Technology, Resource and Mining

[Diogenese]

Hi @Semmel ,

Further to today's recycling agreement announcement with Aurubis and our discussion on recycling, this is Talga's recycling patent application to be used in the process. It was published in January 2024.

WO2024003761A1 GRAPHITE MATERIAL PURIFICATION PROCESS 20220629

A graphite material purification process (10) comprising

a pelletisation step (14),

a caustic baking step (16) providing a sintered product,

a water leach step (18) whereby impurity minerals are solubilised, forwarded for effluent treatment, and separated,

a first sulphuric acid leach step (20) wherein remaining impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a hydrofluoric acid leach step (22) wherein partially leached impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a second sulphuric acid leach step (24) wherein impurity minerals not leached in previous steps and components precipitated in the hydrofluoric acid leach step (22) are solubilised, forwarded for effluent treatment, and separated from leach solids, and

washing stages wherein remaining soluble impurities are separated, and providing a purified graphite material (32).



[0055] The caustic baking step (ii) is undertaken at between about 150 and 300°C and causes the caustic soda and, in particular, silicate impurity minerals to react and be rendered soluble in water and mild acid conditions. The caustic baking step has a residence time in the range of about 60 to 240 minutes, for example about 120 minutes. The amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 moles caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon. The caustic baking step (ii) is undertaken, for example, in a rotating kiln.

[0056] The water leach step (iii) is undertaken at between about 5-60°C, for example about 35°C ±5°C. The water leach step (iii) is undertaken in a single leach step, although in certain circumstances it may be undertaken in multiple, for example three, counter-current leach stages. The water leach step (iii) has a retention time of between about 30 to 240 minutes.



[0057] The first sulphuric acid leach step (iv) is undertaken at between about 5 to 60°C, for example about 40°C ±5 °C with a retention time of between about 30 to 240 minutes, for example about 120 minutes. Concentrated sulphuric acid is added in the first sulphuric acid leach step (iv). Impurities leached in the sulphuric acid leach step (iv) preferably include residual amounts of sodium silicate, sodium alunite, iron oxide and iron hydroxide, and titanium mineral phases not removed in step (iii). Still preferably, the residual free acid at the end of the first sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. The first sulphuric acid leach step (iv) preferably operates with between 5 to 25% solids, for example 10% solids.

[0058] Impurities leached in the first sulphuric acid leach step (iv) include sodium silicate, sodium alunite, iron oxide and iron hydroxide mineral phases formed during the caustic baking step, together with any residual caustic.

[0059] It is envisaged that all, or a portion of, the product of the first sulphuric acid leach step (iv) may be recycled to step (i) in order to expose it to a second baking step (ii). It is understood that this may be advantageous in addressing titanium levels, as the baking step (ii) is the stage of the process of the present invention in which titanium minerals are ‘cracked’ (eg. titanite and rutile).

[0060] The hydrofluoric acid leach step (v) is undertaken at between about 5- 60°C, for example about 40°C ±5°C. Impurities leached in the hydrofluoric leach step (v) include but are not limited to quartz, titanium mineral phases, and residual amounts of albite, biotite, and pyrophyllite. The residual free acid at the end of the hydrofluoric acid leach step (v) is in the range of about 5-75 g/LHF, for example about 25 g/L ±5 g/L HF. The hydrofluoric acid leach step (v) operates with between 5 to 25% solids, for example 10% solids. [0061] The hydrofluoric acid added to the acid leach step (v) is in the range of about 20 to 70% concentration. The hydrofluoric acid concentration in the acid leach step (v) is preferably in the range of 15-50 g/L, depending on the grade and mineralogical composition of the starting graphite material. The leach solids from the hydrofluoric leach step (v) have substantially no, or only trace amounts of, silicon remaining therein.

[0062] The second sulphuric acid leach step (vi) is undertaken at between about 5-60°C, for example about 40°C ±5°C. Impurities leached in the second sulphuric acid leach step (vi) include precipitated fluoride phases, for example calcium fluoride, and remaining base metals. The second sulphuric acid leach step (vi) operates with between 5 to 25% solids, for example 10% solids. The second sulphuric acid leach step (iv) has a retention time of between about 30 to 240 minutes, for example about 120 minutes.

[0063] Concentrated sulphuric acid is added in the second sulphuric acid leach step (vi). The residual free acid at the end of the second sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. Acid solutions from the second sulphuric acid leach step (vi) are recovered and recycled to the first sulphuric acid leach step (iv) and the second sulphuric acid leach step (vi).

 

[cosors]

ASX Release ASX:TLG
10 September 2024
Talga and Aurubis sign battery anoder ecycling agreement

I would like to remind you that the Sustainability Act has recently come into force. All companies in the EU must comply with it. It was also stipulated that suppliers must endeavour to recycle.
So it is not a question of why Talga is doing this. The customers have to prove it. Talga is simply filling a gap that previously existed. Talga and the customers can demonstrate this in their report in order to fulfil the sustainability report.
@Dio: Thanks for the patent. It is quite informative.
Just my thoughts.

 

[brewm0re]

Hi @Semmel ,

Further to today's recycling agreement announcement with Aurubis and our discussion on recycling, this is Talga's recycling patent application to be used in the process. It was published in January 2024.

WO2024003761A1 GRAPHITE MATERIAL PURIFICATION PROCESS 20220629

A graphite material purification process (10) comprising

a pelletisation step (14),

a caustic baking step (16) providing a sintered product,

a water leach step (18) whereby impurity minerals are solubilised, forwarded for effluent treatment, and separated,

a first sulphuric acid leach step (20) wherein remaining impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a hydrofluoric acid leach step (22) wherein partially leached impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a second sulphuric acid leach step (24) wherein impurity minerals not leached in previous steps and components precipitated in the hydrofluoric acid leach step (22) are solubilised, forwarded for effluent treatment, and separated from leach solids, and

washing stages wherein remaining soluble impurities are separated, and providing a purified graphite material (32).



[0055] The caustic baking step (ii) is undertaken at between about 150 and 300°C and causes the caustic soda and, in particular, silicate impurity minerals to react and be rendered soluble in water and mild acid conditions. The caustic baking step has a residence time in the range of about 60 to 240 minutes, for example about 120 minutes. The amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 moles caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon. The caustic baking step (ii) is undertaken, for example, in a rotating kiln.

[0056] The water leach step (iii) is undertaken at between about 5-60°C, for example about 35°C ±5°C. The water leach step (iii) is undertaken in a single leach step, although in certain circumstances it may be undertaken in multiple, for example three, counter-current leach stages. The water leach step (iii) has a retention time of between about 30 to 240 minutes.



[0057] The first sulphuric acid leach step (iv) is undertaken at between about 5 to 60°C, for example about 40°C ±5 °C with a retention time of between about 30 to 240 minutes, for example about 120 minutes. Concentrated sulphuric acid is added in the first sulphuric acid leach step (iv). Impurities leached in the sulphuric acid leach step (iv) preferably include residual amounts of sodium silicate, sodium alunite, iron oxide and iron hydroxide, and titanium mineral phases not removed in step (iii). Still preferably, the residual free acid at the end of the first sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. The first sulphuric acid leach step (iv) preferably operates with between 5 to 25% solids, for example 10% solids.

[0058] Impurities leached in the first sulphuric acid leach step (iv) include sodium silicate, sodium alunite, iron oxide and iron hydroxide mineral phases formed during the caustic baking step, together with any residual caustic.

[0059] It is envisaged that all, or a portion of, the product of the first sulphuric acid leach step (iv) may be recycled to step (i) in order to expose it to a second baking step (ii). It is understood that this may be advantageous in addressing titanium levels, as the baking step (ii) is the stage of the process of the present invention in which titanium minerals are ‘cracked’ (eg. titanite and rutile).

[0060] The hydrofluoric acid leach step (v) is undertaken at between about 5- 60°C, for example about 40°C ±5°C. Impurities leached in the hydrofluoric leach step (v) include but are not limited to quartz, titanium mineral phases, and residual amounts of albite, biotite, and pyrophyllite. The residual free acid at the end of the hydrofluoric acid leach step (v) is in the range of about 5-75 g/LHF, for example about 25 g/L ±5 g/L HF. The hydrofluoric acid leach step (v) operates with between 5 to 25% solids, for example 10% solids. [0061] The hydrofluoric acid added to the acid leach step (v) is in the range of about 20 to 70% concentration. The hydrofluoric acid concentration in the acid leach step (v) is preferably in the range of 15-50 g/L, depending on the grade and mineralogical composition of the starting graphite material. The leach solids from the hydrofluoric leach step (v) have substantially no, or only trace amounts of, silicon remaining therein.

[0062] The second sulphuric acid leach step (vi) is undertaken at between about 5-60°C, for example about 40°C ±5°C. Impurities leached in the second sulphuric acid leach step (vi) include precipitated fluoride phases, for example calcium fluoride, and remaining base metals. The second sulphuric acid leach step (vi) operates with between 5 to 25% solids, for example 10% solids. The second sulphuric acid leach step (iv) has a retention time of between about 30 to 240 minutes, for example about 120 minutes.

[0063] Concentrated sulphuric acid is added in the second sulphuric acid leach step (vi). The residual free acid at the end of the second sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. Acid solutions from the second sulphuric acid leach step (vi) are recovered and recycled to the first sulphuric acid leach step (iv) and the second sulphuric acid leach step (vi).

View attachment 69095

Thanks Dio. Great find. Reinforces this isn’t a company simply digging up some mineral from the ground. Slowly but surely TLG are getting its claws in many areas with a range of companies.

 

[cosors]

Hi @Semmel ,

Further to today's recycling agreement announcement with Aurubis and our discussion on recycling, this is Talga's recycling patent application to be used in the process. It was published in January 2024.

WO2024003761A1 GRAPHITE MATERIAL PURIFICATION PROCESS 20220629

A graphite material purification process (10) comprising

a pelletisation step (14),

a caustic baking step (16) providing a sintered product,

a water leach step (18) whereby impurity minerals are solubilised, forwarded for effluent treatment, and separated,

a first sulphuric acid leach step (20) wherein remaining impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a hydrofluoric acid leach step (22) wherein partially leached impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a second sulphuric acid leach step (24) wherein impurity minerals not leached in previous steps and components precipitated in the hydrofluoric acid leach step (22) are solubilised, forwarded for effluent treatment, and separated from leach solids, and

washing stages wherein remaining soluble impurities are separated, and providing a purified graphite material (32).



[0055] The caustic baking step (ii) is undertaken at between about 150 and 300°C and causes the caustic soda and, in particular, silicate impurity minerals to react and be rendered soluble in water and mild acid conditions. The caustic baking step has a residence time in the range of about 60 to 240 minutes, for example about 120 minutes. The amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 moles caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon. The caustic baking step (ii) is undertaken, for example, in a rotating kiln.

[0056] The water leach step (iii) is undertaken at between about 5-60°C, for example about 35°C ±5°C. The water leach step (iii) is undertaken in a single leach step, although in certain circumstances it may be undertaken in multiple, for example three, counter-current leach stages. The water leach step (iii) has a retention time of between about 30 to 240 minutes.



[0057] The first sulphuric acid leach step (iv) is undertaken at between about 5 to 60°C, for example about 40°C ±5 °C with a retention time of between about 30 to 240 minutes, for example about 120 minutes. Concentrated sulphuric acid is added in the first sulphuric acid leach step (iv). Impurities leached in the sulphuric acid leach step (iv) preferably include residual amounts of sodium silicate, sodium alunite, iron oxide and iron hydroxide, and titanium mineral phases not removed in step (iii). Still preferably, the residual free acid at the end of the first sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. The first sulphuric acid leach step (iv) preferably operates with between 5 to 25% solids, for example 10% solids.

[0058] Impurities leached in the first sulphuric acid leach step (iv) include sodium silicate, sodium alunite, iron oxide and iron hydroxide mineral phases formed during the caustic baking step, together with any residual caustic.

[0059] It is envisaged that all, or a portion of, the product of the first sulphuric acid leach step (iv) may be recycled to step (i) in order to expose it to a second baking step (ii). It is understood that this may be advantageous in addressing titanium levels, as the baking step (ii) is the stage of the process of the present invention in which titanium minerals are ‘cracked’ (eg. titanite and rutile).

[0060] The hydrofluoric acid leach step (v) is undertaken at between about 5- 60°C, for example about 40°C ±5°C. Impurities leached in the hydrofluoric leach step (v) include but are not limited to quartz, titanium mineral phases, and residual amounts of albite, biotite, and pyrophyllite. The residual free acid at the end of the hydrofluoric acid leach step (v) is in the range of about 5-75 g/LHF, for example about 25 g/L ±5 g/L HF. The hydrofluoric acid leach step (v) operates with between 5 to 25% solids, for example 10% solids. [0061] The hydrofluoric acid added to the acid leach step (v) is in the range of about 20 to 70% concentration. The hydrofluoric acid concentration in the acid leach step (v) is preferably in the range of 15-50 g/L, depending on the grade and mineralogical composition of the starting graphite material. The leach solids from the hydrofluoric leach step (v) have substantially no, or only trace amounts of, silicon remaining therein.

[0062] The second sulphuric acid leach step (vi) is undertaken at between about 5-60°C, for example about 40°C ±5°C. Impurities leached in the second sulphuric acid leach step (vi) include precipitated fluoride phases, for example calcium fluoride, and remaining base metals. The second sulphuric acid leach step (vi) operates with between 5 to 25% solids, for example 10% solids. The second sulphuric acid leach step (iv) has a retention time of between about 30 to 240 minutes, for example about 120 minutes.

[0063] Concentrated sulphuric acid is added in the second sulphuric acid leach step (vi). The residual free acid at the end of the second sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. Acid solutions from the second sulphuric acid leach step (vi) are recovered and recycled to the first sulphuric acid leach step (iv) and the second sulphuric acid leach step (vi).

View attachment 69095

The amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 moles caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon. The caustic baking step (ii) is undertaken, for example, in a rotating kiln.

The ann roday mentions Talnode-C and in the patent I read silicon. Does this have anything to do with the process or the end product? Unfortunately, I don't understand enough about it.

 

[Diogenese]

The amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 moles caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon. The caustic baking step (ii) is undertaken, for example, in a rotating kiln.

The ann roday mentions Talnode-C and in the patent I read silicon. Does this have anything to do with the process or the end product? Unfortunately, I don't understand enough about it.

The patent is to recover graphite. The silicon (silicate material) is an impurity which the process removes. Thus I assume it can be used to recycle Talnode-Si.


[0019] The caustic baking step (ii) is preferably undertaken at between about 150 and 300°C and causes the caustic soda and, in particular, silicate impurity minerals to react and be rendered soluble in water and mild acid conditions.

[0020] Preferably, the caustic baking step has a residence time in the range of about 60 to 240 minutes, preferably about 120 minutes.

[0021] Still preferably, the amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 mol caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon.

 

[mpk1980]

I remember MT talking about a programme called RELOAD where he said they were looking to use by-products from recycling to create the silicon needed for Talnode-Si? I recall silicon was being sourced externally but this approach made the process efficient.

Does anyone remember this?

 

[Semmel]

Hi @Semmel ,

Further to today's recycling agreement announcement with Aurubis and our discussion on recycling, this is Talga's recycling patent application to be used in the process. It was published in January 2024.

WO2024003761A1 GRAPHITE MATERIAL PURIFICATION PROCESS 20220629

A graphite material purification process (10) comprising

a pelletisation step (14),

a caustic baking step (16) providing a sintered product,

a water leach step (18) whereby impurity minerals are solubilised, forwarded for effluent treatment, and separated,

a first sulphuric acid leach step (20) wherein remaining impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a hydrofluoric acid leach step (22) wherein partially leached impurity minerals are solubilised, forwarded for effluent treatment, and separated from leach solids,

a second sulphuric acid leach step (24) wherein impurity minerals not leached in previous steps and components precipitated in the hydrofluoric acid leach step (22) are solubilised, forwarded for effluent treatment, and separated from leach solids, and

washing stages wherein remaining soluble impurities are separated, and providing a purified graphite material (32).



[0055] The caustic baking step (ii) is undertaken at between about 150 and 300°C and causes the caustic soda and, in particular, silicate impurity minerals to react and be rendered soluble in water and mild acid conditions. The caustic baking step has a residence time in the range of about 60 to 240 minutes, for example about 120 minutes. The amount of caustic soda added to the graphite material to be purified is calculated using the ratio of at least 1 mol caustic to 1 mol silicon, for example between 2.5 to 5.5 moles caustic to silicon, particularly 3.2 mol caustic : 1 mol silicon. The caustic baking step (ii) is undertaken, for example, in a rotating kiln.

[0056] The water leach step (iii) is undertaken at between about 5-60°C, for example about 35°C ±5°C. The water leach step (iii) is undertaken in a single leach step, although in certain circumstances it may be undertaken in multiple, for example three, counter-current leach stages. The water leach step (iii) has a retention time of between about 30 to 240 minutes.



[0057] The first sulphuric acid leach step (iv) is undertaken at between about 5 to 60°C, for example about 40°C ±5 °C with a retention time of between about 30 to 240 minutes, for example about 120 minutes. Concentrated sulphuric acid is added in the first sulphuric acid leach step (iv). Impurities leached in the sulphuric acid leach step (iv) preferably include residual amounts of sodium silicate, sodium alunite, iron oxide and iron hydroxide, and titanium mineral phases not removed in step (iii). Still preferably, the residual free acid at the end of the first sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. The first sulphuric acid leach step (iv) preferably operates with between 5 to 25% solids, for example 10% solids.

[0058] Impurities leached in the first sulphuric acid leach step (iv) include sodium silicate, sodium alunite, iron oxide and iron hydroxide mineral phases formed during the caustic baking step, together with any residual caustic.

[0059] It is envisaged that all, or a portion of, the product of the first sulphuric acid leach step (iv) may be recycled to step (i) in order to expose it to a second baking step (ii). It is understood that this may be advantageous in addressing titanium levels, as the baking step (ii) is the stage of the process of the present invention in which titanium minerals are ‘cracked’ (eg. titanite and rutile).

[0060] The hydrofluoric acid leach step (v) is undertaken at between about 5- 60°C, for example about 40°C ±5°C. Impurities leached in the hydrofluoric leach step (v) include but are not limited to quartz, titanium mineral phases, and residual amounts of albite, biotite, and pyrophyllite. The residual free acid at the end of the hydrofluoric acid leach step (v) is in the range of about 5-75 g/LHF, for example about 25 g/L ±5 g/L HF. The hydrofluoric acid leach step (v) operates with between 5 to 25% solids, for example 10% solids. [0061] The hydrofluoric acid added to the acid leach step (v) is in the range of about 20 to 70% concentration. The hydrofluoric acid concentration in the acid leach step (v) is preferably in the range of 15-50 g/L, depending on the grade and mineralogical composition of the starting graphite material. The leach solids from the hydrofluoric leach step (v) have substantially no, or only trace amounts of, silicon remaining therein.

[0062] The second sulphuric acid leach step (vi) is undertaken at between about 5-60°C, for example about 40°C ±5°C. Impurities leached in the second sulphuric acid leach step (vi) include precipitated fluoride phases, for example calcium fluoride, and remaining base metals. The second sulphuric acid leach step (vi) operates with between 5 to 25% solids, for example 10% solids. The second sulphuric acid leach step (iv) has a retention time of between about 30 to 240 minutes, for example about 120 minutes.

[0063] Concentrated sulphuric acid is added in the second sulphuric acid leach step (vi). The residual free acid at the end of the second sulphuric leach step (iv) is in the range of 5-75 g/L H2SO4, for example about 50 g/L ±5 g/L H2SO4. Acid solutions from the second sulphuric acid leach step (vi) are recovered and recycled to the first sulphuric acid leach step (iv) and the second sulphuric acid leach step (vi).

View attachment 69095

Hi @Diogenese , thx for digging this patent up!

the moste interesting part here is the end product. Talhite-C. Meaning, the precursor to Talnode-C, Talnode-Si (the carbon part) and Talphene. It appears that the technology that Talga uses does not require a filtering and/or sifting of the particles. This means hey have a way to manufacture Talnode-C, i.e. spheriodization and coating, with smaller particles than everyone else. I guess we all remember the meta-particles of Talnode-Si. This indicates to me, that Talnode-C is also comprised as meta-particles. Meaning, the source material Talphite-C consists of smaller particles that are then baked or clumped up to larger um-sized cupcakes.

So from Talgas point of view, chemical cleaning is all they need for recycling, whereas everyone else cant do that because they dont have meta-particles formed from the source material. That might be the unique property that makes Talnode-C stand out and also maybe the reason it had so extensive testing. If this is correct (and please post a rebuttal if you find one!) then Talga has a significant technological advantage over everyone else in the industry.

This makes a very excited Semmel.

 

[WheresTheMonkey]

I successfully turned on his internet camera and here is @Semmel looking very excited

 

[Semmel]

I successfully turned on his internet camera and here is @Semmel looking very excited

Must be an old me, my glasses are way nerdier than these!

 

[Diogenese]

Hi @Diogenese , thx for digging this patent up!

the moste interesting part here is the end product. Talhite-C. Meaning, the precursor to Talnode-C, Talnode-Si (the carbon part) and Talphene. It appears that the technology that Talga uses does not require a filtering and/or sifting of the particles. This means hey have a way to manufacture Talnode-C, i.e. spheriodization and coating, with smaller particles than everyone else. I guess we all remember the meta-particles of Talnode-Si. This indicates to me, that Talnode-C is also comprised as meta-particles. Meaning, the source material Talphite-C consists of smaller particles that are then baked or clumped up to larger um-sized cupcakes.

So from Talgas point of view, chemical cleaning is all they need for recycling, whereas everyone else cant do that because they dont have meta-particles formed from the source material. That might be the unique property that makes Talnode-C stand out and also maybe the reason it had so extensive testing. If this is correct (and please post a rebuttal if you find one!) then Talga has a significant technological advantage over everyone else in the industry.

This makes a very excited Semmel.

We're singing from the same hymn sheet - it's just that I've got the back side.

 

[anbuck]

Hi @Diogenese , thx for digging this patent up!

the moste interesting part here is the end product. Talhite-C. Meaning, the precursor to Talnode-C, Talnode-Si (the carbon part) and Talphene. It appears that the technology that Talga uses does not require a filtering and/or sifting of the particles. This means hey have a way to manufacture Talnode-C, i.e. spheriodization and coating, with smaller particles than everyone else. I guess we all remember the meta-particles of Talnode-Si. This indicates to me, that Talnode-C is also comprised as meta-particles. Meaning, the source material Talphite-C consists of smaller particles that are then baked or clumped up to larger um-sized cupcakes.

So from Talgas point of view, chemical cleaning is all they need for recycling, whereas everyone else cant do that because they dont have meta-particles formed from the source material. That might be the unique property that makes Talnode-C stand out and also maybe the reason it had so extensive testing. If this is correct (and please post a rebuttal if you find one!) then Talga has a significant technological advantage over everyone else in the industry.

This makes a very excited Semmel.

Isn't one of the benefits of Talga's mines that they have particles of optimal size for batteries though? If Tagla is able to use smaller particles, then that seems to undermine that claimed advantage. Have they said that the recycled graphite would be used for batteries? I'm wondering if they're instead planning for it to be used for other applications where smaller particle sizes are desirable.

 

[Diogenese]

Isn't one of the benefits of Talga's mines that they have particles of optimal size for batteries though? If Tagla is able to use smaller particles, then that seems to undermine that claimed advantage. Have they said that the recycled graphite would be used for batteries? I'm wondering if they're instead planning for it to be used for other applications where smaller particle sizes are desirable.

[0079] The process further comprises a drying step 30 in which the purified graphite material 28 of step (vii) is dried, providing a dried purified graphite material 32 (here also referenced as Talphite-CTM ). It is intended that whilst the purified graphite material 28 of step (vii) will contain about 40% moisture prior to the drying step, the dried purified graphite material contains between 0 to 2.5% moisture, for example less than about 0.1% moisture. The purified graphite material 28 of step (vii) has a pH of 7 ± 2.5 when repulped in water, whereby the purified graphite material is suitable for use directly in calendaring of electrodes (not shown).

[0080] The purified graphite material 28 of step (vii) is classified in the drying step 30, into at least two fractions, for example using cyclone classification. The two fractions would typically include fine and coarse fractions.

[0081] The graphite material concentrate 12 has a moisture content of up to about 26 to 28 %w/w. This concentrate 12 is first passed to a concentrate drying step 34, for example a flash drying stage or rotary drum drier. Whilst a proportion of the material 12 exits in flue gas it is recovered and reintroduced to the dried concentrate that is passed to the pelletisation step 14.

[0082] The pelletisation step 14 comprises the addition, in stepwise fashion, of caustic soda, in the form of caustic prill, and water to the graphite material to be purified. The pellets produced in the pelletisation step 14 are micro-pellets of about 2-10 mm in diameter, for example 5mm ± 2mm.

[0083] Dry fines of the purified graphite material are added during the pelletisation step 14, for example dry fines in the order of about 50 kg/t are added. The dry fines of the purified graphite material are sourced from the drying step 30. The pellets produced in the pelletisation step 14 have a moisture content of about 13 to 24%w/w, for example about 20%w/w.

 

[Semmel]

[0079] The process further comprises a drying step 30 in which the purified graphite material 28 of step (vii) is dried, providing a dried purified graphite material 32 (here also referenced as Talphite-CTM ). It is intended that whilst the purified graphite material 28 of step (vii) will contain about 40% moisture prior to the drying step, the dried purified graphite material contains between 0 to 2.5% moisture, for example less than about 0.1% moisture. The purified graphite material 28 of step (vii) has a pH of 7 ± 2.5 when repulped in water, whereby the purified graphite material is suitable for use directly in calendaring of electrodes (not shown).

[0080] The purified graphite material 28 of step (vii) is classified in the drying step 30, into at least two fractions, for example using cyclone classification. The two fractions would typically include fine and coarse fractions.

[0081] The graphite material concentrate 12 has a moisture content of up to about 26 to 28 %w/w. This concentrate 12 is first passed to a concentrate drying step 34, for example a flash drying stage or rotary drum drier. Whilst a proportion of the material 12 exits in flue gas it is recovered and reintroduced to the dried concentrate that is passed to the pelletisation step 14.

[0082] The pelletisation step 14 comprises the addition, in stepwise fashion, of caustic soda, in the form of caustic prill, and water to the graphite material to be purified. The pellets produced in the pelletisation step 14 are micro-pellets of about 2-10 mm in diameter, for example 5mm ± 2mm.

[0083] Dry fines of the purified graphite material are added during the pelletisation step 14, for example dry fines in the order of about 50 kg/t are added. The dry fines of the purified graphite material are sourced from the drying step 30. The pellets produced in the pelletisation step 14 have a moisture content of about 13 to 24%w/w, for example about 20%w/w.

The pelletisation is just for transport, so hat dust generation and environmental contamination is minimized. The pellets are broken down into dust again at the factory.