-metal compound formation in first distillation step (a), as described elsewhere in this document, are further alleviated by leaving a greater presence of lead in the first bottoms of the first distillation step ( a). Applicants believe that the increased amount of lead remaining in the liquid phase in the distillation equipment has a beneficial effect in better keeping the potentially harmful metals in solution and reducing their tendency to form the potentially nuisance metal-metal compounds during the initial distillation step ( a). Without being bound by theory, Applicants believe that this effect may be based on dilution, but Applicants believe that other factors may play a role in lowering the risk of metal-metal compound formation under the conditions at hand. in the first distillation step (a). In one embodiment, the first bottoms product obtained in the first distillation step (a) by the removal of lead comprises at most 10.0% by weight of lead, preferably at most 9.0% by weight of lead, more preferably at most 8 0 wt%, even more preferably at most 7.0 wt%, preferably at most 6.5 wt%, more preferably at most 6.0 wt%, even more preferably at most 5, 0 wt% and even more preferably at most 4.0 wt% lead. Applicants have found that not exceeding this prescribed level of lead in the first bottoms product of the first distillation step (a) downstream has the advantage that it facilitates further separation of the different metals present in the first bottoms product to obtain a obtain a high quality tin product that meets most of the international industry standards for high quality tin. The applicants have further found that keeping the lead content within the prescribed limits under control achieves a practical and economic balance between the benefits derived from the presence of lead in the liquid throughout the first distillation step (a), and the downstream task of upgrading the first bottoms product of the first distillation step (a) to at least one high quality tin product of high value in combination with one or more by-products containing the other metals present in the first bottoms product, such by-products being suitably are for further processing and trouble-free upgrading to high-quality by-product streams.
Applicants have further found that a limited presence of lead in the first bottoms product is advantageous if precious metals are also present, and those precious metals must be recovered from the first bottoms stream or the first bottoms downstream of the first distillation step (a).
Such recovery can be carried out, for example, in a crystallizer, as described in patent CN102534249 for removing silver from a crude tin product having a high content of silver, which can thus separate a first tin-enriched product from a first silver-enriched liquid tapping product. in which the precious metals are concentrated along with most of the lead present, but in which inevitably also some of the more valuable tin remains.
Applicants have found that limiting the amount of lead remaining in the first bottoms product from the first distillation step (a) decreases the amount of first silver-enriched liquid draw-off product in such a crystallizer and results in a first silver-enriched liquid draw-off product of higher concentration of the desired precious metals, which is consequently more interesting for further processing for the recovery of the precious metals.
An additional advantage is that less of the valuable tin is lost in the first silver-enriched liquid tap product and remains available in the stream leading to the high-quality tin product.
Maintaining the prescribed amount of Pb, together with the higher amount of Sb present as a result, in the Sn-rich first bottoms or residue from first distillation step (a), yields a stream suitable for the downstream combined production of a pure Sn product together with a hard lead stream (mainly Pb, with significant amounts of Sb), for example by distilling a mixture of Pb and Sb as the top product away from a high purity Sn bottoms in a second distillation step.
If this second (Pb / Sb) top product is to be further purified, a "Harris" type process can again be used, but this second "Harris" type process step in the production of hard lead can then only be used. focused on the removal of the remaining traces of Sn and / or As, and not the Sb, as a significant level of Sb may be acceptable in the final hard lead product.
In the "Harris" type process, the Sb is the most difficult to remove, while Sn is easier to oxidize.
The present invention therefore leads to an overall reduction in the consumption of chemicals, also in this arrangement, producing a "hard lead" in combination with pure Pb and pure Sn as the other high performance products.
An additional advantage of the present invention is that it provides an outlet for any Sb present in the solder stream, preferably an outlet in which the Sb can have beneficial effects on performance, and therefore extra-economic value.
Maintaining the prescribed amount of Pb in the Sn-rich first bottoms residue or product from first distillation step (a) has the added advantage that, when silver or other precious metals (PMs), including platinum group metals (PGMs), present in the feed to first distillation step (a), more of the silver and the other PMs remains with the first bottoms residue or product from first distillation step (a) and less of it ends up in the first concentrated lead stream as the top stream.
Techniques are known to recover silver and / or PMs from a lead concentrate, such as the so-called “Parkes” process, which involves the addition of zinc, but they are complex and expensive, they generate by-products containing the removed metals in chemically bound form .
The techniques in question require further processing steps, and can only be justified if sufficiently high levels of such metals are present.
Thus, silver or PMs in the first concentrated lead stream to soft lead refining step (b) are difficult to recover, and small amounts of it usually end up as a trace component in the soft lead product, where they do not contribute economic value.
Silver or PMs in the first bottoms residue or product from first distillation step (a) can be more easily recovered and upgraded, for example in the manner described elsewhere in this document and in the example.
Applicants have further found that the presence of the prescribed amount of lead in the silver and / or PM recovery step downstream on the first bottoms residue or product of first distillation step (a) brings a number of significant benefits to the performance of that recovery step , and as for the by-product obtainable from that step, which also makes it easier to further process that by-product.
In one embodiment of the process of the present invention, the first concentrated lead stream entering soft lead refining step (b) comprises at least 0.0400% by weight and at most 0.3000% by weight tin.
Applicants prefer to have in this stream at least 0.0500% by weight of tin, preferably at least 0.0700% by weight, more preferably at least 0.0800% by weight, more preferably at least 0.0900 weight%, even more preferably at least 0.100 weight% tin.
Optionally, applicants prefer to have at most 0.2500 wt% tin present, preferably at most 0.2250 wt%, more preferably at most 0.2000 wt%, even more preferably at up to 0.1500% by weight of tin.
Applicants have found that the prescribed amount of tin in the top stream from first distillation step (a) represents an advantageous balance between the amount of Sn to be removed in step (bp) and the amounts of Sb still ending up in soft lead refining step (b) and should are removed in soft lead refining step (b) to obtain a high quality soft lead.
Sn is easier to remove in soft lead refining step (b) than Sb because it reacts more readily (III or IV) to form the corresponding sodium metalate.
In one embodiment of the method of the present invention, the third supernatant scratch from soft lead refining step (b) contains less than 1.0% by weight of chlorine, the third supernatant preferably having a chlorine content of at most 0.75% by weight, more preferably at most 0.50% by weight, even more preferably at most 0.25% by weight, preferably at most 0.20% by weight or 2000 ppm by weight, preferably at most 900 ppm by weight, more preferably at most 800 ppm by weight, even more preferably at most 700 ppm by weight, preferably at most 600 ppm by weight, more preferably at most 500 ppm by weight, even more preferably at most 400 ppm by weight , preferably at most 300 ppm by weight, more preferably at most 200 ppm by weight, even more preferably at most 100 ppm by weight.
Preferably, this upper limit applies to all halogens in total.
Applicants have found that soft lead refining step (b) as part of the present invention can be performed without the addition of NaCl, as described in British Patent GB 189013, United States Patent US 1573830 and US Patent US 1674642. Applicants have found that the Recovery of the metal values from the third supernatant scratch from soft lead refining step (b) is possible via different process paths than those described in the art, with steps that do not require the sodium chloride to enable or improve their performance.
Applicants prefer to introduce the third supernatant scratch from soft lead refining step (b) in a pyrometallurgical process step in which - on the contrary - the presence of sodium chloride and / or other halogen containing compounds is preferably low, and those compounds more preferably substantially to be absent.
Applicants have found that in a pyrometallurgical process step, chlorine can form metal chlorides of various valuable metals and that many of those chlorides are quite volatile under the operating conditions of such process step.
The chlorides, like other halogens, escape together with the exhaust gas from the melting furnace, condense in the exhaust gas treatment system on refrigerators, filters, and the like, generally forming a fairly sticky and difficult to handle solid.
When arsenic is also present, as in most common lead recovery processes, the presence of chlorine further creates the risk of forming the highly toxic gas AsClI.
Thus, those problems and / or risks are avoided with the method of the present invention.
In one embodiment of the method of the present invention, the third supernatant scratch from soft lead refining step (b) is recycled to a process step upstream of first distillation step (a), preferably to a pyrometallurgical process step.
Applicants have found that the at least one impurity that is removed by soft lead refining step (b) and ends as its sodium metalate oxide salt can be easily reduced to its elemental metal form, for example, in a pyrometallurgical process step.
Applicants have found that the at least one impurity, when recycled to a process step upstream of first distillation step (a), easily re-emerges in the feed to first distillation step (a), but thanks to the addition of first distillation step (a) as part of the process of the present invention, most of this additional presence of the at least one contaminant ends up in the first bottoms residue or product from first distillation step (a), and therefore it does not lead to additional consumption of chemicals and energy in soft lead refining step (b). The tin in the third supernatant scratch from soft lead refining step (b) which returns to first distillation step (a) becomes easily recoverable if a high purity tin product is obtained from the first bottoms residue or product of first distillation step (a). Elsewhere in this document it is explained that the antimony that ends up in the first bottom residue or product of first distillation step (a) can also be upgraded to become (part of) an end product of commercial value.
Applicants have found that even small amounts of arsenic can be afforded commercial value, for example as a small acceptable impurity in a high performance product such as hard lead. In one embodiment of the method of the present invention, the first base and the first oxidant are mixed together before being introduced in soft lead refining step (b). This brings the advantage of a simplified and easier addition of the chemicals in soft lead refining step (b), compared to the contact and / or addition methods described in the art. Applicants have found that soft lead refining step (b) can be performed in a single operation without any problems. In particular, when the third supernatant scratch is intended to be recycled to a pyrometallurgical process step, the Applicants have found that the recovered impurity together with the lead present in sodium plumbate may have been left over from reaction (I) and which has not been reacted away by any of the reactions (II) to (IV), and with lead possibly physically entrained with the third supernatant scratch after its separation from the purified lead product from soft-lead refining step (b), can be processed together and recovered without any problems. The method of the present invention is also less sensitive than the methods in the art to a limited presence of lead, entrained or in the form of its oxide salt, in the scratch. Such additional lead recycle represents only a limited inefficiency in the process, provided the amounts are kept within limits.
In an embodiment of the method according to the present invention, the first distillation step (a) is carried out at a pressure of at most 15 Pa absolute, preferably at most 10 Pa, more preferably at most 5 Pa, even more preferably at most 1 Pa, even more preferably at most 0.7 Pa absolute. Applicants have found that a lower pressure is beneficial because it promotes separation of the more volatile metals from the less volatile metals. The additional advantage is that the separation can be performed at a lower temperature as compared to the situation when a higher operating pressure is used. This has the advantage that processing is also more energy-efficient. In one embodiment of the method according to the present invention, the first distillation step (a) is carried out at a temperature of at least 800 ° C, preferably at least 850 ° C, more preferably at least 900 ° C, even more preferably at least least 930 ° C. Applicants have found that a higher temperature promotes separation of the metals into a vapor phase and a residual liquid phase, for example, because the higher temperature increases the volatility of the more volatile metal or metals. The higher temperature can also increase the difference in volatility between the metal or metals to be vaporized and the metal or metals to be kept in the liquid phase. Applicants have further found that a higher temperature also reduces the risk that metal-to-metal compounds can form and / or adhere to the walls of the equipment, possibly hindering the distillation operations.
The initial distillation of the solder-type metal mixture in step (a) can be carried out in batches, and such vacuum batch distillation techniques are described in patents CN101696475, CN104141152, CN101570826, and in Yang et al, Recycling of metals from waste Sn- based alloys by vacuum separation ”, Transactions of Nonferrous Metals Society of China, 25 (2015), 1315-1324, Elsevier Science Press.
In one embodiment of the method according to the present invention, the first distillation step (a) is performed in continuous operating mode. The vacuum distillation of metals, as in step (a), can also be performed in continuous mode, and such continuous distillation techniques are described in WO 2018/060202 A1, CN102352443, CN104651626 and CN104593614.
In one embodiment of the method of the present invention, the feedstock for the first distillation step (a) is a crude solder composition containing significant amounts of tin and lead and comprising at least 0.16% by weight and optionally up to 10% by weight of the total of chromium (Cr), manganese (Mn), vanadium (V), titanium (Ti), tungsten (W), copper (Cu), nickel (Ni), iron (Fe), aluminum (Al) and / or zinc (Zn), wherein the feed is available at a temperature of at least 500 ° C, the method further comprising the step of pretreating the crude solder composition before first distillation step (a) to form the molten solder mixture as feed material for the first distillation step (a), the pretreatment step comprising the steps of c) cooling the supplied coarse solder composition to a temperature of not more than 825 ° C, to produce a bath containing a first supernatant scratch that comes under gravity t floating on a first liquid molten metal phase, d) adding a chemical selected from an alkali metal and / or an alkaline earth metal, or a chemical compound comprising an alkali metal and / or an alkaline earth metal, to the first liquid molten metal phase to forming a bath containing a second supernatant scratch that floats by gravity on a second liquid molten metal phase, and e) removing the second supernatant scratch from the second liquid molten metal phase to obtain the molten solder mixture.
The inventors have found that certain metals in the supplied crude solder composition are capable, under the conditions of the first distillation step (a), which are suitable for vaporizing lead from a mixture comprising tin, to form mutual metal-metal bonds between at least two of those particular metals, and / or metal-metal compounds of at least one of the particular metals with tin.
The inventors have further found that many of those metal-metal compounds have a much higher melting point than the temperature of the mixture in which they are formed.
The inventors have therefore found that those high melting metal-metal compounds can come out of solution and form solids.
Those solids can remain in suspension in the liquid metal and lead to the risk of lowering the flowability of the mixture, such as by increasing the viscosity of the liquid mixture.
That in itself can hinder smooth operation of the first distillation equipment, such as by slowing the flow of liquid metals and thereby lowering the capacity of the equipment, requiring the equipment to be operated at a reduced flow rate.
The solids may also stick and / or adhere to the first distillation equipment, thereby creating the risk of interfering with or even blocking the operation of the first distillation equipment, for example by clogging important passageways for the process streams.
The phenomenon described here may even make it necessary to shut down the equipment for opening and cleaning, or to replace the affected pieces of equipment.
The inventors have found that the tendency to form such metal-metal compounds increases at a given temperature as the lead content in the liquid metal mixture is reduced.
The inventors have found that the risk of metal-metal compound formation thereby increases as the molten feed mixture moves from the inlet of the first distillation equipment to the outlet of the first bottoms product, due to the evaporation of lead from the liquid mixture passing through the first distillation equipment.
The inventors have further found that the tendency to form such metal-metal compounds increases with a decrease in the temperature of the molten liquid metal phase.
For example, the inventors have observed that that feed entering the first distillation apparatus can be at a lower temperature than the first bottoms product leaving the first distillation apparatus.
The inventors have therefore found that the adverse effects of the metal-metal compounds can be more pronounced at lower temperatures.
Applicants believe that the inlet section of the first distillation equipment may therefore be particularly susceptible to the above-described problems caused by the metal-metal connections.
The inventors have further found that continuous distillation of lead from tin is even more prone to the problem overcome by the present invention. The inventors believe that this is at least in part because a continuous distillation operation allows more time for a gradual accumulation of solids that come out of solution and can adhere to the equipment. In continuous processing, the solids can therefore accumulate and present greater problems than in batch processing. In addition, in continuous vacuum distillation equipment, the liquid metal stream typically follows a complex narrow pass path. That pathway and those narrow passages are more prone to be clogged by the metal-metal compounds coming out of solution and trying to attach themselves to a solid anchor point. The inventors have found that in particular chromium (Cr), manganese (Mn), vanadium (V), titanium (Ti), tungsten (W), copper (Cu), nickel (Ni), iron (Fe), zinc ( Zn) and aluminum (Al), which are metals whose presence in the solder feed to the first distillation step (a) can lead to the interfering metal-metal connections during the initial distillation of the solder. Of those potentially disturbing metals, Cu, Ni, Fe, Zn and Al are usually the most important to be kept under control. This is because it is more economical to recover tin and / or lead from feedstocks containing Cu, Ni, Fe, Zn and Al. Iron and / or aluminum can also, for process reasons, be introduced into the global process upstream of the tin and / or lead recovery step. The presence of Cu, Ni, Fe, Zn and Al in the crude brazing intermediate product from which the tin and / or lead is to be recovered is therefore more likely, and is the result of choices in the upstream process steps and of the selection of the upstream feed materials. process steps, which are usually of a pyrometallurgical nature.
In one embodiment, the crude solder composition that is pretreated before being supplied to first distillation step (a) comprises at least 0.5% by weight, more preferably at least 0.75% by weight, even more preferably at least 1.0% by weight. %, preferably at least 1.5% by weight, more preferably at least
2.0 wt%, even more preferably at least 2.5 wt%, even more preferably at least 3.0 wt% of the total chromium (Cr),
manganese (Mn), vanadium (V), titanium (Ti), tungsten (W), copper (Cu), nickel (Ni), iron (Fe), aluminum (Al) and / or zinc (Zn) together.
Applicants have found that a crude solder composition containing these compounds at the stated levels can be more easily pretreated successfully such that the downstream first distillation is able to operate for a long time without being affected by the formation of metal-metal bonds.
This brings the advantage of the ability to process a crude brazing composition obtainable by the pyrometallurgical processing of a wide variety of raw materials and using a wide variety of metal-containing auxiliary materials in those upstream process steps.
Particularly advantageous is the ability to handle a crude solder obtained as the copper smelting by-product.
and refining operations, in which secondary feedstocks are supplied.
Those secondary basestocks can come from a wide variety of sources, and thus can contain a wide variety of other compounds, especially metals other than lead and / or tin.
An additional advantage is that also the level of purchaser of the raw solder composition intended as feedstock for the first vacuum distillation does not have to be reduced to very low levels, which alleviates the quality requirements for the performance of the upstream process steps, and thus gives more freedom to those process steps. , and therefore higher efficiency and / or capacity within the same constraints of the equipment.
Applicants have found that the pretreatment steps c), d) and / or e) which may be included in the process of the present invention can handle the indicated significant levels of the undesirable components without any problems.
In addition, the stated levels of those components do not necessarily lead to higher consumption of process chemicals, and to greater problems in any pyrometallurgical steps for the recovery of the metal values from the third supernatant scratch, which is removed in soft lead refining step b), because most of the unwanted components may already be removable or even removed by the indicated physical means, such as step e).
In one embodiment, the crude brazing composition that is pretreated before first distillation step (a) comprises at most 10.0% by weight, preferably at most 8.0% by weight, more preferably at most 6.0% by weight, with an additional more preferably at most 5.0% by weight, preferably at most 4.0% by weight, more preferably at most 3.0% by weight, even more preferably at most 2.0% by weight, of the total of chromium (Cr), manganese (Mn), vanadium (V), titanium (Ti), tungsten (W), copper (Cu), nickel (Ni), iron (Fe), aluminum (Al) and / or zinc ( Zn) together. Applicants have found that adhering to the prescribed upper limit allows the pretreatment steps c), d) and e) that can be included in the process to work more effectively to obtain the desired results, and in a more efficient manner, because energy and chemical requirements remain limited, practical and economical. An additional advantage of a limited presence of the indicated components is that the amount of first and / or second supernatant scratch that is produced remains limited. When scratch is removed, an amount of valuable metals is inevitably entrained. The resulting scratch thus also represents a loss of valuable metals from the main process streams destined to recover the desired metals, in this context mainly tin and / or lead, but possibly also other metals such as antimony and precious metals. Even if the first and / or second supernatant scratch is recycled to an upstream process step, the amount of desired metals recycled with the scratch represents an inefficiency in the process. The reduction of this loss and / or this inefficiency in the process by the above stated limits therefore represents an advantage for the process as a whole. An additional advantage of this feature is also that less lead will also circulate in the overall process in which the crude solder composition is produced and pretreated.
The processing of lead-containing metal streams at high temperatures poses its own problems in terms of industrial hygiene.
The declared characteristic therefore also contributes to a lesser and / or more limited industrial hygiene problem associated with the recovery of tin and / or lead as a by-product from the production of copper or other non-pollutants.
ferrous metals.
In one embodiment, the crude solder composition that is pretreated before first distillation step (a) is available at a temperature of at least 510 ° C, preferably at least 520 ° C, more preferably at least 550 ° C, even more preferably at least 575 ° C, preferably at least 600 ° C, more preferably at least 650 ° C, even more preferably at least 700 ° C, preferably at least 750 ° C, more preferably at least 775 ° C, even more more preferably at least 800 ° C, even more preferably at least 830 ° C.
Applicants have found that a higher feed temperature contributes to a smoother feed stream in the upstream process where the feed stream is prepared.
Applicants have also found that, at a higher temperature, the metal-metal compounds that form between copper and tin and thus will have to be removed to some extent, that those metal-metal compounds then tend to trap less tin for the same amount of copper.
Thus, a higher temperature contributes to a more efficient removal of copper impurities because the removed metal-metal compounds then carry less of the valuable tin from the molten solder composition on its path to the high performance products.
Applicants have further found that due to a higher supply temperature of the crude solder composition, the pretreatment steps can be more effective and efficient.
For example, Applicants have found that a higher supply temperature provides more space for cooling, and that a wider cooling range is more effective in removing the target metal compounds, i.e., those compounds that are capable of producing metal compounds.
form metal compounds downstream in the first distillation, especially for copper removal.
In one embodiment, the crude brazing composition that is pretreated before first distillation step (a) is available at a temperature of at most 1000 ° C, preferably at most 980 ° C, more preferably at most 960 ° C. Applicants have found that limiting the supply temperature below the stated limits has the advantage that the energy requirements of upstream process steps remain practical, sufficiently efficient and economical. Higher temperatures, above the stated limits, have not been found to provide sufficient additional benefits to justify the additional input of energy, whatever form those input of energy takes, including chemical energy. In one embodiment, the crude solder composition that is pretreated before first distillation step (a) is cooled to a temperature of at most 820 ° C, preferably at most 800 ° C, more preferably at most 750 ° C, even more preferably at most 700 ° C, even more preferably at most 650 ° C, preferably at most 600 ° C, even more preferably at most 550 ° C, preferably at most 525 ° C, more preferably at most 500 ° C, even more preferably at most 450 ° C, preferably at most 400 ° C, more preferably at most 370 ° C, even more preferably at most 360 ° C, preferably at most 350 ° C, more preferably at most 345 ° C, even more preferably at most 330 ° C, preferably at most 320 ° C, more preferably at most 310 ° C to produce a bath containing the first supernatant scratch, which will float to the surface by gravity. first liquid molten metal phase. Applicants have found that cooling the crude brazing composition removes at least some of several of the less desirable metals, particularly copper but also nickel, iron, zinc and aluminum, and chromium, manganese, vanadium, titanium and tungsten, if any. Applicants have further found that when the cooling range is wider and / or leads to lower temperatures, more of those metals than come out of solution and end up in the first supernatant scratch.
The wider the cooling path is made, the more suitable the cooling step becomes to be divided into several consecutive cooling steps, preferably combined with intermediate scratch removal.
This brings the advantage that in general less of the first supernatant scratch may need to be removed to remove the same amount of unwanted metals, and that the total amount of first supernatant scratch contains less of the target metals of the process as a whole, which mainly lead and / or tin, but also include the various precious metals that may be present in the crude solder composition, and in certain circumstances also the antimony (Sb) that may be present. Applicants have also found that the cooler the coarse solder composition, the higher its density, which is advantageous for the gravity separation of the first supernatant scratch, because the first supernatant scratch floats more readily on the denser liquid metal phase.
In one embodiment, the crude brazing composition that is pretreated before first distillation step (a) is cooled to a temperature of at least 230 ° C, preferably at least 232 ° C, more preferably at least 240 ° C, even more preferably at least 250 ° C, more preferably at least 270 ° C, even more preferably at least 280 ° C, preferably at least 290 ° C, more preferably at least 300 ° C, even more preferably at least 310 ° C, preferably at least 320 ° C, more preferably at least 325 ° C, even more preferably at least 328 ° C.
Applicants have found that, due to that lower limit of the cooling step, less tin is consumed in binding the same amount of copper to be removed.
Without wishing to be bound by this theory, Applicants believe that this is due to the fact that the formation of CusSns is more favored and the formation of CusSn is less favored at the lower temperatures.
The lower limit of the cooling step therefore lowers the amount of valuable tin to be removed along with the same amount of copper in the first supernatant scratch.
Even if the first supernatant scratch is optionally recycled upstream in the process, this feature represents an improvement in efficiency because less tin needs to be recycled in that process for the same amount of copper removed by the cooling step c). In the cooling step, Applicants have further found that it is preferable to respect the specified minimum temperature as this ensures that the metal remains liquid and that its viscosity remains sufficiently low to resist the solids formed by the cooling and / or by allowing the chemical reactions initiated by the addition of chemical compounds to rise to the surface and be removed from the underlying liquid metal phase by skimming.
The primary purpose of adding the prescribed chemical in step (d) is to remove much of any zinc present in the crude solder stream processed in steps (c) and (d).
The inventors have found that the problems identified in the context of first distillation step (a) can be significantly alleviated and even avoided altogether by keeping the concentration of these metals in the molten solder mixture as feed to the first distillation step within certain limits ( a) wherein the solder mixture is separated into more concentrated streams by evaporation of at least part of the lead.
Applicants point out that the upstream process producing the crude solder composition suitable as a feed stream for first distillation step (a) is usually carried out at a high temperature, usually much higher than the stated 500 ° C, rather in the range of 700 ° C. 1000 ° C. Applicants further point out that step (a), which in most typical cases is a vacuum distillation step, should generally be performed at an even higher temperature. Typical temperatures for removing lead from tin by vacuum distillation are at least 900 ° C, often as high as 1100 ° C. Applicants therefore note that step (c) is counter-intuitive. Applicants note that those of ordinary skill in the art would prefer to maintain the crude solder at the high temperature at which it was produced, and optionally heat it even more, before subjecting the solder to the first distillation step (a) for separating lead from tin.
However, Applicants have found that the cooling step (c) is capable of transferring, without the intervention of additional chemicals, a significant portion of the components in the mixture that are undesirable in the feedstock for first distillation step (a) to a first supernatant scratch phase. thus making said first supernatant scratch phase available to be separated from the liquid metal phase. Applicants have found that this cooling step makes an important contribution to the formation of a discrete scratch phase rich in the unwanted components, leaving behind a liquid metal phase containing less of those unwanted components and therefore more suitable as a feedstock for the first distillation step. (a), with less operational problems caused by the possible formation of metal-metal compounds during the first distillation step (a). Applicants have found that the cooling step is particularly capable of lowering the copper, nickel, iron and / or zinc content in the remaining liquid solder phase.
Applicants note that step d) further decreases the concentration of the unwanted metals in the liquid metal phase on the way to the first distillation step (a). However, that step consumes chemicals, as indicated. Applicants note that the cooling step c) has the additional advantage that the subsequent chemical treatment step d) requires less chemicals. The chemical (s) indicated for step d) will act as a base, and that base will end up in the second supernatant scratch that is removed, at least in step e). The second supernatant scratch contains valuable metals, and it is of economic importance to reuse the scratch phases separated from the liquid metal phase for the recovery of the valuable metals. However, many of the known processes for recovering these metals from such scratch streams are of a pyrometallurgical nature. They occur at very high temperatures, so high that most of the structural steel of the equipment that comes into contact with the high temperature process streams is usually protected with refractory material.
However, the chemical (s) used in step d), which enter the second supernatant scratch phase separated in step e), are aggressive to the most common refractory materials used in typical pyrometallurgical process steps for the recovery of non-ferrous metal.
Applicants note that the cooling step c) therefore not only contributes to keeping the level of the chemical (s) introduced in step d) low, but also contributes to the acceptability of reusing the scratch being separated in step e) to recover metal values therefrom by means of a pyrometallurgical process.
Applicants have found that in the cooling step c), mainly iron and nickel can chemically bond with tin and that those compounds can float, provided that the underlying liquid stream contains sufficient lead, as indicated elsewhere in this document, and thus a sufficient high density.
Applicants have found that the chemical introduced in step d) is capable of binding some of the unwanted metals, mainly zinc, in a form that will also float on its own, under the same conditions set out above for step c ). In one embodiment, the method of the present invention further comprises the step of removing the first supernatant scratch from the bath before step d). Applicants prefer to remove the scratch from any pre-treatment step before starting the next pre-treatment step.
Applicants have found that this has the advantage that the overall amount of scratch is smaller compared to the alternative where the scratch from different steps is combined and all the scratch is removed together at the end of the pre-treatment steps.
A scratch also contains some tin and / or lead, and thus it is disadvantageous if those amounts of valuable metals are removed from the metal stream supplied to the first distillation step (a). Those amounts of valuable metals also increase the burden of reworking the scratch to recover the metal values therein, including the entrained tin and / or lead, but also the other metals removed from the liquid metal stream by the pretreatment.
In one embodiment of the method of the present invention, the process pathway for obtaining the feed composition for step c) comprises a metal melting down step, and at least one of the scratches from steps c) and d) or e) is recycled to the melting down step, wherein preferably any supernatant scratches that are formed and separated are recycled to the melting out step. Applicants have found that an upstream smelting step, such as in a copper smelting furnace, is not only a suitable recovery step for non-ferrous metal, for generating a crude solder stream as a by-product which is a suitable feed composition for step c), and for generating through the pretreatment step of the molten solder mixture which is suitable as a feed to first distillation step (a), but which is also an extremely suitable point for recycling at least one of the scratches produced in the pre-treatment steps c) and d). Applicants prefer to recycle the first supernatant, which is generated by the cooling in step c), as well as the second supernatant, which is removed in step e), after the chemical reaction that takes place in step d).
In step d) an alkali metal and / or an alkaline earth metal can be added as such, such as adding sodium metal. In such a case, Applicants prefer to also add an amount of water to react the sodium to its hydroxide and / or oxide, compounds that bind more readily with zinc. However, Applicants preferably add the alkali metal and / or alkaline earth metal in a chemically bonded form, more preferably as a solid, as Applicants have found that a bonded form works better, and because the solid generally has a lower density than the pure metallic form, and any surpluses consequently float on the liquid metal and can be removed together with the second supernatant scratch. The bound form can be, for example, an oxide, but is preferably a hydroxide. Applicants have found that calcium hydroxide (Ca (OH) 2) and potassium hydroxide (KOH) are also suitable, but applicants prefer to use sodium hydroxide (NaOH), preferably in its solid form, as it is more efficient by weight for binding of a given amount of zinc, and this is the most readily available form of suitable compounds. Applicants have further found that the addition of the prescribed compound aids in better phase separation between the solid second supernatant scratch and the underlying liquid metal phase. Better phase separation contributes to a cleaner scratch that contains less of the high-quality metals lead and tin, and thus more effective and useful recovery of those valuable metals, while also increasing process efficiency.
In an embodiment of the method of the present invention comprising step d), the alkali metal and / or alkaline earth metal is added in step d) in a chemically bound form, preferably as a solid. Applicants have found that the addition of a pure metal form may be suitable, but Applicants prefer to use a chemically bonded form. The chemically bonded form offers the alkali metal and / or the alkaline earth metal in a more accessible form to chemically react with the target metals for removal in the pretreatment steps. Applicants have found that the reaction products of the chemically bound form with the target metals, such as, for example, Na2ZnOO3, are more easily separated from the molten liquid stream by gravity, and therefore more easily removed as a purer stream, which is less valuable. contains metals.
In an embodiment of the method of the present invention comprising step d), the alkali metal and / or alkaline earth metal is added in step d) as an oxide or a hydroxide, preferably as a hydroxide. Applicants have found that the process can easily handle the oxygen and hydrogen that the metal entails in its chemically bound form. Applicants have found that this form also avoids the addition of chemical elements that would make the process more difficult.
In one embodiment of the method of the present invention comprising step d}), sodium hydroxide is added in step d). Applicants have found sodium hydroxide to be most suitable for this pretreatment step. Applicants have also found that sodium hydroxide is more readily available and under more attractive delivery conditions as compared to other chemically bound forms of alkali metals and / or alkaline earth metals.
The inventors have further found that the metals potentially harmful prior to step (a) do not have to be completely removed from the solder in order to make the solder suitable for the first vacuum distillation. For example, the inventors have found that the problems identified can be reduced to a practically and economically acceptable level when small amounts of copper remain in the braze mixture fed to the first distillation step (a). This finding has the advantage that solder streams can be processed that occur as the by-product of the recovery of copper from primary and / or secondary base materials, in particular from secondary base materials, and more importantly from raw materials that are end-of-life materials. use cycle.
In one embodiment of the method of the present invention, the molten solder mixture with lead and tin that forms the feedstock for the first distillation step (a) comprises, by weight: ° at least 90% tin and lead together, ° more lead than tin, ° not more than 0.1% of the total of chromium (Cr), manganese (Mn), vanadium (V), titanium (Ti) and tungsten (W), ° not more than 0.1% aluminum (AI) ° not more than 0 , 1% nickel (Ni) ° not more than 0.1% iron (Fe), and
° not more than 0.1% zinc (Zn).
Applicants have found that the risk of the formation of potentially interfering metal-metal compounds is reduced by keeping the presence of these compounds below lower limits.
In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) at least% by weight and more preferably at least 15% by weight of tin, preferably at least 20% by weight, more preferably at least 22% by weight, still more preferably at least 24 weight%, preferably at least 26 weight%, more preferably at least 28 weight%, even more preferably at least 30 weight% tin. Applicants have found that a higher amount of tin in the molten solder lowers the melting point of the mixture, with the advantage that a wider temperature range is available for the pre-treatment of the crude solder composition to prepare the solder mixture for a flawless first vacuum distillation. A higher content of tin also increases the economic interest in the solder mixture as a feedstock for first distillation step (a) as a raw material for the recovery of high purity high quality tin products.
In one embodiment, the molten solder mixture as feedstock for first distillation step (a) preferably comprises at least 45% by weight, more preferably at least 50% by weight, more preferably at least 55% by weight, even more preferably at least 60% by weight. weight% lead. Applicants have found that a higher amount of lead in the solder mix improves the separation of the scratch from the liquid metal phase.
In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) at most 80% by weight of lead, preferably at most 75% by weight, more preferably at most 70% by weight, even more preferably at most 65% by weight. %, preferably at most 60% by weight of lead. Applicants have found that an excessive amount of lead in the liquid metal mixture does not further increase the benefits associated with a greater amount of lead in the mixture as a feed to first distillation step (a). Applicants have further found that too much lead dilutes the more valuable tin in the metal mixture, thereby lowering interest in this metal mixture as a feedstock for the recovery of high purity tin.
In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) at least 91% by weight of tin and lead together, preferably at least 92% by weight, more preferably at least 93% by weight, even more preferably at least at at least 94% by weight, even more preferably at least 95% by weight, preferably at least 96% by weight, more preferably at least 96.5% by weight, even more preferably at least 97% by weight, even more preferably at least 97.5% by weight, preferably at least 98% by weight, more preferably at least 98.5% by weight, even more preferably at least 98.7% by weight tin and lead together. A higher content of tin and lead together increases the amount of high value products that can be recovered from the molten braze metal mixture and reduces the amount of generally inferior by-product streams that can result from the further purification of the products from the first distillation step (a) to high value product streams. This reduces the effort required to dispose of those non-premium products to a level imposed by the specifications for the premium product, and which should comply as closely as possible with the international trade standards that are in place. In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) at most 10% by weight of antimony (Sb), preferably at most 8% by weight, more preferably at most 6% by weight, preferably less than 6 % by weight, even more preferably at most 5.5% by weight, preferably at most 5.0% by weight, more preferably at most 4.5% by weight, even more preferably at most 4.0% by weight %, even more preferably at most 3.5% by weight, preferably at most 3.0% by weight, more preferably at most 2.5% by weight, even more preferably at most 2.0% by weight %, preferably at most 1.5% by weight, more preferably at most 1.1% by weight of antimony (Sb). Applicants have found that antimony can be acceptable in the molten braze metal mixture as a feedstock for first distillation step (a), within specific limits, without causing problems when the molten braze mix is used as a feedstock for vacuum distillation.
Applicants have found that it is important to keep the amount of antimony below the specified upper limit because antimony can also at least partially evaporate under the distillation conditions.
As the antimony content is higher, the amount of antimony exiting the first distillation step along with the first concentrated lead stream as an overhead product can become more significant.
In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) at least 0.42% by weight and more preferably more than 0.42% by weight of antimony (Sb), preferably at least 0.43% by weight, more preferably at least 0.45% by weight, even more preferably at least 0.47% by weight, preferably at least 0.50% by weight, more preferably at least 0.55% by weight, more preferably at least 0.60% by weight, even more preferably at least 0.65% by weight, preferably at least 0.75% by weight, more preferably at least 1.0% by weight, more preferably at least 1.5% by weight, preferably at least 2.0% by weight, more preferably at least 2.5% by weight of antimony (Sb). Applicants have found that the molten brazing metal mixture as feedstock for the first distillation step (a) can contain measurable, and even significant amounts of antimony, within the stated limits, without the presence of antimony significantly hindering the downstream first distillation step (a ) to which the metal mixture can be subjected.
Applicants have found that this provides additional operational benefit to the upstream processes that provide the feed stream for the method of the present invention.
Thanks to this freedom, the relevant upstream processes are able to absorb an amount of raw materials in which antimony is present.
Applicants have found that significant concentrations of antimony are acceptable in the feedstock for first distillation step (a) without causing significant difficulties for the process of the present invention, nor for the downstream processes by which the first concentrated lead stream and the first bottoms are produced. produced by the first vacuum distillation,
to be further upgraded.
In one embodiment of the method of the present invention, the molten solder mixture comprising lead and tin and supplied to the first distillation step (a) comprises, by weight, at least 1 ppm by weight and at most 5000 ppm by weight of copper, at preferably at least 2 ppm by weight of copper, more preferably at least 3 ppm by weight, even more preferably at least 4 ppm by weight, even more preferably at least 5 ppm by weight of copper, preferably at least 6 ppm by weight, more preferably at least 7 ppm by weight, even more preferably at least 8 ppm by weight, even more preferably at least 9 ppm by weight of copper, preferably at least 10 ppm by weight, with more preferably at least 12 ppm by weight, even more preferably at least 14 ppm by weight, even more preferably at least 15 ppm by weight of copper, preferably at least 16 ppm by weight, more preferably at least 18 ppm by weight g weight and even more preferably at least 20 ppm by weight of copper.
Applicants have found that the amounts of copper in the metal mixture as indicated herein can be left as a feed to first distillation step (a) without neglecting the usefulness of the molten braze metal mixture as feed stream for the first distillation step (a). The inventors have found that the problems identified can be reduced to a practically and economically acceptable level if small amounts of copper remain in the solder feed to the distillation step.
This finding has the advantage that solder streams can be processed that occur as the by-product of the recovery of copper from primary and / or secondary base materials, in particular from secondary base materials, and more importantly from raw materials that are materials at the end of their use cycle. contain.
In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) up to 4500 ppm by weight of copper, preferably up to 4000 ppm by weight, more preferably up to 3500 ppm by weight, even more preferably up to 3000 ppm. ppm by weight, even more preferably at most 2500 ppm by weight, preferably at most 2000 ppm by weight, more preferably at most 1500 ppm by weight, even more preferably at most 1250 ppm by weight, even more preferably at most 1000 ppm by weight, preferably at most 800 ppm by weight, more preferably at most 600 ppm by weight, even more preferably at most 400 ppm by weight, even more preferably at most 200 ppm by weight, preferably at most 150 ppm by weight, more preferably at most 100 ppm by weight, even more preferably at most 75 ppm by weight of copper. Applicants have found that the lower the concentration of copper in the molten solder mixture, the lower the risk of metal-metal compound formation when the metal mixture is subjected to the first distillation step (a) to remove at least some of the lead in the mixture by evaporation. Applicants have further found that the lower the presence of copper in the molten solder mixture, the lower the concentration of copper in the product streams from the downstream vacuum distillation. This lowers the burden of further removing copper from those streams on their way to become high-value products, especially in terms of the consumption of chemicals and the amounts of by-products formed.
The molten solder mixture as feed to the first distillation step (a) preferably comprises at least 0.0001 wt% sulfur (S), preferably at least 0.0002 wt%, more preferably at least 0.0003 wt% , even more preferably at least 0.0005 wt%, preferably at least 0.0010 wt%, more preferably at least 0.0015 wt%, even more preferably at least 0.0020 wt% sulfur . Applicants have found that it is not necessary to reduce sulfur levels to very low levels, such as below the 1 ppm by weight detection limit, in order to achieve the result intended by controlling sulfur content. On the contrary: the presence of sulfur in the metal mixture has an advantageous technical effect.
In one embodiment, the molten solder mixture comprises as feedstock for first distillation step (a) at most 0.10 wt.% Sulfur (S), preferably at most 0.070 wt.%, More preferably at most 0.050 wt.%, Even more preferably at most 0.010 wt.%, preferably at most 0.0050 wt.%, more preferably at most 0.0030 wt.% sulfur. Applicants have found that the presence of sulfur in the molten solder mix as feedstock for first distillation step (a) can cause odor problems, and can pose an industrial hygiene problem, even if the sulfur-containing metal and / or the sulfur-containing slag and / whether scratch has cooled and solidified. These problems can arise during operations and during storage, but can be even more important during maintenance interventions. Applicants therefore prefer to reduce the levels of sulfur in the molten solder mixture to within the stated limits.
Applicants have found that sulfur binds with copper quite readily to form a copper sulfide (such as CuS), and that the copper sulfide is readily separated by gravity from the molten solder mixture containing the two major components in the process, i.e. tin and lead. The presence of sulfur is therefore able to aid in the removal of Cu in any process step which aims to separate Cu in a second supernatant scratch. Although the addition of Al could also be used to remove Cu, Applicants prefer to use S as the chemical process substance at this stage in the process because it is more selective than Al.
Applicants have found that the molten solder mix as defined herein can be subjected to the first distillation step (a) without any problem to remove most of the lead in the composition by evaporation. Applicants have found that such a distillation is capable of producing a first concentrated lead stream as a top stream that can be further purified without difficulty in soft lead refining step (b) to obtain a soft lead product in accordance with many of the commercial standards, and at the same time in first distillation step (a) produce a first bottoms product that is rich in tin but also includes the majority of any antimony (Sb) present in the feed to first distillation step (a), preferably together with a minimal presence of lead (Pb) .
Applicants have further found that the problem of metal-metal bond formation during the first vacuum distillation in step (a) of the molten solder mixture is further alleviated by at least the preferred concentration of lead in the first bottoms product of the first distillation step (a) to let. Applicants believe that this amount of lead has a beneficial effect in better keeping the potentially harmful metals in solution and reducing their tendency to form the potentially nuisance metal-metal compounds.
Applicants have further found that the presence of the preferred minimum amount of lead in the first bottoms product of the first distillation step (a) makes it easier to remove silver or other precious metals in the first bottoms by means of a crystallizer, using a technique as described in patent CN102534249, which discloses a 4 step crystallizer process for purifying a crude tin stream by removing silver, or as described in European Patent Application No. EP19154610.0.
In one embodiment of the present invention, the first bottoms product contains only very small amounts of silver and / or other precious metals, such as up to 120 ppm by weight of silver and up to 20 ppm by weight of gold (Au). That is, the amount of silver and / or other precious metals that can be recovered is insufficient to justify the addition of a silver recovery step to the first bottoms product. Provided that the expected concentration of silver and other precious metals in the high-purity tin product also remains acceptable, Applicants prefer to omit the silver recovery step and send the first bottoms product directly to the second distillation step downstream. Other feed streams that would otherwise be fed to the crystallization step can then also be combined with the feed to the second distillation step.
In one embodiment of the method of the present invention, the first bottoms product contains silver and the first bottoms product is separated by fractional crystallization into a first silver-enriched liquid bleed product at the liquid end of the crystallization step and a first tin-enriched product at the crystal end of the crystallization step. Applicants have found that the first bottoms product, when it contains silver, is highly suitable and interesting to be separated by fractional crystallization into a silver-rich bleed product and a tin-enriched product. This fractional crystallization step can be fully focused on the removal of silver from the main tin stream, such that the content of silver in the final high quality tin product produced downstream is sufficiently low and meets customer expectations.
In particular, silver is undesirable as an impurity in commercial grade tin metal when used in a number of applications. Significant presence of silver in tin metal deteriorates the mechanical properties of tin metal. The presence of silver in tin used in the tin plating of steel also creates the risk of galvanic corrosion, which would corrode the wall of the tin container from the inside to the outside surface. This is a major problem for cans for use in the food industry.
In one embodiment of the process of the present invention, the first bottoms product (8) and / or the feed to the fractional crystallization step comprises at least 0.1% by weight and at most 20.0% by weight of lead. Preferably, the amount of lead in the first bottom product and / or the feed to the crystallization step is at least 0.15% by weight, preferably at least 0.20% by weight, more preferably at least 0.30% by weight, even more preferably at least 0.40 wt%, even more preferably at least 0.50 wt%, preferably at least 0.60 wt%, more preferably at least 0.70 wt%, even more preferably at least 0.80 wt%, preferably at least 0.90 wt%, and more preferably at least 1.00 wt%. The lead stimulates the fractional crystallization step, and acts as a solvent for the silver that the step aims to remove from the main raw tin stream. The silver tends to lag most of the lead and enter the bleed stream, and the composition of the bleed stream approaches the eutectic composition of 38.1 wt% / 61.9 wt% Pb / Sn. Respecting this lower limit for the presence of Pb promotes the feasibility of the fractional crystallization step, for example by ensuring that there is sufficient liquid phase present in the crystallizer steps where good and intimate contact between liquid and crystals is desired to obtain a effective separation. As discussed below, a higher amount of lead also brings advantages in the second downstream distillation step.
Preferably, the first bottoms product and / or the feed to the fractional crystallization step comprises at most 20.0 wt.% Pb, preferably at most 18.0 wt.%, More preferably at most 16.0 wt.%, With an additional more preferably at most 14.0 wt%, preferably at most 12.0 wt% Pb, preferably at most 10.0 wt%, more preferably at most 8.0 wt%, even more preferably at most 7.5 wt%, preferably at most 6.5 wt% Pb, preferably at most 6.0 wt%, more preferably at most 5.5 wt%, even more preferably at most 5.25 wt%, preferably at most 5.00 wt%, more preferably at most 4.90 wt%, even more preferably at most 4.80 wt%, preferably at most 4.00 wt %, more preferably at most 3.00 wt%, even more preferably at most 2.00 wt% Pb, preferably at most 1.50 wt% Pb. With lower amounts of lead in the feed to the fractional crystallization step, Applicants have found that the volume of first silver-enriched liquid tap product can be kept lower and the concentration of silver in the first silver-enriched liquid tap product can be kept higher. This has the advantage that silver can be recovered from more dilute feedstocks, while at the same time producing a first silver-enriched liquid tapping product that is sufficiently rich in silver to allow effective and efficient recovery of the silver therefrom. The lower volume and higher silver content of the first silver-enriched liquid draw-off product is also beneficial to the efficiency and effectiveness of the process steps for recovering the silver from the first silver-enriched liquid draw-off product.
In one embodiment of the method of the present invention, the concentration of lead in the first bottoms product and / or the feed to the fractional crystallization step is at least 3.0 times the concentration of silver in the first bottoms product. Preferably, the amount of lead in the feed to the crystallization step is at least 4.0, more preferably at least 5.0, even more preferably at least 6.0, and even more preferably at least 7.0 times the concentration of silver in the feed. Applicants have found that respecting this lower limit on the ratio of the concentration of lead to silver in the feed to the fractional crystallization step prevents the composition of the first silver-enriched liquid tap product from approaching a eutectic composition in the ternary diagram of lead / tin / silver. In one embodiment of the method of the present invention, the first bottoms product and / or the feed to the fractional crystallization step comprises at least 10 ppm by weight of silver
(Ag) and optionally up to 0.85% by weight of silver.
Preferably, the feed to the fractional crystallization step, as well as the first bottoms product, comprises
at least 10 ppm by weight of silver (Ag), preferably at least 20 ppm by weight, more preferably at least 25 ppm by weight, even more preferably at least 30 ppm by weight, even more preferably at least 50 ppm by weight weight, preferably at least 100 ppm by weight, more preferably at least 200 ppm by weight, even more preferably at least
300 ppm by weight, even more preferably at least 500 ppm by weight, preferably at least 750 ppm by weight, more preferably at least 1000 ppm by weight, even more preferably at least 1100 ppm by weight, even more preferably at least 1200 ppm by weight of silver, and optionally at most 0.85 weight% silver, preferably at most 0.80 weight%, more preferably at most 0.75 weight%,
even more preferably at most 0.70 wt%, even more preferably at most 0.65 wt%, preferably at most 0.60 wt%, more preferably at most 0.55 wt%, with even more preferably at most 0.50 wt%, even more preferably at most 0.45 wt%, preferably at most 0.40 wt%, more preferably at most 0.35 wt%, even more preferably at most
0.30% by weight, even more preferably at most 0.25% by weight, preferably at most 0.20% by weight, more preferably at most
0.175% by weight or at most 1750 ppm by weight, even more preferably at most 1600 ppm by weight, even more preferably at most
1500 ppm by weight.
A higher content of silver in the first bottom product,
and also in the crude tin mixture as feed to the fractional crystallization step, brings with it the advantage that more silver is available to be recovered, and that the first silver-enriched liquid draw-off product from the fractional crystallization step can contain more silver, and thus not only can represent a higher economic value, but also that the recovery of silver from it can be made more efficient and effective.
Respecting the upper limit for the content of silver entails the advantage that the tapping composition has a lower risk of approximating the eutectic composition in the ternary diagram for Pb / Sn / Ag.
The upper limit on the content of silver in the first bottoms and / or the crude tin mixture as feed to the fractional crystallization step also entails the advantage that it allows a significant increase in concentration from feed stream to first silver-enriched liquid tapping product from the crystallizer, such that the process is capable of incorporating feedstocks with a lower content of silver, ie, which can be very dilute with respect to Ag.
In one embodiment of the method of the present invention, the first bottoms and / or the feed to the fractional crystallization step comprises at least 0.1% by weight of antimony (Sb). Preferably, the first bottoms product comprises at least 0.20% by weight of antimony, more preferably at least 0.30% by weight, even more preferably at least 0.40% by weight, preferably at least 0.50% by weight. %, more preferably at least 0.55% by weight, even more preferably at least 0.60% by weight, even more preferably at least 0.65% by weight, preferably at least 0.75% by weight %, more preferably at least 1.0% by weight, even more preferably at least 1.5% by weight, preferably at least 2.0% by weight, more preferably at least 2.5% by weight of antimony (Sb). Applicants have found that the first bottoms product can contain measurable, and even significant amounts of antimony, within the stated limits, without the presence of antimony significantly hindering the capabilities of the process.
Applicants have found that this provides additional efficacy for the upstream processes from which the first bottoms product is obtained.
By allowing an amount of antimony in the first bottoms product to be produced as an intermediate stream, the respective upstream processes are able to take up an amount of raw materials in which antimony is present.
Antimony can be present in various primary and / or secondary base materials for non-ferrous metals, as well as in many materials at the end of their use cycle.
For example, antimony can be present in lead, which has been used for plumbing since the time of the Romans.
Those materials can now be released as breakdown materials, often in combination with copper for pipes and other purposes, and with tin and lead for the solder joints. Allowing an amount of antimony in the first bottoms product enables the upstream processes to accept such mixed materials at the end of their use cycle. Applicants have found that significant concentrations of antimony are acceptable in the first bottoms product without causing significant difficulties for the process of the present invention, nor for the downstream processes for further upgrading the streams generated by the first vacuum distillation step.
Applicants have further found that most of the antimony tends to lag behind the tin in the fractional crystallization step, and the presence of antimony has the advantage of increasing the melting point of the crystals formed, thus increasing the facilitates separations in the crystallizer and provides clearer separation between the Pb / Ag in the first silver-enriched liquid tap product and the Sn / Sb in the first tin-enriched product.
In one embodiment of the process of the present invention, the first silver-enriched liquid draw-off product is partially and / or temporarily recycled to the feed of the fractional crystallization step. This has the advantage that the silver enrichment factor, i.e. the concentration ratio of the silver concentration in the net bleed product removed from the process to the concentration of silver in the fresh feed to the process, is further increased. This entails the advantages already outlined in that (i) base stocks that are more dilute in silver are made acceptable for the process of the present invention, and (ii) further processing of the bleed stream is made more efficient and effective.
In one embodiment of the process of the present invention, at least one product from the liquid end of at least one crystallizer in the fractional crystallization step is at least partially recycled to the feed of the first distillation step, preferably the liquid draw-off stream from the crystallizer that is most concentrated upstream from the flow of tin through the fractional crystallization step. Applicants have found that this provides an additional power to reduce the presence of lead in the fractional crystallization step such that the amount of net bleed stream to be removed from the silver recovery process and the concentration of silver can be reduced. in it can be further increased. In addition, this recycle broadens the acceptable base materials to materials with a lower content of silver.
In one embodiment of the method of the present invention, at least one product from the liquid end of at least one crystallizer in the fractional crystallization step is at least partially recycled to the raw solder pretreatment step feed. This brings the advantage that the concentration of copper in the process of the present invention, which may have increased due to the leakage of copper in the feed of the first distillation step and may have penetrated into the fractional crystallization step, is reduced again because the copper in the recirculation is allowed to exit the process with the first and / or the second supernatant scratch separated in the rough solder pretreatment step.
In one embodiment of the method according to the present invention, the first tin-enriched product and / or the first bottoms product is subjected to a second distillation step that mainly separates lead and antimony from the first tin-enriched product and / or the first bottoms product by evaporation, whereby as a top product a second concentrated lead stream is produced and a second bottom product is produced. Applicants have found that the first tin-enriched product is very suitable as a base material for a high-purity tin product, as the lead and antimony in the stream can be easily removed by distillation, resulting in a residue that is further enriched in tin . As explained above, the first bottoms product can also be very suitable and is preferably fed directly to the second distillation step when its content of silver and / or precious metals is sufficiently low, such that there is no risk of unacceptably high levels of these elements. are achieved as impurities in the high purity high quality tin product obtained downstream, and such that the benefit of performing the silver recovery step between the first and second distillation steps is less than the additional burden of performing the silver recovery step. In one embodiment of the method of the present invention, a fresh feed containing lead is added to the feed of the second distillation step. Applicants have found that an amount of lead is desirable in the feed to the second distillation stage because the lead promotes the evaporation of antimony. This has the advantage that the evaporation of antimony is promoted in the second distillation step, thereby improving the quality of the separation that can be obtained in the second distillation step. The lead dilutes the vapor phase in the distillation step and thus acts as a kind of carrier for the antimony. As a result, the lead promotes the removal of antimony from the main tin stream and thereby contributes to the ultimate obtaining of a high purity, high quality tin product.
In one embodiment of the process of the present invention, the second concentrated lead stream is subjected to a third distillation step that separates predominantly lead and antimony from the second concentrated lead stream by evaporation, thereby producing a third concentrated lead stream as an overhead product and a third bottoms product being produced. Applicants have found that the second concentrated lead stream as the top stream of the second distillation step provides an extremely suitable basis for obtaining a high quality hard lead product, because the tin entrained in this stream can be easily removed from most of the lead and antimony by another distillation step. The third distillation step can focus entirely on the selective evaporation of antimony, and lead, if any, from the feedstock to the third concentrated lead stream as its overhead stream.
In one embodiment of the method of the present invention, a fresh feed containing lead is added to the feed of the third distillation step.
Applicants have found that some amount of lead is also desirable in the feed to the third distillation stage, because the lead promotes the evaporation of antimony.
This has the advantage that the evaporation of antimony is promoted in the third distillation step, thereby improving the quality of the separation that can be obtained in the third distillation step.
The lead dilutes the vapor phase in the distillation step and thus acts as a kind of carrier for the antimony.
As a result, the lead promotes the recovery of most of the antimony in the third concentrated lead stream and thereby contributes to the efficient production of the high quality hard lead product.
For example, the second concentrated lead stream may contain about 40/40/20 weight% Pb / Sn / Sb.
Applicants have found that this feed composition can be further improved.
Applicants prefer to dilute the feedstock for the third distillation step by adding lead-containing fresh feed to about 10-12 weight% Sb and / or 18-10 weight% Sn.
Applicants have found that this produces more vapor phase in the third distillation step, and also lowers the melting point of the feed.
This allows for better removal of Sb to the third concentrated lead stream as the top stream of the Sn remaining in the third bottoms.
The additional advantage is that if the third bottoms product is recycled to a location upstream of the second distillation stage, the better separation in the third distillation stage reduces the amount of antimony circulating over the second and third distillation stages.
In one embodiment of the method according to the present invention, the third bottoms product is at least partially and preferably completely recycled to the feed of the second distillation step and / or to the feed of the fractional crystallization step.
Applicants have found that the third bottoms product has an extremely suitable composition to be recycled to at least one of the designated locations upstream in the process of the present invention, due to its high purity in terms of valuable metals and low content of non-target metals in the third bottom product. This has the advantage that the valuable metals can be recovered in the designated high-quality products without high process costs. Applicants prefer to make the selection of the process site for recycling the third bottoms product dependent on the silver content of the stream, because the fractional crystallization step is capable of removing silver and thereby the accumulation of silver in the stream. prevent the process beyond acceptable levels.
In one embodiment of the method of the present invention, the method further comprises the step of removing at least one contaminant selected from the metals arsenic and tin from the third concentrated lead stream, thereby producing a purified hard lead stream as a hard lead product. Applicants have found that the third concentrated lead stream can be further refined by means known in the art to obtain a purified hard lead stream as the hard lead product.
In one embodiment of the process of the present invention, the second bottoms product is further refined to obtain a high purity high quality tin product. Applicants have found the second bottoms product to be highly suitable for further refining to obtain a high purity tin product of excellent economic value.
In one embodiment of the method of the present invention the second bottoms product is treated with aluminum metal, preferably in stoichiometric excess to the amount of antimony present, preferably in combination with mixing and cooling the reacting mixture to less than 400 ° C followed by separating the scratch containing Al / Sb / As formed by the treatment. Applicants have found that the aluminum easily forms solid metal-metal bonds with trace impurities in the tin stream, especially with antimony.
Applicants prefer to use a stoichiometric excess of aluminum because it is more effective in removing antimony and removes any remaining aluminum with little trouble, as described later in this document.
Applicants preferably use 2 kg of aluminum per 0.01% by weight of Sb present in 70 tons of the second bottoms product.
Mixing and cooling stimulates the reaction and aids the separation of the formed solids from the molten tin.
Applicants prefer to cool to a temperature of about 250 ° C as they have found that this provides a better balance between the reaction kinetics, which is promoted by high temperatures, and improved separation, which is promoted by lower temperatures. .
The formed scratch, containing Al / Sb / As, can be skimmed and recycled to an upstream pyrometallurgical process step.
Applicants prefer to collect the scratch containing AI / Sb / As in steel drums that are closed and sealed to avoid contact of the scratch with water, which could lead to the formation of the highly toxic arsine gases and / or stibine.
The aluminum is preferably added in granular form, which provides a large surface area without causing dust problems.
Applicants prefer to add the granules to a bath without vigorous mixing, preferably static, in order to prevent wet granules from exploding due to the sudden contact with the hot liquid tin.
In an embodiment of the method according to the present invention, the second bottom product, after the treatment with aluminum and preferably also after the removal of the scratch containing Al / Sb / As, is treated with a third base, which is preferably selected from NaOH, Ca (OH) 2 and Na: CO3 and combinations thereof, more preferably NaOH, followed by separating the scratch containing base formed by the treatment.
Applicants prefer to skim off the scratch containing Al / Sb / As before the addition of the third base in order to require less of that base.
Applicants preferably use NaOH as the third base because it forms a sodium aluminate scratch that is more acceptable for recycling to an upstream pyrometallurgical process step. Applicants prefer to perform this treatment iteratively, in successively repeated steps, and based on an analysis of the aluminum content in the tin stream, in order to save on the consumption of chemicals. The contemplated chemistry can generate hydrogen gas, so Applicants prefer to throw a quantity of sulfur grains onto the reacting liquid such that the sulfur ignites at the high process temperatures and burns the hydrogen that may have evolved from the reaction. The scratch can be stiffened by adding silicon dioxide, preferably in the form of sand.
In one embodiment of the method of the present invention, after the treatment with the third base, the second bottom product is treated with sulfur, followed by the separation of the scratch containing S formed by the treatment. The sulfur reacts with the sodium and forms a Na2S scratch. At the end of this treatment, Applicants prefer to intensify the stirring speed to attract more oxygen from the ambient air, oxidizing the sulfur remaining after the reaction, and the sulfur oxides that are formed can easily escape from the liquid end product.
In one embodiment of the method according to the present invention, at least part of the method is electronically monitored and / or controlled, preferably by a computer program. Applicants have found that electronically controlling steps of the method of the present invention, preferably by a computer program, has the advantage of much better processing, with results that are much more predictable and closer to the goals of the method. . For example, on the basis of temperature measurements, if desired also measurements of pressure and / or level, and / or in combination with the results of chemical analyzes of samples taken from process flows and / or analytical results obtained online, the controlling equipment in terms of the supply or removal of electrical energy,
the supply of heat or of a cooling medium, control of a flow and / or of a pressure. Applicants have found that monitoring or controlling in this manner is particularly advantageous in steps performed in continuous mode, but that it may also be advantageous in steps performed in batch mode or semi-batch mode. In addition, the monitoring results obtained during or after performing steps in the method according to the present invention can preferably also be used to monitor and / or control other steps as part of the method according to the present invention, and / or of processes used upstream or downstream of the process of the present invention, as part of a general process in which the process of the present invention is only one part. Preferably, the entire process is electronically monitored as a whole, more preferably by at least one computer program. Preferably, the method as a whole is electronically controlled as much as possible.
Applicants prefer that the computer control also provides for data and instructions to be passed from one computer or computer program to at least one other computer or computer program or module of the same computer program, for monitoring and / or controlling other processes including, but not limited to, the methods described in this document.
EXAMPLE The following example shows in more detail how the method of the present invention can be carried out and how the intended effect is obtained. The example also shows how the method of the invention can be part of a larger global process that yields more high-quality products. The enclosed Figure 1 shows a flow chart of the method steps and their sequence as performed in this example. The compositions reported in the example are expressed in units of weight, and were the result of analyzes of samples taken daily, the results averaged over an operating time of 73 days. In Figure 1, the numbers refer to the following elements of the claims:
1. Crude solder composition as feed to the pretreatment step 100
2. NaOH added in the pretreatment step 100
3. Sulfur added in the pretreatment step 100
4. First supernatant scratch from pretreatment step 100
5. Second supernatant scratch from pretreatment step 100
6. Molten braze mix obtained from pretreatment step 100
7. First concentrated lead stream as top stream from vacuum distillation step 200
8. First bottoms from the first vacuum distillation step 200
9. First silver-enriched liquid bleed product from the liquid end of crystallization step 300
10. First tin-enriched product from crystallization step 300
11. Fresh feedstock added to second vacuum distillation step 400
12. Second concentrated lead stream as overhead product from second vacuum distillation step 400
13. Second bottoms from second vacuum distillation step 400
14. Aluminum nuggets to tin refining step 500
15. Third base added in tin refining step 500
16. Sulfur added in tin refining step 500
17. Scratch containing Al / Sb / As from tin refining step 500
18. Scratch containing base from tin refining step 500
19. Scratch containing sulfur from tin refining step 500
20. High purity tin product from tin refining step 500
21. Third concentrated lead stream overhead from third vacuum distillation step 600
22. Third bottoms, from third vacuum distillation step 600
23. Copper added to soft lead refining step 700
24. First base added in soft lead refining step 700
25. First oxidant added in soft lead refining step 700
26. Third supernatant scratch formed in soft lead refining step 700
27. Purified soft lead stream or purified soft lead product from soft lead refining step 700
28. Purified hard lead stream or product from hard lead refining step 800
29. Remains of top product 21 from previous campaigns
30. Second base added in hard lead refining step 800
31. Second oxidant added in hard lead refining step 800
32. Fourth supernatant scratch formed in hard lead refining step 800
33. Fresh feedstock added to crude solder 100 pretreatment step
34. Fresh feedstock added to third vacuum distillation step 600
35. Fresh feedstock added to fractional crystallization step 300
36. Fresh Feed Adds to First Vacuum Distillation Step 200 100 Pretreatment Step 200 First Vacuum Distillation Step 300 Fractional Crystallization Step 400 Second Vacuum Distillation Step 500 Tin Refining Step 600 Third Vacuum Distillation Step 700 Soft Lead Refining Step 800 Hard Lead Refining Step For the analysis of a molten metal stream, a sample of molten metal is taken into a cast metal stream. refrigerated to solidify. One surface of the solid sample is prepared by passing the sample once, or preferably several times, through a grinding machine of the Herzog HAF / 2 type, until a clean and flat surface is obtained. The clean and flat surface of the sample is then analyzed by means of an optical emission spectroscopy (OES) device with breakdown spark of the Spectrolab M type from the company Spectro Analytical Instruments (US), which is also available from the company Ametek (DE ), where the parameters, crystals,
detectors and tube can be readily selected and adjusted to obtain the most suitable operation for the desired accuracy and / or detection limit. The analysis provides results for several metals in the sample, including copper, bismuth, lead, tin, antimony, silver, iron, zinc, indium, arsenic, nickel, cadmium and even the element sulfur, and that, for most of those metals, up to a detection limit of about 1 ppm by weight.
For the analysis of a scratch, the inventors preferably use a well-calibrated X-ray fluorescence technique (XRF technique), preferably using the XRF spectrometer of the PANalytical Axios type from PANalytical B.V. (NL). This technique is also preferred over the above-mentioned OES for analyzing samples of metals containing significant amounts of impurities, such as stream 6 and streams upstream thereof, in the flow chart in the attached Figure 1. Also in this technique the details can be easily selected. and adapted to optimize the results in terms of the most appropriate accuracy and / or limit of detection for the purpose of the analysis.
The crude solder stock 1 was obtained from the refining of materials containing copper, lead and tin in a copper smelting furnace (not shown) which produces as an intermediate material a "black copper" containing about 85% by weight Cu. This black copper was then subjected in a copper refinery to a series of pyrometallurgical refining steps (not shown) that produce a high purity copper product on the one hand and a number of slag binder products on the other. In the course of the refining process, the crude brazing raw material 1 is recovered from some of those refining slags. Purification of that crude solder was carried out through a series of pretreatment steps 100 to remove a significant amount of the metal impurities present that would otherwise be likely to adversely affect the downstream vacuum distillation steps. The impurities that are the target of the purification steps are mainly Cu, Fe, Ni and / or Zn, and the purpose of the crude solder purification is that the solder can be further processed smoothly and without problems using vacuum distillation.
The crude solder 1 was available from the upstream refining processes at a temperature of about 835 ° C.
In a first step of the purification process sequence 100, the solder was cooled to 334 ° C, which occurred in two steps.
In the first cooling step, the crude solder was cooled to about 500 ° C and a first scratch was removed from the surface of the molten liquid metal.
In the second cooling step, the crude solder was further cooled to 334 ° C and a second scratch was removed from the surface of the molten liquid metal. The cooling step resulted in the formation of a total scratch containing most of the copper present in the crude solder, which was removed as by-product (not shown) and recycled in one of the upstream pyrometallurgical process steps.
The total flow rate and the concentrations of target metals in the remaining brazing intermediate (flow 1) are shown in Table 1. The copper content in the braze was reduced to an average of 3.0000 weight% by this series of cooling steps and scratch removals. The concentrations of Fe and Zn in the solder were also significantly reduced.
Any scratch phases formed during the cooling process were removed (not shown) and recycled upstream in the process to the melting out step so that the valuable metals contained therein could be valorized as much as possible.
Table 1: The crude solder after the cooling step Weight% Crude solder 1 Bi | 00163 3.0000 0.0007 0.0015 Pb | 69.5000 0.8305 26.7414 0.0028 0.0290 0.0010 0.0515 0.0010 0.0125 0.0025 0.0007 | Total [| 100.1914 | In a second part of the purification process sequence 100, solid sodium hydroxide (stream 2) was added to the solder intermediate of Table 1. In this treatment step, zinc was bound by the sodium hydroxide, presumably to form Na 2 ZnO 2, and formed a separate phase which formed as a first supernatant solid scratch separated from the solder, and which was removed as stream 4. As a result, the content of zinc in the solder stream 6 was further reduced. The amount of sodium hydroxide was adjusted so that the concentration of Zn in the solder was reduced to 13 ppm by weight (Table 2). The scratch formed in this step was also recycled (stream 4) to the upstream smelting step, where zinc can be fumigated and recovered as zinc oxide dust.
In the next part of the purification process sequence 100, after the addition of sodium hydroxide and the removal of the first supernatant solid scratch phase 4, an amount of elemental sulfur was also added (stream 3), which represented about 130% stoichiometry relative to the amount of copper present in the metal phase to further reduce the copper content of the solder.
The elemental sulfur used was a granulated form of sulfur available from Zaklady Chemiczne Siarkopol in Tarnobrzeg (PL). The sulfur 3 reacted mainly with copper to form copper sulfides, which turned into a second supernatant scratch.
That second supernatant scratch was then removed as stream 5 and recycled to a suitable upstream process step.
After the addition of sulfur in step 100, an additional amount of sodium hydroxide (stream 2) was added to chemically bind any remaining traces of sulfur, and form another scratch.
After some time for the reaction to take place, a handful of granular sulfur 3 was sprinkled / spread over the surface of the bath.
The sulfur caught fire and burned any hydrogen that might have evolved from the liquid as a byproduct of the reaction.
Then, a small amount of white sand was scattered / spread over the bath to dry / stiffen the scratch before removing it from the process (stream not shown in the drawing) and recycling it to an upstream process step.
The purified solder thus obtained (stream 6, the flow rate and composition of which are indicated in Table 2) contained only 38 ppm Cu and was further processed as the molten solder mixture obtained from pretreatment step 100 by vacuum distillation in step 200. The second supernatant scratch 5 was reprocessed in the upstream refining process so that the valuable metals contained therein could be valorized.
Table 2: Purified solder for vacuum distillation Weight% | Molten solder mix - 6 Bi | 0.0326 0.0038 0.0004 0.0009 Pb | 73.1206 0.8012 25.8694 0.0013 0.0500 0.0871 0.0015 0.0020 0.0202 0.0053 0.0010 99.9973 The molten solder mix 6 was further processed using vacuum distillation (step 200 ), at an average temperature of 982 ° C and an average absolute pressure of 0.012 mbar (1.2 Pa). The vacuum distillation step yielded two product streams.
On the one hand, as top stream 7, a first concentrated lead stream was obtained which mainly contained lead, and on the other hand, as the first bottom product 8 of the first distillation step 200, we obtained a product stream containing mainly tin.
The flow rates and compositions of these two distillation product streams 7 and 8 are indicated in Table 3.
Table 3: Product flows from the first vacuum distillation 200 7 8 Bi | 0.0425 0.0014 0.0000 0.0122 0.0000 0.0015 0.0000 0.0028 Pb | 99.5375 1.0055 0.2233 1.9800 0.1006 96.3129 0.0018 0.0001 0.0031 0.1400 0.0746 0.0700 0.0000 0.0043 0.0024 0.0000 0. 0057 0.0460 0.0071 0.0000 0.0014 0.0000 100.0000 99.5767 The first vacuum distillation step 200 was performed in continuous mode, and was able to continue to function for a period of approximately three (3) years without observing any blockage or plugging of the distillation equipment due to the formation of metal-metal or intermetallic compounds.
The first concentrated lead stream 7 became available from the distillation equipment at a temperature of about 562 ° C. The temperature of stream 7 was controlled to about 450 ° C with stirring before the stream was further refined. Successive volumes of 100-120 tons of stream 7 were collected in a reservoir. Those volumes were subjected in batches to the soft lead refining process 700. A sample was taken from each batch and analyzed for the presence of As, Sn and Sb to determine the amounts of solid sodium hydroxide (stream 24) and solid sodium nitrate (stream 25) that were required. to react with the As, Sn and Sb present in the metal phase, and those amounts were added as the first base and first oxidant. The sampling and analysis was repeated over time for the reaction to take place and after removing the third supernatant scratch 26 formed by the reaction. If the result was not satisfactory, the method step was repeated. For the total volume of soft lead produced during the 73 day operating period, 29.3 tons of sodium hydroxide (401 kg / day) and 15.5 tons of sodium nitrate (212 kg / day) were used in the process to remove most of the the mean 46 kg / day As, 62 kg / day Sn and 138 kg / day Sb, in total mean 246 kg / day of the 3 elements together, present in the feed to step 700 with stream 7. This refining step constituted in each batch a third supernatant scratch phase containing most of the As, Sn and Sb present in the first concentrated lead stream 7 and removed as by-product (stream 26). The third supernatant scratch phase was sampled and analyzed for the presence of chlorine using the method according to the standard DIN EN 14582. The analysis showed that approximately 129 ppm by weight of chlorine was present. The high quality soft lead product 27 was then poured into molds and allowed to solidify and cool to lead ingots.
In most of the batches, a small amount of copper 23 was added in the feed to step 700 to produce an amount of Cu-containing soft lead. The small amount of copper present improves the mechanical properties of the soft lead, making the soft lead more suitable for being rolled into lead film for the construction industry or for plating surfaces with lead. Some batches containing above average levels of Bi were also separately stored as Bi-rich soft lead, which is acceptable in certain end uses and has the advantage of making Bi-containing basestocks more acceptable for the process of the present invention and / or for the upstream processes that provide feedstock for it. This soft lead refining was performed in batches in the same equipment as the hard lead refining discussed later. The transition between the cargoes of soft lead and hard lead produces a quantity of quality intermediate material, which is traded as “unrefined soft lead”. The average daily production rates (spread over the production period of 73 days discussed here) and compositions of the various soft lead end product streams 27 are indicated in Table 4. Table 4: Composition of the soft lead end products 27 (weight%) Soft lead - Unrefined soft lead With Cu Bi-rich products 27 labeled Soft lead Soft lead
[Bi | 0.0905 0.0319 0.0568
0.0001 0.0428 0.0008
0.0000 0.0000 0.0000
0.0000 0.0000 0.0000
Pb | 99.6306 99.9026 99.9240
0.2279 0.0000 0.0000
0.0208 0.0006 0.0004
0.0001 0.0001 0.0001
0.0032 0.0034 0.0025
0.0259 0.0002 0.0002
0.0002 0.0000 0.0000
0.0007 0.0001 0.0001
0.0006 0.0003 0.0003
0.0000 0.0000 0.0000
0.0000 0.0000 0.0000
99.7727 99.9820 99.9852
The first bottoms 8 from first vacuum distillation step 200 was mixed with the third bottoms 22 from downstream third vacuum distillation step 600 and the mixture was fed to the fourth zone of a first crystallizer with 12 temperature zones.
The crystallizer was a cylindrical vessel, slightly tilted from a fully horizontal position, and included an internal rotating screw to move the formed crystals from the bottom end to the top end of the cylindrical vessel.
The temperature zones were numbered 0 to 11 from the bottom end to the top end.
A temperature profile was established within the crystallizer using appropriate heating and cooling means.
The temperature of zone 3, into which the feed entered, was controlled maintained at about 210 ° C.
The temperature increased in steps from Zone 3 to Zone 11 (230-250 ° C), upwards in the crystallizer, where the tin-rich crystals are removed from the device. The temperature decreased slightly in a downward direction in the crystallizer from zone 3 to zone 0 (199 ° C), but rose again in zone 0, to about 220 ° C, to ensure that the temperature in that zone is always above the liquidus line remained in the phase diagram to prevent solids build-up on the propeller blades, which could otherwise result in necessary technician intervention and a temporary shutdown of the equipment. Before the feed stream was supplied to the crystallizer, the stream was passed through a buffer vessel, with a delay of several hours from production, where mixing compensated for any temperature changes that might have occurred upstream such that the temperature of the feed entering the crystallizer entering zone 3 is fairly constant and any changes take place very slowly. In addition, the temperature of the feed to zone 3 was kept slightly higher than the temperature in zone 3 of the crystallizer to prevent the formation of solids in the feed system. By entering zone 3 of the crystallizer, the feed stream is cooled and enters the range where a stream of this composition separates into a solid phase of small crystals enriched in tin, in equilibrium with a liquid phase that is leaner in tin but richer in lead and precious metals. The increase in the temperature of the liquid moving down in the crystallizer from zone 1 to 0 brought the advantage of preventing the solids build-up on the outside of the blades of the screw in the lower part of the cylindrical container, leaving enough space under the vanes of the screw to allow fluid to flow from the top end of the cylindrical container to the bottom end.
The crystallizer was tilted such that the liquid phase in the vessel was readily able to move from the top end to the bottom end of the device under the force of gravity. The rotating screw in the crystallizer moved the crystals in the opposite direction through the continuous liquid phase contained in the crystallizer. The liquid level in the crystallizer was maintained below the crystal overflow point to minimize liquid entrainment with the first tin-enriched product, but high enough to promote heat transfer from the vessel wall to the contents of the vessel. the barrel.
The crystals arriving at the top end were enriched in tin, and substantially all of the lead and precious metals from the feed was recovered in the liquid first bleed stream exiting the crystallizer at the bottom end.
The first bleed stream further contained tin in a significant amount, but at a concentration below the level of tin in the crystallizer feed.
The Sn crystals were removed from the top end of the first crystallizer and introduced into the fourth zone (again zone 3) of a second crystallizer which also had 12 temperature zones numbered from 0 to 11. The second crystallizer was also used. applied a temperature profile, similar to that in the first crystallizer, which caused further separation of a second liquid draw-off stream from the first tin-enriched crystals before those crystals exited the second crystallizer at the top end (stream 10). The antimony entering with the crystallizer feed mainly follows the path of the main inflow.
The bleed stream from the second crystallizer was recycled to the first crystallizer where it was mixed with the feed.
When the concentration of Pb was considered too high, the second crystallizer bleed stream was temporarily recycled to the upstream vacuum first distillation stage 200 feed to maintain a higher Ag concentration factor from vacuum distillation bottoms stream 8 to net first silver enriched liquid bleed product 9. Also As the concentration of Cu increased in the crystallizer streams, and thus also in the take-off stream of the second crystallizer, this take-off stream was - at least temporarily - preferably recycled to a process step further upstream than the feed to the first crystallizer, at Preferably to feed the first step of the purification process sequence 100, to be mixed with the crude solder composition 1.
The first silver-enriched liquid bleed product exited the first crystallizer as an Sn / Pb alloy by-product containing most of the Ag present in the crystallizer feed.
The flow rates and compositions of the outlet product streams 9 and 10 of the assembly of 2 crystallizers in step 300 are shown in Table 5. It was found that enrichment of Sb was also occurring in the first tin-enriched crystal phase exiting the second crystallizer, but some Sb was also recovered in the first silver-enriched liquid tap product.
The silver-enriched liquid draw-off product 9 of Table 5 represents the net draw-off volume and composition.
Temporarily, and depending on its composition, a recycle of the silver-enriched liquid bleed product was carried out from the lower end of the first crystallizer to the feed of the first crystallizer, to further increase the Ag concentration factor of the crystallizer feed (flows 8 + 22) to the net first silver-enriched liquid tap product 9. Table 5: Product flows of the crystallizer assembly Weight% First on First silver-enriched | tin enriched liquid product interception product 10 9
Bi | 0.0079 0.0010
0.2900 0.0014
0.0012 0.0016
0.0215 0.0023
Pb | 165000 0.2387
0.4020 2.1000
79.5000 97.0536
0.0042 0.0000
2.8000 0.0100
0.1144 0.0680
0.0001 0.0000
0.1039 0.0411
0.0000 0.0000
0.0000 0.0000
0.0129 0.0034
99.7581 99.5211
The net first silver-enriched liquid draw-off product 9 from the first crystallizer was transferred to a downstream purification step (not shown) to recover all the noble metals as well as the Sn and Pb.
To this end, the silver-enriched liquid tap product was poured into anodes and subjected to an electrolysis step to produce cathodes containing pure Pb and Sn, and the other metals remained in the anode adhesives.
Typical conditions of this electrolysis step are: an electrolyte based on hexafluorosilicic acid (H2SiFe), fluoroboric acid and / or phenyl sulfonic acid; a temperature of about 40 ° C; a current density of 140-200 A / m °; spacing between the electrodes of about 100 mm.
Antimony can be added to the anode composition, typically up to a concentration of about 1.5% by weight. This has the advantage that the anode adhesives remain attached to the anodes and are not dispersed in the electrolyte.
In order to avoid a complete passivation of the anode, which would lead to an inhibition of the electrolysis, periodically and consecutively a portion of the anodes can be removed from the bath, their anode adhesives removed, for example mechanically, and then the cleaned anodes then can be placed back in the cell.
The anodes can also be designed so that the cleaned anodes have become so thin that it is more efficient and / or effective to melt them into new anodes.
These anode adhesives (on average about 180 kg / day) were recovered, for example by filtration, from the entrained electrolyte, and these anode adhesives contained about 20% by weight of silver and also a much smaller concentration of gold, along with most of the other metals that were present in the first silver-enriched liquid tap product, including antimony and optional platinum group metals (PGMs). The anode adhesives were further processed to recover the silver and other precious metals.
The filtrate was recycled to the electrolytic cell.
The first tin-enriched crystals from the second crystallizer were further processed through the second vacuum distillation step 400, performed at an average temperature of 1049 ° C and an average absolute pressure of 0.005 mbar (0.5 Pa). Over the 73 day run period, an amount of 157.6 tons of lead-containing feedstocks 11, averaging about 2.2 tons per day, was gradually added to the first tin-enriched crystals to keep the solidification point of the top product from step 400 low.
The flow rate and composition of stream 11 are indicated in Table 6. Table 6: Additive feedstock in feed to the second vacuum distillation Weight% Pb-containing feedstock 11 [Bi | 0.0299 0.0161 0.0018 0.0003 Pb | 58.8711 0.0006 41.0558 0.0001 0.0036 0.0015 0.0000 0.0017 0.0002 0.0000 0.0001 99.9827 The second vacuum distillation step 400 yielded two product streams.
On the one hand, we obtained as top product 12 a product stream that mainly contained most of the lead, antimony and silver from the feed, plus a small amount of tin, and on the other hand, as the second bottom product 13, we obtained a product stream that mainly contained tin with only trace amounts of other ingredients.
The flow rates and compositions of these two distillation product streams 12 and 13 are shown in Table 7.
Table 7: Product flows from the second vacuum distillation Weight% | Top current | Soil flow 12 13 Bi | 0.0189 0.0004 0.0000 0.0028 0.0000 0.0019 0.0000 0.0025 Po [| 37.8602 0.0011 13.0000 0.3800 47.7097 99.4584 0.0000 0.0000 0.0560 0.0029 0.3900 0.0178 0.0000 0.0036 0.0000 0.0000 0, 3050 0.0006 0.0001 0.0000 0.0000 0.0000 99.3400 99.8719 The second vacuum distillation stage 400 was run in continuous mode, and was able to continue to function for a period of approximately three (3) years without observing any blockage or plugging of the distillation equipment due to the formation of metal-metal or intermetallic compounds.
The second bottoms 13 from step 400 was further refined in batches in three consecutive steps, which are shown together in the flow chart as tin refining step 500. The first tin refining step consisted of cooling the second bottoms 13 and adding an amount of aluminum nuggets (stream 14). ) to the second bottoms, which had an average temperature of 430 ° C, with stirring, to react with Sb and As and remove those elements to a level that met prevailing international industrial standards.
The amount of Al to be added was based on an analysis of the second bottoms 13, and included an additional amount above the stoichiometric requirement.
After the reaction, the composition was analyzed again, and if the result was unsatisfactory, in particular the content of Sb, an additional amount of Al was added to trigger a second reaction step.
In total, an amount of about 4.3 kg Al per tonne of second bottom product 13 was used on average.
About 30 minutes after the last addition, heating and agitation were stopped and the liquid molten metal composition was allowed to cool.
During cooling, to an average temperature of about 250 ° C, a layer of scratch containing Al / Sb / As was formed, and that scratch was periodically removed from the surface of the molten liquid metal.
The scratch was collected and stored in dry, closed and double-walled steel drums to avoid contact with water or moisture, which could lead to the formation of stibine and / or arsine.
The vessels were removed as by-product (stream 17) and recycled to an upstream pyrometallurgical process step, where they were introduced unopened into a liquid bath of molten metal and / or slag, avoiding any risk of contact with moisture.
After the temperature of the tin product was raised again to about 330 ° C, the molten liquid metal was subjected to a second tin refining step, in which solid sodium hydroxide (stream 15) was added as the third base.
In that treatment step, aluminum was bound by the sodium hydroxide, presumably to form NasAlO3, and formed a separate phase which separated as a supernatant solid scratch from the molten liquid metal and was removed as stream 18. After a period of time every To allow the reaction to take place, a handful of granular sulfur was scattered / spread over the surface of the bath.
The sulfur caught fire and burned any hydrogen that could possibly have evolved from the molten liquid metal as a byproduct of the reaction.
As a result, the content of aluminum in the second bottom product 13 was further reduced.
The amount of sodium hydroxide to be added was adjusted so that the concentration of aluminum in the second bottoms product decreased to less than the detection limit of 1 ppm by weight (Table 8). The scratch formed in this step was also recycled (stream 18) to an upstream pyrometallurgical process step.
In the third and final tin refining step, an amount of elemental sulfur (stream 16) was added to further reduce the copper content of the molten liquid metal and to remove any residual sodium hydroxide from the second tin refining step. The elemental sulfur used was a granulated form of sulfur available from Zaklady Chemiczne Siarkopol in Tarnobrzeg (PL). The sulfur 16 reacted mainly with copper to form copper sulfides and with sodium hydroxide to form Na2SO2, which transitioned to a new supernatant scratch phase. After the addition of sulfur, the stirrer was run for about 10 minutes to oxidize any remaining traces of sulfur and form a new scratch. The scratch was removed from the molten liquid metal as stream 19. The high purity Sn product thus obtained (stream 20, the flow rate and composition of which are indicated in Table 8) contained only 14 ppm Cu and was clumped into lumps. of 22 kg cast, stacked, weighed and tied. The scratch containing sulfur 19 was reprocessed in an upstream pyrometallurgical process step.
Table 8: High purity Sn final product Weight% | High purity Sn Bi | 0.0001 0.0014 0.0004 0.0000 Pb | 0.0008 0.0160 99.9758 0.0000 0.0030 0.0006 0.0001 0.0000 0.0006 0.0000 0.0000 0.0001 99.9989
The overhead product 12 from the second vacuum distillation step 400 was further processed in the third vacuum distillation step 600, performed at an average temperature of 1000 ° C and an average absolute pressure of 0.033 mbar (3.3 Pa). The third vacuum distillation step 600 yielded two product streams.
On the one hand, we obtained as top product 21 a product stream containing mainly lead and antimony, and on the other hand, as the third bottom product 22, we obtained a product stream containing mainly tin and part of the antimony, plus most of the precious metals present in the distillation feed.
The flow rates and compositions of these two distillation product streams 21 and 22 are shown in Table 9. Table 9: Product streams of the third vacuum distillation Weight% | Top current | Soil flow 21 22 Bi | 0.0474 0.0011 0.0000 0.0265 0.0000 0.0004 0.0000 0.0075 Pb | 90.1133 0.7827 9.1014 2.1363 0.5379 96.8647 0.0002 0.0001 0.0100 0.0950 0.4700 0.0730 0.0019 0.0000 0.1860 0.0297 0, 0022 0.0000 0.0013 0.0000 0.0000 0.0000 100.4716 100.0170 The third vacuum distillation step 600 was run in continuous mode, and was able to continue to function for a period of approximately three (3) years without observing any blockage or plugging of the distillation equipment due to the formation of metal-metal or intermetallic compounds.
The third bottoms product 22 was recycled to the first crystallizer from upstream step 300, where it was mixed with first bottoms 8 from step 200, to recover the valuable metals contained therein.
The overhead product 21 was further refined in step 800, in batches, in the same equipment used during the soft lead refining step 700 of the first concentrated lead stream as overhead stream 7 from the first vacuum distillation step 200. During the 73 day run, an additional 810 was added. , 2 tons of top product from the third vacuum distillation left over from previous campaigns (stream 29), averaging about 11.1 tons / day, mixed with stream 21 and co-refined. The refining of this hard lead was done in batches in volumes of 100-120 tons total feed. During the 73 days of operation discussed in this example, approximately 9 days were devoted to refining 1159 tons of hard lead, versus approximately 129 tons / day, and the equipment was used for 43 days to refine 4400 tons of the soft lead products as described above average at about 102 tons / day.
The hard lead molten liquid metal feed stream for hard lead refining step 800 was first heated to about 450 ° C with agitation. A sample was taken and analyzed for the presence of As and Sn to determine the amounts of solid sodium hydroxide (stream 30) and solid sodium nitrate (stream 31) that were considered necessary to remove the As and Sn from the molten liquid metal phase, and those amounts were added as the second base and the second oxidant. Over the 73 day operation period considered for this example, a total of 15.2 tons of sodium hydroxide (average 208 kg / day) plus 7.6 tons of sodium nitrate (average 104 kg / day) was added in this refining step for the removing most of the average 26 kg / day As and 32 kg / day Sn that entered step 800 with flows 21 and 29 together. Almost all of the 1502 kg / day of Sb present in the feed streams to hard lead refining step 800 remained in the purified hard lead product 28. This hard lead refining step formed a total fourth supernatant scratch phase containing most of the As and Sn present in the top products 21 and 29 and removed as by-product (stream 32). The fourth supernatant scratch phase was sampled and analyzed for the presence of chlorine using the method according to DIN EN 14582. The analysis showed that approximately 130 ppm by weight of chlorine was present.
The flow rate and composition of the purified running end product stream 28 are indicated in Table 10. Table 10: Composition of the end running hard product Weight% | Hard lead 28
Bi | 0.0550
0.0000
0.0000
0.0000
Pb | 914680
8.9900
0.0192
0.0001
0.0112
0.0025
0.0002
0.0005
0.0005
0.0000
0.0000
100.5472 Thus, this hard lead refining step in step 800 only intended to remove a total of an average of 58 kg / day of impurities, which is significantly less than the removal intended by step 700.
In addition, the concentrations of As and Sn in the feed to step 800 were also higher than those in the feed to step 700. Step 800 therefore achieves its goals much more easily than step 700. Relative to the total amount (As + Sn + Sb) entering the respective lead refining steps 700 and 800, step 800 consumes significantly less chemicals and also produces significantly less supernatant scratch than step 700, which also has the advantage of putting less burden on recirculating the supernatant scratch in the upstream pyrometallurgical process.
It was also observed that in step 800 As and Sn could be successfully removed to very low levels, while hardly any Sb needed to be removed.
Having now fully described the present invention, it will be apparent to those skilled in the art that the invention can be practiced with a wide range of parameters within the scope of the claims, without departing from the scope of the invention as defined by the claims.

权利要求:
Claims (35)
[1]
A process for the production of a purified soft lead product (27), comprising a) a first distillation step (200) for distilling lead from a molten solder mixture (6) comprising lead and tin to produce as the overhead a first concentrated lead stream ( 7) and produce as the first bottoms product a molten crude tin mixture (8), and b) a soft lead refining step (700) for removing at least one contaminant selected from the metals arsenic, tin and antimony from the first concentrated lead stream ( 7) obtained in step a) (200) by treating the first concentrated lead stream (7) at a temperature of less than 600 ° C with a first base (24) and a first oxidant (25) that is stronger than air, resulting in the formation of a third supernatant scratch (26) containing a metalate compound of the affected contaminant metal, followed by the separation of the third supernatant scratch (26) from the purified soft shed cream or the purified soft lead product (27), wherein the third supernatant scratch (26) from step (b) (700) contains at most 1.0% by weight chlorine, and preferably at most 1.0% by weight of total halogens.
[2]
The method of claim 1 wherein the first oxidant (25) stronger than air in step (b) (700) is selected from NaNO3, Pb (NOs) 2, KNO: 3, ozone, nitric acid, sodium and potassium manganate , sodium and potassium (per) manganate, chromic acid, calcium carbonate (CaCOs), sodium and potassium dichromate, preferably NaNO3, CaCOs, Pb (NO3), or KNOs, more preferably NaNO3.
[3]
The method of claim 1 or 2 wherein the first base (24) is selected from NaOH, Ca (OH) 2 and Na2CO3 and combinations thereof, preferably NaOH.
[4]
The method according to any of the preceding claims, wherein the weight ratio of the first base (24) to the first oxidant (25) used in step (b) (700) is in the range of 1, 5: 1.0 to 4.0: 1.0, preferably in the range of 2: 1 to 3: 1 when NaOH is used as the first base (24) and NaNO: is used as the first, respectively oxidant (25), and recalculated by stoichiometry for when other compounds are used as the first base (24) and / or the first oxidant (25).
[5]
The method according to the preceding claim wherein the weight ratio of the first base (24) to the first oxidant (25) used in step (b) (700) is at most 2.90 when NaOH is used respectively as the first base (24) and NaNO: is used as the first oxidant (25), and recalculated by stoichiometry for when other compounds are used as the first base (24) and / or the first oxidant (25).
[6]
The method of any one of the preceding claims, wherein in the first bottoms (8) of step (a) (200) at least 0.10 wt% lead remains.
[7]
The method according to any of the preceding claims, wherein the first concentrated lead stream (7) comprises at least 0.0400 weight% and at most 0.3000 weight% tin.
[8]
The method of any one of the preceding claims, wherein the third supernatant scratch (26) from step (b) (700) contains less than 1.0% by weight chlorine, and preferably less than 1.0% by weight. % total halogens.
[9]
The method of any one of the preceding claims, wherein the third supernatant scratch (26) from step (b) (700) is recycled to a method step upstream of step (a) (200).
[10]
The method of any one of the preceding claims, wherein the first base (24) and the first oxidant (25) are mixed together before being introduced into step (b) (700).
[11]
The method according to any of the preceding claims, wherein the first distillation step (a) (200) is carried out at a pressure of at most 15 Pa absolute.
[12]
The method of any of the preceding claims, wherein the first distillation step (a) (200) is performed at a temperature of at least 800 ° C.
[13]
The method according to any of the preceding claims, wherein the first distillation step (a) (200) is performed in a continuous operating mode.
[14]
The method of any preceding claim wherein the feedstock for the distillation step (a) (200) is a crude solder composition (1) containing significant amounts of tin and lead and containing at least 0.16% by weight and possibly not more than 10% by weight of the total of chromium (Cr), manganese (Mn), vanadium (V), titanium (Ti), tungsten (W), copper (Cu), nickel (Ni), iron (Fe ), aluminum (Al) and / or zinc (Zn), the feedstock (1) being available at a temperature of at least 500 ° C, the method further comprising the step of pretreating (100) the crude solder composition ( 1) before step (a) (200) to form the molten solder mixture (6) as feedstock for the first distillation step (a) (200), the pretreatment step (100) comprising the steps of C) cooling the feed raw solder composition (1) up to a temperature not exceeding 825 ° C, to produce a bath that has a first e scratch (4) that floats by gravity on a first liquid molten metal phase, d) adding a chemical (2) selected from an alkali metal and / or an alkaline earth metal, or a chemical compound containing an alkali metal and / or an alkaline earth metal, on the first liquid molten metal phase to form a bath containing a second supernatant scratch (5) that floats by gravity on a second liquid molten metal phase, and e) removing the second supernatant scratch ( 5) of the second liquid molten metal phase to obtain the molten solder mixture (6).
[15]
The method of any one of the preceding claims, wherein the molten solder mixture (6) comprising lead and tin and supplied to the first distillation step (a) (200) comprises by weight:
° at least 90% tin and lead together, ° more lead than tin, ° not more than 0.1% of the total of chromium (Cr), manganese (Mn), vanadium (V), titanium (Ti) and tungsten (W ), ° no more than 0.1% aluminum (AI), ° no more than 0.1% nickel (Ni), ° no more than 0.1% iron (Fe), and ° no more than 0.1% zinc (Zn).
[16]
The method according to any one of the preceding claims, wherein the molten solder mixture (6) comprising lead and tin and which is fed to the first distillation step (a) (200), by weight at least 1 ppm by weight and at least maximum 5000 ppm by weight of copper.
[17]
The method of any one of the preceding claims wherein the first bottoms product (8) contains silver and wherein the first bottoms product (8) is separated by fractional crystallization (300) into a first silver enriched liquid tapping product (9) at the liquid end of the crystallization step and a first tin-enriched product (10) at the crystal end of the crystallization step.
[18]
The method according to the preceding claim, wherein the first bottoms product (8) and / or the feed to the fractional crystallization step comprises at least 0.1% by weight and at most 20.0% by weight of lead.
[19]
The method of any of claims 17-18 wherein the concentration of lead in the first bottoms product (8) and / or the feed to the fractional crystallization step is at least 3.0 times the concentration of silver in the first bottoms (8).
[20]
The method according to any one of claims 17-19 wherein the first bottoms product (8) and / or the feed to the fractional crystallization step is at least 10 ppm by weight of silver (Ag) and optionally at most 0, 85% silver by weight.
[21]
The method of any of claims 17-20 wherein the first bottoms product (8) and / or the feed to the fractional crystallization step comprises at least 0.1% by weight of antimony (Sb).
[22]
The method of any of claims 17-21, wherein the first silver enriched liquid bleed product (9) is partially and / or temporarily recycled to the feed of the fractional crystallization step (300).
[23]
The method of any of claims 17-22 wherein at least one product (9) from the liquid end of at least one crystallizer in the fractional crystallization step (300) is at least partially recycled to the feed of the first distillation step a) (200).
[24]
The method of any of claims 17-23 wherein at least one product (9) from the liquid end of at least one crystallizer in the fractional crystallization step (300) is at least partially recycled to the feed of the pretreatment step of crude solder (100).
[25]
The method according to any of claims 17-24 wherein the first tin-enriched product (10) and / or the first bottoms product (8) is subjected to a second distillation step (400) containing predominantly lead and antimony by evaporation. separates from the first tin-enriched product (10) and / or the first bottoms product (8), thereby producing a second concentrated lead stream (12) as the top product and producing a second bottoms product (13).
[26]
The method of the preceding claim, wherein a fresh feed containing lead (11) is added to the feed of the second distillation step (400).
[27]
The method of any of claims 25-26 wherein the second concentrated lead stream (12) is subjected to a third distillation step (600) that separates predominantly lead and antimony from the second concentrated lead stream (12) by evaporation, wherein as a top product a third concentrated lead stream (21) is produced and a third bottoms product (22) is produced.
[28]
The method of the preceding claim, wherein a fresh feed containing lead (34) is added to the feed of the third distillation step (600).
[29]
The method of any of claims 27-28 wherein the third bottoms product (22) is at least partially and preferably completely recycled to the feed of the second distillation step (400) and / or to the feed of the fractional crystallization step (300).
[30]
The method of any of claims 27-29 further comprising the step (800) of removing at least one contaminant selected from the metals arsenic and tin from the third concentrated lead stream (21), thereby a purified hard lead stream is produced as a hard lead product (28).
[31]
The method according to any of claims 25-30, wherein the second bottoms product (13) is further refined to obtain a high purity tin product (20).
[32]
The method of the preceding claim wherein the second bottoms (13) is treated with aluminum metal (14), preferably in stoichiometric excess to the amount of antimony present, preferably in combination with mixing and cooling the reacting mixture to less than 400 ° C, followed by separating the scratch containing Al / Sb / As (17) formed by the treatment.
[33]
The method according to the preceding claim, wherein the second bottom product (13), after the treatment with aluminum and preferably also after the removal of the scratch containing Al / Sb / As (17), is treated with a third base (15). ), which is preferably selected from NaOH, Ca (OH) 3 and Na: CO: and combinations thereof, more preferably NaOH, followed by separating the scratch containing base (18) formed by the treatment.
[34]
The method of the preceding claim wherein the second bottom product (13), after the treatment with the third base (15), is treated with sulfur (16), followed by separating the scratch containing S (19) that is formed. through the treatment.
[35]
The method of any one of the preceding claims, wherein at least a portion of the method is electronically monitored and / or controlled.

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法律状态:
2020-10-12| FG| Patent granted|Effective date: 20200828 |

优先权:

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申请号 | 申请日 | 专利标题

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EP19154606|2019-01-30|

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