WO2013105454A1 - フラッシュベッセル及びその運転方法 - Google Patents
フラッシュベッセル及びその運転方法 Download PDFInfo
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- WO2013105454A1 WO2013105454A1 PCT/JP2012/083948 JP2012083948W WO2013105454A1 WO 2013105454 A1 WO2013105454 A1 WO 2013105454A1 JP 2012083948 W JP2012083948 W JP 2012083948W WO 2013105454 A1 WO2013105454 A1 WO 2013105454A1
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/04—Pressure vessels, e.g. autoclaves
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/008—Feed or outlet control devices
-
- 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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- 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
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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
- C22B3/04—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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00182—Controlling or regulating processes controlling the level of reactants in the reactor vessel
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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 flash vessel and a method for operating the same. More specifically, the raw slurry is leached under high temperature and high pressure in an autoclave (high pressure reaction vessel), and then the leached slurry is cooled to a normal temperature and a normal pressure.
- the present invention relates to a flash vessel and a method for operating the same in a high-pressure acid leaching process including a pressure-decreasing vessel.
- iron as the main impurity is leached in the form of hematite (Fe 2 O 3 ) by controlling the oxidation-reduction potential and temperature of the leaching solution in the pressure leaching reactor in the leaching step.
- nickel and cobalt can be leached selectively with respect to iron, so that there is a very great merit.
- a high-pressure acid leaching method using an autoclave is adopted as a hydrometallurgical method of nickel oxide ore, and the raw slurry is leached under high temperature and high pressure in an autoclave, and then the leached slurry is cooled and depressurized.
- the high-pressure acid leaching process including, usually, the liquid level measurement in the flash vessel is measured by a sensor directly attached to the flash vessel container.
- the flash vessel 100 includes a cylindrical body portion 101 having a bottom, and a slurry is applied to a ceiling portion 102 where the upper portion of the body portion 101 is closed.
- An inlet 103 and a steam outlet 105 are provided, and a slurry outlet 104 is provided in the body 101.
- the slurry charging inlet 103 is provided with a slurry charging pipe 113 for charging the leached slurry (hereinafter simply referred to as “slurry”) lowered to a predetermined temperature and a predetermined pressure into the flash vessel 100.
- a slurry discharge pipe 114 for discharging the slurry charged in the flash vessel 100 is connected to the rally discharge port 104, and a flash vessel 105 is connected to the steam discharge port 105 as the slurry is charged.
- a steam discharge pipe 115 for collecting steam generated in 100 is connected.
- a slurry discharge valve 116 is installed in the slurry discharge pipe 114 connected to the slurry discharge port 104.
- the leached slurry that has been lowered to a predetermined temperature and a predetermined pressure (hereinafter, simply referred to as “slurry”) is charged through the slurry inlet 103, and the flash vessel 100 is filled with the slurry.
- the charged slurry is discharged from the slurry discharge port 104, and the steam generated as the slurry is charged is discharged from the vapor discharge port 105.
- the liquid level measurement result in the flash vessel measured by the liquid level sensors 120A and 120B is used.
- the slurry discharge valve When the liquid level is measured by the upper and lower liquid level sensors 120A and 120B, when the liquid level rises and the liquid level sensor 120A installed at the upper limit of the liquid level detects the liquid level, the slurry discharge valve The slurry is discharged when 116 is opened and the slurry staying in the flash vessel 100 is discharged, and when the liquid level is lowered and the liquid level sensor 120B installed at the lower limit of the liquid level cannot detect the liquid level. The valve 116 is closed and the discharge of the slurry from the flash vessel 100 is stopped. As a result, the slurry liquid level in the flash vessel 100 is controlled between the upper limit and the lower limit.
- the discharge amount of the slurry staying in the flash vessel 100 is increased by increasing the valve opening of the slurry discharge valve 116. Further, when the liquid level becomes lower than the control liquid level, the discharge of the slurry from the flash vessel 100 is suppressed by decreasing the valve opening degree of the slurry discharge valve 116.
- the leaching reaction in the high-pressure acid leaching step is controlled not only by temperature but also by leaching reaction control factors (pH, oxidation-reduction potential) by the leaching agent.
- leaching reaction control factors pH, oxidation-reduction potential
- the pressure in the autoclave is not directly controlled because it is performed at the oxidation-reduction potential in the leachate, and is not necessarily stable during the leaching operation or It is not constant and varies depending on the amount of chlorine gas injected by controlling the redox potential.
- the pressure in the autoclave is due to the saturated vapor pressure accompanying the temperature.
- a high-pressure acid leaching method using an autoclave has been adopted as a wet smelting method for nickel oxide ore.
- an ore slurry containing ore having a predetermined slurry concentration of 2 mm or less is prepared using a pulverization facility and a sieving facility.
- the ore slurry is then supplied to the high pressure acid leaching process.
- the ore slurry is heated and boosted stepwise by a preheater (temperature rising and pressure increasing equipment), and then supplied to the autoclave.
- a preheater temperature rising and pressure increasing equipment
- the leaching slurry is supplied from the autoclave to a flash vessel that lowers and lowers the temperature of the leached slurry to room temperature and normal pressure, and the temperature is lowered and lowered stepwise. Then, it is separated into a leaching residue and a leachate through a pre-neutralization step for neutralizing free sulfuric acid in the leachate, a solid-liquid separation step composed of a multi-stage thickener, and the like.
- the adoption of the flash vessel in the high-pressure acid leaching step fills the gap in operating conditions between the autoclave and the next step in the high-pressure acid leaching step. That is, as the leaching condition of the autoclave, a temperature of about 200 to 300 ° C. is usually selected in order to obtain a high leaching rate of nickel and cobalt.
- the subsequent pre-neutralization step or solid-liquid separation step is usually operated under conditions of atmospheric pressure from the viewpoint of safety and economy. Therefore, in the flash vessel, the temperature is lowered and lowered while recovering the pressurized steam stepwise from the high-temperature and high-pressure slurry after leaching.
- piping for supplying the leaching slurry from the autoclave to the flash vessel piping for supplying the recovered steam to the preheater of the ore slurry, and raising or raising the ore slurry stepwise.
- the pipes, etc. are equipped with extremely expensive pipes made of materials and structures that can withstand high temperatures and pressures, and each facility can be shortened as much as possible according to the overall cost requirements including material costs. Proper placement has been done. For this reason, the leach slurry is transferred from the autoclave to the first stage flash vessel and then to the next stage flash vessel.
- the leaching slurry contains sulfuric acid, which takes into account the durability and cost of the transfer equipment.
- the first stage flash vessel is used for the autoclave. It is installed in a place that hits a height of about 25-35m above.
- the pressurized steam recovered in stages from the high-temperature and high-pressure slurry after the leaching is supplied from each stage of the flash vessel to a preheater having the same temperature and pressure.
- a very expensive pipe made of a material and a structure for withstanding high-temperature and high-pressure pressurized steam is provided.
- the liquid level level is insufficiently controlled as an estimated cause. That is, the slurry is charged into a flash vessel after leaching at high temperature and high pressure, and when the water vapor is generated, the surface of the slurry is not flat. It is considered that the control of the liquid level is insufficient.
- a flash vessel for lowering and lowering the temperature of the slurry after leaching the raw slurry at high temperature and high pressure with an autoclave is a large-sized
- it is a flash vessel applied to a strongly acidic slurry, it is technically difficult to install a viewing window, so it is practically impossible to visually observe it, and it can only be estimated as described above. .
- the liquid level sensor 120A installed at the upper limit of the liquid level cannot be detected due to the fluctuation of the liquid level, and the slurry discharge valve 116 is not detected. Since the liquid level control is not performed, the operation in the state where the liquid level in the flash vessel 100 is high is continued, and the acidic slurry is taken away together with the recovered steam to the preheater, and is recovered by the acidic slurry. There is a risk that corrosion of the steam discharge pipe 104 may proceed. Further, even if the actual liquid level is low, the liquid level sensor 120B installed at the lower limit of the liquid level cannot be detected in the same manner, and the liquid level control by the slurry discharge valve 116 is not performed.
- the actual liquid level becomes lower than that of the slurry discharge pipe 114, and the vapor in the flash vessel 100 is discharged together with the discharged slurry from the slurry discharge pipe 114 to the next flash vessel, and the slurry flow rate in the discharge pipe temporarily increases.
- the slurry discharge pipe 114 and the valve are damaged, the amount of steam flowing from the next-stage flash tank to the recovery steam pipe temporarily increases, the carry-over of acidic slurry increases, and the flow rate increases. There is a possibility that corrosion and wear of the recovered steam pipe may progress due to the increase.
- Patent Document 2 describes a technique for concentrating a slurry of organic sludge, in which a liquid level in a flash vessel is detected so that the liquid level of the concentrated liquid is always positioned in the information from the discharge port.
- a liquid level in a flash vessel is detected so that the liquid level of the concentrated liquid is always positioned in the information from the discharge port.
- Patent Document 3 describes a technique for controlling refrigerant charge into the system using at least one sensor that detects the level of liquid refrigerant in a flash vessel used in a refrigerant vapor compression system.
- it is a technique that can be used when the liquid surface is flat, such as a float type sensor or an ultrasonic sensor, and is difficult to apply to the above problems.
- JP 2010-059489 A Japanese Patent Laid-Open No. 10-080700 Special table 2009-524797
- An object of the present invention is to provide a high-pressure acid leaching process including a flash vessel for leaching a raw slurry at high temperature and high pressure in an autoclave and then lowering and lowering the temperature of the leached slurry to room temperature and normal pressure in view of the conventional problems as described above.
- a flash vessel for leaching a raw slurry at high temperature and high pressure in an autoclave and then lowering and lowering the temperature of the leached slurry to room temperature and normal pressure in view of the conventional problems as described above.
- the inventors of the present invention have disclosed a flash vessel in a high pressure acid leaching process including a flash vessel in which raw slurry is leached in an autoclave under high temperature and high pressure, and then the leached slurry is cooled down to room temperature and normal pressure.
- the liquid level was measured on the side of the still water tower using a flash vessel equipped with a still water tower. Completed the invention.
- the present invention is a flash vessel in a high pressure acid leaching process including a flash vessel in which raw slurry is leached under high temperature and high pressure in an autoclave, and then the leached slurry is cooled to normal temperature and normal pressure.
- a hydrostatic tower whose lower part is in communication with the liquid phase space and whose upper part is in communication with the gas phase space, and is installed at a position at the same level as the upper limit of the predetermined liquid level in the liquid phase space.
- a liquid level sensor for detecting the liquid level, and at least one lower limit for detecting the liquid level in the hydrostatic tower, which is installed at the same level as the predetermined liquid level lower limit in the liquid phase space.
- the lower part of the hydrostatic tower is connected to an arbitrary position from the connection point with the flash vessel on the slurry discharge pipe to the slurry discharge valve, and the lower part of the hydrostatic tower is The upper part of the still water tower can be connected to an arbitrary position on the steam discharge pipe.
- the diameter A of the hydrostatic tower is in a range of 1/100 ⁇ B ⁇ A ⁇ 1/5 ⁇ B as compared with the diameter B of the flash vessel. can do.
- the raw material slurry is a nickel oxide ore slurry
- the leached slurry obtained by leaching the nickel oxide ore slurry with sulfuric acid is lowered to a normal temperature and a normal pressure. it can.
- the present invention is a method for operating a flash vessel in a high pressure acid leaching process including a flash vessel in which a raw slurry is leached in an autoclave under high temperature and high pressure, and then the temperature of the leached slurry is lowered to room temperature and normal pressure.
- the liquid level in the still water tower whose lower part is communicated with the liquid phase space inside and whose upper part is communicated with the gas phase space is at least one installed at the same level as the predetermined liquid level upper limit of the liquid phase space.
- the slurry discharge valve is opened when the upper liquid level sensor detects the liquid level in the still water tower that has risen, and the liquid in the still water tower that has been lowered.
- the raw material slurry is a nickel oxide ore slurry
- the leached slurry obtained by leaching the nickel oxide ore slurry with sulfuric acid is lowered to a normal temperature and a normal pressure. Can do.
- the flash vessel and the operation method thereof in the high-pressure acid leaching step including the flash vessel in which the raw slurry is leached in an autoclave under high temperature and high pressure, and then the leached slurry is cooled and depressurized to room temperature and normal pressure.
- FIG. 1 It is a block diagram which shows the structural example of the flash vessel to which this invention is applied. It is process drawing which shows the leaching procedure of nickel and cobalt by the high pressure acid leaching method of nickel oxide ore. It is a figure which shows schematic structure of a general flash vessel.
- the present invention is applied to a flash vessel 10 having a structure as shown in FIG.
- the flash vessel 10 is a flash vessel in a high pressure acid leaching process in which a raw material slurry is leached in an autoclave under high temperature and high pressure, and then the leached slurry is cooled down to room temperature and normal pressure. And a slurry charging port 3 and a steam discharge port 5 are provided in the ceiling portion 2 where the upper portion of the barrel portion 1 is closed, and a slurry discharge port 4 is provided in the barrel portion 1.
- the slurry charging inlet 3 is connected to a slurry charging pipe 13 for charging the leached slurry, which has been lowered to a predetermined temperature and a predetermined pressure, into the flash vessel 10.
- a slurry discharge pipe 14 for discharging the slurry charged in the flash vessel 10 is connected, and the steam generated in the flash vessel 10 as the slurry is charged is collected in the vapor outlet 5.
- a steam discharge pipe 15 is connected.
- a slurry discharge valve 16 is installed in the slurry discharge pipe 14 connected to the slurry discharge port 4.
- the leached slurry lowered to a predetermined temperature and a predetermined pressure is charged through the slurry charging port 3, and the slurry charged in the flash vessel 10 is loaded into the slurry discharge port 4. Further, the steam generated from the charging of the slurry is discharged from the steam discharge port 5.
- the raw material slurry is nickel oxide ore slurry
- this flash vessel 10 the leached slurry obtained by leaching the nickel oxide ore slurry with sulfuric acid is charged, and the charged slurry is cooled to room temperature and normal pressure.
- the flash vessel 10 further includes a hydrostatic tower 20 having a lower portion communicating with the liquid phase space in the flash vessel 10 and an upper portion communicating with the gas phase space.
- the lower part of the hydrostatic tower 20 is connected to an arbitrary position on the slurry discharge pipe 14 from the connection point with the flash vessel 10 to the slurry discharge valve 16.
- the upper part of the still water tower 20 is connected to an arbitrary position on the steam discharge pipe 15.
- the diameter of the hydrostatic tower 20 is not particularly limited, but the diameter A of the hydrostatic tower 20 is 1/100 ⁇ B ⁇ A ⁇ 1/5 ⁇ B compared to the diameter B of the flash vessel 10. It is preferable that it is the range of these. If it is too wide, there is a concern that the investment cost will increase and the slurry will stay in the hydrostatic tower 20, and if it is too narrow, it will be susceptible to the fluctuation of the liquid level, and the slurry may be easily clogged by the slurry.
- the valve opening degree of the slurry discharge valve 16 is controlled according to the liquid level measurement result by the liquid level sensors 21 ⁇ / b> A and 21 ⁇ / b> B provided in the hydrostatic tower 20, thereby the inside of the flash vessel 10.
- the liquid level is maintained at an appropriate level.
- the flash vessel 10 is a flash vessel in a high-pressure acid leaching process in which the raw slurry is leached in an autoclave under high temperature and high pressure, and then the leached slurry is cooled to room temperature and normal pressure, and is operated as follows.
- the liquid level in the still water tower 20 with the lower part communicating with the liquid phase space in the flash vessel 10 and the upper part communicating with the gas phase space is set at a position at the same level as the predetermined upper limit of the liquid level in the liquid phase space.
- the slurry discharge valve 16 installed on the slurry discharge pipe 14 is opened when the upper liquid level sensor 21A detects the liquid level in the still water tower 20 that has risen, and the slurry discharge valve 16 in the still water tower 20 that has dropped.
- the liquid level is closed when the lower limit liquid level sensor 21B detects it.
- the slurry liquid level in the flash vessel 10 can be controlled within an appropriate range. That is, the situation where the steam flows into the slurry discharge pipe 14 side is less likely to occur, thereby reducing the problem of damage to the slurry discharge valve 16.
- the raw material slurry charged into the flash vessel 10 is not particularly limited, and raw materials containing various metal compounds used when leaching a desired metal by a high pressure acid leaching method, for example, , Metals, sulfides, oxides, ores, etc., for example, ore slurry made of nickel oxide ore is preferred.
- the high pressure acid leaching step is not particularly limited, but in addition to an autoclave and a flash vessel, a preheater that raises and raises the temperature of the ore slurry employed in a general high pressure acid leaching method stepwise. Is included.
- the autoclave is not particularly limited, and a vertical or horizontal pressure vessel heated by blowing external air or pressurized steam is used.
- the lash vessel 10 is not particularly limited, and a multistage type is used.
- the pre-heater is not particularly limited, but a multistage counter-current direct heating heat exchanger is used. At this time, water vapor is used as a heating medium.
- the steam generated by a general method such as a boiler may be used as the steam, but the steam generated in the flash vessel that gradually cools and depressurizes the leach slurry discharged from the autoclave is recovered. It is preferable to circulate and use.
- the high pressure acid leaching method of the nickel oxide ore includes ore processing step P1, high pressure acid leaching step P2, solid-liquid separation step P3, neutralization step P4, dezincification step P5 and nickel / cobalt sulfide.
- Process P6 is included.
- step P1 large blocks, gangue, tree roots, and the like are removed from the nickel oxide ore to prepare an ore slurry having a predetermined slurry concentration.
- the ore slurry transferred from the ore processing step is preheated with a preheater, and the preheated ore slurry is leached with sulfuric acid under high temperature and high pressure while blowing high pressure air and high pressure steam.
- the temperature and pressure of the high temperature and high pressure leaching slurry are lowered by the flash vessel 10.
- the leaching slurry is subjected to solid-liquid separation to obtain a leaching solution and a leaching residue.
- a nickel / cobalt mixed sulfide is obtained from the leachate by a sulfide precipitation method.
- the nickel oxide ore is mainly a so-called laterite ore such as limonite or saprolite ore.
- the nickel content of the laterite ore is usually 0.5 to 2.0% by mass, and is contained as a hydroxide or siliceous clay (magnesium silicate) mineral.
- the iron content is 20 to 50% by mass and is mainly in the form of trivalent hydroxide (goethite, FeOOH), but partly divalent iron is contained in the siliceous clay. .
- the slurry concentration of the ore slurry produced in the ore treatment step P1 is not particularly limited because it depends greatly on the properties of the nickel oxide ore to be treated.
- the higher the slurry concentration of the leaching slurry Preferably, it is usually adjusted to 20 to 50% by mass. That is, when the slurry concentration of the leaching slurry is less than 20% by mass, a large facility is required to obtain the same residence time in each step including the leaching step, and the amount of acid added also increases to adjust the residual acid concentration. .
- the nickel concentration of the obtained leachate becomes low, which ultimately causes a decrease in the actual yield.
- Examples of practical equipment for the high-pressure acid leaching step P2 include, for example, a three-stage preheater, an autoclave, and a three-stage flash vessel.
- a cylindrical container having a flash vessel 10 with a diameter of about 4 to 6 m and a height of about 10 to 12 m is installed vertically.
- the slurry introduced into the first-stage flash vessel is, for example, 200 to 270 ° C., and the pressure is, for example, 1.8 to 5.8 MPaG.
- the flash vessel 10 used in the high pressure acid leaching step P2 is configured as follows.
- the lower part of the hydrostatic tower 20 having a diameter of 250 mm is connected to a position where the slurry is connected to the flash vessel 10 on the slurry discharge pipe 14 and an intermediate position (position about 50 cm from the connection position) between the slurry discharge valve 16 and steam.
- the upper part of the water tower 20 having a diameter of 250 mm was connected to a position of about 50 cm from the connection point with the flash vessel 10 on the discharge pipe 15.
- the hydrostatic tower 20 is provided with one liquid level sensor 21A at a position of about 6.5 m from the bottom of the flash vessel 10 (the same level as the predetermined upper limit of the liquid level).
- One liquid level sensor 21B was installed at a position of about 4.5 m from the bottom (same level as the predetermined lower limit of the liquid level).
- the diameter of the hydrostatic tower 20 is about 5 mm, and the diameter is 1/20 of the main body.
- the valve is turned on when the upper liquid level sensor 21A detects the rising liquid level.
- a signal for opening is sent to the slurry discharge valve 16, and the slurry discharge valve 16 is opened, thereby transferring the slurry in the flash vessel 10 to the next step.
- the slurry liquid level in the flash vessel 10 is lowered, and when the lower liquid level sensor 21B detects the lowered liquid level, the slurry is discharged.
- the slurry level in the flash vessel 10 starts to rise again. By repeating this procedure, operation can be performed continuously.
- Example 1 A practical plant for nickel oxide ore, including examples of practical equipment for the high-pressure acid leaching process described above, was used.
- the leaching slurry prepared by adjusting the ore slurry shown in Table 1 to about 245 ° C. and about 4 MPaG at the outlet of the autoclave is charged into the first-stage flash vessel, and then sequentially into the second-stage and third-stage flash vessels.
- the operation of transferring and lowering the leach slurry to normal pressure was carried out for 6 months.
- Example 1 The same operation as in Example 1 was performed with a conventional facility that does not have a hydrostatic tower, instead of the practical facility example of the high-pressure acid leaching process described above.
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Abstract
Description
前述した高圧酸浸出工程の実用設備例を含む、ニッケル酸化鉱石の実用プラントを用いた。
前述した高圧酸浸出工程の実用設備例ではなく、静水塔を備えない従来の設備で実施例1と同様の操業を行なった。
Claims (6)
- 原料スラリーをオートクレーブで高温高圧下に浸出し、次いで浸出後のスラリーを常温常圧まで降温降圧するフラッシュベッセルを含む高圧酸浸出工程におけるフラッシュベッセルであって、
当該フラッシュベッセル内の液相空間に下部が連通され、気相空間に上部が連通された静水塔と、
上記液相空間の所定の液面上限と同水準の位置に設置され、上昇してきた上記静水塔内の液面を検出する少なくとも1つの上限液面センサーと、
上記液相空間の所定の液面下限と同水準の位置に設置され、下降してきた上記静水塔内の液面を検出する少なくとも1つの下限液面センサーと
を備えることを特徴とするフラッシュベッセル。 - 上記静水塔の下部が、スラリー排出管上の、フラッシュベッセルとの連結箇所から、スラリー排出バルブまでの任意の位置に連結され、上記静水塔の下部が、蒸気排出管上の任意の位置に、静水塔の上部が連結されていることを特徴とする請求項1記載のフラッシュベッセル。
- 上記静水塔の直径Aは、当該フラッシュベッセルの直径Bと比較して、1/100×B≦A≦1/5×Bの範囲であることを特徴とする請求項1又は請求項2に記載のフラッシュベッセル。
- 上記原料スラリーはニッケル酸化鉱石スラリーであり、該ニッケル酸化鉱石スラリーを硫酸で浸出した浸出後のスラリーを常温常圧まで降温降圧することを特徴とする請求項3に記載のフラッシュベッセル。
- 原料スラリーをオートクレーブで高温高圧下に浸出し、次いで浸出後のスラリーを常温常圧まで降温降圧するフラッシュベッセルを含む高圧酸浸出工程におけるフラッシュベッセルの運転方法であって、
上記フラッシュベッセル内の液相空間に下部が連通され、気相空間に上部が連通された静水塔内の液面を、上記液相空間の所定の液面上限と同水準の位置に設置された少なくとも1つの上限液面センサーと上記液相空間の所定の液面下限と同水準の位置に設置された少なくとも1つの上限液面センサーにより検出し、
上記フラッシュベッセルから導出されたスラリー排出管上に設置されたスラリー排出バルブを、上昇してきた上記静水塔内の液面を上記上限液面センサーが検知した際に開放し、下降してきた上記静水塔内の液面を上記下限液面センサーが検知した際に閉鎖することを特徴とするフラッシュベッセルの運転方法。 - 上記原料スラリーはニッケル酸化鉱石スラリーであり、該ニッケル酸化鉱石スラリーを硫酸で浸出した浸出後のスラリーを常温常圧まで降温降圧することを特徴とする請求項5に記載のフラッシュベッセルの運転方法。
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AU2012365089A AU2012365089B2 (en) | 2012-01-13 | 2012-12-27 | Flash vessel and method for operating same |
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JP2013553250A JP5582265B2 (ja) | 2012-01-13 | 2012-12-27 | フラッシュベッセル及びその運転方法 |
CN201280066905.8A CN104039993B (zh) | 2012-01-13 | 2012-12-27 | 闪蒸器及其运转方法 |
US14/370,882 US9464341B2 (en) | 2012-01-13 | 2012-12-27 | Flash vessel and method for operating same |
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JP6819087B2 (ja) | 2016-06-21 | 2021-01-27 | 住友金属鉱山株式会社 | ニッケル粉の製造方法、ニッケル粉の製造装置 |
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