EP3631026A1 - Method of treating a solution comprising metal sulphates - Google Patents
Method of treating a solution comprising metal sulphatesInfo
- Publication number
- EP3631026A1 EP3631026A1 EP18729175.2A EP18729175A EP3631026A1 EP 3631026 A1 EP3631026 A1 EP 3631026A1 EP 18729175 A EP18729175 A EP 18729175A EP 3631026 A1 EP3631026 A1 EP 3631026A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- solution
- metal
- precipitated
- sulphate
- recovered
- 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.)
- Withdrawn
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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present invention relates to a method of treating a solution comprising metal sulphates. Further, the invention relates to a method of obtaining ammonium sulphate ((NH 4 ) 2 S0 4 ). The present invention relates to a method of recovering metal compounds and (NH 4 ) 2 S0 4 from a solution comprising one or more metal sulphates.
- Adjusting the pH with NaOH introduces Na 2 (S0 4 ) into the solution which is difficult to remove from the effluent due to its high solubility.
- CaO and CaC0 3 do not introduce Na 2 (S0 4 ) into the solution but introduce gypsum, which buries all precipitating metals and renders them difficult to recover.
- the burial of precipitating metals in gypsum reduces the economic viability of the metal recovery.
- the gypsum is typically dumped in waste ponds or in waste rock dumps where it accrues and accumulates ad infinitum, eventually causing logistical problems.
- the one or more metal compounds are recovered for further processing to provide a solution comprising (NH 4 ) 2 S0 4 and water, and (NH 4 ) 2 S0 4 is recovered from the solution for further processing to provide a solution comprising essentially water.
- FIGURE 1 is a flow chart illustrating a method of recovering metal compounds and (NH 4 ) 2 S0 4 from a solution comprising one or more metal sulphates in accordance with at least some embodiments of the present invention
- FIGURE 2 is a flow chart illustrating a method of treating a solution comprising metal sulphates in accordance with at least some embodiments of the present invention
- FIGURE 3 is a flow chart illustrating a method of treating a solution comprising metal sulphates in accordance with at least some embodiments of the present invention.
- FIGURE 4 is a flow chart illustrating a method of treating a solution comprising metal sulphates in accordance with at least some embodiments of the present invention.
- FIGURE 5 is a flow chart illustrating a method of treating a solution comprising metal sulphates in accordance with at least some embodiments of the present invention.
- ammonia comprises ammonia, aqueous ammonia, ammonium hydroxide and mixtures thereof.
- metal sulphate laden solution includes leach solutions from mines including quarries, waste water from mines including quarries, runoff water from mines including quarries and mixtures thereof.
- Metal sulphate laden solution also includes wastewater from oil production, such as seawater containing sulphates and wastewater from pharmaceutical factories and textile factories, such as wastewaters from the rayon process, and manufacturers of fine chemicals including products for use in agriculture, as well as agricultural runoff.
- metal finishing plants e.g. metal plating plants, such as nickel plating plants.
- leach solution is taken to mean acidic metal laden water generated from stockpile leaching and heap leaching, including bioheap leaching.
- Controlling the pH of the solution is intended to mean both increasing the pH of the solution until metal compounds precipitate and maintaining the pH of the solution until precipitation ceases, i.e. adjusting the pH of the solution to a suitable range for each metal or metal group to be precipitated.
- a metal- sulphate laden solution e.g. a solution that comprises a low concentration of valuable metal sulphates
- ammonia provides a clean, economically-viable process for the recovery of metal compounds and ammonium sulphate.
- a low grade metal ore that would normally and conventionally be discarded can provide a solution comprising a low concentration of valuable metal sulphates which is then processed according to an embodiment of the invention to provide valuable ammonium sulphate in substantial amounts at little or no additional cost, and metals that otherwise would not have been recovered, e.g. metals that have been described as critical by the European Union in its report on critical raw materials, for example the revised list published in the 2014 Communication On the review of the list of critical raw materials for the EU and the implementation of the Raw Materials Initiative, may be recovered.
- FIGURE 1 is a flowchart describing a method in accordance with at least some embodiments of the invention in which a metal-sulphate laden solution (100) is contacted with ammonia (102) in a first reaction chamber (200) to increase the pH of the solution until a first metal compound (401) is precipitated, which is recovered for further processing, providing a first treated solution (202).
- the first treated solution (202) is contacted with further ammonia (102) to increase the pH of the solution until a second metal compound (401) is precipitated and recovered for further processing.
- the pH of the first treated solution (202) is increased with ammonia (102) stepwise for the further selective precipitation of further metal compounds (402) until substantially all metal compounds (402) have been precipitated and recovered for further processing providing a second treated solution (302).
- the second treated solution (302) comprising ammonium sulphate and water, is directed to a third reaction chamber (400).
- the ammonium sulphate is recovered for further processing to provide a solution comprising essentially water.
- FIGURE 2 illustrates a method in accordance with at least some embodiments of the present invention in which a metal sulphate- laden solution (100) is acidified with hydrogen sulphide (101) in a first reaction chamber (200). The acidified solution (100) is then contacted with ammonia (102) in the first reaction chamber (200) to increase the pH of the solution until a first metal sulphide (201) is precipitated.
- the first metal sulphide (201) is recovered for further processing, providing a first treated solution (202) which is directed to a second reaction chamber (300) into which ammonia(102) is introduced to contact the first treated solution (202), the ammonia (102) being provided to increase the pH of the first treated solution (202) which is directed to a second reaction chamber (300).
- the first treated solution (202) is contacted with ammonia (102), whereby the pH of the first treated solution (202) is increased.
- the increase in pH of the second treated solution (202) results in precipitation of metal compounds (402) which are recovered for further processing.
- FIGURE 3 is a flowchart describing a method in accordance with at least some embodiments of the present invention in which a metal sulphate-laden solution (100) is contacted with ammonia (102) in a first reaction chamber (200), whereby the pH of the solution is increased and a first metal compound (401) is precipitated and recovered for further use, providing a first treated solution which is contacted with ammonia (102) in a second reaction chamber (300). Ammonia (102) is added stepwise until all available metal compounds (402) have been precipitated and recovered for further processing, providing a second treated solution (302) comprising ammonium sulphate and water. The second treated solution is directed to a third reaction chamber (400). The ammonium sulphate is recovered to provide a solution comprising water and one or more Group I sulphates and Group II sulphates.
- FIGURE 4 is a flowchart describing a method in accordance with at least some embodiments of the present invention in which a metal sulphate-laden solution
- the treated solution (100) is treated with hydrogen sulphide (101) in a fourth reaction chamber (500).
- the treated solution (100) is then contacted with Al(OH) 3 (502) in the fourth reaction chamber (500) to increase the pH of the solution until a metal sulphide (501) is precipitated.
- the metal sulphide (501) is recovered for further processing, providing a treated solution (602) which is directed into a fifth reaction chamber (700) into which
- Al(OH) 3 (502) is introduced in a pH controlling step to provide a solution (702).
- the solution (702) is then directed to a sixth reaction chamber (800) in which it is treated with hydrogen sulphide (101).
- This treated solution (702) is then contacted with ⁇ 1( ⁇ ) 3 (502) in the sixth reaction chamber (800) to increase the pH of the solution until one or more further metal sulphides (801) are precipitated.
- the one or more further metal sulphides (801) are recovered for further processing providing a further treated solution (802).
- the further treated solution (802) is directed to a seventh reaction chamber (900) for precipitation of iron.
- the further treated solution is contacted in the seventh reaction chamber (900) with ferrous/ferric hydroxide (3002) until FeS/FeS 2 (901) is precipitated.
- FeS/FeS 2 (901) is recovered and recirculated to the metal sulphate laden solution (100) where it reduces any ferric iron in the metal sulphate laden solution (100) to ferrous iron.
- a first portion (902) is directed to heaps (910) for heap leaching.
- a second portion (903) of the raffinate is directed to a first reaction chamber (200) in which the second portion of the raffinate (903) is contacted with ammonia (102), whereby the pH of the solution is increased and Al(OH) 3 (502) is precipitated and recovered for use in the fourth (500), fifth (700) and sixth (800) reaction chambers.
- the Fe(OH) 3 (3002) is recovered and directed for use in the seventh reaction chamber (900).
- Ammonia (102) is further added stepwise until all available metal compounds (402) have been precipitated and recovered for further processing providing a solution (1600) comprising water, group I and II metals and
- a third portion of the raffinate (904) is directed to an eighth reaction chamber (1000) for an aluminium precipitation step.
- the third portion of the raffinate (904) is contacted with CaC0 3 (1002) until Al(OH) 3 (1), Fe(OH) 3 (2), and CaS0 4 (3) are precipitated and recovered to provide a further solution (1001), which is subjected to a lime treatment in a ninth reaction chamber (1100), whereby the solution is contacted with CaO (1003) to precipitate Fe(OH) 3 (4), Mn(OH) 2 (5), Mg(OH) 2 (6), and CaS0 4 (7), which are precipitated and recovered to provide clean water (1500).
- FIGURE 5 is a flowchart describing a method in accordance with at least some embodiments of the present invention in which a PLS (2100) comprising at least zinc, nickel, cobalt, iron aluminium, manganese and magnesium, is treated with hydrogen sulphide (101) in a fourth reaction chamber (500).
- the treated solution (2100) is then contacted with Al(OH) 3 (502) in the fourth reaction chamber (500) to increase the pH of the solution until ZnS (5100) is precipitated.
- the ZnS (5100) is recovered for further processing, providing a treated solution (602) which is directed into a fifth reaction chamber (700) into which Al(OH) 3 (502) is introduced in a pH controlling step to provide a solution (702).
- the solution (702) is then directed to a sixth reaction chamber (800) in which it is treated with hydrogen sulphide (101)
- This hydrogen sulphide-treated solution (702) is then contacted with Al(OH) 3 (502) in the sixth reaction chamber (800) to increase the pH of the solution until NiCoS (8001) is precipitated.
- the NiCoS (8001) is recovered for further processing providing a further treated solution (8002).
- the further treated solution (8002) is directed to a seventh reaction chamber (900) for precipitation of iron.
- the further treated solution is contacted in the seventh reaction chamber (900) with Fe(OH) 3 (3002) until FeS (901) is precipitated essentially purging the solution (8002) of hydrogen sulphide (101).
- FeS (901) is recovered and recirculated to the PLS (2100) where it reduces any ferric iron in the PLS (2100) to ferrous iron.
- a first portion (902) is directed to heaps for heap leaching.
- a second portion of the raffinate (903) is directed to a first reaction chamber (200) in which it is contacted with ammonia (102), whereby the pH of the solution is increased and Al(OH) 3 (502) is precipitated and recovered for use in the fourth (500), fifth (700) and sixth (800) reaction chambers.
- the second treated solution is directed to a third reaction chamber (400) in which it is treated with H 2 S (101)to introduce a source of sulphide ions into the solution and then is contacted with ammonia(102) whereby the pH increases and MnS (4002) is precipitated out and recovered for further use providing a third treated solution which is subjected to a treatment whereby the third treated solution is contacted with CaO (6002) in a lime boil step in which ammonia (102) is driven out of solution and recycled.
- CaS0 4 (5002) is precipitated providing a final solution comprising essentially clean water (1500).
- the third portion of the raffinate (904) is contacted with CaC0 3 until Al(OH) 3 (1), Fe(OH) 3 (2), and CaS0 4 (3) are precipitated and recovered to provide a further solution (1001), which is subjected to a lime treatment in a ninth reaction chamber (1100), whereby the solution is contacted with CaO (1003) to precipitate Fe(OH) 3 (4), Mn(OH) 2 (5), Mg(OH) 2 (6), and CaS0 4 (7), which are precipitated and recovered to provide clean water (1500).
- the present invention relates to a method for the recovery of metal compounds and ammonium sulphate from a solution comprising one or more metal sulphates.
- Metal sulphates in the solution may include sulphates of various transition metals, actinides, and mixtures thereof e.g. copper, zinc, nickel, cobalt, iron, aluminium manganese, uranium, scandium, titanium, vanadium, chromium, magnesium and alloys thereof.
- the method comprises the steps of a) controlling the pH of the solution by adding ammonia to the solution one or more times to precipitate one or more metal compounds.
- the pH of the solution is controlled one or more times for the selective precipitation of metal compounds, e.g. metal hydroxides, from the solution.
- the method further comprises the steps of b) recovering one or more metal compounds for further processing to provide a first treated solution comprising (NH 4 ) 2 S0 4 and water.
- the first treated solution may also comprise other compounds such as magnesium sulphate.
- metal compounds can be recovered by various means known in the art, such as filtration including membrane filtration, and centrifugation.
- a recovering step c) from the first treated solution is recovered (NH 4 ) 2 S0 4 in a recovering step c) for further processing to provide a second treated solution comprising essentially water.
- (NH 4 ) 2 S0 4 may be recovered by means known in the art such as by evaporation, providing essentially clean water for release.
- a low concentration of valuable metal sulphates e.g. is a concentration of 10% by weight or less, particularly 8% or less, for example 1 to 6%, preferably 2 to 5 % suitably 4%, most suitably 3 % by weight.
- embodiments of the invention are also applicable to higher sulphate concentrations.
- Embodiments of the invention can be applied to all metal-sulphate laden solutions from 1% by weight up to and including solutions saturated with metal sulphates.
- the recovering step b) comprises recovering more than one metal compound, for example 2, 3, 4, 5, 6, 7, 8, 9, or 10 metal compounds for further processing to provide a first treated solution comprising (NH 4 ) 2 S0 4 and water.
- the method comprises the steps of (a) controlling the pH of the solution by adding ammonia to the solution more than one time to precipitate more than one metal compounds, (b) recovering more than one metal compounds for further processing to provide a first treated solution comprising (NH 4 ) 2 S0 4 and water, and (c) recovering (NH 4 ) 2 S0 4 for further processing to provide a second treated solution comprising essentially water.
- the second treated solution comprises sulphates that are not precipitated out with the addition of ammonia.
- the second treated solution further comprises sulphates of one or more Group I or Group II metals.
- metals may include lithium, sodium, potassium, magnesium, calcium and other Group I or Group II metals, as well as mixtures thereof.
- the second treated solution is directed to further processing, whereby non precipitated sulphates are recovered. Such sulphates may be recovered by e.g. evaporation.
- the sulphates of one or more Group I or Group II metals are recovered.
- the sulphates of the Group I or Group II metals are recovered before ammonium sulphate is recovered.
- ammonium sulphate is recovered before sulphates of Group I or Group II metals are recovered.
- the pH controlling step comprises (i) increasing the pH of the solution with ammonia until a first metal compound precipitates, (ii) maintaining the pH of the solution with further ammonia until the first metal compound is precipitated, and repeating steps (i) and (ii) until essentially all metal compounds are precipitated.
- controlling step comprises (i) increasing the pH of the solution with ammonia until a first metal compound precipitates, (ii) maintaining the pH of the solution with further ammonia until the first metal compound is precipitated, optionally (iii) increasing the pH of the solution with ammonia until a further metal compound precipitates and maintaining the pH of the solution with further ammonia until the further metal compound is precipitated, and optionally (iv) repeating step iii until essentially all metal compounds are precipitated.
- This method of selective precipitation ensures that as much of each metal is recovered as possible.
- the pH of the solution is maintained with the addition of further ammonia after each increase of the pH until each metal compound is precipitated and recovered.
- 50 - 98 wt % of the metal compounds are recovered from the metal- sulphate laden solution, preferably 60 - 95 wt %, suitably 70 - 92 wt %, particularly 75 - 90 wt % of the metal compounds are recovered from the metal- sulphate laden solution.
- Various metal compounds are precipitated by means of embodiments of the invention.
- metal compounds selected from the group of oxides, oxyhydroxides, silicates, hydroxides and mixtures thereof are precipitated.
- hydroxides are precipitated.
- the metal compounds precipitated comprise metals selected from the group of transition metals, actinides, and mixtures thereof, preferably selected from the group of copper, zinc, nickel, cobalt, iron, aluminium manganese, uranium, scandium, titanium, vanadium, chromium, magnesium and alloys thereof.
- the solution is a pregnant leach solution, optionally provided by one or more ores by a bioheap leaching process.
- the ores may contain metals as described above, a typical ore may comprise e.g. salts of nickel, copper, zinc, cobalt manganese, magnesium, uranium, sulphur and mixtures thereof.
- An ore may also comprise salts of aluminium, arsenic, calcium, cadmium, chromium, iron, sodium, silicon and mixtures thereof.
- the method further comprises a sulphide precipitation step.
- a pregnant leach solution (PLS) provided by such an ore is contacted with a source of sulphide ions.
- PLS pregnant leach solution
- a source of sulphide ions acidifies the solution, i.e. lowers the pH of the solution by the following example reaction: MeS0 4 (a q) + H 2 S( g ) ⁇ MeS (aq) + H 2 S0 4(aq ) where Me is a metal having an oxidation state II or having two valence electrons.
- the source of sulphide ions is introduced to the solution for the precipitation of metal sulphides.
- the source of sulphide ions is hydrogen sulphide.
- Sulphates in the solution react with hydrogen sulphide to provide metal sulphides and sulphuric acid.
- Adding ammonia to the solution neutralises sulphuric acid to give ammonium sulphate and adjusts the pH, i.e. increases the pH, and causes metal sulphides to precipitate out of solution in turn.
- metal sulphides precipitate out in the order copper sulphide, zinc sulphide, nickel sulphide, cobalt sulphide and iron sulphide. Each metal sulphide being recovered in turn.
- the conditions of the sulphide precipitation step are selected so that metal sulphides selected from the group consisting of transition metals such as copper zinc, nickel, cobalt and iron are recovered.
- metal sulphides selected from the group consisting of transition metals such as copper zinc, nickel, cobalt and iron are recovered.
- the pH of the solution is increased with Al(OH)3.
- the method comprises a sulphide precipitation prior to the controlling step (a), whereby the sulphide precipitation comprises the steps of increasing the pH of the solution with Al(OH) 3 until one or more metal sulphides are precipitated.
- Al(OH) 3 is ideal for precipitating sulphides from a solution having a pH of 3 or lower.
- the sulphide precipitation step further comprises recovering the precipitated one or more metal sulphides for further processing to provide a metal sulphate-laden solution, and directing the metal sulphate- laden solution to the controlling step (a) of any of the herein described embodiments.
- the pH of the solution may be increased with Fe(OH) 3 , which is ideal for precipitating sulphides from a solution having a pH of up to and including 5.
- the pH of the solution is increased with Fe(OH) 3 .
- the agent for increasing the pH of the solution may be switched from Al(OH) 3 to Fe(OH) 3 .
- one or more metal sulphides are precipitated from the solution prior to the controlling step a) using Al(OH) 3 to increase the pH of the solution before one or more further metal sulphides are precipitated from the solution prior to the controlling step a) using Fe(OH) 3 to increase the pH of the solution.
- a source of sulphide ions for example hydrogen sulphide or iron sulphide, or any readily available source of sulphide ions is provided to the solution before the solution is contacted with the pH raising agent, i.e. before the pH of the solution is raised.
- a source of sulphide ions is added continuously to the solution.
- a source of sulphide ions is added to the solution until sulphide precipitation ceases.
- (NH4) 2 S04 is driven back to the bioheaps where the ammonia is essentially lost as a pH controlling agent. In many cases this is desirable, as (NH4) 2 S04 is very suitable as a nutrient for bacteria in many bioheaps. However, in many cases it is more desirable to harvest as much (NH4) 2 S04 as possible.
- alternative pH raising agents such as Al(OH) 3 and Fe(OH) 3 are used.
- the raffinate contains no valuable (NH4) 2 S04.
- Ammonia is then added in subsequent hydroxide and sulphide precipitation steps before either being harvested as (NH4) 2 S04 or being boiled off in a lime boil, thereby enabling recycling of ammonia and after the initial investment to purchase ammonia, the metal recovery process comprises a self-sufficient ammonia loop.
- embodiments concern the recovery of (NH4) 2 S0 4 andfurther embodiments concern recycling ammonia.
- a sulphide precipitation step is not required or not desirable.
- other metal compounds are precipitated in a hydroxide precipitation step as described above in which the pH of the solution is controlled stepwise for the selective precipitation of metal compounds.
- a solution might comprise metals selected from the group consisting of aluminium, arsenic, calcium, cadmium, chromium, iron, magnesium, manganese, sodium, silicon, uranium, copper, zinc, nickel, cobalt and mixtures thereof.
- the conditions of the step for the selective precipitation of one or more metal compounds are selected so that compounds comprising metals selected from the group consisting of aluminium, arsenic, calcium, cadmium, chromium, iron, magnesium, manganese, sodium, silicon, uranium, copper, zinc, nickel, cobalt and mixtures thereof are recovered.
- metal compounds such as hydroxide
- aluminium hydroxide precipitates out at a pH of around 6, along with some iron (III) hydroxide, at a pH of around 8 to 9, copper hydroxide precipitates out along with some nickel hydroxide.
- Further embodiments of the invention relate to a method of obtaining ammonium sulphate.
- the method comprises the steps of obtaining a solution comprising sulphates having a pH of less than or equal to 7, subjecting the solution to a hydroxide precipitation step, whereby the solution is treated with ammonia to precipitate out metal compounds contained therein, to provide a first treated solution comprising ammonium sulphate, and recovering the ammonium sulphate from the first treated solution.
- Ammonium sulphate is formed e.g. as in the following example reaction:
- the ammonium sulphate is recovered, for example, by conventional means including evaporation.
- the method provides an economically viable means of generating ammonium sulphate and harvesting metals from sulphate- bearing solutions from sulphidic ores, even including low-grade sulphidic ore bodies.
- a substantial amount of ammonium sulphate is generated as a side product in the harvesting of metals at little or no additional cost. Only a small cost for the recovery of ammonium sulphate arises.
- valuable metals are harvested as side products from sulphidic ores at no additional cost.
- a pregnant leach solution was obtained from a low grade ore.
- the PLS contained various salts of metals according to Table 1.
- ammonia to increase the pH of the solution to a level of ca. 2.5.
- the pH of the solution was maintained at that level with the addition of further ammonia as zinc sulphide precipitated out.
- the ammonia neutralized the sulphuric acid to provide ammonium sulphate.
- the precipitated zinc sulphate was recovered. After recovery of zinc sulphate, to the solution was added ammonia to increase the pH of the solution to a level of ca. 3.5. The pH of the solution was maintained at that level with the addition of further ammonia as nickel sulphide precipitated out. The ammonia neutralized sulphuric acid to provide ammonium sulphate.
- the precipitated nickel sulphate was recovered. Further metal compounds were recovered stepwise in a hydroxide precipitation step. To the solution was added ammonia to increase the pH to precipitate hydroxides, e.g.
- At least some embodiments of the present invention find industrial application in mining industries, e.g. metal mining, in particular open cast mining, which requires the processing of large volumes of water.
- industries in which some embodiments find industrial application include the textile industry e.g. in the rayon process, the pharmaceutical industry, metal finish plants such as metal plating plants e.g. nickel plating plants as well as in the fine chemical industry, including the manufacture of chemicals for use in agricultural applications, and further in the treatment of run-off, from both agriculture and in mining.
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FI20175473A FI129207B (en) | 2017-05-26 | 2017-05-26 | Method of treating a solution comprising metal sulphates |
PCT/FI2018/050399 WO2018215697A1 (en) | 2017-05-26 | 2018-05-25 | Method of treating a solution comprising metal sulphates |
Publications (1)
Publication Number | Publication Date |
---|---|
EP3631026A1 true EP3631026A1 (en) | 2020-04-08 |
Family
ID=62528457
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP18729175.2A Withdrawn EP3631026A1 (en) | 2017-05-26 | 2018-05-25 | Method of treating a solution comprising metal sulphates |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP3631026A1 (en) |
CA (1) | CA3064679A1 (en) |
FI (1) | FI129207B (en) |
WO (1) | WO2018215697A1 (en) |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1058614A (en) * | 1963-02-13 | 1967-02-15 | Yawata Iron & Steel Co | Process for treating liquid extracted from soda-roasted laterite |
CA930556A (en) * | 1971-01-22 | 1973-07-24 | J. I. Evans David | Acid leaching process for treating high grade nickel-copper mattes |
CA2068982C (en) * | 1992-05-19 | 2000-10-03 | Derek G.E. Kerfoot | Process for the separation of cobalt from nickel |
US8043585B2 (en) * | 2008-01-15 | 2011-10-25 | Vale Inco Limited | Liquid and solid effluent treatment process |
US10144650B2 (en) * | 2014-04-17 | 2018-12-04 | AluChem Companies, Inc. | Method for recovery of the constituent components of laterites |
-
2017
- 2017-05-26 FI FI20175473A patent/FI129207B/en active IP Right Grant
-
2018
- 2018-05-25 CA CA3064679A patent/CA3064679A1/en not_active Abandoned
- 2018-05-25 WO PCT/FI2018/050399 patent/WO2018215697A1/en unknown
- 2018-05-25 EP EP18729175.2A patent/EP3631026A1/en not_active Withdrawn
Also Published As
Publication number | Publication date |
---|---|
WO2018215697A1 (en) | 2018-11-29 |
CA3064679A1 (en) | 2018-11-29 |
FI20175473A1 (en) | 2018-11-27 |
FI129207B (en) | 2021-09-15 |
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