Process for treating ore having recoverable metal values including arsenic containing components

Abstract

Refractory gold ores are roasted in the presence of added fuels in an oxidizing atmosphere in a fluidized bed at a temperature from 450 to 650° C., which is supplied with oxygen-containing gases; to achieve a low ignition and thus low roasting temperature, sulfur, pyrite or mixtures thereof are used as added fuels.

Description

BACKGROUND OF THE INVENTION

1. Technical Field of the Invention

This invention relates to recovering precious metal and/or metal values from ores including refractory ores, ore concentrates, or ore tailing which include arsenic-, carbon- and/or sulfur-containing components and ores which are refractory to the recovery of precious metal values. Another aspect of the invention relates to a process of roasting refractory precious metal ores wherein added fuels, including sulfur, pyrite or mixtures thereof, are either pre-mixed with the ores or directly fed in during the roasting process. This aspect of the invention includes the proper employment of these added fuels in combination with the above process of recovering precious metals and/or metal values from ores.

2. Background Art

Precious metals, such as gold, occur naturally in ores in different forms. Unfortunately, precious metal ores also frequently contain other materials which interfere with the recovery of these precious metal values, rendering these ores refractory to precious metal recovery. Furthermore, the precious metal content may be at a relatively low level. This low level content compounds the effect of the refractory nature of these ores.

The following patents, hereby incorporated by reference, are illustrative of attempts to deal with refractory components in precious metals and other metals recovery as well as efforts in distinctly different fields addressed to solving the arsenic contamination problems encountered when roasting precious metal and other metal ores having arsenic as an unwanted component present in the ore.

U.S. Pat. No. 360,904 to Elizabeth B. Parnell relates to roasting gold or silver bearing ores using a double roasting schedule with the first roasting at 1100 to 1300 degrees Fahrenheit and the second roasting to 1200° F. to 1600° F. (the time occupied in the second roasting can be reduced by supplying oxygen along with the air).

U.S. Pat. No. 921,645 to J. E. Greenwalt discloses the roasting of ore by heating the ore on a porous granular bed through which air is forced from below.

U.S. Pat. No. 1,075,011 to N. C. Christensen, Jr. discloses a process for treating ore by means of a roasting oven which, by regulation of the fuel supply, may be either oxidizing, reducing, or neutral.

U.S. Pat. No. 2,056,564 to Bernart M. Carter discloses suspension roasting of finely divided sulfide ores. Roasting is in air or oxygen in which the temperature of the mixture entering the roasting chamber is controlled and to a corresponding degree the temperatures within the roasting chamber are thus controlled in an effort to prevent the formation of accretions on the walls of the apparatus.

U.S. Pat. No. 2,209,331 to Ture Robert Haglund discloses a process for the production of sulfur from the roasting of sulfide material in oxygen or air enriched with oxygen so that as soon as the free oxygen has been consumed in the formation of SO 2 , the iron sulfide reacts with the sulfur dioxide forming free sulfur and iron oxides.

U.S. Pat. No. 2,536,952 to Kenneth D. McCean relates to roasting mineral sulfides in gaseous suspension.

U.S. Pat. No. 2,596,580 to James B. McKay et al. and U.S. Pat. No. 2,650,169 to Donald T. Tarr, Jr. et al., relates to roasting gold-bearing ores which contain commercially significant amounts of gold in association with the mineral arsenopyrite. The patent describes the importance of closely regulating the availability of oxygen in order to provide enough oxygen so that volatile compounds of arsenic are formed while the formation of nonvolatile arsenic compounds is minimized.

U.S. Pat. No. 2,867,529 to Frank A. Forward relates to treatment of refractory ores and concentrates which contain at least one precious metal, sulfur and at least one arsenic, antimony or lead compound by roasting in a non-oxidizing atmosphere at a temperature above 900 degrees Fahrenheit, but less than the fusion temperature of the material being roasted.

U.S. Pat. No. 2,927,017 to Orrin F. Marvin relates to a method for refining metals, including precious metals, from complex ores which contain two or more metal values in chemical union or in such physical union as to prevent normal mechanical separation of the values. The method uses multiple roasting steps.

U.S. Pat. No. 2,993,778 to Adolf Johannsen et al. relates to roasting a sulfur mineral with its objects being—the production of sulfur dioxide, increasing the completeness of roasting and the production of metal oxides.

U.S. Pat. No. 3,172,755 to Angel Vian-Ortuno et al. relates to a process for treating pyrite ores bearing arsenic by subjecting the arsenic-containing pyrite ore to partial oxidation so as to oxidize only the labile sulfur of the arsenic-containing pyrite and subsequently heating the pyrite ore in a non-oxidizing gas to separate the arsenic from the ore and to form a residual ore free of arsenic.

U.S. Pat. No. 4,731,114 Gopalan Ramadorai et al. relates to a process for the recovery of precious metals from low-grade carbonaceous sulfide ores using partial roasting of the ores following by aqueous oxidation in an autoclave.

U.S. Pat. No. 4,919,715 relates to the use of pure oxygen in roasting of refractory gold-bearing ores at temperatures between about 1000° F. (537.8° C.) and about 1200° F. (648.9° C.). This patent fails to address the problem of arsenic volatilization, is silent on the arsenic content in the ore, and does not address in that context the optimizing of gold recovery from refractory sulfitic, carbonaceous ores or separation of cyanide consuming components before recovery of gold from the ore. The disclosed method requires two fluid beds and stage-wise roasting in these beds and the use of substantially pure oxygen (substantially pure oxygen being defined as at least about 80% by weight.)

European Patent Specification 0 128 887 discloses roasting sulfide concentrates having an average particle size below 1 mm and containing copper and noble metals as valuable metals as well as arsenic as an impurity. Volatization of arsenic is in a circulating fluidized bed under an oxygen partial pressure of 10 −14 to 10 −16 bars and at low temperatures, i.e. temperatures which exceed the breakdown and decomposition temperatures of arsenic compounds. A major part of the solids is removed under the same conditions in a hot cyclone from the suspension discharged from the fluidized bed reactor and is recycled to the fluidized bed reactor. Additional solids are removed from the gas in a second cyclone. After an optional fine purification in an electrostatic precipitator the exhaust gas is discharged through a chimney. The calcine from the circulating fluidized bed and eventually solids collected in the second cyclone are fed to a classical fluidized bed, in which the sulfur containing materials which are present are roasted at an increased oxygen potential. In the event the temperature falls below the sublimation temperature of the arsenic oxides contained in the exhaust gas from the circulating fluidized bed, arsenic oxides may be removed together with the residual solids. That exhaust gas may also contain volatilized sulfur.

German Patent Specification 15 83 184 discloses the removal of arsenic from iron ores and calcined pyrites in a process in which the ores are mixed with calcium oxide or calcium carbonate in an amount of 0.5% to 5% as Ca relative to the weight of the ore and are heated in an oxidizing atmosphere to 800° C. to 1000° C. so that the arsenic is concentrated in a fine-grained fraction. This fraction is separated from the coarser fraction and is leached with acids to remove arsenic. In this patent, in the description of the state of the art in the roasting of pyrites, an addition is described of oxides, hydroxides and various salts of alkali metals and alkaline earth metals. From these additives, corresponding water-soluble arsenates may be formed from the arsenic contained in the ore. The effect of these additives in the roasting stage is constrained by the formation of the corresponding sulfates. The sulfates are almost entirely inactive in a reaction for partitioning arsenic. When the above substances are added to calcined pyrites in an oxidizing atmosphere at 500° C. to 900° C., arsenates will be formed, which may be leached with salt solutions or acid solution. These arsenates should not be dumped in open air dumps. Moreover, the leaching results in an arsenic-containing solution, which is nearly impossible to dispose environmentally in an acceptable manner.

For sulfide ores, any arsenic which is present is an undesired accompanying element and must be removed from the calcine and from the roaster gas. This is typically accomplished by a so-called dearsenication roasting. The arsenic content of the material is volatilized in a roasting zone having a low oxygen content and enters the gaseous effluent as arsenic vapor or arsenic oxide vapor and arsenic sulfide vapor. The above mentioned U.S. patent art deals with such roasting. In the gaseous effluent, arsenic and arsenic sulfides are oxidized to form arsenic oxide vapors under a relatively high oxygen partial pressure.

However, a number of problems are encountered. The dustlike solids contained in the roaster gas are removed at a temperature exceeding the sublimation temperature of the arsenic oxides, which are subsequently separated at lower gas temperatures, or the solids and the arsenic oxides are jointly removed at lower gas temperatures. In the first case, contaminated arsenic oxides will be formed. In the second case, the arsenic which has been removed will be recycled in the process scheme. Recycling is together with the other solids which have been separated, particularly if the solids contain valuable metals and for that reason alone must be recirculated, or the removed solids may be dumped only after taking special precautionary measures because of the arsenic content. In the second case there is also a risk that part of the arsenic oxide may undesirably and unpredictably react with metal oxides to form metal arsenates, e.g., with Fe 2 O 3 to form FeAsO 4 . The metal arsenates deposit on the ore particle surfaces and clog the pores of the particle.

Particularly in the roasting of gold ores, the formation of FeAsO 4 on the particle surfaces will involve a higher cyanide consumption in the leaching and a lower yield of gold.

German Patent Specification 1,132,942 disclosed a process of roasting iron-containing sulfide ores, particularly pyrites in which the ores are roasted in a single stage fluidized bed roaster with oxygen-containing gases at 800° C. to 900° C. under an oxygen partial pressure not in excess of 2.9×10 −8 atm so that the iron content is reacted to form Fe 3 O 4 , some sulfur is sublimated and arsenic, arsenic sulfides and arsenic oxides are vaporized. Solids entrained by the roaster exhaust gas are subsequently removed at temperatures exceeding the condensation temperatures of sulfur and arsenic and the roaster gas is after-burned with a supply of air or oxygen so that the oxygen partial pressure is sufficiently increased to ensure a complete combustion of the sulfur in the purified roaster gas. The arsenic oxides produced by the after burning and removed from the gas stream, will be contaminated by residual dust.

German Patent Specification 1,458,744 discloses the roasting of iron sulfides by a process in which the ores are roasted in a single stage fluidized bed roaster with oxygen-containing gases at 700° C. to 1100° C. and under an oxygen partial pressure of about 10 −2 to 10 −15 atm, whereby Fe 2 O 3 is partly formed, the arsenic which is present is substantially volatilized as As 2 O 3 and the sulfur is volatilized as elementary sulfur. After the solids have been removed from the roaster gas, the oxygen partial pressure in the roaster gas is increased by a supply of air and the elementary sulfur and the arsenic compounds are oxidized. In that process too the volatile arsenic oxides are contaminated by residual dust as they are removed from the gas stream.

From German Patent Specification 30 33 635 it is known that arsenic-containing material, particularly non-ferrous metal ores, may be treated and the arsenic may be volatilized in a first stage at temperatures of 627° C. to 927° C. and under oxygen partial pressures of about 10 −16 bars. The solids are roasted under oxidizing conditions in a second stage. The gas from the second stage is fed in part to a gas purifier and in part to the first stage. Sulfur and oxygen are added to the exhaust gas from the second stage and the arsenic contained therein is completely reacted to form arsenic sulfides, which are partly present as fine dust and partly as vapor. In a scrubber the vaporous arsenic sulfides are condensed and removed together with the solid arsenic sulfides. The arsenic sulfides which have been removed from the scrubbing water are dumped. The presence of SO 2 involves a risk of a formation of arsenic oxides, which must not be dumped because of their solubility. Besides, a high consumption of elementary sulfur is involved.

U.S. Pat. No. 3,479,177 to Veronica et al. relates to a process for removing arsenic from arsenic-containing iron minerals. The process involves adding lime or limestone to the iron minerals which are subjected to heating in the presence of air, but not in the presence of excess oxygen, and in the presence of an additive (CaO or CaCO 3 ).

None of these patents teaches or suggests roasting ores or refractory ores, ore concentrates or ore tailings of the type described herein for recovery of metals such as precious metals in an oxygen-enriched gaseous environment under conditions as described herein in order to minimize and/or eliminate arsenic volatilization, facilitate arsenic conversion to an insoluble, environmentally acceptable form immobilized in a waste product while reducing the effects of carbon- and sulfur-containing components on metal recovery such as precious metal recovery.

Moreover, none of the references deals with the conversion of arsenic to arsenates of environmentally very stable compounds during roasting e.g. a single stage circulating fluid bed roasting of ores. In fact, the opposite is true. The present invention achieves excellent results in a simpler more efficient manner with outstanding metal, e.g. gold recovery with facile arsenic elimination as an environmental problem, while minimizing leaching cyanide consumption and conserving heat given-off in the roasting process.

Furthermore, none of the references teaches or suggests roasting refractory ores in the presence of the added fuels (sulfur, pyrite or mixtures thereof) in an oxidizing atmosphere in a fluidized bed, in particular, either pre-mixing the sulfur, pyrite or mixtures thereof with the ore or directly feeding these fuels prior to or during the roasting. Moreover, none of the references disclose the use of the sulfur, pyrite or mixtures thereof as added fuel for a roasting process in conjunction with at least one additional fuel selected from the group consisting of hydrocarbons containing 1 to 16 carbon atoms, alcohols containing 1 to 6 carbon atoms, and 1 to 2 COH groups, organic ethers containing 2 to 8 carbon atoms and one oxygen atom, CS 2 , and H 2 S. Still further, these references fail to disclose the use of these fuels to lower the ignition temperature of the roasting. In addition, these references fail to disclose the use of these fuels to produce an exhaust gas which is free of or has only low contents of CO, H 2 , and hydrocarbons.

BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS

FIG. 1 is a flow diagram of the process of the present invention;

FIG. 2 is a side elevation in vertical section of the roasting apparatus in accordance with the present invention showing a circulating fluidized bed;

FIG. 3 is a side elevation in vertical section of the roasting apparatus in accordance with the present invention showing an ebullating fluidized bed;

FIG. 4 is a graph of the percent of gold extraction versus the reaction temperature of the oxygen-enriched gaseous atmosphere during roasting based on both leaching with a carbon-in-leach/sodium cyanide leaching and a carbon-in-leach/sodium cyanide leaching with a sodium hypochlorite pretreatment of the roasted ore;

FIG. 5 is a graph of the percent gold extraction versus the percent oxygen by volume in the feed gas to the oxygen-enriched gaseous roasting atmosphere;

FIG. 6 is a graph of the percent of gold extraction versus the reaction temperature of the air atmosphere during roasting based on leaching with a carbon-in-leach/sodium cyanide leaching of the roasted ore;

FIG. 7 is a schematic drawing of an industrial embodiment of the present invention;

FIG. 8 is a flow chart illustrating the process in accordance with the invention wherein various oxygen amounts are introduced in different sections of a circulating fluid bed;

FIG. 9 illustrates the range in which stable arsenates are formed as a function temperature and oxygen partial pressure and in which the process in accordance with the invention is carried out. Some of the arsenates formed in the range in which normal arsenates are formed are water-soluble, however, increased oxygen content in the roasting gas reduces arsenic solubility especially in presence of iron additives, e.g. pyrites, iron oxides or iron sulfates;

FIG. 10 shows the range in which arsenic is volatilized in the Fe 2 O 3 range as a function of temperature and oxygen partial pressure.

FIG. 11 is another flow scheme illustrating the process in accordance with the invention.

BRIEF DESCRIPTION OF THE INVENTION

In accordance with the present invention precious metal and metal values may be recoverable from ore, ore concentrates or tailings which have arsenic- carbon- and sulfur-containing components by

1) comminuting the material to a desired particle size;

2) roasting the comminuted material under the conditions set forth herein which oxidizes, or burns off, the carbon and sulfur values and provides a calcined product amenable to efficient gold recovery; while

3) sequestering in and/or converting arsenic to an insoluble form during roasting of the comminuted material, and

4) leaching with increased efficiency the precious metal values from the roasted materials.

Specifically, the present invention addresses the improved use of fuel selection, temperature management, ignition point and reaction control whereby lower temperatures achieves outstanding roasting results substantially without impairing the access of leachants such as cyanides or thiosulfates to the interior of the particle. Such access is not impaired because of low temperature roasting which avoids surface sintering and yet provides the benefit of arsenic immobilization, fast reaction rates, high through put and an uniform reaction in an oxidizing atmosphere without use of excessive amounts of pure oxygen. Moreover, easily available fuel supplementation such as by pyrites solves additional environmental concerns because pyrites such as iron pyrite helps in sequestering or immobilizing arsenic present in the ore and converting it to scorodite or scorodite-like materials in the presence of water vapors in the reaction zone.

Hence, it is a desideratum to roast refractory gold ores in such a manner that cyanide leaching will result in a high yield of gold, will involve a low consumption of cyanide, and will assure economic environmentally acceptable disposal of arsenic-containing solids.

In accordance with the present invention, the above objective is accomplished by a process of roasting ores containing metal values or refractory gold ores or gold ore concentrates or tailings whereby the roasting is carried out:

a) at temperatures which are between about 450° C. to about 900° C. preferably between about 450° C. to about 550° C. and below the temperature at which a molten phase of a roasted ore material is formed;

b) in an oxygen-containing atmosphere of at least 1% oxygen, on basis of volume, and referenced to a basis amount of oxygen in air;

c) in the presence of or with an addition of at least one or more substances of the group consisting of the free oxides, carbonates, sulfates, hydroxides, and chlorides of calcium, magnesium, iron and barium, or of pyrites, in an amount which is in excess or the amount which is stoichiometrically required to form a stable arsenate; and

d) in the presence of water vapor.

An SO 2 -containing exhaust gas obtained in such reaction is thereafter purified, and may be sent to an acid plant producing sulfuric acid wherein surplus oxygen employed in such acid plant to obtain sulfuric acid is recirculated to an appropriate place in the process, e.g. circulating fluid bed or calcine coolers or ore heaters to utilize more efficiently in such combination oxygen employed in this process.

According to a preferred feature the oxygen content of the gas defined in b) amounts to 20% to 50% by volume; amounts as high as 65% by volume may be employed.

Other advantages of the present process will be further explained such as improved heat recovery, fast reaction rates, lowered emission of gases such as fluorine, etc.

Still further, this invention relates to a process of removing arsenic vapor and arsenic-compound vapor from dust-containing hot gases such as during ore roasting, wherein solids are separated from the gas at a temperature above the condensation temperature of the arsenic and arsenic compounds. These arsenic components are subsequently oxidized with a supply of oxygen-containing gases and immobilized for disposal in an environmentally acceptable manner meeting with ample margins of safety the acceptable environmental disposal requirements.

An another aspect of this invention and as a result of the novel manner of looking to solve the arsenic problem plaguing the industry, this invention is to provide an economic process by which the metallic arsenic and the arsenic compounds found with mineral values upon roasting and contained in the gases are converted to a form that these values may be dumped in an environmentally acceptable manner.

The above is accomplished, in accordance with the invention thusly:

i) solids are removed from the gas;

ii) one or more substances are added to the gas, these substances comprise the group consisting of the oxides, hydroxides, carbonates, and sulfates or iron, calcium, magnesium and barium or pyrites; moreover, these substances have a particle size below 3 mm;

iii) the gas and the added substances are treated in the presence of water vapor and at temperatures of about 300° C. to about 800° C. under oxidizing conditions in such a manner that the exhaust gas contains at least 1% oxygen and the arsenic content is reacted to form stable arsenates; and

iv) these stable arsenates are removed from the gas stream and carried away.

The arsenic compound vapors contained in the gas to be treated may consist of arsenic oxides and arsenic sulfides. The percentages are in percent in volume with reference to gases.

Depending on the source of the gas, it may be free of SO 2 or may contain SO 2 . As discussed above, SO 2 -containing gases are produced, e.g., by the roasting of sulfur-containing materials, such as sulfitic non-ferrous metal ores. SO 2 -free gases are produced, e.g., by the thermal processing of arsenic-containing intermediate products and waste materials, such as sludges, dusts and solutions as it is known in the metallurgical industry. The solids are suitably removed from the gas in cyclones and/or ceramic filters, such as candle filters and/or hot electrostatic precipitators.

The above recited additives in ii) may consist of waste products, such as red mud formed by processes employed in the alumina production industry, filter salts and waste gypsum. Particularly suitable additives are sulfates, e.g. iron sulfates. The particle size of the additives should be as small as possible because small particles will reduce the reaction time and the amount of reactant which is required. The term “stable arsenates” designates those arsenates which have only a low solubility in rainwater. The additives are added in amounts which are sufficient for the formation of the arsenates. Mixtures of additives are used. Water required for the water vapor content in the gas phase may be introduced into the gas to be treated by a corresponding supply of steam, as moisture or even as water of crystallization in the ore or additives. The arsenates are preferably formed at a temperature of 500° C. to 600° C. The maximum oxygen content of the exhaust gas is not critical and may be, e.g., 50% of volume. If the exhaust gas contains SO 2 , it may be processed in a suitable plant for the production of sulfuric acid. The treatment may be effected in a circulating fluidized bed, an ebullating fluidized bed, a classical fluidized bed, a rotary kiln or a multiple-hearth furnace; a circulating fluidized bed is preferred.

The solubility of the stable arsenates is so low that these may be dumped without special precautionary measures.

According to a preferred feature at least 80% of the additives employed have a particle size of about 10 to about 200 μm. With that particle size a substantially complete and fast formation of arsenates will be effected.

According to a preferred feature the water vapor content of the exhaust gas is adjusted to 0.5% to 10%. This content will result in a formation of stable arsenates having a particularly low solubility, e.g. such as scorodites or scorodite like compounds.

According to a preferred feature, gases in which the dust has no content or only a low content of metal are treated to remove only that amount of solids which exceeds the amount of solids required to form arsenates. A typical example for such aspect of the invention is in the roasting of pyrites or calcined pyrites or in the processing of gases in which the dust content consists of iron compounds. It is possible to utilize at least a part of the additives for the reaction with a containing arsenic values and thus these additives need not be separately obtained and added.

According to another preferred feature, the solids suspended in the gas are substantially removed therefrom if the dust in the gas has a valuable metal, e.g. gold. In that case the valuable metal will substantially be introduced into the calcine and can be recovered therefrom. It will then be necessary to add the required additives in the necessary amount to immobilize the arsenic.

Refractory ores which include carbon-and sulfur-containing components, such as organic and inorganic carbonaceous materials and sulfidic minerals, respectively, pose an especially severe problem in the economical, commercial recovery of precious metals, such as gold, because the efficiency and completion of recovery is dependent on the content of those carbon- and sulfur-containing components. The recovery yield of precious metal values in refractory ores can be significantly increased by oxidizing carbon- and sulfur-containing components. The efficient oxidation of carbon is especially important because residual carbon in the roasted ore, or calcine, reduces precious metal recovery during leaching by “preg robbing” because it takes up or “robs” leachant solubilized gold.

However, refractory ores which further include arsenic-containing components pose an even more complex problem. This arsenic content, while amenable to oxidation as discussed above, poses a problem in that the arsenic component or an intermediate product of roasting may volatilize at roasting temperatures, thereby requiring supplemental precautionary processing measures or the oxidized end product in the calcine solubilizes to a presently unacceptable level during leaching and/or after the exhausted calcine, i.e. tailings have been discarded and stored in a heap.

The improved process specifically for precious metal recovery from these refractory ores or their concentrates or tailings may be practiced with improved yields. Thus, not only can improved yields be achieved in an economically efficient manner, but also the problem of arsenic volatilization can be controlled. Consequently, preferably arsenic is immobilized in the calcine upon roasting but further roaster gas treatment such as in the fluidized bed(s) be practiced to immobilize arsenic in the event a gas phase treatment of the volatilized arsenic compounds is desired. As a side benefit, fluorine (while present in very small amounts in the form of RF) is also converted to an unknown insoluble form in the calcine such that only a small percentage must further be treated thereby reducing fluorine levels. On an elemental basis, the reduced HF and arsenic immobilization levels achieved by the present process are far below the present day required limits.

Furthermore, the lower temperatures and lower oxygen concentrations make the process more economically efficient. The process for the recovery of precious metals from refractory ores or their concentrates or tailings (here referred to generically for the sake of simplicity simply as “ore” or “ore material” or “more particles”) which include arsenic-, carbon- and sulfur-containing components according to the present invention includes roasting that ore in an oxygen-enriched gaseous atmosphere such as oxygen augmented air having an initial oxygen content of less than about 65 percent by volume and recovering the thus-roasted ore, whereby the ore is amenable to recovery of the precious metal values in it. In the event a reduced content oxygen atmosphere is used for a vaporized arsenic compound treatment in a gas phase, the specific steps will be discussed proceeding from the above base case as first disclosed in the continuation-in-part application, U.S. Ser. No. 07/684,649, filed Apr. 12, 1991 and now U.S. Pat. No. 5,123,956, granted Jun. 23, 1992.

The term “free oxides” in item c) above indicates that said substances are not present as compounds with arsenic or sulfur but in a form free of these. If calcium and magnesium as carbonates are available in a free form in the ore in a sufficient amount, it will be unnecessary to add said substances.

If iron compounds are present, even in a large excess, an addition will always be required, i.e. if below a ratio of 3.5 to 4.0 moles iron to a mole of arsenic, because a major part of the iron will always be included in compounds with arsenic or sulfur. Hence, iron must be present of at least 3.5 moles of iron for each mole of arsenic. The additives may consist of waste products, such as red mud from the alumina industry, filter salts and waste gypsum. Sulfates are particularly suitable. As seen from the data herein, iron compounds are preferred. The use of an additive is preferable because the additive, in particle form will then be present close to the ore particles and will be able to combine immediately with arsenic which may have been vaporized from the ore particles at the higher temperatures discussed herein.

The term “stable arsenates” designates those arsenates which have only a low solubility in rainwater when stored in a waste dump of an exhausted calcine. Proper roasting is also related to the iron content in the ore, e.g., as pyrites in the ore, the partition of arsenic between oxidation and reaction with an iron, or other compound in the ore, or an added additive and the role of iron in added form (if addition is necessary to the ore) the conversion of arsenic to scorodite or scorodite compounds during roasting and like effects.

The process of the present invention is preferably suitable for use on candidate precious metal ores having arsenic-, sulfur- and carbon-containing components. Typically, iron is in the form of the sulfides in such ores, i.e. pyrites.

Water required for the water vapor may be fed to the reactor by a suitable addition of steam, as moisture or water in the ore, of crystallization in the additives or as a water of crystallization in a component in the ore. Depending on the SO 2 content, the exhaust gas may be processed for a production of sulfuric acid or may be scrubbed to remove the SO 2 or the SO 2 content may be liquified.

Preferably, the ore is roasted in the form of fluidized solids, and more preferably, the ore circulates as fluidized solids in a circulating fluidized bed or in an ebullating fluidized bed (which has a circulation feature to it). The precious metal content can be recovered from the thus-roasted ore or ore concentrate or tailings by separation of cyanide consuming components by solubilization of these and then leaching through cyanidation, carbon-in-leach cyanidation or carbon-in-pulp cyanidation or thiosulfate leaching.

The advantage afforded by the process in accordance with this invention resides in that the calcine which is produced has a very good leachability, with e.g. cyanide, resulting in a high yield of gold and in a low consumption of cyanide. Moreover, the arsenic is bound in the form of stable arsenates, which do not disturb the leaching and which have an extremely low solubility in rainwater such that these calcines may be dumped without a need for special precautionary measures or further treatment(s).

The ores or concentrates may contain up to about 1% arsenic and even up to 2% and more. In addition to the roasting being effected in a circulating fluidized bed, a stationary fluidized bed having a defined upper surface may also be used. Further, an ebullating fluid bed, a rotary kiln or a multiple-hearth furnace, may be employed, provided the proper reactions may be obtained. The temperature at which an undesirable molten phase is formed depends on the composition of the ore in molten phase in or on the ore particle even a partial molten phase, e.g. partial sintering is undesirable as metal recovery by leaching is undesirably affected. The percentages for the gases are stated in percent by volume.

In the event of a low arsenic content in an ore, the gas which is fed is adjusted to have a higher oxygen content. The reaction temperature is achieved by a feeding of hot gases and/or by an addition of fuel. If fuel is added, oxygen in the amount required for the combustion of fuel must be added. If a reaction temperature is low, the required heat is introduced by feeding of suitable hot gases and/or by a sufficient preheating of the charged materials.

Roasting, with two stage oxygen injection may be carried out particularly conveniently. The roasting in the lower portion of the circulating fluid bed reactor is carried out as the first stage. A fluidizing gas contains an oxygen-containing atmosphere having an oxygen content below about 1%. The second oxygen injection during this roasting stage is carried out in the upper portion of the reactor with a supply of secondary gas and optionally even with a supply of tertiary gas having yet more oxygen injected in that phase at a corresponding higher oxygen content.

The candidate ores may have the following levels of arsenic, carbon and sulfur components on a percent by weight basis:

Arsenic up to 1.0% or higher
Carbon  2.5% Maximum
Sulfur  5.0% Maximum

(All percentages are on a weight-to-weight basis unless otherwise stated.)

The ore is primarily pyritic-carbonaceous-siliceous. Candidate ores may be found in the region around Carlin, Nev. Other types of ores which may be used have been identified as siliceous-argillaceous-carbonate-pyritic, pyritic-siliceous, and carbonaceous-siliceous. Small amounts of dolomite, calcite and other carbonate materials may be present in the ore.

A typical mineralogical analysis of these ores shows:

	Quartz	60-85	Percent
	Pyrite	1-10	Percent
	Carbonate	0-30	Percent
	Kaolinite	0-10	Percent
	Fe x O y	0-5	Percent
	Illite	0-5	Percent
	Alunite	0-4	Percent
	Barite	0-4	Percent

A typical chemical analysis of the ore shows an average composition as follows:

	Arsenic	0.2	Percent
	Sulfur (Total)	4.0	Percent
	Carbon (Total)	1.0	Percent
	Iron	3.5	Percent
	Zinc	0.08	Percent
	Strontium	0.03	Percent
	Gold	0.15	Ounces per ton

This ore, if so treated, typically shows gold recovery of less than 10 percent by simple cyanidation and less than 20 percent by simple carbon-in-leach cyanidation.

On the other hand, gold recovery by using the process of the present invention yields from about 75 percent to about 90 percent (and even higher) gold recovery.

While the primary application of the present invention relates to ores (as opposed to ore concentrates or tailings), it appears that ore concentrates may be used or that ore tailings may be used from the recovery of precious metal, or other values. The term “ore” as it is used throughout the remainder of this description encompasses and contemplates not only ores but also ore concentrates and ore tailings.

According to another feature of this invention, the roasting treatment according to items a) to d) described above is preceded by a first roasting stage, in which the roasting is effected at temperatures which are between 450° and 900° C., preferably below 575° C., and below the temperature at which a molten phase is formed of an ore material and in an oxygen-containing atmosphere having an oxygen content below 1%. Such roasting assures vaporization and an immediate reaction of the arsenic with the additive. At the second oxygen injection point, a roasting with two stage oxygen injection may be necessary if the ores contain more than about 1% arsenic but may also be adopted if the ores have a lower arsenic content and are particularly refractory. The additives according to c) and the water vapor according to d) need not be present in the first roasting stage but are preferably added already in the first roasting stage.

According to a preferred feature the water vapor content of the gas defined in d) ranges from about 0.5% to 10% by weight. Arsenates having a particularly low solubility such as scorodites will be formed if the water vapor content is in that range.

The advantages set forth herein-before will be achieved even with ores which contain about 1% to 2% arsenic if the roasting is effected by two stage oxygen injection. Roasting in two stages will produce particularly good results with ores which contain less than about 1% arsenic although equivalent results will also be obtained by proper use of arsenic immobilizing additives and oxygen content in the roasting gas.

According to a desired feature, provided that no molten phase forms on or within the ore particle, the roasting is effected at temperatures of 450° C. to 550° C. even up to 750° C. Thus, the formation of a molten phase may reliably be avoided, and the heat consumption may be low. The arsenic will effectively be bound and immobilized and the calcine will have a good leachability.

According to a preferred feature the substances defined in c) are present in at least about 1.5 to about 3 to 4 times the stoichiometric quantity depending on the particular compound and ore used. This will result in an effective binding of the arsenic in conjunction with a relatively small amount of solids. The amount of the substance added is, of course, determined by the solubility of arsenic in the exhausted calcine.

According to a desirable feature, the substances defined in c) are added in a particle size below 1 mm. That particle size will result in an effective contact and binding of arsenic present in the ore material.

According to a preferred feature 80% of the substances defined in c) are added in a particle size of 10 to 50 μm. Arsenic will be bound very effectively using that particle size.

The ore is comminuted, or ground, before roasting to a range of particle sizes, i.e., from about 50% to about 90% passing through about 200 mesh (−200M) sieve (U.S. or Tyler size), and of a set moisture content, i.e., from about 0% to about 5% (and preferably less than about 1% if clays having water of crystallization are present).

Next, the ground ore is roasted in an oxygen-enriched gaseous atmosphere wherein the carbon and sulfur content is substantially completely oxidized from an initial roaster feed to a final calcine content as follows:

			FINAL CALCINE
	ROASTER FEED		CONTENT
	From		From	To
COMPONENT	About	To About	About	About
Arsenic	0.1%	1.0%	0.1%	1.0%
Carbon	0.5%	2.5%	0.02%	0.1%
(total)
Sulfur	0.5%	5.0%	0.05%	0.1%
(total)

Ninety-eight percent or greater of the sulfur content and 90 percent or greater of the carbon content are respectively oxidized during roasting. For extraction of gold from these refractory ores, an important consideration is the completeness of the oxidation of the carbon and sulfur values. Final carbon values at 0.05% to 0.1% provide good results. The same applies to sulfide sulfur levels, with final sulfide sulfur values at 0.05% to 0.1% providing good results. However, the final carbon level is important since it can negatively affect gold recovery by “preg robbing” during the leaching operation.

While there is no seemingly apparent reduction in arsenic content, this is highly desirable since it is indicative of the lack of volatilization and/or immobilization of the arsenic content and ability of iron and other additives to sequester and/or react with the arsenic in the ore and keep it in a form without causing any interference with gold recovery and subsequent long term arsenic solubilization. In other words, the arsenic content is beneficially retained in the solid phase ore/calcine rather than being volatilized (with a consequent need for supplemental precautionary measures.)

Typically, greater than about 95% of the arsenic is fixed in the calcine by the presence of a e.g. proper amount of iron. If desired, additional iron may be added to facilitate this conversion to an insoluble form. By having greater than a ratio from about 3.5:1 and e.g. 4:1 of iron to arsenic (molar ratio), ferric arsenate compounds formed during roasting render the arsenic in a fixed form in the calcine. Further, the ferricarsenate compound is insoluble in the subsequent leaching and from the tailings in dump storage after the gold values are extracted. Consequently, not only are the arsenic values not volatilized by the process of the present invention by retaining them in the calcine in a nonvolatile form, but also these arsenic values can be retained in a form which is insoluble to the leaching and insoluble over long period while in a dump. A triple benefit results—reduced arsenic volatilization, long-term arsenic immobilization, and no impairment of gold recovery.

For the present invention the reaction temperature of the oxygen-enriched gaseous atmosphere during roasting is controlled preferably such that it is from about 450° C. or 475° C. to about 600° C.

In another aspect of the invention and especially when volatilized arsenic compounds are formed at higher temperatures and thereafter converted to resoluble compounds, higher temperatures are used. However, for the arsenic sequestration without arsenic volatilization and/or solubilization, sintering is to be avoided, i.e. molten phase formation should also be prevented since molten phase silicates formed (or even partial sintering), make the precious metal content of the ore less amenable to recovery. Further, the reaction temperatures in the reactor apparatus must be sufficiently high to optimize the oxidation reaction, particularly the oxidation of carbon- and sulfur-containing components and formation of e.g. ferricarsenate compounds. It has been found that a reaction temperature in the reaction apparatus for the oxygen-enriched gaseous atmosphere of from about 450° C. or 475° C. to about 600° C. is desirable, while a preferred temperature range is from about 475° C. to about 575° C.

While the objective of the oxidation of the carbon and sulfur content is the formation of oxides wherein carbon and sulfur are as completely oxidized as possible, the situation with respect to arsenic has more subtle ramifications since certain of its intermediate oxides, such as arsenic trioxide (As 2 O 3 ) (boiling point 465° C.), volatilize at elevated temperatures as do certain of its sulfides, such as As 2 S 2 (boiling point 565° C.), and As 2 S 5 (sublimates at 500° C.). The focus, therefore, is on the formation of insoluble compounds with the substances recited above, such as ferricarsenate compounds, e.g. scorodite, to avoid the volatization problem and to keep arsenic values out of the process off-gas and keep these in a highly insoluble state. This control is one of the desirable results that the present invention achieves by a combination of steps including the reaction conditions, oxygen content, roasting residence time, iron content, step wise oxygen injection, low ignition temperature achieved via the supplemental fuel disclosed herein etc. However, the present invention also addresses, as will be further discussed herein and shown by examples, the volatilized arsenic treatment in the off-gas by the proper formation of insoluble arsenic compounds.

The gaseous atmosphere in which the gold ore is roasted is an oxygen-enriched gaseous atmosphere, such as oxygen-enriched air, having a total initial oxygen content, after enrichment, of less than about 65 percent (by volume), and desirably from about 25 percent (by volume) to about 60 percent (by volume); industrially a range of oxygen of 35% to 55% by volume is indicated for the process.

The ground ore is roasted as fluidized solids in the oxygen-enriched gaseous environment. In effect, the fluidized ore in the gaseous roasting atmosphere forms a two phase suspension in which ore is a discontinuous phase composed of discrete solid particles and the gaseous atmosphere is the continuous phase. In most instances, the ore concentrates will have sufficient oxidizable content that there will be an autothermal oxidation reaction during roasting. In those instances where there is not sufficient oxidizable content, such as for an ore which does not support an autothermal reaction, additional oxidizable content is provided by adding a comburant so that there will be a thermal reaction during roasting. Typically a low ignition point fuel is added, e.g. coal or butane/propane. Hence, desirably the ignition point should be that of propane or below. Therefore, sulfur, pyrites and a mixture of these will be desirably used to lower the ignition point.

Typical pyrites include, for example, iron pyrite (fool's gold), arsenical pyrite (mispickel), arseno (arsenopyrite), cobalt pyrite (smaltite), copper pyrite (CuFeS 2 ), nickel pyrite (millerite), tin pyrite (stannite), white iron pyrite (marcasite).

Fluidizing the ore facilitates the transfer of reactants and heat produced by the oxidation reaction, i.e., from the ore to the gaseous atmosphere and vice versa. It also increases both reaction velocity and reaction uniformity. Further, as a result of these factors and the law of mass reaction, reaction of e.g. the iron and arsenic values to ferricarsenate compounds and, therefore, arsenic volatilization can be controlled. The reaction pathway for iron and arsenic values appears to be the oxidation of iron and arsenic values to form ferricarsenates. Because of the great complexity of reactions in any ore during roasting such pathway as arsenic to ferricarsenate is merely surmised but the important point is the scorodite formation. For the other substances disclosed herein, similar end results are obtained. However, the ferricarsenates are the desirable end products such as in the scorodite form.

While the oxidation reaction of the carbon- and sulfur-containing components is generally exothermic, it may be necessary to raise initially the temperature of the ore and the temperature of the gaseous reaction atmosphere in order to initiate the oxidation. This may be accomplished by initially adding a comburant, such as a carbonaceous comburant like coal, or butane typically coal; or other low combustion, i.e. flash point fuel. Moreover, if the stoichiometry of the ore is such that supplemental heat input is needed, the below-described fluid beds lend themselves well to such supplementation without any disadvantages.

As another embodiment, an ebullating bed may be used with the overflow from the ebullating bed being constantly circulated. The reaction velocity may be lower in an ebullating fluid bed. Efficiency and control over the oxidation and reaction conditions are improved by circulating the ore as fluidized solids. An advantage of a circulating fluid bed or an ebullating fluid bed is the precise control of the bed temperature; and although an employed temperature is ore specific within the above ranges, the control is maintained within ±15° C. in a broader aspect; with ±10° C. being more typical and ±5° C. being preferred. Such temperature range permits even greater control over oxidation of the arsenic-, carbon- and sulfur-containing components and over reaction of the iron- and arsenic-containing components with each other while minimizing arsenic volatilization.

According to a preferred feature the roasting is performed in a circulating fluidized bed. The fluidized bed system consists of a fluidized bed reactor, a recycling cyclone and a recycling line. That fluidized bed differs from a classical fluidized bed, in which a dense phase is separated by a distinct density step from the overlying gas space and exhibits states of distribution having no defined boundary layer. There is no density step between the dense phase and an overlying dust space but the solids concentration in the reactor decreases continuously from bottom to top. A gas-solid suspension is discharged from the top of the reactor. In a definition of the operating conditions by the Froude and Archimedes numbers the following ranges are obtained: $$ 0.1 ≤ 3 / 4 × Fr 2 × ∫ g ∫ k - ∫ g ≤ 10

and

0.01≦Ar≦100

wherein $$ Ar = d k 3 × g ⁡ ( ∫ k ⁢ - ∫ g ) ∫ g ⁢ × V 2 $$ Fr2 = u 2 g × d k

and

u the relative gas velocity in m/sec

Ar the Archimedes number

Fr the Froude number

∫ g the density of the gas in kg/m 3

∫ k the density of the solid particle in kg/m 3

d k the diameter of the spherical particle in m

V the kinematic viscosity in m 2 /sec

g the constant of gravitation in m/sec 2

The suspension discharged from the fluidized bed reactor is fed to the recycling cyclone(s) of the circulating fluidized bed and substantially all solids are removed from the suspension in said cyclone(s). The solids which have been removed are returned to the fluidized bed reactor in such a manner that the solids circulated in the circulating fluidized bed systems amount to at least four times the weight of solids contained in the fluidized bed reactor.

Circulating fluidized bed technology is further discussed in e.g. G. Folland et al., “Lurgi's Circulating Fluid Bed Applied to Gold Roasting”, E & MJ, 28-30 (October 1989) and Paul Broedermann, “Calcining of Fine-Grained Materials in the Circulating Fluid Bed”, Lurgi Express Information Bulletin—C 1384/3.81, the disclosures of which are incorporated herein by reference.

The residence time of the ore in the oxygen-enriched gaseous atmosphere should be from about 8 to 10 minutes preferably from about 10 minutes to about 12 or more, but constrained by practical design considerations such as vessel size; pump size etc. It should be understood that residence time is a function of ore mineralogy. Control of residence time at temperature also controls silicate melting which is to be avoided since the porosity created by sulfitic sulfur oxidation is then vitiated. High porosity and low sintering is desirable for the subsequent leaching of gold.

Following roasting, the precious metal values are recovered from the thus-roasted ore, or calcine, by leaching, such as by cyanidation, carbon-in-leach cyanidation or carbon-in-pulp cyanidation. Such leaching techniques are known in the art and are described in general in U.S. Pat. Nos. 4,902,345 and 4,923,510, whose disclosures are incorporated herein by reference.

As a bench mark comparison of the roasting efficiency and completion of the present invention, conventional fluid bed roasting for equivalent length of time at the same conditions provides a measure by which the present invention may be evaluated. Another measure of efficiency and completion are the amount of cyanide used to extract an equivalent amount of gold, or residual amounts of gold in ore after standard extraction procedures. According to the above measures, evaluation of ore of the same mineralogy will give the outstanding advantages of the present invention.

The thus-roasted gold ore may be subjected to an oxygen or chlorine treatment after roasting and prior to leaching. This treatment may be in the form of bubbling gaseous oxygen or chlorine through a suspension or a slurry of the thus-roasted ore either in a bath at ambient pressure or in a closed vessel at ambient or elevated pressure prior to leaching the ore.

The precious metal recovery provided by the present invention from refractory ores which include arsenic-, carbon- and sulfur-containing components is much improved, reaching levels of 75-90% and in some cases higher, such as 92%. It must be understood that the mineralogy of the ore will influence the results. Conventionally pyritic sulfides, sulfides and carbon affect recovery and higher or lower arsenic content makes it more or less expensive to treat the ore to meet today's environmental demands.

Another aspect of the invention relates to a process of roasting refractory gold ores in the presence of added fuels (sulfur, pyrite or mixtures thereof) in an oxidizing atmosphere in a fluidized bed. The sulfur, pyrite or mixtures thereof can be added either prior to or during the roasting. Preferably, the fuels are either pre-mixed with the ores or may be directly fed to the fluidized bed. One aspect of the invention is to use a fuel which can be ignited at low temperatures and which can be combusted to produce an exhaust gas which is free of or has only low contents of CO, H 2 and hydrocarbons.

Refractory gold ores are ores which cannot directly be leached with NaCN and which as a gold-bearing material contains arsenopyrites or pyrites which contain more or less organic carbon. These have an extremely low gold content. Before such ores can be leached with cynides, their sulfur and carbon contents must be oxidized as completely as possible. That oxidation is effected by a roasting with oxygen-containing gases. In many refractory gold ores the content of arsenopyrite, pyrite and organic carbon is not sufficient for the generation of the required reaction heat so that fuel must be added. Numerous refractory gold ores must be roasted at a relatively low temperature if a high yield of gold is to be achieved in the subsequent leaching.

European Patent specification 0 508 542 teaches to roast gold ores at a temperature from 475 to 600° C. and particularly from 500 to 575° C. Coal, butane or propane have been mentioned as added fuels. The ignition temperature should be equal to or exceed that of propane. But the proportion of propane and butane which is combusted to CO 2 and H 2 O is unsatisfactorily low. The combustion results in a production of CO and H 2 at considerable rates. CO and H 2 have ignition temperatures from 600 to 650° C. and from 560 to 580° C., respectively.

Gold ores can be roasted best under mild conditions in order to avoid hot spots on the surface of the particle. The yield of gold will highly depend, inter alia, on the roasting temperature. The roasting temperature must be kept below the sintering temperature of the components of the ore which is being roasted.

Most gold ores contain small amounts of pyrite and/or inorganic carbon. Owing to the dissipation of heat during heating up, from the exhaust gas, during the discharge from the roaster and other operations, the heating value of gold ores is not sufficient for a self-sustaining roasting (antogenous roasting) even at temperatures of about 500° C. For this reason a fuel which has low ignition and combustion temperatures must be added to avoid a decrease of the gold yield.

It is an object of the invention to use a fuel which will reliably be ignited at low temperatures and which can be combusted to produce an exhaust gas which is free of or has only low contents of CO, H 2 , and hydrocarbons.

In the process mentioned first hereinbefore that aspect is accomplished in accordance with the invention in that sulfur and/or pyrite is fed as a fuel to the fluidized bed and roasting is carried out at temperatures from about 400 to about 650° C. in conjunction with a supply of oxygen-containing gases. The advantage afforded by the process in accordance with the invention resides in that the combustion of sulfur and/or pyrite does not result in a production of CO, H 2 , and hydrocarbons.

It is surprising that sulfur and pyrite can reliably be ignited at low roasting temperatures. Sulfur will burn at temperatures in the range from 200 to 300° C. and pyrite at temperatures in the range from 450 to 600° C. The sulfur and/or pyrite to be added may be pre-mixed with the gold ore or may directly be fed to the fluidized bed.

In accordance with the invention, refractory gold ores are roasted in an orthodox (noncirculating) or in a circulating fluidized bed. The oxygen-containing gases are supplied as fluidizing gas to the fluidized bed reactor below the nozzle bottom (FIGS. 2 and 7 ). In accordance with the invention, additional oxygen-containing gases may be supplied as primary and secondary gases to the fluidized bed reactor from the sides. The oxygen-containing gases consist of air or oxygen-enriched air.

Still another preferred feature resides in that the roasting is carried out at temperatures from 500 to 550° C. Particularly good gold yields will be achieved at said temperatures.

An additional preferred feature of the invention resides in that sulfur and/or pyrite and at least one additional fuel selected from hydrocarbons containing 1 to 16 carbon atoms, alcohols containing 1 to 6 carbon atoms and 1 to 2 COH groups, organic ethers containing 2 to 8 carbon atoms and 1 oxygen atom, CS 2 , and H 2 S are fed as fuels to the fluidized bed. Because sulfur and/or pyrite are combusted in conjunction with one or more of said additional fuels, the ignition temperature of said additional fuels will be decreased if their ignition temperature exceeds the ignition temperature of sulfur or pyrite. As a result, said additional fuels will be ignited sooner in such a mixture. If the ignition temperature of one of said additional fuels is below the ignition temperature of sulfur or pyrite, sulfur or pyrite will have a lower ignition temperature in a mixture which contains such an additional fuel.

The concentration of the additional fuels in a mixture with sulfur and/or pyrite must exceed the ignition limit. The ignition limit of a fuel is the minimum concentration of a fuel in a gas mixture in which that fuel can be ignited. The concentration of additional fuels should be varied to determine the optimal amount to achieve ignition at low temperatures. The additional fuels will be supplied at a concentration in excess of their ignition limit if the heat content in the reactor is not sufficient for a heating to the required roasting temperature. The heat content in the reactor is determined by the amounts of carbon and sulfur contained in the refractory gold ores and by the rate at which sulfur and/or pyrite is added as a fuel. This means that the roasting temperature can be controlled by a control of the rate at which the additional fuels are added. The additional fuels will be added at such rates that the roasting temperature does not exceed about 950° C., preferably does not exceed about 750° C., more desirably does not exceed about 650° C., even more desirably does not exceed about 550° C. and most desirably does not exceed about 450° C. and that the exhaust gas from the fluidized bed has an H 2 content of less than about 50 vppm (volume parts per million), preferably less than about 25 vppm, more desirably less than about 10 vppm, even more desirably less than about 5 vppm, and most desirably less than about 1 vppm, a CO content of less than about 0.5% by volume, preferably less than about 0.1% by volume, more desirably less than about 100 vppm, even more desirably less than about 50 vppm and most desirably less than about 10 vppm, and a hydrocarbon content less than about 200 vppm, preferably less than about 100 vppm, more desirably less than about 50 vppm, even more desirably less than about 25 vppm, and most desirably less than about 10 vppm.

The additional fuels which may be employed include mixed hydrocarbons which are recovered as fractions by distillation, such as kerosine, or become available as refinery waste products. In addition to hydrocarbons, the additional fuels may include mixed alcohols, which become available as waste products in the distillation of ethanol.

The particle size of the gold ores should be below about 5 mm, preferably, below 2 mm, more desirably below 1 mm, and most desirably below 0.5 mm. A preferred feature of the invention resides in that the particle size of the gold ores is below 1 mm. Good results will be produced with that particle size.

Still another preferred feature of the invention resides in that 60 to 80% of the gold ore have particle sizes below about 100 micrometers, desirably below about 75 micrometers, more desirably below about 50 micrometers, even more desirably below about 25 micrometers, and most desirably below about 10 micrometers. Particularly good results will be produced with that particle size. The term “particle size” stands for the median particle diameter d 50 . The diameter can be ascertained by methods such as ASTM methods or DIN methods.

A preferred feature of the invention resides in that the O 2 content of the gas which is fed to the fluidized bed amounts to 20 to 50% by volume. The use of oxygen-enriched air will result in an improved ignition of the fuel mixture. The use of oxygen-enriched air is particularly economical.

The use of the additional fuels affords the advantage that these are substantially completely combusted at a low temperature and that the resulting exhaust gas has very low contents of CO, H 2 , and hydrocarbons so that said components need not be removed from the exhaust gas by afterburning. In a succeeding production of sulfuric acid it will be desirable that the contents of CO, H 2 , and hydrocarbons are very low because said substances tend to poison the catalyst used for the oxidation of SO 2 to SO 3 .

Still another preferred feature of the invention resides in that a partial stream is branched (a slip stream) from the hot exhaust gas which has been dedusted and said partial stream of exhaust gas is admixed to the fluidizing gas before it is fed to the fluidized bed. The recycling of part of the exhaust gas and the mixing of said part with the fluidizing gas have the result that the fluidizing gas is heated. The recycling of a part of the exhaust gas will enrich SO 2 in the exhaust gas.

Still another preferred feature of the invention resides in that the SO 2 gas which has been formed by the roasting of refractory gold ores and is carried away in the exhaust gas is used for the production of sulfuric acid. The economy of the process in accordance with the invention will be improved if the SO 2 which has been formed by the roasting and is carried away in the exhaust gas is used for a production of sulfuric acid without an afterburning. The SO 2 gas will be scrubbed before it is fed to the plant for producing sulfuric acid.

A further preferred feature of the invention resides in that the roasting is carried out in a circulating fluidized bed. The circulating fluidized bed system comprises a fluidized bed reactor, a recycling cyclone, and a recycling line. The “orthodox” fluidized bed, in which a dense phase is separated by a distinct density step from the overlying gas space, differs from the circulating fluidized bed in that the latter includes states of distribution having no defined boundary layer.

The suspension discharged from the fluidized bed reactor is fed to the recycling cyclone of the circulating fluidized bed system (FIG. 7 ). Substantially all solids are removed from the suspension in said cyclone and the separated solids are recycled to the fluidized bed reactor in such a manner that the amount of solids circulated per hour in the circulating fluidized bed system is at least four times the weight of solids contained in the fluidized bed reactor.

DESCRIPTION OF THE ILLUSTRATIONS SHOWN IN THE DRAWING

In FIG. 1 a self-explanatory flow diagram has been provided. This generic flow diagram should be considered in combination with a schematic industrial embodiment shown in FIG. 7 for gold recovery from gold ores and also amplified further herein by the data shown in Table 7.

As one of the advantageous aspects of this invention, heat recovery (i.e. as a cost advantage) in this process may be readily practiced. For example heat may be recovered not only from the off-gases from the one stage roasting such as derived from a circulating fluid bed or an ebullating fluid bed, but also by cooling a calcine with air or air enriched with oxygen e.g. of up to 65% oxygen by volume. Such air cooling is taught in U.S. Pat. No. 4,919,715 to supposedly reduce the recovery of gold, apparently by as much as 2%, but we have found it not to be detrimental, if anything, such heat recuperation seems to have improved the yields.

Another aspect of the invention which has not been mentioned or apparent from the immediately above-mentioned patent is that subsequent liquid quenching allows reduction of cyanide consuming materials. These materials are rendered soluble by the low temperature oxygen roasting and low temperature oxygen post-finishing of the calcine during cooling. Such post-finishing provides excellent sulfation at acidic conditions, e.g. making of Fe 2 (SO 4 ) 3 and like compounds of metals such as copper, nickel, antimony, zinc, lead etc. The removal of these compounds during liquid quench reduces cyanide consumption during leaching from 2 to 10 pounds more typically from 5 to 10 pounds of cyanide per ton of calcine to less than one pound e.g. typically 0.3 pound of cyanide per ton of calcine.

In FIG. 2 a schematic representation of appropriately labeled circulating fluidized bed (CFB) has been shown. The air input at the bottom of the bed with the recirculating material from the hot cyclone (or a plurality of cyclones in parallel, e.g. two) keep the bed in a high degree of turbulence assuring excellent i.e. almost instantaneous temperature uniformity and reaction conditions. Typically the complete residence time in such bed may be based on a number of passes of the bed contents through the bed, but it is best to express it as overall nominal residence time for the bed contents. It should be understood that a residence time is a summation time of the circulating particles in such bed. It is believed that the post-finishing of the calcine during cooling has the above-mentioned advantageous effect for any particle which may have escaped the necessary residence time in the circulating fluid bed, yet at no overall reduction of residence efficiency and gold recovery.

FIG. 3 shows an ebullating fluid bed which is an embodiment of a fluid bed suitable as another approach in the disclosed process. The appropriately labeled illustration provides for another circulation approach when roasting an ore material.

FIGS. 4 to 6 will be further explained in conjunction with the Examples. FIGS. 4 and 6 illustrate the “knee-in-the-curve” found for the roasting conditions existing as a function of roasting temperature, oxygen content in roasting gas i.e. air, and as a function of gold extraction.

In FIG. 7 an embodiment showing a schematic industrial application of the process is illustrated in greater detail and amplifies the flow chart of FIG. 1 . Other FIGS. i.e. 8 to 11 will be discussed in conjunction with the Examples 8 and 9 herein.

A circulating fluid bed (CFB) reactor 100 is fed from an ore preheat stage identified with stream 200 corresponding to the same stream number in Table 7 further disclosed herein. A start-up gas stream such as butane/propane has been shown entering the CFB reactor 100 at the bottom thereof. Additionally, a combined stream of oxygen unexhausted off-gas and fresh oxygen via preheater 102 is introduced into the CFB reactor 100 . The combined stream is identified as 201 . Further, a preheated, oxygen supplemented air stream 208 is introduced in the CFB reactor 100 and is coming from the post-finishing calcine treatment which will be discussed below. A single cyclone 103 has been shown in FIG. 7 , but more than one may be operated in parallel or in series to assure greater particulate removal from the off-gas. Cyclone 103 bottoms i.e. underflow collections are partially reintroduced into the CFB reactor 100 via seal pot 104 . A slip stream 105 of calcined product is also taken from seal pot 104 and introduced into a four stage pre-heaters (recuperators) 107 to 110 which are in a heat recovery unit 106 . Air augmented with oxygen is brought up to about 450° C. in heat recovery unit 106 . The unit 106 consists of four pre-heaters in the form of fluidized beds 107 , 108 , 109 and 110 , respectively. Because the conditions in each of the pre-heater beds are different, these pre-heaters 107 , 108 , 109 and 110 have been identified by separate numbers. Typically, the CFB reactor 100 is operated at 550° C. The resulting calcine (of retention time of 10 minutes in reactor 100 ) is introduced in the first pre-heater 107 . The calcine is at a temperature of about 525° C. and has a residence time of about 15 minutes in preheater 107 ; in the second pre-heater 108 , the calcine temperature is about 475° C. and residence time is about 10 minutes; in the third pre-heater 109 the calcine temperature is at about 420° C. and the residence time is about 8 minutes; in the fourth pre-heater 110 the calcine temperature is about 350° C. and the residence time is about eight minutes. Air and oxygen enter these preheaters in parallel, fluidized in each the calcine, and is mixed and cleaned in cyclone 112 . After separation of particulates in cyclone 112 , air and oxygen is introduced as stream 208 into the CFB reactor 100 . A second pre-heater unit (not shown) of the same type may be operated in parallel to the first pre-heater unit 106 . The seal pot 104 or a second seal pot (not shown) may feed the second pre-heater unit. In the data shown in Table 7, these are referred to two parallel identical pre-heater units such as 106 , two parallel cyclones such as 112 , and two parallel seal pots such as 104 .

Heated air and oxygen from all four pre-heaters is used and is at about 450° C. as shown in Table 7. However, in addition ambient air is introduced via pump 113 into heating coils 114 immersed in the fluidized calcine in pre-heaters 109 and 110 . This air is used to pre-heat in a CFB type vessel (not shown) the ore introduced as stream 200 in the CFB reactor 100 . Hot air exits heating coils 114 at 200° C. As contemplated, but subject to change in the mineralogy of the ore, the balance of the energy requirement for roasting is made up by the addition of butane or pulverized coal to the CFB reactor 100 . Calcine in stream 209 is quenched in water in tank 115 to a 15% solids content and further worked-up as previously described for removal of a cyanicide materials, neutralization and subsequent leaching.

Off-gases, i.e. cyclone 103 overflows are introduced into a waste heat boiler 116 where the off-gas temperature is reduced to about 375° C., dust from the waste heat boiler 116 is introduced into the pre-heater unit in an appropriate place, e.g. pre-heater 108 and combined with calcine. From waste heat boiler 116 , the off gases are introduced into an electrostatic precipitator 117 , e.g. a five field, hot electrostatic precipitator, to remove substantially all residual dust in the off-gas. A number of precipitators 117 may be used. The exit temperature of the off-gas from the electrostatic precipitator 117 is at about 350° C. and the off-gas comprises about 36% by volume of oxygen. About half of the exit gases are recycled via pump 118 to the CFB reactor 100 . This recycle is a significant benefit because the off-gas cleaning system becomes about half the size if the off-gas is recycled. Precipitates from the electrostatic precipitator are also introduced into the calcine pre-heat unit(s) 106 . The SO 2 laden exit gases may be sent directly to an acid plant and further amounts of oxygen introduced (as needed, for conversion of SO 2 to an acid as it is well known in the art). However, the excess oxygen rich gas from such plant may be recycled to the roasting side of the process and introduced such as in the CFB reactor 100 or used for calcine post-finishing, e.g. in fluidized beds 107 , 108 , 109 and 110 to aid in sulfating i.e. solubilizing the otherwise cyanide consumers.

In accordance with the present invention, a series of experimental runs were conducted which established the significant process parameters which show the previously unachieved results of which the present invention is capable.

The following examples illustrate the process of the present invention in the context of the recovery of gold.

EXAMPLE 1

The ore used in these runs came from a random sampling of arsenic-, sulfitic-, organic carbon-containing, gold-bearing ores from the region around Carlin, Nev. This ore, for the series of runs showed an average gold content of about 0.16 ounces of gold per ton of ore and up to 0.20 oz. of gold per ton, an average content of 0.08 percent arsenic, 2.49 percent sulfide sulfur (2.81 percent total sulfur) and 0.79 percent organic carbon (0.84 percent total carbon.) The ore was classified as pyritic-carbonaceous-siliceous ore and had the following mineralogical and chemical analyses:

Mineralogical Analysis

A typical analysis of this ore shows:

	Quartz	68	Percent
	Kaolinite	10	Percent
	Sericite or Illites	8	Percent
	Pyrite	5	Percent
	Jarosite	4	Percent
	Alunite	3	Percent
	Fe x O y	1	Percent
	Barite	1	Percent
	Carbonates	0	Percent

Chemical Analysis:

A chemical analysis of the ore shows an average composition as follows:

	Arsenic	824	parts per million
	Carbon (Total)	0.84	Percent
	Sulfur (Total)	2.81	Percent
	Gold	0.164	ounces per ton
	Iron	4.0	Percent
	Zinc	400	parts per million
	Strontium	0.02	Percent

The ore was ground in a small ball mill to 100 percent −65 mesh (except as otherwise noted), i.e., 100 percent passed through a 65 mesh sieve, and it had a bulk density of about 57 pounds per cubic foot and a moisture content of about 1 percent.

The ground ore was placed in a simple rotating tube reactor and roasted in a batch operation to evaluate various reaction conditions using a residence time of two hours for the sake of consistency.

The roasted ore, or calcine, was treated by a carbon in leach cyanidation leach using a dosage of 6 pounds of sodium cyanide per ton of roasted ore and 30 grams per liter of activated carbon (available from North American Carbon.)

The leaching was conducted in a continuously rolling bottle under the following conditions:

1. 200 grams of calcine per leach test

2. 40% solids and

3. 24 hours leaching time.

A first series of runs was made roasting the ore with 40% oxygen (by volume) initially in the feed gas, or gaseous atmosphere, at the following temperatures and with the following results:

                     Gold
Roasting Temperature Extraction
(Degree C.)          (Percent)
450                  84
475                  92
500                  86.5
525                  82
550                  80
600                  76.8

(The symbol * in the graph in FIG. 4 also shows these results.) When the roasted ore is treated with sodium hypochlorite at a rate of 25 pounds per ton of ore and using the same leaching technique, the results were as follows:

		Gold
	Roasting Temperature	Extraction	Arsenic in Tailings
	(Degree C.)	(Percent)	ppm	%
	450	86	939	0.094
	475	92.5	913	0.091
	500	87.3	934	0.093
	525	82.5	918	0.092
	550	80.3	950	0.095
	600	78	898	0.090

(The symbol □ on the graph in FIG. 4 also shows these results.)

A second run was undertaken in which the roasting temperature was held at 475 degrees Centigrade and the retention time at 2 hours, but the percent oxygen (by volume) in the feed gas, i.e., the total initial oxygen content of the gaseous atmosphere, was varied as follows and the following percentages of gold extraction were observed:

Total oxygen (by Volume)
in Feed Gas (air + added Gold Extraction
oxygen) (Percent)        (Percent)
10                       80
20                       85.5
30                       87.5
40                       92

(These results are also shown in the graph of FIG. 5. )

Further, the following additional results were observed in the roasted ore and are set forth Table 1.

TABLE 1
CALCINE ASSAYS AND LEACH RESULTS
TOTAL
INITIAL	ARSENIC	SULFUR	CARBON		LEACH	CALCULATED	GOLD	−200
OXYGEN	(PERCENT)	(SULFIDE)	(ORGANIC) 1	GOLD 2	RESIDUE 3	HEAD 4	EXTRN.	MESH 5
%	%	%	%	oz/ton	oz/ton	oz/ton	%	%
10	0.082	0.31	0.17	0.169	0.033	0.164	79.9	84.7
20	0.085	0.20	0.08	0.164	0.025	0.170	85.3	80.5
30	0.080	0.30	0.05	0.165	0.021	0.166	87.5	83.1
40 6	0.091	0.48	0.05	0.162	0.013	0.161	92.2	81.6
1 Organic carbon is defined as acid insoluble carbon to distinguish from carbonates which are acid soluble.
2 By fire assay determination.
3 By fire assay determination.
4 Calculated head is a comparison to the fire assay by using leach residue weight and loaded carbon weight and fire assay. It is used to make a material balance determination to ensure tht there has been good gold accountability in the test.
5 Through a 200 mesh sieve.
6 This was conducted on material which passed through a 20 mesh sieve standard test procedure.

EXAMPLE 2

A series of air roasting tests was run in a six-inch rotating tube furnace with off gas oxygen content. (This resulted in approximately 4% to 6% oxygen by volume in the off-gas.) These tests used specimens of the same composition as the sample used in Example 1. The ore for this series of test runs showed an average gold context of about 0.164 ounces of gold per ton, 2.49 percent sulfide sulfur and 0.79 percent organic carbon. The ore was classified as sulfitic-carbonaceous ore. Sample preparation and test procedures used were the same as in Example 1. Table 2 and FIG. 5 present the comparative results. These tests demonstrate that low gold recoveries are achieved when roasting is conducted with air as the oxidizing atmosphere. These tests also demonstrate that the process of the present invention using oxygen-enriched air (such as 40% oxygen by volume) allows better process control—at lower temperatures—for maximum gold recoveries.

TABLE 2
CALCINE ASSAY AND LEACH RESULTS -- ROASTING IN AIR
	ROAST		LEACH TEST RESULTS
	CONDITIONS		Au in
	WT.	CALCINE HEAD ASSAYS	LEACH	CALC.	AU	−200
TEST	TEMP	LOSS	S 1	C 2	As	Hg	Au	TAIL	HEAD 3	EXTRN	MESH 4
NO.	° C.	%	%	%	ppm	ppm	oz/ton	oz/ton	oz/ton	%	%
2-1	560	4.7	.07	.05	948	.26	.166	.033	.168	80.3	66.3
2-2	580	4.8	.10	.09	894	.18	.170	.029	.167	82.8	68.7
2-3	600	5.3	.05	.04	926	.19	.165	.027	.166	83.7	76.1
2-4	620	5.2	.06	.08	945	.11	.166	.032	.168	80.9	68.9
2-5	640	5.1	.09	.02	981	.09	.167	.034	.171	80.1	68.6
1 Sulfide Sulfur.
2 Organic carbon as residue after hydrochloric acid digestion.
3 Calculated head is a comparison to the fire assay by using leach residue weight and loaded carbon weight and fire assay. It is used to make a material balance determination to ensure that there has been good gold accountability in the test.
4 Percent through a 200 mesh sieve.

EXAMPLE 3

The ore used in these runs came from a random sampling of arsenic-, sulfitic-containing, gold bearing ores from the region around Carlin, Nev. The ore for this series of runs showed an average gold content of about 0.14 ounces of gold per ton of ore, an average content of 0.15 percent arsenic, 2.15 percent sulfide sulfur (2.50 percent total sulfur) and 0.35 percent organic carbon (0.39 percent total carbon.) The ore was classified as pyritic-siliceous ore and had the following mineralogical analysis:

Mineralogical Analysis:

A typical analysis of this ore shows:

	Quartz	80	Percent
	Sericite	6	Percent
	Pyrites	4	Percent
	Jarosite	4	Percent
	Kaolinite	3	Percent
	Alunite	2	Percent
	Barite	1	Percent
	Fe x O y	0	Percent

Chemical Analysis:

An elemental analysis of the ore shows an average composition as follows:

	Arsenic	0.15	Percent
	Carbon (Organic)	0.35	Percent
	Sulfur (Sulfide)	2.15	Percent
	Gold	0.14	Percent
	Iron	2.0	Percent
	Zinc	0.06	Percent
	Strontium	0.05	Percent

The ore was ground in a small ball mill to 100 percent −100 mesh, i.e., 100 percent passed through a 100 mesh sieve (except as otherwise noted) and it had a bulk density of approximately 62 pounds per cubic foot and a moisture content of approximately 1 percent.

The ground ore was placed in a simple rotating tube reactor and roasted in a batch operation to evaluate various reaction conditions using a residence time of two hours for the sake of consistency. The ore feed to roast was 800 grams at −100 mesh.

The roasted ore, or calcine, was treated by a carbon-in-leach cyanidation leach using 5 pounds of sodium cyanide per ton of roasted ore and 30 grams per liter of activated carbon (available from North American Carbon.)

The leaching was conducted in a continuously rotating bottle under the following conditions:

1. 200 grams of calcine per leach test

2. 40% solids and

3. 24 hours leaching time.

The series of runs was made roasting the ore with 40% total oxygen (by volume) initially in the feed gas, or gaseous atmosphere, at the following temperatures and with the following results:

Roasting Temperature Gold Extraction
(Degree C.)          (Percent)
450                  72.2
475                  84.9
500                  82.5
525                  76.8
550                  77.7
600                  75.5

Table 3 also shows these and additional results.

TABLE 3
CALCINE ASSAY AND LEACH RESULTS -- ROASTING IN 40% OXYGEN
	ROAST CONDITIONS		LEACH TEST
	WT.	CALCINE HEAD ASSAYS	LEACH	CALC. 4	GOLD	−200
TEST	TEMP	FEED	LOSS	S 2	C 3	As	Hg	Au	TAIL	HEAD	EXTRN	MESH 5
NO.	° C.	GAS 1	%	%	%	ppm.	ppm.	oz/ton	oz/ton	oz/ton	%	%
3-1	450	40	1.2	.88	.09	1416	.82	.145	.042	.150	72.2	68.2
3-2	475	40	2.0	.29	.29	1394	.22	.148	.023	.153	84.9	67.8
3-3	500	40	2.6	.18	.18	1528	.32	.146	.027	.154	82.5	67.5
3-4	525	40	2.8	.10	.10	1546	.14	.148	.036	.155	76.8	67.8
3-5	550	40	3.0	.04	.01	1327	.29	.147	.034	.152	77.7	72.5
3-6	600	40	3.0	.02	.01	1236	.30	.149	.038	.155	75.5	71.4
1 Total initial oxygen content, percent oxygen by volume.
2 As sulfide.
3 Organic carbon as a residue after hydrochloric acid digestion.
4 Calculated head is a comparison to the fire assay by using leach residue weight and loaded carbon weight and fire assays. It is used to make a material balance determination to ensure that there has been good gold accountability in the test.
5 Percent through a 200 mesh sieve.

EXAMPLE 4

A series of roast tests was run in a six-inch rotating tube furnace with air as the input stream. (This resulted in approximately 4% to 6% oxygen by volume in the off-gas.) Specimens from the same sample as in Example 3 were used for these tests. Sample preparation and test procedures were the same as in Example 1. Table 4 presents the test results. These tests also demonstrate that when comparing to Table 3 results, the former show that gold recovery is maximized when oxygen-enriched air, e.g., 40% total oxygen in the feed gas, is used as the oxidizing medium.

TABLE 4
CALCINE ASSAY AND LEACH RESULTS - AIR ROASTING
	LEACH TEST RESULTS
	ROAST CONDITIONS		LEACH	CALC
	WT.	CALCINE HEAD ASSAYS	TAIL	HEAD	GOLD	−200
TEST	TEMP	MESH	TIME	LOSS	S 2	C 3	As	Hg	Au	ozAu	oz/	EXTR	MESH
NO.	° C.	SIZE 1	Hrs	%	%	%	ppm	ppm	oz/ton	/ton	ton	%	%
4-1	550	−14	1.5	2.5	.31	.08	1125	.54	.146	.043	.148	70.8	81.7
4-2	550	−14	2.5	2.7	.22	.06	1040	.42	.149	.044	.149	70.2	80.8
4-3	650	−14	1.5	2.9	.17	.05	560	.26	.144	.036	.146	75.1	84.7
4-4	650	−100	1.5	2.9	.01	.02	520	.17	.150	.035	.146	75.9	67.7
4-5	650	−14	2.5	3.1	.15	.04	540	.30	.149	.038	.152	74.9	84.5
4-6	650	−100	2.5	3.7	.01	.03	520	.19	.149	.039	.152	74.2	72.4
4-7	600	−14	2	3.9	.20	.03	848	.29	.146	.036	.150	75.8	83.8
4-8	600	−28	2	2.9	.08	.08	500	.30	.141	.034	.148	77.0	89.0
1 Percent passed through a sieve of the specified mesh.
2 Sulfide sulfur.
3 Organic carbon as a residue after hydrochloric acid digestion.

EXAMPLE 5

A series of tests was conducted in a six-inch rotating tube furnace on a sample with high carbonate content to demonstrate that the high gold recoveries are achieved with the process of the present invention. For comparison, three air roasts are presented along with the example that illustrates the present invention. Sample preparation and test procedures used were the same as in Example 1. Table 5 shows the test results. The analysis of the sample was:

Chemical Analysis:

Chemical Analysis
	Gold	0.66	Ounces per ton
	Carbon (total)	3.5	Percent
	Carbon (organic)	0.0	Percent
	Sulfur (total)	2.6	Percent
	Sulfur (sulfide)	2.2	Percent
	Iron	2.8	Percent
	Arsenic	0.43	Percent
	Mercury	56	Parts per million

Mineralogical Analyses:

	X-RAY Diffraction		X-RAY Fluorescence
	Analysis		Analysis
	Quartz	29	Percent	Zirconium	.03	Percent
	Sericite	4	Percent	Titanium	.04	Percent
	Kaolinite	18	Percent	Barium	.85	Percent
	Alunite	26	Percent	Nickel	.02	Percent
	Jarosite	9	Percent	Vanadium	.02	Percent
	Pyrite	3	Percent	Strontium	.04	Percent
	Barite	1	Percent	Zinc	.03	Percent
	Fe x O y	2	Percent
	Diopside	7	Percent

TABLE 5
TEST RESULTS FOR THE HIGH CARBONATE SAMPLE
	LEACH
ROAST	RESIDUE	GOLD	−200
TEMP.	Au	EXTRACTION	MESH 1
DEG. C.	oz/ton	%	%	COMMENTS
525	.077	88	80	oxygen-
				Enriched
				Roast 2
550	.105	84	80	Air
				Roast 3
600	.132	80	89	Air Roast 3
650	.138	79	86	Air Roast 3
1 Passed through a 200 mesh sieve
2 Feed gas was air enriched to 40% total oxygen content (by volume.)
3 Feed gas was air and the off-gas composition was maintained at 6% to 8% oxygen by volume.

EXAMPLE 6

A series of pilot plant tests was conducted in a six-inch fluidized bed reactor and an eight-inch fluidized bed reactor on a sulfitic carbonaceous sample with the following chemical and mineralogical composition:

Chemical Analysis:

Chemical Analysis
	Gold	0.13	Ounces per ton
	Carbon (total)	.82	Percent
	Carbon (organic)	.78	Percent
	Sulfur (total)	3.1	Percent
	Sulfur (sulfide)	2.6	Percent
	Iron	2.7	Percent
	Arsenic	0.09	Percent
	Mercury	4.7	Parts per
			million

Mineralogical Analyses:

	X-RAY Diffraction		X-RAY Fluorescence
	Analysis		Analysis
	Quartz	71	Percent	Zirconium	.01	Percent
	Sericite	5	Percent	Titanium	.12	Percent
	Kaolinite	11	Percent	Barium	.85	Percent
	Alunite	3	Percent	Nickel	.03	Percent
	Jarosite	5	Percent	Vanadium	.05	Percent
	Pyrite	4	Percent	Strontium	.05	Percent
	Barite	1	Percent	Zinc	.10	Percent
	Fe 2 O y	0	Percent	Lead	.01	Percent

The sample preparation procedure for this series of tests included crushing, wet grinding in a ball mill to 100% passing through a 65 mesh sieve, solid/liquid separation, and drying prior to roasting. The dry sample was fed to the roaster via a screw feeder with the combustion gas consisting of either air alone or air enriched to 40% total initial oxygen content by volume. Solids exiting the roaster were carbon-in-leach cyanide leached at the same conditions as in Example 1.

Table 6 presents the test results. From the results it is seen that maximum gold recoveries are achieved by using the process of the present invention. By way of comparison, several air roasts conducted in a circulating fluidized bed roaster and a stationary fluid bed roaster are presented along with three examples that illustrate the present invention.

Residual sulfide sulfur content and organic carbon content of the solids exiting from the pilot plant roaster were less than 0.05 percent by weight in all the tests from this series.

TABLE 6
Test Results From Pilot Plant in Fluidized Bed Roasters
ROAST	OXYGEN	LEACH	CALC	GOLD
TEMP.	IN OFF-	RESIDUE	HEAD	EXTRN
DEG. C.	GAS %	oz/ton	oz/ton	%	COMMENTS
525	37	.019	.131	85	Oxygen Roast 1
550	38	.020	.137	85	Oxygen Roast 1
550	38	.016	.131	88	Oxygen Roast 2
625	6	.046	.131	65	Air Roast 3
675	6	.044	.137	68	Air Roast 3
725	6	.044	.133	67	Air Roast 4
600	6	.034	.134	75	Air Roast 5
600	6	.028	.133	79	Air Roast 5
1 Test conducted in a six-inch circulating fluidized bed roaster with a combustion gas of air enriched to 40% oxygen by volume.
2 Same as in footnote 1 but the test was conducted in an eight-inch circulating fluid bed roaster.
3 Test conducted in a six-inch circulating fluid bed roaster with air as the combustion gas and the composition of the off-gas was maintained at 6% oxygen by volume.
4 Same as in footnote 3 but the test was conducted in an eight-inch circulating fluid bed roaster.
5 Test conducted in a six-inch stationary fluid bed roaster with air as the combustion gas and the composition of the off-gas was maintained at 6% oxygen by volume.

The foregoing examples demonstrate that the process of the present invention produces significantly desirable results from refractory ores with arsenic-, carbon- and sulfur-containing components while reducing the cost of oxygen-based roasting and minimizing arsenic volatilization.

It is noteworthy, particularly by comparing air roasting, such as those in Example 2, with oxygen-enriched air roasting, such as those in Example 1, that the present invention effectively lowers the temperature at which optimum gold recovery occurs. This is graphically demonstrated by comparing FIG. 6 , which is for air roasting, with FIG. 4 which is for 40% oxygen-enriched air roasting. In FIG. 6 (air roast) the maximum gold recovery is at 600 degrees Celsius while in FIG. 4 (oxygen-enriched air roast) the maximum gold recovery is at 475 degrees Celsius. The importance of this is that the process of the present invention is more energy-economical. FIG. 5 shows that the percent gold extraction generally increases as the total oxygen content in the feed gas increases, with a practical, economical upper range based on other considerations such as operating costs, oxygen gas costs, equipment costs, etc.

EXAMPLE 7

In a schematic industrial illustration shown in FIG. 7 and described above, the following process data illustrate the application of the present invention.

The base case roaster feed analysis is as follows:

Carbon Organic                   0.8%
Sulfide Sulfur                   2.5%
Weight Loss on                   6.0%
Ignition - L.O.I.
As                               1200 ppm
Cl                               100 ppm
F                                1000 ppm
Pb                               25 ppm
Hg                               5 ppm
Sb                               80 ppm
Zn                               1000 ppm
SiO                                                                        2 80%
Al                                                                        2                                                                    O                                                                        3 7%

The following x-ray diffraction analysis was used to further characterize the above ore mixture:

Sericite  5%
Kaolinite 11%
Alunite   3%
Jarosite  5%

The ore feed had a specific gravity 2.52; and a bulk density (loose) of 1.0 m.t./m 3 and bulk density (packed) of 1.25 m.t./m 3 . Roaster feed (D50) was: 50% passed at 19μ size and 80% passed at 70μ (estimate). The design roast temperature was 550° C. and the O 2 concentration in off-gas was 36 vol. % wet basis. Organic carbon burn-off was assumed to be 0.7% (for energy calculations).

As illustrated by the above x-ray diffraction analysis it shows the ores to contain a variety of clay compounds predominantly kaolinite but also alunite, jarosite and sericite. These compounds all have varying decomposition energies (all assumed to be endothermic). At a roasting temperature of 525-550° C. all of the clays would be decomposed and hence all of the waters of crystallization would end up in the vapor phase.

Volatilization in roaster was taken for each elements as follows: Mercury 100%; Arsenic 1%; Fluorine 15% and Chlorine 100%.

Based on the above data, an illustration of an industrial operation as described in conjunction with FIG. 7 is shown in Table 7; this table must be read in conjunction with the description of the process in FIG. 7 .

TABLE 7
PROCESS DATA FOR A CIRCULATING FLUID BED ROASTING PLANT
SHOWN IN FIG. 7
Stream
No.	200	201	202	203	204	205	206	207	208	209	210
Medium		Ore	Gas	Gas	Gas	Gas	Gas	Air	Air	Air	Calcine	Calcine
												Slurry
Solids,	mt/h	160		38.5	35						154	154
dry	st/h	176		42	38						170	170
Water	mt/h	4.1*		7.8	7.8	4.1	3.7					873
	st/h	4.5*		8.6	8.6	4.5	4.1					963
Gas,	m 3 n/h		36100	47500	47500	25000	22500	1000	13600	7000
wet	scfm		21365	28100	28100	14790	13315	590	8050	4140
SO 2	vol %		5.7	9.15	9.15	9.15	9.15
SO 3	vol %		0.3	0.45	0.45	0.45	0.45
CO 2	vol %		6.7	10.8	10.8	10.8	10.8	21
O 2	vol %		56.3	36	36	36	36	79	90	48
N 2	vol %		18.2	23.2	23.2	23.2	23.2		10	52
H 2 O	vol %		12.8	20.4	20.4	20.4	20.4
Temp.	° C.	200	325	550	375	350	350	25	325	450	350	˜40
	° F.	392	617	1022	707	662	662	77	617	842	662	˜104
Pressure	mbar	+100	+200	−15	−20	−25	−25	+/−0	+200	+75	+/−0
	inch	+40	+80	−6	−8	−10	−10		+80	+30
*Water of crystallization in ore components
mt/h = metric tons per hour
st/h = short tons per hour
m 3 n/h = cubic meters normal per hour
scfm = standard cubic feet per minute

For the above illustration, a carbon content in the ore was provided for at 0.8% level, but should also be provided for a range from about 0.4% to about 1.15%. However, at still lower amounts of carbon in ore, more coal or fuel needs to be added, while at higher amounts of carbon in ore less or no coal is required (autothermal conditions). Hence, about 330 kg/hr of coal calculated as carbon is added for the above ore in Table 7. Besides the heat recovered in heat recovery unit 106, the waste heat boiler 116 produces at the specified conditions about 6 tons per hour of 55 bar steam.

In the above illustration, it is noted that a total “at temperature” time for the calcine (before quenching) is about 30 minutes. Such “at temperature” time is a combined time in the CFB reactor 100 and during post-finishing in heat recovery unit 106 . This “at temperature” time may range from about 25 minutes to 50 minutes and does not adversely affect the gold recovery even for the longer period; therefore, this process has an advantage because it is also free from the heat sensitivity, i.e. “at temperature” time limits such as cautioned against in some of the prior art processes and disclosures thereof.

While the above process has been illustrated as capable of treating ores of various particulate sizes, the advantageous size is determined for each ore and is typically from about −14 mesh to about −100 and less. At finer particulate sizes e.g. −100 mesh there is no need to wet grind the calcine after quenching in tank 105 but before leaching.

EXAMPLE 8

FIG. 8 illustrates a roasting with two stage oxygen injection carried out in a circulating fluidized bed. The circulating fluidized bed system consists of a fluidized bed reactor 301 , a recycling cyclone 302 , and a recycling line 303 . The fluidized bed reactor 301 was 0.16 m in diameter and had a height of 4 m. By means of a metering screw (not shown) a mixture of refractory gold ore and additives at a rate of 10 kg/h was charged through line 304 into the reactor 301 . The gold ore contained 0.8% arsenic, 1.4% sulfide sulfur and 13 g gold per 1000 kg. It had a particle size below 0.1 mm with a median value (D 50 ) of 20 μm. The types and quantities of the additives are apparent from the following Table 8. 80% of the additives had a particle size below 20 to 50 μm. A gas which contained 0.9% oxygen was fed at a rate of 10 sm 3 /h through line 305 into the gas heater 306 and was heated therein to 550° C. and then fed through line 307 into the reactor 301 as a fluidizing gas. The reactor 301 was indirectly heated and a temperature between 550° and 570° C. was adjusted in the reactor. The reactor 301 was fed through line 308 with secondary oxygen containing gas and through line 309 with tertiary oxygen containing gas. The secondary and tertiary gases consisted of preheated air and oxygen, respectively, and were used to adjust in the upper roasting stage the oxygen content indicated in the table. The calcine was withdrawn through line 310 . A gas-solid suspension was fed from the reactor 301 through line 311 to the recycling cyclone 302 and the solids separated therein were recycled through the recycling line 303 into the reactor 301 . The exhaust gas discharged through line 312 contained 0.1% to 0.5% SO 2 by volume.

In the following Table 8 the yield of gold and the solubility of arsenic in the cyanide leaching are indicated for various additives and oxygen contents. Whereas the addition of sodium compounds gives good results as regards the yield of gold, the solubility of arsenic will be excessively high in that case.

	TABLE 8
	O 2 Content →
	1%	6%	10%	40%
	Gold	Arsenic	Gold	Arsenic	Gold	Arsenic	Gold	Arsenic
	Yield	Solubility	Yield	Solubility	Yield	Solubility	Yield	Solubility
	%	mg/l	%	mg/l	%	mg/l	%	mg/l
Without	75.6	56	80.2	46	82.8	26	84.6	20
Additive
Additive	80.0	20	84.9	15	87.2	18	89.0	15
1.4% iron ore
Additive 2%	83.0	6	89.3	4	92.0	3	94.2	1
FeSO 4 .7H 2 O
Additive 3.2%	83.2	19	89.3	18	92.2	12	95.0	10
Ca(OH) 2
Additive 5%	82.8	10	88.1	7	92.0	3	94.8	2
CaSO 4 .2H 2 O
Additive 2%	82.6	70	87.9	50	91.8	48	96.4	50
Na 2 CO 3
Additive 2%	83.2	65	89.6	46	92.2	36	95.2	40
Na 2 SO 4

Based on the experiments described above a representative, schematic presentation of arsenic immobilization is evident from the oxygen content versus temperature curves from soluble and substantially insoluble arsenate formation. While it is evident from the composite curves shown above that as oxygen and temperature increases arsenic immobilization occurs, it is also evident that for efficient leaching such temperatures must be kept below ore component fusion temperatures which prevent good cyanide leaching. At an oxygen partial pressure of log.pO 2 of −3.0, the arsenate (in case of ferricarsenate—as shown in FIG. 10 ) must be also analyzed as only one component which needs to be considered. Carbon and sulfur must also be eliminated and efficient elimination calls for balancing of temperature and oxygen content. Additional substances such as CaSO 4 . 2H 2 O also favorably immobilize arsenic. Moreover, pyrites in the ore being in intimate contact with arsenic compounds in ore, as shown above, react favorably to immobilize arsenic especially at higher oxygen content in the reactant gas.

EXAMPLE 9

According to FIG. 11 the first circulating fluidized bed system consists of the fluidized bed reactor 401 , the recycling cyclone 402 , and the recycling line 403 . The fluidized bed reactor 401 was 0.2 m in diameter and had a height of 6 m. By a metering screw feeder, gold ore concentrate at a rate of 15 kg/h was charged through line 404 into the reactor. The concentrate contained 2.1% arsenic, 15% sulfide sulfur and 45 g gold per 1000 kg. The particle size was below 0.2 mm with a median size (D 50 ) of 70 μm. Air at a rate of 11 sm 3 /h (sm 3 =standard cubic meter) was fed through line 405 into the heat exchanger 406 and was preheated therein to 600° C. and then fed through line 407 into the reactor 401 as a fluidizing gas. The reactor 401 was fed through line 408 with secondary air at a rate of 9 sm 3 /h and through line 409 at a rate of 3 sm 3 /h with tertiary air, which served to combust the residual sulfur in the reactor 401 . By the distribution of the air supply, the oxygen potential was adjusted to be in the range in which arsenic is volatilized in the Fe 2 O 3 range (FIG. 10 ), below the range in which iron arsenate is formed.

The temperature in the reactor was between 700° C. and 750° C. The calcine withdrawn through line 410 contained 0.02% arsenic and 0.1% sulfur. The leaching of the calcine resulted in a recovery of gold with a yield of 96%. The solubility of arsenic during the leaching of gold was very low and amounted only to less than 2 mg/l.

A gas-solid suspension was fed from the reactor 401 through line 411 into the recycling cyclone 402 . The solids collected there were recycled through the recycling line 403 into the reactor 401 . The exhaust gas conducted in line 412 was dedusted in two cyclones (not shown) and in a candle filter 413 at about 600° C. The collected dusts were returned to the reactor 401 through line 414 . The dust-free exhaust gas contained SO 2 and As 2 O 3 and was fed through line 415 to the fluidized bed reactor 416 of a second circulating fluidized bed system.

The reactor 416 was 0.16 m in diameter and had a height of 4 m. It was heated by indirect electric heating. Hematinic iron ore having a particle size below 0.5 mm, with a medium size of 30 μm, was charged through line 417 at a rate of 0.3 kg/h. Fluidizing air at a rate of 15 sm 3 /h was fed into the reactor 416 .

The suspension leaving through line 419 was adjusted to contain 6% oxygen and 4% water vapor so that the conditions for a formation of stable arsenates ( FIG. 9 ) were established. To adjust a water vapor content of 4%, the moisture content of the iron ore charged through 417 was controlled in dependence on the water vapor content of the gas entering through line 415 and of the fluidizing air entering through line 418 .

The solids collected in the recycling cyclone 420 were returned through the recycling line 421 into the reactor 416 . The arsenic-free roaster gas contained 9.1% SO 2 and was fed through line 22 to a gas purifier and subsequently to a plant for producing sulfuric acid. The solid material which was discharged through line 423 from the reactor 416 contained 17.3% arsenic. Leaching tests with water (corresponding to a DEV-S 4 leaching test) showed that the solubility of arsenic was less than 1 mg/l.

According to a preferred feature of the embodiment shown in Example 9, the dust-containing gases which contain arsenic vapor and arsenic compound vapor(s) are produced by roasting e.g. of sulfide materials which contain iron and arsenic. Such materials are roasted in the Fe 2 O 3 range at temperatures of 500° C. to 1100° C. in a first stage, which is supplied with oxygen-containing gases. In these materials, arsenic is volatilized mainly as arsenic oxides and part of the sulfur content is volatilized as elementary sulfur. Solids are removed from the exhaust gas at temperatures above the condensation temperature of the volatilized components, and the solids are discharged as calcine.

The sulfide materials may consist of arsenic-containing ores or ore concentrates, such as gold ores, copper ores, silver ores, nickel ores, cobalt ores, antimony ores, lead ores and iron ores as well as of arsenic-containing sulfide residues and intermediate products. By the roasting, a small part of the arsenic content is reacted to form arsenic sulfides. In the processing of gold ores or gold ore concentrates, environmentally acceptable dumps of residues are obtained. Further, a product from which gold can be leached with cyanides in a high yield.

Although the above illustrations concerning metal recovery has been with reference to gold, other precious metal and metal recovery of arsenic containing ores may be practiced as described herein—thereby realizing the advantages of the present process, i.e. low temperature (e.g. less than 700° C.), oxygen enriched air roasting in presence of substances such as iron or calcium to immobilize arsenic as e.g. ferricarsenate in the form of scorodite or scorodite like compounds. Scorodite like compounds are intended to mean compounds of ferricarsenate with water of crystallization of varying mole amounts. For scorodite two moles of water of crystallization is typically shown but the amounts of water crystallization may vary. As shown above, the presence of water of crystallization in the added substance the roasting atmosphere or in the ore components, e.g. aids in the immobilization of arsenic. However, the measure for immobilization, i.e. insolubility, is scorodite and represents the level of insolubility which is desired. A “scorodite like” compound is intended to have insolubility of about the same order of magnitude as scorodite.

Moreover, while the process for gold recovery has been found best conducted with the indicated oxygen levels for other metal recovery from ores which contain arsenic, such process may be practiced with even higher oxygen levels (and also temperature levels) as shown above because the improvement concerning arsenic recovery as such may even be practiced with pure oxygen used as the oxidizing medium. When using higher temperatures, i.e. as shown in Example 9, the combination of first stage and second stage treatment provides a double measure of safety that any arsenic which may have been volatilized may be separately immobilized to assure an environmentally double safe treatment of any off gas. Such combination also provides for employment choice of a lower oxygen content in first stage and higher in the second stage. In part such effect may also be achieved by the multiple oxygen injection as shown for the gold ores treated in the combination shown in Example 8.

Because of these advantages including those derived from e.g. circulating fluidized beds, the present invention provides improvements over those shown by the prior art as previously described and pointed out with reference to that art.

While the exact reasons that cause the process of the present invention to produce the herein-observed results are unknown and could not be predicted, the results themselves bespeak the achievements that have been obtained—based merely on the percent of gold extraction and arsenic immobilization—from these refractory ores at great savings of oxygen usage and using a less complicated approach than the best prior art technology can show. It is especially noted for conditions such as apply when using a circulating fluidized bed which provides for significant heat recovery and reutilization.

The following examples are directed to the invention relating to the process of roasting refractory gold ores in the presence of added fuels.

EXAMPLE 10

The refractory gold ore which was used contained 8 mg/kg gold, 1.8% by weight sulfur as pyrite and 0.08% by weight carbon. The median particle size d 50 was 30 micrometers, and 100% of the particles were smaller than 200 micrometers.

The roasting plant was a circulating fluidized bed system and consisted mainly of a fluidized bed reactor, a recycling cyclone, which was directly connected to the gas outlet at the top part of the reactor, and a recycling line (FIG. 7 ). The solids which had been separated in the cyclone were recycled through the recycling line to the reactor.

A mixture containing 48 g pyrite per kg ore was prepared and was charged at a rate of 40 kg/h through a downcomer into the fluidized bed reactor.

Air which contained 21% by weight oxygen and was at a temperature of 400° C. was supplied to the windbox of the fluidized bed reactor at a rate of 22 sm 3 /h (sm 3 =standard cubic meter). The carrier gas flowed through the openings of the perforated bottom. The temperature in the reactor was 520° C. The gas from roasting contained 3.3% by volume SO 2 , 0.2% by volume CO 2 , 20 vppm CO, and 16.3% by volume O 2 . The contents of H 2 and hydrocarbons were below the detection threshold of 1 vppm. The exhaust gas was scrubbed with an alkaline absorbent to remove SO 2 and was then discharged through a chimney. The roasted material contained <0.05% by weight sulfur and <0.01% by weight carbon. Its further processing resulted in a gold yield of 94%.

EXAMPLE 11

Example 11 was carried out like Example 10 but with a carrier gas which contained 32% by volume O 2 and owing to a recycling of exhaust gas contained 7% by volume SO 2 . The fluidized bed reactor was supplied with a mixture which contained 50 g sulfur per kg ore. The gas from roasting contained 12.7% by volume SO 2 , 0.1% by volume CO 2 , 5 vppm CO, and 24.2% by volume O 2 . The contents of H 2 and hydrocarbons were below the detection threshold of 1 vppm. The roasted material contained <0.04% by weight sulfur and <0.01% by weight carbon. Its further processing resulted in a old yield of 96%.

The gold ore used in Examples 10 and 11 had the following composition:

8 mg/kg Au

3.3% by weight FeS 2

0.07% by weight Fe [AsS]

The pyrite used in Example 10 had the following composition;

91% by weight FeS 2

2% by weight FeS

7% by weight SiO 2 , Al 2 O 3 and other components.

The sulfur used in Example 11 had the following composition:

98% by weight S

2% by weight impurities

The above examples 10 and 11 illustrate the benefits obtained by treating precious metal ores by roasting in the presence of added fuels containing sulfur, pyrite and mixtures thereof. In addition, these examples illustrate the use of sulfur, pyrite and mixtures thereof as fuels for roasting in fluidized beds, in particular, circulating fluidized beds. Example 10 and 11 also illustrate that sulfur, pyrite and mixtures thereof are fuels that can be reliably ignited at low temperatures and which can be combusted to produce an exhaust gas which is free of or has only low contents of CO, H 2 and hydrocarbons.

The sulfur, pyrite and mixtures thereof can also be added for roasting of ores for the recovery of metals such as precious metals in an oxygen-enriched gaseous environment under conditions as described above in order to minimize and/or eliminate arsenic volatization, facilitate arsenic conversion to an insoluble, environmentally acceptable form immobilized in a waste product while reducing the effects of carbon and sulfur containing components on metal recovery such as precious metal recovery. In addition to the benefits of having fuels that can reliably be ignited at low temperatures and which can be combusted to produce an exhaust gas which is free of or has only low contents of CO, H 2 and hydrocarbons, the present invention can also achieve precious metal recovery, in particular gold recovery, with facile arsenic elimination as an environmental problem, while also minimizing leaching cyanide consumption and conserving heat given off in the roasting process.

It is also evident from the above that various combinations and permutations may well be practiced and advanced, but these are not to be understood as limiting the invention which has been defined in the claims which follow.

Claims

1. A process for roasting refractory precious metal ores in the presence of fuels in an oxidizing atmosphere in a fluidized zone comprising: (1) combining said metal ores and said fuels, said fuels being different from said precious metal ores and selected from the group consisting of sulfur, pyrite and mixtures thereof, (2) igniting said fuels in said fluidized zone, (3) supplying oxygen-containing gases to said fluidized zone, and (4) roasting said ores at temperatures from about 400 to about 650° C. in said fluidized zone, wherein the O2 content of the gases fed to the fluidized zone is from about 20 to 50% by volume and where said roasting provides an exhaust gas having a hydrocarbon content less than about 200 volume parts per million.

2. A process according to claim 1, wherein said roasting is carried out at temperatures from about 500 to about 550° C.

3. The process as defined in claim 1, wherein sulfur, pyrite or mixtures thereof and at least one additional fuel selected from the group consisting of hydrocarbons containing 1 to 16 carbon atoms, alcohols containing 1 to 6 carbon atoms and 1 to 2 COH groups, organic ethers containing 2 to 8 carbon atoms and one oxygen atom, CS2, and H2S are introduced as additional fuels to said fluidized zone.

4. The process as defined in claim 3 wherein said roasting is carried out at a temperature from 500 to 550° C.

5. A process according to claim 1, wherein the refractory precious metal ores are gold ores having a mean particle size below about 1 mm.

6. A process according to claim 1, wherein 60 to 80% of said refractory precious metal ores are gold ores of a mean particle size below about 75 micrometers.

7. The process in claim 1, and wherein a slip stream as defined from the hot exhaust gas is dedusted and said slip stream of said exhaust gas is admixed to a fluidizing gas before it is fed to said fluidized zone.

8. The process as defined in claim 1, and wherein SO2 gas formed by roasting of said refractory precious metal ores is carried away in an exhaust gas for a production of sulfuric acid.

9. The process as defined in claim 1, and wherein roasting is carried out in a circulating fluidized bed.

10. The process as defined in claim 3, wherein said precious metal ore is gold ore of a mean particle size below about 1 mm.

11. The process as defined in claim 1, wherein an exhaust gas from said fluidized zone has an H2 content of less than about 10 vppm, a CO content of less than about 0.1% by volume, and a hydrocarbon content of less than about 100 vppm.

12. The process as defined in claim 1 wherein said refractory precious metal ore comprises said precious metal and arsenic.

13. The process as defined in claim 12 wherein said arsenic in said precious metal ore is converted during roasting in the presence of a fuel added to the oxidizing atmosphere for lowering ignition temperatures and in the presence of water in said fluidized zone, to an insoluble arsenate, wherein said fuel contains sulfur, pyrite or mixtures of same.

14. The process of claim 1, wherein said fuels consist essentially of sulfur, pyrite or mixtures thereof.

15. The process of claim 1, wherein said fuels consist essentially of sulfur.

16. The process of claim 1, wherein said fuels consist essentially of pyrite.

17. The process of claim 1, where said roasting provides an exhaust gas having an H2 content of less than about 50 volume parts per million.

18. The process of claim 1, where said roasting provides an exhaust gas having a CO content of less than about 0.5% by volume.

19. The process of claim 1, where said roasting provides an exhaust gas having an H2 content of less than about 5 volume parts per million.

20. The process of claim 1, where said roasting provides an exhaust gas having a CO content of less than about 0.1% by volume.

21. The process of claim 1, where said roasting provides an exhaust gas having a hydrocarbon content less than about 50 volume parts per million.

22. The process as claimed in claim 1, wherein said roasting is carried out at a temperature less than about 550° C.

23. The process as claimed in claim 1, wherein said roasting is carried out at a temperature less than about 450° C.

24. The process as claimed in claim 1, wherein said process further comprises the step of pre-mixing said fuels with said metal ores prior to said metal ores being placed in said fluidized zone.

25. The process as claimed in claim 1, wherein said fuels are added to said metal ores during said roasting.

26. The process of claim 1, wherein said fuels are added to said metal ores prior to said roasting.

27. A process for roasting refractory gold ores comprising the steps of: (a) combining said refractory gold ores with a fuel, said fuel being different from said gold ores and containing sulfur, pyrite or mixtures thereof, and (b) roasting the ores in a fluidized zone in an oxidizing atmosphere in the presence of said fuel at a temperature between 400° C. and 650° C.; wherein said fuel is ignitable within the temperature range from 400° C. and 650° C., and wherein the O2 content of gases fed to the fluidized zone is from about 20 to 50% by volume and where said roasting provides an exhaust gas having a hydrocarbon content less than about 200 volume parts per million.

28. The process as defined in claim 27, wherein roasting is carried out at temperatures from 400 to 650° C.

29. The process as defined in claim 27 wherein the refractory gold ores comprise arsenic and said arsenic in said gold ores is converted to an insoluble arsenate during roasting, adding supplemental fuel to the oxidizing atmosphere for lowering ignition temperatures during roasting wherein roasting is at a temperature between 400° C. to 650° C., wherein roasting said ores is in the presence of water in a fluidized zone,, and wherein said fuel contains sulfur, a pyrite or mixtures of same.

30. The process as defined in claim 29, wherein said pyrite is iron pyrite.

31. A process of roasting refractory gold ores comprising roasting the ores in an oxidizing atmosphere in a fluidized zone in the presence of a fuel that contains sulfur, a pyrite or mixtures thereof added directly to or premixed with the ores, wherein the O2 content of gases fed to the fluidized zone is from about 20 to 50% by volume and where said roasting provides an exhaust gas having a hydrocarbon content less than about 200 volume parts per million, wherein said refractory gold ores and said fuel are different.

32. A process according to claim 31 wherein during roasting, sulfur, pyrite or mixtures thereof are fed to said fluidizing zone, as fuels, with at least one additional fuel selected from the group consisting of hydrocarbons containing 1 to 16 carbon atoms, alcohols containing 1 to 6 carbon atoms and 1 to 2 COH groups, organic ethers containing 2 to 8 carbon atoms and one oxygen atom, CS2 and H2S.

33. The process as defined in claim 31 wherein the gold ore has a particle size below about 1 mm.

34. The process of claim 31, where said roasting provides an exhaust gas having an H2 content of less than about 5 volume parts per million.

35. The process of claim 31, where said roasting provides an exhaust gas having a CO content of less than about 0.1% by volume.

36. A process for roasting refractory precious metal ores in the presence of fuels comprising the steps of adding said fuels to said metal ores and roasting the ores in a fluidized zone in an oxidizing atmosphere in the presence of said fuels at a temperature less than 550° C., said fuels different from said refractory precious metal ores and containing sulfur, pyrite or mixtures thereof and wherein the O2 content of gases fed to the fluidized zone is from about 20 to 50% by volume and where said roasting provides an exhaust gas having a hydrocarbon content less than about 200 volume parts per million.

37. The process of claim 36, where said roasting provides an exhaust gas having a CO content of less than about 0.1% by volume.

38. A method for reducing the ignition temperature, the roasting temperature or combinations thereof of a process for roasting refractory precious metal ores comprising the steps of: (a) combining a fuel other than said metal ores to said metal ores, said fuel containing sulfur, pyrite or mixtures thereof and (b) roasting the ores in a fluidized zone in an oxidizing atmosphere in the presence of said fuels at a temperature less than 550° C., wherein the O2 content of gases fed to the fluidized zone is from about 20 to 50% by volume and where said roasting provides an exhaust gas having a hydrocarbon content less than about 200 volume parts per million, thereby performing said process for roasting using a reduced ignition temperature, a reduced roasting temperature or combination thereof relative to performing said roasting without said fuel.

39. The method of claim 38, where said roasting provides an exhaust gas having a hydrocarbon content less than about 50 volume parts per million.

40. The method of claim 38, where said roasting provides an exhaust gas having an H2 content of less than about 50 volume parts per million.

41. The method of claim 38, where said roasting provides an exhaust gas having an H2 content of less than about 5 volume parts per million.

42. The method of claim 38, wherein said roasting provides an exhaust gas having a CO content of less than about 0.1% by volume.

43. The method of claim 38, where said roasting provides an exhaust gas having a CO content of less than about 0.5% by volume.

44. The method of claim 38, wherein said fuels consist essentially of sulfur, pyrite or mixtures thereof.

45. The method of claim 38, wherein said fuels consist essentially of sulfur.

46. The method of claim 38, wherein said fuels consist essentially of pyrite.

47. A process for roasting refractory precious metal ores comprising the steps of: (a) forming a mixture comprising said refractory precious metal ores and an additive comprising pyrite, wherein said refractory precious metal ores and said additive are different and (b) roasting said refractory precious metal ores in a fluidized zone in an oxidizing atmosphere at a temperature from about 450° C. to about 600° C., wherein the O2 content of gases fed to the fluidized zone is from about 35 to 55% by volume.

48. The process of claim 47, wherein said additive consists essentially of pyrite.

49. A process for roasting refractory precious metal ores comprising the steps of: (a) forming a mixture comprising said refractory precious metal ores and an additive consisting essentially of sulfur and (b) roasting the ores in a fluidized zone in an oxidizing atmosphere at a temperature less than 550° C., wherein the O2 content of gases fed to the fluidized zone is from about 20 to 50% by volume and where said roasting provides an exhaust gas having a hydrocarbon content less than about 200 volume parts per million.