CA2360704A1 - Process of leaching a lateritic ore for preparing metal extraction - Google Patents
Process of leaching a lateritic ore for preparing metal extraction Download PDFInfo
- Publication number
- CA2360704A1 CA2360704A1 CA002360704A CA2360704A CA2360704A1 CA 2360704 A1 CA2360704 A1 CA 2360704A1 CA 002360704 A CA002360704 A CA 002360704A CA 2360704 A CA2360704 A CA 2360704A CA 2360704 A1 CA2360704 A1 CA 2360704A1
- Authority
- CA
- Canada
- Prior art keywords
- suspension
- ore
- acid
- mixing line
- tube
- 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.)
- Abandoned
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
- C22B3/04—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
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
-
- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—Sulfurated acids or salts thereof
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Metallurgy (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Environmental & Geological Engineering (AREA)
- Geology (AREA)
- Geochemistry & Mineralogy (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The starting material is lateritic ore which contains nickel oxide and/or cobalt oxide. From water and comminuted ore, of which at least 80 wt-% have grain sizes of not more than 0.5 mm, a pumpable suspension is formed. The ore-containing sus-pension is passed through an indirectly heated preheating tube, the suspension being heated to 150 to 250°C. The heated suspension is passed through a mixing line in which an acid in a minimum amount of 10 kg per 100 kg ore, calculated anhy-drous, is admixed to the suspension, and the acid-containing suspension is passed through a dwell time tube in which the dwell time of the suspension is at least 0.1 minutes. Pref-erably, sulfuric acid is introduced into the mixing line.
Description
Process of Leaching' a Lateritic Ore for Preparing Metal Extraction This invention relates to a process of leaching a lateritic ore, which contains nickel oxide and/or cobalt oxide, for preparing the extraction of at least one metal.
It is known that a tubular reactor plant substantially com-p prises three sections, namely the indirectly heated preheat-ing zone, the reaction zone in the form of a dwell time tube, and finally the cooling and expansion system. During expan-sion, temperature and pressure are decreased by partial evaporation of the suspension. The steam obtained thereby can be used in the preheating zone.
When leaching oxide, it is known to add the chemicals which effect the digestion to the ore-water suspension before the preheater. The consequence is that the digestion reaction can already start before the dwell time tube at a reduced reac-tion rate, so that the entire reaction time is prolonged. It is disadvantageous that already during preheating with rising temperature various digestion products can be formed, which are undesired. Moreover, products of the digestion already starting in the preheater can form crusts therein, which can greatly impede the transfer of heat. This encrustation can lead to increased maintenance costs and an only restricted availability of the plant.
It is the object underlying the invention to perform the above-mentioned process as inexpensively as possible and to ensure that there is no encrustation in the preheating zone.
In accordance with the invention, this is achieved in that from water and comminuted ore, of which at least 80 wt-% have grain sizes of not more than 0.5 mm, a pumpable suspension is formed, that the ore-containing suspension is passed through an indirectly heated preheating tube, the suspension being heated to 150 to 250°C, that the heated suspension is passed through a mixing line in which an acid in a minimum amount of 10 kg and preferably at least 50 kg per 100 kg ore, calcu-lated anhydrous, is admixed to the suspension, and that the acid-containing suspension is passed through a dwell time tube in which the dwell time of the suspension is at least 0.1 minutes and preferably at least 1 minute. Now, encrusta-tion or disturbing corrosion need no longer be expected in the preheating tube.
Advantageously, the ore-containing suspension is pumped into the preheating tube, and in the preheating tube a static pressure of 30 to 200 bar and preferably at least 120 bar is maintained. Expediently, the increased pressure is also main-tained in the mixing line and in the dwell time tube. The in-creased pressure leads to an increase of the boiling tempera-ture and provides for higher operating temperatures. Leaching is thereby intensified quite considerably, but without over-proportionally increasing the investment costs. Surprisingly, sulfuric acid will be admixed to the suspension in the mixing line, but there may also be used some other mineral acid to improve leaching. It may be recommended to introduce the sul-furic acid or some other acid into the mixing line after hav-ing been preheated to temperatures e.g. in the range from 40 to 200°C and preferably at least 80°C.
The dwell time tube mostly is of considerable length, in or-der to achieve the desired dwell time of the suspension. The length of the dwell time tube usually is above 100 m and may also be more than 1000 m. To achieve the desired effect, the acid-containing suspension will be withdrawn from the dwell time tube with temperatures in the range from 250 to 350°C.
By means of the inventive process it is achieved that moving parts, which get in contact with the acid-containing suspen-sion, can be omitted.
Embodiments of the process will be explained with reference to the drawing, in which:
Fig. 1 shows a flow diagram of the process, Fig. 2 shows the region of the mixing line in a longitudi-nal section, and Fig. 3 shows an enlarged cross-section along line III-III
of Fig. 2 .
A container (1) contains an ore-water suspension, which by means of the high-pressure pumpe (2) is first of all passed through the preheating tube (3), then through the mixing line (4) and through the dwell time tube (5). Subsequent to the dwell time tube (5) an expansion container (6) is provided, which may also have a multi-stage design. Subsequently, the suspension flows through line (~'7) to the extraction (8) known per se for metal recovery. The preheating tube is surrounded by a heating jacket (9), through which flows a heating fluid (e.g. steam or heat transfer oil). The preheating tube may also be divided in several portions which are heated differ-ently.
The mixing line (4) is represented in a longitudinal section in Fig. 2 and in a cross-section in Fig. 3. The outer metal tube (4a) surrounds an inner lining in the form of acid-resistant molded bricks (10) which are joined in an inter-locked way. The molded bricks are conically tapered in cer-taro portions in the direction of the flow direction (11) of the suspension. This results in a deliberate irregularity of the inside of the flow region of the mixing line. The acid which is added to the suspension through the feed line (12) is mixed due to the strong turbulence formed in the flow re-gion after a short flow path. In contrast to the representa-tion of Fig. 2, the desired turbulence for quickly mixing suspension and acid in the vicinity of the mixing line (4) can also be achieved by other stationary flow obstacles in the flow region of the suspension.
From the preheating tube (3), the suspension usually comes with a temperature in the range from 150 to 250°C and in the mixing line (4) absorbs the acid in the necessary amount. The amount of acid addition depends on the composition of the ore, in particular with respect to oxidic components which react with the acid. When adding sulfuric acid, reaction heat is produced in the desired way by exothermal formation of sulfate. Subsequent to the mixing line (4) the dwell time tube (5) is provided, which usually has a length of more than 100 m and occasionally more than 1000 m.
In the vicinity of the preheating tube, the mixing line and the dwell time tube, there is usually ensured a static pres-sure of 30 to 200 bar and preferably at least 120 bar, in or-der to optimally achieve the desired digestion. The relief of pressure then is effected in the expansion container (6), where steam is released, which escapes via line (6a). This steam can be used e.g. in the heating jacket (9).
Example:
In a plant corresponding to the drawing, lateritic nickel ore is treated, and in the container (1) an aqueous suspension with a solids content of 32 wt-o and a density of 1.24 kg/1 is provided. Per hour, 18 m3 of this suspension are first in-troduced into the preheating tube (3), and are then passed through the mixing line (4) and the dwell time tube (5).
For the mixing line (4) the following is applicable:
Pressure at the inlet: 98 bar The temperature of the suspension at the inlet is 234°C and at the outlet 266°C.
Dwell time: 5 seconds Flow rate of the suspension: 1.5 m/sec Length of the mixing line: 7.5 m Inside diameter: 70-85 mm Thickness of the acid-resistant brick lining: about 150 mm.
Through line (12), 1.74 t/h sulfuric acid with 98 wt-% H2S04 are supplied, which has a temperature of 30°C. The dwell time tube (5) has a length of 600 m, the dwell time of the suspen-sion therein is 8 min. At the end of the tube (5) the pres-sure is about 108 bar and the temperature is about 273°C.
It is known that a tubular reactor plant substantially com-p prises three sections, namely the indirectly heated preheat-ing zone, the reaction zone in the form of a dwell time tube, and finally the cooling and expansion system. During expan-sion, temperature and pressure are decreased by partial evaporation of the suspension. The steam obtained thereby can be used in the preheating zone.
When leaching oxide, it is known to add the chemicals which effect the digestion to the ore-water suspension before the preheater. The consequence is that the digestion reaction can already start before the dwell time tube at a reduced reac-tion rate, so that the entire reaction time is prolonged. It is disadvantageous that already during preheating with rising temperature various digestion products can be formed, which are undesired. Moreover, products of the digestion already starting in the preheater can form crusts therein, which can greatly impede the transfer of heat. This encrustation can lead to increased maintenance costs and an only restricted availability of the plant.
It is the object underlying the invention to perform the above-mentioned process as inexpensively as possible and to ensure that there is no encrustation in the preheating zone.
In accordance with the invention, this is achieved in that from water and comminuted ore, of which at least 80 wt-% have grain sizes of not more than 0.5 mm, a pumpable suspension is formed, that the ore-containing suspension is passed through an indirectly heated preheating tube, the suspension being heated to 150 to 250°C, that the heated suspension is passed through a mixing line in which an acid in a minimum amount of 10 kg and preferably at least 50 kg per 100 kg ore, calcu-lated anhydrous, is admixed to the suspension, and that the acid-containing suspension is passed through a dwell time tube in which the dwell time of the suspension is at least 0.1 minutes and preferably at least 1 minute. Now, encrusta-tion or disturbing corrosion need no longer be expected in the preheating tube.
Advantageously, the ore-containing suspension is pumped into the preheating tube, and in the preheating tube a static pressure of 30 to 200 bar and preferably at least 120 bar is maintained. Expediently, the increased pressure is also main-tained in the mixing line and in the dwell time tube. The in-creased pressure leads to an increase of the boiling tempera-ture and provides for higher operating temperatures. Leaching is thereby intensified quite considerably, but without over-proportionally increasing the investment costs. Surprisingly, sulfuric acid will be admixed to the suspension in the mixing line, but there may also be used some other mineral acid to improve leaching. It may be recommended to introduce the sul-furic acid or some other acid into the mixing line after hav-ing been preheated to temperatures e.g. in the range from 40 to 200°C and preferably at least 80°C.
The dwell time tube mostly is of considerable length, in or-der to achieve the desired dwell time of the suspension. The length of the dwell time tube usually is above 100 m and may also be more than 1000 m. To achieve the desired effect, the acid-containing suspension will be withdrawn from the dwell time tube with temperatures in the range from 250 to 350°C.
By means of the inventive process it is achieved that moving parts, which get in contact with the acid-containing suspen-sion, can be omitted.
Embodiments of the process will be explained with reference to the drawing, in which:
Fig. 1 shows a flow diagram of the process, Fig. 2 shows the region of the mixing line in a longitudi-nal section, and Fig. 3 shows an enlarged cross-section along line III-III
of Fig. 2 .
A container (1) contains an ore-water suspension, which by means of the high-pressure pumpe (2) is first of all passed through the preheating tube (3), then through the mixing line (4) and through the dwell time tube (5). Subsequent to the dwell time tube (5) an expansion container (6) is provided, which may also have a multi-stage design. Subsequently, the suspension flows through line (~'7) to the extraction (8) known per se for metal recovery. The preheating tube is surrounded by a heating jacket (9), through which flows a heating fluid (e.g. steam or heat transfer oil). The preheating tube may also be divided in several portions which are heated differ-ently.
The mixing line (4) is represented in a longitudinal section in Fig. 2 and in a cross-section in Fig. 3. The outer metal tube (4a) surrounds an inner lining in the form of acid-resistant molded bricks (10) which are joined in an inter-locked way. The molded bricks are conically tapered in cer-taro portions in the direction of the flow direction (11) of the suspension. This results in a deliberate irregularity of the inside of the flow region of the mixing line. The acid which is added to the suspension through the feed line (12) is mixed due to the strong turbulence formed in the flow re-gion after a short flow path. In contrast to the representa-tion of Fig. 2, the desired turbulence for quickly mixing suspension and acid in the vicinity of the mixing line (4) can also be achieved by other stationary flow obstacles in the flow region of the suspension.
From the preheating tube (3), the suspension usually comes with a temperature in the range from 150 to 250°C and in the mixing line (4) absorbs the acid in the necessary amount. The amount of acid addition depends on the composition of the ore, in particular with respect to oxidic components which react with the acid. When adding sulfuric acid, reaction heat is produced in the desired way by exothermal formation of sulfate. Subsequent to the mixing line (4) the dwell time tube (5) is provided, which usually has a length of more than 100 m and occasionally more than 1000 m.
In the vicinity of the preheating tube, the mixing line and the dwell time tube, there is usually ensured a static pres-sure of 30 to 200 bar and preferably at least 120 bar, in or-der to optimally achieve the desired digestion. The relief of pressure then is effected in the expansion container (6), where steam is released, which escapes via line (6a). This steam can be used e.g. in the heating jacket (9).
Example:
In a plant corresponding to the drawing, lateritic nickel ore is treated, and in the container (1) an aqueous suspension with a solids content of 32 wt-o and a density of 1.24 kg/1 is provided. Per hour, 18 m3 of this suspension are first in-troduced into the preheating tube (3), and are then passed through the mixing line (4) and the dwell time tube (5).
For the mixing line (4) the following is applicable:
Pressure at the inlet: 98 bar The temperature of the suspension at the inlet is 234°C and at the outlet 266°C.
Dwell time: 5 seconds Flow rate of the suspension: 1.5 m/sec Length of the mixing line: 7.5 m Inside diameter: 70-85 mm Thickness of the acid-resistant brick lining: about 150 mm.
Through line (12), 1.74 t/h sulfuric acid with 98 wt-% H2S04 are supplied, which has a temperature of 30°C. The dwell time tube (5) has a length of 600 m, the dwell time of the suspen-sion therein is 8 min. At the end of the tube (5) the pres-sure is about 108 bar and the temperature is about 273°C.
Claims (7)
1. A process of leaching a lateritic ore, which contains nickel oxide and/or cobalt oxide, for preparing the ex-traction of at least one metal, characterized in that from water and comminuted ore, of which at least 80 wt-%
have grain sizes of not more than 0.5 mm, a pumpable suspension is formed, that the ore-containing suspension is passed through an indirectly heated preheating tube, the suspension being heated to 150 to 250°C, that the heated suspension is passed through a mixing line in which an acid in a minimum amount of 10 kg per 100 kg ore, calculated anhydrous, is admixed to the suspension, and that the acid-containing suspension is passed through a dwell time tube, in which the dwell time of the suspension is at least 0.1 minutes.
have grain sizes of not more than 0.5 mm, a pumpable suspension is formed, that the ore-containing suspension is passed through an indirectly heated preheating tube, the suspension being heated to 150 to 250°C, that the heated suspension is passed through a mixing line in which an acid in a minimum amount of 10 kg per 100 kg ore, calculated anhydrous, is admixed to the suspension, and that the acid-containing suspension is passed through a dwell time tube, in which the dwell time of the suspension is at least 0.1 minutes.
2. The process as claimed in claim 1, characterized in that the ore-containing suspension is pumped into the pre-heating tube and in the preheating tube a static pres-sure of 30 to 200 bar is maintained.
3. The process as claimed in claim 1 or 2, characterized in that sulfuric acid is admixed to the suspension in the mixing line.
4. The process as claimed in any of claims 1 to 3, charac-terized in that the acid-containing suspension is with-drawn from the dwell time tube with temperatures in the range from 250 to 350°C.
5. The process as claimed in claim 1 or any of the preced-ing claims, characterized in that the suspension and the acid in the mixing line are guided along stationary flow obstacles.
6. The process as claimed in claim 1 or any of the preced-ing claims, characterized in that the acid is preheated to temperatures in the range from 40 to 200°C before they are introduced into the mixing line.
7. The process as claimed in claim 1 or any of the preced-ing claims, characterized in that the mixing line is at least partly brick-lined.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10055550.0 | 2000-11-09 | ||
DE10055550A DE10055550A1 (en) | 2000-11-09 | 2000-11-09 | Process for leaching lateritic ore containing nickel oxide and/or cobalt oxide comprises forming a pumpable suspension made from water and crushed ore, feeding through a preheating tube |
Publications (1)
Publication Number | Publication Date |
---|---|
CA2360704A1 true CA2360704A1 (en) | 2002-05-09 |
Family
ID=7662698
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CA002360704A Abandoned CA2360704A1 (en) | 2000-11-09 | 2001-10-31 | Process of leaching a lateritic ore for preparing metal extraction |
Country Status (5)
Country | Link |
---|---|
AU (1) | AU783488B2 (en) |
CA (1) | CA2360704A1 (en) |
CO (1) | CO5380041A1 (en) |
DE (1) | DE10055550A1 (en) |
MY (1) | MY134152A (en) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU2003903632A0 (en) * | 2003-07-14 | 2003-07-31 | Qni Technology Pty Ltd | Process for recovery of nickel and cobalt by heap leaching of low grade nickel or cobalt containing material |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4541994A (en) * | 1983-07-22 | 1985-09-17 | California Nickel Corporation | Method of liberating nickel- and cobalt-enriched fines from laterite |
US6379937B1 (en) * | 2000-12-18 | 2002-04-30 | Council Of Scientific And Industrial Research | Process for the preparation of a mixture of 19 hydroxyelcosatetraenoic acid and 20 hydroxyeicosatetracnoic acid (10 hete and 20 hete) |
-
2000
- 2000-11-09 DE DE10055550A patent/DE10055550A1/en not_active Withdrawn
-
2001
- 2001-10-31 CA CA002360704A patent/CA2360704A1/en not_active Abandoned
- 2001-11-02 CO CO01094591A patent/CO5380041A1/en not_active Application Discontinuation
- 2001-11-08 AU AU89338/01A patent/AU783488B2/en not_active Ceased
- 2001-11-09 MY MYPI20015166A patent/MY134152A/en unknown
Also Published As
Publication number | Publication date |
---|---|
MY134152A (en) | 2007-11-30 |
AU8933801A (en) | 2002-05-16 |
CO5380041A1 (en) | 2004-03-31 |
AU783488B2 (en) | 2005-11-03 |
DE10055550A1 (en) | 2002-05-23 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US5393320A (en) | Leaching process for nickel cobalt and manganese ores | |
NO131992B (en) | ||
DK2454389T3 (en) | A process for the recovery of base metals from oxidårer | |
CN113265532B (en) | Method for leaching nickel-ammonia solution from nickel-iron alloy by wet method and application | |
RU2434064C1 (en) | Procedure for processing refractory sulphide gold containing raw stock | |
CN105779777A (en) | Method for separating and recycling nickel and cobalt from nickel and cobalt slag | |
US3018170A (en) | Pressure leaching apparatus | |
CA3014489C (en) | Process for the separation of vanadium | |
JP2549614B2 (en) | Liquid phase oxidation | |
Fleming et al. | Basic iron sulphate–a potential killer for pressure oxidation processing of refractory gold concentrates if not handled appropriately | |
CA2360704A1 (en) | Process of leaching a lateritic ore for preparing metal extraction | |
CN106566933B (en) | A method of cobalt content in the mixing slag in being produced for reducing nickel sulfate | |
CA2977456C (en) | Wet smelting method for nickel oxide ore | |
CN100355917C (en) | Recovery of platinum group metals | |
US4472359A (en) | Method of pressure leaching | |
KR20080102383A (en) | Supercritical oxidation process for the treatment of corrosive materials | |
CN106365177B (en) | A kind of method that flash distillation prepares ammonium nitrate concentrated solution | |
CN108530285A (en) | A kind of preparation of p-tert-butyl benzoic acid and post-processing approach | |
CN109457111A (en) | The method of salt Ore Leaching nickel cobalt extracted from laterite-nickel ore | |
US3365341A (en) | Nickel recovery process | |
US1757592A (en) | Autoclave and method of operating same | |
CN107574306A (en) | A kind of method that ambrose alloy cobalt is reclaimed from high iron solution | |
CN109487097A (en) | Coarse antimony refining removes the feeding device and its method of iron | |
AU2022204322B2 (en) | Alkaline oxidation process and device for treating refractory sulfide ore, in particular refractory gold ore | |
CN109896662A (en) | A kind of wastewater from chemical industry deliming technique |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
FZDE | Discontinued |