CA1330627C - Process for the extraction of valuable metals - Google Patents
Process for the extraction of valuable metalsInfo
- Publication number
- CA1330627C CA1330627C CA000574696A CA574696A CA1330627C CA 1330627 C CA1330627 C CA 1330627C CA 000574696 A CA000574696 A CA 000574696A CA 574696 A CA574696 A CA 574696A CA 1330627 C CA1330627 C CA 1330627C
- Authority
- CA
- Canada
- Prior art keywords
- pipeline
- slurry
- leaching
- valuable metal
- region
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/02—Apparatus therefor
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
Abstract
Abstract:
To remove valuable metal from ore, slime, tailings or the like, the matter is caused to pass in the form of a slurry along a pipeline, one or more reagents are supplied to the pipeline so that leaching takes place in the pipeline and the valuable metal is recovered at a recovery plant downstream of the pipeline.
To remove valuable metal from ore, slime, tailings or the like, the matter is caused to pass in the form of a slurry along a pipeline, one or more reagents are supplied to the pipeline so that leaching takes place in the pipeline and the valuable metal is recovered at a recovery plant downstream of the pipeline.
Description
- 133~7 PROCESS FOR THE EXTRACTION OF VALUABLE METALS
This invention relates to the recovery of one or more valuable metals, such as gold, copper, nickel, molybdenum and manganese, from matter contalning such metals. Such matter may be in the form of ores or glacial deposits or in the form of tailings, slimes, calcined ores, or other discarded materials which have already-been processed ln so~e way, but which it is.now economically viable to re-process.
It is commonplace for freshly mlned ores, and materials from mine dumps which are to be further treated, to be transported for comparatively large distances, such as several miles, to a processing plant. The ore of dump material is usually most conveniently transported as a slurry through suitable pipelines. When the slurry reaches the processing plant it is subJected to leaching and subsequent extraction in specially designed apparatus. The overall cost of providing pipelines ls high, especially as it is often necessary to carry out at least the leaching process at elevated temperatures.
According to this invention, in a process for recovering valuable metal from matter containing such metal in which the matter is caused to pass in the form of a slurry through a pipeline, one or more reagents are supplied to the pipellne so that leaching conditions prevail in at least part of the pipeline and ;~ .
. . ., .. ,,.
; . -: . . . ~ . :
.. - ~
. - ~ .. ... .
This invention relates to the recovery of one or more valuable metals, such as gold, copper, nickel, molybdenum and manganese, from matter contalning such metals. Such matter may be in the form of ores or glacial deposits or in the form of tailings, slimes, calcined ores, or other discarded materials which have already-been processed ln so~e way, but which it is.now economically viable to re-process.
It is commonplace for freshly mlned ores, and materials from mine dumps which are to be further treated, to be transported for comparatively large distances, such as several miles, to a processing plant. The ore of dump material is usually most conveniently transported as a slurry through suitable pipelines. When the slurry reaches the processing plant it is subJected to leaching and subsequent extraction in specially designed apparatus. The overall cost of providing pipelines ls high, especially as it is often necessary to carry out at least the leaching process at elevated temperatures.
According to this invention, in a process for recovering valuable metal from matter containing such metal in which the matter is caused to pass in the form of a slurry through a pipeline, one or more reagents are supplied to the pipellne so that leaching conditions prevail in at least part of the pipeline and ;~ .
. . ., .. ,,.
; . -: . . . ~ . :
.. - ~
. - ~ .. ... .
2 1~3a~7 the desired valuable metal is recovered at a recovery plant downstream of the pipellne.
Preferably, the matter ls caused to pass through the pipeline by in~ection of steam and/or heated compressed alr or other gases into the plpeline, a method whlch provldes both motlvatlng force and heat without the presence of moving parts, as ln conventional pumps. However, especially when heat is not required for leaching~ conventional pumping means may be used. ~n the case of alr, the addltlonal advantage is gained of a source of oxygen for oxidation where leaching condltions are advantaged;
alternatively, even stronger oxidlslng gases can be used where needed, e.g. chlorine. Similarly, a motive force of a neutral or reducing gas, e.g. H2S can be used.
The material should be reduced to a suitable particle size to allow lts transport through a pipeline in slurry form, for example to a particle size of less than 350 u, more preferably less than 180 u. The liquid used to slurry the material being processed is preferably a non-corrosive component of the leaching reagent, such as water or brine. More corrosive or environmetally ob~ectional components of the leaching reagent, such as dilute n~tric acid mixed with sulphuric acid, or cyanide, are then added further down the pipeline so that as much as posslble of the plpellne is sub~ected only to non-corroslve fluids.
,...
,~ , ~,~
~ . . .
.. ., ~
1 3 ~ 7 Envlronmentally ob~ectionable material, such as cyanide, is in~ected in totally enclosed conditions.
The steam and/or compressed air may be in~ected at the upstream end of the pipeline and/or at one or more inJection points along the length of the pipeline. If desired, a separation stage can be provided adjacent the upstream end of the pipeline for removing soluble metal values, while allowing the remainder of the slurry to pass along the pipeline for leaching.
While the use of any conventional leaching agent within the pipeline is contemplated, such as cyanide or thiourea, preferred leaching agents comprise a source of halide ions and an oxidising agent, such as nitric acid up to 35% with salt solutlon of 10% NaCl.
Any suitable method may be used to recover the desired valuable metals from the leach liquor.
According to a further aspect of the invention, extraction of the valuable metal from the leach liquor may also be carried out in the pipeline simultaneously with, or downstream of, the leaching.
Further pre~erred features of the invention will now be described with reference to the accompanying flow diagram.
The diagram shows a slurry head 2 feeding slurry to a pipeline 4 which transports slurry to a processing plant 6. The slurry head 2 is conveniently, although not necessarily, ad~acent a mine supplying ore ; .
- , ~ :
1 3 ~ 7 from which valuable metals are to be extracted, or near a dump containing previously processed tailings, slimes, partially calcined ores, etc., which are worth processing further, The material to be processed, if necessary, is ground, for example by ball milling, to a sufficiently small particle size to allow its transport as a slurry. This particle size will depend on the nature of the material being processed and the size of the pipeline used for transportation. In general, to prevent settling of the slurry in the pipeline, it is desirable to have a particle size less than 350 u, more preferably less than 170 to 180 u. If desired sand, or other suitable material may be introduced to the pipeline with the material to be processed so that attrition occurs as a result of turbulence within the pipeline to give a material of fine particle size which can be more readily leached. Examples of materials which can be advantageously treated in this way are calcined ores.
~9 Care must be ta~en that a material for attrition, such as coarse sand, does not adversely affect the materials present in the pipeline, such as an absorbent (e.g. carbon) for the leached products.
While attrition may occur throughout the pipeline, it may be more convenient to provide a special section for attrition, such as coarse sand or hard sintered ceramic pellets. The section may be suitably llned to resist wear and may have a reduced diameter to increase : ~t . ,.. ~
~ ~`
"`, ~i . ., ' l33a~27 turbulence.
The ground material is slurried with a non-corrosive component of the leach liquor, such as brine.
Quantitles of liquld are ad~usted to give a suitable speed and volume of flow through the pipeline. The usual solids content of flowable slurries is in the range of 40 to 60 per cent by weight but higher and lower pulp densities are possible.
~he slurry enters pipeline 4 and is transported along the pipeline by the motive force provided by in~ection of steam and/or hot air from in~ection point 8. While in~ection point 8 is shown at the upstream end of the pipeline, it may be positioned downstream of the slurry head 2 and one or more additional in~ection points 10 may be provided along the pipeline.
The pipeline 4 is of any suitable material to withstand the materials passing through, for example synthetic materials, such as polyvinyl chloride (which can withstand considerable pressure within the pipe~
or mètal tubes lined with synthetic materials.
Different sections of the pipeline may be made of different materials. Thus, the initial section, in contact only with a brine slurry, may be o~ cheap material, such as asbestos cement. The pipeline may be of any desired length, for example up to several miles, or comparatively short. If the slurry head and processing plant are close together, the pipeline may ~ ` - ' '1 ;- I
6 ~3~27 be labyrinthine or splralled to give a longer resldence time, The pipeline may vary ~n diameter, for example from 4 to 12 inches. It may be buried under~round to conserve heat. If necessary, for the leaching process, additional heat may be supplied at one or more selected places, for example by electrical heating or steam ~acket.
The steam and/or hot air, for example supplied from a pressure in~ector with a venturi at a pressure of 8 to 10 atmospheres, provides motive force for transporting the slurry along the pipeline, also heats the slurry to give the correct temperature for leaching and additionally helps to maintain sufficient agitation wlthin the pipeline to promote the leaching.
A suitable minimum speed of slurry is of the order of 4 to S ft./sec. and a suitable overall throughflow is of the order of 25 tons per hour, although higher values are, of course, possible.
As the brine slurry passes through the first portion of pipeline 4, some soluble metal salts containing the desired metal will be extracted into the brine. In order to recover these soluble metal-containing materials, a separatlng tank 12 is positioned, for example, about 200 yards along the pipeline and the soluble extract withdrawn for recovery of the deslred metals while the slurry itself continues to flow along the pipeline, optionally with further addition of brine.
.: :~
, - ''''''- ~ ~ - , !.~
.`~ ' .
1~3~7 At one or more convenient points 14, so as to allow sufficlent residence time for leaching ln the pipeline, for example from half to one hour, the remaining component or components of the leachlng reagent are added. Suitable leaching components are oxidising agents, such as a mixture of dllute nitric and sulphuric acids. Of course, other leaching agents, such as sodium cyanide in an alkaline medium, can be employed and liquids other than brine can be used to slurry the feedstock material, such as halides or a hypohalite (for example sodium hypochlorite). A
mixture of leaching agents may be used, concurrently or consecutively, such as the use of sodium hypochlorlte followed by the use of an acid leaching agent. It may be possible to leach certain materials, such as calclned ores, under relatively mild conditions, for example using only hot brine to release up to two thirds of the gold values present in a starting material.
The processing plant 6 at the downstream end of the pipeline can contain any suitable apparatus for extracting and recovering the desired metals from the leach liquor. Thus, for example, the leach liquor and pulp may be introduced to a separating vessel 16 and the leached unwanted pulp withdrawn on line 18 while the separated liquor passses to one of two absorpt$on vessels 20 ~illed with an absorbent for the desired metals, such as cellulose chaff, activated carbon or ' `? , ' : .` . ` : : , :
,,.. . : ` ` ~ :
1~3~
diatomaceous earth, The metals are then recovered from the absorbent in recovery unit 22. Two vessels 20 are provlded so that one can be stripped while the other is being loaded.
If the metal being recovered is suitable it is possible for not only the leaching but also the extraction to take place within the pipeline 4. Thus, for example, an absorbent with an active surface, such as cellulose chaff, activated carbon or diatomaceous earth, or specially formuiated resins, may be introduced at one or more points to the pipellne before or after the introduction of leaching agent, such as acid, at 14. The absorbent, belng lighter than the slurry, wlll tend to lie above the slurry, but the sufficlent agitatlon ln the pipeline will cause mixing to enable the desired leached metal values to be extracted by the absorbent. The absorbent carrying the desired metal can be separated at the end of the pipeline from the unwanted pulp by a screen or other suitable means.
A further example lies in the recovery of gold, where a speclfic extractant for gold, such as Rhodamine B, can be introduced at one or more points along the pipellne wlth, for example, a further extraction stage introduced where the Rhodamine B
carrying the gold values is taken up by a suitable solvent, such as methyl isobutyl ketone or diisobutyl ketone. Alternatively, the solvent may also be added to .. . .
t,,~, ~
, ..~
.. .
,, $ ;~J 7 -the pipeline, suitably in a widened section to accommodate the additlonal flow volume.
It will be appreciated that the process described above has several advantages. Thus, the pipeline between the supply of ore and the processing plant is being used for the dual purpose of transport and as a leaching vessel and, possibly, as an extraction vessel also. This reduces the cost of equipment. The use of steam and/or hot air provides both motive power for the slurry and heat to promote the leaching reaction but does not interfere with the reaction or cause corrosion. The use of steam is particularly valuable when used for the processing of difficult ores, such as sulphidic ores.
The leaching reagents suggested above minimise corrosion problems, especlally when a non-corosive agent, such as brine, is used to slurry the feedstock material and the oxidising agent, such as dilute nitric acid, added later in the pipeline.
As a pipeline may readily be buried underground, expensive insulation costs can be avoided.
~ . .
~,;..... p. :
.,~
~....... - . . . . ~ ~
F' `. ~
Preferably, the matter ls caused to pass through the pipeline by in~ection of steam and/or heated compressed alr or other gases into the plpeline, a method whlch provldes both motlvatlng force and heat without the presence of moving parts, as ln conventional pumps. However, especially when heat is not required for leaching~ conventional pumping means may be used. ~n the case of alr, the addltlonal advantage is gained of a source of oxygen for oxidation where leaching condltions are advantaged;
alternatively, even stronger oxidlslng gases can be used where needed, e.g. chlorine. Similarly, a motive force of a neutral or reducing gas, e.g. H2S can be used.
The material should be reduced to a suitable particle size to allow lts transport through a pipeline in slurry form, for example to a particle size of less than 350 u, more preferably less than 180 u. The liquid used to slurry the material being processed is preferably a non-corrosive component of the leaching reagent, such as water or brine. More corrosive or environmetally ob~ectional components of the leaching reagent, such as dilute n~tric acid mixed with sulphuric acid, or cyanide, are then added further down the pipeline so that as much as posslble of the plpellne is sub~ected only to non-corroslve fluids.
,...
,~ , ~,~
~ . . .
.. ., ~
1 3 ~ 7 Envlronmentally ob~ectionable material, such as cyanide, is in~ected in totally enclosed conditions.
The steam and/or compressed air may be in~ected at the upstream end of the pipeline and/or at one or more inJection points along the length of the pipeline. If desired, a separation stage can be provided adjacent the upstream end of the pipeline for removing soluble metal values, while allowing the remainder of the slurry to pass along the pipeline for leaching.
While the use of any conventional leaching agent within the pipeline is contemplated, such as cyanide or thiourea, preferred leaching agents comprise a source of halide ions and an oxidising agent, such as nitric acid up to 35% with salt solutlon of 10% NaCl.
Any suitable method may be used to recover the desired valuable metals from the leach liquor.
According to a further aspect of the invention, extraction of the valuable metal from the leach liquor may also be carried out in the pipeline simultaneously with, or downstream of, the leaching.
Further pre~erred features of the invention will now be described with reference to the accompanying flow diagram.
The diagram shows a slurry head 2 feeding slurry to a pipeline 4 which transports slurry to a processing plant 6. The slurry head 2 is conveniently, although not necessarily, ad~acent a mine supplying ore ; .
- , ~ :
1 3 ~ 7 from which valuable metals are to be extracted, or near a dump containing previously processed tailings, slimes, partially calcined ores, etc., which are worth processing further, The material to be processed, if necessary, is ground, for example by ball milling, to a sufficiently small particle size to allow its transport as a slurry. This particle size will depend on the nature of the material being processed and the size of the pipeline used for transportation. In general, to prevent settling of the slurry in the pipeline, it is desirable to have a particle size less than 350 u, more preferably less than 170 to 180 u. If desired sand, or other suitable material may be introduced to the pipeline with the material to be processed so that attrition occurs as a result of turbulence within the pipeline to give a material of fine particle size which can be more readily leached. Examples of materials which can be advantageously treated in this way are calcined ores.
~9 Care must be ta~en that a material for attrition, such as coarse sand, does not adversely affect the materials present in the pipeline, such as an absorbent (e.g. carbon) for the leached products.
While attrition may occur throughout the pipeline, it may be more convenient to provide a special section for attrition, such as coarse sand or hard sintered ceramic pellets. The section may be suitably llned to resist wear and may have a reduced diameter to increase : ~t . ,.. ~
~ ~`
"`, ~i . ., ' l33a~27 turbulence.
The ground material is slurried with a non-corrosive component of the leach liquor, such as brine.
Quantitles of liquld are ad~usted to give a suitable speed and volume of flow through the pipeline. The usual solids content of flowable slurries is in the range of 40 to 60 per cent by weight but higher and lower pulp densities are possible.
~he slurry enters pipeline 4 and is transported along the pipeline by the motive force provided by in~ection of steam and/or hot air from in~ection point 8. While in~ection point 8 is shown at the upstream end of the pipeline, it may be positioned downstream of the slurry head 2 and one or more additional in~ection points 10 may be provided along the pipeline.
The pipeline 4 is of any suitable material to withstand the materials passing through, for example synthetic materials, such as polyvinyl chloride (which can withstand considerable pressure within the pipe~
or mètal tubes lined with synthetic materials.
Different sections of the pipeline may be made of different materials. Thus, the initial section, in contact only with a brine slurry, may be o~ cheap material, such as asbestos cement. The pipeline may be of any desired length, for example up to several miles, or comparatively short. If the slurry head and processing plant are close together, the pipeline may ~ ` - ' '1 ;- I
6 ~3~27 be labyrinthine or splralled to give a longer resldence time, The pipeline may vary ~n diameter, for example from 4 to 12 inches. It may be buried under~round to conserve heat. If necessary, for the leaching process, additional heat may be supplied at one or more selected places, for example by electrical heating or steam ~acket.
The steam and/or hot air, for example supplied from a pressure in~ector with a venturi at a pressure of 8 to 10 atmospheres, provides motive force for transporting the slurry along the pipeline, also heats the slurry to give the correct temperature for leaching and additionally helps to maintain sufficient agitation wlthin the pipeline to promote the leaching.
A suitable minimum speed of slurry is of the order of 4 to S ft./sec. and a suitable overall throughflow is of the order of 25 tons per hour, although higher values are, of course, possible.
As the brine slurry passes through the first portion of pipeline 4, some soluble metal salts containing the desired metal will be extracted into the brine. In order to recover these soluble metal-containing materials, a separatlng tank 12 is positioned, for example, about 200 yards along the pipeline and the soluble extract withdrawn for recovery of the deslred metals while the slurry itself continues to flow along the pipeline, optionally with further addition of brine.
.: :~
, - ''''''- ~ ~ - , !.~
.`~ ' .
1~3~7 At one or more convenient points 14, so as to allow sufficlent residence time for leaching ln the pipeline, for example from half to one hour, the remaining component or components of the leachlng reagent are added. Suitable leaching components are oxidising agents, such as a mixture of dllute nitric and sulphuric acids. Of course, other leaching agents, such as sodium cyanide in an alkaline medium, can be employed and liquids other than brine can be used to slurry the feedstock material, such as halides or a hypohalite (for example sodium hypochlorite). A
mixture of leaching agents may be used, concurrently or consecutively, such as the use of sodium hypochlorlte followed by the use of an acid leaching agent. It may be possible to leach certain materials, such as calclned ores, under relatively mild conditions, for example using only hot brine to release up to two thirds of the gold values present in a starting material.
The processing plant 6 at the downstream end of the pipeline can contain any suitable apparatus for extracting and recovering the desired metals from the leach liquor. Thus, for example, the leach liquor and pulp may be introduced to a separating vessel 16 and the leached unwanted pulp withdrawn on line 18 while the separated liquor passses to one of two absorpt$on vessels 20 ~illed with an absorbent for the desired metals, such as cellulose chaff, activated carbon or ' `? , ' : .` . ` : : , :
,,.. . : ` ` ~ :
1~3~
diatomaceous earth, The metals are then recovered from the absorbent in recovery unit 22. Two vessels 20 are provlded so that one can be stripped while the other is being loaded.
If the metal being recovered is suitable it is possible for not only the leaching but also the extraction to take place within the pipeline 4. Thus, for example, an absorbent with an active surface, such as cellulose chaff, activated carbon or diatomaceous earth, or specially formuiated resins, may be introduced at one or more points to the pipellne before or after the introduction of leaching agent, such as acid, at 14. The absorbent, belng lighter than the slurry, wlll tend to lie above the slurry, but the sufficlent agitatlon ln the pipeline will cause mixing to enable the desired leached metal values to be extracted by the absorbent. The absorbent carrying the desired metal can be separated at the end of the pipeline from the unwanted pulp by a screen or other suitable means.
A further example lies in the recovery of gold, where a speclfic extractant for gold, such as Rhodamine B, can be introduced at one or more points along the pipellne wlth, for example, a further extraction stage introduced where the Rhodamine B
carrying the gold values is taken up by a suitable solvent, such as methyl isobutyl ketone or diisobutyl ketone. Alternatively, the solvent may also be added to .. . .
t,,~, ~
, ..~
.. .
,, $ ;~J 7 -the pipeline, suitably in a widened section to accommodate the additlonal flow volume.
It will be appreciated that the process described above has several advantages. Thus, the pipeline between the supply of ore and the processing plant is being used for the dual purpose of transport and as a leaching vessel and, possibly, as an extraction vessel also. This reduces the cost of equipment. The use of steam and/or hot air provides both motive power for the slurry and heat to promote the leaching reaction but does not interfere with the reaction or cause corrosion. The use of steam is particularly valuable when used for the processing of difficult ores, such as sulphidic ores.
The leaching reagents suggested above minimise corrosion problems, especlally when a non-corosive agent, such as brine, is used to slurry the feedstock material and the oxidising agent, such as dilute nitric acid, added later in the pipeline.
As a pipeline may readily be buried underground, expensive insulation costs can be avoided.
~ . .
~,;..... p. :
.,~
~....... - . . . . ~ ~
F' `. ~
Claims (7)
1. A process for recovering valuable metal from matter containing such metal in which:
a slurry is formed of said matter in particulate form;
said slurry is introduced into a pipeline and is transported through the pipeline to the outlet thereof;
at a region of the pipeline downstream of the slurry input, a leaching reagent comprising a source of halide ions and an oxidising agent is supplied to the pipeline to cause leaching conditions to prevail at said region; and the desired valuable metal is recovered downstream of the leaching region.
a slurry is formed of said matter in particulate form;
said slurry is introduced into a pipeline and is transported through the pipeline to the outlet thereof;
at a region of the pipeline downstream of the slurry input, a leaching reagent comprising a source of halide ions and an oxidising agent is supplied to the pipeline to cause leaching conditions to prevail at said region; and the desired valuable metal is recovered downstream of the leaching region.
2. A process according to claim 1, in which steam and/or heated compressed gas is injected into the pipeline to transport the slurry along the pipeline.
3. A process according to claim 2, in which the steam and/or heated compressed gas is injected into the pipeline upstream of the slurry input and at one or more injection points downstream of the slurry input.
4. A process as claimed in claim 1, in which the leaching reagent comprises a source of halide ions and an oxidising agent.
5. A process as claimed in claim 4, in which the leaching reagent is up to 35% nitric acid and salt solution of 10% NaCl.
6. A process for recovering valuable metal from matter containing such metal in which:
a slurry is formed of said particulate matter and water or brine;
said slurry is introduced into a pipeline and is transported through the pipeline to the outlet nitric acid and salt solution of 10% NaCl is supplied to the pipeline to cause leaching conditions to prevail at the region; and the desired valuable metal is recovered downstream of leaching region.
a slurry is formed of said particulate matter and water or brine;
said slurry is introduced into a pipeline and is transported through the pipeline to the outlet nitric acid and salt solution of 10% NaCl is supplied to the pipeline to cause leaching conditions to prevail at the region; and the desired valuable metal is recovered downstream of leaching region.
7. A process as claimed in claim 6, in which the valuable metal is recovered in a recovery plant at the downstream end of the pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000574696A CA1330627C (en) | 1984-02-08 | 1988-08-12 | Process for the extraction of valuable metals |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB08403318A GB2154221A (en) | 1984-02-08 | 1984-02-08 | Extraction process |
| CA000574696A CA1330627C (en) | 1984-02-08 | 1988-08-12 | Process for the extraction of valuable metals |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1330627C true CA1330627C (en) | 1994-07-12 |
Family
ID=25672050
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000574696A Expired - Fee Related CA1330627C (en) | 1984-02-08 | 1988-08-12 | Process for the extraction of valuable metals |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1330627C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1328397C (en) * | 2005-11-24 | 2007-07-25 | 中南大学 | Tail-mineral pipeline leaching out technology |
-
1988
- 1988-08-12 CA CA000574696A patent/CA1330627C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1328397C (en) * | 2005-11-24 | 2007-07-25 | 中南大学 | Tail-mineral pipeline leaching out technology |
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