Patent Application
20100307977
This invention relates to the removal of cyanide from aqueous streams and to the recovery of metal values from aqueous streams.
Mining operations, in particular gold mining operations, make use of cyanide in leaching steps to extract gold and other precious metals from ore. A portion of leaching solution is discharged as a residue slurry. Contained within the slurry is cyanide in the form of cyanide ions and weak acid dissociable cyanide (WAD cyanide) which is extremely toxic and must be destroyed before the slurry can be disposed of as an aqueous waste stream. According to the International Cyanide Code, WAD concentrations (calculated as WAD cyanide plus free cyanide) in waste streams must be less than 50 ppm.
There are many processes in the prior art which can be used to remove cyanide from aqueous streams, however these processes produce other toxic substances which must then be dealt with and/or are expensive to operate.
It is an object of this invention to provide an improved and economical process for removing cyanide and recovering metal values from aqueous streams.
This invention relates to a cyanide removal method for treating an aqueous stream containing cyanide, typically a tail stream from a carbon in leach (CIL) mining operation, wherein the aqueous stream containing cyanide is contacted with carbon under conditions wherein the Eh (oxygen reduction potential (ORP) measured in mV) of the aqueous stream is 0 or above, to remove cyanide, particularly WAD cyanide, from the stream.
The Eh may be from 0-500, typically from 0-300, preferably from 0-200 mV.
The carbon is preferably in particulate form, for example activated carbon manufactured from coconut shell having a particle size of 2-3 mm.
The carbon is added in an amount of 5-100 g/l, typically 10-60 g/l, preferably 20-60 g/l of the stream containing cyanide.
Preferably, the pH of the aqueous stream is buffered to from 7-9. The buffering preferably takes place over a period of 0.5-1.5 hours, typically about 1 hour.
The Eh of the stream containing cyanide may be controlled by passing the stream containing cyanide through an oxygenating device in multiple passes, before or after the addition of cyanide to the stream.
The oxygenating device is typically operated at a pressure of from above 1 bar up to about 10 bar, typically about 2.5 bar.
Oxygen is preferably introduced into the oxygenating device in the form of bubbles, the bubbles preferably having a size of from 1 micron to 1000 microns, preferably 1 to 500 microns, typically an average of 100 microns. Advantageously, the oxygenating device provides high shearing to the stream.
Preferably, the oxygen line pressure at the point of injection of oxygen is above the pressure of the oxygenating device, typically at a pressure of about 10 bar.
The Oxygen consumption of the oxygenating device may be from 0.25 kg/t to 200 kg/t liquid.
Preferably, the aqueous stream is re-circulated through the oxygenation device in 2 or more passes, typically from 2 to 300, preferably 2 to 200, more preferably 2 to 50, more preferably 2 to 10, most preferably 2 to 5 passes
In a first embodiment of a process of the invention, a tail stream from a carbon in leach (CIL) mining operation containing cyanide is:
The carbon is preferably in particulate form, for example activated carbon manufactured from coconut shell having a particle size of 2-3 mm.
The carbon is added in an amount of 5-100 g/l, typically 10-60 g/l, preferably 20-60 g/l of the stream containing cyanide.
Preferably, the pH of the aqueous stream is buffered to from 7-9.
Preferably, the treatment to control the Eh is with an oxygenating device as described above.
The stream may be passed through the oxygenating device in from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 2 to 10, more preferably 2 to 5, most preferably 2.5 passes.
Preferably, the contact with carbon takes place in a tank separate from the oxygenation device. The tank is typically open to the atmosphere.
The cyanide removal preferably takes place in multiple stages.
In a second embodiment of a process of the invention, an aqueous stream containing metal values is:
Preferably, the treatment to control the Eh is with an oxygenating device as described above.
The stream may be passed through the oxygenating device in from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 5 to 15, most preferably 10 passes.
The pre-oxidation stage preferably takes place at a pH of 9 to 10.
In a third embodiment a process of the invention, an aqueous stream containing metal values is:
The stream may be passed through the oxygenating device in from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 5 to 10, most preferably 5.
Preferably, the Eh of the stream in the oxygenating device is greater than 0.
A preferred integrated process according to the invention for leaching an aqueous stream containing metal values is described below:
This invention relates to a method of removing cyanide in the form of free cyanide (cyanide ions i.e. CN−) and weak acid dissociable cyanide (WAD) from an aqueous stream. WAD is cyanide complexed with metals such as Cu. The method finds particular application in removing cyanide from a tail stream from a carbon in leach (CIL) mining operation.
The method of the invention is carried out by contacting an aqueous stream containing cyanide with carbon under conditions wherein the Eh (oxygen reduction potential (ORP) measured in mV) of the aqueous stream is 0 or above. The Eh may be from 0-500, typically from 0-300, preferably from 0-200 mV. The carbon is preferably in particulate form, for example activated carbon manufactured from coconut shell having a particle size of 2-3 mm. The carbon catalyst is added in an amount of 5-100 g/l, typically 10-60 g/l, preferably 20-60 g/L of the stream containing cyanide. Advantageously the pH of the solution is buffered to from 7-9.
In accordance with the present invention, the desired Eh (above 0) of a stream containing cyanide is controlled by, if necessary adjusting the pH to 7-9, and pumping the stream through an in-line high shear static oxygenation device, while re-circulating it on the tank or any other vessel including pipe columns. The stream is pumped through the oxygenating device generating a slurry back-pressure from 1 bar up to 10 bar, typically about 2.5 bar. The back-pressure of the device is read off a pressure gauge. Oxygen is injected into the device via an appropriately sized flow meter. The oxygen line pressure at the point of injection should be above the back-pressure of the oxygenating device, preferably about 10 bar to overcome the slurry back-pressure of the device and to achieve the desired oxygen flow rates. Non-return valves should be installed on the oxygen lines to prevent the ingress of slurry into the oxygen system.
The number of passes through the oxygenation device could range from 2 or more to 300 passes. The bubble size generated in the oxygenation device could range from 1 micron to 1000 microns, preferably 1 to 500 microns, typically an average size of 100 microns. The stream should be pumped at a rate of 5 to 20 m/s, typically about 10 m/s, through the oxygenating device to create the internal shear within the unit. The back-pressure of the device could range from above 1 bar up to about 10 bar. The device utilises a non-blinding porous media (such as a PTFE fritte) arrangement or a slot or plate nozzle venturi system to inject tiny oxygen bubbles into the pulp. The subsequent pressure chamber system causes the rapid expansion and contraction of these bubbles (cavitation), which assists with the dissolution of the oxygen. The design of the device discourages bubble coalescence, and the pressure hold-up (around 2.5 bar but can range from above 1 bar up to about 10 bar) also encourages oxygen dissolution. Oxygen consumption could range from 20 kg/t to 200 kg/t.
An oxygenating device as described above and manner in which it is operated is able to raise Eh (oxygen reduction potential (ORP) which is measured in volts) of the aqueous stream to a sufficiently high level so as to oxidize free and WAD cyanide to the cyanate (CNO—) ion. The cyanate ion decomposes over time to ammonia and carbon dioxide. With regard to the mechanism of carbon catalysis, it is believed that activated carbon adsorbs both the free and WAD cyanide facilitating the oxidation of the cyanide ion by oxygen. The reaction products (cyanate and metal ions) are then released back into solution. Although in the above described method the oxygenation takes place in the presence of the carbon catalyst, it is possible to conduct the oxygenation using the device and method described above prior to the introduction of the catalyst, with the subsequent introduction of the catalyst to the stream, and achieve the desired removal of cyanide.
It is also possible to control the Eh of a aqueous stream to the desired levels in other ways. For example, this could be achieved by adding acid and/or CuSO4 to the solution. These reagents could also be used in conjunction with an oxygenating device as described above. However, these method/s are not as cost-effective as the present invention as they require the use of additional reagents and can also produce other toxic substances in the stream.
Comparative Examples 1, 2, and 3 show the results of tests conducted on CIL samples from a gold plant where the samples are subjected to an oxygenating device as described above in multiple passes and treated with different amounts of activated carbon. In Examples 1, 2, and 3, multiple passes (up to 80) and up to 50 g/l carbon failed to reduce the CN Wad to an acceptable level below 50 ppm. In Examples 2 and 3, the samples were buffered to pH 9 and 8 respectively and even this and multiple passes (up to 30) and up to 50 g/l carbon failed to reduce the CN Wad to an acceptable level below 50 ppm. In Example 4, however, where the Eh is greater than 0, the level of CN Wad was successfully reduced to below 50 ppm when treated with 50 g/l, irrespective of the number of passes.
In Example 5, a tail from Example 4 was subjected to the process at a Eh greater than 0, and the CN Wad was successfully reduced to less than 1 ppm. In Example 6, a tail from Example 5 was subjected to the process at a Eh greater than 0, and the CN Wad was consistently reduced to less than 1 ppm. This shows the benefit that can be obtained with multi-stages.
Example 7 shows the process carried out with the addition of CuSO4. It is only when the Eh is greater than 0 that the level of CN Wad was successfully reduced to below 50 ppm, when treated with 50 g/l of carbon.
Example 9 shows gold recoveries that can be obtained from a CIL feed stream from a mining operation which has been treated with a process of the present invention.
The above method may be used in an integrated process for leaching an aqueous stream containing metal values (typically precious metals), such as a feed stream in carbon in leach (CIL) mining operation.
With reference to the Drawing, in a first (optional) pre-oxidation stage 10, a feed stream 12 containing precious metals is passed through an oxygenating device as described above in multiple passes (from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 5 to 10, most preferably 5) in a pre-oxidation step.
FeS minerals consume cyanide to various degrees depending on their reactivity. Reactivity increases in the following order: arsenopyrite<pyrite<marcasite<pyrrhotite.
The following equation describes the reaction:
FeS+½O2+7CN—+H2O═Fe(CN)64−+SCN—+2OH— (1)
Equation 1 above illustrates how Fe2+ in solution consumes cyanide by forming the hexa-ferrocyanide complex. Sulphur consumes only one cyanide ion to form thiocyanate. The ferrous ion alone can therefore consume up to six times that of its solution concentration of cyanide ion. This undesirable side reaction can result in unnecessary high cyanide consumption.
Iron is generally present in soluble form as a mix of Fe2+ and F3+ with the proportion of the two being dictated by the redox potential of the solution.
It has been found that the formation of the hexa-ferrocyanide complex may be counteracted by this pre-oxidation stage, prior to a leach, which promotes the formation of ferric ions and the subsequent precipitation of ferric hydroxide with the addition of lime.
Additionally, a pre-oxidation stage promotes the formation of a ferric hydroxide passivating layer on the iron sulphide mineral surface, so reducing the rate of iron sulphide dissolution in the subsequent cyanide leach circuit.
The pre-oxidation stage preferably takes place at a pH of 9 to 10, to provide a pH of 9 at the tail in stage below (the oxidation steps naturally degrade the pH owing to the production of sulphuric acid from sulphur oxidation).
An advantage of the pre-oxidation stage is that it precipitates much of the iron and other base metals as hydroxides, so preventing them from consuming cyanide in the subsequent cyanidation stage. This reduces the cyanide consumption for a given free cyanide level in the leach and so reduce the cyanide load on the circuit, leaving lower levels of cyanide to be dealt with at the tail end of the plant.
A further advantage of the pre-oxidation stage is that Sulphur is oxidized, and this limits the formation of SCN− when cyanide is added.
A further advantage of the pre-oxidation stage is that it causes almost complete hydrolysis of lime resulting in an almost zero protective alkalinity, to enable a natural decay of the pH mentioned above.
After the pre-oxidation stage, in an accelerated leach stage 14, the stream is subjected to an optional accelerated leaching step, by adding cyanide and using an oxygenating device as described above. This boosts kinetics and reduces the number of tanks required in the following CIL process.
It is widely accepted that Elsner's Equation, below, describes the gold leaching reaction:
4Au+8NaCN+O2+H2O=4NaAu(CN)2+4NaOH (2)
It can be seen from the equation that oxygen is a requirement for the leach. The balanced equation seems to suggest a CN:O2 ratio of 8:1. However, work done by Habashi (which takes the diffusivity of cyanide and oxygen into account) seems to suggest that the ratio should be 6:1. E.g. if the free cyanide concentration is 150 ppm, then the DO should be 25 ppm for efficient utilization of the cyanide for leaching.
It is further widely accepted that increased rate of cyanidation can be achieved by the use of oxygen instead of air, under pressure if necessary, increased agitation and elevated temperatures (Stanley).
Conducting the accelerated leach stage 14 (adding 0.1-1, typically 0.5 kg/t cyanide) using an oxidation device as described above in the manner described above multiple passes—from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 5 to 10, most preferably 5). Extra precautions do however need to be taken if there is a preg-robber present in the ore. Precautionary measures include the operation of the high shear oxygenating device on a column with a residence time of under 25 minutes and optionally with diesel addition to the recirculation vessel. Example 10 shows the benefits that can be attained using an accelerated leach step.
After the accelerated leach stage 14, the stream is subjected to a conventional carbon in leach (CIL) process 16 where it is treated in multiple tanks I-V. The CIL may take place in an agitated leach tank open to the atmosphere containing activated carbon.
After the CIL process 16, the stream is subjected to the cyanide removal process of the present invention—a tail stage 18. The stage 18 comprises contacting the stream with an Eh of greater than 0, typically 0-300, preferably 0-200 mV, with a particulate carbon catalyst at a concentration of from 5-100 g/l, typically 30-60 g/l, preferably 45-55 g/l, most preferably 50 g/l.
In this embodiment of the invention, the cyanide removal stage comprises multiple stages—first stage 20 and second stage 22.
In the first stage 20, the stream is introduced into an oxygenating device 20A as described above, if necessary adjusting the pH to 9 to 10, in multiple passes (from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 2 to 10, more preferably 2 to 5, most preferably 2.5 passes) to bring the Eh of the stream to 0 or above, for example from 0-500, typically from 0-300, preferably from 0-200 mV. The stream is than introduced to a tank 20B, where it is contacted with 5-100 g/l, typically 10-60 g/l, preferably 20-60 g/L particulate carbon of the stream containing cyanide. This stage is able to reduce the amount of WAD cyanide in the stream to below 50 ppm.
The stream from the first stage is then subjected to the second stage 22, and is introduced into an oxygenating device 22A as described above, if necessary adjusting the pH to 9 to 10, in multiple passes (from 2 to 300, typically 2 to 200, preferably 2 to 50, more preferably 2 to 10, more preferably 2 to 5, most preferably 2.5 passes) to bring the Eh of the stream to 0 or above, for example from 0-500, typically from 0-300, preferably from 0-200 mV. The stream is then introduced to a tank 22B, where it is contacted with 5-100 g/l, typically 10-60 g/l, preferably 20-60 g/L particulate carbon of the stream containing cyanide. This stage is able to reduce the amount of WAD cyanide in the stream to below 10 ppm.
Further stages may be added to the tail stage 18, or the stream may be subjected to a further cyanide removal step by contacting the stream in an oxygenating device as described above with a copper, iron or zinc or graphite catalyst.
The pre-oxidation stage 10 and accelerator stage 14, although preferred, are optional and the process of the invention can be successfully carried out on a CIL tailing using the tail stage 18 without stages 10 and 14.
The process of the invention could also be carried out successfully without the tail stage 18, with removal of free and WAD cyanide taking place in the CIL stage 16. In this embodiment of the invention, the pH of the stream 12 is adjusted to pH to 9 to 10, and passed, in multiple passes (from 5 to 300, typically 10 to 200, preferably 10 to 50 passes), through an oxygenating device as described above is controlled to provide an Eh in the CIL process of the stream of 0 or above, for example from 0-500, typically from 0-300, preferably from 0-200 mV. The carbon which is ordinarily added to the CIL to adsorb leached gold also catalyses the cyanide destruction when the stream is at an Eh of 0 or above.
A key step of the process of the invention is to raise the Eh (ORP) of the pulp containing the cyanide species to be destroyed sufficiently, utilizing the oxygenating device in a carbon in leach tank. The activated carbon contained in the tank is essential as a catalyst for the oxidation of both free and WAD cyanide. Copper sulphate may be used in addition for more complete destruction. Iron and zinc sulphate may also be used but are less effective. In addition to destroying the free and WAD cyanide species, any residual undissolved gold will also be leached to yield extra revenue. Also the efficiency of gold adsorption by the activated carbon will be markedly improved.
The oxygenating device passes required for cyanide destruction need not be confined to a single tank and may be spread out across an entire tankfarm, provided that the total number of passes is sufficient to raise the Eh of the solution to a point high enough for cyanide destruction when contacted with carbon. With this in mind the oxygenating devices may be run optionally:
Advantages of the processes of the present invention are:
The invention will now be described in more detail with reference to the following non-limiting Examples.
In the Examples, the oxygenating device is an Aachen™ Aerator available from Maelgwyn Mineral Services Ltd.
In the Examples, the following terms have the following meanings:
N/R: Not requested
CN free by ISE: Is theoretically the same as titration (but in practice is closer to stability constant calculated CN free)
CN WAD: Does include CN free (and Zn, Cu and Ni complexed species)
CN Total: CN free, rest of CN WAD and CN SAD accumulated
CN SCN: Cyanide part of thiocyanate
CN: CNO is the oxidation product of cyanide.
g: gram/litre carbon added to the bottle rolls.
CIL tail sample from a gold Plant was used.
pH as received, no buffering carried out.
Aachen run 80 passes maximum.
Temperature, pH and Eh recorded at regular intervals.
Pulp samples were extracted after predetermined Aachen passes and bottle rolled for 24 hours with increasing carbon concentration for each sample taken.
The result of Example 1 was unsuccessful (WAD cyanide was above 50 ppm target)
Failure can be attributed to negative Eh readings and pH>10.
High Aachen passes and high carbon concentration did not reduce WAD to 50 ppm.
Indicates mechanism of adsorption onto carbon alone is not sufficient.
CIL tail sample from a gold Plant was used.
Buffered for 1 h with 3.26 kg/t H2SO4 to pH 9
Aachen run 30 passes maximum
Temperature, pH and Eh recorded at regular intervals
Pulp samples extracted at timed intervals and bottle rolled for 24 hours with increasing carbon concentration for each sample taken.
Example 2 was unsuccessful (WAD cyanide was above 50 ppm target), even though pH was buffered to 9.
Can be attributed to negative Eh values.
CIL tail sample from a gold Plant was used.
pH buffered to 8 with 5.89 kg/t H2SO4 for 1 hour
Aachen run 30 passes
Temperature, pH and Eh recorded at regular intervals
Pulp samples extracted at timed intervals and bottle rolled for 24 hours with increasing carbon concentration for each samples taken.
Example 3 was unsuccessful (WAD cyanide was above 50 ppm target)
Can be attributed to negative Eh values
1 h buffering time is insufficient to yield a positive Eh.
CIL tail sample from a gold Plant was used.
Buffered to pH 7 with 14.6 kg/t H2SO4 for 4 hrs.
Aachen run 30 passes maximum.
Temperature, pH and Eh recorded at regular intervals and tabulated.
Pulp samples extracted at timed intervals and bottle rolled for 24 hours with increasing carbon concentration for each samples taken.
Example 4 was successful—reducing CN Wad from 827 ppm to 7.55 ppm, and reducing CN total from 944 ppm to 85.5 ppm.
Positive Eh values
Increased buffering time (1 h to 4 h) beneficial
50 g/L carbon concentration consistently gave <10 ppm WAD
Sample was Aachen tail from Example 4, agitated for 24 h with 50 g/l carbon
Screened out carbon
Buffered pH to 7 with 2.09 kg/t H2SO4
Aachen run 30 passes
Temperature, pH and Eh recorded at regular intervals
Example 5 was successful—reducing CN Wad from 3.72 ppm to 0.032 ppm, and reducing CN total from 27.3 ppm to 8.32 ppm.
Positive Eh values (more positive than Test 8)
WAD CN<1 ppm consistently achieved.
Shows that multistaging of the Aachening and carbon contact steps yields exceptionally low WAD values (<1 ppm)
Sample was tail from Example 5, agitated for 24 h with 50 g/l carbon
Screened out carbon
Buffered to pH 7 with 1.56 kg/t H2SO4
Aachen run for 30 passes
Temperature, pH and Eh recorded at regular intervals
Example 6 was successful—reducing CN Wad from 0.78 ppm to 0.040 ppm, and reducing CN total from 5.14 ppm to 1.75 ppm.
Positive Eh values (more positive than Example 5)
WAD CN<1 ppm consistently achieved.
Again shows that multistaging is extremely advantageous.
CIL tail sample from a gold Plant was used.
Buffered to pH 9 with 3.93 kg/t H2SO4 for 1 h
Added 0.53 kg/t CuSO4 after 1 pass
Added 1.0 kg CuSO4 after 11 passes
Added 2.0 kg/t CuSO4 after 21 passes
Aachen run 30 passes maximum
Temperature, pH and Eh recorded at regular intervals
Pulp samples extracted at timed intervals and bottle rolled for 24 hours with increasing carbon concentration for each sample taken
Negative Eh values
Example 7 only became successful after Eh increased from negative to zero.
Other essential conditions are pH 9 and 50 g/l carbon addition to the bottle roll.
Sample was CIL tail after Aachen run (10 passes) and 36 hours gold leach. Upfront pH was maintained in the range 9.5 to 10 utilising the Aachen to completely react the lime and render lithe to no protective alkalinity, in order to achieve pH decay residual value of 8 to 8.5 after gold leaching.
Samples were extracted at timed intervals (500 ml slurry) and bottle-rolled for 24 hours with increasing carbon concentration for the different samples. 0.5 kg/t cyanide was added for the leach.
pH and Eh was recorded at regular intervals (Eh remained positive).
Accompanying tables show Temperature, pH, and Eh readings from tests.
This test showed that the process of the present invention successfully brings WAD cyanide to well below 2 ppm.
This testwork incorporated Aachen pre-conditioning where the objective was to oxidise Fe2+ to Fe3+ and precipitate as a hydroxide (along with any other base metals that may be present viz Cu, Ni, Zn and Pb). These base metals would report as SAD and WAD complexes which would have to be dealt with at the tail end of the plant. Precipitating them out thus relieves the load on the detox at the tail end. The effectiveness of this methodology is bourne out by the low WADs feeding the process.
The purpose of the pre-conditioning step is to react more fully, any unreacted lime and so ensure that there is minimum protective alkalinity down the tankfarm. This, coupled with a pH range of between 9.5 and 10 in the pre-conditioning step, allows for a natural decay in the pH to between 8 and 8.5 in the tail. This natural decay of the pH and rise in the Eh would be further assisted by the running of a process of the invention on the tail end of the plant.
Although this particular test showed extremely low WADs, a multistage is still recommended at the tail end of a plant to give more flexibility with the parameters and a continued guarantee of success in the long term. In addition, the added benefit of having a safety net for gold leaching and adsorbtion is a further plus. Soluble losses can easily be reduced to zero and this financial benefit could pay for the costs of the process of the present invention.
Total cyanide was also reduced to below 10 ppm. No cyanate, nitrite or nitrate was detected.
For a plant application, following is recommended (assuming 11 Tanks):
5 Aachen passes for pre-oxidation on Tank1 (Stage 10 in the Drawing).
5 Aachen passes for an accelerated leach (with cyanide) on Tank 2 (Stage 14 in the Drawing).
5 CIL tanks (Stage 16 in the Drawing)
2.5 Aachen passes on Tank 8 (Stage 20A in the Drawing) without carbon.
50 g/l carbon concentration in Tank 9 (Stage 20B in the Drawing).
2.5 Aachen passes on Tank 10 with no carbon (Stage 22A in the Drawing)
50 g/l carbon concentration in Tank 11 (Stage 22B in the Drawing).
Carbon would be added into Tank 11; than pumped to Tank 9; then pumped to Tank 7, and then pumped up the train as per normal
Four Aachen™ Reactor test runs were performed on CIL tailings from a gold plant. Samples were taken from the plant in slurry form containing the residual cyanide and stored in dark containers between test runs.
The following procedure was adopted for the various test runs:
30 litres of sample was transferred “as received” into the Aachen™ recirculation tank
The Aachen™ was run for a total of 40 minutes
Samples were extracted at times 0, 10, 20, 30 and 40 minutes
CuSO4 was added, after the 30 minute sample was taken, to give 50 ppm Cu2+ in solution in the Aachen Recirculation Tank
Suitable aliquots of the samples taken were submitted for analysis in addition to 24 hour bottle rolls being performed
Two bottle rolls were performed at time 30:
One “as is”
One with CuSO4 added to give 50 ppm Cu2+ in solution in the bottle roll
Residue Run 2
30 litres of sample was transferred “as received” into the Aachen™ recirculation tank
CuSO4 was added, before starting up the Aachen, to give 100 ppm Cu2+ in solution
The Aachen™ The Aachen was run for a total of 40 minutes
Samples were extracted at times 0, 10, 20, 30 and 40 minutes
Suitable aliquots of the samples taken were submitted for analysis in addition to 24 hour bottle rolls being performed
30 litres of sample was transferred “as received” into the Aachen™ recirculation tank
CuSO4 and FeSO4 was added, before starting up the Aachen™, to give 100 ppm Cu2+ and Fe2+ in solution
The Aachen™ was run for a total of 40 minutes
Samples were extracted at times 0, 10, 20, 30 and 40 minutes
Suitable aliquots of the samples taken were submitted for analysis in addition to 24 hour bottle rolls being performed
30 litres of sample was ph corrected to 9 using 98% sulphuric acid before being transferred into the Aachen™ recirculation tank
CuSO4 and FeSO4 was added, after taking the 20 minute sample, to give 100 ppm Cu2+ and Fe2+ in solution
The Aachen™ was run for a total of 40 minutes
Samples were extracted at times 0, 10, 20, 30 and 40 minutes
Suitable aliquots of the samples taken were submitted for analysis in addition to 24 hour bottle rolls being performed.
The pH of the stream was adjusted to 9 prior to treatment.
The results of the tests are provided in Table 17 below. With flow rates used, in table, 1 min equals 1 pass through the reactor.
Table 3, above, shows the results obtained for the cyanide destruction test runs on the residue sample. On average, the cyanide destruction test runs yielded a bottle roll tail of 0.20 g/t, 0.15 g/t lower than the “as received” grade of 0.35 g/t.
Residue Run 1 (Aachen™ run for 40 minutes with 100 ppm copper, iron and zinc addition at the start, and Ph corrected to 9 at the start)
pH adjustment to 9 showed a fair reduction in both the free and WAD cyanide levels before the bottle rolls. This is seen by comparing the time 0 result on run 3, where the pH was not adjusted, to the time zero result of run 1, where the ph was adjusted.
WAD values remained largely unchanged before the bottle rolls and upheld the trend of carbon catalysis by showing low WAD values after the bottle rolls.
Residue Run 2 (Aachen™ run for 40 minutes with 100 ppm copper and zinc addition at the start, and Ph corrected to 9 at the start)
Again pH adjustment to 9 showed a fair reduction in both the free and WAD cyanide levels before the bottle rolls. This is seen by comparing the time 0 result on run 3, where the pH was not adjusted, to the time zero result of run 2, where the pH was adjusted.
WAD values remained largely unchanged before the bottle rolls and upheld the trend of carbon catalysis by showing low WAD values after the bottle rolls.
Residue Run 3 (Aachen™ run for 40 minutes with 50 ppm copper, zinc and iron addition at the start, no pH adjustment)
The lower concentration of metals added gave a slightly higher free cyanide value on samples taken from the Aachen recirculation tank before the bottle rolls. WAD values again dropped significantly after the bottle rolls.
This Example shows:
Ph adjustment to 9 significantly reduces both the free and the WAD cyanide values.
Copper addition reduces the free cyanide only leaving the WAD values unchanged.
The addition of iron and zinc had no significant impact on the free and WAD cyanide values.
The most outstanding trend was that of the carbon catalysis of the oxidation of both the free and WAD cyanide, after Aachen™ treatment.
The gold recoveries that can be obtained from CIL tailing by the process.
30 litres of water was first transferred into the Aachen Reactor recirculation tank. The flow rate through the system was measured by recording the time to fill a 5 litre beaker. This data was used to calculate the relationship between running time and the number of passes through an oxygenating device (in this case an Aachen™ Reactor available from Maelgwyn Mineral Services Ltd).
30 litres of thickener underflow sample was transferred into the Aachen™ Reactor recirculation tank.
Cyanide was added to the slurry to yield a free cyanide concentration of 300 ppm.
The Aachen™ Reactor was then run for a period of 35 minutes, at a back-pressure of 3 bar and an oxygen flow rate of 10 litre/minute.
Samples were taken at time 0, 5, 10, 20, 30 and 35 minutes and subjected to standard 24 h CIL bottle rolls with 10 g/l carbon. The sample at time 35 was further spiked with cyanide to give an additional 300 ppm of cyanide in the bottle roll. An aliquot of the samples taken was submitted for assay before the CIL bottle rolls in order to determine the extent of leaching within the Aachen™ Reactor.
pH, temperature and DO (dissolved oxygen) was recorded at regular intervals.
Table 18 presents the Au on solid assay results and recoveries for the thickener underflow sample Leach Aachen runs.
Table 18 above shows extremely fast leaching, with roughly 70% of the leach taking place within the first five minutes of running.
This example shows benefits that can be attained in the accelerated leach step of the present invention.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2007/09865 | Nov 2007 | ZA | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/IB2008/054806 | 11/17/2008 | WO | 00 | 8/17/2010 |
