JP2018127653A - Manufacturing facility and manufacturing method of cobalt carbonate - Google Patents
Manufacturing facility and manufacturing method of cobalt carbonate Download PDFInfo
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Abstract
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本発明は、炭酸コバルトの製造設備、および製造方法に関する。さらに詳しくは、コバルト水溶液と炭酸塩とを反応させて炭酸コバルトを製造する設備および方法に関する。 The present invention relates to a production facility and a production method for cobalt carbonate. More specifically, the present invention relates to equipment and a method for producing cobalt carbonate by reacting a cobalt aqueous solution with a carbonate.
硫化物からニッケル、コバルトを回収する湿式製錬プロセスでは、原料であるニッケルマットやニッケル・コバルト混合硫化物を塩素浸出し、得られた浸出液から不純物を除去する浄液工程などを経て、電解工程で電気ニッケルや電気コバルトを回収する。 In the hydrometallurgical process for recovering nickel and cobalt from sulfides, the nickel matte and nickel-cobalt mixed sulfide as raw materials are leached with chlorine, and the electrolytic process is performed through a purification process that removes impurities from the obtained leachate. Collect electric nickel and cobalt.
前記浄液工程には塩化コバルト水溶液に硫化剤とｐＨ調整剤とを添加して不純物を硫化澱物として除去する工程が含まれる（例えば、特許文献１）。この工程ではｐＨ調整剤として炭酸コバルトが好適に用いられる。塩化コバルト水溶液への不純物の混入を防止できるからである。 The liquid purification step includes a step of removing impurities as sulfided starch by adding a sulfurizing agent and a pH adjuster to the cobalt chloride aqueous solution (for example, Patent Document 1). In this step, cobalt carbonate is preferably used as a pH adjuster. This is because contamination of the cobalt chloride aqueous solution can be prevented.
炭酸コバルトはコバルト電解工程から排出された電解廃液にソーダ灰を添加し、得られたスラリーを固液分離することで得られる。この炭酸コバルトを前記浄液工程のｐＨ調整剤として用いることで、コバルトロスを低減できるとともに、湿式製錬プロセスの水バランスの維持に寄与できる。 Cobalt carbonate is obtained by adding soda ash to the electrolytic waste liquid discharged from the cobalt electrolysis step and solid-liquid separation of the resulting slurry. By using this cobalt carbonate as a pH adjuster in the liquid purification step, it is possible to reduce cobalt loss and contribute to maintaining the water balance of the hydrometallurgical process.
実操業において、スラリーの固液分離に用いられる固液分離装置が異常停止することがある。固液分離装置が異常停止すると、炭酸コバルトの製造工程の操業効率が低下する。この問題に対して、固液分離装置に供給されるスラリーの固形分濃度を低減し、固液分離装置の負荷を抑えることが考えられる。しかし、スラリーの固形分濃度は操業現場で連続的に測定することが困難である。そのため、定期的に、例えば１回／日の頻度でサンプリングしたスラリーを用いて固形分濃度を測定することになる。この場合、スラリーの固形分濃度の変動を十分に抑えることができず、固液分離装置の負荷が増大する可能性がある。 In actual operation, the solid-liquid separator used for the solid-liquid separation of the slurry may stop abnormally. If the solid-liquid separator is abnormally stopped, the operation efficiency of the cobalt carbonate manufacturing process is lowered. In order to solve this problem, it is conceivable to reduce the solid content concentration of the slurry supplied to the solid-liquid separator and to suppress the load on the solid-liquid separator. However, it is difficult to continuously measure the solid content concentration of the slurry at the operation site. Therefore, the solid content concentration is measured periodically using, for example, a slurry sampled at a frequency of once / day. In this case, fluctuations in the solid content concentration of the slurry cannot be sufficiently suppressed, and the load on the solid-liquid separation device may increase.
本発明は上記事情に鑑み、スラリーの固形分濃度の変動を十分に抑えることができ、固液分離装置の負荷を低減できる炭酸コバルトの製造設備、および製造方法を提供することを目的とする。 In view of the above circumstances, an object of the present invention is to provide a cobalt carbonate production facility and a production method capable of sufficiently suppressing fluctuations in the solid content concentration of a slurry and reducing the load of a solid-liquid separator.
第１発明の炭酸コバルトの製造設備は、コバルト水溶液が流れる第１流路と、前記第１流路に設けられ、コバルト水溶液の流量を測定する第１流量計と、前記第１流路に設けられ、コバルト水溶液のコバルト濃度を測定するコバルト濃度計と、希釈水が流れる第２流路と、前記第２流路に設けられ、前記希釈水の流量を制御する流量制御弁と、前記流量制御弁を制御する制御装置と、前記第１流路から供給されたコバルト水溶液と、前記第２流路から供給された前記希釈水とを混合して、希釈後液を得る希釈槽と、前記希釈後液と炭酸塩とを反応させて、炭酸コバルトを含むスラリーを得る反応槽と、前記スラリーを固液分離する固液分離装置と、を備え、前記制御装置は、前記第１流量計および前記コバルト濃度計の測定値に基づき、前記希釈水の流量が前記希釈後液のコバルト濃度が目標濃度となる目標流量となるように、前記流量制御弁の開度を調節することを特徴とする。
第２発明の炭酸コバルトの製造設備は、第１発明において、前記第２流路に設けられ、前記希釈水の流量を測定する第２流量計を備え、前記制御装置は、前記第２流量計の測定値が前記目標流量となるように、前記流量制御弁の開度を調節することを特徴とする。
第３発明の炭酸コバルトの製造設備は、第１または第２発明において、前記固液分離装置はスクリューデカンタであることを特徴とする。
第４発明の炭酸コバルトの製造設備は、第１、第２または第３発明において、前記目標濃度は５０〜６０ｇ／Ｌであることを特徴とする。
第５発明の炭酸コバルトの製造方法は、第１、第２、第３または第４発明の製造設備を用いて炭酸コバルトを製造することを特徴とする。
The cobalt carbonate manufacturing facility according to the first aspect of the present invention is provided with a first flow path through which a cobalt aqueous solution flows, a first flow meter provided in the first flow path for measuring the flow rate of the cobalt aqueous solution, and the first flow path. A cobalt concentration meter that measures the cobalt concentration of the cobalt aqueous solution, a second flow path through which the dilution water flows, a flow control valve that is provided in the second flow path and controls the flow rate of the dilution water, and the flow control A control device for controlling the valve; a cobalt aqueous solution supplied from the first flow path; and a dilution tank for obtaining a diluted liquid by mixing the dilution water supplied from the second flow path; and the dilution A reaction tank for reacting a post-solution with carbonate to obtain a slurry containing cobalt carbonate; and a solid-liquid separation device for solid-liquid separation of the slurry; and the control device includes the first flow meter and the Based on the measured value of cobalt densitometer, As the flow rate of Shakumizu becomes a target flow rate cobalt concentration of target concentration of the diluted solution after, and adjusting the opening of the flow control valve.
A cobalt carbonate production facility according to a second aspect of the present invention includes, in the first aspect, a second flow meter that is provided in the second flow path and measures the flow rate of the dilution water, and the control device includes the second flow meter. The opening degree of the flow control valve is adjusted so that the measured value becomes the target flow rate.
The cobalt carbonate production facility according to a third aspect of the present invention is characterized in that, in the first or second aspect, the solid-liquid separator is a screw decanter.
The cobalt carbonate production facility according to a fourth aspect of the present invention is characterized in that, in the first, second or third aspect, the target concentration is 50 to 60 g / L.
The method for producing cobalt carbonate according to the fifth invention is characterized in that cobalt carbonate is produced using the production equipment according to the first, second, third or fourth invention.
第１発明によれば、コバルト濃度計で測定されたコバルト水溶液のコバルト濃度に基づき、コバルト水溶液と希釈水との混合比を調節することで、間接的にスラリーの固形分濃度を調節できる。そのため、スラリーの固形分濃度の変動を十分に抑えることができ、固液分離装置の負荷を低減できる。
第２発明によれば、第２流量計の測定値を参照するので、希釈水の流量を精度良く調節できる。
第３発明によれば、固液分離装置がスクリューデカンタであるので、設置サイズに対する処理能力が高い。
第４発明によれば、希釈後液のコバルト濃度を５０〜６０ｇ／Ｌとすれば、スラリーの固形分濃度が１００〜１５０ｇ／Ｌとなり、固液分離装置の負荷を十分に低減できる。
第５発明によれば、コバルト濃度計で測定されたコバルト水溶液のコバルト濃度に基づき、コバルト水溶液と希釈水との混合比を調節することで、間接的にスラリーの固形分濃度を調節できる。そのため、スラリーの固形分濃度の変動を十分に抑えることができ、固液分離装置の負荷を低減できる。
According to the first invention, the solid content concentration of the slurry can be indirectly adjusted by adjusting the mixing ratio of the cobalt aqueous solution and the dilution water based on the cobalt concentration of the cobalt aqueous solution measured by the cobalt densitometer. Therefore, the fluctuation | variation of the solid content density | concentration of a slurry can fully be suppressed, and the load of a solid-liquid separator can be reduced.
According to the second invention, since the measurement value of the second flow meter is referred to, the flow rate of the dilution water can be adjusted with high accuracy.
According to the third invention, since the solid-liquid separator is a screw decanter, the processing capacity for the installation size is high.
According to the fourth invention, if the cobalt concentration of the diluted liquid is 50 to 60 g / L, the solid content concentration of the slurry is 100 to 150 g / L, and the load on the solid-liquid separation device can be sufficiently reduced.
According to the fifth invention, the solid content concentration of the slurry can be indirectly adjusted by adjusting the mixing ratio of the cobalt aqueous solution and the dilution water based on the cobalt concentration of the cobalt aqueous solution measured by the cobalt densitometer. Therefore, the fluctuation | variation of the solid content density | concentration of a slurry can fully be suppressed, and the load of a solid-liquid separator can be reduced.
つぎに、本発明の実施形態を図面に基づき説明する。
本発明の一実施形態に係る炭酸コバルトの製造設備１および製造方法は、コバルト水溶液と炭酸塩とを反応させて炭酸コバルトを製造する。コバルト水溶液は特に限定されないが、ニッケル、コバルトを回収する湿式製錬プロセスのコバルト電解工程の電解廃液（塩化コバルト水溶液）を用いることができる。ここで、電解廃液のコバルト濃度は例えば５５〜９５ｇ／Ｌである。炭酸塩としては、ソーダ灰（無水炭酸ナトリウム）、炭酸ナトリウム、炭酸カリウム、炭酸水素カリウムなどが用いられる。
Next, an embodiment of the present invention will be described with reference to the drawings.
The cobalt carbonate production facility 1 and production method according to an embodiment of the present invention produce cobalt carbonate by reacting a cobalt aqueous solution with a carbonate. Although cobalt aqueous solution is not specifically limited, The electrolytic waste liquid (cobalt chloride aqueous solution) of the cobalt electrolysis process of the hydrometallurgical process which collect | recovers nickel and cobalt can be used. Here, the cobalt concentration of the electrolytic waste liquid is, for example, 55 to 95 g / L. As the carbonate, soda ash (anhydrous sodium carbonate), sodium carbonate, potassium carbonate, potassium hydrogen carbonate and the like are used.
図１に示すように、炭酸コバルトの製造設備１は、希釈槽１１と、反応槽１２と、固液分離装置１３とを備えている。希釈槽１１にはコバルト水溶液が流れる第１流路２１と、希釈水が流れる第２流路２２とが接続されており、コバルト水溶液と希釈水とが供給されている。希釈槽１１でコバルト水溶液と希釈水とを混合して希釈後液を得る。 As shown in FIG. 1, the cobalt carbonate production facility 1 includes a dilution tank 11, a reaction tank 12, and a solid-liquid separator 13. The dilution tank 11 is connected to a first flow path 21 through which a cobalt aqueous solution flows and a second flow path 22 through which dilution water flows, and is supplied with a cobalt aqueous solution and dilution water. In the dilution tank 11, the cobalt aqueous solution and the dilution water are mixed to obtain a diluted solution.
希釈槽１１と反応槽１２とは第３流路２３で接続されている。希釈槽１１から排出された希釈後液は、第３流路２３を通って反応槽１２に供給される。反応槽１２には炭酸塩も供給されている。反応槽１２で希釈後液と炭酸塩とを撹拌することにより、希釈後液（コバルト水溶液）と炭酸塩とが反応し、炭酸コバルトが生成される。 The dilution tank 11 and the reaction tank 12 are connected by a third flow path 23. The diluted solution discharged from the dilution tank 11 is supplied to the reaction tank 12 through the third flow path 23. Carbonate is also supplied to the reaction tank 12. By stirring the diluted solution and carbonate in the reaction tank 12, the diluted solution (cobalt aqueous solution) reacts with carbonate to produce cobalt carbonate.
なお、塩化コバルト水溶液に炭酸ナトリウムを添加した場合には、下記化学式（１）の反応により炭酸コバルトが生成される。
ＣｏＣｌ2＋Ｎａ2ＣＯ3 → ２ＮａＣｌ＋ＣｏＣＯ3 ・・・（１）
In addition, when sodium carbonate is added to the cobalt chloride aqueous solution, cobalt carbonate is generated by the reaction of the following chemical formula (1).
CoCl 2 + Na 2 CO 3 → 2NaCl + CoCO 3 (1)
ソーダ灰はコバルトと比べて単価が安い。そのため、反応槽１２に供給されるコバルトの量に対して過剰にソーダ灰を添加することが好ましい。そうすれば、希釈後液に含まれるコバルトの全量を回収することができ、反応槽１２から排出されたスラリーの液相には実質的にコバルトが残留しない。 Soda ash is cheaper than cobalt. Therefore, it is preferable to add soda ash in excess of the amount of cobalt supplied to the reaction tank 12. Then, the total amount of cobalt contained in the diluted solution can be recovered, and substantially no cobalt remains in the liquid phase of the slurry discharged from the reaction vessel 12.
反応槽１２と固液分離装置１３とは第４流路２４で接続されている。反応槽１２から排出されたスラリー（炭酸コバルトを含むスラリー）は、第４流路２４を通って固液分離装置１３に供給される。 The reaction tank 12 and the solid-liquid separator 13 are connected by a fourth flow path 24. The slurry discharged from the reaction tank 12 (a slurry containing cobalt carbonate) is supplied to the solid-liquid separator 13 through the fourth flow path 24.
固液分離装置１３において、スラリーが炭酸コバルトと濾液とに固液分離される。これにより炭酸コバルトが得られる。固液分離により得られる濾液は廃水工程に移送され、廃水処理後に系外に排出される。固液分離装置１３としては、特に限定されないが、デカンタなどの遠心分離機、オリバーフィルターなどの真空脱水機、フィルタープレスなどの加圧脱水機などを用いることができる。なかでも、スクリューデカンタは設置サイズに対する処理能力が高いので好ましい。 In the solid-liquid separator 13, the slurry is solid-liquid separated into cobalt carbonate and a filtrate. Thereby, cobalt carbonate is obtained. The filtrate obtained by solid-liquid separation is transferred to a wastewater process, and discharged outside the system after wastewater treatment. The solid-liquid separation device 13 is not particularly limited, and a centrifugal separator such as a decanter, a vacuum dehydrator such as an oliver filter, a pressure dehydrator such as a filter press, and the like can be used. Among these, a screw decanter is preferable because it has a high processing capacity with respect to the installation size.
上記構成の製造設備１において、固液分離装置１３に供給されるスラリーの固形分濃度が高いと、固液分離装置１３の負荷が高くなり、異常停止することがある。本実施形態の製造設備１は、コバルト水溶液と希釈水との混合比を調節し、希釈後液のコバルト濃度を所定濃度に調節することで、間接的にスラリーの固形分濃度を調節する。これにより、固液分離装置１３の負荷を低減する。以下、この機能を実現する構成を説明する。 In the manufacturing facility 1 having the above-described configuration, when the solid content concentration of the slurry supplied to the solid-liquid separator 13 is high, the load on the solid-liquid separator 13 is increased and may be abnormally stopped. The manufacturing facility 1 of the present embodiment indirectly adjusts the solid content concentration of the slurry by adjusting the mixing ratio of the cobalt aqueous solution and the dilution water and adjusting the cobalt concentration of the diluted solution to a predetermined concentration. Thereby, the load of the solid-liquid separator 13 is reduced. Hereinafter, a configuration for realizing this function will be described.
コバルト水溶液が流れる第１流路２１には、コバルト水溶液の流量を測定する第１流量計３１と、コバルト水溶液のコバルト濃度を測定するコバルト濃度計３２とが設けられている。コバルト濃度計３２としては、操業現場で連続的に測定可能な、密度測定器、吸光度測定器、導電率測定器、屈折率測定器などが用いられる。 The first flow path 21 through which the cobalt aqueous solution flows is provided with a first flow meter 31 that measures the flow rate of the cobalt aqueous solution and a cobalt concentration meter 32 that measures the cobalt concentration of the cobalt aqueous solution. As the cobalt densitometer 32, a density measuring device, an absorbance measuring device, a conductivity measuring device, a refractive index measuring device, or the like that can be continuously measured at the operation site is used.
希釈水が流れる第２流路２２には、希釈水の流量を測定する第２流量計３３と、希釈水の流量を制御する流量制御弁３４とが設けられている。流量制御弁３４には制御装置３５が接続されている。制御装置３５には第１流量計３１、コバルト濃度計３２、第２流量計３３の各測定値が入力されている。なお、制御装置３５はＣＰＵやメモリなどで構成されたコンピュータである。 The second flow path 22 through which the dilution water flows is provided with a second flow meter 33 that measures the flow rate of the dilution water and a flow rate control valve 34 that controls the flow rate of the dilution water. A controller 35 is connected to the flow rate control valve 34. The measurement values of the first flow meter 31, the cobalt concentration meter 32, and the second flow meter 33 are input to the control device 35. The control device 35 is a computer configured with a CPU, a memory, and the like.
制御装置３５には、予め希釈後液のコバルト濃度の目標値（目標濃度）が記憶されている。目標濃度は反応槽１２で得られるスラリーの固形分濃度が固液分離装置１３の負荷を十分に低減できる濃度となるように設定される。例えば、希釈後液のコバルト濃度を５０〜６０ｇ／Ｌとすれば、スラリーの固形分濃度が１００〜１５０ｇ／Ｌとなり、固液分離装置１３の負荷を十分に低減できる。この場合、目標濃度は５０〜６０ｇ／Ｌの間の特定の値に設定される。 The control device 35 stores in advance a target value (target concentration) of the cobalt concentration of the diluted liquid. The target concentration is set so that the solid content concentration of the slurry obtained in the reaction tank 12 is a concentration that can sufficiently reduce the load of the solid-liquid separator 13. For example, if the cobalt concentration of the diluted solution is 50 to 60 g / L, the solid content concentration of the slurry is 100 to 150 g / L, and the load on the solid-liquid separator 13 can be sufficiently reduced. In this case, the target concentration is set to a specific value between 50 and 60 g / L.
第１流路２１を流れるコバルト水溶液の流量およびコバルト濃度は、操業条件により変動する。第１流量計３１およびコバルト濃度計３２により、コバルト水溶液の流量およびコバルト濃度を測定する。制御装置３５は第１流量計３１およびコバルト濃度計３２の測定値に基づき、希釈後液のコバルト濃度が目標濃度となる希釈水の流量（目標流量）を求める。 The flow rate and cobalt concentration of the cobalt aqueous solution flowing through the first flow path 21 vary depending on the operating conditions. The first flow meter 31 and the cobalt concentration meter 32 measure the flow rate and cobalt concentration of the cobalt aqueous solution. Based on the measured values of the first flow meter 31 and the cobalt concentration meter 32, the control device 35 obtains the flow rate (target flow rate) of the dilution water at which the cobalt concentration of the diluted solution becomes the target concentration.
そして、制御装置３５は第２流量計３３の測定値（希釈水の流量）が目標流量となるように、流量制御弁３４の開度を調節する。すなわち、制御装置３５は希釈水の流量を制御量、流量制御弁３４の開度を操作量としたフィードバック制御を行う。 And the control apparatus 35 adjusts the opening degree of the flow control valve 34 so that the measured value (flow volume of dilution water) of the 2nd flow meter 33 may turn into target flow volume. That is, the control device 35 performs feedback control with the flow rate of the dilution water as the control amount and the opening degree of the flow rate control valve 34 as the operation amount.
なお、流量制御弁３４の開度と希釈水の流量との対応関係が常に一定である場合には、第２流量計３３の測定値を参照する必要はない。しかし、第２流量計３３の測定値を参照するよう構成すれば、希釈水の流量を精度良く調節できる。 When the correspondence between the opening degree of the flow control valve 34 and the flow rate of the dilution water is always constant, it is not necessary to refer to the measurement value of the second flow meter 33. However, if the measurement value of the second flow meter 33 is referred to, the flow rate of the dilution water can be adjusted with high accuracy.
以上のように、コバルト濃度計３２で測定されたコバルト水溶液のコバルト濃度に基づき、コバルト水溶液と希釈水との混合比を調節することで、希釈後液のコバルト濃度を目標濃度に調節できる。これにより、間接的にスラリーの固形分濃度を調節できる。そのため、スラリーの固形分濃度の変動を十分に抑えることができ、固液分離装置１３の負荷を低減できる。 As described above, the cobalt concentration of the diluted solution can be adjusted to the target concentration by adjusting the mixing ratio of the cobalt aqueous solution and the dilution water based on the cobalt concentration of the cobalt aqueous solution measured by the cobalt concentration meter 32. Thereby, the solid content density | concentration of a slurry can be adjusted indirectly. Therefore, the fluctuation | variation of the solid content density | concentration of a slurry can fully be suppressed, and the load of the solid-liquid separator 13 can be reduced.
つぎに、実施例を説明する。
（実施例１）
図１に示す構成の製造設備１を用いて炭酸コバルトを製造した。コバルト水溶液としてコバルト電解工程の電解廃液（塩化コバルト水溶液）を用いた。希釈槽１１に供給されるコバルト水溶液の流量は１５〜２５Ｌ／分、コバルト濃度は５５〜９５ｇ／Ｌであった。目標濃度を５６ｇ／Ｌに設定し、コバルト水溶液を希釈水で希釈した。
Next, examples will be described.
Example 1
Cobalt carbonate was manufactured using the manufacturing equipment 1 having the configuration shown in FIG. As the cobalt aqueous solution, an electrolytic waste solution (cobalt chloride aqueous solution) of the cobalt electrolysis process was used. The flow rate of the cobalt aqueous solution supplied to the dilution tank 11 was 15 to 25 L / min, and the cobalt concentration was 55 to 95 g / L. The target concentration was set to 56 g / L, and the cobalt aqueous solution was diluted with dilution water.
反応槽１２において希釈後液にソーダ灰を用いた。ソーダ灰の添加量は、希釈後液に含まれるコバルトの１．１倍等量とした。反応槽１２で得られたスラリーを固液分離装置１３で固液分離した。固液分離装置１３としてスクリューデカンタ（巴工業製 ＰＴＭ３００）を用いた。 Soda ash was used as a solution after dilution in the reaction vessel 12. The amount of soda ash added was 1.1 times the amount of cobalt contained in the diluted solution. The slurry obtained in the reaction vessel 12 was subjected to solid-liquid separation with a solid-liquid separator 13. A screw decanter (PTM300 manufactured by Sakai Kogyo Co., Ltd.) was used as the solid-liquid separator 13.
図２（Ａ）のグラフに希釈後液のコバルト濃度の時間変化を示す。
希釈後液のコバルト濃度の平均値は５６．２ｇ／Ｌであった。また、コバルト濃度のばらつき（±２σ）は±３．９ｇ／Ｌであった。固液分離装置１３の予定外の停止回数は１．５回／月であった。
The graph of FIG. 2A shows the change over time in the cobalt concentration of the diluted solution.
The average value of the cobalt concentration of the diluted solution was 56.2 g / L. Further, the variation (± 2σ) in cobalt concentration was ± 3.9 g / L. The number of unscheduled shutdowns of the solid-liquid separator 13 was 1.5 times / month.
（比較例１）
実施例１において、電解廃液を反応槽１２に直接供給した。すなわち、電解廃液の希釈を行わなかった。その余の条件は実施例１と同様である。
(Comparative Example 1)
In Example 1, the electrolytic waste liquid was directly supplied to the reaction tank 12. That is, the electrolytic waste liquid was not diluted. The other conditions are the same as in Example 1.
図２（Ｂ）のグラフに電解廃液のコバルト濃度の時間変化を示す。
電解廃液のコバルト濃度の平均値は７４．１ｇ／Ｌであった。また、電解廃液のばらつき（±２σ）は±１８．９ｇ／Ｌであった。固液分離装置１３の予定外の停止回数は４回／月であった。
The time change of the cobalt concentration of the electrolytic waste liquid is shown in the graph of FIG.
The average value of the cobalt concentration of the electrolytic waste liquid was 74.1 g / L. Moreover, the variation (± 2σ) of the electrolytic waste liquid was ± 18.9 g / L. The number of unscheduled shutdowns of the solid-liquid separator 13 was 4 times / month.
以上より、実施例１は比較例１に比べて、固液分離装置１３の異常停止の回数を低減できることが確認できた。 From the above, it was confirmed that Example 1 can reduce the number of abnormal stop of the solid-liquid separator 13 as compared with Comparative Example 1.
１ 製造設備
１１ 希釈槽
１２ 反応槽
１３ 固液分離装置
２１ 第１流路
２２ 第２流路
３１ 第１流量計
３２ コバルト濃度計
３３ 第２流量計
３４ 流量制御弁
３５ 制御装置
DESCRIPTION OF SYMBOLS 1 Manufacturing equipment 11 Dilution tank 12 Reaction tank 13 Solid-liquid separator 21 1st flow path 22 2nd flow path 31 1st flow meter 32 Cobalt concentration meter 33 2nd flow meter 34 Flow control valve 35 Control apparatus
Claims (5)
前記第１流路に設けられ、コバルト水溶液の流量を測定する第１流量計と、
前記第１流路に設けられ、コバルト水溶液のコバルト濃度を測定するコバルト濃度計と、
希釈水が流れる第２流路と、
前記第２流路に設けられ、前記希釈水の流量を制御する流量制御弁と、
前記流量制御弁を制御する制御装置と、
前記第１流路から供給されたコバルト水溶液と、前記第２流路から供給された前記希釈水とを混合して、希釈後液を得る希釈槽と、
前記希釈後液と炭酸塩とを反応させて、炭酸コバルトを含むスラリーを得る反応槽と、
前記スラリーを固液分離する固液分離装置と、を備え、
前記制御装置は、前記第１流量計および前記コバルト濃度計の測定値に基づき、前記希釈水の流量が前記希釈後液のコバルト濃度が目標濃度となる目標流量となるように、前記流量制御弁の開度を調節する
ことを特徴とする炭酸コバルトの製造設備。 A first flow path through which a cobalt aqueous solution flows;
A first flow meter provided in the first flow path for measuring the flow rate of the cobalt aqueous solution;
A cobalt concentration meter that is provided in the first flow path and measures the cobalt concentration of the cobalt aqueous solution;
A second flow path through which dilution water flows;
A flow rate control valve provided in the second flow path for controlling the flow rate of the dilution water;
A control device for controlling the flow rate control valve;
A dilution tank for mixing the cobalt aqueous solution supplied from the first flow path and the dilution water supplied from the second flow path to obtain a diluted liquid;
A reaction vessel for reacting the diluted liquid with carbonate to obtain a slurry containing cobalt carbonate;
A solid-liquid separation device for solid-liquid separation of the slurry,
The control device is configured to control the flow rate control valve so that the flow rate of the dilution water becomes a target flow rate at which the cobalt concentration of the diluted liquid becomes a target concentration based on the measurement values of the first flow meter and the cobalt concentration meter. A facility for producing cobalt carbonate, characterized by adjusting the opening degree.
前記制御装置は、前記第２流量計の測定値が前記目標流量となるように、前記流量制御弁の開度を調節する
ことを特徴とする請求項１記載の炭酸コバルトの製造設備。 A second flow meter provided in the second flow path for measuring the flow rate of the dilution water;
The said control apparatus adjusts the opening degree of the said flow control valve so that the measured value of a said 2nd flow meter may become the said target flow volume, The manufacturing apparatus of the cobalt carbonate of Claim 1 characterized by the above-mentioned.
ことを特徴とする請求項１または２記載の炭酸コバルトの製造設備。 3. The apparatus for producing cobalt carbonate according to claim 1, wherein the solid-liquid separator is a screw decanter.
ことを特徴とする請求項１、２または３記載の炭酸コバルトの製造設備。 The said target density | concentration is 50-60 g / L, The manufacturing apparatus of the cobalt carbonate of Claim 1, 2, or 3 characterized by the above-mentioned.
ことを特徴とする炭酸コバルトの製造方法。 Cobalt carbonate is produced using the production facility according to claim 1, 2, 3 or 4.
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