WO2011129395A1 - ニッケル酸化鉱石の湿式精錬プラント及びその操業方法 - Google Patents
ニッケル酸化鉱石の湿式精錬プラント及びその操業方法 Download PDFInfo
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- WO2011129395A1 WO2011129395A1 PCT/JP2011/059266 JP2011059266W WO2011129395A1 WO 2011129395 A1 WO2011129395 A1 WO 2011129395A1 JP 2011059266 W JP2011059266 W JP 2011059266W WO 2011129395 A1 WO2011129395 A1 WO 2011129395A1
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- 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
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- 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
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- 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
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
- C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
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- 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
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- 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 nickel oxide ore wet refining plant and an operation method thereof. More specifically, in the present invention, a nickel oxide ore wet refining plant having a plurality of processing facilities has a trouble that requires a part of the processing facilities to be shut down (hereinafter also simply referred to as “serious trouble”). In this case, the present invention relates to a nickel oxide ore wet refining plant capable of minimizing a reduction in throughput due to this serious trouble and an operation method thereof.
- This application claims priority on the basis of Japanese Patent Application No. 2010-094330 filed on Apr. 15, 2010 in Japan, and is incorporated into this application by reference to these applications.
- High-pressure acid leaching using sulfuric acid has attracted attention as a wet refining method for nickel oxide ore.
- This method does not include dry processing steps such as drying and roasting steps, and consists of a consistent wet process, which is advantageous in terms of energy and cost and improves the nickel quality to about 50 to 60% by weight.
- a nickel-cobalt mixed sulfide can be obtained.
- the high pressure acid leaching method for obtaining the nickel / cobalt mixed sulfide includes, for example, as shown in FIG. 3, a pretreatment step (1), a leaching step (2), a solid-liquid separation step (3), A neutralization process (4), a dezincification process (5), a sulfurization process (6), and a detoxification process (7) are included.
- the nickel oxide ore is crushed and classified into a slurry.
- sulfuric acid is added to the slurry obtained in the pretreatment step (1), and the mixture is stirred at 220 to 280 ° C. to perform high-temperature pressure acid leaching to obtain a leaching slurry.
- the leaching slurry obtained in the leaching step (2) is subjected to solid-liquid separation to obtain a leachate containing nickel and cobalt (hereinafter referred to as “crude nickel sulfate aqueous solution”) and the leaching residue. obtain.
- the neutralization step (4) the crude nickel sulfate aqueous solution obtained in the solid-liquid separation step (3) is neutralized.
- hydrogen sulfide gas is added to the crude nickel sulfate aqueous solution neutralized in the neutralization step (4) to precipitate and remove zinc as zinc sulfide.
- hydrogen sulfide gas is added to the dezincification final solution obtained in the dezincification step (5) to obtain a nickel / cobalt composite sulfide and a nickel poor solution.
- the detoxification process (7) the leaching residue generated in the solid-liquid separation process (3) and the nickel poor liquid generated in the sulfidation process (6) are detoxified (see, for example, Patent Document 1).
- the nickel oxide ore wet refining plant 100 (hereinafter simply referred to as “wet refining plant”) includes, for example, two series of processing equipment, that is, I series processing equipment and II series. And processing facilities.
- These two systems of processing equipment include a pretreatment section (1a, 1b) that performs the pretreatment process (1), a leaching section (2a, 2b) that performs the leaching process (2), and a solid-liquid separation process (3 )
- a pretreatment section (1a, 1b) that performs the pretreatment process (1)
- a leaching section (2a, 2b) that performs the leaching process (2)
- a solid-liquid separation process (3 ) To perform the solid-liquid separation unit (3a, 3b), the neutralization unit (4a, 4b) to perform the neutralization step (4), and the dezincification unit (5a, 5b) to perform the dezincification step (5) ), A sulfidizing section (6a, 6b) for executing the sulfiding step (6), and a detoxifying section (7a, 7b) for executing the detoxifying step (7).
- the two series of processing facilities include utility supply facilities 8a and 8b including a boiler, a water facility, and a power facility as shown in FIG.
- the two series of processing facilities include hydrogen sulfide supply facilities 10a and 10b, neutralizing agent supply facilities 12a and 12b, and flocculant supply facilities 14a and 14b, and processes for executing the respective steps. It consists of piping equipment such as liquid feed pipes that connect equipment sequentially.
- the utility supply facilities 8a and 8b, the hydrogen sulfide supply facilities 10a and 10b, the neutralizer supply facilities 12a and 12b, and the flocculant supply facilities 14a and 14b are also simply referred to as supply facilities.
- the steam, water and power from the utility supply facility 8a are supplied to the I series process processing equipment, and the steam, water and power from the utility supply equipment 8b are supplied to the II series process processing equipment.
- Hydrogen sulfide obtained by the hydrogen sulfide supply facilities 10a and 10b is supplied to the dezincification parts 5a and 5b and the sulfurization parts 6a and 6b.
- the neutralizing agent is supplied from the neutralizing agent supply facilities 12a and 12b to the neutralizing units 4a and 4b and the detoxifying units 7a and 7b.
- the flocculant is supplied to the solid-liquid separation units 3a, 3b and the neutralization units 4a, 4b.
- the piping facility is composed of utility supply pipes 9a and 9b, hydrogen sulfide supply pipes 11a and 11b, neutralizer supply pipes 13a and 13b, and coagulant supply pipes 15a and 15b.
- the main intermediate product is liquid or slurry. Therefore, in the operation of the hydrometallurgical plant 100, for example, if any one of steam, water, electric power, hydrogen sulfide, flocculant, and neutralizer is not supplied due to a serious boiler trouble, the hydrometallurgical plant 100 Generally, after the entire system is stopped and a serious trouble is solved or repaired, the entire hydrometallurgical plant 100 is restarted.
- this load fluctuates as an operation in which a certain load is applied to each process processing equipment and other equipment. Also, in the hydrometallurgical plant 100, the frequency of periodic suspension (periodic inspection) is increased or the suspension period is extended to inspect the facility and repair the facility as necessary. Sudden outbreaks are prevented.
- the hydrometallurgical plant 100 is usually provided with an emergency storage tank so as not to reduce the throughput when the lamp is down.
- the process load before the process in which the trouble has occurred is left as it is or the load is reduced, and excess process liquid is stored in the emergency storage tank. Further, after the trouble is solved, the process load is increased (ramped up), and the process liquid stored in the emergency storage tank together with the normal load is repeatedly processed. This makes it possible to achieve the processing target amount for each quarter or year.
- such an emergency evacuation response is effective when the time required for the recovery of the hydrometallurgical plant 100 is usually within 8 hours, for example, although it depends on the size of the emergency storage tank. However, if the time required for the restoration of the hydrometallurgical plant 100 exceeds 8 hours, the process liquid is stored up to the limit of the emergency storage tank, and the operation must be stopped.
- the inner surface of the drum washer's trommel on the same circumference that is perpendicular to the trommel's rotation axis, has a substantially rectangular cross-sectional shape, and satisfies the specific requirements.
- the nickel / cobalt mixed sulfide produced in the sulfide parts 6a and 6b adheres to the inner surface of the reaction vessel and forms a scale. There is a problem that it grows and the device becomes nonfunctional or destroyed.
- the sulfide parts 6a and 6b circulate and use as a seed crystal nickel sulfide corresponding to a nickel amount 4 to 6 times the amount of nickel in the final zinc removal solution from the dezincification parts 5a and 5b.
- a method for preventing the growth of scale has been proposed (see Patent Document 3).
- the above-mentioned trouble is taken as a representative example because of the process-specific reason of using hard ore particles as a slurry and generating nickel-cobalt mixed sulfide that easily adheres to the inner surface of the reaction vessel. Various troubles occur frequently. Therefore, it is general that the operation rate of the actual wet refining plant 100 is not so high.
- the time required for lowering the temperature to normal temperature and decreasing the pressure to normal pressure and the time required for increasing and increasing the pressure to a predetermined temperature and pressure are summed up to one to two days.
- time hereinafter referred to as “preparation time”. That is, in the leaching sections 2a and 2b, when the processing equipment is stopped, it takes a lot of preparation time to bring down the processing equipment and then start up the processing equipment again.
- preparation time occurs once a month, and the production is reduced by about 5% in a simple calculation on the 30th operating day of the month as compared with the case where continuous operation can be performed without any trouble. Such a reduction in production is a major problem in actual operation.
- the present invention has been proposed in view of the above-described problems of the prior art, and in a hydrometallurgy plant having two or more processing facilities, a utility supply facility, a hydrogen sulfide supply facility, and a neutralization facility for a certain processing facility.
- the present invention provides a nickel oxide ore hydrometallurgical refining plant and a method of operating the same that can minimize a decrease in throughput even when a serious trouble occurs in at least one of the agent supply facility and the flocculant supply facility. Objective.
- the present inventors have solved the above problems by connecting utility supply facilities, hydrogen sulfide supply facilities, and chemical supply facilities among the processing facilities of each series.
- the present invention has been found out that it can be solved.
- the nickel oxide ore hydrometallurgical plant according to the present invention includes a pretreatment unit, a leaching unit, a solid-liquid separation unit, a neutralization unit, a dezincing unit, a sulfurization unit, and a detoxification unit, Utility supply equipment for supplying a utility including steam, irrigation water and electric power to the processing unit, the leaching unit, the solid-liquid separation unit, the neutralization unit, the dezincification unit, the sulfurization unit, and the detoxification unit, Hydrogen sulfide supply equipment for supplying hydrogen sulfide to the dezincification section and the sulfurization section, a flocculant supply equipment for supplying a flocculant to the solid-liquid separation section and the neutralization section, the neutralization section, and the detoxification section
- a nickel oxide ore hydrorefining plant having two or more series of processing facilities including a neutralizing agent supply facility for supplying a neutralizing agent to each other, the utility supply facilities in each series, the hydrogen sulfide supply facility
- each of the connection facilities is characterized in that the supply facilities are connected to each other at the most upstream portion where the utility, the hydrogen sulfide, the flocculant, and the neutralizing agent are supplied.
- the two or more series of processing facilities have the same level of processing capability. Further, the number of the series is two series. Further, the connection facility has an opening / closing mechanism.
- the operation method of the nickel oxide ore wet refining plant according to the present invention is characterized by using the nickel oxide ore wet refining plant.
- the operation method of the nickel oxide ore wet refining plant according to the present invention is at least one of the utility supply facility, the hydrogen sulfide supply facility, the flocculant supply facility, and the neutralizer supply facility in each series.
- the operation is stopped, the operating degree of the processing equipment of each series is lowered.
- each supply facility is connected by a connecting facility in a hydrometallurgical plant, even if a serious trouble occurs in at least one supply facility of a certain processing facility, the stoppage of the processing facility is minimized.
- the reduction in the processing amount can be minimized. Therefore, in the present invention, the operation of the hydrometallurgical plant can be continued without stopping the leaching section unless a serious trouble occurs simultaneously in the same supply equipment of the treatment equipment of each series. Can be minimized.
- FIG. 1 is a schematic view schematically showing a wet refining plant of the present invention.
- FIG. 2 is a schematic view schematically showing the wet refining plant of the present invention.
- FIG. 3 is a flowchart showing a schematic process of the high pressure acid leaching method.
- FIG. 4 is a schematic view schematically showing a conventional hydrometallurgical plant.
- FIG. 5 is a schematic view schematically showing a conventional hydrometallurgical plant.
- the hydrometallurgical plant according to the present invention has two or more series of processing facilities for performing a pretreatment process, a leaching process, a solid-liquid separation process, a neutralization process, a dezincification process, a sulfurization process, and a detoxification process.
- the hydrometallurgical plant has two or more series of processing facilities, for example, the processing amount of nickel oxide ore as a raw material can be increased and the production amount of nickel / cobalt mixed sulfide can be increased.
- the hydrometallurgical plant 20 has two series of processing equipment, that is, I series processing equipment and II series processing equipment.
- These treatment facilities include a pretreatment section (1a, 1b), a leaching section (2a, 2b), a solid-liquid separation section (3a, 3b), a neutralization section (4a, 4b), and a dezincing section ( 5a, 5b), a sulfur treatment section (6a, 6b), and a detoxification section (7a, 7b).
- the pretreatment unit 1 the leaching unit 2, the solid-liquid separation unit 3, the neutralization unit 4, the dezincing unit 5, and the sulfidizing unit 6 except for the case where each series of processing facilities is individually described.
- a detoxification unit 7 it is referred to as a detoxification unit 7.
- the pretreatment unit 1 is composed of, for example, pretreatment equipment such as a pulverizer, and executes a pretreatment process in which nickel oxide ore as a raw material is crushed and classified into a slurry.
- pretreatment equipment such as a pulverizer
- the nickel oxide ore for example, so-called laterite ore such as limonite ore and saprolite ore is used.
- the leaching unit 2 is a leaching step in which sulfuric acid is added to the slurry obtained in the pretreatment unit 1, stirred at 220 to 280 ° C. and acid leached at high temperature and pressure to obtain a leaching slurry composed of a leaching residue and a leachate.
- a high-temperature pressurized container autoclave
- leaching as a sulfate such as nickel and cobalt is leached by, for example, the leaching reaction represented by the following formulas (1) to (5) and the high-temperature thermal hydrolysis reaction. Immobilization of iron sulfate as hematite is performed.
- the leaching slurry obtained usually contains divalent and trivalent iron ions in addition to nickel, cobalt and the like.
- the solid-liquid separation unit 3 performs a solid-liquid separation step of solid-liquid separation of the leaching slurry obtained in the leaching unit 2 to obtain a leaching solution (crude nickel sulfate aqueous solution) containing nickel and cobalt and a leaching residue.
- the solid-liquid separation step is effective for separating and recovering nickel or the like that adheres to the leaching residue and is discarded from the leaching slurry formed in the leaching section 2 into a crude nickel sulfate aqueous solution.
- the solid-liquid separation unit 3 performs solid-liquid separation with a thickener that is a solid-liquid separation facility, using a flocculant supplied from the flocculant supply facilities 14a and 14b described later. .
- the slurry is diluted with the cleaning liquid, and the leaching residue is concentrated as a thickener sediment, so that the nickel content adhering to the leaching residue can be reduced according to the degree of dilution.
- the flocculant for example, an anionic flocculant is used.
- the neutralization part 4 is comprised by neutralization facilities, such as a neutralization tank, for example, and performs the neutralization process which neutralizes the rough
- a neutralizing agent is added to form a neutralized starch slurry containing trivalent iron and a nickel recovery mother liquor. Thereby, in the neutralization part 4, while neutralizing an excess acid, the trivalent iron ion which remains in a solution can be removed.
- the neutralizing agent for example, calcium carbonate is used.
- the pH in the neutralization step is 3.2 to 3.8. By setting the pH within such a range, it is possible to prevent the generation of nickel hydroxide from increasing.
- the temperature in the neutralization step is preferably 50 to 80 ° C. When the temperature is lower than 50 ° C., the starch becomes fine and adversely affects the solid-liquid separation process. When the temperature is higher than 80 ° C., the corrosion resistance of the apparatus material is reduced and the energy cost for heating is increased.
- the dezincification part 5 adds the hydrogen sulfide gas supplied from the hydrogen sulfide supply equipment 10a, 10b to the crude nickel sulfate aqueous solution neutralized by the neutralization part 4, and precipitates and removes zinc as zinc sulfide, thereby removing the dezincing solution.
- a dezincification step is carried out to obtain
- the sulfidation unit 6 is a sulfidation obtained by adding hydrogen sulfide gas supplied from the hydrogen sulfide supply facilities 10a and 10b to the dezincification solution obtained in the dezincification unit 5 to obtain a nickel / cobalt mixed sulfide and a nickel poor solution. Execute the process.
- This nickel poor solution contains a small amount of nickel and cobalt, which are recovery losses, in addition to impurities such as iron, magnesium, and manganese that are contained without being sulfided.
- the harmless part 7 is harmless that renders the leaching residue generated in the solid-liquid separation part 3 and the nickel poor liquid generated in the sulfide part 6 harmless by the neutralizer supplied from the neutralizer supply equipment 12a, 12b. Execute the conversion process. A high nickel yield can be achieved in the hydrometallurgical plant 20 by the above process processing equipment.
- the hydrometallurgical plant 20 includes utility supply facilities 8a and 8b, hydrogen sulfide supply facilities 10a and 10b, neutralizer supply facilities 12a and 12b, and flocculant supply facilities 14a and 14b. And have.
- these supply facilities will be referred to as a utility supply facility 8, a hydrogen sulfide supply facility 10, a neutralizing agent supply facility 12, and a flocculant supply facility 14, unless the processing facilities of each series are individually described.
- the utility supply facility 8 includes, for example, a boiler, a water supply facility, and a power facility.
- the boiler obtains steam for controlling the reaction temperature of each process equipment.
- the steam obtained from the boiler is supplied to the above-described process processing equipment as necessary.
- the water facility is a facility for supplying water used in each process treatment facility.
- the water obtained in the water facility is supplied to the above-described process equipment as necessary.
- the electric power equipment is equipment for supplying electric power used in each process processing equipment.
- the electric power obtained by the power equipment is supplied to the above-described process processing equipment as necessary.
- the utility supply equipment 8a and the I-series process processing equipment are connected by a utility supply pipe 9a. Further, the utility supply facility 8b and the II-series process processing facility are connected by a utility supply pipe 9b. Further, the utility supply pipe 9 a and the utility supply pipe 9 b are connected by a utility connection facility 16.
- the utility connection facility 16 is configured similarly to the utility supply pipes 9a and 9b, for example.
- the utility connection facility 16 connects the utility supply pipe 9a and the utility supply pipe 9b at the most upstream part of the utility (steam, water and electric power) supply.
- the utility connection facility 16 connects, for example, the vicinity of the connection portion between the utility supply pipe 9a and the utility supply facility 8a, the vicinity of the connection portion between the utility supply piping 9b and the utility supply facility 8b.
- the utility supply facility 8b can be efficiently supplied to each series of process equipment.
- the hydrogen sulfide supply facility 10 produces hydrogen sulfide gas, and supplies the produced hydrogen sulfide gas to the dezincification section 5 and the sulfurization section 6 as necessary.
- the hydrogen sulfide supply facility 10a, the dezincification part 5a and the sulfide part 6a are connected by a hydrogen sulfide supply pipe 11a.
- the hydrogen sulfide supply facility 10b, the dezincification part 5b and the sulfide part 6b are connected by a hydrogen sulfide supply pipe 11b.
- the hydrogen sulfide supply pipe 11 a and the hydrogen sulfide supply pipe 11 b are connected by a hydrogen sulfide connection facility 17.
- the hydrogen sulfide connection facility 17 is configured in the same manner as the hydrogen sulfide supply pipe 11, for example.
- the hydrogen sulfide connection facility 17 connects the hydrogen sulfide supply pipe 11a and the hydrogen sulfide supply pipe 11b at the most upstream part of the supply of hydrogen sulfide, so that the hydrogen sulfide can be shared between the respective process processing facilities.
- the hydrogen sulfide connection facility 17 connects, for example, the vicinity of the connection portion between the hydrogen sulfide supply facility 10a and the hydrogen sulfide supply pipe 11a and the vicinity of the connection portion between the hydrogen sulfide supply facility 10b and the hydrogen sulfide supply pipe 11b.
- hydrogen sulfide is supplied from the hydrogen sulfide supply facility 10b (10a) to the respective process treatment facilities via the hydrogen sulfide connection facility 17. It can be supplied efficiently.
- the neutralizing agent supply facility 12 supplies the neutralizing agent described above to the neutralizing unit 4 and the detoxifying unit as necessary.
- the neutralizing agent supply facility 12a, the neutralizing part 4a and the detoxifying part 7a are connected by a neutralizing agent supply pipe 13a.
- the neutralizing agent supply equipment 12b, the neutralization part 4b, and the detoxification part 7b are connected by the neutralizing agent supply piping 13b.
- the neutralizing agent supply pipe 13 a and the neutralizing agent supply pipe 13 b are connected by a neutralizing agent connection facility 18.
- the neutralizing agent connection facility 18 is configured in the same manner as the neutralizing agent supply pipe 13, for example.
- the neutralizing agent connection facility 18 connects these neutralizing agent supply piping 13a and the neutralizing agent supply piping 13b at the most upstream portion of the neutralizing agent supply, so that the neutralizing agent is used in each series of process treatment facilities. Can be shared with each other. That is, the neutralizing agent connection facility 18 is, for example, near the connection portion between the neutralizing agent supply facility 12a and the neutralizing agent supply piping 13a, and near the connection portion between the neutralizing agent supply facility 12b and the neutralizing agent supply piping 13b. And Thereby, for example, even when a serious trouble occurs in the neutralizing agent supply facility 12a, the neutralizing agent is efficiently supplied from the neutralizing agent supply facility 12b to the process treatment facility of each series via the neutralizing agent connection facility 18. Can be supplied to.
- the flocculant supply equipment 14 supplies the above-described flocculant to the solid-liquid separation unit 3 and the neutralization unit 4 as necessary.
- the flocculant supply equipment 14a, the solid-liquid separation unit 3a, and the neutralization unit 4a are connected by a flocculant supply pipe 15a.
- the flocculant supply equipment 14b, the solid-liquid separation unit 3b, and the neutralization unit 4b are connected by a flocculant supply pipe 15b.
- the coagulant supply pipe 15 a and the coagulant supply pipe 15 b are connected by the coagulant connecting equipment 19.
- the flocculant connection facility 19 is configured in the same manner as the flocculant supply pipe 15, for example.
- the flocculant connection facility 19 connects the flocculant supply pipe 15a and the flocculant supply pipe 15b at the most upstream portion of the flocculant supply, thereby allowing the flocculant to be shared by each series of process processing equipment. . That is, the flocculant connection facility 19 connects, for example, the vicinity of the connection portion between the flocculant supply facility 14a and the flocculant supply piping 15a and the vicinity of the connection portion between the flocculant supply facility 14a and the flocculant supply piping 15a. Thereby, for example, even when a serious trouble occurs in the flocculant supply facility 14a, the flocculant is efficiently supplied from the flocculant supply facility 14b to the process processing facilities of each series via the flocculant connection facility 19. Can do.
- the above-described connecting equipment has an opening / closing mechanism (blocking mechanism) for blocking, adjusting, etc., the amount of the moving supply.
- the utility connection facility 16 is preferably provided with a control valve for steam and water, and a switch for electricity.
- Each connection facility can operate the wet refining plant 20 having two processing facilities as an independent single processing facility by operating the opening / closing mechanism and releasing the connection as necessary. .
- the hydrometallurgical plant 20 includes a connection facility having an opening / closing mechanism, so that it is necessary to process raw materials having different compositions, or when it is necessary to change processing conditions even with raw materials having the same composition, It becomes possible to respond preferably. Also, the wet smelting plant 20 can continue operation by adjusting the amount of feed that is moved by the opening and closing mechanism, minimizing the reduction in throughput due to the occurrence of serious troubles. Can be fast.
- the hydrometallurgical plant 20 has many items to consider, such as the number of years in which nickel oxide ore can be mined, the water supply capacity indispensable for operation, and the margin of the plant site. Preferably have similar processing capabilities. Thereby, when a serious trouble occurs in the wet refining plant 20 as will be described in detail later, it is possible to easily control the supply processing equipment of each series and the process processing equipment of each series. Moreover, since the operation / operation manual in actual operation in each individual facility can be substantially the same even if it is in another series, it is possible to reduce the education cost of workers. Furthermore, each processing facility has the same level of processing capacity, so it is possible to reduce pochamis and human errors that misunderstand the processing capacity of other series of processing facilities, and to allow workers to assemble their work structure. Can do.
- each supply facility is connected by a connection facility, for example, even when a serious trouble occurs in at least one supply facility of a certain series of processing facilities, By supplying the supply to the other series of process processing equipment, it is possible to prevent the operation of the leaching unit 2 from being stopped. Therefore, in the hydrometallurgy plant 20, the operation can be continued without stopping the leaching unit 2 unless a serious trouble occurs simultaneously in the same supply equipment of each series, so that the reduction in the throughput in the leaching process is minimized. Can be limited.
- one of the utility supply facility 8a and the utility supply facility 8b of the wet refining plant 20 causes the above-mentioned serious trouble (trouble that requires a part of the processing facility to be shut down), and the steam supply facility.
- the operating capacity of the utility supply facility in which no serious trouble has occurred is increased as compared with that during normal operation.
- the operating capacity (operation load) of the utility supply facility 8b that has been operated in one lung is greater than that during normal operation. Raise.
- the necessary amount of steam can be stabilized in each process treatment equipment without overloading the utility supply equipment 8b. Can be supplied.
- the total operating capacity of each series of processing equipment is set to 120%, and at least the lower limit of the operating capacity of the leaching unit 2 is set to 50%.
- the operating rate of the leaching part 2 can be maintained at 50% of normal time. Therefore, in the hydrometallurgical plant 20, it is possible to prevent the occurrence of the above-described preparation time, which is a cause of a serious problem in actual operation, without stopping the brewing unit 2 that has been forced to stop.
- the total operating capacity of the processing facilities of each series is 120%.
- the normal operating capacity of a series of processing facilities of each series is 100%, the total of these operating capacities is It means 120%.
- the operating capacities of the I-series processing equipment and the II-series processing equipment are 60% of normal times.
- the operating capacity of the I-series processing equipment is 50%
- the operating capacity of the II-series processing equipment is 70%
- the operating capacity of the I-series processing equipment is 70%
- the operating capacity may be 50%.
- the leaching unit 2 can be prevented from being stopped unless serious troubles occur at the same time in the same supply equipment of each series.
- the operation can be continued without stopping. Therefore, in the hydrometallurgical plant 20 according to the present embodiment, it is possible to minimize the reduction in the processing amount in the leaching process.
- the hydrometallurgical plant 20 it is understood that there is a low possibility that a serious trouble will occur simultaneously in the same supply equipment in all series, and therefore it is possible to substantially prevent the processing equipment from being stopped due to a serious trouble.
- the wet refining plant 20 having two series of processing facilities has been described as an example.
- a wet refining plant having three or more series of processing facilities may be applied to the present invention.
- the operating rate in the case of a hydrometallurgical plant having three series of processing facilities, even if only one system is operating among the supply facilities of each supply, by setting the operating rate to 33%, approximately 1 / 3 operation can be continued, and when the two systems are operating, the operating rate should be 66%. In this way, by increasing the number of series, it is possible to reduce the excess load per facility for the facility in the process area where the production must be increased.
- the nickel oxide ore hydrometallurgical plant described above may be used in combination with an emergency storage tank (for example, a tank capable of storing utility for 8 hours).
- an emergency storage tank for example, a tank capable of storing utility for 8 hours.
- the utility stored in the emergency storage tank may be used in combination (100%).
- the operating capacity of the utility supply facility 8b that has been in the above-described one-lung operation is left as it is during normal operation (100%), and the total operating capacity of a series of processing facilities in each series is 100%.
- at least the lower limit of the operating capacity of the leaching unit 2 may be set to 50%.
- the operating capacity of a series of processing equipment in each series may be 50%, and the utility stored in the emergency storage tank described above may be used in combination with 100% as the total.
- the upper limit of the operating capacity of each supply facility in the above-described wet refining plant 20 may be a value larger than 120%, for example, 140%, if possible.
- the total operating capacity of the processing facilities of each series is set to 140%, and the leaching section What is necessary is just to set so that the minimum of the operating capability of 2 may be 50%.
- the hydrometallurgical plant 20 includes a detection unit that detects a serious trouble in each of the above-described supply facilities, and an operating capability of each supply facility and an opening / closing mechanism of a connected facility when the serious trouble is detected by the detection unit. And a control unit for controlling. That is, in the hydrometallurgical plant, the detection unit is connected to each of the supply facilities described above. Further, the control unit is connected to each of the detection units, the supply facilities, and the open / close mechanisms of the connection facilities described above.
- the detection unit detects, for example, whether a serious trouble has occurred in the utility supply facility 8a and the steam supply facility has stopped.
- the detection unit supplies a detection signal to that effect to the control unit.
- the control unit performs control so that the operation capability of the utility supply facility 8b that is in the one-lung operation is increased by 120% from that during normal operation.
- the control unit controls the operating capacity of the process processing equipment so that the operating capacities of the above-described I-series processing equipment and II-series processing equipment are 60% of the normal time, respectively. Controls the operation of the opening and closing mechanism.
- Example 1 ⁇ Operating conditions>
- the wet refining plant 20 of the present invention shown in FIGS. 1 and 2 was used, and the operation was performed for 7 months.
- the hydrometallurgical plant 20 used in Example 1 includes a pretreatment unit 1, a leaching unit 2, a solid-liquid separation unit 3, a neutralization unit 4, a dezincification unit 5, a sulfurization unit 6, and a detoxification unit. 7 and 2 series of process processing equipment.
- the wet refining plant 20 of the present invention includes a utility supply facility 8, a hydrogen sulfide supply facility 10, a neutralizer supply facility 12, and a flocculant supply facility 14.
- hydrometallurgical plant 20 is provided with a utility connection facility 16, a hydrogen sulfide connection facility 17, a neutralizing agent connection facility 18 and a flocculant connection facility 19 at the most upstream part of the supply of each supply means, and the supply facilities of each series The operation was carried out by concatenating.
- the operating capacity of the supply facility in which no serious trouble has occurred is increased to 120%, and a series of processes of each series is performed.
- the total operating capacity of the facilities was set to 120%, and the lower limit was set to 50% or more.
- Comparative Example 1 ⁇ Operating conditions>
- a wet refining plant to which the present invention was not applied that is, a wet refining plant shown in FIGS. 4 and 5 was used, and operation was performed for 7 months. That is, in Comparative Example 1, the utility supply facility 8, the hydrogen sulfide supply facility 10, the neutralizing agent supply facility 12, and the flocculant supply facility 14 are supplied at the most upstream part of the supply as in Example 1. The operation was carried out without connecting the supply facilities of each series without connecting facilities to connect things in a shareable manner.
- Example 1 since all the supply equipment in each series of the hydrorefining plant 20 has the above-mentioned connection equipment, even when a serious trouble occurs in the supply equipment, the same supply of other series We were able to operate the equipment. Thereby, since the operation can be continued without stopping the leaching unit 2, it was confirmed that the reduction of the processing amount in the leaching process can be minimized.
- the present invention is not limited to a nickel oxide ore hydrometallurgical plant, but can be applied to a slurry containing hard particles and a plant accompanied by the formation of precipitates that easily adhere to the surface of the apparatus, and its industrial value is high.
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Abstract
Description
本出願は、日本国において2010年4月15日に出願された日本特許出願番号2010-094330を基礎として優先権を主張するものであり、これらの出願を参照することにより、本出願に援用される。
1.湿式精錬プラント
1-1.工程処理設備
1-2.供給設備
2.重大トラブルが発生した場合の湿式精錬プラントの操業(運転)方法
3.他の実施の形態
4.実施例
本発明に係る湿式精錬プラントは、前処理工程、浸出工程、固液分離工程、中和工程、脱亜鉛工程、硫化工程及び無害化工程を実行する一連の処理設備を2系列以上有する。このように湿式精錬プラントが一連の処理設備を2系列以上有することにより、例えば、原料であるニッケル酸化鉱の処理量を増加してニッケル・コバルト混合硫化物の生産量を増加させることができる。
前処理部1は、例えば粉砕機等の前処理設備で構成され、原料となるニッケル酸化鉱石を解砕分級してスラリーとする前処理工程を実行する。ニッケル酸化鉱石としては、例えば、リモナイト鉱やサプロライト鉱等のいわゆるラテライト鉱が用いられる。
MO+H2SO4→MSO4+H2O (1)
(式中Mは、NI、Co、Fe、Zn、Cu、Mg、Cr、Mn等を表す。)
2Fe(OH)3+3H2SO4→Fe2(SO4)3+6H2O (2)
FeO+H2SO4→FeSO4+H2O (3)
2FeSO4+H2SO4+(1/2)O2→Fe2(SO4)3+H2O(4)
Fe2(SO4)3+3H2O→Fe2O3+3H2SO4 (5)
湿式精錬プラント20は、図1、図2に示すように、ユーティリティー供給設備8a、8bと、硫化水素供給設備10a、10bと、中和剤供給設備12a、12bと、凝集剤供給設備14a、14bとを有する。以下、これらの供給設備は、各系列の処理設備を個別に説明する場合を除いて、ユーティリティー供給設備8、硫化水素供給設備10、中和剤供給設備12及び凝集剤供給設備14という。
次に、重大トラブルが発生した場合の湿式精錬プラント20の操業方法の一例について説明する。以下の説明では、便宜的に上述した図1及び図2に示す湿式精錬プラント20を用いた場合を例にして説明する。
上記説明では、一連の処理設備を2系列有する湿式精錬プラント20を例にして説明したが、一連の処理設備を3系列以上有する湿式精錬プラントを本発明に適用してもよい。例えば、一連の処理設備を3系列有する湿式精錬プラントの場合には、各供給物の供給設備のうち、1系列しか稼動していなくても、稼働率を33%とすることで、約1/3の稼動を継続することが可能であり、2系列が稼動している場合は、稼働率を66%にすればよいことになる。このように、系列数を多くすることにより、増産しなければならない工程領域の設備にかかる1設備あたりの過剰負荷分を小さくすることができる。
<4.実施例>
<操業条件>
実施例1では、図1、2に示す本発明の湿式精錬プラント20を使用し、7ヶ月間の操業を実施した。
ユーティリティーについては、ユーティリティー供給設備8に合計4回のトラブルが発生した。その結果、浸出部2の停止時間は、ゼロであった。硫化水素については、硫化水素供給設備10に34回のトラブルが発生した。その結果、浸出部2の停止時間はゼロであった。中和剤については、中和剤供給設備12に1回のトラブルが発生した。その結果、浸出部2の停止時間は、ゼロであった。凝集剤については、凝集剤供給設備14にトラブルは発生しなかった。なお、いずれのトラブルでも、I系列の処理設備と、II系列の処理設備との双方に同時に重大トラブルが発生することはなかった。
<操業条件>
比較例1では、本発明を適用しない湿式精錬プラント、すなわち、図4、図5に示す湿式精錬プラントを使用し、7ヶ月間の操業を実施した。すなわち、比較例1では、ユーティリティー供給設備8と、硫化水素供給設備10と、中和剤供給設備12と、凝集剤供給設備14とについては、実施例1のように供給の最上流部分で供給物を互いに共有可能に連結する連結設備を設けず、各系列の供給設備を連結することなく操業を実施した。
ユーティリティー(蒸気、用水、電気)については、ユーティリティー供給設備8に合計3回のトラブルが発生した。その結果、浸出部2の停止時間は、235時間であった。硫化水素については、硫化水素供給設備10に30回のトラブルが発生した。その結果、浸出部2の停止時間は、98時間であった。中和剤については、中和剤供給設備12に1回のトラブルが発生した。その結果、浸出部2の停止時間は、4時間であった。凝集剤については、凝集剤供給設備14にトラブルは発生しなかった。なお、いずれのトラブルでも、I系列、II系列の双方に同時にトラブルが発生することはなかった。
Claims (7)
- 前処理部、浸出部、固液分離部、中和部、脱亜鉛部、硫化部及び無害化部を有する工程処理設備と、
前記前処理部、前記浸出部、前記固液分離部、前記中和部、前記脱亜鉛部、前記硫化部及び前記無害化部に、蒸気、用水及び電力を含むユーティリティーを供給するユーティリティー供給設備と、
前記脱亜鉛部及び前記硫化部に硫化水素を供給する硫化水素供給設備と、
前記固液分離部及び前記中和部に凝集剤を供給する凝集剤供給設備と、
前記中和部及び前記無害化部に中和剤を供給する中和剤供給設備と
を含む一連の処理設備を2系列以上有するニッケル酸化鉱の湿式精錬プラントにおいて、
各系列における前記ユーティリティー供給設備同士、前記硫化水素供給設備同士、前記凝集剤供給設備同士及び前記中和剤供給設備同士は、各々前記ユーティリティー、前記硫化水素、前記凝集剤及び前記中和剤を共有可能に連結する連結設備をさらに備えることを特徴とするニッケル酸化鉱石の湿式精錬プラント。 - 前記連結設備は、前記各供給設備が前記ユーティリティー、前記硫化水素、前記凝集剤及び前記中和剤を供給する最上流部分で、該各供給設備を連結することを特徴とする請求項1記載のニッケル酸化鉱石の湿式精錬プラント。
- 前記2系列以上の処理設備は、それぞれ同程度の処理能力を有することを特徴とする請求項1又は2記載のニッケル酸化鉱石の湿式精錬プラント。
- 前記系列の数は、2系列であることを特徴とする請求項1乃至3のいずれか1項記載のニッケル酸化鉱石の湿式精錬プラント。
- 前記連結設備は、開閉機構を有することを特徴とする請求項1乃至4のいずれか1項記載のニッケル酸化鉱石の湿式精錬プラント。
- 請求項1乃至5項のいずれか1項記載のニッケル酸化鉱石の湿式精錬プラントを使用することを特徴とするニッケル酸化鉱石の湿式精錬プラントの操業方法。
- 各系列における前記ユーティリティー供給設備、前記硫化水素供給設備、前記凝集剤供給設備及び前記中和剤供給設備のうち、少なくともいずれか1つの運転が停止した場合には、他の系列の該供給設備を通常の操業度以上で操業し、前記各系列の処理設備の操業度を下げることを特徴とする請求項6記載のニッケル酸化鉱石の湿式精錬プラントの操業方法。
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EP11768916.6A EP2559776A4 (en) | 2010-04-15 | 2011-04-14 | APPARATUS FOR HOT-MELTING LATERITNICKELERZ AND OPERATING METHOD THEREFOR |
US13/639,788 US20130207325A1 (en) | 2010-04-15 | 2011-04-14 | Wet smelting plant for nickel oxide ore and method of operating the same |
AU2011241550A AU2011241550B2 (en) | 2010-04-15 | 2011-04-14 | Plant for wet smelting of laterite nickel ore and method of operating same |
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US9945007B2 (en) | 2012-03-06 | 2018-04-17 | Sumitomo Metal Mining Co., Ltd. | Dezincification plant, method for operating dezincification plant, and hydrometallurgical method for nickel oxide ore |
EP2881364A4 (en) * | 2012-07-31 | 2016-03-16 | Sumitomo Metal Mining Co | PRODUCTION PLANT FOR SULFUR HYDROGEN GAS AND METHOD FOR RECOVERY AND USE OF SULFUR HYDROGEN GAS |
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JP2014074233A (ja) * | 2013-12-05 | 2014-04-24 | Sumitomo Metal Mining Co Ltd | 中和処理プラント |
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EP2559776A1 (en) | 2013-02-20 |
JP2011225908A (ja) | 2011-11-10 |
AU2011241550A1 (en) | 2012-11-01 |
AU2011241550B2 (en) | 2015-07-02 |
JP4888578B2 (ja) | 2012-02-29 |
EP2559776A4 (en) | 2015-11-18 |
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