Patent Application
20080260612
The present invention relates to processes for removal and capture of impurities from metal ores, recycled materials and compounds as part of the extraction, purification and/or refining processes.
The object of the present invention is to provide an improvement in metal extraction processes (and the like) focused on effective realization of target metal compounds, oxides and sub-oxides and the efficient removal of unwanted materials in an energy efficient manner. Materials of adequate purity are to be achieved while reducing overall processing costs, improving the efficiency of environmental protection and allowing for additional energy recovery.
Many metal ores and recovered materials have large portions of metal compounds in the form of sulfides, carbides, hydrides, nitrides and other compound forms that require oxidation purification. Typical processing methods primarily targeting the refining and recovery of metal values from sulfide ores, as an example, may involve mechanical sizing of ores, froth flotation, electro-winnowing, solvent extraction, smelting, roasting, electro-refining, slow oxidation processes assisted by microorganisms, pressure oxidation, digestion of the ores or compounds in acid and molten salt fusion. Other metal and mineral recovery processes produce carbides, hydrides, nitrides, and mixed organic complex materials also requiring oxidation purification. Recovery of merchantable sulfur, carbon, and hydrogen containing by-product compounds can be an important benefit of such processes.
It is disclosed in U.S. Pat. No. 4,552,749 to oxidize metal sulfide materials to sub-oxides. In the referenced patent MoS.sub.2 is oxidized to MoO.sub.2 by reacting it with MoO.sub.3. Finely divided MoO.sub.3 and MoS.sub.2 are mixed together in the ratio of about seven or more moles of MoO.sub.3 to one mole of MoS.sub.2. This mixture is then heated to 600.degree. C.-700.degree. C. in a closed chamber where SO.sub.2 is evolved. The MoO.sub.2 product is then desulfurized at 400.degree. C.-600.degree. C. in an atmosphere containing 10 wgt. % or less SO.sub.2 and thereafter cooled in a neutral or reducing atmosphere to 250.degree. C. A portion of the MoO.sub.2 is removed from the reactor as a product and the remainder is selectively oxidized at a temperature sufficient to generate gaseous MoO.sub.3 which is recycled to the reactor relative to the flow of MoS.sub.2 therein to convert the MoS.sub.2 to MoO.sub.2. Although this method was employed to produce MoO.sub.2 the process could not be carried out in a continuous manner because the second step of the reaction resulted in the sublimation of the MoO.sub.3 in the case of flash reactors or sintering and balling problems in the case that kilns, multiple hearth furnaces or other furnace devices were employed. These sublimation, sintering, and balling problems have made it impractical to effectively recycle the MoO.sub.3 to the first reactor without the need for consolidation and densification or milling and blending operations. These physical handling steps eliminated the ability of the process to operate in a continuous manner and for maximum energy efficiency. Other methods for producing MoO.sub.2 have involved reducing MoO.sub.3 with H.sub.2, NH.sub.3 or carbon and these also have limits of effectiveness.
One other embodiment for producing MoO.sub.2 by reacting MoO.sub.3 with MoS.sub.2 is disclosed in U.S. Pat. No. 3,336,100. The process as claimed comprises mixing MoO.sub.3 with MoS.sub.2 to provide a uniform mixture containing substantially stoichiometric amounts of the reactants. The mixture is reacted at a temperature between 600.degree. C. and 700.degree. C. in a closed chamber to evolve SO.sub.2. The pressure in the chamber is maintained at slightly above atmospheric pressure to prevent air from entering the chamber and form a product having a low sulfuric content. The desulfurization is carried out in an atmosphere containing less than 10 wgt. % SO.sub.2 and at a temperature substantially between 400.degree. C. and 600.degree. C. to obtain MoO.sub.2. Following the reaction, the molybdenum dioxide (MoO.sub.2) is cooled at least to 250.degree. C. under either a neutral or a reducing atmosphere.
Reducing MoO.sub.3 with H.sub.2 or NH.sub.3 is very expensive and reactions with solid reductants usually produce an impure product. Reacting MoS.sub.2 and MoO.sub.3 at 600.degree. C.-700.degree. C. is a slow reaction which requires two hours or longer and which results in a product which must be treated to desulfirize to an acceptable sulfur value. It also requires several furnaces for the different SO.sub.2 levels which are maintained in the gas. Another disadvantage is that a 25% or more stoichiometric excess of MoO.sub.3 must be used in order to obtain a low sulfur product. Thus the product is generally not MoO.sub.2 per se but a mixture of MoO.sub.2 and MoO.sub.3.
The present invention recognizes and fills a need for a process for producing metallic sub-oxides from metallic sulfides, carbides, hydrides, nitrides and other compound forms which is fast, efficient and allows for a continuous recycle of the fully oxidized product of the second reactor wherein that second reactor product exhibits good density and fine particle size structure and which provides a second reactor product which is low in sulfur and can be recycled to the first reactor as an effective oxidizing agent for the first reactor. It would further be desirable if said second reactor product could be recycled to the first reactor at temperature thus providing the system with greatly
As applied to sulfides (and extendable to metal extraction for other metal compounds), the above stated object of the invention is achieved by a two-step looping sulfide oxidation process. The process separates the (inorganic or organic) sulfide oxidation process into at least two reaction steps. In the first step a main metal oxidation process is conducted reacting the sulfide (e.g. metal sulfide) with an oxide solely or primarily derived from the starting material or supplemented by a make-up oxidizer from an external source, or an oxide of another material of desired material content to produce a metallic compound or a metal sub-oxide and, in a subsequent step or steps, the compound or sub-oxide material, as produced in the first step, is further oxidized raising the sub-oxide to a higher oxidation level. All or part of the oxide produced in the second step can be recycled to the first step as a sole or primary oxidizing agent but ultimately can be recovered. The present invention may be applied with particular benefit to the sulfides of the metals: Ag, Ni, Fe, Co, Cu, Zn, Sn, Pb, and mixed sulfide minerals of the following materials: FeNi, NiCo, PbZn and FeCu (chalcopyrite). This process can be further extended and tailored to process inorganic sulfides, organo-sulfides, inorganic sulfates, organo-sulfates, inorganic carbides, inorganic carbonates and organo-carbonates. Two illustrative cases, for metal sulfides, are as follows:
In the example of a metal sulfide ore or derivative (or recycled product) the material can thus be processed in a two step oxidation process that yields a metal sub-oxide and a high concentration sulfur oxide gas stream. Then, in the second step, the sub-oxide is further oxidized to at least a higher oxidation state, preferably to fully oxidized stoichiometry, to efficiently generate energy and an oxide that can be recycled to the first reactor as the oxidizing agent for the first step of the process. Major improvements in the process embodiment have been achieved through a dilute reactant oxidation process as applied to this reaction step. Through dilute reactant processing the sub-oxide to be processed is fed to the second reactor while the second reactor is more than 50% filled with the more fully oxidized product. In this way the reacting sub-oxide is diluted to the point that sublimation can be controlled and sintering and balling is eliminated. It is also possible to expand this process concept to multiple steps of partial oxidation which can allow for the production of commercially interesting intermediate sulfates, carbonates, nitrates, sub-oxides, and combinations of these compounds.
In the example of sulfide ores, the first step efficiently removes sulfur materials in a concentrated manner as sulfur oxide for recovery, use, or for further reaction to produce sulfur, sulfates or other derivatives. In the second step of the process the second oxidation can be carried out in a way that maximizes oxidation kinetics and energy recovery. Since environmentally harmful impurities can be removed in the first step reaction, the second oxidation can be carried out in a way that no sulfur, carbon, or nitrogen containing gases are produced which allows for aggressive energy recovery and minimal environmental costs. The second step reforms the oxidizing agent used in the first reaction.
The separation allows a two step process that efficiently removes unwanted chemicals and environmentally damaging chemicals in the first step. Then in the second step the material can be further oxidized without a contaminated off-gas stream allowing for ease of processing and maximum energy recovery.
The foregoing process can be applied similarly to other chemical families, e.g. carbides, carbonates, hydrides, nitrides and nitrate, organic containing mixtures or compounds containing these materials and materials found separately from or in combination with metal containing materials. The process can also be used in recycling tailings, previously used chemicals, catalysts, carbides, nitrides, organic metal complex materials or mixed waste products.
Other objects, features and advantages will be apparent from the following detailed description of preferred embodiments taken in conjunction with the accompanying drawing in which:
The reactors of the two steps in
In the reactors the reactions of the two steps above may be conducted, generally at 500-1000° C. temperature range and at atmospheric pressure or slightly above (up to 30 psi) except that in some instances a high pressure reaction step (pressure up to 1000 psi) may be used (e.g., via autoclave oxidation or aqueous oxidation or nitric acid oxidation in aqueous environment and at about 90-300° C. range). In the first step pressure is preferably slightly above atmospheric to exclude ambient air and use the oxide from the second step as sole or primary oxidizing agent (with a controlled admission of second make-up oxidizer if needed). The second step can be conducted in a closed environment as in the first step or in air (except for the high pressure variants described above).
Copper sulfide based ores (chalcocites) may be ground to 10-100 micron size range, and mixed with xanthate reagents and subjected to froth flotation to concentrate copper sulfide content, dried and then fed to a rotary kiln for reaction (1), i.e. oxidized in a reaction to produce sulfur oxide and metal sub-oxide and (2) the sub-oxide then oxidized to a higher oxidation state as follows:
(1) Cu2S+CuO→Cu2O+SO2 The sulfur oxide (in gas form) is removed for conversion to sulfur, a sulfate, or other useful form.
(2) The copper sub-oxide can be transferred to a separate rotary kiln or a downhill section of the original kiln partly isolated from the first section and exposed to oxygen or air for the reaction converting from a sub-oxide to oxide;
Cu2O+Air→CuO
CuO may be recycled as the oxidizer for step 1. The metals M, M1, M2 may be single elements or alloyed or mixed elements. The cupric oxide (CuII) produced in step (2) can be returned to the first reactor as the sole or primary oxidizer.
Another example of the process is provided for converting CoS to CoO wherein, CoS in particulate form is blended with Co3O4 and reacted to produce CoO and SO2. The temperature in the reactor is maintained at a level sufficient to cause the reaction to go forward. A portion of the CoO may be removed from the reactor as a product and the remainder is further oxidized in a second reactor at a temperature sufficient to generate Co3O4 which is recycled to the first reactor therein to react with and convert the CoS to CoO.
These examples can be varied as set forth above as to Case A vs. Case B and as applied to other reduced metallic compounds.
It will now be apparent to those skilled in the art that other embodiments, improvements, details, and uses can be made consistent with the letter and spirit of the foregoing disclosure and within the scope of this patent, which is limited only by the following claims, construed in accordance with the patent law, including the doctrine of equivalents.
| Number | Date | Country | |
|---|---|---|---|
| 60912550 | Apr 2007 | US |
